A $.fr;.l ‘ . , 99:1... 5. 1. .5 . .1. ....:1:_;..L . , , . , . . ‘ . . .. f “ x7341... . _ , ~ , ‘12:: I)ate lllllllllllllllllllllIll'llllllllllllllllllllllllllll 31293 01410 2556 This is to certify that the thesis entitled RANKINE 3.0: A STEAM POWER PLANT COMPUTER SIMULATION presented by Wayne Andrew Thelen has been accepted towards fulfillment of the requirements for MS Mechanical Engineering degree in Major professor 12/6/95 0-7639 MS U is an Affirmative Action/Equal Opportunity Institution PLAN RANKINE 3.0: A STEAM POWER PLANT COMPUTER SIMULATION By Wayne Andrew Thelen A THESIS Submitted to Michigan State University in partial fulfillment of the requirements for the degree of Masters of Science Department of Mechanical Engineering 1995 RANKI PLANT Ace-apnea prcgrm l W Sim RAN Semi law a. study 5: manly found in m 7' Wilma; a‘n ‘_ .._ Cl i121: pull ‘ a ABSTRACT RANKINE 3.0: A STEAM POWER PLANT COMPUTER SIMULATION By Wayne Andrew Thelen A computer program has been developed which models the thermal performance of any Rankine cycle based power system. The focus of the development was to create a user friendly, PC compatible program capable of modeling a complex, user specified Rankine cycle based system and provide a basis for optimizing the design and operation of a steam power system. RANKINE 3.0 is a modular program capable of performing a first and second law steady state analysis on any user specified combination of thermal devices commonly found in steam power systems. As a result of the software's flexibility, user friendliness, and internal checks, RANKINE 3.0 is ideal as an educational tool and for preliminary design calculations. The computer program's theoretical basis, objectives, modular structure, and bench marking are discussed. Copyright by Wayne Andrew Thelen 1995 LIST OF TABLES usr or FlGl'RES ClllmR 1 Th: Rankine 1-0 “r113: 1'1 Mia: 1.2 1.3 33312121 Pen'l QUE Code Strum“ 2.0 Code 0. 2‘1 1“?qu 2'2 Inpu: F1 2'3 TIErmo 2'4 Output] 2'5 CodeM 26 Program TABLE OF CONTENTS LIST OF TABLES LIST OF FIGURES CHAPTER 1 The Rankine Cycle and Procedure for System Analysis 1.0 The Rankine Cycle 1.1 Procedure for System Analysis 1.2 Pervious Work and RANKINE 3.0 Objectives 1.3 Sample Input File, ECHODAT File and Output File 2 Code Structure 2.0 Code Overview 2.1 Input File Processing 2.2 Input File Checking 2.3 Thennodynamic Analysis 2.4 Output Processing 2.5 Code Modifications for Additional Thermodynamic Models 2.6 Program Limitations 3 Thermodynamic Modeling and Overall System Evaluation 3.0 Thermodynamic Devices 3.1 The Conservation Principles 3.2 The SIMPLE BOILER Device iv PA GE 11 12 14 17 21 35 41 57 61 63 68 3.3 The SIMPLE TURBINE Device 76 3.4 The SIMPLE PUMP Device 83 3.5 The SIMPLE PIPE Device 87 3.6 The SIMPLE JUNCTION Device 92 3.7 The SIMPLE CONDENSER Device 97 3.8 The SIMPLE HEAT LOAD Device 101 3.9 The SIMPLE OFW HEATER Device 105 3.10 The SIMPLE STEAM TRAP CFW Device 110 3.11 The SIMPLE MOISTURE SEPARATOR Device 119 3.12 The SIMPLE REHEATER Device 126 3.13 Overall System Performance Evaluation 135 4 Code Testing and Verification 4.0 Code Testing and Verification Overview 138 4.1 Active testing efforts 138 4.2 Passive testing efforts 154 5 RANKINE 3.0 User‘s Guide 156 6 Conclusions and Recommendations 6. 1 Conclusions 198 6.2 Recommendations 198 APPENDIX PAGE A Summary of comparison between RANKINE 3.0 and band 200 calculations for individual device verification B RANKINE 3.0 input files for individual device verification 213 C RANKINE 3.0 output files for individual device verification 231 D Hand calculations for benchmark case #1 through case #5 249 E RANKINE 3.0 input file for benchmark case #1 through 257 case #5 F RANKINE 3.0 output files for benchmark case #1 through 270 case #5 Hand calculations for benchmark case #6 281 H RANKINE 3.0 input file for benchmark case #6 285 l RIXKLVE 3. Bibliography I RANKINE 3.0 output file for benchmark case #6 289 Bibliography 293 TABLE TABLE 2- 1 2-2 2-3 24 2-5 2-7 2-8 2-9 2- l 0 2-1 1 2- l 2 2- 1 3 2- 1 4 2- 1 S 2- 1 6 2-17 2- 1 8 2- 19 2-20 2-2 1 2-22 4—1 Subroutine nomenclature Summary of 21151 key phrases Summary of subroutine RANKIN key phrases Thermodynamic models lst key phrase library System related variables Interpretation of DVCDAT(#,1) element Organization of the DVCDAT(100,30) array Organization of the ADDDAT(100,20) array Storage of information related to nodes Required system information Summary of device requirements checked by RANKINE 3.0 Summary of local variable nomenclature Summary of ICALLs and IFINDs Model specific constraints checked by RANKINE 3.0 Requirements to fix a thermodynamic state Steam table units Summary of device total variables Summary of system performance variables System mass and energy balance variables Node data abbreviations Device data abbreviations Subroutines required for new thermodynamic model Unique sets of information required to fix a simple pipe device PAGE 18 23 25 29 30 3 1 32 36 36 $883 56 56 57 58 59 139 4—2 4-3 4-5 4-6 4-7 4-8 4-9 5-1 5-2 5-3 5-4 5-5 5-6 Summary of input parameters for benchmark case #1 to #5 Figures of merit comparison for benchmark case #1 Figures of merit comparison for benchmark case #2 Figures of merit comparison for benchmark case #3 Figures of merit comparison for benchmark case #4 Figures of merit comparison for benchmark case #5 Input parameters for benchmark case #6 Figures of merit comparison for benchmark case #6 ‘ Summary of general key phrases Summary of device specific key phrases Summary of 21!!! key phrases Summary of output file abbreviations Requirements to fix a thermodynamic state Data for example problem #3 146 147 147 148 148 148 151 153 160 161 163 165 176 188 FIGURE PAGE 1-1 Schematic of a simple Rankine cycle 1 1-2 T-S diagram for a simple Rankine cycle 2 1-3 Schematic of the simple reheat Rankine cycle 7 1-4 T-s diagram for a simple reheat Rankine cycle 8 1-5 Schematic of the simple regenerative Rankine cycle 9 1-6 T-s diagram for a simple regenerative Rankine cycle 9 2-1 Overview of RANKINE 3.0 Code Structure 17 2-2 RANKINE 3.0 pseudo flow chart 20 23 Basic structure of input processing subroutine 22 2-4 Basic structure of node checking logic 40 2-5 Basic structure of subroutine RANKAI 42 3-1 ' Symbolic representation for a SIMPLE BOILER device 69 3-2 RAN KINE 3.0 variables for the SIMPLE BOILER device 69 3'3 Symbol for a SIMPLE TURBINE device 77 34 RANKINE 3.0 variables for the SIMPLE TURBINE 77 3-5 Symbol for a SIMPLE PUMP device 83 $6 RANKINE 3.0 variables for the SIMPLE PUMP device 83 3-7 Symbol for a SIMPLE PIPE device 87 3‘8 RANKINE 3.0 variables for the SIMPLE PIPE device 88 3‘9 Symbol for a SIMPLE JUNCTION device 92 3-10 RANKINE 3.0 variables for the SIMPLE JUNCTION 93 device 3-11 Symbol for a SIMPLE CONDENSER device 97 il 31 53 RINGS? do“ Symbol for RANKINE dm Smbo‘; f0: RXXKIXE do: Synbol for RANKINE CF Smbo'; f0: RANKIN: SE 557350‘; ft) RANKINE 351m in Spica: la} Sl'Stm 1.2.3 Sl'Sttm 13‘, System lav SlStcm la' Schema: 83‘ 31312; Schmidt schtmati; 3-12 3-13 3-14 3-15 3-16 3—17 3—18 3-19 3-20 3—21 3-22 4-1 4-2 4—3 45 46 5-1 5-2 5-3 5-4 RANKINE 3.0 variables for the SIMPLE CONDENSER device Symbol for a SIMPLE HEAT LOAD device RANKINE 3.0 variables for the SIMPLE HEAT LOAD device Symbol for a SIMPLE OFW HEATER device RANKINE 3.0 variables for the SIMPLE OFW HEATER device Symbol for a SIMPLE STEAM TRAP CFW device RANKINE 3.0 variables for the SIMPLE STEAM TRAP CFW device Symbol for a SIMPLE MOISTURE SEPARATOR device RANKINE 3.0 variables for the SIMPLE MOISTURE SEPARATOR device Symbol for a SIMPLE REHEATER device RANKINE 3.0 variables for the SIMPLE REHEATER device System layout for benchmark case #1 System layout for benchmark case #2 System layout for benchmark case #3 System layout for benchmark case #4 System layout for benchmark case #5 System layout for benchmark case #6 Schematic for single tln'bine example problem Schematic for example problem #1 Schematic for example problem #2 Schematic for example problem #3 98 101 102 105 106 111 111 120 120 126 127 141 142 143 144 145 150 159 178 181 190 Chi terl The R1 lit The Rankine ‘1 1‘ pg. 1 . . ~ ' .uf YELLOL: 0: mt“; 77. a ti".- .. .. -‘ .. ' diligent L‘Llc ed. inseam: process: r“ Sit-cc the Rent: :gofiwzho h .Iu t _ . not: Slilt‘filS. lb 3 :1 :3aa'1h e :bu‘§n Bison 5‘ Rteri$ Mom I“: laid LhtflhOd} 733: iziicclclc. In '31? "neodymium pix?“ Stool: working fiui.‘ in. fluid is v alcr. tin-:15 shown hole“ 1' I 0H Change: 1 The Rankine Cyele and Preeedgre for System Analysis We The operation of most major electrical generating stations are based upon a theoretical thermodynamic cycle called the Rankine cycle. The Rankine cycle consists of a series of thermodynamic processes intended to convert energy in a heat form to energy in a work form. Since the Rankine cycle is the foundation for most vapor powered electrical generating systems, its analysis is vital to the design and operation of both electric and co-generation systems. llllTlS'lBl'Cl The ideal thermodynamic cycle for a vapor powered system is refereed to as the Simple Rankine cycle. In the simple Rankine cycle, the working fluid undergoes a series of thermodynamic processes and finally returns to its initial state. Since water is the most common working fluid used in vapor powered systems, it is assumed that the cycle working fluid is water. A schematic of a power plant operating on the simple Rankine cycle is shown below in Figure 1-1. . Turbine -> Wout @flL |\ Qin —>| Boiler l @- Condenser 1+ Qout + . Win Figure 1-1. Schematic of a Simple Rankine cycle . - ‘ 1 ------ V run-pr, E“ illnlhlanu 3h: .‘SIII’ :\ . . ,. say-V" i'h ’3' r vn't an}: 0. of it-..O»\ ...r . t ,‘l gzx’ihwafnv,‘, 4. t "“4“ liL'\r\ u. 3.4-5“ ' "th . a‘ . sac: with owns it "\v“t idolllllgam 1’: 353w. tkmea‘ifid \L “L mums \v ‘ (2.3%?" Ofk 1 2 By definition, the simple Rankine cycle does not involve any internal irreversibilities and consists of the following four processes: 1-2 2-3 3-4 4-1 Isentropic compression in a pump Constant pressure heat addition in a boiler Isentropic expansion in a turbine Constant pressure heat rejection in a condenser A temperature-entropy diagram (T -s diagram) graphically illustrates the thermodynamic processes which occurs within a cycle. The T-s diagram for the simple Rankine cycle is shown in Figure 1-2. Figure 1-2. T-S diagram for a simple Rankine cycle In the simple Rankine cycle, water enters the pump at state 1 as a saturated liquid and is compressed isentropically to the operating pressure of the boiler. During this isentropic compression, the water temperature increases due to a slight increase in the water's density. Water enters the boiler as a compressed liquid at state 2 and leaves as a superheated vapor at state 3. The water absorbs heat originating from combustion gases, a nuclear reactor or other sources and the working fluid pressure remains constant during the heat transfer. The superheated water vapor at state 3 enters the turbine where it expands isentropically and produces work by rotating a shaft connected to an electric generator. The water Vapor pressure and temperature decrease during this process and the working fluid exits the turbine as a liquid-vapor mixture. ‘ " libel. UFESSLLT .iq.. . . . ,‘awaa‘. A. 1A1: l5 t0-.ll.r..\. on c a 11“- ,- - ' b 1‘. iALinACI Di \L\ ht ”9,rt:‘; "!"".". ‘WW‘R or. ultra} nib pUuwt \ ln-t .\ I L I '., ‘ ,, ,‘, -,. .itfl rears: 0. he Rt. _. a: 14...: L... t- it if .iquiu plain):- It": - ‘ I ‘ t N t‘e‘flu Nhnfi‘s-' 9‘] “TA trumktlélllkd. I). 'A. I: 52.12;}: Raine :3 :l: :26: born" «also ref-c: “it n‘oisnt executes 1 Staci: again. A c3 :1: an: fluid: taxation Raine cycle. as ShOv allied to rrprcsem to: ill . 1h genera: title Silt efficien: ‘l-h...‘ ' Let!"- P. '. not. oi on. the: A ”’3 valuatin ti “1“ MW therm'Od in lit-“ma oifxcier E the The low pressure liquid-vapor mixture at state 4 enters the condenser where the 2-phase mixture is condensed at a constant pressure by rejecting heat to a cooling medium such as a lake, a river or the atmosphere. Steam exits the condenser as a saturated liquid and enters the pump, completing the cycle. A key feature of the Rankine cycle is that the working fluid compression is confined only to the liquid phase. The advantages of this arrangement are that the high compression work and mechanical problems associated with 2-phase compression are avoided. The simple Rankine cycle may be operated as either an open or closed cycle. A cycle is termed "open" (also refereed to as a non-condensing cycle) if the working fluid is drawn from ambient, executes the cycle once and is then discharged to ambient never to repeat the cycle again. A cycle is termed "closed" (also refereed to as a condensing cycle) if the same fluid repeatedly executes the various processes within the cycle. The simple Rankine cycle, as shown in figure l-l, represents a closed cycle. Figure 1-1 could be modified to represent an open cycle by replacing the text "condenser" with the text "ambient". In general, a closed Rankine cycle is usually utilized since it possesses a higher cycle efficiency and permits better control of working fluid chemistry. For the remainder of this chapter, all cycles are considered to be closed. The overall thermodynamic performance of the Rankine cycle is quantified with the 1.51 law thermal efficiency. For the Rankine cycle, the 151 law thermal efficiency is defined as the ratio of the net work produced to the total heat supplied. Mathematically, the l§1 law thermal efficiency is defined as W -W nth-=1VLI=_W_M_=1_% H 2. 0.. Q. where the work and heat terms are specified in Figure 1-1. If Changes in the kinetic and potential energies are neglected, the heat transferred during a 1' eversible process may be represented by the various areas on a T-s diagram. For the ‘ ~ " ‘1 .1 5:73.: Rams :ltlc. tr. A l i} till-l-I-B-‘t-b. a: ' ' ' J n r- 1 reasoned b\ are a- u- . I - 1 £31.33.) ca“. he define; trimaran l-I. ll :3 tartar: a1 Mint is. lite: heat :3 nirctci he demodyrimcil. x triolcloscd operatx [£2101 cyclc. The Ca ahead and too ail: bisrgoing a qclc or Lair obtainable l5 Aid at: a. bi; “1:1: “ ‘ “Cl and 13 j. 4 simple Rankine cycle, the heat transferred to the working fluid in the boiler is represented by area a-l-2—3-4-b, and the heat rejected by the working fluid in the condenser is represented by area a-l-4-b. Therefore, for the simple Rankine cycle, the thermal efficiency can be defined as areaa-1-4- b 1-2 area a-1-2-3—4- b From equation 1-2, it can be seen that any cycle modification that increases the average temperature at which heat is supplied to the system or decreases the average temperature at which heat is rejected from the system will increase the thermal efficiency of the cycle. The thermodynamically maximum obtainable lfil law thermal efficiency for any cycle (open or closed) operating between two constant temperature reservoirs is defined by the Carnot cycle. The Carnot Cycle is composed of four reversible processes - two isothermal and two adiabatic and may be applied to any vapor or two phase substance undergoing a cycle operating between two constant temperature reservoirs. The maximum obtainable 151 law thermal efficiency is commonly refereed to as the Carnot cycle efficiency and is defined as 1'lth,carnot = 1 - 1'3 Where TL = absolute temperature of low temperature reservoir TH = absolute temperature of high temperature reservoir. Even though the Carnot cycle is very difficult to operate in reality, it is of great value since it represents a standard against which any cycle operating between two constant temperature reservoirs may be evaluated. It should be noted that equation 1-3 indicates that an improved Carnot cycle efficiency may only be obtained by reducing the temperature at which heat is rejected by the system or by increasing the temperature at which heat is added to the system. Since a simple Rankine cycle 131 law thermal efficiency definition makes no reference to the best possible performance for a cycle operating between two temperature reservoirs tit. Cmor cycle cffi: Elam. In order :0 Memorable con-ii: iii illl' cffetvtncss is rim anon. nth ”hi-a" Sm m R3331: cy.‘ m “a in tilt form of m“ Onyclc efficic mm from a Cycle TAM ‘0 add'tss ti - (Alaiiabilirw p (Al'ailabfiiq. C0! ‘i‘i‘m adjusnd hear is l 5 (i.e., Carnot cycle efficiency), the magnitude of the 151 law thermal efficiency may be misleading. In order to quantify the performance of a cycle relative to its performance under reversible conditions while operating between the same temperature reservoirs, a 2nd law effectiveness is defined as nth 1-4 1leffectiveness = "— TI th,camot where "th and "th are define as equations 1-1 and 1-3 respectively. ,car not Since some Rankine cycles applications are intended to have useful outputs or inputs that are not in the form of heat or work (co-generation power plants for example), some measure of cycle efficiency is required which provides “credit" for energy provided to or extracted fiom a cycle in forms other than heat or work. The 2nd Law efficiency was established to address this problem and is defined by the author as __ Availability Produced by Cycle 811 " . . . 1-5 Availablllty Consumed by Cycle e = (Availability Produced) + (Work Produced) + (Adjusted Heat Produced) - 11 (Availability Consumed) + (Work Consumed) + (Adjusted Heat Consumed) Where adjusted heat is defined as Adjusted heat =[1 - “WSW J-Q 1-7 heat reservoir Where: Tdead state = Absolute dead State temperature Theat reservoir = Absolute temperature of reservoir at which heat is coming from or is going to. llliiI . llEffi' fllS'lBl'Cl Since the Rankine cycle is responsible for a majority of the electric power in the world, even small increases in the thermal efficiency can justify modifications to the simple Raise :}cic. The f ‘ p' ..-“I Q 9’» '- ?lffat Sfutlfllt} O. t: . —...Y. a, _ 0 '1 I" ' Ehr‘,'i15c to he sort- . M ' 0' 0‘ ‘ Rifttt‘tl .inlI‘; tilt “07k 23335113 3ft GISCUMCC i' D°"=7§° .l._, ...‘- chokeb up» \'. .. \— mil’Wr 'i‘m L .fint “lull“ LIA; n0 ‘P.I‘~r“, ‘ lamented) lO‘At‘.‘ ti :hich heat is re. axing: temperanr: increase the atria-‘5 them efficiency Illcrtt'tili‘ig me boo-- “id- hcncc. decrees. (1:3thng mos: 6 Rankine cycle. The fundamental idea behind all modifications intended to increase the thermal efficiency of a power cycle is to increase the average temperature at which heat is supplied to the working fluid or to decrease the average temperature at which heat is rejected from the working fluid. Three common methods used to increase the thermal efficiency are discussed below. 1) W - Since the working fluid exists as a saturated mixture within the condenser, the lowering of the condenser operating pressure automatically lowers the temperature of the working fluid and, thus, the temperature at which heat is rejected. 2) WW - Since the thermal efficiency is related to the average temperature at which heat is supplied, increasing the boilers superheat will increase the average temperature at which heat is supplied and, hence, increase the thermal efficiency. It should be noted that, for a fixed boiler operating pressure, increasing the boiler exit temperature shifts the cycle to the right on a T-s diagram and, hence, decreases the moisture content of the steam at the turbine exit. The decreasing the moisture content at the turbine exit is a desired result. 3) Wm - Since the working fluid undergoes a phase change within the boiler, increasing the boiler operating pressure will automatically increase the temperature at which the phase change occurs and, thus, the average temperature at which heat is supplied. It should be noted that, for a fixed boiler exit temperature, increasing the boiler pressure shifts the cycle to the left on a T-s diagram and, hence, increases the moisture content of the steam at the turbine exit. The increasing moisture content at the turbine exit is not a desired result. Each of these methods do, however, have some limitations as to there applicability. Improving the thermal efficiency by decreasing the condenser pressure is limited such that the working fluid temperature in the condenser must be greater than the temperature of the low temperature reservoir. Since the working fluid exists as a 2-phase mixture within the condenser, the condenser operating pressure must have a corresponding saturation temperature which is greater than the temperature of the low temperature reservoir. Improving the thermal efficiency by increasing the boiler exit temperature is limited by the maximum meterlogically safe temperature of the components in the cycle. Improving the cycle efficiency by increasing the boiler exit pressure is limited with . ‘ - .0 'I 4;. assert a he mm: C ‘l 1“ :- ‘V‘ Q or ml: island ‘ 'V . G‘ ‘1. - I Rio 2 do: tar. t. s.” 4.. . Ignitli’llli lilif’ldxi I iii The S imple‘ , r ; Oilf O: the iliTi...‘..l ..,.' {1. . mind. fliitlffid 1 ._,..; . . t.l...\i.lf morsture Embed turbos l .i' ; priority 0‘. triple Rankine o rare ' 5km“ In‘xm it? 1] ‘_ {lot is shown in l 7 respect to the fact that the higher boiler operating pressures result in increased moisture content at the turbine exit. Excessive working fluid moisture within the turbine decreases the turbine efficiency and may increase turbine blade wear. Modifications to the simple Rankine cycle can address some of these concerns and may result in a cycle with a significantly increased thermal efficiency. . ' le One of the limitations associated with increasing the boiler pressure to improve the thermal efficiency is the resulting increase in moisture content at the turbine exit. Since excessive moisture within the turbine decreases the turbine efficiency and may result in increased turbine blade wear, minimizing the moisture content within the turbine is a design priority. One solution to the excessive turbine moisture problem is to modify the simple Rankine cycle by expanding the steam through two turbines and reheating the steam in-between. A schematic of a power plant operating on the simple reheat Rankine cycle is shown in Figure 1-3. Qin —> Boiler (I i P Q I Condenser —> Qout Win Figure 1-3. Schematic of the simple reheat Rankine Cycle The simple reheat Rankine cycle differs from the simple Rankine cycle in that the isentropic expansion takes place in two stages. The reheating process removes any mOisture which may exist and superheats the working fluid. In addition to addressing the eXcessive moisture problem, the reheating process also improves the cycle efficiency by increasing the average temperature at which heat is added to the working fluid. This . r- ”" am: fill? bf >55" ‘ 4, F122“: l ¥ . '1' 9' m PA," hectare te...o:.a.. b a I?” Met. more with the ad. diconpitiit) do not; odious york potion do i“: an more»: it. iigticrnl of this it: imitate and the it: :30: CTTlClCTlClCS due 1 J L lo reheating. a : mimic reduces th .4 lb 13 percent for a ; bow Lit‘tld that The TC? it‘s: the boiler. M boiler: mmon/j' used COHSIS Hg.) The work "Wit borlcr increase 1 “c ““6 Sl’Sltm's therm. 8 increase can be seen on the simple reheat Rankine cycle T-s diagram shown in Figure l- 4. T N a b S Figure 1-4. T-s diagram for a simple reheat Rankine cycle The average temperature at which heat is added to the working fluid may be increased even more with the addition of a second or third reheat leg but, usually, the added cost and complexity do not justify such a modification. Previous work performed by Reynolds and Harris and White indicate that reheating results in an increase in the 151 law thermal efficiency of approximately 5 percent. About 40 percent of this improvement comes from adding heat at a higher than average temperature and the remaining 60 percent comes from improvements in the turbine stage group efficiencies due to reduced moisture and increased reheat factors. As compared with no reheating, a system with a single reheat leg reheating to the initial boiler temperature reduces the throttled and condenser steam flow rates by approximately 17 and 13 percent for a given turbine power output. Reynolds and Harris and White recommend that the reheat pressure should be between 15 to 30 percent of the pressure exiting the boiler. Another commonly used method for increasing the thermal efficiency of a steam power plant consists of regenerative feed water heating. Since a system's thermal efficiency can be increased by increasing the average temperature at which heat is supplied, reheating (or regenerating) the working fluid with extracted turbine steam before the working fluid enters the boiler increases the average temperature at which heat is supplied and, hence, increase the system's thermal efficiency. A schematic of a power plant operating on the I it R Sm: 325351155 v-__, ‘§ ['1 fl'y. :w Rare 1 The simple regeneratzl fraction of the mass T hiring betueeri the t ocle consists of op:- tit-tenor. steam and it iéltftmprOVCS the S} opp-Tied to the S} stem iterzers ‘he boiler car. “i- . ‘ 5:137; l’.‘ . Figure l6. Figure HS. T 9 simple regenerative Rankine cycle with a single open feed water heater is shown in Figure 1-5. Turbine + Wout @T |\ Qin -’l Boiler I @— _ 7 Open 7 6 I Feed te wa r Condenser +Qout + Heater Win Win Figure 1-5. Schematic of simple regenerative Rankine cycle The simple regenerative Rankine cycle differs from the simple Rankine cycle in that a fraction of the mass flow through the turbine is extracted to preheat the feed water traveling between the condenser and the boiler. Since the simple regenerative Rankine cycle consists of open feed water heaters which permit direct contact between the extraction steam and the feed water, two pumps are required. The preheating of the feed water improves the system thermal efficiency since the average temperature of heat supplied to the system is increased. The advantage of reheating the working fluid before it enters the boiler can be seen on the simple regenerative Rankine cycle T-s diagram shown in Figure 1-6. rm. t’ :\ t . . Figure 1-6. T-s diagram for simple regenerative Rankine cycle Bi tension. 2.1. pm a o iniicncc n: 2:- i‘diurbuh he: is he 3)ch. lt shotl.‘ stzpie regeneratise R. 31.1. a “.JZL" 41501115.? tradition to 'he imp: «owes no. a: enters the bozler. therr itinerlsatoidcd. in a. in: condensate that e mingle: ant. Euro: 1.0.6 Additional Ral it: 1“0 fundamen'.” t: :mnC) are {char {Cairn} Fling .1ch 03161 the; ofllntjd'nom ‘ tn: .. t 5171 {if rehem F ktheen the high and Sim-Moisture Sci :‘NIOCH‘ t Hank re 5 Jll )2 ~) [chi L'E‘Catcd (.apOr T {RTE ' E‘ ‘L A . t 4 . d “R The S l ‘‘9 a 15R bl‘ me remain 10 By definition, all processes within the simple regenerative Rankine cycle are reversible and, hence, the heat transfer during the cycle may be represented by the various areas on the T-s diagram. The enclosed area on the T-s diagram represents the net work produced by the cycle. It should be noted that the addition of the open feed water heaters in the simple regenerative Rankine cycle reduces the enclosed area (and, hence, the work output), but also reduces the heat supplied in the boiler. In addition to the improved cycle thermal efficiency, the simple regenerative Rankine cycle possesSes two additional positive features. By preheating the feed water before it enters the boiler, thermal shock resulting from pumping 'cold' feed water into a 'hot' boiler is avoided. In addition, turbine blades can be designed to drain a majority of the liquid condensate that exists in the turbine, and hence, turbine stage group efficiency can be maximized and turbine blade wear can be minimized. The two fundamental techniques used to increase the Rankine cycle's 151 law thermal efficiency are reheating and regenerating. In modern Rankine cycle based designs, components other than reheat legs and open feed water heaters may be utilized to apply these two fundamental techniques and achieve improved 151 law thermal efficiency In the simple reheat Rankine cycle, a reheat leg was used to reheat the working fluid between the high and low pressure turbines. In some modern Rankine cycle based designs, Moisture Separator Reheaters (MSR) are used to accomplish the identical thermodynamic result. Physically, a MSR accomplishes two functions: (1) extracts all entrained moisture from the working fluid traveling between the high and low pressure turbines, and (2) reheats the saturated vapor component of the working fluid to a superheated vapor. The two phase working fluid exiting the high pressure turbine is separated into a saturated liquid and saturated vapor by the moisture separator component of the MSR. The saturated liquid removed by the MSR is drained to the feed water heaters and the remaining saturated vapor is reheated in the reheating component of the MSR by steam that is extracted from the high pressure turbine or the single steam line exiting the boiler. The working fluid extracted by the MSR and the condensed reheat steam exiting the MSR are both drained to the feed water heaters. The advantages of this setup are that the low energy component of the working fluid (saturated liquid) is first ' " " L 2'. . " . T 'P 594 millet: mile lbttbutt. cots tenure ct 21o;- his simple regeneri'. tiring find i tneer tact testis. close- tandem: nesuit t ‘ . . . . g t q: 0 h at stinger sir.- innit: tunes. The 2 fie: yet-e: heaters is the sting finds and. her. red to be identical. :1 not a pump bets ee: feces. ln acidi'ion. c‘ic inactivation press. 1.0.7 Donations of A .‘i‘t‘t‘ , ““ WW PORT Ctr in: Flint he cycle. Phys titre . . .‘tleTa and heat tics 2' M . “Ts-m- lass effic anointed Sl'S ’0- ‘b'. l 18m dc 11 drained before reheating and only one exit from the boiler is required (Reheat legs are a costly feature of a boiler). In the simple regenerative Rankine cycle, an open feed water heat was used to reheat the working fluid between the condenser and the boiler. In some modern Rankine cycle based designs, closed feed water heaters are used to accomplish the identical thermodynamic result. Physically, a closed feed water heater is usually a shell and tube heat exchanger with "hot" extracted steam within the shell and the "cold" feed water within the tubes. The advantage of utilizing closed feed water heater rather than open feed water heaters is the fact that closed feed water heaters do not permit mixing of the working fluids and, hence, the pressure of the extracted steam and the feed water do not need to be identical. As a result, multiple closed feed water heat exchangers do not require a pump between each heat exchanger as required by multiple open feed water heaters. In addition, closed feed water heaters offer a greater potential to optimize since turbine extraction pressures and feed water heater pressures may be decoupled. Actual vapor power cycles differ from the reversible Rankine cycles discussed in sections 1.0.1, 1.0.4 and 1.0.5 due to irreversibilities within the individual components which are part of the cycle. Physical factors such as fluid friction, undesired heat loss, unrestrained expansion and heat transfer at a finite temperature contribute to a reduction in the cycle's 131 and 211-9- law efficiency. The existence of non-ideal components coupled with complicated system designs make the modeling of modern Rankine cycle based designs very difficult and very time consuming. W The sequence of Steps utilized to evaluate the thermal performance of any system is independent of the system layout or the working fluid. This sequence of steps is collectively refereed to as the Procedure for System Analysis and summarizes the process used to evaluate the thermal performance of any well posed system. The Procedure for System Analysis is stated below. 1) The system lay: '. inst 333 coca-3. 21 The notes hens it'll: ' : systen. 3} Attileisconsm. schsmce‘i‘. Xcii: ; Tint. Rate. 15. AK ll With the giyec. Madman 'c in:1 T- L'sing the state heinodynzric in it The system is tta' etch deyice. This conjuncn'on with 71 with the comp}: ‘ e .. 1‘ . . trounced: is ca‘c 31‘ titling the l n‘teaa'icaily min ’1 .4 . “m“ Drona}- titties 12“ 0f minnOan; ; “an; . . mot-lion Within ; liaiiy‘ ' .‘ "9541123 fora c t' \y P73910115 SOTtWam ems. 5“” The 1'1:er ‘tl~.t,, Wm“- These 2 12 l) The system layout is sketched. The devices representing the various processes are placed and connected according to the system description. 2) The nodes between the devices are numbered. These nodes represent locations within the system where the state of the working fluid is of interest. 3) A table is constructed with the following headings (Assuming a simple compressible substance): Node, Temperature, Pressure, Fluid Phase, Enthalpy, Entropy, Mass Flow Rate, and Availability. 4) With the given operating conditions and system description, all known thermodynamic information is entered on the table. 5) Using the state postulate and the working fluid property tables, all obtainable thennodynamic information is added to the table. 6) The system is traversed, device by device, analyzing the fluid as it passes through each device. This analysis provides additional fluid properties, which when used in conjunction with step #5 systematically completes the table. 7) With the completed table, system information (such as thermal efficiency and work produced) is calculated. By employing the Procedure for System Analysis, any well posed system may be systematically analyzed. In essence, the Procedure for System Analysis uses the working fluid property tables, the physical characteristics of each device type, and the 151 and 2051 law of thermodynamics to systematically calculate all unknown thermodynamic information within a well posed system. The repetitive nature of these calculations is ideally suited for a computer application. 1le I! . Ell lRmImIEMQl' Ii Previous software packages dealing with steam power systems fall into one of three groups. The first group consists of simple program developed for use on hand held calculators. These are normally restricted to considering only the simplest steam power systems and, hence, do not provide a realistic analysis of a steam power system. The second group involves software packages that are designed for classroom use only. Preston et a1. and Cengel and Boles have written programs that analyze the operation of the Rankine cycle for a limited number of the simplest Steam power system. Since the primary use of these programs are for classroom instruction, they are not flexible enough to model modern steam power plant designs. Finally, there are some massive industry .f—H —._..._ I CCEQEIprIiJgTai. s at 21 yer) difttcb': tool. The “5135 '1. 1.1514“. ‘32“3_‘,‘,\ of It: cisteio not: 1 nt of assess: by earizer contacted so of nerdy cf see: in: system lay t layouts tip. 0‘ syscn layout. 1n esse 31112: the rela: o accents. and the sy KATIE: 4 did no “nan: heaters. moistur be user to specify tl catheters in an inn- Tthmhip bC'“f€l‘. iftbeters and syste 'iliftfbal dcyices it. slit-ed. JJJJJOn to great “4.11138 and' Inter JJ whiting“ dey ”‘Syult.al ”yfl.‘ Sil'ltSof‘meberS deaSCneS of 1m JJJJ‘DCTIS Siden 011me g‘TICray ,4 4.1th the 13511130 dtwslt'n ”CSCI' nation and are c( J“?! 13 computer programs available for the analysis of actual steam power system; but these are usually very difficult to use, expensive to maintain, and impractical as an educational tool. The RANKINE 3.0 software package was developed as a continuation of the RANKINE family of computer software. The development of RANKINE 3.0 was intended to remove many of the limitations possessed by earlier versions of RANKINE. The earlier versions of RANKINE contained sets of hardwired code logic which performed a thermal analysis for a finite set .of specific system layouts. Although RANKINE 2.4 contained a total of 28 unique system layouts, it provided no method to quantify the effect of slightly modifying the system layout. In essence, RANKINE 2.4 only provided a method to study (and, hence, optimize) the relationship between the operating conditions, device performance parameters, and the system performance for a finite set of system layouts. In addition, RANKINE 2.4 did not provide any mechanism to study system layouts with closed feed water heaters, moisture separators, or reheaters. RAN KINE 3.0 was developed to permit the user to specify the system layout, operating conditions, and device performance parameters in an input file and, hence, provide the user with a method to study the relationship between the system layout, operating conditions, device performance parameters, and system performance. In addition, RANKINE 3.0 increased the number of thermal devices from eight to eleven, which permits additional system layouts to be studied. In addition to greater flexibility, RAN KINE 3.0 was developed to improve user friendliness and internal checks. In order to use RANKINE 3.0 as an educational tool, the program was developed with an input processor that recognizes a key phrase library. As a result, all RANKINE 3.0 input files are composed of English phrases as opposed to a series of numbers separated by commas. Furthermore, RANKINE 3.0 was developed to include a series of internal input file checks to determine if any inconsistencies exist. If an inconsistency is identified, a diagnostic messages informs the user of the inconsistency. The output generated by RANKINE 3.0 also undergoes a series of internal checks, which includes the results of a mass and energy balance on the various control volumes within the system. These internal checks ensure that code results are based upon valid input information and are correct. km: mp3”. tate. r. mete mile the re. - v - b, q '0 O 0. 9 idiom ill-Oils LOT . The RAH-VF; 3.0 tr 530th below. ' 3L5 1M MAME PR: .' 5W 98.31 l4 . l 'tF' H D TF'e nd ut ut ile. A sample input file, ECHO.DAT file, and output file is included within this section in order to provide the reader with a feel for the input and output format of RANKINE 3.0. The system layout for this sample problem is shown below. l: @+ Wout Qin —>| Boiler Condenser l...’ Qout A Win Figure 1-7. Schematic of sample problem The RANKINE 3.0 input file which describes the system layout as shown in Figure 1-7 is shown below. TITLE LINE SAMPLE PROBLEM END TITLE NUMBER OF NODES IS 4 HIGH TEMPERATURE RESERVOIR: 600.0 DEG C LO“I TEMPERATURE RESERVOIR: 25.0 DEG C DEAD STATE TEMPERATURE: 25.0 DEG C DEAD STATE PRESSURE: 101 KPA GENERATOR MECHANICAL LOSS IS 0.0 MW GENERATOR ELECTRICAL LOSS IS 0.0 MW DEVICE #1: SIMPLE TURBINE INLET NODE NUMBER IS 3 EXTRACTION #1 NODE NUMBER IS 4 STAGE GROUP #1 EFFICIENCY IS 75 PERCENT EXTRACTION #1 PRESSURE IS 0.1 MPA END DEVICE DEVICE #2: SIMPLE CONDENSER EXIT NODE NUMBER IS 1 INLET #1 NODE NUMBER IS 4 END DEVICE DEVICE #3: SIMPLE PUMP SUCTION NODE NUMBER IS 1 DISCHARGE NODE NUMBER IS 2 PUMP EFFICIENCY IS 75 PERCENT END DEVICE DEVICE #4: SIMPLE BOILER BOILER INLET NODE NUMBER IS 2 BOILER EXIT NODE NUMBER IS 3 BOILER EXIT PRESSURE IS 20.0 MPA BOILER EXIT TEMPERATURE IS 600 DEG C BOILER EXIT MASS FLOW RATE IS 50 KG/SEC BOILER PRESSURE LOSS IS 0.0 MPA END DEVICE , qmoDfllltfc‘ f‘ Hist .715 mm!" luulfl'"““ '2"- {$13 C‘VUJI) é \ s53; OF 7: .CES ‘ 3x13 mt \tEC‘ ‘ ‘ -b\:‘ ‘ \‘m‘r tic“ HY .- 9:3 131/55]? .' f5 "IlllllllIIIIIIIIII. TEBIGIV-j’ v35; .35 \Efo IEVFE 9-.- \q- .'..'t:; j:I\ r335» ”Fifi LYNCH. as :U- \: EXTRACTHFR‘ . Tait? GRO‘.‘ rs ET] fl: \‘I M q mun.ul‘::§. 15 ~" $53 Em \0: n" {\SER my 3 ”VJ IRE? 3 PW“ ONCE \‘t \tt'; Iln ”utthlt|‘." . . . . 5J1: EXIT. \l :55; ' 394.350; ‘1 254-8,“ s n K \e... r:’~-. “V: 5 i “ \“‘ i I“ 15 The ECHODAT file produced by RANKINE 3.0 is shown below. TITLE #tttitttttttttttttttttittittt******##** SAMPLE PROBLEM NUMBER OF NODES: 4 NUMBER OF DEVICES: 4 DEAD STATE PRESSURE IS .1010 MPA DEAD STATE TEMPERATURE IS 25.00 DEG C HIGH TEMPERATURE RESERVOIR TEMPERATURE IS 600.00 DEG C LOW TEMPERATURE RESERVOIR TEMPERATURE IS 25.00 DEG C GENERATOR MECHANICAL LOSSES: .000 MW GENERATOR ELECTRICAL LOSSES: .000 MW DEVICE NUMBER 1 IS A SIMPLE TURBINE fittitttttit*ittttttfittfittttttttttfittttt TURBINE INLET NODE NUMBER IS 3 TURBINE INLET TEMPERATURE IS 600.00 DEG C TURBINE INLET PRESSURE IS 20.0000 MPA TURBINE INLET MASS FLOW IS 50.00 KG/SEC TURBINE EXTRACTION # l NODE NUMBER IS 4 TURBINE EXTRACTION # l PRESSURE IS .1000 MPA STAGE GROUP # l EFFICIENCY IS .75 DEVICE NUMBER 2 IS A SIMPLE CONDENSER AAAAAAAAAAAA 4 A; LA LALLALALAALALAALAALLAA vw—vvvvrw ivTVVTvTVTTTVVVVTw—T‘fvrif‘Y-v-T‘V‘T CONDENSER EXIT NODE NUMBER IS I CONDENSER INLET # l NODE NUMBER IS 4 CONDENSER INLET # l PRESSURE IS .1000 MPA PUMP DEVICE NUMBER 3 IS A SIMPLE PUMP _.__._LAAAALAAAALALALLLAALLAL_A__.__.__L.._A_.__.__._A_L_.__.__._ PUMP DISCHARGE NODE NUMBER IS 2 PUMP EFFICIENCY IS .75 DEVICE NUMBER 4 IS A SIMPLE BOILER tttttttltittttttti*itlttttttt‘ttttfitttt BOILER INLET NODE NUMBER IS 2 BOILER EXTT NODE NUMBER IS 3 BOILER EXIT TEMPERATURE IS 600.00 DEG C BOILER EXIT PRESSURE IS 20.0000 MPA BOILER EXIT MASS FLOW IS 50.00 KG/SEC BOILER PRESSURE LOSS .0000 MPA The output file produced by RANKINE 3.0 is shown below. RANKINE 3.0: A steam power plant computer simulation Copyright 1994 W.A. Thelen, C.W. Somerton ******fifiii‘fii‘kl‘tti***************** TITLE ii'ki‘ti'ki‘tiiitti'iti‘ki*tiitiiiiititt .SKMPLE PROBLEM t*fi'*******************t‘ktiiti’ii’i‘ NODE DATA ********************#*********** - run a ( h . vi. or l“ \A’ ~A' 1" l".|“l|““‘!"‘1 to... v-. 16 NODE T(C) P(MPa) L Q S(KJ/KG/K) H(KJ/KG) V(M‘3/KG) M(KG/S) A(KJ/KG) 1 99.63 .1000 4 ***** 1.3020 417.31 00104 50.0000 33.47 2 103.52 20.0000 1 ***** 1.3228 448.50 00105 50.0000 58.45 3 600.00 20.0000 3 ***** 6.5052 3536.61 .01808 50.0000 1601.44 4 99.63 1000 2 .990 7.2962 2651.90 1.67621 50.0000 480.88 itttttiititttii‘kiti‘i‘k ******************** DEVICE DATA (DEVICE BEFORE NODE) NODE REV. WRK ACT. WRK IRREV HEAT X-FER MASS ERROR ENERGY ERROR (KW) (KW) (KW) (KW) (KG/S) (KW) 1 22370.37 .00 22370.37 —111729.90 .000 - 008 2 -1249.04 -1559.60 310.56 .00 000 000 3 71843.58 .00 71843.58 154405.60 000 000 4 56028.13 44235.28 11792.86 .00 000 000 *iitii‘fi‘tii'kii’fiii’fiiififi**i******* SYSTEM DATA ***i***ii’ii’fi‘kii’tfitt*iiffi'fii‘kttii TOTAL MASS FLOW RATE EXITING SYSTEM: TOTAL MASS FLOW RATE ENTERING SYSTEM: TOTAL ENTHALPY FLOW RATE EXITING SYSTEM: TOTAL ENTHALPY FLOW RATE ENTERING SYSTEM: TOTAL HEAT AND WORK ENTERING SYSTEM: -. BOILER HEAT (DEVICE # 4): TOTAL BOILER HEAT: TOTAL HEAT LOAD HEAT: CONDENSER HEAT (DEVICE # 2): TOTAL PIPE ENERGY LOSSES: TURBINE WORK (DEVICE # 1): .0000 .0000 .0000 .0000 0039 154405. 154405. .0000 -111729.9000 6000 6000 44235.2800 NET WORK TO GENERATORS: PUMP WORK (DEVICE # 3): TOTAL PUMP WORK: GENERATOR MECHANICAL LOSSES: GENERATOR ELECTRICAL LOSSES: NET ELECTRICAL POWER: SYSTEM HEAT RATE: CARNOT CYCLE EFFICIENCY: IST LAW EFFICIENCY: 2ND LAW EFFICIENCY: 2ND LAW EFFECTIVENESS: 44235. -1559. -1559. 42675. 12345. 65. 27. 42 41. 2800 6010 6010 .0000 .0000 6800 0200 8535 6387 .8466 9699 KW KW KW KW KW KW KW .0000 KW KW KW KW KW KW KW KW _,_ _ __—._ The basic sanctum c AIMS and can be 333mg. 117W to a A Au» 11.1mm (he mla'i E We: The basic structure of RANKINE 3.0 is directly analog to the Procedure for System Analysis and can be visualized as consisting of four independent sections; input file processing, input file checking, thermodynamic analysis and output processing. Figure 2- 1 illustrates the relationship among the four independent sections of RANKINE 3.0. Input File Output File Figure 2-1. Overview of RANKINE 3.0 code structure The input file is a user written ASCII file that contains a description of the system layout, all known thermodynamic information, and all device performance parameters. In order to increase the user friendliness of RAN KINE 3.0, the input file is created using a key phrases library. Using this key phrase library, the system layout, operating conditions and device performance parameters are communicated to RANKINE 3.0 for the analysis. The input file processor prompts the user for an input file and scans the input file, line by line, for key phrases. When a key phrase is identified, the information contained within the line is interpreted and organized. After the entire input file has been scanned and interpreted, RANKINE 3.0 writes all input file information to an external file named ECHODAT. Inspection of the ECHODAT file clarifies any questions associated with the interpretation of an input file. 17 """I I) ”‘1'" F": 4193““ L4 in,» A“: thsL. map-me and £02325:- mMMmm Tit 5mm; a item. and caculazts ii: Mormon. Ca Egon computerized. s bdhmmRm m} to Bach dcxi: lSCliC‘dizitd. over: lb: 0339113 processi 20ml voiumcs I}. “125m Itsulis t 18 The input file checking section verifies that the information obtained from the input file is complete and consistent. A message is provided to the user in the event that either the input file did not provide sufficient information for an analysis or an inconsistency is identified. The thermodynamic analysis section systematically traverses the system layout, device by device, and calculates all unknown thermodynamic device information based on the input file information. Calculation of unknown thermodynamic device information is based upon computerized steam tables and hardwired code logic that applies the 1st and 2nd law of thermodynamics for a control volume (neglecting kinetic and potential energy terms) to each device within the system. After all possible node and device information is calculated, overall system performance parameters, such as the 151 and 211-51 law efficiencies, are calculated based upon the results of the thermodynamic analysis. The output processing section performs a mass and energy balance on each of the various control volumes throughout the system, prompts the user for an output file name, and writes the results of the analysis to the specified file. The user specified output file summarizes the results of the thermodynamic analysis and all important system parameters. The only communication between the four independent sections of RANKINE 3.0 is through two common blocks; 10 and DEAD. Due to the modular structure of the code, additional thermal models may be written and easily integrated into the existing code structure. Walnut Due to the large number of subroutines within RANKINE 3.0, a set of subroutine nomenclature was developed to simplify the code. A summary of the subroutine nomenclature is shown in Table 2-1. Table 2-1. Subroutine nomenclature R . esentation Artificial intelligence Balance CAIL Calculation FD(STA Fix state 19 Table 2-1. Cont'd Abbreviation SCND condenser model heat load model feed water heater model reheater model Simple moisture model For example, the subroutine INSTRB may be interpreted as the input processing subroutine for the simple turbine model. All subroutines employing other combinations of this nomenclature may be interpreted by strict analogy to this example. As a result of this nomenclature, insight into the exact function of each subroutine may be readily obtained by inspection of the subroutine name. It should be noted that the steam table subroutines do not utilize this nomenclature and, therefore, the function of each steam table subroutine must be interpreted independently. Want The ideal method for examining the relationship among the subroutines within RANKINE 3.0 is through a pseudo flow chart. Figure 2-2 shows the pseudo flow chart for RANKINE 3.0. The interpretation of the pseudo flow chart requires the employment of a set of rules. These rules are summarized below: 1) Capitalized text indicates a subroutine with access to common blocks. Lower case text indicates a subroutine without access to common blocks. 2) A single line indicates a subroutine call. A double line indicates a loop. 3) Begin at the top. The subroutine order of execution is down, left, right and up. .1152 .ud‘kv-x - AEIR<' Hod 32:26? 158 Bevan—pang i Emu—mum mung Eva AOnmUm Ea 28m 968m 580m 33.33% 3.3 3a... 350— DZUwU— HURO— Eau gav— nun—MU— Sag _ 63 Eu g 5:.» n2 ASA—3 E: L j... Figure 2-2. RANKINE 3.0 pseudo flow chart 11ij of Fig. 2-. it FORTH pro ; mm and PAS iipcs: level sum: .. ifulr rain: of - l .0 . atoms of RANKIN Widen: section clashing (RKNKIC ;. iilVKO'). Each of 1.7“. mm the tasks reg high the Wm 52 lithe Wm m3) it w I (lfifi Tn: my? PUT-p03 ‘1‘de mm m ”5‘ Moms of inc c “m “in: Engiisl ml “in: by line c pm is identified 21 Inspection of Fig. 2-2 clearly illustrates the basic code structure. At the top of Fig. 2-2, the FORTRAN program name RANK30 and the 4 subroutines RANKIN, RANKIC, RANKAI and RANKO can be identified. The program name RANK30 represents the highest level subroutine within the program and is responsible for setting variables to a default value of -1.0 (representing an unknown value) and calling the four independent sections of RANKINE 3.0. Each one of the four subroutines represent one of the four independent sections of the program: input file processing (RANKIN), input file checking (RANKIC), thermodynamic analysis (RANKAI), and output file processing (RANKO). Each of these four subroutines contain a set of lower level subroutines which perform the tasks required. The use of the pseudo flow chart facilitates navigation through the program structure and provides a visual method from which the internal flow of the program may be identified. We The primary purpose of the input processing section is to identify the important information within the user provided input file and organize the information such that the other sections of the code can utilize the information. Since RANKINE 3.0 input files are written using English phrases, the search for information within the input file is based upon a line by line comparison of the input file with a key phrase library. When a key phrase is identified within a line, hardwired code logic elects to either searches for information or to call another subroutine to search for information. After the information is obtained from the input file, the information is stored within a set of arrays. When RANKINE 3.0 has completed the scan of the input file, the input file is closed and the only information that is accessible to the other sections of RANKINE 3.0 are the arrays. 21] S . Eli l' BE’II' II I IE'I The identification of information within the input file is based upon a line by line comparison of the input file to a key phrase library. The highest level input processing subroutine is RANKIN and is primarily responsible for obtaining information that affects the execution of RANKINE 3.0 and information revenant to the system but not directly applicable to a single device. The subroutines IN STRB, INSPMP, INSPIP, INS] CT, INSCND, INSHLD, INSCFW, INSBOL, INSCFW, INSSEP and INSREI-I are called from subroutine RANKIN and are responsible for identifying and organizing information pertaining to a specific device type (i.e., simple turbine, simple pump, ect.). lb: sari fore to; air} subroutines; C Whom process-.2 new. input ilk line processing subroutine specie sequence of . mm within Ii isoo. located the in: ft: seeding the 8C seeoeoee of numb: manor] of the some for an in 'l “Lyn 4. E undo! 5i: FIE—l E SE “C Fl g1 22 The search for a key phrase or number within an input file line is accomplished by three utility subroutines; GETLIN, FNDSTR, and FNDNUM. Subroutine GETLIN is called by all input processing subroutines to open or close the input file as needed and read the next input file line as a 80A1 format. Subroutine FNDSTR is called by all input processing subroutines to search the 80Al character suing, character by character, for a specific sequence of characters. If a character sequence is located, an integer flag is set to the location within the string that the sequence is identified. If the sequence of characters is not located, the integer flag is set to -l. The utility subroutine FNDNUM is responsible for searching the 80A1 character string, character by character, for a number. After a sequence of numbers is located within the 80A1 string, the equivalent numerical representation of the sequence of numbers is determined. Figure 2-3 illustrates the basic structure for all input processing subroutines. file [ CallFNDSTR FE“ Searchformoreinfomution I.