CN1103438C - 空气分离方法及生产氮的装置 - Google Patents

空气分离方法及生产氮的装置 Download PDF

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CN1103438C
CN1103438C CN96112901A CN96112901A CN1103438C CN 1103438 C CN1103438 C CN 1103438C CN 96112901 A CN96112901 A CN 96112901A CN 96112901 A CN96112901 A CN 96112901A CN 1103438 C CN1103438 C CN 1103438C
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J·P·瑙莫维兹
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Abstract

在单塔氮发生器中生产氮的一种方法，其中用第一和第二冷却剂流使富氮塔顶馏出物冷凝，以提供蒸馏塔的回流。冷却剂流之一是由氮含量高于在蒸馏塔底部产生的富氮液体的氮含量的液体组成。这冷却剂流被压缩、冷却和再循环至蒸馏塔底部，以提高氮的回收率。

Description

空气分离方法及生产氮的装置
发明的领域
本发明涉及一种生产氮的方法及装置，其中空气在蒸馏塔中分离为富氮气体和富氮液体。具体地，本发明涉及这样的一种方法和装置，其中蒸馏塔回流是通过使一股所述的富氮气流与从蒸馏塔中提取的液流进行间接热交换，将该富氮气流冷凝而产生的，而所述的液流则在热交换中气化。更具体地，本发明涉及这样的一种方法和装置，其中上述的气化的液流被压缩、冷却、再引回至蒸馏塔以提高回收率。更加具体地，本发明涉及这样的一种方法和装置，其中上述的液流中的氮含量高于富氧液体中的氮含量。
发明的背景
氮可用本领域内称为氮发生器的单塔空气分离装置产生。在一种特别有效的氮发生器中，经过过滤的压缩纯化空气在一个单独的塔内，被分离成作为塔顶馏出物的富氮气体和作为塔底产物的富氧液体。设有一个塔顶冷凝器，将一股富氮气流冷凝，以产生塔的回流。用以承担这冷凝任务的冷却剂，是由经过阀膨胀的富氧液流提供的。这冷却剂气化了，气流的一部分可在主热交换器(用来把空气冷却至适于进行蒸馏的温度)的冷端或暖端的温度下重新压缩。然后把重新压缩过的该气化的冷却剂引回至蒸馏塔，以增加氮的总回收率。同时，气化的冷却剂的一部分可被部分加温，然后膨胀并作功。膨胀后的气流作为致冷剂为装置提供致冷作用。膨胀功的一部分被用来压缩，以节约能量。
下文将说明，上述类型的方法，可用来进一步提高氮产物的回收率。
发明的概述
本发明提供了一种生产氮的方法。这方法是先将压缩的纯化进料空气冷却至适于进行精馏的温度。把这压缩的纯化进料空气引入至蒸馏塔内，产生富氮的塔顶馏出物和作为塔底产物的富氧液体。至少将由富氮塔顶馏出物组成的富氮气流的一部分冷凝，而且至少将所得冷凝液的一部分引入至蒸馏塔作为回流。一种含氮液体是从蒸馏塔中提取的。这含氮液体中的氮含量高于上述富氧液体的氮含量。让分别由富氧液体和含氮液体组成的第一和第二冷却剂流膨胀。至少有一部分富氮馏出气流通过与第一和第二冷却剂流的间接热交换被冷凝，从而也形成了第一和第二气化的冷却剂流。由富氮馏出气流的另一部分提取氮产物。将第一气化的冷却剂流部分加温，让其膨胀并作功，从而形成致冷剂流。致冷剂流与压缩的纯化空气之间进行间接的热交换。第二气化的冷却剂流在暖的或冷的条件下压缩，然后冷却至适于进行空气蒸馏的温度。再将这第二气化的冷却剂流引入至蒸馏塔的底部区域，以提高氮产物的回收率。
