HHHHH I HI! 3') a A COMPARISON 09 THE BIOCHEMICAL AND HIGH-RATE FILTRATION PROCESSES IN THE TREATMENT OF. MILK WASTES OF THE BORDE‘N CONDENSERY AT PERRINTON, MlCHlGAN Thesis for The Degrce of B. S. MICHIGAN STATE COLLEGE RobertW. Rothe I940 . ‘ | ‘ 2‘5»! mi" .97: T. 4:3. n‘.‘ .'-. ‘véfl'hf,’ ’,“.‘ - a". 't i —, g‘.:r.!-.“l:f)i/' A! /. :f r . . V I I ' (V a “1‘ “r:" . §:£<‘q;:}§ J ' V1 ; --(? L ;\‘r I( u.‘ 9479-4“! 43% . .' ‘1 l- r. ' .fcik‘.‘ 0'1‘ .v, ., .. 57%: if???“ ‘ . .; km 1“. ‘ s?’ " ‘ 3.. r ' "‘ ,1: r. 1 Wk 2; ‘2 a; ." ' L: fW‘tV..I'{2'.. .l“_ :I ' ‘1 ‘, i‘ .}V ?ESA£:§ 5r_v'.\‘; 3’" .. 3- ‘ M , 7 3., -. 3 .“ ' ‘1 \ '_ ' .v:. .1 .pkéi—v, . - Lv 0: . "§ -fi ‘. 5 .. -!~$"\'\ ' ' \{ _ - ~. 9 . y "3‘ .- . O , \ Aral .v. . .. x" ' " A." ‘_. W0“? ”33' . W“ .‘ 4*“ " a? ‘1‘ - . H34 May ‘3. 2". 7" ‘ . ' .H‘T 3. ~ ‘ i .\.'.)v" 'Jy' t” ‘ ‘ " . ,'. J“ "/}.v 4‘ . .1. I - - -, '- ' v» ‘ ' ' l -‘ I , ‘. . ,1: l ., ‘C-w. "' «.3 ‘3 . . _”,< ; [,Eé’l ; f ) .:} . L. p v“ )' Ry ‘ V AL» '-\“~".'. «12ch L . "'3 J '-’ ' 'Q E: a " - T A: M... g. . .‘ . .‘ ‘J,vl-;: u€.;‘ ” Lr' .’ ‘ w~ h . ‘.. _§_$T gnaw-4,2: t' -*= . V . I T g n . 4 .M..q'-.~“"\’Ih's “.. ,, ‘ ‘ A Comparison of the Biochemical and High-Rate Filtration Processes in the treatment of milk wastes of the Borden Condensery at Perrinton, Eichigan A Thesis Submitted to The Faculty of MICHIGAN STATE COLLEGE of AGi CULTURE AND APPLIED SCIEKCE by q Hilbert J. mtha Candidate for the Degree of Bachelor of Science Juno 1940 T H 5815 Q ’23.? . i Acknowledgement I wish to exPreee my sincere appreciation and indebt- edneee to Mr. E.F. Eldridge for his advice\and suggestions rendered to me in the preparation of this thesis. IKTRQQUGTIQN The purpose of this thesis is to compare two processes for the treatment of milk waste as applied to the needs of the Borden Company fiilk Condensery located at Perrinton, Hichigan. This oomnsrison'will involve: (1) A study of the factory and the wastes from it. (a) Source of wastes. (b) Volume. (c) Strength. (3) A preliminary design of the treatment plant as follows: (a) High rate filtration with stone filter. (b) Biochemical treatment with ferric chloride and line. (5) Comparison of duties as to Operation, etc. (4) Determination of cost of each plant. (a) Initial or first cost. (b) Cost of Operation. (5) Comparison sf relative effiencies or each plant as to treatment and Operation. (6) Selection of plant most suitable to Borden Condensery at Perrinton. Experimental plants of both types have been set up and triea at the plant at Pcrrinton. Various rates of applica- tion and dosages being used. From.the results of those tests and analyses compiled by Jr. 3. F. Qldridge, the method giv- - 1 - ing the best results was determined and used in the writing of this thesis. r‘t: :1 -‘!.’.i."."T’1).'“ at“ our. 1'.‘ . '1' ' 3.7m --1 llLa inhibits.) 4‘“ng uvdiafuu OI‘ TIL—‘5 L.n..).‘.l..n.) The selection of methods of treatment for milk wastes should be adapted to the local situation with particular re- ference to the degree of purification necessary and the char- acteristics of the waste from the milk plant in question. The condensery at Ferrinton is equipped for the separa- tion of cream, condensing of milk, and the production of dry milk powder. The individual wastes that make up the comnos- its for any one day at the plant consist of the following: (1) waste water from.washing cans and other uten- . 3118. (3) Scrub and rinse water from the floors. This includes any milk or cream and skimmed milk that Spillod on the floor, and the dirt that collected. (3) Caste water from toilets and washrooms. Volume of Raw Haste The volume of raw waste flow was determined by weir measurements trom.a 90° V-notch weir. The results or these measurements are compiled in Table l. Table No. 1 Flow Data 1-2,: 2.453(lfl5/2 Date 9/14 9/15 10/4 Time 11 Gal/1-11:1. II Gal/£1111. 11 Gal/m6. e A. h. 0.16 11.70 0.19 16.50 0.09 2.78 9 A,.M. 0.19 16.50 0.25 22.2 0.15 9.70 10 2.:2. 