燃煤电厂烟气MDEA/PZ混合胺法碳捕集工艺模拟分析

doi:10.16085/j.issn.1000-6613.2018-0740

化工进展 ›› 2019, Vol. 38 ›› Issue (04): 2046-2055.DOI: 10.16085/j.issn.1000-6613.2018-0740

燃煤电厂烟气MDEA/PZ混合胺法碳捕集工艺模拟分析

林海周^1,²(),罗海中¹,裴爱国¹,方梦祥²()

1. 中国能源建设集团广东省电力设计研究院有限公司，广东广州 510663
2. 浙江大学能源清洁利用国家重点实验室，浙江杭州 310027

收稿日期:2018-04-11 修回日期:2018-05-30 出版日期:2019-04-05 发布日期:2019-04-05
通讯作者: 方梦祥
作者简介:<named-content content-type="corresp-name">林海周</named-content>（1989—），男，博士后，研究方向为燃煤电厂烟气二氧化碳捕集。E-mail：<email>linhaizhou@gedi.com.cn</email>。|方梦祥，教授，博士生导师，研究方向为煤及生物质燃烧和气化技术、CO2控制技术。E-mail：<email>mxfang@zju.edu.cn</email>。
基金资助:
广东省自然科学基金博士启动项目(2018A030310692);基金项目:中国能源建设集团广东省电力设计研究院博士后科研项目(EV04531W)

Simulation and analysis of carbon dioxide capture process using MDEA/PZ blend solution in a coal-fired power plant

Haizhou LIN^1,²(),Haizhong LUO¹,Aiguo PEI¹,Mengxiang FANG²()

1. China Energy Engineering Group Guangdong Electric Power Design Institute Co., Ltd., Guangzhou 510663, Guangdong China
2. State Key Laboratory of Clean Energy Utilization, Zhejiang University, Hangzhou 310027, Zhejiang, China

Received:2018-04-11 Revised:2018-05-30 Online:2019-04-05 Published:2019-04-05
Contact: Mengxiang FANG

摘要/Abstract

摘要：

采用混合胺吸收剂替代传统一乙醇胺（MEA）吸收剂是降低有机胺法碳捕集工艺能耗的重要方法。利用Aspen plus软件模拟了以甲基二乙醇胺(MDEA)/哌嗪(PZ)混合胺为吸收剂的燃煤电厂每年百万吨CO₂捕集工艺系统，考察了贫液负荷、MDEA/PZ混合胺浓度、MDEA/PZ比例和解吸压力等因素对解吸塔再沸器热负荷和冷凝器冷负荷的影响。通过对这些影响因素下吸收塔内液相温度分布和CO₂负荷分布变化揭示了MDEA/PZ对CO₂的吸收特性。此外，进一步分析了不同影响因素下解吸塔内气液相CO₂浓度驱动力和气液相级间温度驱动力分布特性，发现了强浓度驱动力和低温度驱动力分布更有利于降低再生能耗。研究表明，由30%MDEA和20%PZ组成的混合胺液在贫液负荷为0.08和解吸压力为2.02×10⁵Pa时，再沸器热负荷和塔顶冷凝负荷分别为2.76GJ/tCO₂和0.60GJ/tCO₂，相比传统MEA吸收剂降低了20.92%和40.0%。

关键词: 燃煤电厂, 二氧化碳捕集, 混合胺, 过程模拟, 能耗, 驱动力

Abstract:

Amine blend is recognized as a promising alternative to traditional MEA solution for reducing the energy cost of post-combustion chemical absorption CO₂ capture process. In this study, a coal-fired power plant CO₂ capture system using the blend of methyldiethanolamine (MDEA) and piperazine (PZ) as an absorbent was simulated by Aspen plus soft at a capacity of 1 million tons CO₂ one year. The effects of MDEA/PZ blend concentration, MDEA/PZ ratio, CO₂ load in lean solution and stripping pressure on the stripper reboiler heat duty and condenser cool duty were investigated. The liquid phase temperature and CO₂ load of the solution in the absorber under different conditions were analyzed to reveal the absorbing properties of MDEA/PZ blend. The CO₂ concentration driving force and temperature driving force for the stripping process were also studied. The results showed that strong concentration driving force and weak temperature driving force favored the decrease of energy cost. The heat duty and cold duty for CO₂ regeneration in stripper can be as low as 2.76GJ/tCO₂ and 0.60GJ/tCO₂, respectively under optimized conditions (30% MDEA and 20% PZ, 0.08 lean load, 2.02×10⁵Pa stripping pressure), which were reduced by 20.92% and 40.0% compared to using traditional MEA solution.

