CN107614994A - 混合制冷剂液化系统和方法 - Google Patents

混合制冷剂液化系统和方法 Download PDF

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Publication number
CN107614994A
CN107614994A CN201680032085.9A CN201680032085A CN107614994A CN 107614994 A CN107614994 A CN 107614994A CN 201680032085 A CN201680032085 A CN 201680032085A CN 107614994 A CN107614994 A CN 107614994A
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Prior art keywords
outlet
heat exchanger
entrance
steam
gas
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CN201680032085.9A
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CN107614994B (zh
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D.A.迪科特
T.P.古沙纳斯
M.R.格兰维尔
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Chatterton Energy Chemical Ltd By Share Ltd
Chart Energy and Chemicals Inc
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Chatterton Energy Chemical Ltd By Share Ltd
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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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
    • 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
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    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0042—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by liquid expansion with extraction of work
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J1/0057—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream after expansion of the liquid refrigerant stream with extraction of work
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    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/0097—Others, e.g. F-, Cl-, HF-, HClF-, HCl-hydrocarbons etc. or mixtures thereof
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
    • F25J1/0219—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle in combination with an internal quasi-closed refrigeration loop, e.g. using a deep flash recycle loop
    • 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
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    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0229—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock
    • F25J1/023—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock for the combustion as fuels, i.e. integration with the fuel gas system
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    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0235—Heat exchange integration
