CN100363699C - 回收液化天然气冷能的空气分离*** - Google Patents

回收液化天然气冷能的空气分离*** Download PDF

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CN100363699C
CN100363699C CNB2005101241754A CN200510124175A CN100363699C CN 100363699 C CN100363699 C CN 100363699C CN B2005101241754 A CNB2005101241754 A CN B2005101241754A CN 200510124175 A CN200510124175 A CN 200510124175A CN 100363699 C CN100363699 C CN 100363699C
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air
nitrogen
heat exchanger
gas
liquefied natural
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CN1873357A (zh
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林福粦
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Technology Co ltd Fujian Chi Boat
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • 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
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of air
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    • 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
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    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/0406—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of nitrogen
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    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F25J3/04357—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen and comprising a gas work expansion loop
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Abstract

本发明提供了一种回收液化天然气冷能并用于生产液氧、液氮、液氩等液态气体的空气分离***，该***包括氮气制冷循环装置、空气冷却装置和空气分离装置，其中氮气制冷循环装置包括液化天然气换热器和气液分离器，液化天然气换热器用来将液化天然气的冷能隔离交换给氮气制冷循环装置中的氮气，气液分离器用来将经液化天然气换热器换热后的氮气分离为气态氮气和液态氮气，液态氮气在与原料空气交换冷能后汇合气态氮气重新进入液化天然气换热器。该***不仅能够有效回收液化天然气的冷能，减少运行成本和环境污染，而且在生产液态产品时，能够大幅度降低电耗和水耗。

Description

回收液化天然气冷能的空气分离***
