EP0766055B1 - Process and apparatus for the production of pressurized gas by cryogenic distillation - Google Patents

Process and apparatus for the production of pressurized gas by cryogenic distillation Download PDF

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Publication number
EP0766055B1
EP0766055B1 EP96402014A EP96402014A EP0766055B1 EP 0766055 B1 EP0766055 B1 EP 0766055B1 EP 96402014 A EP96402014 A EP 96402014A EP 96402014 A EP96402014 A EP 96402014A EP 0766055 B1 EP0766055 B1 EP 0766055B1
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European Patent Office
Prior art keywords
liquid
make
exchanger
withdrawn
gas
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EP96402014A
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German (de)
French (fr)
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EP0766055A1 (en
Inventor
Mike De L'isle
Yves Koeberlé
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Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—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
    • F25J3/04006—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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • 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
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • F25J3/0426—The cryogenic component does not participate in the fractionation
    • 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.
    • F25J3/04393—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
    • 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
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04951—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network
    • F25J3/04957—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network and inter-connecting equipments upstream of the fractionation unit (s), i.e. at the "front-end"
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/50—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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
    • F25J2240/46—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval the 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/939—Partial feed stream expansion, air
    • Y10S62/94—High pressure column

Definitions

  • the present invention relates to a method and an installation for production of pressurized gas by cryogenic distillation according to the preamble of claim 1, respectively the preamble of claim 9.
  • Such a method and such an installation are known from document EP-A-0 628 778.
  • the pressures discussed are absolute pressures.
  • condensation means "Vaporization” is either condensation or actual vaporization, either a pseudo-condensation or a pseudo-vaporization, depending on whether the pressures are subcritical or supercritical.
  • the object of the invention is to provide the maximum demand in pressurized gas with a device sized to produce only part of the liquid required to supply the maximum gas demand.
  • EP-A-628778 describes the case in which a flow of liquid oxygen of a column and a flow of liquid oxygen from an external source are mixed to form a single flow, pressurized and vaporized in the main exchanger an air separation device.
  • Liquefied make-up gas can have the same composition as the flow rate of liquid withdrawn.
  • the liquid can be an air gas.
  • liquid nitrogen can be withdrawn from the head of a simple column or a low column or medium pressure of a double column.
  • Liquid argon can be obtained at the head of an argon column.
  • the invention also applies to the separation of other cryogenic fluids; the liquid to be sprayed could be methane, carbon monoxide or hydrogen for example.
  • the liquid Before its vaporization, the liquid can be pressurized either by pressure hydrostatic, either with a pump.
  • make-up gas If the make-up gas is already at the vaporization pressure of the withdrawn liquid, after liquefaction, it can be added to the withdrawn liquid downstream of the pressurization means. Otherwise, the liquefied make-up gas mixes liquid upstream of the pump to be pressurized.
  • the liquefied make-up gas constitutes 20% of the flow of vaporized liquid, allowing the device to be sized at a capacity which represents 80% of the maximum demand.
  • a production installation is also provided. of a gas under pressure by cryogenic distillation according to the claim 9.
  • Figure 1 schematically represents an installation according to the invention.
  • An air flow 1 is compressed in a compressor to 5.6 x 10 5 kPa, before being divided into three fractions.
  • the first fraction 1A is compressed by the compressor 3 to 62 x 10 5 kPa, refrigerated in 4 and compressed to 76 x 10 5 kPa.
  • the fraction 1A is cooled in a main exchanger 9.
  • Part of the partially cooled air 11A is drawn off at an intermediate temperature level of the exchanger 9 and then expanded in a turbine 7, which drives the compressor 5, until the pressure of a medium pressure column 13 of a double column 12.
  • the expanded air is then sent to this column 13.
  • the remaining part of the flow 1A continues to cool in the exchanger 9 , condenses and is relaxed in the valve 11 at the pressure of the column 13, before being sent there.
  • the fraction 1B crosses the exchanger 9 before being introduced in column tank 13.
  • the fraction 1C is compressed by the compressor 15 to 8.9 x 10 5 kPa, partially cooled in the exchanger 9 and expanded by the blowing turbine 17 to the pressure of a low pressure column 14.
  • the expanded fraction 1C is sent to column 14, possibly after a sub-cooling step.
  • the insufflation turbine 17 drives the compressor 15.
  • the double column 12 comprising the low pressure column 14 and the medium pressure column 13 is dimensioned to produce an average flow of liquid which vaporizes in the exchanger 9 to form a gas under pressure.
  • the liquid is oxygen withdrawn from the bottom of column 14 through line 31 at a pressure of approximately 1.5 ⁇ 10 5 kPa.
  • the liquid is pressurized to 76 x 10 5 kPa by a pump 25 before being vaporized in the exchanger 9 to form the oxygen under pressure.
  • An additional gaseous oxygen comes from a 19 to 30 x 10 5 kPa network.
  • the make-up gas in line 20 cools in exchanger 9, expands through valve 21 and is separated into two phases in separator 23.
  • the gaseous part of the oxygen is sent at least in part to the low pressure column 14.
  • the liquid part is sent to line 31 when the oxygen demand passes above the maximum capacity of the double column 12, which represents 80% of the maximum demand.
  • the liquid coming from the network is vaporized to supply up to 20% of the maximum demand. This percentage is limited by the liquefaction capacity of the network oxygen acceptable by the exchanger 9.