— - i m, l (=me H Searchformoreinformation |-—— l Matcha'END DEVICE l v w Call FNDSTR IF -——-.| Exit Subroutine I Figure 2-3. Basic structure of input processing subroutine 23 Usually, the first key phrase within a line is sufficient only to describe a position on a specific device. For example, a 151 key phrase such as FEED WATER INLET specifies a position on a device (in this case, an open feed water heater) but no thermodynamic information at this position. In many instances, a 2&4 key phrase is required to specify information pertaining to a particular position. For example, the phrase THE FEED WATER INLET TEMPERATURE IS 197.2 DEG F specifies a position on an device and a piece of thermodynamic information at the position (in this case, a temperature). Frequently, the identification of a 2nd key phrase, a number, and units is accomplished within the utility subroutine FNDINF. The utility subroutine FNDINF is called throughout the input processing subroutines after a 151 key phrase has been identified and a 2911 key phrase is expected. The purpose of subroutine FNDINF is to identify a 2351 key phrase, a number (if expected, based on the 211d key phrase), and the units of the number. The identification of the 2351 key phrase and a number within the 80A1 character suing is accomplished by the utility subroutines FNDSTR and FNDNUM respectively. In addition, subroutine FNDINF applies the appropriate conversion factors to all numbers such that 8.1. units are calculated and stored internally. Table 2-2 contains a list of the acceptable 2351 key phrase and recognized units. In the event that units are not provided within the character string, the number is assumed to be in 8.1. units. Table 2-2. Summary of 2E1 key phrases 3“! iii. HG GAUGE. INCHES HG ABSOLUTE. INCHES SATURATED V Would be note; 80A} chance! exezuion is 510;; sly Miss The highest 1C) Rim. Sub: the section of W to a sac. mm “1.510an ILA“ 53 w ‘ r1 ‘ tr/‘I ’1 i 6; (r1 - r _- n 11 -,_v ' 'v > s C? c "1 $3! AM" I £T' l «‘3 O - P’ ;_-. '1'. I ) (11 ‘1. SI" 51W; I - 1/ 7 r3 1:, E .P . E I E I; :1 u’ is (Q [R a; 24 It should be noted that if a 2114 key phrase is expected and is not contained within the 80A1 character string, a diagnostic message is provided to the user and program execution is stopped Wilma! The highest level input processing subroutine within RANKINE 3.0 is subroutine RANKIN. Subroutine RANKIN is responsible for interpreting 151 key phrases that affect the execution of RANKINE 3.0 and information relevant to the system, but not directly related to a specific device. Table 2-3 contains a list of all 151 key phrases identified within subroutine RANKIN and their impact on the code logic. Table 2-3. Summary of subroutine RANKIN key phrases. 1a Ke Phrase COMMENT Stops RANKINE 3.0 from scannirg the current line. ECHO OFF Indicates that input file information should not be written to the external data file ECHODAT. INPUTCHECKOFF Indicatesthatinputfilecheckingwillbebypassed. Itisreccrnrnended that this feature not be used. lTERATION OFF Indicates that RAN KINE 3.0 should not iterate to converge on a solution to the system. TITLE Indicates the beginning of title information. If a title is include within the input deck, the title information will be written to the output file. The title may be up to 10 lines long. END TITLE Indicates the end of the title infogation. NUMBER OFNODES Indicatesthenumberofnodesinthe system. Thiskeyphraseis followed by a number corresponding to the number of nodes (up to 100) in the system. HIGH TEMPERATURE Indicates the temperature of the hot reservoir with which the system is RESERVOIR interacting. Acceptable units are 'DEG C', 'DEG F, 'DEG R', DEC 14'. LOW TEMPERATURE Indicates the temperature of the cold reservoir with which the system is RESERVOIR interacting. Accgtable units are 'DEG C', 'DEG F', 'DEG R', 'DEG K'. DEAD STATE Indicates a property of the dead state will be specified (such as a temperature or pressure). A second key phrase is expected. GENERATOR Indicates that the Generator Mechanical Losses are known and should MECHANICAL LOSSES be considered. Acceptable units are KW, MW, BTU/HR, HP. GENERATOR Indicates that the Generator Electrical Losses are known and should ELECTRICAL LOSSES be considered. Acceptable units are KW, MW. BTU/HP, HP. SIMPLE TURBINE Indicates that information pertaining to a simple turbine device will be specified. SIMPLE PUMP Indicates that information pertaining to a simple pump device will be specified. SIMPLE PIPE Indicates that information pertaining to a simple pipe device will be specified. SIMPLE JUNCTION Indicates that information pertaining to a simple junction device will be specified. SIMPLE CONDENSER Indicates that information pertaining to a simple condenser device will be specified. SIMPLE HEAT LOAD Indicates that information pertaining to a simple heatload device will be - - ' ted. 18 Its PM. ME Sim Tu} The subroutines [V S 1 33301. IVSCFW. 1 son an input file u soon that the other a made! specific subtt Pbsis identified ti W: Specific input 331th Visually rt‘ WW and teen ' in“ Processing St Mutation teiatec 25 Table 2-3. (cont'd) or K. Phrase SIMPLE OFW HEATER Indicates that information pertaining to a simple open feed water heater device will be Qecified. SIMPLE BOILER Indicates that information pertaining to a simple boiler device will be specified. SIMPLE STEAM TRAP CFW Indicates that information pertaining to a simple steam trap closed feed water heater device will be m‘fied. SIMPLE MOISTURE Indicates that information pertaining to a SEPARATOR simple moisture separator device will be specified. SIMPLE REHEATER Indicates that information pertaining to a sim-le reheater device willbe «3 ified. The subroutines INSTRB, INSPMP, INSPIP, INSJCT, INSCND, INSHLD, INSCFW, INSBOL, INSCFW, INSSEP, and INSREH are responsible for identifying information within an input file related to a specific device type and for organizing the information such that the other sections of the program can utilize the information. Each of these model specific subroutines are called from subroutine RANKIN whenever a 131 key phrase is identified that indicates device specific information. The basic structure of each model specific input processing subroutine is similar to that of subroutine RANKIN and may be visually represented by Fig. 2. The primary difference between subroutine RANKIN and each model specific input processing subroutines is that the model specific input processing subroutines focus on information related to a specific device, not information related to the system. Utilizing this type of organization facilitates the introduction of new thermodynamic models into the existing code structure. Table 24 contain a summary of the 151 key phrase library for each model specific input processing subroutines. Table 2-4. Thermodynamic models 15! key phrase library SIMPLE TURBINE INLET Yes p...r 2nd by pm ‘ ' Exraacnonv #_ Yes pa 2nd key pm... STAGE GROUP a. No 95. PERCENT EFFICIENCY _ DISCHARGE %, PERCENT END DEVICE None x . - ted Detioe Name Mi PLPE MI MGM Women ! 26 Table 2-4. (Cont'd) —_ W__ 211% Phrase ___ SIMPLE PIPE INLET Yes pm 2114 key 91m ‘r----- PHEHHUESUREIfiBS No Ru2m1qupme JHUESURE PIPE PERCENTAGE No %. PERCENT PRESSURELOSS IMPEENTHALPYLEBS No jnnzmlkq,pmmg ENTHALPY PIPE PERCENTAGE No 96. PERCENT ENTHALPYLOSS ENDIMHHCE , 7 No Iwaexnrmd SIMPLE IUIsIIsICIIo ’ ’ ' per 2nd by pm Rn2m1qumnun 'waexr wd SHWHUECONDENSER EXU‘ 1&5 Raniqupmmw IUHDDEVKHE No INmmex- wd FEED‘NATERIDGT FEED\NATERIDGT ISNOTSATURATED FEEDVWKHHIDHJH' _ EXTRACTKHQDHET BOILER PRESSURE No Per 2nd key phrase D033 PRESSURE BOILER PERCENTAGE No 95. PERCENT PRESSURE Loss REHEATLEGL Yes pal-2nd k, pm.” INLET y REHEATLEG#_ Yut EXH' REHEATLEG#_ No PERCENTAGE PRESSURELOSS REHEAT LEG #_ No Per 2115! key phrase PRESSURE Loss PRESSURE . DEVIC__ 27 Table 2-4. (Cont'd) SIMPLE HEAT LOAD 12,, 2nd by pm I Per 2351 key phrase SIMPLE STEAM TRAP FEED WATER INLET Yes pu- 2nd key phrase CFW FEED WATER EXIT Yes pa 2nd key Pm ________fi DRAIN INLET IL Yes Per 2nd key phrase FEED WATER No per 2nd key phrase PRESSURE IDSS PRESSURE ,____fi FEED WATER No %. PERCENTAGE PERCENTAGE PRESSURE EXTRACTION No pawl p1...” PRESSURE LOSS mgm EXTRACTION No %. PERCENTAGE PERCENTAGE PRESSURE TERMINAL No band pm... TEMPERATURE TEMPERATURE DIFFERENCE APPROACH No pa 2nd key m TEMPERATURE DIFFERENCE TEMPERATURE END DEVICE No None e ted SEPARATORINLET ME by pm... I "' 'SEP'ARA"TO" R VAPOR Yes b, 2nd by pm... EXIT SEPARATOR Yes p 2nd pm... CONDENSATE EXIT '5 m SEPARATOR PRESSURE No b. 2nd by pm 1053 PRESSURE SEPARATOR No %. PERCENTAGE PERCENTAGE PRESSURE LOSS ENDDEVICE No Nonee _ 28 Table 2-4. (Cont'd) — CYCLE STEAM INLET Yes Per 2nd key phrase I REHEAT STEAM EXIT Yes Per 2nd key phrase REHEAT STEAM EXIT No None expected 18 NOT A SATURATED LI UID FLOW FRACTION No Per 2116 key phrase CONTROLLED BY JUNCTION DEVICE TEMPERATURE TEMPERATURE DIFFERENCE PRESSURE LOSS msm CYCLE STEAM No %. PERCENTAGE PERCENTAGE PRESSURE PRESSURE LOSS PRESSURE REHEAT STEAM No PERCENTAGE PRESSURE END DEVICE Zlilfi I' Q 'l' After RAN KINE 3.0 has Obtained the information from the input file, the information is Stored within a set Of arrays for future reference. The Storage Of information may be separated into three classes: 1) information related to the entire system, 2) information related to a device, and 3) information related to a node. lefl 'I' [In I'BIIIIIISI An example Of information related to the entire system would be an input file statements such as BYPASS INPUT CHECK FOR THIS ANALYSIS or THE DEAD STATE TEMPERATURE IS 25.5 DEG C. Both statements relate directly to the execution Of RANKINE 3.0 and not to a Specific device or node. The Storage Of this class Of information is accomplished with a set Of common block variables. Table 2-5 contains a summary of the variables used to Store this class Of information. 29 Table 2-5. System related variables block iteration 2150 'I' [IE I' Bllll S 1111' An example Of information related to a Specific device is an input file line such as THE FEED WATER INLET NODE NUMBER IS 7 or THE PUMP EFFICIENCY IS 78 PERCENT. Both statements relate directly to the structure or performance Of a Specific device with the system. Organization Of this class Of information is accomplished within two arrays; DVCDAT(100,30) and ADDDAT(100,30). When RANKINE 3.0 is executed, the elements Of the arrays DVCDAT(100,30) and ADDDAT(100,30) are set to values Of -1 and -1.0 respective (representing an unknown value). AS information is Obtained from the input file, the array is modified to reflect the synthesis Of the input file. The integer array DVCDAT(100,30) is an abbreviation for device data and is responsible for organizing node numbers on each device within the system. The first index Of DVCDAT; . : ’r; ‘ 13.3". .1...” .10. TI: firsr :2 simple It: numerical I 3O DVCDAT(100,30) represents a device number and the second index is used to organize information related to the Specified device number. The first element Of the second index (i.e., DVCDAT(#,1) ) indicates the device type (i.e., Simple turbine, simple pump, ect.). Table 2-6 summarizes the interpretation Of the numerical value contained within DVCDAT(#,1). Table 2-6. Interpretation Of the DVCDAT(#,1) element # Device For example, if DVCDAT(17,1) is equal tO six, then the 17111 device within the system is a Simple heat load. The second element Of the second index (i.e., DVCDAT(#,2)) indicates the last ICALL completed for the device. (The ICALL concept is discussed within Section 2.3.2) Since this element is used only for internal bookkeeping, the user does not directly affect the value Of this element. The organization Of the remaining 28 second index DVCDAT(100,30) elements depends on the device type (i.e., Simple turbine, Simple pump, ect.). Table 2-7 contains a summary Of the remaining 28 second index elements as defined for each thermodynamic model. ' 31 Table 2-7. Organization Of the DVCDAT(100,30) array W SIMPLE TURBINE DVCDAT(#,3) _ DVCDAT(#,I+3) Extraction #1 node number 7 for I'I,10 s- pump * =1) "“ n ’ * * * ” * WWW) ‘ * I DVCWW W W__ __ WW W . SIMPLE PIPE DVCDAT(#,3) DVCDAT #.4 DVCDAT(#.I+2) Inlet #1 nodenumber for 1:1,10 DVCDAT(#,I+12) Exit #1 node mnnber for I=l.10 SIMPLE DVCDAT(#,3) Exitnodenumber CONDENSER DVCDAT(#.I+3) Inlet #1 node number - . WW _ - _W WW _ ,W W___ - ___ WWW WWW SIMPLE HEAT DVCDAT(#,3) Inlet node number I LOAD DVCDAT #,4 Exit node number Dvcmfim) | Feedwater exitnodenumber DVCDAT(#,4) I ' _Extraction inlet node number DVCDAT # 5 Feed water inlet node number DVCDAT(QJ) Boiler inlet node number DVCDAT(JML _ Boiler exit node number DVCDAT(#,2’I+3) Reheat leg #1 inlet node number for I=l,10 DVCDAT(#,2*I+4) Reheat leg #1 exit node number for I=1.IO SIMPLE DVCDAT(#,3) Inletnodenumber MOISTURE DVCDAT #3) I Vapor exit node number SEPARATOR DVCDAT # exit ode number ‘ 32 Table 2-7. (Cont'd) . Definition SIMPLE DVCDAT(#,3) Cycle steam inlet node number REHEATER DVCDAT(#,4) Cycle steam exit node number DVCDAT(#,5) Reheat Steam inlet node number DVCDAT(#,6) Reheat steam exit node number DVCDAT(#,7) Junction device number which controls the flow fraction The DVCDAT( 100,30) array is located within the common block 10 and, hence, is accessible tO each of the four independent sections Of RANKINE 3.0. The real number array ADDDAT(100,30) is an abbreviation for additional data and is responsible for information related tO the performance characteristics Of a particular device. For example, a pipe pressure lOSS or pump efficiency would be Stored within ADDDAT(100,30). The first index Of ADDDAT( 100,30) represents the device number and the second index is for the Storage Of up tO 30 pieces Of information related to the Specified device number. The organization Of the 30 second index elements depends on the device type (i.e., Simple turbine, simple pump, ect.) and can be seen in Table 2-8. Table 2-8. Organization Of the ADDDAT(100,30) array __— SIMPLE Stage #1 isentropic efficiency 0.0->1.0 TURBINE _ __ _ __ _ ADDDAT(”) for I=l .10 SIMPLE PUMP ADDDAT #.1 0.0->1-0 I I 'sIMP _ _ hum—___ ___—___“ pressureloss I—flm “MPA _‘I ADDDAT(#.2) I lP'nie enthalpy loss I KJ/k ADDDAT(#,3) I We pressure loss I 0.0->1 .0 ADDDAT(#,4) I Pipe percents ; e enthal 9 loss 0.0->1.0 ADDDAT(“) Inlet #1 flow fraction for 1:] ,10 ADDDAT(#.I+10) Exit #1 flow fraction for I=l .10 W — _— CONDENSER f f 33 Table 2-8. (Cont'd) I Model I Variable I Definition I Units I SIMPLE HEAT I - I - I - I LOAD SIMPLE OFW I ADDDAT(#,1) \I A +1 slalom that the feed water exit state - I HEATER is not saturated lifluid. pessure ADDDAT(#.I+12) Reheat leg #1 percentage pressure loss SIMPLE MOISTURE ADDDAT(!IJ) Separator pressure loss MPA SEPARATOR ADDDATIIIJI Sfltor geentage Esme loss 0.0->1.0 I temperature temperature steam percentage pressure ADDDAT(#,7) A '+l' indicates that the reheat steam is not The ADDDAT(100,30) array is located within the common block 10 and, hence, is accessible to each of the four independent sections Of RANKINE 3.0. 2150 'I' [IE I'RIIII 5 Will An example Of information related to a Specific node is an input file line such as THE FEED WATER INLET TEMPERATURE IS 175.4 DEG C. The information within this Statements relates directly to a Specific position on a device (or, more precisely, to a node I on a dm'cc). m arrays number “it? mic 5pc. 34 on a device). The organization of node specific information is accomplished with a set of fifteen arrays each dimensioned with 100 elements. The index refers to a specific node number within the system. Table 2-9 contains a summary of the fifteen arrays, their variable type, and definition. Table 2-9. Storage of information related to nodes at node at node at at at node at node index at rate at node #I work device before node #1 transfer of device error before node #I balmoe error For example, if an input file line indicated that the mass flow rate at node number 7 is 14.3 kg/sec, then MNODEU) is internally set to 14.3. All fifteen arrays summarized in Table 2-9 are located within the common block 10 and, hence, are accessible to each of the four independent sections of RAN KINE 3.0. It should be noted that this organizational structure does inherently contain protocol. For example, if a input file stated THE FEED WATER INLET TEMPERATURE 18 175.4 DEG C before the input file stated THE FEED WATER INLET NODE NUMBER IS 7, the program will be unable to store the temperatm'e information since the node number has not yet been specified. As a result of this protocol, the input files must always describe the node structure of each device before the conditions at each node are specified. lit in cm in; submit: ECHO '. in file ceilct' EC} canon blocks 10 alt mismatch ECHODAI fit :‘a Stbroutinc ECHO Willing to the sys ECSW ,ECSSCI, ' ECSREH Each oi EGiODAI file 9 {watts [ht intrc whim i5 Its mint ’ch dc‘V'lt I ‘ .ICSO; W of the f 35 W After the entire input file has been scanned for information, the input file is closed and subroutine ECHO is called. The purpose of subroutine ECHO is to create an external data file called ECHO.DAT which lists most of the information contained within the common blocks 10 and DEAD. Since the common blocks 10 and DEAD contain the only information which exits the input processing subroutines, inspection of the ECHO.DAT file clarifies any questions associated with the interpretation of an input file. Subroutine ECHO is responsible for writing information to the ECHO.DAT file pertaining to the system and calling the model specific subroutines ECSTRB, ECSPMP, ECSPIP, ECSJC'I‘, ECSCND, ECSHLD, ECSCFW, ECSBOL, ECSCFW, ECSSEP, and ECSREH. Each of these eleven subroutines are responsible for writing information to the ECHO.DAT file pertaining to a specific device type. Utilizing this type of organization facilitates the introduction of new thermodynamic models in the existing code structure. 22!]! IE] III I' The primary purpose of the input file checking section is to verify that the information obtained from the input file is complete and consistent. Since RANKINE 3.0 requires the user to describe the system within the input file, the possibility of neglecting information or specifying a physically impossible systemmust be addressed. In order to address this concern, the program verifies that information obtained from the input file is complete and consistent. The input file checking can be separated into three classes; 1) required system information, 2) required device information, and 3) verification of consistent node connections. ZZIB'ISIIE l' The highest level subroutine within the input file checking section is RANKIC. This subroutine is responsible for verifying that all required system information is known and calling the device specific subroutines ICSTRB, ICSPMP, ICSPIP, ICSJC'I‘, ICSCND, ICSHLD, ICSOFW, ICSBOL, ICSCFW, ICSSEP and ICSREH. Table 2-10 contains a summary of the system information checked within subroutine RANKIC. J Vanni: Reauirms “HM If. NEW and mm m‘ i SDEAD)!‘ rid THEM 1H Billlitill .ifltr RNUNE mm Verifics SNPLE PIPE is 1 Wild idtntify the he WM dcvic IW, ICSPMI ICSSEP and H25} SM“ input the Table 2.1 F Lia 5M? 111m 36 Table 2-10. Required system information _— R . uirements - f f meet ,, 1 The state must fixed. Diagnostic #161 The number of nodes in the system Diagnostic #158 must be specified. L A high temperature reservoir must be specified. Diagnostic #159 Alow A turereservoir mustbe . .. ified. Di :4 ostic #160 After RANKINE 3.0 has verified that all required system information is known, the program verifies that all required device information is known. For example, if a SIMPLE PIPE is specified, but the inlet pipe node number is unspecified, the program would identify the error and flag the user with a diagnostic message. The verification of the required device information is accomplished within the device specific subroutines ICSTRB, ICSPMP, ICSPIP, ICSJCT, ICSCND, ICSHLD, ICSOFW, ICSBOL, ICSCFW. ICSSEP and ICSREH. Table 2-11 contains a summary of the information each model specific input checking subroutines checks. Table 2-11. Summary of device requirements checked by RANKINE 3.0 R . uirement meet DVCDAT(#,3)>0 A turbine must have inlet node number specified. DVCDAT(#,4)>0 A turbine must have exit node number specified. ADDDAT(#J)>0 A turbine adiabatic efficiency must be and between 0 and 1.0. ADDDAT(#.I)<1.0 or 1:1..10 DVCDAT(#.3)>0 A pump must have a suction . (inlet) node number specified. DVCDAT(#,4)>0 A pump must have a discharge I exit node number 'fied. ADDDAT(#.1)>=0.0 A pump adiabatic efficiency and must be between 0 and 1.0. ADDDAT # 1 1.0 37 Table 2-1 1. (Cont'd) Model Variable Explanation I If not J Requirement meet SIMPLE DVCDAT(#,3)>0 A pipe must have inlet node Diagnostic PIPE number specified. #1 1 1 DVCDAT(#,4)>0 A pipe must have exit node Diagnostic number specified. #112 ADDDAT(#,1)>=0 A pipe must have a specified Warning or ' treasure loss or specified #130 ADDDAT(#,3)>=0 percentage pressure loss. i ADDDAT(#.3)=<1.0 A pipe percentage pressure Diagnostic loss must be less than 100%. #115 ADDDAT(#.2)>=0 A pipe must have a specified Warning or enthalpy loss or a specified #131 ADDDAT(!L4)>=0 me enthalpy loss. ADDDAT(#,4)=<1.0 A pipe percentage enthalpy Diagnostic loss must be less than 100%. #116 SIMPLE DVCDAT(#.3)>0 A junction must have at least one inlet node Diagnostic JUNCTION number specified. #117 DVCDAT(#.13)>0 A junction must have at least one exit node Diagnostic number . . 'fied. #118 — DVCDAT(#,3)>0 A condenser must have an inlet node number specified. DVCDAT(#.4)>0 A condenser must have at least one exit < . - ified. - DVCDAT(#.3)>0 A heat load must have an inlet node number mecified. DVCDAT(#,4)>0 A heat load must have an exit node num . ' red. _ DVCDAT(#.3)>0 A open feed water heater must have a feed water exit node #123 number specified. DVCDAT(#,4)>0 A open feed water heater must Diagnostic have an extraction inlet node #124 number m'fied. DVCDAT(#.5)>0 A open feed water heater must Diagnostic have a feed water inlet node #125 number specified. mm DVCDAT(#.3)>0 A boiler must have an inlet Diagnostic BOILER node number specified. #126 DVCDAT(#,4)>0 A boiler must have an exit Diagnostic I node number flified. #127 If DVCDAT(#.I)>O Each boiler reheat leg must Diagnostic then have an exit node number #128 DVCDAT(#,I+1)>0 specified. for 125 SIMPLE MOISTURE , sepmmn Variable R - . uirement If DVCDAT(#.I+1)>0 then DVCDAT(#,I)>0 for I:5.23,2 38 Table 2-1 1. (Cont'd) Explanation Each boiler reheat leg must have an inlet node number specified. ADDDAT(#, 1 )>=0 or ADDDAT! #: 12)>=0 Aboilerpressuredropor percartage pressure drop must be specified. ADDDAT(#.I)>=0 or ADDDAT(#,I+1 1)>=0 for 1:45.242 Each boiler reheat leg must specify a pressure drop or a percartage pressure drop. DVCDAT(#,3)>0 A closed feed water heater must have a feed water inlet #132 node number specified. DVCDAT(#,4)>0 A closed feed water heater Diagmstic must have a feed water exit #133 __ node number specified. DVCDAT(#,5)>0 A closed feed water heater Diagnostic must have an extraction #134 inlet node number mecified. DVCDAT(#,16)>0 A closed feed water heater must have a Diagnostic drain exit node number specified. #135 ADDDAT(#.1)>=0 A closed feed water heater must have a Diagnostic or pressure drop or percentage pressure drop #162 ADDDAT§#£)>=0 specified. ADDDAT(#,3)>=0 A closed feed water heater must have an Diagnostic and extraction pressure drop or percentage #163 ADDDAT(#,4)>=0 pressure drop specified. ADDDAT(#,5)>=0 A closed feed water heater must have a Warning terminal temperature difference specified. ADDDAT(#,6)>=0 DVCDAT(#.3)>0 A reheater must have a cycle steam inlet node number specified. DVCDAT(#.3)>0 A moisture separator inlet Diagnostic node number must be specified. #146 DVCDAT(#.4)>0 A moisture separator vapor Diagnostic exit node number must be specified. #147 DVCDAT(#.5)>0 A moisture separator Diagnostic condensate node number must be specified. #148 ADDDAT(#.1)>-I0 A moisture separator tresstrre tie a drop or percentage pressure #149 ADDDAT#,2>~' m-nmstbe...'red. DVCDAT(#.4)>0 A reheater must have a cycle steam exit node number specified. DVCDAT(#.5)>0 A reheater must have a reheat steam inlet _-__n°W _, mam (Card; HI ‘ Sine: RU he possibi cWit, it #3131th - dm5c. Si: 5325315 Sc; 0! “3":ng a ‘5 €111 DOC 533m R; If: um if; 39 Table 2-11. (Cont'd) m“- R -.. uirement meet DVCDAT(#,6)>0 A reheater must have a reheat steam exit node number specified. DVCDAT(#.7)>0 A junction device number which controls the flow fraction through the reheater . must be gecified. ADDDAT(#.1)>=0 A reheater terminal temperatm'e difference must be specified. ADDDAT(#.3)>=0 A reheater cycle steam pressm'e drop or percentage or ADDDAT # 4 pressure drop must be specified. ADDDAT(#,5)>=0 Since RANKINE 3.0 requires the user to describe the system layout within the input file, the possibility of specifying a physically impossible system must be addressed. For example, if an input file stated that a node number is an exit node on one device, it is physically impossible to specify the same node number to be an exit node on a second device. Since all RANKINE 3.0 mass flow rates are positive scalars, the thermodynamic analysis section of RANKINE 3.0 is unaware of whether the mass flow rates are entering ' or exiting a device, and hence, the possibility of connecting an exit node on one device to an exit node on a second device is significant. In order to avoid a physically impossible system, RANKINE 3.0 systematically searches the system for inconsistencies and flags the user if an inconsistency is identified. Inconsistent node connections can be separated into three classes; 1) a node is not connected to any other device, 2) a node is connected to two or more device positions, 'and 3) a node is connected to another device position of the same type (inlet to inlet or exit to exit). RANKINE 3.0 systematically searches for each of these inconsistencies within the model specific subroutines ICSTRB, ICSPMP, ICSPIP, ICSJC’I’, ICSCND, ICSHLD, ICSOFW, ICSBOL, ICSCFW, ICSSEP, and ICSREH. Each of these device specific subroutines contain hardwired code logic that identifies inconsistencies related to one specific device type. The basic code logic for the systematic search for all three types of inconsistencies can be seen in Figure 2-4. I Ema I >I Device=0 1 I Continue I‘ I Exit 1% Device=Device+1 I , m , i IContinue I .nomorenodes iii I INLETnodeondevice 1 r Exitnodeondevice ’ >1 >1 Search forINLET Diagnostic and Search for axrr connections Stop program connections e i=0 . marmaxrr >2 Diagnostic and Search forINLET cormections Stop pro connections =1 :1 wins =0 Ii;mung message message Figure 2-4. Basic structure of node checking logic The search for inlet or exit nodes located on other devices is accomplished by the utility subroutine FNDNOD. Within the utility subroutine FNDNOD. sets of hardwired code logic systematically searches all inlet or exit node position on other devices for a specific node number. The output of subroutine FNDNOD is an integer which represents the number of times a specific node number was found as an inlet or exit on other devices.- By calling subroutine FNDNOD when required, each input checking subroutine can systematically search for inconsistencies within the system. It should be noted that an inconsistency does not always result in a diagnostic message (and, therefore, a program termination). In the event that a node is not connected to any other position within the system, the program only provides a warning message to the user. Since it is physically possible for a system to provide or receive fluid from an unmodeled location, RANKINE 3.0 will only notify the user of an unconnected node with the sysm. I tried in h: . ‘ | 1" x; mm ll: pm: of 1 Minnie inf when hem $155611 in Sadr Ill: proccssing 5 ll 5010:. calcul @3191 than: it“ Times is sui All: in “111310“ limit: pa: “list I” Older for PA? It 0f COdc log; latte. Second ‘3 ttitular un‘ Minna: Mm Subroutine RA M5313 SCCm Mil. Wh “PIP. AIS] AMER 3T! 0: u. Mimi SI"mollllncs C( inknown then: whim ij A] Subroufinc c 41 within the system. The existence of unconnected nodes within the system will, however, be reflected in the system mass and energy balance performed by the subroutine MEBAL in the output processing section. 23111] I .5]. The purpose of the thermodynamic analysis section is to calculate all unknown thermodynamic information within the system. The procedure employed to calculate the unknown thermodynamic information is very similar to the procedure for system analysis discussed in Section 1.1.0 Since all input file information has been organized within the input processing subroutines, RANKINE 3.0 systematically traverses the system, device by device, calculating all unknown thermodynamic information possible based on the physical characteristics of each device. For a well posed system, traversing the system a few times is sufficient to calculate all unknown thermodynamic device information. After all unknown thermodynamic device information has been calculated, the system performance parameters may be calculated utilizing the results of the device by device analysis. In order for RANKINE 3.0 to successfully employ the procedure for cycle analysis, three sets of code logic were developed. First, code logic to traverse the cycle, and if necessary, iterate. Second, code logic to determine when a sufficient amount of information exists to calculate unknown information, and finally, code logic to perform internal checks based upon the thermodynamic and physical constraints associated with each device. WW Subroutine RANKAI represents the highest level subroutine within the thermodynamic analysis section and is responsible for traversing the system, and when necessary, iterating. When RANKAI traverses the system, the subroutines AISTRB, AISPMP, AISPIP, AISJCT, AISCND, AISHLD, AISBOL, AISOFW, AISCFW, AISSEP and AISREH are called to determine when sufficient information exists to calculate unknown thermodynamic information. Each of these device specific AI (artificial intelligence) subroutines contain sets of hardwired logic that reflects the conditions for which unknown thermodynamic information may be calculated. In the event that sufficient information exists for the calculation of some unknown thermodynamic information, the AI subroutine calls the appropriate device specific thermodynamic subroutine to calculate the tumour in: Will i EnalU ‘_ 42 the unknown information. Figure 2-5 illustrates the basic code logic for the subroutine RANKAI. I mm |->| Sam?” I I 1.... I I Iter=Iter+l I I Islter>lter max? I i N° # I Itrav=0 I § _ pl Continue ; Devicew I * - l c... I< - i I Device=Device+1 I - e + | Itrav=ltrav+l IQ-L Device > NDVC 7 I i - w i I It Itrav> Itrav max ? I Call AI subroutine M W Analysis Isalldevice I Y“ I p | Isiwrationrequired? I . pl ExitRANKAI Id— Setallvariables to I Figure 2-5. Basic structure of subroutine RANKAI 43 In addition to traversing the system, subroutine RANKAI is responsible for iteration. As a result of the thermodynamic modeling methods used, only systems which possess a simple reheater device will require iteration. Before RANKAI traverses the system for the first time, the input file information is stored within a set of initial value arrays. For any system which contains a simple reheater device, subroutine RANKAI compares the calculated terminal temperature difference to the input file specified terminal temperature difference after each iteration. If this comparison exceeds 0.1 degree Centigrade, RANKINE 3.0 sets all variables to their initial values, modifies the appropriate junction flow split fraction, and perform the device by device thermodynamic analysis again. RANKINE 3.0 will stop iterating when the prescribe tolerance is achieved or the code iterates 100 times. W The subroutines AISTRB, AISPMP, AISPIP, AISJCT, AISCND, AISBOL, AISHLD, AISOFW, AISCFW, AISSEP, and AISREI-I are called from subroutine RANKAI and are responsible for determining when sufficient information exists to calculate unknown thermodynamic information. In order to simplify the code, each model specific AI subroutine maps the global node variables into local variables. The advantage of mapping global node variables into local variables can be best illustrated with an example. In order to specify the mass flow rate for a turbine inlet using global node variables, the appropriate expression is MNODE(DVCDAT(#,3)). Using a mapped local variable, the identical expression would beMTRIN. Clearly, the mapped local variable enhances clarity and reduces possible confusion. Within all Al subroutines, a set of local variable nomenclature was employed to simplify the code. Table 2-12 contains a summary of the local variable nomenclature. Table 2-12. Summary of local variable nomenclature 44 Table 2- 12. (Cont'd) Abbreviation Communication between the model specific AI subroutine and the corresponding device specific thermodynamic subroutines is based upon the numerical value of two integers; ICALL and IFIND. The variable ICALL is an integer flag used to specify which of the four fundamental calculations should be performed; I) calculate a thermodynamic states on a per-unit mass basis (ICALL=1), 2) calculate a mass flow rates (ICALL=2), 3) perform a 2nd law analysis (ICALL=3), and 4) verify model results (ICALL=4). The variable IFIND is an integer flag used to specify the exact calculation which should be performed. The definition of each IFIND is dependent on the type of device (i.e., simple turbine, simple pump, ect.). Table 2-13 contains a summary of the ICALL and IFIND options for each thermodynamic model. Table 2-13. Summary of ICALLs and IFINDs l) Inlet condition fixed or isfixable. 2) All extraction pressures known. 3) All stage group efficiencies known 2 1 1) Completed ICALL=1 1) Unknown mass flow rate 2)Allbutonemassflowrateis 2)Workandheattramfer m_tb_wn__ 1 Comleted ICALL=3 2 Verifies of model results ,. SIMPLE 45 Table 2-13. Summary of ICALLs and IFINDS m-nu WW SIMPLE 1 l 1) Suction (inlet) condition is fixed 1) Discharge (exit) state PUMP or is fixable . 2) Discharge (exit) pressure is known 3 Efficiency is known 1 . 2 1) Discharge (exit) condition is 1) Suction (inlet) state fixed or is fixable . 2) Suction (inlet) pressure known 3 Efficiency is known _ 2 1 l)Oneoftwomassflowratesare 1)Theoneunknown mass known flow rate 2 2 1) Completed ICALL-J 1) Work and Heat transfa 2) Both mass flow rates are known 3 1 1) Completed ICALL=2 1) Perform zlfl 1“, analysis 4 l 1) Completed ICALL=3 2) Verification of model results SIMPLE 1 1 1)Pipeinletpressureisknown. l)Fixpipeexitpressure PIPE 2) Pipe exit pressure is unknown. 3) Pipe pressure drop or pipe percentap pressure drop is known. _ 1 2 1) Pipe exit pressureisknown. 1)thpipeinlet}xessure 2) Pipe inlet pressure is unknown. . 3) Pipe pressure drop or pipe percentage pressure drop is known. j 1 3 1)Pipe inletenthalpyisknown. 1)Fixpipeexitenthalpy 2) Pipe exit enthalpy is unknoam. 3) Pipe enthalpy drop or pipe percentage enthalpy drop is known. 1 1 4 1)Pipeexiteruhalpyisknown. 1)Fixpipeinletenthalpy 2) Pipe inlet enthalpy is unknown. 3) Pipe enthalpy chop or pipe percartage enthalpy drop rs - tnown. ._ 1 5 1)Eitherinletorexitstateis 1)Trytofixeither unfixed. mlfixed state. 2 l 1)Onemassflowrateisknown. 1)Theoneunknown 2)Onemassflowrateisunknown. nlassflowrate 2 2 1) Completed ICALL=1 1) Work and heat transfer 2) Both mus flow rates are known 4 l 1) Completed ICAIL=3 1) Verification of model results D Q . WEBER // 5m; . WILLS” / 46 Table 2-13. (cont'd) um WNW _ SIMPLE JUNCTION 1) At least one inlet or exit state known 2) Atleastoneinletorexitstate unknown 1)Allunknown states 2 1)Allbutonemassflowrate 1)Tlteoneunknownmss gn_known flow rate 2 1)Allbutoneinletflowfraetionis 1)Theoneunknowninlet known fiflpw fraction 2 1) All but one exit flow fraction is l) The one unknown exit flow known fraction 2 1)Atleastoneinletmassflowrate 1)A11inletmass flowrates known 2) All inlet flow fractions are known 2 1)Atleastoneexitmassflowrate 1)Allexitmassflowrates known 2)Allexitflowfraetionsareknown g 2 1)Allinletmassflowratesare 1)Allexitmassflowrates known 2)All exit flow fractions are known 2 1)Allexitmassflowratesare 1)Allinletmassflowrates - brown 2) All inlet flow fractions are known _ 2 1) Completed lCALIzl 1) Work and heat transfer 2) All mass flow rates known 3 1) Completed [CAI-152 1) Perform 21‘ law analysis 4 1) Completed ICALL=3 1) Verification of model results 1)At1eastonecondenserpessure 1)Allunknownpressures known 2) Atleastonecondenserwessure unlmown 1 1)Atleastonecondenserstateis 1)Trytofixallunknown unfixed s_tates 2 l)0nlyonecondensermassflow 1)Theoneunknownmass rate is unknown flow rate 2 1)Allcondenserstatesareknown 1)Workandheat 2) All condenser mass flow rates tramfer arelmown 3 1) Completed ICALIFZ 1) Perform 2“1 law analysis 4 1) Completed ICALL=3 1) Verification of model fixed or are fixable results nix state 1)Onemassflowrateisknown 2) One mass flow rate is unknown l)'I'heoneunknown massflowrate - l) Inlet and exit state fixed 2 Both mass flow rates are known 1) Work and heat transfer El a r- L SEN. )H,’ «1' i L I $3M OFW m; 3N {VG-"LE 47 , Table 2-13. (cont'd) —-Irfl WW 1) Completed ICALL=2 1) Perform H 1“, analysis 1) Completed ICALL=3 1) Verification of model SIMPLE 1 1 1) At least one pessure is known 1) All urnknown presstu'es OFW 2)_At least one pressure is unktown __ HEATER 1 2 1)Feedwater inletandextraction 1)Feedwater inlet and/or inlet states are fixed or are extraction inlet state fixable _ 1 3 1)Feedwater exit ternperamreor 1)'1'heunlmown feed water pressure is known exit sanitation 2)Feedwaterexitstateistunknown temperamreorpressure 3) lieed water exit state is saturated l 4 1) Feed water exit state is fixable. 1)1‘he feed water exit state 2 1 1)AllOFW enthalpiesareknown 1)Thetwomknwnmass 2) One mass flow rate is known flow rates 3) Two mass flow rates re whom _ 2 2 1)Two mass flow rates are known 1)Theonetmknownmass 2) One mass flow rate is nmknown ._flow rate 2 3 1) Two enthalpies are known. One 1) The one unknown enthalpy enthalpy is unknown. 2) All mass flow rates are known. j 2 4 1)Allstatesarefixed 1)Workandlneattransfer 2)Allmass flowratesareknown 4 l 1) Completed ICALI;3 1) Verification of model results SIMPLE 1 1 1)Anyunknown inletorexit 1) Tryto findallunknown BOILER pressure on boiler pressures l 2 1) Anyunfixed statesonboiler 1) IrLto fix allunfixedstates 2 1 1)Anyunknownmassflowrates 1)Trytofindallunknown on boiler mass flow rates 2 2 1)Allstatesfixedonboi1er 1)Workandlneattransfer 2) Allmass flowrates areknown on boiler 4 l 1) Completed ICALL=3 1) Verification of model results 1)Onefeed waterpressureis lfiheoneunktownfeed known arnd one is unknown water pressure 2)Pressuredropor percentage essure .. . . isktown Mall 1( 5 m M CW Emil) L I new . 48 Table 2- 13. (cont'd) Required information flow rate are known 2) Pressure loss or percentage pressure loss is known SIMPLE ' 1 3 1) One shell side pressure is known 1) All urnknown shell STEAM and one is unknown side pessures TRAP 2) Extraction pressure loss or CFW extraction percentage pressure (Cont'd) lass _ 1 4 1) Terminal temperature 1) Either excaction inlet difference is known pressure or feed water exit 2) Either extraction inlet pressure temperature or feed water exit temperature is known _ 1 5 1) Approach temperature 1) Either feed water inlet difference is known temperature or drairn exit 2) Either feed water inlet temperature temperature or drain exit _ temEIamre is known _ 2 1 r1)OneFeedwatermassflowrate 1)Theoneunknownfeed is known water mass flow rate ‘2)One Feed watermass flowrate is unknown J 2 2 1)Oneunknown shell sidemass 1)Tlneoneunknown shell flow rate side mass flow rate 2 3 1)Allfeedwaterandslnellside 1)Tlneoneunknownshell enthalpies . - side inlet mass flow rate 2) Both feed water mass flow rates 3) All but one inlet slnell side irnlet mass flow rates 4) Exit shell side mass flow rate is unknown ' _ 2 4 1)Allstates fixed 1)Workarndlneattransfer 2) All mass flow rates known 3 l 1) Completed ICALL=2 1) Mom 2nd kw mm 4 1 1) Completed ICALL=3 1) Verification of model results 1) Separator irnlet state is urnknown QTry to fix irnlet state 1) Separator inlet state andmus 1) Separatorvapor exitarnd corndensate exit states arnd mass flow rates 1) Completed ICAfi.=1 1)?mG arnd lneat u-snsfer 1) Completed ICALL-=2 1)Perform2m1aw analysis 1) Completed 167mg 1) Verification of model results 49 Table 2-13. (cont'd) m-riau WW" SIMPLE 1 l 1) ény reheater states urnfixed 1 T to fix all states REHEATER 1 2 1) Either cycle steam inlet or cycle 1) The urnknown cycle steam steam exit wessure is known pressure 2) Either cycle steam inlet or cycle steam exit treasure is unknown 3) Cycle stearrn pressure drop or cycle steam percentage pressure dig is known fl 1 3 1) Eitherreheat steam irnletor 1)Thenmknownrelneatsteam relneat steam exit pressure is pressure known 2) Either reheat steam inlet or reheat steun exit pressure is unknown 3) Either the reheat steam pressure drop or reheat steam percentage pressure drop is known 1 4 1) All entlnalpies except cycle 1) Cycle steam exit erntlnalpy steam exit are known 2) All mass flow rates known 3) Cycle steam exit mass flow rate is positive 1 5 1)All erntlnalpies exceptreheat 1)Reheatsteamexitenthalpy steam exit are known 2) All mass flow rates known 3) Reheat steam exit mass flow rate is positive 3 2 1 1) Either cycle steam irnlet or cycle 1) The one unknown cycle steam exitmassflowrate steammassflowrate is known 2) Eitlner cycle steam irnlet or cycle steam exit mass flow rate is unknown j 2 2 1)Eitlnerrelneatstesrninletorexit 1)Tlneoneunknownreheat mass flow rate is known steam mass flow rate 2) Eitlner reheat steam irnlet or exit mus flow rate is nnrnknown J 2 3 1)Allstates fixed 1) Workandheattransfer 2) All mass flow ratesare known 2) Actual terminal tempaature difference. 3 1 1) Completed ICALL=2 1) Perfornn 2m 1“, mi, 4 1 1) Completed ICALL-=3 1) Verification of model results 233 l! '[i l' [M IIR II In order to insure that all RANKINE 3.0 results are tlnermodynamically and physically possible, each model specific thermodynamic subroutine compares its results against a set of thermodynamic and physical constraints. For example, if an analysis of a turbine resulted in a large negative irreversibility, a warning message would flag the user of a merino , . ms to mgr plyrica SNJL TL 1‘ 7/ 511131;. PLMP 50 thermodynamically impossible result. Each model specific tlnermodynamic subroutine contains a set of hardwired codelOgic which compares the results of its analysis to the thermodynamic and physical constraints associated with the specific device type. Since this comparison is performed in ICALL=4, it is performed after all calculations are complete. Table 2- 14 contains a summary of the model specific thermodynamic and physical constraints verified by the program. Table 2-14. Model specific constraints checked by RANKINE 3.0. “__- R-cuirement SIMPLE MTRIN >= 0.0 A turbine inlet must have a positive Diagnostic TURBINE mass flow rate. #202 ' MTRST(I) >= 0.0 ‘ All turbirne stages group mnnst Diagrnostic for I=1.NTRST have a positive mass flow rates. #204 mm >= PTREXO) A turbirne must have monotonically Diagnostic decreasing extraction pressures. #207 HTRIN >= HTREXO) A turbirne must have monotonically Diagrnostic ‘ decreasing extraction enthalpies. #205 mama) >=- PI'REXG) A turbine must have monotonically Diagrnostic for I=2.NTRST decreasingextraction enthalpies. #208 HTREXO-l) >= A turbirne must have monotonically Diagrnostic HTREXG) decreasing extraction enthalpies. #206 for I=2,NTRST IRTREXO) >= -0.01 A turbine stage group must have a Warning for I=1.NTRST positive irreversibility. #200 STREX(1)-STRIN A turbine must have equal or irncreasing Warning >= -0.01 ' extraction entropy. #201 ST'REXG)-STREX(I+1) . A turbine must have equal or increasing Warnirng >= -0.01 ‘ extraction erntropy. #202 for I: ' ST MPMPO >= 0.0 ,A pump exit must have a positive PUMP ‘ mass flow rate. MPMPI » 0.0 A pump inlet must have a positive mass flow rate. HPMPO>=HPMPI Apumpmustmaintainor irncreasetlne enthalpy of the fluid. PPMPO >= PPMPI A pump must mairntairn or increase the pressure of the fluid. SPMPO-SPMPI >= A pump must irncrease the entropy -0.01 of the fluid. IRPMPO >= -0.01 A pnnrnp must have a positive . irreversibili . H. Manon 5 1 Table 2-14. (cont'd) R . ,' uirement . I MPIPO >= 0.0 A pipe exit must have a positive mass flow rate. MPIPI >= 0.0 A pipe irnlet must have a positive mass flow rate. ABS(PPIPI—PPIPO-PLPIP) A pipe pressure drop must be =< 0.01 - correctly applied. for PLPIP >= 0.0 A ABS((1-PPLPIP)"' A pipe percentage pressure drop must PPIPI-PPIPO) be correctly applied. x 0.01 for PPLPIP >= 0.0 ABS(l-lPIPI-l-IPIPOo A pipe enthalpy drop must QLPIP) =< 0.01 be correctly applied- ‘ for QLPIP >= 0.0 ABS((1 -PQLPIP)"' A pipe percerntage ernthalpy chop must HPIPI-HPIPO) be correctly applied. =< 0.01 for PQLPIP >= 19.0 ABS(SPIPI-SPIPO) A pipe with zero heat =< 0.01 trarnsfer and zero measure for (QLPIP=0.0 or loss must not have an PQLPIP=0.0) entropy irncrease. arnd (PLPIP=0.0 or PPLPIP=0.0) IRPIPO >= -0.01 A pipe irreversibility must be positive. SIMPLE MJCI'IG) >= 0.0 All jurnction inlets must have Diagnostic JUNCTION ‘ for I=1.NJCI'I a positive mass flow rate. #221 MJCI‘OG) >= 0.0 _ All junction exits must have Diagnostic for IfllCTO a positive mass flow rate. #222 All inlet state must be identical to all Diagnostic other irnlet states. #223 All exit state must be identical to all Diagnostic : otlner exit states. . #224 All irnlet state must be identical to all Diagnostic other exit states. #225 MCDO >= 0.0 A condernser exit must have a positive mass CONDENSER . . ' - flow rate. MCDI(I) >= 0.0 All condenser irnlets must have for I=1, NCDIN a positive mass flow rate. ABS(PCDI(I)-PCDO) All corndenser irnlets must have the same Diagrnostic =< 0.01 pressure as the condernser exit. #230 ‘ for I=lflCDIN XCDO =< 0.0 A condenser must reject lneat. ' ' #207 IRCDO >= -0.01 A condernser irreversibility ' must be - . sitive. _ HEATER 52 Table 2- 14. (cont'd) m “M" R . uirement SIMPLE OFW HEATER SIMPLE BOILER _ Aheat load exrt mass flow A rate must be jositive. A heat load inlet mass flow rate must be positive. A heat load irreversibility must be - ... itive. MOFWF >= 0.0 The feed water inlet. extraction inlet. arnd Diagmstic MOFWI >= 0.0 feed water exit mass flow rates #236. #241 or MOFWO >= 0.0 t must be positive. #241 HOFWF >= 0.0 The feed water irnlet. extraction inlet. arnd Diagmstic HOFWI >= 0.0 feed water exit enthalpies #235 HOFWO x 0.0 must be positive. ABS(POFWF-POFWI) An OFW heater is a constant treasure device. Diagnostic =< 0.01 #244 ABS(POFWP-POFWO) An OFW heata is a constant tressure device. Diagnostic =< 0.01 _ #244 IROFWO >= -0.01 An OFW heater irreversibility Warnirng . mustbe .. itive. #210 MBRI >= 0.0 A boiler irnlet must have a positive Diagrnostic mass flow rate. #245 MBRO >= 0.0 A boiler exit must have a Diagrnostic positive mass flow rate. #246 ABS(PBRO+PLBOL- .A boiler pressure drop must Diagnostic PBRI) =< 0.01 be correctly applied. #247 for PLBOL >= 0.0 ABS(PBRO- -A boiler percentage pressure Diagrnosn'c (1-PPLBOL)‘PBRI) drop must be correctly applied. #251 =< 0.01 for PPLBOL >= 0.0 MRlIla) >= 0.0 A boiler reheat leg irnlet must have Diagrnostic for I=1 RRH a Esitive mass flow rate. #248 MRHOG) >= 0.0 A boiler reheat leg exit must ‘ Diagnostic for (=1.NBRRl-l have a positive mass flow rate. #249 ABS(PRl-II(I)- A boila' relneat leg pressnnre Diagnostic PLRHa)-PRl-l0(1)) drop must be correctly applied. #250 =< 0.01 for I=1.NBRRl-l for PLRH >= 0.0 ABS(PRHO-PRHI(I)‘ A boiler relneat leg pacentage measure drop Diagnostic (1-PPLRH(I)) must be correctly applied. #252 =< 0.01 for l=1.NBRRH for PPLRl-lfl) >a0.0 IRBRO >= -0.01 A boiler irreversibility must Warning be positive _L #211 IRRHOO) >= -0.01 A boiler reheat leg irreversibility must Warning forlsl 'RRH be . ositive. #212 Ii] = SW1}, CW Z R ' . uirement SIMPLE CFW HEATER SIMPLE SEPARATOR 53 Table 2-14. (cont'd) H A CFWhetné‘xtr‘awon irnltass ow I MEXTI >= 0.0 Diagrnostnc ‘ rate must be positive. #253 MDRO >= 0.0 A CFW heate drairn exit mass flow rate Diagnostic must be positive. #254 MFWI >= 0.0 A CFW lneater feed water irnlet mass flow Diagnostic ‘ rate must be positive. #255 MFWO >= 0.0 A CFW heater feed wate exit mass flow Diagrnostic _ rate must be positive. #256 MDRIG) >= 0.0 All CFW heate drairn irnlet mass flow rates Diagrnostic FOR I=1.NDRI must be positive. #257 ABS(PFWI-PLFW- A CFW heate feed wate pressure drop Diagrnostic PFWO) =< 0.01 must be correctly applied. #258 for PLFW >= 0.0 . _ ABS(PFWI* A CFW heate feed wate pecentage pressure Diagrnostic (1-PPLFW)-PFWO) drop must be correctly applied. #259 =< 0.01 ~ for PPLFW >= 0.0 ABS(PEXTI-PLEXT- A CFW heate extraction pressure drop Diagnostic PDRO) =< 0.01 must be correctly applied. #261 for PLEXT >= 0.0 _ ‘ ABS(PEXTI* A CFW heate extraction pecentage Diagrnostic (1-PPLEXT)-PDRO) pressure drop must be correctly applied. #169 =< 0.01 . . . for PPLEXT » 0.0 ABS(PDRI(I)-PEXTI) All CFW heate extraction irnlets must Warnirng x 0.01 have identical pressures. #213 for I=1.NDRI for PPLEXT >= 0.0 _ IRFWO >= -0.01 A CFW heater tube side irrevesibility Warrnirng must be positive. #214 IRDRO >= «0.01 A CFW lneater shell side irrevesibility Warning must be - ... itive. #215 TSEPO >= A separator vapor exit tenperature mnnst be Diagrnostic TSAT(@PSEPO) equal to or greater than the saunration #262 _ temperature. TSDRO =< A separator condensate exit temperature must Diagrnostic TSAT(@PSDRO) be equal to or less tlnarn the sanitation #263 . temperature. MSEPI >= 0.0 All separator mass flow rates Diagrnostic MSEPO >= 0.0 must be positive. #264 MSDRO >= 0.0 ABS(PSEPI-PSEPO- A separator measure loss Diagrlnstic PLSEP) =< 0.01 must be correctly applied. #265 for PLSEP >= 0.0 ABS(PSEPI" A separator percentage Diagrnostic (1 -PPLSEP)-PSEPO) pressure loss must be #265 =< 0.01 correctly applied. for PPLSEP >= 0.0 IRSEPO >= -0.01 A separator irrevesibility Warnirng mustbe . v. itive. #221 Model SIMPLE REHEATER 54 Table 2-14. (cont'd) HI SI I' EDESI! III C |' ISI. Ill Subroutine FIXSTA is called tlnroughout the thermodynamic analysis section and is responsible for interfacing between RANKINE 3.0 and the computerized steam tables. Subroutine FIXSTA may performs one of three functions; 1) determines if a state can be fixed (IFIND=1), 2) fixes a state by calling the appropriate steam table subroutine (IFIND=2), or 3) calculates a saturation temperature or pressure given a pressure or temperature (IFIND=3). Even though the state postulate requires two independent intensive thermodynamic properties to fix a state, the information required by RANKINE 3.0 to fix a thermodynamic. state is based upon the requirements (or limitations) of the computerized steam tables. Table 215 contains a summary of the thermodynamic conditions for which a state is fixed and all unknown thermodynamic information may be calculated. . Variable Explanation R a . uirement MCYLI >= 0.0 A reheater mass flow rates Diagnostic MCYLO >= 0.0 must be positive. #266 MRHSI >= 0.0 MRI-ISO >= 0.0 ABS(PCYLl-PCYLO- A cycle stearrn pressure drop Diagnostic PLCYL) =< 0.01 mm be correctly applied. #267 for PLCYL >= 0.0 ABS((1-PPLCYL)‘ A cycle stearrn pecentage Diagnostic PCYLI-PCYID) tressure drop must be #267 . =< 0.01 correctly applied. for PPICYL >= 0.0 ABS(PRHSI-PRHSO- A reheat steam pressure drop Diagnostic PLRHS) =< 0.01 must be correctly applied. #268 for PLRHS >= 0.0 ABS((1-PPLRHS)“ A relneat steam pecentage pressnn'e drop Diagnostic PRHSI-PCYLO) mnnst be correctly applied. #268 =< 0.01 ‘ for PPLRHS >= 0.0 IRCYbO >= -0.01 A cycle steam irrevesibility Warning must be positive. #222 IRRHSO >= -0.01 A reheat steam irreversibility Warnirng must be sitive. #223 55 Table 2-15. Requirements to fix a thermodynamic state Known ‘ Calculates - Tempeature , Specific volume Pressure Enthalpy Subcooled liquid or Entropy SpErheated vapor . Tempeature Satrrration pressure Quality Specific volurnne M phase nnixture Enthalpy Bumpy Pressure ‘ Saturation temperature Quality Specific volume Two phase rrnixtnnre Enthalpy Pressure . Tempeature Entropy Specific vohnme Enthalpy Quality Fluid phase irndex Pressure Ternpeatnnre Enflmlpy . Specific volume We Quality Fluid . ase irndex The methods employed by the computerized steam tables to calculate the unknown thermodynamic information are based upon fundamental relation for the working fluid. The fundamental relation is represented by the steam tables. Since the computerized steam tables were not written by the author, the internal details of the computerized steam tables are beyond the scope of this discussion. It should be noted that the numerical methods used to calculate the steam table properties introduce considerable error whenever the pressure is greater than the critical pressure. Therefdre, the maximum allowable pressure is 22.09 MPa and the maximum allowable temperatm'e is 1300 Deg C. In addition, the computerized steam tables incorporated by RANKINE 3.0 possess a very slight discontinuity between the 2-phase correlation and the compressed liquid and superheated steam correlation. As a result of this discontinuity, RANKINE 3.0 may calculate a working fluid entropy decrease across a device or a negative irreversibility for a device. Since both conditions are physically impossible, RANKINE 3.0 checks each device in the system to insure that neither condition exists and, if necessary, provides a warning message to the user during program execution. Usually, the discontinuity problem may be avoided by n0t modeling very small device pressure losses when the working fluid is close to the saturated liquid or saturated vapor line. ,3. CD” a. llci‘ Wm lathe ...e H. \r m w... i he mun W... .fl We. a we. mu m. .0. l .. . mm. m I .