WO2022179748A1 - Procédé et installation pour fournir de l'azote comprimé - Google Patents

Procédé et installation pour fournir de l'azote comprimé Download PDF

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Publication number
WO2022179748A1
WO2022179748A1 PCT/EP2022/025032 EP2022025032W WO2022179748A1 WO 2022179748 A1 WO2022179748 A1 WO 2022179748A1 EP 2022025032 W EP2022025032 W EP 2022025032W WO 2022179748 A1 WO2022179748 A1 WO 2022179748A1
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WO
WIPO (PCT)
Prior art keywords
pressure
heat exchanger
main heat
pressure range
range
Prior art date
Application number
PCT/EP2022/025032
Other languages
German (de)
English (en)
Inventor
Tobias Lautenschlager
Original Assignee
Linde Gmbh
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Filing date
Publication date
Application filed by Linde Gmbh filed Critical Linde Gmbh
Publication of WO2022179748A1 publication Critical patent/WO2022179748A1/fr

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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
    • F25J3/044—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 single pressure main column system only
    • 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
    • F25J3/04012—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
    • F25J3/0403—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 nitrogen
    • 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
    • F25J3/0406—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 nitrogen
    • 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
    • F25J3/04084—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 nitrogen
    • 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
    • F25J3/04145—Mechanically coupling of different compressors of the air fractionation process to the same driver(s)
    • 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
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/042—Division of the main heat exchange line in consecutive sections having different functions having an intermediate feed connection
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/0423—Subcooling of liquid process streams
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • 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
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • 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

Definitions

  • the invention relates to a method and a system for providing a compressed nitrogen product according to the preambles of the independent patent claims.
  • GB 870349 A discloses a process for separating a gas mixture, for example air, in a rectification column to provide at least one component.
  • the mixture is cooled by passing it through a first passage in heat exchange relationship with a cold refrigerant flowing through a second passage and causing contaminants with a higher freezing point to be deposited in the first passage.
  • a cold fluid e.g., waste fluid
  • a warm coolant capable of heating the cold fluid to remove the deposited contaminants sublimate and transport away
  • a cryogenic rectification process for the production of nitrogen gas under elevated pressure comprises compressing a feedstock containing nitrogen and oxygen, cooling the compressed feedstock and introducing the resulting cooled feedstock into a column, separating the feedstock within the column by cryogenic rectification into nitrogen-rich vapor and oxygen-enriched liquid, the vaporization of the oxygen-enriched liquid by indirect heat exchange with nitrogen-rich vapor to produce nitrogen-rich liquid and oxygen-enriched vapor, pressurizing the nitrogen-rich liquid to produce an elevated pressure nitrogen-rich liquid, evaporating the nitrogen-rich elevated liquid by indirect heat exchange with compressed fluid to produce elevated pressure nitrogen gas and recovering elevated pressure nitrogen gas as product.
  • Air separation plants of the classic type have rectification column systems which can be designed, for example, as two-column systems, in particular as double-column systems, but also as three-column or multi-column systems.
  • rectification columns for obtaining nitrogen and/or oxygen in the liquid and/or gaseous state ie rectification columns for nitrogen-oxygen separation, rectification columns for obtaining further air components, in particular inert gases, can be provided.
  • the rectification columns of the rectification column systems mentioned are operated at pressures in different pressure ranges.
  • Known double column systems have a so-called high-pressure column (also referred to as a pressure column, medium-pressure column or lower column) and a so-called low-pressure column (upper column).
  • the high-pressure column is typically operated at a pressure in a pressure range of 4 to 7 bar, in particular approx. 5.3 bar, while the low-pressure column is operated at a pressure in a pressure range of typically 1 to 2 bar, in particular approx. 1.4 bar.
  • higher pressures can also be used in both rectification columns.
  • the pressures or pressure ranges specified here and below are absolute pressures at the top of the columns specified in each case.
  • Corresponding single-column processes can be carried out in particular as so-called single-column single-condenser processes (SCSC) using so-called residual gas turbines.
