CA2828716A1 - Device and method for separating air by cryogenic distillation - Google Patents

Device and method for separating air by cryogenic distillation Download PDF

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Publication number
CA2828716A1
CA2828716A1 CA2828716A CA2828716A CA2828716A1 CA 2828716 A1 CA2828716 A1 CA 2828716A1 CA 2828716 A CA2828716 A CA 2828716A CA 2828716 A CA2828716 A CA 2828716A CA 2828716 A1 CA2828716 A1 CA 2828716A1
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Canada
Prior art keywords
oxygen
exchanger
pressure
air
column
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CA2828716A
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French (fr)
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CA2828716C (en
Inventor
Marie Cognard
Benoit Davidian
Richard Dubettier-Grenier
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Publication of CA2828716A1 publication Critical patent/CA2828716A1/en
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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
    • F25J3/04006—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
    • F25J3/0228—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 characterised by the separated product 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
    • F25J3/04006—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
    • F25J3/04103—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 using solely hydrostatic liquid head
    • 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
    • F25J3/04206—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
    • 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
    • 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
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low 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
    • F25J3/04406—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
    • F25J3/04406—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
    • F25J3/04418—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 with thermally overlapping high and low pressure columns
    • 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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • F25J3/04824—Stopping of the process, e.g. defrosting or deriming; Back-up procedures
    • 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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • F25J3/04836—Variable air feed, i.e. "load" or product demand during specified periods, e.g. during periods with high respectively low power costs
    • 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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04854—Safety aspects of operation
    • F25J3/0486—Safety aspects of operation of vaporisers for oxygen enriched liquids, e.g. purging of liquids
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • 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
    • F25J2250/30—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
    • F25J2250/40—One fluid 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
    • F25J2250/30—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
    • F25J2250/50—One fluid being 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/62—Details of storing a fluid in a tank

Abstract

Device for separating air comprises a pipe for withdrawing liquid oxygen from the low-pressure column and for sending it to a first pump (39), a pipe for sending liquid oxygen that has been pressurized to a pressure of below 9 bar abs from the first pump to a vaporizer (41), a pipe for sending gaseous oxygen from the vaporizer to a main exchanger (21) where it is heated up, a pipe for sending liquid oxygen for purging from the vaporizer to a second pump (63) to pressurize it and a pipe for sending the pressurized oxygen from the second pump to an exchanger where it vaporizes to form gaseous oxygen.

Description

Appareil et procédé de séparation d'air par distillation cryogénique La présente invention est relative à un appareil et procédé de séparation d'air par distillation d'air.
En particulier elle concerne la production d'oxygène gazeux à une pression inférieure à 9 bars abs, voire inférieure à 5 bars abs. L'oxygène gazeux peut éventuellement contenir moins de 98% mol. d'oxygène.
Il est nécessaire de produire de grandes quantités d'oxygène ayant ces caractéristiques pour alimenter les appareils d'oxycombustion, entre autres.
Il est connu de WO-A-10/109149 de vaporiser un débit d'oxygène liquide à basse pression dans un vaporiseur extérieur pour produire de l'oxygène gazeux qui se réchauffe ensuite dans un échangeur principal.
Il est connu de vaporiser la purge d'une colonne de distillation afin d'en récupérer les frigories, par exemple dans US-A-5408831.
US-A-5765396 et US-A-5251451 décrivent des installations selon la préambule de la revendication 1.
Par contre la présente invention propose de vaporiser la purge de déconcentration d'un vaporiseur dans un échangeur afin de récupérer les frigories, ce vaporiseur étant l'échangeur permettant de vaporiser un liquide de l'appareil sous pression pour produire un produit gazeux sous pression.
Il est souhaitable d'envoyer la purge à un stockage gazeux sous pression permettant de maintenir une production stable aussi bien en débit, qu'en pression.
Selon un objet de l'invention, il est prévu un appareil de séparation d'air comprenant une double colonne comprenant une colonne moyenne pression et une colonne basse pression, un échangeur principal, un vaporiseur, un compresseur principal, des moyens pour envoyer tout l'air à traiter dans la double colonne au compresseur principal pour produire de l'air substantiellement à la pression P1 de la colonne moyenne pression, des moyens pour envoyer une partie de l'air substantiellement à une pression élevée P2 à l'échangeur principal et ensuite au vaporiseur, une conduite pour envoyer de l'air au moins partiellement condensé dans le vaporiseur à au moins Apparatus and method for separating air by cryogenic distillation The present invention relates to an apparatus and method of separation of air by distillation of air.
In particular, it relates to the production of gaseous oxygen at a pressure less than 9 bar abs, or even less than 5 bar abs. oxygen gaseous may optionally contain less than 98 mol%. oxygen.
It is necessary to produce large amounts of oxygen having these features to power oxy-fuel combustion devices, among others.
It is known from WO-A-10/109149 to vaporize a flow of liquid oxygen at low pressure in an outdoor vaporizer to produce oxygen gaseous which then warms up in a main heat exchanger.
It is known to vaporize the purge of a distillation column in order to recover the frigories, for example in US-A-5408831.
US-A-5765396 and US-A-5251451 describe installations according to the preamble of claim 1.
On the other hand, the present invention proposes to vaporize the purge of deconcentration of a vaporizer in an exchanger in order to recover the frigories, this vaporizer being the exchanger for vaporizing a liquid of the apparatus under pressure to produce a gaseous product under pressure.
It is desirable to send the purge to a gaseous storage under pressure to maintain stable production both in terms of throughput and pressure.
According to an object of the invention, there is provided an air separation apparatus comprising a double column comprising a medium pressure column and a low pressure column, a main exchanger, a vaporizer, a main compressor, means to send all the air to be treated in the double column to the main compressor to produce air substantially at the pressure P1 of the medium pressure column, means for sending some of the air substantially to a pressure high P2 at the main heat exchanger and then the vaporizer, a pipe for send air at least partially condensed in the vaporizer to at least