- > a . n . «I» In uh TIM .. 0 ..\. «4K 4...»: ”be nt V 1 nm a . E W he he he .a .4 ts... NV- D D 56 The internal units utilized within RANKINE 3.0 are set by the operating units of the computerized steam tables. Table 2-16 summarizes the steam table units. Table 2-16. Steam tablepunits After all unknown thermodynamic device information is known, subroutine SYSCAL is called. Subroutine SYSCAL is responsible for calculating and/or organizing all important system parameters. The important system parameters can be separated into two classes; 1) information related to device total parameter, and 2) information related to system performance parameter. An example of information related to a device total parameter is total turbine work or . total pump work. Within the subroutine SYSCAL, the system is systematically traversed and information pertaining to the total device parameters are organized and stored within a set of common block variables. Table 2-17 contains a summary of these variables and their definition. Table 2-17. Summary of device total variables __mmn-W Daemon f AJQBOi. Total Adjusted heat ‘ NNODEO Number er unconnected . trarnsfer by all boiles . 1 ~ exit nodes in system DVCBOLG) Device nnnrnber of NODEI(I) Node nnnrnber of #I gsimple boile #I uncornrnected irnlet node DVCI'RBG) Device number of NODEO(I) Node nnrrnber of #I grunge turbine #I urncornrncctcd exit node DVCCNIXI) Device number of ‘ QBOLG) Heat trarnsferred irnto s' lecondenser#I s stenb boile#I DVCI-ILIXI) Device number of QCND(I) ‘ Heat transfered irnto simple heat load #I ' ' system by condense #I DVCPMPG) ‘ Device number of QHLD(I) Heat trarnsferred into s' le m. #I systemmheatloadfl NNODEI Nurnbe of nnrncorunected WKPMPG) Actual work of irnlet nodes inn 8 .tem - w- “I 57 Table 2- 17. (Cont'd) Total punnp Total heat trarnsfer actual work an systen » into all simple heat loads Total actnnal work . Tia] heat transfer DEFINITION DEFINITION into all sirn ole . ' - . Total lneat trasfer intmsten Total heat trarnsfer irnto all boiler Each of the variable specified in Table 2-17 are located within the common block IO, and hence, are accessible to the other sections of RANKINE 3.0. The second class of information subroutine SYSCAL calculates are system performance parameters. By applying the thermodynamic definitions for the system performance parameters, subroutine SYSCAL calculates five System parameters; the lit and 2114 law efficiency, heat rate, CARNOT cycle efficiency, and 2111 law effectiveness. After SYSCAL calculates these system parameters, they are stored within a set of common block variables. Table 2-18 contains a summary of the five variables used to store the five system parameters and their definitions. Table 2-18. Summary of system performance variables Variable Definition Units FLEFF 1it law efiiciency N0” in“: 2‘“1 law efficiency None HRSYS gear rate BTU/KW/HR CCEFF' CARNOT cycle efficiency None SLEWE ' Second law effectiveness None Each of the variable specified in Table 2-18 are located within the common block 10, and hence, are accessible to the other independent sections of RANKINE 3.0. W The purpose of the output processing section is to perform a mass and energy balance on each of the various control volumes throughout the system and to write all results to a user specified file. Subroutine RANKO is the highest level subroutine in the output 58 processing section and is respOnsible for calling subroutine MEBAL, prompting the user for an output file name, and writing the results to the user specified output file. What: Subroutine MEBAL is responsible for performing a mass and energy balance on each of the various control volumes throughout the system. Subroutine MEBAL performs a mass and energy balance with control volumes selected around each device within the system and around the entire system. Performing a mass and energy balance around each device independently verifies the conservation of mass and energy and increases the overall credibility of the program results. Performing a mass and energy balance with a control volume around the entire system determines if unaccounted mass and/or energy is entering or exiting the system. Within the subroutine MEBAL, the system is traversed and the mass and energy flows entering and exiting each control volume is accounted. The results of the mass and energy balances are stored within five common block variables. Table 2-19 contains a summary of these five variables, their definition, and Table 2-19. System mass and energy balance variables Variable definition Units MBERRG) Unaccounted mass flow . kg/sec rate entering the ~ device before r_node #I _ EBERRG) Unaccounted enegy flow KW rate enteing the device before node #I MSERRI Unaccounted mass flow kysec rate enteing the ‘ systen MSERRO Unaccounted mass flow ' kg/sec rate exiting the system ESERRI Unaccounted enegy flow KW - rate enteirng the - system. ESERRO Unaccounted enegy flow KW rate exiting the 8 stern r Each of the variable specified in Table 2-19 are located within the common block 10, and hence, are accessible to the other independent sections of RANKINE 3.0. I r//7/7/ . 59 . ‘It should be noted that the mass and energy balance performed on the various control volumes throughout the system are true balances.‘ For example, when performing an energy balance on a condenser, the Work term in the energy balance is not neglected (i.e., set to zero) even though it is known that a condenser does not do work on the surrounds. By performing a true mass and energy balance, additional model credibility is acquired. W1: Subroutine RANKO is responsible for prompting the user for an output file name and writing all reSults to the user specified output file. The output file name is read as a A12 format and, hence, the output file name is limited to a maximum of 12 characters (including the extension). In addition, an internal check within subroutine RANKO verifies that the output file name is _not identical to the input file name. After the output file name has been specified, the results of the thermodynamic analysis are written the output file. The output file include three types of data; 1) Node data, 2) Device data, and 3) System data. Tables 2-20 and 2-21 contain the definitions of the abbreviations used witlnin the output file. A ' Table 2-20: Node data abbreviations TH _ W _H “De I I ,_ __ I I" ‘— T ' Tempeature De : C P ‘ 1 Pressure ‘ . MPA L Fluid phase index - 1-subcoolcd liquid 24wophase mixture 3-superheatcd vapor 4-saturated liquid 5-saturated vapor Quality r- Entropy K] ; Enthalpy V K]. . 1 . m3 K] Specific volume Mass flow rate vailabnli >Z<=m6 60 Table 2-21: Device data abbreviations REV WRK The revesible work associated with KW the device before the node. ACT WRK _ The actual work associated with KW . the device before the node. IRREV ' The irreversibility associated with KW tile device before tlne node. HEAT X-FER The heat transferred irnto ' KW _ the device before the node. MASS ERR The mass balarnce error associated Kg/sec _with the device before the node. ENG ERR The energy balance eror associated KW . with the device before the node The basic structure of RANKINE 3.0 has been designed to facilitates additional thermodynamic models within the existing framework. In order to add additional thermodynamic model, five subroutines must be written and seven existing subroutines must be modified. Table 2-22 contains a summary of the subroutines which must be written or modified to insert an additional thermodynamic model within the exiting framework. Table 2-22. Subroutines required for new Thermodynamic model Write subroutine subroutine subroutine subroutirne In order to maintain the structure of the program, it is recommended that the five new subroutines required for an additional thermodynamic model be written utilizing the same fundamental structure as the existing code. The creation of the input processing subroutine, echo subroutine and input checking subroutine can be almost entirely written 61 with a cut and paste approach with slight modifications. The creation of the artificial intelligence and thermodynamic subroutine requires the most original programming, however, they should still follow the fundamental frame work of the thermodynamic analysis section. Due to the large size of the RANKINE 3.0 executable file (approximately 390K), it is possible to add additional thermodynamic models and exceed the maximum program executable size. In the event that this upper bound is approached, it is recommended that RANKINE 3.0 be divided into three individual executable files. As a result of the program structure, RANKINE 3.0 may be divided into an input processing executable, an input checking executable, and a thermodynamic analysis/output processing executable file. Since the only communication between each of these sections is through the common blocks 10 and DEAD, the communication between each of the tlnrec executables could be achieved by writing the common blocks to an external data file. A DOS batch file could then be written to run all three executable files and to deleted the external data file after RANKINE 3.0 is run. ' 210 2 I. cl Io Even though RANKINE 3.0 was developed to be as flexible as possible, the program does contain some limitations A summary of these limitations can be seen below. 1) The system must have less than 100 devices. 2) The system must have less than 100 nodes. 3) A SIMPLE TURBINE device may have a maximum of 10 extractions. 4) . A SIMPLE CONDENSER device may have a maximum of 27 irnlets. 5) A SIMPLE BOILER device may have a maximum of 10 reheat legs. 6) A SIMPLE JUNCTION device may have a maximum of 10 inlets and a maximum of 10 exits. 7) Transients can not be modeled by RANKINE 3.0. 8) Working'fluid other than steam can not be modeled by RANKINE 3.0 (such as non condensable gasses). 9) RANKINE 3.0 does not provide insight into the physics within the ‘ thermodynamic control volumes. . . . 62 10) The performance characteristics (such as pipe pressure loss or adiabatic stage group efficiency) of each device must be known before the system performance is analyzed. 11) Due to steam table limitations, the maximum allowable pressure is 22.09 MPa and the maximum allowable temperature is 1300 Deg C. RANKINE 3.0 can model eleven different thermal devices commonly found in steam power systems. Each of these thermal devices are modeled by RANKINE 3.0 as steady state steady flow thermodynamic control volumes capable of performing as specified within the input file. The performance of each thermal device is calculated with hard wired code logic, which applies the 151 and 2M1 law of thermodynamics for a control volume (neglecting kinetic and potential energy terms) and the appropriate performance parameters to calculate the performance of each device. In general, the control volume for the thermodynamic analysis is selected around the physical boundaries of each device, and hence, the only information acquired from the analysis is the state of the working fluid as it crosses the boundary of the control Volume and the net work and/or heat transferred across the boundary of the control volume. For each device, RANKINE 3.0 was developed to identify several different combinations of known information which represent a well posed device. As a result, RANKINE 3.0 is capable of solving for one set of unknown variables related to a specific device given a second set of known variables related to that same device. The conditions in which RANKINE 3.0 can identify a well posed device and perform calculations are based on the standard methods to model each device type. Table 2—1 3 summarizes the conditions in which RANKINE 3.0 may calculation an unknown piece of information. The device performance parameters utilized in the thermodynamic analysis depends on the device type. The device performance parameter captures the physics of the device and may or may not be provided by the user for the analysis. For example, the physics of a 'pipe device' may be captured with a user specified pressure loss and a user specified enthalpy loss. These two parameters quantify the pressure loss encountered when a viscous fluid (in our case, steam) moves within a pipe and the heat loss (which appears in the form of a steam enthalpy decrease) when a 'hot' pipe interacts thermally with its environment. Each of the eleven thermodynamic devices which can be modeled by RANKINE 3.0 is discussed in the following sections. For each device type, the device purpose, common 63 64 symbol, device performance parameters, 151 and 21151 law application, and mass and energy balance equations are discussed. JIIIIIC I'll"! Centuries of experimental data has resulted in the establishment of a set of fundamental principles which describe the behavior of nature. The three most common principles relate directly to the thermodynamic evaluation of the Rankine cycle and are commonly referred to as: 1) the mass conservation principle, 2) the energy conservation principle, and 3) the entropy generation principle. The conservation of mass principle, as it applies to the analysis, state that mass may be neither created or destroyed during any process. The general form of the conservation of mass principle does provide for mass conservation into an energy form, however, this conversion is not applicable to this analysis of the Rankine cycle. The conservation of energy principle is commonly refereed to as the 151 law of thermodynamics and is simply stated by Cengal & Boles as "During an interaction between a system and its surroundings, the amount of energy gained by the system must be exactly equal to the amount of energy lost by the surroundings. " The entropy generation principle is commonly refereed to as the 20d law of thermodynamics and is simply stated as: in order for a process to be physically possible without heat transfer, the entropy of the system must remain the same or increase. Since the thermodynamic analysis of the Rankine cycle requires the application of these three principles on a control volume, all three principles will be discussed in detail as they relate to a steady state steady flow conu'ol volume in the following sections. 3]] i l' I' [II C I' [M 2' 'l The steady state, steady flow conservation of mass principle as it relates to any arbitrarily selected control volume with a single mass species crossing the control boundaries is stated as 2 mini = 2 mm; ' 3'1 Where min; = the ill! mass flow rate entering the control volume, [kg/sec] . 65 mom; = the i111 mass flow rate exiting the control volume, [kg/sec]. It should be noted that equation 3-1 only accounts for mass flow rates that cross the boundaries of the control volume and mass flow within the control boundaries are not considered. For the remainder of this discussion and within the RANKINE 3.0 code, mass flow rates are always positive and a mass flow rate leaving the control volume will be accounted via the sign notation within the equation. The RANKINE 3.0 code possess a series of internal checks to verify that program results are accurate. One of the internal checks is a mass balance on each device after all device thermodynamic information has been determined for the entire system. The device mass balance error is defined as 513m" = ngu- " 2mg“... 3'2 Where merror = device mass balance error, [kg/sec] min; = the ilh mass flow rate entering the control volume, [kg/sec] mom; = the in! mass flow rate exiting the control volume, [kg/sec]. 312 i l' I' [II C l' [E 2' 'l The steady state, steady flow conservation of energy principle neglecting kinetic and potential terms as it relates to any arbitrarily selected control volume with a single mass species crossing the control boundaries is stated as 9.. —W... = 2m. 42...). ->:.. 3-3 1' Where: Qin = total net heat transfer entering the control volume, [kW] Wout = total net work transferred exiting the control volume, [kW] min,i = the i131 mass flow rate entering the control volume, [kg/sec] hinj = the enthalpy of the i111 mass flow entering the conuol For t' com mix: :3ng The R if: a: dais: (NSC 66 volume, [Id/kg] mom; = the i111 mass flow rate exiting the control volume, [kg/sec] ham; = the enthalpy of the ill! mass flow exiting the control volume, [kJ/kg]. For the remainder of this discussion and within the RANKINE 3.0 code, the sign convention used for all heat and work terms shall be heat transferred into the control volume is positive and work transferred out the control volume is positive. In the event that heat uansfer is exiting the control volume or work is entering the control volume, the sign of the scalar will be negative. The RANKINE 3.0 code possess a series of internal checks to verify that program results are accurate. One of the internal checks is an energy balance on each device after all device thermodynamic information has been determined for the entire system. The device energy balance error is defined as is... = 2mm 1 hm - 2mg, . hm. + 9,, - Wm 34 Where Bertor = device energy balance error, [kW] min,i = the i111 mass flow rate entering the conuol volume, [kg/sec] hin,i = the enthalpy of the i311 mass flow entering the control volume, [kl/kg] mom; = the ill! mass flow rate exiting the control volume, [kg/sec]. hout,i = the enthalpy of the i111 mass flow exiting the control volume, [kJ/kg]. Qin = total net heat transfer entering the control volume, [kW] Wont = total net work transferred exiting the control volume, [kW] ill ! l'l’ [IIEI G I'll"! The 2115! law of thermodynamics represents the starting point for the derivation of several thermodynamic concepts which are applicable to the thermodynamic evaluation of the Rankine cycle. The applicable concepts are called availability, reversible work and irreversibility. 67 The property availability is a state variable and quantifies the thermodynamically maximum obtainable useful energy for a working fluid at a particular state. The availability at a particular state, neglecting kinetic and potential energy, is stated as A =(h—hM_m)—To ~(s—swflu) 3-5 Where: A = state availability, [kJ/kg] h = state enthalpy. [Id/kg] hdead_state = dead state enthalpy, [Id/kg] To = dead state temperature, [K] s = state entropy, [kJ/kg/K] Sdead_state = dead state entropy, [kJ/kg]. It should be noted that the calculation of availability always uses the dead state temperatm'e. The definition of reversible work is similar to availability, except that reversible work quantifies the thermodynamically maximum obtainable useful energy for a process as opposed to a state. The reversible work for a steady state steady flow control volume analysis neglecting kinetic and potential energy changes is stated as Wm = 2 (m, '((h.-...- - hm... ) — To“. (SW. 4 SW D) 3-6 Where: Wrev = process reversible work [kW] mi = the i111 mass flow rate entering the control volume, [kg/sec] hin,i = the enthalpy of the i311 flow entering the control volume, [kJ/kg] houtj = the enthalpy of the i111 flow exiting the control volume, [Id/kg] To; = temperature at which heat transfer occurs, [k] sin; = the entropy of the im flow entering the control volume [kJ/kg/K] song = the entropy of the im flow exiting the control volume [kJ/kg/K] It should be noted that equation 3-4 applies for adiabatic as well as non-adiabatic processes. In the event that a process is adiabatic, the To value. is set to the temperature at which heat transfer would occur if it did occur, usually the dead state temperature. 1: sh; v ”a 3" U m.” ‘l‘ 68 Irreversibility is defined as the difference between the maximum amount of work obtainable during a process and the actual work obtained during a process. Physically, irreversibility accounts for the lost potential to do work due to physical factors such as friction, unrestrained expansion, heat transfer due to non-incremental temperatures differences, mixing and turbulence. Mathematically, irreversibility is defined as 1 = Wm — Wm 3-7 Where: I = process irreversibility, [kW] Wrev = process reversible work, [kW] Wout = process actual work, [kW]. It should be noted that a negative irreversibility represents a thermodynamic performance better than the thermodynamically best performance and, hence, violates the 2351 law of thermodynamics. W A boiler is a device where heat originating from combustion gasses, a nuclear reactor, or other source is transferred to the working fluid traveling through the boiler. In an ideal boiler, the heat addition occurs as a constant pressure processes. Frequently, a boiler will have one or more reheat legs. A boiler with a reheat leg permits the working fluid to reenter the boiler after the working fluid has traveled through a high pressure turbine. Since the overall system efficiency increases via reheating and the thermodynamic performance of a turbine decreases with increasing working fluid moisture, the reheat leg is a commonly used technique to increase the efficiency of a system. The symbolic representation for a SIMPLE BOILER device with one reheat leg is shown in Figure 3-1. Even though RANKINE 3.0 is capable of modeling upto 10 reheat legs, only one reheat leg is shown in Fig. 3—1. 69 Heat $ Borler ert I C $- Reheat Leg #1 Inlet F Reheat Leg #1 Exit Boiler Inlet Figure 3-1. Symbolic representation for a SIMPLE BOILER device Figm'e 3-2 shows the relevant state and device variables utilized within the RANKINE 3.0 source code. The conservation of mass, 151 law, and 21151 law application to the SIMPLE BOILER device will utilize the identical state and device variable nomenclature utilized with the RANKINE 3.0 source code. The variable nomenclature utilized by RANKINE 3.0 is defined in Table 2-12. xnno 2 _> MBRO, l-IBRO, snaoanno moan C $— Mnnra). HRHIG). SRIII(I), Anna) F MRHoa), HRHO(I), snnoa). ARI-10(1) MBRI. HBRI. SBRI. ABRI Figure 3-2. RANKINE 3.0 variables for the SIMPLE BOILER device In order to provide the maximum amount of thermodynamic information to the user, the conservation of mass, the 151— law of thermodynamics, and the 2351 law of thermodynamics are applied to multiple control volumes within the SIMPLE BOILER device. The first control volume is selected around the inlet to exit fluid path and, if required, additional control volumes are selected around the fluid paths of each reheat leg. WWW 70 The working fluid pressure drop within the SIMPLE BOILER device is quantified with a user specified pressure drop or percentage pressure drop. If a user specified pressure drop is specified for the boiler inlet to exit path or for a reheat leg, than the relationships between inlet and exit pressure are defined below PBRO = PBRI - PLBOL 3-8 PRHOU) = PRHI(I)-PLRH(I) 3-9 Where: PBRO = working fluid pressure at boiler exit, [MPa] PBRI = working fluid pressure at boiler inlet, [MPa] PLBOL = working fluid pressure loss between boiler inlet to exit, [MPa] PRHO(I) = working fluid pressure at reheat leg #1 exit, [MPa] PRHI(I) = working fluid pressure at reheat leg #I inlet, [MPa] PLRH(I) = working fluid pressure loss between reheat leg #I inlet and exit. [MPa] If a user specified percentage pressure drop is specified for either the boiler or for a reheat leg, than the relationships between inlet and exit pressure are defined below PBRO = PBRI -[1— PPLBOL] 3-10 PRHO(1) = PRHI(I)-[l-PPLRH(I)] 3-11 Where: PBRO = working fluid pressure at boiler exit, [MPa] PBRI = working fluid pressure at boiler inlet, [MPa] PPLBOL = working fluid percentage pressure drop between boiler inlet to exit path, [-] PRI-IO(I) = working fluid pressure at reheat leg #1 exit, [MPa] PRHI(I) = working fluid pressure at reheat leg #I inlet, [MPa] PPLRH(I) = working fluid percentage pressure loss between reheat leg #I inlet and exit, [-] It should be noted that percent pressure losses are based upon percent of inlet pressure, not percent of exit pressure. an: W3: w I la. Wat: “acre 71 322 M C I. E II SIMHEBQHEBD . With a control volume selected around the physical boundaries of the boiler inlet to boiler exit path, the steady state steady flow mass conservation principle yields MBRI = MBRO 3-12 Where: MBRI = working fluid mass flow rate at the boiler inlet, [kg/sec] MBRO = working fluid mass flow rate at the boiler exit, [kg/sec]. With a control volume selected around the physical boundaries of the {IQ reheat leg, the steady state conservation of mass yields MRHI(I) = MRHO(I) 3-13 Where: MRI-11(1) = working fluid mass flow rate at the reheat leg #1 inlet, [kg/sec] MRHO(I) = working fluid mass flow rate at the reheat leg #1 exit, [kg/sec]. 323 III ! I'E II SHIEIEBQIIEBD . With a control volume selected around the physical boundaries of the boiler inlet to exit path, a steady state steady flow 151 Law control volume analysis neglecting the kinetic and potential terms yields XBRO = MBRO - HBRO — MBRI - HBRI 3-14 Where: XBRO = heat transferred from the surrounds during the boiler inlet to exit process, [kW] MBRO = working fluid mass flow rate at boiler exit, [kg/sec] HBRO = working fluid enthalpy at boiler exit, [kl/kg] HBRI = working fluid enthalpy at boiler inlet, [kl/kg]. 72 With a control volume selected around the physical boundaries of the 1111 reheat leg, a steady state 151 Law control volume analysis neglecting the kinetic and potential terms yields XRI-IO(I) = MRHO(I)- HRHOU) — MRHI(I) - HRHI (I )] 3-15 Where: XRHO(I) = heat transferred from the surrounds during the 1111 reheat leg process, [kW] MRHO(I) = working fluid mass flow rate at reheat leg #1 exit, [kg/sec] HRHO(I) = working fluid enthalpy at reheat leg #1 exit, [kl/kg] HRHI(I) = working fluid enthalpy at reheat leg #I inlet, [kJ/kg]. Since the SIMPLE BOILER device does, by definition, no work on the surrounds, all SIMPLE BOILER device work terms are zero. These terms are stated below as WKBRO = 0 3-16 WKRHOU) = 0 3-17 Where: WKBRO = work done on the surrounds by the boiler inlet to exit process,.[kW]. WKRI-IO(I) = work done on the surrounds by the 1m reheat leg process, [kW]. 32' 2” i I 'E II SHEIEBQHEBD . The working fluid availability at each node denoted in Figure 3-1 is defined as ABRI = HBRI — HDEAD - TDEAD - [SBRI - SDEAD] 3- 18 ABRO = I-IBRO - HDEAD — TDEAD - [SBRO - SDEAD] 3-19 ARI-[1(1) = HRH] (I ) — HDEAD — 3-2 TDEAD - [SKI-11(1) - SDEAD] 0 Where: 73 ARI-10(1) = HRHO(I) - HDEAD - 3_21 'I'DEAD - [SRHO(I) — SDEAD] ABRI = working fluid availability at boiler inlet, [kW] HBRI = working fluid enthalpy at boiler inlet, [kl/kg] HDEAD = working fluid enthalpy at dead state conditions, [kJ/Kg] TDEAD = Deai state temperature, [K] SBRI = working fluid entropy at boiler inlet, [kJ/kg/K] SDEAD = working fluid entropy at dead state conditions, [kJ/kg/K] ABRO = working fluid availability at boiler exit, [kW] HBRO = working fluid enthalpy at boiler exit [kl/kg] SBRO = working fluid entropy at boiler exit, [kJ/kg/K] ARHI(I) = working fluid availability at reheat leg #I inlet, [kW] HRHI(I) = working fluid enthalpy at reheat leg #I inlet, [kl/kg] SRHI(I) = working fluid entropy at reheat leg #I inlet, [kJ/kg/K] ARHO(I) = working fluid availability at reheat leg #1 exit, [kW] I~IRHO(I) = working fluid enthalpy at reheat leg #1 exit, [kl/kg] SRHO(I) = working fluid entropy at reheat leg #I exit,[kJ/kg/K] With a conuol volume selected around the physical boundaries of the boiler inlet to exit path, a steady state steady flow 2nd Law conuol volume analysis neglecting the kinetic and potential terms yields Where: WKBRO = MBRI . [HBRI - HBRO - THRES ~ (SBRI - SBRO)] 3-22 WRBRO = reversible work of boiler inlet to exit process, [kW] MBRI = working fluid mass flow rate at boiler inlet, [kg/sec] HBRI = working fluid enthalpy at boiler inlet, [kl/kg] I-IBRO = working fluid enthalpy at boiler exit, [kl/kg] 'I'I-IRES = high temperature reservoir temperature, [K] SBRI = working fluid entropy at boiler inlet, [kJ/kg/K] SBRO = working fluid entropy at boiler exit, [kJ/kg/K] 74 With a control volume selected around the physical boundaries of the reheat leg #I path, a steady state 2351 Law conuol volume analysis neglecting the kinetic and potential terms yields WRRHOU) = MRHI(I) . [HRHI(I) — 3-23 I-IRHO(I) - THRES . (SRHI(I) — SRHO(I))] Where: WRRHO = reversible work of working fluid in reheat leg #1, [kW] MRI-11(1) = working fluid mass flow rate at reheat leg #1 inlet, [kg/sec] I-IRHI(I) = working fluid enthalpy at reheat leg #I inlet, [kl/kg] I-IRHO(I) = working fluid enthalpy at reheat leg #1 exit, [kl/kg] THRES = high temperature reservoir temperature, [K] SRI-II(I) = working fluid entropy at reheat leg #1 inlet, [kJ/kg/K] SRHO(I) = working fluid entropy at reheat leg #1 exit, [kJ/kg/K] It should be noted that RANKINE 3.0 assumes that the boiler inlet to exit path and all reheat legs exchange accept heat from the same high temperature reservoir. For the working fluid traveling within the boiler inlet to exit path, the irreversibility is defined as IRBRO = WRBRO — WKBRO 3-24 Where: IRBRO = irreversibility of inlet. to exit process, [kW] WRBRO = reversible work of inlet to exit path, [kW] WKBRO = work done on the surrounds by the worldng fluid in the boiler inlet to exit process,. [kW] For the working fluid traveling within the reheat #1 path, the irreversibility is defined as IRRHO(I) = WRRHO(I) — WKRHO(I) 3-25 Where: IRRHO(I) = irreversibility of reheat leg #1 process, [kW] WRRHO(I) = reversible work of reheat leg #1 process, [kW] WKRHOG) = work done on the surrounds by the working fluid in the 1111 reheat leg process, [kW]. 5mm 3 1: hr the work! isdcfned as what: its the we What: Forth“ m"Orisdt: “berg; L... 75 S l' 325]] SIMEIEBQIIEBD . 11 IE Bl For the working fluid traveling within the boiler inlet to exit path, the mass balance error is defined as MBBOL = MBRI — MBRO 3-26 Where: MBBOL= mass balance error for boiler inlet to exit path, [kg/sec] MBRI = working fluid mass flow rate at boiler inlet, [kg/sec] MBRO = working fluid mass flow rate at boiler exit, [kg/sec]. For the working fluid traveling within the i311 reheat leg, the mass balance error is defined as MB(I) = MRI-11(1) — MRHO(I) 3-27 Where: MB(I) = mass balance flow rate error for the i111 reheat leg, [kg/sec] MRI-11(1) = working fluid mass flow rate at the i111 reheat leg inlet, [kg/sec] MRHO(I) = working fluid mass flow rate at the ith reheat leg exit,[kg/sec]. For the working fluid traveling within the boiler inlet to exit path, the energy balance error is defined as EBBOL = MBRI * HBRI - MBRO * HBRO + XBRO - WKBRO 3—28 Where: EBBOL= energy balance error for boiler inlet to exit path, [kW] MBRI = working fluid mass flow rate at boiler inlet, [kg/sec] HBRI = working fluid enthalpy at boiler inlet, [kl/kg] MBRO = working fluid mass flow rate at boiler exit, [kg/sec] I-IBRO = working fluid enthalpy at boiler exit, [kl/kg] XBRO = heat transferred from the surrounds to the working fluid in the boiler inlet to exit path, [kW] WKBRO = work done on the surrounds by the boiler inlet to exit process,.[kW]. For I dtin Th: . Show “In 76 For the working fluid traveling within the im reheat leg, the energy balance error is defined as EB(I) = MRHIU) * I-IRI-ll(l) -— MRHO(I) * HRHOU) + XRHOU) —- WKRHO(I) 3-29 Where: EB(I)= energy balance error for ilh reheat leg,[kW] MRHI(I) = working fluid mass flow rate at reheat leg #I inlet, [kg/sec] I-IRHI(I) = working fluid enthalpy at reheat leg #I inlet, [kl/kg]. MRHO(I) = working fluid mass flow rate at reheat leg #1 exit, [kg/sec] HRHO(I) = working fluid enthalpy at reheat leg #1 exit, [kl/kg] XRHO(I) = heat transferred from the surrounds during the 1111 reheat leg process, [kW] WKRHOG) = work done on the surrounds by the 1111 reheat leg process, [kW]. W A turbine is a device which converts energy contained within a working fluid into rotating mechanical energy. As the working fluid passes through the turbine, work is done against rotor blades which are attached to a shaft. When the rotating shaft is connected to an electrical generator, elecuicity is produced. Frequently, a turbine is divided into stage groups. A stage group is defined as a set of stator and rotor blades in which the working fluid undergoes a continuous expansion. Usually, the end of a stage group is indicated by an extraction point. The symbolic representation for a SIMPLE TURBINE device with two extractions are shown in Figtn'e 3-3. Even though RANKINE 3.0 is capable of modeling upto 10 turbine extractions, only two extractions are shown in Fig. 3-3. EC]? l at... 3.0 5 SIM. DOKK Ito» ti C a. 0115: £1:jo dew 1;: 38:3 Work r=—> Extraction #1 Extraction #2 Figure 3-3. Symbol for a SIMPLE TURBINE device Figure 3-4 shows the relevant state and device variables utilized within the RANKINE 3.0 source code. The conservation of mass, 151 law, and 2nd law application to the SIMPLE TURBINE device will utilize the identical state and device variable nomenclature utilized with the RANKINE 3.0 source code. The variable nomenclature utilized by RANKINE 3.0 is defined in Table 2-12. MTREXO). H'I'REXG). MTREXG). S'l'Rl-Zxa). HTREXO). ATREXO) STREXO). ATREXG) Figure 3-4. RANKINE 3.0 variables for the SIMPLE TURBINE In Order to provide the maximum amount of thermodynamic information to the user, the conFicl‘vation of mass, the 151- law of thermodynamics, and the 2nd- law of thennodynamics are applied to multiple control volumes within the SIMPLE TURBINE device. The control volumes for the analysis are selected around each stage group within the Siluple turbine device. For “it it rm} 4’ A) x.) 78 W The thermodynamic performance of a SIMPLE TURBINE device is quantified with a user specified adiabatic stage group efficiency. The adiabatic stage group efficiency is defined as the ratio of actual working fluid enthalpy change divided by the ideal working fluid enthalpy change assuming an isentropic process. For the first stage group, the adiabatic stage group efficiency is defined as n _ HTRIN—I-HREXO) “‘-"”“" HTRIN - HTREXO)“ 3-30 Where: HTRIN = working fluid enthalpy at turbine inlet, [kl/kg] I-ITREX(1) = working fluid enthalpy at turbine extraction #1, [kl/kg] H'I‘REX(1)idca1 = working fluid enthalpy at turbine extraction #1 assuming an isentropic process, [kl/kg]. For the 2nd through 10111 stage group, the adiabatic stage group efficiency is defined as HTREX(I)—HTREX(I+1) . = 3-31 Humane-arm HTR EX( 1) _ HTREXU +1)“ Where: HTREXO) = working fluid enthalpy at turbine extraction #1, [kl/kg] I-ITREX(I+1) = working fluid enthalpy at turbine extraction #(I+1), [kl/kg] H'I'REX(I+1)idcal = working fluid enthalpy at turbine extraction #(1+l) assuming an isentropic process, [kl/kg] In general, the adiabatic stage group efficiency is used to calculate the actual stage group exit enthalpy and, hence, equations 3-30 and 3-31 are algebraically manipulated to solve for H'IREX(1) and HTREX(I+1). 332 M C I' E II SIMEIEIIIBBIIIED . 79 With a control volume selected around each turbine stage group, the steady state steady flow mass conservation principle provides a basis to determine the mass flow rate through each stage group. For the 151 stage group, the working fluid mass flow rate through the stage group is given by MT RST (l) = MT RIN 3-32 Where: MTRST(1) = working fluid mass flow rate through the 151 turbine stage sump. [kg/sec} MTRIN = working fluid mass flow rate at turbine inlet, [kg/sec] For the 1111 stage group, the working fluid mass flow rate through the stage group is given by MTRSTU) = MTRSTU -1)- MTREXU - 1) 3—33 Where: MTRST(I) = working fluid mass flow rate through the 1111 turbine stage group. [kg/soc] MTRST(I-l) = working fluid mass flow rate through the (rush turbine stage grow. [kg/sec} MTREX(I-1) = working fluid mass flow rate at (I-l)lh turbine extraction, Rand 333 III a I 'E II 51112115ntan . With a control volume selected around the first stage group, a steady state steady flow 151 Law control volume analysis neglecting the kinetic and potential terms yields WKTREX (1) = MTRST(1) - [HTRIN - HTREX (1)] 3-34 Where: WKTREX(1) = work done on the surrounds by the 151 turbine stage group process, [kW]. M'I'RST(1) = working fluid mass flow rate through the 15! turbine stage group. [kg/sec] Wile; 80 HTRIN = working fluid enthalpy at turbine inlet, [kl/kg] HTREX(1) = working fluid enthalpy at turbine extraction #1, [kl/kg] With a control volume selected around the 2114 through 10m stage group, a steady state steady flow 131 Law control volume analysis neglecting the kinetic and potential terms yields WKTREXU):MTRST(I)-[lfl'REX(I—l)-HTREX(I)] 3-35 Where: WK'I'REX(I) = work done on the surrounds by the stage group #1 process,.[kW] MTRST(I) = working fluid mass flow rate through the 1111 turbine stage group. [kg/sec] HTREX(I-l) = working fluid enthalpy at turbine extraction #(1-1), [kl/kg] HTREXO) = working fluid enthalpy at turbine extraction #1, [kl/kg] Since the SIMPLE TURBINE device does not exchange heat with the surrounds, all SIMPLE TURBINE device heat transfer terms are zero. These terms are stated below as XTREXU): 0 3—36 Where: XTREX(I) = heat transferred from the surrounds during the 11h stage group process, [kW] 33' 2 ll 5 I . E II SIMHEIIIRBIHED . The worldng fluid availability at each node denoted in Figure 3-4 is defined as ATRIN = HTRIN - HDEAD - TDEAD - [STRIN — SDEAD] 3-37 ATREXU) = HTREX (I) - HDEAD - TDEAD - [STREX(I) — SDEAD] 3-38 Where: ATRIN = working fluid availability at turbine inlet, [kW] HTRIN = working fluid enthalpy at turbine inlet, [kl/kg] HDEAD = working fluid enthalpy at dead state conditions, [kl/Kg] TDEAD = Dead state temperature, [K] 81 STRIN = working fluid entropy at turbine inlet, [kl/kg/K] SDEAD = working fluid entropy at dead state conditions, [kl/kg/K] ATREX(I) = working fluid availability at turbine extraction #1, [kW] HTREX(I) = working fluid enthalpy at turbine extraction #I,[kJ/kg] STREX(I) = working fluid entropy at turbine extraction #1, [kJ/kg/K]. With a control volume selected around the 151 stage group, a steady state steady flow 2951 Law control volume analysis neglecting the kinetic and potential terms yields WRTRST(1)= MTRST(1)-[HTRIN -HI'REX(l)-TDEAD- (ST RIN - ST REX (1))] 3-39 Where: WRTRST(1) = reversible work of turbine stage group #1 process, [kW] MTRST(1) = working fluid mass flow rate through turbine stage group #1 , [kg/sec] HTRIN = working fluid enthalpy at turbine inlet, [kl/kg] HTREX(1) = working fluid enthalpy at turbine extraction #1, [kl/kg] TDEAD = dead state temperature, [K] STRIN = working fluid entropy at turbine inlet, [kJ/kg/K] STREX(l) .—. working fluid entropy at turbine extraction #1, [kJ/kg/K]. With a control volume selected around the 2nd through 10"h stage group, a steady state steady flow 2nd Law control volume analysis neglecting the kinetic and potential terms yields WRTRST(I)= M778ST(I)-[HTREX(I—l)-HTREX(I)-TDEAD- (STREX(I-l)—STREX(I))] 340 Where: WRTRST(I) = reversible work of turbine stage group #1 process, [kW] MTRST(I) = working fluid mass flow rate through turbine stage amp #1. [kg/sec] 1-ITREX(I—1) = working fluid enthalpy at turbine extraction #(I-l), [kl/kg] HTREX(I) = working fluid enthalpy at turbine extraction #1, [kJ/kg] TDEAD = dead state temperature, [K] STREX(I-1)= working fluid entropy at turbine extraction #(I-l), [kJ/kg/K] STREX(I) = working fluid entropy at turbine extraction #1, [kJ/kg/K]. 82 For the working fluid traveling within the 1311 stage group, the irreversibility is defined as IRTREXU) = WRTREXU) - WKTREXU) 3-41 Where: IRTREX(I) = irreversibility of stage group #1 process, [kW] WRTREXO) = reversible work of stage group #1 process, [kW] WKTREXG) = work done on the surrounds by the stage group #1 process,.[kW] The mass balance error for the entire SIMPLE TURBINE device is defined as MB(NTRST) = MTRIN - Ema/5x0) 3-42 I Where: MB(NTRST)= mass balance error for entire turbine device, [kg/sec] NTRST = number of turbine extractions, [-] MTRIN = working fluid mass flow rate at turbine inlet, [kg/sec] MTREX(I) = working fluid mass flow rate at 11h turbine extraction, [kg/sec] The energy balance error for the entire SIMPLE TURBINE device is defined as EB(NTRST)= MTRIN-HTRIN- 2(MTREX(I)'HTREX(I)+XTRD((I)-WKTREXU» 3-43 Where: EBBOL= energy balance error for entire turbine device, [kW] MTRIN = working fluid mass flow rate at turbine inlet, [kg/sec] HTRIN = working fluid enthalpy at turbine inlet, [kl/kg] MTREX(1) = working fluid mass flow rate at 1311 turbine exuaction, [kg/sec] HTREX(I) = working fluid enthalpy at turbine extraction #1, [kl/kg] XTREXO) = heat transferred from the surrounds during the 1111 stage group process, [kW] 83 WKTREX(I) = work done on the surrounds by the stage group #1 process,.[kW] W A pump is a device used to increase the pressure of a working fluid. Work is supplied to this device from an external source through a rotating shaft. The symbolic representation for a SIMPLE PUMP is shown in Figure 3-5. Disc huge . <1) Suction + Work Figure 3-5. Symbol for a SIMPLE PUMP device Figure 3-6 shows the relevant state and device variables utilized within the RANKINE 3.0 source code. The conservation of mass, 151 law, and 2nd law application to the SIMPLE PUMP device will utilize the identical state and device variable nomenclature utilized with the RANKINE 3.0 source code. The variable nomenclature utilized by RANKINE 3.0 is defined in Table 2-12. MPMPO. WMPIQ MPMPI. SPMPO. Q HPMPI. ”MP0 7 SPMPI. APMPI Figure 3-6. RANKINE 3.0 variables for the SIMPLE PUMP device Forth: SM and the 3111 mind the p liLIhi Tflt her-mo smiled ad th’nng fl: Wing flu: h E3116: 3}, 1 he“ eqlla 84 For the SIMPLE PUMP device, the conservation of mass, the 151 law of thermodynamics, and the 2114 law of thermodynamics are applied with a single control volume selected around the physical boundary of the device. “W The thermodynamic performance of a SIMPLE PUMP device is quantified with a user specified adiabatic efficiency. The adiabatic efficiency is defined as the ratio of the ideal working fluid enthalpy change assuming an isentropic process divided by the actual working fluid enthalpy change. Mathematically, the adiabatic efficiency is defined as _ HPMPOLd — HPMPI — 3-44 "M HPMPO - HPMPI Where: HPMPOideal = working fluid enthalpy at pump exit assuming an isentropic process, [kl/kg]. HPMPI = working fluid enthalpy at pump inlet, [kl/kg] HPMPO = working fluid enthalpy at pump exit, [kl/kg] HPMPOidcal = working fluid enthalpy at pump exit assuming an isentropic process, [kl/kg]. In general, the adiabatic efficiency is used to calculate the actual pump exit enthalpy and, hence, equation 3-44 is algebraically manipulated to solve for I-IPMPO. With a control volume selected around the physical boundaries of the SIMPLE PUMP device, the steady state steady flow mass conservation principle yields MPMPO = MPMPI 3-45 Where: MPMPO = working fluid mass flow rate at the pump exit, [kg/sec] MPMPI = working fluid mass flow rate at the pump inlet, [kg/sec]. _ 85 313 Ill ! I'E II SIMHEEIIMED . With a control volume selected around the physical boundaries of the SIMPLE PUMP device, a steady state steady flow 15.1 Law control volume analysis neglecting the kinetic and potential terms yields WKPMPO = MPMPI - [HPMPI - I-IPMPO] 3-46 Where: WKPMPO = work done on the surrounds by the pump process, [kW]. MPMPI = working fluid mass flow rate at the pump inlet, [kg/sec]. I-IPMPI = working fluid enthalpy at pump inlet, [kl/kg] HPMPO = working fluid enthalpy at pump exit, [kJ/kg] Since the SIMPLE PUMP device does not exchange heat with the surrounds, the SIMPLE PUMP device heat transfer term is zero. This term is stated below as XPMPO = 0 3-47 Where: XPMPO = heat transferred from the surrounds during the pump process, [kW] 3“ 2H 5 I 'E II SIMHEEIIMED . The working fluid availability at each node denoted in Figure 3-6 is defined as APMPI = HPMPI - HDEAD - TDEAD - [SPMPI - SDEAD] 3-48 APMPO = HPMPO - HDEAD — TDEAD - [SPMPO - SDEAD] 3-49 Where: APMPI = working fluid availability at pump inlet, [kW] HPMPI = working fluid enthalpy at pump inlet, [kl/kg] HDEAD = working fluid enthalpy at dead state conditions, [kl/Kg] TDEAD = Dead state temperature, [K] SPMPI = working fluid enuopy at pump inlet, [kJ/kg/K] SDEAD = working fluid entropy at dead state conditions, [kJ/kg/K] 86 APMPO = working fluid availability at pump exit, [kW] HPMPO = working fluid enthalpy at pump exit [kl/kg] SPMPO = working fluid entropy at pump exit, [kJ/kg/K] With a control volume selected around the physical boundaries of the SIMPLE PUMP device, a steady state steady flow 2&4 Law conuol volume analysis neglecting the kinetic and potential terms yields WRPMPO = MPMPI - [HPMPI - I-IPMPO — TDEAD- (SPMPI - SPMPO)] 3-50 Where: WRPMPO = reversible work of pump process, [kW] MPMPI = working fluid mass flow rate at pump inlet, [kg/sec] HPMPI = working fluid enthalpy at pump inlet, [kl/kg] I-IPMPO = working fluid enthalpy at pump exit, [kJ/kg] TDEAD = dead state temperature, [K] SPMPI = working fluid entropy at pump inlet, [kl/kg/K] SPMPO = working fluid entropy at pump exit, [kJ/kg/K]. For the SIMPLE PUMP device, the irreversibility is defined as IRPMPO = WRPMPO - WKPMPO 3-51 Where: IRPMPO = irreversibility of pump process, [kW] WRPMPO = reversible work of pump process, [kW] WKBRO = actual work done on the surrounds by pump process,.[kW] For the SIMPLE PUMP device, the mass balance error is defined as MB = MPMPI - MPMPO 3-52 Where: MB = mass balance error for pump device, [kg/sec] MPMPI = working fluid mass flow rate at pump inlet, [kg/sec] MPMPO = working fluid mass flow rate at pump exit, [kg/sec] 87 For the SIMPLE PUMP device, the energy balance error is defined as EB = MPMPI * HPMPI - MPMPO * HPMPO + XPMPO — WKPMPO 3-53 Where: EB = energy balance error for pump device, [kW] MPMPI = working fluid mass flow rate at pump inlet, [kg/sec] I-IPMPI = working fluid enthalpy at pump inlet, [kl/kg] MPMPO = working fluid mass flow rate at pump exit, [kg/sec] HPMPO = working fluid enthalpy at pump exit, [kl/kg] XPMPO = heat transferred from the surrounds during the pump process, [kW] WKPMPO = work done on the surrounds by the pump process, [kW]. W A pipe is a device which directs a working fluid from one location to a second location. The thermodynamic behavior of a pipe device is a working fluid pressure drop and a working fluid enthalpy decreases. Physically, the pressure drop is a result of a flow restriction within the pipe (such as a valve) or the interaction of a viscous working fluid and the pipe walls. The working fluid enthalpy decrease is a result of a hot working fluid interacting thermally with the pipe surrounds. The symbolic representation for a SIMPLE PIPE device is shown in Figure 3-7. Exit 9 OInlet j T Figure 3-7. Symbol for a SIMPLE PIPE device Figure 3-8 shows the relevant state and device variables utilized within the RANKINE 3.0 source code. The conservation of mass, 131 law, and 2nd law application to the SIMPLE PIPE device will utilize the identical state and device variable nomenclature utilized with the RAN KINE 3.0 source code. The variable nomenclature utilized by RAN KINE 3.0 is defined in Table 2-12. nun Q Q 3mm “1 M l ' SPIPIO. 5‘ m APIPO APIPl Figure 3-8. RANKINE 3.0 variables for the SIMPLE PIPE device For the SIMPLE PIPE device, the conservation of mass, the 131 law of thermodynamics, and the 21151 law of thermodynamics are applied with a single control volume selected around the physical boundary of the device. W The working fluid pressure drop within the SIMPLE PIPE device is quantified with a user specified pressure drop or percentage pressure drop. If a user specified pressure drop is specified, than the relationships between inlet and exit pressure is defined as PPIPO = PPIPI - PLPIP 3-54 Where: PPIPO = working fluid pressure at pipe exit, [MPa] PPIP1= working fluid pressure at pipe inlet, [MPa] PLPIP = working fluid pressure loss between pipe inlet and exit, [MPa] If a user specified percentage pressure loss is specified, than the relationships between inlet and exit pressure is defined as PPIPO = PPIPI - [l — PPLPIP] 355 Where: PPIPO = working fluid pressure at pipe exit, [MPa] PPIPI = working fluid pressure at pipe inlet, [MPa] PPLPIP = working fluid percentage pressure loss between pipe inlet and exit, {-1. 89 It should be noted that pipe percent pressure loss is based upon percent of inlet pressure, not percent of exit pressure. The working fluid enthalpy drop within the SIMPLE PIPE device is quantified with a user specified enthalpy drop or percentage enthalpy drop. If a user specified enthalpy drop is specified, than the relationships between inlet and exit enthalpy is defined as HPIPO = HPIPI - QLPIP 3-56 Where: I-IPIPO = working fluid enthalpy at pipe exit, [MPa] HPIPI = working fluid enthalpy at pipe inlet, [MPa] QLPIP = working fluid enthalpy loss between pipe inlet and exit, [MPa] If a user specified percentage enthalpy loss is specified, than the relationships between inlet and exit enthalpy is defined as I-IPIPO = HPIPI - [1 - PQLPIP] , 3-57 Where: I-IPIPO = working fluid enthalpy at pipe exit, [MPa] HPIPI = working fluid enthalpy at pipe inlet, [MPa] PQLPIP = working fluid percentage enthalpy loss between pipe inlet and exit, [-]. It should be noted that percent enthalpy loss is based upon percent of inlet enthalpy, not percent of exit enthalpy. ' 352 M C l' E II SHEIEEIEED . With a control volume selected around the physical boundaries of the SIMPLE PIPE device, the steady state steady flow mass conservation principle yields MPIPO = MPIPI 3-58 Where: MPIPO = working fluid mass flow rate at the pipe exit, [kg/sec] MPIPI = working fluid mass flow rate at the pipe inlet, [kg/sec]. 3531” ! 1'1? 1] SIMPIEEIEED' With a control volume selected around the physical boundaries of the SIMPLE PIPE device, a steady state steady flow 151 Law control volume analysis neglecting the kinetic and potential terms yields XPIPO = MPIPO - [HPIPO - HPIPI] 3—59 Where: XPIPO = heat transferred from the surrounds during the pipe \ process, [kW] MPMPO = working fluid mass flow rate at the pipe exit, [kg/sec]. I-IPMPO = working fluid enthalpy at pipe exit, [kl/kg] HPMP1= working fluid enthalpy at pipe inlet, [kl/kg] Since the SIMPLE PUMP device does not do work on the smrounds, the SIMPLE PIPE device work term is zero. This term is stated below as WKPIPO= 0 3-60 Where: WKPMPO = work done on the surrounds during the pipe process, [kW]. 