Evaporator Heat Transfer Coefficients for Beet Sugar Solution ALLISON S. CHANG l Received for publication January 0, 1964 Evaporaton plays one of the most important roles in the sugar refineries. The existin!l data available to crive a functional relationship between heat transfer coefficients and operating pres SlIres are somewhat limited. Kerr () obtained the heat transfer coefficients for thirty-nine different evapof1tors, double-, triple-, and Quadruple-effect in actual operation. He plotted heat transfer coefficients against operating pressures in pounds gage and in inches of mercury vacuum. The points scattered so badly that it requires a careful judgment to use them. Several European technologists have worked out the formulas which take into consideration brix of the juice and the temperature of the heating vapor. However, the heat transfer coefficients calculated by the formulas do not agree with the actual values obtained by heat balance in this investigation. The data reported here were obtained from full size evaporators in actual operation. Heat transfer coefficients were plotted against solids in solution rather than operating pressures. The result showed a better correlation between heat transfer coefficients and solids in solution. The curve shown on Figure I is applicable to both standard short vertical-tube evaporators and standard horizontal-tube evaporators vvith tubes in normal deanliness. A formula based on the curve shown on Figure I was proposed to estimate the heat transfer coefficients for beet sugar juice in the evaporator. Apparatus The apparatus used in this investigation were quintupleeffect full size evaporators at Factories # I to #4. They were standard short vertical-tube evaporators with center dml'ntake. Evaporators at Factory #5 were horizontal-tube evaporators except the first effect which was a standard vertical-tube evaporator with a center downtake. The sizes of evaporator used in this investigation were as follows: 1 Chemical Engineer, Engineering Department, The Amalgamated Sugar Company, Ogden, Utah. Numbers in parentheses refer to literature cited.
154 JOURNAL OF THE A. S. S. B. T. e factoay NO.1 'ACTORY HO. I) FACTORY NO.... eoo X FACTORY NO".. o rac TO III;V NO.!I ''0, ~ 00 SOUDS IN SOLUTION. 61'1.1 )( Figure I.-Heat transfer coefficient for beet sugar solution. Factory #1 1st Effect: Two bodies ::>,176 sq.ft., 11;4" OD, 14 gao copper tubes, Il'-Vi" long. 10,750 sq.ft., 11;4" OD, 0.049" steel outside, 0.05" copper inside, bi-metal tubes, 9'-61;4" long. nd Effect : Three bodies 16,00 sq.ft., 11;4" OD, 15 gao copper tubes, 9' %" long. 15,400 sq.ft., 11;4" OD, 15 gao copper tubes, 8' 6%" long. 10,70 sq.ft., 11;4" OD, bi-metal tubes, 9'- 61;4" long. rd Effect: 6,900 sq.fl., I 1f' OD, 15 gao copper tubes, 6' %" long. 4th Effect: 6,60 sq.ft., 11;4" OD, 14 gao copper tubes, 6' %" long. 5th Effect: 6,00 sq.ft., 11;4" OD, 14 gao copper tubes, 5' 6%" long. Factory # 1 st Effect: 16,744 sq.ft., 11;4" OD, 14 gao copper tubes, 9' 1;4" long. nd Effect: Two bodies 15, 17 sq.ft., 44 q~" OD, 7/ wall, steel tubes, 9' l/4" long. 5914 qq" OD, 14 gao copper tubes, 9'- 1/4" long. 6,85 sq. ft., I Yz" OD, 14 gao copper tubes, 5' 61;4" long.
