Shell and Tube HX for 4 TRShell and Tube Heat Exchanger Design SpreadsheetProject:EvaporatorProject No.:-Item No.:-Service:Cooling of 23% sodium chloride solutionBy:MASDate/Time:19-Sep-119:40BWG/Tube Wall Thicknesses80.165Step 1. Input flows, conditions and properties data for shellside and tubesideStep 3. Start configuring the exchanger. Begin with the assumed overall heat transfer coefficient to this point:90.1480.017100.1340.014TubeSideShellUstart =1000.00W/m C110.1200.014R-404Fluid NameSodium ChlorideThen the required transfer A =41.714m2120.1090.0111.132Flow (M), Kg/s33.2Number of tubes required =531130.0950.014-13Temp. in, C-9No. of passes =4140.0830.012-13Temp. out, C-10Tubes per pass =134132.85150.0720.011Av. Density903r, Kg/m31050Area of tubes per pass =0.00900m160.0650.007Av. Viscosity0.158m, mNs/m22.300Volumetric flow =0.001254m/sAv. Heat Capacity1.250cp, kJ/kgC4.36Av. Velocity =0.139284m/sHeat Exchanged145Q, kW145Av. Thermal Conductivity0.0376k, W/mC0.5800Fouling Resistance0.0004R,m C/W0.0004Step 6. Shell side heat transfer coefficientTube Pitch =0.015625mPattern =Tri.LMTD3.5CBaffle Spacing =0.237mCorrected LMTD3.5CArea of Shell =0.020363mEquivalent Diameter, de =0.008876mVolumetric flowrate =0.031660m/sStep 2. Input tubing OD, BWG andTube OD0.0125mShellside velocity =1.55m/slength (can be trial and error).BWG16Shellside Reynolds No., NRe =6,300Tube ID, d =0.00925mPrandtl No. =17Tube Length, L =2mSegmental baffle cut 25% page number 673 jh =0.0070Area of one tube =0.079mNusselt number =114Cross sectional area of tube =0.00007mho =7,444W/m CR1 =0.00013For 2 t.pFor 4 t.pFor 6 t.pR2 =0.00040For 2 tube passesk10.2490.1750.0743page number 649Step. 4 Bundle and Shell diameterpage number 648Bundle diameter =0.417758mR3 =0.000042n12.2072.2852.499page number 649Shell diameter =0.430258mR4 =0.0087Clearance0.0125page number 646Step. 5 Tube side heat transfer coefficientTubeside Reynolds No., NRe =7382Overall heat transfer coefficient =107.9W/m CPrandtl No. =5.24Length / ID =216page number 665j h0.0032Nusselt number =40.80hi =165.86W/m CThe values in this block will keep on changing

Sheet3Shell and Tube Heat Exchanger Design SpreadsheetProject:EvaporatorProject No.:-Item No.:-Service:Water coolerBy:MASDate/Time:19-Sep-119:40BWG/Tube Wall Thicknesses80.165Step 1. Input flows, conditions and properties data for shellside and tubesideStep 5. Start configuring the exchanger. Begin with the total calculated transfer coefficient to this point:90.1480.017100.1340.014TubeSideShellUstart =10Btu/hft2oF110.1200.014R-22Fluid NameWaterOver all heat transfer Coefficient, Uo =9.7Btu/hft2oF120.1090.011168.5Flow (M), lb/h11,014.1Then the required transfer A =63ft2130.0950.0145Temp. in, oF86Number of tubes required =239140.0830.0125Temp. out, oF82Reset tubes/pass (Step 3), then no. of passes =2150.0720.011Av. Density0.8053r, lb/ft362.42Total tube count =132160.0650.007Av. Viscosity0.011m, cP1.903Tubeside DP (incl. returns) =5.802psiAv. Heat Capacity0.163cp, Btu/lboF1.003Actual effective transfer area, A =35ft2MTD Correction FactorsHeat Exchanged48,000Q, Btu/h44,188Av. Thermal Conductivity0.0049k, Btu/hftoF0.3351R = ( T1 - T2 ) / ( t2 - t1 ) =0.000Fouling Resistance0.0040R, ft2hoF/Btu0.004Step 4. Select tube arrangementTube Pitch0.65in.Prandtl No.0.87cpm/k13.78and estimate shell diameterPatternTri.S = ( t2 - t1 ) / ( T1 - t1 ) =0.000Corrected MTD79.0oFShell ID from Tube Count Tables8in.Corrected MTD79.0oFSelect Baffle Spacing5in.