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Article(id=1295068231610429854, tenantId=1146029695717560320, journalId=1210938733613449225, issueId=1295068190569164906, articleNumber=null, orderNo=null, doi=10.19666/j.rlfd.202508027, pmid=null, cstr=null, oa=null, hot=null, price=null, onlineType=0, articleFormat=0, articleType=null, articleTypeStr=null, receivedDate=1754928000000, receivedDateStr=2025-08-12, revisedDate=1770998400000, revisedDateStr=2026-02-14, acceptedDate=1772553600000, acceptedDateStr=2026-03-04, onlineDate=1786697927619, onlineDateStr=2026-08-14, pubDate=1782316800000, pubDateStr=2026-06-25, doiRegisterDate=null, doiRegisterDateStr=null, onlineIssueDate=1786697927619, onlineIssueDateStr=2026-08-14, onlineJustAcceptDate=null, onlineJustAcceptDateStr=null, onlineFirstDate=null, onlineFirstDateStr=null, sourceXml=null, magXml=null, createTime=1786697927619, creator=13701087609, updateTime=1786697927619, updator=13701087609, issue=Issue{id=1295068190569164906, tenantId=1146029695717560320, journalId=1210938733613449225, year='2026', volume='55', issue='6', pageStart='1', pageEnd='192', issueExtLink='null', onlineDate='null', pubDate='1782316800000', pubDateStr='2026-06-25', beforeIssueId=null, nextIssueId=null, price=null, status=1, issueComplete=1, articleOrder=1, issueType=1, specialIssue=null, createTime=1786697917835, creator='13701087609', updateTime=1786698816898, updator='13701087609', preIssue=null, nextIssue=null, articleTotal=null, ext={EN=IssueExt(id=1295071961596584952, tenantId=1146029695717560320, journalId=1210938733613449225, issueId=1295068190569164906, language=EN, specialIssueTitle=, coverIllustrator=null, specialIssueEditor=, specialIssueAbout=), CN=IssueExt(id=1295071961596584953, tenantId=1146029695717560320, journalId=1210938733613449225, issueId=1295068190569164906, language=CN, specialIssueTitle=, coverIllustrator=null, specialIssueEditor=, specialIssueAbout=)}, issueFiles=null, downloadFileDto=null}, startPage=102, endPage=114, ext={EN=ArticleExt(id=1295068231794979231, articleId=1295068231610429854, tenantId=1146029695717560320, journalId=1210938733613449225, language=EN, title=Thermodynamic analysis of natural gas SOFC coupled with heat pump for combined heat and power generation system, columnId=1295068192326574197, journalTitle=Thermal Power Generation, columnName=Energy storage technology research, runingTitle=null, highlight=null, articleAbstract=
[Objective]

Conventional combined heating and power (CHP) systems often suffer from suboptimal thermal integration and limited exergy utilization, resulting in low overall energy efficiency and significant carbon emissions. To address these challenges, this study proposes a novel high-efficiency CHP system based on the synergistic integration of a solid oxide fuel cell (SOFC) and a lithium bromide (LiBr) absorption heat pump. The architecture is specifically designed to maximize cascaded energy recovery and enhance comprehensive thermodynamic and economic performance.

[Methods]

A comprehensive steady-state model encompassing thermodynamic and economic analysis was developed to evaluate the system behavior. In the proposed configuration, unreacted fuel in the SOFC anode exhaust is combusted using oxy-fuel technology, yielding a CO2-concentrated flue gas suitable for carbon capture while simultaneously upgrading waste heat quality. The high-temperature flue gas is then recovered through an advanced cascaded heat exchanger network, sequentially enabling cathode air preheating, endothermic methane reforming, and high-pressure steam generation. This steam serves as the thermal driving source for the LiBr absorption heat pump to meet heating demands. A detailed parametric sensitivity analysis was conducted to investigate the effects of the steam-to-carbon ratio, SOFC operating temperature, and fuel utilization factor on key performance indicators.

[Results]

Simulation results show that increasing the steam-to-carbon ratio monotonically reduces both SOFC electrical efficiency and overall thermal energy utilization efficiency, whereas the coefficient of performance (COP) of the absorption heat pump remains stable at approximately 1.72. Higher SOFC operating temperatures significantly improve electrochemical kinetics and flue gas quality, thereby enhancing both electrical and thermal performance. A clear trade-off is observed with fuel utilization: higher fuel utilization factor increases electrical output but diminishes the availability of high-grade heat for downstream recovery. Under optimized conditions (with the steam-to-carbon ratio of 2, temperature of 1 000 ℃, and fuel utilization ratio of 0.85), the system achieves an electrical efficiency of 52%, an exergy efficiency of 56.6%, and an overall thermal energy utilization efficiency of 100.54% (defined on the basis of the fuel’s lower heating value, including all recovered thermal energy). Compared to a conventional natural gas-fired CHP benchmark, the proposed system improves the thermal utilization efficiency by 20%, and increases the exergy efficiency by 2.6%. Economic evaluation yields a levelized cost of exergy of 0.102 6 dollars/(kW·h) and a dynamic payback period of 8 years under current industrial energy pricing.

[Conclusion]

This coupled system significantly improves the energy utilization efficiency and comprehensive performance through the optimization of the energy cascade utilization mode. It demonstrates substantial economic feasibility and potential for engineering applications. The identified influence mechanisms of key parameters provide a theoretical foundation for the optimal design and operational control of such systems.

, authors=Yunjie YANG, Zhewen CHEN, Junjie WEI, Yuming ZHANG, Jiazhou LI, Wei ZHANG, Muyu LIU, authorsList=Yunjie YANG, Zhewen CHEN, Junjie WEI, Yuming ZHANG, Jiazhou LI, Wei ZHANG, Muyu LIU, authorCompany=null, correspAuthors=Zhewen CHEN, 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, fund=null), CN=ArticleExt(id=1295068233128767916, articleId=1295068231610429854, tenantId=1146029695717560320, journalId=1210938733613449225, language=CN, title=天然气SOFC耦合热泵热电联产系统的热力学分析, columnId=1236714914694361723, journalTitle=热力发电, columnName=储能技术研究, runingTitle=null, highlight=null, articleAbstract=
【目的】

为提升热电联产系统的能源利用效率与综合性能，解决传统系统热效率与㶲效率较低的问题，提出一种耦合固体氧化物燃料电池（SOFC）与溴化锂吸收式热泵的新型热电联产系统。

【方法】

首先，构建了系统的热力学与经济性分析模型。该系统利用SOFC进行富氧燃烧，产生的高温烟气依次用于空气预热、甲烷预热、水预热及蒸汽制备，并将所制蒸汽驱动溴化锂吸收式热泵以实现供热；随后，采用参数敏感性分析方法，系统探究了水碳比、SOFC工作温度及燃料利用率3个关键参数对系统性能的影响规律。