技术领域
本发明涉及一种回收液化天然气冷能的空气分离***。
背景技术
液化天然气(LNG)是一种优质能源，具有热值高、洁净、燃烧污染小等特点，且含有大量高品位低温冷量(LNG站高压泵后LNG的温度一般在-150℃～-160℃)。液化天然气汽化时通常是用海水来吸收这部份冷量，再把海水排到海里去，这样不仅浪费了大量冷量，而且造成局部海域低温污染，故如何回收和合理利用这笔可观的冷量就成为人们在使用液化天然气(LNG)时十分关心和为之探索的课题。
空气分离***是以空气为原料，根据氧气、氮气、氩气等气体的不同沸点使之分离，从而生产气态或液态的氧气、氮气、氩气等气体的设备。它们广泛应用于冶金、石化、机械、化肥、玻璃、军工、食品、医疗等领域。但是，普通的空气分离***能耗大，特别是用于生产液态气体时，能耗要成倍地增加。随着国民经济的持续发展，对空气分离***的大型化和空气分离液态产品需求迅速增加。在能源日益趋于短缺的今天，大量能耗的矛盾将更为突出。如何降低其消耗，同样是人们十分关心和为之探索的问题。
发明内容
本发明的目的在于提供一种回收液化天然气冷能并用于生产液氧、液氮、液氩等液态气体的空气分离***，该***不仅能够有效回收液化天然气的冷能，减少运行成本和环境污染，而且在生产液态产品时，能够大幅度降低电耗和水耗。
本发明的空气分离***包括氮气制冷循环装置、空气冷却装置和空气分离装置，所述空气冷却装置用来将所述氮气制冷循环装置中的氮气冷能交换给所述空气分离装置中的原料空气，其中所述氮气制冷循环装置包括液化天然气换热器和气液分离器，所述液化天然气换热器用来将液化天然气的冷能隔离交换给所述氮气制冷循环装置中的氮气，所述气液分离器用来将经所述液化天然气换热器换热后的氮气分离为气态氮气和液态氮气，所述液态氮气在与原料空气交换冷能后汇合所述气态氮气重新进入所述液化天然气换热器。
在本发明的一个优选方案中，所述氮气制冷循环装置还可以包括低温换热器，由所述液化天然气换热器直接换热后的氮气分为两路，一路直接通向所述气液分离器，另一路经由所述低温换热器进入所述气液分离器，所述低温换热器用来将由所述气液分离器所分离出的气态氮气的冷能进一步交换给所述另一路氮气。
在本发明的另一个优选方案中，所述氮气制冷循环装置还可以包括低温氮气循环增压机和/或膨胀增压机和/或增压膨胀机。
在本发明的另一个优选方案中，所述空气冷却装置包括空气冷却器和空气液化器，所述空气冷却器利用所述气态氮气来冷却原料空气，所述空气液化器利用所述液态氮气来进一步冷却由所述空气冷却器冷却后的原料空气并使其液化。
在本发明的另一个优选方案中，所述空气分离装置还包括主换热器，所述空气分离装置中的原料空气分为两路，一路进入所述空气冷却装置或所述空气液化器，另一路进入所述主换热器，所述主换热器用来将由所述空气分离装置所分离出的气体冷能交换给另一路原料空气。
在本发明的另一个优选方案中，由所述空气分离装置所分离出的氮气可以通入所述氮气制冷循环装置。
在本发明的另一个优选方案中，所述空气分离装置还可以包括空气预冷器，所述空气预冷器用来将由所述空气分离装置所分离出的氮气冷能交换给原料空气。
在本发明的另一个优选方案中，所述空气分离装置还可以包括低温空气压缩机和/或净化空气的空气过滤器和/或分子筛纯化器。
本发明的优点在于：1.与传统的生产液态产品的空分装置相比，本发明能节电50％左右甚至能达到60％左右，节水70％以上甚至能达到90％以上；2.可以节省大量用于汽化液化天然气的海水，和减少低温海水注入海里所引起的局部海域的低温污染；3.由于采取了多种防止LNG侵入空分精馏***的措施，空分装置的安全可靠运行，可得到很好的保证；4.结构紧凑，造价低。
附图说明
图1是本发明的一种空气分离***的示意图；
图2是本发明的另一种空气分离***的示意图。
具体实施方式
实施方案一
本发明的第一种空气分离***具体包括用液化天然气冷能作预冷的氮气制冷循环装置、空气液化分离装置、用于连接氮气制冷循环装置和空气液化分离装置的空气冷却器9和空气液化器10、用于启动和正常运行所需的一组阀门及连接管路，其中：