  • SCSC single-column single-condenser processes
  • the rectification column is operated with a top condenser, in which bottom liquid from the rectification column is evaporated and top gas from the rectification column is condensed to form a reflux.
  • a sump reboiler is typically absent.
  • the residual gas turbine at least part of the bottom liquid evaporated in the top condenser, the residual gas, is expanded to obtain cold.
  • EP 3 521 739 A1 discloses a process for obtaining nitrogen in which the low-pressure column of a double column system, or more generally a second rectification column for nitrogen-oxygen separation, has a first rectification column for nitrogen-oxygen separation and the second rectification column Column system, is operated with a top condenser (also referred to as "double condenser, double reboiler” or “double column, double condenser” or DCDC process).
  • a top condenser also referred to as "double condenser, double reboiler” or “double column, double condenser” or DCDC process.
  • gaseous nitrogen under comparatively high pressure typically 50 to 130 bar
  • caloric parameters typically 50 to 130 bar
  • the gaseous nitrogen is obtained from a system designed as explained above at 5 to 10 bar (abs.) and then further compressed in a complex manner. With quantities below 20 kNm 3 /h (the unit Nm 3 denotes standard cubic meters here), the nitrogen is compressed to pressures of over 80 bar (abs.) typically in piston compressors, which have considerable disadvantages due to their design (high investment costs, low efficiency, no partial load behavior, high maintenance costs).
  • the present invention therefore sets itself the task of improving the provision of compressed nitrogen, in particular in the pressure range mentioned and in particular for the applications mentioned, and making it more efficient.
  • a “condenser evaporator” refers to a heat exchanger in which a first, condensing fluid stream enters into indirect heat exchange with a second, evaporating fluid stream.
  • Each condenser evaporator has a condensing space and an evaporating space.
  • Condensation and evaporation chambers have liquefaction and evaporation passages. The condensation (liquefaction) of the first fluid stream is carried out in the liquefaction chamber, and the evaporation of the second fluid stream is carried out in the evaporation chamber.
  • the evaporating and condensing spaces are formed by groups of passages which are in heat exchange relationship with each other.
  • Condenser evaporators are also called “top condenser” and referred to as “bottom reboiler", where a top condenser is a condenser evaporator in which top gas of a rectification column is condensed and a bottom evaporator is a condenser evaporator in which bottom liquid of a rectification column is evaporated.
  • a liquid flow is pushed through the evaporation chamber by its own pressure and partially evaporated there.
  • This pressure is generated, for example, by a liquid column in the feed line to the evaporation space.
  • the fleas of this liquid column corresponds to the pressure loss in the evaporation space.
  • the gas-liquid mixture emerging from the evaporation chamber is separated according to phases and forwarded directly to the next process step or to a downstream device and, in particular, is not introduced into a liquid bath of the condenser evaporator, from which the portion that remains liquid is fed again would be sucked in.
  • expansion turbine or “expansion machine”, which can be coupled to other expansion turbines or energy converters such as oil brakes, generators or compressors via a common shaft, is set up to expand a gaseous or at least partially liquid stream.
  • expansion turbines for use in the present invention can be designed as turboexpanders. If a compressor is driven with one or more expansion turbines, but without energy supplied externally, for example by means of an electric motor, the term “turbine-driven” compressor or alternatively “booster” is used. Arrangements of turbine-driven compressors and expansion turbines are also referred to as “booster turbines" or alternatively as “turbine boosters". If in the following it is mentioned that an expansion takes place in a booster turbine or a turbine booster, this should mean the turbine part. The same applies to the compression, which then takes place in the compressor part of the booster turbine or the turbine booster.
  • turbo compressors In air separation plants, multi-stage turbo compressors are used to compress the feed air to be separated, which are referred to here as "main air compressors".
  • the mechanical structure of turbo compressors is known in principle to those skilled in the art.
  • the compression of the to takes place in a turbo compressor compressing medium by means of turbine blades, which are arranged on a turbine wheel or impeller or directly on a shaft.