【结果】

研究表明：随着水碳比增加，SOFC发电效率与系统热效率呈下降趋势，而热泵性能系数（COP）稳定在1.72左右；随着工作温度升高，发电效率与系统热效率均显著提升；随着燃料利用率提高，发电效率增大，但系统热效率有所降低。在水碳比为2、工作温度1 000 ℃、燃料利用率0.85的优化工况下，系统发电效率达52%，㶲效率为56.6%，热效率达100.54%。相较于参比系统，该系统热效率提升了20%，㶲效率提升2.6%，有效能平准化成本为0.102 6美元/（kW·h），动态投资回收期为8年。

【结论】

该耦合系统通过优化能量梯级利用模式，显著提升了能源利用效率与综合性能，具备良好的经济性与工程应用潜力。研究揭示的关键参数影响机制可为系统优化设计与运行调控提供理论依据。

, authors=杨云杰, 陈哲文, 魏俊杰, 张玉明, 李家州, 张炜, 刘穆禹, authorsList=杨云杰, 陈哲文, 魏俊杰, 张玉明, 李家州, 张炜, 刘穆禹, authorCompany=null, correspAuthors=陈哲文, authorNote=

杨云杰（1999），男，硕士研究生，主要研究方向为热电联供系统，。

, correspAuthorsNote=
陈哲文（1990），男，博士，副教授，主要研究方向为超临界水煤气化基础理论以及发电系统集成与优化，。
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杨云杰（1999），男，硕士研究生，主要研究方向为热电联供系统，。

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杨云杰（1999），男，硕士研究生，主要研究方向为热电联供系统，。

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International Journal of Thermofluids, 2020(5/6): 100039., articleTitle=Latent thermal energy storage technologies and applications: a review, refAbstract=null), Reference(id=1295068242503037490, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1295068231610429854, doi=null, pmid=null, pmcid=null, year=2013, volume=null, issue=null, pageStart=null, pageEnd=null, url=null, language=null, rfNumber=[45], rfOrder=58, authorNames=LAKSHMI T V V S, GEETHANJALI P, KRISHNA P S, journalName=null, refType=null, unstructuredReference=LAKSHMI T V V S, GEETHANJALI P, KRISHNA P S. Mathematical modelling of solid oxide fuel cell using Matlab simulink[C]. 2013 Annual International Conference on Emerging Research Areas and International Conference on Microelectronics, Communications and Renewable Energy. Kanjirapally: IEEE, 2013., articleTitle=Mathematical modelling of solid oxide fuel cell using Matlab simulink, refAbstract=null), Reference(id=1295068242565952051, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1295068231610429854, doi=null, pmid=null, pmcid=null, year=2015, volume=96, issue=null, pageStart=144, pageEnd=150, url=null, language=null, rfNumber=[46], rfOrder=59, authorNames=GUO L J, JIN H, LU Y J, journalName=The Journal of Supercritical Fluids, refType=null, unstructuredReference=GUO L J, JIN H, LU Y J. Supercritical water gasification research and development in China[J]. The Journal of Supercritical Fluids，2015，96：144-150., articleTitle=Supercritical water gasification research and development in China, refAbstract=null)], funds=[Fund(id=1295068237620867571, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1295068231610429854, awardId=52206036; 22278432, language=EN, fundingSource=National Natural Science Foundation of China(52206036; 22278432), fundOrder=null, country=null), Fund(id=1295068237687976436, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1295068231610429854, awardId=52206036; 22278432, language=CN, fundingSource=国家自然科学基金项目(52206036; 22278432), fundOrder=null, country=null), Fund(id=1295068237746696693, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1295068231610429854, awardId=2462024YJRC009, language=EN, fundingSource=Scientific Research Foundation of China University of Petroleum, Beijing(2462024YJRC009), fundOrder=null, country=null), Fund(id=1295068237822194166, 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departmentName=null, remark=中国石油大学（北京）重质油国家重点实验室，北京 102249)])], figs=[ArticleFig(id=1295068235787956701, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1295068231610429854, language=EN, label=Fig.1, caption=Flow chart of the SOFC coupled lithium bromide heat pump system, figureFileSmall=SDxPW7Wlp1CWe9CYkYg6HA==, figureFileBig=ijETun7LXmoe+PL4wtEFww==, tableContent=null), ArticleFig(id=1295068235850871262, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1295068231610429854, language=CN, label=图1, caption=SOFC耦合溴化锂热泵系统流程, figureFileSmall=SDxPW7Wlp1CWe9CYkYg6HA==, figureFileBig=ijETun7LXmoe+PL4wtEFww==, tableContent=null), ArticleFig(id=1295068236027032031, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1295068231610429854, language=EN, label=Fig.2, caption=Energy balance diagram of the system, figureFileSmall=6gDbDC0p5IFHU8xle4saLA==, figureFileBig=XfLYdcYavLSfs0FMFS2aQw==, tableContent=null), 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language=EN, label=Fig.4, caption=Impact of key parameters on system thermal efficiency and SOFC power generation efficiency, figureFileSmall=Qe2dRTO1piu8nj+4+1i4RQ==, figureFileBig=c6hSqlxSKZdtzW9TNY7hOg==, tableContent=null), ArticleFig(id=1295068236349993444, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1295068231610429854, language=CN, label=图4, caption=不同参数对新系统热效率及SOFC发电效率的影响, figureFileSmall=Qe2dRTO1piu8nj+4+1i4RQ==, figureFileBig=c6hSqlxSKZdtzW9TNY7hOg==, tableContent=null), ArticleFig(id=1295068236429685221, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1295068231610429854, language=EN, label=Fig.5, caption=Parametric effects on thermal efficiency of the reference system and SOFC electrical efficiency, figureFileSmall=rbIUpoBsX1GdoCgFKq0xVw==, figureFileBig=nGMskPG/WiMqWGSJQStFmw==, tableContent=null), ArticleFig(id=1295068236492599782, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1295068231610429854, language=CN, label=图5, caption=不同参数对参比系统热效率及SOFC发电效率的影响, figureFileSmall=rbIUpoBsX1GdoCgFKq0xVw==, figureFileBig=nGMskPG/WiMqWGSJQStFmw==, tableContent=null), ArticleFig(id=1295068236559708647, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1295068231610429854, language=EN, label=Fig.6, caption=System economic analysis data, figureFileSmall=t7TRX7ljhOKHkM30lQDw+Q==, figureFileBig=cz/pwqTAdY/wtIqmlAdvjg==, tableContent=null), ArticleFig(id=1295068236639400424, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1295068231610429854, language=CN, label=图6, caption=系统经济分析数据, figureFileSmall=t7TRX7ljhOKHkM30lQDw+Q==, figureFileBig=cz/pwqTAdY/wtIqmlAdvjg==, tableContent=null), ArticleFig(id=1295068236702314985, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1295068231610429854, language=EN, label=Tab.1, caption=

