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1、附录1 物料与能量衡算说明书1.1.1 环氧丙烷环氧化第一工段反应器R01001物料衡算丙烯、丙烷溶解在甲醇中与双氧水一起进入闪蒸罐提浓预热后进入R01001和R01002反应后经加料泵送入T0101和T0102精馏塔中进行粗提纯。R01001和R01002反应投料和反应条件相同。以R01001为例说明环氧丙烷环氧化第一工段反应器物料衡算如表1-1所示。环氧丙烷环氧化第一工段Aspend模拟示意图:图1-1 Aspend模拟示意图表1-1 环氧丙烷环氧化第一工段Aspend模拟图 C1-BOTC1-TOPFEED1R1-OUTSubstream: MIXED Solid Frac0.00 0.
2、00 0.00 0.00 Enthalpy kcal/mol-66.76 -21.34 -32.57 -38.05 Enthalpy kcal/kg-3377.22 -547.90 -1023.33 -1193.10 Enthalpy Gcal/hr-37.91 -20.81 -50.35 -58.70 Mole Flow kmol/hr C3H60.00 529.65 685.18 529.65 C3H80.00 42.40 42.40 42.40 C3H6O0.00 152.43 0.00 152.43 CH4O48.26 32.17 82.92 80.43 H2O509.93 218.5
3、4 573.55 728.47 H2O26.48 0.00 162.01 6.48 C4H10O22.49 0.00 0.00 2.49 C3H8O20.61 0.00 0.00 0.61 Mole Frac C3H60.00 0.54 0.44 0.34 C3H80.00 0.04 0.03 0.03 C3H6O0.00 0.16 0.00 0.10 CH4O0.08 0.03 0.05 0.05 H2O0.90 0.22 0.37 0.47 H2O20.01 0.00 0.10 0.00 C4H10O20.000.000.00 0.00 C3H8O20.00 0.00 0.00 0.00
4、Mass Flow kg/hr C3H60.00 22288.15 28832.96 22288.15 C3H80.00 1869.71 1869.71 1869.71 C3H6O0.00 8853.11 0.00 8853.11 CH4O1546.34 1030.89 2656.96 2577.23 H2O9186.46 3937.06 10332.63 13123.52 H2O2220.43 0.00 5510.74 220.43 C4H10O2224.27 0.00 0.00 224.27 C3H8O246.58 0.00 0.00 46.58 Mass Frac C3H60.00 0.
5、59 0.59 0.45 C3H80.00 0.05 0.04 0.04 C3H6O0.00 0.23 0.00 0.18 CH4O0.14 0.03 0.05 0.05 H2O0.82 0.10 0.21 0.27 H2O20.02 0.00 0.11 0.00 C4H10O20.02 0.00 0.00 0.00 C3H8O20.00 0.00 0.00 0.00 Total Flow kmol/hr567.77 975.20 1546.06 1542.96 Total Flow kg/hr11224.08 37978.92 49203.00 49203.00 Total Flow cum
6、/hr11.98 65.00 75.63 73.81 表1-2 环氧丙烷冷凝器出口物料表 C1-BOTC1-TOPFEED1R1-OUTSubstream: MIXED Solid Frac0.00 0.00 0.00 0.00 Enthalpy kcal/mol-66.76 -21.34 -32.57 -38.05 Enthalpy kcal/kg-3377.22 -547.90 -1023.33 -1193.10 Enthalpy Gcal/hr-37.91 -20.81 -50.35 -58.70 Mole Flow kmol/hr C3H60.00 529.65 685.18 529.
7、65 C3H80.00 42.40 42.40 42.40 C3H6O0.00 152.43 0.00 152.43 CH4O48.26 32.17 82.92 80.43 H2O509.93 218.54 573.55 728.47 H2O26.48 0.00 162.01 6.48 C4H10O22.49 0.00 0.00 2.49 C3H8O20.61 0.00 0.00 0.61 Mole Frac C3H60.00 0.54 0.44 0.34 C3H80.00 0.04 0.03 0.03 C3H6O0.00 0.16 0.00 0.10 CH4O0.08 0.03 0.05 0
8、.05 H2O0.90 0.22 0.37 0.47 H2O20.01 0.00 0.10 0.00 C4H10O20.000.000.00 0.00 C3H8O20.00 0.00 0.00 0.00 Mass Flow kg/hr C3H60.00 22288.15 28832.96 22288.15 C3H80.00 1869.71 1869.71 1869.71 C3H6O0.00 8853.11 0.00 8853.11 CH4O1546.34 1030.89 2656.96 2577.23 H2O9186.46 3937.06 10332.63 13123.52 H2O2220.4
9、3 0.00 5510.74 220.43 C4H10O2224.27 0.00 0.00 224.27 C3H8O246.58 0.00 0.00 46.58 Mass Frac C3H60.00 0.59 0.59 0.45 C3H80.00 0.05 0.04 0.04 C3H6O0.00 0.23 0.00 0.18 CH4O0.14 0.03 0.05 0.05 H2O0.82 0.10 0.21 0.27 H2O20.02 0.00 0.11 0.00 C4H10O20.02 0.00 0.00 0.00 C3H8O20.000.000.000.00Total Flow kmol/
10、hr567.77975.201546.061542.96Total Flow kg/hr11224.0837978.9249203.0049203.00Total Flow cum/hr11.9865.0075.6373.811.1.2 环氧丙烷环氧化第二工段反应器R01003物料衡算由T0101和T0102粗精馏后的双氧水和丙烯、丙烷作为原料进入R01003反应后产物经加料泵P0103送入环氧丙烷精馏塔精馏。物料衡算表如R01003物料衡算1-4表所示。环氧丙烷环氧化第二工段Aspend模拟示意图：图1-2 环氧丙烷环氧化第二工段Aspend模拟表1-4 R01003物料衡算C3-BOTC3
11、-TOPFEED3R3-OUTTemperature50.0050.0060.0050.00Pressure bar1.001.001.001.00Vapor Frac0.000.870.570.54Liquid Frac1.000.130.430.46Solid Frac0.000.000.000.00Substream:MIXEDMole Flow kmol/hrC3H60.00132.41171.30132.41C3H80.0010.6010.6010.60C3H6O0.0038.110.0038.11CH4O12.068.0420.7320.11H2O127.4854.63143.39
12、182.12H2O21.620.0040.501.62C4H10O20.620.000.000.62C3H8O20.150.000.000.15Mole FracC3H60.000.540.440.34C3H80.000.040.030.03C3H6O0.000.160.000.10CH4O0.080.030.050.05H2O0.900.220.370.4H2O20.010.000.100.00C4H10O20.000.000.000.00C3H8O20.000.000.000.00Mass Flow kg/hrC3H60.005572.047208.245572.04C3H80.00467.43467.43467.43C3H6O0.002213.280.002213.28CH4O386.58257.72664.24644.31H2O2296.62984.262583.13280.88H2O255.110.001
