DEPARTMENT OF CHEMICAL AND METALLURGICAL ENGINEERING Heat Transfer Laboratory The University of Michigan Ann Arbor, Michigan ANNUAL REPORT FOR 1962 Report No. 54 Edwin H. Young Professor of Chemical and Metallurgical Engineering Dale E. Briggs Instructor in Chemical and Metallurgical Engineering Project 1592 WOLVERINE.TUBE Division of CALUMET AND HECLA, INCORPORATED ALLEN PARK, MICHIGAN January 1963

ABSTRACT This report contains a summary of the operations of the research group and the work completed during the year 1962. The status of the work of the project is reviewed and discussed.

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INTRODUCTION 1

The heat transfer project sponsored by Wolverine Tube Division of Calumet and Hecia, Incorporated within the Department of Chemical and Metallurgical Engineering at The University of Michigan is in its twentythird year of operation. During the past year the project employed three men on a part-time basis. Of these, one was an instructor in the Department of Chemical and Metallurgical Engineering and the other two were students in the department. Part-time secretarial help was also employed. The project's laboratory facilities are located in the Fluids Building on the North Campus of The University as indicated in Figure 1. The project director maintains an office in the East Engineering Building where many of the files are kept. During 1962, there were many more prospective investigations listed than could be handled simultaneously or could be completed. The investigations were, therefore, undertaken in accordance with the current priority status set as a result of conferences held with the Director of Research and Development Division of Wolverine Tube. The prospective projects were separated into two categories. One consisted of projects requiring laboratory facilities and the others consisted of projects requiring the use of technical information available in the literature to effect a desired design or analysis of heat transfer data in an effort to abstract information of value to Wolverine Tube. In January 1962, the equipment (laboratory) projects in order of priority were: 1. Study of the heat transfer characteristics of boiling refrigerants and investigation of internal fin configurations on boiling refrigerant heat transfer coefficients. 2. Determination of the optimum fin height and fin spacing for refrigerant condensing. 3. Investigation of the steam condensing characteristics of titanium tubes. 4. Investigation of the steam condensing characteristics of corrugated tubes. 5. Determination of the air film heat transfer and pressure drop correlations for banks of finned tubes using the wind tunnel. 2

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6. Study of the performance of Type S/T tubes in large shell and tube heat exchangers. Liquid and gas cooling. The effect of longitudinal unbaffled flow. 7. Study of natural convection heat transfer from plate fins and finned tubes. Non-laboratory studies in order of priority were: 1. Revision of the Ward-Young air cooling heat transfer correlation to include data obtained on additional banks of tubes. 2. Revision of the Williams-Katz report on the performance of Type S/T tubes in shell and tube heat exchangers. Several small projects of higher priority than those mentioned above were added to the project work list during the year. Work on these additional projects were coordinated with existing projects through conferences held with representatives of Wolverine Tube.

At the beginning of the year, the following personnel were employed on the project on a part-time basis: 1, Dale E. Briggs (one-half time) 2. Ardis R. Vukas (one-quarter time) Mr. Briggs is an Instructor in the Department of Chemical and Metallurgical Engineering and was the acting director of the project until February 3, 1962. The project director, Professor E. H. Young, returned to the project on February 3, 1962, having taken a sabbatical leave from The University of Michigan for the fall semester of the 1961-1962 academic year. On February 12, 1962, Mr. Boris Taruntaev and Mr. William D. Hancock were added to the project staff. Both men are students in the Department of Chemical and Metallurgical Engineering. Mr. Taruntaev is working toward a master's degree and Mr. Hancock is working toward a bachelor's degree. At the end of 1962, the following persons were employed on the project: 1. Dale E. Briggs (one-half time) 2. Ardis R. Vukas (one-half time) 3. Boris Taruntaev (one-half time) 4. William D. Hancock (one-half time) 6