Key calculation results

, figureFileSmall=null, figureFileBig=null, tableContent=
参数数值
能斯特电压/V0.970
欧姆损失/V0.128
活化损失/V0.008
扩散损失/V0.036
工作电压/V0.799
电流/A3.989×106
SOFC电堆功率/kW1 789.00
系统净发电量/kW3 185.29
系统发电效率/%49.53
), ArticleFig(id=1295068236777812458, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1295068231610429854, language=CN, label=表1, caption=

主要计算结果

, figureFileSmall=null, figureFileBig=null, tableContent=
参数数值
能斯特电压/V0.970
欧姆损失/V0.128
活化损失/V0.008
扩散损失/V0.036
工作电压/V0.799
电流/A3.989×106
SOFC电堆功率/kW1 789.00
系统净发电量/kW3 185.29
系统发电效率/%49.53
), ArticleFig(id=1295068236865892843, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1295068231610429854, language=EN, label=Tab.2, caption=

Key node flow parameters of the system

, figureFileSmall=null, figureFileBig=null, tableContent=
物流温度/℃压力/MPa摩尔流量/（kmol·s–1）组成摩尔占比/%
125.00.1000.050O2：21，H2：79
3760.01.5000.050O2：21，H2：79
41 000.01.5000.076O2：0.2，N2：51.7，CH4：2.1，H2O：32.9，H2：4.8，CO2：6.7，CO：1.7
51 000.01.5000.040O2：0.4，N2：99.6
6492.00.1000.040O2：0.4，N2：99.6
71 000.01.5000.037CH4：4.3，H2O：68.3，H2：9.9，CO2：13.9，CO：3.5
82 114.01.5000.040O2：0.8，H2O：79.3，CO2：19.8
1340.01.5000.040O2：0.8，H2O：79.3，CO2：19.8
1425.00.1000.008CH4：100
15264.01.5000.008CH4：100
16800.01.5000.008CH4：100
17750.01.5000.029CH4：5.5，H2O：5.5，H2：66.7，CO：22.3
18220.01.5000.037CH4：4.3，H2O：12.2，H2：66.1，CO2：13.9，CO：3.5
1925.00.1000.016H2O：100
26133.00.6000.048H2O：100
2769.00.0041.006H2O：63.6，LiBr：36.4
3564.00.0040.679H2O：63.6，LiBr：36.4
3645.00.7001.234H2O：100
4229.00.0040.035H2O：100
4369.00.0041.006H2O：63.6，LiBr：36.4
4435.00.1000.400H2O：100
), ArticleFig(id=1295068236945584620, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1295068231610429854, language=CN, label=表2, caption=

系统关键点物流参数

, figureFileSmall=null, figureFileBig=null, tableContent=
物流温度/℃压力/MPa摩尔流量/（kmol·s–1）组成摩尔占比/%
125.00.1000.050O2：21，H2：79
3760.01.5000.050O2：21，H2：79
41 000.01.5000.076O2：0.2，N2：51.7，CH4：2.1，H2O：32.9，H2：4.8，CO2：6.7，CO：1.7
51 000.01.5000.040O2：0.4，N2：99.6
6492.00.1000.040O2：0.4，N2：99.6
71 000.01.5000.037CH4：4.3，H2O：68.3，H2：9.9，CO2：13.9，CO：3.5
82 114.01.5000.040O2：0.8，H2O：79.3，CO2：19.8
1340.01.5000.040O2：0.8，H2O：79.3，CO2：19.8
1425.00.1000.008CH4：100
15264.01.5000.008CH4：100
16800.01.5000.008CH4：100
17750.01.5000.029CH4：5.5，H2O：5.5，H2：66.7，CO：22.3
18220.01.5000.037CH4：4.3，H2O：12.2，H2：66.1，CO2：13.9，CO：3.5
1925.00.1000.016H2O：100
26133.00.6000.048H2O：100
2769.00.0041.006H2O：63.6，LiBr：36.4
3564.00.0040.679H2O：63.6，LiBr：36.4
3645.00.7001.234H2O：100
4229.00.0040.035H2O：100
4369.00.0041.006H2O：63.6，LiBr：36.4
4435.00.1000.400H2O：100
), ArticleFig(id=1295068237016887789, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1295068231610429854, language=EN, label=Tab.3, caption=

Exergy destruction distributions across the system components

, figureFileSmall=null, figureFileBig=null, tableContent=
项目本文新系统占比/%参比系统占比/%
㶲输入/kW甲烷6 884.098.86 884.099.3
热网回水59.00.825.00.4
纯氧23.20.423.20.3
总计6 966.2100.06 932.2100.0
㶲输出/kW系统净发电量3 042.045.13 042.043.9
烟气22.50.322.50.3
高温热水62.50.83004.3
热网供水818.412.1500.07.2
㶲损失/kW换热器1129.01.8129.01.9
换热器262.00.962.00.9
换热器31 180.017.01 396.020.1
换热器473.01.050.00.7
换热器5187.02.6135.72.0
换热器6163.02.3145.02.1
换热器7107.01.574.01.1
换热器8247.03.5218.03.1
换热器949.00.737.00.5
压气机126.00.426.00.4
压气机24.00.14.00.1
燃烧室86.01.286.01.2
冷凝器222.03.1222.03.2
透平70.01.070.01.0
节流阀6.00.13.00.1
SOFC模拟器410.03.7410.05.8
总计6 966.2100.06 932.2100.0
㶲效率56.6%55.7%
), ArticleFig(id=1295068237083996654, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1295068231610429854, language=CN, label=表3, caption=

系统各部件㶲损占比

, figureFileSmall=null, figureFileBig=null, tableContent=
项目本文新系统占比/%参比系统占比/%
㶲输入/kW甲烷6 884.098.86 884.099.3
热网回水59.00.825.00.4
纯氧23.20.423.20.3
总计6 966.2100.06 932.2100.0
㶲输出/kW系统净发电量3 042.045.13 042.043.9
烟气22.50.322.50.3
高温热水62.50.83004.3
热网供水818.412.1500.07.2
㶲损失/kW换热器1129.01.8129.01.9
换热器262.00.962.00.9
换热器31 180.017.01 396.020.1
换热器473.01.050.00.7
换热器5187.02.6135.72.0
换热器6163.02.3145.02.1
换热器7107.01.574.01.1
换热器8247.03.5218.03.1
换热器949.00.737.00.5
压气机126.00.426.00.4
压气机24.00.14.00.1
燃烧室86.01.286.01.2
冷凝器222.03.1222.03.2
透平70.01.070.01.0
节流阀6.00.13.00.1
SOFC模拟器410.03.7410.05.8
总计6 966.2100.06 932.2100.0
㶲效率56.6%55.7%
), ArticleFig(id=1295068237251768815, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1295068231610429854, language=EN, label=Tab.4, caption=