0.20 20.05 0.25 22.20 0.17 15.57 11 A..m. 0.19 16.50 0.25 25.20 0.2 20.05 12 Noon 0.25 “2.20 0.22 46.2 0.20 20.05 1 .. .2 0.25 22.20 0.50 55.15 0.60 2 .05 . 1..n. 0.26 52.44 0.50 55.15 0.22 26.50 5 r. .2 0.25 54.75 0.26 52.44 0.27 42.55 4 P. u. 0.25 54.75 0.26 46.25 0.29 50.20 229.09/9 542.54/9 205.05/9 :25.47 :55.04 :22.60 25.47 52.04 22.20 66.59/5 equals 26.9 Average Flow (ca1/:.:1n.) 66.59 Ti:;:h“.TL.Z;Tl-§T OF i-ZUK ?.‘.'.-"9‘-.;5T.i;;13 BY H125 RATES FETPNLTION This method of disposal consists of applying the milk 'waste along with the recirculated effluent to a biological stone filter designed for a continuous application. In this way, the effluent which is returned from the filter>mixes with the raw waste as it enters a holding tank, therefore causing considerable dilution and reducing the B. 0.11).1 of the raw waste. This reduced B. O. D. of the waste makes it possible to increase the amount and the rate in.which it i is applied. A quantity of treated waste equal in amount to the raw'waste entering the holding tank is discharged con- tinuously as the final effluent. Design of a High Rate Filter 2 plant giving complete treatment by this method con- sists of three units: (1) A holding tank to equalize waste and give a longer period of Operation for the filter. (2) The filter. (5) A settling tank to remove suspended materiel from.the waste discharged by the filter. Holding Tank: .— *— Before any attempts wore made at designing, the average daily flaw from.the condensery was determined from flow mea- surements taken over a period of several weeks under 1 Biochemical Oxygen.Demand -4- conditions of.normel Operation. This date and results are shown in teble number 1. Composite samples of the raw waste 'were also taken and analysed for 5 day B, 0. D. as shown in Table number 2. Results of finelyses of.flilk Filter Table No. 2 Composite Samples Date ' SmDay B. O. D, Suspended Solids FTHET"'TR€ducw ‘Final Redue- Raw Effluent tion ReW' Effluent tion nnm. _PPm 2% IBE1‘___Jfl¥; it 9/6 555 _. 27 93.4 304 76 75.0 9/7 675 59 94:4 472 70 Belt 9/8 350 70 89.0 272 98 64.0 9/9 803 49 94.9 ' 1109 120 89.2 9/11 540 49 9.3. 644 76 88.1 9/12 575 47 91.9 see 106 62.4 9/13 407 50 87.7 264 as 66.6 9/14 413 43 99.4 606 128 78.8 9/15 713 99 93.1 404 62 85.‘ 10/4 775 ** IMHO? *** ##III ##3## Avnanen 560 46 91.8 494 92 77.1 The average B. 0. D. of the effluent from the present filter at Perrinton is 46 ppm. The raw waste entering the holding tank has en average B. 0. D. of 560 ppn; Previous experiments have shown that the mixture ep- plied to the filter gave best results if the B. O. D. when erplied was between 150-200 ppm. By recirculating e mixture 8 times the row waste flow, -5- the reduced 8. 0. D. of the mixture by dilution was found to be 110 ppm. 1/8 of recirculation is re” waste--3. O. D.z 560 l x 560: 560 7/8 of recirculation :8 final eff. B. 0. 15.: 46 '7 x 46:: 333 ~— 8 parts 882 B. O, D. of mixture is 832/8 : 110 ppm, which is within the limits prescribed for best results. The holding tank is designed for a capacity equal to the total daily flow plus 359 for night flow. The waste is dis- charged for nine hours a day, the greatest concentration is around four o'clock in the efternoon, when considerable wash- ing up of the plant occurs. The night flow is relatively low and is presticnlly clear meter. Average flos equals 28.8 Gallons per minute. 38.8 x 9 x 60 equals 15,550 Gallons 25% increase equals 5,885 " 19,455 Gallons Required capacity of the tank: 19,455/7.48 ==2,598 Cubic feet. The tank was designed to allow for settling and the removal of sludge accun. stcd. The bottom.of the tank was given a slepe at the entrance so that there is a drOp of one foot in fourteen feet to a sump which is deeper by one foot. The sump was made two feet in width and has a baffle separat- ing it from the rent of the tank. n t one end of the sump there is a drawboff pipe and valve which runs through the wall separating the holding tank from the settling tank. (The same pump and pipe line is used for drawing sludge from - 6 - both tanks. Gate valves are placed in the line so that they my be drawn off separately.) At the far end or the holding tank a 2’ x 2' x 1' sump and pump was placed to punt the mix- ture to the filter. Calculations: Required capacity of tank equals 3,593 cubic feet. I xo’ \L— 1—4—4L ‘N‘ -__4 L4; e /4' if. /4’ A36' Actual volume from adoPted dimensions: Sump (2. x 2 I 1) 35 4.0 Sludge tank (11 x 13.6) .