1.1所述空气冷却器9内设有中压循环氮气换热通道S12→S13和原料空气换热通道S14→S15，所述空气液化器10内设有中压液氮换热通道S16→S17和原料空气换热通道S18→S19；
1.2所述的氮气制冷循环装置包括液化天然气贮罐1、液化天然气增压泵2、低温氮气循环增压机3、膨胀-增压机4、液化天然气换热器5、低温换热器6、增压--膨胀机7、节流阀J1、气液分离器8及其连接管路；
1.2.1所述的液化天然气换热器5内设有液化天然气换热通道S1→S2、高压循环氮气换热通道S3→S4和中压循环氮气换热通道S5→S6；
1.2.2所述的低温换热器6内设有高压循环氮气换热通道S4→S7和中压循环氮气换热通道S8→S9；
1.3所述的空气液化分离装置包括空气过滤器11、空气压缩机12、空气预冷器13、分子筛纯化器14、低温空气压缩机15、主换热器16、上塔17、冷凝蒸发器18、下塔19、过冷器20、粗氩塔21-1，粗氩塔21-2、循环液氩泵22、精氩塔23、液氧贮槽24、液氮贮槽25、液氩贮槽26；
1.3.1所述的空气预冷器13设有上进下出的原料空气通道S21→S22、下进上出的污氮通道S23→S24、下进上出的纯氮通道S25→S26；
1.3.2所述的主换热器16内设有上进下出的原料空气换热通道S18→S29、下进上出的污氮通道S30→S23、下进上出的纯氮通道S31→S25及中压氮气通道S32→S17；
1.4所述的氮气制冷循环装置的连接顺序是：自中压氮气入口S11开始，接液化天然气换热器5内的中压循环氮气换热通道S5→S6，接低温氮气循环增压机3，接膨胀-增压机4，接液化天然气换热器5的高压循环氮气换热通道S3→S4，在接口S4之后分成两路；一路接增压--膨胀机7，另一路接低温换热器6内的高压循环氮气换热通道S4→S7，经节流阀J1与第一路交汇于S10后，再接至气液分离器8；所述气液分离器的顶部出口S12接低温换热器6内的中压循环氮气换热通道S8→S9，再接空气冷却器9内的中压循环氮气换热通道S12→S13后交汇于氮气入口S11；所述气液分离器的底部出口S20分两路出去，一路经通气阀T2连接到空分装置的下塔S28，另一路经通气阀T3接至空气液化器10内的中压液氮换热通道S16→S17；所述天然气贮罐1接液化天然气增压泵2后，接液化天然气换热器5内的液化天然气换热通道S1→S2。
1.5所述的空气分离装置的连接顺序是：自空气进口n1开始，接空气过滤器11，接空气压缩机12，接空气预冷器13中上进下出的原料空气通道S21→S22，接分子筛纯化器14，再经空气冷却器9内的原料空气换热通道S14→S15后，接低温空气压缩机15后分两路，一路接空气液化器10内的原料空气换热通道S18→S19，再接下塔S19，另一路接主换热器16内上进下出的原料空气换热通道S18→S29，再连接至下塔S29；经下塔19后连接上塔17、粗氩塔21-1，粗氩塔21-2、精氩塔23，所述粗氩塔21-1和粗氩塔21-2之间连接有循环液氩泵22，最后连接液氧贮槽24、液氮贮槽25、液氩贮槽26。
这种空气分离***的工作原理为：
(1)氮气循环的流程：装置启动时，关闭通气阀T2、T4，打开通气阀T1、T3。600KPa的氮气从空气分离***的下塔19的上部S27处引出，经通气阀T1进入氮气制冷循环***，经过空气液化器10后节点S17，与经空气冷却器9出来的氮气在S11处汇合，进入液化天然气换热器5(S5→S6)与液化天然气换热(S1→S2)，温度降至-110℃～-120℃，进入低温氮气增压机3增压至3000KPa～3500KPa，再在膨胀机的增压机4压缩到3600KPa-4200KPa；进入液化天然气换热器5再与液化天然气换热(S3→S4)，被冷却到-140℃～-142℃；分成两路：一路去膨胀机7膨胀，进一步降温并产生部份液体，进入气液分离器8进行气液分离；另一路在低温换热器6(S4→S7)与分离器8出来的氮气换热(S8→S9)，温度进一步降到-160℃左右后，去节流阀J1节流膨胀(S7→S10)并产生部份液体，也进入气液分离器8进行气液分离。分离出来的液氮(启动阶段液氮经通气阀T2送回下塔上部S28处)经通气阀T3送到空气液化器10(S16→S17)与低温空气压缩机15过来的部份空气进行换热(S18→S19)并使空气在S19处液化。分离器8分离出来的氮气经其顶部出口S12，经低温换热器6(S8→S9)后，进入空气冷却器9(S12→S13)，与由分子筛纯化器14筛来的原料空气换热(S14→S15)，并使空气温度降到-90℃～-100℃。在空气冷却器9换热后的氮气与在空气液化器10换热后的氮气汇合于节点S11后，进入液化天然气换热器5(S5→S6)；又开始重复上述步骤(待氮气纯度合格后，关闭通气阀T1、T2)，并以此不停循环。
