CN104019628B - 使空分***在lng冷能供应中断期间连续运行的方法 - Google Patents
使空分***在lng冷能供应中断期间连续运行的方法 Download PDFInfo
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- CN104019628B CN104019628B CN201410203695.3A CN201410203695A CN104019628B CN 104019628 B CN104019628 B CN 104019628B CN 201410203695 A CN201410203695 A CN 201410203695A CN 104019628 B CN104019628 B CN 104019628B
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- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
- F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main feed air
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Abstract
本发明公开了一种使空分***在LNG冷能供应中断期间连续运行的方法,空分***包括如下***:过滤***、压缩***、纯化***、冷却***、精馏***、制冷压缩***以及气液分离***,其中制冷压缩***由LNG提供冷能,并对精馏***生成的氮气进行压缩冷却处理,气液分离***对制冷压缩***生成的液氮进行气液分离处理,生成成品液氮,冷却***包括两套换热器,两套换热器根据LNG冷能供应状态交替投入运行,其中一套为主,其冷却介质包括精馏***生成的氮气,其在LNG冷能供应时开启;另一套为辅助,其冷却介质包括气液分离***生成的成品液氮,其在LNG冷能供应中断时开启。本发明能够在LNG中断时维持空分***的连续平稳运行。
Description
技术领域
本发明涉及利用LNG冷能进行空气分离的方法,特别是一种使空分***在LNG冷能供应中断期间连续运行的方法。
背景技术
常压下LNG是一种-162℃的低温液体,在供应给下游用户之前需将其气化并加热至0℃以上,气化时会放出大量的冷能,1.0吨LNG气化大约可释放出约230kWh的冷能,其经济价值非常高,加以利用可节省大量低温冷能制取时的能耗。同时冷能利用过程中几乎无废弃物排放,环境优势突出。将LNG冷能用于相关的工业领域,可减少巨大的能源消耗及取得良好的经济和社会效益,达到节能、环保的目的,所以各接收站均在进行LNG冷能利用技术的研究和工程化应用,国家能源局也将LNG接收站必须建设配套的冷能利用项目作为核准的条件之一。
LNG冷能利用形式有两类:①直接利用,包括冷能发电、空气分离、冷冻仓库、液化二氧化碳等;②间接利用,包括用空气分离得到的液氮、液氧进行低温粉碎、污水处理等。由于空分装置中所需达到的温度比LNG温度还低,因此LNG的冷量在空分装置中的利用是技术上最合理的最佳方式,所以各大接收站的冷能利用项目均会首先考虑建设空分装置。利用LNG冷量的空气分离工艺流程一般采用循环氮气RecycledNitrogen,简称RN作为冷媒来回收LNG的冷量,并将冷量传递给空分装置用于空气原料的预冷、分离及平衡分馏***的下塔冷凝器和上塔再沸器之间的热负荷,所以利用LNG的冷量可以大幅度降低空分装置的压缩制冷能耗,与传统空分装置相比,冷能空分电力消耗可节省50%以上,冷却水节约70%以上,同时LNG气化的费用也可得到降低。
LNG冷能利用可以替代大量的制冷能源费用。然而,目前LNG冷能利用中存在着LNG气化负荷的变动性与冷能利用项目要求连续、稳定运行的矛盾,这一技术症结已严重阻碍了LNG冷能产业的发展。接收站LNG的气化量在不同时段和不同季节会由于下游用户的用气波动而频繁变化,夜间用气低谷时LNG的气化量很少,甚至停止气化,致使利用LNG冷能的装置中断冷量而不能稳定运行,这是LNG冷能利用面临的重大挑战。随着我国管道天然气的高速发展,天然气管网供需平衡必然会要求LNG承担更多的调峰压力,LNG接收站气化量的昼夜变动将会更大,将来这种矛盾更突出。
中国专利CN101943512B发明了一种利用液化天然气冷能的空分方法,该方法将加压到规定压力的LNG的低温冷能与空气分离单元有机地结合起来,充分地利用了LNG的冷能。即将LNG的低温冷能用来生产液体空分产品,以降低液体空分产品的单位能耗,同时使LNG在空分***中气化升温达到要求的管输温度。但是该专利没有涉及LNG外输负荷波动情况下空分装置的运行情况。
接收站LNG下游用气负荷的60~80%均为燃气电厂,由于燃气电厂具有明显的昼夜峰谷负荷,加之丰水期和枯水期的水电不平衡,使得LNG的气化负荷波动非常大,夜间极少甚至没有气化负荷,导致其LNG冷能空分项目在夜间的用冷需求不能满足。国内某接收站LNG空分装置投产的27个月中因LNG供应连续性中断而停产的次数达到82次。
中国专利CN101839612B发明了一种基于LNG卫星站冷能利用的倒灌式空气分离***及方法。但是LNG卫星站规模较小,与本专利所述的接收站有较大区别,而且该专利并没有涉及当LNG供应完全中断时空分装置的运行情况,没有涉及利用外置换热器来供冷。上述专利均未解决LNG冷能供应中断时空分装置停车的问题。
发明内容
本发明为解决公知技术中存在的技术问题而提供一种使空分***在LNG冷能供应中断期间连续运行的方法。
