CN1117129A - 分离气体混合物的方法和装置 - Google Patents

分离气体混合物的方法和装置 Download PDF

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CN1117129A
CN1117129A CN95104375A CN95104375A CN1117129A CN 1117129 A CN1117129 A CN 1117129A CN 95104375 A CN95104375 A CN 95104375A CN 95104375 A CN95104375 A CN 95104375A CN 1117129 A CN1117129 A CN 1117129A
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freezing liquid
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J·比里
F·格拉尼
P·维克多
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Abstract

在从气体混合物(还含有甲烷)制备一氧化碳和氢气的方法中，该气体混合物在一种装置中进行蒸馏。在该装置中一部分分离能是通过一种使用自激冷冻液的制冷循环来提供的。
这一液体可以是氮，它在多个蒸馏塔(9)之一的上部冷凝器中汽化。

Description

分离气体混合物的方法和装置
本发明涉及分离含氢气、一氧化碳和甲烷的气体混合物而制备纯产品氢气和一氧化碳的方法和装置。
在常规方法中，所谓的“部分冷凝”，在冷至低温后从气体混合物中分离的氢气被膨胀至大约5—10巴的压力，以便获得低温以将装置保持在冷冻状态并将气体混合物冷却至-200℃以下。这种类型的装置在US4,217,759中有描述，它使用至少四个塔来制备一氧化碳，其回收率为95％，而纯度为约99％。氢气的回收率约为99.9％，而纯度为约95％。
本发明为其目的在保持这些纯度和这些高回收率的同时，通过减少分离阶段所用塔的数目而简化了工艺和装置。本发明还为其目的确保了该装置的最低温度在常规方法的最低温度之上，并提供了相对于现有技术而言成本降低的装置。
所以，本发明为其目的提供了从主要包含一氧化碳和氢气这两种组分及甲烷的气体混合物中制备一氧化碳和氢气的方法，其特征在于该方法包括以下步骤：
ⅰ)冷却初始气体混合物，以便部分地将它冷凝；
ⅱ)从主要含有氢气的未冷凝部分分离出该混合物的冷凝部分；
ⅲ)将所述冷凝部分送入汽提塔中，在塔上部制得包含氢气的气体级分，在塔底部制得含有一氧化碳和甲烷的液体级分；
ⅳ)在提纯塔中蒸馏该液体级分，在塔上部制得基本纯净的一氧化碳，而在塔底部制得甲烷；
ⅴ)通过一种使用自激冷冻液的制冷循环来提供一部分分离能。
优选地，该冷冻液的作用是冷却提纯塔的上部冷凝器。
该冷冻液还可加热汽提塔的底部，提纯塔的底部，或都加热。
尽管冷冻液优选是氮，但还可从空气、氧、氩和二氧化碳中选择。
本发明还为其目的提供了从主要包含一氧化碳和氢气这两种组分及甲烷的气体混合物制备一氧化碳和氢气的装置，其特征在于它包括：
分相器，汽提塔，提纯塔，将气体混合物导入分相器和排出气体部分(主要包括氢气)和液体部分的装置，将液体部分送至汽提塔、从中排出主要含甲烷和一氧化碳的液体以及将这种液体送至提纯塔的装置，从提纯塔中排出气体一氧化碳的装置，和通过一种使用自激冷冻液的制冷循环来提供一部分分离能的装置。
该制冷循环能够在由冷冻液循环构成的提纯塔的上部提供回流。
冷冻液循环包括压缩机，它能根据在提纯塔底部所使用的再沸体系而将冷冻液压缩至10—34巴的压力。
当该底部被普通再沸器加热时，冷冻液的压力上升至25巴以上。
该循环特别简单并可使用标准型的压缩机，它的成本低，如果需要，可带有为系统提供冷冻的涡轮。
用所要求的这种方法，没有必要按照以前那样将待处理的气体冷至-200℃，-194℃的温度对于该分离方法来说已足够了。
本发明的其他特点和优点将从下面的参考附图给出的叙述中变得很清楚，该附图是根据本发明实施方案的分离操作的简图。
在附图所示的系统中，合成气混合物含有残余甲烷且含有氢气和一氧化碳。这种混合物一般含有50—70mol％氢气，15—45mol％一氧化碳和2—6mol％甲烷，附带少量杂质。
该待处理的气体混合物被压缩至45巴，通过导管1并在交换器3中冷却至约-194℃的温度，它离开时呈部分冷凝状态。从分相器5中排出液体级分和气体级分。该气体级分主要含有氢气，然后在交换器3中被重新加热而构成高压下的氢气产品4的主要部分。
主要含氢气和一氧化碳的液体级分在阀门中膨胀，将其在汽提塔7中的压力降至12.5巴。
来自塔7的含氢气的闪蒸气体能够与主氢气流4混合，以便最大程度地回收氢气。另外，它可构成中压氢气产品。来自塔7的-160.3℃的液体主要由一氧化碳组成，它接着被膨胀至-177.5℃并通过在提纯塔9中在4巴下蒸馏而提纯，制得纯一氧化碳(为上部气体)和甲烷(为底部液体)。该一氧化碳和含有重杂质的甲烷分别通过导管11、13排出并在交换器3中重新加热。
提纯塔9的上部冷凝器15被循环液体是氮的自激冷冻液循环所冷却，该循环彻底与其它所列举液体的导管分开。
来自外部源的、在压缩机17中被压缩至10巴的、通过高压导管19的循环氮在被膨胀和分离成两股氮流之前在交换器3中冷却和液化。第一股氮流被导入上部冷凝器15中，在这里，它在4.5巴下汽化。在10巴下的第二股氮流在阀门20中经焦耳—汤姆逊膨胀至1.2巴，然后被送至交换器3，在其中它在被压缩机17压缩之前重新加热。
在冷凝器中所汽化的氮气在涡轮23中从4.5巴膨胀至1.2巴之前，在交换器3中仅仅被部分地重新加热，在被重新加热之前与通过阀门20膨胀的氮气重新混合，然后被送至压缩机17。
涡轮23可以被另一种制冷方法如向交换器3上游的导管21中注射液氮所代替。在交换器中被汽化之后，多余的气体氮在压缩机17的上游或下游排出。
在该装置的低温部件充分保温好的情况下，可省略所有的制冷装置，因为热损失能被待处理气体的和循环液体的焦耳—汤姆逊效应所补偿。
提纯塔9的底部通过以下方式加热：从塔底部排出来自第一塔板的几乎纯净的液体一氧化碳，这一液体在返回处于其排出部位之下的塔底部之前在交换器3中被部分汽化，在提纯塔9的第一塔板和底部之间的温度梯度特别大。
汽提塔7的底部通过在交换器3中部分汽化来自第一塔板的液体而以同样的方式被加热。

