CN1330761A - 液化天然气的设备 - Google Patents

液化天然气的设备 Download PDF

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CN1330761A
CN1330761A CN99814587A CN99814587A CN1330761A CN 1330761 A CN1330761 A CN 1330761A CN 99814587 A CN99814587 A CN 99814587A CN 99814587 A CN99814587 A CN 99814587A CN 1330761 A CN1330761 A CN 1330761A
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natural gas
heat exchanger
cooled
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equipment
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罗伯特·克莱恩纳格尔沃尔特
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Shell Internationale Research Maatschappij BV
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Abstract

液化天然气的设备,它具有一个带有天然气入口(13)和冷却的天然气出口(14)的预冷却热交换器(2)、一条预冷却的冷却剂环路(3)、一个具有一个与上述冷却的天然气出口(14)相连接的入口(18)并具有两个出口(22、23)的分配器(4)、两个主热交换器(5、5’)和两条分别与一个液化热交换器(5、5’)协作的主冷却剂环路(9,9’)。

Description

液化天然气的设备
本发明涉及使天然气液化的设备。该设备具有一个天然气预冷却热交换器和一个液化热交换器，前者设有天然气进口和已冷却的天然气的出口，后者的第一热区具有一个与冷却的天然气的一个出口相连接的入口和一个位于使天然气液化的液化热交换器之顶部的出口，上述设备还具有一个用于带走天然气预冷却热交换器中的天然气的热量的预冷却的冷却剂环路和一个用于带走流过主热交换器之第一热区的天然气中的热量的液化冷却剂环路。
在通常的作业中，待液化的天然气在天然气预冷却热交换器的热区内通过与冷区内蒸发的冷却剂的热交换而预冷却，已蒸发的冷却剂从热交换器的冷区排出，这种蒸发的冷却剂在预冷却的冷却剂环路中液化。为此，在压缩机内对上述冷却剂加压以提高其压力，而压缩热和蒸发热则在冷凝器中除去。液态的冷却剂可在膨胀装置内膨胀以降低压力，并在该压力下于天然气预冷却热交换器的冷区内蒸发。
随后，使预冷却的天然气在液化热交换器的第一热区内通过与在主热交换器的冷区内蒸发的冷却剂的热交换而进一步冷却、液化和过冷至大气下的沸点附近的温度。已蒸发的冷却剂从液化热交换器的冷区排出，再在主冷却剂环路内液化。为此，在压缩机内对上述冷却剂进行压缩以提高其压力，而压缩热则通过多个热交换器排除。然后使冷却剂冷凝并分成一种轻的气态馏分和一种重的液态馏分，这些馏分在液化热交换器的独立的热区内进一步冷却，而得到液化的过冷的高压馏分。然后使过冷的冷却剂在膨胀装置内膨胀，以降低其压力并在该压力下使冷却剂在主热交换器的冷区内蒸发。
上述设备通常称为单序列液化设备，这种设备的结构使得可液化的天然气的最大量实际上受限于在预冷却环路和主冷却剂环路中用于驱动压缩机的涡轮所能输出的最大功率。为了液化更多的天然气，建立了尺寸相同的第二序列液化设备。由上述两个序列组成的设备称为双序列液化设备。但是，该双序列液化设备的液化能力是单序列液化设备的两倍。由于并不总是需要上述这样大量地增加液化能力，所以只需要使液化能力增加约40％～60％则可。
要达到上述的只使液化能力增加约40％～60％的目的，可将双序列设备的产量下调到所需水平。另外，也可以采用两个其最大液化能力约为较大液化设备序列的70％～80％的较小序列来达到上述的目的。
本发明的目的是提供一种液化能力比较大的液化设备系列高40％～60％的液化天然气的设备，其中，建造这种设备的费用低于建造由两个最大液化能力分别约为较大序列设备的70％～80％的较小序列组成的相关设备的费用。
