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Article(id=1236699939309408674, tenantId=1146029695717560320, journalId=1210938733613449225, issueId=1236699937195479441, articleNumber=null, orderNo=null, doi=10.19666/j.rlfd.202406125, pmid=null, cstr=null, oa=null, hot=null, price=null, onlineType=0, articleFormat=0, articleType=null, articleTypeStr=null, receivedDate=1718380800000, receivedDateStr=2024-06-15, revisedDate=null, revisedDateStr=null, acceptedDate=null, acceptedDateStr=null, onlineDate=1772781842304, onlineDateStr=2026-03-06, pubDate=1727193600000, pubDateStr=2024-09-25, doiRegisterDate=null, doiRegisterDateStr=null, onlineIssueDate=1772781842304, onlineIssueDateStr=2026-03-06, onlineJustAcceptDate=null, onlineJustAcceptDateStr=null, onlineFirstDate=null, onlineFirstDateStr=null, sourceXml=null, magXml=null, createTime=1772781842304, creator=13701087609, updateTime=1772781842304, updator=13701087609, issue=Issue{id=1236699937195479441, tenantId=1146029695717560320, journalId=1210938733613449225, year='2024', volume='53', issue='9', pageStart='1', pageEnd='154', issueExtLink='null', onlineDate='null', pubDate='null', beforeIssueId=null, nextIssueId=null, price=null, status=1, issueComplete=1, articleOrder=1, issueType=-1, specialIssue=null, createTime=1772781841801, creator=13701087609, updateTime=1772781841801, updator=13701087609, preIssue=null, nextIssue=null, ext=null, issueFiles=null}, startPage=78, endPage=84, ext={EN=ArticleExt(id=1236699939787559339, articleId=1236699939309408674, tenantId=1146029695717560320, journalId=1210938733613449225, language=EN, title=Thermodynamic and economic analysis for a liquid air energy storage system coupling cold energy of liquefied ethylene, columnId=1236699939707867559, journalTitle=Thermal Power Generation, columnName=Liquid air energy storage technology, runingTitle=null, highlight=null, articleAbstract=

Liquid air energy storage (LAES) technology stands out as a large-scale energy storage technology due to its superior energy storage density and adaptability to external energy sources. An LAES system that recovers waste cold of liquid ethylene and introduces an external low-temperature heat source is proposed. Moreover, thermodynamical and economic analysis on key parameters, including isentropic efficiency of the compressor and expander, and temperature of the heat source, are conducted. The results reveal that, when the ethylene flow rate is 34 t/h, the energy storage capacity can reach up to 5 MW/40 (MW·h). At isentropic efficiency of the compressor and expander of 90%, the round-trip efficiency can achieve 77.45% by solely relying on an ambient heat source of 25 ℃ for air heating. When the heat source temperature is increased to 125 °C, the system’s optimal round-trip efficiency, net present value, and dynamic payback period reaches 106.99%, 144.73 million yuan, and 3.56 years, respectively. These findings provide reference for research on the coupling of LAES systems with external cold energy.

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液态空气储能（LAES）技术因其高储能密度和与外部能源的灵活耦合特性，成为了一种重要的大规模储能技术。构建了一种回收液态乙烯再气化废冷、引入外部低温热源的LAES系统。从热力学和经济性两方面对压缩机等熵效率、膨胀机等熵效率以及热源温度等系统关键参数进行分析，结果表明：当乙烯流量为34 t/h，储能容量可达5 MW/40 (MW·h)；在90%的压缩和膨胀等熵效率下，仅依赖25 ℃的环境热源加热空气，往返效率为77.45%；当热源温度提升至125 ℃时，系统的最优往返效率、净现值及动态回收期分别达到了106.99%、14 473万元和3.56年。该研究结果能为LAES系统与外部冷能的耦合研究提供参考。

