CN1117260C - 空气的分离方法和装置 - Google Patents
空气的分离方法和装置 Download PDFInfo
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Abstract
一种分离空气的方法和装置，其中，一含气相的氧气流从一单塔氮发生器中去出，然后被分成两个分流。这两个分流被冷凝，然后再相混合而在一汽提塔内进行汽提，以在塔底产生超高纯液氧。两个分流中的一个在一再沸器内和汽提塔的底部区域冷凝。两个分流中的另一个在一与氮汽提塔共同使用的塔顶冷凝器中冷凝。
Description
本发明涉及一种空气的分离方法及其装置，其中空气被分离以生产一种超高纯度液氧产品。具体地说，本发明涉及这样一种方法和装置，其中空气在一单塔氮发生器中被分离而产生含贫空气重组分的气相分馏物的氧气，该氧气液化后在一汽提塔中被去除空气轻组分。更具体地说，本发明涉及这样一种方法和装置，其中含气相分馏物的氧气被分成两个分流，它们分别在位于汽提塔内的再沸器中和单塔氮发生器的塔顶冷凝器中液化。
分离空气以产生富氧而贫二氧化碳、水和烃之类的重组分的分馏物，然后从由该富氧分馏物构成的液流中除去氮、氩、氖、氪和氦之类的轻组分，这种技术已经广为人知。例如，美国专利5,049,173揭示了一种单塔氮发生器，其中一液流从氮发生器中的一个位置处排出，该位置的液流是由富氧而贫重组分的液体构成。然后将液体导入汽提塔顶部在汽提塔内汽提，以产生一下降液相，其液氧越来越浓而轻组分越来越稀。
美国专利5,049,173还揭示了一种纯化从双塔蒸馏装置的高压塔中分离出的、含气相的氧气流的方法。接着，这种含气相的氧气流在被汽提之前在汽提塔的再沸器中被液化。为了从汽提塔中提取液体，必须将液氮加入汽提塔。在将由氮气所组成的液体加入含气相的液氧流中时存在一个问题，即汽提塔的尺寸必须适于汽提纯度比由富氧液体所组成的液流低的合成混合液流。而且，氮的产量将与所分离的液氮的量成正比。
如以下将要讨论的，本发明提供了一种分离空气的方法和装置，其中含贫重组分的气相的氧气流在汽提塔内被液化和汽提，无需液氮流回流加入汽提塔。
本发明提供了一种空气分离方法，其中，经压缩和纯化的空气流被冷却到一个适合于精馏的温度。然后，该空气流被精馏以产生含贫重组分的气相分馏物的氧气。由含气相分馏物的氧气组成的含氧流被分成两个分流，它们分开冷凝。这两个分流在冷凝后在汽提塔中被去除空气流内所存在的轻组分，使得汽提塔的塔底产生超高纯液氧。两个分流中的一个通过与汽提塔的塔底的间接热交换而冷凝，因而在汽提塔内产生沸腾。
在本发明的另一个方面，提供了一种空气分离装置，它具有一将经压缩和纯化的空气流冷却到一个适合于精馏的温度的装置。它装有一个用于精馏该空气流的装置以产生含贫重组分的气相分馏物的氧气。汽提塔在其底部区域装有一再沸器，以使汽提塔内沸腾。该再沸器与精馏装置相连，使得由含气相分馏物的氧气组成的两个分流中的一个在该再沸器内冷凝。该精馏装置还连接一个装置用来冷凝两个分流中的另一个。该冷凝装置和再沸器连接于汽提塔的顶部，使得这两个分流在汽提塔内去除轻组分，并且在汽提塔内的底部产生超高纯液氧。
由以上描述可知，本发明适用于与具有一再沸器的超高纯液氧汽提塔结合的单塔氮发生器。由于两个液流分开冷凝，因而汽提塔只需要设计成能汽提富氧分馏物，而不是汽提与氮气相混合的富氧分馏物。而且在具有氮发生器的情况下，另一个分流可在一与其共同使用的塔顶冷凝器内冷凝。这当然会减小氮的产量。然而，如果液氮被分离的话，减小量也会较小，因为是用冷却介质，通常为富氧液体，来冷凝此分流的，而不是用液体。因此，氮的产量不会达到现有技术的氧气纯化方式所达到的程度，在现有技术中，为了在汽提塔内进一步纯化，需要分离含气相分馏物的氧气。
在说明书和权利要求书中所用的高纯氮，其杂质氧含量小于十亿分之一百(以体积计)。超高纯液氧的杂质(除氧以外的杂质)小于十亿分之一百(以体积计)。并且，说明书和权利要求书中所用的术语“充分加热”是指加热到一个主热交换器或主热交换设备的热端的温度。说明书和权利要求书中所用的术语“充分冷却”是指冷却到一个主热交换器或主热交换设备的冷端的温度。说明书和权利要求书中所用的“部分加热”或“部分冷却”是指加热或冷却到一个介于主热交换器或主热交换设备的热端温度和冷端之间的温度。另外，说明书和权利要求书中所用的术语“轻组分”包括氮、氩、氖、氦和氢，但并不限于这些物质，术语“重组分”包括二氧化碳、水、氪和烃，但并不限于这些物质。
虽然说明书所附的权利要求书明确指出了申请人认为是其发明的主要内容，但是相信，结合附图将能更好地理解本发明，这一附图是本发明的装置和方法的示意图。
