基于MDEA的烟气SO2捕集过程工艺参数和能量集成分析

doi:10.11949/0438-1157.20201861

摘要/Abstract

摘要：

有机胺吸收法是一种高效环保型烟气脱硫技术，而从系统工程的角度对烟气SO₂捕集工艺的分析、优化和能耗评估尚未有详细报道。对N-甲基二乙醇胺（MDEA）为吸收剂的烟气SO₂捕集过程工艺进行研究，考察了MDEA浓度、温度、SO₂解吸率对捕集效果的影响规律。结果显示，MDEA溶液浓度为30%（质量）、烟气温度不高于45℃、回流贫液温度不高于41℃时，SO₂吸收效果较好；增加SO₂解吸率是以降低解吸气中SO₂纯度和增大再沸器负荷为代价，水分汽化是再生能耗增高的主要原因。针对吸收剂再生过程能耗大的问题，采用热泵辅助精馏对解吸过程进行能量集成，吸收剂再生能耗可降低47%，年度总费用（TAC）可降低9.93%。本研究对有机胺体系的SO₂捕集系统工业化应用具有重要的指导作用。

关键词: 有机胺, SO₂捕集, 参数分析, 能量集成, 热泵辅助精馏

Abstract:

Organic amine absorption is an efficient and environmentally friendly flue gas desulfurization technology, and the analysis, optimization and energy consumption evaluation of the flue gas SO₂ capture process from the perspective of system engineering have not been reported in detail. In this paper, SO₂ capture process of flue gas was studied with N-methyldiethanolamine (MDEA) as the absorbent. The effects of MDEA concentration, temperature, and SO₂ desorption rate on the SO₂ capture were investigated. The results show that the optimized parameters for SO₂ absorption are as follows: MDEA concentration, feed temperature of flue gas and absorbent are 30%(mass), below 45℃ and 41℃, respectively. Increasing of the SO₂ desorption ratio is at the expense of the low SO₂ desorption purity and the high energy consumption of absorbent regenerative process, since water gasification is the main reason for the high energy consumption. In order to solve the problem of high energy consumption in the regenerative process, the modified process with heat pump technology was proposed. The energy consumption of absorbent regeneration can be reduced by 47%, TAC can be reduced by 9.93% in the heat pump assistant desorption process. It is expected from the study to strengthen the development of the industrial application of SO₂capture of organic amine system.

Key words: organic amine, SO₂ capture, parameter analysis, energy integration, heat pump assistant distillation

中图分类号:

王东亮, 谢江鹏, 周怀荣, 孟文亮, 杨勇, 李德磊. 基于MDEA的烟气SO₂捕集过程工艺参数和能量集成分析[J]. 化工学报, 2021, 72(3): 1521-1528.

WANG Dongliang, XIE Jiangpeng, ZHOU Huairong, MENG Wenliang, YANG Yong, LI Delei. Parameters analysis and energy integration in flue gas SO₂ capture process based on MDEA[J]. CIESC Journal, 2021, 72(3): 1521-1528.

图/表 10

图1 MDEA溶液捕集烟气SO2工艺流程

Fig.1 Process flowsheet of flue gas SO2 capturewith MDEA

表1 平衡常数表达式中相关系数

Table 1 The correlation coefficient in the equilibrium constant expression

平衡常数	C₁	C₂	C₃	C₄
K₁	-9.42	-4234.98	0	0
K₂	132.90	-13445.90	-22.48	0
K₃	231.47	-12092.10	-36.78	0
K₄	-5.98	637.40	0	0.01
K₅	216.05	-12431.70	-35.48	0
K₆	-25.29	1333.40	0	0

