CN101421574B - 用于液化天然气物流的方法和装置 - Google Patents

用于液化天然气物流的方法和装置 Download PDF

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CN101421574B
CN101421574B CN200780013103XA CN200780013103A CN101421574B CN 101421574 B CN101421574 B CN 101421574B CN 200780013103X A CN200780013103X A CN 200780013103XA CN 200780013103 A CN200780013103 A CN 200780013103A CN 101421574 B CN101421574 B CN 101421574B
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liquid separation
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heat exchange
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CN101421574A (zh
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M·A·凯文内尔
C·K·博赫
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Shell Internationale Research Maatschappij BV
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Abstract

本发明涉及一种液化烃物流如天然气物流的方法，所述方法至少包括以下步骤：向第一气/液分离器(2)提供部分冷凝的烃进料物流(10)；在其中，进料物流(10)分离成气体物流(20)和液体物流(30)；膨胀气体物流(20)，并将其(40)加入第二气/液分离器(3)中；将液体物流(30)加入第二气/液分离器(3)中；从第二气/液分离器底部移出液体物流(60)，并将其加入分馏塔(5)中；从第二气/液分离器(3)顶部移出气体物流(50)，将其导入压缩机(6)中，并对其(70)进行冷却从而获得冷却的压缩物流(80)；使冷却的压缩物流(80)与第一气/液分离器(2)下游和分馏塔(5)上游的物流进行换热(8)，用于对进一步冷却的压缩物流(80c)进行更进一步的冷却和液化(16)。

Description

用于液化天然气物流的方法和装置
技术领域
本发明涉及一种使烃物流例如天然气物流液化的方法。
背景技术
已知多种用于液化天然气物流从而获得液化天然气(LNG)的方法。出于多种原因，期望对天然气物流进行液化。例如，与气体形式相比，天然气更易于以液体形式进行储存和长途运输，因为其占用更少的体积，且不需要在高压下进行储存。
通常，待液化的天然气物流(主要包含甲烷)含有在天然气液化前将要去除至一定程度的乙烷、较重的烃以及其它可能组分。为此，对天然气物流进行处理。其中一种处理方法包括去除至少部分乙烷、丙烷和较重的烃例如丁烷和丙烷(通常称为“NGL提取”和“NGL回收”)。
US 5 291 736公开了天然气液化的已知方法，包括去除比甲烷更重的烃。US 2005/0247078中给出了已知方法的另一实例。
已知方法中 的问题是如果要处理相对贫的进料物流(即含相对少的乙烷、丙烷和其它烃)，无法最佳利用可用的冷却容量。换句话说，用相同的冷却负荷只生产出较少的LNG。
发明内容
本发明的一个目的是最小化上述问题。
本发明的进一步目的是提供一种液化天然气物流的替代方法，同时回收进料物流中的部分乙烷、丙烷和较更重的烃。
根据本发明，通过提供一种液化烃物流如天然气物流的方法实现了上述一个或多个或其它目的，该方法至少包括以下步骤：
(a)向第一气/液分离器提供部分冷凝的烃进料物流；
(b)在第一气/液分离器中将进料物流分离成气体物流和液体物流；
(c)膨胀步骤(b)中获得的气体物流，从而获得膨胀物流并将其在第一进料点加入第二气/液分离器中；
(d)将步骤(b)中获得的液体物流在第二进料点加入第二气/液分离器中；
(e)从第二气/液分离器底部移出液体物流，并将其加入分馏塔中；