LABORATORY INVESTIGATIONS 7

Wind Tunnel Investigation Air film convective heat transfer data were taken on two tube banks in the wind tunnel during the year. Figure 2 shows a view of the wind tunnel. One tube bank contained four rows of 2 inch O.D monometallic aluminum tubes on a 2-3/16 inch equilateral triangular pitch and the other contained six rows of 3/4 inch O.D. monometallic copper tubes on a 15/16 inch equilateral triangular pitch. The data were analyzed to obtain the air film heat transfer coefficient as a function of the maximum air velocity through the tube bank. Isothermal pressure drop data were taken on seven wind tunnel tube banks. Three banks contained six rows of 2-1/4 inch O.D. Type L/C tubes placed on an equilateral triangular pitch. The tube pitches for those banks were 2.700, 3.375, and 4.500 inches. The remaining four banks contained six rows of 1-1/2 inch O.D. Type L/C tubes (Banks 22, 23, 24 and 25) that were placed on 1.930, 1.687, 2.450, and 3. 375 inch equilateral triangular pitches. These data were analyzed and pressure drop correlations were obtained which presented the effect of tube pitch on pressure drop for the tubes studied. Figure 3 gives the pressure drop in inches of water per row as a function of the maximum air velocity through the tube bank for the 1-1/2 inch O.D. tubes and Figure 4 gives the pressure drop in inches of water as a function of the tube pitch with the maximum air velocity as a parameter. The air film convective heat transfer data on the eighteen wind tunnel tube banks studied to date on the project were processed with the IBM 709 digital computer. Eight of the banks were studied by Dr. D. J. Ward while doing his doctoral thesis prior to 1957, and the other ten banks were studied by project personnel since 1957. The processed data on twelve of the tube banks were analyzed with a regression analysis program on the IBM 709 computer and a generalized convective heat transfer correlation was obtained which can be used to predict air film heat transfer coefficients for various operating conditions and tube geometries. Figure 5 gives the general correlation and shows the agreement with the data. A paper was prepared covering the heat transfer and pressure drop correlations and presented by Dale E. Briggs at the Fifth National Heat Transfer Conference sponsored jointly by the American Society of Mechanical Engineers and the American Institute of Chemical Engineers in Houston, Texas, on August 4, 1962. 8

Figure 2. Overall View of Wind Tunnel with Test Section Insulated. ID 0.8 cLLJQ oBank 22- tube p/tch.. 930 in. o Bar 23 - tube pitch/. 687 n. Boank 23 0.4- a Bonk24-tube p/dc'2.450/n. -- 8nlr22 v 8onA'2u-3s ube opich.a5i fo Bnks 2 Bank 25 0 0.2 9 CL& ao 0.08 W 0.02,), 9i i 0.011 I00 200 400 600 I000 2000 4000 10,000 V MAx OF AIR, FT./MIN. AT pI 0.074 LB./CU. FT.

wi 0250.20 0- 0.15 0 0 \ \ Th~xV/=.2000 ft/mmn:) Z~ E a0074 lb/cu ft V/ 0.10 Vmo /500 ft/m/'n r' 0.05 / Vro/000 ft/m/n Vmox500 ft/mIn 0 I I 0 1.0 20 3.0 40 TUBE PITCH - IN. Figure 4. Comparison of Pressure Drop Data for Banks 22, 23, 24, and 25 at Various Constant Air Velocities. 200 1 T 0 100- _ _ _ NlNu 0/34 Re 7651 Pr 115V02,00i 0 134? ISO60 40 _ 0 BANK 2 B ANK 3 BANK 5 x BANK 1 ~+/ ~-I ~I I BANK I Z3 20 j BANK I I # BANK 15 a BANK 16 ~ BANK 17 o BANK IS 10 L_ I, 1000 2000 4000 6000 8000 10000 20000 40000 DV p Re r max. Figure 5. Comparison of Finned Tube Heat Transfer Data with the Correlation Obtained by a Regression Analysis. 10