35'1” 1 l . E II SIMEIEEIEED . The working fluid availability at each node denoted in Figure 3-8 is defined as APIPI = HPIPI - HDEAD - TDEAD - [SPIPI - SDEAD] 3-61 APIPO = HPIPO - HDEAD - TDEAD - [SPIPO - SDEAD] 3-62 Where: APIPI = working fluid availability at pipe inlet, [kW] HPIPI = working fluid enthalpy at pipe inlet, [kl/kg] HDEAD=working fluid enthalpy at dead state conditions, [kl/Kg] TDEAD = Dead state temperature, [K] Fr Fr 91 SPIPI = working fluid entropy at pipe inlet, [kJ/kg/K] SDEAD = working fluid entropy at dead state conditions, [kJ/kg/K] APIPO = working fluid availability at pipe exit, [kW] 1-IPIPO = working fluid enthalpy at pipe exit [kl/kg] SPIPO = working fluid entropy at pipe exit, [kl/kg/K] With a control volume selected around the physical boundaries of the pipe, a steady state steady flow 21!!! Law control volume analysis neglecting the kinetic and potential terms yields WRPIPO = MPIPI - [HPIPI - HPIPO - TDEAD - (SPIPI - SPIPO)] 3-63 Where: WRPIPO = reversible work of pipe process, [kW] MPIPI = working fluid mass flow rate at pipe inlet, [kg/sec] HPIPI = working fluid enthalpy at pipe inlet, [kl/kg] HPIPO = working fluid enthalpy at pipe exit, [kl/kg] TDEAD = dead state temperature, [K] SPIPI = working fluid entropy at pipe inlet, [kJ/kg/K] SPIPO = working fluid entropy at pipe exit, [kJ/kg/K]. For the SIMPLE PIPE DEVICE, the irreversibility is defined as IRPIPO = WRPIPO - WKPIPO 3-64 Where: IRPIPO = irreversibility of pipe process, [kW] WRPIPO = reversible work of pipe path, [kW] WKPMPO = work done on the surrounds during the pipe process, [kW]. For the SIMPLE PIPE DEVICE, the mass balance error is defined as MB = MPIPI - MPIPO 3-65 92 Where: MB= mass balance error for pipe, [kg/sec] MPIPI = working fluid mass flow rate at pipe inlet, [kg/sec] MPIPO = working fluid mass flow rate at pipe exit, [kg/sec]. For the SIMPLE PIPE DEVICE, the energy balance error is defined as EB = MPIPI * HPIPI - MPIPO * HPIPO + XPIPO - WKPIPO 3-66 Where: EB = energy balance error for pipe, [kW] MPIPI = working fluid mass flow rate at pipe inlet, [kg/sec] I-IPIPI = working fluid enthalpy at pipe inlet, [kl/kg] MPIPO = working fluid mass flow rate at pipe exit, [kg/sec] I-IPIPO = working fluid enthalpy at pipe exit, [kl/kg] XPIPO = heat transferred from the surrounds during the pipe process, [kW] WKPIPO = work done on the surrounds by the pipe process, [kW]. W A junction is a device which is used to divide (or connect) a working fluid mass stream into multiple (or one) working fluid mass streams. The thermodynamic state of each mass steam is unaffected by the junction device. The symbolic representation for a SIMPLE JUNCTION device with two inlets and two exits is shown in Figure 3-9. Even though only two inlets and two exits are shown in Fig. 3-9, RANKINE 3.0 is capable of modeling 10 inlets and 10 exits. Inlet #1 Exit #1 Inlet #2 Exit #2 Figure 3-9. Symbol for a SIMPLE JUNCTION device Figure 3-10 shows the relevant state and device variables utilized within the RANKINE 3.0 source code. The conservation of mass, 131 law, and 2nd law application to the 93 SIMPLE JUNCTION device will utilize the identical state and device variable nomenclature utilized with the RANKINE 3.0 source code. The variable nomenclature utilized by RANKINE 3.0 is defined in Table 2-12. MJCI'I(1). WW1). 111010). H1000). srcrlu). srcroo). AJCI‘I(1). moo). srcntz). "1sz AJC'I'I 2. 3100(2) ( ) Araoa). MJC'I'1(2). menu), 9- mama). Figure 3-10. RANKINE 3.0 variables for the SIMPLE JUNCTION device For the SIMPLE JUNCTION device, the conservation of mass, the 151 law of thermodynamics, and the 2m! law of thermodynamics are applied with a single control volume selected around the physical boundary of the device. The division of mass flow within the SIMPLE JUNCTION device may be stated with a user specified flow fraction. The flow fraction is defined as the ratio of a, specific inlet (or exit) mass flow divided by the total device inlet (or exit) mass flow. For the junction inlet paths, this ratio is mathematically defined as MJCTIU) FIG]? I = 3-67 ( ) S MJCTIU) I Where: FJCTI(1) = fraction of total inlet mass flow attributed to the Ithinlet,[-] MJCI'I(1) = working fluid mass flow rate at junction inlet #1, [kg/sec] For the junction exit paths, this ratio is mathematically defined as MJCTOU) 3_68 FJCTO(I) = 2 M16700) 1 94 Where: FJCTO(I) = fraction of total inlet mass flow attributed to the 1th exit,[-] MJCI‘ 0(1) = working fluid mass flow rate at junction exit #1, [kg/sec] 362 M C I' E II SHIRIEHIIICIIQIID . With a control volume selected around the physical boundaries of the boiler inlet to boiler exit path, the steady state steady flow mass conservation principle yields Ewan!) = zmcrou) 3-69 I - I Where: MJCTI(I) = working fluid mass flow rate at junction inlet #1, [kg/sec] MJCTO(I) = working fluid mass flow rate at junction exit #I, [kg/sec]. 363 Ill 5 I 'E II SHIEIEHIMCTIQIID . With a control volume selected around the physical boundaries of the SIMPLE JUNCTION device, a steady state steady flow 151 law control volume analysis neglecting the kinetic and potential terms yields 0: ZMJCTOU)HJCTO(I)—2MJCTI(I)-HJCTI(I) 3-70 I ' I Where: MJCTO(1) = working fluid mass flow rate at junction exit #1, [kg/sec] HJCI‘O(I) = working fluid enthalpy at junction exit #1, [kl/kg] MJCTI(I) = working fluid mass flow rate at junction inlet #1, [kg/sec] HJCTI(I) = working fluid enthalpy at junction inlet #1, [kl/kg] Since the SIMPLE JUNCTION device does no work on the surrounds and does not exchange heat with the surrounds, all SIMPLE JUNCTION device work terms and heat transfer terms are zero. These terms are stated below as WKICTOU) = 0 3-71 XJCT 0(1 ) = 0 3-72 95 Where: WKJCI‘O(I) = work done on the surrounds by the junction,.[kW] XJCTO(I) = heat transferred from the surrounds during the junction process, [kW]. 36! 2 II ! I . E II SHIEIEIIIIICHQND . The working fluid availability at each node denoted in Figure 3-10 is defined as AJCI'IU) = HJCTI (I ) - HDEAD - TDEAD - [SJCTI(I) - SDEAD] 3-7 3 AJCI’ 0(1 ) = HJCT 0(1 ) - HDEAD — TDEAD -[SJC1‘0(I)- SDEAD] 3-74 Where: AJCI'I(I) = working fluid availability at junction inlet #1, [kW] HJCI'I(I) = working fluid enthalpy at junction inlet #1, [kl/kg] HDEAD=working fluid enthalpy at dead state conditions, [kl/Kg] TDEAD = Dead state temperature, [K] SJCT'I(I) = working fluid entropy at junction inlet #1, [kJ/kg/K] SDEAD = working fluid entropy at dead state conditions, [kJ/kg/K] AJCTO(I) = working fluid availability at junction exit #1, [kW] HJCI‘O(1) = working fluid enthalpy at junction exit #1, [kl/kg] SJCTO(I) = working fluid entropy at junction exit #1, [kJ/kg/K] With a control volume selected around the physical boundaries of the SIMPLE JUNCTION device, a steady state steady flow 211d- law control volume analysis neglecting the kinetic and potential terms yields WRJCTO = 0.0 3-75 Where: WRBRO = reversible work of junction, [kW] It should be noted that equation 3-75 is a direct result of the fact that the SIMPLE JUNCTION device does not change the state of the working fluid as it travels through the device (i.e., there is no thermodynamic process). 96 For the SIMPLE JUNCTION device, the irreversibility is defined as IRJCTO(I) = 0.0 3-76 Where: IRBRO = irreversibility of junction, [kW]. It should be noted that equation 3-75 is a direct result of the fact that the SIMPLE JUNCTION device does not change the state of the working fluid as it travels through the device (i.e., there is no thermodynamic process). For the SIMPLE JUNCTION device, the mass balance error is defined as MB= ZMJCTI(I)-2MJCI'0(I) 3-77 I I Where: MB= mass balance error for junction, [kg/sec] MJCTI(I) = working fluid mass flow rate at junction inlet #1, [kg/sec] MJCTO(I) = working fluid mass flow rate at junction exit #1, [kg/sec]. For the SIMPLE JUNCTION device, the energy balance error is defined as EB = X MJCTI(I) - menu) - 2 MJcroa) - HJCTOU) + ’ ’ 3-78 2100100) — 2 WKJcrou) l I Where: EB= energy balance error for junction [kW] MJCTI(I) = working fluid mass flow rate at junction inlet #1, [kg/sec] HJCTI(I) = working fluid enthalpy at junction inlet #1, [kJ/kg]. MJCTO(I) = working fluid mass flow rate at junction exit #I, [kg/sec] HJCI‘O(I) = working fluid enthalpy at junction exit #I, [kl/kg] XJCTO(I) = heat transferred from the surrounds during the junction Process. [kW] WKRHOO) = work done on the surrounds by junction process, [kW]. W A condenser is a device where working fluid energy is rejected to a cooling medium such as a lake, a river, or the atmosphere. In an ideal condenser, the working fluid experiences no pressure drop as it travels through the condenser and the fluid exits the condenser as a saturated liquid. .The symbolic representation for a SIMPLE CONDENSER device with two inlets is shown in Figure 3-11. Even though RANKINE 3.0 is capable of modeling upto 27 condenser inlets, only two are shown in Fig. 3-11. Inlet #1 Inlet #2 -|—O +0 Heat Figure 3-11. Symbol for a SIMPLE CONDENSER device Figure 3-12 shows the relevant state and device variables utilized within the RANKINE 3.0 source code. The conservation of mass, 151 law, and 2“ law application to the SIMPLE CONDENSER device will utilize the identical state and device variable nomenclature utilized with the RANKINE 3.0 source code. The variable nomenclature utilized by RANKINE 3.0 is defined in Table 2-12. ii ,‘I MCDI(1), MCDI(2). HCDI(1). HCDI(2). SCDI(1). SCDI(2), ACDI(I) ACDI(2) +0 XCDO «- MCDO. cho. SCIX), ACIX) Figure 3-12. RANKINE 3.0 variables for the SIMPLE CONDENSER device For the SIMPLE CONDENSER device, the conservation of mass, the 151 law of thermodynamics, and the 2nd law of thermodynamics are applied with a single control volume selected around the physical boundary of the device. The SIMPIE CONDENSER device does not have any device performance parameters. 312 M [I l' E II SHRIECQIIDEIISEBD . With a control volume selected around the physical boundaries of the SIMPLE CONDENSER device, the steady state steady flow mass conservation principle yields XMCDIU) = MCDO 3-79 I Where: MCDI(I) = working fluid mass flow rate at the condenser inlet #1, [kg/sec] MCDO = working fluid mass flow rate at the condenser exit, [kg/sec]. WW 99 With a control volume selected around the SIMPLE CONDENSER device, a steady state steady flow 151 law control volume analysis neglecting the kinetic and potential terms yields xc00= MCDO-HCDO-EMCDIU)HCDI(I) 3-80 I Where: XJCTO = heat transferred from the surrounds during the condensing process, [kW] MCDO(I) = working fluid mass flow rate at condenser exit, [kg/sec] I-ICDO(I) = working fluid enthalpy at condenser exit, [kJ/kg] MCDI(I) = working fluid mass flow rate at condenser inlet #1, [kg/sec] HCDI(1) = working fluid enthalpy at condenser inlet #1, [kl/kg]. It should be noted that the SIMPLE CONDENSER model assumes that condenser exit state is a saturated liquid. Since the SIMPLE CONDENSER device does no work on the surrounds, the SIMPLE CONDENSER device work term is zero. This term is stated below as WKCDO = 0 3-81 Where: WKCDO = work done on the surrounds by the condenser,.[kW] 32' 2 II 1 l . E II SHIEIECQIIDEIISEBD . The working fluid availability at each node denoted in Figure 3— 12 is defined as ACDI (I) = HCDI(I) — HDEAD — TDEAD ~ [SCDI (I ) - SDEAD] 3-82 ACDO = HCDO — HDEAD — TDEAD - [SCDO - SDEAD] 3-83 Where: ACDI(I) = working fluid availability at condenser inlet #1, [kW] HCDI(I) = working fluid enthalpy at condenser inlet #1, [kJ/kg] HDEAD=working fluid enthalpy at dead state conditions, [kJ/Kg] 1m TDEAD = Dead state temperature, [K] SCDI(I) = working fluid entropy at condenser inlet #1, [kJ/kg/K] SDEAD = working fluid entropy at dead state conditions, [kl/kg/K] ACDO = working fluid availability at condenser exit, [kW] HCDO = working fluid enthalpy at condenser exit [kJ/kg] SCDO = working fluid entropy at condenser exit, [kJ/kg/K] With a control volume selected around the physical boundaries of the SIMPLE CONDENSER device, a steady state steady flow 21151 Law control volume analysis neglecting the kinetic and potential terms yields WRCDO = 2 (MCDI(I) . [HCDI(I) - HCDO - TDEAD- (SCDI(I) - swan) 3-84 I Where: WRCDO = reversible work of condenser process, [kW] MCD1(I) = working fluid mass flow rate at condenser inlet #1, [kg/sec] I-ICD1(I) = working fluid enthalpy at condenser inlet #1, [kl/kg] HCDO = working fluid enthalpy at condenser exit [kl/kg] TDEAD = Dead state temperature, [K] SCDI(I) = working fluid entropy at condenser inlet #1, [kJ/kg/K] SCDO = working fluid entropy at condenser exit, [kJ/kg/K] For the SIMPLE CONDENSER device, the irreversibility is defined as IRCDO = WRCDO - WK CDO 3-85 Where: IRCDO = irreversibility of condenser process, [kW] WRCDO = reversible work of condenser process, [kW] WKCDO = work done on the surrounds by the condenser,.[kW] .aqm It' lul' Ikll L (L'lu'ur‘x‘un u' a :ttttr' For the SIMPLE CONDENSER device, the mass balance error is defined as MB= 2MCDI(l)—MCDO 3-86 I 101 Where: MB= mass balance error for condenser, [kg/sec] MCDI(I) = working fluid mass flow rate at condenser inlet #1, [kg/sec] MCDO = working fluid mass flow rate at condenser exit, [kg/sec]. For the SIMPLE CONDENSER device, the energy balance error is defined as EB = ZMCDI(I)- HCDI(I) — MCDO- HCDO + XCDO - WKCDO 3-87 I Where: EB= energy balance error for condenser, [kW] MCDI(I) = working fluid mass flow rate at condenser inlet #1, [kg/sec] HCDI(1) = working fluid enthalpy at condenser inlet #1, [kJ/kg] MCDO = working fluid mass flow rate at condenser exit, [kg/sec]. HCDO = working fluid enthalpy at condenser exit [kl/kg] XCDO = heat transferred from the surrounds during the condensing process, [kW] WKCDO = work done on the surrounds by the condenser,. [kW] W A heat load is a device which transfers heat between the working fluid and the surrounds. Usually, a heat load device is used in the modeling of co- generation power systems. The symbolic representation for a SIMPLE HEAT LOAD device is shown in Figure 3- 13. Inlet W Exit ‘Heat Figure 3-13. Symbol for a SIMPLE HEAT LOAD device 102 Figure 3-8 shows the relevant state and device variables utilized within the RANKINE 3.0 source code. The conservation of mass, 151 law, and 2nd law application to the SIMPLE HEAT LOAD device will utilize the identical state and device variable nomenclature utilized with the RANKINE 3.0 source code. The variable nomenclature utilized by RANKINE 3.0 is defined in Table 2-12. mum * mu r : - MHLDI. sriLno' "mm“ - - SHLDI. Alum arm xnuro Figure 3-14. RANKINE 3.0 variables for the SIMPLE HEAT LOAD device For the SIMPLE HEAT LOAD device, the conservation of mass, the 151 law of thermodynamics, and the 21151 law of thermodynamics are applied with a single control volume selected around the physical boundary of the device. The SIMPLE HEAT LOAD device does not have any device performance parameters. 382 M C l' E II SIMEIEIIEIIIDIDD . With a control volume selected around the physical boundaries of the SIMPLE HEAT LOAD device, the steady state steady flow mass conservation principle yields MHIJJI = MHLDO 3-88 Where: MHLDI = working fluid mass flow rate at the heat load inlet, [kg/sec] MHLDO = working fluid mass flow rate at the heat load exit, [kg/sec]. 383 III 1 I'E II SHIRIEIIElIIQIDD . 103 With a control volume selected around the physical boundaries of the SIMPLE HEAT LOAD device, a steady state steady flow 15! Law control volume analysis neglecting the kinetic and potential terms yields XHLDO = MHLDO - HHLDO - MHLDI - HHLDI 3-89 Where: XHLDO = heat transferred from the surrounds during the heat load process, [kW] MHLDO = working fluid mass flow rate at heat load exit, [kg/sec] III-ILDO = working fluid enthalpy at heat load exit, [kl/kg] MHLDI = working fluid mass flow rate at heat load inlet, [kg/sec] HHLDI = working fluid enthalpy at heat load inlet, [kl/kg]. Since the SIMPLE HEAT LOAD device does no work on the surrounds, all SIMPLE HEAT LOAD device work terms are zero. These terms are stated below as WKHLDO = 0 3-90 Where: WKHLDO = work done on the surrounds by the heat load process ,.[kW] The working fluid availability at each node denoted in Figure 3- 14 is defined as AHLDI = HHLDI - HDEAD - TDEAD ~ [SHLDI - SDEAD] 3-91 AHLDO = IIHLDO — HDEAD — TDEAD - [SHLDO - SDEAD] 3-92 Where: AHLDI = working fluid availability at heat load inlet, [kW] HHLDI = working fluid enthalpy at heat load inlet, [kJ/kg] HDEAD=working fluid enthalpy at dead state conditions, [kl/Kg] TDEAD = Dead state temperature, [K] SI-ILDI = working fluid entropy at heat load inlet, [kJ/kg/K] SDEAD = working fluid entropy at dead state conditions, [kJ/kg/K] 104 AI-ILDO = working fluid availability at heat load exit, [kW] HI-ILDO = working fluid enthalpy at heat load exit [kl/kg] SHLDO = working fluid enuopy at heat load exit, [kJ/kg/K] With a control volume selected around the physical boundaries of the SIMPLE HEAT LOAD device, a steady state steady flow 2351 Law control volume analysis neglecting the kinetic and potential terms yields WRHLDO = MI-ILDI - [HHLDI - I-IHLDO - TDEAD - (SHLDI - SHLDO)] 3-93 Where: WRHLDO = reversible work of heat load process, [kW] MHLDI = working fluid mass flow rate at heat load inlet, [kg/sec] I-II-ILDI = working fluid enthalpy at heat load inlet, [kl/kg] HHLDO = working fluid enthalpy at heat load exit, [kl/kg] TDEAD = dead state temperature, [K] SHLDI = working fluid entropy at heat load inlet, [kJ/kg/K] SHLDO = working fluid entropy at heat load exit, [kJ/kg/K] For the SIMPLE HEAT LOAD device, the irreversibility is defined as IRI-ILDO = WRHLDO - WKHLDO 3-94 Where: IRHLDO = irreversibility of heat load process, [kW] WRHLDO = reversible work of heat load process, [kW] WKHLDO = work done on the surrounds during the heat load process,.[kW] For the SIMPLE HEAT LOAD device, the mass balance error is defined as MB = MHLDI - MHLDO 3-95 Where: MB= mass balance error for heat load device, [kg/sec] MI-ILDI = working fluid mass flow rate at heat load inlet, [kg/sec] 105 MI-ILDO = working fluid mass flow rate at heat load exit, [kg/sec]. For the SIMPLE HEAT LOAD device, the energy balance error is defined as EB = MHLDI * HHLDI — MHLDO * HHLDO + XHLDO - WKI-ILDO 3-96 Where: . EB= energy balance error for heat load device, [kW] MHLDI = working fluid mass flow rate at heat load inlet, [kg/sec] ' HHLDI = working fluid enthalpy at heat load inlet, [Id/kg] MHLDO = working fluid mass flow rate at heat load exit, [kg/sec] HI-ILDO = working fluid enthalpy at heat load exit, [kl/kg]. XHLDO = heat transferred from the surrounds during the heat load process, [kW] WKHLDO = work done on the surrounds by the heat load process ,.[kW]. We: An open feed water (OFW) heater device is a mixing chamber in which streams of different energies are mixed to form a stream with an intermediate energy. Ideally, the mixture leaves the open feed water heater as a saturated liquid. It should be noted that since mixing occurs, the mixing of the extracted steam and the feed water is a constant pressure process. The symbolic representation for a SIMPLE OFW HEATER device is shown in Figure 3- 15. Extraction Inlet I Feed Witter FeedWater Eli! Inlet Figure 345. Symbol for a SIMPLE OFW HEATER device 1‘ . 106 Figure 3-16 shows the relevant state and device variables utilized within the RANKINE 3.0 source code. The conservation of mass, 151 law, and 2nd law application to the SIMPLE OFW HEATER device will utilize the identical state and device variable nomenclature utilized with the RANKINE 3.0 source code. The variable nomenclature utilized by RAN KINE 3.0 is defined in Table 2-12. MOFWO. 1 MOFWI. HOFWO. HOFWI, SOFWO. SOFWL AOFWO AOFWI Figure 3-16. RANKINE 3.0 variables for the SIMPLE OFW HEATER device For the SIMPLE OFW HEATER device, the conservation of mass, the 151 law of thermodynamics, and the 21151 law of thermodynamics are applied with a single control volume selected around the physical boundary of the device. The SIMPLE OFW HEATER device does not have any device performance parameters. With a control volume selected around the physical boundaries of the SIMPLE OFW HEATER Device, the steady. state steady flow mass conservation principle yields MOFWI + MOFWF ='MOFWO 3-97 Where: MOFWII = working fluid mass flow rate at the open feed water heater inlet, [kg/sec] MOFWF = working fluid mass flow rate at the open feed water extraction 107 inlet exit, [kg/sec]. MOFWO = working fluid mass flow rate at the open feed water heater exit, [kg/sec]. 323 III ! I'E II SHIEIEQEEZIIEEIEBD . With a control volume selected around the physical boundaries of the SIMPLE OFW device, a steady state steady flow 151 Law control volume analysis neglecting the kinetic and potential terms yields 0 = MOFWI -I-10FWI + MOFWF- HOFWF - MOFWO- HOFWO 3—98 Where: MOFWI = working fluid mass flow rate at the open feed water heater inlet, [kg/sec] HOFWI = working fluid enthalpy at Open feed water heater inlet, [kl/kg] MOFWF = working fluid mass flow rate at the open feed water extraction inlet exit, [kg/sec]. HOFWF = working fluid enthalpy at open feed water heater extraction inlet. [kl/kg] ’ MOFWO = working fluid mass flow rate at the open feed water heater exit, [kg/sec]. HOFWO = working fluid enthalpy at open feed water heater exit, [kl/kg] Since the SIMPLE OFW HEATER device does no work on the surrounds and does not exchange heat with the surrounds, all SIMPLE OFW HEATER device work terms and heat transfer terms are zero. These terms are stated below as Where: WKOFWOU) = 0 3-99 XOFWO(I) = 0 3- 100 WKOFWO(I) = work done on the surrounds by the open feed water heater device,. [kW] XOFWO(I) = heat transferred from the surrounds during the open feed water heater process, [kW]. W1 Li: H3] ME IN The working fluid availability at each node denoted in Figure 3-16 is defined as Where: AOFWI = HOFWI - HDEAD - TDEAD - [SOFWI —-SDEAD] '3-101 AOFWF = HOFWF - HDEAD — TDEAD - [SOFWF - SDEAD] 3-102 AOFWO = HOFWO - HDEAD - TDEAD - [SOFWO - SDEAD] 3- 103 AOFWI = working fluid availability at open feed water heater inlet, [kW] HOFWI = working fluid enthalpy at open feed water heater inlet, [kJ/kg] HDEAD=working fluid enthalpy at dead state conditions, [kl/Kg] TDEAD = Dead state temperature, [K] SOFWI = working fluid entropy at open feed water heater inlet, [kJ/kg/K] SDEAD = working fluid entropy at dead state conditions, [kJ/kg/K] AOFWF = working fluid availability at extraction inlet, [kW] HOFWF = working fluid enthalpy at extraction inlet [kJ/kg] SOFWF = working fluid entropy at extraction inlet, [kJ/kg/K] AOFWO = working fluid availability at open feed water exit, [kW] HOFWO = working fluid enthalpy at open feed water exit [kl/kg] SOFWO = working fluid entropy at Open feed water exit, [kJ/kg/K]. With a control volume selected around the physical boundaries of the SIMPLE OFW HEATER device, a steady state steady flow 21151 Law control volume analysis neglecting the kinetic and potential terms yields WROFWO = MOFWI - [HOFWI - HOFWO - TDEAD - (SOFWI — SOFWO)] + Where: 3-104 MOFWF - [HOFWF - HOFWO - TDEAD - (SOFWF - SOFWO” WROFWO = reversible work of open feed water heater process, [kW] MOFWI = working fluid mass [flow rate at the open feed water heater inlet. [kg/see] F0. h 109 HOFWI = working fluid enthalpy at open feed water heater inlet, [Id/kg] HOFWO = working fluid enthalpy at open feed water heater exit, [kl/kg] TDEAD = Dead state temperature, [K] SOFWI = working fluid entropy at open feed water heater inlet, [kJ/kg/K] SOFWO = working fluid entropy at open feed water exit, [kJ/kg/K]. MOFWF = working fluid mass flow rate at the Open feed water extraction, [kg/sec] HOFWF = working fluid enthalpy at Open feed water heater extraction inlet. [kl/kg] SOFWF = working fluid entropy at extraction inlet, [kJ/kg/K] For the SIMPLE OFW HEATER device, the irreversibility is defined as IROFWO: WROFWO—WKOFWO 3405 Where: IROFWO = irreversibility of Open feed water heater process, [kW] WROFWO = reversible work Of open feed water heater process, [kW] WKBRO = work done on the surrounds during Open feed water heater process,.[kW] .aurm ' It' lul' Oil's cl e8 1 lr'l'tlt‘. 2:0 l“ i==ltt' For the SIMPLE OFW HEATER device, the mass balance error is defined as MB = MOFWI + MOFWF — MOFWO 3-106 Where: MB= mass balance error for Open feed water heater device, [kg/sec] MOFWI = working fluid mass flow rate at the open feed water heater inlet. [kg/sec] ‘ MOFWF = working fluid mass flow rate at the open feed water extraction, [kg/sec] MOFWO = working fluid mass flow rate at the Open feed water heater exit, [kg/sec]. For the SIMPLE OFW HEATER device, the energy balance error is defined as 110 EB = MOFWI - HOFWI + MOFWF- HOFWF — 3_107 MOFWO- HOFWO + XOFWO — WK OFWO Where: EB= energy balance error for open feed water heater device, [kW] MOFWI = working fluid mass flow rate at the open feed water heater inlet, [kg/sec] HOFWI = working fluid enthalpy at the Open feed water heater inlet. [kl/kg] MOFWF = working fluid mass flow rate at the Open feed water extraction, [kg/sec] HOFWF = working fluid enthalpy at the Open feed .water extraction, [kl/kg] MOFWO = working fluid mass flow rate at the Open feed water heater exit, [kg/sec]. ‘ HOFW O = working fluid enthalpy at the Open feed water heater exit, [kg/sec]. WKOFWO(I) = work done on the surrounds by the open feed water heater device,.[kW] XOFWO(I) = heat transferred from the surrounds during the Open feed water heater process, [kW]. W A steam trap closed feed water (CFW) heater is a heat transfer device where heat is transferred between two fluid streams at different temperatures. Since the two streams do not mix, the streams can be at different pressures. The steam trap within the device permits the shell side liquid to pass but restricts the flow Of steam from the shell side exit. As a result of the steam trap, the shell side working fluid usually exits the device as a saturated or subcooled liquid. ' The symbolic representation for a- SIMPLE STEAM TRAP CFW device with one drain inlet is shown in Figure 3417. Even though RANKINE 3.0 is capable of modeling upto 10 drain inlets, only one drain inlet is shown in Fig. 3-17. Figure 3-17. Symbol for a SIMPLE STEAM TRAP CFW device Figure 3-18 shows the relevant state and device variables utilized within the RANKINE 3.0 source code. The conservation of mass, 151 law, and 2nd law application to the SIMPLE STEAM TRAP CFW device will utilize the identical state and device variable nomenclature utilized with the RANKINE 3.0 source code. The variable nomenclature utilized by RANKINE 3.0 is defined in Table 2-12. MRDI(1). MEXTI. HDRIO). HEXTI. SDRI(1). SEXTI. ADRI(1) AEXTI MFWO. . MFWI. HFWO. HFWI. SFWO. 3m AFWO AFWI MDRO. HDRO. SDRO. ADRO Figure 3-18. RANKINE 3.0 variables for the SIMPLE STEAM TRAP CFW device The M quill ills; Steam, litre Hi [18‘ Wife: 112 In order to provide the maximum amount of thermodynamic information to the user, the conservation Of mass, the 151- law of thermodynamics, and the 2ll—d— law of thermodynamics are applied to_multiple control volumes within the SIMPLE BOILER device. The first control volume is selected around the heat exchanger shell side volume and the second control volume is selected around the heat exchanger tube side volume. The working fluid pressure drop within the SIMPLE STEAM TRAP CFW device is quantified with a user specified pressure drop or percentage pressure drOp. If a user specified pressure drop is specified for either the feed water or the extraction steam, than the relationships between inlet and exit pressure are defined as PDRO = PEXTI - PLEXT 3- 108 PFWO = PFWI - PLFW 3— 109 Where: PDRO = working fluid pressure at drain exit, [MPa] PEXTI = working fluid pressure at extraction inlet, [MPa] PLEXT = working fluid pressure drop between extraction inlet and drain exit, [MPa] PFWO = working fluid pressure at feed water exit, [MPa] PFWI = working fluid pressure at feed water inlet, [MPa] PLFW = working fluid pressure loss between feed water inlet and exit, [MPa] If a user specified percentage pressure drop is specified for either the feed water or the extraction steam, than the relationships between inlet and exit pressure are defined below PDRO: PEXTI-[l-PPLEXT] 3-110 PFWO=PFWI~[1-PPLFW] 3-111 Where: PDRO = working fluid pressure at drain exit, [MPa] it shall nor pelt. The the. “in empty, If a US! heme: Millet it... Ifaus 113 PEXTI = working fluid pressure at extraction inlet, [MPa] PPLEXT = working fluid percentage pressure drop between extraction inlet and drain exit, [-] PFWO = working fluid pressure at feed water exit, [MPa] PFWI = working fluid pressure at feed water inlet, [MPa] PPLFW = working fluid percentage pressure drop between feed water inlet and exit, {-1 It should be noted that percent pressure losses are based upon percent of inlet pressure, not percent of exit pressure. The thermodynamic performance Of a steam trap closed feed water heater may be defined with two user specified parameters; the terminal temperature difference and the approach temperature difference. If a user specified terminal temperature difference is provided, then the relationship between the extraction inlet saturation temperature and the feed water exit temperature is defined as TD = Tm(@ PEXTI) - TFWO 3-112 Where: TD = terminal temperature difference, [K] Tsat(@PEXTI) = saturation temperature of exuaction inlet pressure, [K] TFWO = working fluid temperature at feed water exit, [K] If a user specified approach temperature difference is provided, then the relationship between the drain exit temperature and the feed water inlet temperature is defined as APPRCH = TDRO - TFWI 3-1 13 Where: APPRCH = approach temperature difference, [K] TDRO = working fluid temperature at drain exit, [K] TFWI = working fluid temperature at feed water inlet, [K] | writ: ll‘.‘lill I l' lul’ :u I(:' Ch lr'rh' Will .' $th 5 side. Wit Wit 114 With a control volume selected around the physical boundaries of the heat exchanger shell side, the steady state steady flow mass conservation principle yields MEXTI + Emma) = MDRO 3414 I Where: MEXTI = working fluid mass flow rate at the extraction inlet, [kg/sec] MDR1(I) = working fluid mass flow rate at drain inlet #1, [kg/sec]. NERO = working fluid mass flow rate at the drain exit, [kg/sec]. With a control volume selected around the physical boundaries of the heat exchanger tube side, the steady state conservation of mass yields MFWI = MFWO 3-115 Where: MFWI = working fluid mass flow rate at the feed water inlet, [kg/sec] MFWO = working fluid mass flow rate at the feed water exit, [kg/sec]. ““1” l l 'E II SIIIBIESIEEMIBEECEID . With a control volume selected around the physical boundaries of the heat exchanger shell side, a steady state steady flow 151 law control volume analysis neglecting the kinetic and potential terms yields XDRO = MEXTI - [HEXTI — HDRO] + ZtMDRun-[HDRun—Hmop 3-116 I Where: XDRO = heat transferred from the heat exchanger tube side during the shell side process, [kW] MEXTI = working fluid mass flow rate at extraction inlet. [kg/sec] HEXTIO = working fluid enthalpy at extraction inlet, [kl/kg] I-IDRO = working fluid enthalpy at drain exit, [kJ/kg]. MDRI(I) = working fluid mass flow rate at drain inlet #1, [kg/sec] HDRI(I) = working fluid enthalpy at drain inlet #1, [kl/kg]. 115 With a control volume selected around the physical boundaries of the heat exchanger tube side, a steady state 151 law control volume analysis neglecting the kinetic and potential terms yields XFWO=MFWO~HFWO—MFWI-HFWI 3-117 Where: XFWO = heat transferred from the heat exchanger tube side during the tube side process, [kW] MFWO = working fluid mass flow rate at feed water exit, [kg/sec] I-IFWO = working fluid enthalpy at feed water exit, [kJ/kg] MFWI = working fluid mass flow rate at feed water inlet, [kg/sec] HFWI = working fluid enthalpy at feed water inlet, [kJ/kg]. Since the SIMPLE STEAM TRAP CFW device does no work, all SIMPLE STEAM TRAP CFW device work terms are zero. These terms are Stated below as WKFWO = 0 3-118 WKDRO = 0 3-1 19 Where: WKFWO = work done on the surrounds during the heat exchanger tube side process , [kW]. WKDRO = work done on the surrounds during the heat exchanger shell side process,. [kW] 310I2 II E I . E II SIMBIESIEEMIBEECEEZD . The working fluid availability at each node denoted in Figure 3-18 is defined as AFWI = HFWI — HDEAD - TDEAD - [SFWI - SDEAD] 3-120 AFWO = HFWO - HDEAD - TDEAD - [SFWO - SDEAD] 3- 121 ADRI(I) = HDRI(I) - HDEAD - TDEAD -[SDRI(I) - SDEAD] 3- 122 116 AEXTI = HEXTI - HDEAD — TDEAD - [SEXTI - SDEAD] 3- 123 ADRO = HDRO — HDEAD - TDEAD - [SDRO - SDEAD] 3- 124 Where: AFWI = working fluid availability at feed water inlet, [kW] I-IFWI = working fluid enthalpy at feed water inlet, [Id/kg] HDEAD=working fluid enthalpy at dead state conditions, [kl/Kg] TDEAD = Dead state temperature, [K] SFWI = working fluid entropy at feed water inlet, [kJ/kg/K] SDEAD = working fluid entropy at dead state conditions, [kl/kg/K] 'AFWO = working fluid availability at feed water exit, [kW] HFWO = working fluid enthalpy at feed water exit [kl/kg] SFWO = working fluid entropy at feed water exit, [kJ/kg/K] ADRI(I) = working fluid availability at drain inlet #1, [kW] I-IDRI(I) = working fluid enthalpy at drain inlet #1, [kl/kg] SDRI(I) = working fluid entropy at drain inlet #1, [kJ/kg/K] AEXTI = working fluid availability at extraction inlet, [kW] HEXTI = working fluid enthalpy at extraction inlet, [kJ/kg] SEX'TI = working fluid entropy at extraction inlet, [kl/kg/K] ADRO = working fluid availability at drain exit, [kW] HDRO = working fluid enthalpy at drain exit, [kJ/kg] SDRO = working fluid entropy at drain exit,[kJ/kg/K] With a control volume selected around the physical boundaries of the heat exchanger shell side, a steady state steady flow 2E4. law control volume analysis neglecting the kinetic and potential terms yields WRDRO: MEJITI-[HEXTI—HDRO-(TFW0+TFWI)- 2 (SEXTI-SDRO)]+ZMDRI(I)-[HDRI(I)— 3-125 I - (SDRI (I ) — SDRO)] HDR0_(TFW0+TFWI) Where: WRDRO = reversible work of Shell side process, [kW] MEXTI = working fluid mass flow rate at the extraction inlet, [kg/sec] W11 slit Wt For def: I}, 117 HEXTI = working fluid enthalpy at extraction inlet, [kJ/kg] HDRO = working fluid enthalpy at drain exit, [kl/kg] TFWO = working fluid temperature at feed water exit, [K] TFWI = working fluid temperature at feed water inlet, [K] SEXTI = working fluid entropy at extraction inlet, [kl/kg/K] SDRO = working fluid entropy at drain exit,[kJ/kg/K] MDRI(I) = working fluid mass flow rate at drain inlet #1, [kg/sec]. HDRI(I) = working fluid enthalpy at drain inlet #1, [Id/kg] SDRI(I) = working fluid entropy at drain inlet #1, [kl/kg/K] With a control volume selected around the physical boundaries of heat exchanger tube side, a steady state 2351 law control volume analysis neglecting the kinetic and potential terms yields WKFWO = MFWO - [HFWI - HFWO - Tm(@ PEXTI) - (SFWI - SFWO)] “26 Where: WRFWO = reversible work of tube side process, [kW] MFWO = working fluid mass flow rate at feed water exit, [kg/sec] I-IFWI = working fluid enthalpy at feed water inlet, [kJ/kg] HFWO = working fluid enthalpy at feed water exit [kl/kg] Tsat(@PEXTI) = saturation temperature of extraction inlet pressure, [K] SFWI = working fluid entropy at feed water inlet, [kl/kg/K] SFWO = working fluid entropy at feed water exit, [kJ/kg/K] For the working fluid traveling within the heat exchanger shell _side, the irreversibility is defined as IRDRO = WRDRO - WKDRO 3-127 Where: IRDRO = irreversibility of heat exchanger shell side process, [kW] WRDRO = reversible work of heat exchanger shell side process, [kW] WKDRO = work done on the surrounds during the heat exchanger shell side process,.[kW] Wm For def ll‘h For def. ll 118 For the working fluid traveling within the heat exchanger tube side, the irreversibility is defined as IRFWO = WRFWO - WKFWO 3—128 Where: IRFWO = irreversibility of heat exchanger tube side process, [kW] WRFWO = reversible work of heat exchanger tube side process, [kW] WKFWO = work done on the surrounds during the heat exchanger tube .side process , [kW]. um I It' In" ‘1 :u {t’ l'r'lr'luxtw‘xrlc t'r lrclx' For the working fluid traveling within heat exchanger shell side, the mass balance error is defined as MB = MEXTI + 2 MDRIU) -MDRO 3- 129 I Where: MB= mass balance error for heat exchanger shell side, [kg/sec] MEXT‘I = working fluid mass flow rate at the extraction inlet, [kg/sec] MDRI(I) = working fluid mass flow rate at drain inlet #1, [kg/sec]. MDRO = working fluid mass flow rate at the drain exit, [kg/sec]. For the working fluid traveling within heat exchanger tube side, the mass balance error is defined as MB = MFWI — MFWO 3-130 Where: MB= mass balance error for heat exchanger tube side, [kg/sec] MFWI = working fluid mass flow rate at feed water inlet, [kg/sec] MFWO = working fluid mass flow rate at feed water exit, [kg/sec] For the working fluid traveling within the heat exchanger shell side, the energy balance error is defined as 0 . EB=MEXTI-HEXTI+2MDRI(I)~HDRI(I)- 3 3 l -l l MDRO - HDRO + XDRO - WKDRO W For Ml 119 Where: EB= energy balance-error for heat exchanger shell side, [kW] MEXTI = working fluid mass flow rate at the extraction inlet, [kg/sec] HEXTI = working fluid enthalpy at extraction inlet, [kl/kg] MDRI(I) = working fluid mass flow rate at drain inlet #1, [kg/sec]. HDRI(1) = working fluid enthalpy at drain inlet #1, [kl/kg] MDRO = working fluid mass flow rate at drain exit, [kJ/kg} HDRO = working fluid enthalpy at drain exit, [kJ/kg] XDRO = heat transferred from the heat exchanger tube side during the shell side process, [kW] WKDRO = work done on the surrounds during the heat exchanger shell Side process,.[kW] For the working fluid traveling within the heat exchanger tube side, the energy balance error is defined as EB=MFWI-I-IFWI-MFWO-HFWO+XFWO-WKFWO 3-132 Where: EB(I)= energy balance error for heat exchanger tube side,[kW] MFWI = working fluid mass flow rate at feed water inlet, [kg/sec] HFWI = working fluid enthalpy at feed water inlet, [kl/kg] MFWO = working fluid mass flow rate at feed water exit, [kg/sec] HFWO = working fluid enthalpy at feed water exit [kl/kg] XFWO = heat transferred from the heat exchanger tube side during the tube side process, [kW] WKFWO: work done on the heat exchanger shell side by the heat exchanger tube side,.[kW] W A moisture separator is a device that removes entrained water vapor from a two phase flow. Usually, the moisture separation is accomplished by forcing the two phase flow through a torturous path and providing surfaces for the collection of condensate. 11c Sill Em SN? l'ariat ”Ollie. 120 The symbolic representation for a SIMPLE MOISTURE SEPARATOR device is shown in Figure 3-19. Separatorlnlet ‘ I Separator Condursate Exit Separator Vapor Exit Figure 3-19. Symbol for a SIMPLE MOISTURE SEPARATOR device Figure 3-20 shows the relevant state and device variables utilized within the RANKINE 3.0 source code. The conservation of mass, 151 law, and 2nd law application to the SIMPLE MOISTURE SEPARATOR device will utilize the identical State and device variable nomenclature utilized with the RANKINE 3.0 source code. The variable nomenclature utilized by RANKINE 3.0 is defined in Table 2-12. MSEPI. HSEPI. SSEPI. ASEPI +0 MDRO. HDRO. SDRO. . ADRO +0 MSEPO. HSEPO. SSEPO. ASEPO the 121 Figure 3—20. RANKINE 3.0 variables for the SIMPLE MOISTURE SEPARATOR device For the SIMPLE MOISTURE SEPARATOR device, the conservation of mass, the 151 law of thermodynamics, and the ZD-d law of thermodynamics are applied with a single control volume selected around the physical boundary of the device. C '1' lul' U. ‘1]: 'il; 0: L‘Att"'l0 lliltt‘ki ill."I. The working fluid pressure drop within the SIMPLE MOISTURE SEPARATOR device is quantified with a user specified pressure drop or percentage pressure drop. If a user specified pressure drop is specified , than the relationships between the inlet pressure, drain pressure and exit pressure are PSEPO: PSEPI-PLSEP V 3-133 PDRO = PSEPI — PLSEP 3-134 Where: PSEPO = working fluid pressure at separator vapor exit, [MPa] PSEPI = working fluid pressure at separator inlet, [MPa] PLSEP = working fluid pressure loss between separator inlet and separator vapor exit, [MPa] PDRO = working fluid pressure at condensate exit, [MPa] It should be noted that pressure drops are identical for both the separator condensate exit and separator vapor exit. If a user specified percentage pressure drop is specified , than the relationships between the inlet pressure, drain pressure and exit pressure are PSEPO = PSEPI - [1 - PPLSEP] ' 3-135 PDRO = PSEPI - [l - PPLSEP] 3-136 122 Where: PSEPO = working fluid pressure at separator vapor exit, [MPa] PSEPI = working fluid pressure at separator inlet, [MPa] PPLBOL = working fluid percentage pressure drop between separator inlet and separator vapor exit, {-1 PDRO = working fluid pressure at condensate exit, [MPa] It should be noted that percent pressure losses are based upon percent Of inlet pressure, not percent Of exit pressure. 0 | C ut.‘ ”We: 110 1"U. u. l: 'ri; Itlr‘ltt' With a control volume selected around the physical boundaries of the SIMPLE MOISTURE SEPARATOR device, the steady state steady flow mass conservation principle yields MSEPI = MSEPO + MDRO 3- 137 Where: MSEPI = working fluid mass flow rate at separator inlet, [kg/sec] MSEPO = working fluid mass flow rate at separator vapor exit, [kg/sec]. MDRO = working fluid mass flow rate at condensate exit, [kg/sec]. ‘1 .1‘.';t= A‘ t '|' NV U. I: 'ei; .ih'ltt' With a control volume selected around the physical boundaries of the SIMPLE MOISTURE SEPARATOR device, a steady state steady flow 151 law control volume analysis neglecting the kinetic and potential terms yields 0 = MSEPI - HSEPI - MSEPO - HSEPO - MDRO - HDRO 3-138 Where: MSEPI = working fluid mass flow rate at separator inlet, [kg/sec] HSEPI = working fluid enthalpy at separator inlet, [kJ/kg] MSEPO = working fluid mass flow rate at separator vapor exit, [kg/sec]. HSEPO = wOrking fluid enthalpy at separator vapor exit, [kJ/kg] 123 MDRO = working fluid mass flow rate at condensate exit, [kg/sec]. HDRO = working fluid enthalpy at condensate exit, [kJ/kg] Since the SIMPLE MOISTURE SEPARATOR device does no work on the surrounds and does not exchange heat with the surrounds, the SIMPLE MOISTURE SEPARATOR device work term and heat transfer terms are zero. These terms are stated below as WKSEPO = 0 3-139 WKDRO = 0 ‘ 3- 140 XSEPO = 0 3-141 XDRO = 0 3-142 Where: WKSEPO = work done on the surrounds by the moisture separator,.[kW] WKDRO = work done on the surrounds by the moisture separator,.[kW] XSEPO = heat transferred from the surrounds during the moisture separator process, [kW]. XDRO = heat transferred from the surrounds timing the moisture separator process, [kW]. ' u. ll: 'ri; Oilr‘lh‘ The working fluid availability at each node denoted in Figure 3-20 is defined as ASEPI = HSEPI - HDEAD - TDEAD - [SSEPI — SDEAD] 3-143 ASEPO = HSEPO - HDEAD — TDEAD ~ [SSEPO — SDEAD] 3-144 ADRO = HDRO - HDEAD — TDEAD - [SDRO - SDEAD] 3- 145 Where: ASEPI = working fluid availability at separator inlet, [kW] For an . 124 HSEPI = working fluid enthalpy at separator inlet, [kl/kg] HDEAD=working fluid enthalpy at dead state conditions, [kl/Kg] TDEAD = Dead state temperature, [K] SSEPI = working fluid entropy at separator inlet, [kJ/kg/K] SDEAD = working fluid entropy at dead state conditions, [kl/kg/K] ASEPO = working fluid availability at separator vapor exit, [kW] HSEPO = working fluid enthalpy at separator vapor exit, [kl/kg] SSEPO = working fluid entropy at separator vapor exit, [kl/kg/K] ADRO = working fluid availability at condensate exit, [kW] HDRO = working fluid enthalpy at condensate exit, [kl/kg] SDRO = working fluid entropy at condensate exit, [kJ/kg/K] For the SIMPLE MOISTURE SEPARATOR device, a steady state steady flow 2nd law control volume analysis neglecting the kinetic and potential terms yields WRSEPO = MSEPO ~ [HSEPI - HSEPO - TDEAD - (SSEPI - SSEPO)] + MDRO . [HSEPI - HDRO - TDEAD - (SSEPI - SDRO)] 3- 146 Where: WRSEPO = reversible work of moisture separator process, [kW] MSEPO = working fluid mass flow rate at separator vapor exit, [kg/sec]. HSEPI = working fluid enthalpy at separator inlet, [kl/kg] HSEPO = working fluid enthalpy at separator vapor exit, [kJ/kg] TDEAD = Dead State temperature, [K] SSEPI = working fluid entropy at separator inlet, [kJ/kg/K] SSEPO = working fluid entropy at separator vapor exit, [kJ/kg/K] MDRO == working fluid mass flow rate at condensate exit, [kg/sec]. HDRO = working fluid enthalpy at condensate exit, [kl/kg] SDRO = working fluid enuopy at condensate exit, [kJ/kg/K] For the SIMPLE MOISTURE SEPARATOR device, the irreversibility is defined as IRSEPO= WRSEPO—WKSEPO 3-147 IRDRO=O 3-148 11th EE’ 125 Where: IRSEPO = irreversibility of moisture separator process, [kW] WRSEPO = reversible work of moisture separator process, [kW] WKSEPO = work done on the surrounds by the moisture separator,.[kW] . O Liam l' lu' u. I: 'ai; Illr'lx'tltxrln l'a Balance For the SIMPLE MOISTURE SEPARATOR device, the mass balance error is defined as MB = MSEPI - MSEPO - MDRO 3- 149 Where: MB= mass balance error for moisture separator device, [kg/sec] MSEPI = working fluid mass flow rate at separator inlet, [kg/sec] MSEPO = working fluid mass flow rate at separator vapor exit, [kg/sec]. MDRO = working fluid mass flow rate at condensate exit, [kg/sec]. For the SIMPLE MOISTURE SEPARATOR device, the energy balance error is defined as EB = MSEPI - HSEPI - MSEPO- HSEPO - MDRO . HDRO + XSEPO + XDRO - WKSEPO - WKDRO 3-150 Where: EB= energy balance error for moisture separator device, [kW] MSEPI = working fluid mass flow rate at separator inlet, [kg/sec] HSEPI = working fluid enthalpy at separator inlet, [kl/kg] MSEPO = working fluid mass flow rate at separator vapor exit, [kg/sec]. HSEPO = working fluid enthalpy at separator vapor exit, [kJ/kg] MDRO = working fluid mass flow rate at condensate exit, [kg/sec]. HDRO = working fluid enthalpy at condensate exit, [kJ/kg] WKSEPO = work done on the surrounds by the moisture separator,.[kW] WKDRO = work done on the surrounds by the moisture separator,.[kW] XSEPO = heat uansferred from the surrounds during the moisture separator process, [kW]. XDRO = heat transferred from the surrounds during the moisture separator process, [kW]. 126 W A reheater is a device which transfers heat from a reheat steam mass stream to a cycle steam mass stream. Usually, the reheat steam enters as a superheated vapor and exits as a saturated liquid and the cycle steam enters as a two phase mixture and exits as a superheated vapor. The symbolic representation for a SIMPLE REHEATER device is shown in Figure 3-21. Cycle Steam Inlet +O Reheat Steam Q Inlet I 1 Reheat Steam +0 O 3"“ Cycle Steam Exit Figure 3-21. Symbol for a SIMPLE REHEATER device Figure 3-22 shows the relevant state and device variables utilized within the RANKINE 3.0 source code. The conservation of mass, 131 law, and 2nd law application to the SIMPLE REHEATER device will utilize the identical State and device variable nomenclature utilized with the RANKINE 3.0 source code. The variable nomenclature utilized by RANKINE 3.0 is defined in Table 2-12. ' 127 MCYLI. HCYLI. SCYLI. ACYLI n... 9 +0 HRHSL SRHSI. ARHSI ‘ MRHSO. | HRHSO. SRHSO. +0 ARHSO MCYLO. HCYID. SCYLO. ACYLO Figure 3-22. RANKINE 3.0 variables for the SIMPLE REHEATER device The conservation of mass, the 131 law, and the 2351 law analysis considers multiple control volumes for the SIMPLE REHEATER device. The first control volume is selected around the cycle steam inlet to exit fluid path, the second control volume is selected around the reheat steam inlet to exit path and, if required, the third control volume is selected around the physical boundaries Of the device. W The thermodynamic performance of the SIMPLE REHEATER device is quantified with three device performance parameters: 1) cycle steam pressure drop or percentage pressure drop, 2) reheat steam pressure drop or percentage pressure drop, 3) terminal temperature difference. If a SIMPLE REHEATER device terminal temperature difference is specified, then the relationship between the reheat steam inlet saturation steam and cycle steam exit temperature is defined below T'D=Tsat(@PRHSI)-TCYLO 3-151 Where: TD = terminal temperature difference, [K] Tsat(@PRHSI) = working fluid saturation temperature at reheat steam 128 inlet pressure, [K] TCYLO = worldng fluid temperature at cycle steam exit, [K] It should be noted that the RANKINE 3.0 program assumes that the reheat steam exit state is a saturated liquid. This assumption, however, can be suppressed. The working fluid pressure drop within the SIMPLE REHEATER device is quantified with a user specified cycle steam pressure drop or cycle steam percentage pressure drop. If a user specified cycle steam pressure drop is specified than the relationships between the cycle steam inlet and exit pressure are defined below PCYLO = PCYU - PLCYL 3-152 Where: PCYLO = working fluid pressure at cycle steam exit, [MPa] PCYLI = working fluid pressure at cycle steam inlet, [MPa] PLCYL = working fluid pressure loss between cycle steam inlet and cycle steam exit, [MPa] If a user specified cycle steam percentage pressure drOp is specified, than the relationships between the cycle steam inlet and exit pressure are defined below PCYLO = PCYLI - [l - PPLCYL] 3- 153 Where: PCYLO = working fluid pressure at cycle steam exit, [MPa] PCYLI = working fluid pressme at cycle steam inlet, [MPa] PPLCYL = working .fluid percentage pressure drop between cycle steam inlet and exit path, [-] It should be noted that cycle steam percent pressure lOsses are based upon percent of inlet pressure, not percent of exit pressure. The working fluid pressure drOp within the SIMPLE REHEATER device is quantified with a user specified reheat steam pressure drop or reheat steam percentage pressure drop. If a user specified reheat steam pressure drop rs specified than the relationships between the reheat steam inlet and exit pressure are defined below 129 PRHSO = PRHSI - PLRHS 3-154 Where: PRHSO = working fluid pressure at reheat steam exit, [MPa] PRHSI = working fluid pressure at reheat steam inlet, [MPa] PLRHS = working fluid pressure loss between reheat steam inlet and reheat steam exit, [MPa] If a user specified reheat steam percentage pressure drop is specified, than the relationships between the reheat steam inlet and exit pressure are defined below PRHSO = PRHSI «[1-PPLRHS] 3- 155 Where: PRHSO = working fluid pressure at reheat steam exit, [MPa] PRHSI = working fluid pressure at reheat steam inlet, [MPa] PPLRHS = working fluid percentage pressure drop between reheat steam inlet and exit path, [-] It should be noted that reheat steam percent pressure losses are based upon percent Of inlet pressure, not percent of exit pressure. 3122“ C I' E II SHEIEBEIIEEIEBD . With a control vOlume selected around the physical boundaries of the cycle steam inlet to exit fluid flow path, the steady state steady flow mass conservation principle yields MCYLI = MCYLO 3-156 Where: MCYLI = working fluid mass flow rate at the cycle steam inlet, [kg/sec] MCYLO = working fluid mass flow rate at the cycle steam exit, [kg/sec]. With a control volume selected around the physical boundaries Of the reheat steam inlet to exit fluid flow path, the steady state conservation Of mass yields MRHSI = MRHSO ' 3-157 130 Where: MRHSI = working fluid mass flow rate at the reheat steam inlet, [kg/sec] MRHSO = working fluid mass flow rate at the reheat steam exit, [kg/sec]. “23]” ! I'E II SIIIEIEBEIIENIEBD . With a control volume selected around the physical boundaries of the cycle steam inlet to exit fluid flow path, a steady State steady flow 151 law control volume analysis neglecting the kinetic and potential terms yields XCYLO = MCYLO - [HCYLO-‘ HCYLI] 3-158 Where: XCYLO = heat transferred from the working fluid in the reheat steam fluid path to the working fluid in the cycle steam inlet to exit fluid path, [kW] MCYLO = working fluid mass flow rate at cycle steam exit, [kg/sec] HCYLO = working fluid enthalpy at cycle steam exit, [kl/kg] HCYLI = working fluid enthalpy at cycle steam inlet, [kJ/kg]. With a control volume selected around the physical boundaries of the reheat steam inlet to exit fluid flow path, a steady state steady flow 151 Law control volume analysis neglecting the kinetic and potential terms yields XRHSO = MRI-ISO- [HRHSO - HRHSI] 3-159 Where: XRHSO = heat transferred from the working fluid in the cycle steam fluid path to the working fluid in the reheat steam inlet to exit fluid path, [kW] MRHSO = working fluid mass flow rate at reheat steam exit, [kg/sec] HRHSO = working fluid enthalpy at reheat steam exit, [kl/kg] HRHSI = working fluid enthalpy at reheat steam inlet, [kl/kg]. Since the SIMPLE REHEATER device does no work on the surrounds, all SIMPLE REHEATER device work terms are zero. These terms are stated below as WKCYLO = 0 3-160 hh 131 WKRHSO = o ' 3-161 Where: ' WKCYLO = work done on the surrounds by the working fluid in the cycle steam inlet to exit process,.