(f)从第二气/液分离器顶部移出气体物流，并将其导入压缩机中，从而获得具有50巴以上压力的压缩物流；
(g)冷却步骤(f)中获得的压缩物流，从而获得冷却的压缩物流；
(h)使步骤(g)中获得的冷却的压缩物流与第一气/液分离器下游和分馏塔上游的物流换热；和
(i)在步骤(h)中的换热之后，液化冷却的压缩物流，从而获得液化物流。
已经令人意想不到地发现，根据本发明可提高LNG的产量，尽管使用相同的可用外部冷却负荷。
本发明的附加优点是本方法相对简单，从而导致更低的CAPEX(资本投入)。
关于此方面，应注意在US 4 689 063和US 6 116 050中建议了使几个物流相互换热。然而，US 4 689 063和US 6 116 050的目的不是液化(通常是富含甲烷的)烃物流，因此没有教导提供至少50巴的高压物流(如本发明方法的步骤(f)中的情况)。此外，因为US 4 689 063和US 6 116 050的目的不是液化，所以在这两篇出版物(以及任选的其它相似出版物)中有关效率的考虑不能自动有效应用到目的在于液化(通常是富含甲烷的)烃物流的配置中。
根据本发明，烃物流可为任意适合的待液化含烃物流，但通常是从天然气或石油储层中获得的天然气物流。替代地，天然气物流也可从其它来源获得，还包括合成来源，例如费-托合成法。
通常，天然气物流基本由甲烷构成。优选进料物流包含至少60mol％的甲烷，更优选至少80mol％的甲烷。
取决于来源，天然气可含有不同量的比甲烷重的烃，例如乙烷、 丙烷、丁烷和戊烷以及一些芳烃。天然气物流也可含有非烃类，例如H2O、N2、CO2、H2S和其它硫化合物及类似物。
必要时，进料物流可在加入第一气/液分离器之前进行预处理。该预处理可包括去除不需要的组分例如CO2和H2S，或其它步骤例如预冷却、预加压或类似步骤。因为这些步骤已为本领域技术人员所公知，所以本文不对它们进行进一步论述。
第一和第二气/液分离器可为任意适用于获得气体物流和液体物流的装置，例如洗涤器、分馏塔、蒸馏塔等。必要时，也可存在两个或更多个并联的第一气/液分离器。优选第二气/液分离器是塔例如蒸馏塔。
同样，本领域技术人员将理解膨胀、冷却和换热可以以多种方式进行。因为本领域技术人员已经理解如何使用这些步骤，所以本文不对它们进行进一步论述。
此外，本领域技术人员将易于理解，必要时可对获得的物流进行进一步处理。
同样，换热后步骤(h)中获得的冷却的压缩物流将被液化，从而获得液化物流，例如LNG。该液化可以以多种方式进行。同样，在第一气/液分离器中的气/液分离和液化之间可进行进一步的中间处理步骤。
优选在步骤(h)中进行直接换热，即其中两个(或更多个)待换热的物流在至少一个共用的换热器中一起通过(并流或逆流)。因此，可避免使用例如中间换热流体(如例如US 2005/0247078中所用)。
此外，优选在步骤(h)中，冷却的压缩物流与在步骤e)中从第二气/液分离器移出的液体物流进行换热。
因此，用于对冷却的压缩物流进行冷却的所用致冷剂的负荷(例如在丙烷冷却循环中)降低，从而可提高液化物流的产量。
此外，优选在步骤(h)中，冷却的压缩物流与至少部分在步骤c)中获得的膨胀物流进行换热。
因此，用于对冷却的压缩物流进行冷却的所用致冷剂(例如在丙烷冷却循环中)的负荷可进一步降低。
有利地，从分馏塔顶部移出的气体物流与来自第二气/液分离器的液体物流的至少一部分进行换热。
此外，优选在将步骤(f)中从第二气/液分离器项部移出的气体物流加入压缩机之前，使其与进料物流进行换热。
同样，也优选在从分馏塔移出的气体物流与来自第二气/液分离器的液体物流的至少一部分进行换热之后，使其与从第二气/液分离器移出的气体物流进行换热。
在进一步的方面，本发明提供适用于实施本发明方法的装置，所述装置至少包括：
-第一气/液分离器，具有用于部分冷凝的烃进料物流的入口、用于气体物流的第一出口和用于液体物流的第二出口；
-第二气/液分离器，至少具有用于气体物流的第一出口和用于液体物流的第二出口以及第一和第二进料点；
-膨胀器，用于膨胀从第一气/液分离器第一出口获得的气体物流，从而获得膨胀物流；
-分馏塔，至少具有用于气体物流的第一出口和用于液体物流的第二出口以及第一进料点；
-压缩机，用于压缩从第二气/液分离器的第一出口移出的气体物流，从而获得具有50巴以上压力的压缩物流；
-冷却器，用于冷却从压缩机获得的压缩物流，从而获得冷却的压缩物流；
-第一换热器，用于将冷却的压缩物流与第一气/液分离器下游和分馏塔上游的物流进行换热；和