Price list of the system components

, figureFileSmall=null, figureFileBig=null, tableContent=
部件价格/美元占比/%
压气机15.03×1064.34
压气机29.61×1050.83
换热器11.78×1050.15
换热器28.24×1040.07
换热器31.08×1060.93
换热器46.12×1050.53
换热器53.19×1050.28
换热器63.96×1050.34
换热器74.39×1050.38
换热器85.66×1050.49
换热器94.81×1050.41
燃烧室7.56×1050.65
燃气轮机1.03×1078.88
重整反应器1.01×1078.71
变换反应器4.61×1063.97
SOFC5.31×10745.78
空气分离器2.70×10723.28
总计1.16×108100.00
), ArticleFig(id=1295068237344043504, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1295068231610429854, language=CN, label=表4, caption=

系统各部件价格

, figureFileSmall=null, figureFileBig=null, tableContent=
部件价格/美元占比/%
压气机15.03×1064.34
压气机29.61×1050.83
换热器11.78×1050.15
换热器28.24×1040.07
换热器31.08×1060.93
换热器46.12×1050.53
换热器53.19×1050.28
换热器63.96×1050.34
换热器74.39×1050.38
换热器85.66×1050.49
换热器94.81×1050.41
燃烧室7.56×1050.65
燃气轮机1.03×1078.88
重整反应器1.01×1078.71
变换反应器4.61×1063.97
SOFC5.31×10745.78
空气分离器2.70×10723.28
总计1.16×108100.00
), ArticleFig(id=1295068237406958065, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1295068231610429854, language=EN, label=Tab.5, caption=

Comparative analysis of the reference systems in literatures

, figureFileSmall=null, figureFileBig=null, tableContent=
文献编号系统总效率/%㶲效率/%SOFC电效率/%热源利用方式备注
[18]50~6045~5550~60SOFC尾气显热（液态水）CLC联产系统
[19]62.5055~6555~60LT-SOFC与HT-PEMFC耦合混合燃料电池系统
[30]70.4957.2960~65SOFC余热驱动溴化锂制冷多联产系统
[32]75~8065~7060~65超临界水气化+SOFC近零排放系统
[33]78.3065~7055~60吸收式热泵碳捕集医院CCHP系统
[20]80.0070~7560~65SOFC-GT+太阳能辅助吸收式机组光热互补系统
[21]78.3068~7350~55SOFC余热显热（热水）医院场景动态分析
[34]65~7055~6055~60SOFC冷热电联供梯级利用系统配置优化研究
[26]80.70（光热）33.8055~60太阳能PEMEC-SOFC多联产光热储一体化
[41]85~9070~75吸收式热泵（潜热利用）工质对性能综述
本文新系统100.5456.6%52SOFC余热驱动溴化锂制热多联产系统
), ArticleFig(id=1295068237486649842, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1295068231610429854, language=CN, label=表5, caption=

不同参考文献系统对比

, figureFileSmall=null, figureFileBig=null, tableContent=
文献编号系统总效率/%㶲效率/%SOFC电效率/%热源利用方式备注
[18]50~6045~5550~60SOFC尾气显热（液态水）CLC联产系统
[19]62.5055~6555~60LT-SOFC与HT-PEMFC耦合混合燃料电池系统
[30]70.4957.2960~65SOFC余热驱动溴化锂制冷多联产系统
[32]75~8065~7060~65超临界水气化+SOFC近零排放系统
[33]78.3065~7055~60吸收式热泵碳捕集医院CCHP系统
[20]80.0070~7560~65SOFC-GT+太阳能辅助吸收式机组光热互补系统
[21]78.3068~7350~55SOFC余热显热（热水）医院场景动态分析
[34]65~7055~6055~60SOFC冷热电联供梯级利用系统配置优化研究
[26]80.70（光热）33.8055~60太阳能PEMEC-SOFC多联产光热储一体化
[41]85~9070~75吸收式热泵（潜热利用）工质对性能综述
本文新系统100.5456.6%52SOFC余热驱动溴化锂制热多联产系统
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天然气SOFC耦合热泵热电联产系统的热力学分析
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杨云杰 , 陈哲文 , 魏俊杰 , 张玉明 , 李家州 , 张炜 , 刘穆禹
热力发电 | 储能技术研究 2026,55(6): 102-114
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热力发电 |储能技术研究 2026 , 55 (6) : 102 -114
天然气SOFC耦合热泵热电联产系统的热力学分析
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杨云杰 , 陈哲文 , 魏俊杰, 张玉明, 李家州, 张炜, 刘穆禹
作者信息
  • 中国石油大学（北京）重质油国家重点实验室，北京 102249
通讯作者:
陈哲文（1990），男，博士，副教授，主要研究方向为超临界水煤气化基础理论以及发电系统集成与优化，。
作者简介:

杨云杰（1999），男，硕士研究生，主要研究方向为热电联供系统，。

Thermodynamic analysis of natural gas SOFC coupled with heat pump for combined heat and power generation system
Yunjie YANG , Zhewen CHEN , Junjie WEI, Yuming ZHANG, Jiazhou LI, Wei ZHANG, Muyu LIU
Affiliations
  • State Key Laboratory of Heavy Oil Processing, China University of Petroleum, Beijing 102249, China
出版时间: 2026-06-25 doi: 10.19666/j.rlfd.202508027
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摘要
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【目的】

为提升热电联产系统的能源利用效率与综合性能，解决传统系统热效率与㶲效率较低的问题，提出一种耦合固体氧化物燃料电池（SOFC）与溴化锂吸收式热泵的新型热电联产系统。

【方法】

首先，构建了系统的热力学与经济性分析模型。该系统利用SOFC进行富氧燃烧，产生的高温烟气依次用于空气预热、甲烷预热、水预热及蒸汽制备，并将所制蒸汽驱动溴化锂吸收式热泵以实现供热；随后，采用参数敏感性分析方法，系统探究了水碳比、SOFC工作温度及燃料利用率3个关键参数对系统性能的影响规律。

【结果】

研究表明：随着水碳比增加，SOFC发电效率与系统热效率呈下降趋势，而热泵性能系数（COP）稳定在1.72左右；随着工作温度升高，发电效率与系统热效率均显著提升；随着燃料利用率提高，发电效率增大，但系统热效率有所降低。在水碳比为2、工作温度1 000 ℃、燃料利用率0.85的优化工况下，系统发电效率达52%，㶲效率为56.6%，热效率达100.54%。相较于参比系统，该系统热效率提升了20%，㶲效率提升2.6%，有效能平准化成本为0.102 6美元/（kW·h），动态投资回收期为8年。

【结论】

该耦合系统通过优化能量梯级利用模式，显著提升了能源利用效率与综合性能，具备良好的经济性与工程应用潜力。研究揭示的关键参数影响机制可为系统优化设计与运行调控提供理论依据。

固体氧化物燃料电池  /  溴化锂吸收式热泵  /  热电联产  /  能效评估  /  动态投资回收期
[Objective]

Conventional combined heating and power (CHP) systems often suffer from suboptimal thermal integration and limited exergy utilization, resulting in low overall energy efficiency and significant carbon emissions. To address these challenges, this study proposes a novel high-efficiency CHP system based on the synergistic integration of a solid oxide fuel cell (SOFC) and a lithium bromide (LiBr) absorption heat pump. The architecture is specifically designed to maximize cascaded energy recovery and enhance comprehensive thermodynamic and economic performance.