    • F25J1/0237—Heat exchange integration integrating refrigeration provided for liquefaction and purification/treatment of the gas to be liquefied, e.g. heavy hydrocarbon removal from natural gas
    • F25J1/0238—Purification or treatment step is integrated within one refrigeration cycle only, i.e. the same or single refrigeration cycle provides feed gas cooling (if present) and overhead gas cooling
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    • F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
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Abstract

用于液化气体的系统包括液化热交换器，其具有适于接收原料气的原料气入口和液化气出口，在气体通过与主制冷通道进行热交换而在热交换器的液化通道中液化之后液化气体经过该液化气出口离开。混合制冷剂压缩机系统被配置成向主制冷通道提供制冷剂。膨胀器分离器与液化热交换器的液化气出口连通，以及冷气体管线与膨胀器分离器流体连通。冷回收热交换器接收来自冷气体管线的冷蒸汽和来自混合制冷剂压缩系统的液体制冷剂，使得制冷剂利用冷蒸汽来冷却。

Description

混合制冷剂液化系统和方法
优先权声明
本申请要求于2015年4月10日提交的美国临时申请第62/145,929号和于2015年9月8日提交的美国临时申请第62/215,511号的优先权，各申请内容通过参考特此引入。
技术领域
本发明大体涉及用于冷却或液化气体的系统和方法，更具体而言，涉及混合制冷剂液化系统和方法。
发明内容
本发明主题有若干方面，其可在下面所述及所要求保护的方法、设备和系统中单独或一起实施。这些方面可单独使用或与本文所述主题的其他方面结合使用，并且对这些方面组合的描述无意排除单独使用这些方面或如所附权利要求所述的要求保护单独的或不同组合的这类方面。
在一个方面，提供了用于液化气体的系统，其包括具有热端和冷端的液化热交换器，所述热端包括原料气入口，所述冷端包括液化气出口，并且液化通道位于热端与冷端之间。原料气入口适于接收原料气。液化热交换器还包括主制冷剂通道。混合制冷剂压缩系统被配置成向该主制冷剂通道供应制冷剂。膨胀器分离器与液化热交换器的液化气出口连通。冷气管线与膨胀器分离器流体连通。冷回收热交换器具有与冷气管线连通的蒸汽通道和液体通道，其中所述蒸汽通道被配置成接收来自冷气管线的冷蒸汽。该混合制冷剂压缩系统包括与冷回收热交换器流体连通的液体制冷剂出口。所述冷回收热交换器被配置成在液体通道中接收制冷剂以及利用蒸汽通道中的冷蒸汽冷却液体通道中的制冷剂。
在另一方面，提供了用于液化气体的方法，其包括向液化热交换器供应原料气，该液化热交换器接收来自混合制冷剂压缩系统的制冷剂。气体利用来自混合制冷剂压缩系统的制冷剂在液化热交换器中被液化，使得产生液体产品。至少部分的所述液体产品膨胀并分离成蒸汽部分和液体部分。蒸汽部分被导向冷回收热交换器。制冷剂从混合制冷剂压缩系统被导向冷回收热交换器。利用蒸汽部分在冷回收热交换器中使制冷剂冷却。
在又一方面，提供了用于液化气体的系统，其包括具有热端和冷端的液化热交换器、具有位于所述热端出的入口和位于所述冷端处的出口的液化通道、主冷冻通道和高压制冷剂液体通道。混合制冷剂压缩系统与所述主冷冻通道和高压制冷剂液体通道连通。制冷剂膨胀器分离器具有与所述高压混合制冷剂液体通道连通的入口、与所述主冷冻通道连通的液体出口，以及与所述主冷冻通道连通的蒸汽出口。
在又一方面，提供了用于从原料气去除冷冻组分的系统，其包括重质烃热交换器、返回蒸汽通道和回流冷却通道，所述重质烃热交换器具有带有适于与原料气的源连通的入口的原料气冷却通道。该系统还包括洗涤装置，其具有与热交换器的原料气冷却通道的出口连通的原料气入口、与热交换器的返回蒸汽通道连通的返回蒸汽出口、与热交换器的回流冷却通道的入口连通的回流蒸汽出口，以及与热交换器的回流冷却通道的出口连通的回流混合相入口。回流液体组分通道具有均与所述洗涤装置连通的入口和出口。该洗涤装置被配置成使来自回流液体组分通道的出口的回流液体组分流汽化，以便冷却经该洗涤装置的原料气入口进入洗涤装置的原料气流，使得冷冻组分冷凝并经过冷冻组分出口从洗涤装置移除。已处理原料气管线与热交换器的蒸汽返回通道的出口连通。
在又一方面，一种用于从原料气去除冷冻组分的方法，包括提供重质烃去除热交换器和洗涤装置。利用热交换器冷却原料气，以产生冷却的原料气流。将冷却的气流导向洗涤装置。将来自洗涤装置的蒸汽导向热交换器，并冷却蒸汽，以产生混合相回流物流。将混合相回流物流导向洗涤装置，以便将液体组分回流物流供应给洗涤装置。液体组分回流物流在洗涤装置中被汽化，使得冷冻组分被冷凝并从洗涤装置中的已冷却原料气流中去除，从而产生已处理原料气蒸汽流。将已处理原料气蒸汽流导向热交换器。使已处理原料气蒸汽流在热交换器中加温，产生适于液化的已加温已处理原料气蒸汽流。
附图说明
图1是示出了混合制冷剂液化系统和方法的流程图和示意图，其具有在主热交换器的冷端的液化气流中的蒸汽/液体分离器，其中，来自分离器的冷端闪蒸气体经过主热交换器被导向至额外的制冷通道；
图1A是示出了混合制冷剂液化系统和方法的流程图和示意图，其具有在高压中温混合制冷流上的集成一体化蒸汽/液体分离器的液体膨胀器；
