【《丙烯腈合成工艺热量衡算计算》1400字】

I丙烯腈合成工艺热量衡算计算目录TOC\o"1-3"\h\u6267丙烯腈合成工艺热量衡算计算 1311691.1反应器的物料衡算和热量衡算 155521.1.1反应器的物料衡算 1140371.1.2热量衡算 361431.2水吸收塔的物料衡算 4318431.3回收塔物料衡算 6303341.4乙腈塔物料衡算 755131.5AN精馏塔物料衡算 91.1反应器的物料衡算和热量衡算1.1.1反应器的物料衡算由Aspen模拟得到的数据可知，整个工艺流程丙烯腈产量42.95kmol/h，进入反应器的原料组成摩尔比为C3H6:NH3:O2:H2O=1:1.1:2.4:1.0，操作压力为100kpa，操作温度为470℃。图3-1Aspen模拟反应器表3-1反应器物料平衡表进出物流编号S1S2温度C110360压力bar11摩尔流量（kmol/hr）13221364质量流量（kg/hr）35558.309835558.3098体积流量（l/min）42064.849484020.3312C3H3N072C2H3N04CHN04H2O240484C3H6800NH3888O219258CO00CO2012H2SO400N2722722AMMS00NH4+01.53E-09H3O+01.87E-11NH2COO-01.19E-16HCO3-08.53E-14表3-1反应器物料平衡表OH-01.57E-09HSO4-00CO3-08.78E-21SO4-001.1.2热量衡算表3-2各物质的平均定压比热容CP/[kJ/(kg·k)]物质C3H6C3H8NH3O2N2H2OANCNACNCLCO2CP0～110℃1.8412.052.3010.9411.0461.8830～360℃2.6781.0132.6361.0041.0882.0081.8741.3401.9331.9661.1300～470℃2.9291.3472.9391.0461.1092.2092.0291.7242.102.1721.213∆H∆H∆H∆H=若热损失取∆H的6%，则需由浓相段换热装置取出的热量（即换热装置的热负荷）为Q=浓相段换热装置产生0.405Mpa的饱和蒸汽（饱和温度143℃）143℃饱和蒸汽焓isteam143℃饱和水焓：iH产生的蒸气量=稀相段热衡算求稀相段换热装置的热负荷及产生蒸汽量，以0℃气体为衡算基准进入稀相段的气体带入热为：Q离开稀相段的气体带出热为：Q若热损失为5%，稀相段的热负荷为：Q=稀相段换热装置产生0.405Mpa的饱和蒸汽，产生的蒸汽量=1.2水吸收塔的物料衡算图3-2Aspen模拟水洗塔表3-3水吸收塔的物料衡算进出物流编号12345温度（C）30304078.455960187.8052301压力（bar）11111摩尔流量（kmol/hr）1196.45651791361.999131240.06164132.939488质量流量（kg/hr）31995.9271851.8922035558.30932857.1233555.1006体积流量（l/min）32.77185460.476528940167.137536164.82664.36239889C3H3N96.5665066707261.270501110.7296006C2H3N35.99987512041.34E-441.99998751CHN0.097340647041.989184570.01081561H2O907.62838340.36481.999135374.915061100.884437C3H600000NH35.24E-1107.999111797.903117141.74E-10O20.02339487505857.99740070.00259942CO00000CO20.021729863011.999130411.99758560.00241443H2SO42.44E-078.6400.000148391.79E-06N20.1022148820722721.9886430.01135717AMMS00000NH4+0.8727038100.000880242.23E-1090.09695867H3O+77.3859273901.09E-091.98E-1078.56148829NH2COO-5.92E-2007.97E-0601.55E-20表3-3水吸收塔的物料衡算HCO3-2.40E-0900.000854836.15E-1182.14E-10OH-1.86E-1401.81E-0602.19E-13HSO4-77.25806815001.98E-1078.62118978CO3-9.32E-2006.82E-0602.81E-20SO4-0.500372297001.28E-1090.018637671.3回收塔物料衡算图3-4aspen模拟回收塔表3-4回收塔物料衡算进出物流编号S2S8S9S14温度（C）78.455963071.0066871.00668压力（bar）1111摩尔流量（kmol/hr）1240.0616446799.777447486.243571质量流量（kg/hr）32857.1232828.7028822740.544910945.2812体积流量（l/min）36164.82660.8385986122881.265211.1282732表3-4回收塔物料衡算C3H3N10.72960060061.2705011C2H3N1.99998751000CHN0.01081561001.98918457H2O100.88443745.99999980420.874434C3H60000NH31.74E-1007.847977990.0142099O20.00259942057.99740070CO0000CO20.00241443011.94342510.01353652H2SO41.79E-06001.29E-21N20.011357170721.9886430AMMS0000NH4+0.09695867000.04092582H3O+8.561488299.99E-0801.82E-06NH2COO-1.55E-20001.42E-06HCO3-2.14E-10000.04061431OH-2.19E-139.99E-0802.64E-06HSO4-8.62118978001.25E-08CO3-2.81E-20006.26E-06SO4-0.01863767000.000148361.4乙腈塔物料衡算图3-5aspen模拟乙腈塔表3-5乙腈塔物料衡算进出物流编号S14S11S12温度（C）71.0066851.7421298.67365压力（bar）111摩尔流量（kmol/hr）486.243649.52541436.7316质量流量（kg/hr）10945.282507.1278438.154体积流量（l/min）11.128271.2847039.62239C3H3N61.270544.9986216.27188C2H3N000CHN1.9891851.9891851.97E-19H2O420.87440.443456420.4592C3H6000NH30.014210.0126975.46E-05O2000表3-5乙腈塔物料衡算CO000CO20.0135370.0269374.75E-25H2SO41.29E-214.95E-291.03E-18N2000AMMS000NH4+0.0409260.0272970.000275H3O+1.82E-061.07E-102.27E-05NH2COO-1.42E-060.0148164.37E-28HCO3-0.0406140.0123354.37E-28OH-2.64E-065.21E-081.35E-06HSO4-1.25E-084.95E-294.83E-07CO3-6.26E-067.32E-051.13E-21SO4-0.0001484.95E-290.0001481.5AN精馏塔物料衡算图3-4aspen模拟丙烯腈精馏塔表3-6AN精馏塔物料衡算进出物流编号S11S29S28温度（C）51.7421277.11247-5.4022压力（bar）111摩尔流量（kmol/hr）49.5254145.401844.150795质量流量（kg/hr）2507.1272391.51111.617体积流量（l/min）1.2847031.2463310.156535C3H3N44.9986244.953620.044999C2H3N000CHN1.9891850.0039891.985195H2O0.4434560.4442330.011631C3H6000NH30.0126976.