2 une des colonnes, une conduite pour envoyer de l'air à la pression P1 à la colonne moyenne pression, des moyens de pressurisation, une pompe, une conduite pour soutirer de l'oxygène liquide de la colonne basse pression et pour l'envoyer aux moyens de pressurisation, une conduite pour envoyer de l'oxygène liquide pressurisé à une pression inférieure à 9 bar abs des moyens de pressurisation au vaporiseur, une conduite pour envoyer de l'oxygène gazeux du vaporiseur à l'échangeur principal pour se réchauffer pour former un premier débit d'oxygène gazeux, une conduite de purge pour envoyer de l'oxygène liquide de purge du vaporiseur à la pompe pour le pressuriser caractérisée en ce que la conduite de purge n'est pas reliée à un stockage de liquide de purge et en ce qu'elle comprend une conduite pour envoyer l'oxygène pressurisé de la pompe à un échangeur pour se vaporiser, l'échangeur étant relié à une conduite d'air comprimé reliée au compresseur principal et à une conduite reliée à la double colonne, pour former un deuxième débit d'oxygène gazeux.
Optionnellement :
- l'échangeur relié à la conduite d'oxygène de purge est l'échangeur principal.
- l'échangeur relié à la conduite d'oxygène de purge est un échangeur distinct de l'échangeur principal.
- l'échangeur comprend des passages reliés à une conduite d'amenée d'air d'alimentation et des passages reliés à une conduite d'amenée de fluide frigorigène, provenant éventuellement de la double colonne.
- l'appareil comprend un stockage gazeux sous pression relié à
l'échangeur de vaporisation d'oxygène de purge pour recueillir l'oxygène gazeux.
Selon un autre objet de l'invention, il est prévu un procédé de séparation d'air dans un appareil comprenant une double colonne comprenant une colonne moyenne pression et une colonne basse pression, un échangeur principal, un vaporiseur, un compresseur principal, des moyens de pressurisation, une pompe, dans lequel on envoie tout l'air à traiter dans la double colonne au compresseur principal pour produire de l'air substantiellement à la pression de la colonne moyenne pression, on envoie une partie de l'air substantiellement à une pression élevée P2 à l'échangeur principal et ensuite au vaporiseur, on 2 one of the columns, a pipe to send air to the pressure P1 to the medium pressure column, pressurizing means, a pump, a conduct to withdraw liquid oxygen from the low pressure column and for send it to the means of pressurization, a pipe to send pressurized liquid oxygen at a pressure less than 9 bar abs means pressurizing vaporizer, a pipe to send oxygen gas from the vaporizer to the main heat exchanger to warm up to form a first flow of gaseous oxygen, a purge line for sending liquid oxygen purge from the vaporizer to the pump to pressurize it characterized in that the purge line is not connected to a storage of purge liquid and in that it includes a pipe to send pressurized oxygen from the pump to an exchanger to vaporize, the exchanger being connected to a compressed air line connected to the compressor principal and a line connected to the double column, to form a second flow rate of gaseous oxygen.
Optionally:
the exchanger connected to the purge oxygen line is the exchanger main.
the exchanger connected to the purge oxygen line is an exchanger separate from the main exchanger.
the exchanger comprises passages connected to a supply line supply air and passages connected to a fluid supply line refrigerant, possibly from the double column.
- the apparatus comprises a gas storage under pressure connected to the purge oxygen evacuation exchanger to collect oxygen gaseous.
According to another object of the invention, there is provided a separation process of air in an apparatus comprising a double column comprising a column medium pressure and a low pressure column, a main exchanger, a vaporizer, a main compressor, means of pressurization, a pump, in which we send all the air to be treated in the double column to main compressor to produce air substantially under pressure the middle pressure column, we send some of the air substantially at a high pressure P2 to the main exchanger and then to the vaporizer, one

