基于余热利用的活化MDEA法脱除CO2的天然气液化系统

doi:10.11949/0438-1157.20201517

摘要/Abstract

摘要：

沼气以及CO₂驱采油的伴生气中都含有大量的CO₂。为降低高含CO₂天然气液化的能耗，提出了活化甲基二乙醇胺（MDEA）法脱除CO₂的天然气液化系统，将液化厂中驱动压缩机的燃气轮机烟气余热用于吸收剂的再生过程，实现能耗的降低。采用HYSYS软件对系统进行了模拟研究并对脱碳过程的关键参数进行了分析。结果表明，CO₂含量不超过10%时，脱碳再生的热耗可全部由烟气余热提供，CO₂含量为30%时，烟气余热可提供接近50%的再生热耗；CO₂含量为1%～30%时，系统的比功耗为0.577～0.611 kW·h/kg。

关键词: CO₂, 液化, 天然气, 活化甲基二乙醇胺, 余热利用

Abstract:

Biogas and the associated gas produced by CO₂ flooding oil recovery contain large amount of CO₂. In order to reduce the energy consumption of high CO₂-content natural gas liquefaction process, a natural gas liquefaction system that uses activated methyldiethanolamine (MDEA) to remove CO₂ is proposed, and the waste heat of exhaust from the gas turbine driving the compressors in the liquefaction plant is utilized in the regeneration process of the absorbent. The HYSYS software is used to simulate the system and analyze the key parameters of the decarbonization process. The results show that waste heat of gas turbine exhaust can provide all the heat load for the regeneration system with a CO₂ content not exceeding 10% in feed gas. Even if the CO₂ is up to 30%, it can also provide nearly 50% regenerative heat load. Furthermore, when the CO₂ content in feed gas is 1% — 30%, the specific power consumption of the system is 0.577 — 0.611 kW·h/kg.

Key words: carbon dioxide, liquefaction, natural gas, activated MDEA, waste heat utilization

中图分类号:

TQ 025.4

何婷, 林文胜. 基于余热利用的活化MDEA法脱除CO₂的天然气液化系统[J]. 化工学报, 2021, 72(S1): 453-460.

HE Ting, LIN Wensheng. Natural gas liquefaction system with activated MDEA method for CO₂ removal based on waste heat utilization[J]. CIESC Journal, 2021, 72(S1): 453-460.

图/表 13

参考文献 30

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Parameters	Lower bound	Upper bound
N_301-C1/(kmol/h)	3000	4000
N_301-C2/(kmol/h)	3000	4000
N_301-C3/(kmol/h)	800	1200
N_301-C4/(kmol/h)	200	600
N_301-N2/(kmol/h)	300	800
p₃₀₂/kPa	2000	3500
T₃₁₀/℃	-150	-130
T₃₀₆/℃	-100	-80
T₃₀₄/℃	-45	-20
N₄₀₁/(kmol/h)	3000	7000
p₄₀₂/kPa	1000	1800

Parameters	Lower bound	Upper bound
N_301-C1/(kmol/h)	3000	4000
N_301-C2/(kmol/h)	3000	4000
N_301-C3/(kmol/h)	800	1200
N_301-C4/(kmol/h)	200	600
N_301-N2/(kmol/h)	300	800
p₃₀₂/kPa	2000	3500
T₃₁₀/℃	-150	-130
T₃₀₆/℃	-100	-80
T₃₀₄/℃	-45	-20
N₄₀₁/(kmol/h)	3000	7000
p₄₀₂/kPa	1000	1800

Flow	T/℃	p/kPa	Molar flow/(kmol/h)	CO₂content/%	CH₄ content/%
101	40	101	7200	10	90
103	40	1500	7200	10	90
104	40.03	1440	6473	0	99.56
201	40	150	16869	0.01	0
203	40	1440	16869	0.01	0
204	67.95	1500	17564	4.03	0.03
205	67.91	200	17564	4.03	0.03
208	85	200	17549	4.02	0
210	113.2	150	16790	0.01	0
211	89	150	16790	0.01	0
501	600	120	9410	—	—
502	176	120	9410	—	—
601	100	200	6000	—	—
602	120.2	200	6000	—	—

Flow	T/℃	p/kPa	Molar flow/(kmol/h)	CO₂content/%	CH₄ content/%
101	40	101	7200	10	90
103	40	1500	7200	10	90
104	40.03	1440	6473	0	99.56
201	40	150	16869	0.01	0
203	40	1440	16869	0.01	0
204	67.95	1500	17564	4.03	0.03
205	67.91	200	17564	4.03	0.03
208	85	200	17549	4.02	0
210	113.2	150	16790	0.01	0
211	89	150	16790	0.01	0
501	600	120	9410	—	—
502	176	120	9410	—	—
601	100	200	6000	—	—
602	120.2	200	6000	—	—

Flow	T/℃	p/kPa	Molar flow/(kmol/h)
105	40	1400	6473
107	40	5000	6473
108	-35	5000	6473
109	-112	5000	6473
110	-162.5	5000	6473
111	-160.7	110	6473
301	37	120	8682
303	40	3000	8682
304	-34	3000	8682
306	-94	3000	5416
307	-114.3	120	5416
310	-145	3000	3266
311	-165.6	120	3266
401	35.19	120	5289
403	40	1380	5289
404	-38.25	120	5289

基于余热利用的活化MDEA法脱除CO₂的天然气液化系统

Natural gas liquefaction system with activated MDEA method for CO₂ removal based on waste heat utilization

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参考文献 30

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CO₂content/%	Regeneration heat load /(kJ/m³)	Net regeneration heat load/(kJ/m³)	Purification power consumption/(kW·h/m³)	w/(kW·h/kg)	α/%
1	140.19	0	0.096	0.577	25.1
10	828.99	0	0.087	0.584	84.9
30	2116.19	1092.5	0.099	0.611	92.0

Upgrading technologies	CH₄ purity (vol)/%	Energy consumption (kW·h/m³ of raw biogas)	H₂S/water pre-upgrading	Additional heat
water scrubbing + regeneration	97 (93—99)	0.3 (0.2—0.46)	necessary	not necessary
physical absorption	97 (95—99)	0.25 (0.2—0.3)	necessary	necessary
chemical absorption	98 (97—99)	0.4 (0.3—0.8)	not necessary	necessary
pressure swing absorption	97 (95—99)	0.25 (0.2—0.3)	necessary	not necessary
membrane technology	95 (80—99)	0.3 (0.15—0.43)	not necessary	not necessary

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CO₂content/%	Circulation amine /(kmol/h)	η/%	Replenish solvent water /(kmol/h)
1	4035	0.03	46
10	16870	0.11	56
30	45682	0.28	70

CO₂content/%	Circulation amine /(kmol/h)	η/%	Replenish solvent water /(kmol/h)
1	4035	0.03	46
10	16870	0.11	56
30	45682	0.28	70