基于余热利用的天然气化学吸收脱碳-高温热泵耦合流程研究

doi:10.11949/0438-1157.20250089

摘要/Abstract

摘要：

以醇胺溶液作为吸收剂的化学吸收是目前天然气脱碳领域使用最为广泛的技术，拥有处理量大、循环稳定性好等优点，但是化学吸收剂的再生过程能耗非常高。为降低化学吸收脱碳的能耗，提出了天然气化学吸收脱碳-高温热泵耦合流程，通过高温热泵将气田上的废水余热用于脱碳流程的再生过程，达到节能降碳。利用Aspen HYSYS软件对采用MDEA溶液的脱碳系统进行建模和参数优化。结果表明：经过优化，该套工艺的脱碳率高达95%，系统的单位综合能耗为0.3821 kW·h/kg CO₂，相比于常规脱碳系统（单位综合能耗为0.8828 kW·h/kg CO₂）降低了56.72%。

关键词: 脱碳, 高温热泵, 天然气, 余热利用, 化学吸收, 数值模拟

Abstract:

Chemical absorption using alcohol amine solution as an absorbent is currently the most widely used technology in the field of natural gas decarbonization, with advantages such as large processing capacity and good cycle stability. However, the regeneration process of chemical absorbent consumes a lot of energy. To reduce the energy consumption of chemical absorption decarbonization, a natural gas chemical absorption decarbonization high-temperature heat pump coupling process is proposed. Through the high-temperature heat pump, the waste heat from the wastewater in the gas field is used for the regeneration process of the decarbonization process, achieving energy conservation and carbon reduction. Modeling and parameter optimization of the decarbonization system using MDEA solution was carried out using Aspen HYSYS software. The results showed that the decarbonization rate of the optimized process was as high as 95%, and the unit comprehensive power consumption of the system was 0.3821 kW·h/kg CO₂, which was 56.72% lower than the conventional decarbonization system (unit comprehensive power consumption of 0.8828kW·h/kg CO₂).

Key words: decarbonization, high temperature heat pump, natural gas, waste heat utilization, chemical absorption, numerical simulation

中图分类号:

TE 644

何婷, 黄舒阳, 黄坤, 陈利琼. 基于余热利用的天然气化学吸收脱碳-高温热泵耦合流程研究[J]. 化工学报, 2025, 76(S1): 297-308.

Ting HE, Shuyang HUANG, Kun HUANG, Liqiong CHEN. Research on the coupled process of natural gas chemical absorption decarbonization and high temperature heat pump based on waste heat utilization[J]. CIESC Journal, 2025, 76(S1): 297-308.

图/表 19

图1 常规胺法脱碳工艺流程图

Fig.1 Conventional amine decarburization process flow diagram

表1 原料气的组分设置

Table 1 Component settings for feedstock gas

组分	CH₄	C₂H₆	C₃H₈	i-C₄H₁₀	n-C₄H₁₀
组成/%（mol）	0.938063	0.003600	0.000466	0.000105	0.000108
组分	i-C₅H₁₂	n-C₅H₁₂	H₂O	H₂S	CO₂
组成/%（mol）	0.000045	0.000057	0.000510	0.000466	0.056600

图2 基于余热利用的天然气化学吸收脱碳-高温热泵耦合工艺流程图K—压缩机;AC—空冷机;V—分离器;E—换热器;T-100—吸收塔;T-101—解析塔;VLV—阀门;P—泵;C—蒸发器;MAKEUP—补充;RCY—循环

Fig.2 Process flowchart of natural gas chemical absorption decarbonization high-temperature heat pump coupling based on waste heat utilization

表2 系统关键参数表

Table 2 System key parameter table

流股	T/℃	P/kPa	摩尔流量/(kmol/h)
1-1	25.00	2500	10364.87
1-4	40.00	3700	10364.87
1-7	40.13	3640	9777.00
2-1	40.00	3640	15031.00
2-2	65.04	3700	15618.47
2-6	85.00	170	15618.47
2-7	74.99	167	738.30
2-8	112.00	170	14837.30
3-1	80	220	42708.20
3-3	129	1443	4157.94
3-4	115	166.1	1941.00
3-5	115	169.1	1941.00
3-6	115	1433	4157.94

图3 系统单位综合能耗和单位综合电耗随吸收塔压力的变化曲线

Fig.3 System unit comprehensive energy consumption and unit comprehensive power consumption variation curve with absorption tower pressure

图4 系统单位电耗和再生系统单位电耗随吸收塔压力的变化曲线

Fig.4 The variation curves of system unit power consumption and regeneration system unit power consumption with absorption tower pressure

图5 系统脱碳率随吸收塔压力的变化曲线

Fig.5 Variation curve of system carbon capture rate with absorption tower pressure

图6 净化气中CO2含量随吸收塔入口温度的变化曲线

Fig.6 Variation curve of CO2 content in purified gas with inlet temperature of absorption tower

图7 净化气中CO2含量随吸收塔入口压力的变化曲线

Fig.7 Variation curve of CO2 content in purified gas with the inlet pressure of the absorber tower

图8 再沸器能耗随再生塔入口温度的变化曲线

Fig.8 Variation curve of reboiler energy consumption with inlet temperature of regeneration tower

图9 再沸器能耗随再生塔入口压力的变化曲线

Fig.9 Variation curve of reboiler energy consumption with regeneration tower inlet pressure

表3 纯工质相关系数

Table 3 Correlation coefficients of pure workmass

工质	T_b/℃	T_c/℃	P_c/MPa	ρ_c/(kg/m³)	ODP	GWP	安全等级
R142b	-9.12	137.11	4.055	446.0	0.05700	1980.0	A2
R600	-0.49	151.98	3.796	228.0	0	4.0	A3
R600a	-11.75	134.66	3.571	225.5	0	20.0	A3
R601	36.06	196.50	3.375	629.7	0	20.0	A3
R365mfc	40.15	186.85	3.266	516.08	0	890.0	A2
R1233zd(E)	18.32	165.60	3.571	476.31	0.00034	4.5	A1

图10 COP随冷凝器出水温度的变化

Fig.10 Variation of COP with condenser discharge temperature

图11 压缩机耗电功率随冷凝器出水温度的变化

Fig.11 Variation of compressor power consumption with condenser water temperature

图12 压缩比随冷凝器出水温度的变化

Fig.12 Variation of compressor ratio with condenser outlet water temperature

图13 COP随热源温度的变化

Fig.13 Variation of COP with heat source temperature

图14 压缩机功率随热源温度的变化

Fig.14 Variation of compressor power with heat source temperature

图15 压缩比随热源温度的变化

Fig.15 Variation of compression ratio with heat source temperature

表4 主要运行参数

Table 4 Main operating parameters

工质	P_k/kPa	P_o/kPa	压缩比	T_k/℃	T_o/℃	Q/(m³/h)	COP	P/kW	W/(kW·h/kg CO₂)
R365mfc	776	196	3.959	126	77	430	4.02	5188	0.3850
R601	831	214	3.883	130	77	430	4.01	5200	0.3855
R1233zd(E)	1443	405	3.563	129	77	430	4.08	5115	0.3821

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