换热器总传热系数经验值荟萃

1、各各种种换换热热器器的的总总传传热热系系数数,引引自自Fundamentals of Heat Exchanger Design,Copyright 2003 by John Wiley & Sons, Inc.冷侧流体总总传传热热系系数数热侧流体低压气体中压气体高压气体工艺水1Bar20Bar150Bar低压气体1BarU(W/m2K)5593120102中压气体20BarU(W/m2K)93300350429高压气体150BarU(W/m2K)120350400600经过处理的冷却水U(W/m2K)105484600938低粘度有机液体U(W/m2K)99375450600高粘度液

2、体U(W/m2K)68138200161水,沸腾U(W/m2K)105467550875有机液体,沸腾U(W/m2K)99375450600低粘度有机液体高粘度流体蒸汽凝液烃类冷凝有惰性气体的烃类冷凝9963107100863751205303882404502006004003007141421607764345500130818524286153821731551246771401432722336500130818524286各各种种换换热热器器的的总总传传热热系系数数,引引自自Fundamentals of Heat Exchanger Design,Copyright 2003 by

3、 John Wiley & Sons, Inc.热侧流体各各种种换换热热器器的的总总传传热热系系数数,引引自自Fundamentals of Heat Exchanger Design,Copyright 2003 by John Wiley & Sons, Inc.冷冷侧侧流流体体热负荷/温差单单位位传传热热体体积积成成本本热侧流体q/T,低压气体中压气体高压气体工艺水(W/K)1Bar20Bar150Bar低低压压气气体体1Bar一一千千(1,000)C(/W/K)5.705.025.514.93五五千千(5,000)2.111.632.261.58三三万万(30,000)

4、1.110.761.060.73十十万万(100,000)0.950.580.930.54中中压压气气体体20Bar一一千千(1,000)C(/W/K)5.024.184.814.03五五千千(5,000)1.631.111.891.02三三万万(30,000)0.760.370.620.28十十万万(100,000)0.580.230.350.18高高压压气气体体150Bar一一千千(1,000)C(/W/K)5.514.816.254.56五五千千(5,000)2.261.892.251.10三三万万(30,000)1.060.620.940.40十十万万(100,000)0.930.35

5、0.580.24经经过过处处理理的的冷冷却却水水一一千千(1,000)C(/W/K)4.893.984.563.77五五千千(5,000)1.561.001.100.88三三万万(30,000)0.410.290.400.23十十万万(100,000)0.520.170.240.116低低粘粘度度有有机机液液体体一一千千(1,000)C(/W/K)4.964.094.383.91五五千千(5,000)1.591.051.460.95三三万万(30,000)0.740.330.530.27十十万万(100,000)0.550.200.280.145高高粘粘度度液液体体一一千千(1,000)C(/

6、W/K)5.394.615.504.46五五千千(5,000)1.861.431.931.36三三万万(30,000)0.940.570.730.52十十万万(100,000)0.770.420.640.37水水,沸沸腾腾一一千千(1,000)C(/W/K)4.893.994.913.79五五千千(5,000)1.561.001.200.88三三万万(30,000)0.710.290.490.23十十万万(100,000)0.520.1680.260.121有有机机液液体体,沸沸腾腾一一千千(1,000)C(/W/K)4.964.094.383.91五五千千(5,000)1.591.051.4

7、60.95三三万万(30,000)0.740.330.530.27十十万万(100,000)0.550.200.280.146对于热负荷/温差的值在q/Tm1和q/Tm2之间的情况,其单位传热体积成本CUA的计算使用下列的对数插值法求得 )/()/ln()/()/ln()/ln(expln2112,1 ,1 ,mmmmUAUAUAUATqTqTqTqCCCCDDDD+=低粘度有机液体高粘度流体蒸汽凝液烃类冷凝有惰性气体的烃类冷凝4.965.504.874.955.111.591.951.551.591.680.740.990.710.730.800.550.830.520.550.624.09

8、4.763.954.074.281.051.490.981.051.180.330.630.280.320.420.200.470.160.190.274.385.504.564.824.811.461.931.101.451.450.530.730.400.620.620.280.640.240.320.393.854.593.613.834.120.911.410.830.901.070.250.560.190.240.340.1340.410.0860.1290.213.974.673.813.954.200.991.460.890.981.130.380.590.240.280.380