另一方面，本发明提供了一种生产氮的装置。根据本发明的这一方面，该装置有一个主热交换装置，用以将压缩的纯化进料空气冷却至适于进行精馏的温度。这个主热交换装置的其它作用，是部分地将第一气化的冷却剂流加温，将第二气化的冷却剂流完全冷却至适于进行空气精馏的温度，以及间接地把热从压缩的纯化进料空气传输至致冷剂流。有一个蒸馏塔与主热交换装置相连，接受所述压缩的纯化进料空气，从而产生富氮塔顶馏出物以及富氧液体塔底产物。有一个冷凝装置，它至少将由富氮塔顶馏出物组成的富氮气流的一部分冷凝。该冷凝装置也起着其它的作用：将至少一部分所得到的冷凝液引回至蒸馏塔作为回流，并将第一和第二冷却剂流气化，从而形成第一和第二气化的冷却剂流。冷凝装置连接于蒸馏塔，使第一冷却剂流由所述富氧液体组成，而第二冷却剂流由氮含量高于所述富氧液体的一种含氮液体组成。冷凝装置也连接于主热交换装置，使第一气化的冷却剂流在其中部分地加温。在冷凝装置与蒸馏塔之间装有第一第二膨胀阀，用来分别对第一和第二冷却剂流进行阀膨胀。有一个装置用来从另一部分富氮气流提取氮产物。还有一膨胀装置连接于主热交换装置，让第一气化的冷却剂流膨胀并作功，从而形成致冷剂流。主热交换装置也连接于膨胀装置，使压缩的纯化空气间接地与致冷剂流交换热量。有一压缩装置连接于冷凝装置，用以重新压缩第二气化的冷却剂流。该压缩装置也连接于主热交换装置，使第二气化的冷却剂流在其中冷却。蒸馏塔还在其底部区域与主热交换装置相连，以便将完全冷却至适于进行空气精馏的温度后的第二气化的冷却剂流接受到蒸馏塔内。
将第二气化的冷却剂流再次引回到蒸馏塔内，可提高氮产物的回收率。第二气化的冷却剂流是由氮含量高于所述富氧液体的一种含氮液体流得到的。因此，在温度与富氧液体相同时，它具有较高的露点压力。于是第二气化的冷却剂流对压缩装置的输入压力较高，所以作同样的功可压缩更多的流量。这种流量的增加，可使热量抽提作用增加，从而使回收率大于现有技术(在现有技术中，是使气化的粗液氧流再循环回至蒸馏塔)。而且，含氮液体流的组分接近于蒸馏塔贮液池中的平衡蒸汽的组分。这可使蒸馏塔的底部以比现有技术更可逆的方式运行。
应注意，“完全加温”表示加温到主热交换器的暖端温度。“完全冷却”表示冷却到空气引入至蒸馏塔之前的温度。而“部分加温”则表示加温到一个中间温度，即主加热器暖端和冷端温度之间的一个温度。
附图简述
说明书后列有清楚地指出申请人认为是其发明内容的权利要求，但申请人认为参照附图可更好理解本发明，而附图是用以说明在本发明的装置中分离空气的方法的一张单独的图。
发明的详细描述
参看附图，其中显示了用以生产氮产物的空气分离装置1。将压缩的纯化进料空气流10引入至主热交换器12。虽然未在图中表示，进料空气流10是用本领域中人们熟知的方法，将空气用滤器过滤除去灰尘微粒后，再进行压缩而产生的。用后冷却器将压缩热去除后，再在预纯化单元中将空气纯化，预纯化单元一般包含若干个不同步运行的分子筛床，用以去除进料空气中的二氧化碳、水汽和烃类。