本发明为解决公知技术中存在的技术问题所采取的技术方案是:一种使空分***在LNG冷能供应中断期间连续运行的方法,空分***包括如下***:过滤***、压缩***、纯化***、冷却***、精馏***、制冷压缩***以及气液分离***,所述过滤***、所述压缩***、所述纯化***和所述冷却***依次对原料空气进行过滤、压缩、净化和冷却处理,所述精馏***对冷却后的空气进行分离处理形成氮气和液氧,所述制冷压缩***由LNG提供冷能,并对所述精馏***形成的氮气进行压缩冷却处理后形成液氮,所述气液分离***对所述制冷压缩***形成的液氮进行气液分离处理,形成成品液氮,所述冷却***包括两套换热器,所述两套换热器根据LNG冷能供应状态交替投入运行,其中一套换热器为主换热器,其冷却介质包括所述精馏***形成的氮气,其在LNG冷能供应时开启;另一套换热器为辅助换热器,其冷却介质包括所述气液分离***形成的成品液氮,其在LNG冷能供应中断时开启;同时根据LNG冷能供应状态,调整所述空分***的设备工艺参数,使所述空分***,在LNG冷能供应充足时增加成品液氮产量,而在LNG冷能供应中断时低负荷运转并停止生产成品液氮;在LNG冷能供应中断时,所述制冷压缩***以及所述气液分离***关闭。
所述过滤***包括空气过滤器a1,所述压缩***包括空压机a3,所述纯化***包括纯化器a20,所述冷却***包括主换热器a12和作为辅助换热器的外置换热器a22;所述精馏***包括精馏塔,所述制冷压缩***包括LNG-氮换热器a6和氮气压缩***,所述气液分离***包括第一气液分离器a10和第二气液分离器a11;所述空气过滤器a1、所述空压机a3以及所述纯化器a20依次连接对原料空气A1进行过滤、压缩及净化处理,处理后的净化压缩空气从所述纯化器a20输出后分为两路,两路在LNG冷能供应及供应中断时不同时导通,一路通过阀门输入所述主换热器a12,另一路通过阀门输入所述外置换热器a22;当LNG冷能供应时,关闭所述外置换热器a22,启动所述主换热器a12和所述LNG-氮换热器a6,所述主换热器a12对来自所述纯化器a20的空气进行冷却,处理后输出冷却的空气至所述精馏塔,所述精馏塔对输入的空气进行分馏,形成液氧和氮气,从所述精馏塔下塔a15顶部抽出的氮气一部分经过所述主换热器a12释放冷能,再经过所述LNG-氮换热器a6冷却后输出,所述LNG-氮换热器a6输出的氮气输入所述氮气压缩***进行压缩,并经进一步冷却后成为液氮,再依次经过所述第一气液分离器a10和所述第二气液分离器a11进行气液分离,形成氮气和成品液氮,其中成品液氮输出至储槽,第二气液分离器a11分离的氮气作为冷却介质输入主换热器a12,LNG经过所述LNG-氮换热器a6释放冷能后,升温至管输温度送入天然气管线;当LNG冷能供应中断时,关闭所述主换热器a12、所述制冷压缩***以及所述气液分离***,启动所述外置换热器a22,所述成品液氮作为冷却介质输入所述外置换热器a22,所述外置换热器a22对来自所述纯化器a20的空气进行冷却,处理后输出冷却的空气至所述精馏塔,所述精馏塔设置为低负荷运转。
所述空分***还包括LNG-乙二醇换热器a5,当LNG冷能供应量充足时,将LNG输入至所述LNG-乙二醇换热器a5,利用乙二醇溶液储冷能,当LNG冷能供应量不足时,储冷能的乙二醇水溶液作为冷却介质向所述空压机内的中间冷却器a2和末级冷却器a4提供冷能,用于冷却原料空气。
从所述精馏塔上塔a13顶部抽出的氮气分两路输出,两路在LNG冷能供应及供应中断时不同时导通,其中一路在当LNG冷能供应时作为冷却介质通过阀门输入所述主换热器a12,而另一路当LNG冷能中断时作为冷却介质通过阀门输入所述外置换热器a22,两路氮气经换热后均直接排空或者作为再生气输入所述纯化器a20;从所述精馏塔下塔a15顶部抽出的氮气分三路输出,第一、二路与第三路在LNG冷能供应及供应中断时不同时导通,当LNG冷能供应时,第一路作为冷却介质通过阀门输入所述主换热器a12进行换热,换热后输入所述LNG-氮换热器a6进行冷却,冷却后再输入所述氮气压缩***,第二路通过阀门输入所述LNG-氮换热器a6进行冷却,冷却后再输入所述氮气压缩***;当LNG冷能中断时,第三路作为冷却介质通过阀门输入所述外置换热器a22,换热后输出至外部设备。
所述制冷压缩***还包括液氮-氮换热器a9,所述氮气压缩***输出的氮气经过所述LNG-氮换热器a6冷却后形成低温高压氮气,经过所述液氮-氮换热器a9进一步冷却后,输出液氮,从所述液氮-氮换热器a9输出的液氮输入所述第一气液分离器a10,所述第一气液分离器a10分离的氮气和从所述液氮-氮换热器a9输出后反流液氮作为冷却介质分别输入所述液氮-氮换热器a9,换热后均作为冷却介质输入至所述LNG-氮换热器a6,换热后输入所述氮气压缩***。
所述氮气压缩***包括低温低压循环氮气压缩机a7和低温高压循环氮气压缩机a8,从所述LNG-氮换热器a6输出的氮气依次经过所述低温低压循环氮气压缩机a7、所述LNG-氮换热器a6、所述低温高压循环氮气压缩机a8和所述LNG-氮换热器a6,经过两次压缩和冷却后输出。
所述空分***还包括过冷器a16,所述精馏塔冷凝蒸发器a14输出的液氮、所述精馏塔下塔a15上部输出的污液氮16、所述精馏塔下塔a15下部输出的贫液空18以及所述精馏塔下塔a15底部输出的富氧液空,分别经所述过冷器a16换热后输入所述上塔a13,所述上塔a13顶部输出的氮气和所述上塔a13顶部输出的污氮55经过所述过冷器a16换热后汇合,再分两路输出,其中一路在当LNG冷能供应时作为冷却介质通过阀门输入所述主换热器a12,而另一路当LNG冷能中断时作为冷却介质通过阀门输入所述外置换热器a22。
