CN1185456C - 制备氮的装置和方法 - Google Patents

制备氮的装置和方法 Download PDF

Info

Publication number
CN1185456C
CN1185456C CNB991017366A CN99101736A CN1185456C CN 1185456 C CN1185456 C CN 1185456C CN B991017366 A CNB991017366 A CN B991017366A CN 99101736 A CN99101736 A CN 99101736A CN 1185456 C CN1185456 C CN 1185456C
Authority
CN
China
Prior art keywords
stream
air
cooling agent
purifying
product
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Fee Related
Application number
CNB991017366A
Other languages
English (en)
Other versions
CN1227341A (zh
Inventor
K·V·姆克波伦
J·A·古德博迪
C·M·布鲁克斯
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
BOC Group Inc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by BOC Group Inc filed Critical BOC Group Inc
Publication of CN1227341A publication Critical patent/CN1227341A/zh
Application granted granted Critical
Publication of CN1185456C publication Critical patent/CN1185456C/zh
Anticipated expiration legal-status Critical
Expired - Fee Related legal-status Critical Current

Links

Images

Classifications

    • 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
    • F25J3/04333—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
    • 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
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • 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
    • 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
    • F25J3/0429—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
    • 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
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
    • 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
    • F25J3/044—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 using a single pressure main column system only
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead gas
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/40—Processes or apparatus involving steps for recycling of process streams the recycled stream being air
    • 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
    • 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

本发明公开了一种在单塔氮气发生器中分离氮气的装置和方法，其中通过废气的膨胀加入制冷作用。一部分进料空气流在部分冷却后进行汽轮膨胀以增加提供的制冷量，从而得以回收液体氮产物。