Investigation of the Steam Condensing Characteristics of Corrugated Tubes An investigation to predict the steam condensing capabilities of an internally grooved tube and two corrugated tubes was started in January 1962 and completed in February 1962. Sections of the three tubes were photographed and the photographs were used to obtain accurate measurements of inside and outside heat transfer surface areas. Modified tube-side Wilson plot data were taken in the concentric pipe heat exchanger shown in Figure 6 with hot water flowing in the annulus and cold water flowing through the tubes. Using the calculated values of the heat transfer areas, the data were processed with the IBM 709 digital computer and the inside heat transfer coefficient constants obtained for the Sieder and Tate Equation. Figure 7 gives the calculated Wilson plot results for corrugated tube 489. Tube -side pressure drop data were also taken and processed. A comparison of the anticipated low pressure steam condensing capabilities of the three tubes with those of plain tubes was then made, based on the restriction that each tube would have the same tube-side pressure drop. It was found that the calculated steam condensing capabilities for the internal grooved tube was nearly the same as for plain tubes, while the capabilities of the intermediate and the highly corrugated tubes were 8.2 percent and 3.8 percent higher than for plain tubes, respectively. Exclusive of steam condensate flooding considerations, the results indicate that some optimum corrugations per inch and corrugation height exists for the restriction of constant pressure drop. Investigation of the Steam Condensing Characteristics of Titanium Tubes The purpose of this project was to investigate the condensing mode and related characteristics when condensing low pressure steam on nine 5/8 inch O.D. prime surface titanium tubes placed in a vertical row. The design of the equipment was begun in January 1962 and the first construction materials were received in late May. After considering and reviewing several alternate designs, a closed system method was selected as being the most flexible and useful when considering Wolverine Tube's possible future needs for research in the field of condensing on both prime-surface and finned tubes with condensing vapors other than steam. The equipment consists of a cooling water preheater, a 24 inch O.D. by 6 feet long reboiler, an 18 inch O.D. by 6 feet long condenser, and a make-up 11

Figure 6. View of the Concentric Pipe Heat Exchanger Located in Fluids Building. 1.2 Tube 489 -Cold Water Inside Tube Nu =0.04267 Re"s Pr'/" a )0.14 o 1.0 0.68 E 01 0.6 - - I/ m 0.4 z z Ci 0. 04267 LL 0.2 - Intercept = 0. 000382 0 0.05 0.1 015 0.20 0.25 0.30.O.14 Ao FUNCTION A- i ( Ai 10 k, Re0, p r'13 ( ) Figure 7. Modified Wilson Plot for the Inside Heat Transfer Coefficient of a Corrugated Tube - Tube 489. 12

tank. Cooling water will be heated to the desired temperature in a preheater and will pass through the tubes under study. Steam will be generated inside a reboiler by condensing steam inside horizontal S/T type tubes. The steam will then pass through an 8 inch pipe to the overhead condenser where it will be condensed on the outside of the horizontal titanium tubes. The condensate will return to the reboiler by a condensate return line. A steam jet ejector will be used to remove non-condensibles and a make-up tank will be used as necessary to maintain a sufficient water level in the reboiler. Measuremne2nts of the inlet and outlet water temperature and the water flow rate in each tube will permit the determination of the amount of heat transferred by each tube. Wilson plot techniques will be used to evaluate the inside heat transfer coefficient and the condensing coefficients will be obtained by difference from the overall heat transfer coefficient. The fabrication of the laboratory experimental equipment was nearing completion at the end of the year. 13

THEORETICAL AND NON- LABORATORY INVESTIGATIONS 14

Heat Transfer from Plate Fin Units A mathematical investigation was begun in January 1962 to determine a satisfactory fin spacing, fin thickness, and fin height for plate fin units used in refrigeration systems utilizing thermoelectric cooling. Heat was to be removed from the refrigerated system by natural convection to plate fins on the cold side and heat was to be transferred from the plate fins on the hot side to the ambient air by forced convection. The heat transfer correlations required in this investigation were obtained from the literature. A conference was held with personnel from Wolverine Tube to discuss the significance of the findings upon completion of the investigation in February 1962. Revision of Report on Performance of Finned Tubes in Shell and Tube Heat Exchangers A re-correlation of the heat transfer and pressure drop data in a University of Michigan Engineering Research Institute Report entitled, "Performance of Finned Tubes in Shell and Tube Heat Exchangers," by R. B. Williams and D. L. Katz (1951) was begun in September 1962. After writing an IBM 7090 computer program to obtain the inside heat transfer coefficient constant for the Sieder and Tate equation from Wilson plot data, all the original data were processed and the constants obtained. Table I shows the tabulated computer output results for bundle.1, runs ZA - 2D. The original correlation was prepared by hand calculations. A computer program has been written to analyze all the heat transfer and pressure drop data. The calculated values of the inside heat transfer coefficient constants will be used in the computer program. The analysis will include the devetopment of shell-side heat transfer coefficient and pres-s sure drop correlations by both the Donohue and Bell methods. Comparisons of the correlations for the finned tube bundles with the correlations for the plain tube bundles will be made to obtain the relative performance of finned tube bundles to plain tube bundles over a wide range of Reynolds numbers. Table II shows representative computer output results for plain tube bundle No. 1. 15

