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宁波工程学院毕业设计（论文）

统内部积累起来的物料的量。进行物料衡算时，首先必须确定衡算的体系，对一般体系，均可表示为：输入量＝输出量＋积累量

对于有化学反应的系统，可表示为：物料输入量=物料输出量－生产量+物料消耗量－积累量

当系统处于稳定状态时为：物料输入量=物料输出量

表4-2 反应工段物料平衡状况 Temperature C Pressure bar Vapor Frac Mole Flow kmol/hr Mass Flow kg/hr Volume Flow cum/hr Enthalpy MMkcal/hr IN(FEED) 30 1.013 0 233.966 10000 12.903 -15.535 500 9500 0 0 0 0.05 0.95 0 0 0 27.754 206.212 0 0 0 0.119 0.881 0 0 0 21

OUT(H2) 30 1.013 1 177.221 2323.504 4406.084 -2.581 70.183 402.401 1554.697 0 296.223 0.03 0.173 0.669 0 0.127 3.896 8.735 17.646 0 146.945 0.022 0.049 0.1 0 0.829 OUT(F12) 30 1.013 0 130.218 7676.496 8.881 -11.343 429.817 2328.003 4918.677 0 0 0.056 0.303 0.641 0 0 23.858 50.533 55.827 0 0 0.183 0.388 0.429 0 0 Mass Flow kg/hr WATER ETOH EA HAC H2 Mass Frac WATER ETOH EA HAC H2 Mole Flow kmol/hr WATER ETOH EA HAC H2 Mole Frac WATER ETOH EA HAC H2 宁波工程学院毕业设计（论文）

表4-3 分离工段物料衡算 IN Temperature C Pressure bar Vapor Frac Mole Flow kmol/hr Mass Flow kg/hr Volume Flow cum/hr Enthalpy MMkcal/hr Mass Flow kg/hr WATER ETOH EA GLYCEROL Mass Frac WATER ETOH EA GLYCEROL Mole Flow kmol/hr WATER ETOH EA GLYCEROL Mole Frac WATER ETOH EA GLYCEROL 0.183 0.388 0.429 0 0.184 0.142 0.674 0 0 0 0 1 0 0 0 1 23.858 50.533 55.827 0 7.292 5.636 26.734 0 0 0 0 128 0 0 0 30 0.056 0.303 0.641 0 0.048 0.095 0.858 0 0 0 0 1 0 0 0 1 429.817 2328.003 4918.677 0 131.367 259.645 2355.434 0 0 0 0 11788.124 0 0 0 2762.842 F12 30 1.013 0 130.218 7676.496 8.881 -11.343 FROM-H2 30 1.013 0 39.662 2746.447 3.06 -3.925 EXTRA-1 60 1.013 0 128 11788.124 9.317 -20.201 EXTRA-2 77.3 1.013 0 30 2762.842 2.209 -4.709 OUT Temperature C Pressure bar Vapor Frac Mole Flow kmol/hr PRODUCT 77 1.013 1 81 D5 76.5 1.013 1 22.101 WATER 193.4 0.861 1 26.779 W5 77.8 1.013 0 40 E-4 262.7 0.861 0 158 22

宁波工程学院毕业设计（论文）

Mass Flow kg/hr 7103.913 Volume Flow cum/hr 2263.171 Enthalpy MMkcal/hr WATER ETOH GLYCEROL Mass Frac WATER ETOH EA GLYCEROL Mole Flow kmol/hr WATER ETOH EA GLYCEROL Mole Frac WATER ETOH EA GLYCEROL

0 0.01 0.99 0 0 0.778 80.222 0 0 0.005 0.995 0 -8.445 0.002 35.827 0 Mass Flow kg/hr 1053.349 623.43 -1.33 34.403 832.893 186.053 0 0.033 0.791 0.177 0 1.91 18.079 2.112 0 0.086 0.818 0.096 0 603.153 1201.348 -1.607 443.746 38.424 0.011 120.971 0.736 0.064 0 0.201 24.632 0.834 0 1.314 0.92 0.031 0 0.049 1758.509 2.453 -2.603 60.221 1678.326 19.963 0 0.034 0.954 0.011 0 3.343 36.431 0.227 0 0.084 0.911 0.006 0 14454.99 13.382 -22.997 22.812 2.178 0 14430 0.002 0 0 0.998 1.266 0.047 0 156.686 0.008 0 0 0.992 EA 7068.084 表4-4 总物料平衡图

IN Temperature C Pressure bar Vapor Frac Mole Flow kmol/hr Mass Flow kg/hr Volume Flow cum/hr Enthalpy MMkcal/hr Mass Flow kg/hr WATER ETOH EA H2 GLYCEROL 500 9500 0 0 0 23

FEED 30 1.013 0 233.966 10000 12.903 -15.535 EXTRA-1 60 1.013 0 128 11788.12 9.317 -20.201 0 0 0 0 11788.12 EXTRA-2 77.3 1.013 0 30 2762.842 2.209 -4.709 0 0 0 0 2762.842 宁波工程学院毕业设计（论文）

Mass Frac WATER ETOH EA H2 GLYCEROL Mole Flow kmol/hr WATER ETOH EA H2 GLYCEROL Mole Frac WATER ETOH EA H2 GLYCEROL 0.119 0.881 0 0 0 0 0 0 0 1 0 0 0 0 1 27.754 206.212 0 0 0 0 0 0 0 128 0 0 0 0 30 0.05 0.95 0 0 0 0 0 0 0 1 0 0 0 0 1 OUT PRODUCT 77 1 H2 30 1.013 1 146.945 296.223 3406.084 -2.581 0 0 0 296.223 0 0 0 0 1 24

D5 76.5 1.013 1 22.101 1053.349 623.43 -1.33 34.403 832.893 186.053 0 0 0.033 0.791 0.177 0 W5 77.8 1.013 0 40 1758.509 2.453 -2.603 60.221 1678.326 19.963 0 0 0.034 0.954 0.011 0 E-4 262.7 0.861 0 158 14454.99 13.382 -22.997 22.812 2.178 0 0 14430 0.002 0 0 0 WATER 193.4 0.861 1 26.779 603.153 1201.348 -1.607 443.746 38.424 0.011 0 120.971 0.736 0.064 0 0 Temperature C Vapor Frac Pressure bar 1.013 Mole Flow kmol/hr 81 Mass Flow kg/hr 7 103.913 Volume Flow cum/hr 2 263.171 Enthalpy MMkcal/hr -8.445 Mass Flow kg/hr WATER 0.002 ETOH 35.827 EA 7068.084 H2 GLYCEROL WATER 0 0 0 Mass Frac ETOH 0.005 EA 0.995 H2 0