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Article(id=1236369225485439503, tenantId=1146029695717560320, journalId=1210938733613449225, issueId=1236369220812984708, articleNumber=null, orderNo=null, doi=10.19666/j.rlfd.202404094, pmid=null, cstr=null, oa=null, hot=null, price=null, onlineType=0, articleFormat=0, articleType=null, articleTypeStr=null, receivedDate=1714233600000, receivedDateStr=2024-04-28, revisedDate=null, revisedDateStr=null, acceptedDate=null, acceptedDateStr=null, onlineDate=1772702993984, onlineDateStr=2026-03-05, pubDate=1732464000000, pubDateStr=2024-11-25, doiRegisterDate=null, doiRegisterDateStr=null, onlineIssueDate=1772702993984, onlineIssueDateStr=2026-03-05, onlineJustAcceptDate=null, onlineJustAcceptDateStr=null, onlineFirstDate=null, onlineFirstDateStr=null, sourceXml=null, magXml=null, createTime=1772702993984, creator=13701087609, updateTime=1772702993984, updator=13701087609, issue=Issue{id=1236369220812984708, tenantId=1146029695717560320, journalId=1210938733613449225, year='2024', volume='53', issue='11', pageStart='1', pageEnd='168', issueExtLink='null', onlineDate='null', pubDate='null', beforeIssueId=null, nextIssueId=null, price=null, status=1, issueComplete=1, articleOrder=1, issueType=-1, specialIssue=null, createTime=1772702992871, creator=13701087609, updateTime=1772703093306, updator=13701087609, preIssue=null, nextIssue=null, ext={EN=IssueExt(id=1236369642126627337, tenantId=1146029695717560320, journalId=1210938733613449225, issueId=1236369220812984708, language=EN, specialIssueTitle=, coverIllustrator=null, specialIssueEditor=, specialIssueAbout=), CN=IssueExt(id=1236369642126627338, tenantId=1146029695717560320, journalId=1210938733613449225, issueId=1236369220812984708, language=CN, specialIssueTitle=, coverIllustrator=null, specialIssueEditor=, specialIssueAbout=)}, issueFiles=null}, startPage=139, endPage=146, ext={EN=ArticleExt(id=1236369225841955368, articleId=1236369225485439503, tenantId=1146029695717560320, journalId=1210938733613449225, language=EN, title=Discussions on high pressure steam supply scheme based on reheater recirculation cooling technology, columnId=1211002409397129992, journalTitle=Thermal Power Generation, columnName=Power generation technology forum, runingTitle=null, highlight=null, articleAbstract=

Under the premise that deep peaking of thermal power units has become normal operation, it poses a higher challenge to transformation of industrial steam supply of thermal power units. Three steam supply schemes using reheater recirculation cooling as the core technology are proposed to meet the requirements of high-pressure steam supply transformation of 660 MW supercritical units. Moreover, the feasibility and economy of these schemes are analyzed by thermodynamic calculation under varying working conditions. The calculation results show that, all the three schemes can ensure the safe operation of the reheater under non-overtemperature conditions, and greatly improve the wide load high pressure steam supply capacity of the unit at 30% rated power load or above and under conditions that meet the demand of single unit with 200 t/h, 6.0 MPa and 480 ℃ steam supply. In order to avoid overspeed of the flow rate at the reheater outlet, it is necessary to coordinate the operation of the immediate pressure (IP) control valve to reduce the flow rate of the reheated steam by increasing the pressure of the reheated steam. With the decrease of the load, the reheater recirculation flow rate under the rated steam supply flow rate will increase. The recirculation flow rate under the whole working conditions of scheme 1 and scheme 3 is not much different, and the ratio of the recirculation flow rate under the high and low load of scheme 2 can reach more than 5 times. Among the three steam supply transformation schemes, scheme 2 is the most energy efficient, scheme 3 is second, and the three schemes can produce economic benefits of 39.51, 44.45 and 41.78 million yuan each year, but in the implementation process, the selection of schemes should consider factors such as investment cost, operation and maintenance amount and energy saving income.

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在火电机组深度调峰成为常态化运行的前提下，对机组工业供汽的改造提出了更高的挑战。针对660 MW超临界机组高压供汽改造需求，提出以再热器再循环冷却技术为核心的3种供汽方案，并通过变工况热力计算分析方案的可行性及经济性。计算结果表明：30%及以上额定发电负荷在满足单机200 t/h、6.0 MPa、480 ℃供汽需求时，3种方案均可保证再热器在不超温的工况下安全运行，大幅提高机组宽负荷高压供汽能力；为了避免再热器出口流速超速，还需中调门配合参调运行，通过提高再热蒸汽压力以降低再热蒸汽流速；随着负荷的降低，满足额定供汽流量下的再热器再循环流量就会增加，方案1和方案3全工况下再循环流量相差不大，而方案2的高低负荷下再循环流量的比值可达5倍以上；3种供汽改造方案，方案2最节能，方案3次之，3种方案每年可分别产生3 951、4 445、4 178万元的经济效益，但在实施过程中，对方案的选取要综合考虑投资成本、运行维护量及节能收益等因素。

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杜旭（1986），男，硕士，高级工程师，主要研究方向为火力发电厂节能降耗，。

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杜旭（1986），男，硕士，高级工程师，主要研究方向为火力发电厂节能降耗，。

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杜旭（1986），男，硕士，高级工程师，主要研究方向为火力发电厂节能降耗，。