  • a turbo compressor forms a structural unit which, however, can have several compressor stages in the case of a multi-stage turbo compressor.
  • a compressor stage generally includes a corresponding arrangement of turbine blades. All of these airends can be driven by a common shaft. However, it can also be provided that the compressor stages are driven in groups with different shafts, in which case the shafts can also be connected to one another via gears.
  • the main air compressor is also distinguished by the fact that it compresses the entire amount of air fed into the rectification column system and used for the production of air products, ie the entire feed air.
  • a "post-compressor" can also be provided, in which, however, only part of the air quantity compressed in the main air compressor is brought to an even higher pressure.
  • This can also be designed as a turbo compressor.
  • the use of a common compressor or compressor stages of such a compressor as the main air compressor and booster can also be provided.
  • additional turbo compressors in the form of the boosters mentioned are typically provided in air separation plants, but these usually only perform compression to a relatively small extent compared to the main air compressor or the secondary compressor.
  • Liquids and gases can be rich or poor in one or more components, where “rich” means a content of at least 50%, 75%, 90%, 95%, 99%, 99.5%, 99, 9% or 99.99% and “poor” can stand for a content of at most 50%, 25%, 10%, 5%, 1%, 0.1% or 0.01% on a mole, weight or volume basis .
  • the term “predominantly” may correspond to the definition of "rich”.
  • Liquids and gases can also be enriched or depleted in one or more components, these terms referring to a content in a starting liquid or a starting gas from which the liquid or gas was obtained.
  • the liquid or the gas is "enriched” if this or this at least 1.1 times, 1.5 times, 2 times, 5 times, 10 times, 100 times or 1,000 times the content, and "depleted” if this or this has at most 0.9 times, 0.5 times, 0.1 times, 0.01 times or 0.001 times the content of a corresponding one Component based on the starting liquid or the starting gas contains. If, for example, “oxygen” or “nitrogen” is mentioned here, this also includes a liquid or a gas that is rich in oxygen or nitrogen, but does not necessarily have to consist exclusively of them.
  • air separation plants can be designed differently depending on the air products to be delivered and their required aggregate and pressure states.
  • So-called internal compression is known for providing gaseous pressure products.
  • a cryogenic liquid is removed from the rectification column system, subjected to an increase in pressure in the liquid state and converted to the gaseous or supercritical state by heating.
  • internally compressed gaseous oxygen, internally compressed gaseous nitrogen or internally compressed gaseous argon can be produced in this way.
  • Internal compression offers a number of advantages over external compression, which is also possible as an alternative, and is explained, for example, in Häring (see above), Section 2.2.5.2, "Internal Compression".
  • the present invention proposes a method and a system for providing pressurized nitrogen in the above-mentioned single-column single-condenser configuration, in which up to 100% of the total pressurized nitrogen to be provided is internally compressed to pressures of 60 bar (abs.) up to 150 bar (abs.) can be compressed.
  • a double-column double-condenser configuration can also be used, as was also explained above.
  • gaseous nitrogen from the rectification column used is further compressed and liquefied in the main heat exchanger, with available combination machines being able to be used in a particularly advantageous manner.
  • the invention proposes a process for producing a compressed nitrogen product by cryogenic separation of air, in which an air separation plant with a main heat exchanger and a rectification column used with a head condenser.
  • the top condenser can be designed as a bath, cascade or forced flow condenser, as explained.
  • the pressure energy contained in the top gas of the condenser is used within the scope of the present invention, in particular in a residual gas turbine.
  • a top gas and a bottom liquid are formed at a pressure in a first pressure range, as is known in principle, using compressed air fed into the rectification column and cooled in the top heat exchanger.
  • a first part of the top gas is condensed to obtain a first condensate at a pressure in the first pressure range and at least part of the bottom liquid is evaporated at a pressure in a second pressure range below the first pressure range, as also in particular for the mentioned single-column - Single condenser and double column double condenser configurations are known.
  • nitrogen-rich liquid is withdrawn in a product quantity at a pressure in the first pressure section, subjected to internal compression and used to provide the compressed nitrogen product.