Description

制备氮的装置和方法
本发明涉及从单塔氮发生器中制备氮的装置和方法。本发明特别地涉及通过废气膨胀加入制冷作用的装置和方法。本发明尤其涉及那些通过附加的空气膨胀产生液体产品的装置和方法。
现在已有许多在称为单塔氮发生器的单塔中产生氮的方法和装置。在这些方法中，压缩空气然后纯化以除去二氧化碳、湿气和可能危险的烃类。然后将该经压缩并纯化的空气在一个主热交换器内冷却至适于对它进行精馏的温度，该温度通常是空气在特定的压缩压力时的露点或者接近该露点温度。然后将空气导入至蒸馏塔以产生富氮的塔顶产品和富氧的液态塔底产品。冷凝该塔顶产品并返回至塔内用于回流。然后可以把塔顶产品的其余部分作为气态氮产品，该气态氮在主热交换器中被充分地加热，从而有助于冷却进料空气。也可以将不太纯净的氮作为废料流通过该主热交换器。这种废料流可以用于再生提纯器。
在任何的空气分离设计中，动力消耗是很重要的设计依据。在U.S.4,966,002中，使含有液态塔底产物的废料流进行阀膨胀，随后在塔顶冷凝器中被用作冷却剂。将废料流分成两部分。将废料流的一部分进行部分加热，然后膨胀；而将废料流的其它部分再压缩，并返回至塔中。该压缩既可以发生在主热交换器的热端温度，也可以发生在主热交换器的冷端温度。通过从塔中除去氮含量比塔底产物高的液态流，可实现效率的增加。然后将这样的液流也进行阀膨胀，并导入至塔顶冷凝器用作第二冷却剂以协助冷凝塔顶产物用作回流。将废料流部分地加热，膨胀作功，随后从该主热交换器中排出。将用作第二冷却剂的液流在用作冷却剂后再压缩，冷却返回至它的露点温度并且再导入至塔内。
在如上所述的装置中，从塔直接提供足够的制冷以产生液体是困难的。这是因为多于压缩循环流所需要的膨胀功必须作为热从过程中排出。所以在另一专利中，将氮的液化装置与该过程结合以产生液体。这种结合的缺点在于增加了提供氮的液化装置的费用。
如下所述，本发明提供了一种从单塔氮发生器产生液态氮产品的方法，该方法远比提供一个单独的氮的液化装置来得简单和更加有效。
本发明提供了一种从空气中分离出氮的装置。根据本发明，安装了一个蒸馏塔用以蒸馏空气产生富含氮的塔顶产物和富含氧的液态塔底产物。塔顶冷凝器连接于蒸馏塔以接收包含塔顶产物的塔顶流和包含塔底液体产物的冷却剂流。该塔顶冷凝器可用以液化塔顶产物流从而产生用以回流蒸馏塔的回流物流和液体产物，主热交换器提供有若干通道，这些通道的结构可将经过压缩和纯化的空气流的第一部分冷却至适合于它精馏的温度，并且将经过压缩和纯化的空气流的第二部分进行部分冷却。主热交换器连接于蒸馏塔以使经过压缩和纯化的空气流的第一部分导入其中。第一和第二膨胀装置连接于主热交换器，以便使部分加温的物流和经过压缩和纯化的空气流的第二部分分别进行膨胀。至少产生一种致冷剂流作为第一和第二膨胀装置的产物。所安装的主热交换器通道也充分加热所述的至少一种致冷剂流，从而使液体产物流产生。
本发明的另一方面涉及一种装置和方法，其中空气在蒸馏塔中精馏，由之产生富含氮的塔顶产物和富含氧的液态塔底产物。将包含塔顶产物的塔顶产物流液化。从而产生用以回流蒸馏塔的回流物流，同时产生液体产物流。经过压缩和纯化的空气流的第一部分被冷却至适合于它精馏的温度。通过使部分加温的物流和经过压缩和纯化的空气流的第二部分膨胀作功，产生至少一种冷却剂流。使经过压缩和纯化的空气流的第一和第二部分与所述的至少一种冷却剂流间接交换热量，从而产生液体产物流。
在本发明中，通过一个附加的膨胀装置使部分空气流膨胀，产生附加的制冷作用。然后将这部分膨胀的空气流逆流引入至通入主热交换器的空气中。所述的部分加温的物流可以是一股废气流，它包含由液体塔底产物汽化而产生的、在蒸馏塔的塔顶冷凝器中用作冷却剂的部分或全部废气。然后将加温和膨胀后的空气从设备中排出。较好的是将空气和废氮气充分加温并从设备中排出。正是这增加的制冷作用使得有可能产生液体产物。容易理解，加入一个膨胀装置比加入一个氮气液化器以完成同样的目的要简单得多。
应当注意，本说明书和权利要求书中所用的术语“部分加温”是指加温至主热交换器的冷端和热端之间的温度。而“充分加温”是指加温至主热交换器的热端的温度。“部分冷却”是指冷却至主热交换器的冷端和热端之间的温度。