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王俊杰（1963），男，研究员，主要研究方向为大规模储能技术，。
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李宜洪（2000），男，硕士研究生，主要研究方向为液态空气储能系统固相蓄冷技术，。

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李宜洪（2000），男，硕士研究生，主要研究方向为液态空气储能系统固相蓄冷技术，。

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李宜洪（2000），男，硕士研究生，主要研究方向为液态空气储能系统固相蓄冷技术，。

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Journal of Energy Storage, 2023, 60: 106689., articleTitle=Technoeconomic analysis of a liquid air energy storage system combined with calcium carbide production and waste heat recovery, refAbstract=null), Reference(id=1236699955612667931, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1236699939309408674, doi=null, pmid=null, pmcid=null, year=2023, volume=57, issue=null, pageStart=null, pageEnd=null, url=null, language=null, rfNumber=［23］, rfOrder=25, authorNames=FAN X, JI W, GUO L, journalName=Journal of Energy Storage, refType=null, unstructuredReference=FAN X, JI W, GUO L, et al. Thermo-economic analysis of the integrated system of thermal power plant and liquid air energy storage[J]. Journal of Energy Storage, 2023, 57: 106233., articleTitle=Thermo-economic analysis of the integrated system of thermal power plant and liquid air energy storage, refAbstract=null), Reference(id=1236699955721719839, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1236699939309408674, doi=null, pmid=null, pmcid=null, year=2023, volume=278, issue=null, pageStart=null, pageEnd=null, url=null, language=null, rfNumber=［24］, rfOrder=26, authorNames=LI D, DUAN L, journalName=Energy Conversion and Management, refType=null, unstructuredReference=LI D, DUAN L. Techno-economic analysis of solar aided liquid air energy storage system with a new air compression heat utilization method[J]. Energy Conversion and Management, 2023, 278: 116729., articleTitle=Techno-economic analysis of solar aided liquid air energy storage system with a new air compression heat utilization method, refAbstract=null), Reference(id=1236699955818188836, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1236699939309408674, doi=null, pmid=null, pmcid=null, year=2021, volume=198, issue=null, pageStart=null, pageEnd=null, url=null, language=null, rfNumber=［25］, rfOrder=27, authorNames=CUI S, HE Q, LIU Y, journalName=Applied Thermal Engineering, refType=null, unstructuredReference=CUI S, HE Q, LIU Y, et al. Techno-economic analysis of multi-generation liquid air energy storage system[J]. 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figureFileSmall=jeu3G6FrooNh3Mnz3yxtvQ==, figureFileBig=wGWbH+cubwPuOfbMa+YU6w==, tableContent=null), ArticleFig(id=1236699948809507679, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1236699939309408674, language=EN, label=Tab.1, caption=

Basic design parameters of the system

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参数数值
环境温度/℃25.0
环境压力/MPa0.1
液态乙烯流量/(t·h–1)34
液态乙烯入口压力/MPa3.0
液态乙烯入口温度/℃–104.0[14]
液态乙烯出口温度/℃15.0[15]
液态空气泵的等熵效率/%80[9]
低温透平的等熵效率/%80[16]
液态空气储罐压力/MPa0.1[17]
液态空气储罐温度/℃–194.2
压缩压力/MPa8.0[9]
膨胀压力/MPa6.0[9]
储能时长，释能时长/h8[9]
乙烯换热器、蓄/释冷换热器夹点温差/℃2.0[18]
其他换热器夹点温差/℃10.0[18]
空气液化率/%84.79
年工作日/d330
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系统基本设计参数

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参数数值
环境温度/℃25.0
环境压力/MPa0.1
液态乙烯流量/(t·h–1)34
液态乙烯入口压力/MPa3.0
液态乙烯入口温度/℃–104.0[14]
液态乙烯出口温度/℃15.0[15]
液态空气泵的等熵效率/%80[9]
低温透平的等熵效率/%80[16]
液态空气储罐压力/MPa0.1[17]
液态空气储罐温度/℃–194.2
压缩压力/MPa8.0[9]
膨胀压力/MPa6.0[9]
储能时长，释能时长/h8[9]
乙烯换热器、蓄/释冷换热器夹点温差/℃2.0[18]
其他换热器夹点温差/℃10.0[18]
空气液化率/%84.79
年工作日/d330
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Calculation basis for system components costing