进料空气流10在主热交换器12内冷却至适合于蒸馏的温度以后，引入至蒸馏塔14的中部区域，在蒸馏塔14的顶部区域16产生富氮的气体塔顶馏出物，并在蒸馏塔14的底部区域18产生富氧的液体塔底产物。蒸馏塔14可使用塔板、无规填料或结构填料使待分离的空气的上升的气相与下降的液相紧密接触，从而将空气分馏为富氮气体和富氧液体。蒸馏塔14是设计成使所述的富氮气体是高纯度氮，即所含的氧少于百万分之100(100ppm)的氮。
由蒸馏塔14提取一股富氮气流20。富氮气流由富氮的气体塔顶馏出物组成。富氮气流20的一部分22在冷凝器24内冷凝。所得到的冷凝液引回至蒸馏塔14作为回流。可以理解，全部富氮气流都可以冷凝。在这情况下，只将冷凝液的一部分作为回流，其余部分则可取出作为产物。
从蒸馏塔14也提取出由富氧的液体塔底产物组成的第一冷却剂流26。第二冷却剂流28则是由蒸馏塔14中提取的含氮液体产生的。由于这含氮液体是在蒸馏塔14底部区域18上面的地方提取的，它具有的氮含量比在蒸馏塔14底部区域18收集的富氧液体中的高。第一和第二冷却剂流26和28在低温冷却单元30中低温冷却，然后分别在降压阀32和34内进行阀膨胀。这降压操作使第一和第二冷却剂流26和28的温度降低，使它们可在塔顶冷凝器24内用以使富氮气流20的一部分22冷凝。
富氮气流20的另一部分36先在低温冷却单元30内被加温至主热交换器12冷端的温度。随后富氮气流20的一部分36在主热交换器12内被完全加温，并作为产物氮气流排出(图中标示为PGN2)。
第一冷却剂流26在塔顶冷凝器24内气化，转变为第一气化的冷却剂流38。同样，第二冷却剂流28的气化，产生了第二气化的冷却剂流40。第一气化的冷却剂流38首先在低温冷却单元30内加温至主热交换器12冷端的温度，然后在主热交换器12内再部分地加温。此后，第一气化的冷却剂流38引入至汽轮膨胀器42内，由此产生致冷剂流44。致冷剂流44在低温冷却单元30内加温，然后在主热交换器12内完全加温，最后作为废氮气流排出(图中标示为WN2)。
第二气化的冷却剂流40在一个再循环压缩机46内压缩，然后完全冷却。再循环压缩机40耦合于汽轮膨胀器42，使一部分膨胀功可用来压缩冷却剂流40。其余的膨胀功则通过耗能制动器47转化为热而排除。随后，第二气化的冷却剂流40输入至蒸馏塔14的底部区域18，以提高氮产物的回收率。注意压缩的纯化空气流是在蒸馏塔14的中部区域引入的。这个中间位置就是输入空气的组分与蒸馏塔14内待分离的空气汽相的组分相同的位置。但是，压缩的纯化空气流10可以与第二气化的冷却剂流40合并，并引入至蒸馏塔14的底部区域。但这种方法的热力学效率不如上述实施例高。
在所说明的实施例中，第二气化的冷却剂流40是在基本上等于空气进行蒸馏的温度下压缩的。这里和权利要求中都用了“基本上”这个词，因为第二气化的冷却剂流40可以稍冷于压缩的纯化空气流10在蒸馏塔14中部输入处的温度，亦即稍冷于主热交换器12冷端的温度。虽然在图中未示出，在另一个实施例中，第二气化的冷却剂流40可在主热交换器12内完全加温，重新压缩，然后再完全冷却。
以上参照较佳的实施例说明了本发明，但本领域的技术人员可以理解，在不背离本发明的实质和范围的条件下，可对这实施例作各种改变、增加和删减。