所述空分***还包括循环氮-空气换热器a21,当LNG冷能供应时,从所述纯化器a20输出的空气经所述主换热器a12换热后分为两路,其中一路直接输入所述精馏塔,另一路经所述循环氮-空气换热器a21换热后,输入所述精馏塔,从所述第一气液分离器a10分离出的液氮中,分流一部分液氮输入所述循环氮-空气换热器a21与空气换热。
所述空分***还包括粗氩塔a17和精氩塔a18,氩馏分从所述上塔a13中部抽出,输入所述粗氩塔a17除去其中的氧形成工艺氩,所述工艺氩44输入所述精氩塔a18除去其中的氮形成***氩,作为成品送入储槽;所述精馏塔下塔a15底部抽出富氧液空分流为两路,其中一路输入所述上塔a13,另一路节流降压后作为冷却介质输入所述粗氩塔a17的塔顶冷凝器,换热后输入所述上塔a13;另从所述精馏塔下塔a15顶部抽出一路氮气,依次经过所述精氩塔a18的塔底蒸发器和塔顶冷凝器,换热后输入所述上塔a13;所述精馏塔的冷凝蒸发器a14输出的液氮抽出后分流,一部分输入所述上塔a13,另一部分作为冷却介质输入所述精氩塔a18的塔顶冷凝器,换热后输入所述上塔a13。
本发明具有的优点和积极效果是:冷却***设置两套换热器,根据LNG冷能供应状态交替投入运行,其中一套换热器为主换热器,其冷却介质包括所述精馏***生成的氮气,其在LNG冷能供应时开启;另一套换热器为辅助换热器,其冷却介质包括所述气液分离***生成的成品液氮,其在LNG冷能供应中断时开启;同时根据LNG冷能供应状态,终止所述LNG冷能回收***设备运转,并调整精馏***设备工艺参数,使在LNG冷能供应充足时,增加液氮产量;在LNG冷能供应中断时,低负荷运转并停止生产液氮,这样能够维持空分***的连续平稳运行,解决LNG接收站气化外输负荷与冷能项目需求在时间上的不同步的矛盾,避免空分***频繁停车带来的一系列损失;通过设置LNG-乙二醇换热器a5,利用乙二醇溶液储冷能,当LNG冷能供应量不足时,储冷能的乙二醇水溶液提供冷能,用于初步冷却原料空气,降低LNG冷能供应量不足时的冷能消耗;设置过冷器,吸收精馏塔分馏过程中释放的冷能。
附图说明
图1为本发明的工艺流程图。
图中:a1、空气过滤器;a2、空压机中冷器;a3、空压机;a4、空压机末冷器;a5、LNG-乙二醇换热器;a6、LNG-氮换热器;a7、低温低压循环氮气压缩机;a8、低温高压循环氮气压缩机;a9、液氮-氮换热器;a10、第一气液分离器;a11、第二气液分离器;a12、主换热器;a13、上塔;a14、主冷凝蒸发器;a15、下塔;a16、过冷器;a17、粗氩塔;a18、精氩塔;a19、再生用加热器;a20、纯化器;a21、循环氮-空气换热器;a22、外置换热器;1、空气A;3、空气B;4、空气F;11、富氧液空A;13、液氮A;14、液氮B;15、液氮C;16、污液氮;18、贫液空;20、氮气AA;21、液氧;22、氮气BA;23、氮气BB;25、氩馏分;27、氮气AB;28、氮气AC;31、氮气C;33、氮气D;34、液氮D;35液氮DA;37、液氮E;38、液氮F;39、液氮G;40、氮气F;41、液氮H;42、富氧液空B;43、富氧液空C;44、工艺氩;45、氮气AE;48、***氩;49、液氮I;51、空气C;52、空气D;54、空气E;55、污氮;56、氮气BC;58、氮气AD;60、储罐成品液氮。
具体实施方式
为能进一步了解本发明的发明内容、特点及功效,兹例举以下实施例,并配合附图详细说明如下:
请参阅图1,一种使空分***在LNG冷能供应中断期间连续运行的方法,空分***包括如下***:过滤***、压缩***、纯化***、冷却***、精馏***、制冷压缩***以及气液分离***,所述过滤***、所述压缩***、所述纯化***和所述冷却***依次对原料空气进行过滤、压缩、净化和冷却处理,所述精馏***对冷却后的空气进行分离处理形成氮气和液氧,所述制冷压缩***由LNG提供冷能,并对所述精馏***形成的氮气进行压缩冷却处理后形成液氮,所述气液分离***对所述制冷压缩***形成的液氮进行气液分离处理,形成成品液氮,所述冷却***包括两套换热器,所述两套换热器根据LNG冷能供应状态交替投入运行,其中一套换热器为主换热器,其冷却介质包括所述精馏***形成的氮气,其在LNG冷能供应时开启;另一套换热器为辅助换热器,其冷却介质包括所述气液分离***形成的成品液氮,其在LNG冷能供应中断时开启;同时根据LNG冷能供应状态,调整所述空分***的设备工艺参数,使所述空分***,在LNG冷能供应充足时增加成品液氮产量,而在LNG冷能供应中断时低负荷运转并停止生产成品液氮;在LNG冷能供应中断时,所述制冷压缩***以及所述气液分离***关闭。
