CN1302368A - 对富含甲烷的气流进行液化的方法 - Google Patents

对富含甲烷的气流进行液化的方法 Download PDF

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CN1302368A
CN1302368A CN99806454A CN99806454A CN1302368A CN 1302368 A CN1302368 A CN 1302368A CN 99806454 A CN99806454 A CN 99806454A CN 99806454 A CN99806454 A CN 99806454A CN 1302368 A CN1302368 A CN 1302368A
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亨德里克·F·赫罗特扬斯
罗伯特·克莱因·内格尔伍特
科内利斯·扬·温克
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Shell Internationale Research Maatschappij BV
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Abstract

一种用于对富含甲烷的气流进行液化的方法,该方法包括:a)将高压天然气流(1)输送到一个洗涤塔(5)中,在洗涤塔中将重碳氢化合物从天然气流(1)中除去,从而获得一种气态的塔顶流(8),该气流从洗涤塔(5)的顶部被抽出;对气态塔顶物流进行部分冷凝,该凝结流被返送到洗涤塔的上部来作为回流,并从其中分离去掉冷凝流(91);b)通过将富含甲烷的高压气流在一条管道(15)中和一种复合致冷剂间接地进行热交换而进行液化,该管道布置在一个主热交换器(17)中,所述的致冷剂蒸发成低压致冷剂,并从主热交换器(17)的管际空间(19)内抽出;且在高压状态下进行部分冷凝;以及c)将复合致冷剂在辅助热交换器(35)中的一条管道(38)中进行压缩,并使它们通过和一种辅助复合致冷剂间接地进行换热而获得了步骤b)所用的复合致冷剂,该辅助致冷剂发生低压蒸发,其中对气态的塔顶流进行的部分冷凝是在一条设置在辅助热交换器(35)的管道(83)中进行的。

