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Article(id=1245407858955760358, tenantId=1146029695717560320, journalId=1146123166801305609, issueId=1156262727438951343, articleNumber=null, orderNo=null, doi=10.12404/j.issn.1671-1815.2403435, pmid=null, cstr=null, oa=null, hot=null, price=null, onlineType=0, articleFormat=0, articleType=null, articleTypeStr=research-article, receivedDate=1715184000000, receivedDateStr=2024-05-09, revisedDate=1720454400000, revisedDateStr=2024-07-09, acceptedDate=null, acceptedDateStr=null, onlineDate=1774857972133, onlineDateStr=2026-03-30, pubDate=1741363200000, pubDateStr=2025-03-08, doiRegisterDate=null, doiRegisterDateStr=null, onlineIssueDate=1774857972133, onlineIssueDateStr=2026-03-30, onlineJustAcceptDate=null, onlineJustAcceptDateStr=null, onlineFirstDate=null, onlineFirstDateStr=null, sourceXml=null, magXml=null, createTime=1774857972133, creator=13701087609, updateTime=1774857972133, updator=13701087609, issue=Issue{id=1156262727438951343, tenantId=1146029695717560320, journalId=1146123166801305609, year='2025', volume='25', issue='7', pageStart='2193', pageEnd='3077', issueExtLink='null', onlineDate='null', pubDate='null', beforeIssueId=null, nextIssueId=null, price=null, status=1, issueComplete=1, articleOrder=1, issueType=-1, specialIssue=0, createTime=1753604116544, creator=13701087609, updateTime=1753771263994, updator=13701087609, preIssue=null, nextIssue=null, ext={EN=IssueExt(id=1156963794699248405, tenantId=1146029695717560320, journalId=1146123166801305609, issueId=1156262727438951343, language=EN, specialIssueTitle=, coverIllustrator=, specialIssueEditor=, specialIssueAbout=), CN=IssueExt(id=1156963794699248406, tenantId=1146029695717560320, journalId=1146123166801305609, issueId=1156262727438951343, language=CN, specialIssueTitle=, coverIllustrator=, specialIssueEditor=, specialIssueAbout=)}, issueFiles=null}, startPage=2760, endPage=2766, ext={EN=ArticleExt(id=1245407859593294573, articleId=1245407858955760358, tenantId=1146029695717560320, journalId=1146123166801305609, language=EN, title=LNG Cold Energy Used in Exhaust Gas Reflux Rankine Cycle and CO2 Liquefaction Technology, columnId=1156262729003422020, journalTitle=Science Technology and Engineering, columnName=Papers·Petroleum and Natural Gas Industry, runingTitle=null, highlight=null, articleAbstract=

In order to effectively utilize LNG(liquefied natural gas) cold energy and liquefy CO2 in gas turbine exhaust gas, a new process of LNG cold energy to liquefy CO2 and CO2 power cycle was proposed. In this process, Reheat cycle and regenerative cycle were added on the basis of conventional Rankine cycle, and multi-flow strand heat exchanger was set up. Chemical process simulation software was used to simulate the process flow and sensitivity analysis of reflux temperature, interstage cooling temperature and maximum circulating temperature and pressure was carried out to obtain the best operating parameters. Exergy efficiency, specific work and CO2 liquefaction rate of the system were analyzed and calculated by exergy analysis. Exergy efficiency of exergy was 54.16%, specific work was 335.9 kJ/kg LNG, and CO2 liquefaction rate was 0.621 7 kg/kg LNG in a new process. The evaluation indexes of the new process were better than those of the existing process. As for the exergic efficiency, exergic efficiency of exergic was as the highest and the temperature of CO2 after liquefied was as the constraint condition, exergic efficiency of exergic was 54.28% and specific power was 337.5 kJ /kg LNG, so the system performance was further improved.

, correspAuthors=Yin-di ZHANG, authorNote=null, correspAuthorsNote=null, copyrightStatement=null, copyrightOwner=null, extLink=null, articleAbsUrl=null, sourceXml=null, magXml=null, pdfUrl=null, pdf=null, pdfFileSize=null, pdfExtLink=null, richHtmlUrl=null, mobilePdfUrl=null, reviewReport=null, pdfFirstPage=null, abstractGraph=null, abstractGraphContent=null, abstractVideo=null, citation=null, cebUrl=null, magXmlContent=null, mapNumber=null, authorCompany=null, fund=null, authors=null, authorsList=Wei-hong HE, Yin-di ZHANG, Ying-nan LI, Xiao-hong HUANG, Zheng-qin SHENG), CN=ArticleExt(id=1245407862172791607, articleId=1245407858955760358, tenantId=1146029695717560320, journalId=1146123166801305609, language=CN, title=LNG冷能用于废气回流朗肯循环及CO2液化新工艺, columnId=1156262729603207500, journalTitle=科学技术与工程, columnName=论文·石油、天然气工业, runingTitle=null, highlight=null, articleAbstract=

