CN1141547C - 氮的产生方法和设备 - Google Patents
氮的产生方法和设备 Download PDFInfo
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Abstract
一种在单塔氮发生器中通过分离空气而产生氮的方法和装置。通过作为塔底产物的富氧液流的气化而使富氮气体冷凝形成回流。气化的富氧流在循环压缩机中被部分地重新压缩、冷却并再引回至蒸馏塔,以提高氮的产率。气化的富氧流也部分地膨胀并作功。膨胀功被用于进行压缩。用一个氮液化单元产生的补充致冷剂流可使氮以液体形式回收,并增加可用于压缩的膨胀功的数量。
Description
本发明涉及一种氮的产生方法和设备,在这种方法中,使空气在蒸馏塔中分离为富氮气体和富氧液体馏分。具体地,本发明涉及这样的方法和设备,其中的富氧液体在塔顶冷凝器中气化后,被再次压缩并重新引入塔内,同时部分地膨胀作功,将这些功应用于再压缩。更具体地,本发明涉及这样的方法和设备,其中利用补充的致冷剂流,以增加可用以再压缩气化的富氧液体的膨胀功的数量。
现有技术中有许多方法和设备,将空气在蒸馏塔中蒸馏,产生富氮气体作为产物。例如,美国专利4,966,002公开了一种高纯氮气的制备方法,它采用以废料再压缩循环为特征的单蒸馏塔低温精馏法。在一种使用单个蒸馏塔的空气分离方法和设备中,将空气过滤、压缩和纯化后,在一主热交换器中冷却至适于其精馏的温度。然后将这空气引入至单个蒸馏塔内分离为富氮气体和富氧液体馏分。为了使蒸馏塔回流,使用一个塔顶冷凝器,在其中用富氧液体来使富氮气体冷凝。而气化的富氧液体被再压缩并重新引入至蒸馏塔以提高氮的产量。这压缩操作可在主热交换器的温端或冷端的温度下进行。可将一部分气化的富氧液体部分地加热,然后令其膨胀作功。人们会想到把全部的这种膨胀功用来再压缩气化的富氧液体。但是,对于压缩是在主热交换器冷端的温度下进行的情形,产生的压缩热须在主热交换器内消散。最终结果将是不会产生净致冷作用。于是很大一部分膨胀功必须通过一个耗能的制动器将其排出装置之外。
一般来说,上述的这类装置,以气体作为全部产品。为了使产品转化为液体,气体产品必须在分开的液化器中液化。这样的液化不能不增加能耗。同时,如果要得到高纯度的氮,液化所涉及的设备还会污染氮发生器所产生的高纯氮。于是,如果这种液态氮要用于高纯度的用途的话,必须在液化的下游提供对液氮的净化。
如下文所述,本发明提供一种氮的产生方法和设备,其中有更多的膨胀功可应用于压缩,从而更有效地利用能量以提高液态氮的产量。而且,这种液态氮的产生无需使用下游的液化器。
本发明提供一种生产氮的方法,本方法包括将压缩、纯化的进料空气冷却至适于进行精馏的温度。然后将该压缩、纯化的进料空气引入至蒸馏塔内,产生高纯度的富氮塔顶产物(本文与权利要求中的“高纯度”指的是氧含量小于100ppb),以及富氧液体作为塔底产物。至少一部分由富氮的塔顶产物构成的富氮气流被冷凝,而所得冷凝液的一部分被引回至蒸馏塔作为回流。而从所得冷凝液的剩余部分形成氮产品流。将一股循环气流压缩并冷却至适合于进料空
气进行精馏的温度。该循环气流被引入至蒸馏塔内以提高氮产品的回收率。一股致冷剂流膨胀作功,形成主致冷剂流。在主致冷剂流与压缩的、纯化空气之间进行间接热交换。膨胀功的一部分被用来压缩所述循环气流。使一股补充致冷剂流气化然后重新液化。该补充致冷剂流至少部分地通过与至少一部分富氮气流之间的间接热交换而气化,从而帮助实现一部分富氮气流的冷凝。在补充致冷剂流再液化之前,使所述补充致冷剂流与压缩的纯化空气进行间接热交换,以增加可用以进行压缩的功,使它大于不加入补充致冷作用时所能得到的数量。这可增强压缩作用,进一步提高氮产物的回收率。
另一方面,本发明提供一种氮气发生器。它装有一个主热交换装置,将压缩的、纯化进料空气冷却至适于进行精馏的温度。一个蒸馏塔连接于主热交换装置,将压缩的、纯化进料空气精馏,从而产生高纯度的富氮塔顶产物以及富氧液体塔底产物。 蒸馏塔装有一个塔顶冷凝器,用以将由富氮塔顶产物组成的富氮气流的至少一部分冷凝,并将冷凝液的一部分引回至蒸馏塔作为回流,而将冷凝液的剩余部分回收作为产物流。用一个压缩机来压缩循环气流,在压缩机和蒸馏塔之间插入主热交换器,使循环流体冷却至空气进行精馏的温度,并引入至蒸馏塔内,以提高氮产物的回收率。有一个涡轮膨胀器让致冷剂流膨胀并作功,形成主致冷剂流。涡轮膨胀器连接于主热交换器,使主致冷剂流与压缩的纯化空气间接地进行热交换。有一个装置将涡轮膨胀器与压缩机耦合起来,使所作的功的一部分用以压缩循环气流。有一个补充致冷剂回路,用以循环在循环过程中气化的补充致冷剂流。补充致冷剂回路包括塔顶冷凝器和主热交换器。塔顶冷凝器的结构是使得至少有一部分补充致冷剂流通过与至少一部分富氮气流的间接热交换而被气化。主热交换器的结构也使补充致冷剂流与压缩的纯化空气间接地进行热交换,以增加可用以进行压缩的功,使它大于不加入补充致冷作用时所能得到的数量。这将增加压缩,并进一步提高氮产物的回收率。补充致冷剂回路也包括处于主热交换器与塔顶冷凝器之间的液化器,以将被气化的补充致冷剂流重新液化。