为达到本发明的上述目的，本发明提供了一种液化天然气的设备，具有一个带有天然气入口和冷却的天然气出口的天然气预冷却热交换器、一个带有一个与上述冷却的天然气出口相连接的入口并带有至少两个出口的分配器和至少两个各具有一个与分配器的一个入口相连接的第一热区和一个液化天然气出口的主热交换器，上述设备还具有一个用于带走天然气预冷却热交换器中的天然气的热量和预冷却的冷却剂环路和至少两个用于带走流过相应的主热交换器的第一热区的天然气中的热量的主冷却剂环路。
下面参看附图结合实例较详细说明本发明，附图中：
图1简单示出本发明的液化设备；
图2简单示出图1所示的另一条预冷却冷却剂环路；和
图3简单示出图2的实施例的另一个替代方案。
参看图1。本发明的液化天然气的设备具有一个天然气预冷却热交换器2、一条预冷却的冷却剂环路3、一个分配器4、两个主热交换器5和5’、和两条主冷却剂环路9和9’。
天然气预冷却热交换器2具有一个管状的带有一个天然气入口13和一个冷却的天然气出口14的热区12，该管状热区12设置在天然气预冷却热交换器2的冷区或者说管际空间15内。
分配器4具有一个通过管道19与出口14相连接的入口18和两个出口22和23。
每个液化热交换器5、5’具有一个分别带有一个入口26、26’的第一热区25、25’。第一热区25的入口26通过管道27与分配器4的出口22相连接，而第一热区25’的入口26’则通过管道27’与分配器4的出口23相连接。每个第一热区25、25’具有一个位于液化热交换器5、5’顶部的液化天然气出口28、28’。上述的第一热区25、25’设置在液化热交换器5、5’的带有出口30、30’的冷区29、29’内。
预冷却的冷却剂环路3具有一个由涡轮带动的具有入口33和出口34的预冷却冷却剂压缩机31。上述出口34通过管道35与冷却器(气冷却器或水冷却器)36相连接。管道35通过节流阀式的膨胀装置38延伸至天然气预冷却热交换器2的冷区15的入口39。而冷区15的出口40则通过返回管道41与涡轮带动的预冷却冷却剂压缩机31的入口33相连接。
预冷却的冷却剂环路3不仅预冷却天然气，而且还用来预冷却主冷却剂环路9和9’内的冷却剂。为此，预冷却环路3具有一条附加的环路43、43’。每条附加的环路43、43’具有一条含有节流阀式的膨胀装置45、45’的管道44、44’和一条返回管道46、46’。
每条液化冷却剂环路9、9’具有一个由燃气涡轮带动的具有入口51、51’和出口52、52’的液化冷却剂压缩机50、50’。上述的入口51、51’通过返回管道53、53’与液化热交换器5、5’的冷区29、29’的出口30、30’相连接，上述的出口52、52’通过管道54、54’与冷却器(气冷却器或水冷却器)56、56’相连接，而冷却剂热交换器58、58’的热区57、57’则与分离器60、60’相连接。每个分离器60、60’的下端有一个液体出口61、61’，在其上端则有一个气体出口62、62’。
每条液化冷却剂环路9、9’还包括一条从出口61、61’延伸到第二热区67、67’(该热区67、67’仅延伸至液化热交换器5、5’的中部)的入口的第一管道65、65’、一条管道69、69’、一个膨胀装置70、70’和一个喷嘴73、73’。
每条液化冷却剂环路9、9’还包括一条从出口62、62’延伸至第三热区77、77’(该第三热区延伸至液化热交换器5、5’的顶部)的入口的第二管道75、75’、一条管道79、79’、一个膨胀装置80、80’和一个喷嘴83、83’。
每个冷却剂热交换器58、58’具有一个纳入附设环路43、43’内的冷区85、85’。
主冷却剂环路9、9’最好是彼此相同的，并且，主热交换器5、5’最好也是彼此相同的。
在正常作业过程中，通过管道90将天然气供到天然气预冷却热交换器2的热区12的入口13处。预冷却的冷却剂从天然气预冷却热交换器2的冷区15的出口40排出，并在涡轮带动的预冷却冷却剂压缩机31内受到压缩，提高其压力，然后在冷凝器36内冷凝，并在膨胀装置38内膨胀，降低其压力，再在冷区15内使膨胀的预冷却的冷却剂在较低压力下蒸发，这样就带走了天然气中的热量。
从热区12排出的预冷却的天然气通过管道19进入分配器4。
通过管道27、27’将预冷却的天然气供入主热交换器5和5’的第一热区25和25’的入口26和26’。
在上述第一热区25、25’内，使天然气液化和过冷。过冷的天然气通过管道95和96排出。通过管道27、27’的天然气的量最好彼此相等。过冷的天然气通入一种可对它进行进一步处理的装置(未示出)并贮存到液化天然气罐(未示出)内。
