換熱器總傳熱系數(shù)經(jīng)驗值薈萃

1、各各種種換換熱熱器器的的總總傳傳熱熱系系數(shù)數(shù),引引自自Fundamentals of Heat Exchanger Design,Copyright 2003 by John Wiley & Sons, Inc.冷側(cè)流體總總傳傳熱熱系系數(shù)數(shù)熱側(cè)流體低壓氣體中壓氣體高壓氣體工藝水1Bar20Bar150Bar低壓氣體1BarU(W/m2K)5593120102中壓氣體20BarU(W/m2K)93300350429高壓氣體150BarU(W/m2K)120350400600經(jīng)過處理的冷卻水U(W/m2K)105484600938低粘度有機液體U(W/m2K)99375450600高粘度液

2、體U(W/m2K)68138200161水,沸騰U(W/m2K)105467550875有機液體,沸騰U(W/m2K)99375450600低粘度有機液體高粘度流體蒸汽凝液烴類冷凝有惰性氣體的烴類冷凝9963107100863751205303882404502006004003007141421607764345500130818524286153821731551246771401432722336500130818524286各各種種換換熱熱器器的的總總傳傳熱熱系系數(shù)數(shù),引引自自Fundamentals of Heat Exchanger Design,Copyright 2003 by

3、 John Wiley & Sons, Inc.熱側(cè)流體各各種種換換熱熱器器的的總總傳傳熱熱系系數(shù)數(shù),引引自自Fundamentals of Heat Exchanger Design,Copyright 2003 by John Wiley & Sons, Inc.冷冷側(cè)側(cè)流流體體熱負荷/溫差單單位位傳傳熱熱體體積積成成本本熱側(cè)流體q/T,低壓氣體中壓氣體高壓氣體工藝水(W/K)1Bar20Bar150Bar低低壓壓氣氣體體1Bar一一千千(1,000)C(/W/K)5.705.025.514.93五五千千(5,000)2.111.632.261.58三三萬萬(30,000)

4、1.110.761.060.73十十萬萬(100,000)0.950.580.930.54中中壓壓氣氣體體20Bar一一千千(1,000)C(/W/K)5.024.184.814.03五五千千(5,000)1.631.111.891.02三三萬萬(30,000)0.760.370.620.28十十萬萬(100,000)0.580.230.350.18高高壓壓氣氣體體150Bar一一千千(1,000)C(/W/K)5.514.816.254.56五五千千(5,000)2.261.892.251.10三三萬萬(30,000)1.060.620.940.40十十萬萬(100,000)0.930.35

5、0.580.24經(jīng)經(jīng)過過處處理理的的冷冷卻卻水水一一千千(1,000)C(/W/K)4.893.984.563.77五五千千(5,000)1.561.001.100.88三三萬萬(30,000)0.410.290.400.23十十萬萬(100,000)0.520.170.240.116低低粘粘度度有有機機液液體體一一千千(1,000)C(/W/K)4.964.094.383.91五五千千(5,000)1.591.051.460.95三三萬萬(30,000)0.740.330.530.27十十萬萬(100,000)0.550.200.280.145高高粘粘度度液液體體一一千千(1,000)C(/

6、W/K)5.394.615.504.46五五千千(5,000)1.861.431.931.36三三萬萬(30,000)0.940.570.730.52十十萬萬(100,000)0.770.420.640.37水水,沸沸騰騰一一千千(1,000)C(/W/K)4.893.994.913.79五五千千(5,000)1.561.001.200.88三三萬萬(30,000)0.710.290.490.23十十萬萬(100,000)0.520.1680.260.121有有機機液液體體,沸沸騰騰一一千千(1,000)C(/W/K)4.964.094.383.91五五千千(5,000)1.591.051.4

7、60.95三三萬萬(30,000)0.740.330.530.27十十萬萬(100,000)0.550.200.280.146對于熱負荷/溫差的值在q/Tm1和q/Tm2之間的情況,其單位傳熱體積成本CUA的計算使用下列的對數(shù)插值法求得 )/()/ln()/()/ln()/ln(expln2112,1 ,1 ,mmmmUAUAUAUATqTqTqTqCCCCDDDD+=低粘度有機液體高粘度流體蒸汽凝液烴類冷凝有惰性氣體的烴類冷凝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各各種種換換熱熱器器的的總總傳傳熱熱系系數(shù)數(shù),引引自自Funda