为了有效利用液化天然气(liquefied natural gas,LNG)的冷能并对燃气轮机废气中的CO2进行液化处理,提出了一种利用LNG冷能液化CO2及CO2动力循环的新工艺,该工艺在常规朗肯循环的基础上增加了再热循环和回热循环并且设置了多流股换热器。利用化工过程模拟软件对工艺流程进行模拟并且对回流温度、级间冷却温度和循环的最高温度和压力进行敏感性分析,得到最佳运行参数。采用㶲分析的方法,对系统的㶲效率、比功和CO2的液化率等系统评价指标进行分析计算,并与现有工艺进行对比分析,得到新工艺的㶲效率为54.16%,比功为335.9 kJ/kg LNG,CO2的液化率为0.621 7 kg/kg LNG,可知新工艺的评价指标均优于现有工艺。并且以㶲效率最高为目标,液化后的CO2温度作为约束条件,采用Original优化模式对工艺流程的参数进行优化,优化后的㶲效率为54.28%,比功为337.5 kJ/kg LNG,系统性能进一步提升。

, correspAuthors=张引弟, authorNote=null, correspAuthorsNote=
* 张引弟(1978—),女,汉族,甘肃平凉人,博士,教授。研究方向:油气储运热学与集输节能、CO2捕集与管道输送(CCUS)、燃气技术、管网工艺仿真检测及智能化等。E-mail:。
, copyrightStatement=null, copyrightOwner=null, extLink=null, articleAbsUrl=null, sourceXml=Hn+nRE2aMv86j6O947DXbQ==, magXml=qZgjSAfa3HvNBLuMFewj7g==, pdfUrl=null, pdf=q1wAlUavm4citPu3btt+bg==, pdfFileSize=3620656, pdfExtLink=null, richHtmlUrl=null, mobilePdfUrl=null, reviewReport=null, pdfFirstPage=null, abstractGraph=sLiazOtD9dX0L8tsfJiyew==, abstractGraphContent=null, abstractVideo=null, citation=null, cebUrl=null, magXmlContent=4W5jx1b7FXq/LEJXLcZZog==, mapNumber=null, authorCompany=null, fund=null, authors=

何卫宏(1999—),男,汉族,山东潍坊人,硕士研究生。研究方向:LNG冷能利用等。E-mail:。

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何卫宏(1999—),男,汉族,山东潍坊人,硕士研究生。研究方向:LNG冷能利用等。E-mail:。

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何卫宏(1999—),男,汉族,山东潍坊人,硕士研究生。研究方向:LNG冷能利用等。E-mail:。

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label=Table 1, caption=

LNG gasification process parameters

, figureFileSmall=null, figureFileBig=null, tableContent=
流股 温度/℃ 压力/kPa 流量/(kg·h-1)
L1 -162 150 3 100
L2 -161.6 1 040 3 100
L3 -45 1 030 3 100
L4 -31.93 1 020 3 100
L5 -18 1 010 3 100
NG 14.3 1 000 3 100
), ArticleFig(id=1245407872360755698, tenantId=1146029695717560320, journalId=1146123166801305609, articleId=1245407858955760358, language=CN, label=表1, caption=

LNG气化过程参数

, figureFileSmall=null, figureFileBig=null, tableContent=
流股 温度/℃ 压力/kPa 流量/(kg·h-1)
L1 -162 150 3 100
L2 -161.6 1 040 3 100
L3 -45 1 030 3 100
L4 -31.93 1 020 3 100
L5 -18 1 010 3 100
NG 14.3 1 000 3 100
), ArticleFig(id=1245407872469807614, tenantId=1146029695717560320, journalId=1146123166801305609, articleId=1245407858955760358, language=EN, label=Table 2, caption=

Parameters of CO2 liquefaction process

, figureFileSmall=null, figureFileBig=null, tableContent=
流股 温度/℃ 压力/kPa 流量/(kg·h-1)
C1 600 150 3 500
C2 238 140 3 500
C3 205 130 3 500
C4 93.5 120 3 500
C5 42 115 3 500
C6 42 115 1 984
C7 0 105 1 984
C8 0 105 1 927
C9 62 246 1 927
C10 9 236 1 927
C11 69.68 540 1 927
C12 21.13 530 1 927
LCO2 -55.49 520 1 927
), ArticleFig(id=1245407872570470920, tenantId=1146029695717560320, journalId=1146123166801305609, articleId=1245407858955760358, language=CN, label=表2, caption=

