[go: up one dir, main page]

EP2118601B1 - Procede et appareil de production de gaz de l'air sous forme gazeuse et liquide a haute flexibilite par distillation cryogenique - Google Patents

Procede et appareil de production de gaz de l'air sous forme gazeuse et liquide a haute flexibilite par distillation cryogenique Download PDF

Info

Publication number
EP2118601B1
EP2118601B1 EP08775715.9A EP08775715A EP2118601B1 EP 2118601 B1 EP2118601 B1 EP 2118601B1 EP 08775715 A EP08775715 A EP 08775715A EP 2118601 B1 EP2118601 B1 EP 2118601B1
Authority
EP
European Patent Office
Prior art keywords
turbine
booster
air
pressure
temperature
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.)
Not-in-force
Application number
EP08775715.9A
Other languages
German (de)
English (en)
Other versions
EP2118601A2 (fr
Inventor
Alain Guillard
Patrick Lebot
Xavier Pontone
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.)
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Publication of EP2118601A2 publication Critical patent/EP2118601A2/fr
Application granted granted Critical
Publication of EP2118601B1 publication Critical patent/EP2118601B1/fr
Not-in-force legal-status Critical Current
Anticipated expiration legal-status Critical

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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04109—Arrangements of compressors and /or their drivers
    • F25J3/04139—Combination of different types of drivers mechanically coupled to the same compressor, possibly split on multiple compressor casings
    • 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
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main feed 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04163—Hot end purification of the feed air
    • F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
    • F25J3/04175—Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest 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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—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
    • F25J3/04296—Claude expansion, i.e. expanded into the main or 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
    • F25J3/04248—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
    • F25J3/04248—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.
    • F25J3/04381—Details relating to the work expansion, e.g. process parameter etc. using work extraction by mechanical coupling of compression and expansion so-called companders
    • 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
    • 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
    • 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
    • F25J2215/40—Air or oxygen enriched air, i.e. generally less than 30mol% of 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/04—Multiple expansion turbines in parallel