所述过滤***可包括空气过滤器a1,所述压缩***可包括空压机a3,所述纯化***可包括纯化器a20,所述冷却***可包括主换热器a12和作为辅助换热器的外置换热器a22;所述精馏***可包括精馏塔,所述制冷压缩***可包括LNG-氮换热器a6和氮气压缩***,所述气液分离***可包括第一气液分离器a10和第二气液分离器a11;所述空气过滤器a1、所述空压机a3以及所述纯化器a20可依次连接对原料空气A1进行过滤、压缩及净化处理,处理后的净化压缩空气从所述纯化器a20输出后可分为两路,分别为空气B3和空气E54,两路在LNG冷能供应及供应中断时不同时导通,当LNG冷能供应时,空气B3导通,空气E54截止;当LNG冷能供应中断时,空气B3截止,空气E54导通,一路空气B3通过阀门输入所述主换热器a12,另一路空气E54通过阀门输入所述外置换热器a22;当LNG冷能供应时,关闭所述外置换热器a22,启动所述主换热器a12和所述LNG-氮换热器a6,所述主换热器a12对来自所述纯化器a20的空气进行冷却,处理后输出冷却的空气至所述精馏塔,所述精馏塔对输入的空气进行分馏,形成液氧和氮气,从所述精馏塔下塔a15顶部抽出的氮气一部分经过所述主换热器a12释放冷能,再经过所述LNG-氮换热器a6冷却后输出,所述LNG-氮换热器a6输出的氮气输入所述氮气压缩***进行压缩,并经进一步冷却后成为液氮D34,再依次经过所述第一气液分离器a10和所述第二气液分离器a11进行气液分离,形成氮气和成品液氮H41,其中成品液氮H41输出至储槽,第二气液分离器a11分离的氮气F40作为冷却介质输入主换热器a12,LNG经过所述LNG-氮换热器a6释放冷能后,升温至管输温度送入天然气管线;当LNG冷能供应中断时,关闭所述主换热器a12、所述制冷压缩***以及所述气液分离***,启动所述外置换热器a22,所述成品液氮作为冷却介质输入所述外置换热器a22,所述外置换热器a22对来自所述纯化器a20的空气E54进行冷却,处理后输出冷却的空气至所述精馏塔,所述精馏塔设置为低负荷运转。
所述空分***还可包括LNG-乙二醇换热器a5,当LNG冷能供应量充足时,可将LNG输入至所述LNG-乙二醇换热器a5,利用乙二醇溶液储冷能,当LNG冷能供应量不足时,储冷能的乙二醇水溶液可作为冷却介质向所述空压机内的中间冷却器a2和末级冷却器a4提供冷能,用于冷却原料空气。
从所述精馏塔上塔a13顶部抽出的氮气可分两路输出,两路在LNG冷能供应及供应中断时不同时导通,其中一路在当LNG冷能供应时可作为冷却介质通过阀门导通输入所述主换热器a12,经换热后可直接排空或者作为再生气输入所述纯化器a20,而另一路氮气BC56当LNG冷能中断时可作为冷却介质通过阀门导通输入所述外置换热器a22,经换热后也可直接排空或者作为再生气输入所述纯化器a20;从所述精馏塔下塔a15顶部抽出的氮气AA20可分三路输出,分别为:第一路氮气AB27、第二路氮气AC28和第三路氮气AD58,第一、二路与第三路在LNG冷能供应及供应中断时不同时导通,当LNG冷能供应时,第三路氮气AD58截止,第一路氮气AB27、第二路氮气AC28导通,第一路氮气AB27可作为冷却介质通过阀门导通输入所述主换热器a12进行换热,换热后输入所述LNG-氮换热器a6进行冷却,冷却后再输入所述氮气压缩***,第二路氮气AC28可通过阀门导通输入所述LNG-氮换热器a6进行冷却,冷却后再输入所述氮气压缩***;当LNG冷能中断时,第三路氮气AD58导通,第一路氮气AB27、第二路氮气AC28截止,第三路氮气AD58可作为冷却介质通过阀门导通输入所述外置换热器a22,换热后可输出至外部设备。
所述制冷压缩***还可包括液氮-氮换热器a9,所述氮气压缩***输出的氮气经过所述LNG-氮换热器a6冷却后形成低温高压氮气,可经过所述液氮-氮换热器a9进一步冷却后,输出液氮D34和液氮DA35,从所述液氮-氮换热器a9输出的液氮D34输入所述第一气液分离器a10,所述第一气液分离器a10分离的氮气和从所述液氮-氮换热器a9输出后反流的液氮DA35可作为冷却介质分别输入所述液氮-氮换热器a9,换热后均可作为冷却介质输入至所述LNG-氮换热器a6,换热后输入所述氮气压缩***。
所述氮气压缩***可包括低温低压循环氮气压缩机a7和低温高压循环氮气压缩机a8,从所述LNG-氮换热器a6输出的氮气可依次经过所述低温低压循环氮气压缩机a7、所述LNG-氮换热器a6、所述低温高压循环氮气压缩机a8和所述LNG-氮换热器a6,经过两次压缩和冷却后输出。
所述空分***还可包括过冷器a16,所述精馏塔冷凝蒸发器a14输出的液氮A13、所述精馏塔下塔a15上部输出的污液氮16、所述精馏塔下塔a15下部输出的贫液空18以及所述精馏塔下塔a15底部输出的富氧液空A11,可分别经所述过冷器a16换热后输入所述上塔a13,所述上塔a13顶部输出的氮气BA22和所述上塔a13顶部输出的污氮55可经过所述过冷器a16换热,换热后可汇合为氮气BB23,氮气BB23可再分两路输出,其中一路在当LNG冷能供应时可作为冷却介质通过阀门输入所述主换热器a12,而另一路氮气BC56当LNG冷能中断时可作为冷却介质通过阀门输入所述外置换热器a22。
所述空分***还可包括循环氮-空气换热器a21,当LNG冷能供应时,空气B3导通,从所述纯化器a20输出的空气B3经所述主换热器a12换热后可分为两路,其中一路可直接输入所述精馏塔,另一路可经所述循环氮-空气换热器a21换热后,输入所述精馏塔,从所述第一气液分离器a10分离出的液氮E37中,可分流一部分液氮F38输入所述循环氮-空气换热器a21与空气换热,其余部分液氮G39输入所述第二气液分离器a11。
所述空分***还可包括粗氩塔a17和精氩塔a18,氩馏分25从所述上塔a13中部抽出,输入所述粗氩塔a17除去其中的氧形成工艺氩44,所述工艺氩44输入所述精氩塔a18除去其中的氮形成***氩48,作为成品送入储槽;所述精馏塔下塔a15底部抽出富氧液空A11可分流为两路,分别为富氧液空B42和富氧液空C43,其中一路富氧液空B42输入所述上塔a13,另一路富氧液空C43节流降压后作为冷却介质输入所述粗氩塔a17的塔顶冷凝器,换热后输入所述上塔a13;另从所述精馏塔下塔a15顶部抽出一路氮气AE45,依次经过所述精氩塔a18的塔底蒸发器和塔顶冷凝器,换热后输入所述上塔a13;所述精馏塔的冷凝蒸发器a14输出的液氮抽出后分流,分别为液氮A13和液氮I49,其中液氮I49部分输入所述上塔a13,另外液氮A13部分作为冷却介质输入所述精氩塔a18的塔顶冷凝器,换热后输入所述上塔a13。