当氮气循环***因漏气工作压力小于下塔工作压力时，稳压阀W1自动开启，进行自动补气。
有液氮来源的条件下(如贮存在液氮贮槽的液氮)，可以直接打开通气阀T3、T4引入贮槽中的液氮进行启动，此时通气阀T1、T2、为关闭状态。
上述的通气阀T1、T2、T3的作用是在空分装置起动时(没有液氮来源时)，中压氮气来自下塔19，产生的液氮送回下塔19(用在线分析仪监控LNG踪迹)，当中压氮气的纯度达到要求后，就切断它们的联系；而在装置正常运行时，氮气的循环***因泄漏需要补气时，稳压阀W1开启，补足后关闭，避免空分装置在正常运行时，LNG带入精馏***；通气阀T4是连接液氮贮槽与封闭制冷循环之间的阀门，其作用是用液氮贮槽中的液氮来启动空分装置，防止装置在启动时，把LNG带入精馏***。
(2)空气液化分离的流程：原料空气经空气过滤器11被空气压缩机12吸入，压缩到180KPa～210KPa后，进入空气预冷器13(S21→S22)与返流纯氮(S25→S26)和污氮(S23→S24)换热并降温至15℃～17℃。经过分子筛纯化器14去除CO2和水份后，再进入空气冷却器9(S14→S15)与中压氮气(S12→S13)换热，被冷却到-90℃～-100℃，被低温空气压缩机15吸入，进一步升压到600KPa后，分成两路：一路去空气液化器10(S18→S19)和制冷循环的液氮换热(S16→S17)并全部液化，最后送至空气分离***的下塔19中间S19处，参加下塔19精馏；另一路进入空气分离***的主换热器16(S18→S29)，和返流的污氮(S30→S23)和纯氮(S31→S25)换热至饱和状态，送下塔19底部S29处，参加下塔19精馏；此后，原料空气在下塔19、上塔17、粗氩塔21-1、21-2、精氩塔23内精馏的过程，和传统的液体空分装置相同，最后生产出空分产品——液氧、液氮、液氩，分别放入液氧贮槽24、液氮贮槽25、液氩贮槽26中。
实施方案二
在实施方案一的基础上，其它不变，将空气冷却器9和低温空气压缩机15省略，将节点S6和S9合并为节点S6；将节点S14和S18合并为节点S14。
这种空气分离***的工作原理为：
(1)氮气制冷循环的流程：装置启动时，关闭通气阀T2、T4，打开通气阀T1、T3。600KPa的氮气从空气分离***的下塔19的上部S27处引出，经通气阀T1进入氮气制冷循环***，进入空气液化器10(S16→S17)与来自分子筛4的原料空气换热(S14→S19)后，再进入液化天然气换热器5(S5→S6)，与液化天然气换热(S1→S2)取得冷量，温度降至-120℃～-130℃，进入氮气增压机3增压至3000KPa～3500KPa，再在膨胀机的增压机4压缩到3600KPa～4200KPa，进入液化天然气换热器5(S3→S4)再与液化天然气换热(S1→S2)，被冷却到-140℃～-142℃，分成两路：一路去膨胀机7膨胀，进一步降温并产生部份液体，进入气液分离器8进行气液分离；另一路在低温换热器6(S4→S7)与分离器8出来的氮气换热(S8→S9)，温度进一步降到-160℃左右后，去节流阀J1节流膨胀(S7→S10)并产生部份液体，也进入气液分离器8进行气液分离，分离出来的液氮(启动阶段液氮经通气阀T2送回下塔上部S28处)经通气阀T3送到空气液化器10(S16→S17)与分子筛纯化器14过来的部份空气进行换热(S14→S19)并使空气液化，送入下塔S19处，参加下塔19精馏，分离器8分离出来的氮气经其顶部出口S12，经低温度换热器6(S8→S9)后，与出液化天然气换热器5的中压氮气于节点S6处汇合后，温度变为-120℃～-130℃，进入氮气增压机3增压至3000KPa～3500KPa，又开始重复上述步骤(待氮气纯度合格后，关闭通气阀T1、T2、)，并以此不停循环。