Table I. Modified Wilson Plot Data and Results Calculated by an IBM 7090 Digital Computer for the Inside Heat Transfer Coefficient for Bundle 1. WILSCN PLOT DETERMINATION CF THE INSIDE HEAT-TRANSFER COEFFICIENT FOR BUNDLE I, NUMBER OF RUNS IS 4 SHELL SIDE FLUID IS WATER TUBE SIDE FLUIC IS WATER RUNS BUND TEMP ITER XAO XAI XAM RM CI 4 1 0 4 38.25CC 32.9500 35.5800.625CE-04.240GE-01 NO K L M NN 0 P Q 1.1C124896E 01 -.46678C63E-03.5854C867E-05 -.32721741E-07.72640616E-10 -.00OCOCOE OE -.COOGC OOOE 00 2.10124896E 01 -.46678C63F-03.58540867E-05 -.32721741E-07.72640616E-10 -.0000000CE 00 -.OCOCOGE 00 3.30377927E 00.25267360E-03.9205C520E-05 -.75847219E-07.17507457E-09 -.C0OCOOCGOE 0 -.GOCOOOO1E 00 4.30377927E CC.25267360E-03.9205C0520E-05 -.75847219E-07.17507457E-09 -.00C000OE 00 -.C00C00OOE 00 5 -.COCCOOOCE CC -.0000COOCE OC -.0,00C0000E 00 -.OOOOC000OE 00 -.000000OE 00 -.00COCOCCE 30 -. 000CC0000E 00 6 -.21968737E 01.54722744E 03 -.41363282E 05.16141324E 07 -.24764542E 08 -.00COOOOOE 00 -.OOO000E CO 7 -.21968737E 01.54722744E 03 -.41363282E 05.16141324E 07 -.24764542E 08 -.000000aGE 00 -.0COCOCOE O) 8 -.OOCOOCCCE CC -.OOOOCCCCE 00 -.OCOOCOOQE 00 -.00000000E 00 -.O 0000000E 00 -.00GO0OOGE 00 -.00000000E 00 DIAS AFS AFT DIAT.6250CE-01.508CCE-C1.568C0E-C1.53800E-01 NCTE - INPUT TEMPERATLRES ARE IN FAHR. RUN TSIF TSOF TTIF TTOF W SHELL W TUBE Q SHELL Q TUBE LMID F 2A 177.6C00 165.51C 148.750 157.680 35343 46530 428321 415818 18.245.944 28 177.690 165.560 152.460 158.860 35491 65043 431547 416653 15.792.94 2C 177.3C0 165.110 153.7C00 158.850 35739 83340 436696 429610 14.649.949 20 177.290 164.980 155.050 159.330 35780 103455 441491 443243 13.551.9)4 RUN C AVC PER DEV LMTCC UO RE SHELL RE TUBE PR SHELL PR TUBE 2A 422C72 -1.482 17.263 639.204 49C95 43348 2.296 2.662 28 42410C -1.756 14.93C 742.659 49326 61772 2.294 2.607 2C 43315C -.817 13.8S5 814.964 49522 79530 2.302 2.594 2C 442366.198 12.863 899.101 49554 99429 2.303 2.574

