6-1、附录一物料平衡计算书

“东华科技-恒逸石化杯”第十三届全国大学生化工设计竞赛1目录第一章 总论1第二章 物料衡算的方法22.1. 衡算方程式22.2. 物料衡算的基准32.3. 工艺流程图4第三章 各工段物料衡算63.1. 干气除杂工段63.1.1. 干气除杂工段物料衡算73.2. 乙烯精制工段103.2.1. 乙烯精制工段流程图103.2.2. 乙烯精制工段物料衡算113.3. 醋酸乙烯酯合成工段133.3.1. 醋酸乙烯酯合成工段流程图133.3.2. 醋酸乙烯酯合成工段物料衡算143.4. 醋酸乙烯酯精制工段163.4.1. 醋酸乙烯酯精制工段流程图163.4.2. 醋酸乙烯酯精制工段物料衡算17第四章 主要设备物料衡算194.1. 醋酸乙烯酯反应器194.1.1. 醋酸乙烯酯反应器（R-0301）194.2. 塔设备214.2.1. 乙烯精馏塔（T-0203）214.2.2. 萃取精馏塔（T-0403）234.2.3. 醋酸乙烯酯脱重塔（T-0406）2529第1章 总论物料衡算是以质量守恒定律为基础对物料平衡进行计算，在工艺设计中，物料衡算是在工艺流程确定后进行的。其在确定项目生产工艺及流程后，通过对整个生产系统、部分重要的生产单元进行物料衡算计算出主、副产品的产量、原材料的消耗定额、生产过程中各阶段的消耗量以及产品收率等各项经济技术指标，进而定量地评价初步设计所选择的的工艺路线在技术及经济上的合理性，为后续的热量衡算、其他工艺计算及设备计算打下基础。第2章 物料衡算的方法2.1. 衡算方程式对一般的体系而言，物料分布均可表示为：（物料的累积率）=（物料进入率）-（物料流出率）+（反应生成率）-（反应消耗率）特别地，当系统没有化学反应时，则可简化为：（物料的累积率）=（物料进入率）-（物料流出率）在稳定状态下有：（物料进入率）=（物料流出率）物料衡算包括总质量衡算、组分衡算和元素衡算。各种衡算方法的适用情况如下：表2-1 物料衡算的适用范围类别物料衡算形式无化学反应有化学反应总衡算式总质量衡算式适用适用总物质的量衡算式适用不适用组分衡算式组分质量衡算式适用不适用组分物质的量衡算式适用不适用元素原子衡算式元素原子质量衡算式适用适用由于项目过程中存在化学反应故主要采用总质量衡算方法，主要采用总质量衡算的方法，同时列出每种组分的质量流量以便于查找和计算。2.2. 物料衡算的基准1、对于间歇式操作的过程，常采用一批原料为基准进行计算。2、对于连续式操作的过程，可以采用单位时间产品数量或原料量为基准进行计算。物料衡算的结果应列成原材料消耗定额及消耗量表。3、消耗定额是指每吨产品或以一定量的产品所消耗的原材料量；而消耗量是指以每年或每日等时间所消耗的原材料量。4、制剂车间的消耗定额及消耗量计算时应把原料、辅料及主要包装材料一起算入。物料衡算的主要任务如下：1、保证主要产品醋酸乙烯酯质量合格。2、确定对环境有危害的工业三废的含量，并确定处理措施。3、各主要单元过程的物料衡算，并指导工艺设备的尺寸确定。4、汇总全流程物料衡算，数据用于完成物料流程图等后续设计任务。2.3. 工艺流程图本项目用炼油厂产生的废气为原料，分离提纯得到高纯度的乙烯，然后又通过与氧气、醋酸在一定温度压力下反应制得醋酸乙烯酯，最后通过分离得到产品醋酸乙烯酯。异丁烯氧化制MAL工段采取PMo 12 W 015 Bi 018 Fe 3 Ni 5 CoMgZnB 015 Sb 115Cs 017 SiO x催化剂，MAL氧化酯化制MMA采取PdsPb3Mg3/-Al2O3催化剂等为辅助原料，项目设计年产15万吨醋酸乙烯酯，整个工艺流程由干气除杂工段工段、乙烯精制工段、醋酸乙烯酯合成工段、醋酸乙烯酯精制工段四个工段组成。图2-1 工艺流程示意图第3章 各工段物料衡算3.1. 干气除杂工段图3-1 干气除杂工段流程图3.1.1. 干气除杂工段物料衡算表3-1 消耗定额消耗定额吨/年水2573.655乙醇胺312709.2炼厂干气288423.3表3-2 相关物理化学常数名称数值摩尔气体常数R=8.31433J/（molK）标准大气压1atm=101.325Kpa阿伏伽德罗常数N=6.0220451023mol-1冰点温度0=275.15K标准状态下气体摩尔体积V=22.4138310-3m3/mol（275.15K，101.325Kpa）其余物性数据选用AspenplusV9.0中自带的物性数据库和整合的企业数据库。以AspenPlus9.0的模拟数据为依据得到的物料衡算的结果详见下表：（注：下列表格中0.001表示10-310-6；TRACE表示痕量级10-610-9）表3-3 干气除杂工段流股物料模拟结果ITEMSINPUTOUTPUTS-0101S-0102S-0103S-0107S-0108S-0109S-0201Temperature/25.0040.0025.00119.51162.3138.1538.15Pressure/bar11.7611.6711.952.106.0111.6711.67Vapor Frac0011001Liquid Frac1100110Mole Flow kmol/hr18.001900.001750.00366.451420.75179.791701.00Mass Flow kg/hr324.2839400.6936340.727780.1430723.313239.0034323.23Volume Flow cum/hr0.3340.213630.215696.9336.333.303772.63Enthalpy MMBtu/hr-4.88-511.58-44.46-84.92-366.99-48.54-30.28Mole Flow