( R2 + 1 ) =0.000Number of Baffles =43.80Flow Area across Bundle, as =0.064ft2( 1 - S ) / ( 1 - RS ) =0.000Step 2. Input tubing OD, BWG andTube OD0.5000in.Equivalent Diameter, de (see table) =7.5in.length (can be trial and error).BWG16Mass Velocity, Gs =171,820lb/hft22 - S ( R + 1 - ( R2 + 1 ) ) =0.000Tube ID, d =0.370in.Shellside Reynolds No., NRe =56,431Tube Length, L =2ft.Shellside Friction Factor =0.001532 - S ( R + 1 + ( R2 + 1 ) ) =0.000Flow area per tube, at =0.108in.2Shellside DP =0.357psiEffective transfer area per tube =0.262ft2Outside Transfer Factor, jh =139.7FT =0.000Outside Film Coefficient, ho =179Calculated Uo =9.7Step 3. Estimate the number ofTubes/pass =66Check: % difference, Ucalc. vs Uassum. =0.0%tubes per tube pass.lb/h per tube =3Uclean =10.5lb/h per tube per pass =1.3Av. velocity, fps =1.18Tubeside Reynolds No., NRe =4,025Tubeside Friction Factor, f =0.027Step 6. Check tubeside velocity and DP, shellside DP. If too high or too low,DP per pass, psi =0.00021adjust tube length, number of tubes per pass, number of passes, and/or shellNusselt number, Nr =7.04baffle spacing. Remember to reset shell diameter from tube count tables, asInside Film Coefficient, hi =11required.

Sheet4Shell and Tube Heat Exchanger Design SpreadsheetProject:EvaporatorProject No.:-Item No.:-Service:Water coolerBy:MASDate/Time:19-Sep-119:40BWG/Tube Wall Thicknesses80.165Step 1. Input flows, conditions and properties data for shellside and tubesideStep 5. Start configuring the exchanger. Begin with the total calculated transfer coefficient to this point:90.1480.017100.1340.014TubeSideShellUstart =10Btu/hft2oF110.1200.014R-22Fluid NameWaterOver all heat transfer Coefficient, Uo =9.7Btu/hft2oF120.1090.011168.5Flow (M), lb/h11,014.1Then the required transfer A =63ft2130.0950.0145Temp. in, oF86Number of tubes required =239140.0830.0125Temp. out, oF82Reset tubes/pass (Step 3), then no. of passes =2150.0720.011Av. Density0.8053r, lb/ft362.42Total tube count =132160.0650.007Av. Viscosity0.011m, cP1.903Tubeside DP (incl. returns) =5.802psiAv. Heat Capacity0.163cp, Btu/lboF1.003Actual effective transfer area, A =35ft2MTD Correction FactorsHeat Exchanged48,000Q, Btu/h44,188Av. Thermal Conductivity0.0049k, Btu/hftoF0.3351R = ( T1 - T2 ) / ( t2 - t1 ) =0.000Fouling Resistance0.0040R, ft2hoF/Btu0.004Step 4. Select tube arrangementTube Pitch0.65in.Prandtl No.0.87cpm/k13.78and estimate shell diameterPatternTri.S = ( t2 - t1 ) / ( T1 - t1 ) =0.000Corrected MTD79.0oFShell ID from Tube Count Tables8in.Corrected MTD79.0oFSelect Baffle Spacing5in.( R2 + 1 ) =0.000Number of Baffles =43.80Flow Area across Bundle, as =0.064ft2( 1 - S ) / ( 1 - RS ) =0.000Step 2. Input tubing OD, BWG andTube OD0.5000in.Equivalent Diameter, de (see table) =7.5in.length (can be trial and error).BWG16Mass Velocity, Gs =171,820lb/hft22 - S ( R + 1 - ( R2 + 1 ) ) =0.000Tube ID, d =0.370in.Shellside Reynolds No., NRe =56,431Tube Length, L =2ft.Shellside Friction Factor =0.001532 - S ( R + 1 + ( R2 + 1 ) ) =0.000Flow area per tube, at =0.108in.2Shellside DP =0.357psiEffective transfer area per tube =0.262ft2Outside Transfer Factor, jh =139.7FT =0.000Outside Film Coefficient, ho =179Calculated Uo =9.7Step 3. Estimate the number ofTubes/pass =66Check: % difference, Ucalc. vs Uassum. =0.0%tubes per tube pass.lb/h per tube =3Uclean =10.5lb/h per tube per pass =1.3Av. velocity, fps =1.18Tubeside Reynolds No., NRe =4,025Tubeside Friction Factor, f =0.027Step 6. Check tubeside velocity and DP, shellside DP. If too high or too low,DP per pass, psi =0.00021adjust tube length, number of tubes per pass, number of passes, and/or shellNusselt number, Nr =7.04baffle spacing. Remember to reset shell diameter from tube count tables, asInside Film Coefficient, hi =11required.