3 envoie de l'air au moins partiellement condensé dans le vaporiseur à au moins une des colonnes, on envoie de l'air à la pression P1 à la colonne moyenne pression, on soutire de l'oxygène liquide de la colonne basse pression et on le pressurise, on envoie de l'oxygène liquide pressurisé à une pression inférieure à 5 bar abs au vaporiseur, on envoie un premier débit d'oxygène gazeux du vaporiseur à l'échangeur principal pour se réchauffer et on pressurise de l'oxygène liquide de purge du vaporiseur dans la pompe caractérisé en ce que l'oxygène liquide de purge est pressurisé sans avoir été stocké et ensuite est vaporisé dans un échangeur par échange de chaleur avec de l'air, comprimé
dans le compresseur principal et destiné à la double colonne, pour former un deuxième débit d'oxygène gazeux.
Optionnellement :
- l'oxygène de purge est pressurisé à une pression d'au moins 10 bars abs, de préférence au moins 15 bars abs, voire au moins 20 bars abs dans la deuxième pompe.
- l'oxygène de purge se vaporise dans l'échangeur principal.
- l'oxygène de purge se vaporise dans un échangeur autre que l'échangeur principal.
- le deuxième débit d'oxygène gazeux est envoyé à un stockage gazeux sous pression et sert de production de secours.
- une quantité variable du deuxième débit d'oxygène gazeux est mélangée avec le premier débit afin de produire un débit mélangé
substantiellement constant.
- l'oxygène liquide soutiré de la colonne basse pression contient au moins 80% mol. d'oxygène - l'oxygène liquide soutiré de la colonne basse pression constitue le seul débit contenant au moins 80% mol. d'oxygène soutiré de la colonne basse pression.
- l'oxygène liquide soutiré de la colonne basse pression contient au plus 98% mol. d'oxygène.
L'invention sera décrite en plus de détail en se référant aux figures qui illustrent des appareils de séparation d'air selon l'invention. 3 sends air at least partially condensed in the vaporizer to at least one of the columns, we send air at the pressure P1 to the middle column pressure, liquid oxygen is withdrawn from the low pressure column and the pressurizes, we send pressurized liquid oxygen to a pressure lower at 5 bar abs at the vaporizer, a first flow of gaseous oxygen is vaporizer at the main exchanger to warm up and pressurize the liquid oxygen purge of the vaporizer in the pump characterized in that the purge liquid oxygen is pressurized without being stored and then is vaporized in a heat exchanger by heat exchange with compressed air in the main compressor and intended for the double column, to form a second flow of oxygen gas.
Optionally:
the purge oxygen is pressurized at a pressure of at least 10 bar abs, preferably at least 15 bar abs, or even at least 20 bar abs in the second pump.
the purge oxygen vaporizes in the main exchanger.
the purge oxygen vaporizes in a heat exchanger other than the main exchanger.
the second flow of oxygen gas is sent to a storage gaseous under pressure and serves as backup production.
a variable quantity of the second rate of oxygen gas is mixed with the first flow to produce a mixed flow substantially constant.
the liquid oxygen withdrawn from the low pressure column contains at minus 80 mol%. oxygen the liquid oxygen withdrawn from the low pressure column constitutes the single flow containing at least 80 mol%. of oxygen withdrawn from the lower column pressure.
the liquid oxygen withdrawn from the low pressure column contains at plus 98 mol% oxygen.
The invention will be described in more detail with reference to the figures which illustrate air separation apparatus according to the invention.

