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CN101156038B - 用于液化天然气流的方法和设备 - Google Patents

用于液化天然气流的方法和设备 Download PDF

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CN101156038B
CN101156038B CN2006800118416A CN200680011841A CN101156038B CN 101156038 B CN101156038 B CN 101156038B CN 2006800118416 A CN2006800118416 A CN 2006800118416A CN 200680011841 A CN200680011841 A CN 200680011841A CN 101156038 B CN101156038 B CN 101156038B
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C·布伊斯
W·达姆
E·C·J·N·德容
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Shell Internationale Research Maatschappij BV
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Abstract

本发明涉及一种液化天然气流的方法，其中在30-80巴的压力下提供天然气流(10)，膨胀到压力＜35巴，供应至气/液分离器(31)，并在气/液分离器(31)内分离为蒸气流(40)与液体流(30)。将该蒸气流(40)的压力提高至至少70巴的压力，并液化加压的蒸气流(90)，以获得液化天然气流。

Description

用于液化天然气流的方法和设备
技术领域
本发明涉及一种液化天然气流的方法。
背景技术
已知有若干液化天然气流以获得液化天然气(LNG)的方法。因为一些理由，需要液化天然气流。作为一个实例，天然气以液体可比处于气体形式更容易储存和长距离运送，因为它占据较小的体积，而且不需要以高压储存。
已知的液化气体的方法的实例公开于如US6 272 882与DE 10226 597 A1。
依据DE 102 26 597 A1的图1，将压力70-100巴的天然气流膨胀(膨胀器X)至40-70巴的压力范围，冷却(热交换器E1)，并输入重质烃类(HHC)塔(T1)。将从HHC塔顶部移出的富含C2的馏分进一步冷却(E2)，并输入另一个塔(D)。将此另一个塔(D)的顶部物流加压(V)至50-100巴范围内的压力，随后被液化。
依据DE 102 26 597的方法的问题在于，其是不必要地复杂。上述方法的另一个问题在于比甲烷重的化合物(特别是丙烷和丁烷)的回收是不足的。
发明内容
本发明的目的为使上述问题减到最小。
本发明的另一目的为增加比甲烷重的化合物，特别是丙烷的回收。
本发明的又一目的为提供一种液化天然气流的替代方法。
通过提供一种液化天然气流的方法，依据本发明实现以上或其他目的中的一个或多个，此方法包括以下步骤：
(a)在30-80巴的压力下提供含有天然气的进料流；
(b)使步骤(a)的进料流膨胀，以获得压力＜(低于)35巴的膨胀进料流；
(c)将膨胀进料流供应至气/液分离器；
(d)将气/液分离器内的膨胀进料流分离成为蒸气流与液体流，该蒸气流相对于进料流富含甲烷，而该液体流相对于进料流甲烷减少；
(e)提高步骤(d)中获得的蒸气流的压力到至少70、优选至少84巴的压力；
(f)液化步骤(e)中获得的加压蒸气流，以获得液化天然气流；
其中在步骤(a)提供的进料流的压力直到在步骤(e)中压力增加才增加。
意外地发现，使用依据本发明的方法，可获得比甲烷重的化合物的明显增加的回收。本发明的一个重要优点在于这能以非常简单的方式来实现。