Sheet5Shell and Tube Heat Exchanger Design SpreadsheetProject:EvaporatorProject No.:-Item No.:-Service:Water coolerBy:MASDate/Time:19-Sep-119:40BWG/Tube Wall Thicknesses80.165Step 1. Input flows, conditions and properties data for shellside and tubesideStep 5. Start configuring the exchanger. Begin with the total calculated transfer coefficient to this point:90.1480.017100.1340.014TubeSideShellUstart =10Btu/hft2oF110.1200.014R-22Fluid NameWaterOver all heat transfer Coefficient, Uo =9.7Btu/hft2oF120.1090.011168.5Flow (M), lb/h11,014.1Then the required transfer A =63ft2130.0950.0145Temp. in, oF86Number of tubes required =239140.0830.0125Temp. out, oF82Reset tubes/pass (Step 3), then no. of passes =2150.0720.011Av. Density0.8053r, lb/ft362.42Total tube count =132160.0650.007Av. Viscosity0.011m, cP1.903Tubeside DP (incl. returns) =5.802psiAv. Heat Capacity0.163cp, Btu/lboF1.003Actual effective transfer area, A =35ft2MTD Correction FactorsHeat Exchanged48,000Q, Btu/h44,188Av. Thermal Conductivity0.0049k, Btu/hftoF0.3351R = ( T1 - T2 ) / ( t2 - t1 ) =0.000Fouling Resistance0.0040R, ft2hoF/Btu0.004Step 4. Select tube arrangementTube Pitch0.65in.Prandtl No.0.87cpm/k13.78and estimate shell diameterPatternTri.S = ( t2 - t1 ) / ( T1 - t1 ) =0.000Corrected MTD79.0oFShell ID from Tube Count Tables8in.Corrected MTD79.0oFSelect Baffle Spacing5in.( R2 + 1 ) =0.000Number of Baffles =43.80Flow Area across Bundle, as =0.064ft2( 1 - S ) / ( 1 - RS ) =0.000Step 2. Input tubing OD, BWG andTube OD0.5000in.Equivalent Diameter, de (see table) =7.5in.length (can be trial and error).BWG16Mass Velocity, Gs =171,820lb/hft22 - S ( R + 1 - ( R2 + 1 ) ) =0.000Tube ID, d =0.370in.Shellside Reynolds No., NRe =56,431Tube Length, L =2ft.Shellside Friction Factor =0.001532 - S ( R + 1 + ( R2 + 1 ) ) =0.000Flow area per tube, at =0.108in.2Shellside DP =0.357psiEffective transfer area per tube =0.262ft2Outside Transfer Factor, jh =139.7FT =0.000Outside Film Coefficient, ho =179Calculated Uo =9.7Step 3. Estimate the number ofTubes/pass =66Check: % difference, Ucalc. vs Uassum. =0.0%tubes per tube pass.lb/h per tube =3Uclean =10.5lb/h per tube per pass =1.3Av. velocity, fps =1.18Tubeside Reynolds No., NRe =4,025Tubeside Friction Factor, f =0.027Step 6. Check tubeside velocity and DP, shellside DP. If too high or too low,DP per pass, psi =0.00021adjust tube length, number of tubes per pass, number of passes, and/or shellNusselt number, Nr =7.04baffle spacing. Remember to reset shell diameter from tube count tables, asInside Film Coefficient, hi =11required.

