EP1209431B1 - Procédé et dispositif de production d'oxygène et d'azote - Google Patents

Procédé et dispositif de production d'oxygène et d'azote Download PDF

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Publication number
EP1209431B1
EP1209431B1 EP01127958A EP01127958A EP1209431B1 EP 1209431 B1 EP1209431 B1 EP 1209431B1 EP 01127958 A EP01127958 A EP 01127958A EP 01127958 A EP01127958 A EP 01127958A EP 1209431 B1 EP1209431 B1 EP 1209431B1
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EP
European Patent Office
Prior art keywords
pressure column
low
nitrogen
liquid
oxygen
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 - Lifetime
Application number
EP01127958A
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German (de)
English (en)
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EP1209431A1 (fr
Inventor
Herbert Schoenecker
Jürgen Voit
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
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Linde GmbH
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Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Publication of EP1209431A1 publication Critical patent/EP1209431A1/fr
Application granted granted Critical
Publication of EP1209431B1 publication Critical patent/EP1209431B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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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
    • F25J3/04151—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
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
    • F25J3/04224—Cores associated with a liquefaction or refrigeration cycle
    • 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
    • F25J3/04351—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 nitrogen
    • F25J3/04357—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 nitrogen and comprising a gas work expansion 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
    • 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
    • F25J3/04406—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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • F25J2200/54—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the low pressure column of a double 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
    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • 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
    • F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being nitrogen

Definitions

  • the invention relates to a process for the production of oxygen and nitrogen Cryogenic air separation according to the preamble of patent claim 1.
  • the invention has for its object a method of the type mentioned and specify a corresponding device that is particularly economical work.
  • the cooling liquid is in contrast to the invention by a Liquid formed, the composition of the bottom liquid of the pressure column equivalent.
  • the composition of the cooling fluid can be so be chosen that the product yield, especially the oxygen yield is increased.
  • the intermediate liquid, which is used as cooling fluid in the top condenser, from an intermediate point is subtracted, for example 10 to 20 theoretical floors above the point is where the oxygen-containing liquid fraction from the pressure column in the Low pressure column is fed.
  • the process can use liquid nitrogen from or from the low pressure column Top condenser removed and discharged as a liquid nitrogen product.
  • the process preferably has a nitrogen cycle on.
  • cycle nitrogen becomes gaseous from the upper area of the pressure column withdrawn and compressed in a circuit compressor, a first partial flow of compressed cycle nitrogen is relieved of work and a second Partial stream of the compressed cycle nitrogen liquefied and into the rectification system fed back and / or taken as a further liquid nitrogen product.
  • On such a cycle can also be carried out without oxygen production, for example with Use of the bottom liquid from low pressure column or pressure column as cooling fluid in the top condenser of the low pressure column.
  • the liquefied circulating nitrogen can be one of the Columns of the rectification system are fed, preferably the pressure column. The the corresponding amount can then be a liquid nitrogen and / or oxygen product be withdrawn from the rectification system.
  • Top nitrogen from the pressure column is liquefied in a main condenser. That included generated condensate is at least partly, preferably largely, as Return to the pressure column abandoned. Another part of the condensate can be on top introduced into the low pressure column and / or immediately as a liquid nitrogen product subtracted from.
  • the circuit can be designed as a two or more turbine system by one third partial stream of compressed cycle nitrogen independent of the first Partial stream is relaxed while working.
  • the invention also relates to a device according to claim 8 or 9.
  • An oxygen-containing liquid fraction (8) from the bottom of the pressure column is in one Cooled subcooler 9 and via line 10 at an intermediate point in the , Low pressure column 5 initiated.
  • gaseous top nitrogen is converted into a first part 11 in Main condenser 6 at least partially, preferably completely liquefied.
  • the the condensate 12 produced thereby becomes a first part 13 as a return flow onto the head the pressure column 4 abandoned.
  • a second part 14 of the main capacitor 6 condensed nitrogen 11 is introduced into the low pressure column.
  • Liquid nitrogen 19 is drawn off at the top of the low-pressure column and after Separation of flash gas in a separator 20 via line 21 as a liquid Withdrawn nitrogen product and introduced a tank 22.
  • the flash gas 23 is the Residual gas 16 admixed.
  • the residual mixture 24 is in the subcoolers 25, 9 and Main heat exchanger 2 warmed up and finally via line 27 into the atmosphere blown off and / or as a regeneration gas for the device, not shown Purification of the feed air used.
  • a second partial stream of the compressed cycle nitrogen is passed through line 42 two series-connected post-compressors 43, 45, each of which has an after-cooler 44, 46 follows.
  • the second partial flow continues to the first circuit heat exchanger 37 (Line 47), is further cooled in the second circuit heat exchanger 40 and finally liquefied or - in the third circuit heat exchanger 48 supercritical pressure - pseudo-liquefied.
  • a third partial flow of the compressed cycle nitrogen is combined with the second partial flow through the post-compressors 43, 45 and the first and second Circuit heat exchanger 37, 40 out.
  • the third substream 56 becomes one cold turbine 57 led.
  • the work-relieved, relaxed third partial flow overflows Line 58 through the three circuit heat exchangers 48, 40, 37 to the entry of the Circuit compressor back.
  • the cold parts of the system are in an insulating housing (cold box) 64 arranged.