参照附图，图中示出了一空气分离装置1，它设计用来将空气分离成高纯氮分馏物和超高纯液氧分馏物。空气在用现有技术中的一种公知的方法进行压缩和纯化后，于一热交换设备10内冷却到一个适合于精馏的温度，该温度一般等于或接近于空气的露点。然后，空气在一单塔氮发生器12内精馏成塔顶馏出物为高纯富氮分馏物和塔底物为富氧液体分馏物。一种含气相分馏物的氧气从单塔氮发生器12中的一个位置处取出，该位置的气相分馏物是贫重组分的。在冷凝后，该气相分馏物在一汽提塔14内汽提以产生超高纯液氧产品。这里值得一提的是，本发明并不限于单塔氮发生器，实际上，它能广泛适用于各种多塔装置。上面概括地描述了装置1的操作，下面将进行详细描述。
如上所述在热交换设备10内冷却的压缩和纯化的空气流16，是通过压缩空气、撤走压缩热、然后除去二氧化碳、水分和烃之类的重组分而形成的。然而，应该注意的是，即使在经过这样的纯化后，经压缩和纯化的空气流16中仍存在有此类重组分，它们将集中在精馏所产生的液体分馏物中。
然后，压缩和纯化空气流16导入单塔氮发生器12。单塔氮发生器12具有液体-蒸气接触构件，如塔盘、不规整或结构填料，以将空气精馏成高纯度、富氮和富氧液体分馏物。产生产品氮流18，它由高纯度的富氮分馏物组成。产品氮流18的一部分20在一塔顶冷凝器22内冷凝，然后回流循环到单塔氮发生器12。关于这一点，塔顶冷凝器22是一个板-翅片结构的单通路装置。产品氮流18的其余部分24在主热交换设备10内被充分加热，在那里它作为产品氮(PGN)于环境温度下被排出。
通过取出一液体空气流26和一液体富氧流28的方法，将冷却介质供给塔顶冷凝器22。液体空气流26和液体富氧流28分别在阀30和32内由阀调节膨胀，并在塔顶冷凝器22内汽化。汽化的液体空气流26又在一循环压缩机34内被压缩至单塔氮发生器12的操作压力，以产生一循环流36，它在热交换设备10内经过部分冷却后导入单塔氮发生器12的底部区域。在所示的实施例中，循环流36没有被充分冷却，以防止其液化。富氧液体流28在汽化后被导入一涡轮膨胀器38以产生一冷冻介质流40。冷冻介质流40可与其它废流相混合，而后在主热交换设备10内被充分加热，成一废氮流42。这样的加热可减小进入空气的热函，以补偿诸如热量漏入空气分离装置1之类的不可逆性。循环压缩机34和涡轮膨胀器38可以通过一耗能油闸或一种发生器或类似物相连，使得膨胀做功的若干能量可回收用来驱动循环压缩机34。
应该注意的是，本发明的实施例也可使用一个组分与富氧液流28相同的液流作塔顶冷凝器22的专门的冷却介质，用后可循环回到塔内。但是，如图所示采用汽化液体空气流26将特别有利，因为其含氮量比富氧液流28更高。因此，对于相同温度的富氧液体来说，它具有更高的露点压力。因而，汽化的液体空气流26对压缩机的供给压力将更高，这样，相同量的功就可以压缩更多的流体。这种流体的增加便于增加热泵作用，可增加回收，超过在将富氧液流28再循环回到塔内的情况下应该得到的。而且，汽化的液体空气流26的流体组分接近于塔釜内的平衡蒸气组分。这允许塔底的操作比现有技术的更为可逆。
含贫重组分的气相分馏物的氧从单塔氮发生器12中作为含气相的氧气流46而被排出，它被分成两个分流48和50。分流48经过一位于汽提塔14底部区域54内的再沸器52被冷凝。这可使汽提塔14沸腾。然后，所得到的冷凝物由减压阀5 6减压。另一个分流50在塔顶冷凝器22内冷凝，然后由减压阀58减压。两个分流48和50混合后被导入汽提塔14进行汽提，因而以超高纯液氧产品流60的形式产生超高纯液氧。
虽然以上参照—较佳实施例描述了本发明，但本技术领域的技术人员可以在不脱离本发明的精神和范围的情况下对其进行各种变化、补充和省略。
Claims (10)
1.一种空气分离方法，包括：
将经压缩和纯化的空气冷却到一个适合于精馏的温度；
精馏所述空气流以产生一含贫重组分的气相分馏物的氧；
将含气相分馏物的氧分成两个分流；
分开冷凝所述两个分流，并在一汽提塔中除去所述两个分流中的空气流轻组分，使得在所述汽提塔内的底部产生超高纯液氧；
两个分流中的一个通过与所述汽提塔的塔底的间接热交换而冷凝，以在所述汽提塔中产生沸腾。
2.如权利要求1所述的空气分离方法，其特征在于：
所述空气流在一单塔氮发生器中精馏，以产生一产品氮流；
连接于所述单塔氮发生器的塔顶冷凝器冷凝部分所述产品氮流，以产生对所述单塔氮发生器的回流；
所述产品氮流的其余部分被充分加热；所述两个分流中的另一个在所述塔顶冷凝器内冷凝。
3.如权利要求2所述的空气分离方法，其特征在于：
所述塔顶冷凝器的冷却介质是通过从所述单塔氮发生器中提取一液流并用阀调节膨胀所述液流而产生；
所述液流在所述塔顶冷凝器内汽化；
所述液流在汽化后再被压缩到所述单塔氮发生器的塔压，冷却到所述适合于精馏的温度，并循环进入所述单塔氮发生器。
4.如权利要求3所述的空气分离方法，进一步包括：
通过从所述单塔氮发生器的底部区域排出富氧液流并用阀调节膨胀所述富氧液流而向所述塔顶冷凝器提供另外的冷却介质；
在所述塔顶冷凝器中汽化所述富氧液流，并部分加热所述汽化的富氧液流；
用涡轮膨胀所述富氧液流，以产生一冷冻介质流；
通过在所述压缩和纯化的空气流内间接热交换而充分加热所述冷冻介质流，从而增加冷冻。
5.如权利要求4所述的空气分离方法，其特征在于，所述汽提塔塔顶馏出物与所述冷冻介质流和所述产品氮流的其余部分一起，通过与所述进压缩和纯化的空气流间接热交换而充分加热。
