贫氦管输天然气提氦多元化产品耦合工艺优化设计

doi:10.11949/0438-1157.20240772

化工学报 ›› 2025, Vol. 76 ›› Issue (5): 2251-2261.DOI: 10.11949/0438-1157.20240772

贫氦管输天然气提氦多元化产品耦合工艺优化设计

郭明钢¹^,²(), 杨晓航², 代岩², 米盼盼², 马世鑫³, 贺高红¹^,²(), 肖武¹, 崔福军²

^1.大连理工大学精细化工国家重点实验室，辽宁大连 116024
^2.大连理工大学盘锦产业技术研究院，辽宁盘锦 124221
^3.沈阳化工大学化学工程学院，辽宁沈阳 110142

收稿日期:2024-07-10 修回日期:2024-10-31 出版日期:2025-05-25 发布日期:2025-06-13
通讯作者: 贺高红
作者简介:郭明钢（1988—），男，博士研究生，高级工程师，guomg@dlut.edu.cn
基金资助:
国家自然科学基金项目(22141001);国家自然科学基金创新群体项目(22021005);营口市企业博士双创计划项目(YKSCJH2023-011)

Optimal design of integration process for helium extraction from helium-poor pipeline natural gas with diversified products

Minggang GUO¹^,²(), Xiaohang YANG², Yan DAI², Panpan MI², Shixin MA³, Gaohong HE¹^,²(), Wu XIAO¹, Fujun CUI²

^1.State Key Laboratory of Fine Chemicals, Dalian University of Technology, Dalian 116024, Liaoning, China
^2.Panjin Institute of Industrial Technology, Dalian University of Technology, Panjin 124221, Liaoning, China
^3.College of Chemical Engineering, Shenyang University of Chemical Technology, Shenyang 110142, Liaoning, China

Received:2024-07-10 Revised:2024-10-31 Online:2025-05-25 Published:2025-06-13
Contact: Gaohong HE

摘要/Abstract

摘要：

目前氦气提取过程，存在过度依赖于液化天然气生产过程的富氦尾气、催化氧化破坏式脱氢引入新杂质和高能耗的问题。因此，提出基于资源广泛的贫氦管输天然气的多级膜-电化学氢泵-吸附耦合提氦工艺，利用管输天然气压力和多技术梯度产品化除杂提氦策略，生产氦气、燃料电池氢和二氧化碳多元化产品，实现贫氦管输天然气经济性提氦。运用Aspen HYSYS软件对1.00×10⁵ m³/h贫氦管输天然气耦合提氦工艺模拟优化，考察了回收率、膜性能和氦气浓度对工艺经济性的影响，模拟结果表明：在典型管输压力4.0 MPa和0.04%(体积分数)He时，采用中渗透性中选择性气体分离膜，且氦气回收率为50%~70%时，贫氦管输天然气提氦耦合工艺经济性较好，氦气盈亏平衡价格为115.5~123.2 CNY/m³，且随着氦气浓度增加盈亏平衡价格逐渐减小，为贫氦资源经济性利用提供极具工业前景技术路线。

关键词: 天然气, 优化设计, 膜, 氦气, 电化学氢泵, 过程强化

Abstract:

At present, there are some problems in the helium extraction process, such as excessive dependence on the helium-rich tail gas from liquefied natural gas production process, the introduction of new impurities by catalytic oxidation destructive dehydrogenation and high energy consumption. Therefore, a multi-stage membrane-electrochemical hydrogen pump-adsorption helium extraction integration process based on a wide range of resources for helium-poor pipeline natural gas was proposed to produce diversified products of He, H₂, and CO₂ by utilizing the pressure of the pipeline natural gas and a multi-technology gradient productization strategy of removing impurities and extracting helium, so as to realize the economic helium extraction from helium-poor pipeline natural gas. Aspen HYSYS software was used to simulate and optimize the helium extraction integration process for 1.00×10⁵ m³/h helium-poor pipeline natural gas, and the effects of the recovery, membrane performance, and helium concentration on the process economy were investigated. The simulation results show that, at a typical pipeline natural gas pressure of 4.0 MPa and 0.04%(vol) He, the helium extraction integration process for helium-poor pipeline natural gas is more economical with the medium-permeable and medium-selective gas separation membrane, and the helium recovery rate is 50%—70%, the break-even price of helium is 115.5—123.2 CNY/m³, and the break-even price gradually decreases as the helium concentration increases, providing a technological route with great industrial prospects for the economic utilization of helium-poor resources.

