【生物乙醇法制醋酸乙烯的工艺计算案例3100字】

生物乙醇法制醋酸乙烯的工艺计算案例目录TOC\o"1-3"\h\u14619生物乙醇法制醋酸乙烯的工艺计算案例 1129741.1醋酸乙烯合成工段 1204331.2物料衡算 1311731.3能量衡算 5232931.3.1换热器热量衡算 6124281.3.2泵热量衡算 8166171.3.3反应器热量衡算 998931.3.4塔热量衡算 1049061.3.5气液分离器热量衡算 121.1醋酸乙烯合成工段图2醋酸乙烯合成工段1.2物料衡算物料衡算是根据质量守恒定律，利用某进出化工过程中某些系统中的积累，系统中的积累=输入-输出+生产-消耗式中，生成或消耗项是由于化学反应而生成或消耗的量；积累量可以是正值，也可以是负值，当系统中积累量不为零时称为非稳定状态过程；积累量为零时，称为稳定状态过程。稳定状态过程时，可以简化为：输入=输出-生成+消耗对无化学反应的稳定过程可表示为：输入=输出本设计采用AspenPlus软件进行模拟。表5醋酸乙烯合成工段总物料衡算表进出口进口出口流股信息循环乙烯乙醇胺醋酸液醋酸液醋酸液精制乙烯精制二氧化碳贫液流股编号S0453MEAS0401S0402S0319GASC2H4GASCO2S0331相态液相液相液相液相气相气相温度℃6.464049.8541.1490-5.006075.96压力（巴）101.225.988.8910.1310.131.22摩尔气相分数00000110摩尔流率（kmol/hr）100417.511221.6497.136.111886.0915.03420.5质量流率（kg/hr）5970.79917.6866919.096002.76338.6152902.69653.0610151.3体积流率（cum/hr）5.4513.0969.895.990.433800.3839.5522.59质量流率（kg/hr）H200000000CO00000.03000CO20025.790.1300.18647.0110.43H2O15.56579.883635.68167.44016.895.846576.43CH4O00000000C2H6O00000000C2H405.781943.841.50052885.620.215.75C2H600000000C2H4O0069.9411.69128.96000C3H600000000C4H10O00000.000.0000C4+00000000YWC00000000CH400000.26000NAOH00000000H3O+00000000HCO3-00.88000000.19Na+00000000OH-00.09000000.2Na2CO300000000CO3-202.68000000.04NaHCO300000000N200000000HAC5952.48047838.383919.6366.56000VAC0012653.81853.8567.8000MEA02848.31000002899.2C2H6O200000000C3H4O00130.5418.4760.16000C3H6O200179.4826.6611.83000C2H4O-200000000C6H10O42.720441.643.370000C4H6O200000000MEAH+013900000203.35MEACOO-0221.8900000339.56MDEA0118.8600000118.77MDEAH+00.3000000.39O200000000C4H8O200000000GY00000000ADIPO-0100000000C4H1000000000C5H1200000000H200000000CO00000000CO200000000H2O0000000.990CH4O00.660.050.03000.010.65C2H6O00000000C2H400000000C2H6000.03001.0000C2H4O00000000C3H600000.38000C4H10O00000000C4+00000000YWC00000000CH400000000NAOH00000000H3O+00000000HCO3-00000000Na+00000000OH-00000000Na2CO300000000CO3-200000000NaHCO300000000N200000000HAC00000000VAC100.710.650.20000MEA000.190.310.2000C2H6O200.29000000.29C3H4O00000000C3H6O200000.18000C2H4O-200000.04000C6H10O400000000C4H6O2000.0100000MEAH+00000000MEACOO-00.01000000.02MDEA00.02000000.03MDEAH+00.01000000.01O200000000C4H8O200000000GY00000000ADIPO-0100000000C4H1000000000C5H1200000000H2000000001.3能量衡算主要依据是热量平衡方程：其中，——输入热量的总和——输出热量的总和——损失热量的总和对于连续系统：其中，——设备的热负荷——输入系统的机械能——离开的各物料焓之和——进入的各物料焓之和1.3.1换热器热量衡算（1）反应进料加热器表2热负荷表WQ热负荷（Gcal/hr）00.0994表3流股焓变计算表输入输出物流编号O2INS0304温度（℃）25149.85压力（bar）11气相分率11摩尔流率（kmol/hr）112112质量流率（kg/hr）3583.86563583.8656体积流率（cum/hr）2776.38763938.997焓（Gcal/hr）00.0994表4热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error00.099400.09940（2）反应进料加热器表5热负荷表WQ热负荷（Gcal/hr）010.5267表6流股焓变计算表InOut物流编号S0302S0303温度（℃）32.1427149.85压力（bar）16.6875气相分率0.68921摩尔流率（kmol/hr）3086.93623086.9362质量流率（kg/hr）118360.356118360.356体积流率（cum/hr）54052.936816231.3434焓（Gcal/hr）-83.2967-72.77表7热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error010.5267-83.2967-72.77000（3）朗肯循环冷却器表8热负荷表WQ热负荷（Gcal/hr）0-1.3804表9流股焓变计算表输入输出物流编号S0313S0314温度（℃）6.