Sheet6Shell and Tube Heat Exchanger Design SpreadsheetProject:EvaporatorProject No.:-Item No.:-Service:Water coolerBy:MASDate/Time:19-Sep-119:40BWG/Tube Wall Thicknesses80.165Step 1. Input flows, conditions and properties data for shellside and tubesideStep 5. Start configuring the exchanger. Begin with the total calculated transfer coefficient to this point:90.1480.017100.1340.014TubeSideShellUstart =10Btu/hft2oF110.1200.014R-22Fluid NameWaterOver all heat transfer Coefficient, Uo =9.7Btu/hft2oF120.1090.011168.5Flow (M), lb/h11,014.1Then the required transfer A =63ft2130.0950.0145Temp. in, oF86Number of tubes required =239140.0830.0125Temp. out, oF82Reset tubes/pass (Step 3), then no. of passes =2150.0720.011Av. Density0.8053r, lb/ft362.42Total tube count =132160.0650.007Av. Viscosity0.011m, cP1.903Tubeside DP (incl. returns) =5.802psiAv. Heat Capacity0.163cp, Btu/lboF1.003Actual effective transfer area, A =35ft2MTD Correction FactorsHeat Exchanged48,000Q, Btu/h44,188Av. Thermal Conductivity0.0049k, Btu/hftoF0.3351R = ( T1 - T2 ) / ( t2 - t1 ) =0.000Fouling Resistance0.0040R, ft2hoF/Btu0.004Step 4. Select tube arrangementTube Pitch0.65in.Prandtl No.0.87cpm/k13.78and estimate shell diameterPatternTri.S = ( t2 - t1 ) / ( T1 - t1 ) =0.000Corrected MTD79.0oFShell ID from Tube Count Tables8in.Corrected MTD79.0oFSelect Baffle Spacing5in.( R2 + 1 ) =0.000Number of Baffles =43.80Flow Area across Bundle, as =0.064ft2( 1 - S ) / ( 1 - RS ) =0.000Step 2. Input tubing OD, BWG andTube OD0.5000in.Equivalent Diameter, de (see table) =7.5in.length (can be trial and error).BWG16Mass Velocity, Gs =171,820lb/hft22 - S ( R + 1 - ( R2 + 1 ) ) =0.000Tube ID, d =0.370in.Shellside Reynolds No., NRe =56,431Tube Length, L =2ft.Shellside Friction Factor =0.001532 - S ( R + 1 + ( R2 + 1 ) ) =0.000Flow area per tube, at =0.108in.2Shellside DP =0.357psiEffective transfer area per tube =0.262ft2Outside Transfer Factor, jh =139.7FT =0.000Outside Film Coefficient, ho =179Calculated Uo =9.7Step 3. Estimate the number ofTubes/pass =66Check: % difference, Ucalc. vs Uassum. =0.0%tubes per tube pass.lb/h per tube =3Uclean =10.5lb/h per tube per pass =1.3Av. velocity, fps =1.18Tubeside Reynolds No., NRe =4,025Tubeside Friction Factor, f =0.027Step 6. Check tubeside velocity and DP, shellside DP. If too high or too low,DP per pass, psi =0.00021adjust tube length, number of tubes per pass, number of passes, and/or shellNusselt number, Nr =7.04baffle spacing. Remember to reset shell diameter from tube count tables, asInside Film Coefficient, hi =11required.