VOL. 1, No., JULY 1964 155 rd Effect: 10,0 sq.ft., 6 I ~4/1 OD, 7/ /1 wall, steel tubes, 8'- ~ -4/1 long. 4440 1 ~ /1 OD, 14 gao copper tubes, 8'- ~/1 long. 4th Effect: 6,854 sq.ft., 1~/1 OD, 14 gao copper tubes, 6' ~/1 long. 5th Effect: 7,1 sq.ft., 1~/1 OD, 14 ga o copper tubes, 6' 4~/1 long. Factory # 1st Effect: 16,744 sq.ft., 1~/1 OD, 14 gao copper tubes, 9' Y4/1 long. nd Effect: Two bodies 1l,1 sq.ft., IV4/1 OD, 15 ga. copper tubes, 6' 7%/1 long.,00 sq.ft., /1 OD, 14 gao copper tuoes, 4'- IY4/1 long. rd Effect: 8,614 sq.ft., I ~/1 OD, 15 gao copper tubes, 6' 7%/1 long. 4th Effect: 6,058 sq.ft., I Yz/l OD, 14 gao copper tubes, 5' 9~/1 long. 5th Effect: 6,854 sq.ft., 1~/1 OD, 14 gao copper tubes, 6' ~" long. Factory #4 1st Effect: 15,84 sq.ft.,,640 1 ~/1 OD, 14 gao copper tubes, 9'- %/1 long.,106 /1 OD, 14 gao copper tubes, 9', %/1 long. nd Effect: 8,474 sq.ft., 1~/1 OD, IS goa. copper tubes, 7' 0/1 long. rd Effect: 0,55 sq.ft., 1~/1 OD, 15 gao copper tubes, 5'- /1 long. 4th Effect: 4,540 sq.ft., I ~ /I OD, 15 gao copper tubes, '- 9/1 long. 5th Effect: 5,145 sq.ft., 1 ~/1 OD, 15 gao copper tubes, 4'- /1 long. Factory # 5 1st Effect: 5,860 sq.ft., vertical-tube, /1 OD, 1 gao copper, 5'- 5Yz/l long. nd Effect: 5,86 sq.ft., horizontal-tube, 1/1 OD, 16 gao admiralty brass, 15'- 4/1 long. rd Effect:,945 sq.ft., horizontal-tube, 1/1 OD, 1 G gao admiralty brass, 1'- 7/1 long. 4th Effect: Same as above. 5th Effect: Same as above. Factory steam flow rates, dome pressure and temperature recorders were supplied by Taylor Instruments Company. Thin juice brix to 1st effect and thick juice brix from 5th effect were
156 JOURNAL OF THE A. S. S. B. T. 10,-----------------,... ~ 6 ~ 5,... z ~ ~ ~ I 10 0 0 40 50 60 70 SOLIDS IN SOWTI()'.J. BRIX Figure.-Boiling Point elevation for sugar solution..9.8 measured by laboratory refractometer. All intermediate brixes of juice were measured by laboratory hydrometer. Quantities of thin juice to 1st effect and thick juice from 5th effect at # and #4 factory for run #4 were measured by Foxboro, "Model No. 9650 C, Magnetic Flowmeter. Others were calculated by overall factory heat and material balances. ] uice inlet temperatures at 1st effect were measured by Model R, Dillon Dial Thermometers.," a:.7!i'.6 '9 a:.5!i' :::>.4 to,. ~. I ~.1 U ~ o~_l~~_l~~_l~~_l~~~~ SOLIDS IN SOLUTION. BRIX Figure.-Specific heat of sugar solution taken from laboratory data.
VOL. 1, No., JULY 1964 157 General arrangement of evaporators for factories # and #4 is shown on Figure 4. General arrangements of evaporators and flash tanks for factories # I and # are shown on Figure 5. General arrangement of evaporators for factory #5 is shown on Figure 6. ". FLOW Q[AGRA'" ~~r~, I THIN JUICE I I I THICK JUlCL.. ---STEAM : I :' :~', L~ I r--l~,- L J : I I l c9 i dj CO~ENSATE NOTE:.-"""""1 r--'" r - -------.. UN[ c9 --JUICE LINE --- - WATER OR CONDENSATE L L==== == ~_==~_..: Figure 4.-Flow diagram (top) for factories # and #4. Figure 5.-Flow diagram (below) for factories #1 and #. Over-all Heat Transfer Coefficients The heat transfer coefficients depend on the cleanliness of surfaces on both the vapor and juice sides, on the metal of which the tubes are made, on the ratio length and diameter of the tubes, on the temperature difference between the vapor and juice side and, finally, on the brix of the juice and the temperature of juice.