本说明书和后附的权利要求书清楚地指出了申请人认为是其发明的内容，结合附图当可更好地理解这些内容，其中：
图1是实施本发明方法的一种装置的示意图；
图2是图1所述装置的另一种实施方案的部分示意图；
图3是图1所述装置的再一种实施方案的部分示意图。
为了便于说明，图2和图3中与图1中相同的部件用相同的参考标号表示。除了在图2和图3中具体指明的变化以外，图中没有示出的方案的其余部分都与图1相同。
现结合附图来说明本发明的空气分离装置1。将经过压缩的空气冷却以除去压缩热，并将它纯化。纯化可以在任一已知的设备中进行，例如具有不同步运行的若干床层的压力周期变动吸附单元，以除去进料中的湿气、二氧化碳和烃类。
然后将所得的经压缩和纯化的空气流10导至具有单元14，16和18的热交换器复合体12。在空气部分冷却后，其中的第一部分20冷却至适合于其精馏的温度，而第二部分22以部分冷却的状态从热交换器复合体12中排出。然后将经过压缩和纯化的第一部分空气流20导入蒸馏塔24，该蒸馏塔可以具有诸如塔盘、填料之类的既可以是无规的又可以是有结构的质量传递单元，以使上升的空气的蒸汽相与起始于蒸馏塔24顶部的下降的液相接触。结果，富含氮的塔顶产物在蒸馏塔24的顶部区域26内产生。富含氧的塔底产物在蒸馏塔24的底槽区28产生。
塔顶冷凝器30连接于蒸馏塔以便接收塔顶产物流32。塔顶产物流32在塔顶冷凝器30内液化产生回流物流34，引发下降的液相在蒸馏塔24内形成，并产生液体产物流36(图中标示为“LN2”)。
用于塔顶冷凝器30的冷却剂由第一冷却剂流38和较好还有的第二冷却剂流40组成，该第一冷却剂流38包含富氧的液体塔底产物，第二冷却剂流40由氮含量比塔底产物高、从蒸馏塔24中排出的液体所组成。该第一冷却剂流38和第二冷却剂流40分别在膨胀阀42和44中膨胀，以降低其压力和温度。该第一冷却剂流38和第二冷却剂流40在塔顶冷凝器30中汽化。
第一冷却剂流38在汽化以后形成废物流，该废物流在热交换器复合体12中被部分加温而产生部分加温的物流45。部分加温的物流45在膨胀装置(较好地是汽轮式膨胀机)46中膨胀并产生致冷剂流47。第二冷却剂流40在汽化以后，在循环压缩器48中被再压缩并冷却至热交换器复合体12的露点温度。然后将所得到的经压缩的冷却剂流40循环返回至蒸馏塔24中。汽轮式膨胀机46可偶合至循环压缩器48，以使部分膨胀功在循环压缩器中被回收，而部分膨胀功通过各种已知的能耗装置(如发电机或制动器)消耗掉。
为了制取液体产物，经压缩和纯化的第二部分空气流22在汽轮式膨胀器50中进行汽轮膨胀，产生制冷剂流51。致冷剂流51与致冷剂流47合并起来得到致冷剂流52，该致冷剂流52被引入至热交换器复合体12的冷端，在其中充分加温。应理解，在主热交换器复合体12中可为致冷剂流47和51提供分别的通道(虽然这样做成本较高)。由于存在第二汽轮式膨胀器50以及经压缩和纯化的第二部分空气流22进行了汽轮膨胀，就可能产生液体并将其以液体产物流36的形式提取。虽然在图中未示出，汽轮式膨胀器50可偶合于已知的能量消耗装置。
参看图2，其中显示了另一种实施方式，在该实施方式中，第一冷却剂流38仍在塔顶冷凝器30中汽化，产生废物流与致冷剂流51合并。然后将所得的合并的物流部分加温，形成部分加温的物流45。然后部分加温的物流45膨胀产生致冷剂流47，该致冷剂流在主热交换器复合体12中被充分加温。
进一步参看图3，其中显示了本发明的另一种实施方式，在该实施方式中，第一冷却剂流38在塔顶冷凝器30中汽化，产生部分加温的废物流然后与致冷剂流51合并，形成部分加温的物流45。部分加温的物流45膨胀产生致冷剂流47，然后该致冷剂流在主热交换器复合体中被充分加温。
在蒸馏塔24的顶部区域26中也可得到气体产物流53。气体产物流53在主热交换器复合体12中充分加温，从中以产物氮气流的形式排出(图中标示为“PGN”)。
以上参照较佳的实施方式对本发明作了说明，本领域的技术人员会理解，可以在不背离本发明的实质和范围的条件下作各种改变、增加和省略。