6.一种空气分离装置，包括：
用于将一压缩和纯化的空气流冷却到一个适合于精馏的温度的装置；
用于精馏所述空气流以产生一含贫重杂质的气相分馏物的氧的装置；
一汽提塔，其底部区域具有一再沸器，以使所述汽提塔内产生沸腾；
所述再沸器连接于所述精馏装置，使得由所述含气相分馏物的氧组成的两个分流中的一个在所述再沸器内冷凝；
同样连接于所述精馏装置的、用于冷凝所述两个分流中的另一个的装置；
所述冷凝装置和所述再沸器连接到所述汽提塔的顶部区域，使得所述两个分流在所述汽提塔内除去轻杂质，因而在所述汽提塔中的塔底产生超高纯液氧。
7.如权利要求6所述的空气分离装置，其特征在于：
所述精馏装置包括一单塔氮发生器，以产生一产品氮流；
所述单塔氮发生器连接有一塔顶冷凝器，以冷凝部分所述产品氮流，进而对所述单塔氮发生器产生回流；
所述塔顶冷凝器配置成可接收和冷凝所述两个分流中的另一个，因而用作所述冷凝装置；
所述冷却装置充分加热所述产品氮流的其余部分。
8.如权利要求7所述的空气分离装置，其特征在于：
所述塔顶冷凝器还配置成可接收来自该发生器的液流作为所述塔顶冷凝器的冷却介质，因而所述液流在所述塔顶冷凝器中汽化；
所述塔顶冷凝器和所述单塔氮发生器之间设有一膨胀阀，以用阀调节来膨胀所述液流；
所述塔顶冷凝器连接有一循环压缩机，以将汽化后的所述液流压缩到所述单塔氮发生器的塔压；
所述冷却装置同样将在经过所述汽化和再压缩后的所述液流冷却到所述适合于精馏的温度；
所述单塔氮发生器连接于所述冷却装置，使得所述液流在冷却后循环到所述单塔氮发生器内。
9.如权利要求8所述的空气分离装置，其特征在于，进一步包括：
所述塔顶冷凝器还连接于所述单塔氮发生器，并配置成可接收来自所述单塔氮发生器的富氧液流作为附加的冷却介质，因而汽化所述富氧液流；
在所述塔顶冷凝器和所述单塔氮发生器之间设有另一个膨胀阀，用来以阀调节膨胀所述富氧液流；
所述冷却装置部分加热所述汽化的富氧液流；
所述冷却装置连接有一涡轮膨胀器，使得所述富氧液流被用涡轮膨胀而产生一冷冻介质流；
所述冷却装置通过与所述经压缩和纯化的空气流间接热交换而充分加热所述冷冻介质流，从而增加冷冻。
10.权利要求9的空气分离装置，其特征在于：所述冷却装置通过与所述压缩和纯化的空气流间接热交换来充分加热所述汽提塔塔顶馏出物和所述冷冻介质流，以及所述产品氮流的所述其余部分。
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US08/649,147 US5689973A (en) | 1996-05-14 | 1996-05-14 | Air separation method and apparatus |
| US08/649147 | 1996-05-14 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1177726A CN1177726A (zh) | 1998-04-01 |
| CN1117260C true CN1117260C (zh) | 2003-08-06 |
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| CN97111583A Expired - Fee Related CN1117260C (zh) | 1996-05-14 | 1997-05-13 | 空气的分离方法和装置 |
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| US (1) | US5689973A (zh) |
| EP (1) | EP0807792B1 (zh) |
| JP (1) | JP3940461B2 (zh) |
| KR (1) | KR100207890B1 (zh) |
| CN (1) | CN1117260C (zh) |
| AT (1) | ATE211248T1 (zh) |
| AU (1) | AU737791B2 (zh) |
| CA (1) | CA2202010C (zh) |
| DE (1) | DE69709234T2 (zh) |
| ID (1) | ID19527A (zh) |
| IL (1) | IL120550A (zh) |
| MY (1) | MY115081A (zh) |
| PL (1) | PL185432B1 (zh) |
| SG (1) | SG50821A1 (zh) |
| TR (1) | TR199700338A2 (zh) |
| TW (1) | TW355146B (zh) |