[Methods]

A comprehensive steady-state model encompassing thermodynamic and economic analysis was developed to evaluate the system behavior. In the proposed configuration, unreacted fuel in the SOFC anode exhaust is combusted using oxy-fuel technology, yielding a CO2-concentrated flue gas suitable for carbon capture while simultaneously upgrading waste heat quality. The high-temperature flue gas is then recovered through an advanced cascaded heat exchanger network, sequentially enabling cathode air preheating, endothermic methane reforming, and high-pressure steam generation. This steam serves as the thermal driving source for the LiBr absorption heat pump to meet heating demands. A detailed parametric sensitivity analysis was conducted to investigate the effects of the steam-to-carbon ratio, SOFC operating temperature, and fuel utilization factor on key performance indicators.

[Results]

Simulation results show that increasing the steam-to-carbon ratio monotonically reduces both SOFC electrical efficiency and overall thermal energy utilization efficiency, whereas the coefficient of performance (COP) of the absorption heat pump remains stable at approximately 1.72. Higher SOFC operating temperatures significantly improve electrochemical kinetics and flue gas quality, thereby enhancing both electrical and thermal performance. A clear trade-off is observed with fuel utilization: higher fuel utilization factor increases electrical output but diminishes the availability of high-grade heat for downstream recovery. Under optimized conditions (with the steam-to-carbon ratio of 2, temperature of 1 000 ℃, and fuel utilization ratio of 0.85), the system achieves an electrical efficiency of 52%, an exergy efficiency of 56.6%, and an overall thermal energy utilization efficiency of 100.54% (defined on the basis of the fuel’s lower heating value, including all recovered thermal energy). Compared to a conventional natural gas-fired CHP benchmark, the proposed system improves the thermal utilization efficiency by 20%, and increases the exergy efficiency by 2.6%. Economic evaluation yields a levelized cost of exergy of 0.102 6 dollars/(kW·h) and a dynamic payback period of 8 years under current industrial energy pricing.

[Conclusion]

This coupled system significantly improves the energy utilization efficiency and comprehensive performance through the optimization of the energy cascade utilization mode. It demonstrates substantial economic feasibility and potential for engineering applications. The identified influence mechanisms of key parameters provide a theoretical foundation for the optimal design and operational control of such systems.