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项目数值
空气压缩机成本/(元·kW–1)1 278.26[23]
空气膨胀机成本/(元·kW–1)749.50[23]
低温透平成本/(元·kW–1)5 151.55[23]
液态空气泵成本/(元·kW–1)11 032.52[23]
2 ℃夹点温差换热器成本/(元·kW–1)396.61[23]
10 ℃夹点温差换热器成本/(元·kW–1)224.24[21]
液态空气储罐成本/(元·m–³)1 902.14[23]
甲醇成本/(元·m–³)2 429[19]
甲醇-水溶液储罐成本/(元·m–³)2 008.90[23]
蓄冷填充床成本/(元·m–³)3 628.45[24]
导热油成本/(元·t–1)19 172.71[19]
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系统各部件成本计算依据

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项目数值
空气压缩机成本/(元·kW–1)1 278.26[23]
空气膨胀机成本/(元·kW–1)749.50[23]
低温透平成本/(元·kW–1)5 151.55[23]
液态空气泵成本/(元·kW–1)11 032.52[23]
2 ℃夹点温差换热器成本/(元·kW–1)396.61[23]
10 ℃夹点温差换热器成本/(元·kW–1)224.24[21]
液态空气储罐成本/(元·m–³)1 902.14[23]
甲醇成本/(元·m–³)2 429[19]
甲醇-水溶液储罐成本/(元·m–³)2 008.90[23]
蓄冷填充床成本/(元·m–³)3 628.45[24]
导热油成本/(元·t–1)19 172.71[19]
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The model validation results

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项目She等人[10]复现系统相对误差/%
空气压缩净功耗/kW1 155.01 143.0–1.04
空气膨胀净功率/kW620.4630.0+1.55
布雷顿循环净功率/kW188.0189.9+1.01
空气液化前压力/MPa11.73811.980+2.06
空气液化前温度/K116.8116.9+0.09
空气液化后压力/MPa0.1030.1030
空气液化后温度/K79.579.50
空气液化率0.7070.714+0.99
往返效率/%70.672.7+2.97
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模型验证结果

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项目She等人[10]复现系统相对误差/%
空气压缩净功耗/kW1 155.01 143.0–1.04
空气膨胀净功率/kW620.4630.0+1.55
布雷顿循环净功率/kW188.0189.9+1.01
空气液化前压力/MPa11.73811.980+2.06
空气液化前温度/K116.8116.9+0.09
空气液化后压力/MPa0.1030.1030
空气液化后温度/K79.579.50
空气液化率0.7070.714+0.99
往返效率/%70.672.7+2.97
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Costs of each component of the system with optimal configuration

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部件成本/元占比/%
空气压缩机5.17×10616.85
空气膨胀机3.22×10610.51
低温透平6.57×1052.14
液态空气泵1.09×1063.54
2 ℃夹点温差换热器6.02×10619.62
10 ℃夹点温差换热器2.32×1067.55
液态空气储罐7.36×1052.40
甲醇8.75×1052.85
甲醇-水溶液储罐4.38×10614.27
蓄冷填充床3.81×10612.43
导热油2.40×1067.83
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最优系统各部件成本明细