增加了补充致冷剂流,可将更多的膨胀功用来压缩气化的富含液氧的流体,以便再引回至蒸馏塔内。于是,对于给定供料率的空气,可产生更多的氮,而且可有更多的氮作为液体从塔顶冷凝器回收。如以下所述,补充致冷剂流可以是氮流,它在主热交换器内将其补充致冷作用给予生产装置。但是,由于这补充致冷剂流离开主热交换器时并无很高的压降,再液化所需的能量要比将气化的氮流用不结合在装置内的液化器单独液化时所需的少。因此,可比现有技术节约能量而产生更多的液态氮。而且,由于可在本发明的氮产生器中发生高纯度的氮,而液化器是通过间接热交换而结合在装置中的,对产品不会产生污染;如果液化器是装在氮发生器下游用来液化氮产物的,就可能会发生污染。
说明书后的权利要求书清楚地指出了申请人认为是其发明的内容,但参照附图将可更好地理解本发明,其中:
图1是本发明的氮发生器的示意图;
图2是装在图1所示氮发生器中的氮液化器的示意图;
参看图1,图中显示了本发明的氮发生器1。将空气过滤去除尘埃微粒后压缩,然后纯化去除二氧化碳和水。随后,空气在主热交换器11内冷却成适合进行精馏的温度下的空气流10。空气流10被引入至蒸馏塔12,该蒸馏塔的结构是产生一种富氧液体作为塔底产物以及一种高纯度富氮气体作为塔顶产物。
由富氮气体产生富氮气流14。富氮气流14的一部分16在塔顶冷凝器18中冷凝,产生冷凝的液流20。该冷凝液流的一部分22再被引回至蒸馏塔12。另一部分(在图中所示的实施例中是冷凝液流20的剩余部分)作为液体产物流23被引出,这产物流在送去贮藏前最好先在辅助冷却单元24中冷却,然后再用膨胀阀26进行阀膨胀。本领域的技术人员会想到,图示实施例的一种可能的变化方式是产物流包括富氮气流14的另一部分。
富氧液流28在辅助冷却单元30中冷却,然后通过膨胀阀32膨胀至足够低的温度,以便将上述富氮气流14的一部分16冷凝。富氧液流28在膨胀后被引入到塔顶冷凝器18内,产生气化的富氧液流34。
气化的富氧液流的一部分36在循环压缩器38内被重新压缩,然后在主热交换器11的11B区内冷却至蒸馏塔12的温度。此时经压缩的、气化的富氧液流被再引入至蒸馏塔12中。气化的富氧液流34的剩余部分40被加温至一中间温度,该温度高于进行空气精馏的温度。这也发生在主热交换器11的11B区内。该富氧液流的剩余部分40形成一股致冷剂流,它在涡轮膨胀器42中膨胀,产生主致冷剂流44。涡轮膨胀器42耦合于压缩机38。膨胀功的一部分通过消耗能量的制动器46或可能是一个发电机消耗掉,膨胀功的其余部分则用来为压缩机38供给功率。主致冷剂流44在辅助冷却单元30中加温,然后再在主热交换器11中完全加温,在该处作为废料排出装置之外。
应注意本发明的实施方式中,可以在塔底以上的某个部分引出一股液流,然后,在其使用于蒸馏过程而气化之后,将它重新压缩,冷却并再引入至蒸馏塔内。此外,本发明并不限于其中有由气化的塔底液体形成的致冷剂流的氮发生装置。
由下文将要说明的氮液化单元(图中标为NLU)提供一股补充致冷剂流48。补充致冷剂流48的一部分50在塔顶冷凝器18内气化,然后在辅助冷却单元30中进一步加温。随后它被引入至主热交换器11中,在其中被充分加温,然后送回至氮液化单元中。本发明的另一种可能的实施方式是补充致冷剂流在塔顶冷凝器18内部分气化,然后在主热交换器11内完全气化。
这样就给氮产生器1提供了补充致冷作用。输入的补充致冷剂流的剩余部分51在阀52内进行阀膨胀,然后在相分离器54内进行相分离,产生液流56。液流56对液体产物流23进行辅助冷却。由补充致冷剂分离出来的气相构成的气流58与流56合并起来,作为流59返回至氮液化单元。
参看图2,图中显示了本发明的氮液化单元2。补充致冷剂流48的一部分50与循环流60和气流59合并起来,气流59先按下文所述方式加温。所得到的合并起来的气流在压缩单元62中被再压缩,形成压缩的气流64。压缩热用后冷却器66使之从压缩气流64中排出。然后将压缩气流64引入第一辅助压缩机68,而压缩热用第一后冷却器70使之排出。再把压缩气流64引入第二辅助压缩机72,压缩热通过第二后冷却器74排出压缩气流64之外。此后,压缩气流64的主要部分在热交换器76内冷却,并通过阀77进行阀膨胀至液化,产生补充致冷剂流48。
在压缩气流64在热交换器76内部分地冷却之后,从该气流64中分出一附属气流78。附属气流78在连接于第二辅助压缩机72的第一涡轮膨胀器80之内膨胀。在分出附属气流78之后,压缩气流64进一步冷却,再由它分出附属气流84。附属气流84在第二涡轮膨胀器86内膨胀,该膨胀器在低于第一涡轮膨胀器80的温度运行。第二涡轮膨胀器86连接于第一辅助压缩机68。所得的膨胀后的气流88然后在热交换器76内部分地加温,并与膨胀后的气流82合并成为循环流60。循环流60在与进入液化单元2的补充致冷剂流48的一部分50合并之前先在主热交换器76内充分加温。