Definitions

  • the staggered vaporization stage processes for delivering products under pressure are particularly interesting since they allow the combination of these functions from a single air compressor, high pressure.
  • the energy efficiency of the whole is comparable to the traditional process and the investment is greatly diminished.
  • FR-A-2688052 allows the production of only a small amount of liquid product.
  • US Patent 6257020 describes a cooling and heating unit where an auxiliary turbine is connected to an air passage to be heated, this turbine having a suction temperature higher than the suction temperature of another turbine.
  • the object of this invention is to be able to combine the economic benefits of integrated processes, while retaining the flexibility and flexibility offered by traditional methods.
  • a flow cooling and reheating unit for and from an air separation column system according to claim 1.
  • the unit is incorporated in a known distillation system (thermally connected medium pressure and low pressure columns, optionally an intermediate pressure column and / or a mixing column and / or an argon mixture column, etc.) and sets in play at least two relaxation turbines.
  • a known distillation system thermally connected medium pressure and low pressure columns, optionally an intermediate pressure column and / or a mixing column and / or an argon mixture column, etc.
  • Two flow rates are at substantially equal pressure if their pressures differ only in the pressure drops.
  • the production of liquid product, all final products combined constitutes 1%, or 2% or 5% of the air flow rate sent to the columns (or to the column if only the medium pressure column is supplied with air).
  • a compressed air flow 1 from a main compressor is supercharged in a booster 3 at a high pressure at least 5 bar abs above the pressure of the medium pressure column, this high pressure being called the main pressure.
  • This main pressure may for example be between 10 and 25 bar abs.
  • the flow 5 is then purified with water and carbon dioxide (not shown).
  • the total flow of supercharged and purified air is sent to an exchange line 7 where it cools to a temperature T1. At this temperature, the flow 5 is divided in two to form a flow 9 which liquefies and is sent to the column system and a flow 11.
  • the flow 11 leaves the exchange line 7 at the temperature T1 different from at most ⁇ 5 ° C of the vaporization temperature of the pressurized oxygen 33 and is sent to a cold booster 13 to produce a flow 15 at a pressure substantially greater than the average pressure and possibly greater than the main pressure.
  • the flow rate 15 at a cold booster outlet temperature T2 cools in the exchange line 7 to a temperature T3 higher than T1.
  • T3 the temperature of the flow 15 is divided into two flow rates 17, 19.
  • the flow 17 is expanded in a turbine 21 from the temperature T3 close to the pseudo vaporization temperature of the pressurized oxygen 33.
  • the suction pressure of the turbine 21 is equal to the discharge pressure of the booster 13 thus very substantially greater than the average pressure (greater than 5 bars) and possibly greater than the main pressure and the discharge pressure is higher or equal to the average pressure, preferably substantially equal to the average pressure.
  • the flow rate expanded to a pressure greater than or equal to the average pressure, preferably substantially equal to the average pressure, is sent to the column system as the flow rate 25.
  • the flow 19 continues cooling in the exchange line and is sent in the form gaseous to the column system.
  • the cold booster 13 is driven by the turbine 21.
  • a residual nitrogen flow is heated in the exchange line.
  • a liquid column system other than liquid oxygen, is pressurized, vaporized in the exchange line 7 and then serves as a product under pressure.
  • a fraction of air 25 is taken from the purified air 5 at the main pressure and is cooled in the exchange line 7.
  • the fraction 25 is sent to a turbine 27 where it expands to a temperature T5 forming an air flow 29. This air flow is heated in the exchange line.
  • a liquid product is withdrawn from the column system as final product 32.
  • the only product of the apparatus is liquid oxygen but other products can obviously be produced in liquid form.
  • the air flow 25 treated in the auxiliary turbine 27 is reduced to zero if necessary, the main incoming air flow 1 is reduced by a flow rate at least equal to the reduction of the air flow sent. to the auxiliary turbine 27 and the production of liquid 37 is reduced to zero if necessary.
  • This variation of the air flow 1 between the two modes of operation is provided by the variable vanes of a compressor and / or by the start and / or stop of an auxiliary air compressor.
  • These two modes of operation may be the only modes of operation of the apparatus or there may be other modes of operation.
  • booster 3B There may be a compression step (booster 3B) between the hot booster which brings the air to the main pressure and the cold booster, so that the cold booster is from a pressure above the booster. pressure, as illustrated in the Figure 2 .
  • the turbine 21 is driven by the booster 13 and the booster 3 drives the auxiliary turbine 27.

