Question

Design Project 8.1 Oil Cooler for Marine Application

The following specifications are given :

A shell-and-tube heat exchanger type with geometric parameters can be selected. The heat exchanger must be designed and rated. Different configurations of shell-and-tube types can be tested. Parametric study is expected to come up with a suitable final design; mechanical design will be performed and the cost will be estimated. Follow the chart given in Figure 8.10.

Please use NTU method...

Design Project 8.1 Oil Cooler for Marine Applications The following specifications given: are Fluid SAE-30 Oil Sea Water Inlet temperature, °C Outlet temperature, "C Pressure drop limit, kPa Total mass flow rate, kg/s 65 20 56 32 140 40 20 A shell-and-tube heat exchanger type with geometric parameters can be selected. The heat exchanger must be designed and rated. Different configurations of shell-and-tube types can be tested. Parametric study is expected to come up with a suitable final desigrn; mechanical design will be performed and the cost will be estimated. Follow the chart given in Figure 8.10 Problem Identification The Elements Within this Вох Маy Be CDone By Hand or Computer Selection of a Basic Heat Exchanger Type Selection ofa Tentative Set of Exchanger Design Parameters Modification of the Design Parameters Rating of the Design: Thermal Performance Pressure Drops Evaluation of the Design: Q, ДР Ассерtable? Unacceptable Acceptable Mechanical Design, Costing, Etc FIGURE 8.10 Basic logic structure for process heat exchanger design. (Drawn after Bell, K. J. [1981] Heat Exchangers Thermal-Hydraulic Fundamentals and Design, Taylor & Francis, Washington, D.C.) TABLE 8.2 Heat Exchanger and Condenser Tube Data Cross-Sectional Area Surface Area Schedule Nominal Wall I.D Pipe Size (in) Number or Thickness Inside O.D. Outside Metal Area (in.2) Flow Area Weight (in.) (in.) (in.) (ft/ft) (ft/ft) (in.2) 40 0.113 0.824 0.275 0.216 0.333 0.533 3/4 1.05 80 0.154 0.275 0.742 0.194 0.434 0.432 40 0.133 1.049 0.344 0.275 0.494 0.864 1 1.315 80 0.179 0.957 0.250 0.344 0.639 0.719 40 0.140 1.38 0.434 0.361 0.668 1496 11/4 1.660 80 0.191 1.278 0.434 0.334 0.881 1.283 40 0.145 1.61 0.497 0.421 0.799 2.036 11/2 1.900 80 0.200 1.50 0.497 0.393 1.068 1.767 40 2.067 0.154 0.622 0.541 1.074 3.356 2 2.375 80 0.218 1.939 0.622 0.508 1.477 2.953 40 0.203 2.469 0.753 0.646 1.704 4.79 21 /2 2.875 80 0.276 2.323 0.753 0.608 2.254 4.24 40 0.216 3.068 2.228 0.916 0.803 7.30 3.5 80 0.300 2.900 0.916 0.759 3.106 6.60 0.226 40 3.548 1.047 0.929 2.680 9.89 3 1/2 4.0 80 0.318 3.364 1.047 0.881 3.678 8.89 40 0.237 4.026 1.178 1.054 3.17 12.73 4 0.337 4.5 80 3.826 1.002 1.178 4.41 11.50 10 S 0.134 5.295 1.456 1.386 2.29 22.02 5 5.563 40 0.258 5.047 1.456 1.321 4,30 20.01 0.375 80 4.813 1.456 1.260 6.11 18.19 10 S 0.134 6.357 1.734 1.664 2.73 31.7 6 6.625 40 0.280 6.065 1.734 1.588 5.58 28.9 80 0.432 0.148 5.761 1.734 1.508 8.40 26.1 10 S 8.329 2.180 2.258 3.94 54.5 51.2 8 8.625 0.277 30 8.071 2.258 2.113 7.26 80 0.500 7.625 2.258 1.996 12.76 45.7 10 S 0.165 10.420 2.81 2.73 5.49 85.3 10 10.75 30 0.279 10.192 2.81 2.67 9.18 81.6 Extra heavy 0.500 9.750 2.81 2.55 16.10 74.7 10 S 0.180 12.390 3.34 3.24 7.11 120.6 12.75 30 0.330 12.09 3.17 3.34 12.88 114.8 Extra heavy 0.500 11.75 3.34 3.08 19.24 108.4 10 0.250 13.5 3.67 3.53 10.80 143.1 Standard 14 14.0 0.375 13.25 3.67 3.47 16.05 137.9 Extra heavy 0.500 13.00 3.67 3.40 21.21 132.7 10 0.250 15.50 4.19 4.06 12.37 188.7 16 16.0 Standard 0.375 15.25 4.19 3.99 18.41 182.7 Extra heavy 0.500 15.00 4.19 3.93 24.35 176.7 10 S 0.188 17.624 4.71 4.61 10.52 243.9 18 18.0 Standard 0.375 17.25 4.52 4.71 20.76 233.7 Extra heavy 0.500 17.00 4.45 27.49 4.71 227.0 Note: Courtesy of Tubular Exchanger Manufacturers Association. TABLE 8.2 Heat Exchanger and Condenser Tube Data Cross-Sectional Area Surface Area Schedule Nominal Wall I.D Pipe Size (in) Number or Thickness Inside O.D. Outside Metal Area (in.2) Flow Area Weight (in.) (in.) (in.) (ft/ft) (ft/ft) (in.2) 40 0.113 0.824 0.275 0.216 0.333 0.533 3/4 1.05 80 0.154 0.275 0.742 0.194 0.434 0.432 40 0.133 1.049 0.344 0.275 0.494 0.864 1 1.315 80 0.179 0.957 0.250 0.344 0.639 0.719 40 0.140 1.38 0.434 0.361 0.668 1496 11/4 1.660 80 0.191 1.278 0.434 0.334 0.881 1.283 40 0.145 1.61 0.497 0.421 0.799 2.036 11/2 1.900 80 0.200 1.50 0.497 0.393 1.068 1.767 40 2.067 0.154 0.622 0.541 1.074 3.356 2 2.375 80 0.218 1.939 0.622 0.508 1.477 2.953 40 0.203 2.469 0.753 0.646 1.704 4.79 21 /2 2.875 80 0.276 2.323 0.753 0.608 2.254 4.24 40 0.216 3.068 2.228 0.916 0.803 7.30 3.5 80 0.300 2.900 0.916 0.759 3.106 6.60 0.226 40 3.548 1.047 0.929 2.680 9.89 3 1/2 4.0 80 0.318 3.364 1.047 0.881 3.678 8.89 40 0.237 4.026 1.178 1.054 3.17 12.73 4 0.337 4.5 80 3.826 1.002 1.178 4.41 11.50 10 S 0.134 5.295 1.456 1.386 2.29 22.02 5 5.563 40 0.258 5.047 1.456 1.321 4,30 20.01 0.375 80 4.813 1.456 1.260 6.11 18.19 10 S 0.134 6.357 1.734 1.664 2.73 31.7 6 6.625 40 0.280 6.065 1.734 1.588 5.58 28.9 80 0.432 0.148 5.761 1.734 1.508 8.40 26.1 10 S 8.329 2.180 2.258 3.94 54.5 51.2 8 8.625 0.277 30 8.071 2.258 2.113 7.26 80 0.500 7.625 2.258 1.996 12.76 45.7 10 S 0.165 10.420 2.81 2.73 5.49 85.3 10 10.75 30 0.279 10.192 2.81 2.67 9.18 81.6 Extra heavy 0.500 9.750 2.81 2.55 16.10 74.7 10 S 0.180 12.390 3.34 3.24 7.11 120.6 12.75 30 0.330 12.09 3.17 3.34 12.88 114.8 Extra heavy 0.500 11.75 3.34 3.08 19.24 108.4 10 0.250 13.5 3.67 3.53 10.80 143.1 Standard 14 14.0 0.375 13.25 3.67 3.47 16.05 137.9 Extra heavy 0.500 13.00 3.67 3.40 21.21 132.7 10 0.250 15.50 4.19 4.06 12.37 188.7 16 16.0 Standard 0.375 15.25 4.19 3.99 18.41 182.7 Extra heavy 0.500 15.00 4.19 3.93 24.35 176.7 10 S 0.188 17.624 4.71 4.61 10.52 243.9 18 18.0 Standard 0.375 17.25 4.52 4.71 20.76 233.7 Extra heavy 0.500 17.00 4.45 27.49 4.71 227.0 Note: Courtesy of Tubular Exchanger Manufacturers Association.