Description

La présente invention concerne un procédé et une installation de production de gaz sous pression par distillation cryogénique selon le préambule de la revendication 1, respectivement le préambule de la revendication 9. Un tel procédé et une telle installation sont connus par le document EP-A-0 628 778.The present invention relates to a method and an installation for production of pressurized gas by cryogenic distillation according to the preamble of claim 1, respectively the preamble of claim 9. Such a method and such an installation are known from document EP-A-0 628 778.

Des procédés de ce genre sont bien connus dans le domaine et existent depuis plusieurs décennies.Processes of this kind are well known in the art and have existed for several decades.

Dans le présent mémoire, les pressions dont il est question sont des pressions absolues. De plus, on entend par « condensation » et « vaporisation » soit une condensation ou une vaporisation proprement dite, soit une pseudo-condensation ou une pseudo-vaporisation, selon que les pressions sont subcritiques ou supercritiques.In this submission, the pressures discussed are absolute pressures. In addition, the term “condensation” means "Vaporization" is either condensation or actual vaporization, either a pseudo-condensation or a pseudo-vaporization, depending on whether the pressures are subcritical or supercritical.

Le but de l'invention est de permettre de fournir la demande maximale en gaz sous pression avec un appareil dimensionné pour produire seulement une partie du liquide requis pour fournir la demande maximale en gaz.The object of the invention is to provide the maximum demand in pressurized gas with a device sized to produce only part of the liquid required to supply the maximum gas demand.

EP-A-628778 décrit le cas dans lequel un débit d'oxygène liquide d'une colonne et un débit d'oxygène liquide d'une source extérieure sont mélangés pour former un seul débit, pressurisés et vaporisés dans l'échangeur principal d'un appareil de séparation d'air.EP-A-628778 describes the case in which a flow of liquid oxygen of a column and a flow of liquid oxygen from an external source are mixed to form a single flow, pressurized and vaporized in the main exchanger an air separation device.

