CN1076134A - 氩气热泵的低温精馏系统 - Google Patents

氩气热泵的低温精馏系统 Download PDF

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CN1076134A
CN1076134A CN93102484A CN93102484A CN1076134A CN 1076134 A CN1076134 A CN 1076134A CN 93102484 A CN93102484 A CN 93102484A CN 93102484 A CN93102484 A CN 93102484A CN 1076134 A CN1076134 A CN 1076134A
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fluid
tower
argon
heat pump
column
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CN93102484A
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H·E·霍华德
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Praxair Technology Inc
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Praxair Technology Inc
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04309—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/042—Division of the main heat exchange line in consecutive sections having different functions having an intermediate feed connection
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    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
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    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/0423—Subcooling of liquid process streams
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    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04278—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using external refrigeration units, e.g. closed mechanical or regenerative refrigeration units
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    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
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    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04369—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of argon or argon enriched stream
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/0466—Producing crude argon in a crude argon column as a parallel working rectification column or auxiliary column system in a single pressure main column system
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
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    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/52—One fluid being oxygen enriched compared to air, e.g. "crude oxygen"
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/12—External refrigeration with liquid vaporising loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/58—Quasi-closed internal or closed external argon refrigeration cycle
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    • Y10S62/00—Refrigeration
    • Y10S62/912—External refrigeration system
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
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    • Y10S62/00—Refrigeration
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    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract

低温精馏系统，其中在氩塔的上部使冷凝的热泵 流体再冷却，然后冷却进料和被压缩，最后相对于低 温精馏装置的底部被冷凝以再沸，这样改善了回流比 和提高氩的回收。

Description

本发明一般说来涉及流体混合物的低温精馏，此混合物包括：氧、氮和氩（例如空气）。更具体地说，本发明涉及生产氩的低温精馏。
在众多工业应用中，氩愈来愈重要。例如，不锈钢生产、电子工业以及如钛工艺的活性金属生产。
一般是从空气的低温精馏来生产氩。空气含有约78%的氮、约21%的氧和不足1%的氩。因为空气中氩的浓度很低，因此在主要的大气气体中它的单元价值最高。但是，常规的低温空分工艺仅能回收进料空气中约70%的氩。因此，希望在空气低温精馏生产工艺中提高氩的回收。
据此，本发明的目的是提供一个低温精馏系统，它能以提高的回收率生产氩。
显然，本领域的技术人员根据本发明的公开就可以实现上述或其它目的。
本发明的一个方面是，低温精馏的空分方法，此方法包括：
（A）将冷却了的进料空气供给低温精馏装置，此装置包括至少一个塔和通过低温精馏在低温精馏装置中使进料空气分离，以产生富氮流体（nitrogen-enriched  fluid）和富氧流体（oxygen-enriched  fluid）;
（B）将含氩流体从低温精馏装置送入氩塔和通过低温精馏在氩塔中使含氩流体分离，产生粗氩和较富氧流体（oxygen-richer  fluid）;
（C）从氩塔上部抽出热泵蒸气，温热抽出的热泵蒸气，压缩温热的热泵蒸气和冷却压缩了的热泵蒸气;和
（D）通过与富氧流体的间接热交换来冷凝经冷却和压缩了的热泵蒸气和将产生的冷凝热泵流体送入氩塔。
本发明的另一方面是，低温空分设备，此设备包括：
（A）主热交换器，低温精馏装置，此装置包括至少一个塔，一个氩塔，从主热交换器向低温精馏装置提供流体的装置，和从低温精馏装置向氩塔提供流体的装置;
（B）热泵压缩机，从氩塔的上部向主热交换器提供流体的装置，和从主热交换器向热泵压缩机提供流体的装置;
（C）从热泵压缩机向主热交换器提供流体的装置，和从主热交换器向低温精馏装置的下部提供流体的装置;和
（D）从低温精馏装置的下部向氩塔的上部提供流体的装置。
本文所用的术语“上部”和“下部”是分别指塔的中点之上和之下的塔的那部分。
本文所用的术语“进料空气”是指主要包括氮、氧和氩（如空气）的混合物。
本文所用的术语“涡轮膨胀（turboexpansion）”是指高压气体通过一涡轮机流动来使气体减压和降温，藉此产生冷冻作用。
本文所用的术语“塔”是指蒸馏或分馏塔或区，即接触塔或区，其中液相和蒸气相逆流接触，使流体混合物进行分离，例如，蒸气相和液体相在一系列固定在塔内的垂直隔开的塔盘或塔板上接触和/或在整齐和/或散乱堆积的填料元件上接触。如欲进一步探讨蒸馏塔，可参阅《化学工程手册》第五版（the  Chemicad  Engineer′s  Handbook，fifth  edition，edited  by  R.R.Perry  and  C.H.Chilton，Mc  Graw-Hill  Book  Company，Nwew  York，Section  13，the  Continuous  Distillation  process。本文所用的术语“双塔（double  column）”是指高压塔的上端与低压塔的下端有热交换关系。对双塔的进一步讨论可参见《气体分离》（Ruheman“The  Separation  of  Gases”Oxford  Universitypress，1949，Chapter  Ⅶ，Commercial  Air  Separation）。
