[go: up one dir, main page]

CN1025067C - 精馏分离空气的方法及装置 - Google Patents

精馏分离空气的方法及装置 Download PDF

Info

Publication number
CN1025067C
CN1025067C CN90100334A CN90100334A CN1025067C CN 1025067 C CN1025067 C CN 1025067C CN 90100334 A CN90100334 A CN 90100334A CN 90100334 A CN90100334 A CN 90100334A CN 1025067 C CN1025067 C CN 1025067C
Authority
CN
China
Prior art keywords
column
pipeline
medium pressure
oxygen
argon
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
CN90100334A
Other languages
English (en)
Other versions
CN1045172A (zh
Inventor
迪特里希·罗特曼
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
Linde GmbH
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
Priority claimed from DE19893905521 external-priority patent/DE3905521A1/de
Application filed by Linde GmbH filed Critical Linde GmbH
Publication of CN1045172A publication Critical patent/CN1045172A/zh
Application granted granted Critical
Publication of CN1025067C publication Critical patent/CN1025067C/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
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—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
    • F25J3/04672—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 having a top condenser
    • F25J3/04678—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 having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
    • 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
    • F25J3/0423—Subcooling of liquid process 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
    • F25J3/04327—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 argon or argon enriched stream
    • 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
    • F25J3/04406—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 dual pressure main column system
    • F25J3/04412—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 dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure 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
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04709—Producing crude argon in a crude argon column as an auxiliary column system in at least a dual pressure main column system
    • 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
    • F25J2200/20—Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/52—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/58—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being argon or crude argon
    • 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
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • 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
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/923—Inert gas
    • Y10S62/924—Argon