Claims (7)

1.一种生产氮的方法，所述方法包括：
将压缩的纯化进料空气(10)冷却至适于进行精馏的温度；
将上述压缩的纯化进料空气(10)引入至蒸馏塔(14)，产生富氮的气体塔顶馏出物以及作为塔底产物的富氧液体；
至少使由上述富氮气体塔顶馏出物组成的富氮气流(20)的一部分(22)冷凝，并至少将所得到的冷凝液的一部分引入至所述蒸馏塔(14)作为回流；
从所述蒸馏塔(14)中提取含氮液体(28)，该含氮液体中的氮含量高于所述富氧液体的氮含量；
将分别由所述富氧液体和所述含氮液体组成的第一冷却剂流(26)和第二冷却剂流(28)膨胀；
用所述第一和第二膨胀的冷却剂流(26，28)使所述的至少一部分富氮气流(22)冷凝，并由此产生气化的第一冷却剂流(38)和第二冷却剂流(40)；
从所述富氮气流的另一部分(36)热交换提取氮产物；
部分加温所述第一气化的冷却剂流(38)，使其膨胀并作功，以形成致冷剂流(44)；
在所述致冷剂流(44)和所述压缩的纯化空气(10)之间间接地进行热交换；以及
压缩所述第二气化的冷却剂流(40)，将该第二气化的冷却剂流(40)冷却至适合精馏压缩的纯化空气的温度，并将其引入至所述蒸馏塔(14)的底部，以提高所述氮产物的回收率。
2.如权利要求1所述的方法，其特征还在于所述压缩的纯化进料空气(10)是引入至所述蒸馏塔(14)的中间部位。
3.如权利要求1或2所述的方法，其特征还在于所述第二气化的冷却剂流(40)是在比适合精馏压缩的纯化空气的温度更冷的温度下压缩的。
4.如权利要求3所述的方法，其特征还在于所述第一和第二冷却剂流在膨胀之前先进行低温冷却。
5.如权利要求4所述的方法，其特征还在于：
所述氮产物是以气态氮产物流形式提取的；和
所述气态氮产物流、致冷剂流、和第一气化的冷却剂流与所述第一和第二冷却剂流间接地进行热交换，从而低温冷却所述第一和第二冷却剂流。
6.如权利要求5所述的方法，其特征还在于所述的气态氮产物流和致冷剂流通过与所述的压缩的纯化进料空气和所述的第二气化的冷却剂流间接地进行热交换，而使气态氮产物流完全加温，并使所述第一气化的冷却剂流部分地加温。
7.一种产生氮的装置，该装置包括：
主热交换装置(12)，用以将压缩的纯化进料空气(10)冷却至适于进行精馏的温度，将来自冷凝装置(24)的第一气化的冷却剂流(38)部分加温，将来自该冷凝装置(24)的第二气化的冷却剂流(40)完全冷却至上述温度，并使热量从所述压缩的纯化进料空气(10)间接地传输至致冷剂流；
连接于所述主热交换装置(12)的蒸馏塔(14)，用以接受所述的压缩的纯化进料空气(10)，从而产生富氮塔顶馏出物以及作为塔底产物的富氧液体；
冷凝装置(24)，用以至少将由所述富氮塔顶馏出物组成的富氮气流(20)的一部分(22)冷凝，并至少将所得冷凝液的一部分引入至所述的蒸馏塔(14)中作为回流，而且使所述第一冷却剂流(26)和第二冷却剂流(28)气化，从而形成所述的第一气化的冷却剂流(38)和第二气化的冷却剂流(40)，
所述冷凝装置(24)连接于蒸馏塔(14)，使所述的第一冷却剂流(26)由所述的富氧液体组成，而所述的第二冷却剂流(28)由其氮含量高于所述富氧液体的含氮液体组成，
所述冷凝装置(24)也连接于主热交换装置(12)，使所述的第一气化的冷却剂流(38)在所述主热交换装置(12)中部分加温；
置于所述的冷凝装置(24)与蒸馏塔(14)之间的第一和第二膨胀阀(32，34)，分别用以使所述第一和第二冷却剂流进行阀膨胀；
用以从富氮气流的另一部分(36)中热交换提取氮产物的装置(30)；
连接于所述的主热交换装置(12)的膨胀装置(42)，用以使所述的第一气化的冷却剂流(38)膨胀并作功，从而形成所述的致冷剂流(44)，
所述的主热交换装置(12)连接于所述的膨胀装置(42)，使所述的压缩的纯化空气(10)与致冷剂流(44)间接地进行热交换；和
连接于所述冷凝装置(24)的压缩机(46)，用以压缩所述的第二气化的冷却剂流(40)，
该压缩机(46)也连接于所述的主热交换装置(12)，使所述的第二气化的冷却剂流(40)在所述主热交换装置中冷却；和
所述的蒸馏塔(14)也在其底部区域连接于所述的主热交换装置(12)，将所述的第二气化的冷却剂流(40)，在全部冷却至适合精馏压缩的纯化空气的温度以后，接受至蒸馏塔内，从而提高所述的氮产物的回收率。
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Families Citing this family (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5689973A (en) * 1996-05-14 1997-11-25 The Boc Group, Inc. Air separation method and apparatus
JP2875206B2 (ja) * 1996-05-29 1999-03-31 日本エア・リキード株式会社 高純度窒素製造装置及び方法
US5924307A (en) * 1997-05-19 1999-07-20 Praxair Technology, Inc. Turbine/motor (generator) driven booster compressor
US5836175A (en) * 1997-08-29 1998-11-17 Praxair Technology, Inc. Dual column cryogenic rectification system for producing nitrogen