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

Claims (7)

  1. Procédé en vue de la fabrication d'oxygène et d'azote par fractionnement d'air à basse température dans un système de rectification, qui présente une colonne sous pression (4) et une colonne à basse pression (5), l'air de charge (1, 3) étant introduit au cours du procédé dans la colonne sous pression (4), une fraction fluide contenant de l'oxygène (8, 10) étant prélevée hors de la colonne sous pression (4) et étant injectée dans la colonne à basse pression (5), de l'azote gazeux (17) étant condensé au moins partiellement hors de la colonne à basse pression (5) dans un condenseur de tête (7) par échange thermique indirect avec un réfrigérant qui s'évapore (15), un courant de produit d'azote (19) étant prélevé hors de la colonne à basse pression (5), et un courant de produit d'oxygène (61, 62, 63) étant évacué hors de la colonne à basse pression (5) sous forme fluide et/ou gazeuse, le réfrigérant pour le condenseur de tête (7) de la colonne à basse pression (5) étant formé par un liquide intermédiaire (15) qui est extrait d'un point intermédiaire de la colonne à basse pression (5), caractérisé en ce que le liquide intermédiaire (15) est extrait d'un point intermédiaire, qui se situe au dessus du point où la fraction fluide contenant de l'oxygène (8, 10) est injectée hors de la colonne sous pression (4) dans la colonne à basse pression (5), et en dessous du point où le courant de produit d'azote (19) est prélevé.
  2. Procédé selon la revendication 1, caractérisé en ce que l'azote liquide (19) est extrait de la colonne à basse pression (5) ou de son condenseur de tête (7) et est évacué en tant que produit d'azote fluide (22).
  3. Procédé selon l'une quelconque des revendications 1 à 2, caractérisé en ce que l'azote en circuit fermé (28, 29, 30, 31, 32) est extrait sous forme gazeuse hors du domaine supérieur de la colonne sous pression (4) et est comprimé dans un compresseur en circuit fermé (33), un premier courant partiel (36) de l'azote en circuit fermé comprimé (35) étant détendu en fournissant du travail (38) et un deuxième courant partiel (42, 47, 50) de l'azote en circuit fermé comprimé (35) étant liquéfié et alimenté en retour (52) dans le système de rectification et/ou étant prélevé en tant que produit d'azote liquide supplémentaire.
  4. Procédé selon l'une quelconque des revendications 1 à 3, caractérisé en ce que l'azote de tête (11) est liquéfié hors de la colonne sous pression (4) dans un condenseur principal (6).
  5. Procédé selon la revendication 4, caractérisé en ce que le condensat (12) formé dans le condenseur principal est introduit au moins partiellement (14) dans la colonne à basse pression.
  6. Procédé selon la revendication 4 ou 5, caractérisé en ce que le condensat (12) formé dans le condenseur principal est évacué au moins en partie en tant que produit d'azote liquide (22).
  7. Dispositif en vue de la fabrication d'oxygène et d'azote par fractionnement d'air à basse température à l'aide d'un système de rectification, qui présente une colonne sous pression (4) et une colonne à basse pression (5), avec un conduit de charge (1, 3) en vue de l'introduction de l'air de charge dans la colonne sous pression (4), avec un conduit pour liquide (8, 10) en vue du transfert d'une fraction fluide contenant de l'oxygène hors de la colonne sous pression (4) dans la colonne à basse pression (5), avec un condenseur de tête (7) dont l'espace de liquéfaction est relié (17, 18) au domaine supérieur de la colonne à basse pression (5) et dont l'espace de vaporisation est relié à un conduit de réfrigérant (15) en vue de l'introduction d'un réfrigérant, avec un conduit de produit d'azote (19), qui est relié à la colonne à basse pression (5) et avec un conduit de produit d'oxygène (61, 62, 63), qui est relié à la colonne à basse pression (5), le réfrigérant (15) étant relié à un point intermédiaire de la colonne à basse pression (5), caractérisé en ce que le point intermédiaire, auquel le réfrigérant (15) est relié à la colonne à basse pression (5), se situe au dessus du point, auquel le conduit pour liquide (8, 10) débouche dans la colonne à basse pression (5) en vue du transfert d'une fraction fluide contenant de l'oxygène hors de la colonne sous pression (4), et en dessous du point auquel le conduit de produit d'azote (19) est relié à la colonne à basse pression (5).
EP01127958A 2000-11-24 2001-11-23 Procédé et dispositif de production d'oxygène et d'azote Expired - Lifetime EP1209431B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE10058332A DE10058332A1 (de) 2000-11-24 2000-11-24 Verfahren und Vorrichtung zur Erzeugung von Sauerstoff und Stickstoff
DE10058332 2000-11-24