  • the nitrogen-rich liquid is subjected to a pressure increase to a pressure in a third pressure range of 50 to 110 bar absolute pressure and is converted to the supercritical state in the Flaupt heat exchanger, so that the pressure requirements mentioned at the outset are met by the use of the present invention can become.
  • a second part of the top gas is heated in a recirculation amount in the main heat exchanger, subjected to compression on the warm side of the main heat exchanger to a pressure in a fourth pressure range, condensed in the main heat exchanger to obtain a second condensate, and fed back into the rectification column.
  • the pressure in the third pressure range is at least a factor of 1.5, in particular at least a factor of 1.6 and up to a factor of 2 higher than the pressure in the fourth pressure range, and a ratio between the feed-back quantity and the product quantity is 2:1 up to 1.3:1.
  • a "procedural transmission" is created by the present invention, so to speak.
  • the compressor used for the second portion of the top gas, or corresponding compressor stages compresses a large quantity of compressed nitrogen to a comparatively low pressure and thus drives the internal compression of a small quantity of liquid nitrogen under high pressure.
  • the analogy in a gearbox is high speed with low torque converted to low speed with high torque.
  • the combination of large volume and low pressure enables the corresponding compressor or compressor stages to be designed as turbo compressors (stages), which brings advantages in the areas of investment costs, efficiency, part-load behavior and maintenance.
  • the piston compressors mentioned at the outset can be dispensed with.
  • the first pressure range in which the operating pressure of the rectification column lies, can be in particular from 7 to 15 bar (absolute), for example about 10.5 bar (absolute).
  • the for feeding the rectification column can be at a pressure in a pressure range above this, which depends on the specific configuration.
  • the second pressure range in which the evaporation pressure in the top condenser lies, can be in particular from 3 to 7 bar (abs.), in particular about 5.6 bar (abs.).
  • the fourth pressure range in which the pressure lies to which the second part of the top gas is compressed, is in particular 30 to 70 bar (abs.), for example approx. 36 bar (abs.).
  • a quantity ratio between the second part of the top gas, which is treated accordingly, i.e. the recirculation quantity, and the nitrogen-rich liquid subjected to internal compression, i.e. the product quantity, can in particular be in a range from 2:1 to 1.5:1 or from 1.5:1 to 1.3:1, in each case based on normalized mass flows.
  • compressed nitrogen can also be taken off at a pressure range below the third pressure range, in the form of overhead gas, before or after compression to the pressure in the third pressure range, i.e. to the pressure in the first or the third pressure range.
  • At least part of the first condensate can be fed back to the rectification column and/or used to provide a liquid nitrogen product, if required, within the scope of the present invention.
  • a gas phase can be formed which is used at least in part to form a residual gas stream, the residual gas stream being subjected to a first heating in the main heat exchanger at the pressure in the second pressure range, and then being expanded to a pressure in a fifth pressure range in a booster turbine arrangement, and thereafter at the pressure in the fifth pressure range may be subjected to a second heating in the main heat exchanger.
  • a residual gas turbine can be used to cover the cold balance, with the residual gas turbine being braked by a booster, oil or generator can be executed.
  • the residual gas turbine can be self-boosted or braked by a booster which further compresses the previously compressed second part of the overhead gas before it is liquefied in the main heat exchanger.
  • the residual gas stream after the first heating, can be subjected to compression to a pressure in a sixth pressure range in the booster turbine arrangement, then to the pressure in the sixth pressure range, to intermediate cooling in the main heat exchanger, and thereafter being subjected to the expansion to the pressure in the fifth pressure range in the booster turbine arrangement, and thereafter being subjected to the second heating.
  • the second part of the head gas in particular can also be subjected to a pressure in a seventh pressure range after compression on the warm side of the main heat exchanger to the pressure in the fourth pressure range and before condensation in the main heat exchanger to further compression in the booster turbine arrangement .
  • the seventh pressure range can in particular be 40 to 70 bar (abs.), for example about 48 bar (abs.).