10、mentals of Heat Exchanger Design,Copyright 2003 by John Wiley & Sons, Inc.熱側(cè)流體對于熱負荷/溫差的值在q/Tm1和q/Tm2之間的情況,其單位傳熱體積成本CUA的計算使用下列的對數(shù)插值法求得各各種種換換熱熱器器的的總總傳傳熱熱系系數(shù)數(shù)以以及及每每單單位位傳傳熱熱體體積積成成本本,引引自自Fundamentals of Heat Exchanger Design,Copyright 2003 by John Wiley & Sons, Inc.熱負荷/溫差冷側(cè)流體參數(shù)熱側(cè)流體q/T,低壓氣體中壓氣體高壓氣

11、體工藝水(W/K)1Bar20Bar150Bar1,000低壓氣體U(W/m2K)55931201021BarC(/W/K)5.705.025.514.93中壓氣體U(W/m2K)9330035042920BarC(/W/K)5.024.184.814.03高壓氣體U(W/m2K)120350400600150BarC(/W/K)5.514.816.254.56經(jīng)過處理的冷卻水U(W/m2K)105484600938C(/W/K)4.893.984.563.77低粘度有機液體U(W/m2K)99375450600C(/W/K)4.964.094.383.91高粘度液體U(W/m2K)68138

12、200161C(/W/K)5.394.615.504.46水,沸騰U(W/m2K)105467550875C(/W/K)4.893.994.913.79有機液體,沸騰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.對于熱負荷/溫差的值在q/Tm1和q/Tm2之間的情況,其單位傳熱體積成本CUA的計算使用下列的對數(shù)插值法求得 )/()/ln

13、()/()/ln()/ln(expln2112,1 ,1 ,mmmmUAUAUAUATqTqTqTqCCCCDDDD+=低粘度有機液體高粘度流體蒸汽凝液烴類冷凝有惰性氣體的烴類冷凝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各各種種換換熱熱器器的的總總傳傳熱熱系系數(shù)數(shù)以以及及每每單單位位傳傳熱熱體體積積成成本本,引引自自Fundamentals of Heat Exchanger Design,Copyright 2003 by John Wiley & Sons, Inc.熱側(cè)流體Source: Selection and Costing of Heat Exchangers, ESDU Engineering Data 92013, ESDU Internationa

15、l, London, 1994.對于熱負荷/溫差的值在q/Tm1和q/Tm2之間的情況,其單位傳熱體積成本CUA的計算使用下列的對數(shù)插值法求得各各種種換換熱熱器器的的總總傳傳熱熱系系數(shù)數(shù)以以及及每每單單位位傳傳熱熱體體積積成成本本,引引自自Fundamentals of Heat Exchanger Design,Copyright 2003 by John Wiley & Sons, Inc.熱負荷/溫差冷側(cè)流體參數(shù)熱側(cè)流體q/T,低壓氣體中壓氣體高壓氣體工藝水(W/K)1Bar20Bar150Bar5,000低壓氣體U(W/m2K)55931201021BarC(/W/K)2.11

16、1.632.261.58中壓氣體U(W/m2K)9330035042920BarC(/W/K)1.631.111.891.02高壓氣體U(W/m2K)120350400600150BarC(/W/K)2.261.892.251.10經(jīng)過處理的冷卻水U(W/m2K)105484600938C(/W/K)1.561.001.100.88低粘度有機液體U(W/m2K)99375450600C(/W/K)1.591.051.460.95高粘度液體U(W/m2K)68138200161C(/W/K)1.861.431.931.36水,沸騰U(W/m2K)105467550875C(/W/K)1.561.

