CN101495828B - 蒸汽再液化的方法和设备 - Google Patents

蒸汽再液化的方法和设备 Download PDF

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CN101495828B
CN101495828B CN2007800184802A CN200780018480A CN101495828B CN 101495828 B CN101495828 B CN 101495828B CN 2007800184802 A CN2007800184802 A CN 2007800184802A CN 200780018480 A CN200780018480 A CN 200780018480A CN 101495828 B CN101495828 B CN 101495828B
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working fluid
heat exchanger
natural gas
condenser
steam
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CN101495828A (zh
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V·富克斯
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Cryostar SAS
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Cryostar SAS
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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
    • F25J1/0025—Boil-off gases "BOG" from storages
    • 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
    • F25J1/02—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
    • F25J1/0203—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
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
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    • F17C9/00—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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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
    • F25J1/003—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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    • F25J1/003—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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    • F25J1/0208—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 in combination with an internal quasi-closed refrigeration loop, e.g. with deep flash recycle loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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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
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • 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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    • 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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    • F25J1/02—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
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0275—Construction and layout of liquefaction equipments, e.g. valves, machines adapted for special use of the liquefaction unit, e.g. portable or transportable devices
    • F25J1/0277—Offshore use, e.g. during shipping
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    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0285—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings
    • F25J1/0288—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings using work extraction by mechanical coupling of compression and expansion of the refrigerant, so-called companders
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    • F17C2223/01—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the phase
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    • F25J2230/08—Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler
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    • F25J2230/60—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being hydrocarbons or a mixture of hydrocarbons
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    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Ocean & Marine Engineering (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

蒸发汽化的液化天然气从例如储存罐10流出，并在蒸汽压缩级40和42中压缩。由此产生的压缩蒸汽在冷凝器46中冷凝，冷凝物返回到罐10。冷凝器46通过在布雷顿循环60中流动的例如氮的工作流体冷却。布雷顿循环包括热交换器86，热交换器86将来自其通过冷凝器46的通道上游的压缩天然气蒸汽的压缩热排除。另外，一部分工作流体从来自于冷凝器46的工作流体出口和去往热交换器86的工作流体入口中间的布雷顿循环60区域收回，收回的工作流体流过另一个热交换器88，在热交换器88中，其将来自在压缩级40和压缩级42之间的天然气蒸汽的压缩热排除。收回的工作流体返回到布雷顿循环60。

Description

蒸汽再液化的方法和设备
技术领域
本发明涉及蒸汽再液化的方法和设备，特别是船舶上可操作的再液化天然气蒸汽的方法和设备。
背景技术