本发明的另一个优点在于可使用给定的冷冻动力获得提高的液化天然气产量。因此，对于给定的冷冻动力(例如，使用包含一个或多个低温热交换器、压缩机等的给定设备)，依据本发明的方法提供比已知方法多的LNG。已发现依据本发明，可获得高达20％的LNG产物提升，同时维持冷冻动力不变。
天然气流可为任何欲被液化的适当气流，但通常是从天然气或石油储藏所取得的。作为替代方案，天然气也可从其他来源取得，也包括合成来源，诸如Fischer-Tropsch程序。
通常天然气流主要包含甲烷。优选地，进料流包含至少60mol％的甲烷，更优选为至少80mol％，最优选地，进料流包含至少90mol％的甲烷。
视来源而定，天然气可包含不同量的比甲烷重的烃类，诸如乙烷、丙烷、丁烷和戊烷，以及一些芳香族烃类。天然气流也可含有非烃类，诸如H2O、N2、CO2、H2S及其他硫化合物，以及类似物。
需要的话，可在含天然气的进料流膨胀并输入气/液分离器之前，对其做预处理。此预处理可包括去除不想要的成分，诸如CO2与H2S，或其他步骤，诸如预冷却、预加压或类似步骤。由于这些步骤对于熟悉此项技术的人士而言是熟知的，在此不对其作进一步讨论。
气/液分离器可以是用于获得蒸气流与液体流的任何适当装置，诸如洗涤塔、蒸馏塔等等。需要的话，可存在两个或更多的气/液分离器。
熟悉此项技术的人士将容易地理解到，如果要获得至少70巴、优选为至少84巴的压力，可以用各种方式来进行蒸气流压力的提升。
同样地，熟悉此项技术的人士将理解到，可以用各种方式来进行加压蒸气流的液化，例如使用一个或更多的低温热交换器。
另外，熟悉此项技术的人士将容易地理解到，在液化之后，需要的话，可进一步处理液化的天然气。举例来说，所获得的LNG可借助Joule-Thomson阀或借助低温涡轮膨胀器来减压。同样地，也可在气/液分离与液化之间进行其他中间的处理步骤。
优选地，在步骤(e)中，将压力提高到至少86巴，优选为至少90巴。借此可增加所获得LNG产物的量。作为使用较高压力的结果，根据主要的压力与个别蒸气流的成分，蒸气流可能是超临界的。优选地，蒸气流是超临界的，因为这避免在液化程序中的相变。
另外，优选的是，在步骤(b)中所获得的蒸气流具有低于0.5mol％的C5 +含量，优选为低于0.1mol％。这可使在下游液化单元中的操作问题减到最少。“C5 +含量”是指具有五个或更多个碳原子的烃类成分的含量。
依据一个优选实施例，在步骤(e)中的压力通过在压缩机内的压缩蒸气流来提高，由此获得压缩流。为此目的，可使用一个或更多的压缩机。
另外，优选的是将在步骤(e)中获得的蒸气流冷却，例如在环境热交换器中进行。此外，优选的是使压缩流与在步骤(d)中获得的蒸气流作热交换。
依据本发明方法的特别优选实施例，将用于在步骤(b)中使进料流膨胀的膨胀器与用于压缩蒸气流的压缩机功能性地连接。因此，膨胀器所产生的动力至少部分地用来驱动与其功能性地连接的压缩机。由此，膨胀器与压缩机形成了所谓的“压缩机-膨胀器系统”，因而将整个程序的能量消耗减到最低。熟悉此项技术的人士将容易地理解到“压缩机-膨胀器系统”所指的含义，在此不对其作进一步讨论。
在另一方面，本发明涉及通过依据本发明的方法所获得的LNG产物，尤其是液化甲烷。
在又一方面，本发明涉及适合实施依据本发明的方法的设备，此设备至少包括：
用于在30-80巴的压力下提供含天然气的进料流的装置；
膨胀器，用于膨胀该进料流，由此获得压力＜35巴的膨胀进料流；
气/液分离器，用以将膨胀进料流分离成蒸气流与液体流，该蒸气流相对于进料流富含甲烷，而该液体流相对于进料流甲烷减少；
加压单元，用于将在气/液分离器中获得的蒸气流的压力提高到至少70巴、优选为至少84巴的压力；以及
液体单元，用于液化具有至少70巴、优选至少84巴压力的蒸气流，该液化单元包括至少一个低温热交换器。
优选地，加压单元包括一压缩机。
另外，优选的是，该设备还包括一热交换器，用于使来自压缩机的流出物与在气/液分离中获得的蒸气流做热交换。