~.- 149.6 Remainder of tank (50 x e x 13.6) :M 2601.6 AllOW'3.5 foot freeboard 3: 630.0 3851.6 cubic feet A ctual height of water surface (from.t0p or sump ) 2598 - 4 - (11 x 13.6) :- oo 2: 13.6 h 2598 .- 149.6 3: 408.8 h 2444.4 11 3: . 2:: 6 feet 408 Design of Filter: The filter is designed for the application of 300,000 gallons of water per acre per day. The amount of waste applied is: Q t 8 x average ra' waste flow ::8 x 28.8 x 60 x 24 r 538,000 gallons per day Filter area required: A : (332,000 x 43,560)/2,ooo,coo : 736 square feet a : v x 4/5442 1: '72. t 50.4 The filter consists of a large cylindrical reinforced concrete tank set above the surface of the ground. The bot- tom.wus given a slepe of 1" in 8' in the direction of the outlet. 'Dreinage is by half-tile pipe laid in parallel rows with Open Joints running towards the outlet. To facilitate drainage, a small rectangular channel was set in the floor and covered with loosely jointed brick so that the upper sur- face of the brick is flush with the floor of the filter. At each end of the parallel lines of tile drains on the floor an upright 6“ tile pipe is placed to provide circulation of air to the stone. This pipe is placed to provide circuculation and extends Just to the surface and is suonortcd by the stone surrounding it. The size of stone used varies from four inch diameter for a depth of one foot to a size between 2%" and 3%" up to the surface making a total depth of six feet. A four foot pier was constructed in the center for holding the shaft of the ro- -8- toting distributor. It is of rectangular cross section vary- ing from.a side of two feet at the base to one foot at the top. The shaft of the rotating arm is stationary, and fixed into the concrete so that over 2/3 of it is embedded for sup- port. The pipe line from.the pump at the holding tank Joins this shaft in a tee connection Just above the pier, but below the surface of the stone. Various types of distributors may be purchased from.concerns specializing in their construction. The type contemplated for use in this problem was one which would be supported on the end of the fixed shaft by a ball bear- ing arragement at the end. The influent from.the holding tank is mixed with the re- ciréulated waste from.the filter and applied at the rate of 230 gallons per minute.. This diluted waste was proportioned so that 1/8 of it is raw waste and 7/8 the recirculated ef- fluent from.the settling tank. Thus, a volume equal to 8 times the raw waste from the plant is applied continuously to the filter, and an amount equal in volume to the raw waste is discharged to the stream, after passing through the settling tank. W: The effluent from.the filter flows by gravity into the settling tank. The pipe enters the end of the tank at an angle so that the wall is used as a baffle in abating its velocity; A weir equal in length to the width of the tank was placed at the other end. The effluent flows over this weir into a small channel which in turn discharges into a - 9 - ‘weir box with a 90° V-notch. An outlet in the bottom.of the box returns 7/8 of the fIOW’tO the inlet pipe of the raw waste as it enters the holding tank. The remainder of 1/8 of the effluent, which is equal to the volume of the raw waste flows over the weir and is discharged into the stream. The tank is designed with a heppered bottom,designed so there is a detention period of 30 minutes. A sludge drawaoff pipe and valve is placed at the center of the tank. This same pump and pipe line is used for drawing sludge from.the holding tank. Calculations: Tank Capacitytz 1/24 x detention neriod I flow 1/24 x 1/2 x 3:52.000 :: 6,920 5,920/7.4s 1: 9:35 cubic feet required ——————————_———__—.