Sheet7Shell and Tube Heat Exchanger Design SpreadsheetProject:EvaporatorProject No.:-Item No.:-Service:Water coolerBy:MASDate/Time:19-Sep-119:40BWG/Tube Wall Thicknesses80.165Step 1. Input flows, conditions and properties data for shellside and tubesideStep 5. Start configuring the exchanger. Begin with the total calculated transfer coefficient to this point:90.1480.017100.1340.014TubeSideShellUstart =10Btu/hft2oF110.1200.014R-22Fluid NameWaterOver all heat transfer Coefficient, Uo =9.7Btu/hft2oF120.1090.011168.5Flow (M), lb/h11,014.1Then the required transfer A =63ft2130.0950.0145Temp. in, oF86Number of tubes required =239140.0830.0125Temp. out, oF82Reset tubes/pass (Step 3), then no. of passes =2150.0720.011Av. Density0.8053r, lb/ft362.42Total tube count =132160.0650.007Av. Viscosity0.011m, cP1.903Tubeside DP (incl. returns) =5.802psiAv. Heat Capacity0.163cp, Btu/lboF1.003Actual effective transfer area, A =35ft2MTD Correction FactorsHeat Exchanged48,000Q, Btu/h44,188Av. Thermal Conductivity0.0049k, Btu/hftoF0.3351R = ( T1 - T2 ) / ( t2 - t1 ) =0.000Fouling Resistance0.0040R, ft2hoF/Btu0.004Step 4. Select tube arrangementTube Pitch0.65in.Prandtl No.0.87cpm/k13.78and estimate shell diameterPatternTri.S = ( t2 - t1 ) / ( T1 - t1 ) =0.000Corrected MTD79.0oFShell ID from Tube Count Tables8in.Corrected MTD79.0oFSelect Baffle Spacing5in.( R2 + 1 ) =0.000Number of Baffles =43.80Flow Area across Bundle, as =0.064ft2( 1 - S ) / ( 1 - RS ) =0.000Step 2. Input tubing OD, BWG andTube OD0.5000in.Equivalent Diameter, de (see table) =7.5in.length (can be trial and error).BWG16Mass Velocity, Gs =171,820lb/hft22 - S ( R + 1 - ( R2 + 1 ) ) =0.000Tube ID, d =0.370in.Shellside Reynolds No., NRe =56,431Tube Length, L =2ft.Shellside Friction Factor =0.001532 - S ( R + 1 + ( R2 + 1 ) ) =0.000Flow area per tube, at =0.108in.2Shellside DP =0.357psiEffective transfer area per tube =0.262ft2Outside Transfer Factor, jh =139.7FT =0.000Outside Film Coefficient, ho =179Calculated Uo =9.7Step 3. Estimate the number ofTubes/pass =66Check: % difference, Ucalc. vs Uassum. =0.0%tubes per tube pass.lb/h per tube =3Uclean =10.5lb/h per tube per pass =1.3Av. velocity, fps =1.18Tubeside Reynolds No., NRe =4,025Tubeside Friction Factor, f =0.027Step 6. Check tubeside velocity and DP, shellside DP. If too high or too low,DP per pass, psi =0.00021adjust tube length, number of tubes per pass, number of passes, and/or shellNusselt number, Nr =7.04baffle spacing. Remember to reset shell diameter from tube count tables, asInside Film Coefficient, hi =11required.

Sheet8Shell and Tube Heat Exchanger Design SpreadsheetProject:EvaporatorProject No.:-Item No.:-Service:Water coolerBy:MASDate/Time:19-Sep-119:40BWG/Tube Wall Thicknesses80.165Step 1. Input flows, conditions and properties data for shellside and tubesideStep 5. Start configuring the exchanger. Begin with the total calculated transfer coefficient to this point:90.1480.017100.1340.014TubeSideShellUstart =10Btu/hft2oF110.1200.014R-22Fluid NameWaterOver all heat transfer Coefficient, Uo =9.7Btu/hft2oF120.1090.011168.5Flow (M), lb/h11,014.1Then the required transfer A =63ft2130.0950.0145Temp. in, oF86Number of tubes required =239140.0830.0125Temp. out, oF82Reset tubes/pass (Step 3), then no. of passes =2150.0720.011Av. Density0.8053r, lb/ft362.42Total tube count =132160.0650.007Av. Viscosity0.011m, cP1.903Tubeside DP (incl. returns) =5.802psiAv. Heat Capacity0.163cp, Btu/lboF1.003Actual effective transfer area, A =35ft2MTD Correction FactorsHeat Exchanged48,000Q, Btu/h44,188Av. Thermal Conductivity0.0049k, Btu/hftoF0.3351R = ( T1 - T2 ) / ( t2 - t1 ) =0.000Fouling Resistance0.0040R, ft2hoF/Btu0.004Step 4. Select tube arrangementTube Pitch0.65in.Prandtl No.0.87cpm/k13.78and estimate shell diameterPatternTri.S = ( t2 - t1 ) / ( T1 - t1 ) =0.000Corrected MTD79.0oFShell ID from Tube Count Tables8in.Corrected MTD79.0oFSelect Baffle Spacing5in.