冷却器传热面积计算模版

管壳式冷却器热计算标准状态下气量1085Nm^3/h标准状态气量　Nm3/min16.658999.48气体成分CH465.7072吸入状态气量　m3/min9.8C2H67.8412相对温度%100C3H85.5913一级进气压力kg/cm22C4H105.0329一级进气温度℃35C5H125.6979进气温度下饱和水蒸气压　kg/cm20.05733C6H141.8036N27.3326CO20.9933100一级冷却器冷却器中气体压力4.65kg/cm2气体进口温度T185℃气体出口温度T240℃冷却水进口温度t130℃冷却水出口温度t238℃一级进气压力2kg/cm2一级进气温度35℃有效平均温差ΔTm==20.7℃21222122112122212211212221lnttTTtTtTttTTtTtTttTT计算热负荷计算定性温度冷却水的定性温度（按式8-36）tc=(t1+t2)/2=34℃混合气体的定性温度（按式8-37）Tc=ΔTm+tc=54.7℃管壁温度：按式8-43，取系数B＝0.14tw=BΔTm+tc=36.898℃物性参数的确定冷却水的物性参数在tc=34℃的条件下，各项参数由附录二表26（P654）得知重度γkg/m3比热Cp千卡/kg·℃粘度μ公斤秒/米22.65929公斤/米·时导热系数λ千卡/米·小时·℃普兰德数Pr气体常数，按式2-6Rw=848/Mw=公斤·米/公斤·℃冷却水在平均壁温tw=℃的条件下的粘度为粘度为μw公斤秒/米22.59025公斤/米·时混合气体的物理参数计算标准状态下混合气体的重度γ0m，计算结果见下表成分CH4C2H6C3H8C4H10C5H12C6H14N2CO200容积百分数ri65.70727.84125.59135.03295.69791.80367.33260.993300标准状态下各组分重度γ0i0.7151.3561.972.5853.4573.8451.2511.977007.33E-055.00447.0636.898994.340.9977.53E-050.5366(公斤/米3，查表2-1，2-2）riγ0i0.469810.106330.110150.13010.196980.069350.091730.01963800γ0m=Σriγ0i=1.19408公斤/米3计算混合气体在Tc=54.7℃,压力p=4.65kgf/cm2时的比热Cpm常压下的比热C0pm成分CH4C2H6C3H8C4H10C5H12C6H14N2CO200riγ0i0.469810.106330.110150.13010.196980.069350.091730.01963800常压下的各组分比热C0pi0.5270.410.3890.3970.3970.3980.250.200千卡/kg·℃(查表2-1，2-2)riγ0iC0pi0.247590.043590.042850.051650.07820.02760.022930.00392800按式2-26，C0pm=ΣgiC0pi=Σriγ0iC0pi/γ0m=0.4341千卡/kg·℃计算ΔCpm成分CH4C2H6C3H8C4H10C5H12C6H14N2CO200容积百分数ri65.70727.84125.59135.03295.69791.80367.33260.993300临界温度Tci,°K(查表2-1，2-2）190.5305.37369.81425.01469.62507.7125.9304.100临界压力Pci(kg/cm2）45.848.1942.0137.4733.3129.9233.4972.900(查表2-1，2-2）riTci125.17223.944720.677221.390326.75859.156889.231743.02062500riPci30.09393.778672.348911.885831.897970.539642.455690.72411600分子量Mi,(查表2-1，2-2）16.0430.0744.0958.1272.1586.17284400riMi10.53942.357852.46522.925124.111031.554162.053130.43705200按式2-16，混合气体的假临界温度：T'c=ΣriTci=239.352°K按式2-17，混合气体的假临界压力：P'c=ΣriPci=43.72(kg/cm2）按式2-14，对比温度：Tr=Tc/T'c=1.369按式2-15，对比压力：Pr=P/P'c=0.106按式2-10，混合气体的平均分子量：Mm=ΣriMi=26.443由Pr,Tr查图2-6得ΔCpm0.00605千卡/kg·℃0.16卡/克分子·℃Cpm=C0pm+ΔCpm=0.44015千卡/kg·℃计算混合气体在Tc=54.7℃,压力P=4.65kg/cm2时的导热系数标准状态下的导热系数λ0m成分CH4C2H6C3H8C4H10C5H12C6H14N2CO200容积百分数ri65.70727.84125.59135.03295.69791.80367.33260.993300标准状态下的导热系数λ0i0.02450.0160.20040.27540.35560.48090.02070.01260(千卡/米·小时·℃,查表2-1,按P685)分子量Mi，查表2-1，2-216.0430.0744.0958.1272.1586.17284400Mi1/32.521943.109653.532753.873544.163054.416913.036593.53034800riMi1/31.65710.243830.197530.194950.237210.079660.222660.03506700λ0iriMi1/30.04060.00390.039580.053