4 Dans la Figure 1, l'appareil comprend une ligne d'échange 21 et une double colonne constituée par une colonne moyenne pression 27 et une colonne basse pression 29.
Tout l'air 1 est comprimé dans le compresseur principal 2 pour produire de l'air à la pression P1 substantiellement égale à la pression de la colonne moyenne pression 27. L'air à la pression P1 est refroidi dans un refroidisseur 7, épuré dans une unité d'épuration 9 et divisé en trois fractions. La première fraction 11 est surpressée dans un surpresseur, pouvant être constitué par le dernier étage du compresseur principal, dernier étage qui fait partie de la deuxième partie du compresseur. La pression P1 est inférieure à 5 bars abs, voire à 4.5 bar abs, préférablement inférieure à 4 bar, et encore inférieure à
3.5 bar abs La première fraction 11 est amenée à une pression P2 par le booster 5 ou un compresseur indépendant 5 et se refroidit à cette pression dans un refroidisseur (non-illustré) avant d'être envoyé à la ligne d'échange 21. La ligne d'échange est constituée par un échangeur de chaleur indirect en aluminium à
plaques brasées. La fraction 11 est ensuite envoyée sous forme gazeuse à un vaporiseur 41 où elle se condense au moins partiellement avant d'être détendue et envoyée à la colonne moyenne pression 27. La pression P2 est inférieure à 15 bar abs, préférablement inférieure à 10 bar, et encore inférieure à 6 bar abs. La fraction 11 est inférieure à la moitié du débit 1, et préférentiellement inférieure à un tiers du débit 1 La deuxième fraction 13 à la pression P1 se refroidit complètement dans la ligne d'échange 21 et est divisée en deux flux. Le premier flux 23 est envoyé
à un rebouilleur de cuve 33 de la colonne basse pression 29 où il se condense au moins partiellement et est envoyé à la colonne moyenne pression, mélangé
au débit 11. Le deuxième flux 25 est envoyé sous forme gazeuse à la colonne moyenne pression 27.
La troisième fraction 15 est surpressée dans un surpresseur 17, refroidie partiellement dans la ligne d'échange 21, soutirée de la ligne d'échange à un niveau intermédiaire de celle-ci et détendue dans une turbine 19 couplée au surpresseur 17 avant d'être envoyée à la colonne basse pression 29.
Un débit de liquide enrichi en oxygène 55, un débit intermédiaire 53 et un débit liquide riche en azote Si sont soutirés de la colonne moyenne pression 27, refroidis dans l'échangeur 31, détendus et envoyés à des niveaux différents de la colonne basse pression 29.
De l'azote gazeux moyenne pression 49 est condensé dans un vaporiseur intermédiaire 35 de la colonne basse pression 29 et envoyé comme 4 In Figure 1, the apparatus includes an exchange line 21 and a double column constituted by a medium pressure column 27 and a low pressure column 29.
All air 1 is compressed in the main compressor 2 to produce of air at the pressure P1 substantially equal to the pressure of the column medium pressure 27. The air at pressure P1 is cooled in a cooler purified in a purification unit 9 and divided into three fractions. The first one fraction 11 is overpressed in a booster, which can be constituted by the top floor of the main compressor, top floor which is part of the second part of the compressor. The pressure P1 is less than 5 bar abs, even at 4.5 bar abs, preferably less than 4 bar, and even lower than 3.5 bar abs The first fraction 11 is brought to a pressure P2 by the booster 5 or an independent compressor 5 and cools to that pressure in a cooler (not shown) before being sent to the exchange line 21.
line exchange consists of an indirect aluminum heat exchanger with brazed plates. Fraction 11 is then sent in gaseous form to a vaporizer 41 where it condenses at least partially before being relaxed and sent to the medium pressure column 27. The pressure P2 is less than 15 bar abs, preferably less than 10 bar, and even lower at 6 bar abs. Fraction 11 is less than half of flow 1, and preferentially less than one third of the flow 1 The second fraction 13 at the pressure P1 cools completely in the exchange line 21 and is divided into two streams. The first stream 23 is sent to a bottom reboiler 33 of the low pressure column 29 where it condenses at least partially and is sent to the medium pressure column, mixed at the flow rate 11. The second stream 25 is sent in gaseous form to the column medium pressure 27.
The third fraction is overpressed in a booster 17, cooled partially in the exchange line 21, drawn from the exchange line to a intermediate level thereof and relaxed in a turbine 19 coupled to the booster 17 before being sent to the low pressure column 29.
An oxygen-enriched liquid flow 55, an intermediate flow 53 and a N-rich liquid flow Si are withdrawn from the medium pressure column 27, cooled in the exchanger 31, relaxed and sent to levels different of the low pressure column 29.
Medium pressure nitrogen gas 49 is condensed in a intermediate vaporizer 35 of the low pressure column 29 and sent as