Landscapes

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

Description

  • Les procédés traditionnels de production de gaz de l'air sous forme liquide ou gazeuse présentaient des architectures de procédés distinctes. Ainsi on trouvait :
    • un appareil de séparation de l'air produisant les constituants principaux (02, N2, Ar), à pression atmosphérique ou légèrement supérieure ;
    • une étape de compression des produits au moyen de compresseurs ;
    • un cycle indépendant de liquéfaction d'azote permettant de produire tout ou partie de chacun des constituants sous forme liquide si nécessaire.
  • Cette configuration permettait une grande souplesse d'utilisation car chacune des trois « fonctions » mises en oeuvre (séparation, compression, liquéfaction) pouvait être opérée ou stoppée de façon indépendante sans affecter le fonctionnement des deux autres.
  • Néanmoins, cette configuration souffre d'un manque de compétitivité important, compte tenu du coût très élevé de cette architecture, qui réclame un appareil par fonction.
  • Les procédés plus récents de production de gaz de l'air, que nous appelons procédés intégrés, présentent l'avantage de pouvoir combiner dans un seul équipement ces trois fonctions. Les appareils dits « à pompe », incluant des cycles de détente d'air ou éventuellement d'azote, permettent de produire à partir du même équipement les constituants de l'air sous forme gazeuse sous pression et liquide.
  • Parmi ceux-ci, les procédé à paliers de vaporisation décalés pour délivrer des produits sous pression, tels que décrits dans le brevet EP-A-0504029 ou encore FR-A-2688052 , sont particulièrement intéressants puisqu'ils permettent la combinaison de ces fonctions à partir d'un unique compresseur d'air, à haute pression. L'efficacité énergétique de l'ensemble est comparable au procédé traditionnel et l'investissement est grandement diminué.
  • Par contre la souplesse de production est affectée par la combinaison « 3 en 1 » des fonctions, et on pourra plus difficilement opérer ou arrêter une fonction sans affecter l'ensemble.
  • FR-A-2688052 permet la production de seulement une petite quantité de produit liquide.
  • US-A-6257020 décrit une unité de refroidissement et de réchauffage où une turbine auxiliaire est reliée à un passage d'air à réchauffer, cette turbine ayant une température d'aspiration supérieure à la température d'aspiration d'une autre turbine.
  • Le but de cette invention est de pouvoir combiner les avantages économiques des procédés intégrés, tout en conservant la souplesse et la flexibilité offerte par les procédés traditionnels.
  • Selon un aspect de l'invention, il est prévu une unité de refroidissement et de réchauffage de débits destinés à et provenant d'un système de colonnes de séparation d'air selon la revendication 1.
  • L'unité peut être disposée de sorte qu'en opération, une des conditions suivantes est remplie :
    • la température d'aspiration du surpresseur est inférieure à la température d'aspiration de la première turbine,
    • la température de refoulement du surpresseur est supérieure à la température d'aspiration de la première turbine,
    • la température de refoulement du surpresseur est supérieure à la température de refoulement de la turbine auxiliaire.
  • On se propose ici d'améliorer la flexibilité de production des procédés de type mono-machines tels que décrits précédemment :
    • en offrant la possibilité de produire de façon efficace des liquides avec des procédés tels que décrits dans FR-A-2688052 ;
    • et en offrant la possibilité de faire l'un ou l'autre de façon réversible, et énergétiquement efficace dans les deux cas.
  • L'unité est à incorporée dans un système de distillation connu (colonnes moyenne pression et basse pression thermiquement reliées, éventuellement une colonne à pression intermédiaire et/ou une colonne de mélange et/ou une colonne de mixture argon, etc..) et met en jeu au moins deux turbines de détente.
  • Deux débits sont à pression substantiellement égale si leurs pressions ne différent que par les pertes de charge.
  • En premier mode de fonctionnement, la production de produit liquide, tous produits finaux confondus, constitue 1%, ou 2% ou 5% du débit d'air envoyé aux colonnes (ou à la colonne si seule la colonne moyenne pression est alimentée en air).