  • the second part of the top gas can, after further compression in the booster turbine arrangement to the pressure in the seventh pressure range and before condensation in the main heat exchanger, also undergo (again) further compression in a further
  • Booster turbine assembly is subjected to a pressure in an eighth pressure range. Due to the double further compression of the second part of the top gas, the first compressor used can be designed with fewer stages, which improves the buildability, especially in combination with the main air compressor.
  • the further booster turbine arrangement (or its booster) can be used as a warm or cold booster.
  • the second part of the top gas can therefore in particular after further compression in the booster turbine arrangement to the pressure in the seventh pressure range and before further compression in the further booster turbine arrangement to the pressure in the eighth printing range may be subjected to cooling to a temperature in a temperature range from 0 to -170 °C.
  • the compressed air When the compressed air is compressed to higher values than those in the first pressure range, for example to a pressure in a pressure range of 15 to 25 bar (abs.), in particular 16 to 24 bar (abs.), the compressed air can be brought to the main heat exchanger at a temperature in a first
  • a corresponding configuration can alternatively also include the use of an oil or generator-braked turbine instead of the further booster turbine arrangement for expanding the compressed air.
  • the main heat exchanger can also be provided in several parts (e.g. set up for higher and lower pressures), for example to meet requirements for design pressures, thermal stresses and the like.
  • the compressed air fed into the rectification column and cooled in the main heat exchanger can also represent only part of a compressed total amount of air, with a further part of the compressed total amount of air being cooled in the main heat exchanger, an expansion to a pressure in a ninth, in particular slightly above atmospheric pressure range of, for example, 1, 1 to 1.5 bar (abs.), Subject to heating in the main heat exchanger to the pressure in the ninth pressure range and discharged from the air separation plant.
  • one or more first compressor stages can be used to provide the compressed air
  • one or more (in particular two or three) second compressor stages can be used to compress the second part of the overhead gas on the hot side of the main heat exchanger, with the one or more first and the one or more second Compressor stages are provided in a common compressor.
  • the second portion of the overhead gas can be driven to the compressor stage(s) 5 to 35° C. colder than the other streams, if there is excess cold.
  • FIGS. 1 to 5 show systems according to preferred embodiments of the invention in a simplified, schematic representation.
  • FIG. 1 an air separation plant according to one embodiment of the invention is illustrated and denoted overall by 100.
  • feed air is sucked in by means of a main air compressor 1 or one or more corresponding compressor stages and compressed to a pressure in a pressure range of 7 to 15 bar (abs.), for example approx. 11 bar (abs.).
  • a compressed air flow formed in this way is in a warm part 2 of the air separation plant 100, which can have components known per se and in particular with a pre-cleaning unit 2.1 (Prepurification Unit, PPU) can be equipped in a known way, conditioned to obtain a compressed air stream b.
  • Prepurification Unit, PPU Prepurification Unit
  • the partial flow c is taken from the main heat exchanger 3 of the air separation plant 100 at an intermediate temperature and expanded in a turbine arrangement 4 with an expansion turbine, for example oil-braked.
  • the partial flow c is then heated in the main heat exchanger 3 and discharged, for example, into the atmosphere (so-called excess air).
  • Partial stream d is taken from the cold side of main heat exchanger 3 of air separation plant 100 and fed into a rectification column 5, in which a top gas and a bottom liquid are formed using the air fed in.
  • the rectification column 5 is operated, in particular at the top, at a pressure in a pressure range which, apart from pressure losses, corresponds to that of the compressed air stream a, for example at approx. 10.5 bar (abs.).
  • the top gas is withdrawn from the rectification column 5 in the form of a stream e.
  • a substream f of stream e is condensed in a top condenser 5.1 of the rectification column 5 and, again in portions, used in the form of a stream g to form a reflux stream h to the rectification column 5 and in the form of a stream i optionally in an optionally provided subcooler 6 supercooled and provided as a liquid nitrogen product.
  • Another part of the top gas of stream e is heated in the main heat exchanger 3 in the form of stream k.
