集成NGL回收的新型天然气液化系统AP-XTM的概念设计与模拟分析

doi:10.11949/j.issn.0438-1157.20181212

摘要/Abstract

摘要：

为提高液化天然气能量集成与设备共用水平,提出了一种基于大型AP-X^TM液化流程，综合气体过冷技术（GSP）的集成NGL（天然气凝液）回收工艺的天然气液化系统的概念设计。基于化工流程模拟软件Aspen HYSYS进行模拟和分析，将集成工艺多流股换热器性能、全流程的单位功耗和乙烷回收率作为衡量系统性能的三项指标。模拟和分析的结果表明，集成NGL回收的AP-X^TM液化工艺单位功耗降低至0.45 kW·h·(kg LNG)^-1，较单产系统能耗降低了6%，同时乙烷回收率达到93%，实现了NGL的高效分离。通过热力学分析、?分析和经济性分析得出本设计流程具有较高的性能和经济价值，可为天然气液化工艺的集成设计和技术改造提供指导借鉴。

关键词: 液化, 制冷循环, 烷烃, 优化设计, 模拟

Abstract:

To improve the energy integration and equipment sharing level of LNG, a conceptual design of natural gas liquefaction system based on large-scale AP-X^TM liquefaction process and integrated gas subcooling technology (GSP) integrated natural gas condensate (NGL) recovery process was proposed. The performance of the multi-stream heat exchanger, the unit power consumption and the recovery rate of ethane were considered as the three of basic characteristics to evaluate process performance. The simulation and analysis results show that the unit power consumption of proposed process is reduced to 0.45 kW·h·(kg LNG)^-1 which is reduced by 6% compared with conventional independent process. Furthermore, recovery rate of ethane is 93% which prove that NGL s efficient separation is achieved. The thermodynamic analysis, exergy analysis and economic analysis prove that the proposed configuration has high thermodynamics performance and economic value. This study can provide guidance for natural gas engineering research and retrofitted design of natural gas liquefaction technology.

Key words: liquefaction, refrigeration cycle, alkane, optimal design, simulation

中图分类号:

TE 645

王少靖, 刘琳琳, 张磊, 都健, 吴恺艺. 集成NGL回收的新型天然气液化系统AP-X^TM的概念设计与模拟分析[J]. 化工学报, 2019, 70(2): 508-515.

Shaojing WANG, Linlin LIU, Lei ZHANG, Jian DU, Kaiyi WU. Conceptual design， simulation and analysis of novel AP-X^TM system integrated with NGL recovery process for large-scale LNG plant[J]. CIESC Journal, 2019, 70(2): 508-515.

图/表 11

参考文献 30

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组成	进料天然气	混合制冷剂	氮气膨胀剂
CH₄	86	26.7	—
C₂H₄	—	28.9	—
C₂H₆	7.5	—	—
C₃H₆	3.5	15.2	—
i-C₄H₁₀	1.5	14.4	—
n-C₄H₁₀	1.5	—	—
N₂	—	14.8	100

组成	进料天然气	混合制冷剂	氮气膨胀剂
CH₄	86	26.7	—
C₂H₄	—	28.9	—
C₂H₆	7.5	—	—
C₃H₆	3.5	15.2	—
i-C₄H₁₀	1.5	14.4	—
n-C₄H₁₀	1.5	—	—
N₂	—	14.8	100

流股名称	序号	摩尔流量/(kmol·h^-1)	压力/kPa	温度/℃	塔板位置
入口流股
冷回流流股	108	17060	2480	-7.8	1
膨胀气	109	22010	2500	-70.7	6
冷凝液	114	2214	2500	-54.7	14
冷凝冷液	113	3322	2500	-65.1	9
回流流股	side 1R	2500	2524	-35.0	30
回流流股	side 2R	2500	2518	0.00	27
出口流股
回流流股	side 3R	2500	2503	0.00	21
塔顶贫气	115	37920	2467	-97.9	1
塔底NGL	NGL	6650	2533	-5.0	30
侧线采出流股	side 1	2500	2531	-30.4	29
侧线采出流股	side 2	2500	2525	-57.0	26
侧线采出流股	side 3	2500	2510	-76.8	20

流股名称	序号	摩尔流量/(kmol·h^-1)	压力/kPa	温度/℃	塔板位置
入口流股
冷回流流股	108	17060	2480	-7.8	1
膨胀气	109	22010	2500	-70.7	6
冷凝液	114	2214	2500	-54.7	14
冷凝冷液	113	3322	2500	-65.1	9
回流流股	side 1R	2500	2524	-35.0	30
回流流股	side 2R	2500	2518	0.00	27
出口流股
回流流股	side 3R	2500	2503	0.00	21
塔顶贫气	115	37920	2467	-97.9	1
塔底NGL	NGL	6650	2533	-5.0	30
侧线采出流股	side 1	2500	2531	-30.4	29
侧线采出流股	side 2	2500	2525	-57.0	26
侧线采出流股	side 3	2500	2510	-76.8	20

工况参数	115	NGL	Fuel
温度/℃	-98.0	-4.9	-103
压力/kPa	2467	2533	97
摩尔流率/(kmol·h^-1)	37920	6650	2400
摩尔组成/%
甲烷	99.4	10.4	100
乙烷	0.6	52.9	0
丙烷	0	23.3	0
正丁烷	0	6.7	0
异丁烷	0	6.7	0