ll | l | | | MV 107 812 THS, iS) ae 30 TON REFRIGERATION PLANT THESIS FOR DEGREE OF M. E. OMA eR E ay wal es) PY THESIS Test of a 40 TON REFRIGERATION PLANT by yo "Nd : y iQ \. wt tr _it 'Y 0. W: FAIRBANES ee . a Lansing, Michigan Mic 1922 THESIS THESIS TEST OF A 5O TOM REFRIGERATION PLANT. The plant under test is situated in Holland, Michigan on the edge of Black Lake. The equipment consists of:- 1 - 100 H. P. horozontal fire-tube Boiler, mdde by the Muskegon Boiler Works. See sketch 2. L - 20 ton Ammonia Compressor, made by the Cleveland Ice Machine Co. See picture 3 and sketch 2. Ll - &O H. P. Nagle Corliss Steam Engine, direet con- nected to above compressor. see picture 3 and sketch 2. 1 - 10 ton Ice Tank 14 ft. 6 in. X 36 ft. X 4 ft. deep containing 154 - 500 lb. ice cans and 96 - 2 in. ammonia expansion pipes 30 ft. long and connected three groups in parallel to a proper header. See sketches 2 and 3. 1 - 10 ton Ammonia Compressor, made by the york Mfg. Company. see sketches 2 and 3 and picture 4. l- 40 H. P. Slide Valve Steam Engine, belt connected to above compressor. See picture 4 and sketches 2 and 3. Ll - 5 ton Ice Tank 11 ft. X 22 ft. X 3 ft. deep containing 82 - 200 lb. ice cans and a 20 in. dia. X 6 ft. long ammonia drum with 2 in. tubes. See sketch 2. l1- 32 X 3 X 4 Single Cylinder Double Acting Feed Water Pump. See sketch 2. L-°565X 35 X 3 Duplex Double Acting lake water Pump designated as pump No. 1. See sketch 2. 536076 1-65 X 4X 5 Single Cylinder Double Acting well water Pump, designated as pump No. 2. See sketch 2. l1=- 6 X 4 X & Duplex Double Acting lake water Pump, designated as pump No. 3. see sketch 2. 1-5 H. P. Slide Valve Steam Engine, belt connected to two brine agitators, one in each tank. See sketches 2 anu 3- 1 Open Air Condenser, situated on the roof and consist- | ing of two stands in parallel of 2 in. pipes, 20 pipes high and 20 ft. long. See picture 1 and sketch 3. l Double Tube Condenser, situated inside the engine room, connected in series with the Open Air Condenser and consisting of two stands in parallel of 2 in. pipe outside with 1-1/4 in. inside, 8 pipes high and 15 ft. long. see sketch 2. 1 Flat Cooler, situated inside the engine room and consisting of 4 - 24 in. pipes and 4 - 2 in. pipes outside with 1-1/4 in. pipes inside, 8 pipes high and 18 ft. 10 in. long. See sketch 2. 2 Ammonia traps, 1 Steam Oil Trap, I Pure Water Reboiler, 1 Skimmer, 2 Pure Water Storage Tank (see sketch 2), 1 Ammonia Storage Tank, and many other small necessities not dealt with in this thesis. SIGNIFICANT ITEMS AND PECULIAR CONDITIONS PERTAINING TO THIS PLANT- All ice is made from condensed steam, reboiled, skimmed, filtered and cooled after leaving the exhaust from the engines and pumps. Tne boiler feed water is obtained from two open wells about 22 ft. deep, at an average temperature of 53.2° F. It is forced through the double pipe condenser and flat cooler before being pumped into the boiler by the boiler feed water pump. Its temperature as it enters the boiler is about 110°F. The open air condenser is partly protected from winds from the south by the upright portion of the building and the windbrake built above the building, and from the west by a windbrake built between it and the smoke stack. see photo 1 and sketch 3. The cooling water for the single tube condenser is pumped directly from the lake by pumps 1 and 3. The tem- perature of the water varies with the temperature of the lake. During the test it varied from 72 to 80° PF, see log sheets la and lb. OBJECT OF TEST. The object of the test was to determine;- A. The direct cost of manufacturing ice at this plant. B. The rate of heat transfer from the pure water thru the various stages until it finally reaches the cooling water. C. The influence of air temperatures and wind directions and velocities on the condensing properties of the single tube condenser. D. The influence of cooling water temperatures on the condensing properties of the condensers. From the required data taken many empirical plant constants were determined which are of value in comparing the plant performance of this plant with that of other plants. It was found necessary to take separate data on both ice tanks and on both ammonia compressors. From this data comparative values were deduced. These values on the ice tanks are of interest in that they show the comparative performance of the 5 ton ammonia drum tank with the 10 ton ammonia pipe tank. A. DIRECT COST. In determining the direct cost of manufacturing ice only these three items were considered:- Fuel, labor and oil. To determine the cost per ton of ice produced, it was necessary to determine the amount of ice produced per unit of time. From 50 to 65 tests were taken to determine; first, the amount of fuel used and cost of same per hour; second, the amount of ice produced per day for each day of the test. The oil used was approximated over several days and an average taken. Cup grease and three kinds of oil were used, and the amounts used, price and price per hour are given below. Cost per Hr. Kind Amt. Used Time Cost in dollars. Compressor oil 1 pint 9 hrs. 42¢ per gal. 0.006 Cylinder oil 3 qts. 14 hrs. 85¢ per gal. 0.046 Machine oil 1 gal. 24 hrs. 42¢ per gal. 0.018 Cup grease 1/4 lb. 24 hrs. 15¢ per lb. 0.001 Total cost per hour $0.071 Labor costs cover the wages of three engineers and two ice pullers per day of 24 hours. Their wages are as follows:- Chief Engineer"s salary is $1300.00 per year. First Assistant Engineer receives $5.00 per day of 9 hrs. Second Assistant Engineer receives $4.00 per day of 9 hrs. Ice Pullers each receive $3.75 per day for 12 hours pull. Total labor cost per 24 hour day is $20.85 (the sum of three engineers and two ice pullers* daily wages). Labor cost per hour is §20.85 / 24 = §$0.869 The table showing fuel comsumed is given on B. P. l. The general averages show that 460 pounds of coal were consumed per hour at an average cost of $1.662 per hour. The amount of ice produced is shown on B. P. 2&2. This shows that during the test 1,983,000 pounds or 991.5 tons of ice were produced. This was at an average rate of 1858 pounds per hour or 22.3 tons per day of 24 hours. DIRECT COSTS PER TON OF ICE. Oil cost