—1 /0’ //’ ___/4 ’ ““”‘l'§;l‘ /4 ’ 7 3.! ‘ 8 Volume of designed tank: 2 x 8 x 2 ix: 8 28 2(1x7)x2-: 61:21:50 2360 e/zxexzso z 540 956 cubic feet 3.5 x 8 x 30 .2: 840 " " Freebosrd Pipe frietion e 120 - fairly smooth f 0.0269 b fI/d x vg/ag o 0269 x Vz/Zg 4 2 0.0807 x vg/eg 2, V'lgs DISTRIBUTOR Lose in distributor 30 Openings assume 3/8“ diameter A 0.7856(1/32)2 item 0.00076? Entry L.00 90 Bond 0.50 C per nozzle - 5' -4*P1pe 0.42 0.513 0.0171 c.r.s. 90 Band 0050 30 - 4! Pipe 0.32 v Q/A 90 Bend 0.50 10’ Pipe 0.81 030171 22.3'/see. 45 Bend 0.15 0.90076? 2 13v Pipe 1.45 1-5 ve/zg 1.5(22.e) 90 Bend 0.50 64.4 7' Pipe 0.56 Lose 11.64‘ Tee 1.50 2' " 5"?1136 0.21 Total 9.46 we elevation of diet. 103.5 ".3. ' in bold tank 93.0 Area of 4' pipe 0.0873 ' static head 10.5 diet. lose 11.64 0 25004 gopomo p1pe 108833 5:;0 0.513 o.f.e. Total pumping head 27.24 V 0[A 0.513 5.87'/sec. 5.5853 v2 2 5 a7 2 34.7 0.558 / s 155.7). m Loss - 9.46 X 00538 5.10 -11- Item vg/Zg €11th 1.00 Gate valve 0.10 1'-§”Pipe 0.11 Toe 1.50 90 Bond 0.50 12 1/2'Pipe 1.01 90 Band .50 Pump 90 Bend 0.50 6 l/Z'Pipe 0.64 90 Band 0.50 2. - 5"T’1pe 0.20 Gate Valve 0.10 Dischar e 1.00 Total 7.56 h 7.66 x 0.00405 0.031 :? PUMP N IN 7197' ‘——s. filer/fee $5 .5" 00.5:- 2'- 6" 6505 ’ n Gui Pal-1P i ’2'~o' .7 fi— 357711” ,L 4"f: /’.4’ raw—1M : - , ><1— ”ow/w 7'79 ”K Pike friction e V 2 V leg 120 fairly smooth 0.0269 fl/d x vang 0.0262_ L véng 4712 0.0807(L) vglzg 4' pipe 000875 20 gopomo 0.0445 OOfOBC 030445 0051 ‘/8800 0.0873 (0.5123 64.4 G/A 0.2615 0.00405 Static heed 3.000 friction ' Total pumping “ 0,03 3.03 feet BIOCHBIJICAL TISLLYI‘LEET The biochemical treatment process of milk waste treat- ment is known as the Guggenheim.Prooess, patented by the Guggenhein.8rothers, Hew'York City. In this process the milk waste is treated with ferric chloride and line and then aerated. The floo resulting from aeration is allowed to settle, and the sludge which is ao~ cunulated is returned to the raw waste to pass again through the process. From previous tests run on the raw wastes at Perrinton. it was found that line applied at the rate of 100 ppm and ferric chloride at 50 to 40 ppm.gave the best results when aerated for a period of four hours. 1) .EBIGN 0F TKEETII’T PLAH’I‘ The plant for this type of treatment consists of the following'units: {1) A holding tank for receiving the raw waste. (2) Chemical tanks. (3) Mixing device. {4) Aeration tank. (5) Settling tank. chaininsuissh; The volume of the tank is designed so that is is pos- sible to pump at a constant rate and have the tank emptied once every 24 hours. The pumping rate was determined from - 15 - The average hourly flows compiled from the flow data of the plant. A pumping rate of 25 gallons per minute was found to be sufficient. Hy starting the pump in Operation at 10 A. LL, there is sufficient accumulation of raw waste to permit a constant Operation of the pump through the whole working day. The maximum.raw waste flow occurs at 4 o'clock when consider- able washing up occurs in the plant. The maximum volume which will he in the tank will occur at about this time and amounts to 6.32 gallons. The raw waste flowing into the tank gradually decreases after four o'clock so-thnt the pumping rate soon exceeds it and eventually empties the tank. a tank of 8,000 gallons capacity was required. %*%§9~ : 1,070 cubic feet Thus the pump will be in Operation about 12 hours each day. I The table below shows volume of waste in the tank for any hour of the day. Time Pm: u‘aste fi‘low Draw Down Volume of haste By'Pump In Tank Gal/Kin 081/ nr 1500 Gal/Hr Gallons 7-8 all 10.33 20 None 620 8-9 am 14.80 888 Reno 1508 9-10 hm: 20.54 1230 btart Pum 2738 10.11 14; 21.553 1395 1500 25:53 11-12 am. 51.50 1890 1500 2933 12-1 392.1 54.50 2070 1500 3403 1-2 111 40.03 2400 1500 4393 2-3 P21 38.51, 2310 1500 5203 5-4PLI 43.73 2635 1500 6328 BIOUILILICL 1:431; 111.? 