[kW] WKRHSO = work done on the surrounds by the working fluid in the reheat steam inlet to exit process, [kW]. ““2 II 1 l 'E II SHIEIEBEIIEIIEBD . The working fluid availability at each node denoted in Figure 3-22 is defined as ACYLI = HCYLI - HDEAD - TDEAD - [SCYLI — SDEAD] 3-162 ACYLO = I-ICYLO - HDEAD — TDEAD - [SCYLO — SDEAD] 3-163 ARHSI = HRHSI — HDEAD — TDEAD - [SRHSI — SDEAD] 3-164 ARHSO = HRHSO - HDEAD - TDEAD :[SRI-IOS — SDEAD] 3-165 Where: ACYLI = working fluid availability at cycle steam inlet, [kW] HCYLI = working fluid enthalpy at cycle steam inlet, [kJ/kg] HDEAD=working fluid enthalpy at dead state conditions, [kl/Kg] TDEAD = Dead state temperatrue, [K] SCYLI = working fluid entropy at cycle steam inlet, [kJ/kg/K] SDEAD = working fluid enuopy at dead state conditions, [kJ/kg/K] ACYLO = working fluid availability at cycle steam exit, [kW] HCYLO = working fluid enthalpy at cycle steam exit, [kl/kg] SCYLO = working fluid entropy at cycle steam exit, [kJ/kg/K] ARHSI = working fluid availability at reheat steam inlet, [kW] HRHSI = working fluid enthalpy at reheat steam inlet, [kl/kg] SRHSI = working fluid entropy at reheat steam inlet, [kJ/kg/K] ARHSO = working fluid availability at reheat steam exit, [kW] HRHSO = working fluid enthalpy at reheat steam exit, [kl/kg] SRHSO = working fluid entropy at reheat steam exit, [kJ/kg/K]. 132 With a control volume selected around the physical boundaries of the cycle steam inlet to exit fluid flow path, a steady state steady flow 2351 Law control volume analysis neglecting the kinetic and potential terms yields WKCYLO = MCYLI - [HCYU - HCYLO— Where: 7 ‘ PRHSI + T PRHSO 3-166 WRCYLO = reversible work of cycle steam inlet to exit process, [kW] MCYLI = working fluid mass flow rate at the cycle steam inlet, [kg/sec] HCYLI = working fluid enthalpy at cycle steam inlet, [kJ/kg] HCYLO = working fluid enthalpy at cycle steam exit, [kl/kg] PRHSI = working fluid pressure at reheat steam inlet, [MPa] PRHSO = working fluid pressure at reheat steam exit, [MPa] SCYLI = working fluid entropy at cycle steam inlet, [kJ/kg/K] SCYLO = working fluid entropy at cycle steam exit, [kJ/kg/K]. With a control volume selected around the physical boundaries of the reheat steam fluid flow path, a steady state 2M1 Law control volume analysis neglecting the kinetic and potential terms yields Where: WRRI-ISO = MRHSI - [HRHSI - HRHSO - 3- 167 (TCYLI :TCYLO) . (SRHSI — SRHSO)] WRRHSO =. reversible work of working fluid in reheat steam inlet to exit . Process. [kW] MRHSI = working fluid mass flow rate at the reheat steam inlet, [kg/sec] HRHSI = working fluid enthalpy at reheat steam inlet, [kl/kg] HRHSO = working fluid enthalpy at reheat steam exit, [kJ/kg] TCYLI = working fluid temperature at cycle steam inlet, [K] TCYLO = working fluid temperature at cycle steam exit, [K] SRHSI = working fluid enuopy at reheat steam inlet, [kJ/kg/K] SRHSO = working fluid entropy at reheat steam exit, [kJ/kg/K]. 133 For the working fluid traveling within the cycle steam inlet to exit fluid flow path, the irreversibility is defined as IRCYLO = WKCYLO — WKCYLO 3-168 Where: IRCYLO = irreversibility of cycle steam inlet to exit process, [kW] WRCYLO = reversible work Of cycle steam inlet to exit process, [kW] WKCYLO = work done on the surrounds by the working fluid in the cycle steam inlet to exit process,.[kW] For the working fluid traveling within the reheat steam fluid flow path, the irreversibility is defined as ‘ - IRRHSO = WRRHSO - WKRHSO 3-169 Where: IRRHSO = irreversibility of reheat Steam inlet to exit process, [kW] WRRHSO = reversible work of working fluid in reheat steam inlet to exit process, [kW]. WKRHSO = work done on the surrounds by the working fluid in the reheat steam inlet to exit process, [kW]. 3181111 _ It' lul’ ’ D ' r t o ; tlr'lst'trt‘xrlo I'I'A -==t~l' For the working fluid traveling within the cycle steam inlet to exit fluid flow path, the mass balance error is defined as MB = MCYLI - MCYLO 3-170 Where: MB= mass balanceerror for cycle steam inlet to exit path, [kg/sec] MCYLI = working fluid mass flow rate at the cycle steam inlet, [kg/sec] MCYLO = working fluid mass flOw rate at the cycle steam exit, [kg/sec]. For the working fluid traveling within the reheat steam inlet to exit fluid flow path, the mass balance error is defined as MB = MRHSI - MRHSO 3-171 Where: 134 MB = mass balance flow rate error for reheat steam inlet to exit path, [kg/sec] MRHSI = working fluid mass flow rate at the reheat steam inlet, [kg/sec] MRHSO = working fluid mass flow rate at the reheat steam exit, [kg/sec]. For the working fluid traveling within the cycle steam inlet to exit fluid flow path, the energy balance error is defined as Where: EB = MCYU * HCYLI - MC YLO * I-ICYLO + XCYLO - WKCYLO 3-172 EB= energy balance error for cycle steam inlet to exit path, [kW] MCYLI = working fluid mass flow rate at the cycle steam inlet, [kg/sec] HCYLI = working fluid enthalpy at cycle steam inlet, [kl/kg] MCYLO = working fluid mass flow rate at the cycle steam exit, [kg/sec]. HCYLO = working fluid enthalpy at cycle steam exit, [kJ/kg] XCYLO = heat transferred from the working fluid in the reheat steam ' fluid path to the working fluid in the cycle steam inlet to exit fluid path, [kW] WKCYLO = work done on the surrounds by the working fluid in the cycle steam inlet to exit process,.[kW] For the working fluid traveling within the reheat steam inlet to exit fluid flow path, the energy balance error is defined as Where: EB = MRI-[SI - HRHSI - MRHSO - HRHSO + XRHSO - WKRHSO 3-173 EB= energy balance error for reheat steam inlet to exit fluid flow process, [kW] . MRHSI = working fluid mass flow rate at the reheat steam inlet, [kg/sec] HRHSI = working fluid enthalpy at reheat steam inlet, [kl/kg] MRHSO = working fluid mass flow rate at the reheat steam exit, [kg/sec]. HRHSO = working fluid enthalpy at reheat steam exit, [kl/kg] XRHSO = heat transferred from the working fluid in the cycle steam fluid path to the working fluid in the reheat steam inlet to exit fluid path, [kW] 135 WKRHSO = work done on the surrounds by the working fluid in the reheat steam inlet to exit process, [kW]. SI'SIJIISIEE Ell' The overall cycle performance is quantified with five parameters: 1) Carnot cycle efficiency, 2) 131 law efficiency, 3) heat rate, 4) 2051 law effectiveness, and 5) 2nd law efficiency. The Carnot cycle efficiency establishes the thermodynamically best obtainable 151 law thermal efficiency for any cycle Operating between two constant temperature reservoirs. Even though the Carnot cycle is very difficult to Operate in reality, the Carnot cycle it is very important since it establishes the maximum obtainable 151 law thermal efficiency for a cycle operating between two constant temperature reservoirs. The Carnot cycle efficiency is defined mathematically as CCEFF =1— "RES 3"“ THRES Where: CCEFF = carnot cycle efficiency. {-1 TLRES = absolute temperature of low temperature reservoir, [K] THRES = absolute temperature of high temperature reservoir, [K]. The 151 law thermal efficiency is defined as the ratio of net work produced by the system divided by the heat supplied to the system. Mathematically, the 151 law thermal efficiency is defined as ' 2 WK + 2 WK — GENML - GENEL FLEFF = “”bi’” ’"m'p 3-175 2X boiler Where: FLEFF = 1st law thermal efficiency, [-] WK = device work, [kW] GENML = generator mechanical losses, [kW] GENEL = generator electrical losses, [kW] 136 X = device heat transfer, [kW]. The system heat rate is defined as the amount Of heat supplied to the cycle (in BTUs) required to produce 1 kWh Of electricity. In reality, the system heat rate is only an algebraic manipulation of the 151 law thermal efficiency calculated in equation 3-175, however, the system heat rate is an important system parameter since it quantifies the amount of heat which must be supplied to the system (and, hence, the cost of producing the heat) required to produce a: fixed amount of electricity (and, hence, the income generated by selling the elecuicity). Mathematically, the heat rate is defined as ‘ HRSYS = 3412 3-176 . FLEFF Where: I-IRSYS = system heat rate, [BTU/kWh] FLEFF = 151 law thermal efficiency, H. The 2nd law effectiveness is defined as the ratio of the system's 151 law efficiency divided by the thermodynamically best obtainable 151 law efficiency for a system operating between the same constant temperature reservoirs. The 2351 law effectiveness is an important system parameter since it quantifies how closely a system approaches the best thermodynamic performance. Mathematically, the 2951 law effectiveness is defined as SLAWE = FLEFF 3-177 CCEFF Where: SLAWE = second law effectiveness, {-1 FLEFF = 151 law thermal efficiency, [-] CCEFF = carnot cycle efficiency, H. The 2114 law efficiency is defined as the ratio Of availability produced by the cycle divided by the availability consumed by the cycle. The 2nd law efficiency is important since it provides "credit" for availability transferred to or from the cycle. Mathematically, the 2119 law efficiency is defined as 137 2Availa‘bility Produced + ZWK _ system turbines SL5" ‘ zAvailability Supplied + zwx + GENML system _ pumps + GENEL + 2 AJQBOL boiler Where: SLEFF = 2nd law efficiency, {-1 WK = device work, [kW] GENML = generator mechanical losses, [kW] GENEL = generator electrical losses, [kW] AJQBOL = adjusted boiler heat, [kW]. It should be noted that AJQBOL is defined by equation 1-7. 3-178 InnCIII' Illifil' Q .. The code testing and verification efforts may be separated into two categories; active testing and passive testing. The active testing represents the efforts Of the author to verify the RANKINE 3.0 program by bench marking against hand calculations, RANKINE 2.4, and the industry equivalent of RAN KINE 3.0, PEPSE version 58H (Performance Evaluation of Blant System Efficiencies by Nuclear Utilities Services (NUS), Idaho Falls, ID, created march 12, 1993). The passive testing efforts represent the hard wired internal checks integrated within the program structure by the author which insure that program calculations are consistent with the physical and thermodynamic constraints imposed on any thermal system. The combination of active and passive testing result in a high level of program creditability. Ill! 1|' 1|' Efl‘ll The active testing efforts may be subdivided into three phases; 1) individual device testing via comparison with hand calculations, 2) complete cycle testing via comparison with hand calculations and RANKINE 2.4, and 3) complete cycle testing via comparison with hand calculations and PEPSE version 581-1. It is the intent of the active testing efforts to insure that RANKINE 3.0 possesses both the flexibility and the creditability to be used as a tool during steam power plant design and Optimization studies. Ill Il"l ID . I l' The individual device testing efforts consists of a series of 11 tests. Each test focuses on one individual device type and is intended to test all aspects associated with that single device including input processing, input checking, thermodynamic calculations and output processing. As an example, consider the individual device test associated with the simple pipe device. For the simple pipe device, six unique sets of information exist which define a well posed device. For this discussion, a well posed device is defined as a device which possesses at least the minimum amount of independent thermodynamic information and performance 138 139 parameters required to 'fix' the thermal performance Of the device. For the simple pipe device, the six unique sets of information are shown in Table 4-1 Table 4—1. Unique sets Of information required to fix a simple pipe device. In order to test the simple pipe device, a RANKINE 3.0 input file was created which modeled six unconnected well posed simple pipe devices each possessing a different set Of user provided information. After the input file was created, RANKINE 3.0 was executed, and the RANKINE 3.0 output file was compared to hand calculations performed by the author. Based on the comparison between the RANKINE 3.0 output file and the hand calculations, the simple pipe device model was verified. For each Of the eleven devices modeled by RANKINE 3.0, a matrix was developed similar to Table 4-1 and RANKINE 3.0 was used to model the thermal performance of each device within the matrices. In order to maximize the effectiveness Of the testing, the some code was consulted to insure that the maximum number of logic paths within the program were tested. The RANKINE 3.0 output file was compared to hand calculations performed by the author and any discrepancies between the RANKINE 3.0 output file and the hand calculations were addressed. After this phase of the code testing, the only discrepancies that existed between the RANKINE 3.0 output files and the hand calculations were attributed to steam table rounding errors in the hand calculation. Additional details associated this phase Of the code testing can be found in Appendix A, B, and C. Appendix A contains a detailed summary associated with the comparison between the RANKINE 3.0 output files and the hand calculations. Appendix B contains a listing Of all RANKINE 3.0 input files used during this phase of the testing and 140 Appendix C contains a listing Of each RANKINE 3.0 output file obtained during the individual device testing phase. . C ‘0 I . 9.. 1'15 lttHIJt 0011' iii ill! :1: tektlkl The second phase of the active code testing consisted of bench marking RANKINE 3.0 to hand calculations performed by the author and RANKINE 2.4. In order to accomplish this objective, five representative RANKINE 2.4 configurations were chosen and were designated as benchmark case #1 through case #5. The five benchmark cases ranged in complexity from the Simple Rankine cycle (case #1) to a co—generation system which employed two reheat legs and four regenerative Open feed water heaters (case #5). The design variations incorporated within the five benchmark cases insured that the RANKINE 3.0 program possessed the flexibility required to model complex steam power systems. ‘ The system layout for benchmark cases #1 to #5 are presented in Figure 4-1 to Figure 4-5 respectively and the input parameters utilized in benchmark cases #1 to #5 are presented in Table 4-2. Using the system layout and the input parameters, input files were created for each benchmark cases and the thermal performance of each benchmark case was evaluated using RANKINE 2.4 and RANKINE 3.0. In addition, a hand calculation was performed by the author which included a first and second law analysis for each device and for the entire system. A detailed comparison between the RANKINE 3.0 output file, RANKINE 2.4 output file and the hand calculation was made and any discrepancies were addressed. A comparison of the figures of merit for each of the five benchmark sequences is presented in Table 43 to Table 4-7. Based on the comparison between the RANKINE 3.0 results, RANKINE 2.4 results and the hand calculations, the flexibility and accuracy of RANKINE 3.0 is verified. Additional details associated this phase of the code testing can be found in Appendix D, E, and F. Appendix D contains a copy of the hand calculations performed by the author applicable to this phase of the code testing. Appendix E contains a listing Of all RANKINE 3.0 input files used during this phase of the' testing and Appendix F contains a listing of each RANKINE 3.0 output file obtained. It should be noted that the RANKINE 141 2.4 input and output files are not include within the appendices since the nodilization scheme employed by RANKINE 2.4 is not consistent with Figures 4-1 to 4-5. a... (_wa ' ...... v'v.. we *0 .... 9? C... a... 1‘4— Figure 4-1. System layout for benchmark case #1 142 1991i? Q... 0:. Figure 4-2. System layout for benchmark case #2 143 99 0+5; Figure 43. System layout for benchmark case #3 144 Figure 44. System layout for benchmark case #4 145 Figure 45. System layout for benchmark case #5 146 Table 4-2. Summary of input parameters for benchmark case #1 to #5 1 47 Table 4-2. (Cont'd) Table 4,3, Figures Of merit comparison for benchmark case #1 2.4 law effectiveness Table 4-4. Figures Of merit comparison for benchmark case #2 2.4 effectiveness 148 Table 4-5. Figures Of merit comparison for benchmark case #3 2.4 Table 4-6. Figures Of merit comparison for benchmark case #4 2.4 law effectiveness Table 4-7. Figures Of merit comparison for benchmark case #5 I49 ‘I 9101 A! 01“:qu 1.310 =~1=Hl =10 Us The third and final phase of the active code testing consisted of bench marking RANKINE 3.0 to hand calculations performed by the author and the industry equivalent of RANKINE 3.0, PEPSE version 58H. In order to accomplish this objective, a representative Pressurized Water Reactor Nuclear Power Station (PWR NPS) was selected and the systems layout and operating conditions were Obtained. The system layout for the representative PWR NPS, designated as benchmark case #6, consists of one high pressure turbine, three low pressure turbines, two 2-Stage moisture separator reheaters, two parallel strings of three high pressure steam trap closed feed water heaters, and three parallel strings Of four low pressure Steam trap closed feed water heaters. For modeling purposes, the three low pressure turbines were treated as a single low pressure turbine and the two 2-stage moisture separator reheaters were treated as a single moisture separator in series with two reheating stages. In addition, the parallel string strings of closed feed water heaters were combined into a Single string 'of seven closed feed water heaters. After all model condensing was completed, the system layout is shown in Figure 4-6. The operating conditions and the device performance parameters Obtained by the author are provided in Table 4-8. Using the system layout, operation conditions, and device performance parameters, a RANKINE 3.0 input file was created and RANKINE 3.0 was executed. Due to the iterative nature of benchmark case #6, RANKINE 2.4 was unable to model this system. Using the converged results Obtained from the RANKINE 3.0 program, a hand calculation was performed which consisted of a first and second law analysis for each device and for the entire system. A figure of merit comparison between the RANKINE 3.0 output file, the hand calculation performed by the author, and PEPSE version 58H results are presented in Table 49. Additional details associated with this phase of the code testing can be found in Appendix G, H, and 1. Appendix G contains a copy of the hand calculations performed by the author applicable to this phase of the code testing. Appendix H contains a listing of all RANKINE 3.0 input files used during this phase of the code testing and Appendix 1 contains a listing of each RANKINE 3.0 output file obtained from each input file. 150 one ®.GCO® 9 0 G 0 afialo 0(‘0 o oo oo o O e on e- 9 com .6 9 0:6 09.5qu o o o e H. o e e c e |o Figure 4-6. System layout for benchmark case #6 151 Table 4—8. Input parameters for benchmark case #6 152 Table 4-8. (Cont'd) 1 53 Table 4-9. Figure of merit comparison for benchmark case #6 law law effectiveness Inspection Of Table 4—9 shows excellent agreement between the RANKINE 3.0 results and the hand calculation and moderate agreement between the RANKINE 3.0 results and PEPSE version .58H results. Each major difference encountered in Table 4-9 is discussed below. ‘ 1) 2) The RANKINE 3.0 reheater terminal temperature difference tolerance is internally set at 10.05 'C. For PEPSI version 58H, this tolerance appears to be approximately i0.005 ‘F. This difference could be reduced by internally adjusting the terminal temperature difference tolerance, however, at the expense of computer computational time. The turbine models employed by RANKINE 3.0 and PEPSE version 58H are significantly different. The RANKINE 3.0 SIMPLE TURBINE device requires a user specified stage group adiabatic efficiency while the PEPSE version 58H turbine device internally calculates the stage group adiabatic efficiency based on the working fluid state and the mass flow rate. In addition, the PEPSE version 58H code accounts for the moisture removal provisions between stage groups and the effects of turbine shaft leakage. In the RANKINE 3.0 SIMPLE TURBINE 154 device, neither is consider. This problem may be addressed with the development of a more sophisticated turbine device and its integration into the existing RANKINE 3.0 structure. 3) The accuracy of the total pump work predicted by PEPSE version 58H is questionable. The PEPSE version 58H results indicated that the electric pump drawing from the condenser possessed an overall adiabatic efficiency of 186%. Based on the authors experience, this error is most likely due to a saturated liquid! compressed liquid discontinuity problem in the computerized steam tables employed by PEPSE version 58H. 4) The turbine driver feed pump is modeled differently in RANKINE 3.0 and PEPSE version 58H. Since RANKINE 3.0 does not possess a "SIMPLE TURBINE DRIVER FEED PUMP" device, the turbine driven feed pump was modeled in the RANKINE 3.0 input file as two unconnected devices; a SIMPLE PUMP and a single stage SIMPLE TURBINE. In order to account for this modeling difference, the total net work to generators for PEPSE version 58H was adjusted and Table 49 presents this adjusted value. This problem may be corrected by developing a "SIMPLE TURBINE DRIVEN FEED PUMP" device and integrating it into the existing RANKINE 3.0 structure. Disspite theses differences, the excellent agreement between the RANKINE 3.0 131 law efficiency and PEPSE version 58H 151 law efficiency increases the overall program creditability and demonstrates the flexibility of the RANKINE 3.0 program. ”"2 . CIII' The passive code testing efforts may be subdivided into two areas; 1) the hard wired checks distributed throughout the program, and 2) the mass and energy balances performed on the various control volumes within the system. It is the intent of the passive code testing to provide an additional level of program creditability and to insure that any untested code logic performs as intended by the author. The hard wired checks distributed though out the program structure are intended to identify problems .during program execution and, when a problem exists, provide a message to the user. These checks are distributed throughout the entire program and, hence, all input files are checked for Consistency and all program results are checked for validity.- Additional information associated with the input file checks may be found in 155 Sections 2.2.0 through 2.2.3 and additional information associated with the checks associated with the internally calculated results may be found in Section 2.3.3. The mass and energy balances performed on each of the various control volumes within the system is intended to identify fundamental program errors not identified by the author during active code testing or by the hard wired checks distributed throughout the program. The mass and energy balances are performed on each device within the system and on the entire system and, hence, a failure of the program to conserve mass or energy within any system will be quickly identified. Additional information associated with the mass and energy balances performed on the various control volumes within the system may be found in Section 2.4.1. 156 157 RANKINE 3.0: A Steam Power Plant Computer Simulation [USERS MANUAL by Wayne A. Thelen and Craig W. Somerton Qboilor steam Boiler “shim )Wm 61:1 Department of Mechanical Engineering Michigan State University East Lansing, Michigan 48824 c Copyright 1995 158 Introduction RANKINE 3.0 is a PC-DOS compatible program capable of modeling a complex, user specified steam power system and providing a basis for optimization of the design and operation of a steam power system. The user specified system may include up to 100 thermal equipment components commonly found in commercial steam power systems such as boilers, turbines, pumps, pipes, junctions, heat loads, condensers, Open feed water heaters, closed feed water heaters, moisture separators, and reheaters. In addition to the system layout, the user also specifies the system operating conditions and equipment performance parameters required for the analysis. The output generated by RANKINE 3.0 summarizes the results of a first and second law analysis for the system operating under the given conditions. It is the intent Of RANKINE 3.0 to provide a fast and detailed thermal analysis which permits innovative steam power system designs to be investigated for the potential of increased system efficiency. It Fil n in The first step required in using RANKINE 3.0 is to sketch the complete system layout that will be modeled. On this sketch, every thermal equipment device should be assigned a device number and every device inlet/exit should be assigned a node number. Due to program limitations, the device numbers and node numbers should begin at l and not exceed 100. The second step is to convert the information on this sketch into a format which may be used by the program. Since RANKINE 3.0 Operates in a batch mode, the information on this sketch must be translated into an input file. The creation of the input file may be accomplished with the DOS editor. The purpose Of the input file is to communicate the system layout, operating conditions, and device performance parameters to the program. All input files contain two types of information; system information and device information. The system information is applicable to the entire system and may be used during the analysis of each device in the system. An example of system information is the system's dead state temperature. The device information consists of a summary Of all known information pertaining to each device within the system including the nodes on the device, all known operating 159 conditions, and all known device performance parameters. Due to the calculation procedure, the order in which the device information appears within the input file is not important, but the information within the input file must represent a well posed system. In the event that a required piece of information is neglected within the input file (such as a pump without a specified adiabatic efficiency), internal checks within the program will identify the error, provide a message tO the user, and stop program execution. In an attempt to maximize the program's user fiiendliness, RANKINE 3.0 was developed with an input processor that recognizes a key phrase library. The input processor reads the input file line by line and searches the first 80 characters of each line for key phrases. In general, two key phrases are required to specify information about the system. The 151 key phrase identifies a location in the system (such as a turbine inlet) and a 21151 key phrase specifies some information about the position (such as the pressure or temperature). By combining 151 and 21151 key phrases, information pertaining to the system of interest can be communicated to the program. In addition, the user can specify units for each operating condition; and, hence, RANKINE 3.0 can account for a variety Of units within an input file. As an example, consider using RANKINE 3.0 to perform a 151 and 2051 law analysis for a non-ideal turbine with 375,0001bm/hr of steam entering the turbine at 850 psig and 860 °F. With a control volume selected around the physical boundaries of the turbine, the turbine is modeled as a thermodynamic control volume with one inlet and 'n' extractions. In this example,.the turbine has three extractions; one at 188 psig, one at 88 psig, and the third at -21 inches HG gauge. In addition, the mass flow rate of extraction #1 is 9.5 kg/sec, the mass flow rate of extraction #2 is 225,0001bm/hr, and all stage groups have an adiabatic efficiency of 91 percent. A diagram of this turbine can be seen in Figure 5-1. Pr=sso psig T1=860 deg F M1=375,000 lbtnl. P4=-21.0" 113 93:33 psig M2=9.5 kg/sec M3=225.000 lbm/hr Figure 5-1. Schematic for single turbine example problem 160 Since this example problem is well posed, the work produced from this system may be calculated. In this example, the 'system' consists of a single turbine. In order to use RANKINE 3.0 to model this system, an input file, as described above, must be created. The general key phrases, 151 key phrases, and 214 key phrases recognized by RANKINE 3.0 are summarized in Tables 5-1, 5-2, and 5-3 respectively. Table 5-1. Summary Of general key phrases not to converge on a a the input deck. information will be written to the output file. stem. followed by a number corresponding to the number nodes temperature temperature 3W 10 SIMPLE STEAM TRAP CFW Indicates that information pertaining to a simple steam trap closed feed water heater 161 , Table 5-1. (cont'd) is it. an... SIMPLE MSOITURE Indicates thatmformation pertainingto a SEPARATOR simple moisture separator device will be specified. SIMPLE REHEATER SIMPLE TURBINE INLET EXTRACTION #_ STAGE GROUP #_ EFFICIENCY END DEVICE DISCHARGE EFFICIENCY END DEVICE EXIT Y“ Per 2114 key phrase PIPE PRESSURE LOSS NO pa 2nd key phrase PRESSURE PIPE PERCENTAGE NO %. PERCENT PRESSURE LOSS PIPE ENTHALPY LOSS NO pa 2nd key PM” ENTHAIPY PIPE PERCENTAGE NO ‘5, PERCENT ENT'HALPY LOSS END DEVICE No None ex ’ SLEN 7"— SIMPLE CONDENSER Per2nd key phrase Nnorleex 162 Table 5-2. (Cont'd) Device Name 151 Ke Phrase 2nd Ke Phrase Units PERCENTAGE— PRESSURE LOSS PRESSURE LOSS PERCENTAGE P hrase PRESSURE LOSS er key p EXTRACTION PERCENTAGE %. PERCENTAGE Per key phrase TEMPERATURE TEMPERATURE Per key phrase TEMPERATURE TEMPERATURE 163 Table 5-2. (Cont'd) SEPARATOR SEPARATOR VAPOR Yes pa 2nd key phrase EXIT SEPARATOR Yes pa 2nd kc phrase CONDENSATE EXIT y SEPARATOR PRESSURE No Per 211:! key phrase 1055 PRESSURE SEPARATOR , No %. PERCENTAGE PERCENTAGE PRESSURE LOSS END DEVICE No None e ted SIMPLE REHEATER CYCLE STEAM INLET Yes Per 2 key phrase REHEAT STEAM EXIT Yes pa- 2nd key phrase REHEAT STEAM EXIT No None expected IS NOT A SATURATED LI UID CONTROLLED BY JUNCTION DEVICE mwAL N0 Per 234 key phrase IEMI 1 ”RE TEMPERATURE DIFFERENCE CYCLE STEAM No pa 2nd pkg.” PRESSURE LOSS PRESkgyURE CYCLE STEAM No %. PERCENTAGE PERCENTAGE PRESSURE REHEAT STEAM No pa 2nd PRESSURE LOSS PRES?! IRME REHEAT STEAM No ‘5. PERCENTAGE PERCENTAGE PRESSURE END DEVICE No None ex Table 5-3. Summary of 2nd key phrases Kc Phrase Number Acceptable UflitS NODE Yes ““ NONE EXPECTED ““ PRESSURE Yes MPA. KPA. PA. PSIA. PSIG, PSID. INCHES HG GAUGE. INCHES HG ABSOLUTE, INCHES . H20 GAUGE. INCHES H20 ABSOLUTE TEMPERATURE Yes DEG c. DEG K, KELVIN. DEG F. DEO R. KELVIN TEMPERATURE Yes DEG C. DEG K. KELVIN. DEG F. DEG R. KELVIN DIFFERENCE ENTHALPY Yes KJ/KG, J/KG. BTU/LEM ENTROPY Yes KJ/KG/K. J/KG/K. BTU/13M!!! 1 64 Table 5-3. (cont'd) Number Acceptable Units tee: tees eeee NONE tttt SUPERHEATED DFfl C, DEG KELVIN. DEG F, DEG R LIQUID. SATURA 2 PHASE MIXTURE. SATURATED VAPOR. SUPERHEATED VAPOR es PERCENT % es NONE FLOW FRACTION Yes PERCENT % For the single turbine example problem, the input file consists of the following statements. NUMBER OF NODES IN THIS SYSTEM IS 4 THE DEAD STATE TEMPERATURE IS 25 DEG c THE DEAD STATE PRESSURE IS 101 KPA THE HIGH TEMPERATURE RESERVOIR IS 860 DEG F THE LOW TEMPERATURE RESERVOIR IS 25 DEG C DEVICE 1 IS A SIMPLE TURBINE THE INLET NODE NUMBER IS 1 EXTRACTION #1 NODE NUMBER IS 2 EXTRACTION #2 NODE NUMBER IS 3 EXTRACTION #3 NODE NUMBER IS 4 INLET TEMPERATURE IS 860 DEG F INLET PRESSURE IS 850 PSIG INLET MASS FLOW RATE IS 375000 LBM/HR EXTRACTION #1 PRESSURE IS 188 PSIG EXTRACTION #1 MASS FLOW RATE IS 9.5 KG/SEC EXTRACTION #2 PRESSURE IS 88 PSIG EXTRACTION #2 MASS FLOW RATE 18 225000 LBM/HR EXTRACTION #3 PRESSURE IS -21.0 INCHES HG GAUGE STAGE GROUP #1 EFFICIENCY IS 91 PERCENT STAGE GROUP #2 EFFICIENCY IS 91 PERCENT STAGE GROUP #3 EFFICIENCY IS 91 PERCENT END DEVICE 165 For clarity, the key phrases have been emphasized with bold typeface. All phrases not emphasized with bold typeface are not key phrases and, hence, are ignored by the program. After the input file has been created and saved, RANKINE 3.0 may be executed by typing the executable file name at the DOS prompt. This command is shown below. a:/> RANK30 During program execution, the program will prompt the user for the input file name, analyze the system with the given operating conditions, and prompt the user for an output file name. An internal check verifies that the output file name is not identical to the input file name. It should be noted that the input filename and output file name may be a maximum Of 12 characters long (including all extensions). The execution Of RANKINE 3.0 generates three types Of data; 1) Node data, 2) Device data, and 3) System data. For any given system, the information associated with each type of data is summarized within the user specified output file. Table 5-4 defines the abbreviations contained within the output file. Table 5-4. Summary of output file abbreviations '— _ Abbrevratrno _ _ chfinlk I e 1 T Temperature De ; C P Pressure MPA L Fluid phase index - l-subcooled liquid 2-two phase mixture 3-superheated vapor 4-saturated liquid S—saturated vapor Enthaljy KI Specific volume . m _ Mass flow rate kg/sec Q Wily _ - S Entropy KJ/k III ; ‘V M A Availability REV WRK The reversible work associated with the device before the node. KJI. KW ACT WRK The actual work associated with KW KW KW the device before the node. IRREV . The irreversibility associated with the device before the node. HEAT X-FER The heat transferred into the device before the node. 166 Table 5-4. (Cont'd) The mass balance error associated _gith the device before the node. Theemngybdmmzenormwafimed with the devcei before the node In addition to providing the results of the thermodynamic analysis, the execution of RANKINE 3.0 also generates a file named ECHO.DAT. The ECHO.DAT file contains a listing of the input file information identified by RANKINE 3.0. By inspecting the ECHO.DAT file, questions associated with the interpretation of an input file may be easily addressed. For the Single turbine example problem, the output generated by RANKINE 3.0 is shown below. RANKINE 3.0: A steam power plant computer simulation Copyright 1994 W.A. Thelen, C.W. Somerton ******************************** NODE DATA ********************************* NODE TIC) P(MPa) L Q 8(KJ/KG/K) H(KJ/KG) V(M‘3/KG) M(KG/S) A(XJ/KG) 1 460.00 5.9619 3 ***** 6.7569 3326.99 .05340 47.2500 1316.75 2 267.38 1.3975 3 ***** 6.8236 2967.67 .17059 9.5000 937.54 3 194.21 .7081 3 ***** 6.8527 2831.16 .29217 28.3500 792.37 4 69.29 . 0302 2 .886 6. 9889 2359. 46 4 . 60281 9. 4000 280. 05 ********************t DEVICE DATA (DEVICE BEFORE NODE) **********t********** NODE REV. WRK ACT . WRK IRREV HEAT X-FER MASS ERROR ENERGY ERROR (KW) (KW) (KW) (KW) (KG/S) , (KW) 1 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 2 17917.62 16977.93 939.69 .00 .000 .000 3 5480.34 5153.16 327.18 .00 .000 .000 4 4815.80 4434.00 381.80 .00 7.000 -.004 *************************tttttt SYSTEM DATA ****t********t*********ttttittti TOTAL MASS FLOW RATE EXITING SYSTEM: 47.2500 RG/SEC TOTAL MASS FLOW RATE ENTERING SYSTEM: 47.2500 KG/SEC TOTAL ENTHALPY FLOW RATE EXITING SYSTEM: 130635.3000 KW TOTAL ENTHALPY FLOW RATE ENTERING SYSTEM: 157200.4000 KW TOTAL HEAT AND WORK ENTERING SYSTEM: . -26565.0900 KW TOTAL BOILER HEAT: .0000 NW TOTAL HEAT LOAD HEAT: .0000 KW TOTAL PIPE ENERGY LOSSES: .0000 KW TURBINE WORK (DEVICE If 1): 26565.0900 KW NET WORK TO GENERATORS: 26565.0900 KW 167 TOTAL PUMP WORK: .0000 KW GENERATOR MECHANICAL LOSSES: - .0000 KW GENERATOR ELECTRICAL LOSSES: .0000 KW NET ELECTRICAL POWER: 26565.0900 KW SYSTEM HEAT RATE: -1.0000 BTU/KW*HR CARNOT CYCLE EFFICIENCY: 59.3330 PERCENT 1$T LAW EFFICIENCY: -100.0000 PERCENT 2ND LAW EFFICIENCY: ' 97.3501 PERCENT 2ND LAW EFFECTIVENESS: -100.0000 PERCENT The procedure utilized to specify any device type within an input file may be interpreted .to be strictly analog to the single turbine example problem. In the event that the system of interest contained several devices, the information required to describe the other devices within the system would proceed the simple ttu'bine device in the input file. Using the DOS editor and the key phrase library provided in Tables 1-3, an input file for any steam system may be created. The only limitation with respect to the system layout is that the system must have less than 100 device, less than 100 nodes, and the system must be well posed. It is recommended that a hard copy of an existing input file be referred to as questions arise associated with input file construction. For the more experienced RANKINE users, it may be easier to modify an existing input file to represent a new system than to construct a new input file from scratch. Wt: RANKINE 3.0 can model eleven different thermal devices commonly found in steam power systems. Each of these thermal devices are modeled by RANKINE 3.0 as thermodynamic control volumes capable of performing as specified within the input file. The performance of each thermal device is calculated with hard wired code logic, which applies the 151 and 21151 law of thermodynamics for a Control volume (neglecting kinetic and potential energy) and the appropriate performance parameters to calculate the performance of each device. The control volume for the thermodynamic analysis is selected around the physical boundaries of each device, and hence, the only information acquired from the analysis is the state of the working fluid as it crosses the boundary of the conuol volume and the net work and/or heat transferred across the boundary of the control volume. 168 RANKINE 3.0 was developed to utilize several different combinations of known information to calculate the thermodynamic performance of each device type. The conditions in which RANKINE 3.0 can perform calculations are based on the standard methods to model each device type. A summary of these methods can be found in reference [1]. The device performance parameters utilized in the thermodynamic analysis depends on the device type. The device performance parameter captures the physics of the device and may be provided to RANKINE 3.0 for the analysis. For example, the physics of a 'pipe device' may be captured with a user specified pressure loss and a user specified enthalpy loss. These two parameters quantify the pressure loss encountered when a viscous fluid (in our case, steam) moves within a pipe and the heat loss (which appears in the form of a steam enthalpy decrease) when a 'hot' pipe interacts thermally with its environment. Each of the eleven thermodynamic devices which can be modeled by RANKINE 3.0 is discussed below. For each device type, the device purpose, common symbol, performance parameters and program limitations are discussed. ngigg; SIMPLE EQILER Purpose: A boiler is a device where heat originating from combustion gasses, a nuclear reactor, or other source is transferred to the working fluid traveling through the boiler. In an ideal boiler, the heat addition occurs as a constant pressm'e processes. Frequently, a boiler will have one or more reheat legs. A boiler with a reheat leg permits the working fluid to reenter the boiler after the working fluid has traveled through a high pressure turbine. Since the performance of a turbine decreases with increasing working fluid moisture, the reheat leg is a practical solution to the excessive moisture problem in turbines. 169 Heat ‘ i Borler Brut . C $ Reheat Leg #1 Inlet Boiler Inlet Performance Parameters: 1) Boiler pressure loss or boiler percentage pressure Symbol: loss. 2) .For each reheat leg, a reheat leg pressure loss or ' reheat leg percentage pressure loss. Program Limitations: 1) Each boiler device may have a maximum of 10 'reheat legs. Comments: 1) Percentage pressure losses are based upon the inlet pressure. W Purpose: A turbine is a device which converts the energy contained within the working fluid into rotating mechanical energy. As the working fluid passes through the turbine, work is done against rotor blades which are attached to a shaft. When the rotating shaft is connected to an electrical generator, electricity is produced. Frequently, a turbine is divided into stage groups. A stage group is defined as a set of stator and rotor blades in which the working fluid undergoes a continuous expansion. Usually, the end of a stage group is indicated by an extraction point. Symbol: Inlet Work =. —> Extraction #1 Extraction #2 Performance Parameters: 1) For each stage group, an adiabatic stage group efficiency. 170 Program Limitations: 1) A simple turbine may have a maximum of 10 extractions. 2) Shaft leakage is not modeled. Purpose: A pump is a device used to increase the pressure of a working fluid. Work is supplied to this device from an external source through a rotating shaft Symbol: Performance Parameters: 1) An adiabatic pump efficiency. Program Limitations: None W Purpose: ' A pipe is a device 'which directs a working fluid from one location to a ' second location. The thermodynamic behavior of a pipe device is a working fluid pressure drop and a working fluid enthalpy decreases. Physically, the pressure drop is a result of a flow restriction within the pipe (such as a valve) or the interaction of a viscous working fluid and the pipe walls. The working fluid enthalpy decrease is a result of a hot working fluid interacting thermally with the pipe surrounds. Exit 9 anlet Symbol: Performance Parameters: 1) Pipe pressure loss or pipe percentage pressure loss. 2) Pipe enthalpy loss or pipe percentage enthalpy loss. Program Limitations: None Comments: 1) Percentage pressure loss and percentage enthalpy loss are based upon the inlet pressure and inlet enthalpy. 171 Purpose: A junction is a device which is used to divide (or connect) a working fluid mass stream into multiple (or one) working fluid mass streams. The thermodynamic state of each mass steam is unaffected by the junction device. Symbol: Inlet at Exit #1 Inlet #2 Exit” Performance Parameters: None Program Limitations: 1) A simple junction device may have a maximum of 10 inlets and 10 exits. O . P Purpose: A condenser is a device where working fluid energy is rejected to a cooling medium such as a lake, a river, or the atmosphere. In an ideal condenser, the working fluid experiences no pressure drop as it travels through the condenser and the fluid exits the condenser as a saturated liquid. Symbol: Inlet #1 Inletn Heat —> Performance Parameters: None Program Limitations: 1) A simple condenser device may have a maximum of 27 inlets. Comments: 1) The condenser exit state is assumed to be a saturated liquid. 172 Purpose: A heat load is a device which transfers heat from the working fluid to the surrounds. Usually, a heat load device is used in the modeling of co- generation power systems. Symbol: ‘ Heat Performance Parameters: None Program Limitations: None Purpose: An open feed water heater device is a mixing chamber in which streams of different energies are mixed to form a stream with an intermediate energy. Ideally, the mixture leaves the open feed water heater as a saturated liquid. It should be noted that since mixing occurs, the mixing of the extracted steam and the feed water is a constant pressure process. Symbol: Extraction Inlet I Feed Water Feed Water Exit ‘ * Inlet Performance Parameters: None Program Limitations: 1) Open feed water heater pressure drops can not be modeled. Comment: 1) The feed water exit state is assumed to be a saturated liquid. (this assumption can be suppressed) n_:-_ 173 W Purpose: A steam trap closed feed water heater is a heat transfer device where heat is transferred between two fluid streams at different temperatures. Since the two streams do not mix, the streams can be at different pressures. The steam trap within the device permits the shell side liquid to pass but restricts the flow of steam from the shell side exit. As a result of the steam trap, the shell side working fluid usually exits the device as a saturated or subcooled liquid. Symbol: Performance Parameters: . 1) 2) 3) 4) Program Limitations: 1) Drain Exit Feed water pressure loss or feed water percentage pressure loss. Extraction pressure loss or extraction percentage pressure loss. Terminal temperature difference. Approach temperature difference. A steam trap closed feed water heater device may have a maximum of 10 drain inlets. Comments: 1) The performance of a steam trap closed feed water heater is defined with two parameters; the terminal temperature difference and the approach temperature difference. The terminal temperature difference is defined as the difference between the extraction inlet saturation temperature and the feed water exit temperature. The approach temperature difference is defined as the difference between the drain exit temperature and the feed water inlet temperature. 2 gyigg; SIMPLE Morsmgg SEPARAIQB Purpose: A moisture separator is a device that removes entrained water vapor from a two phase flow. Usually, the moisture separation is accomplished by 174 forcing the two phase flow through a torturous path and providing surfaces for the collection of condensate. Symbol: Separator Inlet Separator Condensate Exit Separator Vapor Exit ' Performance Parameters: 1) Separator pressure loss or separator percentage pressure loss. Program Limitations: None Comments: 1) Separator percentage pressure loss is based upon the inlet pressru'e. 2) Pressure drops are identical for both the separator condensate exit and separator vapor exit. ' ° PLER E Purpose: A reheater is a device which transfers heat from a reheat steam mass stream to a cycle steam mass stream. Usually, the reheat steam enters as a superheated vapor and exits as a saturated liquid and the cycle steam enters as a two phase mixture and exits as a superheated vapor. Symbol: Cycle Steam Inlet "l-O Reheat Steam 9 Inlet I | Reheat Steam , 6 Exit Cycle Steam Exit 175 Performance Parameters: 1) Terminal temperature difference. 2) . Cycle steam pressure drop or percentage pressure drop. 3) Reheat steam pressure drop .or percentage pressure drop. Program Limitations: None Comments: 1) The reheat steam exit state is assumed to be" saturated liquid. (this assumption can be suppressed) 2) The 'FLOW FRACTION CONTROLLED BY JUNCTION DEVICE NUMBER' statement required for the simple reheater model indicates the junction device number which controls the ratio of mass flow through the cycle steam path to the mass flow through the reheat steam path. The program iterates with this flow fraction until .the user specified terminal temperature difference is achieved. An initial guess for this flow fraction must be provided to the program. 3) The terminal temperature difference for the simple reheater model is defined as (the temperature difference between the reheat steam exit temperature and the cycle steam exit temperature. WW RANKINE 3.0 incorporates a set of computerized steam tables which represent fundamental equation for steam. Even though the state postulate requires two independent intensive properties to fix a thermodynamic state, the information required by RANKINE 3.0 to fix a thermodynamic state is based upon the requirements (or limitations) of the computerized steam tables. Table 5-5 contains a summary of the thermodynamic conditions for which a state is. fixed and all unknown thermodynamic information which may be calculated. 176 Table 5-5. Requirements to fix a thermodynamic state Specific volume WW Subcooled liquid or . Entropy SuErheated vapor Temperature Saturation pessure Quality Specific volume Two phase mixture Enthalpy Entropy Pressure Saturation tempaature Qtality Specific volume Two phase mixture Enthalpy Pressure Temperature Entropy Specific volume Enthalpy Quality Fluid phase index Temperature Specific volume It should be noted that the numerical methods used to calculate the steam table properties introduce considerable error whenever the pressure is greater than the critical pressure. Therefore, the maximum allowable pressure is 22.09 MPa and the maximum allowable temperature is 1300 Deg C. In addition, the computerized steam tables incorporated by RANKINE 3.0 possess a very slight discontinuity between the 2-phase correlation and the compressed liquid and superheated steam correlations. As a result of this discontinuity, RANKINE 3.0 may calculate a working fluid entropy decrease across a device or a negative irreversibility for a device. Since both conditions are physically impossible, RANKINE 3.0 checks each device in the system to insure that neither condition exists and, if necessary, provides a warning message to the user during program execution. Usually, the discontinuity problem may be avoided by not modeling very small device pressure losses when the working fluid is close to the saturated liquid or saturated vaporiine. E I' 'I I' Even though RANKINE 3.0 was developed to be as flexible as possible, the program does contain some limitations. A summary of these limitations are presented below. 1) 2) 3) 4) 5) 6) 7) 3) 9) 10) 11) 177 The system must have less than 100 devices. The system must have less than 100 nodes. A SIMPLE TURBINE device may have a maximum of 10 extractions. A SIMPLE CONDENSER device may have a maximum of 27 inlets. A SIMPLE BOILER device may have a maximum of 10 reheat legs. A SIMPLE JUNCTION device may have a maximum of 10 inlets. and a maximum of 10 exits. , Transients can not be modeled by RANKINE 3.0. Working fluid other than steam can not be modeled by RANKINE 3.0 (such as non condensable gasses). ' RANKINE 3.0 does not provide insight into the physics within the thermodynamic control volumes. The performance characteristics (such as pipe pressure loss or adiabatic stage group efficiency) of each device must be known before the system performance is analyzed. Due to steam table limitations, the maximum allowable pressure is 22.09 MPa and the maximum allowable temperature is 1300 Deg C. W As an example, consider the problem of determining the 151 and 20d law efficiency for a steam power system consisting of one boiler, one turbine, one condenser and one pump. The system layout for this example is shown in Figure 5-2. 178 Tubine W... °°“°' " Qt... _f‘??