pet ton of ice is 0.071 X 2000 / 1858 = $0.076 Labor cost per ton of ice is 0.869 X 2000 / 1858 = 0.936 Fuel cost per ton of ice is 1.662 X 2000 / 1858 = 1.789 Total direct cost per ton of ice is +2 .800 Bs HEAT TRANSFER. The well water is pumped from the wells by pump No. 2. It passes through the double tube ammonia condenser, through the flat cooler, through the preheater, and through the boiler feed pump into the boiler. On this part of its journey it absorbs heat. It leaves the boiler as steam, passes through the engines and pumps, through the steam condenser where it is condensed into water, through the reboiler and skimmer, through the flat cooler and into the pure water storage tank. Here an ammonia coil removes heat from it and reduces its temperature from 87.7°F. to 46.7°F. ( see page 10) From the storage tank the water is drawn into the ice cans and is frozen into ice. The brine in the ice tank absorbs the heat from the pure water through the cans, and it in turn gives up its heat to the ammonia in the ammonia pipes or drum through which it is caused to circulate by the brine agitators. Hence all the heat, including that taken directly from the water in the storage tank, that absorbed from the brine in both the ice tanks and that absorbed by the ammonia coils in cooling the cold storage room, must pass into the ammonia before it reaches the compressors. In passing through the compressors the ammonia absorbs still more heat from the energy of compression. However the ammonia in the 10 ton compressor gives up a small amount of its heat to the water in the water jacket around its cyl- inders. The rest of the heat must be removed from the ammonia by the cooling waters in the single tube condenser and in the double tube condenser. In order to determine the heat transfer per unit from the pure water to the brine, from the brine to the ammonia, from the ammonia to the cooling water, it was necessary to take the temperature and pressure measurements as tabulated below. Many of these values vary somewhat during the day so it was thought advisable to take the readings as near the same time each day as possible. The time chosen was between 2 and 3 P. M. Temperature readings were taken of the following:- lL. Pure water as it enters the storage tank. g- Pure water as it enters the ice cans to be frozen. 3. Outside air taken in the shade. 4. Cooling water from the lake as it leaves the pump to flow over the single tube condenser. 5S. Cooling water as it leaves the single tube condenser. 6. Cooling water from the well as it enters the double tube condenser. 7. Cooling water as it leaves the double tube condenser. 8. Liquid ammonia as it enters the expansion coils and drum in the ice tanks. 9. Ammonia gas as it leaves the expansion coils and drum and enters the compressors. 10 & 11. Ammonia gas as it leaves each compressor. 12 & 13. The brine in each tank. The high and low ammonia pressures were taken each day. The high shows the pressure of the ammonia entering the condenser pipes. The low shows the pressure of the ammonia leaving the expansion coils and drun. The R. P. M. of both compressors and the double strokes of the three pumps pumping cooling water were taken for 47 days. Temperatures 1, 6. and 7 of the water were taken by obtaining water through a valve at the desired location and by reading the temperature directly from a thermometer placed in it. Temperatures 2, 4 and 5 were taken by thrusting the the thermometer directly into the water where it was exposed. AMMONIA TEMPERATURES. A flat place was filed on one side of the pipe through which the ammonia was passing. A piece of copper tubing about 4 inches long and big enough to easily hold a thermometer was filed flat on one side, plugged at the lower end and partly filled with mercury. This was tied to the pipe with the flat sides together. A piece of woolen cloth was bound round and round the tube and pipe together until it formed a covering about 1 or 1-1/2 inches thiek. The cloth at the top was left slightly loose so that a thermometer could be thrust down into the mercury well and the temperature taken. See photo No. 2 and sketch No. l. The first readings of the temperatures showed that the cooler cooling water was flowing over the single tube condenser whereas the double tube condensers, where the final ammonia cooling took place, was receiving the warmer water. This condition was caused by pumping both the well water through pump No. 2 and the lake water through pump No. 1 onto the single tube condenser and using only lake water through pump No. 3 in the double tube condenser. The temperature of the well water was 52°F., of the lake water was 73°F. and of the well and lake water combined was 66°F. The pumps were changed about during the afternoon so that the cold water from the well was used in the double tube condenser and the lake water on the single tube condenser. There was an immediate drop of 10 pounds in the high ammonia pressure showing that there had been an improve- ment in the plant performance. Readings of the various items given above were taken nearly every day from June 28th to August 3lst. This data is given on log sheets la, lb, 2a and 2b. The different readings of any one item fluctuated somewhat from day to day due to the varying conditions prevalent; when the brine temperature went up less ice was pulled, when the lake water was cold the liquid ammonia temperature was reduced causing a drop in nearly all temperatures as well as in the ammonia pressures. Hence these individual values do not furnish a satisfactory basis for thermodynamic computations, but the general averages of these values will show the average conditions and will form a very satisfactory basis for computations. The arithmetical averages of these items are given below. All readings of June 28th 2 P. M. were omitted due to the change in pumps. LO AVERAGES. Average temperature of pure water entering storage tank = 87.7°F Average temperature of pure water entering ice cans = 46.7 F Average temperature of cooling water entering single tube condenser = 76.2°F Average temperature of cooling water leaving single tube condenser = 80.9°F Average temperature of cooling water entering double tube condenser = 53.2°F Average temperature of cooling water leaving double O tube condenser = 81.1 °F Average temperature of ammonia liquid entering 0 expansion coils and drum = a 69.6 F -. Average temperature of ammonia gas leaving expansion coils and drum = 12.9°F Average temperature of ammonia gas leaving 20 ton 6 compressor = 240.6 F Average temperature of ammonia gas leaving 10 ton 0 compressor = 188.0 F Average temperature of brine in 10 ton tank = 15.0°R Average temperature of brine in 5 ton tank = 13.9°F Average low ammonia pressure = c2.