solid oxide fuel cell  /  lithium bromide absorption heat pump  /  cogeneration  /  energy efficiency evaluation  /  dynamic payback period
杨云杰, 陈哲文, 魏俊杰, 张玉明, 李家州, 张炜, 刘穆禹. 天然气SOFC耦合热泵热电联产系统的热力学分析. 热力发电, 2026 , 55 (6) : 102 -114 . DOI: 10.19666/j.rlfd.202508027
Yunjie YANG, Zhewen CHEN, Junjie WEI, Yuming ZHANG, Jiazhou LI, Wei ZHANG, Muyu LIU. Thermodynamic analysis of natural gas SOFC coupled with heat pump for combined heat and power generation system[J]. Thermal Power Generation, 2026 , 55 (6) : 102 -114 . DOI: 10.19666/j.rlfd.202508027
正文
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在全球能源结构低碳转型背景下，传统化石能源的高碳稳定性与可再生能源的低碳间歇性矛盾日益凸显[1]。国际能源署（IEA）数据显示，2023年全球化石能源仍占一次能源消费的80%以上，其中天然气作为“桥梁能源”占比达24%，在能源转型中承担关键过渡角色[2]。2023年全球天然气需求同比增长1.5%（590亿m3）[3]。预计2024年将进一步增长2.1%（870亿m3），贡献全球能源新增需求的40%以上[4]。
然而，天然气主流利用方式——直接燃烧发电技术的应用面临双重瓶颈：
1）碳排放强度超标，碳排放强度0.4~0.5 kg/（kW·h）远超“双碳”目标限值（0.1 kg/（kW·h））[5]；
2）能效提升见顶，传统燃气-蒸汽联合循环效率逼近理论极限（<65%）[6]。
此矛盾揭示：亟需突破燃烧化学能转化范式，开发新型高效低碳天然气利用技术[7]。固体氧化物燃料电池（SOFC）因其燃料灵活性与高能效特性成为突破方向[8]。天然气在SOFC内发生电化学反应，化学能直接转化为电能，效率可达到50%~60%[9]。其高温尾气（700~900 ℃）可进一步回收，整体能源转化效率可突破85%[10]。在分布式场景中，SOFC因小型化、模块化特性，可摆脱对集中式电网的依赖，实现就地供能，碳排放强度较燃气联合循环降低30%~40%[11]。然而，其中温余热（300~500 ℃）利用率不足导致㶲损失大于15%[12-15]，成为系统能效提升的首要瓶颈。
针对SOFC中温余热（300~500 ℃）利用率较低的问题，近年来学者们提出将SOFC与溴化锂吸收式热泵耦合的创新系统。该方案将SOFC排放的余热作为吸收式热泵的热源，实现能源品位温度对口、梯级利用[16-19]。Zhang等人[19]构建的SOFC-LiBr系统实验表明，耦合后系统综合能源利用效率提升至92%；Ran等人[20]引入超临界CO2循环与溴化锂制冷技术，综合能效可达70.49%；Wang等人[21]提出基于吸收式热泵的热电联产系统，总热效率提升至61.8%。此外，SOFC与可再生能源的耦合（如太阳能、生物质等）也展示了良好的脱碳潜力[22-23]。
然而，深入分析上述文献发现，现有研究在SOFC与溴化锂热泵的耦合设计中，高温热源多依赖液态水的显热传递（如80~150 ℃热水驱动热泵）。这种显热驱动模式存在显著的技术缺陷：首先，受限于液态水较低的能量密度与换热过程中的大温差不可逆损失，传统系统的综合热效率通常难以突破85%，且热泵性能系数（COP）普遍被限制在1.2~1.6[24-25]；其次，基于显热的余热回收模式需配置大流量循环水泵，导致系统寄生功耗增加，进一步削弱了系统在变工况下的适应性与经济性[26-31]。
针对上述瓶颈，本文从热力学能量梯度利用原则出发，提出以富氧燃烧产生的高温烟气制取高压水蒸气，并以水蒸气相变潜热替代液态水显热作为溴化锂热泵的高温驱动源。其优势在于：一方面，水蒸气的相变潜热较液态水显热高5~8倍，能够显著提升热源端的能量密度，缩小换热器体积；另一方面，通过蒸汽驱动可显著减小换热过程中的传热温差损失，使热源品位与两级吸收循环实现精准深度匹配。模拟表明，该设计有望将系统总热效率由传统的80%提升至100%以上，并将热泵COP提升至1.7以上。本文提出以水蒸气替代液态水作为溴化锂热泵的高温热源，利用SOFC烟气中的高温热源，结合两级吸收循环实现余热品位的深度匹配。这一创新为SOFC-热泵耦合系统的能效突破与工程化推广提供了新路径。
1　系统描述
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图1给出了SOFC热电联产系统的流程。整个系统主要由2部分组成：SOFC发电与尾气回收子系统（上循环），溴化锂吸收式热泵子系统（下循环）。
SOFC发电与尾气回收子系统以天然气（主要成分CH4）为燃料，通过燃料预处理、SOFC发电与尾气回收实现发电与热源制备。具体流程如下：甲烷经压缩机加压后，与系统高温尾气进行换热，随后与重整水混合进入SOFC内部重整器，发生蒸汽重整反应生成H2和CO；生成的合成气再与部分水进入变换器，通过水煤气变换反应转化为H2和CO2。氢气随后进入燃料电池阳极，与经压缩并预热后的空气发生电化学反应直接发电并释放热量。与此同时，重整水经水泵加压后分别进入重整器与变换器参与反应。SOFC排出的高温尾气首先经过分离器，分离出的残余空气经冷却后排放；剩余富含未反应燃料的尾气则进入燃烧室充分燃烧，产生更高温的烟气。该高温烟气随后依次流经4个换热器，实现热量梯级回收，依次预热压缩后的空气、压缩后的甲烷气体、重整水，最终用于加热并产生饱和蒸汽，作为驱动溴化锂吸收式热泵系统的高温热源。
该溴化锂吸收式热泵子系统由发生器、冷凝器、蒸发器、吸收器及溶液热交换器构成，旨在利用SOFC子系统产出的200 ℃饱和蒸汽为驱动热源，回收35 ℃工业废水等低位热能，将45 ℃的热网回水提升至80~85 ℃。在循环过程中，驱动蒸汽在发生器内加热稀溴化锂溶液并析出制冷剂蒸汽，该蒸汽随后在冷凝器中冷凝放热，实现对热网回水的二次加热；冷凝后的液态制冷剂经节流降压进入蒸发器，吸收低温热源热量气化后进入吸收器，被来自发生器的浓溶液吸收并释放溶解热，完成对热网回水的一次加热。在溶液循环侧，吸收器输出的稀溶液经泵增压，进入溶液热交换器吸收来自发生器的高温浓溶液余热，实现回热升温后返回发生器，从而维持工质的持续循环。在热能输出侧，系统通过耦合吸收热与冷凝热的梯级放热机制，对热网回水进行分段加热，在显著提升低品位能源回收效率的同时，实现了能量的高效转化与梯级利用。
参比系统与原系统不同的地方在于，进入热泵系统的高温热源由原来的驱动蒸汽变为了高温驱动水。其优点是减少了相变，缺点是整个热泵系统无法利用水的潜热，导致整个系统的能量利用效率降低。参比系统的流程与原系统一致。
2　数学建模与评价
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本文采用AspenPlus软件对SOFC热电联产系统进行仿真。本文所采用的SOFC电化学模型已在课题组前期研究中得到了详细验证[32-45]。选择ELECNRTL模型[28]作为全局物性方法，为了简化模拟过程，便于计算，模拟过程做如下假设：
1）所有运行单元均忽略热损失与压力损失；
2）热评价基于稳定的模拟过程，化学反应处于化学平衡状态；
3）空气由21%（摩尔分数）的氧气和79%的氮气组成，环境温度设定为25 ℃，压力为101.325 kPa；
4）只考虑CO2的分离，不考虑CO2的压缩和储存。
2.1　SOFC模型[28-29，32]
甲烷需要经过重整变换生成氢气作为燃料电池的燃料，SOFC中的重整变换反应和电化学反应如下：
甲烷重整反应：
CH4+H2O→CO+3H2
变换反应：
CO+H2O→CO2+H2
SOFC中发生的总电化学反应：
2H2+O2→2H2O
