换热器电脑计算公式

T1T2t1755030①热负荷和冷却水流量定性温度/ºC密度ρ（kg/m³）苯62.5833.925循环水35994②两流体平均温度差平均传热温差Δtmˊ平均传热温差Δtm26.8041043925.14166809③总传热系数K（选用Ф25×2.5的碳钢管，管内流速取1.5m/s）ud。di1.050.0250.021/KK0.001978206800④计算传热面积考虑15%的面积裕度传热面积Sˊ/m²传热面积S/m²30.8514111235.5⑤工艺结构尺寸（选用Ф25×2.5传热管（碳钢），取管内流速ui=1.2m/s）单程传热管数ns传热管长度L换热器管程数Np49.47671159.0392669531.506544492502传热管排列和分程方法管心距t（焊接法）横过管束中心线的管数nc0.0312511.90.03212圆整取D/m0.4015968130.45折流板（采用弓形折流板，取弓形折流板圆缺高度为壳体内径的25%）圆缺高度h/m折流板间距B/m折流板数NB0.11250.135390.1250.15接管壳程流体进出口接管接管内苯流速u/m/s接管内径d1.60.117433527管程流体进出口接管循环水流速u/m/s接管内径d1.70.110560654核算1热量核算壳程对流传热系数克恩公式α。/W/(m·ºC)1077.532956当量直径de（正三角形排列）壳程流通截面积So/m²壳程流体流速uo0.0201877710.0132890631.303405368管程对流传热系数管程流通截面积Si/m²管程流体流速ui雷诺数Rei0.0194680.8379120544869.202811/K传热系数K0.001846137541.6716433传热面积S/m²实际传热面积Sp换热器的面积裕度48.5776086251.87286.8%换热器内流体的流动阻力管程流动阻力FtNp管程流通面积Ai/m²1.420.019468ΣΔPj/PaΔP1/PaΔP2/Pa12896.896753559.2085181046.826035壳程阻力NsFsF11.150.5ΣΔP。/PaΔP1ˊ/PaΔP2ˊ/Pa6979.7622893526.2471882543.111324t2PRR²+1的平方根400.2222222222.52.692582404粘度μ（Pa·s）比热容Cp/KJ/(kg·ºC)导热系数λ/W/(m·ºC)流量W/kg/h0.000371251.8320.129925520000.0007254.080.62558372.5490214.44444444173991.7593dmReαi/W/(m·ºC)α。/W/(m·ºC)0.022528791.724144943.5537071000传热管的总根数N折流的平均温度差Δtm传热管长l/m12425.141668096100b壳程内径D/m0.0250.402标准管径内径矫正流速133*60.1211.507070094标准管径内径矫正流速133*60.1211.419316907雷诺数Reo普兰特准数Pr黏度校正30266.128415.2347893020.910554581普兰特准数Prαi/W/(m·ºC)4.73287049.913712传热系数K。415507.2622476.8%1.3052328751.067833545ui雷诺数Rei相对粗糙度ε/dλi/W/(m·ºC)0.8379120522976.126270.0050.034雷诺数Re。f。折流挡板间距h/mNB21615.330260.4756766550.319ψΔtR+10.9379782933.51.8205738670.623870577热流量Q/KW冷却水用量Ω/kg/h661.555658372.54902238160016.21459695261335.6753Rsi/m²·℃/WRso/m²·℃/W管壁的导热系数λ/W/(m·℃)0.000343940.00017197450.000343940.00017197污垢热阻A。/m²u。0.0450.384911898