9、.1620.440.1250.1580.244.515.164.424.504.331.381.711.321.371.480.530.830.500.530.600.380.650.350.380.453.874.603.643.854.130.931.420.840.911.080.250.560.200.250.350.1370.410.0910.1330.223.974.673.813.954.200.991.460.890.981.130.280.590.240.280.380.1620.440.1250.1580.24各各种种换换热热器器的的总总传传热热系系数数,引引自自Funda

10、mentals of Heat Exchanger Design,Copyright 2003 by John Wiley & Sons, Inc.热侧流体对于热负荷/温差的值在q/Tm1和q/Tm2之间的情况,其单位传热体积成本CUA的计算使用下列的对数插值法求得各各种种换换热热器器的的总总传传热热系系数数以以及及每每单单位位传传热热体体积积成成本本,引引自自Fundamentals of Heat Exchanger Design,Copyright 2003 by John Wiley & Sons, Inc.热负荷/温差冷侧流体参数热侧流体q/T,低压气体中压气体高压气

11、体工艺水(W/K)1Bar20Bar150Bar1,000低压气体U(W/m2K)55931201021BarC(/W/K)5.705.025.514.93中压气体U(W/m2K)9330035042920BarC(/W/K)5.024.184.814.03高压气体U(W/m2K)120350400600150BarC(/W/K)5.514.816.254.56经过处理的冷却水U(W/m2K)105484600938C(/W/K)4.893.984.563.77低粘度有机液体U(W/m2K)99375450600C(/W/K)4.964.094.383.91高粘度液体U(W/m2K)68138

12、200161C(/W/K)5.394.615.504.46水,沸腾U(W/m2K)105467550875C(/W/K)4.893.994.913.79有机液体,沸腾U(W/m2K)99375450600C(/W/K)4.964.094.383.91Source: Selection and Costing of Heat Exchangers, ESDU Engineering Data 92013, ESDU International, London, 1994.对于热负荷/温差的值在q/Tm1和q/Tm2之间的情况,其单位传热体积成本CUA的计算使用下列的对数插值法求得 )/()/ln

13、()/()/ln()/ln(expln2112,1 ,1 ,mmmmUAUAUAUATqTqTqTqCCCCDDDD+=低粘度有机液体高粘度流体蒸汽凝液烃类冷凝有惰性气体的烃类冷凝9963107100864.965.504.874.955.113751205303882404.094.763.954.074.284502006004003004.385.504.564.824.8171414216077643453.854.593.613.834.125001308185242863.974.673.813.954.20153821731551244.515.164.424.504.33677

14、14014327223363.874.603.643.854.135001308185242863.974.673.813.954.20各各种种换换热热器器的的总总传传热热系系数数以以及及每每单单位位传传热热体体积积成成本本,引引自自Fundamentals of Heat Exchanger Design,Copyright 2003 by John Wiley & Sons, Inc.热侧流体Source: Selection and Costing of Heat Exchangers, ESDU Engineering Data 92013, ESDU Internationa

15、l, London, 1994.对于热负荷/温差的值在q/Tm1和q/Tm2之间的情况,其单位传热体积成本CUA的计算使用下列的对数插值法求得各各种种换换热热器器的的总总传传热热系系数数以以及及每每单单位位传传热热体体积积成成本本,引引自自Fundamentals of Heat Exchanger Design,Copyright 2003 by John Wiley & Sons, Inc.热负荷/温差冷侧流体参数热侧流体q/T,低压气体中压气体高压气体工艺水(W/K)1Bar20Bar150Bar5,000低压气体U(W/m2K)55931201021BarC(/W/K)2.11

16、1.632.261.58中压气体U(W/m2K)9330035042920BarC(/W/K)1.631.111.891.02高压气体U(W/m2K)120350400600150BarC(/W/K)2.261.892.251.10经过处理的冷却水U(W/m2K)105484600938C(/W/K)1.561.001.100.88低粘度有机液体U(W/m2K)99375450600C(/W/K)1.591.051.460.95高粘度液体U(W/m2K)68138200161C(/W/K)1.861.431.931.36水,沸腾U(W/m2K)105467550875C(/W/K)1.561.

17、001.200.88有机液体,沸腾U(W/m2K)99375450600C(/W/K)1.591.051.460.95Source: Selection and Costing of Heat Exchangers, ESDU Engineering Data 92013, ESDU International, London, 1994.对于热负荷/温差的值在q/Tm1和q/Tm2之间的情况,其单位传热体积成本CUA的计算使用下列的对数插值法求得 )/()/ln()/()/ln()/ln(expln2112,1 ,1 ,mmmmUAUAUAUATqTqTqTqCCCCDDDD+=低粘度有机液

18、体高粘度流体蒸汽凝液烃类冷凝有惰性气体的烃类冷凝9963107100861.591.951.551.591.683751205303882401.051.490.981.051.184502006004003001.461.931.101.451.4572014216077643450.911.410.830.901.075001308185242860.991.460.890.981.13153821731551241.381.711.321.371.4867714014327223360.931.420.840.911.085001308185242860.991.460.890.981.

