基于自热再生的一种低温甲醇洗工艺建模与优化

doi:10.11949/0438-1157.20250280

化工学报 ›› 2025, Vol. 76 ›› Issue (9): 4601-4612.DOI: 10.11949/0438-1157.20250280

• 专栏：过程模拟与仿真 • 上一篇下一篇

基于自热再生的一种低温甲醇洗工艺建模与优化

田鹏¹(), 张忠林¹(), 任超¹, 孟国超¹^,², 郝晓刚¹(), 刘叶刚¹^,³, 侯起旺¹^,⁴, ABUDULA Abuliti⁵, 官国清⁶

^1.太原理工大学化学与化工学院，山西太原 030024
^2.中控技术股份有限公司，浙江杭州 311401
^3.上海电气集团国控环球工程有限公司，山西太原 030001
^4.中化二建集团有限公司，山西太原 030021
^5.弘前大学科学技术研究生院，日本青森 030-0813
^6.弘前大学区域创新研究所能源转换工程实验室，日本青森 030-0813

收稿日期:2025-03-21 修回日期:2025-04-14 出版日期:2025-09-25 发布日期:2025-10-23
通讯作者: 张忠林,郝晓刚
作者简介:田鹏（1999—），男，硕士研究生，2448771441@qq.com
基金资助:
国家自然科学基金项目(U1710101);山西科化技术服务有限公司项目(KHZ2023002)

Modeling and optimization of rectisol process based on self-heat regeneration

Peng TIAN¹(), Zhonglin ZHANG¹(), Chao REN¹, Guochao MENG¹^,², Xiaogang HAO¹(), Yegang LIU¹^,³, Qiwang HOU¹^,⁴, Abuliti ABUDULA⁵, Guoqing GUAN⁶

^1.College of Chemistry and Chemical Engineering, Taiyuan University of Technology, Taiyuan 030024, Shanxi, China
^2.SUPCON Technology Co. , Ltd. , Hangzhou 311401, Zhejiang, China
^3.Shanghai Electric Group State Owned Huanqiu Engineering Co. , Ltd. , Taiyuan 030001, Shanxi, China
^4.China Chemical Engineering Second Construction Corporation, Taiyuan 030021, Shanxi, China
^5.Graduate School of Science and Technology, Hirosaki University, Aomori 030-0813, Japan
^6.Laboratory of Energy Conversion Engineering, Institute of Regional Innovation, Hirosaki University, Aomori 030-0813, Japan

Received:2025-03-21 Revised:2025-04-14 Online:2025-09-25 Published:2025-10-23
Contact: Zhonglin ZHANG, Xiaogang HAO

摘要/Abstract

摘要：

低温甲醇洗工艺存在运行能耗高和CO₂捕集不充分的问题。为优化捕集性能、降低能耗，设计了一种“双级减压闪蒸耦合半贫液循环”工艺，降低再生能耗的同时提高CO₂捕集效率，结果显示CO₂产量增加12.16%。设计两种“自热再生”优化方案，并对其进行换热网络设计，从能耗、㶲损、CO₂排放量、年度运行费用、单位CO₂产品成本等多个维度进行评价。结果表明，基于自热再生的两种甲醇洗工艺较原工艺㶲效率有所提升，热力学性能得到优化，能耗分别降低36.98%、37.20%，㶲损分别降低26.72%，26.86%，年度运行费用分别降低17.25%、15.06%，单位CO₂产品成本分别降低13.33%、10.91%。改进后的低温甲醇洗工艺在经济性以及节能、减排、环保方面表现出更好的性能。

关键词: 低温甲醇洗, 自热再生, 优化设计, 计算机模拟, 经济, ?

Abstract:

The rectisol process has the problems of high operating energy consumption and insufficient CO₂ capture. In order to optimize performance and reduce energy consumption, a "two-stage reduced pressure flash coupled semi-lean liquid circulation" process is designed to reduce regeneration energy consumption while improving CO₂ capture efficiency. The results show that CO₂ production increases by 12.16%. Two "self-heat regeneration" optimization schemes are designed and their heat exchange network designs are carried out. The evaluation is carried out from several dimensions such as energy consumption, exergy loss, CO₂ emissions and annual operating costs. The results show that the two methanol scrubbing processes based on self-heating regeneration have improved scrubbing efficiency and optimized thermodynamic performance compared to the original process. Energy consumption is reduced by 36.98% and 37.20% respectively, and exergy loss is reduced by 26.72% and 26.86% respectively. Annual operating costs are reduced by 17.25% and 15.06% respectively, and unit CO₂ production cost reduced by 13.33% and 10.91% respectively. The improved rectisol process has better performance in terms of economy, energy conservation, emission reduction and environmental protection.

Key words: rectisol, self-heat regeneration, optimal design, computer simulation, economics, exergy

中图分类号:

TQ 015.2

田鹏, 张忠林, 任超, 孟国超, 郝晓刚, 刘叶刚, 侯起旺, ABUDULA Abuliti, 官国清. 基于自热再生的一种低温甲醇洗工艺建模与优化[J]. 化工学报, 2025, 76(9): 4601-4612.

Peng TIAN, Zhonglin ZHANG, Chao REN, Guochao MENG, Xiaogang HAO, Yegang LIU, Qiwang HOU, Abuliti ABUDULA, Guoqing GUAN. Modeling and optimization of rectisol process based on self-heat regeneration[J]. CIESC Journal, 2025, 76(9): 4601-4612.