  • L'invention sera décrite en plus de détail en se référant aux figures, qui montrent des unités de refroidissement et de réchauffage selon l'invention à incorporer dans des installations de séparation d'air.
  • Dans la Figure 1, un débit d'air comprimé 1 provenant d'un compresseur principal est surpressé dans un surpresseur 3 à une haute pression au moins 5 bar abs au-dessus de la pression de la colonne moyenne pression, cette haute pression étant appelée pression principale. Cette pression principale peut par exemple être entre 10 et 25 bars abs. A cette pression principale le débit 5 est ensuite épuré en eau et dioxyde de carbone (non-illustré). Le débit total d'air surpressé et épuré 5 est envoyé à une ligne d'échange 7 où il se refroidit jusqu'à une température T1. A cette température, le débit 5 est divisé en deux pour former un débit 9 qui se liquéfie et est envoyé au système de colonnes et un débit 11. Le débit 11 quitte la ligne d'échange 7 à la température T1 différent d'au plus ±5°C de la température de vaporisation de l'oxygène pressurisé 33 et est envoyé à un surpresseur froid 13 pour produire un débit 15 à une pression très sensiblement supérieure à la moyenne pression et éventuellement supérieure à la pression principale. Le débit 15 à une température T2 de sortie de surpresseur froid se refroidit dans la ligne d'échange 7 jusqu'à une température T3 plus élevée que T1. A cette température T3, le débit 15 est divisé en deux débits 17, 19. Le débit 17 est détendu dans une turbine 21 à partir de la température T3 proche de la température de pseudo vaporisation de l'oxygène pressurisé 33.
  • La pression d'aspiration de la turbine 21 est égale à la pression de refoulement du surpresseur 13 donc très sensiblement supérieure à la moyenne pression (supérieure d'au moins 5 bars) et éventuellement supérieure à la pression principale et la pression de refoulement est supérieure ou égale à la moyenne pression, préférablement sensiblement égale à la moyenne pression. Le débit détendu jusqu'à une pression supérieure ou égale à la moyenne pression, préférablement sensiblement égale à la moyenne pression est envoyé au système de colonne comme débit 25. Le débit 19 poursuit son refroidissement dans la ligne d'échange et est envoyé sous forme gazeuse au système de colonnes.
  • Le surpresseur froid 13 est entraîné par la turbine 21.
  • Un débit d'azote résiduaire se réchauffe dans la ligne d'échange.
  • Un débit d'oxygène liquide 35 pressurisé dans une pompe 33 se vaporise dans la ligne d'échange 7.
  • Optionnellement un liquide du système de colonnes, autre que l'oxygène liquide, est pressurisé, vaporisé dans la ligne d'échange 7 et sert ensuite de produit sous pression.
  • Selon un premier mode de fonctionnement, une fraction d'air 25 est prélevé dans l'air épuré 5 à la pression principale et est refroidi dans la ligne d'échange 7. A une température T4 inférieure à -100°C et supérieure à T2, la fraction 25 est envoyée à une turbine 27 où elle se détend jusqu'à une température T5 formant un débit d'air 29. Ce débit d'air se réchauffe dans la ligne d'échange.
  • Un produit liquide est soutiré du système de colonnes comme produit final 32. Dans l'exemple le seul produit de l'appareil est de l'oxygène liquide mais d'autres produits peuvent évidemment être produits sous forme liquide.
  • Selon un deuxième mode de fonctionnement le débit d'air 25 traité dans la turbine auxiliaire 27 est réduit éventuellement à zéro, le débit d'air principal entrant 1 est réduit d'un débit au moins égal à la réduction du débit d'air envoyée à la turbine auxiliaire 27 et la production de liquide 37 est diminuée éventuellement à zéro.
  • Cette variation du débit d'air 1 entre les deux modes de fonctionnement est assurée par les aubages variables d'un compresseur et/ou par la mise en route et/ou l'arrêt d'un compresseur d'air auxiliaire.
  • Ces deux modes de fonctionnement peuvent constituer les seuls modes de fonctionnement de l'appareil ou bien il peut y avoir d'autres modes de fonctionnement.
  • Il peut y avoir une étape de compression (surpresseur 3B) entre la surpression chaude qui amène l'air à la pression principale et la surpression froide, de sorte que la surpression froide s'effectue à partir d'une pression au-dessus de la pression principale, tel qu'illustré dans la Figure 2.
  • De préférence, la turbine 21 est entraînée par le surpresseur 13 et le surpresseur 3 entraîne la turbine auxiliaire 27.