| ZA (1) | ZA973115B (zh) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101424478A (zh) * | 2007-10-25 | 2009-05-06 | 林德股份公司 | 用于低温空气分馏的方法 |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US5924307A (en) * | 1997-05-19 | 1999-07-20 | Praxair Technology, Inc. | Turbine/motor (generator) driven booster compressor |
| US6279345B1 (en) * | 2000-05-18 | 2001-08-28 | Praxair Technology, Inc. | Cryogenic air separation system with split kettle recycle |
| US6460373B1 (en) | 2001-12-04 | 2002-10-08 | Praxair Technology, Inc. | Cryogenic rectification system for producing high purity oxygen |
| FR2860576A1 (fr) * | 2003-10-01 | 2005-04-08 | Air Liquide | Appareil et procede de separation d'un melange gazeux par distillation cryogenique |
| US20070204652A1 (en) * | 2006-02-21 | 2007-09-06 | Musicus Paul | Process and apparatus for producing ultrapure oxygen |
| DE102007024168A1 (de) * | 2007-05-24 | 2008-11-27 | Linde Ag | Verfahren und Vorrichtung zur Tieftemperatur-Luftzerlegung |
| DE102007051184A1 (de) * | 2007-10-25 | 2009-04-30 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Tieftemperatur-Luftzerlegung |
| EP2789958A1 (de) | 2013-04-10 | 2014-10-15 | Linde Aktiengesellschaft | Verfahren zur Tieftemperaturzerlegung von Luft und Luftzerlegungsanlage |
| KR101637292B1 (ko) | 2015-02-16 | 2016-07-20 | 현대자동차 주식회사 | 환류 세퍼레이터를 구비한 가스 응축 장치 |
| US10408536B2 (en) * | 2017-09-05 | 2019-09-10 | Praxair Technology, Inc. | System and method for recovery of neon and helium from an air separation unit |
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| JPS61110872A (ja) * | 1984-11-02 | 1986-05-29 | 日本酸素株式会社 | 窒素製造方法 |
| US4867772A (en) * | 1988-11-29 | 1989-09-19 | Liquid Air Engineering Corporation | Cryogenic gas purification process and apparatus |
| US5049173A (en) * | 1990-03-06 | 1991-09-17 | Air Products And Chemicals, Inc. | Production of ultra-high purity oxygen from cryogenic air separation plants |
| US5205127A (en) * | 1990-08-06 | 1993-04-27 | Air Products And Chemicals, Inc. | Cryogenic process for producing ultra high purity nitrogen |
| US5385024A (en) * | 1993-09-29 | 1995-01-31 | Praxair Technology, Inc. | Cryogenic rectification system with improved recovery |