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部件成本/元占比/%
空气压缩机5.17×10616.85
空气膨胀机3.22×10610.51
低温透平6.57×1052.14
液态空气泵1.09×1063.54
2 ℃夹点温差换热器6.02×10619.62
10 ℃夹点温差换热器2.32×1067.55
液态空气储罐7.36×1052.40
甲醇8.75×1052.85
甲醇-水溶液储罐4.38×10614.27
蓄冷填充床3.81×10612.43
导热油2.40×1067.83
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耦合液态乙烯冷能的液态空气储能系统热力学及经济性分析
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李宜洪 1, 2 , 刘纪云 3 , 李保坤 3 , 高诏诏 1, 2 , 陈六彪 1, 2 , 王俊杰 1, 2
热力发电 | 液态空气储能技术 2024,53(9): 78-84
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热力发电 | 液态空气储能技术 2024, 53(9): 78-84
耦合液态乙烯冷能的液态空气储能系统热力学及经济性分析
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李宜洪1, 2 , 刘纪云3, 李保坤3, 高诏诏1, 2, 陈六彪1, 2, 王俊杰1, 2
作者信息
  • 1.中国科学院理化技术研究所低温科学与技术重点实验室，北京　100190
  • 2.中国科学院大学，北京　100049
  • 3.中绿中科储能技术有限公司，北京　100020

    • 李宜洪（2000），男，硕士研究生，主要研究方向为液态空气储能系统固相蓄冷技术，。

通讯作者:

王俊杰（1963），男，研究员，主要研究方向为大规模储能技术，。
Thermodynamic and economic analysis for a liquid air energy storage system coupling cold energy of liquefied ethylene
Yihong LI1, 2 , Jiyun LIU3, Baokun LI3, Zhaozhao GAO1, 2, Liubiao CHEN1, 2, Junjie WANG1, 2
Affiliations
  • 1.Key Laboratory of Cryogenic Science and Technology, Technical Institute of Physics and Chemistry, Chinese Academy of Sciences, Beijing 100190, China
  • 2.University of Chinese Academy of Sciences, Beijing 100049, China
  • 3.China Green Development Investment Group Co., Ltd., Beijing 100020, China
出版时间: 2024-09-25 doi: 10.19666/j.rlfd.202406125
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摘要
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液态空气储能（LAES）技术因其高储能密度和与外部能源的灵活耦合特性，成为了一种重要的大规模储能技术。构建了一种回收液态乙烯再气化废冷、引入外部低温热源的LAES系统。从热力学和经济性两方面对压缩机等熵效率、膨胀机等熵效率以及热源温度等系统关键参数进行分析，结果表明：当乙烯流量为34 t/h，储能容量可达5 MW/40 (MW·h)；在90%的压缩和膨胀等熵效率下，仅依赖25 ℃的环境热源加热空气，往返效率为77.45%；当热源温度提升至125 ℃时，系统的最优往返效率、净现值及动态回收期分别达到了106.99%、14 473万元和3.56年。该研究结果能为LAES系统与外部冷能的耦合研究提供参考。

液态空气储能  /  液态乙烯  /  冷能回收

Liquid air energy storage (LAES) technology stands out as a large-scale energy storage technology due to its superior energy storage density and adaptability to external energy sources. An LAES system that recovers waste cold of liquid ethylene and introduces an external low-temperature heat source is proposed. Moreover, thermodynamical and economic analysis on key parameters, including isentropic efficiency of the compressor and expander, and temperature of the heat source, are conducted. The results reveal that, when the ethylene flow rate is 34 t/h, the energy storage capacity can reach up to 5 MW/40 (MW·h). At isentropic efficiency of the compressor and expander of 90%, the round-trip efficiency can achieve 77.45% by solely relying on an ambient heat source of 25 ℃ for air heating. When the heat source temperature is increased to 125 °C, the system’s optimal round-trip efficiency, net present value, and dynamic payback period reaches 106.99%, 144.73 million yuan, and 3.56 years, respectively. These findings provide reference for research on the coupling of LAES systems with external cold energy.