Claims (4)

  1. Unité de refroidissement et de réchauffage de débits destinés à et provenant d'un système de colonnes de séparation d'air comprenant une ligne d'échange (7), une première turbine (21), une turbine auxiliaire (27), un surpresseur (13), la ligne d'échange comprenant :
    i) au moins un passage pour recevoir un premier débit d'air épuré, l'au moins un passage pour recevoir un premier débit d'air épuré étant relié à l'aspiration du surpresseur,
    ii) au moins un passage relié au refoulement du surpresseur, l'au moins un passage relié au refoulement du surpresseur étant relié à l'aspiration de la première turbine,
    iii) au moins deux passages pour recevoir au moins deux fluides (35,37) qui se réchauffent,
    iv) au moins un passage pour recevoir un deuxième débit d'air épuré, l'au moins un passage pour recevoir le deuxième débit d'air épuré étant relié à l'aspiration de la turbine auxiliaire et le refoulement de la turbine auxiliaire étant relié à au moins un passage d'air à réchauffer et
    caractérisée en ce que ces passages sont reliés de sorte qu'en opération, la température d'aspiration de la turbine auxiliaire est supérieure à la température d'aspiration de la première turbine et la température d'aspiration de la turbine auxiliaire est supérieure à la température d'aspiration du surpresseur.
  2. Unité selon la revendication 1 disposée de sorte qu'en opération la température d'aspiration du surpresseur (13) est inférieure à la température d'aspiration de la première turbine (21).
  3. Unité selon la revendication 1 ou 2 disposée de sorte qu'en opération la température de refoulement du surpresseur (13) est supérieure à la température d'aspiration de la première turbine (21).
  4. Unité selon la revendication 1, 2 ou 3 disposée de sorte qu'en opération la température de refoulement du surpresseur (13) est supérieure à la température de refoulement de la turbine auxiliaire (27).
EP08775715.9A 2007-03-13 2008-03-12 Procede et appareil de production de gaz de l'air sous forme gazeuse et liquide a haute flexibilite par distillation cryogenique Not-in-force EP2118601B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR0753788A FR2913759B1 (fr) 2007-03-13 2007-03-13 Procede et appareil de production de gaz de l'air sous forme gazeuse et liquide a haute flexibilite par distillation cryogenique.
PCT/FR2008/050418 WO2008129198A2 (fr) 2007-03-13 2008-03-12 Procede et appareil de production de gaz de l'air sous forme gazeuse et liquide a haute flexibilite par distillation cryogenique

Publications (2)

Publication Number Publication Date
EP2118601A2 EP2118601A2 (fr) 2009-11-18
EP2118601B1 true EP2118601B1 (fr) 2017-12-20

Family

ID=38870300

Family Applications (1)

Application Number Title Priority Date Filing Date
EP08775715.9A Not-in-force EP2118601B1 (fr) 2007-03-13 2008-03-12 Procede et appareil de production de gaz de l'air sous forme gazeuse et liquide a haute flexibilite par distillation cryogenique

Country Status (8)

Country Link
US (1) US20110011130A1 (fr)
EP (1) EP2118601B1 (fr)
JP (1) JP5032596B2 (fr)
CN (1) CN101883963B (fr)
BR (1) BRPI0808718B1 (fr)
FR (1) FR2913759B1 (fr)
RU (1) RU2479806C2 (fr)
WO (1) WO2008129198A2 (fr)