( R2 + 1 ) =0.000Number of Baffles =43.80Flow Area across Bundle, as =0.064ft2( 1 - S ) / ( 1 - RS ) =0.000Step 2. Input tubing OD, BWG andTube OD0.5000in.Equivalent Diameter, de (see table) =7.5in.length (can be trial and error).BWG16Mass Velocity, Gs =171,820lb/hft22 - S ( R + 1 - ( R2 + 1 ) ) =0.000Tube ID, d =0.370in.Shellside Reynolds No., NRe =56,431Tube Length, L =2ft.Shellside Friction Factor =0.001532 - S ( R + 1 + ( R2 + 1 ) ) =0.000Flow area per tube, at =0.108in.2Shellside DP =0.357psiEffective transfer area per tube =0.262ft2Outside Transfer Factor, jh =139.7FT =0.000Outside Film Coefficient, ho =179Calculated Uo =9.7Step 3. Estimate the number ofTubes/pass =66Check: % difference, Ucalc. vs Uassum. =0.0%tubes per tube pass.lb/h per tube =3Uclean =10.5lb/h per tube per pass =1.3Av. velocity, fps =1.18Tubeside Reynolds No., NRe =4,025Tubeside Friction Factor, f =0.027Step 6. Check tubeside velocity and DP, shellside DP. If too high or too low,DP per pass, psi =0.00021adjust tube length, number of tubes per pass, number of passes, and/or shellNusselt number, Nr =7.04baffle spacing. Remember to reset shell diameter from tube count tables, asInside Film Coefficient, hi =11required.

Sheet9Shell and Tube Heat Exchanger Design SpreadsheetProject:EvaporatorProject No.:-Item No.:-Service:Water coolerBy:MASDate/Time:19-Sep-119:40BWG/Tube Wall Thicknesses80.165Step 1. Input flows, conditions and properties data for shellside and tubesideStep 5. Start configuring the exchanger. Begin with the total calculated transfer coefficient to this point:90.1480.017100.1340.014TubeSideShellUstart =10Btu/hft2oF110.1200.014R-22Fluid NameWaterOver all heat transfer Coefficient, Uo =9.7Btu/hft2oF120.1090.011168.5Flow (M), lb/h11,014.1Then the required transfer A =63ft2130.0950.0145Temp. in, oF86Number of tubes required =239140.0830.0125Temp. out, oF82Reset tubes/pass (Step 3), then no. of passes =2150.0720.011Av. Density0.8053r, lb/ft362.42Total tube count =132160.0650.007Av. Viscosity0.011m, cP1.903Tubeside DP (incl. returns) =5.802psiAv. Heat Capacity0.163cp, Btu/lboF1.003Actual effective transfer area, A =35ft2MTD Correction FactorsHeat Exchanged48,000Q, Btu/h44,188Av. Thermal Conductivity0.0049k, Btu/hftoF0.3351R = ( T1 - T2 ) / ( t2 - t1 ) =0.000Fouling Resistance0.0040R, ft2hoF/Btu0.004Step 4. Select tube arrangementTube Pitch0.65in.Prandtl No.0.87cpm/k13.78and estimate shell diameterPatternTri.S = ( t2 - t1 ) / ( T1 - t1 ) =0.000Corrected MTD79.0oFShell ID from Tube Count Tables8in.Corrected MTD79.0oFSelect Baffle Spacing5in.( R2 + 1 ) =0.000Number of Baffles =43.80Flow Area across Bundle, as =0.064ft2( 1 - S ) / ( 1 - RS ) =0.000Step 2. Input tubing OD, BWG andTube OD0.5000in.Equivalent Diameter, de (see table) =7.5in.length (can be trial and error).BWG16Mass Velocity, Gs =171,820lb/hft22 - S ( R + 1 - ( R2 + 1 ) ) =0.000Tube ID, d =0.370in.Shellside Reynolds No., NRe =56,431Tube Length, L =2ft.Shellside Friction Factor =0.001532 - S ( R + 1 + ( R2 + 1 ) ) =0.000Flow area per tube, at =0.108in.2Shellside DP =0.357psiEffective transfer area per tube =0.262ft2Outside Transfer Factor, jh =139.7FT =0.000Outside Film Coefficient, ho =179Calculated Uo =9.7Step 3. Estimate the number ofTubes/pass =66Check: % difference, Ucalc. vs Uassum. =0.0%tubes per tube pass.lb/h per tube =3Uclean =10.5lb/h per tube per pass =1.3Av. velocity, fps =1.18Tubeside Reynolds No., NRe =4,025Tubeside Friction Factor, f =0.027Step 6. Check tubeside velocity and DP, shellside DP. If too high or too low,DP per pass, psi =0.00021adjust tube length, number of tubes per pass, number of passes, and/or shellNusselt number, Nr =7.04baffle spacing. Remember to reset shell diameter from tube count tables, asInside Film Coefficient, hi =11required.