Description

对富含甲烷的气流进行液化的方法
本发明涉及一种对富含甲烷的气流进行液化的方法，该气流来源于天然气，由本方法所生产出的产品也被称作为液化天然气(LNG)。
在1989年10月17日至20在法国的Nice举行的第九届国际LNG大会中，由R Klein Nagelvoort、I Poll和A J Ooms撰写的论文“液化循环流程的进展”中就曾描述了这样的方法。
现有技术中的对富含甲烷的气流进行液化的方法包括如下的步骤：(a)将天然气加压后输送到一个洗涤塔中，在洗涤塔中将重碳氢化合物从天然气中除去，重碳氢化合物从洗涤塔的底部被抽出，从而获得一种气态的塔顶流，该气流从洗涤塔的顶部被抽出；对气态塔顶物流进行部分冷凝，并将冷凝流体从其中分离出去，从而获得了富含甲烷的高压流；
(b)将富含甲烷的高压气流在一条管道中通过与一种复合致冷剂间接地换热而进行液化，该管道布置在一个主热交换器中，该致冷剂在主热交换器的管际空间内进行低压吸热蒸发；以及
(c)将从主热交换器的管际空间内抽出的复合致冷剂进行压缩，并使其在一个辅助热交换器的一条管道中通过与一种辅助复合致冷剂间接地进行换热而实现在高压下进行部分冷凝，其中辅助致冷剂在辅助热交换器的管际空间内以进行低压蒸发，以获得步骤(b)所用的复合致冷剂。
在洗涤塔中，气态流会接触到具有较低温度的回流液，因而还能进一步冷却气态流。结果就使得气流中的重碳氢化合物发生冷凝而形成液体，这些液体聚流到洗涤塔的底部，并从此处被抽到外面。
在现有的方法中，重碳氢化合物是从洗涤塔的底部抽出去的，气态塔顶流中分离出的冷凝流被输送到一个分馏单元中，来进行部分冷凝。在分馏塔中分离出一种液流，它被用作洗涤塔中的回流液。
在进行将天然气输送到洗涤塔中的(a)步骤之前，要先对天然气进行冷却。回流液的温度应当显著低于输送到洗涤塔中的天然气流的温度。这一要求也对输送到洗涤塔中的天然气流设定了一个温度下限。
在已知的方法中，天然气流在被导入到洗涤塔中之前，先在设置在辅助热交换器中的一条管道中进行冷却。因而辅助热交换器的冷端温度受回流温度的限制。因而为了对富含甲烷的气流进行液化，主热交换器必须要吸收更多的热量。
本发明的目的是要在辅助热交换器的冷端实现更低的温度，从而减少了对富含甲烷的气流进行液化时所要吸收的热量。
为了实现该目的，根据本发明的液化富含甲烷气流的方法具有这样的特征：塔顶流在设置于辅助热交换器中的一条管道中被部分冷凝。
用这样的方法，辅助热交换器的冷端温度就可在实用的范围内尽可能低地进行选择。
在现有的方法中，从辅助热交换器的冷端所抽出的复合致冷剂的温度同样也受回流温度的限制。而本发明方法的优点在于不会有这样的限制条件。相应地，也降低了对复合致冷剂循环速率的要求。
下面将参照附图举例来详细描述本发明，在附图中：
图1示意地表示了一套采用本发明方法的设备的流程图；
图2表示了对复合致冷剂进行部分冷凝的变化方案。
在本发明的方法中，天然气流1以高压状态被输送到洗涤塔5中。在该洗涤塔5中，密度大于甲烷的碳氢化合物被从天然气流中分离出来，该重碳氢化合物经导管7从洗涤塔5的底部抽出。这样就获得了气态的塔顶流，该塔顶流的甲烷浓度高于天然气，气态塔顶物流经导管8从洗涤塔5的顶部抽出。
该气态塔顶物流被部分冷凝，将凝结流从中分离出去就获得一种富含甲烷的高压气流，该凝结流经管道10流向设置在一个主热交换器17中的一条第一管道15中，在该管道中气流进行液化。我们在讨论对气态塔顶流的部分冷凝之前，将首先详细讨论液化过程。
对富含甲烷的压力气流进行液化的工作是在主热交换器17上的一条管道15中进行的，该过程是通过与主热交换器15的管际空间19内的、发生低压蒸发的复合致冷剂间接换热而实现的。液化气以高压状态经导管20从主热交换器17中流出，并被进行进一步的处理(图中未示出)。
蒸发后的复合致冷剂经导管25从主热交换器17管际空间19的暖端被抽出。复合致冷剂在压缩机27中被提高压力。压缩产生的热量由一个空冷器30散掉。复合致冷剂由导管32输送到一个辅助热交换器35中，高压状态的复合致冷剂通过和辅助复合致冷剂进行间接的热交换而发生部分冷凝，其中的辅助致冷剂在辅助热交换器35的管际空间39中发生低压蒸发(吸热)，这样就获得了要输送到主热交换器17中的复合致冷剂。
从第一管道38流出的复合致冷剂经一条导管42流向一个分离器45中，在该分离器中致冷剂被分离成气态的塔顶流和液态的塔底流。气态塔顶流经一条导管47输送到主热交换器15中的一条第二管道49中，在该管道中，高压的气态塔顶流被进行冷却、液化、并进行二级冷却。气态塔顶流在液化并二级冷却后，经导管50被输送到主热交换器17管际空间19的冷端处，在该管际空间内可使致冷剂发生低压蒸发，其中的导管50中设置了一个为膨胀阀51形式的膨胀装置。而液态塔底流则经一条导管57输送到一条设置在主热交换器17中的第三管道59中，在该管道中液态塔底流在高压下进行冷却。冷却后的液态塔底流经导管60被输送到主热交换器17管际空间19的中部，在此其吸热而蒸发成低压致冷剂，其中在导管60中也设置了一个为膨胀阀61形式的膨胀装置。复合致冷剂在蒸发时不但要从流过第一管道15中的流体吸收热量，以对其进行液化，同时还从在第二和第三管道49、59中流过的致冷剂中吸收热量。