通常，天然气以液化状态运输很远距离。例如，远洋油轮用于将液化天然气从天然气被液化的第一场所运送到其被汽化并被送到气体分配系统的第二场所。由于天然气在低温，即低于-100℃的温度下被液化，在任何实际的储存系统中液化天然气将持续蒸发汽化。因此，需要提供设备以便再液化蒸发汽化的蒸汽。在这样的设备中执行制冷循环，包括在多个压缩机中压缩工作流体，通过间接热交换冷却压缩的工作流体，膨胀工作流体，以及加热与压缩的工作流体进行间接热交换的膨胀的工作流体，以及使加热的工作流体返回到压缩机中的一个。压缩级下游的天然气蒸汽，与被加热的工作流体进行间接热交换而被至少部分冷凝。用于执行这样的制冷方法的设备的一个例子是美国专利3857245中公开的。
根据美国专利3857245，工作流体来自天然气自身，因此运行开放的制冷循环。工作流体的膨胀由阀执行。得到部分冷凝的天然气。部分冷凝的天然气分成返回储罐的液相和与被送到燃烧器燃烧的天然气混合的汽相。工作流体在同一热交换器中既被加热又被冷却，因此只需要一个热交换器。热交换器位于第一滑动安装平台上，工作流体压缩机位于第二滑动安装平台上。
现在，优选使用不燃气体作为工作流体。进一步地，为了降低需要被外部提供的压缩功，优选使用膨胀涡轮，而非阀来膨胀工作流体。
设备的一个例子体现为WO-A-98/43029给出的两个改进。现在使用两个热交换器，一个与要被部分冷凝的压缩天然气蒸汽进行热交换来加热工作流体，另一个冷却压缩的工作流体。
WO-A-98/43029指出，天然气蒸汽的不完全冷凝降低了制冷循环中消耗的能量(与完全冷凝相比)，并提出残留的蒸汽-其相对富含氮-将被排放到大气。实际上，WO-A-98/43029中披露的部分冷凝遵循公知的热力学定律，其指出冷凝率(condensate yield)完全是冷凝发生时压力和温度的函数。
典型地，液化天然气可以在稍高于大气压力的压力下储存，蒸发汽化的蒸汽可以在4bar的压力下部分冷凝。由此产生的部分冷凝混合物典型地闪过(flashed)膨胀阀进入分相器，从而使蒸汽能够在大气压下排出。即使进入膨胀阀的液相在4bar下包括达到10摩尔百分数的氮，由此产生的汽相在1bar下仍包括大约50％体积的甲烷。因此，在典型的运行中，每天可能需要从分相器排出大约3000到5000kg的甲烷。由于甲烷被认为是导致温室效应的气体，这种实际情况在环保上是不能接受的。
另一个与根据WO-A-98/43029设备的运行有关的问题是，存在由一方面是压缩天然气的温度和焓，以及另一方面是工作流体的温度和焓之间的不匹配引起的可观的热力学无效。
EP-A-1132698披露了一种方法，其减轻当蒸汽带着冷凝天然气返回到液化天然气(LNG)储存罐时引起的问题。
在根据EP-A-1132698的方法中，蒸发汽化的蒸汽和/或天然气冷凝物与来自储罐的液化天然气混合。
由于氮气在液化天然气中的摩尔分数少于氮气在蒸发汽化的蒸汽中的摩尔分数，甚至也少于通过冷凝的蒸发汽化的蒸汽的阀而膨胀形成的闪蒸气体，带有冷凝器上游或下游或二者的液化天然气的蒸发汽化的蒸汽的稀释，倾向于抑制在储存罐中汽相的成分中的波动，否则会没有蒸发汽化的蒸汽或天然气冷凝物与来自储罐的液化天然气的混合的发生。
但是，根据EP-A-1132698的方法没有显著提高整体热力学效率。
发明内容
根据本发明，提供一种用于再液化从至少一个储存罐中储存的至少一个体积的液化天然气中蒸发汽化的蒸汽的方法，包括：压缩在串联的第一和第二蒸汽压缩级中的蒸汽，在冷凝器中通过与在主环形工作流体循环中流动的工作流体进行热交换来冷凝压缩的蒸汽，使至少一些由此产生的冷凝物返回到所述储存罐，其中在主环形工作流体循环中，工作流体依次地，在至少一个工作流体压缩机中被压缩，在第一热交换器中被冷却，在膨胀涡轮中膨胀，在冷凝器中用于执行天然气蒸汽的冷凝，在所述第一热交换器中与被冷却的压缩工作流体进行热交换而被加热，并返回到所述工作流体压缩机中，其特征在于，在主工作流体循环中，在通过冷凝器的工作流体的通道和通过第一热交换器的通道的中间，工作流体在第二热交换器中使用在第二蒸汽压缩级下游、也是冷凝器上游的压缩天然气蒸汽预冷；工作流体的流动从主工作流体循环区域转向，在主工作流体循环区域处工作流体从冷凝器流到第二热交换器，并通过至少一个第三热交换器，从而冷却第一和第二蒸汽压缩级中间的天然气蒸汽，在工作流体从第二热交换器流到第一热交换器的区域，转向的工作流体返回到主工作流体循环。