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

本发明披露了藉精馏并接着制取粗氩的空气分离工艺及装置。粗氩精馏段(20)的运行压力比两级空气精馏塔(2)的中压塔(4)的压力要低。

Description

本发明涉及一种精馏分离空气的方法，其中将空气压缩、预净化、冷却，然后在两级精馏塔的高压塔中粗分馏成富氮馏分和富氧液体，并将这两种馏分至少部分地输入精馏塔的中压塔中分离成氧和氮，从中压塔中抽出含氩的氧气流并送往粗氩精馏塔中;此外，本发明的还涉及实施该方法的装置。
这种用空气分离之后制取粗氩的方法，已由联邦德国专利局公开说明书DE-OS    3436897所公开。
如同在迄今运用的方法中所习以为常的那样，在先前已公开的方法中，粗氩的精馏是在含氩的氧馏分由中压塔取出的压力条件下进行的。从粗氩精馏塔取出的液态氧在大体相同的部位回送至中压塔。
如果中压塔基本上在大气压力下工作，从而粗氩精馏也基本上在大气压力下进行，则这种工艺是有利的。但在许多情况下，例如在煤气化装置中或者为在采油采气时进行吹氮时，中压塔产生的氧和/或氮却处于高压下。因此，为获得具有一定压力的氮和氧，使中压塔在约2.0～8.0bar的高压下运行，这比起对无压力情况下获得的产物最后再进行压缩的方法，经济上更有利一些。
但由于在已知方法中，粗氩精馏塔也必须在高压下运行，故而也产生一些不足之处，因为在此条件下，只能达到相当小的氩产率。
本发明的任务是，要对本说明书开始部分所提到的 那种方法及装置加以改进，使之不仅能经济地生产具有一定压力的氮和氧，而且也能以低成本制取氩。
此项任务是通过使粗氩精馏塔在低于中压塔压力的条件下运行来解决的。
因此，粗氩精馏时的压力比不再受中压塔压力比约束，从而可保持对氩产率来说最佳的值为1.1～2.0bar，优选1.3～1.5bar。尽管如此，中压塔还能在高压下放出氧和氮。
按照本发明的方法，在含氩的氧流被输入粗氩精馏塔之前先予以作功膨胀是有益的。膨胀时所回收的能量可用来压缩其他的过程料流。除此以外，作功膨胀时还会产生很多分离空气所需的冷量。以此方法，至少可以部分地取消外加冷量的输入。
同时，在作功膨胀之前，将含氩的氧流加热也是有利的。这可通过与其他的过程料流换热来进行，以与待分离的空气换热来进行为佳。
通常所产生的液态粗氩精馏剩余馏分，主要由氧组成。由于将此馏分废弃是不经济的，根据本发明的另一特征，将该液态馏分从粗氩精馏塔回输至中压塔，并在输入中压塔之前，用泵增至中压塔的压力。
事实证明，使粗氩精馏塔顶的气相馏分通过与来自高压塔的、蒸发着富氧液体进行间接换热而冷凝是有利的。以此方法，可利用工艺中现有的冷量来形成供粗氩精馏用的回流，并可取消在此工作区使用外加冷量。
最好将由此产生的被蒸发富氧馏分，再回输到中压 塔。
被蒸发的富氧馏分须在输入中压塔之前予以压缩。为此目的，按本发明方法的另一种方案，将含氩的氧流作功膨胀时所得到的功，至少部分地用来压缩被蒸发的富氧馏分。
此外，将被蒸发的富氧馏分压缩后进行冷却也是有利的。
本发明还涉及一种实施本发明所述的精馏分离空气的方法的装置。
附图中用示意图示出了本发明方法的一种实施方式，下面根据该图来进一步阐述本发明及本发明的其它细节。
经压缩并预净化的空气，经由管道1引入，在换热器36中经与产品流间接换热而冷却，并输入两级精馏塔2的高压塔3。用一个公用的冷凝器/蒸发器13将高压塔3（工作压力：6～20bar，以8～17bar为佳）同中压塔4（工作压力：1.5～10bar，以2.0～8.0bar为佳）相连，并使二者进行热交换。输入的空气在高压塔3中被粗分馏成氮和富氧馏分。液态富氧馏分经由管道6抽出，在换热器32中过冷，并有一部分经由阀门10节流而输入中压塔4。高压塔3顶部的氮同样以液态形式经由管道5抽出，在换热器32中过冷，其中一部分经由管道8作为液态产品抽出。由高压塔3出来的另一部分氮，经由管道9作为回流送到中压塔4。
液态氧（经管道14）、气态纯氮（经管道15）及不纯氮（经管道16）作为中压塔4的产品予以抽出，并在换热器 36中被加热，上述两股氮流则另外还在换热器32中被辅助加热。
除了至此已提及的物流外，还有一股含氩的氧流经由管道17从中压塔4抽出，使该氧流经换热器36复热，并输入粗氩精馏塔20，该塔在1.1～2.0bar的压力下工作，以在1.3～1.5bar的压力下工作为佳。在粗氩精馏塔20底部附带产生的其余馏分经由管道22予以抽出，并按本发明用泵23增压到向中压塔4回输所需的压力。除此以外，还使富氩氧流17在输入粗氩精馏塔20之前，经透平膨胀机18作功膨胀，使之一方面减到粗氩精馏塔20工作的低压，另一方面产生冷量。
在粗氩精馏塔20顶部产生的气态粗氩，经由管道33导入冷凝器35，部分被液化，并有一部分经由管道34作为回流输回粗氩精馏塔20，另一部分经由管道21作为中间产物抽出，并在换热器36中予以加热。
冷凝器35由来自高压塔的一部分富氧馏分（经管道6抽出）冷却，该部分馏分经由管道11引入，在换热器24中过冷，并经由管道25导入冷凝器35。同粗氩精馏塔20的塔顶气体进行间接换热时被蒸发的部分经由管道26抽出，并在换热器24及36中予以复热。
由于将该物流中所含的氧废弃在经济上不合算，所以在该实施例所述的方法中，将其回输到中压塔4。为达到所需的压力，将该富氧物流在两个压缩级27及29中进行压缩，每级压缩之后都要进行冷却（经水冷却器28及30）。接着，将富氧物流经由管道31输入换热器36， 在该换热器中再被冷却，随后输至中压塔4。在此过程中将含富氩的氧馏分17膨胀时所得的功用来驱动压缩机29是用利的。
可将管道1中的一部分空气在输入高压塔3之前在换热器中用来自中压塔4底部的氧予以冷凝。为此，可将来自中压塔底部的液体用泵增至高压，并在换热时部分蒸发。然后将部分冷凝的空气在高于附图所示的第一输入部位（管道1的输入部分）的位置输入高压塔3。此部分工艺在附图中未示出，但在给定的精馏压力下可能是有利的。
对于有经济意义的氩产率来说，必须生产出纯度至少为99.5%的产品氧（经管道14抽出），以便在富氩的氧流（流经管道17）中富集足量的氩。为此，在中压塔4中压力为5bar时，常规的方法需要的空气系数为5.86。而在本发明方法中该系数则减至5.45，从而节省能量7.0%。