Sheet10Shell and Tube Heat Exchanger Design SpreadsheetProject:EvaporatorProject No.:-Item No.:-Service:Water coolerBy:MASDate/Time:19-Sep-119:40BWG/Tube Wall Thicknesses80.165Step 1. Input flows, conditions and properties data for shellside and tubesideStep 5. Start configuring the exchanger. Begin with the total calculated transfer coefficient to this point:90.1480.017100.1340.014TubeSideShellUstart =10Btu/hft2oF110.1200.014R-22Fluid NameWaterOver all heat transfer Coefficient, Uo =9.7Btu/hft2oF120.1090.011168.5Flow (M), lb/h11,014.1Then the required transfer A =63ft2130.0950.0145Temp. in, oF86Number of tubes required =239140.0830.0125Temp. out, oF82Reset tubes/pass (Step 3), then no. of passes =2150.0720.011Av. Density0.8053r, lb/ft362.42Total tube count =132160.0650.007Av. Viscosity0.011m, cP1.903Tubeside DP (incl. returns) =5.802psiAv. Heat Capacity0.163cp, Btu/lboF1.003Actual effective transfer area, A =35ft2MTD Correction FactorsHeat Exchanged48,000Q, Btu/h44,188Av. Thermal Conductivity0.0049k, Btu/hftoF0.3351R = ( T1 - T2 ) / ( t2 - t1 ) =0.000Fouling Resistance0.0040R, ft2hoF/Btu0.004Step 4. Select tube arrangementTube Pitch0.65in.Prandtl No.0.87cpm/k13.78and estimate shell diameterPatternTri.S = ( t2 - t1 ) / ( T1 - t1 ) =0.000Corrected MTD79.0oFShell ID from Tube Count Tables8in.Corrected MTD79.0oFSelect Baffle Spacing5in.( R2 + 1 ) =0.000Number of Baffles =43.80Flow Area across Bundle, as =0.064ft2( 1 - S ) / ( 1 - RS ) =0.000Step 2. Input tubing OD, BWG andTube OD0.5000in.Equivalent Diameter, de (see table) =7.5in.length (can be trial and error).BWG16Mass Velocity, Gs =171,820lb/hft22 - S ( R + 1 - ( R2 + 1 ) ) =0.000Tube ID, d =0.370in.Shellside Reynolds No., NRe =56,431Tube Length, L =2ft.Shellside Friction Factor =0.001532 - S ( R + 1 + ( R2 + 1 ) ) =0.000Flow area per tube, at =0.108in.2Shellside DP =0.357psiEffective transfer area per tube =0.262ft2Outside Transfer Factor, jh =139.7FT =0.000Outside Film Coefficient, ho =179Calculated Uo =9.7Step 3. Estimate the number ofTubes/pass =66Check: % difference, Ucalc. vs Uassum. =0.0%tubes per tube pass.lb/h per tube =3Uclean =10.5lb/h per tube per pass =1.3Av. velocity, fps =1.18Tubeside Reynolds No., NRe =4,025Tubeside Friction Factor, f =0.027Step 6. Check tubeside velocity and DP, shellside DP. If too high or too low,DP per pass, psi =0.00021adjust tube length, number of tubes per pass, number of passes, and/or shellNusselt number, Nr =7.04baffle spacing. Remember to reset shell diameter from tube count tables, asInside Film Coefficient, hi =11required.