图2是示出了混合制冷剂液化系统和方法的流程图和示意图，其具有在主热交换器的冷端的液化气流中的蒸汽/液体分离器，其中，来自分离器的冷端闪蒸气体被导向冷回收热交换器，用于冷却混合制冷剂；
图2A是示出了混合制冷剂液化系统和方法的流程图和示意图，其具有在主热交换器的冷端的液化气流中的蒸汽/液体分离器，其中，来自分离器的冷端闪蒸气体经过主热交换器被导向至额外的制冷通道，以及导向至冷回收热交换器，用于冷却混合制冷剂；
图3是示出了混合制冷剂液化系统和方法的流程图和示意图，其具有在主热交换器的冷端的液化气流中的蒸汽/液体分离器，其中，来自分离器的冷端闪蒸气体被导向至冷回收热交换器，用于冷却混合制冷剂；其中冷回收热交换器还接收来自产品储罐的蒸发气；
图4是示出了混合制冷剂液化系统和方法的流程图和示意图，其中主热交换器冷端的液化气流被导向至储罐，其中终端闪蒸气体与液体产品分离且来自储罐的终端闪蒸气体和蒸发气被压缩并被导向至冷回收热交换器，用于冷却混合制冷剂；
图5是示出了混合制冷剂液化系统和方法的流程图和示意图，其中主热交换器冷端的液化气流被导向至储罐，其中终端闪蒸气体与液体产品分离且终端闪蒸气体和来自储罐的蒸发气被压缩并被导向至冷回收热交换器，用于冷却混合制冷剂；
图6是示出了混合制冷剂液化系统和方法的流程图和示意图，其中原料气首先用重质烃去除热交换器冷却，并且冷冻组分从原料气被去除；
图7是示出了混合制冷剂液化系统和方法的流程图和示意图，其中原料气首先用重质烃去除热交换器冷却，并且冷冻组分从原料气被去除。
具体实施方式
混合制冷剂液化系统和方法的实施方式图示于图1-7中。应注意尽管下面依据使天然气液化产生液化天然气而解释和描述了所述实施方式，然而本发明可用于液化其他类型的气体。
基本液化处理和混合制冷剂压缩系统可以如Gushanas等的共同拥有的美国专利公开号2011/0226008、美国专利申请号12/726,142中所述，该两篇专利申请的内容通过参考特此引入。通常，参考图1，该系统包括通常以10表示的多路热交换器，其具有热端12和冷端14。该热交换器接收高压天然气进料流16，该高压天然气进料流在冷却或液化通道18中通过与热交换器中的制冷流进行热交换来去除热而被液化。结果，产生液化天然气(LNG)产品流20。该热交换器的多路设计允许数种流方便且能量有效地结合到单一交换器中。合适的热交换器可购自德克萨斯州的The Woodlands的Chart Energy&Chemicals,Inc.。可从Chart Energy&Chemicals,Inc.购得的板翅式多路热交换器提供了物理上紧凑的额外优势。
包括热交换器10在内的图1的系统可被配置成执行现有技术中已知的其他气体处理选项。这些处理选项可能需要气流离开及再进入热交换器一次或多次，并且可包括例如天然气液体回收或氮排除。
热去除在热交换器中利用混合制冷剂来实现，该混合制冷剂利用通常以22标示的混合制冷剂压缩系统来处理和调节。混合制冷剂压缩系统包括高压储存器(accumulator)43，其在最后的压缩和冷却循环之后接收并分离混合制冷剂(MR)混合相流11。尽管描述了聚集鼓(accumulator drum)43，然而可使用可选的分离装置，其包括但不限于另一类型的容器、旋风分离器、蒸馏装置、聚结分离器或者筛型或叶轮型除雾器。高压蒸汽制冷剂流13离开储存器43的蒸汽出口并行进至热交换器10的热侧。
高压液体制冷剂流17离开储存器43的液体出口，并且还行进至热交换器的热端。在热交换器10中冷却之后，其作为混合相流47行进至中温立管(stand pipe)128。
在来自储存器43的高压蒸汽流13在热交换器10中冷却之后，混合相流19流至冷蒸汽分离器21。所得到的蒸汽制冷剂流23离开分离器21的蒸汽出口，并且在热交换器10中冷却之后作为混合相流29行进至低温立管27。蒸汽和液体流41和45离开低温立管27并进料到热交换器10的冷侧上的主制冷通道125中。
离开冷蒸汽分离器21的液体流25在热交换器10中被冷却，并作为混合相流122离开热交换器，以下文所述的方式对其进行处理。
图2-7的系统示出了类似于上述那些的组件。
图1所示的系统利用膨胀器分离器24，其可以是带有集成蒸汽/液体分离器的液体膨胀器，或者其可以是与任何蒸汽/液体分离装置串联的液体膨胀器，以便随着压力降低将能量从高压LNG流20中提取出来。这导致LNG温度降低并产生终端闪蒸气体(end flashgas)(EFG)，由此，在相同MR功率下提供了改进的LNG生产以及改进的能耗/吨所产LNG。由液体膨胀产生的冷端闪蒸气体作为流26离开蒸汽/液体分离器24，并被送至主液化热交换器10的冷端，并通过引入额外的冷冻通道28而与热交换器整合，使得其有助于液化的总体制冷要求，从而进一步改进相同MR功率下的LNG生产，而无需对主热交换器10增加大量的资本成本。仅作为实例，EFG流26可具-254°F的温度和19psia的压力。
在图1的系统中，EFG制冷或者全部在热交换器10中回收或者可以部分回收，以最佳配合设备和工艺设计。热端闪蒸气体作为流32离开热交换器，并且在可选地经过压缩机31的压缩之后，能够再循环至工厂原料气，用作燃气涡轮机/工厂燃料35或者以任何其他可接受的方式处置。LNG液体膨胀器可与下面参考图1A所述的中温液体膨胀器一起使用或不与其一起使用。
图2系统为图1所示的EFG冷回收配置的可选方案。在该可选方案中，来自蒸汽/液体分离器36的EFG冷制冷流34被导向至冷回收热交换器38，在那里其与热高压混合制冷(MR)流或者来自MR压缩系统22的高压储存器43的流42进行热交换。高压MR流42利用来自流34的EFG冷却，然后经管线46和中温立管(中等温度立管)48(如图3中的管线49所示)或者可选地经由中温液体膨胀器52(如图2中的管线46所示)或冷立管54(如图2中的虚线管线51所示)返回至液化热交换器44的制冷通道55。一旦来自冷回收热交换器38的冷却的高压MR流被中温立管48或中温液体骤冷分离器52接收，其通过(图2的)管线57a和57b被输送到液化热交换器44的制冷通道55。