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Thermal Power Generation, 2018, 47(10): 103-107., articleTitle=Thermal economy research on back pressure turbine-driven scheme for feed water pumps based on industrial steam supply, refAbstract=null), Reference(id=1236369236201885973, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1236369225485439503, doi=null, pmid=null, pmcid=null, year=2019, volume=null, issue=null, pageStart=1, pageEnd=null, url=null, language=null, rfNumber=［18］, rfOrder=33, authorNames=null, journalName=null, refType=null, unstructuredReference=石油化工蒸汽喷射式抽空器技术规范: SH/T 3118—2018[S]. 北京: 中国石化出版社, 2019: 1., articleTitle=null, refAbstract=null), Reference(id=1236369236298354969, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1236369225485439503, doi=null, pmid=null, pmcid=null, year=2019, volume=null, issue=null, pageStart=1, pageEnd=null, url=null, language=null, rfNumber=［18］, rfOrder=34, authorNames=null, journalName=null, refType=null, unstructuredReference=Technical specification for ejectors in petrochemical engineering: SH/T 3118—2018[S]. Beijing: China Petrochemical Press, 2019: 1., articleTitle=null, refAbstract=null)], funds=null, companyList=[AuthorCompany(id=1236369227859415785, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1236369225485439503, xref=1., ext=[AuthorCompanyExt(id=1236369227863610090, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1236369225485439503, companyId=1236369227859415785, language=EN, country=null, province=null, city=null, postcode=null, companyName=null, departmentName=null, remark=1.Beijing Tianrui Teda Electric Power Engineering Co., Ltd., Beijing 101200, China), AuthorCompanyExt(id=1236369227871998699, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1236369225485439503, companyId=1236369227859415785, language=CN, country=null, province=null, city=null, postcode=null, companyName=null, departmentName=null, remark=1.北京天瑞泰达电力工程有限公司，北京　101200)]), AuthorCompany(id=1236369227943301873, tenantId=1146029695717560320, 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articleId=1236369225485439503, companyId=1236369228060742399, language=EN, country=null, province=null, city=null, postcode=null, companyName=null, departmentName=null, remark=3.Key Laboratory for Thermal Science and Power Engineering of Ministry of Education, Tsinghua University, Beijing 100084, China), AuthorCompanyExt(id=1236369228073325312, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1236369225485439503, companyId=1236369228060742399, language=CN, country=null, province=null, city=null, postcode=null, companyName=null, departmentName=null, remark=3.清华大学热科学与动力工程教育部重点实验室，北京　100084)])], figs=[ArticleFig(id=1236369230250169268, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1236369225485439503, language=EN, label=Fig.1, caption=Flow chart of steam supply system of scheme 1, figureFileSmall=M8vqShFoGKSwdYkceHDvlQ==, figureFileBig=oijA++fWQtG8i4G9t+cEcQ==, tableContent=null), ArticleFig(id=1236369230338249659, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1236369225485439503, language=CN, label=图1, caption=方案1供汽系统流程, figureFileSmall=M8vqShFoGKSwdYkceHDvlQ==, figureFileBig=oijA++fWQtG8i4G9t+cEcQ==, tableContent=null), ArticleFig(id=1236369230543770569, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1236369225485439503, language=EN, label=Fig.2, caption=Flow chart of steam supply system of scheme 2, figureFileSmall=73B2Dw0r/zaddm+k4oixIw==, figureFileBig=xqk1bxkI1nUupTaOSxqTIA==, tableContent=null), ArticleFig(id=1236369230640239569, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1236369225485439503, language=CN, label=图2, caption=方案2供汽系统流程, figureFileSmall=73B2Dw0r/zaddm+k4oixIw==, figureFileBig=xqk1bxkI1nUupTaOSxqTIA==, tableContent=null), ArticleFig(id=1236369230715737049, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1236369225485439503, language=EN, label=Fig.3, caption=Flow chart of steam supply system of scheme 3, figureFileSmall=fP5cb7He8N2TNUuXpwQQ7A==, figureFileBig=yiTOQrF5Xkp8H2msqrofaA==, tableContent=null), ArticleFig(id=1236369230816400350, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1236369225485439503, language=CN, label=图3, caption=方案3供汽系统流程, figureFileSmall=fP5cb7He8N2TNUuXpwQQ7A==, figureFileBig=yiTOQrF5Xkp8H2msqrofaA==, tableContent=null), ArticleFig(id=1236369230908675044, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1236369225485439503, language=EN, label=Fig.4, caption=Change of boiler efficiency with evaporation capacity, figureFileSmall=KIIbhrC8nuIbMoPDfPL4Rw==, figureFileBig=vFFNFZ1x1FFvI7nCB7z1Yw==, tableContent=null), ArticleFig(id=1236369231021921259, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1236369225485439503, language=CN, label=图4, caption=不同蒸发量下锅炉效率, figureFileSmall=KIIbhrC8nuIbMoPDfPL4Rw==, figureFileBig=vFFNFZ1x1FFvI7nCB7z1Yw==, tableContent=null), ArticleFig(id=1236369231202276336, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1236369225485439503, language=EN, label=Fig.5, caption=Comparison of recirculation flow at different loads, figureFileSmall=5lX9JphvMItDkVwgcn17NA==, figureFileBig=WzUZNGGpFM5XfVbsHgyJMQ==, tableContent=null), ArticleFig(id=1236369231323911165, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1236369225485439503, language=CN, label=图5, caption=不同负荷下再循环流量对比, figureFileSmall=5lX9JphvMItDkVwgcn17NA==, figureFileBig=WzUZNGGpFM5XfVbsHgyJMQ==, tableContent=null), ArticleFig(id=1236369231420380162, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1236369225485439503, language=EN, label=Fig.6, caption=Comparison of coal consumption for power generation at different loads, figureFileSmall=x7b3AIl+r9h/ZMc3ZkxS9A==, figureFileBig=z3NDrfhawcrvruQ1K/h5vQ==, tableContent=null), ArticleFig(id=1236369231537819656, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1236369225485439503, language=CN, label=图6, caption=不同负荷下发电煤耗对比, figureFileSmall=x7b3AIl+r9h/ZMc3ZkxS9A==, figureFileBig=z3NDrfhawcrvruQ1K/h5vQ==, tableContent=null), ArticleFig(id=1236369231713980428, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1236369225485439503, language=EN, label=Tab.1, caption=