5 reflux en tête de la colonne moyenne pression 27. Un autre débit d'azote gazeux moyenne pression 47 se réchauffe dans la ligne d'échange.
De l'oxygène liquide 37, contenant au moins 80% mol. d'oxygène et éventuellement au plus 98% mol. d'oxygène, est soutiré en cuve de la colonne basse pression 29, pressurisé par une pompe 39 à une pression inférieure à 9 bars abs, voire inférieure à 5 bars abs et envoyé au vaporiseur 41. A part une purge de liquide 43, l'oxygène se vaporise dans le vaporiseur 41 par échange de chaleur avec la fraction d'air 11 à la pression P2. Cet oxygène forme ensuite le premier débit d'oxygène gazeux pressurisé 45 qui se réchauffe dans la ligne d'échange 21. La fraction d'air 11 se trouve partiellement condensée et est envoyée à la double colonne.
Le liquide de purge 43 est pressurisé jusqu'à une pression d'au moins 10 bars abs, ou d'au moins 15 bar abs, voire au moins 20 bars abs dans une pompe 63 puis se vaporise dans la ligne d'échange 21. Le deuxième débit gazeux ainsi produit 59 est envoyé à un stockage gazeux sous pression 3 et détendu pour être mélangé avec le débit 45 via la conduite 61.
Ici la vaporisation de liquide de purge s'effectue en utilisant principalement de la chaleur sensible, de sorte qu'aucun débit d'air sortant de l'échangeur 21 n'est totalement condensé, voire n'est condensé.
Alternativement comme illustré dans la Figure 2, le liquide de purge pressurisé 43 peut être vaporisé dans un échangeur auxiliaire 21A, distinct de la ligne d'échange, contre un débit d'air 25A et avec un débit de fluide frigorigène, par exemple un débit d'azote 57A se réchauffant du procédé de séparation.
Le débit 25A refroidi dans l'échangeur 21A se mélange avec le débit refroidi 25 et le débit d'azote 57A réchauffé dans l'échangeur 21A se mélange avec le débit réchauffé 57.
Le deuxième débit d'oxygène gazeux 59, 61 formé par la vaporisation peut être utilisé comme gaz de secours lors d'une interruption de la production d'oxygène gazeux 45. 5 reflux at the top of the medium pressure column 27. Another flow of nitrogen gaseous medium pressure 47 heats up in the exchange line.
Liquid oxygen 37, containing at least 80 mol%. of oxygen and optionally at most 98 mol%. of oxygen, is withdrawn in the bottom of the column low pressure 29, pressurized by a pump 39 at a pressure less than 9 abs bars, or even less than 5 bar abs and sent to the vaporizer 41. Apart from a purge of liquid 43, the oxygen vaporizes in the vaporizer 41 by exchange of heat with the fraction of air 11 at the pressure P2. This oxygen forms then the first rate of pressurized gaseous oxygen 45 that is warming in the line 21. The air fraction 11 is partially condensed and is sent to the double column.
The purge liquid 43 is pressurized to a pressure of at least 10 bar abs, or at least 15 bar abs, or even at least 20 bar abs in a pump 63 then vaporizes in the exchange line 21. The second flow gaseous product 59 is sent to a gaseous storage under pressure 3 and expanded to be mixed with flow 45 via line 61.
Here the vaporization of purge liquid is carried out using mainly sensible heat, so that no outgoing air flow of the exchanger 21 is completely condensed, or even condensed.
Alternatively, as shown in Figure 2, the purge fluid pressurized 43 may be vaporized in an auxiliary exchanger 21A, distinct from the exchange line, against an air flow 25A and with a flow of fluid refrigerant, for example a flow of nitrogen 57A warming the process of separation.
The flow 25A cooled in the exchanger 21A mixes with the flow cooled 25 and the flow of nitrogen 57A reheated in the exchanger 21A mixes with heated flow 57.
The second flow of gaseous oxygen 59, 61 formed by the vaporization can be used as backup gas during an interruption of the production of gaseous oxygen 45.