SOFC电流和电流密度计算式为：
I=e×(nH2+nCO+4nCl)×F×Ufuel
i=INcellAac
式中：I为电流，A；e为电子数，以氢气为燃料时，e=2；nH2、nCO、nC1为氢气、一氧化碳、甲烷的质量流量，mol/s；F为法拉第常数，96 485 c/mol；i为电流密度，A/m2；Ufuel为燃料利用率；Aac为有效表面积；Ncell为电池数量。
SOFC电压计算式为：
V=EN−Vact−Vohmic−VCONC
式中：V、EN、Vact、Vohmic、VCONC分别为实际输出电压、能斯特电压、激活极化电压、欧姆极化电压、浓度极化电压，V。
能斯特电压计算公式为：
EN=E0−RTUFlnPH2OPH2PO212
式中：E0为标准态可逆电压，V；R为理想气体常数，R=8.314 kJ/（kmol·K）；T为工作温度，K；Pi为H2O、H2和O2的平均分压，Pa；U为电化学过程中转移的电子数，以氢为燃料时U=2。
氢气作为燃料时，燃料电池在标准状态下的可逆电压（E0）计算式为：
E0=1.253−2.451 6×10−4T
欧姆极化计算公式为：
Vohmic=i∑krk
rk=∑kρkδkASOFC
ρk=∑kakexp(bkT)
式中：rk为欧姆电阻，Ω；ρk为材料电阻率；系数ak和bk与材料有关，是温度的指数函数；δk为各组分的厚度，mm；ASOFC为电池堆的激活面积，m2。
利用Butler-Volmer方程可以确定激活极化电压，B-V方程变形可以得到阴极和阳极的激活极化电压方程：
Valign=Vact,a+Vact,c
Vact,a=2RTeFsinh−1(i2i0,a)
Vact,c=2RTeFsinh−1(i2i0,c)
式中：Vact，a为阳极极化电压，V；Vact，c为阴极极化电压，V；i0，c和i0，a分别为阴极和阳极的交换电流密度，A/cm2。
i0,a=γa⋅(PH2PRef)(PH2OPRef)exp(−Eact,aRT)
i0,c=γc⋅(PO2PRef)0.25exp(−Eact,cRT)
式中：γa和γc为阳极和阴极扩散系数，A/cm2；Eact，c和Eact，a分别为阴极和阳极的活化能；PRef为参考压强，Pa。
SOFC温度高，浓度极化很小，浓度极化电压可以忽略不计。浓度极化电压的公式为：
Vconc=RT2Fln(1−ii1)
式中：il为极限电流密度，A/cm2。
2.2　经济模型
单位小时运行成本是1 h内消耗的总成本，包括燃料成本、固定设备成本、运行维护成本、二氧化碳排放成本等。计算总成本率为：
Z˙TOTAL=Z˙fuel+Z˙K,TOTAL−Z˙env=Z˙fuel+(Z˙K+Z˙OM)−Z˙env
式中：Zfuel、ZK，TOTAL、ZK、ZOM和Zenv分别为燃料、固定投资、设备投资、运行维护和二氧化碳排放的成本率，美元/h。该系统不产生二氧化碳，节省了二氧化碳排放成本。因此，二氧化碳排放成本需要从总支出中减去。使用下式计算燃料成本率，燃料成本率表示每小时燃料消耗所花费的总费用：
Z˙fuel=Cfuel×Mfuel×LHV
式中：Cfuel为燃料价格，其值为7.6美元/kJ；Mfuel为燃料流量，kg/h；LHV为燃料的低位热值，kJ/kg。
固定投资成本率表示每小时用于系统运行的设备支出，包括投资、运行、维护等成本。计算公式为：
Z˙TOTAL=∑KZK×CRF×φN
式中：∑KZK为各设备总投资；N为年运行时数，取8 000 h[36]；φ为运行维护系数，取1.06；资本回收系数（CRF）为固定年金与投资期间收到的年金现值之比，计算方法如下：
CRF=ir(1+ir)y(1+ir)y−1
式中：i为利率，取12%；y为系统生命周期，取20年。
二氧化碳排放成本率是每小时排放二氧化碳所支付的成本，计算方法如下：
Z˙env=CCO2×mCO2
式中：CCO2为CO2的排放价格，取0.045美元/kg；mCO2为CO2排放流量，kg/h。
热电联产系统的平准化㶲成本（LCOE），即包括电和热水在内的㶲平准化成本，计算方法如下：
LCOE=Z˙TOTALWnet+EXH
式中：LCOE为能源平准化成本，美元/（kW·h）；Wnet为净输出功率，kW；EXH为输出热耗，kW。
持续升级平准化因子（CELF）的计算方法如下：
CELF=kOM×(1−kOMn)1−kOM×CRF
kOM=1+r1+ir
式中：r为通货膨胀率，取2%。
热电联产系统年净利润AP为：
AP=((Wnet×CELE+QH×CH)×N−FIC×CELF×φ)×(1−τ)
式中：CELE为电价，取0.2美元/（kW·h）；CH为供热价格，取0.024美元/（kW·h）[24]；FIC为固定投资成本，美元；φ=0.06；τ为税率，取25%；QH为年输出热量，kW。
固定投资成本（FIC）和总投资成本（TIC）的计算方法如下：
FIC=∑KZk×φ
TIC=FIC+(Z˙fuel−Z˙env)×N
投资回收期（DPP）的计算方法如下：
DPP=ln(TIC×(r−ir)AP+1)ln(1+r1+ir)
2.3　㶲模型
有效能即能转化为功的那部分能量。本系统的㶲包括化学㶲和物理㶲，计算方法如下：
ex=exph+exch
exph=∑xi[H−H0−T0(S−S0)]i
exch=∑xiexch0,i+8.314T0∑xilnxi
式中：exph为物流的物理能量，kJ/mol；exch为物流的化学能，kJ/mol；xi为组分i的摩尔分数；T0为环境温度298.15K；H0和H分别表示标准和工作条件下的摩尔焓，kJ/mol；S0和S分别表示标准和工作条件下的摩尔熵，kJ/（mol⋅K）；exch0,i为标准条件下组分i的摩尔化学能，kJ/mol。
热耗计算公式如下：
EXH=Q(1−T0T)
式中：EXH为热耗，kW；T为加热温度，K。
3　效率评价指标
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效率指标是评价绩效优势的基础。本文采用的主要效率指标包括发电效率（ηELE）、燃料电池效率（ηSOFC）、㶲效率（ηEXE）和热效率（ηTOTAL）。
燃料电池效率的计算公式为：
ηSOFC=WSOFCnfuel×LHV
式中：WSOFC为SOFC的交流功率，kW；nfuel为燃油流量，mol/s；LHV表示甲烷低位热值，kJ/mol。
发电效率计算公式为：
ηELE=WSOFC+WGT+WST−WCONSnfuel×LHV
式中：WGT为燃气轮机输出功，kW；WST为汽轮机输出功，kW；WCONS为燃油压缩机、水泵和空压机消耗的总功率，kW。
总热效率（ηTOTAL）计算公式如下：
ηTOTAL=WSOFC+WGT+WST+QH−WCONSnfuel×LHV
式中：QH为输出热量，kW。系统的净输出电功定义为：
Wnet,elec=WSOFC+WGT+WST−WCONS
因此，式（36）可转化为：
ηtotal=Wnet,elec+QHmfuel⋅LHV
输出热量QH可表示为：
QH=Qabsorber+Qcondenser+Qambient
式中：Qabsorber为吸收器的放热量；Qcondenser为冷凝器的放热量；Qambient为从环境中获得的热量，并非燃料输入的化学能。因此，系统净输入功和输出热量之和可能大于燃料低位热值的总和，总系统热效率可能大于100%。
燃料充分燃烧所产生的热量称为热值，根据燃烧产物中水的相态，即蒸汽或液体，分为高热值（HHV）和低热值（LHV）。甲烷燃烧产生的水蒸气进入换热网络生产生活热水，而大部分水蒸气在该系统中通过热交换冷凝成液态水。因此，在计算总热效率时，燃料的能量输入基于低位热值计算。
㶲效率ηEXE计算如下：
ηEXE=WSOFC+WGT+WST+EXH−WCONSnfiuel×EXin
式中：EXH为提供给热用户的热耗，kW；EXin为甲烷的标准摩尔化学能，kJ/mol。
4　结果与讨论
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4.1　计算结果
用AspenPlus软件对本文搭建的系统进行模拟，并以文献[46]中的实验数据为初始数据，甲烷的摩尔流量为0.008 kmol/s，溴化锂的质量分数为0.58，重整变换水的摩尔流量为0.016 kmol/s，主要计算结果见表1。SOFC内部的欧姆损失、扩散损失和活化损失无法避免，系统关键点物流参数见表2。
