CIESC Journal ›› 2025, Vol. 76 ›› Issue (6): 2434-2450.DOI: 10.11949/0438-1157.20241438
• Reviews and monographs • Previous Articles Next Articles
Haohao ZHANG1,2(
), Li GUO1,2, Xinyi LI1,2, Jinyi CHEN1, Chao HUA1, Ping LU1(
)
Received:2024-12-12
Revised:2025-01-22
Online:2025-07-09
Published:2025-06-25
Contact:
Ping LU
张豪豪1,2(
), 郭莉1,2, 李馨怡1,2, 陈锦溢1, 华超1, 陆平1(
)
通讯作者:
陆平
作者简介:张豪豪(1998—),男,博士研究生,zhanghaohao20@mails.ucas.ac.cn
基金资助:CLC Number:
Haohao ZHANG, Li GUO, Xinyi LI, Jinyi CHEN, Chao HUA, Ping LU. Research progress on optimal design and dynamic control of dividing wall column[J]. CIESC Journal, 2025, 76(6): 2434-2450.
张豪豪, 郭莉, 李馨怡, 陈锦溢, 华超, 陆平. 隔板精馏塔的优化设计及动态控制研究进展[J]. 化工学报, 2025, 76(6): 2434-2450.
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| 年份 | 设计/建造公司 | 地点 | 应用装置/体系 | 效果 | 标志 | 文献 |
|---|---|---|---|---|---|---|
| 1999 | Sumitomo | 日本Kyowa Yuka公司 | 乙酸乙酯分离装置 | 侧线乙酸乙酯纯度99.99% 节省30%设备投资和40%能耗 | — | [ |
| 2000 | Kellogg, BP | 英国Coryton炼油厂 | 改造烷基重整流程 | 改造后塔操作能力增加一倍 中间产物产量增加50% | — | [ |
| 2000 | BASF Montz | 南非Sosol公司 | 费托合成中回收碳氢化合物 | 板式塔,塔高107 m,塔径5.2 m | 当时世界上最大的隔板塔 | [ |
| 2002 | Koch-Glitsch | 西班牙CEPSA炼油厂 | 改造烷烃和异构烷烃分离精馏塔 | 增产异己烷的同时节能40% | — | [ |
| 2002 | BASF | 德国BASF SE工厂 | 未公开 | — | 全球首座工业化的四产品隔板塔 | [ |
| 2004 | Uhde | 德国ARAL芳烃公司 | 重整生成油中回收苯 | 能耗节省20% | 世界上第一座工业化的萃取隔板塔 | [ |
| 2005 | ExxonMobil | 英国Fawley炼油厂 法国Port Jerome炼油厂 | 改造二甲苯回收塔 | 二甲苯纯度提高,能耗降低53% | — | [ |
| 2005 | ExxonMobil | 荷兰鹿特丹石化厂 | 新建苯-甲苯-二甲苯隔板分离塔 | — | — | [ |
| 2010 | Lonza | 瑞士Visp生产基地 | 未公开 | 隔板塔可替代带侧线的精馏塔、间歇精馏塔和带薄膜蒸发器的精馏塔 | 全球首个多用途隔板塔 | [ |
Table 1 Industrialization of DWC technology abroad
| 年份 | 设计/建造公司 | 地点 | 应用装置/体系 | 效果 | 标志 | 文献 |
|---|---|---|---|---|---|---|
| 1999 | Sumitomo | 日本Kyowa Yuka公司 | 乙酸乙酯分离装置 | 侧线乙酸乙酯纯度99.99% 节省30%设备投资和40%能耗 | — | [ |
| 2000 | Kellogg, BP | 英国Coryton炼油厂 | 改造烷基重整流程 | 改造后塔操作能力增加一倍 中间产物产量增加50% | — | [ |
| 2000 | BASF Montz | 南非Sosol公司 | 费托合成中回收碳氢化合物 | 板式塔,塔高107 m,塔径5.2 m | 当时世界上最大的隔板塔 | [ |
| 2002 | Koch-Glitsch | 西班牙CEPSA炼油厂 | 改造烷烃和异构烷烃分离精馏塔 | 增产异己烷的同时节能40% | — | [ |
| 2002 | BASF | 德国BASF SE工厂 | 未公开 | — | 全球首座工业化的四产品隔板塔 | [ |