仅作为实例，图2的EFG流34可具有-252°F的温度和30psia的压力。
图1和2的冷回收方案可组合，如图2A所示。更具体而言，离开蒸汽/液体分离器58的EFG流56被分开，形成流62和流68，流62进入主热交换器66的制冷通道64，而流68进入冷回收热交换器72，以冷冻如上关于图2的系统所述的流经该冷回收热交换器72的MR流74。因此，冷EFG以最佳比例在主热交换器66和冷回收热交换器72两者中回收，以配合设备和工艺。流向流62和流68的EFG流56的部分可通过阀69来控制。
图3的系统显示了另一可选方案，用于EFG流75自蒸汽/液体分离器77以及蒸发汽(boil-off gas)(BOG)自LNG产品储罐76和其他来源的冷回收。在该配置中，BOG流78离开储罐76并行进至设置于冷回收热交换器82中的BOG冷回收通道80。或者，冷回收热交换器82可以具有单一共享的EFG和BOG通道、且EFG流75和BOG流78在进入冷回收热交换器82之前组合，如在图3中以虚线84所示。在任一种情况中，高压MR通过EFG和BOG冷却并如上所述用作制冷。
在可选实施方式中，参考图4，系统可利用LNG产品储罐88作为蒸汽/液体分离器，以从离开液体膨胀器94的液体产品流92获得EFG。应注意，焦耳-汤姆森(JT)阀可替换液体膨胀器94以冷却流。根据上面的描述清楚的是，液体膨胀器94接收来自主热交换器98的液体产品流96。因此，图4的系统提了EFG和BOG两者的冷回收，其中EFG分离自LNG储罐中的LNG，且EFG和BOG均通过流104被导至冷回收热交换器102。因此，流至冷回收热交换器102的高压MR流105被EFG和BOG冷却。
在图4的系统中，EFG和BOG流104被导向至压缩机106，在那里其被压缩至第一级压力。选择该压力，以便(1)为离开压缩机的流108提供适当的压力和温度，从而允许在冷回收热交换器102中的较高压降，并且降低成本；和(2)适于向该冷回收热交换器供应一温度，该温度使得离开的MR流112用作主热交换器98中的制冷剂。仅作为实例，离开压缩机106的MR流的压力和温度可以是-175°F和30psia。离开冷回收热交换器102的EFG和BOG流114可经压缩机116压缩并用作进料再循环118或燃气涡轮机/工厂燃料122或以任何其他可接受的方式进行处置。
如图5所述，图4的预热交换器压缩机106可省略，使得来自LNG罐88的EFG和BOG流104直接行进至冷回收热交换器102。因此，在冷回收热交换器之后仅发生EFG和BOG流104的压缩(经由压缩机116)。在其他方面，图5的系统与图4的系统相同。
返回至图1，可选的液体膨胀器分离器120通过管线117接收至少一部分高压中温MR制冷剂流122，液体膨胀器分离器120可以是具有集成的蒸气/液体分离器的液体膨胀器，或串联的两部件。该液体膨胀器从MR流提取功(work)、降低温度并且在离开液体膨胀器的MR流体经管线119行进至中温立管分离器128然后经流123a和123b加入热交换器制冷流125，以及改善循环效率。相应回路具有阀124和126。在阀126至少部分打开以及阀124至少部分闭合的情况下，液体膨胀器120与中温立管分离器128串联使用。
可选地，参考图1A，可使用带有集成蒸汽/液体分离器/液体泵的液体膨胀器分离器130(或者串联的三个组件)，以消除中温立管(图1的128)并提供单独的液体MR制冷流132和单独的蒸汽MR制冷流134，其加入热交换器136的制冷流135，以促进主热交换器136的适当的蒸汽/液体分布，而无需使用立管分离器。使用带有集成蒸汽/液体分离器/液体泵的液体膨胀器130，以便增加对液体流的压力(如在热交换器中通过喷射设备利用液体所要求的)，以及改善液体在热交换器内的分布。仅作为实例，离开泵130的液体流的压力和温度可以是-147°F和78psia。这降低了对船舶运动的灵敏度，而不会增加立管中的液体体积(高度)，因为在该构造中消除了立管。
图1(120)和图1A(130)的中温液体膨胀器可与图1(24)、图2(36)、图2A(58)、图3(77)和4(94)的LNG液体膨胀器一起使用或不与上面所述的图1(24)、图2(36)、图2A(58)、图3(77)和4(94)的LNG液体膨胀器一起使用。
现在将参考图6和7描述在主热交换器中液化之前从原料气中去除冷冻组分的系统和方法。尽管这些系统的部件示于剩下的图中，但是它们可用于本文公开的系统。此外，在液化之前用于从原料气去除冷冻组分的系统和方法可用于使用混合制冷剂的那些系统之外的液化系统。如图6所示，在任何预处理系统144之后，进料气流142在重质烃去除热交换器146中被冷却。然后经由JT阀或者，如虚线管线175所示，经由气体膨胀器/压缩机组152a/152b，降低出口流148的压力，并将其进料至洗涤塔或鼓154或其他洗涤(scrub)设备。如果使用膨胀器/压缩机组152a/152b，则管线148的气体膨胀器152a驱动管线175中的压缩机152b来压缩气体，其在主热交换器178中被液化。结果，膨胀器/压缩机组152a/152b通过降低管线148中的气体的压力以及增加管线176中的气体的压力而降低了主热交换器的能量需求。
如图6(和图7)182所示，温度传感器182与管线148连通，并控制冷却旁路管线186的旁路阀184。温度传感器182检测已冷却气流148的温度并将其与相关控制器(未显示)的设置进行比较，以便使进入洗涤塔154的流实现所需的温度或温度范围。如果流148的温度低于预设水平，则阀184打开，以引导更多流体经过旁路管线186。如果流148的温度高于预设水平，则阀184闭合，以引导更多流体经过热交换器146。作为替代方案，温度传感器182可位于洗涤塔(scrubcolumn)154中。如图7所示，旁路管线186可以可选地直接进入洗涤塔154的底部。图6中所示的旁路管线186和管线148的汇合点相比洗涤塔154的底部处于较高压力。结果，图7的实施方式提供了较低的旁路管线186出口压力，这提供了更精确的温度控制并允许使用较小的(且更经济的)旁路阀184。