JP3719832B2 (ja) * 1997-10-14 2005-11-24 日本エア・リキード株式会社 超高純度窒素及び酸素の製造装置
US5868006A (en) * 1997-10-31 1999-02-09 The Boc Group, Inc. Air separation method and apparatus for producing nitrogen
US5934106A (en) * 1998-01-27 1999-08-10 The Boc Group, Inc. Apparatus and method for producing nitrogen
US6279345B1 (en) 2000-05-18 2001-08-28 Praxair Technology, Inc. Cryogenic air separation system with split kettle recycle
US6494060B1 (en) 2001-12-04 2002-12-17 Praxair Technology, Inc. Cryogenic rectification system for producing high purity nitrogen using high pressure turboexpansion
CN100443838C (zh) * 2005-04-20 2008-12-17 苏州市兴鲁空分设备科技发展有限公司 一种返流膨胀空气分离的方法和装置
CN100400995C (zh) * 2006-11-22 2008-07-09 苏州市兴鲁空分设备科技发展有限公司 空气分离的方法和装置
DE102007024168A1 (de) * 2007-05-24 2008-11-27 Linde Ag Verfahren und Vorrichtung zur Tieftemperatur-Luftzerlegung
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JP5415192B2 (ja) * 2009-03-16 2014-02-12 Ｊｆｅスチール株式会社 空気の成分分離方法および装置
EP2236964B1 (de) * 2009-03-24 2019-11-20 Linde AG Verfahren und Vorrichtung zur Tieftemperatur-Luftzerlegung
EP2662653A1 (de) 2012-05-08 2013-11-13 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung von wasserstofffreiem Stickstoff
EP2789958A1 (de) 2013-04-10 2014-10-15 Linde Aktiengesellschaft Verfahren zur Tieftemperaturzerlegung von Luft und Luftzerlegungsanlage
CN103776240B (zh) * 2014-01-13 2016-07-06 浙江海天气体有限公司 单压缩双增压双膨胀高纯氮制取装置
EP3059536A1 (de) 2015-02-19 2016-08-24 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung eines Druckstickstoffprodukts
EP3290843A3 (de) 2016-07-12 2018-06-13 Linde Aktiengesellschaft Verfahren und vorrichtung zur erzeugung von druckstickstoff und flüssigstickstoff durch tieftemperaturzerlegung von luft

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2120374B (en) * 1982-05-11 1985-09-18 Petrocarbon Dev Ltd Improvements in the production of nitrogen from air
JPS61110872A (ja) * 1984-11-02 1986-05-29 日本酸素株式会社 窒素製造方法
JPH05187767A (ja) * 1992-01-14 1993-07-27 Teisan Kk 超高純度窒素製造方法及びその装置
US5363657A (en) * 1993-05-13 1994-11-15 The Boc Group, Inc. Single column process and apparatus for producing oxygen at above-atmospheric pressure
US5396772A (en) * 1994-03-11 1995-03-14 The Boc Group, Inc. Atmospheric gas separation method

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