主冷却剂从液化热交换器5、5’的冷区29、29’的出口30、30’排出，并在燃气涡轮带动的液化冷却剂压缩机50、50’内压缩到高压。压缩的热量在冷却器56、56’中散失。剩下的热量则由冷却剂热交换器58、58’内的主冷却剂带走而获得部分冷凝的冷却剂。上述部分冷凝的冷却剂再在分离器60、60’中分离成一种重的液态馏分和一种轻的气态组分，这两种馏分分别在第二热区67、67’和第三热区77、77’内进一步冷却，得到液化的过冷的高压馏分。然后使过冷的冷却剂分别在膨胀装置70、70’和80、80’内膨胀以降低其压力，再使该冷却剂在该压力下于液化热交换器5、5’的冷区29、29’内蒸发，以带走通过第一热区25、25’的天然气中的热量。
在上述的实施例中，预冷却的冷却剂最好是一种单组分冷却剂例如丙烷，或烃类组分的混合物或其他的适合于在压缩冷却循环中或吸收冷却循环中使用的冷却剂，上述的主冷却剂最好是一种含有氮、甲烷、乙烷、丙烷和丁烷的多组分冷却剂。
天然气预冷却热交换器2最好是一组两个或多个串联排列的热交换器，其中，预冷却冷却剂可在一个或多个压力值下蒸发。冷却剂热交换器58和58’最好是一组两个或多个串联排列的热交换器，其中，预冷却冷却剂可在一个或多个压力值下蒸发。
下面参看图2，该图简单示出图1所示的预冷却冷却剂环路3和附加环路43和43’的另一个实施例。将图1所示的天然气预冷却热交换器2和冷却剂热交换器58和58’综合成一个整体的热交换器102。该热交换器102具有一个内部设有正常作业时天然气流过的热区12的冷区115和分别附属于主冷却剂环路9和9’的热区57和57’。在本实施例中，预冷却的冷却剂最好是含有氮、甲烷、乙烷、丙烷和丁烷的多组分冷却剂。在正常作业过程中，蒸发的预冷却冷却剂通过管道41从冷区115排出，并由预冷却冷却剂压缩机31压缩，提高其压力，然后在冷却器36内冷却，并供入设置在整体热交换器102的冷区内的附加热区143中。在该附加热区143内，预冷却的冷却剂发生液化，而不蒸发。液化的冷却剂从附加热区143排出，流过带有节流阀式的膨胀装置146的管道145，在装置146内膨胀而降低压力。冷却剂在这一低压下通过喷嘴148供入冷区115。
下面参看示出图2实施例的另一替代方案的图3，其特征在于，预冷却冷却剂压缩机31是一种两级压缩机。该两级压缩机31将高压的冷却剂供入第一级整体预冷却热交换器102’的附加的热区143’内，其中一部分冷却剂在冷区115’内的中等压力下蒸发。其余的冷却剂则通过管道150到达第二级整体预冷却热交换器102的附加热区143，这种冷却剂可在冷区115内于低压下蒸发。天然气在第一级和第二级热交换器102、102’中受到预冷却，其中，两个热区12通过管道151互相连接。每条液化冷却剂环路的液化冷却剂在热区57和57’内受到预冷却。为了清晰起见，图中未示出后两个热区互相连接的管道。
上述的整体预冷却热交换器可以是三级串联排列的(而不是两级的)热交换器。
主热交换器5和5’可以是任何具有合适结构的交换器例如绕管式热交换器或散热片式热交换器。
在参考图1所述的实施例中，液化热交换器5和5’分别具有第二和第三热区67、67’和77、77’。在一个替换实施例中，上述的液化热交换器只有一个由第二和第三热区组合的热区。在这种实施例中，部分冷凝的主冷却剂直接供入第三热区77、77’，而不分离成重的液态馏分和轻的气态馏分。
上述的压缩机31、50和50’可以是带有中间冷却器的多级压缩机，或者说是与置于两个压缩机之间的中间冷却器串联组合的压缩机，或平行排列的压缩机组合。
在预冷却冷却剂环路3和两个主冷却剂环路9和9’中可以用电动马达而不用涡轮来带动压缩机31、50和50’。
预冷却冷却剂环路中的涡轮(未示出)最好是蒸汽涡轮。在这种实施例中，驱动蒸汽涡轮所需的蒸汽最好用由冷却主冷却剂环路的燃气涡轮(未示出)废气放出的热量加热产生。
本发明提供一种有发展潜力的液化天然气的设备，其特征在于，第一步，建造具有100％液化能力的单列设备，第二步，再增加尺寸与第一种设备相同的第二液化热交换器和第二液化冷却剂环路，以使液化能力提高到大约140％～160％。
上述的预冷却冷却剂环路可服务于两条主冷却剂环路，这样，天然气预冷却的程度可能会降低。但是，本发明的优点在于容易修改预冷却和液化条件例如冷却剂的成分而达到有效地工作。而且，在万一有一条冷却剂环路不得不停止工作的情况下，也可以修改上述的条件而用单级液化设备有效地工作。
这样，液化能力可以提高而不必增加第二预冷却环路，这也显著地节约成本。
而且，计算结果表明，采用一个服务于两个主冷却剂环路的预冷却的冷却剂环路对于液化效率(压缩机所做的单位功产生的液化天然气的量)没有不利的影响。