-液化装置，用于在第一换热器的下游对冷却的压缩物流进行液化，该液化装置包括至少一个低温换热器。
附图说明
在下文中，本发明将进一步通过下列非限定性附图进行说明。这里给出：
图1示意性给出了本发明的工艺流程图；和
图2示意性给出了本发明的另一个实施方案的工艺流程图。
为用于本说明书的目的，将指定一个参考标记给一条管线以及该管线中携带的物流。相同的参考标记指类似的部件。
具体实施方式
图1示意性给出了用于烃物流例如天然气液化的工艺流程图(通常用参考标记1表示)，其中在实际液化进行之前将乙烷和更重的烃除去(“NGL回收”)至一定的程度。
图1的工艺流程图包括第一气/液分离器2、第二气/液分离器3(在图1和图2的实施方案中为蒸馏塔例如吸收塔)、膨胀器4、分馏塔5、压缩机6(其可为包括一个或多个压缩机的序列)、冷却器7、第一换热器8、第二换热器9、第三换热器11和液化装置16。本领域技术人员将易于理解，必要时可存在其它元件。
使用过程中，在一定的入口压力和入口温度下，将含有天然气的部分冷凝的进料物流10加入第一气/液分离器2的入口21。典型地，第一气/液分离器2的入口压力为10至80巴，温度通常为0至-60℃。
在第一气/液分离器2中，进料物流10分离成气态塔顶物流20(在第一出口22处移出)和塔底物流30(在第二出口23处移出)。相对于进料物流10，塔顶物流20富含甲烷(和通常也富含乙烷)。
在分离器2的第一出口22处移出的气体物流20于膨胀器4中进行膨胀，并随后作为物流40在第一进料点33处加入第二气/液分离器3中。通常第二气/液分离器3是吸收塔。
第一气/液分离器2的塔底物流30通常为液体且通常含有一些当处于甲烷被液化的温度下可冻凝的组分。塔底物流30也可含有可单独处理形成液化石油气(LPG)产品的烃。在第二进料点34将物流30加入第二气/液分离器3中，第二进料点34通常比第一进料点33低。
在第一出口31处从第二气/液分离器3的顶部移出气态塔顶物流50，并将其导入压缩机序列6。
在第二出口32处从第二气/液分离器3底部移出液体物流60，将 其导入分馏塔5，通过第一进料点53加入其中。优选分馏塔5在与吸收塔3相等或者更高的压力下进行操作。
在压缩机6中进行压缩，从而获得压缩物流70；典型地，压缩物流70的压力为50-95巴，优选60巴以上，更优选70巴以上。可将一个(和多个)用于获得物流70的压缩机与膨胀器4功能上耦连(如图1所示)。随后在冷却器7中冷却压缩物流70(例如空气或水冷却器或者其中循环外部致冷剂的换热器)，从而获得冷却的压缩物流80，随后将其与第一气/液分离器2下游和分馏塔5上游的物流进行换热，即介于第一气/液分离器2的第二出口23和分馏塔5的第一进料点53之间的物流。
在根据图1的实施方案中，将冷却的压缩物流80与从第二气/液分离器3移出的液体物流60进行换热，并随后作为物流180导入液化装置(通常用附图标记16表示)，以获得液化物流190，例如LNG。为此，液化装置16包括至少一个主低温换热器(未示出)。本领域技术人员将易于理解该液化过程如何进行，因此本文不对它进行进一步论述。
如图1所示，液体物流60在第二气/液分离器3的第二出口32处移出，并作为物流90泵送至第一换热器8用于与冷却的压缩物流80进行换热，之后，将其作为物流110在第一进料点53处加入分馏塔5中。在图1所示的实施方案中，在进入第一换热器8之前，将部分物流90(即物流90a)导入另外的换热器(‘第二换热器9’)。
从分馏塔5的顶部移出气体物流130(在第一出口51处)，其与物流90a在第二换热器9中进行换热，并随后作为物流140加入罐18。将罐18的顶部部分(物流150)导入换热器14(用于与物流50进行换热)，并随后作为物流160在第三进料点35处加入第二气/液分离器3中，第三进料点35通常比第一进料点33位置高。此外，将罐18的底部物流170移出，并作为例如燃料物流排除。必要时，物流170可在换热器11和12中进行换热。在第二进料点54处，可将部分物流170作为物流170a加入分馏塔中，第二进料点54通常比第一进料点53位置高。此外，可存在再沸器17以将物流200作为物流210在第三进 料点55处循环至分馏塔5。
从分馏塔5的底部移出液体物流120(在第二出口52处)，其可被进一步处理以从中获得特定组分。