  • a part of the heated material flow k is recompressed in the form of a material flow I in a compressor 7 or one or more compressor stages, which can also be installed in a common machine with the compressor stage(s) of the main air compressor 1 .
  • the recompression can take place, for example, to a pressure in a pressure range from 40 to 70 bar (abs.), for example approx. 44 bar (abs.).
  • the stream I is cooled again in the main heat exchanger 3 and condensed in the process, expanded at a throttle valve 8 and used to form the return stream h already mentioned.
  • top condenser 5.1 of the rectification column 5 bottom liquid from the rectification column 5, which is removed from this in the form of a stream m, is supercooled in a subcooler 9 and expanded at a throttle valve 10, evaporated.
  • a purge stream n is removed from the top condenser 5.1 of the rectification column 5 to avoid the accumulation of less volatile components.
  • Residual gas which is formed by the evaporation of the bottom liquid of the rectification column 5, is carried out in gaseous form in the form of a stream o from the top condenser 5.1 and passed through the subcoolers 6 (if present) and 9.
  • the removal takes place at a pressure in a pressure range at which the bottom liquid of the rectification column 5 is also evaporated in the top condenser 5.1, in particular at 3 to 6 bar (abs.), for example at approx. 5.6 bar (abs.).
  • the material flow o is then brought to a higher pressure in a booster turbine arrangement 11, fed back to the main heat exchanger 3 on the hot side, removed from it at an intermediate temperature, expanded in the booster turbine arrangement 11, completely heated in the main heat exchanger 3, and discharged from the air separation plant 100 or used in the pre-cleaning unit 2.1 in a known manner as regeneration gas.
  • Liquid nitrogen is removed from the rectification column 5 in the form of a liquid nitrogen stream p, pressurized in liquid form in an internal compression pump 12, heated in the main heat exchanger 3 and discharged as compressed nitrogen product from the air separation plant (100).
  • FIG. 2 an air separation plant according to a further embodiment of the invention is illustrated and denoted overall by 200.
  • an air separation plant according to a further embodiment of the invention is illustrated and denoted overall by 300.
  • air separation plant 300 according to FIG brought higher pressure, whereas the flow o experiences no such increase in pressure.
  • the material flow o is only heated to an intermediate temperature in the auxiliary heat exchanger 3 , then expanded in the booster turbine arrangement 11 and then completely heated in the auxiliary heat exchanger 3 .
  • the air separation plant 300 according to FIG. 3 can essentially correspond to the air separation plant 200 according to FIG.
  • FIG. 4 an air separation plant according to a further embodiment of the invention is illustrated and denoted overall by 400.
  • a further booster turbine arrangement 13 is used in the air separation plant 400 according to FIG.
  • the further booster turbine arrangement 13 is driven by the material flow b provided here as in the air separation plant 200 according to FIG. 2 and in the air separation plant 300 according to FIG.
  • the material stream b is cooled to an intermediate temperature in the Flaupt heat exchanger 3, then expanded in the further booster turbine arrangement 13 and, after being fed back into the Flaupt heat exchanger 3, further cooled to a further intermediate temperature.
  • an air separation plant according to a further embodiment of the invention is illustrated and denoted overall by 500.
  • the booster of the further booster turbine arrangement 13 is operated as a cold booster in the air separation plant 500 according to FIG.
  • the material flow I (see also connection point L) is cooled further in the booster turbine arrangement 11 after its compression in the booster turbine arrangement 11 and before further compression in the further booster turbine arrangement 13 .