158 JOURNAL OF THE A. S. S. B. T. I THICK JUICt....CTOAY t-in. Figure 5.-Flow diagram for factory # 5. Dessin has worked out the following formula which takes into consideration brix of the juice leaving the evaporator and the temperature of the heating steam or vapor. U = 960 (100 - Ex) (tv - 10) 16,000 The above formula gives higher heat transfer coefficients for 1st, nd and rd effect and lower heat transfer coefficients for 4th and 5th effect under investigation. Swedish technologists propose the following formula: U = 49. (tj - ) Bx The above formula gives lower heat transfer coefficients for 4th and 5th effect in this investigation. MacDonald and Rodgers propose the following formula: 55 (tj - U = 100 ) V/Lj X aj The above formula gives lower heat transfer coefficients for every effect from 1st to 5th body in this investigation. Data shown in Table 1 were 4 hours average. Dome pressures, dome temperatures, exhaust steam pressures were recorded every hour on the hour. Juice inlet temperatures, brixes of juice to and from each effect between nd and 4th effect were measured and recorded once every two hours. Juice and steam flow rates to 1st effect and thick juice from 5th effect were calculated by overall heat and material balance to within % accuracy for every factory without magnetic flo\,vmeter.
., 1 " Factory No. Run No. I Thin Juice to 1st Eff.ect # / hr. Brix 551,000 1.6 58,000 1.5 700,000 1.9 TABLE I. Exhaust steam to 1st etrect Pressure Temp. #/hr. psig OF 19,000 5.6 66 19,500 5.6 66 8,000 8.0 70 Pressure psig 17. 17. 0. 1st effect Sat. vapor temp. o f 51 51 55 1st vapor to process # / hr. 4,600,900 8,00 Juice out brix 18.7 0. 0.7 Condensate to 1st flash tank #/hr. 180,700 <: 0 r..:>" Z 9!'O '--< C t" ><:... <D 0> >f>. 1 4 51,000 497,000 504,000 510,000 1.4 1. 1.5 1. 175,000 187,000 195,500 188,000 4.5 5.1 7.5 4.5 64 65 68 64 1.4 1.4 J5.4 1.4 44 44 48 44 67,100 57,000 66,00 54,400 18. 0. 0.8 0. 98,900" 117,500 111,700 10,100 1 4 46,000 450,000 49,000 514,000 1. 1.4 1.7 1.0 151,000 15 1,000 169,000 178,700 8.5 7.0 7.5 6.4 70 67 68 66 18.1 16.0 16.8 15. 5 49 50 47 44,00 55,00 7,700 7,800 19. 19.5 18.6 19.4 4 1 4 78,000 9,000 5,000 6,000 1.9 1. 1. 1. 11,000 17,500 141,000 18,500 6.5 7.0 6. 6. 66 67 65 65 18.7 J8.5 J 5.5 16. 50 49 47 48 7, 100.85,000 97,150 91.500 19.4 0.9 0.0 0.8 5 1 4 5,000 4,000,000 6,000 14. 1 1.7 1.7 14.1 57,500 81,00 7,700 77,500 18.8. 1.9. 5 59 58 59 10.1 10.8 10.8 11. 4 6 6 7 0,100 4,500 5,00 9,000 18.7 1. 0. 1.1 " 1st flash tank in service only. v'" <D