如图1的实施方案中所示，为获得部分冷凝的进料物流10，其可以以多种方式进行预冷却，例如在换热器12、13和11中分别作为物流10c、10b和10a进行换热。在换热器11和12中，进料物流(作为物流10a和10c)与从第二气/液分离器3的第一出口31移出的塔顶物流50进行换热，所述物流50导入压缩机6。在换热器13中，进料物流10作为物流10b与外部致冷剂例如在丙烷(“C3”)致冷剂线路中循环的致冷剂进行换热。
此外，如图1中所示，在换热器11和12中进行换热之前，在换热器14中使塔顶物流50进行换热(与从罐18移出的顶部物流即物流150换热)。
必要时，可在将进料物流10加入第一气/液分离器2之前，已经对进料物流10进行了进一步的预处理。作为实例，也可在进入分离器2之前，从进料物流10至少部分去除CO2、H2S和具有与戊烷一样或者更高分子量的烃组分。
此外，冷却的压缩物流80可在第一换热器8中与物流90进行换热之前，进行进一步冷却。为此，图1显示了液化装置16上游的3个换热器15a、15b和15c，其中可循环一种或多种外部致冷剂(在这种情况下为丙烷；“C3”)。在换热器15a和15b中冷却后，物流80(作为物流80b)在第一换热器8中进行换热，之后将其作为物流80c在换热器15c中进行进一步冷却以获得物流180。典型地，物流80c的温度低于0℃，且优选在-35℃以上。必要时，可在液化装置16中进行液化前对物流180进行进一步的处理步骤。
图2示意性给出了本发明的替代实施方案，其中冷却的压缩物流80与至少部分从膨胀器4获得的膨胀物流40(物流40a)进行换热。在图2中示出的实施方案中，膨胀物流40分流成分物流40a和40b，其中物流40b旁路通过第一换热器8。
不用说，必要时，可组合图1和2中的实施方案。
表I和II概述了图1的实例方法中不同部位物流的压力和温度。还给出了甲烷的mol％。图1的管线10中的进料物流近似包括下列组成：91％甲烷，4％乙烷，3％丙烷，差不多2％的丁烷和戊烷以及0.1％的N2。之前已经去除了其它组分，例如H2S，CO2和H2O。
表I
管线 压力(巴) 温度(℃) Mo1％甲烷
10c 57.7 19.8 90.6
10b 57.5 -1.3 90.6
10a 57.2 -11.5 90.6
10 57.0 -33.4 90.6
20 56.9 -33.4 93.5
30 56.9 -33.5 48.6
40 22.0 -75.4 93.5
50 21.7 -79.8 94.9
60 21.9 -68.3 34.3
70 73.0 89.4 93.9
80 72.7 53.0 93.9
80a 72.4 21.0 93.9
80b 72.0 -11.5 93.9
80c 71.8 -27.3 93.9
90 24.0 -68.2 34.3
130 22.4 2.7 52.7
140 22.2 -76.8 52.7
180 71.4 -27.5 93.9
作为对比，使用与图1相同的配置，但与本发明不同，冷却的压缩物流80未与第一气/液分离器2下游和分馏塔5上游的物流换热(特别是未与从第二气/液分离器3移出的液体物流60换热)。
如表II中所示，使用相同的可用外部冷却负荷时，当与对比相比时，本发明使LNG产量提高2.83％。
表II
图1(本发明) 图1中无换热(对比)
LNG流量(1000吨LNG/天) 22.9 22.2
具体功率(kW/吨LNG/天) 15.2 15.6
LNG产量提高(％) 2.83 -
本领域技术人员将易于理解，在不偏离本发明范围的情况下，可以作出多种调整。例如，每个换热器可以包括序列换热器。

Claims (18)

1.一种液化烃物流的方法，所述方法至少包括以下步骤：
(a)向第一气/液分离器(2)提供进料物流(10)，其中进料物流(10)为部分冷凝的烃物流；
(b)在第一气/液分离器(2)中将进料物流(10)分离成气体物流(20)和液体物流(30)；
(c)膨胀步骤(b)中获得的气体物流(20)，从而获得膨胀物流(40)，并将其在第一进料点(33)加入第二气/液分离器(3)中；
(d)将步骤(b)中获得的液体物流(30)在第二进料点(34)加入第二气/液分离器(3)中；
(e)从第二气/液分离器底部移出液体物流(60)，并将其加入分馏塔(5)中；
(f)从第二气/液分离器(3)顶部移出气体物流(50)，并将其导入压缩机(6)中，从而获得具有50巴以上压力的压缩物流(70)；
(g)冷却步骤(f)中获得的压缩物流(70)，从而获得冷却的压缩物流(80)；
(h)使步骤(g)中获得的冷却的压缩物流(80)与第一气/液分离器(2)下游和分馏塔(5)上游的物流换热；和