同样地，该设备优选还包括一膨胀器，用于膨胀进料流。
依据特别优选的实施例，压缩机与膨胀器功能性地连接，由此形成所谓的“压缩机-膨胀器系统”。
此后，将通过以下非限制性的附图来进一步说明本发明。
附图说明
图1为依据本发明的实施例的程序方案示意图。
具体实施方式
为了说明的目的，将会对一管线以及在此管线中携带的物流指定单一个参考数字。相同的参考数字是指相同的组件。
图1示意性地示出一个基本负载液化天然气(LNG)输出程序及一个用于实施此输出程序的设备(总体上以参考数字1来指示)。将含有天然气的进料流10在膨胀器12中膨胀之后，以特定的入口压力与入口温度供应至气/液分离器31。典型地，物流10的压力将会介于30巴至80巴之间(优选为＞60巴且＜70巴)，而且温度将会接近环境温度，通常是在5℃至50℃之间。
需要的话，可在进料流10输入膨胀器12之前对其作预处理。举例来说，进料流10可在一个热交换器(未示出)内被冷却剂预冷却，或在一系列的热交换器，例如包括两个或更多个在不同冷却压力等级下操作的热交换器中预冷却。
将膨胀器12中的膨胀选择为形成部分冷凝的膨胀进料流25。另外，将膨胀器12中的膨胀选择为最适合后续在分离器31内的分离步骤。
将膨胀流25输入气/液分离器31。在那里，管线25内的进料流会被分成蒸气顶部流40与液体底部流30。顶部流40相对于膨胀的进料流25富含甲烷(而且通常还富含乙烷)。
底部流30通常是液体的，而且通常含有一些当被带到甲烷液化的温度下时可凝固的成分。根据从进料流去除可凝固成分所需的分离，分离器31可为分离器容器或蒸馏塔，诸如洗涤塔。典型地，可凝固成分为CO2、H2S及具有戊烷的分子量或更高分子量的烃类成分。这些可凝固成分也可在进入分离器31之前，至少部分地从进料流中去除。
底部流30也可包含可被单独处理以形成液化石油气(LGP)产物的烃类。
通常，底部流30经过一个或更多的分馏步骤，以收集各种的天然气液体产物。顶部流40经由压缩机52压缩，由此获得压缩流。
压缩流在高于70巴、优选高于84巴的压力下释放到管线65中。根据各分离压力与液化压力的选择，此压缩步骤中的压力增加选择为介于30巴与150巴之间。
于此压缩步骤期间所增加的热的一部分由环境从物流65去除，例如使用空气冷却器61或水冷器。之后在一个或更多的外部冷却阶段中将所得的环境冷却物流75进一步冷却。这可包括预冷却阶段，此处描述为热交换器81。也可以取而代之地使用一系列相继的热交换器。
然后在液化单元5中将预冷流90进一步冷却液化，液化单元5至少包括一主低温热交换器91。任何适当类型的热交换器都可以使用。这里所描述的是通过混合的冷却剂来操作的低温热交换器91，其轻质和重质馏分先在与预冷流(未示出)平行延伸的管内自动冷却，之后分别经由入口装置95和96膨胀至壳程。经由出口97从主低温热交换器91的壳程引出用过的重质与轻质馏分。管线97内用过的冷却剂可被再压缩并冷却而形成液体，或是在混合冷却剂的情况下，则是形成混合的蒸气轻质馏分与液体重质馏分。
再参考物流65，将液化压力选择为超过至少84巴，更优选为高于86巴的压力。因此，物流65中的蒸气可能会处于超临界状态。
作为下一个步骤，将经由管线100离开主低温热交换器91的液化流在闪蒸步骤中进一步冷却，其中压力经由阀或液体膨胀器101释放。适当地，膨胀后的压力约为大气压力。从液化流释放出膨胀热，从而使得温度进一步降低至液化产物在大气压力下仍维持液态的温度。在闪蒸罐111中将典型地包含氮与一些甲烷的闪蒸气体130从物流110分离。部分的闪蒸气体130可用来作为燃料气体，用于给液化程序提供能量。物流110的液体部分从管线120内闪蒸罐111的底部排出。这可作为LNG来储存和运输。