kmol/hrH20.000.00410.730.000.000.00410.73O20.000.0014.000.000.000.0014.00N20.000.00117.080.000.000.00117.08CH40.000.00453.780.000.000.00453.78C2H40.000.00350.000.000.000.00350.00C2H60.000.00201.250.000.000.00201.25C3H80.000.0012.250.000.000.0012.25C3H60.000.00124.250.000.000.00124.25C4H80.000.003.500.000.000.003.50C4H100.000.004.380.000.000.004.38C5H120.000.002.800.000.000.002.80CO0.000.007.000.000.000.007.00MEA0.00120.080.001.01119.070.000.00H2O18.001779.920.00316.441301.69179.790.00CO20.000.0035.0035.000.000.000.00H2S0.000.0014.0014.000.000.000.00表3-4 干气除杂工段物料衡算表Mass-flow kg/hrSummationInput76065.68Output76065.68Rel.diff03.2. 乙烯精制工段3.2.1. 乙烯精制工段流程图图3-2 乙烯精制工段流程图3.2.2. 乙烯精制工段物料衡算表3-5 乙烯精制工段流股物料模拟结果ITEMSINPUTOUTPUTS-0201S-0205S-0207S-0202S-0206S-0304Temperature/38.15-20.0020.0039.43-93.84-58.28Pressure/bar11.6732.0032.0010.1330.008.00Vapor Frac111010.82Liquid Frac000100.18Mole Flow kmol/hr1701.001930.00320.0025.512950.00346.00Mass Flow kg/hr34323.2330962.539622.281289.0643512.199707.64Volume Flow cum/hr3772.631269.44243.732.441465.97562.72Enthalpy MMBtu/hr-30.28-139.19-25.50-1.73-180.9315.22Mole Flow kmol/hrH2410.730.000.000.00410.720.00O214.000.000.000.0014.000.00N2117.080.000.000.00117.070.00CH4453.781930.000.000.002383.770.00C2H4350.000.000.000.004.38345.48C2H6201.250.00320.000.0012.790.52C3H812.250.000.005.900.010.00C3H6124.250.000.008.940.240.00C4H83.500.000.003.500.000.00C4H104.380.000.004.370.000.00C5H122.800.000.002.800.000.00CO7.000.000.000.007.000.00表3-6 乙烯精致工段物料衡算Mass-flow kg/hrSummationInput74908.04 Output74908.04 Rel.diff03.3. 醋酸乙烯酯合成工段3.3.1. 醋酸乙烯酯合成工段流程图图3-3 醋酸乙烯酯合成工段流程图3.3.2. 醋酸乙烯酯合成工段物料衡算表3-7 醋酸乙烯酯合成工段流股物料模拟结果ITEMSINPUTOUTPUTS-0301S-0304S-0309S-0318S-0324S-0331S-0403S-0328S-0333S-0335S-0401Temperature/25.00-58.28165.0015.0020.00110.00201.1417.2525.0092.4811.91Pressure/baapor Frac00.8210000100.000Liquid Frac10ole Flow kmol/hr300.00346.002400.0060.00105003002161.6338.69520.631058.53Mass Flow kg/hr17763.549707.6471217.673552.71180.1527036.2218011.3963713.59804.4628107.5654843.20Volume Flow cum/hr16.61562.7210928.773.280.1840.4322.267425.830.9042.4556.65Enthalpy MMBtu/hr-136.2615.229.38-27.31-2.71-95.38-130.24-0.58-9.28-92.73-353.18Mole Flow