经由回流流155使塔154回流所需的制冷通过(任选在JT阀226之后(图7)的)来自塔的返回蒸汽156来提供(返回蒸汽156在热交换器146中升温)，或者可选地通过来自液化压缩系统(通常以162表示)的混合制冷剂(MR)流例如158(图6)来提供，该混合制冷剂(MR)流也被导向至热交换器146。混合制冷剂流可来自162的任何压缩MR流或任何组合MR流。离开洗涤塔的流153尽管优选全部为蒸汽，但是含有在较高温度下液化的组分(与离开该塔顶部的蒸汽流156相比)。结果，经过热交换器146之后进入塔154的流155为两相，并且液体组分流进行回流。液体组分流流过回流液体组分通道，其仅作为示例可包括回流液体组分管线，该管线可在洗涤装置的外部(157)或内部，或者可以是下导管或者位于洗涤装置154内的其他内部液体分配设备。如上所述，液化压缩系统的操作可以如Gushanas等的共同拥有的美国专利申请公开号2011/0226008、美国专利号12/726,142中所述。当MR经由管道164在重质烃热交换器中初步冷却之后，使其在JT阀166上闪蒸，以向重质烃去除热交换器提供冷混合制冷剂流168。
通过控制混合制冷剂的沸腾压能够控制该混合制冷剂的温度。
将经由流172从洗涤塔154底部去除的组分返回至热交换器146，以回收制冷，然后送至另外的分离步骤，诸如通常以174所示的凝液汽提系统，或者送至燃料或其他处理方法。
然后将离开热交换器146且冷冻组分已去除的进料气流176送至主液化热交换器178，或者在包括膨胀器/压缩机的情况中，将其首先压缩，然后送至主热交换器178。
现在将参考图7描述在主热交换器208中在液化之前用于从进料气流去除冷冻组分的系统和方法。应理解，图7仅示出了液化系统的诸多可能选项之一，其总体以209表示。下面参考图7描述的去除冷冻组分的系统和方法可用于任何其他液化系统或方法(包括但不限于图1-6公开的那些)并且在一些情况下可合并于所述液化系统和方法内。
在图7的系统和方法中，流经管线210的进料气利用膨胀器212降低压力，膨胀器212连接至压缩机214或诸如制动器或发电机的其他装载装置。通过膨胀过程来冷却气体，然后使其在重质烃去除热交换器216中进一步冷却，然后送至洗涤塔或分离鼓218或其洗涤装置，以从进料气中分离冷冻组分。
任选地，可将原料气在膨胀器212之前经由加热装置222来加热，以增加通过膨胀器回收的能量，并因此提供额外的压缩功率。加热装置可以是热交换器或本领域已知的任何其他加热装置。
如图6中的实施方式，经由回流流223使洗涤塔回流所需的制冷通过来自塔的返回蒸汽224来提供，其在热交换器216中被加热之前经由JT阀226来进一步降低压力和温度，或者可选地通过流经由例如管线228来自液化压缩机系统(大体以227表示)的混合制冷剂(MR)来提供。混合制冷剂流可来自227的任何压缩MR流或任何MR流组合。进入塔218的流223为两相且液体组分流进行回流。液体组分流流经回流液体组分通道，其可包括仅作为示例的回流液体组分管线，该管线可在洗涤装置的外部(225)或内部，或者可以是下导管或者位于洗涤装置218内的其他内部液体分配设备。如上所述，液化压缩机系统的操作可以如授予Gushanas等的共同拥有的美国专利申请公开号2011/0226008、美国专利号12/726,142中所述。在混合制冷剂在重质烃热交换器中冷却之后，其在JT阀232上闪蒸，以向重质烃去除热交换器提供冷混合制冷剂。
通过控制混合制冷剂的沸腾压能够控制该混合制冷剂的温度。
所去除的组分在行进经过洗涤塔底部的冷冻组分出口之后可返回至热交换器216，以经由管线234回收冷制冷(cold refrigeration)，然后送至其他分离步骤，诸如如图7所述经由管线236至凝液汽提系统238，或者送至燃料或其他处置方法，且回收或不回收冷制冷。
然后将冷冻组分已去除的原料气流244，在膨胀器/压缩机的压缩机214中压缩之后，送至液化系统的主热交换器208。如果需要额外的原料气压缩，则可用下述代替膨胀器/压缩机：能够配合该膨胀器的压扩器、额外的压缩级(如果需要)，以及另一驱动器，诸如电动机246蒸汽涡轮机等。另一选择是简单增加与膨胀器驱动的压缩机串联的增压压缩机。在所有情况中，增加的原料气压力降低了液化所需的能量并改进了液化效率，这进而能够增加液化容量。
尽管已经显示和描述的本发明的优选实施方式，然而对于本领域技术人员显而易见的是，可在其中进行改变和修饰而不会背离本发明的实质，其范围由所附权利要求书限定。

Claims (62)

1.一种用于液化气体的系统，其包括：
a.具有热端和冷端的液化热交换器，所述热端包括原料气入口，所述冷端包括液化气出口，且液化通道位于所述原料气入口和所述液化气出口之间，其中所述原料气入口适于接收原料气，所述液化热交换器还包括主制冷通道；
b.混合制冷剂压缩机系统，其配置成向所述主制冷通道提供制冷剂；
c.与所述液化热交换器的液化气出口连通的膨胀器分离器；
d.与所述膨胀器分离器流体连通的冷气管线；
e.具有液体通道和与所述冷气管线连通的蒸汽通道的冷回收热交换器，其中所述蒸汽通道被配置成从所述冷气管线接收冷蒸汽；和
f.所述混合制冷剂压缩机系统包括与所述冷回收热交换器的液体通道流体连通的液体制冷剂出口，所述冷回收热交换器被配置成接收所述液体通道中的制冷剂以及利用蒸汽通道中的冷蒸汽冷却所述液体通道中的制冷剂。
2.如权利要求1所述的系统，其中所述膨胀器分离器包括液体产品出口和终端闪蒸气体出口，且其中冷气管线与所述终端闪蒸气体出口连通，以便向所述冷回收热交换器的蒸汽通道提供终端闪蒸气体。
3.如权利要求2所述的系统，其中所述液化热交换器包括也与膨胀器分离器的终端闪蒸气体出口连通的终端闪蒸气体通道。.