CO2液化过程参数

, figureFileSmall=null, figureFileBig=null, tableContent=
流股 温度/℃ 压力/kPa 流量/(kg·h-1)
C1 600 150 3 500
C2 238 140 3 500
C3 205 130 3 500
C4 93.5 120 3 500
C5 42 115 3 500
C6 42 115 1 984
C7 0 105 1 984
C8 0 105 1 927
C9 62 246 1 927
C10 9 236 1 927
C11 69.68 540 1 927
C12 21.13 530 1 927
LCO2 -55.49 520 1 927
), ArticleFig(id=1245407872725660185, tenantId=1146029695717560320, journalId=1146123166801305609, articleId=1245407858955760358, language=EN, label=Table 3, caption=

Cycle parameters

, figureFileSmall=null, figureFileBig=null, tableContent=
流股 温度/℃ 压力/kPa 流量/(kg·h-1)
R1 -83.5 130 3 500
R2 -78.55 15 000 3 500
R3 -15.69 14 990 3 500
R4 4 15 14 980 3 500
R5 169.1 1 100 3 500
R6 216.3 1 090 3 500
R7 70.64 150 3 500
R8 -60.89 140 3 500
), ArticleFig(id=1245407872822129188, tenantId=1146029695717560320, journalId=1146123166801305609, articleId=1245407858955760358, language=CN, label=表3, caption=

循环参数

, figureFileSmall=null, figureFileBig=null, tableContent=
流股 温度/℃ 压力/kPa 流量/(kg·h-1)
R1 -83.5 130 3 500
R2 -78.55 15 000 3 500
R3 -15.69 14 990 3 500
R4 4 15 14 980 3 500
R5 169.1 1 100 3 500
R6 216.3 1 090 3 500
R7 70.64 150 3 500
R8 -60.89 140 3 500
), ArticleFig(id=1245407872935375409, tenantId=1146029695717560320, journalId=1146123166801305609, articleId=1245407858955760358, language=EN, label=Table 4, caption=

Process performance parameters

, figureFileSmall=null, figureFileBig=null, tableContent=
参数 性能
泵P-1功率/kW 2.078
泵P-2功率/kW 14.31
压缩机K-1功率/kW 28.66
压缩机K-2功率/kW 28.22
膨胀机T-1功率/kW 231.1
膨胀机T-2功率/kW 131.4
净功/kW 289.3
比功/[kJ·(kg LNG)-1] 335.9
液化率/[kg·(kg LNG)-1] 0.621 7
㶲效率/% 54.16
), ArticleFig(id=1245407873065398848, tenantId=1146029695717560320, journalId=1146123166801305609, articleId=1245407858955760358, language=CN, label=表4, caption=

工艺性能参数

, figureFileSmall=null, figureFileBig=null, tableContent=
参数 性能
泵P-1功率/kW 2.078
泵P-2功率/kW 14.31
压缩机K-1功率/kW 28.66
压缩机K-2功率/kW 28.22
膨胀机T-1功率/kW 231.1
膨胀机T-2功率/kW 131.4
净功/kW 289.3
比功/[kJ·(kg LNG)-1] 335.9
液化率/[kg·(kg LNG)-1] 0.621 7
㶲效率/% 54.16
), ArticleFig(id=1245407873203810895, tenantId=1146029695717560320, journalId=1146123166801305609, articleId=1245407858955760358, language=EN, label=Table 5, caption=

Comparison of existing processes

, figureFileSmall=null, figureFileBig=null, tableContent=
参数 工艺1 工艺2 本文
新工艺
LNG气化压力/MPa 3 1 1
LNG出口温度/℃ 37.17 15 14.3
废气最高温度/℃ 630 600 600
工质最高压力/MPa 15 15 15
工质最高温度/℃ 630 267 415
CO2液化率/[kg·(kg LNG)-1] 0.273 0.60 0.621 7
比功/[kJ·(kg LNG)] 284.74 237.7 335.9
㶲效率/% 36.33 49.70 54.16
), ArticleFig(id=1245407873317057120, tenantId=1146029695717560320, journalId=1146123166801305609, articleId=1245407858955760358, language=CN, label=表5, caption=