kmol/hrH20.000.000.000.000.000.000.000.000.000.000.00O20.000.000.420.000.000.000.000.370.000.000.03N20.000.000.580.000.000.000.000.630.000.000.03CH40.000.000.000.000.000.000.000.000.000.000.00C2H40.001.000.000.000.000.000.000.000.120.060.02C2H60.000.000.000.000.000.000.000.000.000.000.00C3H80.000.000.000.000.000.000.000.000.000.000.00C3H60.000.000.000.000.000.000.000.000.000.000.00C4H80.000.000.000.000.000.000.000.000.000.000.00C4H100.000.000.000.000.000.000.000.000.000.000.00C5H120.000.000.000.000.000.000.000.000.000.000.00CO0.000.000.000.000.000.000.000.000.000.000.00MEA0.000.000.000.000.000.000.000.000.000.000.00H2O0.020.000.000.021.000.700.120.000.820.620.29CO20.000.000.000.000.000.000.000.000.060.020.01H2S0.000.000.000.000.000.000.000.000.000.000.00CH3COOH0.980.000.000.980.000.00299.870.000.000.000.36VAM0.000.000.000.000.000.000.010.000.000.000.25KC2H3O20.000.000.000.000.000.000.000.000.000.000.00K2CO30.000.000.000.000.000.300.000.000.000.290.00CH3CHO0.000.000.000.000.000.000.000.000.000.000.00C4H8O20.000.000.000.000.000.000.000.000.000.000.00表3-8 醋酸乙烯酯合成工段物料衡算表Mass-flow kg/hrSummationInput147469.32Output147469.32Rel.diff03.4. 醋酸乙烯酯精制工段3.4.1. 醋酸乙烯酯精制工段流程图图3-4 醋酸乙烯酯精制工段流程图3.4.2. 醋酸乙烯酯精制工段物料衡算表3-9 醋酸乙烯酯精制工段流股物料模拟结果ITEMSINPUTOUTPUTS-0401S-0409S-0413S-0403S-0405S-0411S-0420S-0416S-0422S-0423Temperature/11.91170.50294.31201.135.00168.71277.28-2.0667.59175.408Pressure/bar881.28.00218.0050.850.90.850.946Vapor Frac0110101110Liquid Frac1001010001Mole Flow kmol/hr1058.5310.00940.00300.0082.17305.331006.0324.50252.0038.50Mass Flow kg/hr54843.20180.1586569.0418011.392775.596904.2387821.73860.1121694.813524.54Volume Flow cum/hr56.6543.9136085.7422.261893.468.4753318.48610.108118.143.18Enthalpy MMBtu/hr-353.18-2.25-479.98-130.24-3.63-85.18-496.42-2.07-74.23-22.14Mole Flow kmol/hrH20.000.000.000.000.000.000.000.000.000.00O231.320.000.000.0026.590.000.004.730.000.00N230.950.000.000.0028.140.000.002.820.000.00CH40.000.000.000.000.000.000.000.000.000.00C2H424.290.000.000.0014.510.140.009.640.000.00C2H60.230.000.000.000.110.010.000.120.000.00C3H80.000.000.000.000.000.000.000.000.000.00C3H60.000.000.000.000.000.000.000.000.000.00C4H80.000.000.000.000.000.000.000.000.000.00C4H100.000.000.000.000.000.000.000.000.000.00C5H120.000.000.000.000.000.000.000.000.000.00CO0.000.000.000.000.000.000.000.000.000.00MEA0.000.000.000.000.000.000.000.000.000.00H2O303.1410.000.000.120.92272.0440.050.010.000.00CO213.080.000.000.007.310.010.005.760.000.00H2S0.000.000.000.000.000.000.000.000.000.00CH3COOH386.170.000.00299.870.0232.1654.120.000.000.00VAM263.320.000.000.014.380.462.120.94251.993.42KC2H3O20.000.000.000.000.000.000.000.000.000.00K2CO30.000.000.000.000.000.000.000.000.000.00CH3CHO3.210.000.000.000.160.392.170.490.000.00C4H8O22.800.000.000.000.020.122.500.000.010.14C3H8O30.000.00940.000.000.000.00905.060.000.0034.94表3-10 醋酸乙烯工段物料衡算表Mass-flow kg/hrSummationInput141592.40 Output141592.40 Rel.diff0第4章 主要设备物料衡算4.1. 