Table I. (continued) AFTER 4 ITERATIONS, INTERCEPT IS.56427354E-03, CI IS.02440117 RUN FUNCTICN A FUNCTION B 2A.22584083E-04.14861342E-02 28.17147771E-04 12697446E-02 2C.1404377CE-04.11508752E-02 2C.11782061E-04.10370004E-C2 RUN TSAV TWALL 0 TWALL I TTAV 2A 171.555 - -16-4.246 —— 163.5c4- 1-53 215 2B 171.625 164.255 163.510 155.660 2C 171.205 163.604 162.843 156.275 20 171.135 163.594 162.817 157.190 -,,i RUN FI PRIME RFIN IN HI HO PRIME RFIN OUT HO NU SHELL NU IUBE RE SHELL NU/PR-VISC 2A 1244.935.000OE 00 1244.935 1770.549 -.OOOOE 00 1770.549 286.139 175.215 49C95 218.536 28 1639.515.000OE 00 1639.515 1.i-750.462 -.OOOOE 00 1750.462 282.880 230.384 49326 216.G98 2C 2001.366.C00CE CO0 2001.366 1724.647 -.0000E 00 1724.647 278.784 281.120 49522 212,796 20 2385.695.COOCE 00 2385.695 179-0.690 -.0000E 00 1790.690 289.472 334.908...49554 22C.902 VISCOSITIES LB/FT-HR RUN VISC. SHELL VISC SH WALL VISS/VISSW VISC. TUBE VISC TU WALL VIST/VISTW 2A.8857.9341.9481 1.0167.9385 — 1.0833 28.8852.9341.9477.9973.9388 1.0624 2C.8879 -,9386.9460.9926. 46- 1.0519 2C.8883.9387.9464.9855.9439 1.0441 WILSCN PLOT CONSTANT EQUALS.02440117, INTERCEPT ECUALS.56427354E-03

Table II. Representative Shell-side Heat Transfer Coefficient and Pressure Drop Friction Factor Results Calculated with an IBM 7090 Digital Computer for Bundle 1. HEAT tRANSFER AND PRESSURE CROP ANALYSIS OF THE WILLIAMS - KATZ DATA uUNCLE 1 NO. RUNS 4 SHELL-SIDE FLUID WATER IUBE-SIDE FLUID WATER TEMPERATURES FAHRENHEIT IUeE Il - IN.6460 IUBE OC - IN.7510 lUBE RU - IN. 7510 lUBE DEQ - IN.7510 1UBE PITCP - IN.9400 SHELL MEAN FLOW AREA (DONOHUE) - SQDFT.05150 SHELL MEAN FLOW AREA (bELL) - SQFT.0655 WINDOW AREA - SQFT.04160 AFLOW C/L MIDDLE - SLFT.05140 AFLOW C/L ENOS - S(FT.09570 AFLOW TUBE - SCFT.05680 TUBE OUTSIDE AREA - SI(FT 38.250 TUBE INSIDE AREA - SUFT 32.920 TUBE METAL AREA - SUFT 35.580 NO. BAFFLES 9 eAFFLE SPACING MICOLE - IN 3.9300 BAFFLE SPACING END - IN 7.3200 NO. RESTRICTIOf\S FROM CENT. TC CENT. 3.1100 NO. RESTRICTIONS FROM CENT. TC SHELL.8900 NO. RESTRICTIONS (BELL) 2.420 NO. RESTRICTIONS IN WINDOW 1.580 INSIDE COEFFICIENT CONSTANT.02440 WINDOW VOL. EQ. DIA. - FT.1132 HL/HNL.8281 DPL/CPNL.6580 PHI 1.0630 CHI LAMINAR FLCW 1.3380 CHI TURBULENT FLOW.9150 XI PRESSURE DRCP LAMINAR.2620 AI PRESSURE DRCP TURbLLENT.322C XI HEAT TRANSFER.6890 METAL RESISTANCE hALL/K.0000625 NO K L M NN 0 P; 1.1- 124896E 01 -.46678063E-03.58540867E-05 -.32721741E-07.72640616E-1C -.0000000C'E 00 -.00000O'E CO 2.1S124896E 01 -.46678C63E-C3.58540867E-05 -.32721741E-07.72640616E-10 -.CCCCOOU E CC -,000 00%Lt CO 3.33377927E CC.2526736CE-C3.9205C520E-05 -.75847219E-07.17507457E-9 -CGOCOCOCCE O0 -., )000000;'DE;0 4,30377927E O0.25267360E-03.92050520E-05 -.75847219E-07.17507457E-09 -.COUC0C0OE 0J -.OOOC'OOOE CO 5 -.O OOCC~E 0C -.OlC3OCCCE 00 -- CC0 O OD-OOE D -.fCO OCOOOE 30 - OCGI0OOE QO EC 00000EUCOOOOE 20 -.-OC.0000E C0 6 -.21968737E C1.54722744F 03 -.41363282E 05.16141324E 07 -.24764542E 08 -.CCOCCOCOE 30 -.0000000C13 GC 7 -.21968737E 01.54722744E 03 -.41363282E 05.16141324E 07 -.24764542E 08 -.00COOOOE CO' -.GOOOOOOOE 0I 8.63129934F C2 -.117-00 5 CE-0 l -.OO)OUOOOOE 00 -.OG3OOOCE 00 -.,CODOO0U0E CC -.GOCOU6C0UE C0 -.OCOU000E CO