-5 lbs. per sq. in. gage Average high ammonia pressure = 165.1 lbs. per sq. in. gage Average R. P. M. of 20 ton compressor = 101.5 Average R. P. M. of 10 ton compressor = 175.6 Average double strokes of pump No. 1 = 115.0 Average double strokes of pump No. 2 = 47.0 Average double strokes of pump No. 3 = 50.5 Total number of hours plant was under operation during test = 1067 HEAT TRANSFER FROM PURE WATER TO BRINE. The total amount of heat transferred from the pure water to the brine per hour is equivalent to the heat lost by the water in changing from water at 46.7°F to ice at 15.0°F. in the 10 ton tank or to ice at 13.9°F. in the 5 ton tank. TH =W(t- 32 f/L# B( 32 - tz)) Where T.H. is the total heat transferred from the pure water to the brine. W is the weight of ice frozen. t is the temperature of the water entering the ice cand. L is the latent heat of fusion of ice = 144 B. T. U. 8 is the specific heat of ice = 0.5 ts is the temperature of the ice taken from the brine and equals the temperature of the brine. Lil W for the 10 ton tank is equal to 300 X N. Where N is the number of 300 lb. cakes produced divided by the number of hours the plant was in operation. See log sheets 2a and 2b. W for the 5 ton tank is equal to 200 X Ni Where N, is the number of 200 lb. cakes produced divided by the number of hours the plant was in operation. W for 10 ton tank W for 5 ton tank 1387 lbs. 471 lbs. Total heat transferred from pure water to brine in the 10 ton tank per hour = 1387 ( 46.7 - 32 # 144 # 0.5 (32 - 15)) = 231,906 B. T. U. Total heat transferred from pure water to brine in the 5 ton tank per hour is 471 ( 46.7 - 32 #¢ 144 # 0.5 (32 - 13.9)) = 79,010 B. T. U. The rate of heat transfer through the ice cans = T.H./nA Where T.H. is the total heat transferred, n is the number of ice cans in the tank and A is the area of each can where it is exposed to the brine.. n is 154 for the 10 ton tank and 82 for the 5 ton tank. see page 1 of this thesis. Area of ice can exposed to brine = 1/2 L(B/D/b/d)?7 bd. Where L is the length of the can exposed to the brine, B and D are width and thickness of the can at the upper surface of the brine and b ahd d are the width and thickness at the small end of the can. See sketch No. 4 for these values. A for 300 lb. can = 40.5/2 ( 22 # 11 ¢ 20.5 7/ 9.5) # 20.5 X¥ 9.5 = 1470.5 sq. in. or 10.21 sq. ft. A for 200 lb. can = 26.5/2 ( 22 £ 11.5 # 21 # 10.25) + 21%X% 10.25 = 1073.2 sq. in. or 7.45 sq. ft. L2 Rate of heat transfer through ice cans in 10 ton tank = 231,906 /( 154 X 10.21) = 141 B. T. U. per sq. ft. per hr. Rate of heat transfer through ice cans in 5 ton tank 79,010 /( 82 X 7.45) = 129 B. T. U. per sq. ft. per hr. HEAT TRANSFER TO AMMONIA. The ammonia absorbs heat at four different places before it reaches the compressors:- in the pure water storage tank, in both ice tanks and in the cold storage roon. In the pure water storage tank the heat passes directly from the pure water through the ammonia pipes of the ammonia coil into the ammonia. The amount absorbed by the ammonia equals the amount lost by the pure water. Heat lost by the water in the storage tank per hour =Wi(t'-t ) Where W is the weight of water passing through the tank per hour and is equivalent to the weight of ice frozen = 1858 lbs. per hour. See B. P. 2. t* is the temperature of the water entering the tank = 87.7°F. See page 10 item l. t is the temperature of the water leaving the tank and entering the ice cans = 46.7°F. See page 10 item 2. Heat lost by water in storage tank = 1858 ( 87.7 - 46.7) = 76,178 B. T. U. per hour. Heat absorbed by the ammonia in the 10 ton tank = heat transferred from the pure water to the brine. The brine gives up to the ammonia as much as it absorbs from the water in the ice cans, for it remains at a fairly constant temp- erature. Therefore the heat absorbed by the ammonia in the 10 ton tank = 231,906 B.T.U. per hour. See page ll item 5. Heat absorbed by the ammonia in the 5 ton tank = 79,010 B.T.U. per hour. See page 11 item 6. 15 Heat absorbed by ammonia in the cold storage room is estimated at 10% of the total heat taken up by the ammonia in the plant = 10/90 ( 231,906 / 79,010 / 76,178 ) = 43,010 B. T. U. per hour. Total heat absorbed by the ammonia = 231,906 # 79,010 # 76,178 # 435,010 = 450,104 B. T. U. per hour. Rate of heat transfer through the ammonia pipes in the 10 ton tank per sq. ft. of pipe surface = T.H. / A, Where T.H. i8 the total heat. transferred per hour = 251,906 B. T. Ue. See page ll item 5. A = area of the ammonia pipes in sq. ft. in the tank = N, xP2 X 3.1416 X RL / 12 Where N_ is the number of pipes in the tank = 96. see page 1 ifem 4 under equipment. R is the radius of the pipes or half the diameter = l inch. See page 1 item 4 under equipment. | L is the length of each pipe in feet = 30 ft. See page 1 item 4 under equipment. A, = 96 X 2X 3.1416 X 1X 30 / 12 = 1,508 sq. ft. Rate of heat transfer through the ammonia pipes in the 10 ton tank = 231,90€ / 1,508 = 154 B. T. U. per hour per sq. ft. of pipe surface. Total heat extracted from the pure water by the ammonia = 251,906 # 79,010 # 76,178 = 587,094 B. T. U. per hour. Percent extracted in storage tank = 76, 178/587, 0oe4 = 19.7 Percent extracted in the 10 ton ice tank = 251,906 /{ 587,004 = - - - -© + = 59.9 Percent extracted in ° ‘ton ice tank = 79,010 / 587,094 = = - - = = = = = «© 20.4 Note: The total amount of heat absorbed by the ammonia is somewhat in excess of the amounts shown above due to the Slow leak of heat from the surrounding atmosphere through the insulation into the tanks and from the atmosphere into the uninsulated pipes leading to the compressors. Some heat. is 14 given up to the atmosphere from the discharge pjpes from the compressors. These heat losses are comparatively small and will not be used in these calculations. While being compressed in the ammonia compressors the ammonia absorbs heat from the energy of compression. The amount thus absorbed can be determined by a comparison of the total heat contained in the ammonia before and after compression. The total heat contained in a pound of ammonia depends upon its pressure and temperature. The total heat gained then equals the change in heat content per pound of ammonia multiplied by the total weight of ammonia pumped per hour. The superheated ammonia fas enters the compressors at 22.5 lbs. per sq. in. gage pressure and 12.9°F. and leaves the 20 ton compressor at 163.1 lbs. per sq. in. gage pressure and 240.6°F., and leaves the 10 ton compressor at 163.1 lbs. per sq. in, and 188.0°F. See averages on page 10. 