CN105008834B - 用于再液化天然气的方法和装置 - Google Patents

用于再液化天然气的方法和装置 Download PDF

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CN105008834B
CN105008834B CN201380067110.3A CN201380067110A CN105008834B CN 105008834 B CN105008834 B CN 105008834B CN 201380067110 A CN201380067110 A CN 201380067110A CN 105008834 B CN105008834 B CN 105008834B
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gas
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natural gas
pipeline
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CN105008834A (zh
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V.富赫斯
M.拉戈
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Cryostar SAS
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C13/00—Details of vessels or of the filling or discharging of vessels
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C9/00—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure
    • F17C9/02—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure with change of state, e.g. vaporisation
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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
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    • 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
    • F25J1/0025—Boil-off gases "BOG" from storages
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—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"
    • F25J1/0045—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 vaporising a liquid return stream
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    • 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
    • F25J1/0047—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
    • F25J1/005—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 expansion of a gaseous refrigerant stream with extraction of work
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    • 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
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    • F25J1/0204—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 single-component refrigerant [SCR] fluid in a closed vapor compression cycle as a single flow SCR cycle
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    • 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
    • F25J1/02—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
    • F25J1/0228—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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    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
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    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0244—Operation; Control and regulation; Instrumentation
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    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0262—Details of the cold heat exchange system
    • F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
    • F25J1/0265—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer
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    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop

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Abstract

从通常位于航海船只上的LNG储存罐4、6、8、10和12汽化的天然气在包括压缩级26、28、30和32的多级压缩器24中被压缩。压缩天然气流的至少一部分被发送到液化器47，该液化器通常以布雷登循环操作以便被再液化。来自最后级32的压缩天然气的温度通过穿过热交换器22而降低到低于0℃。第一压缩级26作为冷压缩器而操作且所得的冷压缩天然气被用于热交换器22中以实现对来自所述压缩级32的流的必要冷却。在其穿过所述热交换器22的下游，所述冷压缩天然气流过所述压缩器24的其余级28、30和32。如果需要，所述压缩天然气的一部分作为燃料可被供应到航海船只的发动机。

Description

用于再液化天然气的方法和装置
本发明涉及一种用于再液化天然气的方法和装置。
特别而言，本发明涉及一种用于再液化从通常在船上或其它航海船只上的液化天然气(LNG)储存罐汽化的天然气的方法。
美国专利申请2007/0256450 A、2009/0158773 A和2009/0158774都公开了液化从其中从其压缩上游的汽化气体恢复制冷的储存罐汽化的天然气(“汽化”气体)的方法。压缩的汽化气体在其压缩的下游被再液化。压缩的汽化气体在热交换器中被预冷却，通过该热交换器的相同气体以以下方式穿过其压缩的上游：压缩汽化气体的温度可降低到远低于环境温度且因此被提供在液化器中以便液化天然气所需的制冷的量降低。
然而，上面描述的布置具有显著缺点。汽化气体从其中放出的液化天然气储存罐被设计为在仅稍高于大气压的液面上方空间压力下操作。在汽化气体压缩器的上游提供热交换器可引起压力下降到低于大气压，其结果是，具有空气被吸入装置内的重大风险。这种空气的存在可引起爆炸风险，特别是在所有的汽化气体被再液化并返回到储存罐的时候。即使热交换器过大，仍然会有显著压降，这将引起在整个系统保持足够压力上的操作困难。
根据本发明，提供了一种回收从盛装液化天然气(LNG)的至少一个储存容器放出的汽化气体的方法，其包括使汽化气体的流在第一压缩级中冷压缩，通过热交换来加热冷压缩汽化气体的流，进一步压缩冷压缩汽化气体的加热流，和采用汽化气体的进一步压缩的流的至少一部分以在所述热交换中加热冷压缩汽化气体的流并因此降低进一步压缩的汽化气体的所述部分的温度，和再液化经受温度降低的汽化气体的进一步压缩的流的所述部分的至少一部分。
本发明还提供了一种用于回收来自盛装液化天然气的至少一个储存容器的汽化气体的装置，其包括与所述储存容器连通的第一冷压缩级；用于进一步压缩冷压缩级的下游的汽化气体的多个串联的其它压缩级；和用于再液化汽化气体的其它压缩级的下游的液化器，其中有具有至少一个热交换通道的热交换器，所述热交换通道具有与第一冷压缩级的出口连通的入口和与其它压缩级连通的出口；和与所述第一热交换通道处于热交换关系中的至少一个第二热交换通道，所述第二热交换通道具有与其它压缩级连通的入口和与液化器连通的出口。