Claims (19)

1.从主要包含氢气和一氧化碳这两种组分及甲烷的气体混合物中制备一氧化碳和氢气的方法，其特征在于它包括以下步骤：
ⅰ)冷却初始气体混合物，以便部分地将它冷凝；
ⅱ)从主要含有氢气的未冷凝部分分离出该混合物的冷凝部分；
ⅲ)将所述冷凝部分送入汽提塔(7)中，在塔上部制得包含氢气的气体级分，而在塔底部制得含有一氧化碳和甲烷的液体级分；
ⅳ)在提纯塔(9)中蒸馏该液体级分，在塔上部制得基本纯净的一氧化碳，而在塔底部制得甲烷；
ⅴ)通过一种使用自激冷冻液的制冷循环来提供一部分分离能。
2.根据权利要求1的方法，其中提纯塔(9)的上部通过汽化冷冻液而被冷却。
3.根据权利要求1或2的方法，其中提纯塔(9)的底部和/或汽提塔(7)的底部通过冷冻液来加热。
4.根据权利要求1或2的方法，其中冷冻液选自氮、空气、氧、氩和二氧化碳。
5.根据权利要求3的方法，其中冷冻液选自氮、空气、氧、氩和二氧化碳。
6.根据权利要求1或2的方法，其中冷冻液在提纯塔(9)的上部冷凝器中汽化之前被液化和压缩至10—34巴的压力。
7.根据权利要求6的方法，其中用来冷却冷凝器(15)的冷冻液在涡轮(23)中膨胀以便提供冷却该装置所需的低温并被重新加热和返回压缩机(17)的入口。
8.根据权利要求7的一项的方法，其中一部分处在液相的冷冻液经历了焦耳—汤姆逊膨胀(20)并在被重新加热之后返回到压缩机(17)的入口。
9.根据权利要求1，2，7或8的方法，其中通过使处在液相的冷冻液流返回到循环中，然后在交换器(3)中汽化来制冷。
10.根据权利要求1，2，7或8的方法，其中提纯塔(9)的底部被从提纯塔的第一塔板下方排出的、在交换器(3)中至少部分汽化的并在低于排出部位的位置重新导入提纯塔(9)的液体所加热。
11.根据权利要求1，2，7或8的方法，其中汽提塔(7)的底部被从汽提塔(7)的第一塔板下方排出的、在交换器(3)中至少部分汽化的并在低于排出部位的位置重新导入汽提塔(7)的液体所加热。
12.从主要包含氢气和一氧化碳这两种组分及甲烷的气体混合物制备一氧化碳和氢气的装置，其特征在于它包括：
分相器，汽提塔(7)，提纯塔(9)，将气体混合物导入分相器(5)和从中排出主要包含氢气的气体部分和液体部分的装置(1)，将液体部分送至汽提塔(7)、从中排出主要含甲烷和一氧化碳的液体并将这种液体送至提纯塔(9)的装置，从提纯塔(9)中排出气体一氧化碳的装置(11，13)和通过一种使用自激冷冻液的制冷循环来提供一部分分离能的装置。
13.根据权利要求12的装置，其中冷冻液循环冷却提纯塔(9)的上部。
14.根据权利要求12的装置，它包括将提纯塔(9)的底部和由冷冻液循环构成的汽提塔(7)的底部加热的装置。
15.根据权利要求13的装置，它包括将提纯塔(9)的底部和由冷冻液循环构成的汽提塔(7)的底部加热的装置。
16.根据权利要求12或13的装置，其中冷冻液选自氮、空气、氧、氩和二氧化碳。
17.根据权利要求12或13的装置，其中冷冻液循环包括用来将冷冻液压缩至10—34巴的压力的压缩机(17)。
18.根据权利要求17的装置，其中，为了保持系统低温，用来冷却提纯塔(9)的上部的冷冻液在涡轮(23)中被膨胀、重新加热并重新送至压缩机(17)。
19.根据权利要求18的装置，它包括由焦耳—汤姆逊效应将一部分压缩液体在使它返回压缩机(17)之前膨胀的装置(20)。
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