Calculation of typical working conditions of scheme 1

, figureFileSmall=null, figureFileBig=null, tableContent=
工况VWOTHA75% Pe50% Pe30% Pe
发电负荷/MW659.89581.58495.00330.00198.00
主汽流量/(t·h–1)2 080.001 822.851 554.201 091.30738.80
主汽压力/MPa24.2024.2021.4915.8410.66
主汽温度/℃566566566566566
再热蒸汽流量/(t·h–1)1 607.471 427.371 230.72881.38603.94
再热蒸汽压力/MPa3.933.503.032.421.50
再热蒸汽温度/℃566566566566566
再热器入口蒸汽温度/℃311.87298.08296.86298.48305.82
中调门是否参调是是是是是
中调门前后压差/MPa0.050.110.150.210.25
低压缸排汽量/(t·h–1)1 020.95904.64787.70565.08372.11
机组排汽焓值/(kJ·kg–1)2 309.002 327.782 350.562 437.432 531.59
主汽供汽量/(t·h–1)198.19198.20196.10192.13188.99
供汽减温水量/(t·h–1)1.811.803.907.8711.01
再循环主汽抽汽量/(t·h–1)16.8025.2129.3035.3641.50
再循环再热抽汽量/(t·h–1)36.9555.4667.3888.40103.75
再循环减温水量/(t·h–1)14.2522.3225.8230.2432.75
热耗/(kJ·(kW·h)–1)7 403.207 436.367 487.047 780.418 213.89
锅炉效率/%93.6393.8593.6993.2893.03
发电煤耗/(g·(kW·h)–1)272.52273.10275.42287.48304.32
), ArticleFig(id=1236369231831420949, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1236369225485439503, language=CN, label=表1, caption=

方案1典型工况计算

, figureFileSmall=null, figureFileBig=null, tableContent=
工况VWOTHA75% Pe50% Pe30% Pe
发电负荷/MW659.89581.58495.00330.00198.00
主汽流量/(t·h–1)2 080.001 822.851 554.201 091.30738.80
主汽压力/MPa24.2024.2021.4915.8410.66
主汽温度/℃566566566566566
再热蒸汽流量/(t·h–1)1 607.471 427.371 230.72881.38603.94
再热蒸汽压力/MPa3.933.503.032.421.50
再热蒸汽温度/℃566566566566566
再热器入口蒸汽温度/℃311.87298.08296.86298.48305.82
中调门是否参调是是是是是
中调门前后压差/MPa0.050.110.150.210.25
低压缸排汽量/(t·h–1)1 020.95904.64787.70565.08372.11
机组排汽焓值/(kJ·kg–1)2 309.002 327.782 350.562 437.432 531.59
主汽供汽量/(t·h–1)198.19198.20196.10192.13188.99
供汽减温水量/(t·h–1)1.811.803.907.8711.01
再循环主汽抽汽量/(t·h–1)16.8025.2129.3035.3641.50
再循环再热抽汽量/(t·h–1)36.9555.4667.3888.40103.75
再循环减温水量/(t·h–1)14.2522.3225.8230.2432.75
热耗/(kJ·(kW·h)–1)7 403.207 436.367 487.047 780.418 213.89
锅炉效率/%93.6393.8593.6993.2893.03
发电煤耗/(g·(kW·h)–1)272.52273.10275.42287.48304.32
), ArticleFig(id=1236369231927889949, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1236369225485439503, language=EN, label=Tab.2, caption=

Calculation of typical working conditions of scheme 2

, figureFileSmall=null, figureFileBig=null, tableContent=
工况VWOTHA75% Pe50% Pe30% Pe
发电负荷/MW662.52584.30495.00330.00198.00
主汽流量/(t·h–1)2 080.001 822.851 546.351 084.25738.80
主汽压力/MPa24.2024.2021.4015.7410.66
主汽温度/℃566566566566566
再热蒸汽流量/(t·h–1)1 617.151 427.221 225.30878.47603.94
再热蒸汽压力/MPa3.953.503.012.171.50
再热蒸汽温度/℃566566566566566
再热器入口蒸汽温度/℃312.48298.08296.75299.05305.82
中调门是否参调是是是是是
中调门前后压差/MPa0.120.160.180.240.25
低压缸排汽量/(t·h–1)1 006.08889.21772.62553.71372.11
机组排汽焓值/(kJ·kg–1)2 310.502 329.582 352.872 441.702 531.59
主汽供汽量/(t·h–1)127.07136.47148.53158.86188.99
再热供汽量/(t·h–1)66.0857.3244.5631.77
供汽减温水量/(t·h–1)6.856.226.919.3711.01
再循环主汽抽汽量/(t·h–1)7.9116.4627.3941.50
再循环再热抽汽量/(t·h–1)17.4037.8668.46103.75
再循环减温水量/(t·h–1)6.6914.0723.3932.75
热耗/(kJ·(kW·h)–1)7 354.607 329.507 431.847 709.138 213.89
锅炉效率/%93.6393.8593.6893.2893.03
发电煤耗/(g·(kW·h)–1)270.73271.01273.43284.86304.32
), ArticleFig(id=1236369232036941859, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1236369225485439503, language=CN, label=表2, caption=

