Forced Convection Week 1Q1Q 6TkCPm 20oCm 40oCExothermic Reaction in stirred tank(oC)(W m-1 K-1)(kg m-3)(J kg-1K-1)(kg m-1 s-1)(kg m-1 s-1)water200.597100141561.01E-036.96E-04Q10000W/m3oil200.14588817700.7990.21H2mair 1 atm200.02621.20310041.84E-051.93E-05D2mV6.28318Q62831.8WFlow2m/sA12.56636m2Diameter0.2mU150Tr80CDT33.3333333333CRePrNuhTj46.6666666667Cwater3976177.011512.14513.7oil4459753.31N/AMaximum diameter if Tj is limited to 30oCair 1 atm261520.7168.49.0Q=UA(Tr-Tj)Q/A=U(Tr-Tj)Q2A=piDHQ=10,000*pi/D^2/4*HCalculate the heat transfer coefficients in the previous question using the Sieder Tate CorrelationQ/A=10,000*D/4D=4*Q/A/10,000D=4*U(Tr-Tj)/10,000Tj30Tr80DT50UDT7500D3In both cases assume the wall is at 40oCNuhwater1631.124868.9oilair 1 atm81.7310.7Q3If one side of an exchanger had air flowing at 2 m/s and the other water at 2 m/s which would be the controlling resistance?1/U0.0936038319U10.683U is approximately equal to h for the Air. The air would be the controlling resistanceQ4Water flowing through smooth pipe, heated by condnesing steam, assume waters resistance is controlling1 m pipeFlowrate0.2kg/s0.1kg/sdiameter0.02m0.01marea0.000314159m20.0000785398m2u0.6359843258m/s1.2719686515m/sRe1.26E+041.26E+04f0.00373443520.0037344352DP302.4000300513Pa/m2419.2Pa/mPr7.017.01Nu95.835170374695.8351703746h2860.7W/m2K5721.4W/m2KhA179.7W/K359.5W/KQ5 Concentric Pipe Heat ExchangerWaterCold StreamTkCPmWater(oC)(W m-1 K-1)(kg m-3)(J kg-1K-1)(kg m-1 s-1)Tin20oC200.597100141561.01E-03Tout40oC400.62899541786.96E-04Flow0.11kg/s1000.6896142162.82E-04ID0.015m1200.68594542501.59E-04IA0.0001767146m2r998u0.6237201065m/sm0.000837181Pressure Drop Inside PipeCp4167k0.6125Re1.12E+04Re11153f0.003853427Pr5.70DP544Nu79.7730675953h3257.4002601431W/m2KHot Stream Outer PipeWaterTin120oCTout100oCFlow0.11kg/sID0.02mOD0.03mIA0.0003926991m2dm0.01mr953u0.2939272821m/sm0.0002117499Pressure Drop Outside PipeCp4233k0.6825Re1.32E+04Re13228f0.0036924767Pr1.31DP174Nu50.8490770042h3470.4495055359W/m2KSteel Wallk60W/m/KAo/(hiAi)0.0004093244ln(ro/ri)/kxro0.0000479471/ho0.0002881471Uo1341.5282810554LMTD80KQ9167.4WA0.0854193695m2L1.36m

Natural Convection Week 2Question 1Question 2Question 3Question 4Estimate the heat transfer coefficient from a horizontal pipe 0.15m in diameterEstimate the heat transfer coefficient and the rate of heatingEstimate the heat loss though a the gap between double glazed windows.If the thermal resistance of glass is 0.003with a surface temperature of 400K to air at 294Kfrom a flat vertical convenction heater.R glass0.003DimensionsDimensionsDimensionsWidth2mGap (L)0.015mGap (L)0.015mHeight0.8mHeight (H)2mHeight (H)2mTheater60CWidth2mWidth2mTroom15CThot10CTroom20Delta T glass0.2347712776do0.15Tmean310.65Tcold-10CThot19.77CDelta T glass0.2347714473Tpipe400Tmean273.15Tcold-19.77Cdiff0Tamb294Physical PropertiesToutside-20Tmean347r1.1377143403kg/m3Physical PropertiesTmean273.15Delta T air40b0.0032190568r1.293907962kg/m3Physical propertiesm1.93E-05Pa.sb0.0036609921Physical Propertiesr1.0185330254kg/m3Cp1100J/kg/Km1.60E-05Pa.sr1.293907962kg/m3b0.0028818444k0.02702375W/mKCp1050J/kg/Kb0.0036609921m2.00E-05Pa.sg9.81m/s2k0.02421125W/mKm1.60E-05Pa.sCp1100J/kg/Kg9.81m/s2Cp1050J/kg/Kk0.02975W/mKGr2.53E+09k0.02421125W/mKg9.81m/s2Pr7.86E-01Gr1.59E+04g9.81m/s2GrPr1.99E+09Pr6.94E-01Gr2.62E+07GrPr1.10E+04Gr3.13E+04Pr7.39E-01C'0.13Ra1.10E+04Pr6.94E-01GrPr1.94E+07n0.33500H/L6.67E+04GrPr2.17E+04h5.14W/m2KRa2.17E+04C'0.53Q370.1W500H/L6.67E+04n0.25h6.98W/m2KC"1.24n0.33h4.36W/m2KNu1.11E+00C"1.32Q314.3Wh1.80W/m2/Kn0.25R0.5558500124Km2/WNu1.23E+00h6.81W/m2KQ143.9Wh1.98W/m2/KR0.5051354102Km2/Wq348.5W/mRglass0.006340.0W/mRtotal0.5111354102Q313.0W