热交换器的位置避免了压缩级上游的压降。第一压缩级作为冷压缩级的操作使得可被液化的进一步压缩的汽化气体的所有或一部分在其液化上游可能被预冷却至低于0℃。因此，没有必要包括在第一压缩级上游的任何热交换器(或其它装置)以便加热汽化天然气，该热交换器将引起不希望的压降。
一般而言，根据本发明的方法和装置能够被调适以满足针对供应天然气和宽范围的不同供应压力的很多不同需求。
根据本发明的方法和装置特别地，但不排他地旨在用于船上或其它航海船只上。如果航海船只是LNG从生产现场到使用现场的运输机构，那么基本上所有的汽化气体可被再液化。然而，在一些情况下，一些天然气用于航海船只上以发电，例如，用于航海船只本身的推进。在这种情况下，进一步压缩的汽化气体的仅一些需要被再液化且其的其余部分被供应用于发电的目的。
在进一步实例中，用于发电的天然气取自所述储存容器并被泵送到合适压力。在这样的实例中，所有的汽化气体可被再液化，而返回到所述储存容器的一些被可采取用于发电。此外，在这些实例中，可从泵送的天然气中恢复制冷并且被用来提供对待液化的进一步压缩的汽化气体的流的进一步温度降低。
经受温度降低的天然气的进一步压缩的流的部分(或该部分的所选部分)的再液化优选通过布雷登(Brayton)循环的方式实现。氮优选是布雷登循环中的工作流体。
现在将参考附图通过举例的方式来描述根据本发明的方法和装置，在附图中：
图1至图4是其中仅通常示出的用于液化器的制冷循环的根据本发明的不同天然气供应设备的广义示意流程图，且图5和图6是其中更详细地示出制冷循环的这些设备的示意流程图。
附图中的类似部件由相同参考数字指示。
参考图1，其示出LNG储存罐或容器的组2。储存罐位于航海LNG船只上。五个基本相同的储存罐4、6、8、10和12示于图1中。虽然示出了五个储存罐，但是组2可包括任何数量的这样的储存罐。LNG储存罐4、6、8、10和12中的每个隔热，以便控制其内容物(LNG)从周围环境吸收热量的速率。储存罐4、6、8、10和12中的每个在图1中被示为包含LNG的容积14。自然地，在这些罐中的每个中具有高于其中的液体水平的液面上方空间16。由于天然气在远低于-100℃的温度下沸腾，所以LNG从其上部的液面上方空间16的每个容积14连续蒸发。根据本发明，蒸发的LNG从罐4、6、8、10和12取回且处于至少部分被液化的正常操作。因此，罐4、6、8、10和12中的每个都具有汽化蒸汽的出口18。出口18都与汽化蒸汽的管线20连通。
管线20与多级压缩器24连通。如图1所示，压缩器24具有四个压缩级26、28、30和32，其将天然气逐渐推进到越来越高的压力。不是必须使用刚好四个这样的压缩级。最佳数量的压缩级将取决于需要压缩器24供应天然气的压力以及压缩器24在操作时遇到的入口温度的变化。一般而言，所需的供应压力越高，可能需要更多压缩级。类似地，最大入口温度越高，可能需要更多压缩级。
由于来自储存罐4、6、8、10和12的组2的汽化天然气的速率随环境温度和航海条件的变化波动，所以用于补偿这种变化的装置设置在如图1所示的装置中。补偿装置包括提供用于每个压缩级或一些压缩级的入口导向叶片(未示出)或可变的扩散器叶片(未示出)。此外，还有在最后压缩级32下游的再循环管线36和位于该再循环管线36中的流量控制阀38。再循环管线36为压缩器24提供防喘振控制，其中阀38在必要时打开。或者，每个级或每对级可具有单独的防喘振系统。
根据本发明，第一压缩级26作为具有远低于环境温度的入口温度的冷压缩级而操作。另一方面，剩余压缩级28、30和32中的压缩热量足以将其中的温度升高至远高于环境温度。因此，冷却器25、27和29分别设置在压缩级28、30和32的下游。冷却器25、27和29中的每个都通常采用水的流动来实现冷却并可采取任何常规类型的热交换器的形式。冷却器25和27两者都是级间冷却器，即冷却器25位于压缩级28和30中间且冷却器27位于压缩级30和32中间。冷却器29是后冷却器，其位于最后压缩级32的下游的于压缩级32的出口和再循环管线36与主天然气供应管线40的联合体的中间的位置处，压缩器24将压缩天然气供应到主天然气供应管线40。根据需要，压缩器24可包括具有中间冷却器的附加级。
如图1中所示，一些天然气流至管线40的端部，通常用于供应到发动机或用于做功的其它机器(未示出)且天然气的其余部分流到管线42，管线42的入口位于后冷却器29和再循环管线36与主供应管线40的联合体的中间。
被供应到管线42的压缩天然气的至少一部分被发送到液化器47。根据本发明，流过管线42的天然气在其液化的上游被预冷却。通过与从压缩器24的第一(冷压缩)级26流到其第二压缩级28的天然气的逆流热交换而在热交换器22中实现预冷却。沿管线42流出热交换器22的所得到的天然气流穿过液化器47，天然气流在液化器47中被液化。管道64从管线42分支并终止于主要气体供应管线40。流量控制阀44被定位在其与管道64的联合体的上游的管线40中。类似的流量控制阀62位于管道64中。