方案2典型工况计算

, figureFileSmall=null, figureFileBig=null, tableContent=
工况VWOTHA75% Pe50% Pe30% Pe
发电负荷/MW662.52584.30495.00330.00198.00
主汽流量/(t·h–1)2 080.001 822.851 546.351 084.25738.80
主汽压力/MPa24.2024.2021.4015.7410.66
主汽温度/℃566566566566566
再热蒸汽流量/(t·h–1)1 617.151 427.221 225.30878.47603.94
再热蒸汽压力/MPa3.953.503.012.171.50
再热蒸汽温度/℃566566566566566
再热器入口蒸汽温度/℃312.48298.08296.75299.05305.82
中调门是否参调是是是是是
中调门前后压差/MPa0.120.160.180.240.25
低压缸排汽量/(t·h–1)1 006.08889.21772.62553.71372.11
机组排汽焓值/(kJ·kg–1)2 310.502 329.582 352.872 441.702 531.59
主汽供汽量/(t·h–1)127.07136.47148.53158.86188.99
再热供汽量/(t·h–1)66.0857.3244.5631.77
供汽减温水量/(t·h–1)6.856.226.919.3711.01
再循环主汽抽汽量/(t·h–1)7.9116.4627.3941.50
再循环再热抽汽量/(t·h–1)17.4037.8668.46103.75
再循环减温水量/(t·h–1)6.6914.0723.3932.75
热耗/(kJ·(kW·h)–1)7 354.607 329.507 431.847 709.138 213.89
锅炉效率/%93.6393.8593.6893.2893.03
发电煤耗/(g·(kW·h)–1)270.73271.01273.43284.86304.32
), ArticleFig(id=1236369232162770990, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1236369225485439503, language=EN, label=Tab.3, caption=

Calculation of typical working conditions of scheme 3

, figureFileSmall=null, figureFileBig=null, tableContent=
工况VWOTHA75% Pe50% Pe30% Pe
发电负荷/MW659.86581.70495.00330.00198.00
主机发电负荷/MW658.71580.55492.20323.94193.00
小背压机发电负荷/MW8.968.969.149.355.01
电加热器负荷/MW7.817.816.343.25
主汽流量/(t·h–1)2 080.001 822.851 551.351 084.45726.05
主汽温度/℃566566566566566
主汽压力/MPa24.2024.221.4615.7410.47
再热蒸汽流量/(t·h–1)1 608.041 427.531 231.20878.18597.83
再热蒸汽压力/MPa3.943.503.032.171.49
再热蒸汽温度/℃566566566566566
再热器入口蒸汽温度/℃312.02298.08297.15299.02307.27
中调门是否参调是是是是是
中调门前后压差/MPa0.060.110.160.230.26
低压缸排汽量/(t·h–1)1 019.20902.83784.00556.57365.36
机组排汽焓值/(kJ·kg–1)2 309.152 327.972 351.092 440.672 535.25
主汽供汽量/(t·h–1)200.00200.00200.00200.00188.88
供汽减温水量/(t·h–1)11.12
再循环主汽抽汽量/(t·h–1)17.9626.1931.6538.5343.08
再循环再热抽汽量/(t·h–1)39.5057.6372.8096.34107.69
再循环减温水量/(t·h–1)14.5422.1827.0432.9333.83
热耗/(kJ·(kW·h)–1)7 403.567 435.777 475.767 730.888 036.40
锅炉效率/%93.6393.8593.6893.2893.01
发电煤耗/(g·(kW·h)–1)272.53273.07275.03285.66297.79
), ArticleFig(id=1236369232280211507, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1236369225485439503, language=CN, label=表3, caption=

方案3典型工况计算

, figureFileSmall=null, figureFileBig=null, tableContent=
工况VWOTHA75% Pe50% Pe30% Pe
发电负荷/MW659.86581.70495.00330.00198.00
主机发电负荷/MW658.71580.55492.20323.94193.00
小背压机发电负荷/MW8.968.969.149.355.01
电加热器负荷/MW7.817.816.343.25
主汽流量/(t·h–1)2 080.001 822.851 551.351 084.45726.05
主汽温度/℃566566566566566
主汽压力/MPa24.2024.221.4615.7410.47
再热蒸汽流量/(t·h–1)1 608.041 427.531 231.20878.18597.83
再热蒸汽压力/MPa3.943.503.032.171.49
再热蒸汽温度/℃566566566566566
再热器入口蒸汽温度/℃312.02298.08297.15299.02307.27
中调门是否参调是是是是是
中调门前后压差/MPa0.060.110.160.230.26
低压缸排汽量/(t·h–1)1 019.20902.83784.00556.57365.36
机组排汽焓值/(kJ·kg–1)2 309.152 327.972 351.092 440.672 535.25
主汽供汽量/(t·h–1)200.00200.00200.00200.00188.88
供汽减温水量/(t·h–1)11.12
再循环主汽抽汽量/(t·h–1)17.9626.1931.6538.5343.08
再循环再热抽汽量/(t·h–1)39.5057.6372.8096.34107.69
再循环减温水量/(t·h–1)14.5422.1827.0432.9333.83
热耗/(kJ·(kW·h)–1)7 403.567 435.777 475.767 730.888 036.40
锅炉效率/%93.6393.8593.6893.2893.01
发电煤耗/(g·(kW·h)–1)272.53273.07275.03285.66297.79
), ArticleFig(id=1236369232385069112, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1236369225485439503, language=EN, label=Tab.4, caption=

Coal saving calculation

, figureFileSmall=null, figureFileBig=null, tableContent=
工况VWO75%Pe50%Pe30%Pe
小时数/h1 0002 6002 800500
方案2节煤量/t1 181.42 574.02 420.90
方案3节煤量/t–6.6514.81 681.7644.5
), ArticleFig(id=1236369232527675459, tenantId=1146029695717560320, journalId=1210938733613449225, articleId=1236369225485439503, language=CN, label=表4, caption=