5268-0.8784压力（bar）11气相分率10摩尔流率（kmol/hr）250250质量流率（kg/hr）14530.8514530.85体积流率（cum/hr）5813.313821.0962焓（Gcal/hr）-7.6176-8.998表10热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0-1.3804-7.6176-8.9980（4）冷却器表11热负荷表WQ热负荷（Gcal/hr）01.7514表12流股焓变计算表InOut物流编号S0316S0317温度（℃）590压力（bar）99气相分率11摩尔流率（kmol/hr）1907.3111907.311质量流率（kg/hr）53929.709153929.7091体积流率（cum/hr）4901.00716398.7083焓（Gcal/hr）21.419523.1709表13热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error01.751421.419523.170901.3.2泵热量衡算表14热负荷表WQ热负荷（Gcal/hr）0.00110表15流股焓变计算表InOut物流编号S0314S0311温度（℃）-0.8784-0.7559压力（bar）12气相分率00摩尔流率（kmol/hr）250250质量流率（kg/hr）14530.8514530.85体积流率（cum/hr）21.096221.1015焓（Gcal/hr）-8.998-8.9969表16热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0.00110-8.998-8.996901.3.3反应器热量衡算表17热负荷表WQ热负荷（Gcal/hr）0-7.2366表18流股焓变计算表输入输出物流编号S0306S0307温度（℃）159.85181.85压力（bar）6.68756.6875气相分率11摩尔流率（kmol/hr）3191.33743107.9339质量流率（kg/hr）121941.2216121945.3855体积流率（cum/hr）17196.31517581.2554焓（Gcal/hr）-73.7091-80.9457表19热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0-7.2366-73.7091-80.94570.1.3.4塔热量衡算（1）醋酸洗塔表20热负荷表WQ热负荷（Gcal/hr）00表21流股焓变计算表输入输出物流编号S0452S0310S0315S0402温度（℃）533.712663.032341.1405压力（bar）3108.88.8气相分率00.983410摩尔流率（kmol/hr）100.00001883.29491886.162397.1326质量流率（kg/hr）5970.696755026.292154991.23056002.7583体积流率（cum/hr）5.44554727.00865740.02265.9912焓（Gcal/hr）-10.923317.209816.2728-9.9835表22热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error006.296.290（2）二氧化碳吸收塔表23热负荷表WQ热负荷（Gcal/hr）00表24流股焓变计算表输入输出物流编号S0318MEAS0320S0321温度（℃）904040.289443.0993压力（bar）91.21591.01331.2132气相分率10.000510摩尔分率（kmol/hr）1901.1971417.50962013.5961289.0974质量流率（kg/hr）53591.10089917.678955208.66148300.1183体积流率（cum/hr）6378.19713.089951508.72058.5063焓（Gcal/hr）23.4985-28.566716.5369-21.6051表25热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error00-5.0682-5.0681-0.0001（3）二氧化碳解吸塔表26热负荷表WQ热负荷（Gcal/hr）01.2704表27流股焓变计算表输入输出物流编号S0322S0323S0324温度（℃）9095.4987116.1089压力（bar）1.21321.01331.2159气相分率010摩尔流率（kmol/hr）289.0974100201.0354质量流率（kg/hr）8300.11832189.92346110.1945体积流率（cum/hr）8.76483005.18465.6252焓（Gcal/hr）-21.3244-6.2596-13.7944表28热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error01.2704-21.3244-20.054001.3.5气液分离器热量衡算（1）反应出料气液分离器表29热负荷表WQ热负荷（Gcal/hr）0-13.8917表30流股焓变计算表输入输出物流编号S0309S0310S0311温度（℃）181.8549.8549.85压力（bar）6.68755.97825.9782气相分率110摩尔流率（kmol/hr）3107.93391883.29491221.639质量流率（kg/hr）121945.385555026.292166919.0934体积流率（cum/hr）17581.25548460.177669.8941焓（Gcal/hr）-80.945717.7406-112.578表31热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0-13.8917-80.9457-91.83740（2）气液分离器表32热负荷表WQ热负荷（Gcal/hr）0-1.1015表33流股焓变计算表输入输出物流编号S0315S0407S0403S0316温度（℃）63.0323555压力（bar）8.80.01699气相流率1101摩尔流率（kmol/hr）1886.162376.381455.23271907.3110质量流率（kg/hr）54991.23052305.04953369.570953929.7091体积流率（cum/hr）5740.0226110401.24083.15564901.0071焓（Gcal/hr）16.27280.5609-5.687321.4195表34热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0-1.101516.833715.73