Claims (9)

1.一种从空气中分离氮的装置，它包括：
用以精馏空气的蒸馏塔(24)，它产生富含氮的塔顶产物(32)和富含氧的液体塔底产物(38)；
与所述的蒸馏塔相连的塔顶冷凝器(30)，用以接收所述塔顶产物(32)，该塔顶冷凝器的结构可液化所述的塔顶产物，从而产生用以回流该蒸馏塔的回流物流(34)以及液体产物流(36)；
具有通道的主热交换器(12)，这些通道的结构可将经压缩和纯化的空气流的第一部分冷却至适合于精馏的温度，并使经压缩和纯化的空气流的第二部分进行部分冷却；
所述主热交换器与所述蒸馏塔相连，使所述的经压缩和纯化的空气流的第一部分引入所述蒸馏塔中；
连接于主热交换器的第一膨胀装置(46)和第二膨胀装置(50)，分别用以膨胀部分加温的物流(45)和用以膨胀所述的经压缩和纯化的空气流的第二部分，从而产生至少一种制冷剂流(51)作为所述的第一和第二膨胀装置的产物，所述经压缩和纯化的空气流的所述第二部分以与所述经压缩和纯化的空气流的第一部分在引入与所述蒸馏塔相连的主热交换器时相同的压力提供给所述第二膨胀装置，所述部分加温的物流(45)由液体塔底产物(38)经热交换形成；
所述主热交换器通道的结构也可接收和充分加温所述的至少一种制冷剂流，从而引入制冷作用并可产生所述的液体产物流；
用于塔顶冷凝器(30)的冷却剂流包含第一冷却剂流(38)；
所述的塔顶冷凝器(30)还连接于蒸馏塔(24)以接收第二冷却剂流(40)，该第二冷却剂流(40)包含所述的经压缩和纯化的空气流的第一部分的液相，其氮含量高于所述的塔底产物的氮含量；
在所述的塔顶冷凝器(30)与蒸馏塔(24)之间插入一个膨胀阀(44)，用以膨胀所述的第二冷却剂流(40)；
有一个循环压缩器(48)连接于所述的塔顶冷凝器(30)，用以将所述的第二冷却剂流(40)再次压缩至蒸馏塔的塔内压力；和
所述的主热交换器(12)连接于循环压缩器(48)与蒸馏塔(24)之间，以将经再压缩后的第二冷却剂流(40)返回至所述的蒸馏塔(24)内，而其所述的热交换通道的结构也可使所述的第二冷却剂流冷却至露点温度或其附近。
2.如权利要求1所述的从空气中分离氮的装置，其特征还在于：
包含所述的液体塔底产物的冷却剂流在与蒸馏塔相连的塔顶冷凝器内气化，从而形成废物流；
主热交换器通道的结构还可将所述的废物流部分加温，从而产生所述的部分加温的物流。
3.如权利要求1所述的从空气中分离氮的装置，其特征还在于：
包含所述的液体塔底产物的冷却剂流在与蒸馏塔相连的塔顶冷凝器内气化，从而形成废物流；
所述的第二膨胀装置和塔顶冷凝器连接于所述的主热交换器，使所述的废物流和所述的经压缩和纯化的空气流的第二部分在膨胀后合并起来，并在该主热交换器中部分加温，形成所述的部分加温的物流。
4.如权利要求1所述的从空气中分离氮的装置，其特征还在于：
包含所述的液体塔底产物的冷却剂流在与蒸馏塔相连的塔顶冷凝器内气化，从而形成废物流；
主热交换器连接于所述的塔顶冷凝器以部分加温所述的废物流；和
第二膨胀装置与主热交换器相连接，使所述的经压缩和纯化的空气流的第二部分在所述的废物流中膨胀之后形成所述的部分加温的物流。
5.如权利要求1所述的从空气中分离氮的装置，其特征还在于所述的主热交换器连接于所述的蒸馏塔，主热交换器的通道的结构也可接收包含所述的塔顶产物的气流并将该气流充分加温，从而形成气体氮产物流。
6.一种从空气中分离氮的方法，包括以下步骤：
在蒸馏塔(24)中精馏空气，由此产生富含氮的塔顶产物(32)和富含氧的液体塔底产物(38)；
在使包含所述的塔顶产物(32)的塔顶产物流液化的同时使废物流汽化，由之产生用以回流所述的蒸馏塔(32)的回流物流(34)以及液体产物流(36)；
将经压缩和纯化的空气流的第一部分冷却至适合于精馏的温度，并使经压缩和纯化的空气流的第二部分进行部分冷却；
将经压缩和纯化的空气流的第一部分(20)引入至所述的蒸馏塔(24)；
使部分加温的物流(45)和所述的经压缩和纯化的空气流的第二部分膨胀作功，产生至少一种制冷剂流(51)，所述经压缩和纯化的空气流的所述第二部分以与所述经压缩和纯化的空气流的第一部分在引入与所述蒸馏塔相连的主热交换器时相同的压力提供给膨胀装置，所述部分加温的物流(45)由液体塔底产物(38)经热交换形成；和
使所述的经压缩和纯化的空气的第一和第二部分与所述的制冷剂流之间间接交换热量，从而引入制冷作用，以产生所述的液体产物流；
用于塔顶冷凝器(30)的冷却剂流包含第一冷却剂流(38)；
还有第二冷却剂流(40)与所述的塔顶产物(32)间接交换热量并气化，该第二冷却剂流(40)包含所述的经压缩和纯化的空气流的第一部分的液相，其氮含量高于所述的塔底产物的氮含量；
第二冷却剂流(40)在与所述的塔顶产物流(32)进行间接热交换之前先进行膨胀；
将所述的第二冷却剂流(40)再压缩至所述的蒸馏塔(24)的塔内压力；
将所述的第二冷却剂流(40)冷却至露点温度或其附近，然后引入至所述的蒸馏塔(24)内。
7.如权利要求6所述的从空气中分离氮的方法，其特征还在于：
所述的塔顶产物流是相对于包含所述的液体塔底产物的冷却剂流的气化而同时冷凝的，从而使所述的冷却剂流在汽化后形成废物流；和
将所述的废物流部分加温，从而形成所述的部分加温的物流。
8.如权利要求6所述的从空气中分离氮的方法，其特征还在于：
所述的塔顶产物流是相对于包含所述的液体塔底产物的冷却剂流的气化而同时冷凝的，从而使所述的冷却剂流在汽化后形成废物流；和
将所述的废物流和经压缩和纯化的空气的第二部分在膨胀后合并起来并部分加温，以形成所述的部分加温的物流。
9.如权利要求6所述的从空气中分离氮的方法，其特征还在于：
所述的塔顶产物流是相对于包含所述的液体塔底产物的冷却剂流的气化而同时冷凝的，从而使所述的冷却剂流在汽化后形成废物流；
部分加温所述的废物流；和
将所述的经压缩和纯化的空气的第二部分在膨胀后与所述的废物流合并而形成所述的部分加温的物流。
CNB991017366A 1998-01-27 1999-01-26 制备氮的装置和方法 Expired - Fee Related CN1185456C (zh)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US09/013,830 1998-01-27
US09/013,830 US5934106A (en) 1998-01-27 1998-01-27 Apparatus and method for producing nitrogen