节煤量计算

, figureFileSmall=null, figureFileBig=null, tableContent=
工况VWO75%Pe50%Pe30%Pe
小时数/h1 0002 6002 800500
方案2节煤量/t1 181.42 574.02 420.90
方案3节煤量/t–6.6514.81 681.7644.5
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基于再热器再循环冷却技术的高压供汽方案探讨
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杜旭 1 , 叶明星 2 , 王晨 2 , 张攀 3
热力发电 | 发电技术论坛 2024,53(11): 139-146
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热力发电 | 发电技术论坛 2024, 53(11): 139-146
基于再热器再循环冷却技术的高压供汽方案探讨
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杜旭1 , 叶明星2, 王晨2, 张攀3
作者信息
  • 1.北京天瑞泰达电力工程有限公司，北京　101200
  • 2.国能河北沧东发电有限责任公司，河北　沧州　061113
  • 3.清华大学热科学与动力工程教育部重点实验室，北京　100084

    • 杜旭（1986），男，硕士，高级工程师，主要研究方向为火力发电厂节能降耗，。

Discussions on high pressure steam supply scheme based on reheater recirculation cooling technology
Xu DU1 , Mingxing YE2, Chen WANG2, Pan ZHANG3
Affiliations
  • 1.Beijing Tianrui Teda Electric Power Engineering Co., Ltd., Beijing 101200, China
  • 2.Guoneng Hebei Cangdong Power Generation Co., Ltd., Cangzhou 061113, China
  • 3.Key Laboratory for Thermal Science and Power Engineering of Ministry of Education, Tsinghua University, Beijing 100084, China
出版时间: 2024-11-25 doi: 10.19666/j.rlfd.202404094
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在火电机组深度调峰成为常态化运行的前提下，对机组工业供汽的改造提出了更高的挑战。针对660 MW超临界机组高压供汽改造需求，提出以再热器再循环冷却技术为核心的3种供汽方案，并通过变工况热力计算分析方案的可行性及经济性。计算结果表明：30%及以上额定发电负荷在满足单机200 t/h、6.0 MPa、480 ℃供汽需求时，3种方案均可保证再热器在不超温的工况下安全运行，大幅提高机组宽负荷高压供汽能力；为了避免再热器出口流速超速，还需中调门配合参调运行，通过提高再热蒸汽压力以降低再热蒸汽流速；随着负荷的降低，满足额定供汽流量下的再热器再循环流量就会增加，方案1和方案3全工况下再循环流量相差不大，而方案2的高低负荷下再循环流量的比值可达5倍以上；3种供汽改造方案，方案2最节能，方案3次之，3种方案每年可分别产生3 951、4 445、4 178万元的经济效益，但在实施过程中，对方案的选取要综合考虑投资成本、运行维护量及节能收益等因素。

高压供汽  /  再热器再循环  /  减温减压  /  蒸汽喷射器  /  背压机

Under the premise that deep peaking of thermal power units has become normal operation, it poses a higher challenge to transformation of industrial steam supply of thermal power units. Three steam supply schemes using reheater recirculation cooling as the core technology are proposed to meet the requirements of high-pressure steam supply transformation of 660 MW supercritical units. Moreover, the feasibility and economy of these schemes are analyzed by thermodynamic calculation under varying working conditions. The calculation results show that, all the three schemes can ensure the safe operation of the reheater under non-overtemperature conditions, and greatly improve the wide load high pressure steam supply capacity of the unit at 30% rated power load or above and under conditions that meet the demand of single unit with 200 t/h, 6.0 MPa and 480 ℃ steam supply. In order to avoid overspeed of the flow rate at the reheater outlet, it is necessary to coordinate the operation of the immediate pressure (IP) control valve to reduce the flow rate of the reheated steam by increasing the pressure of the reheated steam. With the decrease of the load, the reheater recirculation flow rate under the rated steam supply flow rate will increase. The recirculation flow rate under the whole working conditions of scheme 1 and scheme 3 is not much different, and the ratio of the recirculation flow rate under the high and low load of scheme 2 can reach more than 5 times. Among the three steam supply transformation schemes, scheme 2 is the most energy efficient, scheme 3 is second, and the three schemes can produce economic benefits of 39.51, 44.45 and 41.78 million yuan each year, but in the implementation process, the selection of schemes should consider factors such as investment cost, operation and maintenance amount and energy saving income.