Claims (13)

1、精馏分离空气的方法，其中空气(经管道1)经压缩、预净化、冷却(经换热器36)，以及在两级精馏塔(2)的高压塔(3)中粗分馏成富氮馏分(经管道5抽出)和富氧液体(经管道6抽出)，并将这两种馏分至少部分地输入精馏塔(2)的中压塔(4)，然后分离成氧和氮，将含氩的氧流(经管道17)从中压塔(4)抽出，并输向粗氩精馏塔(20)，其特征在于，粗氩精馏塔(20)的运行压力低于中压塔(4)的工作压力。
2、如权利要求1所述的方法，其特征在于，使含氩的氧流（经管道17）在被引入粗氩精馏塔（20）之前作功膨胀。
3、如权利要求2所述的方法，其特征在于，使含氩的氧流（经管道17）在作功膨胀（经透平膨胀机18）之前先进行加热。
4、如权利要求1至3中任一项所述的方法，其特征在于，将来自粗氩精馏塔（20）的液态馏分（经管道22）回输至中压塔（4），并在输入中压塔（4）之前用泵（23）增至中压塔（4）的压力。
5、如权利要求1至4中任一项所述的方法，其特征在于，使粗氩精馏塔（20）顶部的气态馏分（经管道33）在与来自高压塔（3）的蒸发着的富氧液体（经管道25）间接换热（经冷凝器35）的过程中冷凝。
6、如权利要求5所述的方法，其特征在于，将蒸发过的富氧馏分（经管道26）回输到中压塔（4）。
7、如权利要求6所述的方法，其特征在于，将蒸发过的富氧馏分（经管道26）在输入中压塔（4）之前进行压缩（经压缩级27、29）。
8、如权利要求7所述的方法，其特征在于，至少部分地将含氩的氧流（经管道17）作功膨胀（经膨胀机18）时所得的功用来压缩（经压缩级29）已蒸发的富氧馏分（经管道26）。
9、如权利要求7或8所述的方法，其特征在于，使已蒸发的富氧馏分（经管道31）在压缩（经压缩级27、29）后进行冷却（经换热器36）。
10、实施权利要求1至9任一项所述方法的装置，该装置包括一座由高压塔（3）和中压塔（4）构成的两级精馏塔（2），并包括一座粗氩精馏塔（20）和位于中压塔（4）和粗氩精馏塔（20）之间的第一连接管道（17、19）及第二连接管道（22），其特征在于，在第一连接管道（17、19）中，装有减压装置（18）。
11、如权利要求10所述的装置，其特征在于，在第二连接管道（22）中装有一台泵（23）。
12、如权利要求10或11所述的装置，其特征在于，包括一台经由第一气体导管（33）及经由第一液体导管（34）与粗氩精馏塔（20）连通并经由第二液体导管（25）与高压塔（3）连通的换热器（35），一根使换热器（35）与中压塔（4）连通的第二气体导管（26、31），以及一台位于第二气体导管（26、31）上的压缩机（27、29）。
13、如权利要求12所述的装置，其特征在于，用一台透平膨胀机作减压装置（18），并使该机器同第二气体导管上的压缩机（29）偶联。
CN90100334A 1989-02-23 1990-01-23 精馏分离空气的方法及装置 Expired - Fee Related CN1025067C (zh)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE19893905521 DE3905521A1 (de) 1989-02-23 1989-02-23 Verfahren und vorrichtung zur luftzerlegung durch rektifikation
DEP3905521.3 1989-02-23
US07/483,142 US5034043A (en) 1989-02-23 1990-02-22 Air separation with argon recovery