本领域技术人员会理解,虽然上面参照较佳实施例对本发明作了说明,但可在不背离本发明的实质和范围的情况下作出各种变化、增加和删减。
Claims (8)
1.一种制备氮的方法,该方法包括:
将经压缩的纯化进料空气(10)冷却至适合精馏的温度;
将所述经压缩的纯化进料空气(10)引入蒸馏塔(12),产生高纯度的富氮塔顶产物(14)与富氧液体塔底产物(28);
使由上述富氮塔顶产物构成的富氮气流(14)的至少一部分(16)冷凝,并将所得冷凝液(20)的一部分(22)引入至所述的蒸馏塔(12)作为回流;
从所得冷凝液的剩余部分(23)形成氮产物流;
压缩一股由部分气化的富氧液流(34)形成的循环流(36),使该循环流冷却至所述温度,并将其引入至所述蒸馏塔以提高所述氮产物的回收率;
使由所述气化的富氧液流(34)的剩余部分(40)形成的致冷剂流膨胀作功,形成主致冷剂流(44),并使该主致冷剂流(44)与所述经压缩的纯化空气(10)和所述循环流(36)进行间接热交换;
将一定数量的上述膨胀功用于所述对循环气流(36)的压缩;
使来自氮液化单元的补充致冷剂流(48)气化然后重新液化;
所述补充致冷剂流(48)通过与所述富氮气流(14)的至少一部分(16)进行间接热交换而至少部分地气化,从而帮助实现所述一部分富氮气流(16)的冷凝;以及
在所述补充致冷剂流(48)重新液化之前,使该补充致冷剂流(48)与所述经压缩的纯化空气(10)和循环流(36)进行间接热交换,以增加可用以进行所述压缩的所述膨胀功的数量,使其大于不加入补充致冷作用时所能获得的数量,从而进一步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:由所述蒸馏塔中引出一股所述富氧液体流,进行阀膨胀,并与所述富氮气流进行间接热交换,以帮助使该富氮气流的至少一部分冷凝,从而形成所述气化的富氧流。
3.如权利要求2所述的方法,其特征还在于所述补充致冷剂流通过与所述氮塔顶产物的间接热交换而完全气化。
4.如权利要求3所述的方法,其特征还在于所述补充致冷剂流是通过在两个温度水平下压缩该补充致冷剂流和使该补充致冷剂流膨胀而液化的。
5.如权利要求2所述的方法,其特征还在于所述氮产物包含所述冷凝液的一部分,并且分为两股产物流;
其中一股产物流通过与所述经压缩的纯化空气进行间接热交换而气化;
另一股产物流通过与由所述补充致冷剂流的一部分所组成的附属流的间接热交换而被低温冷却;以及
所述附属流在液化之前先与所述补充致冷剂流的剩余部分合并起来。
6.一种氮发生器,它包括:
主热交换器(11),其结构是使经压缩的纯化进料空气(10)冷却至适合于精馏的温度;
连接于上述主热交换器(11)的蒸馏塔(12),用以精馏所述经压缩的纯化进料空气(10),产生高纯度富氮塔顶产物(14)和富氧液体塔底产物(28);
连接于上述蒸馏塔(12)的塔顶冷凝器(18),用以冷凝由所述富氮塔顶产物构成的富氮气流(14)的至少一部分(16),并将所得冷凝液(20)的一部分(22)引回至蒸馏塔(12)内作为回流,而将所得冷凝液(20)的剩余部分作为产物流排出装置之外;
一个压缩机(38),用以压缩由部分气化的富氧液流(34)形成的循环气流(36);
所述主热交换器(11)置于所述压缩机(38)与所述蒸馏塔(12)之间,使所述循环流(36)冷却至所述温度,并引入至蒸馏塔(12)中,以提高所述氮产物的回收率;
一个涡轮膨胀器(42),用以使由所述气化的富氧液流(34)的剩余部分(40)形成的致冷剂流膨胀并作功,形成主致冷剂流(44);
所述涡轮膨胀器(42)连接于所述主热交换器(11),使主致冷剂流(44)与经压缩的纯化空气(10)进行间接热交换;
将所述涡轮膨胀器(42)与所述压缩机(38)相互耦合的装置,使一定数量的所述膨胀功用于进行所述循环气流的压缩;以及
一补充致冷剂回路,用以环流在环流过程中气化的补充致冷剂流,所述补充致冷剂回路包括,
所述塔顶冷凝器(18),该塔顶冷凝器的结构是使得所述补充致冷剂流(48)通过与所述富氮气流(14)的至少一部分(16)的间接热交换而至少部分地气化,
所述主热交换器(11),该主热交换器(11)的结构也是使得补充致冷剂流(48)与所述经压缩的纯化空气(10)进行间接热交换,从而增加可用于所述压缩的所述膨胀功的数量,使它大于不加入补充致冷作用时所能获得的数量,从而进一步提高所述氮产物的回收率,和
一个氮液化单元,它置于所述主热交换器与所述塔顶冷凝器之间,用以使所述补充致冷剂流在气化之后重新液化。
7.如权利要求6所述的氮发生器,其特征在于它还包括:
所述塔顶冷凝器,其结构也可使所述富氧液流发生间接热交换;
一个膨胀阀,置于所述塔顶冷凝器与所述蒸馏塔之间,用以使所述富氧液流进行阀膨胀,从而形成气化的富氧流;
所述压缩机和涡轮膨胀器连接于所述塔顶冷凝器,使所述循环气流包含所述气化的富氧液流的一部分,而所述致冷剂流包含该气化的富氧液流的其余部分。
8.如权利要求6所述的氮发生器,其特征还在于补充致冷剂流液化器包括具有在两个不同温度水平运行的两个涡轮膨胀器的一个氮液化器。