气液接触分离过程由这些组分的蒸气压的差别决定。较高蒸气压的（或难挥发的或高沸点的）组分易于在气相浓集，而较低蒸气压的（或难挥发的或高沸点的）组分则易于在液相中浓集。分凝（partial  condensation）是分离方法，用此法蒸气混合物的冷却可用于在气相中浓集易挥发性组分和在液相中浓集难挥发组分。精馏或连续蒸馏也是分离方法，此方法将气液相的逆流处理所获得的连续部分蒸发与冷凝结合起来。气液相的逆流接触是绝热的和可以包括相之间的整体或局部接触。应用精馏原理来分离混合物的分离方法设计常常可以互相转化地称之为精馏塔、蒸馏塔或分馏塔。低温精馏是至少一部分在温度等于或低于123°K下进行精馏过程。
本文所用的术语“间接热交换”是指引入两种流体物流进行热交换，但两流体之间不发生物理接触和混合。
本文所用的术语“氩塔”是指一个塔，此塔处理包括氩的进料和生产氩浓度超过进料的氩，此塔可包括热交换器或在它上部的上冷凝器。
本文所用的术语“平衡级（equili  brium  stage）”是指蒸气和液相之间的接触过程，使存在的蒸气流和液流处于平衡状态。
本文所用的术语“低温精馏装置”是指一装置，其中，虽然其它辅助工艺组件或设备可以在高于123°K下工作，但气/液接触的分离过程至少一部分是在等于或低于123°K的温度下进行。
本文所用的术语“富氧流体（oxygen-enriched  fluid）包括在单塔低温精馏装置中产生的含氧流体（oxygen-containing  fluid）或在双塔低温精馏装置的高压塔中产生的含氧流体，但不包括在双塔低温精馏装置的低压塔中产生的含氧流体。
图1是本发明一个优选实施方案的流程示意图，其中低温精馏装置包括一双塔。
图2是本发明另一实施方案的流程示意图，其中氩塔包括一上冷凝器。
图3是本发明一优选实施方案的流程示意图，其中氩热泵回路包括一涡轮膨胀器。
图4是本发明另一实施方案的流程示意图，其中低温精馏装置包括一单塔。
一般来说，本发明包括在低温空分装置的下部和氩塔的上部之间引入一特定的氩热泵回路，藉此，将主要传热移至高温，同时对低压分离提供更多回流，从而提高氩的回收。下面参考附图详述本发明。
现在参考图1，进料空气30通过压缩机1压缩，通过冷却器32冷却和通过吸附器2净化和干燥。与返回气流（下将详述）间接热交换，此净化了的经压缩的空气81通过主热交换器冷却。在图1所示的实施方案中，包括占25-45%的净化了的经压缩的空气81的部分33通过压缩机4进一步被压缩，通过冷却器34被冷却、通过主热交换器3进一步冷却、通过热交换器4再冷却和通过阀20进入塔6，此塔为双塔低温精馏装置的高压塔和在65-220psia压力下工作。另一路净化了的经压缩的空气81的部分35直接通入主热交换器3。气流35的部分36仅部分地通过主热交换器3和通过为产生冷冻的涡轮膨胀器5而冷却至更低温度。所得的物流37再通过主热交换器和然后进入低压塔7，此塔即双塔低温精馏装置的低压塔和在低于塔6的压力下工作，其压力范围在15-75psia。进料空气的主要部分38则从主热交换器通入塔6。
在塔6中进料空气通过低温精馏而分离为富氮（nitrogen-enriched）蒸气和富氧（oxygen-enriched）液体。富氧液体作为液流39从塔6中抽出、通过热交换器12再冷却和通过阀16进入塔7。富氮蒸气作为气流40从塔6中抽出、经与塔7的沸腾塔底进行间接热交换而在主冷凝器9中冷凝，部分41作为回流返回塔6，而另一部分42则通过热交换器11再冷却和通过阀15进入塔7。如需要，液流39中一部分富氧液体也可用于冷却氩塔的上部，和得到的富氧蒸气及其余液体通入塔7。
在塔7内，各种进料通过低温精馏而分离成富氧（oxygen-rich）流体和富氮（nitrgen-rich）流体。富氧液体作为液流43从塔7中抽出，经由泵19加压、通过热交换器14和3温热和可以在物流44中作为氧产品而回收。富氮蒸气作为气流45从塔7中抽出，通过热交换器11、12和3温热和可以在物流46中作为氮产品而回收。为保证产品纯度含氮废物流47从塔7顶部偏下处除去和在以物流48从系统中除去之前经过热交换器11、12和3。
含约5-30%氩的流体作为物料49从低温精馏装置的低压塔送入氩塔系统8，此氩塔系统包括热交换器13。在氩塔内，经低温精馏物流49被分离为粗氩和较富氧（oxygen-richer）流体。较富氧流体作为物流50送入塔7。氩浓度至少约为80%的粗氩通过热交换器13温热和在物流51中作为粗氩产品回收。