表2 MDEA水溶液捕集SO2过程的模拟结果

Table 2 Simulation results of the SO2 trapping process in MDEA aqueous solution

项目	吸收塔			解吸塔			废液	补充液
项目	原烟气	回流贫液	净烟气	高温富液	解吸气	高温贫液	废液	补充液
温度/°C	45	41	38	90	40	106	41	41
压力/kPa	120	120	110	120	44	118	120	120
塔板数	10			12
进料位置	1	10		5
液气比/回流比	0.15			9.62
流量/(kg/h)	90254	13575	90580	13249	337	12912	118	781
组成/% (mass)
N₂	73.05	0	72.79	0	0.03	0	0	0
CO₂	16.05	0	15.99	0	0	0	0.27	0
SO₂	0.39	0	0.01	0	94.43	0.02	0	0
SO₃	0.01	0	0.01	0.02	0.60	0	0	0
H₂O	2.67	69.83	3.40	65.76	4.93	68.05	0.11	88.73
O₂	7.83	0	7.80	0	0.01	0	0	0
MDEA	0	30.17	0	21.63	0	31.12	8.08	11.27
MDEA⁺	0	0	0	9.37	0	0.61	66.76	0
H₃O⁺	0	0	0	0	0	0	0	0
HCO₃^-	0	0	0	0.01	0	0.01	0.65	0
HSO₃^-	0	0	0	0.21	0	0.01	4.78	0
CO₃^2-	0	0	0	0	0	0	0	0
SO₃^2-	0	0	0	3.01	0	0.19	19.28	0
OH^-	0	0	0	0	0	0	0.07	0
再沸器负荷/kW				2326
冷凝器负荷/kW	206			1815

图2 MDEA浓度对吸收剂流量及再生能耗的影响

Fig.2 Effect of MDEA concentration on absorbent mass flow and regeneration energy consumption

图3 温度对SO2捕集效果的影响

Fig.3 Effect of temperature on SO2 capture

图4 解吸率对SO2浓度及再生热耗的影响

Fig.4 Effect of SO2 desorption ratio on SO2 concentration and regeneration energy consumption

图5 再沸器负荷与解吸塔塔顶蒸汽的关系

Fig.5 Relationship between reboiler duty and the top stream in desorption column

图6 带热泵精馏的烟气SO2捕集工艺

Fig.6 Flue gas SO2 capture process with heat pump assistant distillation

图7 有无热泵的解吸过程再生能耗对比

Fig.7 Energy consumption in desorption process with or without heat pump

表3 经济分析计算公式

Table 3 Economic analysis calculation formula

项目	计算式
IC
塔壳成本/CNY	17640×(D)^1.066×(H)^0.802×E_r
塔盘成本/CNY	482×(D)^1.066×(H′)^0.802×E_r
塔径D/m	Aspen tray sizing
塔高H/m	1.2×0.6×N_T
塔有效高度H′/m	0.6×N_T
换热器成本/CNY	7296×(A)^0.65×E_r
压缩机成本/CNY	50715×(0.746P)^0.82×E_r
OP
蒸汽成本/CNY	8000×220×Q_R
冷却水成本/CNY	8000×0.4×Q_C
用电成本/CNY	8000×0.55×Q_E
MDEA价格/(CNY/t)	3700
水价格/(CNY/m³)	1
TAC/CNY	$O P + I C p e r i o d$

表3 经济分析计算公式

Table 3 Economic analysis calculation formula

项目	计算式
IC
塔壳成本/CNY	17640×(D)^1.066×(H)^0.802×E_r
塔盘成本/CNY	482×(D)^1.066×(H′)^0.802×E_r
塔径D/m	Aspen tray sizing
塔高H/m	1.2×0.6×N_T
塔有效高度H′/m	0.6×N_T
换热器成本/CNY	7296×(A)^0.65×E_r
压缩机成本/CNY	50715×(0.746P)^0.82×E_r
OP
蒸汽成本/CNY	8000×220×Q_R
冷却水成本/CNY	8000×0.4×Q_C
用电成本/CNY	8000×0.55×Q_E
MDEA价格/(CNY/t)	3700
水价格/(CNY/m³)	1
TAC/CNY	$O P + I C p e r i o d$

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基于MDEA的烟气SO₂捕集过程工艺参数和能量集成分析

Parameters analysis and energy integration in flue gas SO₂ capture process based on MDEA

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