case_03偏三甲苯分离实例

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1、分离工程工业应用实例：三甲苯分离及精制1工艺流程描述偏三甲苯、均三甲苯分离精制系统模拟流程图如图1-1所示。由催化重整来的碳九重芳烃原料经预分馏塔进行切割，预分馏塔塔顶轻组分进入富集均三甲苯塔，通过精馏操作脱除轻组分，塔釜得到纯度为26.5％的富集均三甲苯产品。预分馏塔塔釜重组分进入偏三甲苯塔，通过精馏操作脱除重组分，塔顶得到精制后纯度为99％的偏三甲苯产品。图1-1偏三甲苯、均三甲苯分离精制系统模拟流程图2原料组成某原料组成如下所示，处理量按4万吨/年设计：表2-1原料组成组分名称原料x0.1对二甲苯1.34间二甲苯异丙苯2.33邻二甲苯8.17正丙苯

2、6.62对甲乙苯6.45间甲乙苯16.52均三甲苯5.55邻甲乙苯8.49偏三甲苯31.15异丁基苯0.23另丁基苯0.25X10.73连三甲苯7.19印满1.72C103.16合计100单元操作参数如下表2-2所示表2-2单元操作参数预分馏塔富集均三塔偏三甲苯塔操作压力，kPa101.3101.3101.2全塔压降，kPa7.682.72.3理论板数140140122进料板553975回流比（采出）9.416.49.6塔底出料量，kg/h947.5915.2393.13.主要结果：'T103','预分离塔'(Cont)理论板温度压力液相汽相进料产品热负

3、荷DEGCKPAKG/HRM*KJ/HR-------------------------------------------------------------------1C157.9101.0030187.23018.7L-10.81412159.6101.0030394.333205.93160.7101.0630532.433413.04161.4101.1130620.333551.25161.9101.1730675.233639.06162.3101.2330709.033693.97162.6101.2930729.833727.781

4、62.8101.3430742.433748.59163.0101.4030750.033761.110163.1101.4630754.333768.711163.2101.5230756.433773.012163.4101.5730756.933775.113163.5101.6330756.233775.614163.6101.6930754.533774.915163.7101.7530751.833773.216163.8101.8030748.333770.517163.9101.8630744.033767.018164.0101.923

5、0738.933762.719164.1101.9830733.133757.720164.1102.0330726.633751.821164.2102.0930719.433745.322164.3102.1530711.533738.123164.4102.2130703.133730.324164.5102.2630694.033721.825164.5102.3230684.533712.726164.6102.3830674.433703.227164.7102.4330663.933693.128164.8102.4930653.13368

6、2.729164.8102.5530641.933671.830164.9102.6130630.433660.631165.0102.6630618.733649.132165.0102.7230606.833637.433165.1102.7830594.833625.534165.2102.8330582.633613.535165.3102.8930570.533601.436165.3102.9530558.333589.237165.4103.0030546.133577.038165.5103.0630534.033564.939165.5

7、103.1230522.033552.840165.6103.1730510.133540.741165.6103.2330498.233528.842165.7103.2930486.533516.943165.8103.3430474.833505.244165.8103.4030463.233493.545165.9103.4630451.733481.946166.0103.5130440.233470.447166.0103.5730428.633458.948166.1103.6230417.033447.349166.2103.683040

8、5.233435.750166.2103.7430393.233423.9511