Publications (2)

Publication Number Publication Date
CN1227341A CN1227341A (zh) 1999-09-01
CN1185456C true CN1185456C (zh) 2005-01-19

Family

ID=21761976

Family Applications (1)

Application Number Title Priority Date Filing Date
CNB991017366A Expired - Fee Related CN1185456C (zh) 1998-01-27 1999-01-26 制备氮的装置和方法

Country Status (6)

Country Link
US (1) US5934106A (zh)
EP (1) EP0932004A3 (zh)
JP (1) JPH11287552A (zh)
CN (1) CN1185456C (zh)
MY (1) MY118100A (zh)
TW (1) TW546464B (zh)

Families Citing this family (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6125656A (en) * 1999-11-03 2000-10-03 Praxair Technology, Inc. Cryogenic rectification method for producing nitrogen gas and liquid nitrogen
US6279345B1 (en) * 2000-05-18 2001-08-28 Praxair Technology, Inc. Cryogenic air separation system with split kettle recycle
GB0119500D0 (en) * 2001-08-09 2001-10-03 Boc Group Inc Nitrogen generation
US20080216511A1 (en) * 2007-03-09 2008-09-11 Henry Edward Howard Nitrogen production method and apparatus
DE102007024168A1 (de) * 2007-05-24 2008-11-27 Linde Ag Verfahren und Vorrichtung zur Tieftemperatur-Luftzerlegung
DE102007051183A1 (de) 2007-10-25 2009-04-30 Linde Aktiengesellschaft Verfahren zur Tieftemperatur-Luftzerlegung
DE102007051184A1 (de) 2007-10-25 2009-04-30 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Tieftemperatur-Luftzerlegung
DE102008064117A1 (de) 2008-12-19 2009-05-28 Linde Ag Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
EP2236964B1 (de) 2009-03-24 2019-11-20 Linde AG Verfahren und Vorrichtung zur Tieftemperatur-Luftzerlegung
US9726427B1 (en) 2010-05-19 2017-08-08 Cosmodyne, LLC Liquid nitrogen production
EP2789958A1 (de) 2013-04-10 2014-10-15 Linde Aktiengesellschaft Verfahren zur Tieftemperaturzerlegung von Luft und Luftzerlegungsanlage