现有工艺对比

, figureFileSmall=null, figureFileBig=null, tableContent=
参数 工艺1 工艺2 本文
新工艺
LNG气化压力/MPa 3 1 1
LNG出口温度/℃ 37.17 15 14.3
废气最高温度/℃ 630 600 600
工质最高压力/MPa 15 15 15
工质最高温度/℃ 630 267 415
CO2液化率/[kg·(kg LNG)-1] 0.273 0.60 0.621 7
比功/[kJ·(kg LNG)] 284.74 237.7 335.9
㶲效率/% 36.33 49.70 54.16
), ArticleFig(id=1245407873463857772, tenantId=1146029695717560320, journalId=1146123166801305609, articleId=1245407858955760358, language=EN, label=Table 6, caption=

Optimization results

, figureFileSmall=null, figureFileBig=null, tableContent=
变量 最高循环
温度/℃		 K-2出口
温度/℃		 液化CO2
温度/℃		 㶲效率/%
上限 420.0 9 — —
下限 410.0 8 -56.00 —
优化前 415.0 9 -55.49 54.16
优化后 417.1 8.7 -55.97 54.28
), ArticleFig(id=1245407873614852731, tenantId=1146029695717560320, journalId=1146123166801305609, articleId=1245407858955760358, language=CN, label=表6, caption=

优化结果

, figureFileSmall=null, figureFileBig=null, tableContent=
变量 最高循环
温度/℃		 K-2出口
温度/℃		 液化CO2
温度/℃		 㶲效率/%
上限 420.0 9 — —
下限 410.0 8 -56.00 —
优化前 415.0 9 -55.49 54.16
优化后 417.1 8.7 -55.97 54.28
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LNG冷能用于废气回流朗肯循环及CO2液化新工艺
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何卫宏 1, 2 , 张引弟 1, 2, * , 李颖楠 3 , 黄孝红 1, 2 , 盛钲钦 1, 2
科学技术与工程 | 论文·石油、天然气工业 2025,25(7): 2760-2766
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科学技术与工程 | 论文·石油、天然气工业 2025, 25(7): 2760-2766
LNG冷能用于废气回流朗肯循环及CO2液化新工艺
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何卫宏1, 2 , 张引弟1, 2, * , 李颖楠3, 黄孝红1, 2, 盛钲钦1, 2
作者信息
  • 1 长江大学石油工程学院, 武汉 430100
  • 2 低碳催化与二氧化碳利用国家重点实验室, 兰州 730000
  • 3 中海油江苏天然气有限责任公司, 盐城 224000

    • 何卫宏(1999—),男,汉族,山东潍坊人,硕士研究生。研究方向:LNG冷能利用等。E-mail:。

通讯作者:

* 张引弟(1978—),女,汉族,甘肃平凉人,博士,教授。研究方向:油气储运热学与集输节能、CO2捕集与管道输送(CCUS)、燃气技术、管网工艺仿真检测及智能化等。E-mail:。
LNG Cold Energy Used in Exhaust Gas Reflux Rankine Cycle and CO2 Liquefaction Technology
Wei-hong HE1, 2 , Yin-di ZHANG1, 2, * , Ying-nan LI3, Xiao-hong HUANG1, 2, Zheng-qin SHENG1, 2
Affiliations
  • 1 College of Petroleum Engineering, Yangtze University, Wuhan 430100, China
  • 2 State Key Laboratory of Low-carbon Catalysis and Carbon Dioxide Utilization, Lanzhou 730000, China
  • 3 CNOOC Jiangsu Natural Gas Co., Ltd., Yancheng 224000, China
出版时间: 2025-03-08 doi: 10.12404/j.issn.1671-1815.2403435
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摘要
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为了有效利用液化天然气(liquefied natural gas,LNG)的冷能并对燃气轮机废气中的CO2进行液化处理,提出了一种利用LNG冷能液化CO2及CO2动力循环的新工艺,该工艺在常规朗肯循环的基础上增加了再热循环和回热循环并且设置了多流股换热器。利用化工过程模拟软件对工艺流程进行模拟并且对回流温度、级间冷却温度和循环的最高温度和压力进行敏感性分析,得到最佳运行参数。采用㶲分析的方法,对系统的㶲效率、比功和CO2的液化率等系统评价指标进行分析计算,并与现有工艺进行对比分析,得到新工艺的㶲效率为54.16%,比功为335.9 kJ/kg LNG,CO2的液化率为0.621 7 kg/kg LNG,可知新工艺的评价指标均优于现有工艺。并且以㶲效率最高为目标,液化后的CO2温度作为约束条件,采用Original优化模式对工艺流程的参数进行优化,优化后的㶲效率为54.28%,比功为337.5 kJ/kg LNG,系统性能进一步提升。