&0‘ v4. Figure 5-2. Schematic for example problem #1 For this example problem, it will be assumed that: (l) The boiler operates at 20.0 MPa, 600°C and generates 50 kg/sec of steam. (2) The condenser operating pressure is 0.1 MPa. (3) All stage groups and pumps are 75% efficient. (4) No pipe pressure losses or enthalpy losses. (5) No boiler pressure losses. Since this is a well posed problem, obtaining the 151 and 2111 law efficiency is a task ideally suited for RANKINE 3.0. ' In order to use RANKINE 3.0 to model this system, an input file must be created that describes the system layout, operating conditions and performance parameters for example problem #1. Using Tables 5-1, 5-2, and 5—3, the system may be traversed and all information required to specify a well posed problem can be communicated to the program. For example problem #1 , the input file generated by‘RANKINE 3.0 is presented below. TITLE UNE » HIGH TEMPERATURE RESERVOIR: 600.0 DEG C SINH’LE RANKINE CYCLE - EXAMPLE LOW TEMPERATURE RESERVOIR: 25.0 DEG C PROBLEM #1 DEAD STATE TEMPERATURE: 25.0 DEG C END TITLE DEAD STATE PRESSURE: 101 KPA GENERATOR MECHANICAL LOSS 18 0.0 MW NUAJBER OF NODES IS 4 GENERATOR ELECTRICAL LOSS IS 0.0 MW 179 DEVICE #1: SIMPLE TURBINE SUCTION NODE NUMBER IS I INLET NODE NUMBER IS 3 DISCHARGE NODE NUMBER IS 2 EXTRACTION #1 NODE NUMBER IS 4 PUMP EFFICIENCY IS 75 PERCENT STAGE GROUP #1 EFFICIENCY IS 75 % . END DEVICE EXTRACTION #1 PRESSURE 18 0.1 MPA END DEVICE DEVICE #4: SIMPLE BOILER BOILER INLET NODE NUMBER IS 2 DEVICE #2: SIMPLE CONDENSER BOILER EXIT NODE NUMBER IS 3 EXIT NODE NUMBER IS 1 BOILER EXIT PRESSURE IS 20.0 MPA INLET #1 NODE NUMBER IS 4 BOIIER EXIT TEMPERATURE IS 600 DEG C END DEVICE BOILER EXIT MASS FLOW RATE IS 50 KG/SEC BOILER PRESSURE LOSS IS 0.0 MPA DEVICE #3: SIMPLE PUMP END DEVICE The output file for example problem #1 is presented below. RANKINE 3.0: A steam power plant computer simulation Copyright 1994 W.A. Thelen, C.W. Somerton ********************************** TITLE *********************************** SIMPLE RANKINE CYCLE - EXAMPLE PROBLEM #1 ******it************************ NODE DATA ********************************* NODE T(C) P(MPa) L Q S(KJ/KG/K) H(KJ/KG) V(M"3/KG) M(KG/S) A(KJ/KG) 99.63 .1000 4 ***** 1.3020 417.31 .00104 50.0000 33.47 103.52 20.0000 1 ***** 1.3228 448.50 .00105 50.0000 58.45 600.00 20.0000 3 ***** 6.5052 3536.61 .01808 50.0000 1601.44 99.63 .1000 2 .990 7.2962 2651.90 1.67621 50.0000 480.88 bUNH *aaaaaataaaaataaassaa DEVICE DATA (DEVICE BEFORE NODE) **************t****** NODE REV. WRK ACT . WRK IRREV HEAT X-FER MASS ERROR ENERGY ERROR (KW) (KW) (KW) (KW) (KG/S) (“I 1 22370.37 .00 22370.37 -111729.90 .000 -.008 2 -1249.04, -1559.60 310.56 .00 .000 .000 3 71843.58 .00 71843.58 154405.60 .000 .000 4 56028.13 44235.28 11792.86 .00 .000 .000 ****fit*t*******t*******i**i**** SYSTEM DATA *************tit**************** TOTAL MASS FLOW RATE EXITING SYSTEM: .0000 KG/SEC TOTAL MASS FLOW RATE ENTERING SYSTEM: .0000 KG/SEC TOTAL ENTHALPY FLOW RATE EXITING SYSTEM: .0000 KW TOTAL ENTHALPY FLOW RATE ENTERING SYSTEM: .0000 KW TOTAL HEAT AND WORK ENTERING SYSTEM: -.0039 KW BOILER HEAT (DEVICE # 4): 154405.6000 KW TOTAL BOILER HEAT: 154405.6000 KW TOTAL HEAT LOAD HEAT: .0000 KW CONDENSER HEAT (DEVICE # 2): -11-l729.9000 KW TOTAL PIPE ENERGY LOSSES: .0000 KW TURBINE WORK (DEVICE # 1): 44235.2800 KW NET WORK TO GENERATORS: 44235.2800 KW PUMP WORK (DEVICE I 3): -1559.6010 KW 180 TOTAL PUMP WORK: -1559.6010 KW GENERATOR MECHANICAL LOSSES: .0000 KW GENERATOR ELECTRICAL LOSSES: .0000 KW NET ELECTRICAL POWER: 42675.6800 KW SYSTEM HEAT RATE: 12345.0200 BTU/KW*HR CARNOT CYCLE EFFICIENCY: 65.8535 PERCENT IST LAW EFFICIENCY: 27.6387 PERCENT 2ND LAW EFFICIENCY: 42.8466 PERCENT 2ND LAW EFFECTIVENESS: 41 . 9699 PERCENT From this'output file, it can be seen that system's 151 law efficiency is 27.6387 percent and the 7114 law efficiency is 42.8466 percent. As an example, consider the problem of determining the 151 and 2051 law efficiency for a co-generation steam power system consisting of three turbines, two reheat legs, three open feed water heaters, and three heat loads. The system layout for this example is shown in Figure 5-3. For this example problem, it will be assume that (l) The boiler operates at 20.0 MPa, 600°C and generates 50 kg/sec of steam. (2) Both reheat legs raise the temperature of the working fluid to 600°C. (3) Extraction pressures are 15.0, 10.0, 7.5, 5.0, 2.5, 1.0, 0.5, 0.25, and 0.1 MPa. (4) All stage groups and pumps are 75% efficient. (5) The heat load mass flow rates are 1.0, 5.0 and 5.0 kg/sec. (6) No pipe pressure losses or enthalpy losses. (7) No boiler pressure losses. Since this is a well posed problem, obtaining the 131 and 2114 law efficiency is a task ideally suited for RANKINE 3.0. 181 Figure .5-3. Schematic for example problem #2 182 In order to use RANKINE 3.0 to model this system, an input file must be created that describes the system layout, operating conditions and performance parameters for example problem #2. The input file for example problem #2 is presented below. TITLE LINE EXAMPLE PROBLEM #2 END TITTE LINE NUMBER OF NODES: 46 HIGH TEMPERATURE RESERVOIR: 600.0 DEG C LOW TEMPERATURE RESERVOIR: 25.0 DEG C DEAD STATE TEMPERATURE: 25.0 DEG C DEAD STATE PRESSURE: 101 KPA - GENERATOR MECHANICAL LOSS: 0.0 MW GENERATOR ELECTRICAL LOSS: 0.0 MW DEVICE #1: SIMPLE BOILER BOILER INLET NODE NUMBER IS 16 BOILER EXIT NODE NUMBER IS 17 BOILER REL-{EAT LEG #1 INLET NODE NUMBER IS 21 BOILER REHEAT LEG #1 EXIT NODE NUMBER IS 22 BOILER REHEAT LEG #2 INLET NODE NUMBER IS 26 BOILER REHEAT LEG #2 EXIT NODE NUMBER IS 27 BOILER EXIT TEMPERATURE IS 600.0 DEG C BOILER EXIT PRESSURE IS 20 MPA BOILER EXIT MASS FLOW RATE 18 50.0 KG/SEC BOILER REHEAT LEG #1 EXTT TEMPERATURE IS 600.0 DEG C BOILER REL-{EAT LEG #2 EXTT TEMPERATURE IS 600.0 DEG C BOILER PERCENTAGE PRESSURE LOSS IS 0.0 PERCENT REL-{EAT LEG #1 PERCENTAGE PRESSURE LOSS IS 0.0 PERCENT REHEAT LEG #2 PERCENTAGE PRESSURE LOSS 18 0.0 PERCENT END DEVICE DEVICE #2: SIMPLE PIPE INLET NODE NUMBER IS 17 EXIT NODE NUMBER IS 18 PIPE PRESSURE LOSS 18 0.0 MPA PIPE EN'THALPY LOSS IS 0.0 III/KG END DEVICE DEVICE #3: SIMPLE TURBINE INLET NODE NUMBER IS 18 EXTRACTION #1 NODE NUMBER IS 19 EXTRACTION #2 NODE NUMBER IS 20 STAGE GROUP #1 EFFICIENCY IS 75% STAGE GROUP #2 EFFICIENCY IS 75% EXTRACTION #1 PRESSURE IS 15.0 MPA EXTRACTION #2 PRESSURE IS 10.0 MPA EXTRACTION #1 MASS FLOW RATE IS 1.0 KGISEC END DEVICE DEVICE #4: SIMPLE PIPE INLET NODE NUMBER IS 20 EXIT NODE NUMBER IS 21 PIPE PERCENTAGE PRESSURE LOSS IS 0.0 ' PERCENT PIPE PERCENTAGE ENTHALPY LOSS IS 0.0 PERCENT END DEVICE DEVICE #5: SIMPLE PIPE INLET NODE NUMBER IS 22 EXIT NODE NUMBER IS 23 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY IOSS IS 0.0 KJ/KG END DEVICE DEVICE #6: SIMPLE TURBINE INLET NODE NUMBER IS 23 EXTRACTION #1 NODE NUMBER IS 24 EXTRACTION #2 NODE NUMBER IS 25 STAGE GROUP #1 EFFICIENCY IS 75% STAGE GROUP #2 EFFICIENCY IS 75% EXTRACTION #1 PRESSURE IS 7.5 MPA EXTRACTION #2 PRESSURE 18 5.0 MPA EXTRACTION #1 MASS FLOW RATE 18 5.0 KGISEC END DEVICE DEVICE #7: SIMPLE PIPE INLET NODE NUMBER IS 25 EXIT NODE NUMBER IS 26 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 ”MG END DEVICE DEVICE #8: SIMPLE PIPE INLET NODE NUMBER IS 27 EflT NODE NUMBER IS 28 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS 18 0.0 KJ/KG END DEVICE DEVICE #9: SIMPLE TURBINE INLET NODE NUMBER IS 28 EXTRACTION #1 NODE NUMBER IS 29 BCTRACIION #2 NODE NUMBER IS 30 EXTRACTION #3 NODE NUMBER IS 32 EXTRACTION #4 NODE NUMBER IS 34 EXTRACTION #5 NODE NUMBER IS 36 STAGE GROUP #1 EFFICIENCY IS 75% STAGE GROUP #2 EFFICIENCY IS 75% STAGE GROUP #3 EFFICIENCY IS 75% STAGE GROUP #4 EFFICIENCY IS 75% STAGE GROUP #5 EFFICIENCY IS 75% BITRACIION #1 PRESSURE 18 2.5 MPA ECTRACIION #2 PRESSURE IS 1.0 MPA EXTRACTION #3 PRESSURE IS 0.5 MPA EXTRACTION #4 PRESSURE LS 0.25 MPA EXTRACTION #5 PRESSURE TS 0.10 MPA EXTRACTION #1 MASS FLOW RATE IS 5.0 KGISEC END DEVICE DEVICE #10: SIMPLE PIPE INLET NODE NUMBER IS 30 EXIT NODE NUMBER IS 31 PIPE PRESSURE LOSS IS 0 .0 MPA PIPE ENTHALPY LOSS IS 0 .0 ”MG END DEVICE DEVICE #11: SIMPLE PIPE INLET NODE NUMBER IS 32 EXTT' NODE NUMBER IS 33 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 KJIKG END DEVICE DEVICE #12: SIMPLE PIPE INLET NODE NUMBER IS 34 EXIT NODE NUMBER IS 35 PIPE PRESSURE LOSS '18 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 IU/KG END DEVICE DEVICE #13: SIMPLE PIPE INLET NODE NUMBER IS 36 EXT'T‘ NODE NUMBER IS 37 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 IU/KG END DEVICE DEVICE #14: SIMPLE CONDENSER EXIT NODE NUMBER IS 1 INLET #1 NODE NUMBER IS 37 INLET #2 NODE NUMBER IS 44 INLET #3 NODE NUMBER IS 45 INLET #4 NODE NUMBER IS 46 END DEVICE DEVICE #15: SIMPLE PIPE INLET NODE NUMBER IS 1 EXIT NODE NUMBER IS 2 PIPE PRESSURE LOSS IS 0.0 MPA PIPE EN'II-LALPY LOSS IS 0.0 TUIKG END DEVICE DEVICE #16: SIMPLE PUMP SUCTION NODE NUMBER IS 2 DISCHARGE NODE NUMBER IS 3 PUMP EFFICIENCY IS 75% END DEVICE DEVICE #17: SMLE PIPE INLET NODE'NUMBER IS 3 EXIT NODE NUMBER IS 4 PIPE PRESSURE L088 18 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 KJIKG END DEVICE DEVICE #1 8: SIMPLE OFW HEATER FEED WATER INLET NODE NUMBER IS 4 FEED WATER EXIT NODE NUMBER IS 5 EXTRACTION INLET NODE NUMBER IS 35 END DEVICE DEVICE #19: SIMPLE PIPE INLET NODE NUMBER IS 5 EXIT NODE NUMBER IS 6 PIPE PRESSURE LOSS 18 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 KJIKG END DEVICE DEVICE #20: SIMPLE PUMP SUCTION NODE NUMBER IS 6 DISCHARGE NODE NUMBER IS 7 PUMP EFFICIENCY IS 75% END DEVICE DEVICE #21: SIMPLE PIPE INLET NODE NUMBER IS 7 EXIT NODE NUMBER IS 8 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 ”KG END DEVICE DEVICE #22: SIMPLE OFW HEATER FEED WATER INLET NODE NUMBER IS 8 FEED WATER EXIT NODE NUMBER IS 9 EXTRACTION INLET NODE NUMBER IS 33 END DEVICE DEVICE #23: SIMPLE PIPE INLET NODE NUMBER IS 9 EXIT NODE NUMBER IS 10 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 KJIKG END DEVICE DEVICE m: SIMPLE PUMP SUCTION NODE NUMBER IS 10 DISCHARGE NODE NUMBER IS 11 PUMP EFFICIENCY IS 75% END DEVICE DEVICE #25: SIMPLE PIPE INLET NODE NUMBER IS 11 EXIT NODE NUMBER IS 12 PIPE PRESSURE LOSS IS 0 .0 MPA PIPE ENTHALPY TOSS IS 0 .0 KJIKG END DEVICE DEVICE #26: SIMPLE OFW HEATER FEED WATER EXIT NODE NUMBER IS 13 FEED WATER INLET NODE NUMBER IS 12 EXTRACTION INLET NODE NUMBER IS 31 END DEVICE DEVICE #27: SIMPLE PIPE INLET NODE NUMBER IS 13 EXIT NODE NUMBER IS 14 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 KIIKG END DEVICE DEVICE #28: SIMPLE PUMP 184 SUCTION NODE NUMBER IS 14 DISCHARGE NODE NUMBER IS 15 PUMP EFFICIENCY IS 75% END DEVICE DEVICE #29: SIMPLE PIPE INLET NODE NUMBER IS 15 EXIT NODE NUMBER IS 16 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS 18 0.0 KJIKG END DEVICE DEVICE #30: SIMPLE PIPE INLET NODE NUMBER IS 19 EXIT NODE NUMBER IS 38 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 KIIKG END DEVICE . DEVICE #31: SIMPLE HEAT LOAD INLET NODE NUMBER IS 38 EXIT NODE NUMBER IS 39 EXIT TEMPELATURE IS 175.7 DEG C END DEVICE DEVICE #32: SIMPLE PIPE INLET NODE NUMBER IS 39 EXTT NODE NUMBER IS 44 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 KJIKG END DEVICE DEVICE #33: SIMPLE PIPE INLET NODE NUMBER IS 24 EXIT NODE NUMBER IS 40 PIPE PRESSURE LOSS IS 0 .0 MPA For example problem #2, the output file generated by RANKINE 3 .0 13 presented below. PIPE ENTHALPY LOSS IS 0.0 “MG END DEVICE DEVICE #34: SIMPLE HEAT LOAD INLET NODE NUMBER IS 40 EXIT NODE NUMBER IS 41 EXIT TEMPERATURE IS 175.7 DEG C END DEVICE DEVICE #35: SIMPLE PIPE INLET NODE NUMBER IS 41 EXIT NODE NUMBER IS 45 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 KJIKG END DEVICE DEVICE #36: SIMPLE PIPE INLET NODE NUMBER IS 29 EXIT NODE NUMBER IS 42 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 KJIKG END DEVICE DEVICE #37: SIMPLE HEAT LOAD INLET NODE NUMBER IS 42 EXIT NODE NUMBER IS 43 EXIT TEMPERATURE IS 175.7 DEG C END DEVICE DEVICE #38: SIMPLE PIPE INLET NODE NUMBER IS 43 EXIT NODE NUMBER IS 46 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 KJ/KG END DEVICE RANKINE 3.0: A steam power plant: computer simulation Copyright 1994 ILA. Thelen, C.W. Somerton ***************‘k‘kt‘kfifitfit‘ktttitttit TITLE *tit‘ktttt******************t****‘kt'k EXAMPLE PROBLEM #2 *********************i********** NODE DATA *fi******ttt********************** NODE T(C) P(MPa) L Q S(KJ/KG/K) H(KJ/KG) V(M‘3/KGI “(KG/S) A(KJ/KG) 1 99.63 .1000 4 ***** 1.3020 417.31 .00104 43.6475 33.47 2 99.63 .1000 4 ***** 1.3020 417.31 .00104 43.6475 33.47' 3 99.68 .2500 1 ***** 1.3022 417.59 .00104 43.6475 33.70 4 99.68 .2500 1 ***** 1.3022 417.59 .00104 43.6475 33.70 5 127.43 .2500 4 ***** 1.6065 535.09 .00107 45.7481 60.45 6 127.43 .2500 4 ***** 1.6065 535.09 .00107 45.7481 60.45 7 127.52 .5000 1 ***** 1.6069 535.66 .00107 45.7481 60.91 8- 127.52 .5000 1 ***** 1.6069 535.66 .00107 45.7481 60.91 9 151.84 .5000 4 ***** 1.8595 639.79 .00109 47.6790 89.73 10 151.84 .5000 4 ***** 1.8595 639.79 .00109 47.6790 89.73 11 152.05 1.0000 1 ***** 1.8601 640.98 .00109 47.6790 90.71 12 152.05 1.0000 1 ***** 1.8601 640.98 .00109 47.6790 90.71 13 179.87 1.0000 4 ***** 2.1367 762.23 .00113 50.0000 129.52 179.87 185.00 185.00 600.00 600.00 554.33 494.41 494.41 600.00 600.00 557.45 501.09 501.09 600.00 600.00 505.66 395.43 395.43 320.86 320.86 253.64 253.64 175.68. 175.68 554.33 175.70 557.45 175.70 505.66 175.70 175.70 175.70 175.70 1.0000 20.0000 20.0000 20.0000 20.0000 15.0000 10.0000 10.0000 10.0000 10.0000 7.5000 5.0000 5.0000 5.0000 5.0000 2.5000 1.0000 .1.0000 .5000 .5000 .2500 .2500 .1000 .1000 15.0000 .1000 7.5000 .1000 2.5000 .1000 .1000 .1000 .1000 umout»wuuwuwwwwwwwwwwwwwwuwwwwwooh-Ha. 44444 44444 44444 44444 44444 44444 44444 44444 44444 44444 44444 44444 44444 44444 44444 44444 44444 44444 44444 44444 44444 44444 44444 44444 44444 44444 44444 44444 44444 44444 44444 44444 44444 185 2.1367 2.1542 2.1542 6.5052 6.5052 6.5358 6.5799 6.5799 6.8991 6.8991 6.9314 6.9777 6.9777 7.2540 7.2540 7.3367 7.4490 7.4490 7.5329 7.5329 7.6171 7.6171 7.7309 7.7309 6.5358 7.7310 6.9314 7.7310 7.3367 7.7310 7.7310 7.7310 7.7310 762.23 794.40 794.40 3536.61 3536.61 3460.98 3360.38 3360.38 3621.73 3621.73 3541.65 3435.14 3435.14 3662.39 3662.39 3472.55 3253.16 3253.16 3106.73 3106.73 2976.46 2976.46 2827.51 2827.51 3460.98 2827.54 3541.65 2827.54 3472.55 2827.54 2827.54 2827.54 2827.54 .00113 .00113 .00113 .01808 .01808 .02304 .03242 .03242 .03828 .03828 .04878 .06862 .06862 .07860 .07860 .14102 .30442 .30442 .54259 .54259 .96451 .96451 2.05840 2.05840 .02304 2.05849 .04878 2.05849 .14102 2.05849 2.05849 2.05849 2.05849 50.0000 50.0000 50.0000 50.0000 50.0000 1.0000 49.0000 49.0000 49.0000 49.0000 5.0000 44.0000 44.0000 44.0000 44.0000 5.0000 2.3210 2.3210 1.9309 1.9309 2.1007 2.1007 32.6475 32.6475 1.0000 1.0000 5.0000 5.0000 5.0000 5.0000 1.0000 5.0000 5.0000 I 129.52 156.46 156.46 1601.44 1601.44 1516.67 1402.94 1402.94 1569.12 1569.12 1479.39 1359.07 1359.07 1503.96 1503.96 1289.44 1036.57 1036.57 865.14 865.14 709.77 709.77 526.88 526.88 1516.67 526.90 1479.39 526.90 1289.44 526.90 526.90 526.90 526.90 444444444444444444444 DEVICE DATA (DEVICE BEFORE NODE) 444444444444444444444 NODE REV. WRK ACT. WRK IRREV HEAT X-FER MASS ERROR ENERGY ERROR (KW) (KW) (KW) (KW) (KG/S) (KW) 1 21536.46 .00 21536.46 -105199.70 .000 _ .016 2 .00 ~00 .00 ' .00' .000 .000 3 -10.11 -12.63 2.53 .00 .000 .000 4 .00 .00 .00 .00 .000 .001 5 196.52 ' .00 196.52 .00 .000 .000 6 .00 .00 .00 _.00 .000 .000 ‘7 -21.30 -26.17 4.87 .00 .000 .000 8 .00 .00 .00 .00 . .000 .001 9 178.76 .00 178.76 .00 .000 .000 10 .00 .00 .00 .00 .000 .000 11 ~46.72 -56.63 9.91 .00 .000 .000 12 .00 .00 .00 .00 .000 .000 13 254.86 .00 254.86 .00 .000 .002 14 .00 .00 .00 .00 .000 .002 15 -1346.88 -1608.31 261.43 .00 .000 .002 16 .00 .00 .00 .00 .000 .000 17 52840.78 .00 52840.78 137110.60 .000 .000 18 .00 .00 .00 .00 .000 .000 19 4238.50 3781.70 456.80 .00 .000 .000 20 5572.79 4929.13 643.66 .00 .000 .005 21 .00 .00 .00 .00 .000 .006 22 850.56 .00 850.56 12806.20 ..000 -.006 23 ‘ .01 .00 .01 .00 .000 .005 24 4396.73 3924.03 472.70 .00 .000 .000 25 .5294.03 4686.43 607.60 .00 .000 .007 186 26 .00 _.00 .00 .00 .000 .001 27 613.13 .00 613.13 9998.87 .000 .001 28 .01 .00 .01 .00 .000 .005 29 9438.87 8352.90 1085.97 .00 .000 .000 30 9861.99 8556.09 1305.90 .00 .000 .000 31 .00 .00 .00 .00 .000 .000 32 6287.99 5370.97 917.02 .00 .000 .000 33 .00 .00 .00 .00 .000 .000 34 5398.73 4526.77 871.96 .00 .000 .000 35 .00 .00 .00 .00" .000 .000 36 5970.83 4862.75 1108.08 .00 .000 .000 37 .00 .00 .00 .00 .000 .002 38 .00 .00 .00 .00 .000 .000 39 989.77 .00 989.77 -633.43 .000 .000 40 .00 .00 .00 .00 .000 .000 41 4762.47 .00 4762.47. -3570.52 - .000 .000 42 .00 .00 .00 .00 .000 .000 43 3812.74 .00 3812.74 -3225.02 .000 .000 44 .00 .00 .00 .00 . .000 .000 45 .00 .00 .00 .00 .000 .000 46 .00 .00 .00 .00 .000 .000 ******************************* SYSTEM DATA it*ti’tfiii’ii‘k‘ki’*fi**************** .0000 KG/SEC .0000 KG/SEC .0000 TOTAL MASS FLOW RATE EXITING SYSTEM: TOTAL MASS FLOW RATE ENTERING SYSTEM: TOTAL ENTHALPY FLOW RATE EXITING SYSTEM: TOTAL ENTHALPY FLOW RATE ENTERING SYSTEM: .0000 TOTAL HEAT AND WORK ENTERING SYSTEM: -.0039 BOILER HEAT (DEVICE 4 1): .159915.7000 TOTAL BOILER HEAT: 159915.7000 -633.4307 -3570.5250 -3225.0180 -7428.9740 -105199.7000 .0000 HEAT LOAD HEAT (DEVICE # 31): HEAT LOAD HEAT (DEVICE 4 34):. HEAT LOAD HEAT (DEVICE I 37): TOTAL HEAT LOAD HEAT: ‘ CONDENSER HEAT (DEVICE # 14): TOTAL PIPE ENERGY LOSSES: TURBINE WORK (DEVICE 4 3) : TURBINE WORK (DEVICE # 6): TURBINE WORK (DEVICE # 9): NET WORK TO GENERATORS: 8610.4610 31669.4800 48990.7800 -12.6342 '-26.1689 -56.6334 -1608.3100 -1703.7460 .0000 .0000 47287.0400 KW KW KW KW KW KW KW KW KW KW KW .8710.8320 KW KW KW KW PUMP WORK (DEVICE 4 16): KW PUMP WORK (DEVICE 9 20): KW PUMP WCEK:(DEVICE 4 24): KW PUMP WORK (DEVICE 4 28): KW TOTAI.INLMP WORK: KW GENERATOR MECHANICAL LOSSES: KW GENERATOR ELECTRICAL LOSSES: KW NET'EUULUTRICAL POWER: KW 11538.7300 BTU/KW*HR 65.8535 PERCENT 29.5700 PERCENT 57.0444 PERCENT 44.9027 PERCENT SYSUTTIIUEAT RATE: CARNOT CYCLE EFFICIENCY: IST LAW EFFICIENCY: 2ND LAW EFFICIENCY: 2ND LAW EFFECTIVENESS: From this- output file, it can be seen that the 131 law efficiency is 29.5700 percent and the 211d law efficiency is 57.0444 percent. 187 W As an example, consider the problem Of determining the 151 and 2nd law efficiency for a typical Pressurized Water Reactor nuclear power station. A typical system layout consists of one high pressure turbine, three low pressure turbines, two 2-stage moisture separator reheaters, two parallel strings Of three high pressure steam trap closed feed water heaters, and three parallel strings Of four low pressure steam trap closed feed water heaters. For modeling purposes, the three low pressure turbines can be treated as a single low pressure turbine and the two 2-stage moisture separator reheaters can be treated as one moisture separator in series with two reheating stages. In addition the parallel strings Of closed feed water heaters can be combined into a single string Of seven feed water heaters. After all model condensing has been completed, the system layout is shown in Figure 5-4. The Operating conditions and device performance parameters are provided in Table 5-6 below. 188 Table 5-6: Data for example problem #3 189 Table 5-6. (Cont'd) Since this is a well posed problem, Obtaining the 151 and 2951 law efficiency is a task ideally suited for RANKINE 3.0. The iterative nature Of this problem makes this type Of problem exceptionally difficult (if not impossible) without a computer program such as RANKINE 3.0. ' as... OI 190 '@C‘:)l__q 0‘. ®-.0WM...0® MWGOOM‘0QO loam, O..® @: G 00 0 0 OO O . OO _ a. 4.6 n .56 «2.! L . 2 .G Iv.@_ 1.". G Figure 5-4. Schematic for example problem #3 In order to use RANKINE 3.0 to model this system, an input file must be created which describes the system layout, Operating conditions and performance parameters to the program. For example problem #3, the input file is presented below. TITLE LINE EXAMPLE PROBLEM #3 END TITLE LINE NUMBER OF NODES IS 71 HIGH TEMPERATURE RESERVOIR: 543.4 DEG F LOW TEMPERATURE RESERVOIR: 55.0 DEG F DEAD STATE TEMPERATURE: 75.0 DEG F DEAD STATE PRESSURE: 14.7 PSIA GENERATOR MECHANICAL LOSS: 5725 KW GENERATOR ELFLTRICAL LOSS: 15150 KW DEVICE #1: SIMPLE BOILER BOILER INLET NODE NUMBER IS 65 BOILER EXIT NODE NUMBER IS 1 BOILER EXI'T TEMPERATURE IS 543.4 DEG F BOILER EXIT PRESSURE IS 990 PSIA BOILER EXTT MASS FLOW RATE IS 15913429 IBM/HR BOILER PRESSURE LOSS IS 138.2 PSID END DEVICE DEVICE #2: SIMPLE JUNCTION INLET #1 NODE NUMBER IS 1 EXIT #1 NODE NUMBER IS 2 HOT #2 NODE NUMBER IS 3 EXIT #1 FLOW FRACTION IS 94 PERCENT END DEVICE DEVICE #3: SIMPLE TURBINE INLET NODE NUMBER IS 2 EXTRACTION #1 NODE NUMBER IS 4 EXTRACTION #1 PRESSURE IS 431.3 PSIA STAGE GROUP #1 EFFICIENCY IS 81 % END DEVICE DEVICE #4: SIMPLE JUNCTION INLET #1 NODE NUMBER IS 4 EXIT #1 NODE NUMBER IS 6 ELIT #2 NODE NUMBER IS 5 EXIT #1 FLOW FRACTION IS 91 PERCENT END DEVICE DEVICE #5: SIMPLE TURBINE INLET NODE NUMBER IS 6 EXTRACTION #1 NODE NUMBER IS 10 EXTRACTION #2 NODE NUMBER IS 11' STAGE GROUP #1 EFFICIENCY IS 84 ‘5 STAGE GROUP #2 EFFICIENCY IS 83 % EXTRACTION #1 PRESSURE IS 293 PSIA EXTRACTION #2 PRESSURE IS 182 PSIA END DEVICE DEVICE #6: SIMPLE JUNCTION INLET #1 NODE NUMBER IS 11 EXIT #1 NODE NUMBER IS 12 EXIT #2 NODE NUMBER IS 13 END DEVICE DEVICE #7: SIMPLE MOISTURE SEPARATOR SEPARATOR INLET NODE NUMBER IS 13 SEPARATOR VAPOR EXIT NODE NUMBER IS 15 SEPARATOR CONDENSATE EXIT NODE NUMBER IS 14 SEPARATOR PRESSURE LOSS IS 5.4 PSID END DEVICE DEVICE #8: SIMPLE JUNCTION INLET #1 NODE NUMBER IS 7 EXIT #1 NODE NUMBER IS 9 EXIT #2 NODE NUMBER IS 8 END DEVICE DEVICE #9: SIMPLE PIPE INLET N ODE NUMBER IS 9 EXIT NODE NUMBER IS 62 PIPE PRESSURE LOSS 18 12.0 PSID PIPE ENTHALPY LOSS 18 0.0 BTU/LEM END DEVICE DEVICE #10: SIMPLE REHEATER CYCLE STEAM INLETNODE NUMBER ISIS CYCLE STEAM EXIT NODE NUMBER IS 17 REHEAT STEAM INLET NODE NUMBER IS 8 REHEAT STEAM EXIT NODE NUMBER IS 16 FLOW FRACTION CONTROLLED BY JUNCTION DEVICE NUMBER 4 TERMINAL TEMPERATURE DIFFERENCE IS 25.0 DEG F CYCLE STEAM PRESSURE LOSS IS 2.6 PSID REHEAT STEAM PRESSURE LOSS IS 4.3 PSID END DEVICE DEVICE #11: SIMPLE REHEATER CYCLE STEAM INLET NODE NUMBER Is 17 CYCLE STEAM EXIT NODE NUMBER IS 19 REIIEAT STEAM INLET NODE NUMBER IS 3 REHEAT STEAM Eer NODE NUMBER Is 18 FLOW FRACTION CONTROLLED BY JUNCTION DEVICE NUMBER 2 TERMINAL TEMPERATURE DIFFERENCE rs 25.0 DEGF ' CYCLE STEAM PRESSURE Loss 15 2.6 PSID RBIIEAT STEAM PRESSURE LOSS IS 10.0 PSID END DEVICE DEVICE #12: SIMPLE PIPE INLET NODE NUMBER IS 10 EXIT NODE NUMBER IS 57 PIPE PRESSURE LOSS 18 9.0 PSID PIPE ENTHALPY LOSS IS 0.0 BTU/IBM END DEVICE DEVICE #13: SIMPLE PIPE INLET NODE NUMBER IS 12 EXIT NODE NUMBER IS 53 PIPE PRESSURE LOSS LS 5.4 PSID PIPE ENTHALPY LOSS IS 0.0 BTU/LEM END DEVICE DEVICE #14: SIMPLE PIPE INLET NODE NUMBER IS 16 EXIT NODE NUMBER IS 54 PIPE ENTHALPY LOSS IS 0.0 BTU/LEM END DEVICE DEVICE #15: SIMPLE PIPE INLET NODE NUMBER IS 18 EXIT NODE NUMBER IS 61 PIPE ENTHALPY LOSS IS 0.0 BTU/LEM END DEVICE DEVICE #16: SIMPLE PIPE INLET NODE NUMBER IS 19 EXIT NODE NUMBER IS 20 PIPE PRESSURE LOSS IS 0.0 PSID PIPE ENTHALPY LOSS LS 0.0 BTU/LEM END DEVICE DEVICE #17: SIMPLE JUNCTION INLET #1 NODE NUMBER IS 20 EXIT #1 NODE NUMBER IS 21 EXIT #2 NODE NUMBER IS 22 EXTT #2 MASS FLOW RATE IS 198275 LEM/HR END DEVICE DEVICE #18: SIMPLE TURBINE INLET NODE NUMBER IS 21 EXTRACTION #1 NODE NUMBER IS 3 EXTRACTION #2 NODE NUMBER IS 24 EXTRACTION #3 NODE NUMBER IS 25 EXTRACTION #4 NODE NUMBER IS 26 EXTRACTION #5 NODE NUMBER IS 27 EXTRACTION #6 NODE NUMBER IS 28 STAGE GROUP #1 EFFICIENCY IS 91.5 % STAGE GROUP #2 EFFICIENCY IS 91.0 % STAGE GROUP #3 EFFICIENCY IS 91.0 % STAGE GROUP #4 EFFICIENCY 18 87.8 % STAGE GROUP #5 EFFICIENCY IS 86.7 % STAGE GROUP #6 EFFICIENCY IS 70.0 % EXTRACTION #1 PRESSURE 18 89.4 PSIA EXTRACTION #2 PRESSURE IS 41.3 PSIA EXTRACTION #3 PRESSURE IS 17.1 PSIA EXTRACTION #4 PRESSURE 18 10.7 PSIA EXTRACTION #5 PRESSURE IS 6.0 PSIA EXTRACTION #5 MASS FLOW RATE IS 158865 LEM/HR EXTRACTION #6 PRESSURE IS 1.7 PSIA END DEVICE DEVICE #19: SIMPLE PIPE INLET NODE NUMBER IS 22 EXIT NODE NUMBER IS 29 PIPE PRESSURE LOSS 18 0.0 PSID PIPE ENTHALPY LOSS IS 0.0 BTU/LEM END DEVICE ' 192 DEVICE #20: SIMPLE TURBINE INLET NODE NUMBER IS 29 EXTRACTION #1 NODE NUMBER IS 30 STAGE GROUP #1 EFFICIENCY IS 78.0 ‘79 END DEVICE DEVICE #21: SIMPLE PIPE INLET NODE NUMBER IS 23 EXIT NODE NUMBER IS 46 PIPE PRESSURE LOSS IS 2.7 PSID PIPE ENTHALPY LOSS IS 0.0 BTU/LEM END DEVICE DEVICE #22: SIMPLE PIPE INLET NODE NUMBER IS 24 EXIT NODE NUMBER IS 43 PIPE PRESSURE LOSS IS 1.3 PSID PIPE ENTHALPY LOSS IS 0.0 BTU/LEM END DEVICE DEVICE #23: SIMPLE PIPE INLET NODE NUMBER IS 25 EXTI‘ NODE NUMBER IS 40 PIPE PRESSURE IOSS IS 0.5 PSID PIPE ENTHALPY LOSS IS 0.0 BTU/IBM END DEVICE DEVICE #24: SIMPLE PIPE INLET NODE NUMBER IS 26 BOT NODE NUMBER IS 37 PIPE ENTHALPY LOSS IS 0.0 BTU/LEM END DEVICE DEVICE #25: SIMPLE PIPE INLET NODE NUMBER IS 27 EXIT NODE NUMBER IS 36 PIPE PRESSURE LOSS IS 0.2 PSID PIPE ENTHALPY IOSS IS 0.0 BTU/LEM END DEVICE DEVICE #26: SIMPLE PIPE INLET NODE NUMBER IS 28 EXIT NODE NUMBER IS 31 PIPE PRESSURE LOSS IS 0.0 PSID PIPE ENTHALPY LOSS IS 0.0 BTU/IBM END DEVICE DEVICE #27: SIMPLE PIPE INLET NODE NUMBER IS 30 EXIT NODE NUMBER IS 32 PIPE PRESSURE LOSS IS 0.0 PSID PIPE ENTHALPY LOSS IS 0.0 BTU/LEM END DEVICE DEVICE #28: SIMPLE CONDENSER EXIT NODE NUMBER IS 34 INLET #1 NODE NUMBER IS 31 INLET #2 NODE NUMBER IS 32 INLET #3 NODE NUMBER IS 33 END DEVICE DEVICE #29: SIMPLE PUMP SUCTION NODE NUMBER IS 34 193 DISCHARGE NODE NUMBER IS 35 DISCHARGE PRESSURE IS 540 PSIA PUMP EFFICIENCY IS 95.0 PERCENT END DEVICE DEVICE #30: SIMPLE PIPE IITLET NODE NUMBER IS 39 EXIT NODE NUMBER IS 33 PIPE ENTHALPY LOSS IS 0.0 BTU/LEM EITD DEVICE DEVICE #31: SIMPLE STEAM TRAP CFW FEED WATER INLET NODE NUMBER IS 35 FEED WATER EXIT NODE NUMBER IS 38 EXTRACTION INLET NODE NUMBER IS 36 DRAIN INLET #1 NODE NUMBER IS 37 DRAIIT LITLET #2 NODE NUMBER IS 70 DRAIN EXIT NODE NUMBER IS 39 EXTRACTION PRESSURE LOSS IS 0.0 PSID FEED WATER PRESSURE LOSS IS 0.0 PSID TERMINAL TEMPERATURE DIFFERENCE 15 5.0 DEG F APPROACH TEMPERATURE DIFFERENCE IS 10.0 DEG F END DEVICE DEVICE #32: SIMPLE STEAM TRAP CFW FEED WATER INLET NODE NUMBER‘ IS 38 FEED WATER EXIT NODE NUMBER IS 41 EXTRACTION INLET NODE NUMBER IS 40 DRAIN INLET #1 NODE NUMBER IS 69 DRAIN EXIT NODE NUMBER IS 42 EXTRACTION PRESSURE LOSS IS 0.0 PSID FEED WATER PRESSURE LOSS IS 0.0 PSID TERMINAL TEMPERATURE DIFFERENCE IS 5.0 DEG F APPROACH TEMPERATURE DIFFERENCE IS 10.0 DEG F END DEVICE DEVICE #33: SIMPLE STEAM TRAP CFW FEED WATER INLET NODE NUMBER IS 41 FEED WATER EXIT NODE NUMBER IS 44 EXTRACTION INLET NODE NUMBER IS 43 DRAIN INLET #1 NODE NUMBER IS 68 DRAIN EXIT NODE NUMBER IS 45 EXTRACTION PRESSURE LOSS IS 0.0 PSID FEED WATER PRESSURE LOSS IS 0.0 PSID TERMINAL TEMPERATURE DIFFERENCE IS 5.0 DEG F APPROACH TEMPERATURE DIFFERENCE IS 10.0 DEG F END DEVICE DEVICE #34: SIMPLE STEAM TRAP CFW FEED WATER IITLET NODE NUMBER IS 44 FEED WATER EXIT NODE NUMBER IS 47 EXTRACTION INLET NODE NUMBER IS 46 DRAIIT EXIT NODE NUMBER IS 48 EXTRACTION PRESSURE LOSS IS 0.0 PSID FEED WATER PRESSURE LOSS IS 0.0 PSID APPROACH TEMPERATURE DIFFEREITCE IS 10.0 DEG F END DEVICE DEVICE #35: SIMPLE OFW HEATER FEED WATER EXIT NODE NUMBER IS 52 ETTRACTION INLET NODE NUMBER IS 49 FEED WATER INLET NODE NUMBER IS 47 FEED WATER EXIT IS NOT SATURATED END DEVICE DEVICE #36: SIMPLE PUMP SUCTION NODE NUMBER IS 51 DISCHARGE NODE NUMBER IS 50 PUMP EFFICIENCY IS 95.0 PERCENT END DEVICE DEVICE #37: SIMPLE OFW HEATER FEED WATER EXIT NODE NUMBER IS 51 EXTRACTION INLET NODE NUMBER IS 71 FEED WATER INLET NODE NUMBER IS 14 FEED WATER BITT IS NOT SATURATED END DEVICE DEVICE #38: SIMPLE STEAM TRAP CFW FEED WATER INLET NODE NUMBER IS 52 FEED WATER EXIT NODE NUMBER IS 55 ECTRACIION INLET NODE NUMBER IS 53 DRAIN INLET #l NODE NUMBER IS 54 DRAIN INLET #2 NODE NUMBER IS 67 DRAIN EXIT NODE NUMBER IS 56 DRAIN EXIT FLUID PHASE IS A SATURATED LIQUID DRAIN EXIT QUALITY 18 0.0 PERCENT EXTRACTION PRESSURE LOSS IS 0.0 PSID FEED WATER PRESSURE LOSS IS 0.0 PSID TERMINAL TEMPERATURE DIFFERENCE IS 5.0 DEG F APPROACH TEMPERATURE DIFFERENCE IS 39.593 DEG F END DEVICE DEVICE #39: SIMPLE STEAM TRAP CFW FEED WATER INLET NODE NUMBER IS 55 FEED WATER EXIT NODE NUMBER IS 58 EXTRACTION INLET NODE NUMBER IS 57 DRAIN LITLET #1 NODE NUMBER IS 66 DRAIN EXIT NODE NUMBER IS 59 EXTRACTION PRESSURE IOSS IS 0.0 PSID FEED WATER PRESSURE LOSS IS 0.0 PSID TERMINAL TEMPERATURE DIFFERENCE IS 5.0 DEG F APPROACH TEMPERATURE DIFFERENCE IS 10.0 DEG F END DEVICE DEVICE #40: SIMPLE PUMP SUCTION NODE NUMBER IS 58 DISCHARGE NODE NUMBER IS 60 PUMP EFFICIENCY IS 65.0 % END DEVICE DEVICE #41: SIMPLE STEAM TRAP CFW FEED WATER INLET NODE NUMBER IS 60 FEED WATER EXIT NODE NUMBER IS 63 EXTRACTION INLET NODE NUMBER IS 61 DRAIN IITLET #1 NODE NUMBER IS 62 DRAIN EXIT NODE NUMBER IS 64 EXTRACTION PRESSURE LOSS IS 0.0 PSID FEED WATER PRESSURE LOSS IS 0.0 PSID TERMINAL TEMPERATURE DIFFERENCE IS 5.0 DEG F 194 APPROACH TEMPERATURE DIFFERENCE IS 10.0 DEG F ‘ END DEVICE DEVICE #42: SIMPLE PIPE INLET NODE NUMBER IS 63 ' EXIT NODE NUMBER IS 65 PIPE PRESSURE LOSS IS 0.0 PSID PIPE ENTHALPY L088 18 0.0 BTU/LEM END DEVICE . DEVICE #43: SIMPLE PIPE INLET NODE NUMBER IS 5 EXIT NODE NUMBER IS 7 PIPE PRESSURE LOSS IS 1.0 PSID PIPE ENTHALPY IOSS IS 0.0 BTU/LEM END DEVICE DEVICE #44: SIMPLE PIPE INLET NODE NUMBER IS 64 EXIT NODE NUMBER IS 66 PIPE ENTHALPYLOSS IS 0.0 BTU/LBM END DEVICE DEVICE #45: SIMPLE PIPE INLET NODE NUMBER IS 59 EXIT NODE NUMBER IS 67 PIPE ENTHALPY LOSS IS 0.0 BTU/LEM END DEVICE DEVICE #46: SIMPLE PIPE INLET NODE NUMBER IS 50 EXIT NODE NUMBER IS 49 PIPE PRESSURE LOSS IS 0.0 PSID PIPE ENTHALPY LOSS IS 0.0 BTU/LEM END DEVICE DEVICE #47: SIMPLE PIPE INLET NODE NUMBER IS 48 EXIT NODE NUMBER IS 68 PIPE ENTHALPY LOSS IS 0.0 BTU/LEM END DEVICE DEVICE #48: SIMPLE PIPE INLET NODE NUMBER IS 45 EXIT NODE NUMBER IS 69 PIPE ENTHALPY IOSS IS 0.0 BTU/LEM END DEVICE DEVICE #49: SIMPLE PIPE INLET NODE NUMBER IS 42 EXIT NODE NUMBER IS 70 PIPE ENTHALPY LOSS IS 0.0 BTU/LEM END DEVICE DEVICE #50: SIMPLE PIPE INLET NODE NUMBER IS 56 EXIT NODE NUMBER IS 71 PIPE ENTHALPY LOSS IS 0.0 BTU/LEM END DEVICE For example problem #3, the output file generated by RANKINE 3.0 is presented below. Copyright 1994 ILA. Thelen, C.W. Somerton RANKINE 3.0: A steam power plant computer simulation *********************************1' TITI‘E *********************************** EXAMPLE PROBLEM #3 *tittttttttt*t*****t********t*it NODE DATA t****itti*ttttttttttttttttttttttt NODE T(C) 'P(MPa) L Q S(KJ/KG/K) H(KJ/KG) V(M“3/KG) M(RG/S) A(RJ/RG) 1 284.11 6.8258 3 ***** 5.8269 2774.96 .02818 2005.0920 1048.06 2 284.11 6.8258 3 ***** 5.8269 2774.96 .02818 1900.2050 1048.06 3 284.11 6.8258 3 *ff** 5.8269 2774.96 .02818 104.8874 1048.06 4 233.35 2.9737 2 .915 5.8851 2649.43 .06170 1900.2050 905.25 5 233.35 2.9737 2 .915 5.8851 2649.43 .06170 145.5357 905.25 6 233.35 2.9737 2 .915 5.8851 2649.43 .06170 1754.6690 905.25 7 233.22 2.9668 2 .915 5.8859 2649.43 .06184 145.5357 905.00 8 233.22 2.9668 2 .915 5.8859 2649.43 .06184 65.0102 905.00 9 233.22 2.9668 2 .915 5.8859 2649.43 .06184 80.5255 905.00 10 212.88 2.0202 2 .891 5.9081 2590.77 .08803 103.1886 839.76 11 189.98 1.2548 2 .868 5.9383 2522.44 .13594 1651.4800 762.45 12 189.98 1.2548 2 .868 5.9383 2522.44 .13594 88.3536 762.45 13 189.98‘ 1.2548 2 .868 5.9383 2522.44 .13594 1563.1270 762.45 188.61 188.61 232.67 218.83 -283.42 269.49 269.49 269.49 269.49 190.59 131.77 104.30 91.35 76.70 40.90 269.49 40.90 40.90 40.90 40.90 40.90 49.32 75.00 75.00 73.10 54.07 103.45 100.67 70.66 130.69 127.91 106.23 190.13 155.63 133.47 109.31 109.31 100.61 166.61. 188.61 188.61 185.83 188.61 .211.30 208.52 191.39 209.94 231.67 231.67 228.89 215.49 228.89 211.30 188.61 130.69 103.45 75.88 188.61 1.2176 1.2176 2.9372 1.1997 6.7568 1.1818 1.1818 1.1818 1.1818 .6164 .2848 .1179 .0738 .0414 .0117 1.1818 .0117 .0117 .0117 .0117 .0117 3.7232 .0400 .0400 3.7232 .0400 .1145 3.7232 .1145 .2758 3.7232 .2758 .5978 3.7232 .5978 3.7232 3.7232 1.2176 3.7232 1.2176 1.2176 3.7232 1.2176 1.9581 3.7232 1.9581 7.7786 2.8841 2.8841 7.7786 2.8841 7.7786 1.9581 1.2176 .2758 .1145 .0400 1.2176 JIBDBJBDBDEJF‘P‘h‘thJh‘h‘h‘h)£bh‘k)BDF‘BLF'F'F.h‘h’h‘h‘h’F‘F‘BDP‘FIBJRJF‘JDBDBJBDhihlhih)BDBDBJhDhihihDhlfibh)h>UMh *tttt *ttti *ttit ***** ***** *ittt ***** t**** ***t* **t** .995 .952 .933 -.912 .884 44444 .912 .884 .912 .010 ***** ***** .912 .945 44444 44444 .952 44444 44444 .995 44444 44444 44444 ‘44444 44444 44444 44444 44444 44444 .868 .102 44444 44444 .891 44444 44444 44444 .142 .915 44444 *ittt ***** .010 .006 '.006 .005 .005 ****t 195 2.2207 6.5144 2.6329 6.6859 3.0974 6.9200 6.9200 6.9200 6.9200 6.9464 6.9795 7.0154 7.0403 7.0732 7.2335 6.9200 7.4443 7.2335 7.4443 .7663 .6898 .6905 7.0874 7.3027 .9877 .7654 7.0282 1.3094 1.0582 6.9937 1.6069 1.3757 6.9601 1.8924 1.6695 2.2212 2.2212 2.2207 2.0015 5.9494 2.6574 2.1879 2.2207 5.9195 2.4021 2.2439 2.4077 3.1321 5.8963 2.5816 2.4684 2.5816 2.4754 2.2482 1.6709 1.3764 1.0586 2.2207 801.00 2783.28 1002.59 2862.15 1254.43 2979.64 2979.64 2979.64 2979.64 2846.25 2710.82 2573.78 2508.55 2433.39 2312.92 2979.64 2380.83 2312.92 2380.83 229.52 204.87 209.53 2433.39 2508.55 308.76 229.52 2573.78 424.39 329.12 2710.82 539.53 445.26 2846.25 658.10 561.07 805.27 805.27 801.00 705.64 2522.44 1002.59 789.86 801.00 2590.77 891.41 813.69 899.25 1254.43 2649.43 985.93 922.92 985.93 922.92 813.69 561.07 445.26 329.12 801.00 .00114 .16110 .00121 .17840 .00134 .20420 .20420 .20420 .20420 .34131 .63268 1.38167 2.09972 3.52771 11.16561 .20420 11.52524 11.16561 11.52524 .13157 .00101 .00101 3.64422 3.77363 .00102 .00101 1.42151 .00104 .00103 .65230 .00107 .00105 .35194 .00110 .00107 .00114 .00114 .00114 .00111 .14005 .01741 .00114 .00114 .09002 .00117 1.00114 .00117 .01091 .06364 .00121 .00118 .00121 .00221 .00216 .00470 .00891 .02115 .00114 205.6862 1357.4410 65.0102 1357.4410 104.8874 1357.4410 1357.4410 1332.4580 24.9826 70.4334 65.3857 62.9030 31.0590 20.0170 1082.6600 24.9826 24.9826 1082.6600 24.9826 249.7981 1357.4410 1357.4410 20.0170 31.0590 1357.4410 249.7981 62.9030 1357.4410 198.7221 65.3857 1357.4410 135.8191 70.4334 1357.4410 70.4334 647.6515 647.6515 647.6515 2005.0920 88.3536 65.0102 2005.0920 441.9653 103.1886 2005.0920 288.6014 2005.0920 104.8874 80.5255 2005.0920 185.4129 2005.0920 185.4129 288.6014 70.4334 135.8191 198.7221 441.9653 145.28 852.18 224.43 880.10 338.30 928.05 928.05 928.05 928.05 786.81 641.56 493.85 421.24 336.29 168.21 928.05 173.51 168.21 173.51 5.82 3.89 8.34 332.09 343.28 19.30 6.08 490.04 39.38 18.71 637.33 66.13 40.55 782.74 99.90 69.09 149.42 149.42 145.28 115.03 759.16 217.17 143.87 145.28 836.37 181.82 151.08 187.99 328.00 901.92 223.03 193.62 223.03 191.56 149.80 68.66 40.33 18.60 145.28 444444444444444444444 DEVICE DATA (DEVICE BEFORE NODE) 444444444444444444444 NODE REV. WRK (KW) ACT. (KW) WRK IRREV HEAT X-FER MASS ERROR ENERGY ERROR (KW) (KW) (KG/S) (KW) OOQGUQUNH 39073.68 .00 .00 271364.90 .00 .00 36.71 .00 .00 114907.50 127678.00 .00 .00 .00 5138.71 6213.08 10790.37 11382.03 17484.69 .00 .00 .00 188197.70 183304.60 176759.10 82320.40 93674.75 181965.40 .00 18850.46 .00 .00 65.34 263424.80 -6035.67 84.08 2421.21 6095.37 5012.34 239.35 7493.96 6205.63 276.63 6811.39 5911.38 286.20 6401.92 6337.50 .00 -2680.83 .00 1729.77 290.46 472.40 3752.41 4500.66 349.84 4371.07 5058.86' -12370.51 1080.70 247.92 2183.92 3551.05 .00 .00 .00 238541.50 .00 .00 .00 .00 .00 102921.40 112850.60 .00 .00 .00 .00 .00 .00 .00 .00 .00 .00 .00 177739.30 170906.30 163995.60 73947.20 82880.06 130425.60 .00 14959.90 .00 .00 .00 .00 -6327.46 .00 .00 .00 .00 .00 .00 .00 .00 .00 .00 .00 .00 .00 .00 -2769.12 .00 .00 .00 .00 .00 .00 .00 .00 .00 -15724.26 .00 .00 .00 .00 196 39073.68 .00 .00 32823.39 .00 .00 36.71 .00 .00 11986.09 14827.36 .00 .00 .00 5138.71 6213.08 10790.37 11382.03 17484.69 .00 .00 .00 10458.38 12398.25 12763.52 8373.20 10794.69 51539.79 .00 3890.56 .00 .00 65.34 263424.80 291.79 84.08 2421.21 6095.37 5012.34 239.35 7493.96 6205.63 276.63 6811.39 5911.38 286.20 6401.92 6337.50 .00 88.29 .00 1729.77 290.46 472.40 3752.41 4500.66 349.84 4371.07 5058.86 3353.75 1080.70 247.92 2183.92 3551.05 3587170.00 .00 .00 .00 .00 .00 .00 .00 .00 .00 .00 .00 .00 .00 .00 ~107061J50 107061.50 -159484.80 159484.70 .00 .00 .00 .00 ‘ .00 .00 .00 .00 .00 .00 .00. .00 .00 .00 -2342823.00 .00 .00 .00 134691.70 -134691.70 .00 156968.90 -156968.90 .00 156292.90 -156292.90 .00 160952.70 -160952.70 .00 .00 .00 .00 .00 .00 168862.50 -168862.50 .00 203627.80 -203627.80 .00 .00 .00 173798.70 -173798.70 .000 .000 .000 .000 .000 .000 .000 .000 .000 .000 .000 .000 .000 .000 .000 .000 .000 .000 .000 .000 .000 .000 .000 .000 .000 .000 .000 .000 '.000 .000 .000 .000 .000 ,.000 .000 .000 .000 .000 .000 .000 .000 .000 .000 .000 .000 .000 .000 .000 .000 .000 .000 .000 .000 .000 ..000 .000 .000 .000 .000 .000 .000 .000 .000 .000 .000 .022 .000 .109 .000 .112 -.013 .000 -.020 .000 .219 .177 .000 .000 -.198 .008 .063 .000 .078 .113 .064 .000 .000 .000 .000 .000 .000 -.219 -.001 -.001 -.087 -.001 -.001 -.250 -.012 .000 -.002 .000 .000 .001 .000 .016 .004 .016 .016 -.002 .000 .000 .002 -.002 .029 .020 -.004 .000 .016 .016 .014 -.031 .016 .002 -.006 .007 .000 -.016 197 65 .00 .00 .00 .00 .000 -.053 66 380.60 .00 380.60 .00 .000 -.006 67 368.90 .00 368.90 .00 .000 .004 68 29.95 .00 29.95 .00 .000 .000 69 29.64 .00 29.64 .00 .000 .000 70 21.05 .00 21.05 .00 .000 .001 71 .00 .00 .00 .00 .000 -.004 4444444444444444444444444444444 SYSTEM DATA 44444444444444444444444444444444 .0000 KG/SEC .0000_KG/SEC TOTAL MASS FLOW RATE EXITING SYSTEM: TOTAL MASS FLOW RATE ENTERING SYSTEM: From this output file, it can be seen that the 151 law efficiency 1s 34.1069 percent and the 2114 law efficiency 1s 74. 6609 percent. W925 1) W.A. Thelen, LLIIJII Thesis, Michigan State University, 1995. TOTAL ENTHALPY FLOW RATE EXITING SYSTEM: .0000 KW TOTAL ENTHALPY FLOW RATE ENTERING SYSTEM: .0000 KW TOTAL HEAT AND WORK ENTERING SYSTEM: -.1250 KW BOILER HEAT (DEVICE 4 1): 3507170.0000 KW TOTAL BOILER HEAT: 3507170.0000 KW TOTAL HEAT LOAD HEAT: .0000 KW CONDENSER HEAT (DEVICE I 20): -2342023.0000 KW TOTAL PIPE ENERGY LOSSES: .0000 KW TURBINE WORR‘(DEVICE 4 3): 230541.5000 KW TURBINE WORK (DEVICE 4 5): 215772.1000 KW TURBINE WORK (DEVICE 4 10): 799094.2000 KW 'TURBINE WORK (DEVICE 4 20): 14959.9000 KW NET WORK TO GENERATORS: 1269160.0000 KW PUMP WORK (DEVICE 4 29): -6327.4590 KW PUMP WORK (DEVICE 4 36): -2769.1210 KW PUMP WORK (DEVICE 4 40): —15724.2600 KW TOTAL PUMP WORK: -24020.0400 KW GENERATOR MECHANICAL LOSSES: 5725.0000 KW GENERATOR ELECTRICAL LOSSES: 15150.0000 KW NET ELECTRICAL POWER: 1223472.0000 KW SYSTEM HEAT RATE: 10003.0400 BTU/KW*RR CARNOT CYCLE EFFICIENCY: 40.6905 PERCENT IST LAW EFFICIENCY: 34.1069 PERCENT 2ND LAW EFFICIENCY: 74.6609 PERCENT 2ND LAW EFFECTIVENESS: 70.0403 PERCENT CIIECI' IR ll' Minions The following conclusions are supported by this analysis: .. - The RANKINE 3.0 computer program represents a major revision Of the RANKINE family of computer software and provides the engineering community with an additional tool for modeling Rankine cycle based systems. - The modular structure of RANKINE 3.0 establishes a framework from which additional thermodynamic models may be developed and easily integrated into the RANKINE 3.0 Program. - The RANKINE 3.0 input/output format permits the entire array of computer users the ability to utilize the RANKINE 3.0 computer software package with confidence that program predicted results are accurate. - The active and passive code testing permits a high level of confidence associated with program results. - The eleven thermodynamic models within RANKINE 3.0 permit modern power plant designs to be studied and provided results which are consistent with power plant indusz programs. W The following recommendations are suggested by the author: - Rankine 3.0 program improvements - Additional thermodynamic model integration - Detailed turbine model - Turbine drive feed water pump model - Forward draining closed feed water heater model 198 199 - Electrical Generator model - Cooling tower model (Mechanical and Natural) - Include real device models which utilize physical parameters such as pipe diameter, pipe materials, pipe geometry, ect. rather than total pipe pressure drop. - Include effects such as elevation and velocity changes between components. - Utilize a visual programming language to automate the development of the input file. - Provide for graphically based outputs for system layouts and parameter studies. - Integrate Optimization techniques within code structm'e. - Permit user input device performance parameters in table format. - Permit user input cost functions. Additional benchmarking to industry programs and to data Obtained from Operating power plants. Appendix A: Summary of comparison between RANKINE 3.0 and hand calculations for individual device verification .3413 g: «4 .3. lo: 3!: :40 an 4.31 .455 :3 «4 41¢ to =40 NI 4.! =44 «- 4E 03- 2.3 N: 4...! 5. :40 an 1...! :4. N- 4:! 3x 53:... .3: n. 4...: .24.:- 31 a. .21 m .EEENJI: Esau-EEIN-JE 3x 3.2:. .8: .4 ._z . .25 «4 .3. to. 8.1.4- .41. 8.3a he. .25 a. 4.! 3: 15.2035 3d. 4.... .0: N. 41¢ 3: 3.53:. a. 41¢ . 3 use I... u. 5:: 2.x 9‘5 .u a: on." .0: a. 4.! ix 50.20.65 8. 23- E... «n 42! 22 {53822.1 vii—.4. = a”. 3x {goignnax 38.5240: 4.! 3x {30.533.441. gs! : 44! ac. to! 4341.452 . 0 EU .4 4.! 3.. {08.9.3- 2d. a... an. pt: 3.. :5! '30- E 4: i =8 —. 4.! 3.. {ch .28- : a... 2.4 .4 4.! 3! ED! '3 3. gun = 4.3 I :2 .5. . . 2.8 a... I... .4 4.! '44.] 45.35.28... 35.61.33. '31 39.3. . .4... 0...: 51.5.! I! .8. . N a... s. = it '3'. 43.454- . .88 .4... Sun—4...! :3 .8. . .4 3: 33. :2. .4 '3' .8. :3: .1114. :38 s: .- i 39 . . .15 —. 42¢ “I: .323»- ...o 0.6! a: . 3.: cm 433.. lo- 48E :8 2.9- ..x. 8- .8:. saw um=£ . :4. o...‘ a: . sum lays... a s:- o..n§ 4! saw 7. :3 3.: 4! saw 7. 3 03.. =8 0.43 a... a I! .53 $442.94.... 584 .fiw 0a 54 . .5. 2.0- .... . 5. 3 9.5. .28....- Is 2...- ..x . .1»- .4! 03?. 3- :4: I... 2.8 5:. 48 .IE .8. 9:3. lac. s: o...“ a! 3‘... .0: tags... be. .03 0.6- 1.: ‘2. Z . .0: 0.6- 4: ‘3 T. 4. v3- .0: 0.6. 4: 3 I. r! 534 . .25 2.0. .1 453. .42. 0 on... .0: o. 2 ._x .5. .0: £5 :6 201 202 203 5.40... to: n. =5 :3...)- nu =uw 204 I; 8.3.5.. am 205 8": ’ 206 207 208 209 5:8. as... 3...: 34%... 58 45 210 Simple Closed Food Water Ham Dulce 212 :é?§-4-?:6§:;;:; 5.23445 ~-x~°°§§..i 2 E I I 5 TEE 3:5: Appendix B: RANKINE 3.0 input files for individual device verification 213 TITLE LINE SIMPLE BOILER MODEL TEST END TITLE NUMBER OF NODES IS 22 HIGH TEMPERATURE RESERVOIR: 600 DEG C LOW TEMPERATURE RESERVOIR: 25.0 DEG C DEAD STATE TEMPERATURE: 25.0 DEG C DEAD STATE PRESSURE: 101 KPA GENERATOR MECHANICAL LOSS IS 10.0 KW GENERATOR ELECTRICAL LOSS IS 5.0 KW DEVICE #1: SIMPLE BOIIER COMMENT: THIS DEVICE WILL TEST ICALL-=1. IFIND=1.2 COMMENT: THIS DEVICE WILL TEST ICALL=2. IFIND=2.2 COMMENT: THIS DEVICE WILL TEST ICALL-=3. IFIND=1 COMMENT: THIS DEVICE WILL TEST ICALL=4. IFIND=1 BOILER INLET NODE NUMBER IS 1 BOILER EXIT NODE NUMBER IS 2. BOILER INLET TEMPERATURE IS 100.0 DEG C BOILER EXIT TEMPERATURE IS 600.0 DEG C BOILER EXIT PRESSURE IS 18 MPA BOILER EXIT MASS FLOW RATE IS 5.0 KG/SEC BOILER PERCENTAGE PRESSURE LOSS IS 10 PERCENT BOILER REHEAT LEG #l INLET NODE NUMBER IS 3 BOILER REHEAT LEG #1 EMT NODE NUMBER IS 4 BOILER REHEAT LEG #1 INLET TEMPERATURE IS 100.0 DEG C BOILER REHEAT LEG #1 INLET PRESSURE IS 20.0 MPA BOILER REHEAT LEG #1 EXIT TEMPERATURE IS 600.0 DEG C BOILER REHEAT LEG #1 EMT MASS FLOW RATE IS 5.0 KG/SEC BOILER REHEAT LEG #1 PERCENTAGE PRESSURE LOSS IS 10 PERCENT BOILER REHEAT LEG #2 INLET NODE NUMBER IS 5 BOILER REHEAT LEG #2 EXIT NODE NUMBER IS 6 BOILER REHEAT LEG #2 INLET TEMPERATURE IS 100.0 DEG C BOILER REHEAT LEG #2 INLET PRESSURE 18 20.0 MPA BOILER REHEAT LEG #2 INLET MASS FLOW RATE IS 5.0 KG/SEC BOILER REHEAT LEG #2 EXIT TEMPERATURE IS 6m.0 DEG C BOILER REHEAT LEG #2 PRESSURE LOSS IS 2 MPA BOILER REHEAT LEG #3 INLET NODE NUMBER IS 7 BOILER REHEAT LEG #3 EXIT NODE NUMBER IS 8 BOILER REHEAT LEG #3 DILET TEMPERATURE IS 100.0 DEG C BOILER REHEAT LEG #3 INLET MASS FLOW RATE IS 5.0 KG/SEC BOILER REHEAT LEG #3 EMT TEMPERATURE IS 600.0 DEG C BOILER REHEAT LEG #3 EXIT PRESSURE IS 18.0 MPA BOILER REHEAT LEG #3 PRESSURE LOSS IS 2.0 MPA BOILER REHEAT LEG #4 INLET NODE NUMBER IS 9 BOILER REHEAT LEG #4 EXIT NODE NUMBER IS 10 BOILER REHEAT LEG #4 INLET TEMPERATURE IS 100.0 DEG C BOILER REHEAT LEG #4 INLET MASS FLOW RATE IS 5.0 KG/SEC BOILER REHEAT LEG #4 EXIT TEMPERATURE IS 6m.0 DEG C BOILER REHEAT LEG #4 EXIT PRESSURE IS 18.0 MPA BOILER REHEAT LEG #4 PRESSURE LOSS IS 2.0 MPA BOILER REHEAT LEG #5 INLET NODE NUMBER IS 11 BOILER REHEAT LEG #5 EXIT NODE NUMBER IS 12 BOILER REHEAT LEG #5 INLET TEMPERATURE IS 100.0 DEG C BOILER REHEAT LEG #5 INLET MASS FLOW RATE IS 5.0 KG/SEC BOILER REHEAT LEG #5 EXIT TEMPERATURE IS 6WD DEG C BOILER REHEAT LEG #5 EXIT PRESSURE IS 18.0 MPA BOILER REHEAT LEG #5 PRESSURE LOSS IS 2.0 MPA BOILER REHEAT LEG #6 INLET NODE NUMBER IS 13 BOILER REHEAT LEG #6 EMT NODE NUMBER IS 14 BOILER REHEAT LEG #6 INLET TEMPERATURE IS 100.0 DEG C BOILER REHEAT LEG #6 INLET MASS FLOW RATE IS 5.0 KG/SEC BOILER REHEAT LEG #6 EXIT TEMPERATURE IS 6m.0 DEG C 214 BOILER REHEAT LEG #6 EMT PRESSURE IS 18.0 MPA BOILER REHEAT LEG #6 PRESSURE LOSS IS 2.0 MPA BOILER REHEAT LEG #7 INLET NODE NUMBER IS 15 BOILER REHEAT LEG #7 EXIT NODE NUMBER IS 16 BOILER REHEAT LEG #7 INLET TEMPERATURE IS 100.0 DEG C BOILER REHEAT LEG #7 INLET MASS FIOW RATE IS 5.0 KGISEC BOILER REHEAT LEG #7 EMT TEMPERATURE IS 600.0 DEG C BOILER REHEAT LEG #7 EMT PRESSURE IS 18.0 MPA BOILER REHEAT LEG #7 PRESSURE LOSS IS 2.0 MPA BOILER REHEAT LEG #8 INLET NODE NUMBER IS 17 BOILER REHEAT LEG #8 EXIT NODE NUMBER IS 18 BOILER REHEAT LEG #8 INLET TEMPERATURE IS 100.0 DEG C BOILER REHEAT LEG #8 INLET MASS FLOW RATE IS 5.0 KG/SEC BOILER REHEAT LEG #8 EMT TEMPERATURE IS 600.0 DEG C BOILER REHEAT LEG #8 EXIT PRESSURE IS 18.0 MPA - BOILER REHEAT LEG #8 PRESSURE LOSS IS 2.0 MPA BOILER REHEAT LEG #9 INLET NODE NUMBER IS 19 BOILER REHEAT LEG #9 EMT N ODE NUMBER IS 20 BOILER REHEAT LEG #9 INLET TEMPERATURE 18 100.0 DEG C BOILER REHEAT LEO #9 INLET MASS FLOW RATE IS 5.0 KG/SEC BOILER REHEAT LEG #9 EXIT TEMPERATURE IS 6m.0 DEG C BOILER REHEAT LEG #9 EXIT PRESSURE IS 18.0 MPA BOILER REHEAT LEG #9 PRESSURE IOSS IS 2.0 MPA BOILER REHEAT LEG #10 INLET NODE NUMBER IS 21 BOILER REHEAT LEG #10 EXIT NODE NUMBER IS 22 BOILER REHEAT LEG #10 INLET TEMPERATURE IS 100.0 DEG C BOILER REHEAT LEG #10 INLET MASS FLOW RATE IS 5.0 KGISEC BOILER REHEAT LEG #10 EXIT TEMPERATURE IS 600.0 DEG C BOILER REHEAT LEG #10 EMT PRESSURE 18 18.0 MPA BOILER REHEAT LEG #10 PRESSURE LOSS IS 2.0 MPA END DEVICE 215 TITLE LINE SIMPLE TURBINE MODEL TEST END TTTI.E NUMBER OF NODES IS 4 HIGH TEMPERATURE RESERVOIR IS 600 DEG C LOW TEMPERATURE RESERVOIR IS 25.0 DEG C DEAD STATE TEMPERATURE IS 25.0 DEG C DEAD STATE PRESSURE IS 101 KPA GENERATOR MECHANICAL LOSS IS 10.0 KW GENERATOR ELECTRICAL LOSS IS 5.0 KW DEVICE #1: SIMPLE TURBINE COMMENT: THIS DEVICE WILL TEST ICALL=1. IFIND=1 COMMENT: THIS DEVICE WILL TEST ICALL=2. IFIND=1 COMMENT: THIS DEVICE WILL TEST ICALL=3. IFIND=1 COMMENT: THIS DEVICE WILL TEST ICALL=4. IFIND=1 INLET NODE NUMBER IS 1 EXTRACTION #1 NODE NUMBER IS 2 EXTRACTION #2 NODE NUMBER IS 3 EXTRACTION #3 NODE NUMBER IS 4 STAGE GROUP #1 EFFICIENCY IS 90 PERCENT STAGE GROUP #2 EFFICIENCY IS 85 PERCENT STAGE GROUP #3 EFFICIENCY IS 80 PERCENT INLET TEMPERATURE IS 600 DEG C INLET PRESSURE IS 20 MPA INLET MASS FLOW RATE IS 5.0 KG.SEC EXTRACTION #1 PRESSURE IS 10.0 MPA EXTRACTION #1 MASS FLOW RATE IS 1.0 KGISEC EXTRACTION #2 PRESSURE IS 5.0 MPA EXTRACTION #2 MASS FLOW RATE IS 2.0 KG/SEC EXTRACTION #3 PRESSURE IS 0.1 MPA END DEVICE 216 TITLE LINE SIMPLE PUMP MODEL TEST END TITLE NUMBER OF NODES IS 4 HIGH TEMPERATURE RESERVOIR IS 500 DEG C LOW TEMPERATURE RESERVOIR 18 25.0 DEG C DEAD STATE TEMPERATURE IS 25.0 DEG C DEAD STATE PRESSURE IS 101 KPA GENERATOR MECHANICAL LOSS IS 0.0 MW GENERATOR ELECTRICAL IOSS IS 0.0 MW DEVICE #1: SIMPLE PUMP COMMENT: THIS DEVICE WILL TEST ICALL=1. IFIND=1 COMMENT: THIS DEVICE WILL TEST ICALL=2. IFIND=1.2 COMMENT: THIS DEVICE WILL TEST ICALL=3. IFIND=1 COMMENT: THIS DEVICE WILL TEST ICALL=4, IFIND=1 SUCTION NODE NUMBER IS 1 DISCHARGE NODE NUMBER IS 2 SUCTION PRESSURE IS 0.5 MPA SUCTION TEMPERATURE IS 130.0 DEG C SUCTION MASS FLOW RATE IS 1.0 KG/SEC DISCHARGE PRESSURE IS 10.0 MPA PUMP EFFICIENCY IS 100 PERCENT END DEVICE DEVICE #2: SIMPLE PUMP COMMENT: THIS DEVICE WILL TEST ICALLfiI. IFIND=2 COMMENT: THIS DEVICE WILL TEST ICALL=2. IFIND=1.2 COMMENT: THIS DEVICE WILL TEST ICALL=3. IFIND=1 COMMENT: THIS DEVICE WILL TEST ICALL=4. IFIND=1 SUCTION NODE NUMBER IS 3 DISCHARGE NODE NUMBER IS 4 SUCTION PRESSURE IS 1.0 MPA DISCHARGE TEMPERATURE IS 170 DEG C DISCHARGE PRESSURE IS 10 MPA DISCHARGE MASS FLOW RATE IS 1.0 KG/SEC PUMP EFFICIENCY IS 80 PERCENT ETD DEVICE 217 TITLE LINE SIMPLE PIPE MODEL TEST ETD TITLE NUMBER OF NODES IS 12 HIGH TEMPERATURE RESERVOIR IS 500 DEG C LOW TEMPERATURE RESERVOIR IS 25.0 DEG C DEAD STATE TEMPERATURE IS 25.0 DEG C DEAD STATE PRESSURE IS 101 KPA GETERATOR MECHANICAL LOSS IS 0.0 MW GENERATOR ELECTRICAL IOSS IS 0.0 MW DEVICE #1: SIMPLE PIPE COMMENT: THIS DEVICE WILL TEST ICALL=1. IFIND=1.3.5 COMMENT: THIS DEVICE WILL TEST ICALL=2. IFIND=I.2 COMMENT: THIS DEVICE WILL TEST ICALL=3. IFIND-1 COMMENT: THIS DEVICE WILL TEST ICALL=4. IFIND=1 INLET NODE NUMBER IS 1 EXIT NODE NUMBER IS 2 INLET TEMPERATURE IS 500 DEG C IITLET PRESSURE IS 10 MPA INLET MASS FLOW RATE IS 1 KGISEC PIPE PRESSURE LOSS IS 1.0 MPA PIPE ENTHALPY LOSS IS 100 KJIKG END DEVICE DEVICE #2: SIMPLE PIPE COMMENT: THIS DEVICE WILL TEST ICALL-=1. IFIND=2.4.5 COMMENT: THIS DEVICE WILL TEST ICALL=2. IFIND=I.2 COMMENT: THIS DEVICE WILL TEST ICALL=3. IFIND=1 COMMENT: THIS DEVICE WILL TEST ICALL=4. IFIND=1 INLET NODE NUMBER IS 3 EXIT NODE NUMBER IS 4 EXIT TEMPERATURE IS 456.10 DEG C EXIT PRESSURE IS 9 MPA EXIT MASS FLOW RATE IS 1 KGISEC PIPE PRESSURE LOSS IS 1.0 MPA PIPE ETTHALPY IOSS IS 100 IUIKG ETD DEVICE DEVICE #3: SIMPLE PIPE COMMET'T: THIS DEVICE WILLTEST ICALL=1. IFIND=1.4,5 COMMENT: THIS DEVICE WILL TEST ICALL=2. IFIND=1,2 COMMENT: TI-IIS DEVICE WILL TEST ICALL=3. IFIND=1 COMMENT: THIS DEVICE WILL TEST ICALL=4. IFIND=1 INLET NODE NUMBER IS 5 EXIT NODE NUMBER IS 6 INLET PRESSURE IS 10.0 MPA EXIT ENTHALPY IS 3274.66 KJIKG INLET MASS FLOW RATE IS 1 KGISEC PIPE PERCENTAGE PRESSURE LOSS IS 10 PERCETT PIPE PERCENTAGE ENTHALPY IOSS IS 2.959 % ETD DEVICE 218 DEVICE #4: SIMPLE PIPE COMMET'T: THIS DEVICE WILL TEST ICALL=1. IFIND=2.3.5 COMMENT: THIS DEVICE WILL TEST ICALL=2. IFIND=I.2 COMMENT: THIS DEVICE WILL TEST ICALL=3. IFIND=1 COMMENT: THIS DEVICE WILL TEST ICALL=4. IFIND=1 INLET NODE NUMBER IS 7 EXIT NODE NUMBER IS 8 EXIT PRESSURE 18 9.0 MPA IITLET ET'THALPY IS 3374.66 KJ/KG EXIT MASS FLOW RATE IS 1 KG/SEC PIPE PERCENTAGE PRESSURE LOSS IS 10 PERCENT PIPE PERCENTAGE ENTHALPY IOSS IS 2.959 % END DEVICE DEVICE #5: SIMPLE PIPE COMMENT: THIS DEVICE WILL TEST ICALL=1. IFIND=5 COMMENT: THIS DEVICE WILL TEST ICALL=2. IFIND=I.2 COMMENT: THIS DEVICE WILL TEST ICALL=3. IFIND=1 COMMENT: THIS DEVICE WILL TEST ICALL=4. IFIND=1 INLET NODE NUMBER IS 9 EXIT NODE NUMBER IS 10 INLET TEMPERATURE IS 500.0 DEG C INLET PRESSURE IS 10.0 MPA EXIT TEMPERATURE 18 456.14 DEG C EXIT PRESSURE IS 9.0 MPA EXIT MASS FLOW RATE IS 1 KG/SEC END DEVICE DEVICE #6: SIMPLE PIPE COMMENT: THIS DEVICE WILL TEST ICALL=1. IFIND=3.5 mMMENT: THIS DEVICE WILL TEST ICALL=2. IFIND=I.2 COMMET’T: THIS DEVICE WILL TEST ICALL=3. IFIND=1 COMMENT: THIS DEVICE WILL TEST ICALL=4. IFIND=1 INLET NODE NUMBER IS 11 EXIT NODE NUMBER IS 12 INLET TEMPERATURE IS 500.0 DEG C INLET PRESSURE IS 10.0 MPA EXIT PRESSURE IS 9.0 MPA EXIT MASS FLOW RATE IS 1 KGISEC PIPE ENTHALPY LOSS IS 100 TUIKG END DEVICE 219 TITLE LINE SIMPLE JUNCTION MODEL TEST ETD TITLE NUMBER OF NODES IS 25 HIGH TEMPERATURE RESERVOIR IS 500 DEG C LOW TEMPERATURE RESERVOIR IS 25.0 DEG C DEAD STATE TEMPERATURE IS 25.0 DEG C DEAD STATE PRESSURE IS 101 KPA GETERAT’OR MECHANICAL LOSS IS 0.0 MW GENERATOR ELECTRICAL LOSS 18 0.0 MW DEVICE #1: SIMPLE JUNCTION COMMENT: THIS DEVICE WILL TEST ICALL=1. IFIND=1 COMMENT: THIS DEVICE WILL TEST ICALL-=2. IFIND=2.3.4.6.8 COMMENT: THIS DEVICE WILL TEST ICALL=3. IFIND=1 COMMETT: THIS DEVICE WILL TEST ICALL=4. IFIND=1 INLET #1 NODE NUMBER IS 1 IITLET #2 NODE NUMBER IS 2 INLET #3 NODE NUMBER IS 3 EXIT #1 NODE NUMBER IS 4 EXIT #2 NODE NUMBER IS 5 EXIT #3 NODE NUMBER IS 6 INLET #1 MASS FLOW RATE IS .31 KG/SEC INLET #2 FLOW FRACTION IS 22 PERCETT INLET #3 FLOW FRACTION IS 47 PERCENT EXIT #1 FLOW FRACTION IS 41 PERCENT EXIT #2 FLOW FRACTION IS 50 PERCENT INLET #2 PRESSURE IS 5.0 MPA INLET #2 TEMPERATURE IS 445.0 DEG C END DEVICE DEVICE #2: SIMPLE JUNCTION COMMENT: THIS DEVICE WILL TEST ICALL=1. IFIND=1 COMMENT: TI-IIS DEVICE WILL TEST ICALL-'2. IFIND=I.2.8 COMMETT: THIS DEVICE WILL TEST ICALL=3. IFIND=1 COMMENT: THIS DEVICE WILL TEST ICALL=4. IFIND=1 INLET #1 NODE NUMBER IS 7 EXIT #1 NODE NUMBER IS 8 EXIT #2 NODE