Selon l'invention, il est prévu un procédé de production d'un gaz sous pression dans un appareil de séparation cryogénique comprenant les étapes de :

  • i) refroidir un fluide à séparer dans un échangeur de chaleur et l'envoyer à une colonne de distillation de l'appareil ;
  • ii) soutirer un débit liquide d'une colonne de l'appareil et le réchauffer dans l'échangeur ;
  • iii) on rajoute au moins un liquide d'appoint au débit liquide soutiré de l'étape ii) ;
  • iv) on vaporise dans l'échangeur le mélange ainsi formé par le liquide d'appoint et le débit soutiré par échange thermique indirect ; et
  • v) on récupère en sortie d'appareil le gaz sous pression,
    caractérisé en ce que l'on envoie un gaz d'appoint provenant d'une source extérieure à l'échangeur, on y refroidit le gaz d'appoint et on le condense au moins partiellement pour former le liquide d'appoint par échange de chaleur avec le mélange qui se vaporise.
    • According to the invention, there is provided a method for producing a gas under pressure in a cryogenic separation apparatus comprising the steps of:
  • i) cooling a fluid to be separated in a heat exchanger and sending it to a distillation column of the apparatus;
  • ii) withdrawing a liquid flow from a column of the apparatus and heating it in the exchanger;
  • iii) at least one makeup liquid is added to the liquid flow rate withdrawn from step ii);
  • iv) the mixture thus formed is vaporized in the exchanger by the make-up liquid and the flow withdrawn by indirect heat exchange; and
  • v) the pressurized gas is recovered on leaving the appliance
    characterized in that a make-up gas is sent from an external source to the exchanger, the make-up gas is cooled there and at least partially condensed to form the make-up liquid by heat exchange with the vaporizing mixture.

    • De cette manière, un gaz provenant d'une source extérieure sert d'appoint pour suppléer au manque de liquide lorsque l'appareil fonctionne à sa capacité maximale.In this way, a gas from an external source serves to make up for the lack of liquid when the appliance is running at its maximum capacity.

    Le gaz d'appoint liquéfié peut avoir la même composition que le débit de liquide soutiré.Liquefied make-up gas can have the same composition as the flow rate of liquid withdrawn.

    Le liquide peut être un gaz de l'air. Par exemple, de l'azote liquide peut être soutiré de la tête d'une simple colonne ou d'une colonne basse ou moyenne pression d'une double colonne. De l'argon liquide peut être obtenu en tête d'une colonne argon. Néanmoins, l'invention s'applique également à la séparation d'autres fluides cryogéniques ; le liquide à vaporiser pourrait être du méthane, du monoxyde de carbone ou de l'hydrogène par exemple.The liquid can be an air gas. For example, liquid nitrogen can be withdrawn from the head of a simple column or a low column or medium pressure of a double column. Liquid argon can be obtained at the head of an argon column. However, the invention also applies to the separation of other cryogenic fluids; the liquid to be sprayed could be methane, carbon monoxide or hydrogen for example.

    Avant sa vaporisation, le liquide peut être pressurisé soit par pression hydrostatique, soit avec une pompe.Before its vaporization, the liquid can be pressurized either by pressure hydrostatic, either with a pump.

    Si le gaz d'appoint se trouve déjà à la pression de vaporisation du liquide soutiré, après sa liquéfaction, il peut être rajouté au liquide soutiré en aval des moyens de pressurisation. Sinon, le gaz d'appoint liquéfié se mélange au liquide en amont de la pompe afin d'y être pressurisé.If the make-up gas is already at the vaporization pressure of the withdrawn liquid, after liquefaction, it can be added to the withdrawn liquid downstream of the pressurization means. Otherwise, the liquefied make-up gas mixes liquid upstream of the pump to be pressurized.

    De préférence, le gaz d'appoint liquéfié constitue 20 % du débit de liquide vaporisé, permettant ainsi à l'appareil d'être dimensionné à une capacité qui représente 80 % de la demande maximale.Preferably, the liquefied make-up gas constitutes 20% of the flow of vaporized liquid, allowing the device to be sized at a capacity which represents 80% of the maximum demand.

    Selon l'invention, il est également prévu une installation de production d'un gaz sous pression par distillation cryogénique selon la revendication 9.According to the invention, a production installation is also provided. of a gas under pressure by cryogenic distillation according to the claim 9.