2 1b. ammonia gas at 22.5 lbs. per sq. in. gage pressure and a temperature of 12.9°F. contains 536 B. T. U. using the atmospheric pressure as 14.7 lbs. per Sq. IN. See Marks' Mechanical Engineers Handbook Page 334. lL lb. superheated armonia gas at 163.1 fage pressure and 240.6°F. contains 655 B. T. U. lL Lb. superheated ammonia gas at 163.1 gage pressure and 188.0°F. contains 625 B. T. U. 1 1b. ammonia liquid at 6¢.6°F, temperature contains 42.1 B. T. U. and, if it is at the saturation point it will have an absolute pressure of 129.2 lbs. per sq. in. L& Amount of ammonia pumped per hour = total heat absorbed by the ammonia / heat absorbed per lb. of ammonia = 430,104 { ( 535 - 42.1 ) = 872.6 lbs. The amount. of ammonia pumped by each compressor equals its percentage of total volumetric displacement times 872.6 This supposes the efficiencies of the two machines to be the same. Volumetric displacement of compressor piston per minute = 3.1416 XR° XSXDXCXR.P.M. / 1728 Where R is the ragius of the cylinder in inches. » is the stroke in inches. Dis 1 for single acting and 2 for double acting. C is the number of cylinders. R.P.M. is the speed of the compressor in revolutions per minute. For values see page 10. The 20 ton compressor is 9" X 16" single cylinder and double acting. The 10 ton compressor is 7-1/2 X 7-1/2" double cylinder and single acting. Volumetric displacement of 20 ton compressor piston 5+1416 X 9% /2° X16X2X1X 101.5 / 1728 = 120 cu. ft. Volumetric displacement of 10 ton compressor piston = 3.1416 X (3-3/4)" X 7-1/2 X 1 X 2X 175.6 / 1728 = 67 cu.ft. Weight of ammonia pumped by 20 ton compressor is 120 / ( 120 # 67 ) X 872.6 = 560 lbs. per hour. | Weight of ammonia pumped by 10 ton compressor is 67 / ( 120 i 67 ) X 872.6 = 512.6 lbs. per hour. Part of gas pumped by 20 ton compressor = 560 / 872.6 64.1 BZ. Part of gas pumped by 10 ton compressor = 512.6 / 872.6 = 55.9 p. Heat absorbed by ammonia from the energy of compression 872.6 ( 655 - 535 ) = 104,712 B. T. U. per hour. LE HEAT TRANSFER TO COOLING WATER. The amount of heat extracted in the 10 ton compressor by the cooling water in its water jacket = weight of ammonia pumped times loss in heat content below that of the 20 ton compressor = 312.6 ( 655 - 625 ) = 9,378 B. T. U. per hour. This is true because both compressors have the same suction pressure and temperature and the same compression pressure, hence the difference in the compression temperatures must be due to the cooling effect of the water in the water jacket. Total heat extracted from the ammonia by the wooling water = 450,104 * 104,712 = 554,816 B. T. U. per hour. The amount of heat extracted in each of the condensers depends directly upon the amount of cooling water supplied to each. It was impossible to measure the amounts of water supplied by each pump each day. If we assume the efficiencies of the pumps to be the same, then the volumetric displace- ments will be in direct proportion to the weight of water pumped. The volumetric efficiency of a pump depends upon its condition and length of stroke. The longer the stroke the higher the efficiency. Pump No. 1 has the shorter stroke (3") but it was in slightly better condition than Nos. 2 and 3, so it seems fair to assume the efficiencies the same. Efficiencies of Cooling Water Pumps. Volumetric displacement of the pistons of a pump = 2X 3.1416 X R° X LXCXD.S. Where R is the radius of the cylinders in inches. L is the length of the stroke in inches. 17 C is the number of cylinders. D.S. is the number of double strokes per minute. For values see pages l, 2 and 10. Volumetric displacement of pistons of pump No. l = 2X 3.1416 X 1.5° X 3X 2X 113 = 9,582 cu. in. per min. Volumetric displacement of piston of pump No. 2 = 2X 3.1416 X 2° X 5X 1X 47 = 5,922 cu. in. per min. Volumetric displacement of pistons of pump No. 3 = 2X 3.1416 X 2° X & X 2 X 50.5 = 12,692 cu. in. per min. Theoretical weight of water pumped per hour = V.D. xX 60 X 62.4 / 1728 Where V. D. is the volumetric displacement in Cu. in. 62.4 is the weight of 1 cu. ft. of water. Theoretical weight of water pumped by pump No. 2 per hour = 5,922 X 60 X 62.4 / 1728 = 12,840 pounds. Theoretical weight of water pumped by pumps No. 1 and 3S per hour = ( 12,692 # 9,582 ) X 60 X 62.4 / 1728 = 48,240 pounds. Theoretical amount of heat extracted in double tube condenser and in water jacket around 10 ton compressor = weight of water pumped times rise in temperature of the water = 12,840 ( 81.1 - 53.2 ) = 358,236 B. T. U. per hour at 100 % volumetric efficiency of pumps. The same for the single tube condenser = 48,240 ( 80.9 - 76.2 ) = 226,728 B. T. U. per hour at 100% volumetric efficiency of the pumps. Temperature values taken from page 10. Volumetric efficiency of pumps = actual ‘emount of heat extracted divided by theoretical amount = 534,816 / (358,236 7# 226,728 ) = 91.4%. See page 16 PP. 2. 