本发明的最佳工艺流程如下:
空分装置的规模如下表1所示:
表1正常设计工况下空分装置规模
进料空气A1的初始状态参数为0.1MPa、303K,摩尔组分为:N2:0.781;O2:0.21;Ar:0.009。LNG在送入管网前加压至7.42MPa,其温度为-145℃。LNG摩尔组分为:CH4:91.46%;C2H6:4.74%;C3H8:2.59%;N-C4H10:0.57%;I-C4H10:0.54%;N-C5H12:0.01%;N2:0.09%。
由于LNG的气化负荷波动非常大,白天LNG冷能充足时,冷能空分装置在正常设计工况下运行;夜间极少甚至没有气化负荷时,LNG冷能空分装置的用冷需求不能满足,当LNG冷能供应大于规定值时,作为LNG冷能供应充足工况处理,当LNG冷能供应低于或等于设定的极限值时,作为LNG冷能中断工况处理,当LNG冷能供应大于设定的极限值时,作为LNG冷能供应正常工况;冷能空分装置需在LNG冷能中断工况下运行,即通过外置换热器a22及关闭设备及改变设备参数等方法来维持空分装置连续运行。
一正常设计工况:LNG冷能供应正常
流量为49200Nm3/hr的原料空气A1在过滤器a1中除去灰尘和机械杂质后,进入空压机a3,空压机a3为空气透平压缩机,空压机a3将空气压缩至约0.62MPa,储冷能的乙二醇水溶液作为冷却介质向所述空压机内的中间冷却器a2和末级冷却器a4提供冷能,用于冷却原料空气,将原料空气A1冷却至10℃,进入纯化***的纯化器a20吸附空气中的水分、二氧化碳、乙炔、丙烯、丙烷、重烃、N2O等杂质,进行进一步净化处理。
出纯化器a20的空气B3进入主换热器a12冷却至-171℃,主换热器a12冷源为来自下塔a15顶部的氮气AB27和来自上塔a13塔顶的氮气BB23,空气B3经所述主换热器a12换热后为空气F4,空气F4分为两路,分别为空气C51和空气D52,一路空气C51直接输入所述精馏塔,另一部分空气D52经过循环氮-空气换热器a21换热后,深冷至-176℃后再进入下塔a15。
在下塔a15,其操作压力为0.56MPa,已压缩净化冷却的空气初步分离。利用上升气体和下流液体的浓度差和组分差进行热质交换,低沸点的氮被蒸发,高沸点的氧被冷凝,经过多级塔板的冷凝和蒸发在下塔a15塔釜形成富氧液空。在下塔a15塔顶形成高纯度氮气,大部分氮蒸气经过主冷凝蒸发器a14,与上塔a13底部液氧进行热交换,液氧被蒸发,而氮蒸气被冷凝,部分冷凝的液氮抽出,其中一部分液氮I49抽出后再回到下塔a15作回流液。另外一部分液氮A13,其流量为1000kg/hr,温度及压力分别为-178℃、0.56MPa,在过冷器a16中过冷至-186℃后分为两路,分别为液氮B14和液氮C15,其中一路流量为587kg/hr的液氮B14输入上塔a13作为上塔a13的回流液;另外一路液氮C15先节流降压至0.15MPa,然后去精氩塔a18塔顶冷凝器提供冷量,其出口温度为-192℃,之后输入上塔a13。
从下塔a15底部抽出30337kg/hr的富氧液空A11,其温度为-173℃,在过冷器a16中过冷至-177℃后分流为富氧液空B42和富氧液空C43,其中流量为13100kg/hr的富氧液空B42输入上塔a13作为回流液,另外一部分0.58MPa的富氧液空C43先节流降压至0.15MPa,然后输入粗氩塔a17的塔顶冷凝器提供冷量,其出口温度为-185℃,之后输入上塔a13。下塔a15上部抽出9731kg/hr、-177℃的污液氮16、下塔a15下部抽5435kg/hr、-175℃的贫液空18,分别在过冷器a16中过冷至-190℃、-178℃,之后输入上塔a13,增加上塔a13的回流比,上塔a13的操作压力为0.13MPa。
从下塔a15顶部抽出两路氮气,一路525kg/hr,-177℃的氮气AE45,输入精氩塔a18的塔底蒸发器,另外一路33620kg/hr、-177℃的氮气AA20,分流为三路,分别为氮气AB27、氮气AC28和氮气AD58,其中氮气AB27、氮气AC28在LNG冷能供应导通,氮气AD58在LNG冷能供应时截止,其中流量为24122kg/hr的氮气AB27经主换热器a12升温至14℃后,输入LNG-氮换热器a6,另外氮气AC28经过液氮-氮换热器a9,升温至-144℃后进LNG-氮换热器a6,12860kg/hr、-180℃的液氧21从主冷凝蒸发器a14抽出,作为成品出冷箱送入储槽。
从上塔a13顶部抽出温度为-192℃、压力为0.13MPa、流量为14523kg/hr的氮气BA22,从上塔a13顶部抽出温度为-192℃、压力为0.13MPa、流量为8905kg/hr的污氮55,分别输入过冷器a16,在过冷器a16中与液氮A13、污液氮16、贫液空18和富氧液空A11进行热交换,交换后汇合成为-175℃的氮气BB23,氮气BB23分成两路,其中一路为氮气BC56,在LNG冷能供应时截止,在LNG冷能供应中断时导通并输入外置换热器a22;另外一路在LNG冷能供应中断时截止,在LNG冷能供应时导通并输入主换热器a12升温至14℃输出,输出的氮气一部分去纯化器a20作为再生气,其余部分排空。
14951kg/hr、-180℃及0.14MPa的氩馏分25从上塔a13中部抽出送入粗氩塔a17,粗氩塔a17的操作压力为0.13MPa,在粗氩塔a17中除去其中的氧,得到工艺氩44。410kg/hr、-183℃的工艺氩44送入精氩塔a18,精氩塔a18的操作压力为0.12MPa,在精氩塔中除去其中的氮,在精氩塔a18的底部得到410kg/hr、-183℃的***氩48,作为成品送入储槽。