17、001.200.88有機液體,沸騰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.對于熱負荷/溫差的值在q/Tm1和q/Tm2之間的情況,其單位傳熱體積成本CUA的計算使用下列的對數(shù)插值法求得 )/()/ln()/()/ln()/ln(expln2112,1 ,1 ,mmmmUAUAUAUATqTqTqTqCCCCDDDD+=低粘度有機液

18、體高粘度流體蒸汽凝液烴類冷凝有惰性氣體的烴類冷凝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各各種種換換熱熱器器的的總總傳傳熱熱系系數(shù)數(shù)以以及及每每單單位位傳傳熱熱體體積積成成本本,引引自自Fundamentals of Heat Exchanger Design,Copyright 2003 by John Wiley & Sons, Inc.熱側(cè)流體Source: Selection and Costing of Heat Exchangers, ESDU Engineering Data 92013, ESDU International, London, 1994.對于熱負荷/溫差的值在q/Tm1和q/Tm2之間的情況,其單位傳熱體積成本CUA的計算使用下列的對數(shù)

20、插值法求得各各種種換換熱熱器器的的總總傳傳熱熱系系數(shù)數(shù)以以及及每每單單位位傳傳熱熱體體積積成成本本,引引自自Fundamentals of Heat Exchanger Design,Copyright 2003 by John Wiley & Sons, Inc.熱負荷/溫差冷側(cè)流體參數(shù)熱側(cè)流體q/T,低壓氣體中壓氣體高壓氣體工藝水(W/K)1Bar20Bar150Bar30,000低壓氣體U(W/m2K)55931201021BarC(/W/K)1.110.761.060.73中壓氣體U(W/m2K)9330035042920BarC(/W/K)0.760.370.620.28高壓

21、氣體U(W/m2K)120350400600150BarC(/W/K)1.060.620.940.40經(jīng)過處理的冷卻水U(W/m2K)105484600938C(/W/K)0.410.290.400.23低粘度有機液體U(W/m2K)99375450600C(/W/K)0.740.330.530.27高粘度液體U(W/m2K)68138200161C(/W/K)0.940.570.730.52水,沸騰U(W/m2K)105467550875C(/W/K)0.710.290.490.23有機液體,沸騰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.對于熱負荷/溫差的值在q/Tm1和q/Tm2之間的情況,其單位傳熱體積成本CUA的計算使用下列的對數(shù)插值法求得 )/()/ln()/()/ln()/ln(expln2112,1 ,1 ,mmmmUAUAUAUATqTqTqTqCCCCDDDD+=低粘度有機液體高粘度流體蒸汽凝液烴類冷凝有惰性氣體的烴類冷凝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各各種種換換熱熱器器的的總總傳傳熱熱系系數(shù)數(shù)以以及及每每單單位位傳傳熱熱體體積積成成本本,引引自自Fundamentals o

24、f Heat Exchanger Design,Copyright 2003 by John Wiley & Sons, Inc.熱側(cè)流體Source: Selection and Costing of Heat Exchangers, ESDU Engineering Data 92013, ESDU International, London, 1994.對于熱負荷/溫差的值在q/Tm1和q/Tm2之間的情況,其單位傳熱體積成本CUA的計算使用下列的對數(shù)插值法求得各各種種換換熱熱器器的的總總傳傳熱熱系系數(shù)數(shù)以以及及每每單單位位傳傳熱熱體體積積成成本本,引引自自Fundamental

25、s of Heat Exchanger Design,Copyright 2003 by John Wiley & Sons, Inc.熱負荷/溫差冷側(cè)流體參數(shù)熱側(cè)流體q/T,低壓氣體中壓氣體高壓氣體工藝水(W/K)1Bar20Bar150Bar100,000低壓氣體U(W/m2K)55931201021BarC(/W/K)0.950.580.930.54中壓氣體U(W/m2K)9330035042920BarC(/W/K)0.580.230.350.18高壓氣體U(W/m2K)120350400600150BarC(/W/K)0.930.350.580.24經(jīng)過處理的冷卻水U(W/m2K)105484600938C(/W/K)0.520.170.240.116低粘度有機液體U(W/m2K)99375450600C(/W/K)0.550.200.280.145高粘度液體U(W/m2K)68138200161C(/W/K)0.770.420.640.37水,沸騰U(W/m2K)105467550875C(/W/K)0.520.1680.260.121有機液體,沸騰U(W/m2K)99375450600C(/W/K)0.550.200.280.14