high pressure steam supply  /  reheater recirculation  /  temperature and pressure reduction  /  steam ejector  /  back pressure-type turbine
杜旭, 叶明星, 王晨, 张攀. 基于再热器再循环冷却技术的高压供汽方案探讨. 热力发电, 2024 , 53 (11) : 139 -146 . DOI: 10.19666/j.rlfd.202404094
Xu DU, Mingxing YE, Chen WANG, Pan ZHANG. Discussions on high pressure steam supply scheme based on reheater recirculation cooling technology[J]. Thermal Power Generation, 2024 , 53 (11) : 139 -146 . DOI: 10.19666/j.rlfd.202404094
正文
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近年来随着人们环保意识的增强以及国家相关政策的提出，高污染、高能耗的小型燃煤锅炉逐步被取缔关停，将大型火力发电机组进行供热改造，实现热电联产承接此部分的热力市场，符合国家的环保要求以及相关的节能政策，具有显著的经济效益、环保效益和社会效益[1-3]。
鉴于目前清洁能源的迅猛发展，清洁能源具有随机性和间歇性发电的特点，大规模的新能源并网在一定程度上会给电网的稳定运行带来负面影响[4-6]，电力系统可调节能力需求猛增，因此在电网负荷中占据主体地位的火电机组除了需要保证稳定的电力供应外，还应承担电力系统调峰的义务[7-10]。从2016年开始，国家能源局就开始实施分批火电灵活性改造试点，在考虑机组对外供热改造时，尤其要重点考虑热电解耦，满足供热需求的同时还要保证机组具备深调能力[11-12]。
为了研究机组宽负荷工况条件下满足大流量高压工业供汽的可能，本文以某超临界660 MW机型作为研究对象，针对外部供热需求参数为6.0 MPa、480 ℃、200 t/h的高压供汽提出3种技术方案，并结合变工况热力计算论证宽负荷范围内供汽的可靠性及经济性。
1　常规供汽方案探讨
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以某超临界660 MW燃煤发电机组为例，该机组汽轮机为超临界参数、一次中间再热、单轴、三缸四排汽、双背压抽汽凝汽式汽轮机；锅炉为超临界参数变压运行、四角切向燃烧方式、一次中间再热、单炉膛平衡通风、固态排渣、半露天布置、全钢构架的∏型直流炉。拟通过对机组进行供热改造，对外实施供给高压过热蒸汽，结合生产企业用热需求，综合考虑供汽管线沿途压降及温降，初步拟定电厂侧出口蒸汽参数为6.0 MPa，蒸汽温度不低于480 ℃，单机宽负荷工况条件下需满足200 t/h的供汽能力。
在中高压工业供汽领域，不考虑进行汽轮机本体改造的前提下，目前较为常见的供汽方案有中调门参调、供热用小背压机、蒸汽喷射器以及高压蒸汽直接减温减压等[13-17]。结合目前高压供汽参数情况，中调门参调的方式无法满足宽负荷提供6.0 MPa的高压供汽要求，因此考虑可行的方案有：1）主蒸汽（主汽）减温减压后供给到热用户；2）采用蒸汽喷射器，用主汽匹配热再蒸汽供给到热用户；3）供热小背压机组，主汽经小背压机组做功后排汽供给到热用户。
1.1　减温减压方案
由于热用户需求蒸汽参数较高，结合深度调峰的大背景下，要求单机在30%额定发电负荷及以上工况满足供汽需求，考虑采用主蒸汽抽汽减温减压的方式直接供给热用户，参照主机厂提供的滑压运行曲线，在满足热用户需求的同时，采用该供汽方式各工况条件下主汽抽汽量均在180 t/h以上，主汽抽汽量过多，易造成锅炉再热器超温，根据主机厂家的抽汽指导意见，在考虑机组现有再热器温度调节手段（包括再热器减温水、尾部烟气挡板）的前提下，额定进汽参数（THA）工况条件下主汽最大抽汽量为120 t/h、50%THA工况条件下仅为60 t/h，超过该最大抽汽量，再热器出口就会出现超温现象，影响机组安全运行。所以单纯主汽减温减压的方式并不能满足单机200 t/h的供汽要求。
1.2　蒸汽喷射器方案
蒸汽喷射器是一种结构简单、易于维护的利用高压流体抽吸低压流体的能混装置，近年来普遍开始推广于供热改造领域，基于6.0 MPa，480 ℃的供汽参数，采用蒸汽喷射器则高压汽源可取主蒸汽，低压汽源可取再热蒸汽，由于供汽参数较高，蒸汽喷射器的引射比（低压汽源流量/高压汽源流量）偏小，机组额定蒸发工况也仅为0.5左右，若满足单机200 t/h的高压供汽量，主汽抽汽量依然超过了主机厂推荐的限制抽汽量；且随着负荷的降低，主汽压力及再热蒸汽压力逐渐下降，在40%以下低负荷工况，蒸汽喷射器的引射比趋于0，因此考虑主机的运行安全，单纯采用蒸汽喷射器的方案仍不可行。
1.3　供热小背压方案
利用高压汽源在小背压机组中做功后，排汽供给到热用户，经济性较好且符合能源梯级利用的用能原则。但是就本项目而言，由于供汽压力和温度均偏高，若采用小背压机组利用主汽做功后排汽对外供给，其存在的问题如下：一是主汽抽汽量较大，依然会超过主机厂允许的抽汽量，再热器仍存在超温风险；二是当背压排汽满足供汽压力时，做完功后的排汽温度会偏低，无法满足用汽的温度需求。所以单纯采用背压机的方案也无法满足宽负荷的供汽需求。
2　再热器再循环技术
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从上面3个常规供汽技术进行分析，主汽抽汽量过大造成再热器运行超温是限制机组供汽能力的主要因素，为解决此问题，特提出再热器再循环冷却技术，该技术核心设备采用蒸汽喷射器，通过少量主蒸汽作为动力蒸汽对部分再热蒸汽进行提压，提压后的混合蒸汽经减温器减温后返回至再热器入口，增加再热器的冷却流量，以解决在主汽抽汽量过多时再热器的超温问题。
针对6.0 MPa、480 ℃、200 t/h供热需求，以再热器再循环技术作为保障点，对比常规供汽方案提出3种优化配置，简要描述如下。
2.1　方案1 主汽减温减压+再热器再循环
主汽减温减压+再热器再循环的技术方案流程图如图1所示。