03‘ LLBJL '3 -LuaLJJ heretion time ; 4 hours Settling time : 2 hours 1.11116 : 1-30 13.13.10. Ferric chloride : 80 p.p.m. 5-day B. O. D, Aeration tank Raw Treated Reduction Air Suepenfied non: rm Zero-art 02... ft ..- ”111. 501503413111 123 5 95.8 - 3540 150 10 93.4 1.5 5004 190 40 79.0 - - 200 16 92.0 5.7 2792 204 15 92.8 1.5 2868 251 50 87.0 1.1 1048 833 5 97.8 2.5 4476 258 33 91.1 1.3 ~- 263 17 93.6 3.6 2404 266 17 93.6 2.0 2168 285 55 80.6 2.0 - 290 59 86.5 2.5 ~- 290 23 92.0 3.1 - are 30 91.0 1.1 1616 358 52 90.6 1.4 5844 343 60 82.5 2.0 2352 356 48 86.5 1.6 2568 400 37 91.0 2.8 3156 400 37 91.0 2.5 4293 408 13 68. 5 - ~- 415 34 91. 7 2.6 3924 447 54 85.7 - e“ 450 35 92.3 3.4 2208 480 34 93.0 3.0 1024 450 35 94.4 2.5 3664 500 36 92.9 3.0 3000 525 57 89.2 2.0 2264 538 52 90.2 2.0 1904 624 78 87.5 200 2800 650 58 92.6 2.7 1016 654 3 93.6 3.0 2524 554 147 77.9 2.0 2200 740 f42 94.4 3.0 1032 815 107 86.8 2.8 3000 1000 107 89.3 3.0 7520 1004 120 88.0 3.0 1761 1268 135 89.5 2.0 2175 1300 1:3 96.5 3.0 gg40 6 90.0 2.0 0g avg 47% 51 89.8 2.4 2746 1) Emma or HOLDING nun: 511051136 DEIEEJSIONS rem vowrms 20' _J L A5" '1 F B _ __ B ‘T e b A e u L /o' -1, m' J 2' f‘ '1 V91. 312120: 240 391203780 4 1:10 :__A&L_ 1060 cf (Assume 1’ free- -_ p board) 15 x 20 LE9... Maximmn Volume I 1360 01‘ (required volume = 1070 of) Volume of tank assuming one foot freeboerd equals 1360 cubic feet. The tank was given a happered bottom.to prevent any accumulation of solids on the sides. The draw off pipe was placed in the center so the exit is flush with bottom or the tank. The drewoff pipe runs to a pump set in the bottom of a well at the same elevation as the draw off pipe. The tank is also provided with two lengths or air pipe, each 18 feet long to keep the raw waste in a fresh condi- tion. A.velve on the line permits adjustment in the amount of flow. The raw waste pump is of the centrifugal type. The pipe line from.tank to pump was designed to give a velocity of 215 feet per second at the point of‘discharge, into a mixing be: 10% feet directly above the pump. A pipe 2 inches in - 15 - diameter was used to give this Velocity and thereby provide turbulence for the mixing of the chemicals in the box. The calculations for the pipe line and the horsepower required follow: Pipe (fiction I o = 120 L—1 f = 0.033 '/oec. h : tl/d x lie/23 : 0.033 1. V2/23 hm J- 2712 2 ti ,2,_ 6" PUMP = 0.193 1.“! /23) e C :25 g.p.m. = 0.0556 “Orbs. V::20/sgc. Item v3/23 Use a 8' pipe Entry 0.10 A=O.7856 x (2/12)? V VZO/A 12.5.P1p3 2.50 __O 0556 :2.55./8800 Discharge 1.00 V's/23 : (2.55 22 _, A 64.4 ' Friction head : 6.40 x 0.1012: 0.646' Static head =:10 50 Total head ==il.143' Horse power of pump required. (assume 50% efficient) H.P.:-25 x 8.34 1 11,146 2:0.1448 330000 x 0.50 Assuming motor is 85% efficient - H.P.::0,l448 2:0.1700 Ugo c 1/4 H.P. motor 0.85 . lazing B9; and Cher: 4%; Fgedgm: The velocity from.the centrifugal pump upon discharge into the mixing box gives sufficient turbulence to the waste so that the lime and ferric chloride which are added at this point are kept in constant motion. The box is of rectangular cross-section with e 60 degree Vonotch outlet at one end. .ggonnt 9: Line: The lime is applied by means of an electrically vibrated feeder manufactured by the Jeffry-Treylor Co. The capacity is regulated by means of a calibrated dial transformer. For this installation it is to be set to deliver 100 ppm or 1.25 pounds per hour. Q 2 25 Gallons per minute 1 ppm. : 8.34 pounds per million gallons 5 e , 1,000,000 ‘ 1‘35 *b3-/h°ur The feeder can be provided with one, three, or five cubic foot h0pper capacities, furnished by the manufacturer. ‘ F C d : .A 40% solution of ferric chloride is to be ap- plied by means of a siphon set to deliver 50 ppm.or 0.375 pounds per hour. §9_z;2§;r_dggndiddi . 1,000,009 . 