异丙醇-异丙醚-水三元物系分离的模拟与研究

Simulation study on separation process for wastewater containing isopropanol and isopropyl ether

提出了非均相层析-萃取精馏分离工艺,并基于Aspen Plus对该分离过程进行模拟研究,以得到质量分数为98.3%的异丙醚和99%的异丙醇,水相异丙醚的质量分数小于2×10-5,异丙醇的质量分数小于1×10-4为目标,确定了粗馏塔、醚精制塔、异丙醇精制塔、乙二醇回收塔最佳工艺参数。粗馏塔的理论塔板数为26,进料板位置为第13块理论板,摩尔回流比为0.14。醚精制塔的理论塔板数为23,进料板位置分别为第3和15块理论板,摩尔回流比为0.92。异丙醇精制塔的理论塔板数为25,进料板位置为第3和第18块理论板,摩尔回流比为2.85。乙二醇回收塔的理论塔板数为40,进料板位置为第15块理论板,摩尔回流比为0.08。总体工艺具有流程简单、产品纯度高、易于操作的特点。

A heterogeneous chromatography extraction distillation separation process is proposed. Aspen Plus is used to simulate the separation process. The optimum technological parameters of distillation column,ether refining tower,isopropyl alcohol refining tower and ethylene glycol recovery tower are achieved by using the following evaluation index,such as 98. 3% mass fraction of isopropyl ether and 99% mass fraction of isopropyl alcohol,less than 2 × 10^-5 mass fraction of isopropyl ether in water and less than 1 × 10^-4 mass fraction of isopropyl alcohol in water. For crude distillation tower,the optimum process parameters are： 26 of theoretical plate number,13 theoretical plates of feed position and 0. 14 of the molar reflux ratio. For ether refining column,the theoretical plate number is 23,the feed position is 3rd and 15 th theoretical plates,respectively,and the molar reflux ratio is 0. 92. For isopropanol refining column,the theoretical plate number is 25,the feed position is 3rd and 18 th theoretical plate,and the molar reflux ratio is 2. 85. For ethylene glycol recovery column,the theoretical plate number is 40,the feed position is 15 th theoretical plate and the molar reflux ratio is 0. 08. The overall process has the characteristics of easy operation and high product purity.