CN101048636A - 天然气液化系统 - Google Patents

天然气液化系统 Download PDF

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CN101048636A
CN101048636A CN200580037261.XA CN200580037261A CN101048636A CN 101048636 A CN101048636 A CN 101048636A CN 200580037261 A CN200580037261 A CN 200580037261A CN 101048636 A CN101048636 A CN 101048636A
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H·E·霍沃德
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Praxair Technology Inc
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Abstract

用于产生液化天然气的方法，其中将高压液体天然气过冷且然后闪蒸，以形成闪蒸蒸汽和液化天然气产品，且闪蒸蒸汽在致冷循环中被使用以生成用于将液体天然气过冷的致冷，且已冷却的致冷气也用于将液体天然气过冷。

Description

天然气液化系统
技术领域
本发明一般地涉及液化天然气的生产。
背景技术
天然气传输管道典型地以700至1500psia的范围的压力运行。天然气降压点经常被称为降压站。这样的站使得能实现天然气区域性分配(典型地处于150到500psia的压力)。一般地，降压站不设计为用于压力能的有用回收。用于降压天然气而同时产生为液化天然气的入口气的部分的过程经常被称为膨胀机循环或膨胀机车间。
本发明的目的是提供用于利用压力能来产生液化天然气的改进的方法。
发明内容
在阅读此披露时将对于本领域技术人员变得显见的以上的和其他的目的通过本发明获得，本发明是：
用于产生液化天然气的方法，包括：
(A)压缩致冷气且涡轮膨胀已压缩的致冷气以产生冷却的致冷气；
(B)将液体天然气过冷且闪蒸已过冷的天然气以产生闪蒸蒸汽和液化天然气；和
(C)将闪蒸蒸汽和已冷却的致冷气通过与液体天然气的间接换热加热，以实现液体天然气的过冷。
如在此所使用，术语“闪蒸”意味着通过膨胀设备对液体减压使得液体的部分转化为汽相。
如在此所使用，术语“Joule-Thomson膨胀”意味着使用等焓降压设备的膨胀，该设备典型地可以是节流阀、节流孔或毛细管。
如在此所使用，术语“涡轮膨胀”意味着使用产生轴功的膨胀设备的膨胀。这样的轴功由轴的旋转产生，轴的旋转由通过一个或多个连接到轴，例如涡轮机轮盘的流体通道的流体的减压导致。
如在此所使用，术语“间接换热”意味着使两个流体处于换热关系而无任何流体的相互混合。
如在此所使用，术语“过冷”意味着将液体冷却到低于该液体对于现有压力的饱和温度的温度。
附图说明
唯一的附图是本发明的天然气液化方法的一个优选实施例的简化的示意性表示。
具体实施方式
一般地，本发明包括用于使用天然气的压力能来液化天然气的改进的方法，其中在致冷循环中使用来自天然气减压的闪蒸蒸汽，用于使高压天然气在闪蒸前过冷。
本发明将参考附图更详细地描述。现在参考附图，高压天然气流1处于一般地从700到1500磅/平方英寸绝对压力(psia)的范围内，通过使高压天然气流1通过处理系统160将它清除高沸杂质，例如水和硫化氢，该处理系统160可以是变温吸附系统。作为结果的天然气流2被分为部分60和部分3。部分60在热交换器110中被冷却，从热交换器110中作为已冷却的流62出来。部分3通向附加的净化系统165，用于将二氧化碳去除到通常低于50ppm的水平。作为结果的进一步清洁的天然气流50由通过热交换器110而被冷却，作为两相流52从热交换器110出来。已冷却的气体流62由于与热交换器120内的已膨胀的气体的间接换热而被进一步冷却，如将更完整地在下文中描述，以产生进一步已冷却的流63，流63具有低于-116.5的温度，该温度是甲烷的临界温度。
已冷却的天然气流63在第一膨胀中被膨胀，例如由于通过Joule-Thomson阀125被膨胀，以产生处于第一温度的已膨胀的气体流64，该温度典型地在从-120至-200的范围内。第一膨胀可以产生或不产生轴功。在图中图示的本发明的实施例中，第一膨胀是导致两相流64的Joule-Thomson膨胀，两相流64通过相分离器130，其中为分配的目的，将它分离为蒸汽流65和液体流66，进入热交换器120共同的通路且随后在热交换器110内。替代地，流66和流65可以在热交换器120和110的每个的分开的通道中被加热。虽然在图中图示为分开的元件，但本领域技术人员将认识到热交换器120和110可以组合在单个的芯内。