流量为58197kg/hr的-145℃的LNG在LNG-氮换热器a6中气化、升温,一部分升温至环境温度,另外51002kg/hr、-70℃的LNG从LNG-氮换热器a6的中部抽出,输入冷却LNG-乙二醇换热器a5,之后两部分汇合、送入天然气管线。流量为24122kg/hr的氮气AB27经主换热器a12升温至14℃输入LNG-氮换热器a6,氮气AC28经过液氮-氮换热器a9,升温至-144℃后进LNG-氮换热器a6,这两者均在LNG-氮换热器a6中换热后汇合输出氮气C31,通过低温低压循环氮气压缩机a7压缩至2.3MPa,然后再通过低温高压循环氮气压缩机a8压缩至7MPa成为氮气D33。氮气D33输入液氮-氮换热器a9与节流返流的液氮DA35换热、液化,液氮D34在第一气液分离器a10中节流分离,a10底部的液氮E37分流为两路,分别为液氮F38和液氮G39,其中18372kg/hr、-192℃的液氮F38输入循环氮-空气换热器a21与空气换热,将冷量传递给分馏***;另一液氮G39送入第二气液分离器a11进行气液分离,12677kg/hr、-192℃的液氮H41作为液氮成品送入储槽,第二气液分离器a11分离生成的氮气F40,输入主换热器a12,换热后输入外部设备,第一气液分离器a10和第二气液分离器a11设计压力分别为0.58MPa和0.15MPa。
二LNG冷能供应中断工况
流量为36900Nm3的原料空气A1在过滤器a1中除去灰尘和机械杂质后,进入空压机a3中,将空气压缩至约0.62MPa,储冷能的乙二醇水溶液作为冷却介质向所述空压机内的中间冷却器a2和末级冷却器a4提供冷能,用于冷却原料空气,将原料空气A1冷却至10℃,进入纯化***的纯化器a20吸附空气中的水分、二氧化碳、乙炔、丙烯、丙烷、重烃、N2O等杂质,进行进一步净化处理。
LNG-氮换热器a6停用,终止循环氮气压缩、冷凝过程,停止生产液氮。出纯化器a20的空气E54进入外置换热器a22冷却至-174℃,外置换热器a22的冷源除了上塔a13塔顶氮气BC56和下塔a15顶部氮气AD58外,还需10000kg/hr、-192℃的储罐成品液氮60提供冷能,储罐液氮来自成品液氮H41。
在下塔a15,其操作压力为0.56MPa,已冷却的空气初步分离。利用上升气体和下流液体的浓度差和组分差进行热质交换,低沸点的氮被蒸发,高沸点的氧被冷凝,经过多级塔板的冷凝和蒸发在下塔a15塔釜形成富氧液空。在下塔a15塔顶形成高纯度氮气,大部分氮蒸气经过主冷凝蒸发器a14,与上塔a13底部液氧进行热交换,液氧被蒸发,而氮蒸气被冷凝形成液氮抽出,抽出液氮I49部分再回到下塔a15作回流液。另外一部分液氮A13,其流量为875kg/hr,温度及压力分别为-178℃、0.56MPa,在过冷器a16中过冷至-186℃后分为两路分别为液氮B14和液氮C15,一路流量为462kg/hr的液氮B14送入上塔a13作为上塔a13的回流液;另外一路液氮C15先节流降压至0.15MPa,然后去精氩塔a18的塔顶冷凝器提供冷量,其出口温度为-192℃,之后返回上塔a13。
从下塔a15底部抽出29140kg/hr的富氧液空A11,其温度为-174℃,在过冷器a16中过冷至-179℃,分为两路为富氧液空B42和富氧液空C43,其中流量为12095kg/hr的富氧液空B42输入上塔a13作为回流液,另一路0.58MPa的富氧液空C43先节流降压至0.15MPa,然后输入粗氩塔a17的塔顶冷凝器为其提供冷量,其出口温度为-187℃,之后输入上塔a13。下塔a15上部抽出的10346kg/hr、-177℃的污液氮16、下塔a15下部抽出的5347kg/hr、-175℃的贫液空18,分别经过过冷器a16过冷至-190℃、-178℃,之后输入上塔a13,增加上塔a13的回流比,上塔a13的操作压力为0.13MPa。
从下塔a15顶部抽出两路氮气,分别为氮气AA20和氮气AE45,其中一路375kg/hr、-177℃的氮气AE45,输入精氩塔a18的塔底蒸发器,另外625kg/hr、-177℃的氮气AA20,分流为三路,分别为氮气AB27、氮气AC28和氮气AD58,其中氮气AB27、氮气AC28在LNG冷能供应中断时截止,氮气AD58在LNG冷能供应中断时导通,625kg/hr、-177℃的氮气AD58输入外置换热器a22中冷却空气E54,升温至14℃输出至外部设备。
9856kg/hr、-180℃的液氧21从主冷凝蒸发器a14抽出,作为成品送入储槽。
流量为35780kg/hr、温度为-193℃、压力为0.13MPa的氮气BA22,从上塔a13顶部抽出在过冷器a16中与液氮A13、污液氮16、贫液空18和富氧液空A11进行热交换,升温至-175℃,然后进入外置换热器a22升温至14℃,一部分去纯化器a20作为再生气,其余的放空。
13423kg/hr、-180℃及0.14MPa的氩馏分25从上塔a13中部抽出送入粗氩塔a17,在粗氩塔a17中除去其中的氧,得到工艺氩44。232kg/hr、-183℃的工艺氩44送入精氩塔a18除去其中的氮,在精氩塔a18底部得到226kg/hr、-183℃的***氩48,作为成品送入储槽。
由于LNG冷能中断,将没有LNG冷量冷却乙二醇溶液,所以白天LNG冷能充裕时利用乙二醇溶液储冷,冷能中断时直接用于冷却压缩后的原料空气。
三恢复正常工况:LNG冷能供应恢复正常