4.如权利要求2所述的系统，还包括与所述膨胀器分离器的液体产品出口连通的液体产品储罐，且其中所述冷回收热交换器包括第二蒸汽通道，所述液体产品储罐被配置成从离开液体产品出口进入储罐的液体产品流产生产品终端闪蒸气体，所述液体产品储罐具有与所述第二蒸汽通道连通的顶部空间，使得产品终端闪蒸气体被提供给所述冷回收热交换器的第二蒸汽通道。
5.如权利要求2所述的系统，还包括与所述膨胀器分离器的液体产品出口连通的液体产品储罐，所述液体产品储罐被配置成从离开液体产品出口进入储罐的液体产品流产生产品终端闪蒸气体，所述液体产品储罐具有还与所述冷回收热交换器的蒸汽通道连通的顶部空间，使得来自所述产品储罐的顶部空间的产品终端闪蒸气体和来自所述膨胀器分离器的终端闪蒸气体出口的终端闪蒸气体被提供给所述冷回收热交换器的蒸汽通道。
6.如权利要求1所述的系统，其中所述膨胀器分离器包括液体产品出口，且还包括与所述液体产品出口连通的液体产品储罐，所述液体产品储罐被配置成从离开液体产品出口进入储罐的液体产品流产生产品终端闪蒸气体，所述液体产品储罐具有与所述冷气管线连通的顶部空间，使得产品终端闪蒸气体被提供给所述冷回收热交换器的蒸汽通道。
7.如权利要求6所述的系统，还包括位于所述冷气管线内的压缩机。
8.如权利要求1所述的系统，其中所述冷回收热交换器的液体通道的出口与所述主制冷通道流体连通，以便向所述主制冷通道提供在所述冷回收热交换器中冷却的液体制冷剂。
9.如权利要求1所述的系统，其中所述冷回收热交换器的蒸汽通道的出口与压缩机连通。
10.如权利要求1所述的系统，其中所述混合制冷剂压缩系统包括分离装置，其包括分离装置液体出口和分离装置蒸汽出口，且其中所述分离装置液体出口与所述冷回收热交换器的液体通道流体连通。
11.如权利要求1所述的系统，其中所述膨胀器分离器是带有集成蒸汽/液体分离器的液体膨胀器。
12.如权利要求1所述的系统，其中所述膨胀器分离器包括与蒸汽/液体分离器串联的液体膨胀器。
13.一种用于液化气体的方法，包括以下步骤：
a.向从混合制冷剂压缩机系统接收制冷剂的液化热交换器提供原料气；
b.利用来自所述混合制冷剂压缩系统的制冷剂以在所述液化热交换器中液化气体，从而产生液体产品；
c.使所述液体产品的至少一部分膨胀并分离成蒸汽部分和液体部分；
d.将所述蒸汽部分导向至冷回收热交换器；
e.将来自所述混合制冷剂压缩系统的制冷剂导向至冷回收热交换器；和
f.利用所述蒸汽部分以在所述冷回收热交换器中冷却所述制冷剂。
14.如权利要求13所述的方法，其中步骤c包括：
g.利用液体膨胀器将所述液体产品膨胀为第一蒸汽部分和第一液体部分；
h.将所述第一液体部分闪蒸为第二蒸汽部分和第二液体部分；和
其中步骤d包括将所述第一和第二蒸汽部分导向至所述冷回收热交换器。
15.如权利要求14所述的方法，还包括储存第二液体部分的步骤。
16.如权利要求13所述的方法，还包括在将蒸汽部分导向至冷回收热交换器之前将其压缩的步骤。
17.如权利要求13所述的方法，还包括在蒸汽部分离开冷回收热交换器之后将其压缩的步骤。
18.一种用于液化气体的系统，包括
a.液化热交换器，其具有热端和冷端以及：
i)具有位于所述热端的入口和位于所述冷端的出口的液化通道；
ii)主制冷通道；
iii)高压制冷剂液体通道；
b.与所述主制冷通道和所述高压制冷剂液体通道连通的混合制冷剂压缩机系统；
c.制冷剂膨胀器分离器，其具有与高压混合制冷剂液体通道连通的入口、与主制冷通道连通的液体出口和与主冷冻通道连通的蒸汽出口。
19.如权利要求18所述的系统，其中所述制冷剂膨胀器分离器还包括泵。
20.如权利要求18所述的系统，还包括立管，所述立管具有与所述制冷剂膨胀器分离器的液体和蒸汽出口连通的入口、和与主制冷通道连通的液体出口以及与主制冷通道连通的蒸汽出口。
21.一种用于从原料气去除冷冻组分的系统，其包括：
a.具有出口和适于与原料气的源连通的入口的原料气管线；
b.具有出口和与原料气管线的出口连通的入口的膨胀器，所述膨胀器可操作地连接至装载装置；
c.重质烃去除热交换器，其具有原料气冷却通道，所述原料气冷却通道具有适于与膨胀器的出口连通的入口、返回蒸汽通道和回流冷却通道；
d.洗涤装置，其具有：
i)与热交换器的原料气冷却通道的出口连通的原料气入口；