Key words: coal-fired power plant, carbon dioxide capture, amine blends, process simulation, energy cost, driving force

中图分类号:

林海周, 罗海中, 裴爱国, 方梦祥. 燃煤电厂烟气MDEA/PZ混合胺法碳捕集工艺模拟分析[J]. 化工进展, 2019, 38(04): 2046-2055.

Haizhou LIN, Haizhong LUO, Aiguo PEI, Mengxiang FANG. Simulation and analysis of carbon dioxide capture process using MDEA/PZ blend solution in a coal-fired power plant[J]. Chemical Industry and Engineering Progress, 2019, 38(04): 2046-2055.

图/表 17

图1 CO2捕集的工艺流程

表1 MDEA-PZ-CO2-H2O体系反应方程及参数

序号	方程	指前因子	活化能 /J·mol^?1
	平衡反应
(1)	2H₂OH₃O⁺+OH^?	—	—
(2)	HCO₃ ^? + H₂OCO₃ ^2?+H₃O⁺	—	—
(3)	PZH⁺ + H₂OPZ+H₃O⁺	—	—
(4)	H₂O + H⁺PZCOO^?H₃O⁺+PZCOO^?	—	—
(5)	MDEAH⁺ + H₂OMDEA+H₃O⁺	—	—
	动力学反应
(6)	CO₂ + OH^?HCO₃ ^?	1.33×10¹⁷	55458.99
(7)	HCO₃ ^?CO₂ + OH^?	6.63×10¹⁶	107393.5
(8)	PZ + CO₂ + H₂OPZCOO^?+H₃O⁺	1.70×10¹⁰	1335.302
(9)	PZCOO^? + H₃O⁺PZ+CO₂+H₂O	3.40×10²³	59272.34
(10)	PZCOO^? + CO₂ + H₂OPZ(COO)₂ ^2? + H₃O⁺	1.04×10¹⁴	33647.52
(11)	PZ(COO)₂ ^2? + H₃O⁺PZCOO^?+CO₂+H₂O	3.20×10²⁰	36383.84
(12)	MDEA + CO₂ + H₂OMDEAH⁺+HCO₃ ^?	6.85×10¹⁰	37794.49
(13)	MDEAH⁺ + HCO₃ ^?MDEA+CO₂+H₂O	6.62×10¹⁷	92638.15

图2 不同温度下MDEA-PZ-CO2-H2O体系中CO2分压与CO2负荷之间的关系[27]

表2 吸收塔和解吸塔初始参数

设备	直径/m	塔高/m	级数	填料	操作压力/atm
吸收塔	16	25	20	Mellapak 250Y	1.0
解吸塔	10	8	20	Mellapak 250Y	2.0

图3 不同吸收剂下贫液负荷对解吸塔再生冷热负荷的影响

图4 不同吸收剂下吸收塔液相温度和CO2负荷分布

图5 不同吸收剂下解吸过程驱动力分布

图6 不同浓度混合胺下贫液负荷对解吸塔冷热负荷的影响

图7 不同浓度吸收剂下吸收塔液相温度和各级吸收CO2比例分布

图8 不同吸收剂下解吸过程驱动力分布

图9 不同比例混合胺下贫液负荷对解吸冷热负荷的影响

图10 不同比例混合胺下最佳解吸冷热负荷和CO2负荷分布

图11 不同比例混合胺在最佳贫液负荷下吸收塔中液相温度分布

图12 不同比例混合胺在最佳贫液负荷下吸收塔中各级吸收的CO2比例分布

图13 不同吸收剂下解吸过程驱动力分布

图14 解吸压力对解吸塔冷热负荷和出入口温度的影响

图15 不同解吸压力下解吸过程驱动力分布

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燃煤电厂烟气MDEA/PZ混合胺法碳捕集工艺模拟分析

Simulation and analysis of carbon dioxide capture process using MDEA/PZ blend solution in a coal-fired power plant

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