Families Citing this family (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2010536004A (ja) * 2007-08-10 2010-11-25 レール・リキード−ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード 極低温蒸留によって空気を分離する方法及び装置
JP4908634B2 (ja) * 2007-08-10 2012-04-04 レール・リキード−ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード 極低温蒸留によって空気を分離する方法及び装置
FR2948184B1 (fr) * 2009-07-20 2016-04-15 Air Liquide Procede et appareil de separation d'air par distillation cryogenique
DE102010052544A1 (de) * 2010-11-25 2012-05-31 Linde Ag Verfahren zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft
DE102010052545A1 (de) * 2010-11-25 2012-05-31 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft
FR2973486B1 (fr) * 2011-03-31 2013-05-03 Air Liquide Procede de separation d'air par distillation cryogenique
TWI643814B (zh) * 2011-06-03 2018-12-11 半導體能源研究所股份有限公司 單層和多層石墨烯，彼之製法，含彼之物件，以及含彼之電器裝置
US9249524B2 (en) * 2011-08-31 2016-02-02 Semiconductor Energy Laboratory Co., Ltd. Manufacturing method of composite oxide and manufacturing method of power storage device
FR2985305B1 (fr) * 2012-01-03 2017-12-22 L'air Liquide Sa Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede et appareil de production de gaz de l'air sous pression utilisant un surpresseur cryogenique
WO2014154339A2 (fr) 2013-03-26 2014-10-02 Linde Aktiengesellschaft Procédé de séparation d'air et installation de séparation d'air
EP3179186A1 (fr) * 2015-12-07 2017-06-14 Linde Aktiengesellschaft Procede de production d'un produit comprime riche en oxygene, gazeux et liquide dans une installation de decomposition de l'air et installation de decomposition de l'air
US10359231B2 (en) 2017-04-12 2019-07-23 Praxair Technology, Inc. Method for controlling production of high pressure gaseous oxygen in an air separation unit
FR3069913B1 (fr) * 2017-08-03 2020-06-26 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Appareil et procede de separation d'air par distillation cryogenique
EP3438585A3 (fr) 2017-08-03 2019-04-17 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé de dégivrage d'un appareil de séparation d'air par distillation cryogénique et appareil adapté pour être dégivré par ce procédé
FR3072451B1 (fr) * 2017-10-13 2022-01-21 Air Liquide Procede et appareil de separation d'air par distillation cryogenique

Family Cites Families (23)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SU645007A1 (ru) * 1972-03-03 1979-01-30 Предприятие П/Я А-3605 Способ совместного получени газообразных и жидких компонентов воздуха
IT1019710B (it) * 1974-07-12 1977-11-30 Nuovo Pignone Spa Processo ed apparato per la produ zione di elevate percentuali di os sigeno e/o azoto allo stato liquido
DE3012062A1 (de) * 1980-03-28 1981-10-08 Linde Ag, 6200 Wiesbaden Verfahren und vorrichtung zur erzeugung von gasfoermigen sauerstoff
DE3738559A1 (de) * 1987-11-13 1989-05-24 Linde Ag Verfahren zur luftzerlegung durch tieftemperaturrektifikation
JP2736543B2 (ja) * 1989-04-17 1998-04-02 日本酸素株式会社 空気液化分離方法
FR2652409A1 (fr) * 1989-09-25 1991-03-29 Air Liquide Procede de production frigorifique, cycle frigorifique correspondant et leur application a la distillation d'air.
JP2909678B2 (ja) 1991-03-11 1999-06-23 レール・リキード・ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード 圧力下のガス状酸素の製造方法及び製造装置
FR2688052B1 (fr) * 1992-03-02 1994-05-20 Maurice Grenier Procede et installation de production d'oxygene et/ou d'azote gazeux sous pression par distillation d'air.
FR2692664A1 (fr) * 1992-06-23 1993-12-24 Lair Liquide Procédé et installation de production d'oxygène gazeux sous pression.
US5355681A (en) * 1993-09-23 1994-10-18 Air Products And Chemicals, Inc. Air separation schemes for oxygen and nitrogen coproduction as gas and/or liquid products
US5475980A (en) * 1993-12-30 1995-12-19 L'air Liquide, Societe Anonyme Pour L'etude L'exploitation Des Procedes Georges Claude Process and installation for production of high pressure gaseous fluid
GB9515907D0 (en) * 1995-08-03 1995-10-04 Boc Group Plc Air separation
JP2875206B2 (ja) * 1996-05-29 1999-03-31 日本エア・リキード株式会社 高純度窒素製造装置及び方法
US5678425A (en) * 1996-06-07 1997-10-21 Air Products And Chemicals, Inc. Method and apparatus for producing liquid products from air in various proportions
FR2787560B1 (fr) * 1998-12-22 2001-02-09 Air Liquide Procede de separation cryogenique des gaz de l'air
US6808364B2 (en) * 2002-12-17 2004-10-26 General Electric Company Methods and apparatus for sealing gas turbine engine variable vane assemblies
FR2851330B1 (fr) * 2003-02-13 2006-01-06 Air Liquide Procede et installation de production sous forme gazeuse et sous haute pression d'au moins un fluide choisi parmi l'oxygene, l'argon et l'azote par distillation cryogenique de l'air
FR2854682B1 (fr) * 2003-05-05 2005-06-17 Air Liquide Procede et installation de separation d'air par distillation cryogenique
FR2854683B1 (fr) * 2003-05-05 2006-09-29 Air Liquide Procede et installation de production de gaz de l'air sous pression par distillation cryogenique d'air
US6962062B2 (en) * 2003-12-10 2005-11-08 L'Air Liquide, Société Anonyme à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Proédés Georges Claude Process and apparatus for the separation of air by cryogenic distillation
FR2865024B3 (fr) * 2004-01-12 2006-05-05 Air Liquide Procede et installation de separation d'air par distillation cryogenique
US7272954B2 (en) * 2004-07-14 2007-09-25 L'air Liquide, Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Proceded Georges Claude Low temperature air separation process for producing pressurized gaseous product
US20060272353A1 (en) * 2005-05-20 2006-12-07 Gabbita Venkata Maruthi Prasad Process and apparatus for the separation of air by cryogenic distillation