Table II. (continued) RUN TTI TTC W TUbE TSI TSO W SHELL PRESSURE DROP F F LB/HR F F LB/HR PSI 2A 148.750 157.680 46530 177.600 165.510 35343 3.150 4A 149.200 159.220 461CC 177.51C 167.970 49100 5.810 5A 148.860 159.640 45800 177.160 168.850 60600 8.850 6A 149.290 156.700 461;0 177.080 162.880 25000 1.540 RUN Q SHELL C TLE Q AVG PER ]EV LMTD F LMTDC UCO RE TUBE BTU/HR HTU/HR BTU/HR F F H/H-SF-F 2A 428327 415818 422072 -1;482 18.295.944 17.263 639.204 43375 4A 469611 462293 465952 -.785 18.529.952 17.635 690.786 43313 5A 504889 494122 499506 -1.078 18.728.956 17.901 729.522 43045 6A 355790 341847 348819 -1.999 16.756.933 15.641 583.029 42899 RUN TSAV T WALL 0 iT ALL I TTAV PR TUB8 NU TUBE HI DE SHELL PR SHELL HO RFIN HO PRIME F F F F B/H-SF-F LB/CUFT B/H-SF-F H-SF-F/B B/H-SF-F 2A 171.555 164.256 163.515 153.215 2.662 175.303 1244.786 61.123 2.296 1773.568 -. 30000 1773.568 4A 172.740 166.424 165.606 154.210 2.639 174.803 1242.044 61.109 2.275 2247.412 -.00000 2247.412 5A 173.005 167.395 166.517 154.250 2.638 174.076 1236.912 61.106 2.270 2745.669 -.00OO00 2745.669 6A 169.980 162.207 161.594 152.995 2.667 173.557 1232.210 61.141 2.324 1418.350 -.000000 1418.350 VISCCSITIES LB/FT-HR RUN VISC. SHELL VISC SH WALL VISS/VISSW VISC. TUBE VISC TU WALL VIST/VISTI 2A.8857.9341.9482 1.0167.9384 1.0834 4A.8783.9192.9555 1.0087.9238 1.0920 5A.8766.9127.9605 1.0084.9175 1.991 6A.8957.9485.9444 1.0185.9523 1.U695