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DE102008064117A1 (de) | 2008-12-19 | 2009-05-28 | Linde Ag | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft |
CN101492156B (zh) * | 2009-03-12 | 2010-12-29 | 四川空分设备(集团)有限责任公司 | 低能耗制氮方法和装置 |
EP2236964B1 (de) | 2009-03-24 | 2019-11-20 | Linde AG | Verfahren und Vorrichtung zur Tieftemperatur-Luftzerlegung |
US8720591B2 (en) | 2009-10-27 | 2014-05-13 | Engineered Corrosion Solutions, Llc | Controlled discharge gas vent |
US9726427B1 (en) | 2010-05-19 | 2017-08-08 | Cosmodyne, LLC | Liquid nitrogen production |
US20130341055A1 (en) | 2012-05-31 | 2013-12-26 | Engineered Corrosion Solutions, Llc | Electrically operated gas vent for fire protection sprinkler systems |
EP2789958A1 (de) | 2013-04-10 | 2014-10-15 | Linde Aktiengesellschaft | Verfahren zur Tieftemperaturzerlegung von Luft und Luftzerlegungsanlage |
CN108601964B (zh) * | 2015-02-14 | 2021-09-21 | 泰科消防产品有限合伙公司 | 用于强制通风空隙空间的水雾保护 |
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JP2020521098A (ja) * | 2017-05-16 | 2020-07-16 | イーバート,テレンス,ジェイ. | 気体を液化するための装置およびプロセス |
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GB975729A (en) * | 1963-11-12 | 1964-11-18 | Conch Int Methane Ltd | Process for the separation of nitrogen and oxygen from air by fractional distillation |
US3370435A (en) * | 1965-07-29 | 1968-02-27 | Air Prod & Chem | Process for separating gaseous mixtures |
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GB2126700B (en) * | 1982-09-15 | 1985-12-18 | Petrocarbon Dev Ltd | Improvements in the production of pure nitrogen |
US4655809A (en) * | 1986-01-10 | 1987-04-07 | Air Products And Chemicals, Inc. | Air separation process with single distillation column with segregated heat pump cycle |
US5006137A (en) * | 1990-03-09 | 1991-04-09 | Air Products And Chemicals, Inc. | Nitrogen generator with dual reboiler/condensers in the low pressure distillation column |
US5275003A (en) * | 1992-07-20 | 1994-01-04 | Air Products And Chemicals, Inc. | Hybrid air and nitrogen recycle liquefier |