| US5582034A (en) * | 1995-11-07 | 1996-12-10 | The Boc Group, Inc. | Air separation method and apparatus for producing nitrogen |
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1996
- 1996-05-14 US US08/649,147 patent/US5689973A/en not_active Expired - Lifetime
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- 1997-04-09 JP JP09043997A patent/JP3940461B2/ja not_active Expired - Fee Related
- 1997-04-11 ZA ZA9703115A patent/ZA973115B/xx unknown
- 1997-04-15 ID IDP971250A patent/ID19527A/id unknown
- 1997-04-17 SG SG1997001257A patent/SG50821A1/en unknown
- 1997-05-02 TR TR97/00338A patent/TR199700338A2/xx unknown
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- 1997-05-12 PL PL97319928A patent/PL185432B1/pl not_active IP Right Cessation
- 1997-05-13 EP EP97303252A patent/EP0807792B1/en not_active Expired - Lifetime
- 1997-05-13 AT AT97303252T patent/ATE211248T1/de not_active IP Right Cessation
- 1997-05-13 CN CN97111583A patent/CN1117260C/zh not_active Expired - Fee Related
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101424478A (zh) * | 2007-10-25 | 2009-05-06 | 林德股份公司 | 用于低温空气分馏的方法 |
Also Published As
| Publication number | Publication date |
|---|---|
| KR970075808A (ko) | 1997-12-10 |
| DE69709234T2 (de) | 2002-08-14 |
| ID19527A (id) | 1998-07-16 |
| TR199700338A2 (xx) | 1997-12-21 |
| ATE211248T1 (de) | 2002-01-15 |
| CA2202010A1 (en) | 1997-11-14 |
| EP0807792B1 (en) | 2001-12-19 |
| MY115081A (en) | 2003-03-31 |
| AU1773397A (en) | 1997-11-20 |
| PL185432B1 (pl) | 2003-05-30 |
| JPH1047853A (ja) | 1998-02-20 |
| IL120550A (en) | 2000-08-13 |
| ZA973115B (en) | 1997-11-05 |
| JP3940461B2 (ja) | 2007-07-04 |
| TW355146B (en) | 1999-04-01 |
| IL120550A0 (en) | 1997-07-13 |
| CA2202010C (en) | 2000-03-21 |
| SG50821A1 (en) | 1998-07-20 |
| AU737791B2 (en) | 2001-08-30 |
| MX9703268A (es) | 1997-11-29 |
| DE69709234D1 (de) | 2002-01-31 |
| US5689973A (en) | 1997-11-25 |
| EP0807792A2 (en) | 1997-11-19 |
| CN1177726A (zh) | 1998-04-01 |
| PL319928A1 (en) | 1997-11-24 |
| KR100207890B1 (ko) | 1999-07-15 |
| EP0807792A3 (en) | 1998-03-11 |
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