本发明还提供用于再液化天然气蒸汽的设备，包括至少一个储存罐，用于储存至少一个体积的液化天然气，串连的第一和第二蒸汽压缩级，用于压缩与所述储存罐中的至少一个蒸汽空间相连通的蒸发汽化的天然气蒸汽，用于冷凝压缩蒸汽的冷凝器，冷凝器具有与第二蒸汽压缩级相连通的天然气入口和与所述储存罐相连通的出口，其中冷凝器设置成在使用中被工作流体冷却，形成部分环形主工作流体循环的冷凝器，主工作流体循环依次包括：(a)至少一个工作流体压缩机，用于压缩工作流体流，(b)通过第一热交换器的冷却路径，用于冷却工作流体流，(c)膨胀涡轮，用于膨胀工作流体流，(d)冷凝器，(e)通过第一热交换器的加热路径，用于加热工作流体，和(f)去往所述工作流体压缩机的入口，其特征在于，主工作流体循环包括第二热交换器，用于与工作流体进行热交换来冷却天然气，第二热交换器具有第二蒸汽压缩级和冷凝器中间的天然气蒸汽路径，以及来自于冷凝器的工作流体出口和去往通过第一热交换器的加热路径入口中间的工作流体路径；且具有第三热交换器，用于与从主工作流体循环转向的工作流体进行热交换来冷却第一和第二天然气蒸汽压缩级中间的天然气蒸汽，第三热交换器具有工作流体路径，由此在其入口连通来自于冷凝器的工作流体出口和去往第二热交换器的工作流体入口中间的工作流体循环区域，在其出口连通来自于第二热交换器的工作流体出口和去往通过第一热交换器的加热路径入口之间的工作流体循环区域。
相比于上述的在先文献披露的相应方法和设备，根据本发明的方法和设备能够获得运行的改善的热力学效率。我们把改善的热力学效率归因于不仅在冷凝器中还在第二和第三热交换器中的工作流体循环和天然气冷凝的整合。热力学效率的改善可以依靠减少的能量消耗被利用。
优选地，响应去往第二蒸汽压缩级的入口的温度，从主工作流体循环转向到第三热交换器的工作流体的比例被控制。
优选地，当所述储存罐完全装满液化天然气时，这样运行冷凝器以使过冷的液化天然气从其中离开。但是，有时，当所述储存罐只包括相对少量的液化天然气，冷凝物返回到储罐具有使蒸发汽化的蒸汽富含氮的作用。由此，出现在冷凝器用于冷凝的蒸汽可能包含过量的氮，并且因此冷凝物不但不过冷，而且其甚至不完全冷凝。在这样的情况下，或者，如果储存罐包含具有高氮含量的液化天然气，例如，提供包含20-40％体积的氮的蒸发汽化气体，包含不冷凝蒸汽的冷凝物闪入分相器，由此得到的液相返回到储存罐，且由此得到的汽相被送到船舶发动机(在船舶使用中如果发动机由天然气供给动力的情况下)或者燃烧并排放到大气中。
第一和第二蒸汽压缩级优选由单独的多速度马达驱动。
优选地，第一蒸汽压缩级上游的蒸汽，通过与来自冷凝器的冷凝天然气流混合被预冷。优选地，响应去往第一压缩级的入口的温度，冷凝的天然气蒸汽流的流速被控制。
附图说明
现在，根据本发明的方法和设备将通过参考附图的实施例进行描述，其中：
图1是液化天然气(LNG)储罐的船用装置的示意性流程图。
具体实施方式
附图不是按比例绘制的。
参考附图，在海船或其它远洋船舶的船体(未示出)中提供五个绝热的储存罐2、4、6、8和10。储存罐2、4、6、8和10中的两个或更多个设有位于其底部区域的潜孔口管12，LNG通过潜孔口管12被导入。因为附图的简易，储罐2、4和6中的孔口管在图中未示出。如果只有一些储存罐设有潜孔口管，返回的LNG到未被如此提供的罐的重新分配是通过液泵(未示出)的运行。在常规运行中，孔口管12浸没在LNG的容积16中。在每个罐2、4、6、8和10中，在LNG的容积16之上具有蒸汽空间18。
虽然储存罐2、4、6、8和10是绝热的，但因为LNG在常压下的沸点大大低于环境温度，所以在每个储存罐2、4、6、8和10中LNG持续地蒸发。每个罐具有用于蒸汽的顶部出口22，其与蒸发汽化气体集管24相连通。从集管24伸出来的是用于蒸发汽化气体的主管道26。位于管道26中的是混合器28，其中，在运行中，蒸汽可以与来自装置下游部分的冷凝LNG混合。在运行中，冷凝的LNG在蒸发汽化的气体中蒸发，并由此降低该气体的温度。传感器27被提供在混合器下游，并产生代表去往第一压缩级40的入口处的温度的信号，该信号传递到阀控制器30，其反过来控制在LNG冷凝管道34中的流控制阀32的调节，LNG冷凝管道34在混合器28内的喷雾嘴36中终止。因而，可以运行混合器28从而在选择的实质恒定的低温，例如低于负100℃，向第一压缩级40提供天然气。
蒸发汽化的气体从混合器28流进第一压缩级。第一压缩级40的出口与第二压缩级42的入口间接连通。压缩级40和42典型地由单一马达44驱动，如果需要通过整体齿轮箱45驱动。
马达44典型地可以在两个不同速度下运行。
由此得到的压缩气体从第二压缩级42提供到冷凝器46，冷凝器46典型地是板翅式或螺旋缠绕式热交换器，在其中，压缩气体被冷凝并一次冷凝到过冷。由此得到的过冷冷凝物从冷凝器46沿着管道48流到冷凝返回集管50，集管50向在罐8和10底部区域中的孔口管12供给，或者，如果每个罐安装有孔口管12，则向罐2、4、6、8和10供给。
由在实质封闭的制冷循环60中，例如布雷顿循环，以第一压力流动的工作或热交换流体，例如氮，提供用于冷凝器46的冷却。