    Un exemple de mise en oeuvre de l'invention est illustré à la figure 1 qui représente schématiquement une installation selon l'invention.An example of implementation of the invention is illustrated in Figure 1 which schematically represents an installation according to the invention.

    Un débit d'air 1 est comprimé dans un compresseur jusqu'à 5,6 x 105 kPa, avant d'être divisé en trois fractions. La première fraction 1A est comprimée par le compresseur 3 jusqu'à 62 x 105 kPa, réfrigérée en 4 et comprimée à 76 x 105 kPa. Après une deuxième étape de réfrigération en 6, la fraction 1A est refroidie dans un échangeur principal 9. Une partie de l'air 11A partiellement refroidie est soutirée à un niveau de température intermédiaire de l'échangeur 9 puis détendue dans une turbine 7, qui entraíne le compresseur 5, jusqu'à la pression d'une colonne moyenne pression 13 d'une double colonne 12. L'air détendu est ensuite envoyé dans cette colonne 13. La partie restante du débit 1A poursuit son refroidissement dans l'échangeur 9, se condense et est détendue dans la vanne 11 à la pression de la colonne 13, avant d'y être envoyée.An air flow 1 is compressed in a compressor to 5.6 x 10 5 kPa, before being divided into three fractions. The first fraction 1A is compressed by the compressor 3 to 62 x 10 5 kPa, refrigerated in 4 and compressed to 76 x 10 5 kPa. After a second refrigeration step in 6, the fraction 1A is cooled in a main exchanger 9. Part of the partially cooled air 11A is drawn off at an intermediate temperature level of the exchanger 9 and then expanded in a turbine 7, which drives the compressor 5, until the pressure of a medium pressure column 13 of a double column 12. The expanded air is then sent to this column 13. The remaining part of the flow 1A continues to cool in the exchanger 9 , condenses and is relaxed in the valve 11 at the pressure of the column 13, before being sent there.

    La fraction 1B traverse l'échangeur 9 avant d'être introduite en cuve de la colonne 13.The fraction 1B crosses the exchanger 9 before being introduced in column tank 13.

    La fraction 1C est comprimée par le compresseur 15 à 8,9 x 105 kPa, partiellement refroidie dans l'échangeur 9 et détendue par la turbine d'insufflation 17 jusqu'à la pression d'une colonne basse pression 14. La fraction détendue 1C est envoyée à la colonne 14, éventuellement après une étape de sous-refroidissement. La turbine d'insufflation 17 entraíne le compresseur 15.The fraction 1C is compressed by the compressor 15 to 8.9 x 10 5 kPa, partially cooled in the exchanger 9 and expanded by the blowing turbine 17 to the pressure of a low pressure column 14. The expanded fraction 1C is sent to column 14, possibly after a sub-cooling step. The insufflation turbine 17 drives the compressor 15.

    La double colonne 12 comprenant la colonne basse pression 14 et la colonne moyenne pression 13 est dimensionnée pour produire un débit moyen de liquide qui se vaporise dans l'échangeur 9 pour former un gaz sous pression. En l'occurrence, le liquide est l'oxygène soutiré en cuve de la colonne 14 par la conduite 31 à une pression d'environ 1,5 x 105 kPa. Le liquide est pressurisé jusqu'à 76 x 105 kPa par une pompe 25 avant de se vaporiser dans l'échangeur 9 pour former l'oxygène sous pression.The double column 12 comprising the low pressure column 14 and the medium pressure column 13 is dimensioned to produce an average flow of liquid which vaporizes in the exchanger 9 to form a gas under pressure. In this case, the liquid is oxygen withdrawn from the bottom of column 14 through line 31 at a pressure of approximately 1.5 × 10 5 kPa. The liquid is pressurized to 76 x 10 5 kPa by a pump 25 before being vaporized in the exchanger 9 to form the oxygen under pressure.