辅助复合致冷剂在辅助热交换器35的管际空间39中发生低压蒸发，蒸发后的致冷剂从此处经导管65流出。在压缩机67中辅助复合致冷剂被加压成高压辅助致冷剂。压缩热用一个空冷器70散发掉。辅助复合致冷剂经导管72流入到辅助热交换器35中的一条第二管道78中，并在该管道中被冷却。冷却后的辅助复合致冷剂经导管80输送到辅助热交换器35管际空间39的冷端处，在该空间内辅助致冷剂蒸发成低压致冷剂，其中的导管80中设置了一个为膨胀阀81形式的膨胀装置。
上文详细讨论完液化循环流程之后，下面我们将讨论经导管8从洗涤塔5的上方抽出的气态塔顶流是如何进行部分冷凝的。
气态塔顶流经导管8被输送到设置在辅助热交换器35中的一条第三管道83中。在该第三管道83中，气态塔顶流发生部分冷凝。部分冷凝后的气态塔顶流从第三管道83中排出，并经导管85流向一个分离器90。在分离器90中，一种冷凝流被除去，从而就获得了富含甲烷的高压流体，它经导管10流向主热交换器17中的第一管道15。而冷凝流则经导管91回送到洗涤塔5的上部，作为回流液。
本发明的方法区别于现有方法之处在于：在现有的方法中，天然气在其被输送到洗涤塔之前要先在辅助热交换器中进行冷却。在现有的方法中，回流是从一个分馏单元中获得的，且该回流的温度决定了要输送到洗涤塔的冷却后的天然气的上限温度。
在现有的方法中，天然气所能被冷却的温度是在-22℃左右，这是因为要使该温度要高于回流液的温度。这就意味着在辅助热交换器的冷端所能达到的最低温度也只能是-22℃。该温度同样也是部分冷凝后的复合致冷剂的温度。此外，由于从洗涤塔底部抽去的液态重碳氢化合物会带走部分冷量，因而在洗涤塔的上游就将天然气冷却到-22℃还预示着工艺流程存在能耗损失，且效率较低。
但在本发明的方法中，经导管8从洗涤塔5的顶部抽走的气态塔顶流则在大约为-50℃的更低的温度下进行部分冷凝，可以这样做的原因是由于在洗涤塔50中设置了回流液。
由于辅助热交换器35的冷端温度要远低于在现有方法中的温度。因而复合致冷剂进行冷却的温度更低，这样就使得复合致冷剂可以用更低的速率进行环流。
天然气流在气进入到洗涤塔5之前最好能进行预冷却和干燥。预冷却最好是通过与流经导管72的辅助复合致冷剂的一个支流进行间接热交换来有效地进行，其中的支流分支点在空冷器70的下游位置。为了实现这样的热交换，辅助复合致冷剂还经一条设置了膨胀阀95的导管93流向导管1流路上的一个热交换器97。应注意到，为了简单起见，我们两次表示了热交换器97，第一次是说它在导管1中，第二次说它在导管72和65的环路中，但事实上，它们是同一个热交换器。
复合致冷剂最好是以两个阶段进行部分冷凝的。下面参照附图2对本发明的实施例进行描述。
图2中的辅助热交换器包括一个第一辅助热交换器35′和一个第二辅助热交换器35″。
复合致冷剂经导管32输送到第一辅助热交换器35′中，在第一辅助热交换器35′的第一管道38′中，复合致冷剂通过和在第一辅助热交换器35′管际空间39′中进行蒸发的中等压力的辅助复合致冷剂进行间接热交换而进行高压冷却。冷却后的复合致冷剂经连接管道98被输送到第二辅助热交换器35″中。
在第二辅助热交换器35″的第一管道38″中，复合致冷剂在高压状态下通过和在第二辅助热交换器35″管际空间39″中的进行蒸发的低压致冷剂进行间接的热交换而发生部分冷凝，从而获得了要经导管42输送到主热交换器(图2中没有示出)中的复合致冷剂。
在第一辅助热交换器35′的管际空间39′中以中等压力进行蒸发的辅助复合致冷剂从管道65′流出。在本实施例中，压缩机67是一个双级压缩机。在该压缩机67的第二压缩级，辅助复合致冷剂被压缩成高压致冷剂。压缩热用一个空冷器70散掉。辅助复合致冷剂经一条导管72输送到第一辅助热交换器35′的第二管道78′中，在该管道中致冷剂被进行冷却。一部分冷却后的辅助复合致冷剂经导管80′输送到第一辅助热交换器35′管际空间39′的冷端，在该空间内致冷剂在中等压力下发生蒸发，其中的导管80′上设置有一个为膨胀阀81′形式的膨胀装置。致冷剂蒸发时从流经管道38′和78′的流体中吸收热量。
剩余的辅助复合致冷剂经连接管99输送到第二辅助热交换器35″中的第二管道78″内，并在该管道内进行冷却。冷却后的辅助复合致冷剂经导管80″输送到第二辅助热交换器35″管际空间39″的冷端处，并在空间内进行低压吸热蒸发，其中的导管80″上设置有膨胀阀81″形式的膨胀装置。致冷剂的蒸发要从流经管道38″和78″的流体、以及从洗涤塔5的顶部抽来的流经第三管道83的气态塔顶流中吸热。
蒸发后的低压辅助复合致冷剂从导管65流出。在双级压缩机67中辅助复合致冷剂被压缩成高压辅助致冷剂。
作为替代方案，从洗涤塔5上部抽出的气态塔顶流还可以同时在第一和第二辅助热交换器35′和35″中发生部分冷凝。
天然气流在进入到洗涤塔5之前最好能进行预冷却和干燥。预冷却最好是通过与流经导管72的辅助复合致冷剂的一个支流进行间接热交换来有效地进行，其中的支流分支点在空冷器70的下游位置。为了实现这样的热交换，辅助复合致冷剂还经一条设置了膨胀阀95′的导管93′流向布置在导管1流路上的一个热交换器97′中。
还可很合适地通过使天然气同从连接管99流过的辅助致冷剂的一个支流进行换热而进一步对其进行冷却。为此，辅助复合致冷剂由设置了膨胀阀95″的导管93″输送到导管1上的热交换器97″中。
如果需要的话，空冷器30和70也可以用水冷器来取代，这些空冷器或水冷器还可以增补热交换器，在这些热交换器中使用了另外一些散热剂。
也可以用一个膨胀涡轮来代替膨胀阀61。
辅助热交换器35、35′、35″可以是卷轴式或板肋式热交换器。