热泵蒸气从氩塔上部抽出。在图1所示的实施方案中，热泵蒸气包括从热交换器13抽出的粗氩。此在物流52中抽出的热泵蒸气然后通过主热交换器3温热，藉此使进料空气冷却和将冷冻作用提供给低温精馏装置。经温热的热泵蒸气通过热泵压缩机18压缩。热泵压缩机18压缩温热的热泵蒸气，一般使其压力约增加至原来的三倍。通过冷却器54使热泵蒸气除去由于压缩产生的热和再通过主热交换器3而冷却。
然后，经冷却和压缩的热泵蒸气56与富氧流体（oxygen-enriched  fluid）进行间接热交换而冷凝。在图1所示的实施方案中，冷却了的压缩的热泵蒸气56是通过热泵冷凝器10来冷凝的，此冷凝器是在低温精馏装置较低部分的塔6下部。得到的冷凝了的热泵流体57通入氩塔上部。在图1所示的实施方案中，流体57通过热交换器13，与温热的粗氩进行间接热交换而再冷却，粗氩一部分作为热泵蒸气使用。在热交换器13和塔之间经阀17有适量流体通过。
图2示出本发明另一实施方案，其中氩塔包括上冷凝器而不是热交换器。图2所示的方案是：热泵回路可以封闭和热泵流体无需含氩。根据图2的方案在可用于实施本发明的热泵流体中，除了如精氩的含氩流体外，还可以指定空气、氧和氮。对于共同元件图2方案的编号与图1相对应，因此这些共同元件将不再将详细描述。现在参阅图2，粗氩部分58通过与热泵流体的间接热交换而在冷凝器59中冷凝和用作氩塔的回流液。热泵蒸气60从氩塔8的上冷凝器60中抽出、通过主热交换器温热、通过热泵压缩机18压缩、通过主热交换器3冷却和通过热泵冷凝器10与富氧流体间接热交换而冷凝。一般说来其运行方式与参考图1所详述的方式相同。所得的冷凝了的热泵流体57通过阀95进入塔8上部的冷凝器59，其中它用于冷凝粗氩蒸气58和从而为氩塔提供回流液。如需要，从低温精馏装置的较上部分的某些含氮流体可以通入热泵回路和某些冷凝的热泵流体也可以通入低温精馏装置，例如作为低压塔和高压塔中单个或两个都有的回流。
在本发明的另一实施方案中，富氧液体并不直接从高压塔通入低压塔，而是在从高压塔进入低压塔之前先在氩塔上部与热泵流体进行热交换。在此实施方案中，热泵流体从氩塔中抽出是从上冷凝器的内部而不是外部。
图3示出本发明另一实施方案，其中空分是在升高的塔压下进行和包括利用一部分热泵蒸气的涡轮膨胀产生致冷和从双塔系统的上塔回收高压氧气而无需泵抽。对于共同元件图3方案的编号与图1相对应和因此这些共同元件将不再详述。参考图3，完全净化了的压缩的进料空气流81通入主热交换器，在其中被冷却，然后作为气流81通入低温精馏装置的塔6。富氧蒸气61从塔7的主冷凝器9之上处抽出，通过热交换器3温热和可以作为氧产品在物流44中回收。在产品氧线不需要使用泵。在图3的实施方案中，塔6是在压力范围65-220  psia下操作和塔7是在压力范围15-75  psia下操作。经压缩的热泵蒸气55的一部分62在仅部分穿过主热交换器3之后从其中送出和通过涡轮膨胀器63进行涡轮膨胀以产生致冷。经涡轮膨胀的物流64然后再返回主热交换器3，在其中与热泵蒸气52汇合和在通过主热交换器之后，用于冷却进料空气和将致冷作用供给低温精馏装置以有助于进行低温致冷。其余压缩的热泵蒸气65则完全通过主热交换器3和然后通过热泵冷凝器10和通至氩塔8，正如原先参考附图1所描述的。
图4示出本发明另一实施方案，其中低温精馏装置包括单塔。对于共同元件图4方案中的编号相对应于图1，和因此这些共同元件不再详述。参考图4，经净化了的压缩进料空气81通过主热交换器3而冷却和然后作为物流82通入低温精馏装置，此装置包括在65-220  psia压力范围内操作的单塔66，在此塔内通过低温精馏，进料空气分离成富氧流体和富氮流体。富氧流体作为物流39从塔66中抽出、通过热交换器67再冷却和通过阀16进入氩塔68，此塔通过冷凝器69与塔66进行热交换和此塔在15-75  psia压力范围内操作。富氮蒸气作为气流70从塔66中除去、在冷凝器69中与塔68的塔底进行间接热交换而冷凝和作为物流71返回塔66作回流。富氮蒸气70的一部分72可以通过主热交换器3和在物流73中作为产品氮回收。含氮废物流90从塔66上部引出、部分通过热交换器3而被温热、通过涡轮膨胀器91涡轮膨胀以产生致冷和再通过热交换器3来冷却引入的进料空气，从而为低温精馏提供致冷作用。产生的废物流92从系统中除去。在氩塔68中物流39中的流体通过低温精馏而分离成粗氩和富氧流体。富氧流体从塔68中作为物流74抽出、通过热交换器67和3而温热和可以在物流75中作为产品氧而回收。粗氩从氩塔热交换器13作为物流51而回收，和也可作为热泵蒸气的物流52而使用，其运行方式与图1所示方案所述相类似。
下述实施例给出按图1所示方案进行本发明的模拟结果，其中全部塔在所有塔截面上都使用整齐排布填料。唯一的液体需要是涉及为保持氩精制所需的液氮流。低压塔顶的压力保持在足以从低温精馏装置除去氮的压力。作为用于吸附床再生的废氮，以约13.5%的空气流作为补偿。此实施例是例示性的，而不应限制本发明。