LNG冷能利用  /  液化CO2  /  废气回流  /  朗肯循环  /  敏感性分析

In order to effectively utilize LNG(liquefied natural gas) cold energy and liquefy CO2 in gas turbine exhaust gas, a new process of LNG cold energy to liquefy CO2 and CO2 power cycle was proposed. In this process, Reheat cycle and regenerative cycle were added on the basis of conventional Rankine cycle, and multi-flow strand heat exchanger was set up. Chemical process simulation software was used to simulate the process flow and sensitivity analysis of reflux temperature, interstage cooling temperature and maximum circulating temperature and pressure was carried out to obtain the best operating parameters. Exergy efficiency, specific work and CO2 liquefaction rate of the system were analyzed and calculated by exergy analysis. Exergy efficiency of exergy was 54.16%, specific work was 335.9 kJ/kg LNG, and CO2 liquefaction rate was 0.621 7 kg/kg LNG in a new process. The evaluation indexes of the new process were better than those of the existing process. As for the exergic efficiency, exergic efficiency of exergic was as the highest and the temperature of CO2 after liquefied was as the constraint condition, exergic efficiency of exergic was 54.28% and specific power was 337.5 kJ /kg LNG, so the system performance was further improved.

LNG cold energy utilization  /  liquefied CO2  /  exhaust gas reflux  /  rankine cycle  /  sensitivity analysis
何卫宏, 张引弟, 李颖楠, 黄孝红, 盛钲钦. LNG冷能用于废气回流朗肯循环及CO2液化新工艺. 科学技术与工程, 2025 , 25 (7) : 2760 -2766 . DOI: 10.12404/j.issn.1671-1815.2403435
Wei-hong HE, Yin-di ZHANG, Ying-nan LI, Xiao-hong HUANG, Zheng-qin SHENG. LNG Cold Energy Used in Exhaust Gas Reflux Rankine Cycle and CO2 Liquefaction Technology[J]. Science Technology and Engineering, 2025 , 25 (7) : 2760 -2766 . DOI: 10.12404/j.issn.1671-1815.2403435
正文
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天然气作为化石能源,因其清洁性被广泛使用,为了方便运输会对其进行液化储存[1]。截至2023年底,中国已投产接收站28座,总接卸能力达1.16亿t/年[2],预计到2040年,全球液化天然气(liquefied natural gas,LNG)需求将达到6.25亿t/年[3]。LNG气化过程中会释放大量冷能,直接排放会造成环境污染和能源浪费[4],所以要将这部分冷能加以利用。LNG冷能的利用方式包括冷能发电、制冷、碳捕获、空气分离、海水淡化等方式[5],而近年来随着化石能源的大规模使用使得CO2大量排放,2023年CO2的排放量达到374亿t,减少CO2排放刻不容缓[6-7],通过利用LNG冷能来发电,在减少能源浪费的同时对CO2进行捕集[8],缓解环境问题。