TABLE l.-(continued) >-' C'l 0 nd effect Condensate rd effect Sat. nd vapor to nd flash Sat. rd vapor Juice Factory Run Pressure vapor to process Juice out tank Pressure vapor to process out No. No. psig temp. of #/hr. brix #/hr. psig "Hg vac. temp. OF #/hr. brix I 9. 5 11.500 0.9 1.11 1 7,800 7. 7.58 1 1,500 7.1 0.55 07 1,500 44. 9.96 7 155,000 6.0 148,990 1.11 1 19,000 4. I 7.40 1 51,00 5.6.14 15 7,470.6 5.87 6 86,100.5 151,900 0.71 10 1,750 40. 8.5 76,700. 149,900.14 15 15,550 40. 4 6.40 8 74,00 1.9 169,00 0. 07,000 4.5 I 9.57 8.76 8.8 4 51,700 46,500 5,800 7.8 7.4 5. 1.59 1.1 1.89 11 10 1 18,500 11,500 1,50 4 7.97 0 49,700 7..50 14 14,500 5.0 ~ :>r 0 4 I 9.8 4 18,50 5.1.4 1 6,090.0 '" 9.8 9.8 4 4 1,400 1,650 6. 4.S 4 10.0 8 1,650 5.8 4.9 19,5 10 1.4?' sn 5 I 4.1 ~8 11,000.7 4.97 19,100 9.9 sn.0 15 9,500 1..15 197 4,50 8. to.0 15 8.900 9.6 4.06 195 4,40 6.7 4.50 16 9,00 I.l 4.06 195 5,850 8.7 ~.4 4.15 16 17 1,915,650 6. 4.7.4.1 0.1 '-< 0 c:: >-l :I: Oi t\ ;,
Factory Jlio. Run No. Condensate to nl fbsh tank # / hr. Pressure "Hg yac. T,iBLE L-(Continucd) 0 <! 4th Effect 5th Effect Thin juice uo Sal, Sat, Thick juice inlet temp. vapor Juke out Pressure vapor Juice out fr0111 5th effect at 1st effect Z temp. 0 F brix "Hgvac. tcmp. OF brix # / hr. OF? XV 1 1,0 181 45,6,5 15 6Q,4 11 5, I OO '--' c:: 11,7 18 50.7 Ll 144 60,7 Jl 9.00 r.-< 19,970 11.4 18 48.5 1,0 145 59,5 151,00 4 -<.0 1 10,9 18 1,8, 15 68,1 94,9()0 176,850 9,89 186 49,1 1,5 140 68,7 95,700 5 176,550 9,1 188 49,7 0,8 141 69,5 97.900 0 4 190,900 11.4 18 51,5, 15 70,0 96,800 0'> H> 8,96 185 45,8 1,5 10 64, 95,700 5 10,5 l SI 44,5 Lfi 19 6,6 94,700 9,96 18 4,4 1,5 10 6,1 98,900 0 4 9,6 184 44,8 1, 1 64, 10,600 5 4 I 11,85 175 4,0.5 101,5 68,0 7.000 44 8,6 185 41,8 1,5 16 6,0 7,000 46 6.10 191 8, 19,7 140 54,5 79,100 41 4 7,1 188 40, 0.4 15 58,0 8,400 9 5 1 14,8 16 40,0, Jl4 6,5 5,80 11,5 175 46,9 19,9 16 6, 49.4 :)0 1, 17 46,1 Ll 16 6,8 47.950 5 4 1, 17 47,9 1,0 17 6,6 49.550 5 Atmospheric pressure Factory 7'\0. 1: 1,59 psia, 7,6 "Hg. factory No.: 1,41 psia. 7, "Hg. Factory :'-;0. : 1,81 psia. 6,0 "Hg, FacLory No.4: 1.56 psia, 5,:) "Hg. foctory No.5 : 1,4 psia, 5, "Hg. -0'>
16 JOURNAL OF THE A. S. S. B. T. Overall heat transfer coefficients were calculated by - Q u - ~T X A and tabulated in Table. Where ~T = effective temperature difference, OF = apparent temperature difference - b.p.r., OF. Apparent temperature difference: 1st effect = exhaust steam temperature 1st vapor sat. temperature, OF. nd effect = 1st vapor sat. temperature nd vapor sat. temperature, OF. rd effect = nd vapor sat. temperature rd vapor sat. temperature, of. 4th effect = rd vapor sat. temperature 4th vapor