燃料油換熱器計算講解

燃料油換熱器計算手冊》數(shù)opopqu(一)1500m3/h(1)計算熱負(fù)荷Whp(2)導(dǎo)熱油的量(2)平均溫度差R=12==11P=21==P=21==0.333311Δt(3)初選換熱器規(guī)格KmJBT)：折流擋板間距B=300mm系數(shù)為：== ==m(1)管程壓強(qiáng)降管程平均通道面積Ai=0.1290m2ui=V1500i82.74106d20.0152ΔP2=3=3=13928Pa22(2)殼程阻力降ΔP1′=Ffn(N+1)pu2oocB2LNB=1h6=1=190.3mOcooA2puBD2p=(p'+p')FNo12ss(1)管程對流傳熱系數(shù)αi故αi=0.023()Re0.8Pr0.33di=0.023(0.09748)(573857.87)0.81570.7970.33(2)殼程對流傳熱系數(shù)αot0.025=Prp=23.7Prp=23.7=0.3663191.300.5523.71/30.95(3)確定污垢熱阻(4)計算總傳熱系數(shù)1bdodd經(jīng)計算=+Rso++1bdoddKoa入ddaidOmm=+0.000182561.2445171568598.5915(二)800m3/h(1)計算熱負(fù)荷hp(2)導(dǎo)熱油的量(2)平均溫度差R=12==11Δt(3)初選換熱器規(guī)格mJBT)：折流擋板間距B=300mm若采用這臺換熱器，要求過程的總傳系數(shù)為：m(3)管程壓強(qiáng)降管程平均通道面積Ai=0.0707m280i以管壁粗糙度ε為0.25mm，則ε/d==0.0167d20.01522(4)殼程阻力降ocB2N=BLh6=1=190.3OcooApuBD2p=(p'+p')FNo12ss(4)管程對流傳熱系數(shù)αi入故αi=0.023()Re0.8Pr0.33di(5)殼程對流傳熱系數(shù)αot0.025uo==3.665m/sPrp=23.7Prp=23.7=0.3644882.970.5523.71/30.95(6)確定污垢熱阻(4)計算總傳熱系數(shù)1bdodd經(jīng)計算=+Rso++1bdoddKoa入ddaidOmmKo=551(三)800m3/h，因殼程導(dǎo)熱油壓降大，放大一級(1)計算熱負(fù)荷hp(2)導(dǎo)熱油的量(2)平均溫度差R=12==11Δt(3)初選換熱器規(guī)格mJBT)：m(5)管程壓強(qiáng)降管程平均通道面積Ai=0.089m2ui==800i以管壁粗糙度ε為0.25mm，則ε/d==0.0167d20.01522(6)殼程阻力降ocB2nN=BLh4.5=1=143OcooApuBD2p=(p'+p')FNo12ss(7)管程對流傳熱系數(shù)αi入故αi=0.023()Re0.8Pr0.33di(8)殼程對流傳熱系數(shù)αot0.025uo==3.30m/ooPrp=23.7Prp=23.7=0.36404130.5523.71/30.95(9)確定污垢熱阻(4)計算總傳熱系數(shù)1bdodd經(jīng)計算=