完全的进料空气流先被压缩至大约6的压缩比，和通入吸附床来除去水蒸气、二氧化碳和烃。相当于总空气流约三分之一的一部分再压缩至更高压力，接着用冷水冷却，和通入主热交换器中，在此冷却至接近它的露点。空气流的另一部分在中间温度下抽出和经涡轮膨胀而产生致冷。此空气流膨胀至足以克服在此后通过的热交换器带来的压力降的压力值。此经膨胀的空气再返回主热交换器，在此进一步冷却至接近其露点的温度。此低压空气送入低压塔的中间位点。压缩空气的其余部分直接送入高压塔的中间位点。
压缩到最高压力的空气部分由于泵抽的液氧而被液化，液氧从低压塔底抽出。泵抽的液氧在基本上高于低压塔压力下蒸发。此液化了的空气也送入高压塔的中介点。从高压塔收回占总空气流约39.0%的气流作为低压塔的回流。来自高压塔底的富氧液体经再冷却和闪蒸而在中点处进入低压塔，以便提供为分离而附加的中间回流。在此液氧进料点下方，经冷却的涡轮膨胀空气送入低压蒸馏塔。在还要低的位置供氩塔的进料被抽出。送入氩塔的进料流大约占总空气流的12.4%。此进料流直接送入氩塔底。在氩塔顶部的氩再冷却器所得的蒸气流占总空气流的12.6%。此作为热泵流体的物流被温热和压缩至压缩比约为3.3和再通入主热交换器，在此被冷却到接近它露点的温度。它被抽出和与高压塔底的富氧液体进行潜热交换而冷凝。此物流接着再冷却和闪蒸而返回氩塔作为回流。
上述的工艺条件提供了应用氩塔内已有的热泵含氩蒸气的实例。对于给定的条件，氩的回收率达到94.74%。这比用常规方法所可能达到的回收率要明显高多了，因常规方法虽使用与图1所示相似的设备，但不包括本发明的热泵回路。
现在，使用本发明的方法和设备，可以实现低温空分，其氩的回收明显超过用常规系统所达到的。之所以使氩的回收得到改进是由于例如在低压塔上部存在的更有利的回流比。在低温精馏装置的较低部分（如在低温精馏装置的高压塔的下部）冷凝热泵蒸气使进料空气中所含的更大部分的氮用作回流。本发明将冷凝氩的潜热交换给升高的温度，同时例如给低压分离提供更多的回流。
虽然本发明结合某些优选实施方案进行详细描述，但本领域技术人员会理解：本发明其它实施方式也在本发明构思和权利要求的范围内。

Claims (14)

1、低温精馏的空分方法，此方法包括：
(A)向至少包括一个塔的低温精馏装置供给冷却了的进料空气和通过低温精馏在低温精馏装置中使进料空气分离，产生富氮流体和富氧流体；
(B)将含氩流体从低温精馏装置送入氩塔和通过低温精馏在氩塔中使含氩流体分离，产生粗氩和较富氧流体；
(C)从氩塔上部抽出热泵蒸汽，温热抽出的热泵蒸汽，压缩温热的热泵蒸汽和使压缩的热泵蒸汽冷却；和
(D)通过与富氧流体的间接热交换来冷凝经冷却和压缩了的热泵蒸汽和将产生的冷凝了的热泵流体送入氩塔。
2、根据权利要求1的方法，其中低温精馏装置包括双塔，此塔分为一高压塔和一低压塔，其中富氮流体和富氧流体从高压塔送入低压塔，和在其中通过低温精馏而分离为富氮流体和富氧流体和其中含氩流体从低压塔送入氩塔。
3、根据权利要求1的方法，其中低温精馏装置包括单塔，和含氩流体从单塔送入氩塔。
4、根据权利要求1的方法，其中热泵流体包括氩。
5、根据权利要求1的方法，其中热泵蒸汽通过与进料空气的间接热交换而温热，同时使进料空气冷却。
6、根据权利要求1的方法，其中一部分压缩的热泵流体经涡轮膨胀而致冷，并与进料空气间接热交换而温热，同时使进料空气冷却，从而提供低温精馏所需的致冷作用。
7、根据权利要求1的方法，其中热泵流体包括氮，和一部分冷凝的热泵流体通入低温精馏装置。
8、根据权利要求2的方法，其中富氧流体在从高压塔进入低压塔之前先通过与氩塔上部的热泵流体有关的热交换。
9、低温空分设备，包括：
（A）主热交换器，低温精馏装置，此装置包括至少一个塔，一氩塔，从主热交换器向低温精馏装置提供流体的装置，和从低温精馏装置向氩塔提供流体的装置;
（B）热泵压缩机，从氩塔的上部向主热交换器提供流体的装置，和从主热交换器向热泵压缩机提供流体的装置;
（C）从热泵压缩机向主热交换器提供流体的装置，和从主热交换器向低温精馏装置的下部提供流体的装置;和
（D）从低温精馏装置的下部向氩塔的上部提供流体的装置。
10、根据权利要求9的设备，其中低温精馏装置包括：双塔，此双塔分为一高压塔和一低压塔，从主热交换器向低温精馏装置提供流体的装置，它与高压塔相连，从低温精馏装置向氩塔提供流体的装置，它与低压塔相连，以及此双塔还包括从高压塔向低压塔提供流体的装置。
11、根据权利要求9的设备，其中低温精馏装置包括：单塔;从主热交换器向低温精馏装置提供流体的装置，它与单塔相连，和从低温精馏装置向氩塔提供流体的装置，它与单塔相连。
12、根据权利要求9的设备，其中氩塔包括一上热交换器。
13、根据权利要求9的设备，其中氩塔包括一上冷凝器。
14、根据权利要求9的设备，其其还包括：涡轮膨胀器，从热泵压缩机向涡轮膨胀器提供流体的装置，和从涡轮膨胀器向主热交换器提供流体的装置，和从涡轮膨胀器向热泵压缩机提供流体的装置。
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