690.084350.038310.004610.0004400按附录2中式2（P685）混合气体在标准状态下的导热系数λ0m=(Σλ0iγiMi1/3)/(ΣγiMi1/3)=0.09257千卡/米·小时·℃由Pr,Tr查附录图27得λm/λ0m=1(由该图可见，此情况下无法查值，从走向看，可视其为1，)λm=0.09257千卡/米·小时·℃计算混合气体在Tc=54.7℃,压力P=4.65kg/cm2时的粘度成分CH4C2H6C3H8C4H10C5H12C6H14N2CO200容积百分数ri65.70727.84125.59135.03295.69791.80367.33260.993300标准状态下的粘度μ0i0.010.0090.1250.1740.2290.3130.0170.0137(厘泊,查表2-1,2-2)分子量Mi，查表2-1，2-216.0430.0744.0958.1272.1586.17284400Mi1/24.0055.483616.640037.623658.494129.282785.29156.6332500riMi1/22.631570.429980.371260.383690.483990.167420.3880.06588800riMi1/2μ0i0.026320.003870.046410.066760.110830.05240.00660.00090300按附录P680μ0m=(Σμ0iγiMi1/2)/(ΣγiMi1/2)=0.0638厘泊查附录图25μm/μ0m=1.05(由该图可见，此情况下无法查值，从走向看，可视其为1，)μm=0.06699厘泊=0.24116公斤/米·时计算混合气体在tw=36.898℃,压力P=4.65kg/cm2时的粘度此情况下的对比温度：Tr=Tc/T'c=1.29474此情况下的对比压力：Pr=P/P'c=0.10636查附录图25μm/μ0m=1.05(由该图可见，此情况下无法查值，从走向看，可视其为1，)μm=0.06699厘泊=0.24116公斤/米·时计算混合气体的气体常数，按式2-6Rm=848/Mm=32.069公斤·米/公斤·℃计算冷却器的热负荷冷却器中混合气体的质量流量Ws=Vdγ0m=1295.57kg/h气体冷却时放出的热量，按式8-23Q1＝WsCpm(T1-T2)=25661.1千卡/时水蒸汽冷凝时放出的热量：查表2-7，气缸吸入温度时的饱和蒸汽压Psa1=0.05733kg/cm2冷却器出口温度的饱和蒸汽压Psa2＝0.0752kg/cm2取冷却器相应级吸入时的气体相对湿度ψ=1按式8-26χ1=RmPsa1ψ/(Rw(P1-Psa1ψ))=0.0201按式8-26χ2=RmPsa2ψ/(Rw(P-Psa2ψ))=0.0112按式8-25Q2＝Ws[0.46(χ1T1-χ2T2)+(597-0.56T2)(χ1-χ2)]=7376.69千卡/时按式8-22Q＝Q1+Q2＝33037.8千卡/时计算冷却水的消耗量按式8-27W＝Q/（Cp(t2-t1))4142kg/h确定壳程给热系数　α0确定折流板切去部分的效应系数：按式8-66，壳体中心线垂直流动最小流通面积　垂直流动是在壳体中心线的最小流通面积Ac=BP(D's-n3*do)0.0076m2按式8-63，折流板缺口部分流道面积Ab＝K1D's2-0.7854*n4*do2弓形面积系数K1，查表8-170.0651取13.5%用插值法Ab=0.00066m2折流板缺口部分的传热面积与总传热面积之比r=2n4/N=0.25806按式8-74，折流板切去部分的效应修正系数　ΦΦ＝1-r+0.524r0.32(Ac/Ab)0.03=1.10746确定壳体与管束间的间隙影响修正系数ξh按式8-80，管束与壳体间的间隙面积Ad=(Ds'-n3Pt)BP=0.0006m20.0006按式8-79，Fbp=Ad/Ac=0.078950.0789474流体的质量流速　Gc=W/Ac545000公斤/米2·时按式8-76，雷诺数Re'=doGc/μ3366.47Re'100,按式8-78a,ξh=(2.72)-1.35Fbp=0.89884确定管排数影响修正系数xre'4000时，x=0.93/(hm/h∞)Nc'=(Nb+1)Nc+(Nb+2)Nw60按P497说明，本例Nw可以不计及查表8-19，hm/h∞＝0.985则确定管排数影响修正系数x=0.94416无间隙时壳程给热系数　αNO,按式8-85，千卡/米2·时·℃查图8-62，F2＝1查图8-63，jH=0.015考虑存在间隙时，壳程给热系数αo的确定按式8-87，折流板上管孔与管子之间的间隙面积2948.050643αNO＝F2jH(φξh/x)(CpGc)(Cpμ/λ)-2/3(μ/μw)0.14STb=nB*π*(dH2-d02)/40.00034米2按式8-88，折流板边沿与壳体间的间隙面积Ssb=(360-A)/360*(π/4)((Ds2-Db2)0.00033按式8-89，SL＝STb+Ssb=0.00067米2SL/AC=0.088查图8-64得修正系数　α＝0.12按式8-86α0＝αNO*[1-α(STb+2SSb)/SL]=2418.2确定管内给热系数　αi按式8-47，管内气体质量流速Gi=Wi/Fi=369527公斤/米2·小时雷诺数Re=diGi/μ18387.2管内给热系数αi=jH(λ/di)(Cpμ/λ)1/3(μ/μw)0.14=484.457传热因子jH，查图8-4860验算壁温按式8-39，36.704℃确定污垢系数查表8-14，管内污垢系数γi=0.0002米2·时·℃/千卡管外污垢系数γ0=0.0004米2·时·℃/千卡确定管壁金属导热系数，查表8-1545千卡/米2·时·℃计算冷却器传热系数)(α0)dodiαi(αi(di/do)tc