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2126700B (en) * 1982-09-15 1985-12-18 Petrocarbon Dev Ltd Improvements in the production of pure nitrogen
JPS61110872A (ja) * 1984-11-02 1986-05-29 日本酸素株式会社 窒素製造方法
JPS62102074A (ja) * 1985-10-30 1987-05-12 株式会社日立製作所 ガス分離方法及び装置
FR2651035A1 (fr) * 1989-08-18 1991-02-22 Air Liquide Procede de production d'azote par distillation
US5419136A (en) * 1993-09-17 1995-05-30 The Boc Group, Inc. Distillation column utilizing structured packing having varying crimp angle
US5396772A (en) * 1994-03-11 1995-03-14 The Boc Group, Inc. Atmospheric gas separation method
US5582034A (en) * 1995-11-07 1996-12-10 The Boc Group, Inc. Air separation method and apparatus for producing nitrogen
US5704229A (en) * 1996-12-18 1998-01-06 The Boc Group, Inc. Process and apparatus for producing nitrogen

Also Published As

Publication number Publication date
CN1227341A (zh) 1999-09-01
EP0932004A2 (en) 1999-07-28
MY118100A (en) 2004-08-30
TW546464B (en) 2003-08-11
US5934106A (en) 1999-08-10
JPH11287552A (ja) 1999-10-19
EP0932004A3 (en) 1999-11-24

Similar Documents

Publication Publication Date Title
JP3086857B2 (ja) 寒冷の発生方法、この方法を用いた冷却サイクル並びにこの方法を用いた空気精留方法及び装置
CN101460801B (zh) 二氧化碳纯化方法
CA1174587A (en) Nitrogen generator cycle
US4592766A (en) Parallel stream heat exchange for separation of ethane and higher hydrocarbons from a natural or refinery gas
CA1161745A (en) Low power, freon refrigeration assisted air separation
US3508412A (en) Production of nitrogen by air separation
US4382366A (en) Air separation process with single distillation column for combined gas turbine system
KR102261625B1 (ko) 중압 극저온 공기 분리 유닛으로부터의 질소 및 아르곤의 고 회수율을 위한 시스템 및 방법
US4806136A (en) Air separation method with integrated gas turbine
RU2397412C2 (ru) Способ и устройство для выделения продуктов из синтез-газа
EP0357299B1 (en) Air separation
CN201199120Y (zh) 一种空气回热式的矿井瓦斯气的分离液化设备
JP4057668B2 (ja) 空気を成分分離して窒素を生産する方法及び装置
CN102047057B (zh) 分离空气的方法和设备
CN1185456C (zh) 制备氮的装置和方法
CN1141547C (zh) 氮的产生方法和设备
US4746343A (en) Method and apparatus for gas separation
CN1136426C (zh) 通过冷冻分离从空气中生产高纯氮的方法及其采用的设备
CN115069057B (zh) 一种低温精馏提纯回收二氧化碳的方法
US3740962A (en) Process of and apparatus for the recovery of helium from a natural gas stream
US3241327A (en) Waste heat recovery in air fractionation
CN101509722A (zh) 蒸馏方法和设备
MXPA96005403A (en) Nitrogen generation method and apparatus
CN1117260C (zh) 空气的分离方法和装置
CN1952569A (zh) 含空气煤层气液化工艺及设备

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
C14 Grant of patent or utility model
GR01 Patent grant
ASS Succession or assignment of patent right

Owner name: LINDE AKTIENGESELLSCHAFT

Free format text: FORMER OWNER: BCC INC.

Effective date: 20050218

C41 Transfer of patent application or patent right or utility model
TR01 Transfer of patent right

Effective date of registration: 20050218

Address after: German Horace in Leningrad Sikeluosi

Patentee after: Linde AG

Address before: new jersey

Patentee before: Boc Group Inc.

EE01 Entry into force of recordation of patent licensing contract

Assignee: Linde Engineering (Hangzhou) Co., Ltd.

Assignor: Linde AG

Contract fulfillment period: 2006.7.30 to 2015.7.30 contract change

Contract record no.: 2009990000828

Denomination of invention: Apparatus and method for producing nitrogen

Granted publication date: 20050119

License type: Exclusive license

Record date: 2009.7.31

LIC Patent licence contract for exploitation submitted for record

Free format text: EXCLUSIVE LICENSE; TIME LIMIT OF IMPLEMENTING CONTACT: 2006.7.30 TO 2015.7.30; CHANGE OF CONTRACT

Name of requester: LINDE ENGINEERING( HANGZHOU ) CO., LTD.

Effective date: 20090731

CF01 Termination of patent right due to non-payment of annual fee

Granted publication date: 20050119

Termination date: 20160126

EXPY Termination of patent right or utility model