Also Published As

Publication number Publication date
US20110011130A1 (en) 2011-01-20
WO2008129198A2 (fr) 2008-10-30
FR2913759A1 (fr) 2008-09-19
JP2010531424A (ja) 2010-09-24
BRPI0808718A2 (pt) 2014-08-12
RU2479806C2 (ru) 2013-04-20
CN101883963A (zh) 2010-11-10
RU2009137758A (ru) 2011-04-20
JP5032596B2 (ja) 2012-09-26
BRPI0808718B1 (pt) 2019-09-24
FR2913759B1 (fr) 2013-08-16
WO2008129198A3 (fr) 2011-07-07
CN101883963B (zh) 2013-09-18
EP2118601A2 (fr) 2009-11-18

Similar Documents

Publication Publication Date Title
EP2118601B1 (fr) Procede et appareil de production de gaz de l'air sous forme gazeuse et liquide a haute flexibilite par distillation cryogenique
CA2828179C (fr) Procede et appareil de liquefaction de co2
FR2913760A1 (fr) Procede et appareil de production de gaz de l'air sous forme gazeuse et liquide a haute flexibilite par distillation cryogenique
EP1014020B1 (fr) Procédé de séparation cryogénique des gaz de l'air
JP4908634B2 (ja) 極低温蒸留によって空気を分離する方法及び装置
EP2510294A1 (fr) Procede et appareil de separation d'air par distillation cryogenique
EP2691718B1 (fr) Procede de production d'un gaz de l'air sous pression par distillation cryogenique
EP2788699B1 (fr) Procédé et appareil de liquéfaction d'un gaz riche en co2
WO2011030050A2 (fr) Procede et installation de production d'oxygene par distillation d'air
FR2831249A1 (fr) Procede et installation de separation d'air par distillation cryogenique
EP2895811B1 (fr) Procédé et appareil de séparation d'air par distillation cryogénique.
FR2972793A1 (fr) Procede et appareil de liquefaction d'un gaz riche en co2 contenant au moins une impurete legere
WO2010109149A2 (fr) Appareil et procédé de séparation d'air par distillation cryogénique
WO2009112744A2 (fr) Appareil de separation d'air par distillation cryogenique
FR2943408A1 (fr) Procede et installation de separation d'air par distillation cryogenique
EP2795215B1 (fr) Procede et appareil de separation d'air par distillation cryogenique
FR2863348A1 (fr) Compresseur de gaz, appareil de separation d'un melange gazeux incorporant un tel compresseur et procede de separation d'un melange gazeux incorporant un tel compresseur
FR2985305A1 (fr) Procede et appareil de production de gaz de l'air sous pression utilisant un surpresseur cryogenique