    Un appoint d'oxygène gazeux provient d'un réseau 19 à 30 x 105 kPa. Le gaz d'appoint de la conduite 20 se refroidit dans l'échangeur 9, se détend à travers la vanne 21 et est séparé en deux phases dans le séparateur 23. La partie gazeuse de l'oxygène est envoyée au moins en partie à la colonne basse pression 14. La partie liquide est envoyée à la conduite 31 quand la demande en oxygène passe au-dessus de la capacité maximale de la double colonne 12, qui représente 80 % de la demande maximale. Ainsi, le liquide provenant du réseau est vaporisé pour fournir jusqu'à 20 % de la demande maximale. Ce pourcentage est limité par la capacité de liquéfaction de l'oxygène du réseau acceptable par l'échangeur 9.An additional gaseous oxygen comes from a 19 to 30 x 10 5 kPa network. The make-up gas in line 20 cools in exchanger 9, expands through valve 21 and is separated into two phases in separator 23. The gaseous part of the oxygen is sent at least in part to the low pressure column 14. The liquid part is sent to line 31 when the oxygen demand passes above the maximum capacity of the double column 12, which represents 80% of the maximum demand. Thus, the liquid coming from the network is vaporized to supply up to 20% of the maximum demand. This percentage is limited by the liquefaction capacity of the network oxygen acceptable by the exchanger 9.

    De cette manière, avec un appareil sous-dimensionné, on peut néanmoins fournir toute la demande en oxygène gazeux sous pression, pour un coût énergétique moindre.In this way, with an undersized device, you can nevertheless supply all the demand for gaseous oxygen under pressure, to lower energy cost.

    Claims (14)

    1. Process for producing a gas under pressure in a cryogenic separation apparatus, comprising the steps of:
      i) cooling a fluid to be separated in a heat exchanger (9) and sending it to a distillation column (12) of the apparatus;
      ii) withdrawing a liquid stream from the column (12) of the apparatus and warming it in the exchanger (9) ;
      iii) at least one make-up liquid is added to the liquid stream withdrawn in step ii) ;
      iv) the mixture thus formed by the make-up liquid and the withdrawn stream is warmed and vaporized by indirect heat exchange; and
      v) the gas under pressure is recovered at the outlet of the apparatus,
      characterized in that a make-up gas coming from an external source (19) is sent to the exchanger, the make-up gas is cooled therein and is at least partially condensed by heat exchange with the mixture, which vaporizes, in order to form the make-up liquid.
    2. Process according to Claim 1, in which the make-up liquid and the withdrawn stream have substantially the same composition.
    3. Process according to either of Claims 1 and 2, in which the withdrawn liquid is a liquid enriched in oxygen, in nitrogen, in argon or in methane.
    4. Process according to one of the preceding claims, in which most of the gas under pressure comes from the distillation column (14).
    5. Process according to Claim 4, in which at least 80% of the gas under pressure comes from the distillation column.
    6. Process according to one of Claims 1 to 5, in which the make-up liquid is added to the withdrawn stream upstream or downstream of a pressurization means (25).
    7. Process according to one of the preceding claims, in which the fluid to be separated condenses, at least partially, in the exchanger (9) where the liquid withdrawn in step ii) vaporizes.
    8. Process according to one of the preceding claims, in which no final product in liquid form is produced.
    9. Plant for producing a gas under pressure by cryogenic distillation, comprising at least one distillation column (13, 14), a heat exchanger (9), means (1A, 1B, 1C) for sending a fluid to be separated by distillation to the distillation column (13, 14), means (31) for withdrawing a liquid from the distillation column (14), means for sending the withdrawn liquid to the heat exchanger (9) in order to warm the liquid, means (27) for adding a make-up liquid to the withdrawn liquid upstream of the exchanger and means for sending the mixture thus formed to the exchanger (9) so as to form the gas under pressure by vaporizing the liquid,
      characterized in that it comprises means (20) for sending a make-up gas coming from an external source to the exchanger (9) so as to cool the make-up gas and means (21, 23) for at least partially liquefying the cooled make-up gas by heat exchange with the mixture, which vaporizes, in order to form the make-up liquid.
    10. Plant according to Claim 9, in which the withdrawn liquid is a liquid enriched in oxygen, in nitrogen or in argon.
    11. Plant according to Claim 9 or 10, in which the means for withdrawing a liquid are connected to the low-pressure column (14) of a double air-distillation column (12).
    12. Plant according to one of Claims 9 to 11, in which the means for sending the withdrawn liquid to the exchanger are connected to a pressurization means (25) upstream of the exchanger.
    13. Plant according to Claim 12, in which the means for adding liquefied make-up gas to the withdrawn liquid are connected to the means for sending the withdrawn liquid to the exchanger downstream or upstream of the pressurization means (25).
    14. Plant according to one of Claims 9 to 13, in which the means (1A, 1B, 1C) for sending the liquid to be separated to a column pass, at least partially, through the exchanger (9).
    EP96402014A 1995-09-29 1996-09-24 Process and apparatus for the production of pressurized gas by cryogenic distillation Expired - Lifetime EP0766055B1 (en)