Key words: natural gas, optimal design, membranes, helium, electrochemical hydrogen pump, process intensification

中图分类号:

TQ 028.8

郭明钢, 杨晓航, 代岩, 米盼盼, 马世鑫, 贺高红, 肖武, 崔福军. 贫氦管输天然气提氦多元化产品耦合工艺优化设计[J]. 化工学报, 2025, 76(5): 2251-2261.

Minggang GUO, Xiaohang YANG, Yan DAI, Panpan MI, Shixin MA, Gaohong HE, Wu XIAO, Fujun CUI. Optimal design of integration process for helium extraction from helium-poor pipeline natural gas with diversified products[J]. CIESC Journal, 2025, 76(5): 2251-2261.

图/表 13

表1 某管输天然气基础条件

Table 1 Basic conditions of the pipeline natural gas

天然气基础条件	值
气相分率	1.00
温度/℃	40
压力/MPa	4.0
标准状态体积流率/(m³/h)	1.00 ×10⁵
组分体积分数/%
He	0.0400
H₂	0.0020
CO₂	1.0200
CH₄	98.1190
C₂H₆	0.2930
C₃H₈	0.0080
N₂	0.5180

表2 分离膜气体渗透速率

Table 2 Gas permeation rates in membrane for process simulation

气体	渗透速率（Prism-Ⅱ, 80℃）/GPU
He	200
H₂	210
N₂	2.2
C₁	1.5
C₂	1.4
C₃	1.3
CO₂	51
H₂O	1000

图1 多级膜-电化学氢泵-吸附耦合工艺示意流程图E-1~4—预热器；PR-1~4—预处理单元；M-1~4—膜单元；K-1~4—压缩机单元；CO2-AU—CO2吸收单元；EHP—电化学氢泵单元；He-PSA—He深度净化吸附单元

Fig.1 Chematic diagram of multi-stage membrane-electrochemical hydrogen pump-adsorption integration process

图2 He回收率对膜面积和压缩机功率影响

Fig.2 Influence of helium recovery on membrane area and compressor power

图3 He回收率对经济性和He盈亏平衡价格影响

Fig.3 Influence of He recovery on economy and He breakeven price

图4 高纯氦价格对不同回收率工艺投资回收期影响

Fig.4 Influence of He price on payback with different helium recovery

表3 固定投资及年化设备成本占比情况

Table 3 Fixed investment and percentage contributions of equipment items annualized cost

项目	膜	压缩机	吸收	吸附	电化学氢泵	其他
设备投资/10⁴CNY	2094.50	597.14	33.00	18.07	0.11	694.08
折旧占比/%	82.00	7.79	0.43	0.71	0.01	9.06

图5 膜He/N2选择性对膜面积及压缩机功率影响

Fig. 5 Influence of membrane He/N2 selectivity on membrane area and compressor power

图6 膜He/N2选择性对He盈亏平衡价格的影响

Fig.6 Influence of membrane He/N2 selectivity on He breakeven price

图7 膜N2渗透性(JN2)对He盈亏平衡价格的影响

Fig.7 Influence of membrane N2 permeability (JN2) on He breakeven price

图8 不同He回收率下多种类膜对He盈亏平衡价格的影响

Fig. 8 Influence of membrane categories on He breakeven price with different helium recovery

图9 原料He浓度对He产量及He盈亏平衡价格影响

Fig.9 Influence of feed gas He concentration on He production and He breakeven price

表4 氦气生产成本的经济比较

Table 4 Economic comparison of the cost of helium production

分离技术	原料	He体积分数/%		He回收率/%	He盈亏平衡价格/ （CNY/m³）	文献
分离技术	原料	原料	产品	He回收率/%	He盈亏平衡价格/ （CNY/m³）	文献
二级膜工艺	贫氦天然气	0.05	90.000	95	505.5	[16]
二级膜工艺	富氦天然气	4.00	97.000	90	1.7	[24]
深冷+三级膜耦合工艺	富氦天然气	0.50	99.000	91	11.2	[36]
深冷+吸附耦合工艺	NRU尾气	3.00	99.999	-	3.7	[10]
二级膜+吸附耦合工艺	NRU尾气	3.47	99.999	91	2.5	[32]
本文研究	贫氦天然气	0.04	99.999	60	115.5

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贫氦管输天然气提氦多元化产品耦合工艺优化设计

Optimal design of integration process for helium extraction from helium-poor pipeline natural gas with diversified products

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