sat. temperature, of. 5th effect = 4th vapor sat. temperature 5th vapor sat. temperature, of. Sample calculations: Factory #, Run 4. Thin juice to 1st effect = 510,000 # / hr. Solids in juice = 67,800 # / hr. @ 1. brix. Steam to 1st effect = 188,000 # / hr. @ 4.5 psig and 64 of. 1st Effect: Heat from steam = 188,000 (96) = 176,000,000 Btu/ hr. Heating juice = 510,000 (45-) (0.95) = 10,50,000 Btu/ hr. Available heat = 165,650,000 Btu/ hr. 165,650,000 174500 # / h 1 st vapor = 949.5 ' r. Juice _ Brix 510,000 #/hr. To process = 54,400 # / hr. -174,500 # / hr. To nd effect = 10,100 # / hr. 5,500 # /hr. 0. B.P.R. = l.o F from Figure ~T = 64-44 - 1 = 19 F Heating surface = 16,744 sq.ft. U = 176,000,000 = 55 Btu per hr. per sq.ft. per of. 19 X 16,744 nd Effect: Heat from vapor = 10,100 (949.5) = 114,000,000 Btu/ hr. Juice flash = 5,500 (45-0) 0.8 = 4,1 0,000 Btu/ hr. Available heat = 118,10,000 Btu/ hr.
VOL. 1, No., JULY 1964 16 nd vapor = 1189~~~iOOO = 1,00 # / hr. J. Ulce Brix To process - 74,00 # / hr. 5,500 # / hr. To rd effect = 49,100 # / hr. -1,00 # / hr.. 1,00 # / hr. 1.9 B.P.R. =.0 OF T = 44-8 - = 14 of Heating surface = 1,60 sq.ft. 114,000,000 U = 14 X 1,60 = 77 Btu per hr. per sq. ft. per cf. 1st Flash Tank: Condensate = 10,100 # / hr. 10,100 (1.4-196.). Vapor = 960.1 =,0 0 # / hr. to rd.effect rd Effect: Heat from vapor = (49,100 +,00) 960.1 = 49,100,000 Btu/ hr. Juice flash = 1,00 (0-10.) 0.77 =,0,000 Btu/ hr. Available heat = 5,0,000 Btu/ hr. rd vapor = 5,: 0 000 = 5,700 # / hr. 7.J uice Brix To process =,000 # / hr. 1,00 # / hr. To 4th effect = 1,700 # / hr. - 5,700 # / hr. 159,500 # / hr. 4.5 B.P.R. =. OF T = 8-07 -. = 17.8 OF Heating surface = 10,0 sq.ft. 49,100,000 U = 17.8 X 10,0 = 75 Btu per hr. per sq.ft. per OF. nd Flash Tank: Condensate = 169,00 # / hr. 169,00 (196. - 175) Vapor = 97 =,690 # / hr. to 4th effect 4th Effect: Heat from vapor = (1,700 +,690) 97 = 4,700,000 Btu/ hr. Juice flash = 159,500 (10. - 186.5) 0.7 =,70,000 Btu/ hr. Available heat = 7,40,000 Btu/ hr. 7,40,000 4th vapor = 989 = 7,700 # / hr.. JUIce Brix 159,500 # / hr. B.P.R. = 4.5 OF - 7,700 # / hr. T = 07-18 - 4.5 = 0.5 OF 11,800 # / hr. 51.5
JOURNAL OF THE A. S. S. B. T. = G,854 sq.ft. 4,700,000 u 176 Btu hr. sq.ft. per of. X rd Flash Tank: Condensate 190,~)()O (175 1 to Eith 5th Effect: Heat from vapor = flash = 11 Available heat 5th vapor Brix B.P.R. 9. OF T= 1-15 - 0. = 7.S OF 70 surface 7 1 100,000 u X II.5 Btu per hr. per heat transfer codficients are ()ne of the most important data for sugar relineries. 'With the data of heat transfer coefficients it enables the refineries to estimate the by rearranging the equation A 1st effect: 1st vapor perature 1st effect. nd effect: nd difference L>T B.P.R. at rd effect: 4th effect: rd vapor sat. perature apparent nd effect. sat. tem at 5th effect: 5th vapor sat. apparent