当氮气循环***因漏气工作压力小于下塔工作压力时，稳压阀W1自动开启，进行自动补气。
有液氮来源的条件下(如贮存在液氮贮槽的液氮)，可以直接打开通气阀T3、T4引入贮槽中的液氮进行启动，此时通气阀T1、T2为关闭状态。
(2)空气分离***的实施流程：原料空气经空气过滤器11，被空气压缩机12吸入，压缩到600KPa～620KPa，进入空气预冷器13(S21→S22)与返流纯氮(S25→S26)和污氮(S23→S24)换热并降温至13℃～17℃。经过分子筛纯化器14去除CO2和水份后，分成两路：一路去空气液化器10(S14→S19)和液氮(S16→S17)换热并全部液化，最后送至空分装置的下塔19中间S19处，参加下塔19精馏；另一路进入空分装置的主换热器16(S14→S29)，和返流的污氮(S31→S25)和纯氮(S30→S23)换热至饱和温度，送下塔19底部S29处，去参加下塔19精馏。此后，原料空气在下塔19、上塔17、粗氩塔21-1、21-2、精氩塔23内精馏的过程，和传统的液体空分装置相同，最后生产出空分产品——液氧、液氮、液氩，分别放入液氧贮槽24、液氮贮槽25、液氩贮槽26中。
本发明不仅能够有效回收液化天然气的冷能，减少运行成本和环境污染，而且在生产液态产品时，能够大幅度降低电耗和水耗，具有较大的应用推广价值。

Claims (9)

1.一种空气分离***，包括氮气制冷循环装置、空气冷却装置和空气分离装置，所述空气冷却装置用来将所述氮气制冷循环装置中的氮气冷能交换给所述空气分离装置中的原料空气，其特征在于：
所述氮气制冷循环装置包括液化天然气换热器和气液分离器，所述液化天然气换热器用来将液化天然气的冷能隔离交换给所述氮气制冷循环装置中的氮气，所述气液分离器用来将经所述液化天然气换热器换热后的氮气分离为气态氮气和液态氮气，所述液态氮气在与原料空气交换冷能后汇合所述气态氮气重新进入所述液化天然气换热器。
2.根据权利要求1所述的空气分离***，其特征在于：所述氮气制冷循环装置还包括低温换热器，由所述液化天然气换热器直接换热后的氮气分为两路，一路直接通向所述气液分离器，另一路经由所述低温换热器进入所述气液分离器，所述低温换热器用来将由所述气液分离器所分离出的气态氮气的冷能进一步交换给所述另一路氮气。
3.根据权利要求2所述的空气分离***，其特征在于：所述氮气制冷循环装置还包括低温氮气循环增压机、膨胀增压机和增压膨胀机。
4.根据权利要求1所述的空气分离***，其特征在于：所述空气冷却装置包括空气冷却器和空气液化器，所述空气冷却器利用所述气态氮气来冷却原料空气，所述空气液化器利用所述液态氮气来进一步冷却由所述空气冷却器冷却后的原料空气并使其液化。
5.根据权利要求1所述的空气分离***，其特征在于：所述空气分离装置包括主换热器，所述空气分离装置中的原料空气分为两路，一路进入所述空气冷却装置，另一路进入所述主换热器，所述主换热器用来将由所述空气分离装置所分离出的气体冷能交换给另一路原料空气。
6.根据权利要求4所述的空气分离***，其特征在于：所述空气分离装置包括主换热器，所述空气分离装置中的原料空气分为两路，一路进入所述空气液化器，另一路进入所述主换热器，所述主换热器用来将由所述空气分离装置所分离出的气体冷能交换给另一路原料空气。
7.根据权利要求1-6之任一项所述的空气分离***，其特征在于：由所述空气分离装置所分离出的氮气通入所述氮气制冷循环装置。
8.根据权利要求1-6之任一项所述的空气分离***，其特征在于：所述空气分离装置还包括空气预冷器，所述空气预冷器用来将由所述空气分离装置所分离出的氮气冷能交换给原料空气。
9.根据权利要求1-6之任一项所述的空气分离***，其特征在于：所述空气分离装置还包括低温空气压缩机、净化空气的空气过滤器和分子筛纯化器。
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