0.575 lbs./hour .375 x loco/212 : 170.5 grams A 40% solution is used: 170.5/.4o x/e x 255.5 g of 11.0 170.5 g of.FeCl .0 O. 3 - 18 - l70.5/255.5 :: .677 grams per cubic centimeter 855.5/60 : 4.36 so per minute .67? x 4.36 x 3.2/1,000 x co = 0.375 a per hour. Therefore, the ferric chloride siphon is set so that it delivers 4.26 cubic centimeters per min- ute. fiith a constant flow of this amount, a five gallon bottle is of sufficient capacity to allow a run of six days before refilling. 1 gallon = 3,785 cubic centimeters 5 x 3.785 _ 4.26 x 60 I 12 " 6'18 days angitx_£lgp to Aeratiginagg; The milk waste flows by gravity from the mixing tank to the aeration tank. t is carried by means of a 60° tri- angular trough with a side of one foot in length attached to the outlet at the end of the box. The trough has a slaps of a foot in ten feet from.thc mixing box to the return sludge pipe. At this point, the trough changes its direc- tion 90° and follows the wall of the aeration tank tO'with- in one foot of the end wall where the waste is discharged. This slope of the trough and the 90° bend provides a hy- draulic pump effect so that the with waste chemicals and return sludge should be well mixed upon discharge into the .aeration tank. W: The capacity of this tank is designed so that there is four hours retention. 4.0 x 25 x 60 equals 6000 gallons Twenty-five percent of the total flow is allowed in the aeration tank also for return sludge. 6000 plus 1500 equals 7500 gallons r 7.48 equals 100 cubic feet required. 1r 20‘ A 3"," '1 L—q Vol. 8 x 6.25 x 20 : 10000: Assume 1 foot freeboard 20 x 6.25 : __Jg§L_. 1125 c. f. The aeration tank woe made rectangular, and the sens in depth and length as the holding tank to make possible the use of a common well for the two tanks. The total volume of the tank including one foot freeboard is 1185 cubic feet. Previous experiments show that a quantity of air equal to 5 cubic feet per gallon give the best results, with 15% of the surface area provided as aeration area. The diffuser pipe used in the esperiments were of 18" lengths perforated with 3/8 inch circular Openings. Each length of pipe was wrefppod in cloth fabric of the following dimensions: mathzcn 3 E3 __‘1_0 per 1. 5' of pipe. Length—:1!“ =1 ' 3' of pipe. Surface area of tank - a, 20 x 6.0 = 120 159! of surface are: is for aeration «- 120 x 0.15 =18 sq. ft. 18 1 3254 ft. of fabric covered pipe required. Three lines or 131' " pipe at 13' per line were placed at the bottom of the tank. A header was placed above the surface of the tank as shown in the sketch. ~. ' .\. 1/5005: ~ V { UNION The header is provided with valves, so that each line of air pipe may be regulated separately, or be removed for repairs without interrupting the Operation of the others. Two air meters were placed m the delivery line from the air compressor so that the quantity of flow may be measured for the aeration tank and the air lift. The effluent from the aeration tank flows into the set- tling through a triangular outlet located disagonally op- posite the point ot which the waste enters. SQIIJIEF ngk: The settling tank is designed for a retention period of one hour.‘ 25‘: 60 x l x 1500 gallons A llowing 23%, or about 400 gallons for the sludge which is being continually recirculated back with the raw waste, 2000 gallons capacity is sufficient. 2.999. 7.48 equals 267 cubic feet required I l /5’ I k 7 l __!L_ p.24 :44 The tank is designed with hoerered bottom and small sump at bottom of 2 cubic feet capacity. an air lift pipe is used to lift the settled sludge to the surface where it is dis- charged into the raw waste as it flows to the aeration tank. :13; L113: 25% of the flow is recirculated into the raw ‘ waste by the air lift ngfii:5.25 gepeme Z 0.0139 00:03. 