NUMBER IS 9 EXIT #3 NODE NUMBER IS 10 INLET #1 MASS FLOW RATE IS 10 KGISEC EXIT #1 MASS FLOW RATE IS 2 KGISEC EXIT #3 MASS FLOW RATE IS 4 KG/SEC EMT #2 PRESSURE IS 5.0 MPA EXIT #2 TEMPERATURE IS 445.0 DEG C END DEVICE DEVICE #3: SIMPLE JUNCTION COMMENT: THIS DEVICE WILL TEST ICALL=1. IFIND=1 COMMENT: THIS DEVICE WILL TEST ICALL;2. IFIND=2.3.4.8 mMMENT: THIS DEVICE WILL TEST ICALL=3. IFIND=1 COMMENT: THIS DEVICE WILL TEST ICALL=4. IFIND=1 INLET #1 NODE NUMBER IS 11 IITLET #2 NODE NUMBER IS 12 INLET #3 NODE NUMBER IS 13 EXIT #1 NODE NUMBER IS 14 INLET #1 PRESSURE IS 5.0 MPA INLET #1 TEMPERATURE IS 445.0 DEG C INLET #1 MASS FLOW IS 0.40 KGISEC IITLET #1 FLOW FRACTION LS 0.40 INLET #2 FLOW FRACTION IS 22.9745% ETD DEVICE 220 DEVICE #4: SIMPLE JUNCTION COMMENT: THIS DEVICE WILL TEST ICALL=1. IFIND=1 COMMENT: THIS DEVICE WILL TEST ICALL=2. IFIND=2.5,7.8 COMMENT: THIS DEVICE WILL TEST ICALL=3. IFIND=1 COMMENT: THIS DEVICE WILL TEST ICALL=4. IFIND=1 INLET #1 NODE NUMBER IS 15 EXIT #1 NODE NUMBER IS 16 EXIT #2 NODE NUMBER IS 17 EXIT #3 NODE NUMBER IS 18 EXIT #4 NODE NUMBER IS 19 EXIT #5 NODE NUMBER IS 20 EXIT #6 NODE NUMBER IS 21 EXIT #7 NODE NUMBER IS 22 EXIT #8 NODE NUMBER IS 23 EXIT #9 NODE NUMBER IS 24 EXIT #10 NODE NUMBER IS 25 INLET #1 PRESSURE 18 5.0 MPA INLET #1 TEMPERATURE IS 445.0 DEG C INLET #1 MASS FLOW RATE IS 10 KG/SEC EXIT #1 FLOW FRACTION IS 10.0 PERCENT EXIT #2 FLOW FRACTION IS 10.0 PERCENT EXIT #3 FLOW FRACTION IS 10.0 PERCENT EXIT #4 FLOW FRACTION 18 10.0 PERCENT EXIT #5 FLOW FRACTION IS 10.0 PERCENT EXIT #6 FLOW FRACTION IS 10.0 PERCENT EXIT #7 FLOW FRACTION IS 10.0 PERCENT EXIT #8 FLOW FRACTION IS 10.0 PERCENT m #9 FLOW FRACTION IS 10.0 PERCENT EXIT #10 FLOW FRACTION IS 10.0 PERCENT END DEVICE 221 TITLE LINE SIMPLE CONDENSER MODEL TEST ENDTTTIE NUMBER OF NODES IS 33 HIGH TEMPERATURE RESERVOIR IS 500 DEG C LOW TEMPERATURE RESERVOIR 18 25.0 DEG C DEAD STATE TEMPERATURE IS 25.0 DEG C DEAD STATE PRESSURE IS 101 KPA GENERATOR MECHANICAL LOSS IS 0.0 MW GENERATOR ELECTRICAL LOSS IS 0.0 MW DEVICE #1: SIMPLE CONDENSER COMMENT: THIS DEVICE WILL TEST ICALL=1. IFIND=1.2 COMMENT: THIS DEVICE WILL TEST ICALL=2. IFIND=1.2 - COMMENT: THIS DEVICE WILL TEST ICALL=3. IFIND=1 COMMENT: TIIIS DEVICE WILL TEST ICALL=4. IFIND=1 EXIT NODE NUMBER IS 1 INLET #1 NODE NUMBER IS 2 INLET #1 PRESSURE IS 05 MPA INLET #1 TEMPERATURE IS 200 DEG C INLET #1 MASS FLOW RATE IS 10 KG/SEC END DEVICE DEVICE #2: SIMPLE CONDENSER COMMENT: THIS DEVICE WILL TEST ICALL=1. IFIND=I.2 COMMENT: THIS DEVICE WILL TEST ICALL=2. IFIND=I.2 COMMENT: THIS DEVICE WILL TEST ICALL=3. IFIND=1 COMMENT: THIS DEVICE WILL TEST ICALL=4. IFIND=1 EXIT NODE. NUMBER IS 3 INLET #1 NODE NUMBER IS 4 INLET #2 NODE NUMBER IS 5 EXIT PRESSURE IS 05 MPA EXIT MASS FLOW IS 10 KGISEC INLET #1 TEMPERATURE IS 200 DEG C INLET #2 TEMPERATURE IS 200 DEG C INLET #2 MASS FLOW RATE IS 5 KGISEC END DEVICE DEVICE #3: SIMPLE CONDENSER COMMENT: THIS DEVICE WILL TEST ICALL-=1. IFIND=I.2 COMMENT: THIS DEVICE WILL TEST ICALL=2. IFIND=1.2 COMMENT: THIS DEVICE WILL TEST ICALL;3. IFIND=1 COMMENT: THIS DEVICE WILL TEST ICALL=4. IFIND=1 EXIT NODE NUMBER IS 6 INLET #1 NODE NUMBER IS 7 INLET #2 NODE NUMBER Is a INLET #3 NODE NUMBER Is 9 INLET a4 NODE NUMBER Is 10 INLET” NODENUMBER IS 11 INLET #6 NODE NUMBER IS 12 INLET #7 NODE NUMBER IS 13 INLET #8 NODE NUMBER IS 14 INLET #9 NODE NUMBER IS 15 INLET #10 NODE NUMBER Is 15 INLET #11 NODE NUMBER IS 17 INLET #12 NODE NUMBER Is 1s INLET #13 NODE NUMBER IS 19 INLET #14 NODE NUMBER IS 20 INLET #15 NODE NUMBER Is 21 INLET #16 NODE NUMBER IS 22 INLET m NODE NUMBER Is 23 INLET #18 NODE NUMBER IS 24 INLET #19 NODE NUMBER IS 25 222 INLET #20 NODE NUMBER IS 26 INLET #21 NODE NUMBER IS 27 INLET #22 NODE NUMBER IS 28 INLET #23 NODE NUMBER IS 29 INLET #24 NODE NUMBER IS 30 INLET #25 NODE NUMBER IS 31 INLET #26 NODE NUMBER IS 32 INLET #27 NODE NUMBER IS 33 INLET #17 PRESSURE IS 0.5 MPA INLET #1 TEMPERATURE IS 200 DEG C INLET #1 MASS FLOW RATE IS 0.3703 KG/SEC INLET #2 TEMPERATURE IS 200 DEG C INLET #2 MASS FLOW RATE IS 03703 KG/SEC INLET #3 TEMPERATURE IS 200 DEG C INLET #3 MASS FLOW RATE IS 0.3703 KG/SEC INLET #4 TEMPERATURE IS 200 DEG C INLET #4 MASS FLOW RATE IS 0.3703 KGISEC INLET #5 TEMPERATURE IS 200 DEG C INLET #5 MASS FLOW RATE IS 0.3703 KG/SEC INLET #6 TEMPERATURE IS 200 DEG C INLET #6 MASS FLOW RATE 18 0.3703 KG/SEC INLET #7 TEMPERATURE IS 200 DEG C INLET #7 MASS FLOW RATE IS 0.3703 KG/SEC INLET #8 TEMPERATURE IS 200 DEG C INLET #8 MASS FLOW RATE IS 0.3703 KG/SEC INLET #9 TEMPERATURE IS 200 DEG C INLET #9 MASS FLOW RATE IS 03703 KGISEC INLET #10 TEMPERATURE IS 200 DEG C INLET #10 MASS FLOW RATE IS 0.3703 KG/SEC INLET #11 TEMPERATURE IS 200 DEG C INLET #11 MASS FLOW RATE IS 0.3703 KG/SEC INLET #12 TEMPERATURE IS 200 DEG C INLET #12 MASS FLOW RATE IS 0.3703 KG/SEC INLET #13 TEMPERATURE IS 200 DEG C INLET #13 MASS FLOW RATE IS 03703 KG/SEC INLET #14 TEMPERATURE IS 200 DEG C INLET #14 MASS FLOW RATE LS 0.3703 KG/SEC INLET #15 TEMPERATURE IS 200 DEG C INLET #15 MASS FLOW RATE IS 0.3703 KG/SEC INLET #16 TEMPERATURE IS 200 DEG C INLET #16 MASS FLOW RATE IS 03703 KG/SEC INLET #17 TEMPERATURE IS 200 DEG C INLET #17 MASS FLOW RATE IS 03703 KG/SEC INLET #18 TEMPERATURE IS 200 DEG C INLET #18 MASS FLOW RATE IS 03703 KG/SEC INLET #19 TEMPERATURE IS 200 DEG C INLET #19 MASS FLOW RATE IS 0.3703 KG/SEC INLET #20 TEMPERATURE IS 200 DEG C INLET #20 MASS FLOW RATE IS 0.3703 KGISEC INLET #21 TEMPERATURE LS 200 DEG C INLET #21 MASS FLOW RATE LS 0.3703 KG/SEC INLET #22 TEMPERATURE IS 200 DEG C INLET #22 MASS FLOW RATE IS 0.3703 KG/SEC INLET #23 TEMPERATURE IS 200 DEG C INLET #23 MASS FLOW RATE IS 0.3703 KG/SEC INLET #24 TEMPERATURE IS 200 DEG C INLET #24 MASS FLOW RATE IS 03703 KG/SEC INLET #25 TEMPERATURE IS 200 DEG C INLET #25 MASS FLOW RATE IS 0.3703 KG/SEC INLET #26 TEMPERATURE IS 200 DEG C INLET #26 MASS FLOW RATE IS 03703 KG/SEC INLET #27 TEMPERATURE IS 200 DEG C INLET #27 MASS FLOW RATE LS 0.3703 KG/SEC END DEVICE 223 TIITE LINE SIMPLE HEAT LOAD MODEL TEST END TITLE NUMBER OF NODES IS 4 HIGH TEMPERATURE RESERVOIR IS 500 DEG C LOW TEMPERATURE RESERVOIR IS 25.0 DEG C DEAD STATE TEMPERATURE IS 25.0 DEG C DEAD STATE PRESSURE IS 101 KPA GEITERATOR MECHANICAL LOSS IS 0.0 KW GENERATOR ELECTRICAL LOSS IS 0.0 KW DEVICE #1: SIMPLE HEAT LOAD COMMENT: THIS DEVICE WILL TEST ICALL=1. IFIND=1 COMMENT: THIS DEVICE WILL TEST ICALL=2. IFIND=I.2 COMMENT: THIS DEVICE WILL TEST ICALL=3. IFIND=1 COMMENT: THIS DEVICE WILL TEST ICALL=4. IFIND=1 INLET NODE NUMBER IS 1 ' EXIT NODE NUMBER IS 2 INLET TEMPERATURE IS 500 DEG C INLET PRESSURE IS 10 MPA INLET MASS FLOW RATE IS 1.0 KG/SEC EXIT TEMPERATURE IS 400 DEG C EXIT PRESSURE IS 9 MPA END DEVICE DEVICE #2: SIMPLE HEAT LOAD COMMENT: THIS DEVICE WILL TEST ICAlel. IFIND=1 (DMMENT: THIS DEVICE WILL TEST ICALL=2. IFIND=I.2 COMMENT: THIS DEVICE WILL TEST ICALL=3. IFIND=1 COMMENT: THIS DEVICE WILL TEST ICALL=4. IFIND=1 INLET NODE NUMBER IS 3 ' EXIT NODE NUMBER IS 4 INLET TEMPERATURE IS 500 DEG C INLET PRESSURE IS 10 MPA EXIT TEMPERATURE IS 400 DEG C EXIT PRESSURE IS 9-MPA EXIT MASS FLOW RATE IS 1.0 KG/SEC END DEVICE “"- 224 TITLE LINE SIMPLE OPEN FEED WATER HEATER MODEL TEST ETD TITLE NUMBER OF NODES IS 18 HIGH TEMPERATURE RESERVOIR IS 500 DEG C LOW TEMPERATURE RESERVOIR IS 25.0 DEG C DEAD STATE TEMPERATURE IS 25.0 DEG C DEAD STATE PRESSURE IS 101 KPA GENERATOR MECHANICAL LOSS IS 0.0 MW GETERATOR ELECTRICAL IOSS IS 0.0 MW DEVICE #1: SIMPLE OFW HEATER COMMENT: THIS DEVICE WILLTES'T ICALL=1. IFIND=I.2.3 COMMENT: THIS DEVICE WILL TEST ICALL=2. IFIND=1.4 COMMENT: THIS DEVICE WILL TEST ICALL=3. IFIND=1 COMMENT: THIS DEVICE WILL TEST ICALL=4. IFIND=1 FEED WATER EXIT NODE NUMBER IS 1 EXTRACTION INLET NODE NUMBER IS 2 FEED WATER INLET NODE NUMBER IS 3 FEED WATER EXIT PRESSURE IS 6.0 MPA EXTRACTION INLET TEMPERATURE IS 430.6 DEG C FEED WATER INLET TEMPERATURE IS 251.07 DEG C FEED WATER IITIET MASS FLOW IS 23.5837 KG/SEC END DEVICE DEVICE #2: SIMPLE OFW HEATER COMMENT: THIS DEVICE WILL TEST ICALL=1. IFIND=1.2.4 COMMENT: THIS DEVICE WILL TEST ICALL=2. IFIND=1.4 COMMENT: THIS DEVICE WILL TEST ICALL=3. IFIND=1 COMMENT: THIS DEVICE WILL TEST ICALL=4. IFIND=1 FEED WATER EXIT NODE NUMBER IS 4 EXTRACTION INLET NODE NUMBER IS 5 FEED WATER INLET NODE NUMBER IS 6 FEED WATER INLETPRESSURE IS 6.0 MPA EXTRACTION INLET TEMPERATURE IS 430.6 DEG C EXTRACTION INLET MASS FLOW IS 1.4163 KG/SEC FEED WATER INLET TEMPERATURE IS 251.07 DEG END DEVICE DEVICE #3: SIMPLE OFW HEATER COMMENT: THIS DEVICE WILLTEST ICALL=1. IFIND=1” COMMENT: THIS DEVICE WILL TEST ICALL=2. IFIND=1.4 COMMETT: THIS DEVICE WILL TEST ICALL=3. IFIND=1 COMMENT: THIS DEVICE WILL TEST ICALL=4, IFIND=1 FEED WATER EXIT NODE NUMBER IS 7 EXTRACTION INLET NODE NUMBER IS 8 FEED WATER INLET NODE NUMBER IS 9 FEED WATER EXIT MASS FLOW RATE '18 25.0 KGISEC EXTRACTION INLET PRESSURE IS 6.0 MPA EXTRACTION INLET TEMPERATURE IS 430.6 DEG C FEED WATER INLETTEMPERATURE IS 251.07 DEG C END DEVICE 225 DEVICE #4: SIMPLE OFW HEATER COMMENT: THIS DEVICE WILL TEST ICALL=1. IFIND=I.2.4 COMMETT: THIS DEVICE WILL TEST ICALL=2. IFIND=2.3.4 COMMENT: THIS DEVICE WILL TEST ICALL-=3. IFIND=1 COMMENT: THIS DEVICE WILL TEST ICALL;4. IFIND=1 FEED WATER EXIT NODE NUMBER IS 10 EXTRACTION INLET NODE NUMBER IS 11 FEED WATER INLET NODE NUMBER IS 12 FEED WATER EXIT MASS FLOW IS 25.0000 KG/SEC EXTRACTION INLET PRESSURE 18 6.0 MPA EKTRACIION INLET TEMPERATURE IS 430.6 DEG C FEED WATER INLET MASS FLOW IS 23.5837 KGISEC END DEVICE DEVICE #5: SIMPLE OFW HEATER COMMENT: THIS DEVICE WTLLTEST ICALL=1. IFINIkl.2.4 COMMETT: THIS DEVICE WILL TEST ICALL=2. IFIND=2.3.4 COMMENT: THIS DEVICE WILL TEST ICALL=3. IFIND=1 COMMENT: THIS DEVICE WILL TEST ICALL=4. IFIND=1 FEED WATER EXIT NODE NUMBER IS 13 EXTRACTION INLET NODE NUMBER IS 14 FEED WATER INLET NODE NUMBER IS 15 FEED WATER INLET PRESSURE 18 6.0 MPA FEED WATER INLET TEMPERATURE IS 251.07 DEG C FEED WATER EXIT MASS FLOW IS 25.0000 KG/SEC EXTRACTION INLET MASS FLOW IS 1.4163 KG/SEC END DEVICE DEVICE #6: SIMPLE OFW HEATER COMMENT: THIS DEVICE WTLLTEST ICALL=1. IFIND=I.2.4 COMMETT: THIS DEVICE WILL TEST ICALL=2. IFIND=2.3.4 COMMENT: THIS DEVICE WILL TEST ICALL=3. IFIND=1 COMMENT: THIS DEVICE WILL TEST ICALL=4. IFIND=1 FEED WATER EXIT NODE NUMBER IS 16 EXTRACTION INLET NODE NUMBER IS 17 FEED WATER INLET NODE NUMBER IS 18 EXTRACTION INLET PRESSURE IS 6.0 MPA EXTRACTION INLET TEMPERATURE IS 430.6 DEG C EXTRACTION INLET MASS FLOW IS 1.4163 KG/SEC FEED WATER INLET TEMPERATURE IS 251.07 DEG C FEED WATER INLET MASS FLOW IS 23.5837 KGISEC FEED WATER EXIT IS NOT SATURATED ETD DEVICE 226 TITLE LWE SIMPLE CLOSED FEED WATER HEATER MODEL TEST ETD TITLE NUMBER OF NODES IS 19 HIGH TEMPERATURE RESERVOIR IS 500 DEG C LOW TEMPERATURE RESERVOIR IS 25.0 DEG C DEAD STATE TEMPERATURE IS 25.0 DEG C DEAD STATE PRESSURE IS 101 KPA GETERATOR MECHANICAL LOSS IS 0.0 MW GETERATOR ELECTRICAL LOSS IS 0.0 MW DEVICE #1: SIMPLE STEAM TRAP CFW COMMETT: THIS DEVICE WILL TEST ICALLzl. IFWD=1.2.3.4,5 COMMENT: THIS DEVICE WILL TEST ICALL=2. IFWD=1.2.3.4 COMMENT: THIS DEVICE WILL TEST ICALL=3. IFWD=1 COMMENT: THIS DEVICE WILL TEST ICALL=4. IFWD=1 FEED WATER INLET NODE NUMBER IS 1 FEED WATER EXIT NODE NUMBER IS 2 EXTRACTION INLET NODE NUMBER IS 3 DRAIN WLET #1 NODE NUMBER IS 4 DRAW EXIT NODE NUMBER IS 5 FEED WATER WLET TEMPERATURE IS 80 DEG C FEED WATER INLET PRESSURE IS 25 MPA FEED WATER WLET MASS FLOW RATE IS 10 KG/SEC FEED WATER PRESSURE LOSS LS 0.25 MPA EXTRACTION WLET PRESSURE IS 10.0 MPA EXTRACTION INLET TEMPERATURE LS 320 DEG C EXTRACTION PRESSURE LOSS IS 0.5 MPA DRAIN INLET #1 TEMPERATURE IS 140 DEG C DRAW INLET #1 MASS FLOW IS 1.0 KG/SEC TERMINAL TEMPERATURE DIFFERENCE IS 111.06 DEG C APPROACH TEMPERATURE DIFFERENCE IS 20.0 DEG C END DEVICE DEVICE #2: SIMPLE STEAM TRAP CFW COMMENT: THIS DEVICE WILL TEST ICALL=1. IFWD=1.2.3.4.5 COMMENT: THIS DEVICE WILL TEST ICALL=2. IFWD=1.2.3.4 COMMENT: THIS DEVICE WILL TEST ICALL=3. IFWD=1 COMMENT: THIS DEVICE WILL TEST ICALL-4, IFWD=1 FEED WATER INLET NODE NUMBER IS 6 FEED WATER EXIT NODE NUMBER IS 7 EXTRACTION INLET NODE NUMBER IS 8 DRAIN WLET #1 NODE NUMBER IS 9 DRAIN INLET #2 NODE NUMBER IS 10 DRAW WLET #3 NODE NUMBER IS 11 DRAW WLET #4 NODE NUMBER IS 12 DRAW WLET #5 NODE NUMBER IS 13 DRAW WLET #6 NODE NUMBER IS 14 DRAW WLET #7 NODE NUMBER IS 15 DRAW WLET #8 NODE NUMBER IS 16 DRAW WLET #9 NODE NUMBER IS 17 DRAW WLET #10 NODE NUMBER IS 18 DRAW EXIT NODE NUMBER IS 19 FEED WATER WLET TEMPERATURE IS 80 DEG C FEED WATER EXIT PRESSURE LS 2.25 MPA FEED WATER EXIT MASS FLOW RATE IS 10 KGISEC FEED WATER PERCENTAGE PRESSURE LOSS IS 10 PERCENT EXTRACTION WLET TEMPERATURE IS 320 DEG C EXTRACTION PERCENTAGE PRESSURE LOSS IS 5 PERCETT DRAW WLET #1 TEMPERATURE 18140 DEG C DRAW WLET#I MASS FLOW IS 0.1 KG/SEC DRAW WLET #2 TEMPERATURE IS 140 DEG C DRAW WLET#2 MASS FLOW IS 0.1 KG/SEC 227 DRAW WLET #3 TEMPERATURE IS 140 DEG C DRAW WLET #3 MASS FLOW IS 0.1 KG/SEC DRAW WLET #4 TEMPERATURE IS 140 DEG C DRAW WLET #4 MASS FLOW IS 0.1 KG/SEC DRAW WLET #5 TEMPERATURE IS 140 DEG C DRAW WLET #5 MASS FLOW IS 0.1 KGISEC DRAW WLET #6 TEMPERATURE IS 140 DEG C DRAW WLET #6 MASS FLOW IS 0.1 KG/SEC DRAW WLET #7 TEMPERATURE IS 140 DEG C DRAW WLET #7 MASS FLOW 15 0.1 KG/SEC DRAW WLET #8 TEMPERATURE LS 140 DEG C DRAW WLET #8 MASS FLOW IS 0.1 KG/SEC DRAW WLET #9 TEMPERATURE LS 140 DEG C DRAW WLET #9 MASS FLOW IS 0.1 KG/SEC DRAW WLET #10 TEMPERATURE IS 140 DEG C DRAW WLET #10 MASS FLOW IS 0.1 KG/SEC DRAW EXIT PRESSURE IS 9.5 MPA TERMWAL TEMPERATURE DIFFERENCE 18111.06 DEG C APPROACH TEMPERATURE DIFFERENCE IS 20.0 DEG C ETD DEVICE 228 TITLE IWE SIMPLE SEPARATOR MODEL TEST END TITLE LWE NUMBER OF NODES IS 9 HIGH TEMPERATURE RESERVOIR IS 500.0 DEG C LOW TEMPERATURE RESERVOIR IS 25.0 DEG C DEAD STATE TEMPERATURE IS 25.0 DEG C DEAD STATE PRESSURE IS 101 KPA GENERATOR MECHANICAL IOSS 18 0.0 MW GENERATOR ELECTRICAL LOSS LS 0.0 MW DEVICE #1: SIMPLE MOISTURE SEPARATOR COMMETT: THIS DEVICE WILL TEST ICALL=1. IFWD=1.2 COMMENT: THIS DEVICE WILL TEST ICALL=2. IFWD=1 - COMMETT: THIS DEVICE WILL TEST ICALL-=3. IFWD=1 COMMETT: THIS DEVICE WILL TEST ICALL=4. IFWD=1 SEPARATOR WLET NODE NUMBER IS 1 SEPARATOR VAPOR EXIT NODE NUMBER IS 2 SEPARATOR CON DENSATE EXIT NODE NUMBER IS 3 SEPARATOR WLET PRESSURE LS 1.00 MPA SEPARATOR WLET QUALITY IS 50 PERCENT SEPARATOR WLET FLUID PHASE IS A 2 PHASE MIXTURE SEPARATOR WLET MASS FLOW IS 1.0 KGISEC SEPARATOR PRESSURE LOSS IS 0.1 MPA END DEVICE DEVICE #2: SIMPLE MOISTURE SEPARATOR COMMENT: THIS DEVICE WILL TEST ICALL=1. IFWD=1.2 COMMENT: THIS DEVICE WILL TEST ICALL=2. IFWD=1 COMMENT: THIS DEVICE WILL TEST ICALL=3. IFWD=1 COMMENT: THIS DEVICE WILL TEST ICALL=4. IFWD=1 SEPARATOR WLET NODE NUMBER IS 4 SEPARATOR VAPOR EXIT NODE NUMBER IS 5 SEPARATOR CONDETSATE EXIT NODE NUMBER IS 6 SEPARATOR WLET PRESSURE IS 1.00 MPA SEPARATOR WLET TEMPERATURE IS 500 DEG C SEPARATOR WLET MASS FLOW IS 1.0 KGISEC SEPARATOR SEPERATOR PERCENTAGE PRESSURE LOSS IS 10% ETD DEVICE DEVICE #3: SIMPLE MOISTURE SEPARATOR COMMETT: THIS DEVICE WILL TEST ICALL;1. IFWD=1.2 COMMENT: TIIIS DEVICE WILL TEST ICALL=2. IFWD=1 COMMETT: THIS DEVICE WILL TEST-ICALL=3. IFWD=1 COMMENT: THIS DEVICE WILL TEST ICALL-=4. IFWD=1 SEPARATOR WLET NODE NUMBER IS 7 SEPARATOR VAPOR EXIT NODE NUMBER IS 8 SEPARATOR CONDENSATE EXIT NODE NUMBER IS 9 SEPARATOR WLET PRESSURE LS 1.00 MPA SEPARATOR WLET TEMPERATURE IS 100 DEG C SEPARATOR WLET MASS FLOW IS 1.0 KG/SEC SEPARATOR SEPERATOR PERCETT AGE PRESSURE IOSS IS 10% ETD DEVICE 229 TITLE LWE SIMPLE REHEATER MODEL TEST END TITLE LWE NUMBER OF NODES: 18 HIGH TEMPERATURE RESERVOIR IS 500. 0 DE} C LOW TEMPERATURE RESERVOIR IS 25 .0 DEG C DEAD STATE TEMPERATURE IS 25.0 DEG C DEAD STATE PRESSURE IS 101 KPA GENERATOR MECHANICAL IOSS IS 0.0 MW GENERATOR ELECTRICAL LOSS IS 0.0 MW COMMENT: THESE 3 DEVICES WILL TEST SREH ICALL=1. FWD=1.2.3.4.6 COMMENT: THESE 3 DEVICES WILL TEST SREH ICALL=2. IFWD=1.2.3 COMMENT: THESE 3 DEVICES WTLLTEST SREH ICALL;3. IFIND=1 COMMENT: THESE 3 DEVICES WILL TEST SREH ICALL=4. IFIND=1 DEVICE #1: SIMPLE JUNCTION WLET #1 NODE NUMBER IS 1 EXIT #1 NODE NUMBER IS 2 EXIT #2 NODE NUMBER IS 3 WLET #1 MASS FLOW RATE IS 91 KGISEC WLET #1 TEMPERATURE IS 300 DEG C WLET #1 PRESSURE IS 1.5 MPA EXIT #1 FLOW FRACTION IS 98 .9011 PERCENT ETD DEVICE DEVICE #2: SIMPLE HEAT LOAD WLET NODE NUMBER IS 2 EXIT NODE NUMBER IS 4 EXIT TEMPERATURE IS 180 DEG C EXIT PRESSURE IS 1.0 MPA ETD DEVICE DEVICE #3: SIMPLE REHEATER CYCLE STEAM WLET NODE NUMBER IS 4 CYCLE STEAM EXIT NODE NUMBER IS 5 REHEAT STEAM WLET NODE NUMBER IS 3 REHEAT STEAM EXIT NODE NUMBER IS 6 FLOW FRACTION CONTROLED BY JUNCTION DEVICE NUMBER 1 CYCLE STEAM PRESSURE LOSS LS 0.10 MPA REHEAT STEAM PRESSURE IOSS LS 0.15 MPA TERMWAL TEMPERATURE DIFFERENCE IS 10.0 DEG C ETD DEVICE COMMENT: THESE 3 DEVICES WILL TEST SREH ICALL=1. IFWD=1.2.3.4 COMMENT: THESE 3 DEVICES WILL TEST SREH ICALL=2. IFWD=1.2.3 COMMENT: THESE 3 DEVICES WILL TEST SREH ICALL-=3. IFWD=1 COMMENT: THESE 3 DEVICES WTLLTEST SREH ICALL=4. IFIND=1 DEVICE #4: SIMPLE JUNCTION WLET #1 NODE NUMBER IS 7 EXIT #1 NODE NUMBER IS 8 EXIT #2 NODE NUMBER IS 9 WLET #1 MASS FLOW RATE IS 91 KG/SEC EXIT #2 TEMPERATURE IS 300 DEG C EXIT #1 FLOW FRACTION IS 98.9011 PERCENT ETD DEVICE DEVICE #5: SIMPLE HEAT LOAD WLET NODE NUMBER IS 8 ELIT NODE NUMBER IS 10 EXIT TEMPERATURE IS 180 DEG C END DEVICE 230 DEVICE #6: SIMPLE REHEATER CYCLE STEAM WLET NODE NUMBER IS 10 CYCLE STEAM EXIT NODE NUMBER IS 12 REHEAT STEAM WLET NODE NUMBER IS 9 REHEAT STEAM EXIT NODE NUMBER IS 11 FLOW FRACTION CONTROLED BY JUNCTION DEVICE NUMBER 4 CYCLE STEAM EXIT PRESSURE IS 0.9 MPA CYCLE STEAM PERCENTAGE PRESSURE LOSS IS 10.0 PERCENT REHEAT STEAM EXIT PRESSURE LS 1.35 MPA REHEAT STEAM PRECENTAGE PRESSURE LOSS 18 10.0 PERCENT TERMINAL TEMPERATURE DIFFERENCE IS 10.0 DEG C END DEVICE COMMETT: THESE 3 DEVICES WILL TEST SREH ICALL=1. IFWD=1.2.3.5 COMMETT: TI-LESE 3 DEVICES WILL TEST SREH ICALL=2. IFWD=1.2.3 COMMENT: THESE 3 DEVICES WTLLTEST SREH ICALL=3. IFWD=1 COMMENT: THESE 3 DEVICES WTLLTEST SREH ICALL=4. IFWD=1 DEVICE #7 : SIMPLE JUNCTION WLET #1 NODE NUMBER IS 13 EXIT #1 NODE NUMBER IS 14 EXIT #2 NODE NUMBER IS 15 WLET #1 MASS FLOW RATE IS 91 KG/SEC WLET #1 TEMPERATURE LS 300 DEG C WLET#I PRESSURE IS 1.5 MPA , ' EXIT #1 FLOW FRACTION IS 98.9011 PERCENT ETD DEVICE DEVICE #8: SIMPLE HEAT LOAD WLET NODE NUMBER IS 14 EXIT NODE NUMBER IS 16 EXIT TEMPERATURE IS 180 DEG C EXIT PRESSURE IS 1.0 MPA END DEVICE DEVICE #9: SIMPLE REHEATER CYCLE STEAM WLET NODE NUMBER IS 16 CYCLE STEAM EXIT NODE NUMBER IS 18 REHEAT STEAM WLET NODE NUMBER IS 15 REHEAT STEAM EXIT NODE NUMBER IS 17 FLOW FRACTION CONTROLED BY JUNCTION DEVICE NUMBER 7 CYCLE STEAM PERCENTAGE PRESSURE LOSS IS 10.0 PERCENT REHEAT STEAM EXIT TEMPERATURE IS 193 DEG C REHEAT STEAM EXIT IS NOT A SATURATED LIQUID REHEAT STEAM PRECENTAGE PRESSURE LOSS IS 10.0 PERCENT TERMWAL TEMPERATURE DIFFERENCE IS 10.0 DEG C ETD DEVICE Appendix C: RANKINE 3.0 output files for individual device verification 231 RANKINE 3.0: A steam power plant computer simulation W .Copyright 1994 .A. Thelen, CO". Somerton t**********itii**tfi*******iit*t*t* TITLE i*titiitittii*************t******* SIMPLE BOILER MODEL TEST i*******i***************ti****** NODE DATA ******************************** NODE T(C) P(MPa) L Q S(RJ/KG/K) H(KJ/KG) V(M*3/KG) M(KG/S) A(KJ/KG) 1 100.00 20.0000 1 ***** 1.2834 433.79 .00104 5.0000 55.48 2 600.00 18.0000 3 ***** 6.5690 3554.01 .02033 5.0000 1599.81 3 100.00 20.0000 1 ***** 1.2834 433.79 .00104 5.0000 55.48 4 600.00 18.0000 3 ***** 6.5690 3554.01 .02033 5.0000 1599.81 5 100.00 20.0000 1 ***** 1.2834 433.79 .00104 5.0000 55.48 6 600.00 18.0000 3 ***** 6.5690 3554.01 .02033 5.0000 1599.81 7 100.00 20.0000 1 ***** 1.2834 433.79 .00104 5.0000 55.48 8 600.00 18.0000 3 ***** 6.5690 3554.01 .02033 5.0000 1599.81 9 100.00 20.0000 1 ***** 1.2834 433.79 .00104 5.0000 55.48 10 600.00 18.0000 3 ***** 6.5690 3554.01 .02033 5.0000 1599.81 11 100.00 20.0000 1 ***** 1.2834 433.79 .00104 5.0000 55.48 12 600.00 18.0000 3 ***** 6.5690 3554.01 .02033 5.0000 1599.81 13 100.00 20.0000 1 ***** 1.2834 433.79 .00104 5.0000 55.48 14 600.00 18.0000 3 ***** 6.5690 3554.01 .02033 5.0000 1599.81 15 100.00 20.0000 1 ***** 1.2834 433.79 .00104 5.0000 55.48 16 600.00 18.0000 3 ***** 6.5690 3554.01 .02033 5.0000 1599.81 17 100.00 20.0000 1 ***** 1.2834 433.79 .00104 5.0000 55.48 18 600.00 18.0000 3 ***** 6.5690 3554.01 .02033 5.0000 1599.81 19 100.00 20.0000 1 ***** 1.2834 433.79 .00104 5.0000 55.48 20 600.00 18.0000 3 ***** 6.5690 3554.01 .02033 5.0000 1599.81 21 100.00 20.0000 1 ***** 1.2834 433.79 .00104 5.0000 55.48 22 600.00 18.0000 3 ***** 6.5690 3554.01 .02033 5.0000 1599.81 **fi***t*fi**********i* DEVICE DATA (DEVICE BEFORE NODE) ********************* NODE REV. WRK ACT. WRK IRREV HEAT X-FER MASS ERROR ENERGY ERROR (KW) (KW) (KW) (KW) (KG/s) (KW) 1 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 2 7474.36 .00 7474.36 15601.11 .000 .000 3 -1.00 -1.00 -1.00 —1.00 -1.000 -1.000 ‘4 7474.36 .00 7474.36 15601.11 .000 .000 5 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 6 7474.36 .00 7474.36 15601.11 .000 .000 7 -1.00 -1;oo -1.00 -1.00 -1.000 -1.000 6 7474.36 .00 7474.36 15601.11 .000 .000 9 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 10 7474.36 .00 7474.36 15601.11 .000 .000 11 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 12 7474.36 .00 7474.36 15601.11 .000 .000 13 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 14 7474.36 .00 7474.36 15601.11 .000 .000 15 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 16 7474.36 .00 7474.36 15601.11 .000 .000 17 -1.00 —1.00 -1.00 -1.00 -1.000 -1.000 18 7474.36 .00 7474.36 15601.11 .000 .000 19 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 20 7474.36 .00 7474.36 15601.11 .000 .000 21 —1.00 —1.00 -1.00 -1.00 -1.000 -1.000 22 7474.36 .00 7474.36 15601.11 .000 .000 232 ************t*fi**i*t**i**titi‘ki SYSTEM DATA itit*‘kitttii’i'iiifiifi'kittti'tititi’i TOTAL MASS FLOW RATE EXITING SYSTEM: 55.0000 KG/SEC TOTAL MASS FLOW RATE ENTERING SYSTEM: 55.0000 KG/SEC TOTAL ENTHALPY FLOW RATE EXITING SYSTEM: 195470.7000 KW TOTAL ENTHALPY FLOW RATE ENTERING SYSTEM: 23858.4600 KW TOTAL HEAT AND WORK ENTERING SYSTEM: 171612.2000 KW BOILER HEAT (DEVICE O 1): 171612.2000 KW TOTAL BOILER HEAT: 171612.2000 KW TOTAL HEAT LOAD HEAT: .0000 KW TOTAL PIPE ENERGY LOSSES: .0000 KW NET WORK TO GENERATORS: .0000 KW TOTAL PUMP WORK: .0000 KW GENERATOR MECHANICAL LOSSES: .0000 KW GENERATOR ELECTRICAL LOSSES: .0000 KW NET ELECTRICAL POWER: .0000 KW SYSTEM HEAT RATE: -1.0000 BTU/KW’HR CARNOT CYCLE EFFICIENCY: 65.8535 PERCENT 1$T LAW EFFICIENCY: .0000 PERCENT 2ND LAW EFFICIENCY: 69.0844 PERCENT 2ND LAW EFFECTIVENESS: . -100.0000 PERCENT 233 RANKINE 3.0: A steam power plant computer simulation Copyright 1994 W.A. Thelen, C.W. Somerton it**i************************i**it TITLE *t******************************t** SIMPLE TURBINE MODEL TEST ****************t*************** NODE DATA i**i*****t************t********** NODE T(C) P(MPa) L Q S(KJ/KG/K) H(KJ/KG) V(M*3/KG) M(KG/S) A(KJ/KG) 1 600.00 20.0000 3 ***** 6.5052 3536.61 .01808 5.0000 1601.44 2 481.53 10.0000 3 ***** 6.5362 3327.14 .03167 1.0000 1382.72 3 382.71 5.0000 3 ***** 6.5832 3153.98 .05586 2.0000 1195.54 4 99.63 .1000 2 .940 6.9952 2539.67 1.59208 2.0000 458.40 *titttttttttttittitit DEVICE DATA (DEVICE BEFORE NODE) *ttttttttitttttitttti NODE REV. WRK ACT. WRK IRREV HEAT X-FER MASS ERROR ENERGY ERROR (KW) (KW) (KW) (KW) (KG/S) (KW) 1 -1.00 ' -1.00 -1.00 -1.00 -1.000 -1.000 2 1093.61 1047.36 46.25 .00 .000 .000 3 748.72 692.64 56.08 .00 .000 .000 4 1474.26 1228.61 245.65 .00 .000 .000 ******************************* SYSTEM DATA ***tti************************** TOTAL TOTAL TOTAL TOTAL TOTAL TOTAL TOTAL TOTAL MASS FLOW RATE EXITING SYSTEM: MASS FLOW RATE ENTERING SYSTEM: ENTHALPY FLOW RATE EXITING SYSTEM: ENTHALPY FLOW RATE ENTERING SYSTEM: HEAT AND WORK ENTERING SYSTEM: -BOILER HEAT: HEAT LOAD HEAT: PIPE ENERGY LOSSES: TURBINE WORK (DEVICE i 1): NET WORK TO GENERATORS: TOTAL PUMP WORK: GENERATOR MECHANICAL LOSSES: GENERATOR ELECTRICAL LOSSES: NET ELECTRICAL POWER: SYSTEM HEAT RATE: CARNOT CYCLE EFFICIENCY: 1$T LAW EFFICIENCY: 2ND LAW EFFICIENCY: 2ND LAW EFFECTIVENESS: 5.0000 5.0000 14714.4400 17683.0500 -2968.6050 .0000 .0000 .0000 2968.6050 2968.6050 .0000 10.0000 5.0000 2953.6050 -1.0000 65.8535 -100.0000 95.6541 -100.0000 KG/SEC KG/SEC §§§§ §§ §§§ 2%?! BTU/KW*HR PERCENT PERCENT PERCENT PERCENT 234 RANKINE 3.0: A steam power plant computer simulation. Copyright 1994 W.A. Thelen, C.W. Somerton it***i*******************iiiiittit TITLE *ii******************************** SIMPLE PUMP MODEL TEST i************************tfitiiti NODE DATA tit**i************************i** NODE T(C) P(MPa) L Q S(KJ/KG/K) H(KJ/KG) V(M‘3/KG) M(KG/S) A(KJ/KG) 1 130.00 .5000 1 ***** 1.6331 546.21 .00107 1.0000 63.64 '2 131.15 10.0000 1 ***** 1.6331 557.57 .00107 1.0000 74.99 3 167.98 1.0000 1 ***** 2.0191 710.08 .00111 1.0000 112.42 4 170.00 10.0000 1 ***** 2.0253 723.88 .00111 1.0000 124.37 *ttttttittttitttttttt DEVICE DATA (DEVICE BEFORE NODE) tittttttttttttttttttt NODE REV. WRK ACT. WRK IRREV HEAT X-FER MASS ERROR ENERGY ERROR (KW) (KW) (KW) (KW) (KG/S) (KW) 1 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 2 -11.35 -11.35 .00 .00 .000 .000 3 -1.00 -1.00 -1.00 -l.00 -1.000 -1.000 4 -11.94 -13.80 1.85 .00 .000 .000 *tiittttttittttttittttsi*titttt SYSTEM DATA it*ititttttt******************** TOTAL MASS FLOW RATE EXITING SYSTEM: TOTAL MASS FLOW RATE ENTERING SYSTEM: 2.0000 KG/SEC 2.0000 KG/SEC TOTAL ENTHALPY FLOW RATE EXITING SYSTEM: 1281.4440 TOTAL ENTHALPY FLOW RATE ENTERING SYSTEM: 1256.2930 TOTAL HEAT AND WORK ENTERING SYSTEM: 25.1510 TOTAL BOILER HEAT: .0000 TOTAL HEAT LOAD HEAT: .0000 TOTAL PIPE ENERGY LOSSES: .0000 NET WORK TO GENERATORS: KW KW KW KW KW KW .0000 KW KW KW KW KW KW KW PUMP WORK (DEVICE O 1): -11.3542 PUMP WORK (DEVICE I 2): -13.7968 TOTAL PUMP WORK: -25.1510 GENERATOR MECHANICAL LOSSES: .0000 GENERATOR ELECTRICAL LOSSES: .0000 NET ELECTRICAL POWER: -25.1510 SYSTEM HEAT RATE: CARNOT CYCLE EFFICIENCY: IST LAW EFFICIENCY: 2ND LAW EFFICIENCY: 2ND LAW EFFECTIVENESS: -1.0000 BTU/KW*HR 61.4370 PERCENT -100.0000 99.0782 -100.0000 PERCENT 235 RANKINE 3.0: A steam power plant computer simulation W.A. Thelen, Copyright 1994 CO“. Somerton ***********i********************** TITLE *************************t*******it SIMPLE PIPE MODEL TEST *fi******i***********t*****i***** NODE DATA *i******************************* NODE T(C) P(MPa) L Q S(KJ/KG/K) H(KJ/KG) V(M“3/KG) M(KG/S) A(KJ/KG) 1 500.00 10.0000 3 ***** 6.5984 3374.66 .03275 1.0000 1411.69 2 456.09 9.0000 3 ***** 6.5096 3274.66 .03389 1.0000 1338.17 3 500.01 10.0000 3 ***** 6.5984 3374.69 .03275 1.0000 1411.71 4 456.10 9.0000 3 ***** 6.5096 3274.69 .03390 1.0000 1338.19 5 499.94 10.0000 3 ***** 6.5982 3374.51 .03274 1.0000 1411.60 6 456.09 9.0000 3 ***** 6.5096 3274.66 .03389 1.0000 1338.17 7 500.00 10.0000 3 ***** 6.5984 3374.66 .03275 1.0000 1411.69 8 456.14 9.0000 3 ***** 6.5098 3274.80 .03390 1.0000 1338.26 9 500.00 10.0000 3 ***** 6.5984 3374.66 .03275 1.0000 1411.69 10 456.14 9.0000 3 ***** 6.5098 3274.80 .03390 1.0000 1338.25 11 500.00 10.0000 3 ***** 6.5984 3374.66 .03275 1.0000 1411.69 12 456.09 -9.0000 3 ***** 6.5096 3274.66 .03389 1.0000 1338.17 ********************* DEVICE DATA (DEVICE BEFORE NODE) ********************* NODE REV. WRK ACT. WRK IRREV HEAT X-FER MASS ERROR ENERGY ERROR (KW) (KW) (KW) (KW) (KG/S) (KW) 1 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 2 73.52 .00 73.52 -100.00 .000 .000 3 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 4 73.52 .00 73.52 -100.00 .000 .000 5 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 6 73.43 .00 73.43 -99.85 .000 .000 7 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 8 73.43 .00 73.43 -99.86 .000 .000 9 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 10 73.44 .00 73.44 -99.86 .000 .000 11 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 12 73.52 .00 73.52 -100.00 .000 .000 *tttttttti*ttt*i*************t* SYSTEM DATA ******************************** TOTAL TOTAL TOTAL TOTAL TOTAL TOTAL TOTAL TOTAL MASS FLOW RATE EXITING SYSTEM: MASS FLOW RATE ENTERING SYSTEM: ENTHALPY FLOW RATE EXITING SYSTEM: ENTHALPY FLOW RATE ENTERING SYSTEM: HEAT AND WORK ENTERING SYSTEM: BOILER HEAT: HEAT LOAD HEAT PIPE ENERGY LOSSES: NET WORK TO GENERATORS: TOTAL PUMP WORK: GENERATOR MECHANICAL LOSSES: GENERATOR ELECTRICAL LOSSES: NET ELECTRICAL POWER: SYSTEM HEAT RATE: 6.0000 6.0000 19648.2700 20247.8400 -59 -59 9.5688 .0000 .0000 9.5688 .0000 .0000 .0000 .0000 .0000 1.0000 §§§§ ii §§§ §§§ BTU/KW*HR 236 CARNOT CYCLE EFFICIENCY: 61.4370 PERCENT 1$T LAW EFFICIENCY: -100.0000 PERCENT 2ND LAW EFFICIENCY: 94.7951 PERCENT 2ND LAW EFFECTIVENESS: -100.0000 PERCENT 237 RANKINE 3.0: A steam power plant computer simulation W.A. Copyright 1994 Thelen, C.W. Somerton ********************************** TITLE t****t*******tt*******t***tt******* SIMPLE JUNCTION MODEL TEST it*******tttitittttttttttttttiit NODE DATA ********************************* NODE T(C) P(MPa) L Q S(KJ/KG/K) H(KJ/KG) V(M‘3/KG) M(KG/S) A(KJ/KG) 1 445.00 5.0000 3 ***** 6.8027 3304.57 .06274 .3100 1280.70 2 445.00 5.0000 3 ***** 6.8027 3304.57 .06274 .2200 1280.70 3 445.00 5.0000 3 ***** 6.8027 3304.57 .06274 .4700 1280.70 4 445.00 5.0000 3 ***** 6.8027 3304.57 .06274 .4100 1280.70 5 445.00 5.0000 3 ***** 6.8027 3304.57 .06274 .5000 1280.70 6 445.00 5.0000 3 ***** 6.8027 3304.57 .06274 .0900 1280.70 7 445.00 5.0000 3 ***** 6.8027 3304.57 .06274 10.0000 1280.70 8 445.00 5.0000 3 ***** 6.8027 3304.57 .06274 2.0000 1280.70 9 445.00 5.0000 3 ***** 6.8027 3304.57 .06274 4.0000 1280.70 10 445.00 5.0000 3 ***** 6.8027 3304.57 .06274 4.0000 1280.70 11 445.00 5.0000 3 ***** 6.8027 3304.57 .06274 .4000 1280.70 12 445.00 5.0000 3 ***** 6.8027 3304.57 .06274 .2297 1280.70 13 445.00 5.0000 3 ***** 6.8027 3304.57 .06274 .3703 1280.70 14 445.00 5.0000 3 ***** 6.8027 3304.57 .06274 1.0000 1280.70 15 445.00 5.0000 3 ***** 6.8027 3304.57 .06274 10.0000 1280.70 16 445.00 5.0000 3 ***** 6.8027 3304.57 .06274 1.0000 1280.70 17 445.00 5.0000 3 ***** 6.8027 3304.57 .06274 1.0000 1280.70 18 445.00 5.0000 3 ***** 6.8027 3304.57 .06274 1.0000 1280.70 19 445.00 5.0000 3 ***** 6.8027 3304.57 .06274 1.0000 1280.70 20 445.00 5.0000 3 ***** 6.8027 3304.57 .06274 1.0000 1280.70 21 445.00 5.0000 3 ***** 6.8027 3304.57 .06274 1.0000 1280.70 22 445.00_ 5.0000 3 ***** 6.8027 3304.57 .06274 1.0000 1280.70 23 445.00 5.0000 3 ***** 6.8027 3304.57 .06274 1.0000 1280.70 24 445.00 5.0000 3 ***** 6.8027 3304.57 .06274 1.0000 1280.70 25 445.00 5.0000 3 ***** 6.8027 3304.57 .06274 1.0000 1280.70 ******t*********i**** DEVICE DATA (DEVICE BEFORE NODE) ********************* NODE REV. WRK ACT. WRK IRREV HEAT X-FER MASS ERROR ENERGY ERROR (KW) (KW) (KW) (KW) (KG/S) (KW) 1 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 2 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 3 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 4 .00 .00 .00 .00 .000 .000 5 .00 .00 .00 .00 .000 .000 6 .00 .00 .00 .00 .000 .000 7 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 8 .00 .00 .00 .00 .000 -.002 9 .00 .00 .00 .00 .000 .000 10 .00 .00 .00 .00 .000 .000 11 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 12 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 13 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 14 .00 .00 .00 .00 .000 .000 15 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 16 200 .00 .00 .00 .000 -.003 17 .00 .00 .00 .00 .000 .000 18 .00 .00 .00 .00 .000 .000 19 .00 .00 .00 .00 .000 .000 20 .00 .00 .00 .00 .000 .000 238 21 .00 .00 .00 .00 .000 .000 22 .00 .00 .00 .00 .000 .000 23 .00 .00 .00 .00 .000 .000 24 .00 .00 .00 .00 .000 .000 25 .00 .00 .00 .00 .000 .000 *tttttttttttiitttttttttt*tttttt SYSTEM DATA ********t*****t*****t*********** TOTAL MASS FLOW RATE EXITING SYSTEM: 22.0000 KG/SEC TOTAL MASS FLOW RATE ENTERING SYSTEM: 22.0000 KG/SEC TOTAL ENTHALPY FLOW RATE EXITING SYSTEM: 72700.6300 KW TOTAL ENTHALPY FLOW RATE ENTERING SYSTEM: 72700.6300 KW TOTAL HEAT AND WORK ENTERING SYSTEM: .0000 KW TOTAL BOILER HEAT: .0000 KW TOTAL HEAT LOAD MEAT: .0000 KW TOTAL PIPE ENERGY LOSSES: .0000 KW NET WORK TO GENERATORS: .0000 NW TOTAL PUMP WORK: , .0000 KW GENERATOR MECHANICAL LOSSES: .0000 KW GENERATOR ELECTRICAL LOSSES: .0000 KW NET ELECTRICAL POWER: .0000 KW SYSTEM HEAT RATE: -1.0000 BTU/KW*ER CARNOT CYCLE EFFICIENCY: 61.4370 PERCENT 1ST LAW EFFICIENCY: -100.0000 PERCENT 2ND LAW EFFICIENCY: 68.1818 PERCENT 2ND LAW EFFECTIVENESS: -100.0000 PERCENT ".A. 239 Copyright 1994 Thelen, C.W. Somerton RANKINE 3.0: A steam power plant computer simulation *i***iiiiititttttt******t***fi***** TITLE *********i*******************i***** SIMPLE CONDENSER MODEL TEST *******************it*****fi***** NODE DATA *****i****t*******************i** NODE T(C) P(MPa) L Q S(KJ/KG/K) H(KJ/KG) V(M‘3/KG) M(KG/S) A(KJ/KG) 1 151.84 .5000 4 ***** 1.8595 639.79 .00109 10.0000 89.73 2 200.00 .5000 3 ***** 7.0598 2855.58 .42513 10.0000 755.03 3' 151.84 .5000 4 ***** 1.8595 639.79 .00109 10.0000 89.73 4 200.00 .5000 3 ***** 7.0598 2855.58 .42513 5.0000 755.03 5 200.00 .5000 3 ***** 7.0598 2855.58 .42513 5.0000 755.03 6 151.84 .5000 4 ***** 1.8595 639.79 .00109 9.9981 89.73 7 200.00 .5000 3 ***** 7.0598 2855.58 .42513 .3703 755.03 8 200.00 .5000 3 ***** 7.0598 2855.58 .42513 .3703 755.03 9 200.00 .5000 3 ***** 7.0598 2855.58 .42513 .3703 755.03 10 200.00 .5000 3 ***** 7.0598 2855.58 .42513 .3703 755.03 11 200.00 .5000 3 ***** 7.0598 2855.58 .42513 .3703 755.03 12 200.00 .5000 3 ***** 7.0598 2855.58 .42513 .3703 755.03 13 200.00 .5000 3 ***** 7.0598 2855.58 .42513 .3703 755.03 14 200.00 .5000 3 ***** 7.0598 2855.58 .42513 .3703 755.03 15 200.00 .5000 3 ***** 7.0598 2855.58 .42513 .3703 755.03 16 200.00 .5000 3 ***** 7.0598 2855.58 .42513 .3703 755.03 17 200.00 .5000 3 ***** 7.0598 2855.58 .42513 .3703 755.03 18 200.00 .5000 3 ***** 7.0598 2855.58 .42513 .3703 755.03 19 200.00 .5000 3 ***** 7.0598 2855.58 .42513 .3703 755.03 20 200.00 .5000 3 ***** 7.0598 2855.58 .42513 .3703 755.03 21 200.00 .5000 3 ***** 7.0598 2855.58 .42513 .3703 755.03 22 200.00 .5000 3 ***** 7.0598 2855.58 .42513 .3703 755.03 23 200.00 .5000 3 ***** 7.0598' 2855.58 .42513 .3703 755.03 24 200.00 .5000 3 ***** 7.0598 2855.58 .42513 .3703 755.03 25 200.00 .5000 3 ***** 7.0598 2855.58 .42513 .3703 755.03 26 200.00 .5000 3 ***** 7.0598 2855.58 .42513 .3703 755.03 27 200.00 .5000 3 ***** 7.0598 2855.58 .42513 .3703 755.03 28 200.00 .5000 3 ***** 7.0598 2855.58 .42513 .3703 755.03 29 200.00 .5000 3 ***** 7.0598 2855.58 .42513 .3703 755.03 30 200.00 .5000 3 ***** 7.0598 2855.58 .42513 .3703 755.03 31 200.00 .5000 3 ***** 7.0598 2855.58 .42513 .3703 755.03 32 200.00 .5000 3 ***** 7.0598 2855.58 .42513 .3703 755.03 33 200.00 .5000 3 ***** 7.0598 2855.58 .42513 .3703 755.03 ******fi********t*t*** DEVICE DATA (DEVICE BEFORE NODE) ********************* NODE REV. WRK ACT. WRK IRREV HEAT X-FER MASS ERROR ENERGY ERROR (KW) (KW) (KW) (KW) (KG/S) (KW) 1 6652.92 .00 6652.92 -22157.89 .000 .000 2 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 3 6652.92 .00 6652.92 -22157.89 .000 .000 4 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 5 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 6 6651.65 .00 6651.65 -22153.67 .000 .002 7 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 8 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 9 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 10 -1.00 '1.00 -1.00 -1.00 -1.000 -1.000 11 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 12 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 ***********************t******* SYSTEM DATA TOTAL TOTAL TOTAL TOTAL TOTAL TOTAL TOTAL 240 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 -1.00 MASS FLOW RATE EXITING SYSTEM: MASS FLOW RATE ENTERING SYSTEM: '1.00 -1.000 -1.000 -1.00 -1.000 -1.000 -1.00 -1.000 -1.000 -1.00 -1.000 -1.000 -1.00 -1.000 -1.000 -1.00 -1.000 -1.000 -1.00 ~1.000 -1.000 -1.00 -1.000 -1.000 -1.00 -1.000 -1.000 -1.00 -1.000 -1.000 -1.00 -1.000 -1.000 -1.00 -1.000 -1.000 -1.00 -1.000 -1.000 -1.00 -1.000 -1.000 -1.00 -1.000 -1.000 -1.00 -1.000 -1.000 -1.00 -1.000 -1.000 -1.00 -1.000 -1.000 -1.00 -1.000 -1.000 -1.00 -1.000 -1.000 -1.00 -1.000 -1.000 ******************************** 29.9981 29.9981 ENTHALPY FLOW RATE EXITING SYSTEM: ENTHALPY FLOW RATE ENTERING SYSTEM: HEAT AND WORK ENTERING SYSTEM: BOILER HEAT: HEAT LOAD HEAT: CONDENSER HEAT (DEVICE 4 1): CONDENSER HEAT (DEVICE l 2): CONDENSER HEAT (DEVICE 4 3): TOTAL PIPE ENERGY LOSSES: NET WORK TO GENERATORS: TOTAL PUMP WORK: GENERATOR MECHANICAL LOSSES: GENERATOR ELECTRICAL LOSSES: NET ELECTRICAL POWER: SYSTEM HEAT RATE: CARNOT CYCLE EFFICIENCY: 1$T LAW EFFICIENCY: 2ND LAW EFFICIENCY: 19192.4100 85661.8800 -66469.4500 .0000 .0000 -22157.8900 -22157.8900 -22153.6700 .0000 .0000 .0000 .0000 .0000 .0000 §§§§ E 32321522 §§§ 2ND LAW EFFECTIVENESS: -1.0000 BTU/KW*HR 61.4370 PERCENT -100.0000 PERCENT 15.7808 PERCENT -100.0000 PERCENT 241 RANKINE 3.0: A steam power plant computer simulation Copyright 1994 W.A. Thelen, C.W. Somerton *tt'kitiiit***********************‘k TITLE *********************************** SIMPLE HEAT LOAD MODEL TEST it*********tttttttttt*****t***** NODE DATA *ittit*t***t***t***************** NODE T(C) P(MPa) L Q S(KJ/KG/K) H(KJ/KG) V(M“3/KG) M(KG/S) A(KJ/KG) 1 500.00 10.0000 3 ***** 6.5984 3374.66 .03275 1.0000 1411.69 2 400.00 9.0000 3 ***** 6.2890 3120.18 .02995 1.0000 1249.46 3 500.00 10.0000 3 ***** 6.5984 3374.66 .03275 1.0000 1411.69 4 400.00 9.0000 3 ***** 6.2890 3120.18 .02995 1.0000 1249.46 **t*************t**** DEVICE DATA (DEVICE BEFORE NODE) ********************* NODE REV. WRK ACT. WRK IRREV HEAT X-FER MASS ERROR ENERGY ERROR (KW) (KW) (KW) (KW) (KG/S) (KW) 1 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 2 162.23 .00 162.23 r254.48 .000 .000 3 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 4 162.23 .00 162.23 -254.48 .000 .000 ****************************iii SYSTEM DATA *t****************************** TOTAL MASS FLOW RATE EXITING SYSTEM: 2.0000 KG/SEC TOTAL MASS FLOW RATE ENTERING SYSTEM: 2.0000 KG/SEC TOTAL ENTHALPY FLOW RATE EXITING SYSTEM: 6240.3570 KW TOTAL ENTHALPY FLOW RATE ENTERING SYSTEM: 6749.3160 KW TOTAL HEAT AND WORK ENTERING SYSTEM: -508.9595 KW TOTAL BOILER HEAT: .0000 KW HEAT LOAD HEAT (DEVICE O 1): -254.4797 KW HEAT LOAD HEAT (DEVICE O 2): -254.4797 KW TOTAL HEAT LOAD HEAT: -508.9595 KW TOTAL PIPE ENERGY LOSSES: .0000 KW NET WORK TO GENERATORS: .0000 KW TOTAL PUMP WORK: .0000 KW GENERATOR MECHANICAL LOSSES: .0000 KW GENERATOR ELECTRICAL LOSSES: .0000 KW NET ELECTRICAL POWER: .0000 KW SYSTEM HEAT RATE: -1.0000 BTU/KW*HR CARNOT CYCLE EFFICIENCY: 61.4370 PERCENT 18T LAW EFFICIENCY: -100.0000 PERCENT 2ND LAW EFFICIENCY: 100.0000 PERCENT 2ND LAW EFFECTIVENESS: -100.0000 PERCENT 242 RANKINE 3.0: A steam power plant computer simulation W.A. Thelen, Copyright 1994 C.W. Somerton *iittiti************t********ttiti TITLE ***i**i**************t************t SIMPLE OPEN FEED WATER HEATER MODEL TEST fi**************t**************** NODE DATA *******t************************* NODE T(C) P(MPa) L Q S(KJ/KG/K) H(KJ/KG) V(M‘3/KG) M(KG/S) A(KJ/KG) 1 275.56 6.0000 4 ***** 3.0251 1213.37 .00132 25.0002 315.78 2 430.60 6.0000 3 ***** 6.6542 3255.19 .05033 1.4165 1275.58 3 251.07 6.0000 1 ***** 2.7861 1090.73 .00125 23.5837 264.39 4 275.56 6.0000 4 ***** 3.0251 1213.37 .00132 24.9968 315.78 5 430.60 6.0000 3 ***** 6.6542 3255.19 .05033 1.4163 1275.58 6 251.07 6.0000 1 ***** 2.7861 1090.73 .00125 23.5805 264.39 7 275.56 6.0000 4 ***** 3.0251 1213.37 .00132 25.0000 315.78 8 430.60 6.0000 3 ***** 6.6542 3255.19 .05033 1.4165 1275.58 9 251.07 6.0000 1 ***** 2.7861 1090.73 .00125 23.5835 264.39 10 275.56 6.0000 4 ***** 3.0251 1213.37 .00132 25.0000 315.78 11 430.60 6.0000 3 ***** 6.6542 3255.19 .05033 1.4163 1275.58 12 251.07‘ 6.0000 1 ***** 2.7862 1090.75 .00125 23.5837 264.40 13 275.56 6.0000 4 ***** 3.0251 1213.37 .00132 25.0000 315.78 14 430.71 6.0000 3 ***** 6.6546 3255.47 .05034 1.4163 1275.73 15 251.07 6.0000 1 ***** 2.7861 1090.73 .00125 23.5837 264.39 16 275.67 6.0000 1 ***** 3.0066 1213.35 .00132 25.0000 321.27 17 430.60 6.0000 3 ***** 6.6542 3255.19 .05033 1.4163 1275.58 18 251.07 6.0000 1 ***** 2.7861 1090.73 .00125 23.5837 264.39 tittittttttttttttittt DEVICE DATA (DEVICE BEFORE NODE) tittttwtttititiittiti NODE REV. WRK ACT. WRK IRREV HEAT X-FER MASS ERROR ENERGY ERROR (KW) (KW) (KW) (KW) (KG/S) (KW) 1 147.46 .00 147.46 .00 .000 .000 2 -1.00 -1.00 -1.00 —1.00 -1.000 -1.000 3 -1.00 -1.00 -1.00 —1.00 -1.000 -1.000 4 147.44 .00 147.44 .00 .000 .000 5 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 6 .-1.00 -1.00 -1.00 -1.00 -1.000 -1.000 7 147.46 .00 147.46 .00 .000 .001 s -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 9 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 10 147.45 .00 147.45 .00 .000 .001 11 '-1.00 -1.00 -1.00 -1.00 -1.000 -1.000 12 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 13 147.50 .00 147.50 .00 .000 .001 14 -1.00 —1.00 -1.00 -1.00 -1.000 -1.000 15 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 16 10.20 .00 10.20 .00 .000 .000 17 —1.00 -1.00 -1.00 -1.00 -1.000 -1.000 10 -1.00 -1.00 —1.00 -1.00 -1.000 -1.000 *t**********ttt**t*ttitttttttti SYSTEM DATA ******************************it TOTAL MASS FLOW RATE EXITING SYSTEM: TOTAL MASS FLOW RATE ENTERING SYSTEM: TOTAL ENTHALPY FLOW RATE EXITING SYSTEM: TOTAL ENTHALPY FLOW RATE ENTERING SYSTEM: TOTAL HEAT AND WORK ENTERING SYSTEM: 149.9970 KG/SEC 149.9970 KG/SEC 182001.0000 KW 182001.0000 KW .0000 KW TOTAL BOILER HEAT: TOTAL HEAT LOAD HEAT: TOTAL PIPE ENERGY LOSSES: NET WORK TO GENERATORS: TOTAL PUMP WORK: GENERATOR MECHANICAL LOSSES: GENERATOR ELECTRICAL LOSSES: NET ELECTRICAL POWER: SYSTEM HEAT RATE: CARNOT CYCLE EFFICIENCY: 1$T LAW EFFICIENCY: 2ND LAW EFFICIENCY: 2ND LAW EFFECTIVENESS: 243 .0000 .0000 .0000 .0000 .0000 .0000 .0000 .0000 -1.0000 61.4370 -100.0000 118.1409 -100.0000 §§§§ § §§§ BTU/KW*HR PERCENT PERCENT PERCENT PERCENT 244 RANKINE 3.0: A steam power plant computer simulation W.A. Copyright 1994 Thelen, C.W. Somerton it**************t***************** TIT“ *********************************** SIMPLE CLOSED FEED WATER HEATER MODEL TEST titttttttt*ttttttttttttttttttttt NODE DATA *tttttittttitiitt*ttttttttttttttt NODE T(C) P(MPa) L Q S(KJ/KG/K) H(KJ/KG) V(M‘3/KG) M(KG/S) A(KJ/KG) 1 80.00 2.5000 1 ***** 1.0716 336.65 .00103 10.0000 21.48 2 199.95 2.2500 1 ***** 2.3245 852.14 .00116 10.0000 163.44 3 320.00 10.0000 3 ***** 5.7144 2783.86 .01930 2.1144 1084.45 4 140.00 10.0000 1 ***** 1.7250 595.13 .00108 1.0000 85.15 5 100.00 9.5000 1 ***** 1.2952 425.90 .00104 3.1144 44.08 6 80.00 2.5000 1 ***** 1.0716 336.65 .00103 10.0000 21.48 7 199.95 2.2500 1 ***** 2.3245 852.14 .00116 10.0000 163.44 8 320.00 10.0000 3 ***** 5.7144 2783.86 .01930 2.1144 1084.45 9 140.00 10.0000 1 ***** 1.7250 595.13 .00108 .1000 85.15 10 140.00 10.0000 1 ***** 1.7250 595.13 .00108 .1000 85.15 11 140.00 10.0000 1 ***** 1.7250 595.13 .00108 .1000 85.15 12 140.00 10.0000 1 ***** 1.7250 595.13 .00108 .1000 85.15 13 140.00 10.0000 1 ***** 1.7250 595.13 .00108 .1000 85.15 14 140.00 10.0000 1 ***** 1.7250 595.13 .00108 .1000 85.15 15 140.00 10.0000 1 ***** 1.7250 595.13 .00108 .1000 85.15 16 140.00 10.0000 1 ***** 1.7250 595.13 .00108 .1000 85.15 17 140.00 10.0000 1 ***** 1.7250 595.13 .00108 .1000 85.15 18 140.00 10.0000 1 ***** 1.7250 595.13 .00108 .1000 85.15 19 100.00 9.5000 1 ***** 1.2952 425.90 .00104 3.1144 44.08 *tttttttititttttttttt DEVICE DATA (DEVICE BEFORE NODE) *ittiitttttttttitttit NODE REV. WRK ACT. WRK IRREV HEAT X-FER MASS ERROR ENERGY ERROR (KW) (KW) (KW) (KW) (KG/S) (KW) 1 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 2 2163.68 .00 2163.68 5154.93 .000 .000 3 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 4 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 5 1117.10 .00 1117.10 -5154.93 .000 .000 6 . -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 7 2163.68 .00 2163.68 5154.93 .000 .000 8 -1.00 -1.00 -1.00 -l.00 -l.000 -1.000 9 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 10 . -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 11 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 12 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 13 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 14 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 15 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 16 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 17 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 18 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 19 1117.10 .00 1117.10 -5154.93 .000 .000 it*********************tttttttt SYSTEM DATA **t**t******tittttttttttttttittt TOTAL MASS FLOW RATE EXITING SYSTEM: TOTAL MASS FLOW RATE ENTERING SYSTEM: TOTAL ENTHALPY FLOW RATE EXITING SYSTEM: TOTAL ENTHALPY FLOW RATE ENTERING SYSTEM: 26.2288 KG/SEC 26.2288 KG/SEC 19695.6400 KW 19695.6500 KW 245 TOTAL HEAT AND WORK ENTERING SYSTEM: TOTAL BOILER HEAT: TOTAL HEAT LOAD HEAT: TOTAL PIPE ENERGY LOSSES: NET WORK TO GENERATORS: TOTAL PUMP WORK: GENERATOR MECHANICAL LOSSES: GENERATOR ELECTRICAL LOSSES: NET ELECTRICAL POWER: SYSTEM HEAT RATE: CARNOT CYCLE EFFICIENCY: IST LAW EFFICIENCY: 2ND LAW EFFICIENCY: 2ND LAW EFFECTIVENESS: .0010 .0000 .0000 .0000 .0000 .0000 .0000 .0000 .0000 -1.0000 61.4370 -100.0000 68.8929 -100.0000 §§§§ § §§§ Q BTU/KW*HR PERCENT PERCENT PERCENT PERCENT t**** 246 RANKINE 3.0: A steam power plant computer simulation Copyright 1994 W.A. Thelen, ***t************************* TITLE SIMPLE SEPARATOR MODEL TEST it*********************i******** NODE DATA ********************************* C.W. Somerton *********************************** NODE T(C) P(MPa) L Q S(KJ/KG/K) H(KJ/KG) V(M“3/KG) M(KG/S) A(KJ/KG) 1 179.87 1.0000 2 .500 4.3598 1769.26 .09779 1.0000 473.74 2 175.35 .9000 5 ***** 6.6191 2772.27 .21498 .5059 803.12 3 175.35 .9000 4 ***** 2.0927 742.27 .00112 .4941 122.66 4 500.00 1.0000 3 ***** 7.7586 3475.99 .35405 1.0000 1167.10 5 499.51 .9000 3 ***** 7.8069 3475.99 .39345 1.0000 1152.71 6 175.35 .9000 4 ***** 2.0927 742.27 .00112 .0000 122.66 7 100.00 1.0000 1 ***** 1.3049 419.52 .00104 1.0000 34.79 8 175.35 .9000 5 ***** 6.6191 2772.27 .21498 .0000 803.12 9 100.02 .9000 1 ***** 1.3053 419.52 .00104 1.0000 34.70 *ttttttttittttitttttt DEVICE DATA (DEVICE BEFORE NODE) t******************** NODE REV. WRK ACT. WRK IRREV HEAT X-FER MASS ERROR ENERGY ERROR (KW) (KW) (KW) (KW) (KG/S) (KW) 1 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 2 6.83 .00 6.83 .00 .000 .000 3 .00 .00 .00 .00 .000 .000 4 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 5 14.39 .00 14.39 .00 .000 .000 6 .00 .00 .00 .00 .000 .000 7 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 8 .09 .00 .09 .00 .000 .000 9 .00 .00 .00 .00 .000 .000 *ttitttttitttttitttttittttiittt SYSTEM DATA *tttttttttit******************t* TOTAL MASS FLOW RATE EXITING SYSTEM: 3.0000 KG/SEC TOTAL MASS FLOW RATE ENTERING SYSTEM: 3.0000 KG/SEC TOTAL ENTHALPY FLOW RATE EXITING SYSTEM: 5664.7700 KW TOTAL ENTHALPY FLOW RATE ENTERING SYSTEM: 5664.7700 KW TOTAL HEAT AND WORK ENTERING SYSTEM: .0000 KW TOTAL BOILER HEAT: .0000 KW TOTAL HEAT LOAD HEAT: .0000 KW TOTAL PIPE ENERGY LOSSES: .0000 KW NET WORK TO GENERATORS: .0000 KW TOTAL PUMP WORK: .0000 KW GENERATOR MECHANICAL LOSSES: .0000 KW GENERATOR ELECTRICAL LOSSES: .0000 KW ‘NET ELECTRICAL POWER: .0000 KW SYSTEM HEAT RATE: -1.0000 BTU/KW*HR CARNOT CYCLE EFFICIENCY: 61.4370 PERCENT IST LAW EFFICIENCY: -100.0000 PERCENT 2ND LAW EFFICIENCY: 98.7282 PERCENT 2ND LAW EFFECTIVENESS: -100.0000 PERCENT 247 RANKINE 3.0: A steam power plant computer simulation W.A. Copyright 1994 Thelen, C.W. Somerton *iitiiiiii**************i****ttiit TITLE *********t******************t****** SIMPLE REHEATER MODEL TEST *fi*************i**************** NODE DATA ********************************fi NODE T(C) P(MPa) L Q S(KJ/KG/K) H(KJ/KG) V(M‘3/KG) M(KG/S) A(KJ/KG) 1 300.00 1.5000 3 ***** 6.9184 3037.88 .16977 91.0000 979.49 2 300.00 1.5000 3 ***** 6.9184 3037.88 .16977 90.3395 979.49 3 300.00 1.5000 3 ***** 6.9184 3037.88 .16977 .6605 979.49 4 180.00 1.0000 3 ***** 6.5832 2776.53 .19441 90.3395 818.08 5 183.38 .9000 3 ***** 6.6643 2792.73 .22006 90.3395 810.11 6 193.34 1.3500 4 ***** 2.2659 822.13 .00115 .6605 150.91 7 300.00 1.5000 3 ***** 6.9184 3037.88 .16977 91.0000 979.49 8 300.00 1.5000 3 ***** 6.9184 3037.88 .16977 90.3395 979.49 9 300.00 1.5000 3 ***** 6.9184 3037.88 .16977 .6605 979.49 10 180.00 1.0000 3 ***** 6.5832 2776.53 .19441 '90.3395 818.08 11 193.34 1.3500 4 ***** 2.2659 822.13 .00115 .6605 150.91 12 183.38. .9000 3 ***** 6.6643 2792.73 .22006 90.3395 810.11 13 300.00 1.5000 3 ***** 6.9184 3037.88 .16977 91.0000 979.49 14 300.00 1.5000 3 ***** 6.9184 3037.88 .16977 90.3740 979.49 15 300.00 1.5000 3 ***** 6.9184 3037.88 .16977 .6260 979.49 16 180.00 1.0000 3 ***** 6.5832 2776.53 .19441 90.3740 818.08 17 193.00 1.3500 1 ***** 2.2603~ 820.61 .00115 .6260 151.05 18 183.05 .9000 3 ***** 6.6625 2791.89 .21985 90.3740 809.82 t****************t*** DEVICE DATA (DEVICE BEFORE NODE) *****t**************i NODE REV. WRK ACT. WRK IRREV HEAT X-FER MASS ERROR ENERGY ERROR (KW) (KW) (KW) (KW) (KG/S) (KW) 1 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 2 .00 .00 .00 .00 .000 -.014 3 .00 .00 .00 .00 .000 .000 4 14581.51 .00 14581.51‘ -23610.50 .000 -.008 5 1971.08 .00 1971.08 1463.54 .000 .005 6 65.76 .00 65.76 -1463.54 .000 .000 7 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 8 .00 .00 .00 .00 .000 -.014 9 .00 .00 .00 .00 .000 .000 10 14581.51 .00 14581.51 -23610.50 .000 -.008 11 65.76 .00 65.76 -1463.54 .000 .000 12 1971.08 .00 1971.08 1463.54 .000 .005 13 -1.00 -1.00 -1.00 -1.00 -1.000 -1.000 14 .00 .00 .00 .00 .000 -.001 15 .00 .00 .00 .00 .000 .000 16 14587.08 .00 14587.08 -23619.52 .000 -.002 17 62.17 .00 62.17 -1387.97 .000 .000 18 1969.77. .00 1969.77 1387.98 .000 .005 ****************************44* SYSTEM DATA *ittti***********ttttttttttiittt TOTAL MASS FLOW RATE EXITING SYSTEM: TOTAL MASS FLOW RATE ENTERING SYSTEM: TOTAL ENTHALPY FLOW RATE EXITING SYSTEM: TOTAL ENTHALPY FLOW RATE ENTERING SYSTEM: TOTAL HEAT AND WORK ENTERING SYSTEM: 273.0000 KG/SEC 273.0000 KG/SEC 758500.9000 KW 829341.4000 KW -70840.5100 KW ’ TOTAL BOILER HEAT: HEAT LOAD HEAT (DEVICE i 2): HEAT LOAD HEAT (DEVICE i 5): HEAT LOAD HEAT (DEVICE 4 8): TOTAL HEAT LOAD HEAT: TOTAL PIPE ENERGY LOSSES: NET WORK TO GENERATORS: TOTAL PUMP WORK: GENERATOR MECHANICAL LOSSES: GENERATOR ELECTRICAL LOSSES: NET ELECTRICAL POWER: SYSTEM HEAT RATE: CARNOT CYCLE EFFICIENCY: 1$T LAW EFFICIENCY: 2ND LAW EFFICIENCY: 2ND LAW EFFECTIVENESS: 248 .0000 -23610.5000 -23610.5000 -23619.5200 -70840.5200 .0000 .0000 .0000 .0000 .0000 .0000 -1.0000 61.4370 -100.0000 99.2231 -100.0000 3%? i5 §§§§§§ BTU/KW*HR PERCENT PERCENT PERCENT PERCENT Appendix D: Hand calculations for benchmark case #1 through case #5 249 I!" 000...? in. II. ‘N 3089 g g g! g g g oodovvm- nodvo: nodvo: gggfigggg owl-OE 05333:... .32 _ all .0 S (Iain: gai . 0.8%.: said; Sag-egos 250 I072 40 um?! 40 as... Emmi .3. z. s. 3: noun. :5. :2. I «so: to! :01 3x ooohdnvnm '3..- So: 3:8 0.8 3. 3n 8» 85.. o. .2: .93 in 839% .:a .9... .«I {.3 :1 .828. o n .2. 0.8 9 com .2. .5 o o. .8 { Eaaééé 3.8... I 88. 8 .. n 88 . 8...... 2 EEEEEEEE 88. 888898. 3888808808. 88 . 88888. .2 EEEEIEIEENHIIEN'E 88. 8... a 88 u 8..... 8 EEEEEE‘EE 88 8... n 88 u 8.... 8 EEEEEEEE 2...... 588889 8888988888. 8......N 880889 .8 Imialfillmfi'aiééa 88 8... a 88 a 2.8. 8 IRENE-Haggai .8. 8... a 88 a 2.2.“ 2 EEEEEEEE .8. 588889 8889808888. 88 a 88888. .8 EEEE'E'EEEE .86 8... n 88 . 8.8. a. EEIEEEEE 8.: 88888. 588808.888... 88 . 888.89 .8 lfi'lfiififiééaé 82. 8... a 88 . 8.... .. EEE‘EE‘EEE 8.: 8... a 88 . 8.... 8 I IEEEEE 8... .8888... 8880808888. 88.. .88888. .8 . EE%%% 8... 8... a 88 . 8.... 2 E Egan. .8... 888889 8888888939 88 . 880889 .2 IE' gang .8». 8.. a 88.2 8.8. .. EHI . Egg .8. _ 8.. n _ 88.2 8.8. : gagging. :8. _ 8.. . H 88.2 8.8. 2 EEEEIIEI .3... 8.. . 88.2 8.8. 2 EEEEE 8... 588882 3880889889 88.2 88888 .2 , 8... 8..... gal-EH5. :8 8.. . 88.. 8.8. .. _ 8.. r 3.2 p S 2 _ 8.. _ 8...... gall—a. 3.. _ 8.. . L 88.» 8.8. 2 _ 8.. _ 8... _ 88 _ . . 2... _ 8.. . _ 88.. 2.2. 2 8.. 2... 8... . . 2... 8.. . 88.. 2.2a .. EEEEEEEE 8.. 888988. 