学者对LNG冷能用于朗肯循环发电和液化CO2进行了大量研究,Sun等[9]提出了利用烃类混合物回收LNG冷能的新型朗肯循环,得出提高膨胀机的入口温度可以提高循环的发电量。薛菲尔等[10]总结了LNG冷能用于朗肯循环结构改进类型,提出了参数研究和结构改进的多样性。黄美斌等[11]提出了使用高温废气作为热源,以LNG作为低温冷源和CO2作为循环工质的CO2跨临界朗肯循环并对系统的参数进行了敏感性分析。刘梅梅等[12]提出了CO2跨临界朗肯循环发电和回收CO2新工艺并且分析了烟气温度、循环工质压力和流量对系统的影响。熊永强等[13]提出了一种集成工艺,保证CO2液化所需的冷能不变,将深冷部分的LNG冷㶲转换为电能,提高系统的㶲效率。曹兴起等[14]提出了低品位热能与LNG综合利用的复合循环系统,实现不同温度区间的循环匹配及热能梯级利用。杨富斌等[15]设计了两级有机朗肯循环尾气余热回收系统,对两级有机朗肯循环系统的热力学性质进行分析。Choi等[16]提出了梯级朗肯循环,并且提出的循环在㶲效率、净功率和热效率指标要明显优于传统循环。
目前利用LNG冷能液化CO2和朗肯循环发电方面已经有很多研究,但这些研究存在缺乏整体分析、工艺流程繁杂和只分析朗肯循环发电过程忽略了LNG冷能液化CO2的工艺改进及CO2的液化率低等问题,针对这些问题,提出一种LNG冷能用于废气回流朗肯循环及CO2液化新工艺,该工艺在常规的朗肯循环基础上设置了再热循环和回热循环并且采用了多流股换热器,使热流回流,提高系统的㶲效率和比功。
1 工艺流程模拟及㶲效率分析
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1.1 LNG冷能用于废气回流朗肯循环及CO2液化的工艺流程
图1中L1~NG(蓝色流股)表示LNG气化为天然气的过程,LNG先经过泵P-1提高自身压力,与换热器HEX-1与CO2进行换热,利用自身冷能将CO2冷却为液体并且进一步冷却循环工质,再依次通过换热器HEX-6、HEX-5、HEX-7换热后逐渐升温至完全气化,使其达到外输要求。
图1中C1~LCO2(红色流股)表示高温废气的余热利用和液化CO2的过程。在废气分离水并液化CO2的过程中,废气通过换热器HEX-3、HEX-4与循环工质换热后,考虑到进入空冷器的流股温度过高会导致空冷器的能量损失过大,导致整个系统的㶲效率降低,故在高温流股进入空冷器之前使其回流至换热器HEX-3,与高温废气一起为CO2循环工质提供热量,使得循环工质进入膨胀机时的温度升高,提升膨胀机的发电能力及系统的效率。高温流股在HEX-3通过回流换热之后进入空冷器进行降温,降温之后在分离器中分离出气体中夹杂的水组分,防止在HEX-7换热器中水组分与低温气体进行换热造成能量损耗,在分离器V-1中分离出大部分水之后,通过换热器HEX-7使其降温至0 ℃并且再一次进行气液分离,防止液体进入压缩机造成压缩机损坏和效率降低,之后通过K-1压缩机加压升温后进入换热器HEX-5与低温气体换热后,进入压缩机K-2再次加压升温后进入换热器HEX-6进行换热,最终进入HEX-1换热器进行液化。
图1中R1~R8(黄色流股)表示朗肯循环利用膨胀机发电的过程,在常规朗肯循环的基础上添加了回热循环和再热循环以及多流股换热器,在换热器HEX-3中使高温废气与回流热流共同与CO2循环工质换热,使循环工质进入膨胀机的温度更高,在换热器HEX-1中使LNG与低温循环工质共同与C12流股换热,使其液化。循环工质R1增压后进入回热器HEX-2换热后,在HEX-3换热器中完全气化后进入膨胀机T-1膨胀作功,经膨胀降温后通过再热器HEX-4通过与高温气体换热后温度升高,之后再次进入膨胀机T-2进行膨胀作功,最后经换热器HEX-2、HEX-1连续降温使其液化,完成一个循环。
1.2 工艺系统能量及㶲效率分析
在对系统进行能量分析过程中假定系统在稳定工况下运行,可以得到膨胀机的输出功、压缩机和泵的能耗。系统的输出净功作为系统的评价指标,故系统净功的定义为
Wnet=WT-WP-WK
式(1)中:Wnet为系统的净功;WT为膨胀机的输出功包括T-1和T-2的输出功;WP为泵的能耗包括P-1和P-2的能耗;WK为压缩机的能耗,包括K-1和K-2的能耗。
在分析整个系统的效率时引入了回收单位质量LNG所输出的净功,即比功也作为系统评价指标,系统比功表示为
w=$\frac{{W}_{net}}{{q}_{mLNG}}$
式(2)中: qmLNG为LNG的质量流量。
定义产品CO2的液化率也作为评价指标[12],计算公式为
YC=$\frac{{q}_{mLC{O}_{2}}}{{{q}_{m}}_{LNG}}$
式(3)中:qmLCO2为液化CO2的质量流量。
系统的㶲效率作为评价系统的关键指标,系统的㶲效率表示为
η=$\frac{\sum {X}_{out}}{\sum {X}_{in}}$
式(4)中:∑Xin为进入系统的㶲流,包括泵和压缩机的输入㶲、LNG所含㶲、废气所含㶲;∑Xout为输出系统的㶲流,包括LNG气化之后的天然气所含㶲、液化后的CO2所含㶲以及膨胀机的输出㶲。