图/表 25

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参数	原料气	甲醇
表压/MPa	5.8	5
温度/℃	-15.4	-52.4
质量流率/(kg·h^-1)	289221.8	425494
摩尔流量/(kmol·h^-1)	12972.8	13281.2
CO₂	4663.5919	0
H₂	5730.7344	0
N₂	30.3564	0
H₂S	21.4050	0
H₂O CH₄	22.3132 10.7674	4.6235 0
CO	2487.5344	0
AR COS CH₃OH	14.3998 0.6486 0	0 0 13276.57

参数	原料气	甲醇
表压/MPa	5.8	5
温度/℃	-15.4	-52.4
质量流率/(kg·h^-1)	289221.8	425494
摩尔流量/(kmol·h^-1)	12972.8	13281.2
CO₂	4663.5919	0
H₂	5730.7344	0
N₂	30.3564	0
H₂S	21.4050	0
H₂O CH₄	22.3132 10.7674	4.6235 0
CO	2487.5344	0
AR COS CH₃OH	14.3998 0.6486 0	0 0 13276.57

流股	参数
净化气	S≤1.0×10^-7，CO₂≤2.3%±0.2%
克劳斯气	H₂S+COS≥25%
尾气	H₂S≤2.5×10^-5，S≤2.3 kg·h^-1，甲醇≤1.0×10^-4，甲醇流量≤50 kg·h^-1

流股	参数
净化气	S≤1.0×10^-7，CO₂≤2.3%±0.2%
克劳斯气	H₂S+COS≥25%
尾气	H₂S≤2.5×10^-5，S≤2.3 kg·h^-1，甲醇≤1.0×10^-4，甲醇流量≤50 kg·h^-1

参数	传统工艺	循环工艺
CO₂产量/(kmol·h^-1)	2788	3127
CO₂产量增加/%	—	12.16
CO₂捕集效率/%	60.17	67.49
尾气CO₂排放量/(kmol·h^-1)	1683	1322

基于自热再生的一种低温甲醇洗工艺建模与优化

Modeling and optimization of rectisol process based on self-heat regeneration

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图/表 25

参考文献 42

相关文章 15

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Metrics

本文评价

参数	传统工艺	循环工艺	单塔压缩	双塔压缩
电/kW	1529.96	2463.01	7773.04	7980.94
蒸汽/kW	36655.43	29328.53	9014.18	8444.78
冷却剂/kW	39762.04	33992.63	18710.80	18484.72
总能耗/kW	81007.35	70710.17	51044.10	50872.32
能耗减少/%	—	12.71	36.98	37.20

参数	单位CO₂捕集能耗/（kWh·t^-1）
文献[17]	319.47
企业数据^[40]	250~400
文献[41]	380.28
文献[42]	280.00
单塔压缩工艺	257.57
双塔压缩工艺	253.59

参数	传统工艺	循环工艺	单塔压缩	双塔压缩
原料/kW	624575.17	624575.17	624575.17	624575.17
电量㶲/kW	1529.96	2463.01	7773.04	7980.94
热量㶲/kW	10182.95	8248.69	2052.24	1915.08
冷量㶲/kW	6710.02	5626.34	3674.99	3578.22
总输入/kW	642998.11	640913.17	638075.44	638049.41
引入系统㶲量/kW	18422.93	16338.04	13500.27	13474.24
㶲量减少/%	—	11.32	26.72	26.86
总输出/kW	615312.90	615179.97	615180.40	615179.97
㶲损失/kW	27685.21	25709.59	22895.04	22869.44
㶲效率/%	95.69	95.98	96.41	96.42

项目	传统工艺	单塔压缩	双塔压缩
换热器㶲损失/kW	12217.48	8035.49	7982.75
混合器和塔设备㶲损失/kW	8590.72	7631.28	7629.64
阀门等压力设备㶲损失/kW	5883.11	5097.32	5089.81
电功率设备㶲损失/kW	993.90	2130.95	2167.24

参数	传统工艺	改进工艺	单塔压缩	双塔压缩
塔/10⁶ USD	21.09	23.83	23.83	23.83
泵/10⁶ USD	0.45	0.58	0.58	0.58
压缩机/10⁶ USD	0.89	2.67	12.43	12.89
换热器/10⁶ USD	12.34	11.17	13.34	15.23
闪蒸器/10⁶ USD	0.17	0.19	0.19	0.19
再沸器/10⁶ USD	1.56	1.39	—	—
甲醇/10⁶ USD	0.18	0.16	0.16	0.16
设备成本/10⁶ USD	36.68	39.99	50.53	52.88
固定资本/10⁶ USD	93.90	102.37	129.35	135.37
营运资本/10⁶ USD	18.34	19.99	25.26	26.44
总资本投资/10⁶ USD	112.24	122.36	154.61	161.81

参数	传统工艺	循环工艺	单塔压缩	双塔压缩
蒸汽/10⁶ USD	8.21	6.57	2.02	1.89
电量/10⁶ USD	0.74	1.19	3.82	3.92
冷却剂/10⁶ USD	6.87	5.83	3.24	3.20
总运行成本/10⁶ USD	15.82	13.59	9.08	9.01
年度运行费用/10⁶ USD	23.30	21.75 (-6.65%)	19.38 (-17.25%)	19.79 (-15.06%)
新增设备静态回收期/年	—	4.53	6.43	7.27
设备折旧年限/年	15	15	15	15
总生产成本/10⁶ USD	38.05	37.34	36.98	38.02
单位CO₂产品成本/（USD·t^-1）	38.77	33.92 (-12.50%)	33.6 (-13.33%)	34.54 (-10.91%)

参数	传统工艺	循环工艺	单塔压缩	双塔压缩
蒸汽CO₂/(kg·h^-1)	18711.04	14970.87	4601.41	4310.75
电CO₂/(kg·h^-1)	98.95	376.97	2455.85	2536.85
总CO₂排放/(kg·h^-1)	18809.99	15347.84	7057.26	6847.60
排放减少/%	—	18.41	62.48	63.59

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