0 Try a 2' sludge pipe A =20.01228 n a 1/20 811' U A, = 0.00136 -0: 0139 _-: 1e25'/8€Ge v zo/A = o 0139 _ 0.01228 - 0.00135 0.01092 The air pipe is placed within the eduction pipe. The amount of air for the lift is regulated by a valve placed between the delivery pipe and the main line. To take care of excess sludge, a sludge pipe was placed at the tap of the eduction pipe to carry the excess off where it can be discharged or hauled away. A valve was placed on both lines so that the flow of sludge through each may be regulated. The elevation of the water surface in the aeration and settling tanks is kept constant by a rectangular weir placed on the discharte side of the settling tank. The supernatant effluent discharges over the weir into a small flume which in turn discharges into a weir box and thence to the stream. The weir box will enable measurement of flow so that the pumping rate from the holding tank may be known at any time. DETEIEZBIATIOH OF COLE'I' Co a F re 0 P L : (1) Holding and settling tanks: 2005 cu.ft. (assuming a wall 10 thick) (8) Filter base and wall (1" thick) 1810 cu.ft. Covering of holding tank .§§l§.0u.ft. was assumed 6" 27 141.5 cu.yfi. nggpggg jg Biochemical Plant: All walls and floors 10" thick Holding tank cover 6" thick “air and mixing boxes 6" thick Total volume required : 1647.7 cu.ft. 61.0 cu.yd. COST OF FILTRATION PLANET Item. Quantity' Unit. Amount Price hsssvation -540 eu.yd. 0 1.00 3 340.00 Reinforced Concrete and forms 141.5 " 50.00 4250.00 4“ C. I. Pipe 76.5' .60 46.00 4" 90° Bends 9 1.25 12.50 4" 45° Bends 1 1.25 1.35 4" Gate Valves 2 50.00 100.00 4" x 4 x 2 Tees 2 1.25 2.50 Valve Stands 2 20.00 40.00 230 gpm.Punp and Meter 1 400.00 400.00 20 gpm. " " " 1 _ 150.00 150.00 Rotating Distributor 1 150.00 150.00 Split drain tile 200 ' .10 20.00 Brick 200 $15./iooo 3.00 6" Tile Uprights 54 .40 21.60 Filter Stone 18? cu.yd. 5.00 561.00 Electric ¥iring - 75.00 75.00 g 5 6172.00 Contingencies : 15% 925.00 Estimated Total Cost 5 7093.85 -24- COST OF BIOCIEEJCAL TREJ TIMI? PIJLNT Item. Quantity Unit Amount Price Excavation 200 cu. yd. 5 1.00 5 200.00 Reinforced Concrete and forms 61 cu. Yd. 50.00 1830.00 4" Gate Valves 1 50.00 50.00 25 gpm.pump and motor 1 150.00 150.00 Air1meters 2 75.00 150.00 Air compressor 1 250.00 250.00 1%” Air Pipe Galvan. .150' .14 21.00 ii" Brass Valves 6 6.00 56.00 ii" Elbows 5 .50 l.50 it" Tees . :8 150 2.40 Lime Feeder /' 1 1/1 125.00 125.00 2" Pipe [46' .25 11.50 Concrete-Triangular 0' ’ Trough .75 cu. yd- 30.00 23.50 4" C. I. Pipe 17.5' .60 10.60 4" 90° Bend 2 1.25 2.50 5 2562.90 Contingencies: 15% 400.00 Estimated Total Cost: 0 3062.90 0rnnns*ue COSTS High Rate Filtration: (l) Depreciation: A life of 20years is assumed with depreciation at 5% per year. $7097.25 1 0.05 : 5 660.00 UN labor: The labor required amounts to about two hours per day. Assuming $1.00 per day, 1 x 505 565.00 (5) Euuping costs: The raw waste pump is the largest item. Cost of electricity is assumed to 2 cents per kilowatt hours. For a 3 H. P. pump. 3 x .746 x 24 x .02 x 365 : 592.00 Sludge pumping costs: ‘ 8.00 Total Operating cost: 5 1125.00 B T ent.e : (1) Depreciation: at 12% .12 x 55062 : 5 566.00 (2) Labor: Aprroximntely % day by skilled oper— ator. 5100 per month. 9100 x 12 : 1200.00 (5) Lino: 1.25 e per hour: 12 hour Operation. 1.25 x 12 x 6 x 52 : 4675 1bs.per _., year 4625/2000 e ele./Ton in sacks : 42.00 (4) Ferric Chloride: 0.575%[Hr. 01575 x 12 x 6‘1 52 : 1400 #/1113 .07: 92.00 -26... (5) Punping Cost: @ $.02 per kilowatt hour For a 2 horsepower motor, 2 x .746 x 24 x .02 x 565 : 2 260.00 Total Operating Cost: 0 1966.00 COJPA41303 OF.DUTI33 (1) Three to four weeks is required to develOp the filter organisms. To aid in building it up, 2 enter extract of manure may be used. (2) Composite samples should be collected and anal sod occasionally to determine the strength of the waste applied. If it becomes too strong, provision must be made for diluting it with clean water. (5 The holes of the distributor arms must be made clean occasionally. (1) .A trained Operator Should be at hand at lenst half of the day. He should run tests and analyses occasionally to check the efficiency of treutrent. (2) The holding tank must be coupletely