| 2004 | Uhde | 德国ARAL芳烃公司 | 重整生成油中回收苯 | 能耗节省20% | 世界上第一座工业化的萃取隔板塔 | [ |
| 2005 | ExxonMobil | 英国Fawley炼油厂 法国Port Jerome炼油厂 | 改造二甲苯回收塔 | 二甲苯纯度提高,能耗降低53% | — | [ |
| 2005 | ExxonMobil | 荷兰鹿特丹石化厂 | 新建苯-甲苯-二甲苯隔板分离塔 | — | — | [ |
| 2010 | Lonza | 瑞士Visp生产基地 | 未公开 | 隔板塔可替代带侧线的精馏塔、间歇精馏塔和带薄膜蒸发器的精馏塔 | 全球首个多用途隔板塔 | [ |
| 体系 | 隔板类型 | 目标函数 | 模拟软件 | 优化算法 | 优化结果 | 文献 |
|---|---|---|---|---|---|---|
| 乙酸提纯 | DWC | 再沸器负荷 | Hysys | 迭代试错法 | 较常规精馏序列能耗减少37.8% | [ |
异丙醇和水分离 吡啶和水分离 | ADWC-VRAP | TAC | Aspen | 迭代试错法 | 较常规ADWC能耗减少47%~80% | [ |
| 乙酸正丙酯生产 | RDWC | TAC | Matlab & Aspen | 网格自适应直接搜索算法 | 较常规反应精馏工艺TAC减少10.44% | [ |
| 混合醇分离 | DWC | TAC | Matlab & Aspen | 改进的粒子群算法 | 较常规粒子群算法TAC减少1.18% | [ |
| 苯和环己烯分离 | EDWC | TAC | Matlab & Aspen | 粒子群算法 | 较常规萃取精馏工艺可减少19.15%的TAC、36.08%的二氧化碳排放量、19.99%的㶲损失以及8.03%的萃取剂消耗量 | [ |
| 乙腈和正丙醇分离 | EDWC | TAC | Python & Aspen | 改进的和声搜索算法 | 较顺序迭代算法TAC可减少12.97% | [ |
| 混合苯分离 | DWC | 总投资成本 总运营成本 二氧化碳排放量 苯、二甲苯回收率 | Matlab & Aspen | 多目标NSGA-Ⅱ算法 | 较常规精馏序列总投资成本减少23%、总运营成本减少45%、二氧化碳排放量减少45% | [ |
| 二乙二醇单甲醚和N-甲基吡咯烷酮分离 | EDWC | 总投资成本 总运营成本 | Matlab & Aspen | 多目标遗传算法 | 较常规萃取精馏工艺能耗减少26.29%、TAC减少24.15% | [ |
| 乙酸乙酯和甲醇分离 | EDWC | TAC 二氧化碳排放量 过程安全指数(PRI) | Matlab & Aspen | 多目标粒子群算法 | 较四塔基础工艺TAC减少20.20%、二氧化碳排放量降低33.81%、安全指数提高18% | [ |
| 环己烷和环己烯分离 | EDWC | TAC 二氧化碳排放量 | Matlab & Aspen | 多目标NSGA-Ⅱ算法 | 较常规萃取精馏流程可减少9.46%的TAC和17.25%的二氧化碳排放 | [ |
Table 2 Summary of research progress on optimal design of DWC
| 体系 | 隔板类型 | 目标函数 | 模拟软件 | 优化算法 | 优化结果 | 文献 |
|---|---|---|---|---|---|---|
| 乙酸提纯 | DWC | 再沸器负荷 | Hysys | 迭代试错法 | 较常规精馏序列能耗减少37.8% | [ |
异丙醇和水分离 吡啶和水分离 | ADWC-VRAP | TAC | Aspen | 迭代试错法 | 较常规ADWC能耗减少47%~80% | [ |
| 乙酸正丙酯生产 | RDWC | TAC | Matlab & Aspen | 网格自适应直接搜索算法 | 较常规反应精馏工艺TAC减少10.44% | [ |
| 混合醇分离 | DWC | TAC | Matlab & Aspen | 改进的粒子群算法 | 较常规粒子群算法TAC减少1.18% | [ |
| 苯和环己烯分离 | EDWC | TAC | Matlab & Aspen | 粒子群算法 | 较常规萃取精馏工艺可减少19.15%的TAC、36.08%的二氧化碳排放量、19.99%的㶲损失以及8.03%的萃取剂消耗量 | [ |
| 乙腈和正丙醇分离 | EDWC | TAC | Python & Aspen | 改进的和声搜索算法 | 较顺序迭代算法TAC可减少12.97% | [ |