liquid air energy storage  /  liquefied ethylene  /  cold energy recovery
李宜洪, 刘纪云, 李保坤, 高诏诏, 陈六彪, 王俊杰. 耦合液态乙烯冷能的液态空气储能系统热力学及经济性分析. 热力发电, 2024 , 53 (9) : 78 -84 . DOI: 10.19666/j.rlfd.202406125
Yihong LI, Jiyun LIU, Baokun LI, Zhaozhao GAO, Liubiao CHEN, Junjie WANG. Thermodynamic and economic analysis for a liquid air energy storage system coupling cold energy of liquefied ethylene[J]. Thermal Power Generation, 2024 , 53 (9) : 78 -84 . DOI: 10.19666/j.rlfd.202406125
正文
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大规模储能技术能够缓解可再生能源并网冲击，同时平衡电网负荷峰谷差，因此受到广泛关注[1-2]。在众多的大规模储能技术中，液态空气储能（liquid air energy storage，LAES）以其常压贮存、不受地理条件限制、易于扩展的系统以及较高储能密度而被广泛研究[3-4]。独立型LAES系统工作流程为：在电网的谷时电或可再生能源电力驱动下，系统中的压缩机将空气压缩至高压，然后进行冷却、降压液化并储存，从而实现电能的储蓄；当电网负荷过载时，液态空气被加压、气化并升温，然后驱动透平膨胀机做功，以释放电能。
然而，独立型LAES系统往返效率较低，通常低于60%[4]。引入液化天然气（LNG）的再气化废冷是提高LAES系统效率的有效手段，已有相关研究较多。肖力木等[5]通过引入LNG再气化废冷辅助冷却压缩后的空气，并耦合有机朗肯循环发电，实现了系统的冷热电联产。Park等人[6]利用LNG冷能实现空气的低温压缩，并在释能阶段以海水为热源加热空气，达到了187.4%的往返效率。Lu等人[7]提出将LAES系统、LNG再气化废冷、太阳能与海水淡化结合，同时实现了淡水产出和145.57%的往返效率。Cao等人[8]同时耦合LAES、LNG再气化废冷、废热以及两级ORC，实现了能量梯级利用。
实际上，不仅是LNG的再气化废冷可以用于LAES系统，液态乙烯（liquefied ethylene，LE）的再气化过程也存在大量冷能浪费，同样可以回收用于LAES系统中。液态乙烯的温度为–104~–101 ℃，气化压力为0.6~5.0 MPa，通过管路送往下游用户前通常被低温蒸汽或者环境热源直接加热以实现气化[9]，在该过程中存在大量的乙烯气化冷能被浪费。然而，却罕有LAES系统回收液态乙烯再气化冷能的研究。
基于上述现状，本文构建了回收利用液态乙烯再气化废冷，实现空气低温压缩的LAES-LE系统，既能引入液态乙烯再气化冷能提高LAES系统效率，又能避免液态乙烯再气化冷能的浪费。同时，LAES-LE系统还引入了低温热源以提供空气升温的热量。通过构建仿真模型，探究了系统中关键参数对系统热力学性能和经济效益的影响，包括压缩机绝热效率、膨胀机绝热效率以及低温热源温度。
1　系统布置