Table II. (continued) HEAT TRANSFER REStLTS BASED ON THE METHOD OF DONOHUE RUN RE SHELL NU SHELL NU/PR-VISC FUNCTION C FUNCTION D FUNCTI-ON E LN RE SH LN PR SH LN VIS RAT LN NU S 2A 48492.6 287.0C9 219.192 219.192120 5.389948 10.789166 10.789166.831C35 -.053171 5.65i513 4A 67937.8 363.409 278.082 278.082031 5.627916 11.126348 11.126348.821986 -.045567 5.895529 5/A 84007.4 443.901 339.654 339.654160 5.827928 11.338660 11.338660.819970 -.04,334 6.C9561 1 6A 33916.5 229.758 174.861 174.860924 5.163991 10.431656 10.431656.843149 -.057222 5.43(J27 i'RqESSURE CROP RESULTS BASED CN THE METHOD OF DONOHUE;~UN DP SHELL VEL WINDOW OP WINDOW OP CROSSFLOW RE CL ENDS RE CL CENTER FRICTION FACTOR BASED PSI FT/SEC PSI PSI ON RE CL CENTER 2A 3.150 3.861 1.804 1.346 26095.8 48586.9.189258 4A 5.810 5.365 3.483 2.327 36560.1 68070.0. 16977 5A 8.850 6.622 5.306 3.544 45207.7 84170.8.169195 6A 1.540 2.73C.902.638 18251.8 33982.5.179141 0 HEAT TRANSFER RESULTS BASED ON THE METHOD OF BELL RUN HOP LEAK HOP NO LEAK RE C/L J IDEAL NU IDEAL LN RE LN PR LN VIS-RAT LN NU B/H-SF-F P,/H-SF-F 2A 1773.568 2141.732 38127.8.008545 432.993 10.548697.831C35 -.053171 6.070723 4A 2247.412 2713.937 53416.8.007754 548.254 10.885880.821986 -.C45567 6.306738 5A 2745.669 3315.6 2 5 66051.6.007671 669.687 11.98191.819970 -. 4,;334 6.506811 6A 1413.35C 1712.776 26667.2.009735 346.622 10.191188.843149 -. 57222 5.848236 PRESSURE DROP RESULTS BASE GON THE METHOD CF BELL RUN DP LEAK DP NO LEAK VZ ENDS VZ CENTER DP WINIDOW D)P C-F RE EN)S R CENTER FRICTION-F PSI PSI FT/SEC FT/SEC PSI PSI 2A 3.150 4.787 2.546 3.474 1.895 2.893 26095.8 48586.9 1.580619 4A 5.810 8,83C 3.537 4.827 3.657 5.172 36560.1 6800C.0 1.465657 5A 8.850 13.450 4.35. 5.957 5.512 7.87, 45201. 84175.8 1.466517 6A 1.540 2. 34 1.80C 2.456.948 1.3q3 18251.8 33982.5 1.523611

OTHER ACTIVITIES 21

Many special projects were performed for Wolverine Tube during the past year. One of these projects was the processing,with the IBM 709 computer at The University of Michigan, of the Wilson plot data taken on Wolverine Tube's concentric pipe heat exchanger. Project personnel also served in an advisory capacity for the Wolverine Tube Research and Development Division's concentric pipe heat exchanger program. Project personnel further assisted Wolverine Tube in the areas of plate fin heat transfer, base board heaters, and similar projects. During the year project personnel reviewed heat transfer literature and the heat transfer papers presented at technical meetings. Information pertinent to the project's present or anticipated future needs were placed in the project's files. Similar information of importance to Wolverine Tube's Research and Development work was forwarded to Wolverine Tube. A close liaison was maintained by Professor E. H. Young between the research project and the Bureau of Ships, Navy Department, Washington, D. C. and the U. S. Naval Engineering Experiment Station, Annapolis, Maryland. Professor Young participated in conferences at the Boiler and Heat Exchanger Branch of the Bureau of Ships with Mr. D. F. Grimm of Wolverine Tube on May 21, 1962, and with Mr. E. F. Hill of Wolverine Tube on September 26, 1962. Professor Young and Mr. Hill also participated in conferences with representatives of the U. S. Naval Engineering Experiment Station at Annapolis, Maryland. Professor E. H. Young and other members of the research group participated in a total of 30 meetings with representatives of Wolverine Tube for the purpose of reporting results and planning future project activities. Additional conferences were held with representatives of several other companies concerning project activities, Wolverine Tube activities or project experience in certain areas. Professor Young participated in conferences at the PattersonKelly Company, East Stroudsburg, Pennsylvania, on February 13, 1962, and at the York Division of Borg-Warner Corporation, York, Pennsylvania on February 14, 196Z, with Mr. D. F. Grimm of Wolverine Tube and Mr. R. Egan of Unifin Tube. On June 18, 1962, Professor Young attended a meeting on refrigerant condensing at the American-Standard Industrial Division in Detroit, Michigan, with several representatives of Wolverine Tube. On June 19, 1962, Professor Young met with Mr. R. L. Eichhorn of Whirlpool Corporation at St. Joseph, Michigan, to discuss their current work in thermoelectric refrigeration. Professor Young and Mr. D. M. Mellen of Wolverine Tube attended meetings on refrigerant condensing at the York Division of Borg-Warner Corporation on June 28, 1962. On July 10, 1962, Professor Young, Mr. D. F. Grimm 22