ii)与热交换器的返回蒸汽通道的入口连通的返回蒸汽出口；
iii)与热交换器的回流冷却通道的入口连通的回流蒸汽出口；
iv)与热交换器的回流冷却通道的出口连通的回流混合相入口；
e.具有入口和与洗涤装置连通的出口的回流液体组分通道；
f.所述洗涤装置被配置成使来自回流液体组分通道的出口的回流液体组分流蒸发，从而冷却经由洗涤装置的原料气入口进入洗涤装置的原料气流，使得冷冻组分被冷凝且经冷冻组分出口从洗涤装置中被去除；和
g.与热交换器的蒸汽返回通道的出口连通的已处理原料气管线。
22.如权利要求21所述的系统，其中所述装载装置是压缩机，且所述热交换器的蒸汽返回通道的出口与所述压缩机的入口连通以及所述压缩机的出口与所述已处理原料气管线连通。
23.如权利要求22所述的系统，还包括与压缩机连接以向压缩机提供额外功率的发动机。
24.如权利要求22所述的系统，还包括与压缩机和已处理原料气管线连通的附加压缩机级以及连接至该附加压缩机级以为该附加压缩机级提供动力的发动机。
25.如权利要求21所述的系统，其中所述装载装置为发电机。
26.如权利要求21所述的系统，其还包括加热装置，其具有与原料气管线的出口连通的入口和与膨胀器的入口连通的出口。
27.如权利要求21所述的系统，还包括膨胀装置，且其中热交换器包括第一混合制冷剂通道和第二混合制冷剂通道，所述第一混合制冷剂通道具有适于与混合制冷剂的源连通的入口和与膨胀装置的入口连通的出口，且所述第二混合制冷剂通道具有与膨胀装置的出口连通的入口。
28.如权利要求27所述的系统，其中所述膨胀装置是焦耳-汤姆森阀。
29.如权利要求21所述的系统，还包括膨胀装置，其具有与洗涤装置的返回蒸汽出口连通的入口和与热交换器的返回蒸汽通道的入口连通的出口。
30.如权利要求29所述的系统，其中所述膨胀装置是焦耳-汤姆森阀。
31.如权利要求21所述的系统，其中热交换器包括具有与洗涤装置的冷冻组分出口连通的入口的制冷回收通道。
32.如权利要求31所述的系统，其中热交换器的制冷回收通道具有与凝液汽提系统连通的出口。
33.如权利要求21所述的系统，其中洗涤装置的冷冻组分出口与凝液汽提系统连通。
34.一种用于液化气体的系统，其包括：
a.具有热端和冷端以及具有在热端的入口和在冷端的出口的液化通道的液化热交换器；
b.与所述液化热交换器连通且适于冷却所述液化通道的混合制冷剂压缩系统；
c.连接至液化通道的出口的液化气出口管线；
d.具有出口和适于与原料气的源连通的入口的原料气管线；
e.具有出口和与原料气管线的出口连通的入口的膨胀器，所述膨胀器可操作连接至装载装置；
f.重质烃去除热交换器，其具有带有适于与膨胀器的出口连通的入口的原料气冷却通道、返回蒸汽通道和回流冷却通道；
g.洗涤装置，其具有：
i)与去除热交换器的原料气冷却通道的出口连通的原料气入口；
ii)与去除热交换器的返回蒸汽通道的入口连通的返回蒸汽出口；
iii)与去除热交换器的回流冷却通道的入口连通的回流蒸汽出口；
iv)与去除热交换器的回流冷却通道的出口连通的回流混合相入口；
h.具有入口和与洗涤装置连通的出口的回流液体组分通道；
i.所述洗涤装置被配置成使来自回流液体组分通道的出口的回流液体组分流蒸发，从而冷却经洗涤装置的原料气入口进入洗涤装置的原料气流，使得冷冻组分被冷凝且通过冷冻组分出口从洗涤装置去除；和
j.与热交换器的蒸汽返回通道的出口和与液化热交换器的液化通道的入口连通的已处理原料气管线。
35.如权利要求34所述的系统，其中所述装载装置是压缩机，其具有与热交换器的蒸汽返回通道的出口连通的入口和经由已处理原料气管线与液化热交换器的液化通道连通的出口。
36.如权利要求35所述的系统，还包括与压缩机连接以向压缩机提供额外功率的发动机。
37.如权利要求35所述的系统，还包括与压缩机和液化热交换器的液化通道连通的附加压缩机级以及连接至该附加压缩机级以为该附加压缩机级提供动力的发动机。
38.如权利要求34所述的系统，其中所述装载装置是发电机。
39.如权利要求34所述的系统，还包括加热装置，其具有与原料气管线的出口连通的入口和与膨胀器的入口连通的出口。