    Applications Claiming Priority (2)

    Application Number Priority Date Filing Date Title
    FR9511474A FR2739439B1 (en) 1995-09-29 1995-09-29 METHOD AND PLANT FOR PRODUCTION OF A GAS UNDER PRESSURE BY CRYOGENIC DISTILLATION
    FR9511474 1995-09-29

    Publications (2)

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    EP0766055A1 EP0766055A1 (en) 1997-04-02
    EP0766055B1 true EP0766055B1 (en) 2001-04-18

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    EP (1) EP0766055B1 (en)
    AR (1) AR003711A1 (en)
    CA (1) CA2186837A1 (en)
    ES (1) ES2158262T3 (en)
    FR (1) FR2739439B1 (en)
    PL (1) PL316350A1 (en)

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    FR2800859B1 (en) * 1999-11-05 2001-12-28 Air Liquide METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION
    US6253576B1 (en) * 1999-11-09 2001-07-03 Air Products And Chemicals, Inc. Process for the production of intermediate pressure oxygen
    JP3715497B2 (en) * 2000-02-23 2005-11-09 株式会社神戸製鋼所 Method for producing oxygen
    US6484533B1 (en) * 2000-11-02 2002-11-26 Air Products And Chemicals, Inc. Method and apparatus for the production of a liquid cryogen
    MY143107A (en) * 2006-06-28 2011-03-15 Air Liquide Process for the production of pressurised oxygen and nitrogen by cryogenic distillation of air
    US8136369B2 (en) 2006-07-14 2012-03-20 L'air Liquide Societe Anonyme Pour L'etude System and apparatus for providing low pressure and low purity oxygen
    US8640496B2 (en) * 2008-08-21 2014-02-04 Praxair Technology, Inc. Method and apparatus for separating air
    US9238477B2 (en) * 2014-03-03 2016-01-19 Xtreme Manufacturing, Llc Method and system for a lift device having independently steerable wheels
    US10281207B2 (en) * 2016-06-30 2019-05-07 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method for the production of air gases by the cryogenic separation of air with variable liquid production and power usage

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    EP0383994A3 (en) * 1989-02-23 1990-11-07 Linde Aktiengesellschaft Air rectification process and apparatus
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    FR2706195B1 (en) * 1993-06-07 1995-07-28 Air Liquide Method and unit for supplying pressurized gas to an installation consuming an air component.

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    Also Published As

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    FR2739439B1 (en) 1997-11-14
    EP0766055A1 (en) 1997-04-02
    CA2186837A1 (en) 1997-03-30
    AR003711A1 (en) 1998-09-09
    PL316350A1 (en) 1997-04-01
    FR2739439A1 (en) 1997-04-04
    ES2158262T3 (en) 2001-09-01
    US5685173A (en) 1997-11-11

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