Stirred Tank Week 3Question 1Question 2Question 3Question 4Exothermic Reaction in stirred tankh Jacket2000W/m2KDiameter2mDiameter2mh Vessel350W/m2KHeight1mHeight2.5mQ10000W/m3H2mOverall298W/m2KVolume3.14159m3Impeller0.5mD2mArea6.28318m2150rpmV6.28318Effect of stirrer diameter2.5rev/sQ62831.8W1.5U450k0.6W/mKA12.56636m21.7217190594Ti65cp4kJ/kg/KU150New h VesselTf434000J/kg/KTr80C525W/m2KTj37mu0.001Pa.sDT33.3333333333C603W/m2Kdensity1000kg/m3Tj46.6666666667CDensity900kg/m3Nbl4New OverallMass2827.431kgTheta90Maximum diameter if Tj is limited to 30oC416W/m2K463W/m2Kcp4kJ/kg/KQ=UA(Tr-Tj)4000J/kg/KQ/A=U(Tr-Tj)40%A=piDH55%ln term1.5404450409Q=10,000*pi/D^2/4*HQ/A=10,000*D/4UA/Mcp0.00025D=4*Q/A/10,000D=4*U(Tr-Tj)/10,000t6161.7801637886seconds1.7116056011hoursTj300.7116056011Tr8042.6963360631Re625000Re^2/37310.0443455322DT50UDT7500Pr6.6666666667Pr^1/31.8820720578D3mu/muw1Nu10180.9423507584h3054.2827052275W/m2K

Shell and Tube Wk4&5Question 1Question 2Question 3Data for Q 4Question 4 Example 12.1 C&R vol 6Example 12.3 C&R vol 6Kern's MethodOilKeroseneOilMethanolMethanolMethanolHeat Transfer coefficientShell Side Pressure DropFlow2kg/sFlow10kg/sFlow10kg/sShell sideFlowrate100000kg/hrShell sidecp2000J/kg/Kcp2450J/kg/Kcp2000J/kg/KFlowrate100000kg/hr27.78kg/sFlowrate100000kg/hrAs0.0636528m2Cross Flow ZoneInlet T80CInlet T100CInlet T90CCp2840J/kg/KCp2840J/kg/KCp2840J/kg/KGs436.3952218563kg/m2sOutlet T40COutlet T60CInlet Temp95CInlet Temp95CInlet Temp95CRe25670jF5.60E-02from fig 12.36WaterOutlet Temp40COutlet Temp40COutlet Temp40CPr5.08us0.5818602958m/sQ160000WQ980000WFlow20kg/sdensity750kg/m3Q4338888.88888889Wdensity750kg/m3jH5.30E-03from fig 12.31DPi1137.5663168967Pacp4200J/kg/Km3.40E-04Pa.sm3.40E-04Pa.shoc2210.17WaterWaterInlet T25Ck0.19W/m/KWaterk0.19W/m/KBypass Correctioncp4200J/kg/Kcp4200J/kg/Kfouling5000W/m2KCp4200J/kg/Kfouling5000W/m2KTube Row Correction FactorInlet T25CInlet T20CA200m2Inlet Temp25CF'b0.6700625903Outlet T35COutlet T90CU150WaterOutlet Temp40CWaterTube row vertical pitchTube sideFlowrate68.8712522046kg/sTube sidep't0.02175Leakage CorrectionFlow3.81kg/sFlow3.33kg/sR4.2Cp4200J/kg/KCp4200J/kg/KBaffle cut heightNTUc0.3571428571Inlet Temp25CDTLM30.7862109245Inlet Temp25CHc0.2235AL/As0.4383211605DTLM27.3071767988C or KDTLM21.6404256133C or KOutlet Temp40COutlet Temp40CHeight between baffle tipsb'L0.52From fig 12.38From Figure 3.22m8.00E-04Pa.sR3.66666666673.6666666667m8.00E-04Pa.s0.447F'L0.3127181947R4R0.5714285714q0.47k0.59W/m/KP or S0.2142857143k0.59W/m/KNcv20.5517241379P0.1818181818P0.875P0.17density995kg/m3density995kg/m3Ncv20DPc238.3665146416PaF0.85From Figure 3.8 HewittF (1 exchanger) 0.8 not in cross over

MBD00057814.unknown

MBD00118C65.unknown

MBD001A6466.unknown

MBD001A6DC0.unknown

MBD0011B3BF.unknown

MBD00086C6C.unknown

MBD000057C9.unknown

MBD00036222.unknown

MBD0001EE83.unknown