18 HEAT TRANSFER TO COOLING WATER. Heat extracted from ammonia thru single tube condenser $1.4 & of 226,728 = 207,288 B.T.U. per hour. See page 17. Heat extracted from ammonia through double tube condenser = 91.4 % of 358,236 = 9,378 = 318,150 B.T.U. per hour. 9,578 B.T.U. were extracted in water jacket. See pages 16-17. Per cent of heat extracted through single tube condenser 207,288 / 554,816 = 38.8 Per cent of heat extracted through double tube condenser = 318,150 / 534,816 = 59.5 Per cent of heat extracted by water in water jacket of 10 ton compressor = 9,378 / 534,816 = 1.7 Area of pipe surface in a condenser =n X 3.1416 X D XL / 12 Where n is the number of pipes. D is the diameter of the pipe in inches. L is the length of the pipe in feet. For the values see page 2 items 4 and 5. Effective area of single tube condenser pipes = 40 X 3.1416 X 2X 20 / 12 = 419 aq. ft. Effective area of double tube condenser pipes = 16 X 3.1416 X 1.25 X 15 / 12 = 78.5. sq. ft. Heat transfer per sq. ft. from single tube condenser 207,288 / 419 = 450 B.T.U. per hour = 7.6 B.T.U. per min. Heat transfer per sq. ft. from double tube condenser 518,150 / 78.5 = 4,053 B.T.U. per hour = 67.6 B. T.U. per min. LO C. TESTS TO SHOW THE EFFECTS OF AIR TEMPERATURES AND WIND VELOCITIES ON THE CONDENSING PROPERTIES OF TEE SINCLE TUBE CONDENSER. The object is to determine if the temperature of the air surrounding the condenser, and if the velocity of the wind have any marked effect upon the effectiveness of the open air condenser. This effect will be shown by a lowering of the temperature of the cooling water leaving the condenser. However the temperature of the cooling water fluctuates with the temperature of the lake (See item 4 page 3) and the temperature of the cooling water leaving the condenser under fixed conditions would have a similar variation. That is, the change in the temperature of the water as it flows over the condenser would be a constant fixed value if all other condit- ions remained changeless. The variation in the change of temperature of the cooling water will, therefore, be the indicator for any effect of the air temperature or wind upon the condenser. This presupposes that the amount of ammonia pumped and the heat content of same is constant. This is not. strictlg true, but the percentage of fluctuation of these amounts would be low, as the compressors run at a constant speed and the temperature of the brine is kept as nearly constant as possible by varying the amounts of ice pulled., The following items were taken for each day of the test and the values are given on log sheets la, lb, 2a, and 2b. Temperature of the air taken in the shade. Direction and approximate strength of the wind. Temperature of the cooling water entering the condenser. Temperature of the cooling water leaving the condenser. 20 AIR TEMPERATURES AND CONDENSING PROPERTIES. The right hand portion of curve sheet No. 1 shows the air temperatures and the cooling water temperatures plotted for each day of the test. The graphs show that the curve of the air temperatures has the same general trend as the curves showing the cooling water temperatures. When it is high, they are high; when it is low they are low. The curve of the air temperatures fluctuates much more than the curves of the eooling water. Curve sheet No. & shows graphically the variations in the change of temperature of the cooling water above and below an average of & degrees and the air temperatures above and below the average of 75°F. These graphs show that when the air temperature is high a greater change in temperature of the cooling water is required ( see Aug. 11-17 ), and when the air is cooler than normal the change in the cooling water temperature is less than normal (see July 3, July 18, August 1-3, 7-11, amd 25-27 ). The change in the air temperature is several times the change in the increase of the cooling water temperature, and there are places where these curves do not follow each other. These places may be explained by the effects of the wind, the amounts of heat. being pumped into the condenser, etc. ol WIND DIRECTION AND VELOCITIES AND CONDENSING PROPERTIES. The single tube condenser is protected from the wind on the west by the wind-brake between it and the smoke stack, and on the south by the upright part of the building and a wind brake up to the top of the condensers. It is open on the north and east. The condenser pipes run east and west so that a north wind would affect it most. Wind from the northeast and northwest would affect it considerably, and wind from the southwest would affect it somewhat, but wind from due west or south would have but little effect. The curve on the left half of curve sheet No. 5 is drawn aceord- ing to the above considerations. The general arrangement of the condenser can be seen on sketch No. 3 and on photo 2. The general trend of the wind curve on curve sheet No. 5 follows to some extent the curve showing the variations in the increase in temperature of the cooling water above or below its normal of 5°F. The following instances will serve to illustrate:- On July 3rd the wind was strong from the north and the cooling water increase curve is 7° below normal, in fact the cooling water itself was cooled 1.5° more than it was heated by the condenser. See curve sheet No. l. On July 19th with the temperature of the air normal, the increase in the temperature of the cooling water is 3° below normal due to a slight northwest wind. On July 25th with the air 4° above normal, the increase curve shows 2° below normal due to a light east wind changing Le from the northeast on the 24th. On August 18th the cooling water leaving the condenser was colder than when it entered, due partly to an air temperature 6° below normal and partly to a medium northwest breeze. On August Zlst the air temperature dropped 6, to 4° below normal, but the increase in temperature of the cooling water increased from normal 1° due to a shift in the wind from a Blight northeast to a slight south breeze. ‘On August 25th the increase in temperature of the cooling water was 1°, or 4° below normal due to an air temperature 6° below normal and a strong northwest wind. Prom these illustrations it is evident that the wind can be made to aid materially in the condensing process, and, although it adds an uncertain factor to the operation of an iee plant, still the plant which ignores this factor and exeludes the wind by housing in the condensers will increase the cost of ice production materially. Whether the beneficial results are sufficient to warrant the installation of power driven fans to produce artifically blown air or not is hard to say. Experiments