6 Ainsi le seul débit d'air qui sert à vaporiser l'oxygène de purge 43 reste sous forme gazeuse dans l'échangeur 21A et la vaporisation se réalise par échange de chaleur sensible.
La pressurisation par la pompe 39 et/ou 63 peut être remplacée par une pressurisation hydrostatique dans tous les cas décrits.
Pour toutes les figures, une quantité variable du deuxième débit d'oxygène gazeux est mélangée avec le premier débit afin de produire un débit mélangé substantiellement constant.
Cette quantité variable du liquide de purge vaporisé peut être mélangée au premier débit 45 pour lisser les variations de débits, dues, par exemple à
des variations de la pression du réseau d'oxygène.
En détectant une réduction de pression dans la ligne 45, due, par exemple à une demande accrue d'oxygène, de l'oxygène peut être détendu et envoyé du stockage 3 vers la ligne 45 par la conduite 61.
En cas de panne de l'appareil de séparation d'air, le débit d'oxygène 45 réduira ou sera inexistant. Dans ce cas, le débit d'oxygène 63 du stockage 3 peut alimenter un client, le temps qu'un vaporiseur de secours se mette en marche pour éviter tout arrêt de production.
Le débit 37 est le seul débit contenant plus que 60% mol. d'oxygène soutiré de la colonne basse pression.
Le stockage 3 opère à une pression plus élevée que le débit 45. 6 Thus the only air flow that serves to vaporize purge oxygen 43 remains in gaseous form in the exchanger 21A and the vaporization is carried out by sensible heat exchange.
The pressurization by the pump 39 and / or 63 can be replaced by a hydrostatic pressurization in all cases described.
For all the figures, a variable quantity of the second flow of gaseous oxygen is mixed with the first flow to produce a flow mixed substantially constant.
This variable amount of the vaporized purge liquid can be mixed at the first flow rate 45 to smooth the variations of flow rates, due, for example to variations in the pressure of the oxygen network.
By detecting a pressure reduction in line 45, due, by example to an increased demand for oxygen, oxygen can be relaxed and sent from storage 3 to line 45 via line 61.
In case of failure of the air separation device, the oxygen flow rate 45 will reduce or be non-existent. In this case, the oxygen flow 63 of the storage 3 can feed a customer, the time it takes for an emergency vaporizer to to avoid any production stoppage.
Flow 37 is the only flow containing more than 60 mol%. oxygen withdrawn from the low pressure column.
Storage 3 operates at a higher pressure than flow 45.

Claims (15)

1. Appareil de séparation d'air comprenant une double colonne comprenant une colonne moyenne pression (27) et une colonne basse pression (29), un échangeur principal (21), un vaporiseur (41), un compresseur principal (2), des moyens pour envoyer tout l'air à traiter dans la double colonne au compresseur principal pour produire de l'air substantiellement à la pression de la colonne moyenne pression, des moyens (5) pour envoyer une partie de l'air substantiellement à une pression élevée P2 à l'échangeur principal et ensuite au vaporiseur, une conduite pour envoyer de l'air au moins partiellement condensé dans le vaporiseur à au moins une des colonnes, une conduite pour envoyer de l'air à la pression P1 à la colonne moyenne pression, des moyens de pressurisation (39), une pompe (63), une conduite pour soutirer de l'oxygène liquide de la colonne basse pression et pour l'envoyer aux moyens de pressurisation, une conduite pour envoyer de l'oxygène liquide pressurisé à