19、13各各种种换换热热器器的的总总传传热热系系数数以以及及每每单单位位传传热热体体积积成成本本,引引自自Fundamentals of Heat Exchanger Design,Copyright 2003 by John Wiley & Sons, Inc.热侧流体Source: Selection and Costing of Heat Exchangers, ESDU Engineering Data 92013, ESDU International, London, 1994.对于热负荷/温差的值在q/Tm1和q/Tm2之间的情况,其单位传热体积成本CUA的计算使用下列的对数

20、插值法求得各各种种换换热热器器的的总总传传热热系系数数以以及及每每单单位位传传热热体体积积成成本本,引引自自Fundamentals of Heat Exchanger Design,Copyright 2003 by John Wiley & Sons, Inc.热负荷/温差冷侧流体参数热侧流体q/T,低压气体中压气体高压气体工艺水(W/K)1Bar20Bar150Bar30,000低压气体U(W/m2K)55931201021BarC(/W/K)1.110.761.060.73中压气体U(W/m2K)9330035042920BarC(/W/K)0.760.370.620.28高压

21、气体U(W/m2K)120350400600150BarC(/W/K)1.060.620.940.40经过处理的冷却水U(W/m2K)105484600938C(/W/K)0.410.290.400.23低粘度有机液体U(W/m2K)99375450600C(/W/K)0.740.330.530.27高粘度液体U(W/m2K)68138200161C(/W/K)0.940.570.730.52水,沸腾U(W/m2K)105467550875C(/W/K)0.710.290.490.23有机液体,沸腾U(W/m2K)99375450600C(/W/K)0.740.330.530.27Source

22、: Selection and Costing of Heat Exchangers, ESDU Engineering Data 92013, ESDU International, London, 1994.对于热负荷/温差的值在q/Tm1和q/Tm2之间的情况,其单位传热体积成本CUA的计算使用下列的对数插值法求得 )/()/ln()/()/ln()/ln(expln2112,1 ,1 ,mmmmUAUAUAUATqTqTqTqCCCCDDDD+=低粘度有机液体高粘度流体蒸汽凝液烃类冷凝有惰性气体的烃类冷凝9963107100860.740.990.710.730.80375120530

23、3882400.330.630.280.320.424502006004003000.530.730.400.620.6271414216077643450.250.560.190.240.345001308185242860.380.590.240.280.38153821731551240.530.830.500.530.6067714014327223360.250.560.200.250.355001308185242860.280.590.240.280.38各各种种换换热热器器的的总总传传热热系系数数以以及及每每单单位位传传热热体体积积成成本本,引引自自Fundamentals o

24、f Heat Exchanger Design,Copyright 2003 by John Wiley & Sons, Inc.热侧流体Source: Selection and Costing of Heat Exchangers, ESDU Engineering Data 92013, ESDU International, London, 1994.对于热负荷/温差的值在q/Tm1和q/Tm2之间的情况,其单位传热体积成本CUA的计算使用下列的对数插值法求得各各种种换换热热器器的的总总传传热热系系数数以以及及每每单单位位传传热热体体积积成成本本,引引自自Fundamental

25、s of Heat Exchanger Design,Copyright 2003 by John Wiley & Sons, Inc.热负荷/温差冷侧流体参数热侧流体q/T,低压气体中压气体高压气体工艺水(W/K)1Bar20Bar150Bar100,000低压气体U(W/m2K)55931201021BarC(/W/K)0.950.580.930.54中压气体U(W/m2K)9330035042920BarC(/W/K)0.580.230.350.18高压气体U(W/m2K)120350400600150BarC(/W/K)0.930.350.580.24经过处理的冷却水U(W/m2K)105484600938C(/W/K)0.520.170.240.116低粘度有机液体U(W/m2K)99375450600C(/W/K)0.550.200.280.145高粘度液体U(W/m2K)68138200161C(/W/K)0.770.420.640.37水,沸腾U(W/m2K)105467550875C(/W/K)0.520.1680.260.121有机液体,沸腾U(W/m2K)99375450600C(/W/K)0.550.200.280.14