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LAES-LE系统工作流程如图1所示。鉴于液态空气储能系统的储/释能过程间歇性，为保证液态乙烯的24 h不间断气化，采用甲醇-水溶液（甲醇质量分数80%）作为蓄冷介质，24 h持续储蓄乙烯冷能。甲醇-水溶液蓄冷过程和储能过程在时间上的重叠可通过多个储罐交替运行解决。甲醇-水溶液储蓄液态乙烯的高品位冷能：–104 ℃的液态乙烯与15 ℃的甲醇-水溶液换热，乙烯被加热到大约–13 ℃，而甲醇-水溶液被冷却至–100 ℃。乙烯的低品位冷能直接排放：乙烯被环境加热至15 ℃，并最终送往下游的乙烯用户。甲醇-水溶液所储蓄的冷能用于储能时期内空气的四级低温压缩过程：每级压缩机入口空气温度为–90 ℃，压缩的目标压力为8.0 MPa。被压缩后的高压空气经过两级释冷换热器被冷却至约–175.2 ℃，然后通过低温透平降温降压至–194.2 ℃、0.1 MPa，实现了空气的部分液化。未液化的气态空气反流经过两级释冷换热器，释放冷能以辅助冷却来流空气；而已经液化的空气储蓄于液态空气罐中，标志储能阶段完成。释能阶段：首先液态空气罐中的常压低温液态空气被液态空气泵加压至6.0 MPa，然后在两级蓄冷换热器中换热；低温空气将冷能传递给中间载冷的常压空气完成初步升温，然后中间载冷空气再将冷能传递给固相填充床进行冷能的储蓄；初步升温后的空气接着吸收来自回收的低温热源的热量进一步升温，然后驱动空气膨胀机产生机械功，带动发电机以释放电能。
2　仿真和数学模型
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2.1　仿真及假设
上述LAES-LE系统通过Aspen HYSYS软件建立仿真模型进行分析，进行以下假设：流股物性采用P-R方程计算[7]；空气组成为N2（0.781 2）、O2（0.209 6）以及Ar（0.009 2）[10]；在稳态下分析，忽略系统动态效应[11]；忽略换热器、管道、储罐中的热泄露，忽略流动压降[11]；以导热油传递热源的热量[11]；四级压缩和五级膨胀采用等压比布置[12]；储能时长和释能时长均为8 h[13]。LAES-LE系统的基本设计参数见表1。
2.2　热力学模型
空气压缩机或液态空气泵的功耗为[19]：
W=m×(hout−hin)
空气膨胀机或低温透平的功率为[19]：
W=m×(hin−hout)
式中：m表示工质流量，kg/s；h表示工质的焓值，kJ/kg；下标in和out表示部件的入口和出口。不同的部件以下标进行区分，空气压缩机为AC（air compressor），液空泵为LAP（liquid air pump），空气膨胀机为AE（air expander），低温透平为CT（cryogenic turbine）。
LAES系统最重要的热力学性能指标是往返效率RTE（round-trip efficiency），定义为释能时期的净电量输出和储能时期的净电量输入之比[20]：
RTE=Wout,net×trWin,net×ts=(∑WAE−WLAP)×tr(∑WAC−WCT)×ts
式中：Wout,net和Win,net分别为系统释能时期的净功率输出和储能时期的净功率输入，kW；tr和ts分别为释能时长和储能时长，均为8 h。
2.3　经济性模型
液态空气储能系统的盈利来自电网电价的峰谷差值。液态空气系统在用电低谷期购入低价电产生液态空气从而储电，并在用电高峰期气化空气驱动空气膨胀机释放所储蓄的电能，从而实现盈利。
系统经济性首先需要计算年购电成本（annual electricity cost，AEC），即1年内在储能时期从电网购入低谷电的花费[21]：
AEC=Win,net×cvalley×ts×330
式中：330为系统年工作330天；cvalley为低谷电价，取值0.25元/(kW·h)[19]。
系统的年总成本（annual total cost，ATC）包括年购电成本以及系统运维成本[21]：
ATC=β×∑Ci+AEC
式中：∑Ci为系统各部件成本总和，具体计算参考表2；β为运行维护系数，取值0.05[22]。
系统的年总收入（annual total income，ATI）主要来自负荷高峰期售电，可通过下式计算[21]：
ATI=Wout,net×cpeak×tr×330
式中：cpeak为高峰电价，1.24元/(kW·h)[19]。
系统的年总利润（annual total profit，ATP）为年总收入和年总成本的差值[21]：
ATP=ATI−ATC