it Fac tory N o. R un N o. Heat load If)Btu/ hr. B. P.R. o f 1st Effect Appal'ent T, OF TABLE. -< 0 Effective T, o F V," Heat load 10 Btu / hr. B. P. R. o f nd Effect Apparent T, o f E ffec tive T, o f u* r-'... :,>0 Z Sl I 4 179,500 181,000 6,000 164,000 175,000 18,000 176,000 0.9 0.9 15 15 15 0 1 0 0 14,1 14.0 14.0 19.1 0.0 19.0 19.0 508 517 :' 51 5 57 55 16,000 149,000 170,500 94,000 II 1,500 105,700 114,000 1.9.5.4 1.4,1.0.0 16 0 18 1 18 16 16 14,1 17.5 15,6 11.6 15.9 14.0 14.0 04 69 58 75 4 49 77 ~ '-< c r ><:... ~ 0'> ~ " 4 1 4 141,000 141,000!57,500 167,00 1,500 10,500 141,000 19,500 0.9 0.9 1. 0 17 18 18 19 16 18 18 17 16, 1 17.1 17.1 18,0 15,0 17.0 17.0 15.9 5: 496 550 554 516 448 489 515 90,600 81,00 79,100 90,900 51,000 8,400 7,00 9,800 1.6 1.6 1.4 1.6 1.4 1.5 1.4 1.4 1~ 17 17 17 16 ] :; 1 1 17.1 15.+ 15.6 15.4 11.6 1 ~.5 11.6 11.6 61 70 55 409 '11 6 79 405 5 ' Btll per hollr per " J.ft. per " F '1 54,00 76,500 68,500 7,600 0.9 l.l 1.1 1.1 19 19 18.1 1.9 0.9 17,9 51 596 5'>9 5v 4,500 4,600 4,700 44,00 1. 1.9 1.8 1.9 16 1 1 1 11.8 19! 19. I g.! 400 8 89 90... Cl (,,;. ' ~
rd effect TABLE. (Continued) 4th effect Factory Run Heat load B. P. R. Apparent Effective Heat load B.P. R. Apparent Effective No. No. 10Btu/ hr. o f T, o F T, o f u* 10' Btu/ hr. OF T, OF T, o f u* 0"> 0">,100.5 0.5 9 9,600.6 1 7.4 19 7,00.4 4 0.6 19 17,700 4. 5 0.7 15,100. 1 5 1.9 1,00 4.0 9 5.0 158 I 49,600.0 16 14.0 5 45,500. 8.1-1 5,00.9 16 1. 1 68 6,700 4.0 4 0.0 195 8,00.9 17 14. 1 70 8,400 4.1 7.9 181 1 49,100. 1 17.8 75 4,700 4.5 5 0.5 176 ' I 46,00.1 0.6 6 1,000.6 6.4 8 41,00. IS.7 57,700.4 9 5.6 19 49,400.0 1 19.0 01 40,700. 1 9 5.9 59 48,00. 16 1.7 5 1 7,400.5 0 6.5 '-< 0 C :;0 4 7,000.0 1 19.0 07 4,500. 8 4.7 J9 Z ;> 8,100.0 J8 16.0 76 8,600.1 1 7.9 (, t" 7,600 1. 9 17 15. 1 9 1 7,500.7 6. 60 0." 4 9,00 1.9 16 14. 1 7 9,400.8 1 8. 0.., :t M 5 6,100 1.8 5. 85 5,800.8 0 7. 41 > 16,50.7 18 15. 70 1,550. 8 18. 186 ~ 18,00. 5 0 17.5 64 15,450.7 19. 0 4 ~ 18,50.7 1 18. 55 14,150.9 19. 1 188 ' Btu per hour per sq.ft. per OF.!=d :-l