and Mr. D. M. Mellen participated in conferences at the Trane Company, LaCrosse, Wisconsin. Professor Young and Mr. D. F. Grimm and Mr. A. L. Kaspark of Wolverine Tube held a conference on boiling refrigerants with Mr. Abdelmessih and Mr. M. W. Timby of the United States Air Conditioning Corp. in Delaware, Ohio, on July 17, 1962. On October 5, 1962, Professor Young and Mr. J. G. Lavin participated in boiling heat transfer conferences with Professor W. E. Fontaine, Professor J. B. Chaddock, and Mr. R. C. Johnston, Jr., of the Ray W. Herrick Laboratories at Purdue University, Lafayette, Indiana. Professor E. H. Young and Mr. D. E. Briggs participated in heat transfer conferences at The University of Michigan with Mr. A. H. Abdelmessih and Mr. Wayne Timby of the United States Air Conditioning Corp. of Delaware, Ohio, and Mr. J. Roehmof Wolverine Tube, Columbus, Ohio, on November 26, 1962. Mr. D. E Briggs attended a conference at Wolverine Tube on December 7, 1962, with Messrs E. F. Hill, R. C. Cash, R. E. Seaton, and H. F. Powell of Wolverine Tube and Mr. J. J. Taborek of Phillips Petroleum. On December 8, 1962, Professor E. H. Young and Mr. D. E. Briggs held a conference at The University of Michigan with Mr. R. C. Cash and Mr. H. F. Powell of Wolverine Tube and Mr. J. J. Taborek of Phillips Petroleum. Project personnel attended important heat transfer conferences, Professor Young attended the Symposium on Evaporation at the A.I.Ch.E. National Meeting in Baltimore, Maryland, on May 21, 1962. Professor E. H, Young and Mr. D. E. Briggs attended the Fifth National Heat Transfer Conference sponsored by the American Institute of Chemical Engineers and the American Society of Mechanical Engineers at Houston, Texas, August 5-8, 1962. Professor Young and Mr. Briggs presented a paper entitled "Convection Heat Transfer and Pressure Drop of Air Flowing Across Banks of Finned Tubes" at the meeting. Professor Young attended heat transfer symposia at the Annual Meeting of the American Institute of Chemical Engineers, Chicago, Illinois, December 2-6, 1962, While at the meeting, Professor Young participated in a meeting of the Executive Committee of the Heat Transfer Division of the American Institute of Chemical Engineers. Professor Young has been elected to a three-year term as a member of the Executive Committee starting January 1, 1963. Effective January 1, 1963, the name of the Heat Transfer Division will become the "Energy Conversion and Transport Division" of the American Institute of Chemical Engineers. During the year Professor Young continued to remain active on the ASME Atmospheric Cooling Equipment Code Committee. 23

The research project received many requests for copies of the reports and technical papers which have been published as a result of the research program. The requests were fulfilled whenever possible. 24

CURRENT STATUS 25

The current priority list established by Wolverine Tube divided the project activities into two categories. One consisted of projects requiring laboratory facilities and the other consisted of non-laboratory investigations. At the end of 1962, the current priority list of projects was: Equipment (laboratory) projects in order of priority 1. Investigation of the steam condensing characteristics of titanium tube s. Non-laboratory projects in order of priority 1. Revision of the Williams-Katz report on the performance of Type S/T tubes in shell and tube heat exchangers. 2. Completion of a final report on the bond resistance of Type L/C finned tubes at elevated temperature s. 26

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