2 模拟结果及分析
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2.1 参数设定
使用化工过程模拟软件对工艺流程进行模拟,状态方程方面,考虑到各物流的热力学性质,由于Peng-Robinson(P-R)状态方程对于天然气热物性的计算较为成熟,故状态方程选择P-R方程[17]。为了简化模拟流程,假设整个系统稳定运行,设定泵的绝热效率为80%,膨胀机和压缩机的绝热效率为90%,换热器压降为10 kPa,空冷器压降为5 kPa,本文中假设燃气轮机为纯氧燃烧,废气中水蒸气与CO2摩尔比为2∶1,朗肯循环工质选取CO2,LNG组分摩尔分数为甲烷90.38%、乙烷5.37%、丙烷4.04%、氮气0.21%。已知CO2的三相点压力为0.518 MPa,温度为-56.6 ℃,本文中设定温度为-56 ℃,压力为520 kPa。
2.2 模拟结果
经过模拟计算,得到表1~表3所示工艺流程的关键参数。
通过模拟与公式计算可知,新工艺性能参数见表4。
2.3 性能参数对比
工艺1[11]、工艺2[12]各自介绍了一种利用LNG冷能液化CO2并且通过循环发电的工艺流程,本文中工艺基于上述的几种流程,增加了废气回流换热。由表5可知,本文工艺相较于已有的工艺流程,其㶲效率、比功和CO2的液化率均有较大的提升。新工艺的液化率比工艺1提高127.73%,比工艺2提高3.62%;新工艺比功比工艺1提高17.97%,比工艺2提高41.31%;新工艺㶲效率比工艺1提高49.08%,比工艺2提高8.97%。
3 工艺参数影响规律分析
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3.1 回流温度对系统的影响
本文中回流温度指的是高温废气经过第一次换热及循环工质换热后再次进入HEX-3换热器的物流温度即C3流股的温度,回流温度是影响整个流程性能的关键参数,由图2可以看出,随着温度的升高,系统的㶲效率和比功都逐渐减小。呈现该规律的原因是:随着温度的升高,C2流股和C3流股之间的温差逐渐减小,导致在换热器中传递给循环工质的热量减少,使得循环工质进入T-2膨胀机的温度降低,导致膨胀机的输出功率减小,导致系统的净功、比功和㶲效率均减小。
3.2 级间冷却温度对系统的影响
改变压缩级间冷却温度即换热器HEX-7和HEX-5换热器热流股的出口温度可知,对压缩机吸气冷却工艺优化设计[18],利用LNG冷能将CO2压缩机进气、压缩机级间压缩气冷却至-40 ℃,以降低CO2压缩机的能耗。考虑到本文中的废气组分中含有水组分,防止水组分在低温条件下冷却结冰堵塞管道,故本文中换热器HEX-7热流出口温度最低为0 ℃,改变压缩机K-1和压缩机K-2的进口温度来分析级间冷却对系统的影响。
在不改变压缩机K-2的进口温度条件下,改变压缩机K-1的进口温度, 㶲效率和比功变化如图3所示,液化率随温度的变化如图4所示。
由图3可以看出,随着压缩机K-1进口温度的不断升高,系统的㶲效率和比功都不断下降, 㶲效率由52.87%下降到52.56%,比功由319.6 kJ/kg LNG下降到317.2 kJ/kg LNG,而随着温度的增加,CO2的液化率提高,由0.611 7 kg/kg LNG提升到0.623 3 kg/kg LNG。对此分析可知,冷却温度增加,换热器HEX-7在进口热流股温度不变的情况下,出口温度增加,级间温度变化会影响到含CO2流股的组分,会导致经过分离器时组分存在差异。此外,冷却温度增加会导致增压设备能耗增加,同时会导致加压后气体温度更高,影响压缩机K-2。由此可知,压缩机K-1的进口温度选择0 ℃时,系统的㶲效率、比功和CO2液化率达到最佳值。
在压缩机K-1进口温度选择0 ℃时,保持压缩机K-1进口温度不变,改变压缩机K-2的进口温度来分析级间冷却对系统的影响。其结果如图5所示。
由于压缩机进口温度在8 ℃时,压缩机进口流股的气相分数为0.998 9会使一部分液体进入压缩机,对压缩机造成损害,故压缩机K-2的进口温度从9 ℃开始。由图5可知,随着压缩机K-2进口温度的增加,系统的㶲效率和比功均减小。㶲效率从52.95%下降到52.87%,比功由321 kJ/kg LNG下降到319.5 kJ/kg LNG。造成这一现象的原因同样是级间温度变化会影响流股的组分而且冷却温度增加会导致压缩机的能耗增加,使得系统的净功减少,导致㶲效率和比功减小。故压缩机K-2最佳的进口温度为9 ℃。
3.3 最高温度和压力对循环的影响
对于循环的性能,循环的最高温度和压力及冷凝温度是形象循环的关键因素,由于本循环的介质为CO2,介质本身受其三相点的限制,因此只分析循环的最高温度和压力对系统的影响。图6、图7所示为循环最高温度和循环最高压力对系统的影响。