40.如权利要求34所述的系统，还包括膨胀装置，且其中热交换器包括第一混合制冷剂通道和第二混合制冷剂通道，所述第一混合制冷剂通道具有适于与混合制冷剂压缩系统连通的入口和与膨胀装置的入口连通的出口，且所述第二混合制冷剂通道具有与膨胀装置的出口连通的入口和与混合制冷剂压缩系统连通的出口。
41.如权利要求40所述的系统，其中所述膨胀装置是焦耳-汤姆森阀。
42.如权利要求34所述的系统，还包括膨胀装置，其具有与洗涤装置的返回蒸汽出口连通的入口和与热交换器的返回蒸汽通道的入口连通的出口。
43.如权利要求42所述的系统，其中所述膨胀装置是焦耳-汤姆森阀。
44.如权利要求34所述的系统，其中所述热交换器包括具有与洗涤装置的冷冻组分出口连通的入口的制冷回收通道。
45.如权利要求44所述的系统，其中所述热交换器的制冷回收通道具有与凝液汽提系统连通的出口。
46.如权利要求34所述的系统，其中所述洗涤装置的冷冻组分出口与凝液汽提系统连通。
47.一种用于从原料气去除冷冻组分的系统，其包括：
a.重质烃去除热交换器，其具有带有适于与原料气的源连通的入口的原料气冷却通道、返回蒸汽通道和回流冷却通道；
b.洗涤装置，其具有：
i)与热交换器的原料气冷却通道的出口连通的原料气入口；
ii)与热交换器的返回蒸汽通道的入口连通的返回蒸汽出口；
iii)与热交换器的回流冷却通道的入口连通的回流蒸汽出口；
iv)与热交换器的回流冷却通道的出口连通的回流混合相入口；
c.具有入口和与洗涤装置连通的出口的回流液体组分通道；
d.所述洗涤装置被配置成使来自回流液体组分通道的出口的回流液体组分流蒸发，从而冷却通过洗涤装置的原料气入口进入洗涤装置的原料气流，使得冷冻组分被冷凝且经冷冻组分出口从洗涤装置去除；和
e.与热交换器的蒸汽返回通道的出口连通的已处理原料气管线。
48.如权利要求47所述的系统，还包括膨胀装置，且其中热交换器包括第一混合制冷剂通道和第二混合制冷剂通道，所述第一混合制冷剂通道具有适于与混合制冷剂的源连通的入口和与膨胀装置的入口连通的出口，且所述第二混合制冷剂装置具有与膨胀装置的出口连通的入口。
49.如权利要求48所述的系统，其中所述膨胀装置是焦耳-汤姆森阀。
50.如权利要求47所述的系统，还包括膨胀装置，其具有与洗涤装置的返回蒸汽出口连通的入口和与热交换器的返回蒸汽通道的入口连通的出口。
51.如权利要求50所述的系统，其中所述膨胀装置是焦耳-汤姆森阀。
52.一种用于从原料气去除冷冻组分的方法，包括以下步骤：
a.提供重质烃去除热交换器和洗涤装置；
b.利用热交换器冷却原料气，以产生经冷却的原料气流；
c.将经冷却的原料气流导向至洗涤装置；
d.将来自洗涤装置的蒸汽导向至热交换器并冷却该蒸汽，以产生混合相回流流；
e.将混合相回流流导向至洗涤装置，使得液体组分回流流被提供给洗涤装置；
f.使洗涤装置中的液体组分回流流蒸发，使得冷冻组分被冷凝并从洗涤装置中的经冷却原料气流中去除，以产生已处理原料蒸汽流；
g.将已处理原料气蒸汽流导向至热交换器；和
h.在热交换器中加温该已处理原料气蒸汽流，以产生适合液化的加温的已处理原料气蒸汽流。
53.如权利要求52所述的方法，还包括在利用热交换器冷却原料气之前使其膨胀的步骤。
54.如权利要求53所述的方法，还包括在使原料气膨胀之前将其加热的步骤。
55.如权利要求53所述的方法，还包括压缩所述加温的已处理原料气蒸汽流的步骤。
56.如权利要求55所述的方法，其中压缩所述加温的已处理原料气蒸汽流利用膨胀器驱动的压缩机完成，所述膨胀器用于在利用热交换器冷却原料气之前使其膨胀。
57.如权利要求55所述的方法，还包括对压缩的且加温的已处理原料气蒸汽流进行液化的步骤。
58.如权利要求52所述的方法，其中所述已处理原料气蒸汽流在离开洗涤装置之后且在被导向至热交换器之前利用膨胀装置来冷却。
59.如权利要求52所述的方法，还包括将已冷凝且已去除的冷冻组分导向至热交换器以回收冷制冷以及产生冷冻组分热交换器出口流的步骤。
60.如权利要求59所述的方法，还包括在冷冻组分热交换器出口流上进行额外的分离步骤。
61.如权利要求52所述的方法，还包括在已冷凝且已去除的冷冻组分上进行额外的分离步骤。
62.如权利要求52所述的方法，还包括对加温的已处理原料气蒸汽流进行液化的步骤。
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