une pression inférieure à 9 bar abs des moyens de pressurisation au vaporiseur, une conduite pour envoyer de l'oxygène gazeux du vaporiseur à
l'échangeur principal pour se réchauffer pour former un premier débit d'oxygène gazeux, une conduite de purge pour envoyer de l'oxygène liquide de purge (43) du vaporiseur à la pompe pour le pressuriser caractérisée en ce que la conduite de purge n'est pas reliée à un stockage de liquide de purge et en ce qu'elle comprend une conduite pour envoyer l'oxygène pressurisé de la pompe à un échangeur (21, 21A) pour se vaporiser, l'échangeur étant relié à une conduite d'air comprimé reliée au compresseur principal et à une conduite reliée à la double colonne, pour former un deuxième débit d'oxygène gazeux. 1. Air separation apparatus comprising a double column comprising a medium pressure column (27) and a low pressure column (29), a main heat exchanger (21), a vaporizer (41), a compressor main (2), means for sending all the air to be treated in the double column to main compressor to produce air substantially under pressure of the medium-pressure column, means (5) for sending a part of the air substantially at a high pressure P2 at the main exchanger and then to the vaporizer, a pipe to send air at least partially condensed in the vaporizer to at least one of the columns, a conduct to send air at the pressure P1 to the medium pressure column, pressurizing means (39), a pump (63), a pipe for drawing off liquid oxygen from the low pressure column and to send it to the means of pressurization, a conduit for sending pressurized liquid oxygen to a pressure lower than 9 bar abs pressurizing means to vaporizer, a pipe for sending gaseous oxygen from the vaporizer to the main exchanger to warm up to form a first flow oxygen gaseous, purge line for supplying purge liquid oxygen (43) from the vaporizer to the pump to pressurize it characterized in that the purge line is not connected to a purge liquid storage and in that that it includes a pipe to send the pressurized oxygen from the pump an exchanger (21, 21A) for vaporizing, the exchanger being connected to a compressed air line connected to the main compressor and a pipe connected to the double column, to form a second flow of gaseous oxygen. 2. Appareil suivant la revendication 1 dans lequel l'échangeur relié à la conduite d'oxygène de purge est l'échangeur principal (21). 2. Apparatus according to claim 1 wherein the exchanger connected to the Purge oxygen line is the main exchanger (21). 3. Appareil suivant la revendication 1 dans lequel l'échangeur relié à la conduite d'oxygène de purge est un échangeur (21A) distinct de l'échangeur principal. 3. Apparatus according to claim 1 wherein the exchanger connected to the Purge oxygen line is a heat exchanger (21A) separate from the heat exchanger main. 4. Appareil suivant la revendication 2 ou 3 dans lequel l'échangeur (21, 21A) comprend des passages reliés à une conduite d'amenée d'air d'alimentation et des passages reliés à une conduite d'amenée de fluide frigorigène, provenant éventuellement de la double colonne. 4. Apparatus according to claim 2 or 3 wherein the exchanger (21, 21A) comprises passages connected to an air supply duct supply and passages connected to a fluid supply line refrigerant, possibly from the double column. 5. Appareil suivant une des revendications 1 à 4 comprenant un stockage gazeux sous pression (3) relié à l'échangeur (21, 21A) de vaporisation d'oxygène de purge pour recueillir l'oxygène gazeux. 5. Apparatus according to one of claims 1 to 4 comprising a pressurized gas storage (3) connected to the exchanger (21, 21A) of vaporization Purge oxygen to collect gaseous oxygen. 6. Procédé de séparation d'air dans un appareil comprenant une double colonne comprenant une colonne moyenne pression (27) et une colonne basse pression (29), un échangeur principal (21), un vaporiseur (41), un compresseur principal (2), des moyens de pressurisation (43), une pompe (63), dans lequel on envoie tout l'air à traiter dans la double colonne au compresseur principal pour produire de l'air substantiellement à la pression P1 de la colonne moyenne pression, on envoie une partie de l'air substantiellement à une pression élevée P2 à l'échangeur principal et ensuite au vaporiseur, on envoie de l'air au moins partiellement condensé dans le vaporiseur à au moins une des colonnes, on envoie de l'air à la pression P1 à la colonne moyenne pression, on soutire de l'oxygène liquide de la colonne basse pression et on le pressurise, on envoie de l'oxygène liquide pressurisé à une pression inférieure à 5 bar abs au vaporiseur, on envoie un premier débit d'oxygène gazeux du vaporiseur à