由图6、图7可以看出,通过模拟可知,循环最高温度为420 ℃时,最终液化的CO2温度为-57.83 ℃,要低于CO2的三相点温度,包括循环压力超过15 000 kPa时,液化的CO2温度要小于-56 ℃,同样低于三相点温度,故本文模拟中循环最高温度最高取为415 ℃,循环最高压力取15 000 kPa,此时的最高温度和最高压力取得最优值,此时的㶲效率为54.16%,比功为335.9 kJ/kg LNG。由图6、图7可知,循环最高温度和最高压力与㶲效率均有正相关关系,最高压力和最高温度的提高会使系统的㶲效率和比功提高,其中最高温度每增加5℃,比功提高约3.75 kJ/kg LNG,最高压力每增加500 kPa,比功增加约1.3 kJ/kg LNG。
3.4 参数优化
采用优化器对参数进行优化,流程建立且收敛后,可以使用优化器寻找一个使目标函数最小化或最大化的操作条件,采用序贯二次规划算法采用牛顿迭代法约束优化问题[19],序贯二次规划用于求解一连串近似于非线性规划的二次规划即以目标函数为二次函数,约束函数为线性函数的最优化问题[20]。采用Original优化模式对工艺流程的参数进行优化,以最大的㶲效率为目标函数,最高循环温度和压缩机K-2进口温度作为决策变量,液化CO2的温度不低于-56 ℃作为约束函数,最大迭代次数为100次,优化变量范围以及结果见表6,经过优化后使得最高循环温度增加2.1 ℃,压缩机K-2进口温度减少0.3 ℃,使得液化的CO2温度变为-55.97 ℃, 㶲效率提高0.22%,比功增加了0.48%。
4 结论
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(1)本文提出了LNG冷能用于液化CO2和发电的新工艺,对工艺流程进行模拟分析,并与现有工艺进行对比,得到的新工艺的系统㶲效率为54.16%,比功为335.9 kJ/kg LNG,CO2的液化率为0.621 7 kg/kg LNG。
(2)基于㶲分析方法,研究了回流温度、级间冷却温度、循环最高温度和最高压力对工艺流程㶲效率和比功的影响。研究表明: 㶲效率和比功随着回流温度升高而降低,随着压缩机进口温度的升高而降低,随着循环最高温度和最高压力升高而升高。
(3)采用序贯二次规划算法Original优化模式对工艺参数进行优化,经过优化后使得最高循环温度增加2.1 ℃,压缩机K-2进口温度减少0.3 ℃,使得液化的CO2温度变为-55.97 ℃, 㶲效率提高0.22%,比功提高0.48%。
基金
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  • 国家自然科学基金(52274060)
  • 国家自然科学基金(51974033)
  • 长江人才计划领军人才项目(Yz2021239)
文献
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doi: 10.12404/j.issn.1671-1815.2403435
  • 接收时间：2024-05-09
  • 首发时间：2026-03-30
  • 出版时间：2025-03-08
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  • 收稿日期：2024-05-09
  • 修回日期：2024-07-09
基金
国家自然科学基金(52274060)
国家自然科学基金(51974033)
长江人才计划领军人才项目(Yz2021239)
作者信息
    1 长江大学石油工程学院, 武汉 430100
    2 低碳催化与二氧化碳利用国家重点实验室, 兰州 730000
    3 中海油江苏天然气有限责任公司, 盐城 224000

通讯作者:

* 张引弟(1978—),女,汉族,甘肃平凉人,博士,教授。研究方向:油气储运热学与集输节能、CO2捕集与管道输送(CCUS)、燃气技术、管网工艺仿真检测及智能化等。E-mail:。
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2种不同金属材料的力学参数
科
Family		 属数
Number of
genus		 种数
Number of
species		 占总种数比例
Percentage of
total species (%)		 属
Genus		 种数
Number of
species		 占总种数比例
Percentage of total
species (%)
鹅膏菌科Amanitaceae 2 11 5.26 鹅膏菌属 Amanita 10 4.78
小菇科 Mycenaceae 2 12 5.74 丝盖伞属 Inocybe 5 2.39
多孔菌科 Polyporaceae 8 14 6.70 蜡蘑属 Laccaria 5 2.39
红菇科 Russulaceae 3 23 11.00 小皮伞属 Marasmius 6 2.87
小菇属 Mycena 11 5.26
光柄菇属 Pluteus 5 2.39
红菇属 Russula 17 8.13
栓菌属 Trametes 5 2.39
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