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US5363657A (en) * | 1993-05-13 | 1994-11-15 | The Boc Group, Inc. | Single column process and apparatus for producing oxygen at above-atmospheric pressure |
-
1995
- 1995-12-18 US US08/573,838 patent/US5611218A/en not_active Expired - Lifetime
-
1996
- 1996-09-30 IL IL11933396A patent/IL119333A/xx not_active IP Right Cessation
- 1996-10-02 AU AU67979/96A patent/AU725907B2/en not_active Ceased
- 1996-10-03 SG SG1996010781A patent/SG44978A1/en unknown
- 1996-10-04 ZA ZA968399A patent/ZA968399B/xx unknown
- 1996-10-04 TW TW085112165A patent/TW338025B/zh not_active IP Right Cessation
- 1996-10-09 CA CA002187494A patent/CA2187494A1/en not_active Abandoned
- 1996-10-22 TR TR96/00831A patent/TR199600831A2/xx unknown
- 1996-11-06 MX MX9605403A patent/MX9605403A/es unknown
- 1996-12-04 JP JP32390096A patent/JP3938797B2/ja not_active Expired - Fee Related
- 1996-12-16 PL PL96317512A patent/PL317512A1/xx unknown
- 1996-12-17 DE DE69614815T patent/DE69614815T2/de not_active Expired - Lifetime
- 1996-12-17 EP EP96309185A patent/EP0780648B1/en not_active Expired - Lifetime
- 1996-12-17 MY MYPI96005312A patent/MY113546A/en unknown
- 1996-12-17 KR KR1019960066685A patent/KR100191987B1/ko not_active IP Right Cessation
- 1996-12-18 CN CNB961232692A patent/CN1141547C/zh not_active Expired - Fee Related
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EP0780648B1 (en) | 2001-08-29 |
TW338025B (en) | 1998-08-11 |
IL119333A (en) | 2000-07-16 |
CN1163386A (zh) | 1997-10-29 |
EP0780648A3 (en) | 1998-02-04 |
JP3938797B2 (ja) | 2007-06-27 |
ZA968399B (en) | 1997-05-13 |
KR100191987B1 (ko) | 1999-06-15 |
DE69614815D1 (de) | 2001-10-04 |
IL119333A0 (en) | 1996-12-05 |
KR970047715A (ko) | 1997-07-26 |
US5611218A (en) | 1997-03-18 |
AU725907B2 (en) | 2000-10-26 |
CA2187494A1 (en) | 1997-06-19 |
TR199600831A2 (tr) | 1997-07-21 |
JPH09269189A (ja) | 1997-10-14 |
MX9605403A (es) | 1997-06-28 |
PL317512A1 (en) | 1997-06-23 |
SG44978A1 (en) | 1997-12-19 |
DE69614815T2 (de) | 2002-04-11 |
AU6797996A (en) | 1997-06-26 |
EP0780648A2 (en) | 1997-06-25 |
MY113546A (en) | 2002-03-30 |
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