主汽抽汽分为2部分：一部分主蒸汽通过减温减压后直接供给到热用户，以满足供热需求；另外一部分通过蒸汽喷射器引射再热蒸汽，混合蒸汽经减温器减温后返回至再热器入口。
2.2　方案2 蒸汽匹配+再热器再循环
蒸汽匹配+再热器再循环的技术方案如图2所示。
采用蒸汽喷射器1，利用主蒸汽抽吸再热蒸汽，混合蒸汽经减温器减温后供给热用户；采用蒸汽喷射器2，同样利用主蒸汽抽吸再热蒸汽，混合蒸汽经减温器减温后返回至再热器入口。
2.3　方案3 小背压机+再热器再循环
小背压机+再热器再循环的技术方案流程图如图3所示。
主汽抽汽分为2部分：一部分主汽抽汽经小背压机做功后供给到热用户；另外一部分主汽抽汽通过蒸汽喷射器引射再热蒸汽，混合蒸汽经减温后返回至再热器入口作为再热器再循环冷却蒸汽。由于热用户对供汽温度要求较高，当小背压机排汽温度不能满足需求时，考虑在背压机出口增设电加热器，小背压机组的发电一部分用于电加热背压排汽，剩余部分接入厂用电系统。
3　方案计算
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3.1　计算基础
采用基于再热器再循环系统的3种优化方案对外实施工业供汽，同时考虑目前调峰要求，分别在主汽调阀全开（VWO）工况、THA工况、75% Pe（Pe为机组的额定发电功率）、50% Pe、30% Pe工况下进行变工况核算。为保证比较的基准一致，计算前提要求如下。
1）发电负荷的规定　方案1、方案2的发电负荷即为主机的发电负荷，方案3的发电负荷为主机发电负荷+小背压机发电负荷-电加热器用电负荷。
2）再热器再循环流量的确定　首先确定各纯凝工况下再热器的换热量，以锅炉蒸发的主汽流量作为参考值，计算该工况下再热器的换热量；其次考虑再热器汽温的调节裕量，为简化计算，参考汽轮机厂推荐的典型工况最大抽汽流量，量化该工况下再热器换热量和纯凝工况换热量的关系，从而确定不同主汽流量下再热器的最小换热量；进一步通过再热器的最小换热量反推优化方案中满足供汽要求下再热器的最低冷却流量；最后根据再热器的最低冷却流量，确定再热器需要的再循环流量。
Qrh,min=ηQrh=ηDrh'（hrh''−hrh'）
Drh,x=Qrh,minhrh,g''−hrh,g'−Drh,g'
式中：Drh,x、D＇rh、D＇rh,g分别为再热蒸汽流量再循环流量、纯凝工况下高压缸排汽流量和供热工况下高压缸排汽流量，kg/h；Qrh、Qrh,min分别为纯凝工况下再热器的换热量以及该主汽量下再热器的最小换热量，kJ/h；η为某一主汽流量下再热器允许的最小换热量与该主汽流量纯凝工况下再热器换热量的比值；h＂rh、h＇rh、h＂rh,g、h＇rh,g分别为纯凝工况下热再蒸汽焓值、冷再蒸汽焓值以及供热工况下热再蒸汽焓值、冷再蒸汽焓值，kJ/kg。
3）再热器流速的确定　再热器再循环主要是增加了供热工况条件下再热器的蒸汽流量，从而避免了再热器的超温现象，因此需确定再热器中蒸汽流速是否存在超速的问题。以再热器出口体积流量作为参考值，计算公式如下：
vrh''=DrhVrh3600
式中：v″rh再热器出口体积流量，m3/s；Drh为再热器出口流量，kg/h；Vrh为再热蒸汽比容，m3/kg；为便于分析，考虑采用VWO纯凝工况下再热器出口的体积流量作为参考值，经核算该工况下体积流量为43 m3/s，因此各方案核算时，流速超过43 m3/s时需配合中调门进行适度参调，提高再热器的运行压力以降低再热蒸汽流速。
4）机组热耗率以及发电煤耗的计算
机组热耗率为：
qgr=D0(h0−hfw)+Drh(hrh,g''−hrh,g')−Dgr(hgr−hbs)P
机组发电煤耗为：
bgr=qgrηgdηglQar,net
式中：qgr为机组热耗率，kJ/(kW·h)；bgr为机组发电煤耗，g/(kW·h)；D0、Drh、Dgr分别为主汽流量、再热器出口流量以及供汽流量，kg/h；h0、hfw、hgr、hbs分别为主汽焓值、给水焓值、供汽焓值以及机组补水焓值，kJ/kg；P为机组发电功率，kW；ηg1为锅炉效率，变工况下锅炉效率参照图4选取；ηgd为管道效率，取99%；Qar,net为标煤低位发热量，取29.307 kJ/g。
5）蒸汽喷射器引射系数的核算　蒸汽喷射器的引射系数表示在一定工况下，单位质量的动力蒸汽通过喷射器所抽吸的引射蒸汽的量，计算公式为[18]：
μ=0.834WpkWck[1−(pHpp)kp−1kp]kp+1kp−1[1−(pHpc)kc−1kc]kc+1kc−1−1
式中：pH、pc、pp分别为蒸汽喷射器吸入侧蒸汽压力、出口蒸汽压力及动力蒸汽压力，MPa；kp、kc分别为动力蒸汽和混合蒸汽绝热指数，因均为过热蒸汽，均取1.3；Wpk、Wck分别为动力蒸汽通过喷嘴喉管的临界速度和混合蒸汽通过扩压室喉管的临界速度，m/s。
3.2　计算方法
热力系统的变工况计算是针对机组在非基准工况下运行时的校核计算。在变工况计算前先根据基准工况数据进行设计计算，确定进汽参数、抽汽参数、各级组通流量、级组经济性指标等；然后给定变工况下的电负荷、热负荷，并假定主汽流量进行迭代计算流程，以弗留格尔公式为基础确定变工况下的抽汽参数、各级组通流量，当迭代收敛后进行方案经济性的核算。
本文根据汽轮机厂家提供的热平衡图，基于EXCEL中的VBA功能，参照汽轮机厂提供的热力计算书，搭建机组供汽技术方案的计算模型，THA工况下最大主汽抽汽能力工况下试算，该模型计算结果与汽轮机厂提供的热平衡对比，热耗率最大计算误差为0.13%，满足工程计算的精度需求。
4　计算结果及分析
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4.1　额定供汽量下方案1计算
通过对热力系统的变工况计算，额定供汽流量下方案1相关计算数据见表1。
由表1计算可知：1）在VWO工况条件下，满足供汽需求的同时，机组最高负荷可达659.89 MW，基本上不影响机组满发能力；2）30% Pe供汽工况下，低压缸排汽量约372.11 t/h，低压缸排汽未出现过热情况；3）为保证再热器内蒸汽流速在安全运行范围内，额定供汽流量下全工况均需要中调门参调，随着负荷的降低，中调门参调幅度增大，但最大工况下（30% Pe）中调门前后压差也仅为0.25 MPa。
4.2　额定供汽量下方案2计算
通过对热力系统的变工况计算，额定供汽流量下方案2相关计算数据见表2。