优选地，压缩机序列52使用来自至少膨胀器12的膨胀能量。为此目的，将压缩机序列52的至少一个压缩机功能性地与膨胀器12连接，由此形成所谓的“压缩机-膨胀器系统”。然而，可提供额外的压缩动力，以实现高达84巴的压力。优选地，将压缩机52所消耗的额外压缩马达动力选择为接近或等同于冷却剂压缩机(未示出)所需的动力，从而使得相同的驱动机可用于两种目的，由此提供成本与维护上的效益。
与将在表I后面的段落中说明的另一替代实施例不同，在图1的实施例中没有热联合(如另一替代实施例的流出物流热交换器中的情况)施加于赋予顶部流40的冷，从而使得在靠周围环境(在冷却器61中)将管线65内的压缩顶部流冷却之后，其会经由管线75直接输送至热交换器81内的外部冷却步骤。
表I给出在图1示范流程中，不同部分处的物流的压力与温度概要。同时也示出甲烷的mol％。图1的管线10中的进料流大致包括以下成分：80％甲烷，8％乙烷，5％丙烷，4％丁烷，1％C5 +及2％N2。可凝固的成分，诸如H2S、CO2以及H2O，已于先前去除。
表I
  管线   压力(巴)   温度(℃)   Mol％甲烷
  10   67   32   80
  管线   压力(巴)   温度(℃)   Mol％甲烷
  25   32.8   -30   80
  40   30.4   50.6   90
  65   93   160.8   90
  75   92.6   51   90
  90   89   -41.5   90
  100   81.5   -151.3   90
  110   5.4   -157.8   90
在依据本发明的另一替代实施例中，将顶部流40导引通过流出物流热交换器，在此其被周围环境温度的物流间接地加热。之后，将从流出物流热交换器排出的物流经由压缩机52或一系列两个或更多的压缩机压缩。在高于84巴的压力下将压缩流排出至管线中，在例如空气冷却器61中冷却，由此获得所述周围环境温度的物流。然后将所得的环境冷却的周围环境温度的物流导引至流出物流热交换器，在此其在与冷的顶部流40的间接热交换中被冷却，由此产生一物流，该物流在热交换器81中进一步冷却。
表II给出使用依据本发明如图1中所描述的方法而在丙烷与丁烷回收上的增加的指示。作为比较，使用与图1相同的设备(line-up)，但是，与本发明相反的，在膨胀器12中发生了膨胀至大约45巴。如表II所示，本发明在物流30中产生了增加的丙烷与丁烷回收率(16％和36％分别相对于9％和20％)。
表II
表III给出使用依据本发明如图1中所描述的方法而在LNG产物上增加的指示。作为比较，使用与图1相同的冷冻动力与设备，但是，与本发明相反的，在压缩机序列52中并未发生压缩；因此，管线65内的压力与管线40比较是相同的，即约30.4巴。从表III可以看出，LNG产物的增加约为19％。
表III
性能(单元) 依据本发明的图1   比较-在图1的压缩机序列52中没有压缩
 提供给交换器81的冷冻循环的动力(MW) 80 80
 提供给交换器91的冷冻循环的动力(MW) 80 80
 低温热交换器81和91的组合大小(kW/K) 61,500 61,500
 LNG生产量(tpd)     13,169   11,080

Claims (15)

1.一种液化天然气流的方法，所述方法包括以下步骤：
(a)在30巴和70巴之间的压力下并在接近环境温度的在5℃至50℃之间的温度下提供含有天然气的进料流；
(b)使步骤(a)的进料流膨胀，由此获得压力＜35巴的膨胀进料流；
(c)将膨胀进料流供应至气/液分离器；
(d)将气/液分离器内的膨胀进料流分离成蒸气流与液体流，所述蒸气流相对于进料流富含甲烷，而所述液体流相对于进料流甲烷减少；
(e)将在步骤(d)中获得的蒸气流的压力提高到至少70巴的压力；
(f)液化在步骤(e)中获得的加压蒸气流，由此获得液化天然气流；
其中在步骤(a)中提供的进料流的压力直到在步骤(e)中的压力增加才增加。
2.如权利要求1的方法，其中在步骤(e)中，所述压力增加到至少90巴。
3.如权利要求1的方法，其中在步骤(d)中所获得的蒸气流具有低于0.5mol％的C5 +含量。