along this line would be interesting. D. TESTS TO SHOW EFFECT OF COOLING WATER TEMPERATURES ON THE CONDENSING PROPERTIES OF CONDENSERS. The above tests have shown that the cooling water on the Single tube condenser does not increase the same amount every day. Referring to curve sheet No. 5, it will be seen that ZO there is a variation in this increase of as much as 4° above normal and 7° below normal. These variations are caused mainly by (1) deposits on the condenser from the condensing water, (2) variations in the heat content of the ammonia pumped into the condenser, (3) variations in the air temper- ature and (4) changes in the velocity and direetion of the Wind. Exeept for these slight variations, the temperature of the cooling water leaving the condenser follows very closely the temperature of the entering water. The curves on curve sheet No. 1 show that the temperature of the water leaving the double tube condenser follows very closely the temperature of the entering water. The increase in temper- ature there is nearly constant. A comparison of the curves on curve sheets No. l and « shows that the high ammonia pressure is dependent in a large degree on the temperature of the condensing water leaving each of the condensers ( This is varied somewhat. by varying the amount of ice pulled). This is what we would expect, for the colder the cooling water, the colder it will leave the ammonia, and tables of saturate ammonia vapor show that the colder the point of vaporization the lower the condensing pressure will be. The cooler water then provides more rapid condensation and greatly aids the condensing properties of the condensers. In fact, if sufficient water could be obtained from the wells at 52.3 °F. for both the condensers, the efficiency of the plant could be increased from 10 to 15 %. The €ompany has spent several hundreds of dollars trying to increase their well water supply. 24 PLANT PERFORMANCE UPON STARTING AFTER A SHUTDOWN. The plant was shut down from 10 A. M. July 4th to 6 A. M. July Sth. Readings of several of the parts were taken as shown by log sheet No. 5 every hour. Curve sheet No. 3 shows the changes, in the temperature of the air, cooling water in the single tube condenser, and the brine in each of the tanks for the first 10 hours of running. Notice the rise in the temperature of the air from 64° at 6 A. M. to its maximum 79° at 5 P. M. The cooling water entering the single tube condenser is taken directly from the lake, and it has a rise in ten- perature corresponding to that of the air but of only 1.5°. The temperature of the cooling water leaving the conden- ser has its maximum from 7 to 8 A. M. when the temperature difference amounts to 7°. This is due to the large amount of heat pumped from the brine and pure water tank through the ammonia into the condenser at starting. Also the wind was due south and did not help the condensing properties of the water. The rise in temperature of the cooling water decreased as the wind changed and as the brine beeame cooled, until at 12 M. it reached a minimum of 3°. The wind had changed to southwest where it could partly reach the conden- ser and, by evaporating part of the water, aid its conden- Sing properties. The brine in the 5 ton tank started at 27° at 6 A. M. and dropped rapidly till about 11 A. M. when the decrease became less until at 4 P. M. it reached its minimum value of 15°. zo The brine in the 10 ton tank was at 25° at 6 A. M. or just 2° lower than the brine in the 5 ton tank. This is probably due to the cooling effect of the ammonia liquid left in the 96 pipes in the 10 ton tank when the plant was shut down. The 5 ton tank, having a drum instead of pipes, stopped the cooling process immediately and consequently warmed 2° more. The 10 ton tank's brine made a quick drop between 6 and 7 A. M. of 3.5°. This is due to the starting of the agitator. The decrease is small from 7 to & A. M. because it took time to fill the 96 pipes with ammonia. From 8 A. M. on the decrease is rapid, easing off gradually until at 3 P. M. it reached a minimum of 13.5. 26 COMPARISON OF TANKS. 10 ton tank. 5 ton tank. Total. Size of cakes - - - - 300 lb. 200 lb. Total No. of cakes pro- duced in 1067 hrs. 4954 2514 7448 Total weight produced in pounds. - - = = - 1,480,200 502,800 1,983,000 in tons. ---+efe-- 740.1 251.4 991.5 Part of total : production. - - - - - 74.6% 25.4% 100% Tons per 24 hrs. 16.65 5.65 L205 Pounds per hour. 13587 471 1858 Frequeney of pulling 55 hours 55 hours 55 hours Heat transferred per hour. rr cr rec— are 251,906 B.T.U. 79,010 B.T.U. 310,916 B.T.U. Part of heat transferred. - - - 74.6% 25.4% 100% Cans per ton of ice each 24 hours. - - - - 9.2 14.5 27 PLANT CONSTANTS DERIVED FROM DATA TAKEN. Plant overload is ( 22.3 - 15 ) / 15 = 48.7 &. Weight of ammonia pumped per minute per ton of ice produced each 24 hours = 872.6 / ( 60 X 22.3 ) = 0.65 lbs. Tons of ice produced per ton of coal consumed = 1858 / 460 = 4.04 Amount of cooling water pumped per ton of ice produced each 24 hours = ( 48,240 ¢ 12,840 ) X 0.914 / 22.3 = 2,003 lbs. per hour. 41.7 lbs. per min. 5.6 gal. per min. Condenser areas per ton of refrigeration. 9.4 sq. ft. _i-8 sq. ft. -ll.2 SQe ft. Single tube = 419 / 22.3 X .50 Double tube = 78.5 / 22.35 X.50 Total - Volumetric displecement of compressors per ton of ice produced each 24 hours = ( 120 # 67 ) / 22.3 = 8.4 cu. ft. per min. or 14,490 cu. in. per min. 28 SUMMARY. A. The direct cost of manufacturing ice = 52.80 per ton. B. The rates of heat transfer per hour in B. T. U. are as follows:- B.T.U. From. To. Place Remarks per Hr. Pure water Brine 5 ton tank 79,010 Pure water Brine 10 ton tank 251,906 Through ice cans 5 ton tank Per sq. ft, 129 Through ice cans LO ton tank Per sq. ft. 141 Pure water Ammonia Storage tank 76,178 Brine Ammonia 5 ton tank 79,010 Brine Ammonia 10 ton tank 231,806 Through Ammonia Pipes 10 ton tank Per sq. ft. L54 Air Ammonia storage room 43,010 Energy of Comp. Ammonia Compressors 104,712 Ammonia Cooling water 10 ton compr. jacket 9,578 Ammonia Cooling water Single tube condenser 207,288 Ammonia Cooling water Double tube condenser 318,150 Through pipes in single tube condenser per sq. ft. 450 Through pipes in double tube condenser per sq. ft. 4,053 C. The influence of the air temperature and wind vel- ocity and direction on the condensing properties of the open air condenser is relatively small. However they do have a direct. infltence and this should be considered in opsrating an ice making or refrigeration plant. 