由表2计算可知：1）在VWO工况条件下，满足供汽需求的同时，机组最高负荷可达662.52 MW，完全不影响机组满发能力；2）30% Pe供汽工况下，低压缸排汽量约372.11 t/h，低压缸排汽未出现过热情况；3）额定供汽流量下全工况均需要中调门参调，中调门参调幅度随着负荷的降低而增大，但最大工况下（30% Pe）中调门前后压差也仅为0.25 MPa。
4.3　额定供汽量下方案3计算
通过对热力系统的变工况计算，额定供汽流量下方案3相关计算数据见表3。
由表3计算可知：1）在VWO工况，额定供汽条件下机组最高负荷可达659.86 MW，其中主机发电负荷658.71 MW，小背压机发电负荷8.96 MW，电加热耗电7.81 MW，背压机大多数的发电量用于蒸汽的二次加热，以满足用户温度需求；2）30% Pe供汽工况下，低压缸排汽量约365.36 t/h，低压缸排汽未出现过热情况；3）30% Pe负荷工况下，背压机的排汽温度已高于用户需求，因此电加热器不需投运，但需配置减温器；4）额定供汽流量下全工况均需要中调门参调，最大工况下（30% Pe）中调门前后压差也仅为0.26 MPa，可在工程实践中实现。
4.4　结果分析
4.4.1　不同负荷下再循环流量特性
不同负荷下再循环流量对比如图5所示。由图5可知，随着负荷的降低，主汽抽汽能力减弱，满足额定供汽流量下的再热器再循环流量就会增加。方案1和方案3全工况下再循环流量相差不大，两者均是主汽抽汽做为供汽的唯一汽源；在30%Pe工况下再循环流量是VWO工况的2倍以上，因此考虑蒸汽喷射器的选型时需按最大工况能力设计并兼顾良好的进汽调节特性，建议分2支设计。方案2 50%Pe及以上负荷工况再循环流量均相对较少，得益于再热蒸汽补充了部分供汽，降低了主汽抽汽份额，但高低负荷下再循环流量相差太大，30%Pe工况再热器再循环流量是THA工况的5倍以上，对再循环用蒸汽喷射器的选型配置要求更高，增加了系统配置、运行调整的难度。
4.4.2　不同负荷下发电煤耗特性
不同负荷下发电煤耗对比如图6所示。
由图6可知：额定供汽流量下，50%Pe及以上负荷工况方案2的发电煤耗均为最低，30%Pe工况下，由于主汽压力、再热蒸汽压力的降低，供汽用蒸汽喷射器的引射比已降低为零，因此该工况下方案2实际与方案1相同，为主汽减温减压后直接供给；方案3 30%Pe负荷工况发电煤耗相比另外2个方案最低，中高负荷下较方案2偏高，较方案1优势也并不明显，主要是因为虽然小背压机组利用了主汽的余热余压进行发电，但中高负荷下大部分的电量仍需反补到排汽加热，因此节能量并不理想，而低负荷工况下，由于主汽焓值更高，可利用的焓差更大，因此节能性更具优势。
4.4.3　节能性分析
以方案1作为基准工况，比较3个工况的节能效益。机组年运行小时数按6 900 h核算，简单划分各负荷段的运行小时数及节煤量参照表4。如表4计算可得，方案2较方案1每年可节省标煤6 176.3 t，方案3较方案1每年可节省标煤2 834.4 t。系统配置上，方案2需增加供汽用蒸汽喷射器，而且再循环用蒸汽喷射器也需多支配置，增加了投资成本及后续运行调整的难度；方案3需配套小背压机及附属设施，投资成本更高。
4.4.4　经济性分析
改造后较改造前各负荷段均提高了机组的供汽能力，以方案1为例，按照表4中各负荷段运行小时数进行核算，则全年可增加供热量约250.9万GJ，根据《大中型火力发电厂设计规范》（GB50660—2021）中的方法计算供热煤耗，则全年需增加标煤消耗量9.35万t，高压供汽热价50元/GJ，标煤单价800元/t，除盐水成本15元/t，则每年可增加利润约3 951万元，方案2、方案3较方案1更具节能性，采用这2种改造方式较改造前每年分别可增加利润约4 445、4 178万元，但投资成本、调节方式要求更高，工程实施时对方案的选取需综合考量投资成本、运行维护及节能收益等。
5　结论
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针对外部高压供汽需求，以超临界660 MW机组作为研究对象，在现有的技术路线基础上，提出了3种适应宽负荷运行的高压供汽方案，并建立计算模型对其进行变工况计算，分析方案的可行性及经济性，结论如下。
1）基于再热器再循环冷却技术，可解决大流量高压抽汽供热时锅炉再热器超温的问题，同时为了保证再热器的安全运行，还需辅以中调门参调的形式以避免再热器出口流速超速的现象。
2）随着负荷的降低，主汽抽汽能力减弱，满足额定供汽流量下的再热器再循环流量就会增加；方案1和方案3全工况下再循环流量相差不大，高低负荷下流量偏差也较小，而方案2的高低负荷下再循环流量的比值可达5倍以上。
3）3种供汽改造方案，节能性方面方案1最差、方案2最节能，方案3次之，3种改造方案较改造前每年可分别产生3 951、4 445、4 178万元经济效益，但实施过程中，对方案的选取要综合考虑投资成本、运行维护量及节能收益等因素。
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2024年第53卷第11期
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doi: 10.19666/j.rlfd.202404094
  • 接收时间：2024-04-28
  • 首发时间：2026-03-05
  • 出版时间：2024-11-25
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  • 收稿日期：2024-04-28
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    1.北京天瑞泰达电力工程有限公司，北京　101200
    2.国能河北沧东发电有限责任公司，河北　沧州　061113
    3.清华大学热科学与动力工程教育部重点实验室，北京　100084
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2种不同金属材料的力学参数
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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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