4.如权利要求1的方法，其中在步骤(e)中的压力通过压缩所述蒸气流而提高，由此获得压缩流。
5.如权利要求1的方法，其中在步骤(e)中获得的蒸气流被冷却。
6.如权利要求4的方法，其中所述压缩流在步骤(f)中被液化之前，与在步骤(d)中获得的蒸气流做热交换。
7.如权利要求1的方法，其中用于在步骤(b)中使进料流膨胀的膨胀器与用于压缩蒸气流的压缩机功能性地连接，以致，膨胀器所产生的动力至少部分地用来驱动所述压缩机。
8.如权利要求1的方法，其中，在步骤(d)中所获得的蒸气流具有低于0.1mol％的C5 +含量。
9.如权利要求1、3-8中任一项的方法，其中，在步骤(e)中，所述蒸气流的压力增加到至少84巴。
10.一种用于液化天然气流的设备(1)，所述设备至少包括：
被布置成用于提供在30巴和70巴之间的压力下并在接近环境温度的在5℃至50℃之间的温度下的含有天然气的进料流(10)的装置；
膨胀器(12)，所述膨胀器用于膨胀所述进料流(10)，由此获得压力＜35巴的膨胀进料流(25)；
气/液分离器(31)，所述气/液分离器用于将膨胀进料流(25)分离成蒸气流(40)与液体流(30)，所述蒸气流(40)相对于进料流(10)富含甲烷，而所述液体流(30)相对于进料流(10)甲烷减少；
加压单元(52)，所述加压单元用于将在气/液分离器(31)中获得的蒸气流的压力提高到至少70巴的压力；以及
液化单元(5)，所述液化单元用于液化所述具有至少70巴压力的蒸气流，所述液化单元包括至少一个低温热交换器(91)。
11.如权利要求10的设备(1)，其中所述加压单元(52)包括压缩机。
12.如权利要求11的设备(1)，其中所述设备还包括热交换器(41)，所述热交换器用于使来自压缩机(52)的流出物与在气/液分离器(31)中获得的蒸气流做热交换。
13.如权利要求11的设备(1)，其中压缩机(52)与膨胀器(12)功能性地连接，以致，膨胀器所产生的动力至少部分地用来驱动所述压缩机。
14.如上述权利要求10的设备(1)，其中在被布置成用于提供在30巴和70巴之间的压力下并在接近环境温度的在5℃至50℃之间的温度下的含有天然气的进料流(10)的装置与加压单元(52)之间不存在另外的加压单元。
15.如上述权利要求10-14之一的设备(1)，其中，所述加压单元(52)被布置成用于将所述蒸气流的压力提高到至少84巴、所述液化单元(5)用于液化所述具有至少84巴压力的蒸气流。
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EA200702213A1 (ru) 2008-02-28
EP1869383A1 (en) 2007-12-26
KR20080006571A (ko) 2008-01-16
US20090064713A1 (en) 2009-03-12
TWI390167B (zh) 2013-03-21
MY142263A (en) 2010-11-15
RU2400683C2 (ru) 2010-09-27
TW200700683A (en) 2007-01-01
AU2006233914A1 (en) 2006-10-19
RU2007141716A (ru) 2009-05-20
WO2006108821A1 (en) 2006-10-19
EP1869382A1 (en) 2007-12-26
CN101156038A (zh) 2008-04-02
AU2006233914B2 (en) 2009-09-03
NO20075778L (no) 2007-11-09
KR101269914B1 (ko) 2013-05-31
WO2006108820A1 (en) 2006-10-19
US20090064712A1 (en) 2009-03-12

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