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

Abstract

La présente invention concerne un procédé de production d'un produit à base d'azote comprimé par séparation cryogénique d'air, dans lequel procédé une installation de séparation d'air (100-500) ayant un échangeur de chaleur principal (3) et ayant une colonne de rectification (5) avec un condenseur supérieur (5.1) est utilisée. Dans la colonne de rectification (5), un gaz supérieur et un liquide inférieur sont formés en utilisant de l'air comprimé qui est à une pression dans une première plage de pression, l'air comprimé étant introduit dans la colonne de rectification (5) et étant refroidi dans l'échangeur de chaleur principal (3) ; dans le condenseur supérieur (5.1), une première partie du gaz supérieur est condensée à une pression dans la première plage de pression de telle sorte qu'un premier condensat est obtenu, et au moins une partie du liquide inférieur est évaporée à une pression dans une deuxième plage de pression au-dessous de la première plage de pression ; et un liquide riche en azote est extrait à une pression dans la première plage de pression, selon une quantité de produit, à partir d'une région supérieure de la colonne de rectification (5), est soumis à une compression interne et est utilisé pour fournir le produit à base d'azote comprimé. Selon la présente invention, le liquide riche en azote est soumis, à l'état liquide, à une augmentation de pression jusqu'à une pression dans une troisième plage de pression de 50 à 110 bars de pression absolue pendant la compression interne et est mis dans l'état supercritique dans l'échangeur de chaleur principal (3), et une seconde partie du gaz supérieur, selon une quantité de retour, est chauffée dans l'échangeur de chaleur principal (3), est soumis, sur le côté chaud de l'échangeur de chaleur principal (3), à une compression jusqu'à une pression dans une quatrième plage de pression, est condensé dans l'échangeur de chaleur principal (3) de telle sorte qu'un second condensat est obtenu, et est au moins partiellement renvoyé dans la colonne de rectification (5). La pression dans la troisième plage de pression est supérieure à la pression dans la quatrième plage de pression au moins d'un facteur de 1,5, et un rapport de quantités entre la quantité de retour et la quantité de produit est de 2:1 à 1,3:1. La présente invention concerne également une installation de séparation d'air (100-500) correspondante.
PCT/EP2022/025032 2021-02-25 2022-02-02 Procédé et installation pour fournir de l'azote comprimé WO2022179748A1 (fr)

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Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB870349A (en) 1957-11-14 1961-06-14 Joy Mfg Co Method and apparatus for the separation of gas mixtures
JPS6237675A (ja) * 1985-08-12 1987-02-18 株式会社神戸製鋼所 窒素発生装置
US5303556A (en) 1993-01-21 1994-04-19 Praxair Technology, Inc. Single column cryogenic rectification system for producing nitrogen gas at elevated pressure and high purity
EP1314941A2 (fr) * 2001-11-23 2003-05-28 Messer AGS GmbH Procédé et dispositif pour la production d'azote à partir de l'air
WO2015014485A2 (fr) * 2013-08-02 2015-02-05 Linde Aktiengesellschaft Procédé et dispositif de production d'azote comprimé
EP3521739A1 (fr) 2018-02-02 2019-08-07 Linde Aktiengesellschaft Procédé et dispositif de récupération d'azote comprimé par décomposition à basse température de l'air

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GB870349A (en) 1957-11-14 1961-06-14 Joy Mfg Co Method and apparatus for the separation of gas mixtures
JPS6237675A (ja) * 1985-08-12 1987-02-18 株式会社神戸製鋼所 窒素発生装置
US5303556A (en) 1993-01-21 1994-04-19 Praxair Technology, Inc. Single column cryogenic rectification system for producing nitrogen gas at elevated pressure and high purity
EP1314941A2 (fr) * 2001-11-23 2003-05-28 Messer AGS GmbH Procédé et dispositif pour la production d'azote à partir de l'air
WO2015014485A2 (fr) * 2013-08-02 2015-02-05 Linde Aktiengesellschaft Procédé et dispositif de production d'azote comprimé
EP3521739A1 (fr) 2018-02-02 2019-08-07 Linde Aktiengesellschaft Procédé et dispositif de récupération d'azote comprimé par décomposition à basse température de l'air

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ANONYMOUS ED - DARL KUHN: "Process And Apparatus For The Production Of Gaseous and Liquid Nitrogen", IP.COM, IP.COM INC., WEST HENRIETTA, NY, US, 30 June 2003 (2003-06-30), XP013010332, ISSN: 1533-0001 *
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