| 混合苯分离 | DWC | 总投资成本 总运营成本 二氧化碳排放量 苯、二甲苯回收率 | Matlab & Aspen | 多目标NSGA-Ⅱ算法 | 较常规精馏序列总投资成本减少23%、总运营成本减少45%、二氧化碳排放量减少45% | [ |
| 二乙二醇单甲醚和N-甲基吡咯烷酮分离 | EDWC | 总投资成本 总运营成本 | Matlab & Aspen | 多目标遗传算法 | 较常规萃取精馏工艺能耗减少26.29%、TAC减少24.15% | [ |
| 乙酸乙酯和甲醇分离 | EDWC | TAC 二氧化碳排放量 过程安全指数(PRI) | Matlab & Aspen | 多目标粒子群算法 | 较四塔基础工艺TAC减少20.20%、二氧化碳排放量降低33.81%、安全指数提高18% | [ |
| 环己烷和环己烯分离 | EDWC | TAC 二氧化碳排放量 | Matlab & Aspen | 多目标NSGA-Ⅱ算法 | 较常规萃取精馏流程可减少9.46%的TAC和17.25%的二氧化碳排放 | [ |
| 体系 | 隔板类型 | 控制结构 | MPC的预测模型 | 仿真软件 | 文献 |
|---|---|---|---|---|---|
| 乙醇/正丙醇/正丁醇分离 | DWC | 9输入9输出 MPC控制结构 | 稳态点近似线性化状态空间模型 | Simulink & Aspen Dynamic | [ |
| 氯硅烷混合物分离 | DWC | 7输入7输出 MPC控制结构 4输入4输出 MPC-PI混合控制结构 | 稳态点近似线性化状态空间模型 | Simulink & Aspen Dynamic | [ |
| 甲苯和2-甲氧基乙醇分离 | EDWC | 4输入4输出 MPC-PI混合控制结构 | 系统辨识获得的线性状态空间模型 | Matlab & Simulink & Aspen Dynamic | [ |
| 苯和环己烯分离 | EDWC | 4输入4输出 MPC控制结构 | 系统辨识获得的线性ARX模型 | Python & Matlab & Simulink & Aspen Dynamic | [ |
| C3的选择性加氢和分离 | RDWC | 8输入8输出 MPC控制结构 | 稳态点近似线性化状态空间模型 | Simulink & Aspen Dynamic | [ |
| 甲酸生产 | RDWC | 11输入11输出 MPC-PI混合控制结构 | 稳态点近似线性化状态空间模型 | Simulink & Aspen Dynamic | [ |
| 乙酸己酯和丁醇酯交换反应 | RDWC | 8输入8输出 MPC-PI混合控制结构 | 系统辨识得到的线性状态空间模型 | Matlab & Simulink & Aspen Custom Modeler | [ |
Table 3 Summary of research progress on MPC control structures for DWC
| 体系 | 隔板类型 | 控制结构 | MPC的预测模型 | 仿真软件 | 文献 |
|---|---|---|---|---|---|
| 乙醇/正丙醇/正丁醇分离 | DWC | 9输入9输出 MPC控制结构 | 稳态点近似线性化状态空间模型 | Simulink & Aspen Dynamic | [ |
| 氯硅烷混合物分离 | DWC | 7输入7输出 MPC控制结构 4输入4输出 MPC-PI混合控制结构 | 稳态点近似线性化状态空间模型 | Simulink & Aspen Dynamic | [ |
| 甲苯和2-甲氧基乙醇分离 | EDWC | 4输入4输出 MPC-PI混合控制结构 | 系统辨识获得的线性状态空间模型 | Matlab & Simulink & Aspen Dynamic | [ |
| 苯和环己烯分离 | EDWC | 4输入4输出 MPC控制结构 | 系统辨识获得的线性ARX模型 | Python & Matlab & Simulink & Aspen Dynamic | [ |
| C3的选择性加氢和分离 | RDWC | 8输入8输出 MPC控制结构 | 稳态点近似线性化状态空间模型 | Simulink & Aspen Dynamic | [ |
| 甲酸生产 | RDWC | 11输入11输出 MPC-PI混合控制结构 | 稳态点近似线性化状态空间模型 | Simulink & Aspen Dynamic | [ |
| 乙酸己酯和丁醇酯交换反应 | RDWC | 8输入8输出 MPC-PI混合控制结构 | 系统辨识得到的线性状态空间模型 | Matlab & Simulink & Aspen Custom Modeler | [ |
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