Claims (4)

1．一种用于对富含甲烷的气流进行液化的方法，其包括如下的步骤：
a)将高压天然气流输送到一个洗涤塔中，在洗涤塔中将重碳氢化合物从天然气流中除去，重碳氢化合物从洗涤塔的底部被抽出，从而获得一种气态的塔顶流，该气流从洗涤塔的顶部被抽出；对气态塔顶物流进行部分冷凝，并将冷凝流从其中分离去掉，而冷凝流被返送到洗涤塔的上部来作为回流液，从而获得了富含甲烷的高压流；
(b)通过将富含甲烷的高压气流在一条管道中和一种复合致冷剂间接地进行热交换而进行液化，该管道布置在一个主热交换器中，所述的致冷剂在主热交换器的管际空间内进行低压蒸发；以及
(c)将从主热交换器的管际空间内抽出的复合致冷剂进行压缩，并使它们在一个辅助热交换器的一条管道中通过与一种辅助复合致冷剂间接地进行热交换而发生高压态部分冷凝，其中辅助致冷剂在辅助热交换器的管际空间内发生低压蒸发，这样就能获得了步骤(b)所用的复合致冷剂，
其特征在于：对气态的塔顶流进行的部分冷凝是在辅助热交换器的一条管道中进行的。
2．根据权利要求1所述的方法，其特征在于：其中对复合致冷剂进行部分冷凝的步骤包括：复合致冷剂在一个第一辅助热交换器的一条管道中在高压状态下和一种辅助复合致冷剂发生间接热交换而进行冷却，其中的辅助致冷剂在第一辅助热交换器的管际空间内以中等压力进行蒸发；然后复合致冷剂在一个第二辅助热交换器的一条管道中通过和一种辅助复合致冷剂发生间接热交换而进行冷却，其中的辅助致冷剂在第二辅助热交换器的管际空间内进行低压蒸发；而且对气态塔顶流进行的部分冷凝是在布置在第一和第二辅助热交换器的管道中进行的。
3．根据权利要求2所述的方法，其特征在于：对气态塔顶流进行的部分冷凝是在一条设置在第二辅助热交换器的管道中进行的。
4．根据权利要求1到3之一所述的方法，其特征在于：其中的天然气流通过和辅助复合致冷剂的一个支流进行间接换热而进行预冷却。
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