系统的投资经济性可以通过净现值（net present value，NPV）表征。NPV为一段时间内的净现金流入量，通过下式计算[21]：
NPV=∑j=1nATPj(1+a)j−∑Ci
式中：n为系统寿命，取值30年[25]；ATPj表示第j年的年总利润；α为折现率，取值0.05[19]。
系统经济性还需要考虑投资回收的速度，可通过动态回收期（dynamic payback period，DPP）进行表征。DPP本质上是NPV恰好为0的时间，通过下式计算[21]：
DPP=t−1+|NPVt−1|ATPt
式中：t表示NPV为正值的第1年。
2.4　模型验证
为验证本文假设和模型的可行性，复现了She等人[10]所提出的液态空气储能系统，所复现的系统和原系统的对比见表3。由表3可知：由于本研究所采用的假设忽略了管路中流动压损，因此空气压缩阶段的净功耗更低，空气膨胀阶段的净功率更高；并且空气液化前的压力更高，使得复现系统的空气液化率比She等人[10]所提出的原系统的高出0.99%，往返效率高出2.97%；相对误差均在3%以内，因此本研究中提出的假设和模型准确、可靠。
3　结果与讨论
收起
考虑到液态空气储能系统的热力学性能和经济性能都与压缩功耗、膨胀功率相关，因此探讨了压缩机、膨胀机的等熵效率对系统热力学性能和经济性表现的影响。此外，还讨论了同样会影响系统性能的热源温度。
3.1　热力学分析
在限定膨胀机等熵效率为90%、25 ℃环境加热的条件下，压缩机等熵效率对往返性能的影响规律如图2所示。由图2可见，压缩机的等熵效率越高，系统的往返效率越高。当压缩机等熵效率从70%升至90%后，系统的往返效率从59.81%升至77.45%。其原因在于：在压缩机入口温度和压缩初终压力固定的条件下，压缩机等熵效率的提高会导致压缩过程的温度升高量减少，压缩后的温度因此降低，温度的降低使得压缩阶段的总功耗减少，从而提高往返效率。在压缩效率从70%提高至90%后，空气压缩机出口的平均温度从7.0 ℃降低至–12.6 ℃，总压缩功耗因此从约6 429 kW减少至5 000 kW，系统的往返效率从59.81%升至77.45%。
在限定压缩机等熵效率为90%、25 ℃环境加热的条件下，膨胀机等熵效率对往返效率的影响规律如图3所示。
由图3可见，与压缩机等熵效率的影响规律类似，系统往返效率随膨胀机等熵效率的提高而提高。其原因在于：在固定热源温度下，膨胀机等熵效率的提高使得膨胀机能够更有效地利用所吸收的热量，膨胀机出口的平均温度更低，从而使膨胀机输出更多的功量。图3中，当膨胀效率从70%提高至90%后，空气膨胀机出口的平均温度从–28.9 ℃降至–40.6 ℃，总膨胀功率因此从约3 012 kW增至3 872 kW，系统往返效率从59.68%升至77.45%。
而对于低温热源温度而言，在固定的换热温差下，热源温度的提高能够使每级膨胀机前的入口空气温度提高，从而显著增加其膨胀机功输出量。热源温度对系统性能的影响如图4所示。由图4可见，低温热源温度从25 ℃升至125 ℃后，膨胀机的总输出功率从3 872 kW显著提升至5 302 kW。因此，系统往返效率从77.45%升至106.99%。
3.2　经济性分析
压缩机等熵效率对系统经济性影响如图5所示。提高压缩机等熵效率会减少压缩阶段的功耗，从而降低年购电成本，提高系统的经济性。然而，由于低谷电价较低，提高压缩机等熵效率带来的经济性收益并不显著。当压缩机等熵效率从70%升至90%后，年购电成本从约414万元降至约320万元，30年净现值从约5 623万元提高至约7 468万元，增加了约33%，而动态回收期从7.75年缩短至5.99年。
膨胀机等熵效率对系统经济性的影响如图6所示。由图6可见，膨胀机等熵效率对系统经济性的影响比压缩机等熵效率的影响更加显著。当膨胀机等熵效率从70%升至90%后，由于膨胀机功率更大，系统的年总收入从约946万元提高到约1 228万元，而30年净现值从约3 286万元提高至约7 468万元，净现值翻了1倍多，而动态回收期从10.42年缩短至5.99年。膨胀机等熵效率和压缩机等熵效率对经济性影响程度不同的原因在于：系统的经济性盈利来自于电网在峰/谷时期的电价差，峰时电价比谷时电价高得多。这说明，膨胀时释放更多的功率比减少更多的压缩功耗带来的收益更大。因此，膨胀机等熵效率的提高允许系统在释能阶段的功率更大，经济性得到显著提高。
