丙酮缩甘油反应精馏工艺全流程模拟与优化

doi:10.16085/j.issn.1000-6613.2020-1329

摘要/Abstract

摘要：

针对丙酮缩甘油的传统生产工艺单程转化率低、生产设备投资高、后处理过程长及环境污染等缺点，本文设计了一种高效节能的反应精馏（RD）生产工艺。基于反应动力学和热力学基础数据，建立丙酮缩甘油反应精馏严格数学模型对反应精馏工艺全流程进行理论探究。通过对塔内浓度分布的分析，揭示了产物水对丙酮缩甘油反应精馏合成效果的影响。探究不同丙酮循环量对全流程生产工艺的影响；并以反应精馏塔和丙酮回收塔塔釜再沸器负荷为目标函数，对全流程的参数进行探究和优化，结果表明全流程优化后相比单塔优化的总能耗可节约3.6%。同时与工业传统先反应后精馏流程相比，优化后的反应精馏全流程节约能耗15.1%。该结果可为丙酮缩甘油工业化生产工艺设计提供参考和依据。

关键词: 缩酮反应, 反应精馏, 精馏

Abstract:

In order to solve the disadvantages of traditional synthesis process for solketal production with low conversion per pass, high investment in production equipment, long post-treatment process and environmental pollution, in this paper, an energy efficient process, reactive distillation (RD) was proposed. Based on the basic data of kinetics and thermodynamics, the strict mathematical model of RD was established, and the theoretical research of RD process was investigated. The influence of the water in RD process was revealed by the analysis of the concentration distribution in the RD column. The impact of the mass of recycled acetone was explored, take reboiler duty of RDC and recovery column as objective function, the parameters of total process were explored and optimized. The results showed that the total energy consumption could be saved by 3.6% compared with the optimization of single column. Compared with the traditional industrial process, the optimized RD process could save energy consumption by 15.1%. The research results can provide basis and reference for the design of solketal industrial production.

Key words: ketalization, reactive distillation, distillation

中图分类号:

TQ215

赖佳宁, 高鑫, 从海峰, 李洪, 李鑫钢. 丙酮缩甘油反应精馏工艺全流程模拟与优化[J]. 化工进展, 2021, 40(7): 3584-3590.

LAI Jianing, GAO Xin, CONG Haifeng, LI Hong, LI Xingang. Simulation and optimization of synthesizing solketal by reactive distillation process[J]. Chemical Industry and Engineering Progress, 2021, 40(7): 3584-3590.

图/表 12

参考文献 20

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化合物	分子式	CAS号	分子量	沸点（101.3 kPa）/℃
丙酮	C₃H₆O	67-64-1	58.08	56.5
甘油	C₃H₈O₃	56-81-5	92.09	290
4-羟甲基-2,2-二甲基-1,3-二氧戊环	C₆H₁₂O₃	100-79-8	132.16	189
5-羟基-2,2-二甲基-1,3-二氧六环	C₆H₁₂O₃	4728-12-5	132.16	216.78
水	H₂O	7732-18-5	18.01	100

化合物	分子式	CAS号	分子量	沸点（101.3 kPa）/℃
丙酮	C₃H₆O	67-64-1	58.08	56.5
甘油	C₃H₈O₃	56-81-5	92.09	290
4-羟甲基-2,2-二甲基-1,3-二氧戊环	C₆H₁₂O₃	100-79-8	132.16	189
5-羟基-2,2-二甲基-1,3-二氧六环	C₆H₁₂O₃	4728-12-5	132.16	216.78
水	H₂O	7732-18-5	18.01	100

组分	安托尼方程参数			摩尔汽化焓（298.15K）/kJ·mol^-1
组分	A	B	C	摩尔汽化焓（298.15K）/kJ·mol^-1
丙酮	21.704	3022.8	-32.52	31.2213
甘油	23.387	5574.1	-94.708	89.8224
水	23.385	3949	-40.384	43.8605
丙酮缩甘油	23.167	4644.5	-63.778	64.2634

组分	安托尼方程参数			摩尔汽化焓（298.15K）/kJ·mol^-1
组分	A	B	C	摩尔汽化焓（298.15K）/kJ·mol^-1
丙酮	21.704	3022.8	-32.52	31.2213
甘油	23.387	5574.1	-94.708	89.8224
水	23.385	3949	-40.384	43.8605
丙酮缩甘油	23.167	4644.5	-63.778	64.2634

参数	单塔优化结果		全流程优化结果
参数	RD	T₁	RD′	T₁′
回流比	0.5	1.1	0.5	0.9
理论板数	14	6	14	5
精馏段理论板数	0	3	0	2
反应段理论板数	10	—	10	—
提馏段理论板数	3	2	2	1
单程转化率/%	99.5（以甘油计）		99.5（以甘油计）
丙酮缩甘油产品纯度/%	99.5		99.5
再沸器负荷/kW	166.45	152.43	163.84	143.60
全流程能耗节省/%			3.6