VOL. 1, No., J ULY 1964 167 TABLE.-(Continucd) 5 th eflect Factory Run Heat load B. P.R. Appa rent Effe ctive No. No. lo a Hln/ h... OF T, OF T, OF u* I,800 6.6 16.0 9.4 l il8 0,580 6.6 8.0 1.4 106 0,700 6.5 S.0 1.5 15 50, 140 9.1 4S.0 8.9 178.800 9. 46.6 6. 7 17 6,00 9.1 44.0 4.9 1'1.5 4,100 9. 47.0 7.8 117.5 I 5,160 7.6 55.0 47.4 10S.5 7, 150 7.5 5.0 44.5 1 44,S40 7.1 5.0 45.9 14.5 4 41,580 7.7 5.0 44. 17 4 I 8,760 9.5 7.5 64.0 141 1,800 6.7 59.0 5. I IS 0,70 5.1 5 45.9 19 4,980 5.9 5.0 47.1 16 5 I 8,0 7. 49.0 41.7 179 14.700 7. 9.0 1.8 117.5 16,750 7.7 46.0 S. II! 4 15,470 7. 45.0 7.8 10.5. Btu per hour per sq.(t. per 0 F. It also enables the refineries to estimate the vapor temperature and pressure for existing heating surface by rearranging the equation to the following form. Q 6.T A XU From the data obtained 111 this investigation, the following formula is proposed. U 40 (tj - ) (1 - n X 0. 08).... (1) Bx Over-all heat tran.sfer coefficients calculated by the above formula agree with the values obtained from Figure 1. Summary and Conclusions The result of this investigation showed a better correlation between heat transfer coefficients and solids in solution. The curve shown on Figure 1 is applicable to both standard short vertical-tube evaporators and standard horizontal-tube evaporators with tubes in normal cleanliness provided that the tube size and operating conditions are within the following ranges:
168 OJ THE A. S. S. B. T. For vertical-tube 1st effect: L/D - 105.8 t,. = /HoF 55 OF Ju icc hrix out. ]8.~1-0.R Tube material: copper or tubes nd effect: I = 4.6 91.4 (j'f - 7 F brix out: 4.S.1 ube material: copper or steel or hi-metal tuhes rd effect: L./D = 50.4 77 t, ~ 07 of :!I9F 0.1-44. or steel tl1 bes 4th effect: F out:.')r.~) be material: copper tubes 5th effect: L/D = 40.8 Gl tv: 101.5 OF 145 OF brix out: a/l') 70 nbc material: tubes Tube data and for horiwntal-tube evaporator are showll on Table 1 at 5. 1 and Equal (1) mayor may not be applicable to long--tubc since the data were not available and no a was rnade to the overall heat transfer coefilcients [or vertical long--tube (1) or I 'will to a or to estimate the pressure from the exist- Nomenclature l' t transfer coefficient, Btu per hour per,quare f()ot ]Jer 0 Q B.LU. hour. A leet. j.t lcavillg evaporator, ti illld brix c\;jporator. 'F. oc the'cvaporator, 1.,1.. " elc,
VOL. 1, No., JULY 1961 169 Acknowledgments Cooperations from Engineering Department, Operating Department and Research Department of The Amalgamated Sugar Company made this work possible. Mr. S. M. Heiner, Chief Engineering, assisted in the investigation. Literature Cited (1) HONIG, P., "Principles of Sugar Technology." 196. Vol. III, Elsevier Publishing Company, New York. () KERR, Trans. Am. Soc. Mech. Engrs., 8, 67 (1917). () SPENCER, G. L. and G. P. MEADE. 1945. "Cane Sugar Handbook," 8th Edition, John 'Wiley and Sons, Inc., New York.