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Kind code of ref document: A2

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MT NL NO PL PT RO SE SI SK TR

RIN1 Information on inventor provided before grant (corrected)

Inventor name: GUILLARD, ALAIN

Inventor name: LEBOT, PATRICK

Inventor name: PONTONE, XAVIER

17P Request for examination filed

Effective date: 20120109

RBV Designated contracting states (corrected)

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MT NL NO PL PT RO SE SI SK TR

DAX Request for extension of the european patent (deleted)
GRAP Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOSNIGR1

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: GRANT OF PATENT IS INTENDED

INTG Intention to grant announced

Effective date: 20171004

GRAS Grant fee paid

Free format text: ORIGINAL CODE: EPIDOSNIGR3

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE PATENT HAS BEEN GRANTED

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MT NL NO PL PT RO SE SI SK TR

REG Reference to a national code

Ref country code: GB

Ref legal event code: FG4D

Free format text: NOT ENGLISH

REG Reference to a national code

Ref country code: CH

Ref legal event code: EP

REG Reference to a national code

Ref country code: IE

Ref legal event code: FG4D

Free format text: LANGUAGE OF EP DOCUMENT: FRENCH

REG Reference to a national code

Ref country code: AT

Ref legal event code: REF

Ref document number: 956744

Country of ref document: AT

Kind code of ref document: T

Effective date: 20180115

REG Reference to a national code

Ref country code: DE

Ref legal event code: R096

Ref document number: 602008053428

Country of ref document: DE

REG Reference to a national code

Ref country code: FR

Ref legal event code: PLFP

Year of fee payment: 11

REG Reference to a national code

Ref country code: NL

Ref legal event code: MP

Effective date: 20171220

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SE

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20171220

Ref country code: FI

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20171220

Ref country code: LT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20171220

Ref country code: NO

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180320

REG Reference to a national code

Ref country code: LT

Ref legal event code: MG4D

REG Reference to a national code

Ref country code: AT

Ref legal event code: MK05

Ref document number: 956744

Country of ref document: AT

Kind code of ref document: T

Effective date: 20171220

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180321

Ref country code: HR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20171220

Ref country code: LV

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20171220

Ref country code: BG

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180320

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: NL

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20171220

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20171220

Ref country code: CZ

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20171220

Ref country code: CY

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20171220

Ref country code: EE

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20171220

Ref country code: ES

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20171220

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: IS

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180420

Ref country code: IT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20171220

Ref country code: AT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20171220

Ref country code: RO

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20171220

Ref country code: PL

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20171220

REG Reference to a national code

Ref country code: DE

Ref legal event code: R097

Ref document number: 602008053428

Country of ref document: DE

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: MT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20171220

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

26N No opposition filed

Effective date: 20180921

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: MC

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20171220

Ref country code: DK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20171220

REG Reference to a national code

Ref country code: BE

Ref legal event code: MM

Effective date: 20180331

REG Reference to a national code

Ref country code: IE

Ref legal event code: MM4A

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LU

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20180312

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: IE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20180312

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: BE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20180331

Ref country code: CH

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20180331

Ref country code: SI

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20171220

Ref country code: LI

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20180331

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 20190321

Year of fee payment: 12

Ref country code: GB

Payment date: 20190320

Year of fee payment: 12

Ref country code: FR

Payment date: 20190322

Year of fee payment: 12

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: TR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20171220

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: HU

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT; INVALID AB INITIO

Effective date: 20080312

Ref country code: PT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20171220

REG Reference to a national code

Ref country code: DE

Ref legal event code: R119

Ref document number: 602008053428

Country of ref document: DE

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20201001

Ref country code: FR

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20200331

GBPC Gb: european patent ceased through non-payment of renewal fee

Effective date: 20200312

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GB

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20200312