emptied once each day to prevent septic conditions. The walls should be washed with water once a week to prevent septic actions. (5) Raw waste should be kept fresh by passing a small on ntity or air into it. (4) The line feeder should be maintained to deliver 1.25% per hour at a pumping rate of 25 gpm. - 27 - (5) The ferric chloride siphon should be set to de- liver ahout 4 cubic centimeters per minute. (6) The amount of air delivered to the aeration tank should be 5 cubic feet per gallon or 135 cu.ft. ner'min- ute when pumping at 35 gallons per'ninute. (7) The sludge in the setling tank must be kept moving into the aeration tank. If an accumulation of sludge occurs septic conditions will develop which may upset the process. (8) Suspended solids in the aeration should be maintained at 3000 p.p.m. COELZPARIS‘ ”*"I 03? AD Vi-"J‘J‘I‘hGiiS _ 4 _ Average Treatment First Operating Cost Reduction in Cost Per Yeah 1:34 04 D. Filtration 3 7097.85 is 1125,00 91.8 % Biochemical $ $062.90 $ 1966.00 89.2 % From the comparison of duties it is evident that the high rate filtration process requires the least attention for ef- ficient Operation. The first cost of this plant is twice that of the biochemical treatment, but the Operating costs of the letter is higher since much more attention is required to main- tein the proper pronortioning of chemicals, Wests, and air. The average B. 0. 5. reduction is about the some for each plant, both processes being very efficient. -28.. v . t on . . O . . - OD| ‘ . , A ll'l n M o )1 1 o 1 .4 . . . n "‘7'“ - .‘ I - .Mg4 (‘0‘ ‘1' i, , o ,p r. n. ' ' 4! a: . . . I .,.' t N- I a". I o 0 ‘~' .‘. ‘ ”:1 ...;;4 .’ O a 0 I" .w -' ‘ ‘ ~.. 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' II D 11'0“"- . u ' x O" - . . . ovhp ‘ t u 4 v\ \ .1 k' ‘1 P“ u y...“ ‘0 cm I, .q. .,... ,, “ 0. our U'VI .' l .I ~-' “ . 37.- 5A.. ~ - l . _‘ .. .n-u. h o “who.“ . ~ H. mm - ‘ .. 4. u . ‘ I 5" ' . . . u .“N‘ ... . a VI \" “' ‘ D. ‘ ' .45...” . q t on..- l‘ “0 ‘ o u‘i'i u . .y . II V... bv\¢ ‘ . brav~.0.l II . («he s i . .7... J; H... O‘ 5“ »Q'..‘n.~~( b‘Ozvs not 4...»: o ' n 11236273.. :9. *0. \ gn,y~ u I II t n . not out 8.22:3: ‘1 .. ‘.u.-. ....'.,. . ,...... ‘4,” y-t'uo O‘Mth . CNN «55.. “not? ylo'~.. .c‘ofl M»~ u. , My 1...... .0 .1...“ 04 'aa\‘. U ‘5 ‘05.. ”Ms.”- . ..... . p, u'. . . _ A In. 0.1 y». ... . Qte'fi-H hush: , 1 $er .w m. s . Nut, o- .s...” ol , no I r L h-uvl . .fil’ perv. t . ‘ up \ )'.‘)'1 ., ‘ 1.:A“ o -,..~IN| V « Q'\-. n huh}! :......:.. | , "TO-0 ua . “u ‘nn-uh nun. .M . . ‘ .Rfinxl :J: ’2‘ ‘1 h‘flzvl >'\c| we -. I“. w l o . truer “rut-d ms t \ nu» \¢~ ,.,. ( 'un‘vu: w. ' .n'o.uu“ x..~ ( A " l -; ULJL :33“) 't 'r:;..~" . A . ~01 . v 1 1 . I ‘.~ vuz‘t J‘. ' Q1 .05 900'“ sew ‘ h- to” '. “51.. 1;» h ‘ .. my.“ '43:. «I am- '5 .QV“"‘ 4‘ 0 t .fil‘ QM 0 Q t . a la n a .sh I . .0 it u 0. o .- BIBLIOGRAPHY Fldridgo. E.F., "A Further Study of Eilk waste Treatment Processes.” Bulletin 77, Mich. Eng. Exp. Sta. East Lansing. Mich. Nbv. 1937. Fldridge, E.F.. ' The DicpoSal of Whats: FTbm Milk Prod- ucts Plants.“ Bulletin 272, Mich. Eng. Exp. Sta. East Lansing, Mich. June 1936. Eldridge. E.F. and Theronx.F.R.. ' Bo ort on Sanitary Engineering Projects Year 19 6' Bulletin 71, hlch. Eng. Exp. Sta.. Boot Lancing. hich..ch.1936. Stool. E. W. and Zoller. P.J.A.. ' The Treatment of Dairy Wastes,“ Bulletin 38. Texas Eng. Exp. Sto..hey 1930. Ruf,H. and Whrrick.L.F.. ' 211k Waste Treatment Studies In Wisconsin.“ Reprint from Sewage Works Journal. Vol.10, NO. 1’ Jan. 1938. Eldridge. E.F.. ' Report On sanitary Engineering Projects 1938,“ Bulletin 83 Mich. Eng. Exp. Sta.. East Lansing. Mich. Nov. 1938. Apar. Q.A., ' Practical methods of Preventing Dairy waste _ nuisance," Reprint from Sewage works Journal, vol. 10, Jan. 1938. r.";' A \‘?.‘HQV'D a" '0 art.» \" “fin-I vvv" ' ' r“- " V- ' .' ' ’ ' - V ' ' ' ' _ ' . ' .. - o ' '-;‘ ' ' . . gnaw ' ‘ M‘fi-o‘ s "11'1le Tl|‘f"‘“\’. '3. 0316 951-) ‘ LL. .O' .1 al.ll. (- 0'7 4' ' . I