Answer 1

FAGE CATE Acte ad heat transecate Inan mar 14 Aelerainel b epression NTU i NTO= Coip value locoer Where Gi1dicales amongst to Ga calle ((he Cmin ratic apacity offge avaible r deterniniog chats be bascdupo hichachal truosler are eness be evaluated tate heat CaD +la

dayen Meatiheness keat G2 Sactval mar Cmi (T-Tet) tem p dieres ce TheTe Th-Tei CPTThe Caio ET-T oinisact Tce-T OcCe CTTe Th Tei cCPe for Cmin pa 163-1re p16 cates oo chaut Ve chant fesallel eap C-NTO -) NTOC1-0 Countes loco eap

FAGE CATE Tet, let HOoc.(Tor) : H Tr, tolet 100w/ Calculafe 1000 KJ 222a Cre meEGAloo 6600 1/a 2 32-0 ComiD A 400 Bmar :リ760Kll 1000 COIL 09t >Thi- The fni Tei Ti-The Th Tet The Thi-E(h 0'568- 800 200 -h00

RC 000 YIO : HOO Tco sc SS1 1- erp C-N-0 CeupN 0 400 0.66 Cmin C 2 Croase exp-NC-066 apCo(-0-66 C$68 1-Y 0.S68 E = +-066 Y0 0625 Y0432 E-Ecy1-y R-Aa1-3a t -00y GOMN E-1) ap C Co 3)) 25 1 O.G9 Ec- 226 NT10S TACO NTU UA
Whenever Heat Exchanger has only two known temperatures the LMTD canot be used for analysis,in such cases we use NTU method. Here we make use of Effectiveness and NTU (no. of Thermal units). Please follow images for more details and example to find area of Heat exchanger with NTU method is given.