在正常操作中，期望在近似恒定速率的速率下将天然气供应到航海船只的推进系统(未示出)(其可包括双燃料发动机)。该速率可被设置或通过双燃料发动机(未示出)前面的气体阀单元(未示出)的操作来调节。管线40中的阀门44和管道64中的阀门62用于改变穿过热交换器22的受压天然气的比例以便调节汽化的蒸气温度，以便调节流过其中的蒸汽的温度。液化器47可包括第二热交换器(或热交换器48的阵列)，在其中它通过与流过制冷循环50(优选布雷登循环)的工作流体的间接热交换而被冷凝。所得冷凝物通常经由管线52而被返回到储存罐4、6、8、10和12，用于调节待液化的汽化气体的速率的流量控制阀54位于管线52中。
因为依赖于流量控制阀44和62的设置，所以主供应管线40中的压缩天然气流可具有零度以下的温度，加热器60优选设置在管线40中。加热器60可通过与蒸汽或其它加热介质进行热交换而加热天然气。
还设想，本发明可供应其它消耗品，包括但不限于：2冲程或4冲程双或三燃料发动机、用于机械蒸汽或发电的燃气涡轮机或锅炉。典型的压力范围对于蒸汽设备可以是0巴到3巴、对于双燃料4-冲程发动机是0巴至7巴、对于双燃料2-冲程发动机是130巴至320巴，且对于燃气涡轮机设备是20巴至50巴。
对于图1所示的设备有大量替代选项，所有替代选项都采用汽化天然气在第一压缩级26中的冷压缩来为待液化的压缩天然气提供冷却，冷却设置在热交换器22中。
图2示出适于在对用于船或其它航海船只的发电或推进的天然气没有需求时使用的设备。在这样的实例中，船的发动机可专门采用燃料油(例如，HFO、MDO、MGO)作为它们的燃料。因此，与图1相比，现在没有主要气体供应管线40且除了管线36中的防喘振流量，来自压缩器24的所有天然气都被发送通过换热器22并且在液化器47中被液化。
在图3所示的设备中，天然气被取出以用于船的推进的目的，但在这种情况下，天然气从罐4、6、8、10和12中以液体状态被取出。因此，至少两个罐被设置有经浸没的低压泵300。每个泵300都连接到主LNG管线302中，高压LNG泵304位于主LNG管线302中。如果发电装置(即船的发动机)需要高燃料气体检查压力，则泵304可包括可安装的泵送级并且可使压力升高到通常在20巴至50巴或200巴至300巴的范围内的值。因为用于船的推进的目的的天然气从组2中被取出，所以无需管线40且类似地无需图2中所示的布置，在压缩器24中被压缩的基本上所有的天然气都返回通过热交换器22以在液化器47中进行液化。如果需要，这种液体中的一部分或全部可不返回到罐4、6、8、10和12，而是经由流量控制阀306到达高压泵304上游的管线302。
图4示出对图3中所示的设备的改进，其使得采用用于船只的发电的LNG中的一些制冷以进一步冷却其在液化器47中的液化的上游的压缩天然气。因此，来自热交换器22的天然气被发送到位于液化器47上游的管线42的一个或多个其它预冷却热交换器400。现在，高压泵304的下游的管线302延伸通过热交换器400。预冷却热交换器400由制冷循环50(或由附加的制冷循环)和来自泵304的高压LNG两者来制冷。其结果是，来自泵304的高压LNG进一步预冷却来自热交换器22的天然气。
加热器500设置在热交换器400下游的管线302。此外，管道510被提供以使来自泵304的一些高压天然气根据位于管道510和302中的流量控制阀512的位置而绕过热交换器400。来自加热器500的高压天然气可用于供应到在船上的发动机(未示出)或气体涡轮机(未示出)。
对于用于冷却图1至图4中所示的设备中的热交换阵列48的制冷循环具有多种不同选择。这些选择中的一个被示于图5中，其基于其中没有加压的LNG从储存容器被取出来补充汽化气体的设备。设备因此与图1中所示的设备具有许多相似之处。
参考图5，布雷登循环用于冷却热交换器48。循环中的最低压力下的工作流体(优选氮)在压缩/膨胀机70(有时被称为“扩张器”)(其具有串联的三个压缩级72、74和76，和在压缩级76的下游的单一涡轮膨胀器78)的第一压缩级72的入口处被接收。压缩级72、74和76都在操作上与相同驱动机构(未示出)相关联。在操作中，氮工作流体依次流过压缩膨胀器70的压缩级72、74和76。在级72和74的中间，工作流体在第一级间冷却器74中被冷却到近似环境温度；且在压缩级74和76的中间，压缩的氮在第二级间冷却器86中被冷却。离开最后压缩级76的压缩氮在后冷却器88中被冷却。冷却器84、86和88的水可从航海船只本身的清洁水回路(未示出)中提供。
在后冷却器88的下游，压缩的氮流过热交换器90，在热交换器90中，氮与返回的氮气流进行间接热交换而被进一步冷却。所得到的压缩、冷却的氮气流流到涡轮膨胀器78，在涡轮膨胀器78中氮气流随外部工作的性能而膨胀。可提供外功作为在压缩级72、74和76中压缩氮所需要的必要能量的一部分。氮工作流体的膨胀具有进一步降低其温度的影响。其结果是，氮工作流体处于适合于天然气在冷凝热交换器中由间接逆流热交换进行冷凝的温度下。氮工作流体(现在由于其与冷凝天然气蒸气的热交换而被加热)流过预冷却热交换器92(除了热交换器22之外)，在该预冷却热交换器92中，氮工作流体预冷却在其进入冷凝热交换器48的入口的上游的天然气。其结果是，氮工作流体被进一步加热。该氮气流形成返回氮气流以在热交换器90中对压缩氮进一步冷却。所得氮气流在压缩-膨胀机70的第一压缩级72中被最终接收，从而完成回路。