在LNG供应恢复初始阶段,其流程与正常设计工况基本相同,区别在于此时增加下塔塔顶氮气AA20的流量,达到38370kg/hr,同时需增加LNG的气化量。流量为60595kg/hr的-145℃的LNG在LNG-氮换热器a6中气化、升温,一部分升温至环境温度,另外51002kg/hr、-70℃的LNG从中部抽出输出至LNG-乙二醇换热器a5,去冷却乙二醇水溶液,之后两部分汇合、送出。通过该操作增加液氮产量,补充夜间冷能中断时所消耗的液氮。当液氮液氧产量达到平衡后,即可将装置恢复到正常设计工况运行。
各工况模拟结果如下表2所示:
表2流程模拟结果
从表中可以看出:
a正常设计工况下,液氧产量为12.86t/h,液氮产量为12.68t/h,液氩产量为0.41t/h。LNG-氮换热器a6需LNG提供5616kW冷量,而乙二醇冷却需5912kW冷量。为了满足这两部分冷量,需58t/h的LNG气化供冷。同时,循环氮气压缩所消耗的功为2610kW。
b在LNG冷能供应中断工况下,利用液氮供冷。将空分装置的负荷降低至正常设计工况的75%,同时通过改变工艺,使不产液氮,从而降低夜间所需的冷量负荷。若夜间LNG冷能供应中断持续时间为6个小时,则根据模拟结果可知:晚间液氧产量为9.86×6=59.16t,液氮产量为0t,液氩产量为0.23×6=1.38t。外置换热器a22需液氮提供1152kW冷量,即需要10t/h液氮。按晚间6小时计算,夜晚LNG冷能供应中断期间需消耗60t液氮。虽然夜间消耗了液氮,但是这样的操作维持了冷能空分装置的连续运行,而且停止生产液氮可节省较大部分的压缩功耗。
乙二醇冷却需4125kW冷量,这部分冷量较大,所以在白天LNG冷能供应充足阶段,用LNG将乙二醇溶液冷却到所需温度,进行储冷。当LNG冷能供应中断时,用低温乙二醇溶液储存的冷能来冷却压缩后的原料空气。
c恢复正常工况下,通过改变工艺改变产品分布状况,增加液氮产量,从而补充夜间LNG冷能中断时消耗的液氮。若LNG冷能供应充足持续时间为18个小时,则根据模拟结果可知:白天液氧产量为9.59×18=172.62t/h,液氮产量为16.60×18=298.80t/h,液氩产量为0.26×18=4.68t/h。LNG-氮换热器a6中需LNG提供6087kW冷量;而乙二醇冷却需5912kW冷量。为了满足这两部分冷量,需61t/h的LNG气化供冷。同时,循环氮气压缩所消耗的功为2954kW。
d当液氮液氧产量达到平衡后,即可将装置恢复到正常设计工况运行,利用LNG气化供冷。
总之,通过外置换热器利用液氮供冷,同时改变负荷以及产品分布状况,可解决LNG接收站气化外输负荷与冷能项目需求在时间上的不同步的矛盾,保障空分项目的连续平稳运行。
尽管上面结合附图对本发明的优选实施例进行了描述,但是本发明并不局限于上述的具体实施方式,上述的具体实施方式仅仅是示意性的,并不是限制性的,本领域的普通技术人员在本发明的启示下,在不脱离本发明宗旨和权利要求所保护的范围情况下,还可以做出很多形式,这些均属于本发明的保护范围之内。
Claims (9)
1.一种使空分***在LNG冷能供应中断期间连续运行的方法,其特征在于,空分***包括如下***:过滤***、压缩***、纯化***、冷却***、精馏***、制冷压缩***以及气液分离***,所述过滤***、所述压缩***、所述纯化***和所述冷却***依次对原料空气进行过滤、压缩、净化和冷却处理,所述精馏***对冷却后的空气进行分离处理形成氮气和液氧,所述制冷压缩***由LNG提供冷能,并对所述精馏***形成的氮气进行压缩冷却处理后形成液氮,所述气液分离***对所述制冷压缩***形成的液氮进行气液分离处理,形成成品液氮,所述冷却***包括两套换热器,所述两套换热器根据LNG冷能供应状态交替投入运行,其中一套换热器为主换热器,其冷却介质包括所述精馏***形成的氮气,其在LNG冷能供应时开启;另一套换热器为辅助换热器,其冷却介质包括所述气液分离***形成的成品液氮,其在LNG冷能供应中断时开启;同时根据LNG冷能供应状态,调整所述空分***的设备工艺参数,使所述空分***,在LNG冷能供应充足时增加成品液氮产量,而在LNG冷能供应中断时低负荷运转并停止生产成品液氮;在LNG冷能供应中断时,所述制冷压缩***以及所述气液分离***关闭。
2.根据权利要求1所述的使空分***在LNG冷能供应中断期间连续运行的方法,其特征在于,所述过滤***包括空气过滤器(a1),所述压缩***包括空压机(a3),所述纯化***包括纯化器(a20),所述冷却***包括主换热器(a12)和作为辅助换热器的外置换热器(a22);所述精馏***包括精馏塔,所述制冷压缩***包括LNG-氮换热器(a6)和氮气压缩***,所述气液分离***包括第一气液分离器(a10)和第二气液分离器(a11);所述空气过滤器(a1)、所述空压机(a3)以及所述纯化器(a20)依次连接对原料空气A(1)进行过滤、压缩及净化处理,处理后的净化压缩空气从所述纯化器(a20)输出后分为两路,两路在LNG冷能供应及供应中断时不同时导通,一路通过阀门输入所述主换热器(a12),另一路通过阀门输入所述外置换热器(a22);当LNG冷能供应时,关闭所述外置换热器(a22),启动所述主换热器(a12)和所述LNG-氮换热器(a6),所述主换热器(a12)对来自所述纯化器(a20)的空气进行冷却,处理后输出冷却的空气至所述精馏塔,所述精馏塔对输入的空气进行分馏,形成液氧和氮气,从所述精馏塔下塔(a15)顶部抽出的氮气一部分经过所述主换热器(a12)释放冷能,再经过所述LNG-氮换热器(a6)冷却后输出,所述LNG-氮换热器(a6)输出的氮气输入所述氮气压缩***进行压缩,并经进一步冷却后成为液氮,再依次经过所述第一气液分离器(a10)和所述第二气液分离器(a11)进行气液分离,形成氮气和成品液氮,其中成品液氮输出至储槽,第二气液分离器(a11)分离的氮气作为冷却介质输入主换热器(a12),LNG经过所述LNG-氮换热器(a6)释放冷能后,升温至管输温度送入天然气管线;当LNG冷能供应中断时,关闭所述主换热器(a12)、所述制冷压缩***以及所述气液分离***,启动所述外置换热器(a22),所述成品液氮作为冷却介质输入所述外置换热器(a22),所述外置换热器(a22)对来自所述纯化器(a20)的空气进行冷却,处理后输出冷却的空气至所述精馏塔,所述精馏塔设置为低负荷运转。