2g D. The cooling water temperature has a fundamental effect upon the condensing properties of condensers and hence on all the principal operating units of a refriger- ation plant. The location of plants is often determined, to a large extent, om the availability of large quantities of cold water. When cold water is not available at very reasonable rates, it is necessary to cool the water in cooling towers or ponds. 50 CONCLUSIONS BASED ON TESTS. 1. The low ammonia pressure is too low for securing very high efficiencies with the compressors. The pressure could as well be carried at 25 lbs per sq. in. gage and still keep the brine temperature below 15°F. saturated ammonia gas at 25 lbs. gage or 39.7 lbs. absolute has a temperature of 11°F. See page 333 Marks’ Mechanical Engi- neers handbook. The higher the low pressure the more ammonia the compressors would pump per stroke and the greater their efficiency. A higher low pressure could be supplied best by supplying more tank space. 2- The frequency of pulling the cans is too great. Kent page 1316 states that it should be 54 hours for both 11X22X44 and 11X22X32 inch cans. Marks' Mechanical Engin- eers Handbook page 1740 gives the time of freezing 200 lb. cans as 55 hours and 300 lb. as 60 hours. The 35 hours used at present could be lengthened out by using a higher brine temperature. This would use less ammonia per hour. The ammonia thus released could be used in another tank. 3- It was clearly shown in the test that the wind has a marked effect on the cooling properties of the single tube condenser. This condenser should be raised above all surrounding projections, and the pipes should be formed into a hollow square. Suitable V shaped trays should be Supplied between the pipes to keep the water from blowing off the pipes and yet allow the wind to reach the water. OL 4. All live steam and cold ammonia pipes should be covered with an ample thickness of asbestos. The ratio of 4.04 tons of ice per ton of coal is too low. Frank L, Fairbanks on page 1741 of Marks" M. E. Handbook gives 2.25 to 8.22 tons of ice per ton of coal depending on the size of the plant. The lower values applying to small plants. Kent page 1514 gives 6 lbs. of ice per pound of good coal. 5. Colder water should be secured for cooling the open air condenser and the flat cooler if possible. The tests clearly show that the colder the cooling water, the lower the temperatures and the lower the ammonia pres- sures will be, and finally the easier and cheaper the plant can be run. The pure water from the flat cooler should be lowered from 87.7° to about 55°, This would cut down the amount of ammonia per hour used in the pure water tank and also reduce the temperature of the pure water to the ice cans to about 35°F. 6. Items 1 and 2 point to more tank space. I would Suggest throwing the 5 ton tank out and installing a duplicate of the 10 ton tank touching it on the east. The space released by the 5 ton tank could be well used as ice storage. With 308 eans and pulling 7 cans per hour or the whole tank every 44 hours, the production would be increased to 25.2 tons per day. 52 INDEX TO CURVE SHEETS, BLUE PRINTS» SKETCHES AND PHOTOS. CURVE SHEETS 1. This shows the temperatures for each da: of the test of:- 1. Pure water to storage tank. <- Pure water to ice cans. 5. Cooling water entering double tube condenser. 4. Cooling water leaving double tube condenser. 5. Ammonia entering expansion coils. 6. Air in shade. 7. Cooling water entering single tube condenser. 8. Cooling water leaving single tube condenser. Wind pressure and direction. 2. This shows the temperature or pressure for each day of the test of:- L- High ammonia pressure. 2. Low ammonia pressure. 5.» Temperature of the brine in the 10 ton tank. 4. Temperature of the brine in the 5 ton tank. 5.» This shows the hourly variations in temperatures from 6 A. Me. to 4 P. M. on July Sth after a shut down of 20 hours of the following:- 1. Cooling water entering single tube condenser. 2- Cooling water leaving single tube condenser. 5. Air in shade, 4. Brine in 5 ton tank. Se Brine in 10 ton tank. 4. This shows the following items on the production of ice for each day of the test:- 1. Production each day. 2. Average hourly production each day. 3- Total production. 5. This shows the following items for each day of the test:- le. Velocity and direction of the wind laid out as a curse according to its possibilities in affecting the conden- sing properties of the condenser. 2. The rise in temperature of the cooling water while passing over the Single tube condenser, above or below the average rise of 5°F. 5. The variations above or below the average temper- ature of the air. 6. This shows the heat content of the water as it passes from the well, through the many stages, to the ice cans into ice, taking the heat content of ice at O°F. as 0. SHOAL Raa het Se! eo 2s — 1b a Baa as ka ah a eee MS feet 2 ‘ “INIAFILNG ie cr Bile face : . | A IENIINQI, FBO) F7IN/S INIAV TTY ILYM, UY. el Soe ) Eseettsht . ee | Ree oe eee Ge ene a ! Ffestees Fuse i eeeeea Behe bay Pe! ie ' To ae : As hg errs eS “ie oe fi | | | eee Sees Siete ESS: aes Pe ; ea a ef A isTe iehids bbc Bl bodcttiinee Cob Ts a kale 0 | 8b 3 x MESA | as | | = elie | <4 ry FY PS | citcehiicldes i2 Pee 95 S-RPEMOTDS SENSE ED aa FARE EITele ee INITOO9 | | ie | SiS) ) 1dXI INSSIINI VION te a ace 1. iS , MNYI 39¢ neni a aur meek aml Ale CURVE SHEET NO 2 TEMPERATURES a — E IN DEGREES FAHRENHE! i ; i } ; _ "WwW 4 am rél 5 ye ee, J oT TG Ww al ie Stes | | | | | . : 4 / ae tine ; : cera SLagears TET GSSTERE Grape GgGGRE FSPETULEC OPO”, ~F--eos THOT PHN ELD . | ras at ; | Bar ata | : | ! AT] Ae te i : a IMYILNF oe Pee 28 _— — | saws WISNTONOD EAP ae AZ NO s SPR Rots SSsaetel! & F 3 wy | w EA CLEPs a Tae LE ZO OT ae: | ee os ; j } Sas SeeSsaaSes Se eG — a fe See ae Ne eA ee Se i Hee at USL CSE ETF Ls ME ey a ; = ee fi ered men Ze oe | ] } ' ! ' SHEET