4.2　系统能量平衡和㶲平衡
对系统进行能量平衡分析，得到如图2所示的能流平衡图。
本系统总输入能量为甲烷的低位热值，系统净发电量包括SOFC发电量、燃气透平发电量、吸收器放热和冷凝器放热，SOFC发电量占系统总输入能量的50%。从图2中可以看出，系统总输出量大于总输入量。这是因为：吸收式溴化锂系统热泵使用少量的高温热源和低温热源可以制取大量中温热源，导致热泵的COP可以达到1.5~1.7，所以总的系统效率大于1。另外，系统耗功部件主要由压气机、水泵和燃烧室组成；整个系统的效率为100.54%。
新系统和参比系统的㶲平衡如表3所示。系统的总输入㶲为6 966.2 kW，其中甲烷的输入㶲占98.8%，其余㶲输入包括热网回水和纯氧；系统的总㶲输出包括系统净发电量、高温热水、烟气和热网供水，占总㶲输入的56.6%；系统各部件都存在㶲损失，其中换热器3㶲损最大。这是由于换热器3有3股流体需要换热，且换热温差较大，换热过程中还存在相变，所以㶲损失在整个系统中占比最大，占比为17%，系统的总㶲效率为56.6%。
换热器3是连接燃烧室与热泵发生器的关键部件，也是发生相变的场所，该部件㶲损可分为传热不可逆㶲损和流阻不可逆㶲损。相较于参比系统，新系统中换热器3利用相变过程的等温特性，削减了换热器内的无效传热温差，从而降低了传热引起的㶲损。
4.3　敏感性分析
前文研究了SOFC燃料利用率为0.85、工作温度1 000 ℃、压力15 MPa、水碳比为2时系统的热力学性能。本节讨论不同水碳比、不同氢气转化率、不同SOFC工作温度工况对系统效率的影响规律。不同参数对系统热效率的影响如图3所示。分析图3可知，本系统把驱动热泵系统的高温热源由水变为水蒸气，使系统的总效率提升了24%。通过敏感性对比分析可知，水碳比、SOFC工作温度、氢气转化率对2个系统的效率影响趋势相同。
图4为不同参数对新系统热效率及SOFC发电效率的影响。从图4a）可以看出，随着水碳比的增加，系统的总效率降低。原因为：水碳比增加，导致SOFC发电效率降低；水碳比增加，进入燃烧室的水增多，水的比热容增大，燃烧室中存在大量水分，会吸收燃烧后产生的部分热量，降低燃烧后的温度；水蒸发吸热，进一步导致燃烧后的温度降低。
从图4b）可以看出，随着SOFC工作温度的升高，系统总效率升高。原因为：SOFC工作温度升高，SOFC发电效率升高，热电联产总效率升高；SOFC工作温度升高，SOFC出口温度升高，进入热泵的总热量升高，热电总效率升高。从图4c）可以看出，随着氢气转化率升高，系统的总效率降低。原因为：随着氢气转化率升高，进入燃烧室的氢气减少，导致燃烧后的温度降低，热泵系统中吸收器和冷凝器的放热量减少，减少量大于SOFC增加的发电量，导致系统的总效率降低。
图5分别展示了参比系统不同水碳比、不同SOFC工作温度以及不同燃料转化率对整个系统性能的影响。分析可知，参比系统的SOFC发电效率没有变化，是由于参比系统仅降低了溴化锂热泵的高温热源温度，且相态由水变为了水蒸气；热泵COP有所降低，是由于热泵系统高温热源温度降低，导致其COP降低；整个系统的总效率降低十分明显，主要是由于热泵系统的高温热源由原来的水蒸气变为了水，缺少了相变过程的潜热，进而导致整个系统的能量效率降低。由图5a）可见，随水碳比增加，稀释效应与显热损失导致电效率及参比热效率同步下降。新系统则利用热泵回收随水碳比升高而增加的水蒸气潜热，有效补偿了电效率损失。这种潜热代偿机制显著提升了系统对组分波动的响应弹性。
图5b）揭示了温度对性能的正向驱动作用。高温优化了电解质电导率并提升了余热能级，同步增强了电热产出。为抑制高过热度导致的换热㶲损，新系统需通过精细化热管理消除进入蒸发器前的过热度，从而维持热泵的高COP运行及整体能效增益。图5c）揭示了燃料转化率对电热效率的解耦作用。随着燃料转化率增加，SOFC发电效率升高，但参比系统热效率降低，是由于燃料转化率提升，导致富氧燃烧的废弃燃料减少，热泵可利用的烟气废热减少，导致总的热效率降低。
4.4　经济性分析
系统经济分析数据如图6可见。
从图6可以看出：主系统成本是经济性分析的重中之重，其优化潜力最大；同时，维护成本和辅助系统成本的优化也是提升经济效益的重要方向；通过综合管理和技术改进，可以进一步提升该系统的经济性。
SOFC和空气分离器是成本最高的部件，共占总成本的69.06%。表4给出了系统各部件价格，优化核心设备和辅助设备的性价比是提升经济性的重点。同时，应针对中长期运行成本进行综合评估，确保系统的经济性和高效性。
本文提出了一种基于固体氧化物燃料电池（SOFC）余热驱动的新型多联产系统，通过利用SOFC排放的高温水蒸气潜热替代传统液态水显热作为溴化锂热泵热源，显著提升能源利用效率。不同参考文献系统对比见表5。现有文献系统总效率普遍低于90%，而本文系统总效率达100.54%，㶲效率为56.6%，SOFC电效率为52%。相较于传统显热回收方案（如文献[18]、[21]效率50.0%～78.3%），本设计通过潜热梯级利用与多能协同优化，突破系统能效瓶颈，为分布式能源高效低碳化提供了新路径。
5　结论
收起
本文提出了一种固体氧化物燃料电池耦合吸收式溴化锂热泵热电联产系统，并对设计工况下的系统进行了热力学分析并研究了不同关键参数对系统性能的影响，主要结论如下。
1）通过SOFC烟气富氧燃烧与水蒸气潜热驱动溴化锂热泵的深度耦合，直接利用烟气水蒸气潜热替代传统液态水显热，减少换热温差损失20%~30%，解决了中温余热品位错配导致的㶲损失问题。
2）水碳比、SOFC工作温度与燃料转化率呈显著关联性：水碳比增至2.0时，热泵COP稳定于1.72，但SOFC发电效率由52%降低至48%，系统热效率由100.54%降低至95.3%；SOFC温度升至1 000 ℃，发电效率由48%升高至52%，㶲效率由55.7%升高至56.6%；燃料转化率0.85时，系统热效率达峰值100.54%，但㶲效率因余热回收不足而降低。
3）经模拟计算，水碳比为2，SOFC工作温度为1 000 ℃，燃料转化率为0.85是最优工况，此时发电效率为52%，㶲效率为56.6%，热效率为100.54%。相较于参比系统，热效率提升20%，㶲效率提升2.6%；其中，有效能平准化成本为0.102 6美元/（kW·h），动态投资回收期8年，为分布式能源场景提供商业化路径。
基金
收起
  • 国家自然科学基金项目(52206036; 22278432)
  • 北京市中国石油大学（北京）科研基金项目(2462024YJRC009)
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2026年第55卷第6期
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文章信息
doi: 10.19666/j.rlfd.202508027
  • 接收时间：2025-08-12
  • 首发时间：2026-08-14
  • 出版时间：2026-06-25
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  • 收稿日期：2025-08-12
  • 修回日期：2026-02-14
  • 录用日期：2026-03-04
基金
National Natural Science Foundation of China(52206036; 22278432)
国家自然科学基金项目(52206036; 22278432)
Scientific Research Foundation of China University of Petroleum, Beijing(2462024YJRC009)
北京市中国石油大学（北京）科研基金项目(2462024YJRC009)
作者信息
    中国石油大学（北京）重质油国家重点实验室，北京 102249

通讯作者:

陈哲文（1990），男，博士，副教授，主要研究方向为超临界水煤气化基础理论以及发电系统集成与优化，。
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