在布雷顿循环60中，通过冷凝器46的氮，在气-气热交换器62中高于第一压力的第二压力下，与返回的压缩氮进行热交换而被加热。由此得到的加热氮流到压缩机64，压缩机64典型地包括三个压缩级66、68和70，它们均具有安装在整体齿轮箱(未示出)上或同一轴72上的转子(未示出)，能够由发动机74通过齿轮箱75驱动。第一中间冷却器78设置在来自于第一压缩级66的出口的下游和去往第二压缩级68的入口的上游。第二中间冷却器80设置在来自于第二压缩级68的出口的下游和去往第三压缩级70的入口的上游。后冷却器82设置在来自于第三压缩级70的出口的下游。中间冷却器78和80以及后冷却器82典型地被水冷却，并运行从而从在布雷顿循环运行中的循环氮中移除压缩热。得到的后冷却压缩氮作为在前提到的返回的冷氮流流过热交换器63。由此，压缩氮流在热交换器62中被冷却到较低温度。压缩的冷却氮流通到膨胀涡轮84，在此处随额外功的工作被膨胀。膨胀涡轮84典型地安装在同一整体齿轮箱(未示出)上或同一轴上，与压缩级66、68和70一样。因此，膨胀涡轮84帮助驱动压缩级66、68和70。在涡轮84中，氮的膨胀产生在冷凝器46中天然气蒸汽的冷凝需要的制冷。由此，氮持续地通过环形回路。
在附图中描述的布雷顿循环60的特殊特征是，氮不直接通过从冷凝器46到达热交换器62。而是通过第二气-气逆流热交换器86。该热交换器的目的是在进入冷凝器46的上游，预冷天然气到接近其冷凝温度的温度。从而，在典型的运行环境中，当罐2、4、6、8和10完全装满LNG时，在冷凝器46中天然气不仅液化而且过冷。当LNG返回到罐时，液化天然气的过冷阻止了闪蒸气体的形成。
图中显示的布雷顿循环6的特殊形式的进一步特征是，一部份氮从布雷顿循环在来自于冷凝器46的出口的下游、去往第二热交换器86的入口的上游的区域退回，并流过位于第一天然气压缩级40的下游、第二天然气压缩级42的上游的第三热交换器88，从而用于将由第一压缩级40的运行在天然气产生的压缩热排除。作为结果，通过第三热交换器88的氮被加热。加热的氮流在来自于第二热交换器86的出口的下游区域、去往通过第一热交换器62的加热通道的入口的上游返回到布雷顿循环60。典型地，控制阀90响应于去往第二天然气压缩级42的入口的温度传感器(未示出)，控制通过第三热交换器的氮工作流体的流速。在典型的布置中，操作控制阀90以维持去往第二天然气压缩级42的入口的恒定的温度。
在冷凝器46中，不是所有天然气都被液化，其典型地通过管道50返回罐2、4、6、8和10。一部份冷凝物通过管道34被送到混合器28，从而预冷第一压缩级40上游的天然气。
在运行中，根据如何在罐2、4、6、8和10中装载LNG，用不同方法运行图中显示的设备。当这些罐完全装满时，去往第一天然气压缩级40的入口的温度典型地为大约负100℃或甚至更低。入口的压力典型地稍高于1bar。天然气典型地在大约2bar压力、大约负65℃温度下离开第一压缩级。气体典型地在热交换器中被冷却到大约负130℃的温度，并在该温度下进入第二天然气压缩级。天然气典型地在大约5bar压力、大约负75℃温度下离开第二压缩级42。天然气在第二热交换器中被冷却到其将要开始冷凝的温度。该温度的精确值取决于天然气的成份。在天然气中氮的摩尔分数越大，开始冷凝的温度越低。因为在常规运行中，冷凝器46不需要使天然气过热后冷却，所以热交换可能比先前已知的循环更有效率，在已知循环中，相应的冷凝器需要同时使天然气过热后冷却和冷凝。作为中间冷却、过热后和带有过冷的分离冷凝的结果，制冷循环的能量消耗被降低。
如前所述，天然气作为过冷液体离开冷凝器46。典型地，取决于天然气的成份，其离开温度为大约负165℃。如此低的离开温度的一个优点是，在LNG通过孔口管12再引导进入罐2、4、6、8和10中时，即便有也是相对很少的闪蒸气体形成。此外，当罐完全装满时，形成的任何闪蒸气体在其到达表面之前，可以在液体中溶解或冷凝。
在常规运行中，当罐完全装满时，膨胀涡轮84典型地具有大约负104℃的入口温度，大约负168℃的出口温度，大约10bar的出口压力。如果天然气的成份是，例如，8.5％体积的氮和91.5％体积的甲烷，对于冷凝器46中产生的冷凝物，该温度足够低，从而具有过冷所需要的程度。但是，有时，在其中设置有罐2、4、6、8和10的船需要运送用于罐中液压头的足够的少于最大量的LNG，其不足以阻止通过孔口管12返回的冷凝物的闪蒸，或保证在LNG的容积16中形成的闪蒸气体的细小泡沫全部溶解。结果，从罐2、4、6、8和10流到第一压缩级40的蒸汽富含氮。因而，其在第二天然气蒸汽压缩级42出口压力下的冷凝温度下降。实际上，当罐相对较少地装载LNG时，富含程度可能变得如此大，以至于冷凝器46不再完全冷凝蒸汽。在这种情况下，冷凝物和不冷凝蒸汽的混合物可能有选择性地通过阀100被导向进入分相器102，而不是通到管道50。液体从分相器102底部退回，并送到管道50。蒸汽从分相器102通到排放管线104，排放管线104通过集管106通向气体燃烧单元108，从而蒸汽的天然气含量可以燃烧，并且由此产生的燃烧气体被排放到大气中。