3.根据权利要求2所述的使空分***在LNG冷能供应中断期间连续运行的方法,其特征在于,所述空分***还包括LNG-乙二醇换热器(a5),当LNG冷能供应量充足时,将LNG输入至所述LNG-乙二醇换热器(a5),利用乙二醇溶液储冷能,当LNG冷能供应量不足时,储冷能的乙二醇水溶液作为冷却介质向所述空压机内的中间冷却器(a2)和末级冷却器(a4)提供冷能,用于冷却原料空气。
4.根据权利要求2所述的使空分***在LNG冷能供应中断期间连续运行的方法,其特征在于,从所述精馏塔上塔(a13)顶部抽出的氮气分两路输出,两路在LNG冷能供应及供应中断时不同时导通,其中一路在当LNG冷能供应时作为冷却介质通过阀门输入所述主换热器(a12),而另一路当LNG冷能中断时作为冷却介质通过阀门输入所述外置换热器(a22),两路氮气经换热后均直接排空或者作为再生气输入所述纯化器(a20);从所述精馏塔下塔(a15)顶部抽出的氮气分三路输出,第一、二路与第三路在LNG冷能供应及供应中断时不同时导通,当LNG冷能供应时,第一路作为冷却介质通过阀门输入所述主换热器(a12)进行换热,换热后输入所述LNG-氮换热器(a6)进行冷却,冷却后再输入所述氮气压缩***,第二路通过阀门输入所述LNG-氮换热器(a6)进行冷却,冷却后再输入所述氮气压缩***;当LNG冷能中断时,第三路作为冷却介质通过阀门输入所述外置换热器(a22),换热后输出至外部设备。
5.根据权利要求2所述的使空分***在LNG冷能供应中断期间连续运行的方法,其特征在于,所述制冷压缩***还包括液氮-氮换热器(a9),所述氮气压缩***输出的氮气经过所述LNG-氮换热器(a6)冷却后形成低温高压氮气,经过所述液氮-氮换热器(a9)进一步冷却后,输出液氮,从所述液氮-氮换热器(a9)输出的液氮输入所述第一气液分离器(a10),所述第一气液分离器(a10)分离的氮气和从所述液氮-氮换热器(a9)输出后反流的液氮作为冷却介质分别输入所述液氮-氮换热器(a9),换热后均作为冷却介质输入至所述LNG-氮换热器(a6),换热后输入所述氮气压缩***。
6.根据权利要求2所述的使空分***在LNG冷能供应中断期间连续运行的方法,其特征在于,所述氮气压缩***包括低温低压循环氮气压缩机(a7)和低温高压循环氮气压缩机(a8),从所述LNG-氮换热器(a6)输出的氮气依次经过所述低温低压循环氮气压缩机(a7)、所述LNG-氮换热器(a6)、所述低温高压循环氮气压缩机(a8)和所述LNG-氮换热器(a6),经过两次压缩和冷却后输出。
7.根据权利要求2所述的使空分***在LNG冷能供应中断期间连续运行的方法,其特征在于,所述空分***还包括过冷器(a16),所述精馏塔冷凝蒸发器(a14)输出的液氮、所述精馏塔下塔(a15)上部输出的污液氮、所述精馏塔下塔(a15)下部输出的贫液空以及所述精馏塔下塔(a15)底部输出的富氧液空,分别经所述过冷器(a16)换热后输入所述精馏塔的上塔(a13),所述精馏塔的上塔(a13)顶部输出的氮气和所述精馏塔的上塔(a13)顶部输出的污氮经过所述过冷器(a16)换热后汇合,再分两路输出,其中一路在当LNG冷能供应时作为冷却介质通过阀门输入所述主换热器(a12),而另一路当LNG冷能中断时作为冷却介质通过阀门输入所述外置换热器(a22)。
8.根据权利要求2所述的使空分***在LNG冷能供应中断期间连续运行的方法,其特征在于,所述空分***还包括循环氮-空气换热器(a21),当LNG冷能供应时,从所述纯化器(a20)输出的空气经所述主换热器(a12)换热后分为两路,其中一路直接输入所述精馏塔,另一路经所述循环氮-空气换热器(a21)换热后,输入所述精馏塔,从所述第一气液分离器(a10)分离出的液氮中,分流一部分液氮输入所述循环氮-空气换热器(a21)与空气换热。
9.根据权利要求2所述的使空分***在LNG冷能供应中断期间连续运行的方法,其特征在于,所述空分***还包括粗氩塔(a17)和精氩塔(a18),氩馏分从所述精馏塔的上塔(a13)中部抽出,输入所述粗氩塔(a17)除去其中的氧形成工艺氩,所述工艺氩输入所述精氩塔(a18)除去其中的氮形成***氩,作为成品送入储槽;所述精馏塔下塔(a15)底部抽出富氧液空分流为两路,其中一路输入所述精馏塔的上塔(a13),另一路节流降压后作为冷却介质输入所述粗氩塔(a17)的塔顶冷凝器,换热后输入所述精馏塔的上塔(a13);另从所述精馏塔下塔(a15)顶部抽出一路氮气,依次经过所述精氩塔(a18)的塔底蒸发器和塔顶冷凝器,换热后输入所述精馏塔的上塔(a13);所述精馏塔的冷凝蒸发器(a14)输出的液氮抽出后分流,一部分输入所述精馏塔的上塔(a13),另一部分作为冷却介质输入所述精氩塔(a18)的塔顶冷凝器,换热后输入所述精馏塔的上塔(a13)。
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