Claims (5)

1.一种液化天然气的设备，它具有：一个带有天然气入口和冷却的天然气出口的预冷却热交换器；一个具有一个与上述冷却的天然气出口相连接的入口并具有至少两个出口的分配器；和至少两个主热交换器，该热交换器分别具有一个带有一个与上述分配器的一个出口相连接的一个入口和一个液化天然器的出口的第一热区，上述设备还具有一条用于带走预冷却热交换器中的天然气的热量的预冷却冷却剂环路和至少两条用于带走流过相应的主热交换器的第一热区的天然气中的热量的主冷却剂环路。
2.根据权利要求1的液化天然气的设备，其特征在于，上述的冷却剂环路含有一个由合适的驱动器带动的压缩机。
3.根据权利要求2的液化天然气的设备，其特征在于，上述预冷却的冷却剂环路中的压缩机的驱动器是蒸汽涡轮。
4.根据权利要求3的液化天然气的设备，其特征在于，每条液化冷却剂环路中的压缩机的驱动器是燃气涡轮，并且在正常作业过程中，驱动蒸汽涡轮所需的蒸汽由冷却主冷却剂环路中的燃气涡轮废气放出的热量加热产生。
5.根据权利要求1～4中任一项的液化天然气的设备，其特征在于，上述的分配器带有两个出口，上述的设备具有两个主热交换器和两条主冷却剂环路。
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US6389844B1 (en) 2002-05-21
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