l'échangeur principal pour se réchauffer et on pressurise de l'oxygène liquide de purge du vaporiseur dans la pompe caractérisé en ce que l'oxygène liquide de purge est pressurisé sans avoir été stocké et ensuite est vaporisé dans un échangeur par échange de chaleur avec de l'air, comprimé dans le compresseur principal et destiné à la double colonne, pour former un deuxième débit d'oxygène gazeux. 6. Method of separating air in an apparatus comprising a double column comprising a medium pressure column (27) and a low column pressure (29), a main heat exchanger (21), a vaporizer (41), a compressor (2), pressurizing means (43), a pump (63), wherein we send all the air to be treated in the double column to the main compressor to produce air substantially at the pressure P1 of the column average pressure, we send a part of the air substantially to a pressure high P2 to the main exchanger and then to the vaporizer, air is sent to less partially condensed in the vaporizer to at least one of the columns, sends air at the pressure P1 to the medium pressure column, it withdraws from the liquid oxygen of the low pressure column and pressurize it, we send of pressurized liquid oxygen at a pressure of less than 5 bar abs at vaporizer, a first flow of gaseous oxygen is sent from the vaporizer to the main exchanger to warm up and pressurized liquid oxygen of purge of the vaporizer in the pump characterized in that the liquid oxygen of purge is pressurized without being stored and then is vaporized in a exchanger by heat exchange with air, compressed in the main compressor and intended for the double column, to form a second flow rate of gaseous oxygen. 7. Procédé selon la revendication 6 dans lequel l'oxygène de purge est pressurisé à une pression d'au moins 10 bars abs, de préférence au moins 15 bars abs, voire au moins 20 bars abs dans la deuxième pompe (63). The method of claim 6 wherein the purge oxygen is pressurized to a pressure of at least 10 bar abs, preferably at least 15 bar abs, or even at least 20 bar abs in the second pump (63). 8. Procédé selon l'une des revendications 6 et 7 dans lequel l'oxygène de purge se vaporise dans l'échangeur principal (21). 8. Method according to one of claims 6 and 7 wherein the oxygen purge vaporizes in the main exchanger (21). 9. Procédé selon l'une des revendications 6 et 7 dans lequel l'oxygène de purge se vaporise dans un échangeur (21A) autre que l'échangeur principal. 9. Method according to one of claims 6 and 7 wherein the oxygen purge vaporizes in a heat exchanger (21A) other than the main exchanger. 10. Procédé selon l'une des revendications 6 à 9 dans lequel le deuxième débit d'oxygène gazeux est envoyé à un stockage gazeux sous pression (3) et sert de production de secours. 10. Method according to one of claims 6 to 9 wherein the second flow of gaseous oxygen is sent to a gaseous storage under pressure (3) and serves as backup production. 11. Procédé selon l'une des revendications 6 à 10 dans lequel une quantité variable du deuxième débit d'oxygène gazeux (61) est mélangée avec le premier débit (45) d'oxygène gazeux afin de produire un débit mélangé
substantiellement constant. 11. Method according to one of claims 6 to 10 wherein a variable amount of the second rate of oxygen gas (61) is mixed with the first flow (45) of gaseous oxygen to produce a mixed flow substantially constant. 12. Procédé selon l'une des revendications 6 à 11 dans lequel l'oxygène liquide (37) soutiré de la colonne basse pression contient au moins 80% mol.
d'oxygène. 12. Method according to one of claims 6 to 11 wherein the oxygen liquid (37) withdrawn from the low pressure column contains at least 80 mol%.
oxygen. 13. Procédé selon la revendication 12 dans lequel l'oxygène liquide (37) soutiré de la colonne basse pression constitue le seul débit contenant au moins 80% mol. d'oxygène soutiré de la colonne basse pression. The method of claim 12 wherein the liquid oxygen (37) withdrawn from the low-pressure column constitutes the only flow containing at less 80 mol% of oxygen withdrawn from the low pressure column. 14. Procédé selon l'une des revendications 6 à 13 dans lequel l'oxygène liquide (37) soutiré de la colonne basse pression contient au plus 98% mol.
d'oxygène. 14. Method according to one of claims 6 to 13 wherein the oxygen liquid (37) withdrawn from the low pressure column contains at most 98 mol%.
oxygen. 15. Procédé selon l'une des revendications 6 à 14 dans lequel aucun débit d'air ne se condense entièrement, voire ne se condense dans l'échangeur où se vaporise l'oxygène de purge. 15. Method according to one of claims 6 to 14 wherein no air flow does not condense completely or even condenses in the heat exchanger where the oxygen purge vaporizes.
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WO2012127148A3 (en) 2014-12-04
US20130340476A1 (en) 2013-12-26
ZA201306723B (en) 2015-03-25
FR2972794B1 (en) 2015-11-06
AU2012230171B2 (en) 2017-03-30
FR2972794A1 (en) 2012-09-21
WO2012127148A2 (en) 2012-09-27
ES2859549T3 (en) 2021-10-04
EP2686628B1 (en) 2021-01-13
CN104067079A (en) 2014-09-24

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