醋酸乙烯酯反应器4.1.1. 醋酸乙烯酯反应器（R-0301）表4-1 R-0301流股物料模拟结果ITEMSINPUTOUTPUTS-0310S-0311Temperature/165.00180Pressure/bar88Vapor Frac11Liquid Frac00Mole Flow kmol/hr12952.7112867.46Mass Flow kg/hr398379.54398379.54Volume Flow cum/hr58982.1560599.90Enthalpy MMBtu/hr-195.15-228.96Mole Flow kmol/hrH20.000.00O24171.154057.49N26876.996876.99CH40.000.00C2H41111.83931.85C2H65.335.33C3H80.000.00C3H60.000.00C4H80.000.00C4H100.000.00C5H120.000.00CO0.000.00MEA0.000.00H2O6.92196.37CO2380.05398.99H2S0.000.00CH3COOH395.60225.09VAM2.08172.59KC2H3O20.000.00K2CO30.000.00CH3CHO2.762.76C4H8O20.000.00C3H8O30.000.00表4-2 R-0301流股物料衡算表Mass-flow kg/hrSummationInput398379.54Output398379.54Rel.diff04.2. 塔设备4.2.1. 乙烯精馏塔（T-0203）表4-5 T-0203流股物料模拟结果ITEMSINPUTOUTPUTS-0210S-0212S-0304Temperature/-20.0032.87-58.28Pressure/bar42.0042.438Vapor Frac000.82Liquid Frac110.18Mole Flow kmol/hr3493.473147.47346.00Mass Flow kg/hr111704.64101997.009707.64Volume Flow cum/hr237.89292.20562.72Enthalpy MMBtu/hr-223.34-200.3615.22Mole Flow kmol/hrH20.000.000.00O20.000.000.00N20.000.000.00CH40.000.000.00C2H4346.150.67345.48C2H62540.262539.750.52C3H831.6931.690.00C3H6575.36575.360.00C4H80.000.000.00C4H100.000.000.00C5H120.000.000.00CO0.000.000.00MEA0.000.000.00H2O0.000.000.00CO20.000.000.00H2S0.000.000.00CH3COOH0.000.000.00VAM0.000.000.00KC2H3O20.000.000.00K2CO30.000.000.00CH3CHO0.000.000.00C4H8O20.000.000.00C3H8O30.000.000.00表4-6 T-0203流股物料衡算表Mass-flow kg/hrSummationInput111704.64Output111704.64Rel.diff04.2.2. 萃取精馏塔（T-0403）表4-7 T-0403流股物料模拟结果ITEMSINPUTOUTPUTS-0412S-0414S-0415S-0419Temperature/30.05294.34186.45-51.28Pressure/bar8.001.201.021Vapor Frac00.5100.00Liquid Frac10.4911.00Mole Flow kmol/hr381.031760.001826.03315.00Mass Flow kg/hr27332.15162086.71163339.4026079.46Volume Flow cum/hr29.5434772.58144.4425.12Enthalpy MMBtu/hr-124.37-952.04-1069.32-111.95Mole Flow kmol/hrH20.000.000.000.00O24.730.000.004.73N22.820.000.002.82CH40.000.000.000.00C2H49.640.000.009.64C2H60.120.000.000.12C3H80.000.000.000.00C3H60.000.000.000.00C4H80.000.000.000.00C4H100.000.000.000.00C5H120.000.000.000.00CO0.000.000.000.00MEA0.000.000.000.00H2O40.060.