在图中显示的设备的运行中，天然气蒸汽的最小和最大流动可以在很大范围内改变。因此，典型优选地，使用两套第一和第二天然气压缩级40和42，两套装置彼此并联。因此，典型地，具有两个第三热交换器88彼此并联。使用一套还是两套设备，取决于罐2、4、6、8和10中的天然气的蒸发速度。同样地，可能有两套或者更多套氮压缩级66、68和70并联，以及两个或更多膨胀涡轮84并联。

Claims (11)

1.一种用于再液化从至少一个储存罐中储存的至少一个体积的液化天然气中蒸发汽化的蒸汽的方法，包括：在串联的第一和第二蒸汽压缩级中压缩蒸汽，在冷凝器中通过与在环形主工作流体循环中流动的工作流体进行热交换来冷凝压缩的蒸汽，使至少一些由此产生的冷凝物返回到所述储存罐，其中在工作流体循环中，工作流体依次地，在至少一个工作流体压缩机中被压缩，在第一热交换器中被冷却，在膨胀涡轮中膨胀，在冷凝器中用于执行天然气蒸汽的冷凝，在所述第一热交换器中与要被冷却的工作流体进行热交换而被加热，以及返回到所述工作流体压缩机中，其特征在于，在主工作流体循环中，在通过冷凝器的工作流体的通道和通过第一热交换器的通道的中间，工作流体在第二热交换器中使用在第二蒸汽压缩级下游、但是在所述冷凝器上游的压缩天然气蒸汽预冷；工作流体的流动从主工作流体循环区域转向，在主工作流体循环区域处工作流体从冷凝器流到第二热交换器，并通过至少一个第三热交换器，从而冷却第一和第二蒸汽压缩级中间的天然气蒸汽，在工作流体从第二热交换器流到第一热交换器的区域，转向的工作流体返回到主工作流体循环。
2.如权利要求1所述的方法，其特征在于，响应去往第二蒸汽压缩级的入口的温度，从主工作流体循环转向到第三热交换器的工作流体的比例被控制。
3.如权利要求1或2所述的方法，其特征在于，当所述储存罐完全装满液化天然气时，运行冷凝器以使过冷的液化天然气从其中离开。
4.如权利要求1或2所述的方法，其特征在于，第一蒸汽压缩级上游的蒸汽通过与来自冷凝器的冷凝天然气流混合被预冷。
5.如权利要求4所述的方法，其特征在于，响应去往第一压缩级的入口的温度，冷凝蒸汽流的流速被控制。
6.一种用于再液化天然气蒸汽的设备，包括至少一个储存罐，用于储存至少一个体积的液化天然气；串连的第一和第二蒸汽压缩级，用于压缩与所述储存罐中的至少一个蒸汽空间相连通的蒸发汽化的天然气蒸汽；用于冷凝压缩蒸汽的冷凝器，冷凝器具有与第二蒸汽压缩级相连通的天然气入口和与所述储存罐相连通的出口，其中冷凝器设置成在使用中被工作流体冷却，形成部分环形主工作流体循环的冷凝器，环形主工作流体循环依次包括：(a)至少一个工作流体压缩机，用于压缩工作流体流，(b)通过第一热交换器的冷却路径，用于冷却工作流体流，(c)膨胀涡轮，用于膨胀工作流体流，(d)冷凝器，(e)通过第一热交换器的加热路径，用于加热工作流体，和(f)去往所述工作流体压缩机的入口，其特征在于，主工作流体循环包括第二热交换器，用于与工作流体进行热交换来冷却天然气，第二热交换器具有第二蒸汽压缩级和冷凝器中间的天然气蒸汽路径，以及来自于冷凝器的工作流体出口和去往通过第一热交换器的加热路径的入口中间的工作流体路径；且具有第三热交换器，用于与从主工作流体循环转向的工作流体进行热交换来冷却第一和第二天然气蒸汽压缩级中间的天然气蒸汽，第三热交换器具有工作流体路径，由此在其入口连通来自于冷凝器的工作流体出口和去往第二热交换器的工作流体入口中间的工作流体循环区域，在其出口连通来自于第二热交换器的工作流体出口和去往通过第一热交换器的加热路径的入口之间的工作流体循环区域。
7.如权利要求6所述的设备，其特征在于，具有阀，用于响应去往第二蒸汽压缩级的入口的温度，控制从主工作流体循环转向到第三热交换器的工作流体的比例。
8.如权利要求6或7所述的设备，其特征在于，第一和第二蒸汽压缩级由单独的多速度马达驱动。
9.如权利要求6到7中任一项所述的设备，其特征在于，还包括第一蒸汽压缩级上游的混合器，在其中天然气蒸汽可以被冷却，混合器具有与冷凝器连通的冷凝天然气的入口。
10.如权利要求9所述的设备，其特征在于，包括阀，用于控制到混合器的冷凝物的流动，并可操作地维持去往第一压缩级的入口的温度恒定。
11.如权利要求6到7中任一项所述的设备，其特征在于，用于冷凝物离开冷凝器的出口可以选择性地通过膨胀阀以与分相器连通，分相器具有用于使液体返回到储存罐的出口和使蒸汽通到燃烧单元的出口。
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