对于低温热源温度而言，温度的提高意味着空气吸收的热量更多，从而使膨胀机输出功率更大，因此系统经济性更好。热源温度对系统经济性的影响如图7所示。由图7可见，当热源温度为25 ℃时，系统的年总收入约为1 228万元，30年净现值约为7 468万元，动态回收期约为5.99年。当热源温度提高至125 ℃后，年总收入提高到了1 696万元，而30年净现值增加了近90%，约为14 473万元，而动态回收期从5.99年缩短至3.56年。
经济性效益最优的系统配置为90%压缩等熵效率、90%膨胀等熵效率以及125 ℃热源温度。上述配置系统成本见表4。系统主要成本在于空气压缩机与膨胀机（27.36%）、换热器（27.17%）、蓄冷甲醇-水溶液及其储罐（17.12%），以及蓄冷填充床（12.43%）。
4　结论
收起
本文构建了一种利用低温液态乙烯冷能和回收低温热源的耦合液态空气储能系统。该系统利用液态乙烯的再气化冷能实现空气的多级低温压缩，并利用低温热源加热释能阶段的空气。探讨了系统中压缩机等熵效率、膨胀机等熵效率以及热源温度对系统热力学性能、经济性的影响规律。
1）基于34 t/h流量的液态乙烯，建立了5 MW/ 40 MW·h规模的LAES系统。在由环境热源提供空气膨胀前的吸热量条件下，系统往返效率为77.45%，显著高于独立式LAES系统。
2）由于峰时电价比谷时电价高得多，提高膨胀机等熵效率带来的经济收益比提高压缩机等熵效率大得多。对于膨胀机等熵效率而言，从70%提高到90%后，30年净现值从约3 286万元增长至7 468万元，增长率超过1倍。而对于压缩机等熵效率而言，相同程度的效率提升下，30年净现值从5 623万元增长至7 468万元，增加幅度仅有33%。
3）提高热源温度，既能够有效提高系统效率，又能够显著提高系统的经济性。当低温热源温度从25 ℃升至125 ℃后，系统往返效率可从77.45%增至高达106.99%，而系统的30年净现值从约7 468万元增加至14 473万元，动态回收期从5.99年缩短至约3.56年。
基金
收起
  • 国家资助博士后研究人员计划(GZC20241778)
  • 中国绿发科技创新项目(202309CHDD020)
文献
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2024年第53卷第9期
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doi: 10.19666/j.rlfd.202406125
  • 接收时间：2024-06-15
  • 首发时间：2026-03-06
  • 出版时间：2024-09-25
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  • 收稿日期：2024-06-15
基金
Postdoctoral Fellowship Program of CPSF(GZC20241778)
国家资助博士后研究人员计划(GZC20241778)
Technological Innovation Projects of China Green Development Investment Group Co., Ltd.(202309CHDD020)
中国绿发科技创新项目(202309CHDD020)
作者信息
    1.中国科学院理化技术研究所低温科学与技术重点实验室，北京　100190
    2.中国科学院大学，北京　100049
    3.中绿中科储能技术有限公司，北京　100020

通讯作者:

王俊杰（1963），男，研究员，主要研究方向为大规模储能技术，。
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