Publications (2)

Publication Number Publication Date
EP1209431A1 EP1209431A1 (fr) 2002-05-29
EP1209431B1 true EP1209431B1 (fr) 2004-06-09

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Family Applications (1)

Application Number Title Priority Date Filing Date
EP01127958A Expired - Lifetime EP1209431B1 (fr) 2000-11-24 2001-11-23 Procédé et dispositif de production d'oxygène et d'azote

Country Status (4)

Country Link
US (1) US6490884B2 (fr)
EP (1) EP1209431B1 (fr)
AT (1) ATE268893T1 (fr)
DE (2) DE10058332A1 (fr)

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20150168058A1 (en) * 2013-12-17 2015-06-18 L'air Liquide, Societe Anonyme Pour I'etude Et I'exploitation Des Procedes Georges Claude Apparatus for producing liquid nitrogen
US20150168057A1 (en) * 2013-12-17 2015-06-18 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process for producing liquid nitrogen
CN109676367A (zh) * 2018-12-28 2019-04-26 乔治洛德方法研究和开发液化空气有限公司 一种热交换器组件及装配所述热交换器组件的方法

Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4439220A (en) * 1982-12-02 1984-03-27 Union Carbide Corporation Dual column high pressure nitrogen process
US4832719A (en) * 1987-06-02 1989-05-23 Erickson Donald C Enhanced argon recovery from intermediate linboil
US5006139A (en) * 1990-03-09 1991-04-09 Air Products And Chemicals, Inc. Cryogenic air separation process for the production of nitrogen
US5137559A (en) * 1990-08-06 1992-08-11 Air Products And Chemicals, Inc. Production of nitrogen free of light impurities
US5697229A (en) * 1996-08-07 1997-12-16 Air Products And Chemicals, Inc. Process to produce nitrogen using a double column plus an auxiliary low pressure separation zone
US5682762A (en) * 1996-10-01 1997-11-04 Air Products And Chemicals, Inc. Process to produce high pressure nitrogen using a high pressure column and one or more lower pressure columns
DE19735154A1 (de) * 1996-10-30 1998-05-07 Linde Ag Verfahren und Vorrichtung zur Gewinnung von Druckstickstoff
EP0955509B1 (fr) * 1998-04-30 2004-12-22 Linde Aktiengesellschaft Procédé et appareil pour la production d'oxygène à haute pureté
DE19902255A1 (de) 1999-01-21 2000-07-27 Linde Tech Gase Gmbh Verfahren und Vorrichtung zur Gewinnung von Druckstickstoff

Also Published As

Publication number Publication date
US20020062658A1 (en) 2002-05-30
EP1209431A1 (fr) 2002-05-29
DE10058332A1 (de) 2002-05-29
DE50102525D1 (de) 2004-07-15
US6490884B2 (en) 2002-12-10
ATE268893T1 (de) 2004-06-15

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