88888888... 88... 888082 .: 8 o 8... 8.. . 8.. 8... . 88.. 5.!- 2 — 8.. _ 8.8 _ 8.8 . 8.. _ 8... . 88.. 3.... L _ 8.. _ 8o _ 8... S... _ 8... . _ 88.. 8.8. 8.... S... 2.8 .2. 8... . 88.. 8.... Egg .2. 388889 8888889888. 88.. .88888. : 8 o 8.... 8... . a... 8.. . 88.. 8.8. _ 8o _ .3. _ 3.“. . a... 8.. . 88.. 8.8. _ 8.. _ 8... _ 8... . 82 _ 8... . _ 88.. 8.8. 8. 8.: 8.... . . 82 8... . 88.. 3.8. EEEEEE :2 .88888. 8898828883 83.. 680883 .n EIEEE'EE'EEE :2 8.. . 88.. 8.... EEEEE‘EE‘E =2 _ 8.. . .8... 3.2. .s: z... x i 9.5. a: .x 3.3.... .E .35. a 3 3 u: 3.5.... is .83.... .833! I... 228...... .888 gm :25 _ 5.8 82...... _ 5.8... 8..!!!» .3. .9 4:5..- ..I .88.: 8. 2.2.: .5 .88... a! .88: .5. . .24.: .9 . .22: .3 . 4...... .3 . 2...: .9 . .2: .5 . 44.: .5 . .3: a: . .2: .8 . .88.: a: . .28.: .9 . .88 .: .9 . .88: .5 . .88.: aEQiJZ. .0 £3 . .25 .t 252 3! : 0;; sf..eo..o..£. . 1.2.3.8330 lull. at 39.101 I‘z = 9.2—0.1 I; .03 5 253 8 6 66 6 8 6 66 6 l .66 88. .6 66.666. 66.6666 866. .. _ 6 _ 66 8 6 66.36 66.666 66 666. l .66 668.6 66,666.. 66 6666 866 .. 6 66 3883.. i338. 868868. xxxxxg 38888. 888868. 6:666 6666 888886. .66 8 6 66 666 6.6666 66 6666 66 666. 886 66.66.... 66.666 6666. .. 6 66 88888. 588886. 888682 88888. 688868. 588886. 66.366 6666 5868686. .66 86 66.6 8 6 666 6. .66.. 88.66 66.636 66 686 6666, .. 6 .6 66 6 66.666 66.36 66.6666 6. .66.. 88.66 66.636 66.6666 6666. .. 6 66 888886. 868886. 88888. 888686. 888686. 868868. 2.6666 6666. 888886. 666 8.6 6.666 6.6666 66.666. 66.86. 6666.6 $66.6 3.6666 6666. .. 6 w 6. 886886. 888886. 8686869 886888. 688886. 888886. 66.666 66.6. 888886. . 66. 666 86 86 66.6 6.666. 88.66 66.6666 666666 66.6. .. 6 _ 6. 8 .6666. 66.6666. 66.6666. 86 6.666. 88.66 66.6666 66.6666 66.6. _ .. _ 6 _ 2 86 8.6 86 66 6 2.66. 88.66 6966... .66: 666.. .. _ . _ 6. 8 6 66.6.. 66.666. 66 666. 6.66. 88.66 66.66... .66: 666.. .. . 6. 886889 586888. 88888. 888086. 586888. 888686. 66.6: 666.. .6. 66.6 86 66 6 66.6 66.66. 6666.66 66.66... 66.6: 666.. 6 6 6. 86 66.66. 66.66. 86 66.66. 668.66 66.66... 66.666 .66.. 6 _ 6 _ 6. 8.6 66.6 666 8 6 6666 6666.66 6366.. 66.666 6666. .. _ . _ 6. 86 .66 65.6. :66. 6666 6666.66 66.66... 66666 6666. .. . .. 888868. 868886. 588889 686888. 888886. 88888. 66666 6666. 88888. 6.. 66.6 8.6 666 66.6 :66 6666.66 66.68.. 66,666 6666. 6 6 _ 6. 8.6 :66. 2.66. 66.6 :66 6666.66 66.68.. 66.666 6666. 6 _ 6 _ 8.6 66.6 666 66.6 6666 666666 8.6.6.. 66.666 6666. _ .. _ . _ 8 6 .66 6. 6.. 66.66. 66 66 6666.66 696.... 66.666 6666. .. . . 888886. 88888. 88888. 888688. 886886. 8888... 66.666 6666. 588688. .. 66.6 8.6 666 8.6 6666 6666.66 3666.. 66.666 6666. 6 _ 8 6 .6666 .6666 66.6 66 66 686.66 66.68.. 66.666 6666. 6 _ _ 66,6 66.6 66,6 86 :6. 666666 69666.. . 66 6 66 6 .66. 66.... :6. 6666.66 8.666.. 88888. 898886. 888688. 868886. 888688. 88888. 8.6 8.6 66 6 66.6 66 6. 6666.66 66.66.... 66.66.66. 3.6.66. 66.6.66. 86 66.6. 6666.66 66.666. 2... x 3.. z... E x u: x :9... .66... .8: 6.... .8: 5... £6... .52 I} x I: .2. 88 66...... .66.: ..o 6.5... .626 .5 6.5... .6166 .6 66...... £166 .5 Sinai-3.. 6.5... .6166 .0 .28. mi 1.6: 6 6.5... .616. .0 £625. BEN. .38 6 6:63. .26. ,.o Said-8.. 6.5... .26. ..o 6.6. all .3... 6 6x5. .6... ._o SEQ-.6. 6.5... .26 .6 Silt 66 2: "£3. .2 .o M.“ Ni .66 66 3 x5. .66 8 . in... 66 6:5. .768 iii. .62... 6.5... .26 SEMI-66666696665 6.5... .6266 ...EI.666656.666£. 6.3... .6066 .o 3 El .6. 66 so 6.6 66 a. 6:5. £6.66 .0 ...NHI.666.666.6665 6:5. .6666 .o 3 El .6. .6 6a 6.6 R 6.. 6.5... .6666 .o 3 El .6. 6. 6G 6.6 66 6.. 6.3... .6666 .o 3 El .66 : to 6.6 66 a. 6:5. ..6.66 ..o 3 El .66 66 65 6.6 .6 6: 6x5. . .62. ._o SEMI .6. .6 6.0 6.6 .6 6.. 254 Etc. 3 86 issue-m §§§83888§§58089x§888889§ 8880889” :8 8 o 8 o 8.0 88 .888... 88,... «38 n 2.8 8 88. 9 8. 3,8. 8 o .8883 88 a. 8.8.... I .3... 8 o 8 o 8.0 8 o .888: 88.3 8.8.... I .8: 8° 3...: 8.28 8.88 .838: 88.8 8.9: I .88 gggggg 8888080.]! 88 8 a 8 on. 3.8.... 8.2.. .83.»... 88 . «98".... I. .88 80.36958959898888888888580808588895. 8088808189.. 8 o 8 o 8 o 8... 3.3.8. 88.8 gm... .88 we a. :2 8 88.. 8.8.3 8 8 8.3.8. 88 8 3m... .38 8 o 8... 8... 8... 88.8.3. 88 8 _ 8.8... .8. 8 o .m .8. 2.82. 8.8... "8.3.3. 88 o... 8.8... .8. 880889 880889 880889 88888. 588088. 688088. 8888882 8.. 8.. 8... 88 8... 828.8. 88.8 8&2. . 8 o 3 3.. 8.3... 8... 828 on. 88.8 8.8... 8... 8 o 8.. 8.0 8.38.... «a... C _ 8.8.... 8 o 8.... 3...? 2.3. 82898 8...... 8.8.... 880889 888088. 688088. 888808. 88888. 888808. 6888808. 8... 8 o 8... 8... 882.... 8;... 8.8.... 8 o 8.2. 8.... 8... 832...- ~2..= _ 8&8. 8 o 8.0 8... 8... 88898 3...... 8.5.... 8 o a: 1.... 2.8. 8238.8 3...... RES. 880889 88888. 580888. 880889 888889 880889 588888... 8... 8... 86 8.9 .8288 8:8 8&8. 8.0 8.8. 8.8. 8... .2298 3...: _ 8.8.... 8 o 8... 8... 8.o .3338 :38 8&8. 8 o I N 8.... 3...... .5832 28.9 8&8. 588889 5808082 688088. 68888... 88.888. 8888... 8880889 8... 8... 8... 8... 32.3.2 :3... 8&1... 8.882. 3.3...“ 8 o 2.23.... 23.... 8.8.... 5 5. x 3.. x5. 8.. x :95 fi 3... to: 8:. to... t... .8; .33 .9... a: l.- 3... 25.2. 8.88 2.2—9° .38 ..o 2...... a... .88 .5 I! . a! . 8. . a! . n! . 9...... . 41:0 8 . 9...... . 878.0 1! . 3.5. . 415...... r! . 8.5. . .32 ..o p! . 9...... . J... .0 I! . 3...... . 4.... .0 I! . 9...... .2... .6 p! . 3...... 8....0 p! . 9...... 4.7.0 I! . 8...... .35 n! . 9...... .36 s! . 8...... .u. .0 I! . 9...... .3840 r! . 3...... .33 .0 a! . 9...... .33 .o p! . 3...... .886 a! . 9...... .8... .5 p! . 9...... .88 ..o a! . 9...! land“ .5 DI. , 9...... .36... .0 I! . .5 . 3.5. . .3... ,.o .928. 8 88 539'... Appendix E: RANKINE 3.0 input files for benchmark case #1 through case #5 257 TITLE LINE BENCHMARK CASE #1 END TITLE NUMBER OF NODES IS 4 HIGH TEMPERATURE RESERVOIR: 600.0 DEG C DOW TEMPERATURE RESERVOIR: 25.0 DEG C DEAD STATE TEMPERATURE: 25.0 DEG C DEAD STATE PRESSURE: 101 KPA GENERATOR MECHANICAL LOSS IS 0.0 MW GENERATOR ELECTRICAL LOSS IS 0.0 MW DEVICE #1: SIMPLE TURBINE INLET NODE NUMBER IS 3 EXTRACTION #1 NODE NUMBER IS 4 STAGE GROUP #1 EFFICIENCY IS 75 PERCENT EXTRACTION #1 PRESSURE IS 0.1 MPA END DEVICE ' DEVICE #2: SIMPLE CONDENSER EXIT NODE NUMBER IS 1 INLET #1 NODE NUMBER IS 4 END DEVICE DEVICE #3: SIMPLE PUMP SUCTION NODE NUMBER IS 1 DISCHARGE NODE NUMBER IS 2 PUMP EFFICIENCY IS 75 PERCENT END DEVICE DEVICE #4: SIMPLE BOILER BOILER INLET NODE NUMBER IS 2 BOILER EXIT NODE NUMBER IS 3 BOILER EXIT PRESSURE IS 20.0 MPA BOILER EXIT TEMPERATURE IS 600 DEG C BOILER EXIT MASS FIDW RATE IS 50 KG/SEC BOILER PRESSURE LOSS 18 0.0 MPA END DEVICE 258 TITLE LINE BENCHMARK CASE #2 END TITLE NUMBER OF NODES IS 21 HIGH TEMPERATURE RESERVOIR: 500.0 DEG C LOW TEMPERATURE RESERVOIR: 25.0 DEG C DEAD STATE TEMPERATURE: 25.0 DEG C DEAD STATE PRESSUREzlol KPA GENERATOR MECHANICAL LOSS: 0.0 MW GENERATOR ELECTRICAL LOSS: 0.0 MW DEVICE #1: SIMPLE TURBINE INLET NODE NUMBER IS 10 EXTRACTION #1 NODE NUMBER IS 11 EXTRACTION #2 NODE NUMBER IS 12 EXTRACTION #3 NODE NUMBER IS 14 STAGE GROUP #1 EFFICIENCY IS 75 PERCENT STAGE GROUP #2 EFFICIENCY IS 75 PERCENT STAGE GROUP #3 EFFICIENCY IS 75 PERCENT EXTRACTION #1 PRESSURE IS 8.0 MPA EXTRACTION #1 MASS FLOW RATE IS 5.0 KG/SEC EXTRACTION #2 PRESSURE IS 6.0 MPA EXTRACTION #3 PRESSURE 18 4.0 MPA END DEVICE DEVICE #2: SIMPLE PUMP SUCTION NODE NUMBER IS 2 DISCHARGE NODE NUMBER IS 3 PUMP EFFICIENCY IS 75 PERCENT END DEVICE DEVICE #3: SIMPLE PUMP SUCTION NODE NUMBER IS 6 DISCHARGE NODE NUMBER IS 7 PUMP EFFICIENCY IS 75 PERCENT END DEVICE DEVICE #4: SIMPLE PIPE INLET NODE NUMBER IS 14 EXIT NODE NUMBER IS 15 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 “MG END DEVICE DEVICE #5: SIMPLE PIPE INLET NODE NUMBER IS 12 EXIT NODE NUMBER IS 13 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 ”KG END DEVICE DEVICE #6: SIMPLE PIPE INLET NODE NUMBER IS 1 EXIT NODE NUMBER IS 2 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 “MG END DEVICE DEVICE #7: SIMPLE PIPE INLET NODE NUMBER IS 3 EXIT NODE NUMBER IS 4 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 ”MG END DEVICE DEVICE #8: SIMPLE PIPE INLET NODE NUMBER IS 5 EXTT NODE NUMBER IS 6 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS 18 0.0 ”MG END DEVICE DEVICE #9: SIMPLE PIPE INLET NODE NUMBER IS 7 m NODE NUMBER IS 8 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 KJIKG END DEVICE DEVICE #10: SIMPLE PIPE INLET NODE NUMBER IS 9 EXIT NODE NUMBER IS 16 PIPE PERCENTAGE PRESSURE LOSS 0.0 PERCENT PIPE PERCENTAGE ENTHALPY LOSS 0.0 PERCENT END DEVICE DEVICE #11: SIMPLE PIPE INLET NODE NUMBER IS 11 DOT NODE NUMBER IS 19 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 IO/KG END DEVICE DEVICE #12: SIMPLE PIPE INLET NODE NUMBER IS 20 EXIT NODE NUMBER IS 21 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 KJ/KG END DEVICE DEVICE #13: SIMPLE PIPE INLET NODE NUMBER IS 18 EXIT NODE NUMBER IS 10 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 ”KG END DEVICE DEVICE #14: SIMPLE JUNCTION INLET #1 NODE NUMBER IS 16 EXIT #1 NODE NUMBER IS 17 EXIT #2 NODE NUMBER IS 18 EXIT #1 MASS FLOW RATE IS 0.0 KG/SEC END DEVICE DEVICE #15: SIMPLE CONDENSER EXIT NODE NUMBER IS 1 INLET #1 NODE NUMBER IS 15 INLET #2 NODE NUMBER IS 21 END DEVICE 259 END DEVICE DEVICE #16: SIMPLE HEAT LOAD - INLET NODE NUMBER IS 19 DEVICE #18: SIMPLE BOILER EXIT NODE NUMBER IS 20 BOILER INLET NODE NUMBER IS 8 EXIT TEMPERATURE IS 380.21 DEG C BOILER EXIT NODE NUMBER IS 9 END DEVICE BOILER EXIT PRESSURE IS 10 MPA BOILER EXIT TEMPERATURE IS 500 DEG C DEVICE #17: SIMPLE OFW HEATER BOILER EXIT MASS FLOW RATE IS 25 FEED WATER EXIT NODE NUMBER IS 5 KG/SEC EXTRACTION INLET NODE NUMBER IS 13 BOILER PRESSURE LOSS IS 0.0 MPA FEED WATER INLET NODE NUMBER IS 4 END DEVICE ‘ 260 TITLE LINE BENCHMARK CASE #3 END TITLE LINE NUMBER OF NODES IS 36 HIGH TEMPERATURE RESERVOIR: 500 DEG C LOW TEMPERATURE RESERVOIR: 25.0 DEG C DEAD STATE TEMPERATURE: 25.0 DEG C DEAD STATE PRESSURE: 101 KPA GENERATOR MECHANICAL LOSS: 0.0 MW GENERATOR ELECTRICAL LOSS: 0.0 MW DEVICE #1: SIMPLE BOILER BOILER INLET NODE NUMBER IS 16 - BOILER EXIT NODE NUMBER IS 17 BOILER EXIT TEMPERATURE IS 500 DEG C BOILER EXIT PRESSURE IS 10.0 MPA BOILER EXIT MASS FLOW RATE IS 22.0 KG/SEC BOILER PRESSURE LOSS IS 0.0 MPA END DEVICE DEVICE #2: SIMPLE PIPE INLET NODE NUMBER IS 17 EXIT NODE NUMBER IS 18 PIPE PRESSURE LOSS 0.0 MPA PIPE ENTHALPY LOSS 0.0 IU/KG END DEVICE DEVICE #3: SIMPLE TURBINE INLET NODE NUMBER IS 18 EXTRACTION #1 NODE NUMBER IS 19 EXTRACTION #2 NODE NUMBER IS 20 EXTRACTION #1 PRESSURE IS 8.0 MPA EXTRACTION #2 PRESSURE IS 6.0 MPA EXTRACTION #1 MASS FLOW RATE IS 2.0 KG/SEC STAGE GROUP #1 EFFICIENCY IS 50% STAGE GROUP #2 EFFICIENCY IS 50% ETD DEVICE . DEVICE #4: SIMPLE PIPE INLET NODE NUMBER IS 20 EXIT NODE NUMBER IS 21 PIPE PRESSURE LOSS 0.0 MPA PIPE ENTHALPY LOSS 0.0 KJ/KG ETD DEVICE DEVICE #5: SIMPLE TURBINE INLET NODE NUMBER IS 21 EXTRACTION #1 NODE NUMBER IS 22 EXTRACTION #2 NODE NUMBER IS 23 EXTRACTION #3 NODE NUMBER IS 25 EXTRACTION #4 NODE NUMBER IS 27 EXTRACTION #5 NODE NUMBER IS 29 EXTRACTION #1 PRESSURE 18 4.0 MPA EXTRACTION #2 PRESSURE IS 3.0 MPA EXTRACTION #3 PRESSURE 18 2.0 MPA EXTRACTION #4 PRESSURE IS 1.5 MPA ECTRACTION #5 PRESSURE IS 1.0 MPA EXTRACTION #1 MASS FLOW RATE 18 2.0 KGISEC STAGE GROUP #1 EFFICIETCY IS 50% STAGE GROUP #2 EFFICIENCY IS 50% STAGE GROUP #3 EFFICIENCY IS 50% STAGE GROUP #4 EFFICIENCY IS 50% STAGE GROUP #5 EFFICIENCY IS 50% ETD DEVICE DEVICE #6: SIMPLE PIPE INLET NODE NUMBER IS 23 EXIT NODE NUMBER IS 24 PIPE PRESSURE IOSS 0.0 MPA PIPE ENTHALPY LOSS 0.0 KJIKG END DEVICE DEVICE #7 : SIMPLE PIPE IITLET NODE NUMBER IS 25 EXIT NODE NUMBER IS 26 PIPE PRESSURE IOSS 0.0 MPA PIPE ENTHALPY LOSS 0.0 “KG END DEVICE DEVICE #8: SIMPLE PIPE INLET NODE NUMBER IS 27 EXIT NODE NUMBER IS 28 PIPE PRESSURE LOSS 0.0 MPA PIPE ENTHALPY LOSS 0.0 IU/KG ETD DEVICE DEVICE #9: SIMPLE PIPE INLET NODE NUMBER IS 29 EXIT NODE NUMBER IS 30 PIPE PRESSURE LOSS 0.0 MPA PIPE ENTHALPY LOSS 0.0 “KG END DEVICE DEVICE #10: SIMPLE CONDETSER EXIT NODE NUMBER IS 1 INLET #1 NODE NUMBER IS 30 INLET #2 NODE NUMBER IS 35 INLET #3 NODE NUMBER IS 36 ETD DEVICE DEVICE #11: SIMPLE PIPE INLET NODE NUMBER IS 1 EXIT NODE NUMBER IS 2 PIPE PRESSURE LOSS 0.0 MPA PIPE ENTHALPY LOSS 0.0 KJ/KG END DEVICE DEVICE #12: SIMPLE PUMP SUCTION NODE NUMBER IS 2 DISCHARGE NODE NUMBER IS 3 PUMP EFFICIETCY IS 50% ETD DEVICE DEVICE #13: SIMPLE PIPE INLET NODE NUMBER IS 3 EXIT NODE NUMBER IS 4 PIPE PRESSURE LOSS 0.0 MPA PIPE ENTHALPY LOSS 0.0 KJ/KG END DEVICE DEVICE #14: SIMPLE OFW HEATER FEED WATER EXIT NODE NUMBER IS 5 261 EXTRACTION INLET NODE NUMBER IS 28 FEED WATER INLET NODE NUMBER IS 4 END DEVICE DEVICE #15: SIMPLE PIPE INLET NODE NUMBER IS 5 EXIT NODE NUMBER IS 6 PIPE PRESSURE LOSS 0.0 MPA PIPE ENTHALPY LOSS 0.0 “MG END DEVICE DEVICE #16: SIMPLE PUMP SUCTION NODE NUMBER IS 6 DISCHARGE NODE NUMBER IS 7 PUMP EFFICIENCY IS 50% END DEVICE . DEVICE #17: SIMPLE PIPE INLET NODE NUMBER IS 7 EXIT NODE NUMBER IS 8 PIPE PRESSURE LOSS 0.0 MPA PIPE ENTHALPY LOSS 0.0 ”MG END DEVICE DEVICE #18: SIMPLE OFW HEATER FEED WATER EXIT NODE NUMBER IS 9 ECTRACIION INLET NODE NUMBER IS 26 FEED WATER INLET NODE NUMBER IS 8 END DEVICE DEVICE #19: SIMPLE PIPE INLET NODE NUMBER IS 9 EXIT NODE NUMBER IS 10 PIPE PRESSURE IOSS 0.0 MPA PIPE ENTHALPY LOSS 0.0 IU/KG END DEVICE DEVICE #20: SIMPLE PUMP SUCTION NODE NUMBER IS 10 DISCHARGE NODE NUMBER IS 11 PUMP EFFICIENCY IS 50% END DEVICE DEVICE #21: SIMPLE PIPE INLET NODE NUMBER IS 11 EXIT NODE NUMBER IS 12 PIPE PRESSURE LOSS 0.0 MPA PIPE ENTHALPY IOSS 0.0 ”MG END DEVICE DEVICE #22: SIMPLE OFW HEATER FEED WATER EXIT NODE NUMBER IS 13 EXTRACTION INLET NODE NUMBER IS 24 FEED WATER INLET NODE NUMBER IS 12 END DEVICE DEVICE #23: SIMPLE PIPE INLET NODE NUMBER IS 13 EXIT NODE NUMBER IS 14 PIPE PRESSURE LOSS 0.0 MPA PIPE EN'TI-IALPY LOSS 0.0 ”MG END DEVICE DEVICE #24: SIMPLE PUMP SUCTION NODE NUMBER IS 14 DISCHARGE NODE NUMBER IS 15 PUMP EFFICIENCY IS 50 % END DEVICE DEVICE #25: SIMPLE PIPE INLET NODE NUMBER IS 15 EXIT NODE NUMBER IS 16 PIPE PRESSURE LOSS 0.0 MPA PIPE ENTHALPY LOSS 0.0 “MG END DEVICE DEVICE #26: SIMPLE PIPE INLET NODE NUMBER IS 22 EXIT NODE NUMBER IS 33 PIPE PRESSURE LOSS 0.0 MPA PIPE ENTHALPY LOSS 0.0 “MG END DEVICE DEVICE #27: SIMPLE HEAT LOAD INLET NODE NUMBER IS 33 EXIT NODE NUMBER IS 34 EXTT TEMPERATURE IS 297.54 DEG C END DEVICE DEVICE #28: SIMPLE PIPE INLET NODE NUMBER IS 34 EXIT NODE NUMBER IS 35 PIPE PRESSURE IOSS 0.0 MPA PIPE ENTHALPY LOSS 0.0 KJ/KG END DEVICE DEVICE #29: SIMPLE PIPE INLET NODE NUMBER IS 19 EXIT NODE NUMBER IS 31 PIPE PRESSURE LOSS 0.0 MPA PIPE ENTHALPY IOSS 0.0 KJ/K END DEVICE . DEVICE #30: SIMPLE HEAT LOAD INLET NODE NUMBER IS 31 EXIT NODE NUMBER IS 32 EXIT TEMPERATURE IS 297.54 DEG C END DEVICE DEVICE #31: SIMPLE PIPE INLET NODE NUMBER IS 32 EXIT NODE NUMBER IS 36 PIPE PRESSURE LOSS 0.0 MPA PIPE ENTHALPY LOSS 0.0 “KG END DEVICE 262 TITLE LINE BENCHMARK CASE #4 END TITLE LINE NUMBER OF NODES IS 44 HIGH TEMPERATURE RESERVOIR: 400 DEG C LOW TEMPERATURE RESERVOIR: 25.0 DEG C DEAD STATE TEMPERATURE: 25.0 DEG C DEAD STATE PRESSURE: 101 KPA GENERATOR MECHANICAL LOSS: 0.0 MW GENERATOR ELECTRICAL LOSS: 0.0 MW DEVICE #1: SIMPLE BOILER BOILER INLET NODE NUMBER IS 16 BOILER EXIT NODE NUMBER IS 17 BOILER REHEAT LEG #1 INLET NODE NUMBER IS 24 BOILER REHEAT LEG #1 EXIT NODE NUMBER IS 25 BOILER EXIT ENTHALPY IS 3099.05 KJ/KG BOILER EXIT PRESSURE IS 10.0 MPA BOILER EXIT MASS FLOW RATE IS 45.0 KG/SEC BOILER REHEAT LEG #1 EXIT TEMPERATURE IS 400.0 DEG C BOILER PRESSURE LOSS IS 0.0 MPA BOILER REHEAT LEG #1 PRESSURE LOSS 18 0.0 MPA END DEVICE DEVICE #2: SIMPLE PIPE INLET NODE NUMBER IS 17 EXIT NODE NUMBER IS 18 PIPE PRESSURE IOSS IS 0.0 MPA PIPE ENTHALPY LOSS 18 0.0 KJIKG END DEVICE DEVICE #3: SIMPLE TURBINE INLETNODE NUMBER IS 18 EXTRACTION #1 NODE NUMBER IS 19 EXTRACTION #2 NODE NUMBER IS 20 STAGE GROUP #1 EFFICIENCY IS 75% STAGE GROUP #2 EFFICIENCY IS 75% EXTRACTION #1 PRESSURE IS 8.0 MPA EXTRACTION #2 PRESSURE IS 6.0 MPA EXTRACTION #1 MASS FLOW RATE IS 2.0 KGISEC END DEVICE DEVICE #4: SIMPLE PIPE INLET NODE NUMBER IS 20 EXTT NODE NUMBER IS 21 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY IOSS IS 0.0 KJ/KG END DEVICE DEVICE #5: SIMPLE PIPE INLET NODE NUMBER IS 23 EXIT NODE NUMBER IS 24 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY IOSS IS 0.0 IU/KG END DEVICE DEVICE #6: SIMPLE PIPE INLET NODE NUMBER IS 25 EXIT NODE NUMBER IS 26 PIPE PRESSURE IOSS IS 0.0 MPA PIPE ENTHALPY IOSS IS 0.0 KJIKG END DEVICE DEVICE #7: SIMPLE TURBINE INLET NODE NUMBER IS 26 EXTRACTION #1 NODE NUMBER IS 27 EXTRACTION #2 NODE NUMBER IS 28 EXTRACTION #3 NODE NUMBER IS 30 — EXTRACTION #4 NODE NUMBER IS 32 EXTRACTION #5 NODE NUMBER IS 34 STAGE GROUP #1 EFFICIENCY IS 75% STAGE GROUP #2 EFFICIENCY IS 75% STAGE GROUP #3 EFFICIENCY IS 75% STAGE GROUP #4 EFFICIENCY IS 75% STAGE GROUP #5 EFFICIENCY IS 75% EXTRACTION #1 PRESSURE 18 2.0 MPA EXTRACTION #2 PRESSURE IS 1.0 MPA EXTRACTION #3 PRESSURE 18 0.5 MPA EXTRACTION #4 PRESSURE IS 0.25 MPA EXTRACTION #5 PRESSURE LS 0.05 MPA EXTRACTION #1 MASS FLOW RATE IS 2.0 KGISEC END DEVICE DEVICE #8: SIMPLE PIPE INLET NODE NUMBER IS 28 EXIT NODE NUMBER IS 29 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 KJ/KG END DEVICE DEVICE #9: SIMPLE PIPE INLET NODE NUMBER IS 30 EXIT NODE NUMBER IS 31 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 KIIKG END DEVICE DEVICE #10: SIMPLE PIPE INLET NODE NUMBER IS 32 EXIT NODE NUMBER IS 33 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 KJ/KG END DEVICE DEVICE #11: SIMPLE PIPE INLET NODE NUMBER IS 34 EXTT NODE NUMBER IS 35 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY IOSS IS 0.0 ”KG END DEVICE DEVICE #12: SIMPLE CONDENSER EXIT NODE NUMBER IS 1 INLET #1 NODE NUMBER IS 35 INLET #2 NODE NUMBER IS 38 INLET #3 NODE NUMBER IS 39 INLET #4 NODE NUMBER IS 44 END DEVICE 263 DEVICE #13: SIMPLE PIPE INLET NODE NUMBER IS 1 EXIT NODE NUMBER IS 2 PIPE PRESSURE IOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 T(J/KG END DEVICE DEVICE #14: SIMPLE PUMP SUCTION NODE NUMBER IS 2 DISCHARGE NODE NUMBER IS 3 PUMP EFFICIENCY IS 75% END DEVICE DEVICE #15: SIMPLE PIPE INLET NODE NUMBER IS 3 EXIT NODE NUMBER IS 4 PIPE PRESSURE IOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 IU/KG END DEVICE DEVICE #16: SIMPLE OFW HEATER FEED WATER EXIT NODE NUMBER IS 5 EXTRACTION INLET NODE NUMBER IS 33 FEED WATER INLET NODE NUMBER IS 4 END DEVICE DEVICE #17: SIMPLE PIPE INLET NODE NUMBER IS 5 EXIT NODE NUMBER IS 6 PIPE PRESSURE IOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 TUIKG END DEVICE DEVICE #18: SIMPLE PUMP SUCTION NODE NUMBER IS 6 DISCHARGE NODE NUMBER IS 7 PUMP EFFICIENCY IS 75% END DEVICE DEVICE #19: SIMPLE PIPE INLET NODE NUMBER IS 7 EXIT NODE NUMBER IS 8 r PIPE PRESSURE IOSS IS 0.0 MPA PIPE ENTHALPY IOSS IS 0.0 ”MG END DEVICE DEVICE #20: SIMPLE OFW HEATER FEED WATER EXTT NODE NUMBER IS 9 EXTRACTION INLET NODE NUMBER IS 31 FEED WATER INLET NODE NUMBER IS 8 END DEVICE DEVICE #21: SIMPLE PIPE INLET NODE NUMBER IS 9 EXIT NODE NUMBER IS 10 PIPE PRESSURE IOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 KJIKG END DEVICE DEVICE #22: SIMPLE PUMP SUCTION NODE NUMBER IS 10 DISCHARGE NODE NUMBER IS 11 PUMP EFFICIENCY IS 75% END DEVICE DEVICE #23: SIMPLE PIPE INLET NODE NUMBER IS 11 EXIT NODE NUMBER IS 12 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY IOSS IS 0.0 ”MG END DEVICE DEVICE #24: SIMPLE OFW HEATER FEED WATER EXIT NODE NUMBER IS 13 EXTRACTION INLET NODE NUMBER IS 29 FEED WATER INLET NODE NUMBER IS 12 END DEVICE DEVICE #25: SIMPLE PIPE INLET NODE NUMBER IS 13 EXIT NODE NUMBER IS 14 PIPE PRESSURE IOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 KJIKG END DEVICE DEVICE #26: SIMPLE PUMP SUCTION NODE NUMBER IS 14 DISCHARGE NODE NUMBER IS 15 PUMP EFFICIENCY IS 75% END DEVICE DEVICE #27: SIMPLE PIPE INLET NODE NUMBER IS 15 EXIT NODE NUMBER IS 16 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 IU/KG END DEVICE DEVICE #28: SIMPLE PIPE INLET NODE NUMBER IS 19 EXTT NODE NUMBER IS 42 PIPE PRESSURE IOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 KJ/KG END DEVICE DEVICE #29: SIMPLE HEAT LOAD INLET NODE NUMBER IS 42 BOT NODE NUMBER IS 43 EXIT ENTHALPY IS 2580.28 KJ/KG/K END DEVICE DEVICE #30: SIMPLE PIPE INLET NODE NUMBER IS 43 EXIT NODE NUMBER IS 44 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 KJ/KG END DEVICE DEVICE #31: SIMPLE PIPE INLET NODE NUMBER IS 22 EXIT NODE NUMBER IS 41 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 ”KG END DEVICE DEVICE #32: SIMPLE HEAT TOAD ‘ INLET NODE NUMBER IS 41 . 264 EXIT NODE NUMBER IS 40 EXIT ENTHALPY IS 2580.28 10me EXIT ENTHALPY IS 2580.28 KJ/KG/K END DEVICE END DEVICE DEVICE #36: SIMPLE PIPE DEVICE #33: SIMPLE PIPE INLET NODE NUMBER IS 37 INLET NODE NUMBER IS 40 EXIT NODE NUMBER IS 38 EXIT NODE NUMBER IS 39 PIPE PRESSURE LOSS IS 0.0 MPA PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY IOSS IS 0.0 KJ/KG PIPE ENTHALPY IOSS IS 0.0 KJ/KG END DEVICE END DEVICE DEVICE #37: SIMPLE TURBINE DEVICE #34: SIMPLE PIPE INLET NODE NUMBER IS 21 INLET NODE NUMBER IS 27 EXTRACTION #1 NODE NUMBER IS 22 EXIT NODE NUMBER IS 36 EXTRACTION #2 NODE NUMBER IS 23 PIPE PRESSURE LOSS IS 0.0 MPA STAGE GROUP #1 EFFICIENCY IS 75% PIPE EN’TI-IALPY LOSS IS 0.0 KJ/KG STAGE GROUP #2 EFFICIENCY IS 75% END DEVICE EXTRACTION #1 PRESSURE IS 4.0 MPA EXTRACTION #2 PRESSURE IS 3.0 MPA DEVICE #35: SIMPLE HEAT LOAD EXTRACTION #1 MASS FLOW RATE IS 2.0 INLET NODE NUMBER IS 36 KGISEC EXIT NODENUMBER IS 37 END DEVICE 265 TITLE LINE BENCHMARK CASE #5 END TITLE LINE NUMBER OF NODES IS 46 HIGH TEMPERATURE RESERVOIR: 600.0 DEG C LOW TEMPERATURE RESERVOIR: 25.0 DEG C DEAD STATE TEMPERATURE: 25.0 DEG C DEAD STATE PRESSURE: 101 KPA GENERATOR MECHANICAL LOSS: 0.0 MW GENERATOR ELECTRICAL LOSS: 0.0 MW DEVICE #1: SIMPLE BOILER BOILER INLET NODE NUMBER IS 16 BOILER EXIT NODE NUMBER IS 17 BOILER REHEAT LEG #1 INLET NODE NUMBER IS 21 BOILER REHEAT LEO #1 EXIT NODE NUMBER IS 22 BOILER REHEAT LEG #2 INLET NODE NUMBER IS 26 BOILER REHEAT LEG #2 EXIT NODE NUMBER IS 27 BOILER EXIT TEMPERATURE IS 600.0 DEG C BOILER EXIT PRESSURE IS 20 MPA BOILER EXIT MASS FLOW RATE IS 50.0 KG/SEC BOILER REHEAT LEG #1 EXIT TEMPERATURE TS 600.0 DEG C BOILER REHEAT LEG #2 EXIT TEMPERATURE IS 600.0 DEG C BOILER PERCENTAGE PRESSURE LOSS IS 0.0 PERCENT REHEAT LEG #1 PERCENTAGE PRESSURE LOSS LS 0.0 PERCENT REHEAT LEG #2 PERCENTAGE PRESSURE LOSS IS 0.0 PERCENT END DEVICE DEVICE #2: SIMPLE PIPE INLET NODE NUMBER IS 17 EXIT NODE NUMBER IS 18 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 KJ/KG END DEVICE DEVICE #3: SIMPLE TURBINE INLET NODE NUMBER IS 18 EXTRACTION #1 NODE NUMBER IS 19 EXTRACTION #2 NODE NUMBER IS 20 STAGE GROUP #1 EFFICIENCY IS 75% STAGE GROUP #2 EFFICIENCY IS 75% EXTRACTION #1 PRESSURE IS 15.0 MPA EXTRACTION #2 PRESSURE LS 10.0 MPA EXTRACTION #1 MASS FLOW RATE IS 1.0 KG/SEC END DEVICE DEVICE #4: SIMPLE PIPE INLET NODE NUMBER IS 20 EXIT NODE NUMBER IS 21 PIPE PERCENTAGE PRESSURE LOSS IS 0.0 PERCENT PIPE PERCENTAGE ENTHALPY LOSS IS 0.0 PERCENT END DEVICE DEVICE #5: SIMPLE PIPE INLET NODE NUMBER IS 22 EXIT NODE NUMBER IS 23 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTIIALPY LOSS IS 0.0 KJ/KG END DEVICE DEVICE #6: SIMPLE TURBINE INLET NODE NUMBER IS 23 266 EXTRACTION #1 NODE NUMBER IS 24 EXTRACTION #2 NODE NUMBER IS 25 STAGE GROUP #1 EFFICIENCY IS 75% STAGE GROUP #2 EFFICIENCY IS 75% EXTRACTION #1 PRESSURE IS 7.5 MPA EXTRACTION #2 PRESSURE LS 5.0 MPA EXTRACTION #1 MASS FLOW RATE IS 5.0 KG/SEC END DEVICE DEVICE #7: SIMPLE PIPE INLET NODE NUMBER IS 25 EXIT NODE NUMBER IS 26 PIPE PRESSURE LOSS LS 0.0 MPA PIPE ENTHALPY LOSS 18 0.0 KJ/KG END DEVICE DEVICE #8: SIMPLE PIPE INLET NODE NUMBER IS 27 EXIT NODE NUMBER IS 28 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 KJ/KG END DEVICE DEVICE #9: SIMPLE TURBINE INLET NODE NUMBER IS 28 EXTRACTION #1 NODE NUMBER IS 29 EXTRACTION #2 NODE NUMBER IS 30 EXTRACTION #3 NODE NUMBER IS 32 EXTRACTION #4 NODE NUMBER IS 34 EXTRACTION #5 NODE NUMBER IS 36 STAGE GROUP #1 EFFICIENCY IS 75% STAGE GROUP #2 EFFICIENCY IS 75% STAGE GROUP #3 EFFICIENCY IS 75% STAGE GROUP #4 EFFICIENCY IS 75% STAGE GROUP #5 EFFICIENCY IS 75% EXTRACTION #1 PRESSURE IS 2.5 MPA EXTRACTION #2 PRESSURE IS 1.0 MPA EXTRACTION #3 PRESSURE LS 0.5 MPA EXTRACTION #4 PRESSURE LS 0.25 MPA EXTRACTION #5 PRESSURE LS 0.10 MPA EXTRACTION #1 MASS FLOW RATE 18 5.0 KG/SEC END DEVICE DEVICE #10: SIMPLE PIPE INLET NODE NUMBER IS 30 EXIT NODE NUMBER IS 31 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS LS 0.0 KJ/KG END DEVICE DEVICE #11: SIMPLE PIPE INLET NODE NUMBER IS 32 EXIT NODE NUMBER IS 33 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 ”MG END DEVICE DEVICE #12: SIMPLE PIPE INLET NODE NUMBER IS 34 EXIT NODE NUMBER IS 35 PIPE PRESSURE LOSS LS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 T(JIKG END DEVICE 267 DEVICE #13: SIMPLE PIPE INLET NODE NUMBER IS 36 EXIT NODE NUMBER IS 37 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS LS 0.0 KJIKG END DEVICE DEVICE #14: SIMPLE CONDENSER EXIT NODE NUMBER IS 1 INLET #1 NODE NUMBER IS 37 INLET #2 NODE NUMBER IS 44 INLET #3 NODE NUMBER IS 45 INLET #4 NODE NUMBER IS 46 END DEVICE DEVICE #15: SIMPLE PIPE - INLET NODE NUMBER IS 1 EXIT NODE NUMBER IS 2 PIPE PRESSURE LOSS LS 0.0 MPA PIPE ENTHALPY LOSS LS 0.0 LU/KG END DEVICE DEVICE #16: SIMPLE PUMP SUCTION NODE NUMBER IS 2 DISCHARGE NODE NUMBER IS 3 PUMP EFFICIENCY IS 75% END DEVICE DEVICE #17: SIMPLE PIPE INLET NODE NUMBER IS 3 EXIT NODE NUMBER IS 4 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 KJ/KG END DEVICE DEVICE #18: SIMPLE OFW HEATER FEED WATER INLET NODE NUMBER IS 4 FEED WATER EXIT NODE NUMBER IS 5 EXTRACTION INLET NODE NUMBER IS 35 END DEVICE DEVICE #19: SIMPLE PIPE INLET NODE NUMBER IS 5 EXIT NODE NUMBER IS 6 PIPE PRESSURE LOSS LS 0.0 MPA PIPE ENTHALPY LOSS LS 0.0 ”MG END DEVICE DEVICE #20: SIMPLE PUMP SUCTION NODE NUMBER IS 6 DISCHARGE NODE NUMBER IS 7 PUMP EFFICIENCY IS 75% END DEVICE DEVICE #21: SIMPLE PIPE INLET NODE NUMBER IS 7 EXIT NODE NUMBER IS 8 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 KJIKG END DEVICE DEVICE #22: SIMPLE OFW HEATER FEED WATER INLET INLET NODE NUMBER IS 8 FEED WATER EXIT NODE NUMBER IS 9 EXTRACTION INLET NODE NUMBER IS 33 268 END DEVICE DEVICE #23: SIMPLE PIPE INLET NODE NUMBER IS 9 EXIT NODE NUMBER IS 10 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 KJ/KG END DEVICE DEVICE #24: SIMPLE PUMP SUCTION NODE NUMBER IS 10 DISCHARGE NODE NUMBER IS 11 PUMP EFFICIENCY IS 75% ETD DEVICE DEVICE #25: SIMPLE PIPE INLET NODE NUMBER IS 11 EXIT NODE NUMBER IS 12 PIPE PRESSURE LOSS LS 0.0 MPA PIPE ETT'HALPY LOSS IS 0.0 LU/KG END DEVICE DEVICE #26: SIMPLE OFW HEATER FEED WATER EXIT NODE NUMBER IS 13 FEED WATER INLET NODE NUMBER IS 12 EXTRACTION INLET NODE NUMBER IS 31 END DEVICE DEVICE #27: SIMPLE PIPE INLET NODE NUMBER IS 13 EXIT NODE NUMBER IS 14 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 KJ/KG END DEVICE DEVICE #28: SIMPLE PUMP SUCTION NODE NUMBER IS 14 DISCHARGE NODE NUMBER IS 15 PUMP EFFLCLETCY IS 75% ETD DEVICE DEVICE #29: SIMPLE PIPE INLET NODE NUMBER IS 15 EXIT NODE NUMBER IS 16 PIPE PRESSURE LOSS LS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 KJ/KG END DEVICE DEVICE #30: SIMPLE PIPE INLET NODE NUMBER IS 19 EXIT NODE NUMBER IS 38 PIPE PRESSURE LOSS LS 0.0 MPA PIPE ENTHALPY LOSS LS 0.0 KJIKG ETD DEVICE DEVICE #31: SIMPLE HEAT LOAD INLET NODE NUMBER IS 38 EXIT NODE NUMBER IS 39 EXIT TEMPERATURE LS 175.7 DEG C ETD DEVICE DEVICE #32: SIMPLE PIPE LITLET NODE NUMBER IS 39 EXIT NODE NUMBER IS 44 269 PIPE PRESSURE LOSS LS 0.0 MPA PIPE ETTHALPY LOSS IS 0.0 KJ/KG END DEVICE DEVICE #33: SIMPLE PIPE INLET NODE NUMBER IS 24 EXIT NODE NUMBER IS 40 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 LU/KG END DEVICE DEVICE #34: SIMPLE HEAT LOAD IITLET NODE NUMBER IS 40 EXIT NODE NUMBER IS 41 DOT TEMPERATURE LS 175.7 DEG C ETD DEVICE DEVICE #35: SIMPLE PIPE INLET NODE NUMBER IS 41 E70? NODE NUMBER IS 45 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 KJ/KG END DEVICE DEVICE #36: SIMPLE PIPE INLET NODE NUMBER IS 29 EXIT NODE NUMBER IS 42 PIPE PRESSURE LOSS LS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 ”MG END DEVICE DEVICE #37: SIMPLE HEAT LOAD INLET NODE NUMBER IS 42 EXIT NODE NUMBER IS 43 EXIT TEMPERATURE TS 175.7 DEG C END DEVICE DEVICE #38: SIMPLE PIPE IITLET NODE NUMBER IS 43 EXIT NODE NUMBER IS 46 PIPE PRESSURE LOSS IS 0.0 MPA PIPE ENTHALPY LOSS IS 0.0 KJ/KG END DEVICE Appendix F: RANKINE 3.0 output files for benchmark case #1 through case #5 270 RANKINE 3.0: A steam power plant computer simulation Copyright 1994 W.A. Thelen, C.W. Somerton *********i***fi******************** TITLE *******************************t*** BENCHMARK CASE #1 ******************fi**i*****tttii NODE DATA *i*************i***************** NODE T(C) P(MPa) L Q 5(KJ/KG/K) H(KJ/KG) V(M‘3/KG) M(KG/S) A(KJ/KG) 1 99.63 .1000 4 ***** 1.3020 417.31 .00104 50.0000 33.47 2 103.52 20.0000 1 '***** 1.3228 448.50 .00105 50.0000 58.45 3 600.00 ,20.0000 3 ***** 6.5052 3536.61 .01808 50.0000 1601.44 4 99.63 .1000 2 .990 7.2962 2651.90 1.67621 50.0000 480.88 *ittttttttt****ttt*** DEVICE DATA (DEVICE BEFORE NODE) *tttitttitttttittttit NODE REV. WRK ACT. WRK IRREV HEAT X-FER MASS ERROR ENERGY ERROR (KW) (KW) (KW) (KW) (KG/ S) (KW) 1 22370.37 .00 22370.37 ~111729.90 .000 -.008 2 -1249.04 -1559.60 310.56 .00 .000 .000 3 71843.58 .00 71843.58 154405.60 .000 .000 4 56028.13 44235.28 11792.86 .00 .000 .000 t****************************** SYSTEM DATA it*********************tttttttit TOTAL MASS FLOW RATE EXITING SYSTEM: .0000 KG/SEC TOTAL MASS FLOW RATE ENTERING SYSTEM: .0000 KG/SEC TOTAL ENTHALPY FLOW RATE EXITING SYSTEM: .0000 KW TOTAL ENTHALPY FLOW RATE ENTERING SYSTEM: .0000 KW TOTAL HEAT AND WORK ENTERING SYSTEM: -.0039 KW BOILER HEAT (DEVICE # 4): 154405.6000 KW TOTAL BOILER HEAT: 154405.6000 KW TOTAL HEAT LOAD HEAT: .0000 KW CONDENSER HEAT (DEVICE # 2): -111729.9000 KW TOTAL PIPE ENERGY LOSSES: .0000 KW TURBINE WORK (DEVICE # 1): 44235.2800 KW NET WORK TO GENERATORS: 44235.2800 KW PUMP WORK (DEVICE # 3): -1559.6010 KW TOTAL PUMP WORK: ~1559.6010 KW GENERATOR MECHANICAL LOSSES: .0000 KW GENERATOR ELECTRICAL LOSSES: .0000 KW NET ELECTRICAL POWER: 42675.6800 KW SYSTEM HEAT RATE: 12345.0200 BTU/KW*HR CARNOT CYCLE EFFICIENCY: 65.8535 PERCENT IST LAW EFFICIENCY: 27.6387 PERCENT 2ND LAW EFFICIENCY: 42.8466 PERCENT 2ND LAW EFFECTIVENESS: 41.9699 PERCENT W.A. 271 Copyright 1994 Thelen, C.W. Somerton RANKINE 3.0: A steam power plant computer simulation *********************************i TITLE *ttitii**************************** BENCHMARK CASE #2 *ttttttttttt***********t******tt NODE DATA *****t************************t** NODE T(C) P(MPa) L Q S(KJ/KG/K) H(KJ/KG) V(M‘3/KG) M(KG/S) A(KJ/KG) 1 250.34 4.0000 4 ***** 2.7947 1087.16 .00125 23.6636 258.27 2 250.34 4.0000 4 ***** 2.7947 1087.16 .00125 23.6636 258.27 3 252.58 6.0000 1 ***** 2.7997 1098.06 .00126 23.6636 267.66 4 252.58 6.0000 1 ***** 2.7997 1098.06 .00126 23.6636 267.66 5 275.56 6.0000 4 ***** 3.0251 1213.37 .00132 25.0000 315.78 6 275.56 6.0000 4 ***** 3.0251 1213.37 .00132 25.0000 315.78 7 280.24 10.0000 1 ***** 3.0345 1235.51 .00133 25.0000 335.10 8 280.24 10.0000 1 ***** 3.0345 1235.51 .00133 25.0000 335.10 9 500.00 10.0000 3 ***** 6.5984 3374.66 .03275 25.0000 1411.69 10 500.00 10.0000 3 ***** 6.5984 3374.66 .03275 25.0000 1411.69 11 468.79 8.0000 3 ***** 6.6225 3321.17 .03951 5.0000 1351.00 12 430.55 6.0000 3 ***** 6.6540 3255.07 .05032 1.3364 1275.50 13 430.55 6.0000 3 ***** 6.6540 3255.07 .05032 1.3364 1275.50 14 380.21 4.0000 3 ***** 6.6993 3167.23 .07073 18.6636 1174.18 15 380.21 4.0000 3 ***** 6.6993 3167.23 .07073 18.6636 1174.18 16 500.00 10.0000 3 ***** 6.5984 3374.66 .03275 25.0000 1411.69 17 500.00 10.0000 3 ***** 6.5984 3374.66 .03275 .0000 1411.69 18 500.00 10.0000 3 ***** 6.5984 3374.66 .03275 25.0000 1411.69 19 468.79 8.0000 3 ***** 6.6225 3321.17 .03951 5.0000 1351.00 20 380.21 4.0000 3 ***** 6.6993 3167.23 .07073 5.0000 1174.18 21 380.21 4.0000 3 ***** 6.6993 3167.23 .07073 5.0000 1174.18 *********t***i*i***** DEVICE DATA (DEVICE BEFORE NODE) ********************* NODE REV. WRK ACT. WRK IRREV HEAT X-FER MASS ERROR ENERGY ERROR (KW) (KW) (KW) (KW) (KG/S) (KW) 1 21673.79 .00 21673.79 -49221.96 .000 .000 2 .00 .00 .00 .00 .000 .000 3 -222.35 -257.97 35.62 .00 .000 .000 4 .00 .00 .00 .00 .000 .000 5 143.95 .00 143.95 .00 .000 .001 6 .00 .00 .00 .00 .000 .001 7 -483.05 -553.59 70.55 .00 .000 .001 8 .00 .00 .00 .00 .000 .001 9 15406.16 .00 15406.16 53478.70 .000 .000 10 .00 .00 .00 .00 .000 -.002 11 1517.32 1337.32 179.99 .00 .000 .000 12 1509.85 1321.96 187.89 .00 .000 .000 13 .00 .00 .00 .00 .000 .000 14’ 1891.02 1639.32 251.69 .00 .000 .000 15 .00 .00 .00 .00 .000 .000 16 .00 .00 .00 .00 .000 -.002 17 .00 .00 .00 .00 .000 -.002 18 .00 .00 .00 .00 .000 .000 19 .00 .00 .00 .00 .000 .000 20 884.08 .00 884.08 -769.69 .000 .000 21 .00 .00 .00 .00 .000 .000 272 ****************************iii SYSTEM DATA ********************t*********** TOTAL MASS FLOW RATE EXITING SYSTEM: .0000 KG/SEC TOTAL MASS FLOW RATE ENTERING SYSTEM: .0000 KG/SEC TOTAL ENTHALPY FLOW RATE EXITING SYSTEM: .0000 KW TOTAL ENTHALPY FLOW RATE ENTERING SYSTEM: .0000 KW TOTAL HEAT AND WORK ENTERING SYSTEM: .0042 KW BOILER HEAT (DEVICE 4 18): 53478.7000 KW TOTAL BOILER HEAT: 53478.7000 KW HEAT LOAD HEAT (DEVICE 4 16): -769.6887 KW TOTAL HEAT LOAD HEAT: -769.6887 KW CONDENSER HEAT (DEVICE I 15): -49221.9600 KW TOTAL PIPE ENERGY LOSSES: .0000 KW TURBINE WORK (DEVICE 4 1): 4298.6090 KW NET WORK TO GENERATORS: 4298.6090 KW PUMP WORK (DEVICE 4 2): -257.9682 KW PUMP WORK (DEVICE 4 3): -553.5919 KW TOTAL PUMP WORK: -811.5601 KW GENERATOR MECHANICAL LOSSES: .0000 KW GENERATOR ELECTRICAL LOSSES: .0000 KW NET ELECTRICAL POWER: 3487.0490 KW SYSTEM HEAT RATE: 52327.7200 BTU/KW*HR CARNOT CYCLE EFFICIENCY: 61.4370 PERCENT 1$T LAW EFFICIENCY: 6.5204 PERCENT 2ND LAW EFFICIENCY: 27.9568 PERCENT 2ND LAW EFFECTIVENESS: 10.6132 PERCENT 273 RANKINE 3.0: A steam power plant computer simulation 0 Copyright 1994 W.A. Thelen, C.W. Somerton ********************************** TITLE *************************i********* BENCHMARK CASE #3 *************i*********tt**t**** NODE DATA iiiititit************t*********** NODE T(C) P(MPa) L Q S(KJ/KG/K) H(KJ/KG) V(M‘3/KG) M(KG/S) A(KJ/KG) 1 179.87 1.0000 4 ***** 2.1367 762.23 .00113 19.8440 129.52 2 179.87 1.0000 4 ***** 2.1367 762.23 .00113 19.8440 129.52 3 180.43 1.5000 1 ***** 2.1396 764.89 .00113 19.8440 131.31 4 180.43 1.5000 1 ***** 2.1396 764.89 .00113 19.8440 131.31 5 198.28 1.5000 4 ***** 2.3127 844.32 .00115 20.5434 159.12 6 198.28 1.5000 4 ***** 2.3127 844.32 .00115 20.5434 159.12 7 199.08 2.0000 1 ***** 2.3167 848.13 .00115 20.5434 161.74 8 199.08 2.0000 1 ***** 2.3167 848.13 .00115 20.5434 161.74 9 212.37 2.0000 4 ***** 2.4450 908.29 .00118 21.0980 183.65 10 212.37 2.0000 4 ***** 2.4450 908.29 .00118 21.0980 183.65 11 213.70 3.0000 1 ***** 2.4516 914.73 .00118 21.0980 188.14 12 213.70 3.0000 1 ***** 2.4516 914.73 .00118 21.0980 188.14 13 233.84 3.0000 4 ***** 2.6437 1008.11 .00122 22.0000 224.25 14 233.84 3.0000 4 ***** 2.6437 1008.11 .00122 22.0000 224.25 15 238.95 10.0000 1 ***** 2.6678 1033.26 .00123 22.0000 242.19 16 238.95 10.0000 1 ***** 2.6678 1033.26 .00123 22.0000 242.19 17 500.00 10.0000 3 ***** 6.5984 3374.66 .03275 22.0000 1411.69 18 500.00 10.0000 3 ***** 6.5984 3374.66 .03275 22.0000 1411.69 19 475.93 8.0000 3 ***** 6.6465 3339.00 .04002 2.0000 1361.70 20 446.67 6.0000 3 ***** 6.7093 3294.36 .05182 20.0000 1298.34 21 446.67 6.0000 3 ***** 6.7093 3294.36 .05182 20.0000 1298.34 22 408.49 4.0000 3 ***** 6.7994 3234.06 .07455 2.0000 1211.16 23 383.09 3.0000 3 ***** 6.8636 3192.52 .09644 .9020 1150.47 24 383.09 3.0000 3 ***** 6.8636 3192.52 .09644 .9020 1150.47 25 349.69 2.0000 3 ***** 6.9555 3136.46 .13854 .5547 1067.02 26 349.69 2.0000 3 ***** 6.9555 3136.46 .13854 .5547 1067.02 27 327.25 1.5000 3 ***** 7.0207 3097.87 .17902 .6994 1008.99 28 327.25 1.5000 3 ***** 7.0207 3097.87 .17902 .6994 1008.99 29 297.54 1.0000 3 ***** 7.1138 3045.89 .25684 15.8440 929.25 30 297.54 1.0000 3 ***** 7.1138 3045.89 .25684 15.8440 929.25 31- 475.93 8.0000 3 ***** 6.6465 3339.00 .04002 2.0000 1361.70 32 297.54 1.0000 3 ***** 7.1138 3045.90 .25685 2.0000 929.25 33 408.49 4.0000 3 ***** 6.7994 3234.06 .07455 2.0000 1211.16 34 297.54 1.0000 3 ***** 7.1138 3045.90 .25685 2.0000 929.25 35 297.54 1.0000 3 ***** 7.1138 3045.90 .25685 2.0000 929.25 36 297.54 1.0000 3 ***** 7.1138 3045.90 .25685 2.0000 929.25 ************i*t*t**** DEVICE DATA (DEVICE BEFORE NODE) ********************* NODE REV. WRK ACT. WRK IRREV HEAT X-FER MASS ERROR ENERGY ERROR (KW) (KW) (KW) (KW) (KG/S) (KW) 1 15869.79 .00 15869.79 -45316.91 .000 -.004 2 .00 .00 .00 .00 .000 .000 3 -35.56 -52.81 17.26 .00 .000 .001 4 .00 .00 .00 .00 .000 .000 5 42.51 .00 42.51 .00 .000 -.001 6 .00 .00 .00 .00 .000 .001 7 -53.80 ~78.31 24.51 .00 .000 .001 8 .00 .00 .00 .00 .000 .001 9 .00 39.97 .00 .000 .001 39.97 274 10 .00 .00 .00 .00 .000 -.001 11 -94.71 -135.85 41.14 .00 .000 -.001 12 .00 .00 .00 .00 .000 .000 13 73.62 .00 73.62 .00 .000 .001 14 .00 .00 .00 .00 .000 -.001 15 -394.70 -553.28 158.58 .00 .000 -.001 16 .00 .00 .00 .00 .000 -.001 17 15345.20 .00 15345.20 51510.73 .000 .000 18 .00 .00 .00 .00 .000 .004 19 1099.83 784.57 315.27 .00 .000 .000 20 1267.15 892.64 374.51 .00 .000 .000 21 .00 .00 .00 .00 .000 .001 22 1743.64 1205.98 537.65 .00 .000 .000 23 1092.44 747.89 344.55 .00 .000 .000 24 .00 .00 .00 .00 .000 .000 25 1426.84 958.52 468.32 .00 .000 .000 26 .00 .00 .00 .00 .000 .000 27 959.94 638.26 321.68 .00 .000 .000 28 .00 .00 .00 .00 .000 .000 29 1263.42 823.70 439.72 .00 .000 .000 30 .00 .00 .00 .00 .000 -.001 31 .00 .00 .00 .00 .000 .000 32 864.89 .00 864.89 -586.20 .000 .000 33 .00 .00 .00 .00 .000 .000 34 563.81 .00 563.81 -376.34 .000 .000 35 .00 .00 .00 .00 .000 .000 36 .00 .00 .00 .00 .000 .000 ******t************************ SYSTEM DATA *tttttttttt*t*t*t*tt*t********** TOTAL MASS FLOW RATE EXITING SYSTEM: TOTAL MASS FLOW RATE ENTERING SYSTEM: .0000 .0000 TOTAL ENTHALPY FLOW RATE EXITING SYSTEM: .0000 TOTAL ENTHALPY FLOW RATE ENTERING SYSTEM: .0000 TOTAL HEAT AND WORK ENTERING SYSTEM: -.0010 BOILER HEAT (DEVICE 4 1): 51510.7300 TOTAL BOILER HEAT: 51510.7300 HEAT LOAD HEAT (DEVICE 4 27): HEAT LOAD HEAT (DEVICE 4 30): TOTAL HEAT LOAD HEAT: CONDENSER HEAT (DEVICE 4 10): TOTAL PIPE ENERGY LOSSES: -376.3354 -586.1978 -962.5332 -45316.9100 .0000 TURBINE WORK (DEVICE 4 3): TURBINE WORK (DEVICE 4 5): NET WORK TO GENERATORS: 4374.3420 6051.5500 PUMP WORK (DEVICE 4 12): PUMP WORK (DEVICE 4 16): PUMP WORK (DEVICE 4 20): PUMP WORK (DEVICE 4 24): TOTAL PUMP WORK: GENERATOR MECHANICAL LOSSES: GENERATOR ELECTRICAL LOSSES: NET ELECTRICAL POWER: KW KW KW KW KW KW KW KW KW KW 1677.2080 KW KW KW -52.8148 KW -78.3066 KW -135.8547 KW -553.2777 KW -820.2538 KW .0000 KW .0000 KW 5231.2960 KW SYSTEM HEAT RATE: CARNOT CYCLE EFFICIENCY: 1$T LAW EFFICIENCY: 2ND LAW EFFICIENCY: 2ND LAW EFFECTIVENESS: 33596.7700 BTU/KW*HR 61.4370 PERCENT 10.1557 PERCENT 30.9454 PERCENT 16.5303 PERCENT 275 Copyright 1994 W.A. Thelen, C.W. Somerton RANKINE 3.0: A steam power plant computer simulation *ifititfitii*ttt*****iiittitttii*tii TITLE *****i*******t********tttttttttttti BENCHMARK CASE 44 ********************fi**fi**iii*** NODE DATA i***iittttiiiii********i********* NODE T(C) P(MPa) L Q S(KJ/KG/K) H(KJ/KG) V(M‘3/KG) M(KG/S) A(KJ/KG) 1 81.35 .0500 4 ***** 1.0903 340.37 .00103 37.5634 19.64 2 81.35 .0500 4 ***** 1.0903 340.37 .00103 37.5634 19.64 3‘ 81.39 .2500 1 ***** 1.0905 340.68 .00103 37.5634 19.88 4 81.39 .2500 1 ***** 1.0905 340.68 .00103 37.5634 19.88 5 127.43 .2500 4 ***** 1.6065 535.09 .00107 40.8093 60.45 6 127.43 .2500 4 ***** 1.6065 535.09 .00107 40.8093 60.45 7 127.52 .5000 1 ***** 1.6069 535.66 .00107 40.8093 60.91 8 127.52 .5000 1 ***** 1.6069 535.66 .00107 40.8093 60.91 9 151.84 .5000 4 ***** 1.8595 639.79 .00109 42.6969 89.73 10 151.84 .5000 4 ***** 1.8595 639.79 .00109 42.6969 89.73 11 152.05 1.0000 1 ***** 1.8601 640.98 .00109 42.6969 90.71 12 152.05 1.0000 1 ***** 1.8601 640.98 .00109 42.6969 90.71 13 179.87 1.0000 4 ***** 2.1367 762.23 .00113 45.0000 129.52 14 179.87 1.0000 4 ***** 2.1367 762.23 .00113 45.0000 129.52 15 182.43 10.0000 1 ***** 2.1453 778.01 .00113 45.0000 142.73 16 182.43 10.0000 1 ***** 2.1453 778.01 .00113 45.0000 142.73 17 400.00 10.0000 3 ‘***** 6.2158 3099.05 .02643 45.0000 1250.14 18 400.00 10.0000 3 ***** 6.2158 3099.05 .02643 45.0000 1250.14 19 371.03 8.0000 3 ***** 6.2382 3055.87 .03190 2.0000 1200.28 20 335.76 6.0000 3 ***** 6.2676 3002.49 .04065 43.0000 1138.15 21 335.76 6.0000 3 ***** 6.2676 3002.49 .04065 43.0000 1138.15 22 289.76 4.0000 3 ***** 6.3099 2931.51 .05718 2.0000 1054.54 23 259.48 3.0000 3 '***** 6.3400 2883.70 .07277 41.0000 997.76 24 259.48 3.0000 3 ***** 6.3400 2883.70 .07277 41.0000 997.76 25 400.00 3.0000 3 ***** 6.9215 3230.96 .09936 41.0000 1171.67 26 400.00 3.0000 3 ***** 6.9215 3230.96 .09936 41.0000 1171.67 27 353.22 2.0000 3 ***** 6.9681 3144.31 .13945 2.0000 1071.12 28 280.89 1.0000 3 ***** 7.0503 3010.18 .24854 2.3031 912.47 29 280.89 1.0000 3 ***** 7.0503 3010.18 .24854 2.3031 912.47 30 216.57 .5000 3 ***** 7.1331 2890.85 .44173 1.8876 768.45 31 216.57 .5000 3 ***** 7.1331 2890.85 ,.44173 1.8876 768.45 32 159.46 .2500 3 ***** 7.2163 2784.95 .78322 3.2458 637.74 33 159.46 .2500 3 ***** 7.2163 2784.95 .78322 3.2458 637.74 34 81.35 .0500 2 .972 7.4088 2580.28 3.14808 31.5634 375.69 35 81.35 .0500 2 .972 7.4088 2580.28 3.14808 31.5634 375.69 36 353.22 2.0000 3 ***** 6.9681 3144.31 .13945 2.0000 1071.12 37 81.35 .0500 2 .972 7.4088 2580.28 3.14808 2.0000 375.69 38 81.35 .0500 2 .972 7.4088 2580.28 3.14808 2.0000 375.69 39 81.35 .0500 2 .972 7.4088 2580.28 3.14808 2.0000 375.69 40 81.35 .0500 2 .972 7.4088 2580.28 3.14808 2.0000 375.69 41 289.76 4.0000 3 ***** 6.3099 2931.51 .05718 2.0000 1054.54 42 371.03 8.0000 3 ***** 6.2382 3055.87 .03190 2.0000 1200.28 43 81.35 .0500 2 .972 7.4088 2580.28 3.14808 2.0000 375.69 44 81.35 .0500 2 .972 7.4088 2580.28 3.14808 2.0000 375.69 *ttittiittttttttttttt DEVICE DATA (DEVICE BEFORE NODE) tttitttitttttttttittt NODE REV. WRK ACT. WRK IRREV HEAT X-FER MASS ERROR ENERGY ERROR (KW) (KW) (KW) (KW) (KG/S) (KW) 1 13374.69 .00 13374.69 -84138.79 .008 276 2 .00 .00 .00 .00 .000 .000 3 ‘ -9.31 -11.79 2.48 .00 .000 .002 4 .00 .00 .00 .00 .000 .000 5 350.10 .00 _350.10 .00 -000 -.001 6 .00 .00 .00 .00 .000 .001 7 -19.00 -23.34 4.34 .00 .000 .001 8 .00 .00 .00 .00 .000 .001 9 105.04 .00 105.04 .00 .000 .000 10 .00 .00 .00 .00 .000 .000 11 -41.84 -50.72 8.87 .00 .000 .000 12 .00 .00 .00 .00 .000 .000 13 146.20 ,.00 146.20 .00 .000 -.002 14 .00 .00 .00 .00 .000 -.002 15 -594.18 -709.90 115.71 .00 .000 -.002 16 .00 .00 .00 .00 .000 .002 17 18856.23 .00 18856.23 104447.00 .000 .000 18 .00 .00 .00 .00 .000 -.002 19 2243.78 1942.94 300.83 .00 .000 .000 20 2671.75 2295.33 376.42 .00 .000 .000 21 .00 .00 .00 .00 .000 .000 22 3595.13 3052.43 542.70 .00 .000 .000 23 2327.83 1960.23 367.60 .00 .000 .001 24 .00 .00 .00 .00 .000 -.001 25 1810.01 .00 1810.01 14237.95 .000 .000 26 .01 .00 .01 .00 .000 .001 27 4122.44 3552.83 569.61 .00 .000 .000 28 6187.20 5230.97 956.23 .00 .000 .000 29 .00 .00 .00 .00 .000 .000 30 5285.17 4379.08 906.09 .00 .000 .000 31 .00 .00 .00 .00 .000 .000 32 4549.93 3686.26 863.67 .00 .000 .000 33 .00 .00 .00 .00 .000 .000 34 8271.18 6460.11 1811.07 .00 .000 .006 35 .00 .00 .00 .00 .000 .000 36 .00 .00 .00 .00 .000 .000 37 1390.86 .00 1390.86 -1128.06 .000 .000 38 .00 .00 .00 .00 .000 .000 39 .00 .00 .00 .00 .000 .000 40 1357.70 .00 1357.70 -702.45 .000 .000 41 .00 .00 .00 .00 .000 .000 42 .00 .00 .00 .00 .000 .000 43 1649.18 .00 1649.18 -951.19 .000 .000 44 .00 .00 .00 .00 .000 .000 *************t***************** SYSTEM DATA *iit*‘k****************t*****fi*** TOTAL MASS FLOW RATE EXITING SYSTEM: TOTAL MASS FLOW RATE ENTERING SYSTEM: .0000 KG/SEC .0000 KG/SEC TOTAL ENTHALPY FLOW RATE EXITING SYSTEM: .0000 KW TOTAL ENTHALPY FLOW RATE ENTERING SYSTEM: .0000 KW TOTAL HEAT AND WORK ENTERING SYSTEM: -.0039 KW BOILER HEAT (DEVICE 4 1): 118684.9000 KW TOTAL BOILER HEAT: 118684.9000 KW HEAT LOAD HEAT (DEVICE 4 29): -951.1870 KW HEAT LOAD HEAT (DEVICE 4 32): -702.4536 KW HEAT LOAD HEAT (DEVICE 4 35): ~1128.0580 KW TOTAL HEAT LOAD HEAT: -2781.6990 KW CONDENSER HEAT (DEVICE 4 12): -84138.7900 KW TOTAL PIPE ENERGY LOSSES: .0000 KW TURBINE WORK (DEVICE 4 3): 4238.2780 KW TURBINE WORK (DEVICE 4 7): 23309.2500 KW TURBINE WORK (DEVICE 4 37): 5012.6660 KW NET WORK TO GENERATORS: PUMP WORK (DEVICE 4 14): PUMP WORK (DEVICE 4 18): PUMP WORK (DEVICE 4 22): PUMP WORK (DEVICE 4 26): TOTAL PUMP WORK: GENERATOR MECHANICAL LOSSES: GENERATOR ELECTRICAL LOSSES: NET ELECTRICAL POWER: SYSTEM HEAT RATE: CARNOT CYCLE EFFICIENCY: 1$T LAW EFFICIENCY: 2ND LAW EFFICIENCY: 2ND LAW EFFECTIVENESS: 277 32560.1900 -11.7890 -23.3438 -50.7156 -709.8953 -795.7437 .0000 .0000 31764.4500 12748.6200 55.7082 26.7637 56.6917 48.0426 §§§§§§§§ § 278 Copyright 1994 W.A. Thelen, C.W. Somerton RANKINE 3.0: A steam power plant computer simulation fi*******fi************************* TITLE **************************iti****** BENCHMARK CASE 45 *i****************************** NODE DATA *****i***********t*************** NODE T(C) P(MPa) L Q S(KJ/KG/K) H(KJ/KG) V(M‘3/KG) M(KG/S) A(KJ/KG) 1 99.63 .1000 4 ***** 1.3020 417.31 .00104 43.6475 33.47 2 99.63 .1000 4 ***** 1.3020 417.31 .00104 43.6475 33.47 3 99.68 .2500 1 ***** 1.3022 417.59 .00104 43.6475 33.70 4 99.68 .2500 1 ***** 1.3022 417.59 .00104 43.6475 33.70 5 127.43 .2500 4 ***** 1.6065 535.09 .00107 45.7481 60.45 6 127.43 .2500 4 ***** 1.6065 535.09 .00107 45.7481 60.45 7 127.52 .5000 1 ***** 1.6069 535.66 .00107 45.7481 60.91 8 127.52 .5000 1 ***** 1.6069 535.66 .00107 45.7481 60.91 9 151.84 .5000 4 ***** 1.8595 639.79 .00109 47.6790 89.73 10 151.84 .5000 4 ***** 1.8595 639.79 .00109 47.6790 89.73 11 152.05 1.0000 1 ***** 1.8601 640.98 .00109 47.6790 90.71 12 152.05 1.0000 1 ***** 1.8601 640.98 .00109 47.6790 90.71 13 179.87 1.0000 4 ***** 2.1367 762.23 .00113 50.0000 129.52 14 179.87 1.0000 4 ***** 2.1367 762.23 .00113 50.0000 129.52 15 185.00 20.0000 1 ***** 2.1542 794.40 .00113 50.0000 156.46 16 185.00 20.0000 1 ***** 2.1542 794.40 .00113 50.0000 156.46 17 600.00 20.0000 3 ***** 6.5052 3536.61 .01808 50.0000 1601.44 18 600.00 20.0000 3 ***** 6.5052 3536.61 .01808 50.0000 1601.44 19 554.33 15.0000 3 ***** 6.5358 3460.98 .02304 1.0000 1516.67 20 494.41 10.0000 3 ***** 6.5799 3360.38 .03242 49.0000 1402.94 21 494.41 10.0000 3 ***** 6.5799 3360.38 .03242 49.0000 1402.94 22 600.00 10.0000 3 ***** 6.8991 3621.73 .03828 49.0000 1569.12 23 600.00 10.0000 3 ***** 6.8991 3621.73 .03828 49.0000 1569.12 24 557.45 7.5000 3 ***** 6.9314 3541.65 .04878 5.0000 1479.39 25 501.09 5.0000 3 ***** 6.9777 3435.14 .06862 44.0000 1359.07 26 501.09 5.0000 3 ***** 6.9777 3435.14 .06862 44.0000 1359.07 27 600.00 5.0000 3 ***** 7.2540 3662.39 .07860 44.0000 1503.96 28 600.00 5.0000 3 ***** 7.2540 3662.39 .07860 44.0000 1503.96 29 505.66 2.5000 3 ***** 7.3367 3472.55 .14102 5.0000 1289.44 30 395.43 1.0000 3 ***** 7.4490 3253.16 .30442 2.3210 1036.57 31 395.43 1.0000 .3 ***** 7.4490 3253.16 .30442 2.3210 1036.57 32 320.86 .5000 3 ***** 7.5329 3106.73 .54259 1.9309 865.14 33 320.86 .5000 3 ***** 7.5329 3106.73 .54259 1.9309 865.14 34 253.64 .2500 3 ***** 7.6171 2976.46 .96451 2.1007 709.77 35 253.64 .2500 3 ***** 7.6171 2976.46 .96451 2.1007 709.77 36 175.68 .1000 3 ***** 7.7309 2827.51 2.05840 32.6475 526.88 37 175.68 .1000 3 ***** 7.7309 2827.51 2.05840 32.6475 526.88 38 554.33 15.0000 3 ***** 6.5358 3460.98 .02304 1.0000 1516.67 39 175.70 .1000 3 ***** 7.7310 2827.54 2.05849 1.0000 526.90 40 557.45 7.5000 3 ***** 6.9314 3541.65 .04878 5.0000 1479.39 41 175.70 .1000 3 ***** 7.7310 2827.54 2.05849 5.0000 526.90 42 505.66 2.5000 3 ***** 7.3367 3472.55 .14102 5.0000 1289.44 ‘43 175.70 .1000 3 ***** 7.7310 2827.54 2.05849 5.0000 526.90 44 175.70 .1000 3 ***** 7.7310 2827.54 2.05849 1.0000 526.90 45 175.70 .1000 3 ***** 7.7310 2827.54 2.05849 5.0000 526.90 46 175.70 .1000 3 ***** 7.7310 2827.54 2.05849 5.0000 526.90 279 ***i*t*************** DEVICE DATA (DEVICE BEFORE NODE) ********************* NODE REV. WRK ACT. WRK IRREV - HEAT X-FER MASS ERROR ENERGY ERROR (KW) (KW) (KW) (KW) (KG/S) (KW) 1 21536.46 .00 21536.46 -105199.70 .000 .016 2 p .00 .00 .00 .00 .000 .000 3 -10.11 -12.63 2.53 .00 .000 .000 4 .00 .00 .00 .00 .000 .001 5 196.52 .00 196.52 .00 .000 .000 6 .00 .00 .00 .00 .000 .000 7 -21.30 -26.17 4.87 .00 .000 .000 8 .00 .00 .00 .00 .000 .001 9 178.76 .00 178.76 .00 .000 .000 10 .00 .00 .00 .00 .000 .000 11 -46.72 -56.63 9.91 .00 .000 .000 12 .00 .00 .00 .00 .000 .000 13 254.86 .00 254.86 .00 .000 .002 14 .00 .00 .00 .00 .000 .002 15 -1346.88 -1608.31 261.43 .00 .000 .002 16 .00 .00 .00 .00 .000 .000 17 52840.78 .00 52840.78 137110;60 .000 .000 18 .00 .00 .00 .00 .000 .000 19 4238.50 3781.70 456.80 .00 .000 .000 20 5572.79 4929.13 643.66 .00 .000 .005 21 .00 .00 .00 .00 .000 .006 22 850.56 .00 850.56 12806.20 .000 .006 23 .01 .00 .01 .00 .000 .005 24 4396.73 3924.03 472.70 .00 .000 .000 25 5294.03 4686.43 607.60 .00 .000 .007 26 .00 .00 .00 .00 .000 .001 27 613.13 .00 613.13 9998.87 .000 .001 28 .01, .00 .01 .00 .000 .005 29 9438.87 8352.90 1085.97 .00 .000 .000 30 9861.99 8556.09 1305.90 .00 .000 .000 31 .00 .00 .00 .00 .000 .000 32 6287.99 5370.97 917.02 .00 .000 .000 33 .00 .00 .00 .00 .000 .000 34 5398.73 4526.77 871.96 .00 .000 .000 35 .00 .00 .00 .00 .000 .000 36 5970.83 4862.75 1108.08 .00 .000 .000 37 .00 .00 .00 .00 .000 .002 38 .00 .00 .00 .00 .000 .000 39 989.77 .00 989.77 -633.43 .000 .000 40 .00 .00 .00 .00 .000 .000 41 4762.47 .00 4762.47 -3570.52 .000 .000 42 .00 .00 .00 .00 .000 .000 43 3812.74 .00 3812.74 -3225.02 .000 .000 44 .00 .00 .00 .00 .000 .000 45 .00 .00 .00 .00 .000 .000 46 .00 .00 .00 .00 .000 .000 ******************************* SYSTEM DATA *iiti*****************t********* TOTAL MASS FLOW RATE EXITING SYSTEM: TOTAL MASS FLOW RATE ENTERING SYSTEM: .0000 KG/SEC .0000 KG/SEC TOTAL ENTHALPY FLOW RATE EXITING SYSTEM: .0000 KW TOTAL ENTHALPY FLOW RATE ENTERING SYSTEM: .0000 KW TOTAL HEAT AND WORK ENTERING SYSTEM: -.0039 KW BOILER HEAT (DEVICE 4 1): 159915.7000 KW TOTAL BOILER HEAT: 159915.7000 KW HEAT LOAD HEAT (DEVICE 4 31): -633.4307 KW HEAT LOAD HEAT (DEVICE 4 34): -3570.5250 KW 280 'HEAT LOAD HEAT (DEVICE 4 37): TOTAL HEAT LOAD HEAT: CONDENSER HEAT (DEVICE 4 14): TOTAL PIPE ENERGY LOSSES: TURBINE WORK (DEVICE 4 3): TURBINE WORK (DEVICE 4 6): TURBINE WORK (DEVICE 4 9): NET WORK TO GENERATORS: PUMP WORK (DEVICE 4 16): PUMP WORK (DEVICE 4 20): PUMP WORK (DEVICE 4 24): PUMP WORK (DEVICE 4 28): TOTAL PUMP WORK: GENERATOR MECHANICAL LOSSES: GENERATOR ELECTRICAL LOSSES: NET ELECTRICAL POWER: SYSTEM HEAT RATE: CARNOT CYCLE EFFICIENCY: IST LAW EFFICIENCY: 2ND LAW EFFICIENCY: 2ND LAW EFFECTIVENESS: -3225.0180 -7428.9740 -105199.7000 .0000 8710.8320 8610.4610 31669.4800 48990.7800 -12.6342 -26.1689 -56.6334 -1608.3100 -1703.7460 .0000 .0000 47287.0400 11538.7300 65.8535 29.5700 57.0444 44.9027 §§§§§§§§ §§§§ §§§§ Appendix G: Hand calculations for benchmark case #6 281 9...... E .3... 6 .4. 2:. a 5.. c... .u... E... 6.. co... id» 6.23. .. 3.6 o .23 6 gfind E. .4325! ugiétizln .. tau 2.... o on i -: x o o c o o 3.3. 8.... .23... 6 .3. E... .5. 2.6 9.... 33 co... El .9 15...... I .30 2.2%..3. 6 gal... 2.3.3.53... ugiégpifio 32%;... 6 Tammi... 5.33053... ogiéuiihfifo or. is: 15...: a. 3.6 3.3. 88 o .3... ..o r! 926 o .8... .E no.0 Hi4: Iii: .. 3.3 5.2%....6 52%;... ...EHI-...=.§. 9...... a .3... .6 a... 5...... d 3 ”Mi... a. 9...... 35. E .3... 6 a! €4.98 z 3 Sui... : 95.. 9..3.%..3~ 6 23%....8 .E ..fli......§nsrt 9.3. a .3... 6 .9 Haul .8... d . Jamal... I an 9. r... 23.5.0320 igién .. Zuni-SIS... r: 2.2%....“ .o axial. : Sal... .- .8... r... 9...... E 6.2 6 .3. €37... 3.. 3 Hi... 9 .3 2. 2.. oégfiéau 6 .5583 .. 3i... «.3... E. meifiéa... 6 lags“... .. Sailing r... 32%;”... 6 said... .. :al....§§2.u.t! «(PE-.3. 6 salié .... :EI.§=S.8«:.! 32%....6 lanai-3...... :Ei.......u€:r! 2...: _w 9. not-2.8 a... 5.... “.3... o... :8. p a... 3.2.34.2..{0 .201... .61. a... a... .3... .4. I 33 «.523... .32.... .3... . 3.4-2.3.3.0 5.35 3... .34.. a... arts-4.33.6 .1 .... 4.4. .tIsnISIuo no.6... .3...» 3.333.325... 6.98:... 48.35.13 3.4.4.638 6.93.. 3.326.244... Its-8.8:: :8...“ 6:42:46: wig-.438 mods... not-3.6.9.13 . 1:66.43.in .983... égtg =z