Publications (2)

Publication Number Publication Date
CN1045172A CN1045172A (zh) 1990-09-05
CN1025067C true CN1025067C (zh) 1994-06-15

Family

ID=47087703

Family Applications (1)

Application Number Title Priority Date Filing Date
CN90100334A Expired - Fee Related CN1025067C (zh) 1989-02-23 1990-01-23 精馏分离空气的方法及装置

Country Status (6)

Country Link
US (1) US5034043A (zh)
EP (1) EP0384213B1 (zh)
JP (1) JPH02247485A (zh)
CN (1) CN1025067C (zh)
DE (1) DE59000514D1 (zh)
ZA (1) ZA901345B (zh)

Families Citing this family (25)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5129932A (en) * 1990-06-12 1992-07-14 Air Products And Chemicals, Inc. Cryogenic process for the separation of air to produce moderate pressure nitrogen
US5161380A (en) * 1991-08-12 1992-11-10 Union Carbide Industrial Gases Technology Corporation Cryogenic rectification system for enhanced argon production
DE4126945A1 (de) * 1991-08-14 1993-02-18 Linde Ag Verfahren zur luftzerlegung durch rektifikation
US5235816A (en) * 1991-10-10 1993-08-17 Praxair Technology, Inc. Cryogenic rectification system for producing high purity oxygen
US5207066A (en) * 1991-10-22 1993-05-04 Bova Vitaly I Method of air separation
US5255522A (en) * 1992-02-13 1993-10-26 Air Products And Chemicals, Inc. Vaporization of liquid oxygen for increased argon recovery
US5245831A (en) * 1992-02-13 1993-09-21 Air Products And Chemicals, Inc. Single heat pump cycle for increased argon recovery
US5228296A (en) * 1992-02-27 1993-07-20 Praxair Technology, Inc. Cryogenic rectification system with argon heat pump
US5275003A (en) * 1992-07-20 1994-01-04 Air Products And Chemicals, Inc. Hybrid air and nitrogen recycle liquefier
CA2100402A1 (en) * 1992-07-20 1994-01-21 Lawrence Walter Pruneski Elevated pressure liquefier
US5305611A (en) * 1992-10-23 1994-04-26 Praxair Technology, Inc. Cryogenic rectification system with thermally integrated argon column
US5311744A (en) * 1992-12-16 1994-05-17 The Boc Group, Inc. Cryogenic air separation process and apparatus
FR2699992B1 (fr) * 1992-12-30 1995-02-10 Air Liquide Procédé et installation de production d'oxygène gazeux sous pression.
US6082136A (en) * 1993-11-12 2000-07-04 Daido Hoxan Inc. Oxygen gas manufacturing equipment
US5469710A (en) * 1994-10-26 1995-11-28 Praxair Technology, Inc. Cryogenic rectification system with enhanced argon recovery
AU743283B2 (en) 1998-04-21 2002-01-24 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and installation for air distillation with production of argon
FR2777641B1 (fr) * 1998-04-21 2000-05-19 Air Liquide Procede et installation de distillation d'air avec production d'argon
FR2787562B1 (fr) * 1998-12-22 2001-02-09 Air Liquide Procede et installation de distillation d'air avec production d'argon
US6318120B1 (en) * 2000-08-11 2001-11-20 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Cryogenic distillation system for air separation
EP1300640A1 (de) * 2001-10-04 2003-04-09 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung von hoch reinem Stickstoff durch Tieftemperaturzerlegung von Luft
US7549301B2 (en) * 2006-06-09 2009-06-23 Praxair Technology, Inc. Air separation method
CN100445671C (zh) * 2007-02-12 2008-12-24 庞启东 利用尾气余热的氨水吸收式制冷装置
US8448463B2 (en) * 2009-03-26 2013-05-28 Praxair Technology, Inc. Cryogenic rectification method
FR2953915B1 (fr) * 2009-12-11 2011-12-02 Air Liquide Procede et appareil de separation d'air par distillation cryogenique
CN104406364B (zh) * 2014-11-06 2016-10-05 杭州杭氧股份有限公司 一种双塔耦合的氩气回收纯化设备及氩气回收纯化方法

Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3127260A (en) * 1964-03-31 Separation of air into nitrogen
US3079759A (en) * 1961-03-22 1963-03-05 Air Prod & Chem Separation of gaseous mixtures
FR2041701B1 (zh) * 1969-05-05 1974-02-01 Air Liquide
DE1922956B1 (de) * 1969-05-06 1970-11-26 Hoechst Ag Verfahren zur Erzeugung von argonfreiem Sauerstoff durch Rektifikation von Luft
IT1034545B (it) * 1975-03-26 1979-10-10 Siad Processo ed impianto per l otte nimento dell argon a partire da un processo di frazionamento dell aria
DE3436897A1 (de) * 1984-10-08 1986-04-10 Linde Ag, 6200 Wiesbaden Verfahren und vorrichtung zum betreiben einer luftzerlegungsanlage
US4756731A (en) * 1986-02-20 1988-07-12 Erickson Donald C Oxygen and argon by back-pressured distillation
GB2198514B (en) * 1986-11-24 1990-09-19 Boc Group Plc Air separation
US4842625A (en) * 1988-04-29 1989-06-27 Air Products And Chemicals, Inc. Control method to maximize argon recovery from cryogenic air separation units

Also Published As

Publication number Publication date
EP0384213B1 (de) 1992-12-02
US5034043A (en) 1991-07-23
ZA901345B (en) 1992-06-24
EP0384213A3 (en) 1990-10-24
DE59000514D1 (de) 1993-01-14
JPH02247485A (ja) 1990-10-03
CN1045172A (zh) 1990-09-05
EP0384213A2 (de) 1990-08-29

Similar Documents

Publication Publication Date Title
CN1025067C (zh) 精馏分离空气的方法及装置
EP0496355B1 (en) Method and apparatus for producing elevated pressure nitrogen
US4433989A (en) Air separation with medium pressure enrichment
US4702757A (en) Dual air pressure cycle to produce low purity oxygen
JP2865274B2 (ja) 酸素と窒素を気体及び／又は液体製品として同時に製造するための空気の低温蒸留法
CN1119606C (zh) 制备氧的有效方法
US4133662A (en) Production of high pressure oxygen
EP0153673B1 (en) Dual feed air pressure nitrogen generator cycle
EP0147460B1 (en) Cryogenic triple-pressure air separation with lp-to-mp latent-heat-exchange
CN1069329A (zh) 精馏分离空气的方法和设备
US4254629A (en) Cryogenic system for producing low-purity oxygen
EP0425738B2 (en) Process for the production of high pressure nitrogen with split reboil-condensing duty
CN1057380C (zh) 低温空气分离方法和设备
US5373699A (en) Process for the production of nitrogen by cryogenic distillation of atmospheric air
JPH05157448A (ja) 供給材料空気流れを構成成分に分離する極低温法
US4704147A (en) Dual air pressure cycle to produce low purity oxygen
EP0921367A2 (en) Production of nitrogen
EP1258690A1 (en) Nitrogen rejection method
CN113405318A (zh) 一种使用单个精馏塔生产纯氮的装置及其使用方法
NO169977B (no) Fremgangsmaate for separering av luft ved kryogen destillasjon
JPH10185425A (ja) 純粋でない酸素と純粋窒素の製造方法
US4783208A (en) Air separation
CN1068883A (zh) 按照需求变化的模式供给气态氧的空气分离方法
KR20220166824A (ko) 공기의 극저온 분류 공정, 공기 분류 플랜트 및 적어도 2개의 공기 분류 플랜트로 구성된 통합 시스템
US5230217A (en) Inter-column heat integration for multi-column distillation system

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
C15 Extension of patent right duration from 15 to 20 years for appl. with date before 31.12.1992 and still valid on 11.12.2001 (patent law change 1993)
OR01 Other related matters
C19 Lapse of patent right due to non-payment of the annual fee
CF01 Termination of patent right due to non-payment of annual fee