现在参考图6，示出图4中所示的设备的制冷循环，在该设备中汽化气体被补充有从LNG储存容器取回的加压LNG。在图6中所示的设备的实例中，在泵304中产生的高压LNG与制冷循环中的氮保持分离。如果高压LNG要与热交换器400中的氮热交换，则由于这两个燃料流(氮处于小于15巴(a)的最大压力下，LNG处于大于20巴(a)且高达300巴(a)的压力下)之间的典型压力差而具有天然气进入氮的风险。通过以压缩天然气独立地恢复高压LNG的冷却，由于两种流体的组成主要是甲烷而不存在相关的安全或污染的风险。
在图1至图5所示的设备的正常操作中，汽化天然气压缩器24通常具有在6巴至8巴范围内的出口压力。当例如在从天然气开采现场到LNG分配现场的向外航程中储存罐4、6、8、10和12的组2充满了例如LNG时，压缩的汽化天然气体在低压发动机的情况下沿管线40被供应到航海船只的推进系统。然而，汽化的速率通常超过压缩天然气所需的速率。因此多余的天然气在热交换器50中被液化并返回到储存罐4、6、8、10和12的组2。因此避免了在气体燃烧单元(GCU)中浪费地燃烧多余的天然气的任何需要。如果需要，在返回航程期间，制冷循环可能无法操作且因此不对任何汽化天然气进行再液化。此外，在返回航程中，管线20中天然气的温度趋于比罐4、6、8、10和12被完全充满LNG时的温度高得多。入口温度在这些情况下通常常见的是高于-50℃。通过流量控制阀44和62的适当设置，进入压缩器24的天然气的温度可被设置为与负载航行期间相同的预选值。
在正常负载操作中，热交换器22中的压缩天然气的冷却减少了在液化天然气中由制冷循环50完成所需的功的量。因此，根据本发明的方法和装置使得有可能控制附图中所示的压缩液化系统的总功耗。

Claims (11)

1.一种回收从盛装液化天然气（LNG）的至少一个储存容器(4,6,8,10,12)放出的汽化气体的方法，其包括：
- 使所述汽化气体的流在第一压缩级(26)中冷压缩，
- 通过热交换器(22)中的热交换来加热被冷压缩的汽化气体的流，
- 进一步压缩被冷压缩的汽化气体的加热流，和采用所述汽化气体的被进一步压缩的流的至少一部分以在所述热交换中加热所述被冷压缩的汽化气体的流并因此降低被进一步压缩的汽化气体的所述部分的温度，以及
- 在液化器(47)中使经受温度降低的所述汽化气体的被进一步压缩的流的所述部分的至少一部分再液化，
其特征在于，该方法还包括：
- 将所述汽化气体的被进一步压缩的流的另一部分供应给气体供应管线(40)，以及
- 通过作用于第一控制阀(62)并且通过作用于第二控制阀(44)来对经受温度降低的所述被进一步压缩的汽化气体的比例进行控制，所述第一控制阀(62)位于管道(64)中，所述管道(64)从始自所述热交换器(22)至所述液化器(47)的管线(42)分支至用于发动机的所述气体供应管线(40)，所述第二控制阀(44)被定位在其与所述管道(64)的联合体的上游的所述气体供应管线(40)中。
2.根据权利要求1所述的方法，其中用于再液化的制冷由布雷登循环提供。
3.根据权利要求2所述的方法，其中所述布雷登循环还提供对待再液化的所述汽化气体的所述进一步压缩的流的预冷却。
4.根据权利要求2所述的方法，其中用于再液化的附加制冷由从所述储存容器取出的天然气的高压流提供。
5.根据前述权利要求1至4中任一项所述的方法，其中，所述方法是在船上操作的。
6.根据前述权利要求1至4中任一项所述的方法，其中所述第一压缩级的出口温度低于-5℃。
7.一种用于回收来自盛装液化天然气的至少一个储存容器(4,6,8,10,12)的汽化气体的装置，其包括：
- 与所述储存容器(4,6,8,10,12)连通的第一冷压缩级(26)；
- 多个其它压缩级(28,30,32)，它们串联用于进一步压缩所述冷压缩级的下游的所述汽化气体进入到气体供应管线(40)，和
- 液化器(47)，其在所述其它压缩级(28,30,32)的下游用于再液化所述汽化气体，
其中有具有至少一个热交换通道的热交换器(22)，所述热交换通道具有与所述第一冷压缩级(26)的出口连通的入口和与所述其它压缩级(28,30,32)连通的出口；和与所述热交换通道处于热交换关系中的至少一个第二热交换通道，所述第二热交换通道具有与所述其它压缩级(28,30,32)连通的入口和与所述液化器(47)连通的出口，
其特征在于，它还包括：
- 第一控制阀(62)，其位于管道(64)中，所述管道(64)从始自所述热交换器(22)至所述液化器(47)的管线(42)分支至用于发动机的所述气体供应管线(40)，以及
- 第二控制阀(44)，其被定位在其与所述管道(64)的联合体的上游的所述气体供应管线(40)中。
8.根据权利要求7所述的装置，其中所述液化器适于以布雷登循环操作。
9.根据权利要求7所述的装置，其中所述装置在航海船只上。
10.根据权利要求8所述的装置，其中所述装置在航海船只上。
11.根据权利要求7至10中任一项所述的装置，其还包括用于加压从所述储存容器取回的液化天然气（LNG）的至少一个泵，和用于预冷却待液化的压缩天然气的附加热交换器，所述附加热交换器具有与所述泵连通的一个或多个预冷却通道。
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