已膨胀的气体流由于通过热交换器120被加热，以提供对产品天然气流的冷却，如将在下文中更完整地描述。作为结果的已膨胀的气体流67进一步在热交换器110内被加热，以通过间接换热提供对产品天然气流的冷却且也提供对气体流60的冷却。
流67的典型地从流67的30％到60％的部分80在部分地横穿热交换器110后被收回，且通向涡轮膨胀机145，其中它被涡轮膨胀以提供具有第二温度的已涡轮膨胀的气体流81，该第二温度超过第一温度。一般地，已涡轮膨胀的气体流81的温度将比已膨胀的气体流64的温度至少高30。已涡轮膨胀的气体流81的温度典型地在从-30至-100的范围内。
在图中图示的本发明的替代实施例中，已涡轮膨胀的流81通向相分离器140且蒸汽和液体馏分以各流83和84通到热交换器110的共同的通路。在热交换器110内，已涡轮膨胀的气体流被间接换热加热，以提供对气体流60的冷却且也提供对产品天然气流的冷却。作为结果的已加热的已涡轮膨胀的气体流37被从热交换器110收回且可以在流38中回收。
已膨胀的气体流67的不通向涡轮膨胀机的部分68通向压缩机150，压缩机150优选地由从涡轮膨胀机145获得的膨胀的轴功驱动，且轴功在图4中以代表形式4图示。在压缩后，在流69内的气体可以在热交换器155内被冷却且作为结果的流70可以与流60组合以通向热交换器110且如前述处理。
两相天然气流52通向相分离器115。液体从相分离器115以流90收回，通过阀135且在图示中图示的实施例中以流91通过，用于与流81组合且进一步如前述处理。蒸汽从相分离器115以流53收回且进一步由于通过热交换器120被间接换热冷却和对已Joule-Thomson膨胀的天然气加热，以形成流11内的液体天然气，该液体天然气的压力一般地在从700至1500psia的范围内，且温度一般地在从-120至-180的范围内。流11由于通过热交换器205被过冷到在从-200至-260范围内的温度，以形成过冷的液体天然气流13。流13由于通过阀210被闪蒸以形成两相流14，两相流14的压力一般地在从14.7至40psia的范围内。
两相流14包括闪蒸蒸汽和液化天然气，它通向相分离器212内，从相分离器212收回产品液化天然气且在流15内回收。闪蒸蒸汽从相分离器212被收回在流30内且与流44内的致冷气组合以使液体天然气11过冷，如将在下文中更完整地描述。
致冷气33由于通过热交换器215已被加热到大约环境温度，它由于通过压缩机220被压缩，且作为结果的已压缩的致冷气34由于通过热交换器225被冷却去压缩的热，已形成流35。流35的部分36从致冷气循环被移除且优选地作为天然气被回收，最优选地如在图中所图示，通过与流37的组合以形成流38。已压缩的致冷气的剩余的部分40由于通过压缩机230被进一步压缩，以形成进一步压缩的致冷气41，致冷气41具有从150至350psia的范围内的压力。流41由于通过冷却器235被冷却去压缩的热，且作为结果的致冷气流42由于通过热交换器215被冷却到从-70至-170的范围内的温度。已冷却的致冷气从热交换器215以流43通向涡轮膨胀机240，其中它被涡轮膨胀到从14.7至40psia的范围内的压力，以生成致冷。由涡轮膨胀机240产生的轴功优选地用于提供运行压缩机230的动力的至少一些。
来自涡轮膨胀机240的具有作为结果的致冷的致冷气在热交换器205内被加热，以实现流11内的液体天然气的过冷。优选地，如在图中图示，在流44内已冷却的致冷气与流30内的闪蒸蒸汽组合以形成组合流31，组合流31通向热交换器205且被间接换热加热，以实现液体天然气的过冷。作为结果的已加热的致冷气以流32通过以加热热交换器215，从热交换器215以流33出来用于如前述处理。
虽然本发明已参考某个优选实施例详细描述，但本领域技术人员将认识到在权利要求书的精神和范围内存在本发明的其他实施例。

Claims (5)

1.一种用于产生液化天然气的方法，其包括：
(A)压缩致冷气且涡轮膨胀已压缩的致冷气以产生冷却的致冷气；
(B)将液体天然气过冷且闪蒸已过冷的天然气以产生闪蒸蒸汽和液化天然气；和
(C)将闪蒸蒸汽和已冷却的致冷气通过与液体天然气的间接换热加热，以实现液体天然气的过冷。
2.根据权利要求1所述的方法，其中在通过与过冷液体天然气的间接换热加热前将闪蒸蒸汽和已冷却的致冷气组合。
3.根据权利要求1所述的方法，其中致冷气的部分在涡轮膨胀前被收回。
4.根据权利要求1所述的方法，其中闪蒸蒸汽和已冷却的致冷气在所述的加热后被压缩以形成所述的已压缩的致冷气。
5.根据权利要求1所述的方法，其中过冷的液体天然气具有在从700至1500psia的范围内的压力，且作为闪蒸过冷的天然气的结果的闪蒸蒸汽和液化天然气具有在从14.7至40psia的范围内的压力。
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