(i)在步骤(h)中的换热之后，液化冷却的压缩物流，从而获得液化物流(190)。
2.根据权利要求1的方法，其中在步骤(h)中冷却的压缩物流(80)与步骤(e)中从第二气/液分离器(3)移出的液体物流(60)进行换热。
3.根据权利要求1的方法，其中在步骤(h)中冷却的压缩物流(80)与至少部分步骤(c)中获得的膨胀物流进行换热。
4.根据权利要求1的方法，其中步骤(f)中从第二气/液分离器(3)顶部移出的气体物流(50)在加入压缩机(6)之前与进料物流(10a，10c)进行换热。
5.根据权利要求2的方法，其中步骤(f)中从第二气/液分离器(3)顶部移出的气体物流(50)在加入压缩机(6)之前与进料物流(10a，10c)进行换热。
6.根据权利要求1-5任一项的方法，其中从分馏塔(5)顶部移出的气体物流(130)与来自第二气/液分离器(3)的液体物流(60)的至少一部分(90a)进行换热。
7.根据权利要求6的方法，其中从分馏塔(5)移出的气体物流(130)在与来自第二气/液分离器(3)的液体物流(60)的至少一部分(90a)进行换热后与从第二气/液分离器(3)移出的气体物流(50)进行换热。
8.根据权利要求1-5任一项的方法，其中所述部分冷凝的烃物流是天然气物流。
9.根据权利要求6的方法，其中所述部分冷凝的烃物流是天然气物流。
10.根据权利要求7的方法，其中所述部分冷凝的烃物流是天然气物流。
11.一种用于液化烃物流的装置(1)，所述装置(1)至少包括：
-第一气/液分离器(2)，具有用于进料物流(10)的入口(21)、用于气体物流(20)的第一出口(22)和用于液体物流(30)的第二出口(23)，其中进料物流(10)为部分冷凝的烃物流；
-第二气/液分离器(3)，至少具有用于气体物流(50)的第一出口(31)和用于液体物流(60)的第二出口(32)以及第一进料点(33)和第二进料点(34)；
-膨胀器(4)，用于膨胀从第一气/液分离器(2)的第一出口(22)获得的气体物流(20)，从而获得膨胀物流(40)，膨胀器(4)的出口连接至第二气/液分离器(3)的第一进料点(33)；
-分馏塔(5)，至少具有用于气体物流(130)的第一出口(51)和用于液体物流(120)的第二出口(52)以及第一进料点(53)，所述第一进料点(53)用于接收从第二气/液分离器(3)的第二出口(32)移出的液体物流(60)；
-压缩机(6)，用于压缩从第二气/液分离器(3)的第一出口(31)移出的气体物流(50)，从而获得压缩物流(70)；
-冷却器(7)，用于冷却从压缩机(6)获得的压缩物流(70)，从而获得冷却的压缩物流(80)；
-第一换热器(8)，用于将冷却的压缩物流(80)与第一气/液分离器(2)下游和分馏塔(5)上游的物流换热；和
-液化装置(16)，用于在第一换热器(8)的下游对冷却的压缩物流(80)进行液化，从而获得液化物流(190)，该液化装置(16)包括至少一个低温换热器。
12.根据权利要求11的装置(1)，其中冷却的压缩物流(80)可在第一换热器(8)中与从第二气/液分离器(3)移出的液体物流(60)进行换热。
13.根据权利要求11的装置(1)，其中冷却的压缩物流(80)可在第一换热器(8)中与至少部分膨胀物流进行换热。
14.根据权利要求11的装置(1)，进一步包括第三换热器(11)，在第三换热器(11)中从第二气/液分离器(3)的第一出口(31)移出的气体物流(50)可在加入压缩机(6)之前与进料物流(10)进行换热。
15.根据权利要求11的装置(1)，其中第二气/液分离器(3)的第一出口(31)位于第二气/液分离器(3)的顶部。
16.根据权利要求11的装置(1)，其中分馏塔(5)的第一出口(51)位于分馏塔(5)的顶部。
17.根据权利要求11-16任一项的装置(1)，进一步包括在第二气/液分离器(3)的第二出口(32)与分馏塔(5)的第一进料点(53)之间的第二换热器(9)，在第二换热器(9)中，从分馏塔(5)的第一出口(51)移出的气体物流(130)可与来自第二气/液分离器(3)的液体物流(60)的至少一部分进行换热。
18.根据权利要求17的装置(1)，进一步包括换热器(14)，用于使从分馏塔(5)移出的气体物流(130)在第二换热器(9)中换热之后与从第二气/液分离器(3)移出的气体物流(50)进行换热。
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