NO. | CURVE 4 — —_ Za) es 200 } i | | Pee SE 500 FOO 300 __€00 _ 500_ TOWS OF GE 7a fal4a) et | } ' 1000 9C0 nll ye de Said LSC RO GE LRA ATE tt ht BE RO BEE AE be ZZ Of. 8l 2 Aes ANS RL ARR ETSI LOSE CRED REESE Eee OST POE ae | Peres ran oe 0 eeu ra bee rey 13 ess eae her Oe ae Ome Ne Neeaiae b Per BEE Ua | Lana aan an ee R167 Ie ag PTA SD eT ae er Vd Ayer emer eae A CEL MLM Aa LL Ea 1A eteteaecteatal 4toG SO IDVSIAY M0778, ONY FNCEY YISNIGNIP FNL eke LAA ‘NO AIL al INITIOD 40 ae ae MAE So ‘Wy ig eh CURVE SHEET NOS | | { ; a sreake . : x | | Raies ES x es rl s oa 7 Ss Rie { 7 aa | a eae ent a as el -_- a Saeed bg Mi Py Shs 4 Opa at up fe ekder we be bh bn MOC Sn Eee eae! IN TEMP. FROM AVERAGES SfFes O's ela VARIATIONS, (S55 / 1, i. k {3 : i { Vf j I ’ I ' ‘ H ] iss ease y ; t ater BS i a! - meas} riers eer ; i 5 ; i | i ' or i } | ; | r ip: .s : | H iar | a | i hs 4 } \ NIG Si ose CH RL eet to BCE, & 1 51 hee Ad ee BE ik: ea RES ey malWarap that had Ot Lee, ! Sef New | f > ; Rar r ri ss i As i ri | i ie neds Sears tote Bake ab ts acces | | Pare eS oectiE ty aby, | ed A: ME APL ALARA ee Phe ae i | : , — Pr | 4 NS a a i | ay ca re ea x ee = # in| Me ER re = eee WIND VELOCITIES B&\DIRECTION — mea ees er th ; i epee Be rod me ats ad Sava ie aed GMM 40 TER AMIOTIN aNIMOHS TAYAI ————__ - »#y a Fg SeuGES SETEEA i} a | + a Te. comune ESR fe deo SSESTRS REPERES od od STRESS BESTESSE A LEEGECY Sarees 499 ———— 8. T.U. PER 148. | ; } : ) r Be ae See | foqiaeaaite eee) eee Eesti ———— ee WES LEGSS SESE TENT OT NEE SF cre AGE Peeps | . } | M. } ne ie would ie = ae } | Tea | | ! ikea ZN CVRV eT Z, us beeen ve ) a, ~ FLAT COOLER ~ \ i} & a ee os: -+—- R' ~ a % F TE eeseasoe SET | SKIMIMER Sa | | Qa Dr : [Tsp 2 Wo i. . : Sie : = ena ar aeegrea eR Le ol, ht a id / T ; Bes ad : mtu i ri el fideo! been i ‘SHOWING TOTAL HEAT IN THE WATER eras Ice AT 02 FROM THE WELLS INTO ICE, A 1 Seen eae WELL WATER LEAVING eTTeS PTSwAaTees obs CSSes | eshe as bE Ott Bet aaa ae a) | | | | +} |__| 1M S1DE-FEAF-GOOLER——+_-— | : | | coe CONDENSER ee a a et tH oH } eat eeteg pwd dere td: SHEET eae A Pune’ WT. OF COAL FUEL COST AWTONOF COALS 2 EVEL COST LBS. PER HR. PER HR. LBS. PER HR. | PER HR ITY Y BP EE CR Ole: SET eae a aE 460 Riek Ea Oi ee Wea ee Cae as Sl AL VLA lens Cea Rr REPELS TR Re oe a Ware Ce ones | ee ae Siew eek mies / 443 FOL oe ACR) TADRE ACAD Cees eis en wl ae 408 (ie ees rd) PE EASE FIS VET VES 472 TREK ie ae =) cake | ERM 42/ EUR ERS OOS Tap lie A a ean ae Cre: NT eee Fy era i (a ee FIRS ET AT ES ae a ee ee 440 Re oie th ORE E a el eer ae Ag Ely /.388 ee {ear pean a 2 STE a cas MO iiuer of ae SEA ae rm USGA ak al BB Se ft Sr ek aa Re A So 457 vars Re | 464 2.54/ va we MEL! ees eke, t LOA Wee So eS aed Be Pe Pe CEL eal | ep oae 2 Ban ee ha 468 Vie eS ee Z.4ZO 437 1.420 eA Li Zod Aes EBS ee} Var ws 436 ee g Wie A 1-67/ AVERAGE F460 AVERAGE / 662 COhsumption of fuel por Z4hrs = 460X2ZF 7Z000 = 5.52 tons. Cost of fuel per LFhrs.= 1.662 X 24 =839.97 Le of coa@/l used er hover in VL ho a eR wesghT vsed sh pounds = length of time st lasted iA froves. Fuel cost per hr. =Cost per ton X& weighT of coal used per Ar. +2000. Original data used is gwen on Log sieets 2a and 2b: PRODUCTION OF ICE TOTAL PRODUCTION | L&S. PER |TOTAL PRODUCTION LBS. PER LBS. reek HOUR ache TONS La a PY 1743 REBT [6-7 EXY 24400 eae 1743 3279700 16-5 ee) 28600 14.3 2043 Um Als 16.0 he go Bs wr rT -Y Ee ‘Whe #8) Reread 16-7 otek VEIT 13-2 1/878 I/F 00 ET 1777 IT EP /878 | 34000 | /7.0 EK 26300 ERE 4 /878 CYP Ter (Eee ee 26300 Be /878 36000 /8.0 EET 28200 ew) 20/4 34200 ey! had 1Z600 a 1575 34-200 Th ae: TT) 26300 ce /878 OLS EY 2900 26500 TEER Uke! 34/00 a 1/874 26500 EE EXE 34200 ae KY) 26400 ‘Epes /886 PEE 15.6 ER) eText) a) ei PEMA ey /828 26590 EX} Eek 3/700 16-0 1772 A917 28300 13.2 202/ 42900 DES: 1/787 28000 ie 2000 PPA a Re A 17 63 IXIA Te) 13.3 Uke! 44700 22.4 TX: eet E ea 2000 44400 Pa (850 287060 14.4 ae! 44000 22.0 ei 339700 17.0 /883 43400 21:7 pete! 27200 A Vr A) 444-00 oe ed PE ee XE aE MOEA 44000 22.0 Eee! Si eels 16-7 /850 45300 22.7 RoPo ho} eRe ITe A eek eee we ees /850 32800 16.4 1/822 4F4FFO0O 22.2 1gs0 KREIS Bt 1/850 44400 Rs 1850 eer lé.7 aE mA i ya 1850 34000 VA Ki 44400 22-2 EX TOTAL & AVERAGES L983,000| 99/.5 FFs =| AVerage proavction for 24hrs.= 1858 X 24 + Z000=22.3 Tons Tota/ production = 300X no. of 300/b Ccancs + 200 X no. of 200 ib Cakes. Total prodvction in tons = total production in lbs. +2000. Povnds per hour = tota/ production in lbs + ho of Ars oF required to produce therm. Original data used is given on log Sheets 2a and 2b. Pa =e COMPARISON OF COSTS OF DIFFERENT FUELS TIME {COST PER FVEL AMOUNT COST le PRMALLAL hh da KINDLING wooDd 4 CORDS | 2725 PrERCO] 2 |20| 84.7/ 16BEECH & MAPLE | 2 coRos |\329 PER col 2 G5 2-88 | Ee ee Fee ea 2-06 Cano coAL J) (| 840 Js. | 6 £9 PER To POCAHONTAS SLACK| 5720 /65 |B2°PER TON / cs gs SOFT COAL aT) ee eee / Pe deh By) ae) 460 Ibs\/O7 PERT) | ear: yy yy “460 Ibs) /{22 PERT) / Pee Y =. RELATIVE COST OF FUELS ms ] : | 5 5 ey i) A bere ny : 2) RS ~ | ray . NI | Q a ih S| 9 3 s S a > 4 _ ay wR sd | M4 y y 4 2 a c e r = Ss : < eT) Q ES a 9 ry ed S) ‘Y s) ad) 88] y] ay s y =i Oe S SKETCH W “e = THERMOMETER as Lae N yy Y VA \’ ff : TY ae ht TR ca PIPE % \ SONG ores ait) woo. CLOTH —~* BY aa ee f aS a be iW Fi I | MERCURY \ is pedal) eee \ w COPPER TUBE NY \ I NAAAAAAAAAAARAAAARANNNS = METHOD OF TAKING AMMON/A__TEMPERA TURES | PUMPS GAD @o CAD oo 100 KP STEAM BOILER at aw A COOLER 2Z0T /0 Rtn a TERY WA 1 Ll *—. BRINE AGITATOR CEL ES an 154-300 # ICE Le | > FILTERS Sed ICE STORAGE ROOM CAPACITY — 40 TONS OF 300 4% CAKES EACH LAYER 3_TON BRINE TANK 82—200# ICE CANS SKETCH WN CAPACITY 45 TONS LL Te la NH3 CONDENSER Z| oa y. SSE ea a po (-110. 82013 aa | a ' iH] 2 me & le 3 | | rel e lie I Sy | a Set PRM ee ie | 4 | i | as Q INV 7d OD WRI1AIS JO NOILVAITI WNOILDIS SSOYD SYIONO. = TP 71,0) 5 Fo , _SNVO_39/ E/N MERLE TAT A Ore Te ee Se 7a SIZ) Ey Z°((N ae Fed \ Toa Farol a ro KO) = Ae ahaa YISNIINOD WVILS YWISVNIGNOI V/NOWWY IMWHG GNIM SIdid YILYM IN/7TAOZ Foe Ee Aden en ee) 5 at css") a Wh a 2 Y’ A ES 22 —1< | me Pe | , + ~Iny y * Bee ea fi 30018. /CE CAN thao nae 1 Neen: fag Sek | \s MOKE STACK Swine BRAKE = ROOM USE GALY 2 se : ed 5 Ti