EP3027988A2 - Procédé et dispositif de production d'azote comprimé - Google Patents

Procédé et dispositif de production d'azote comprimé

Info

Publication number
EP3027988A2
EP3027988A2 EP14744775.9A EP14744775A EP3027988A2 EP 3027988 A2 EP3027988 A2 EP 3027988A2 EP 14744775 A EP14744775 A EP 14744775A EP 3027988 A2 EP3027988 A2 EP 3027988A2
Authority
EP
European Patent Office
Prior art keywords
pressure
stream
pressure column
column
liquid
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP14744775.9A
Other languages
German (de)
English (en)
Inventor
Alexander Alekseev
Dimitri Goloubev
Thomas Eckert
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Priority to EP14744775.9A priority Critical patent/EP3027988A2/fr
Publication of EP3027988A2 publication Critical patent/EP3027988A2/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—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
    • F25J3/04424—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 without thermally coupled high and low pressure columns, i.e. a so-called split columns
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—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
    • F25J3/04024—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 purified feed air, so-called boosted air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—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
    • F25J3/04115—Arrangements of compressors and /or their drivers characterised by the type of prime driver, e.g. hot gas expander
    • 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
    • F25J3/04115—Arrangements of compressors and /or their drivers characterised by the type of prime driver, e.g. hot gas expander
    • F25J3/04121—Steam turbine as the prime mechanical driver
    • 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
    • F25J3/04115—Arrangements of compressors and /or their drivers characterised by the type of prime driver, e.g. hot gas expander
    • F25J3/04127—Gas turbine as the prime mechanical driver
    • 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
    • F25J3/04248—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
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    • 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
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    • 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
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    • 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
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    • 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
    • F25J3/04339—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 air
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    • 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
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    • 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.
    • F25J3/04387—Details relating to the work expansion, e.g. process parameter etc. using liquid or hydraulic turbine expansion
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    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
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    • 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
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    • 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
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04563—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating
    • F25J3/04569—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating for enhanced or tertiary oil recovery
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    • 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
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    • 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
    • F25J3/04787—Heat exchange, e.g. main heat exchange line; Subcooler, external reboiler-condenser
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    • 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
    • F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
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    • 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
    • F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
    • F25J3/04878—Side by side arrangement of multiple vessels in a main column system, wherein the vessels are normally mounted one upon the other or forming different sections of the same column
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    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/20—Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
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    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • F25J2200/52—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the high pressure column of a double pressure main column system
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    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • F25J2200/54—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the low pressure column of a double pressure main column system
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    • 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
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
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    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/40—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/52—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen enriched compared to air ("crude oxygen")
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/04—Multiple expansion turbines in parallel
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    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/10—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream the fluid being air
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    • 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
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
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    • 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
    • F25J2245/40—Processes or apparatus involving steps for recycling of process streams the recycled stream being air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop

Definitions

  • the invention relates to a method for producing pressurized nitrogen according to the preamble of patent claim 1.
  • a method of the type mentioned is known from US 6141989.
  • pressurized nitrogen is produced under a product pressure of 12 bar by internal compression.
  • nitrogen is brought to liquid product pressure and then evaporated in indirect heat exchange with air and warmed to about ambient temperature.
  • the natural pressure losses are usually not included here.
  • pressures are considered “equal” if the pressure difference between the corresponding points is not greater than the natural conduction losses caused by pressure losses in piping, heat exchangers, coolers, adsorbers, etc.
  • the internal compression nitrogen flow experiences a pressure loss in the passages of the main heat exchanger; nevertheless, here the discharge pressure of the pressurized nitrogen product downstream of the
  • condenser-evaporator refers to a heat exchanger in which a first condensing fluid stream undergoes indirect heat exchange with a second evaporating fluid stream.
  • Each condenser evaporator has a
  • Condensing passages or evaporation passages exist.
  • the condensation (liquefaction) of a first fluid flow is performed, in the evaporation space the evaporation of a second fluid flow.
  • Evaporation and liquefaction space are formed by groups of passages that are in heat exchange relationship with each other.
  • the "main heat exchanger" is used for cooling of feed air in indirect
  • Heat exchange with recycle streams from the distillation column system can be composed of a single or several parallel and / or serially connected
  • Heat exchanger sections may be formed, for example, from one or more plate heat exchanger blocks.
  • the main heat exchanger in this sense is formed, for example, in US Pat. No. 6,141,989 by the combination of a gas-gas exchanger with a condenser-evaporator, in which pumped high-pressure column nitrogen is vaporized in indirect heat exchange with a condensing substream of the feed air.
  • the "internal condensing nitrogen stream” is vaporized (or, if its pressure is supercritically pseudo-vaporized) against a high pressure air stream and warmed.
  • the high-pressure air is thereby cooled and liquefied or, if its pressure is supercritical, pseudo-liquefied.
  • no separate condenser-evaporator is used for nitrogen evaporation, but the (pseudo) evaporation and the
  • Heating takes place in an integrated main heat exchanger.
  • oxygen-enriched product gas stream any gaseous product or residual stream that is discharged from the system and that has an oxygen content that is higher than that of air. It can be very pure oxygen or just a light one
  • oxygen-enriched residual gas may comprise one or more such streams.
  • Air separation plant using a gas compressor are further compressed, for example, to 100 bar.
  • the known method therefore requires two externally driven compressors 3 and 5, as shown schematically in FIG. 1, in order to deliver a pressurized nitrogen product below more than 12 bar.
  • two externally driven compressors 3 and 5 as shown schematically in FIG. 1, in order to deliver a pressurized nitrogen product below more than 12 bar.
  • High-pressure nitrogen (HPGAN - High Pressure Gaseous Nitrogen) can be delivered, for example, to support oil production (to EOR - Enhanced Oil Recovery).
  • HPGAN High Pressure Gaseous Nitrogen
  • EOR EOR - Enhanced Oil Recovery
  • the invention is based on the object to produce a pressurized nitrogen product under very high pressure in an energetically particularly favorable manner and thereby to use a relatively inexpensive apparatus.
  • a pressurized nitrogen product is obtained directly by internal compression under a pressure of 15 to 100 bar. If this pressure for the
  • Air separation plant not to be densified and the corresponding energy and equipment expense is eliminated.
  • an external further compression above the internal compression pressure also in the invention is possible; but even then the energy consumption is relatively low and it is sufficient for a relatively small nitrogen gas compressor.
  • the operating pressures of the columns (at the top of each head) are in the invention
  • the expenditure on equipment can be kept comparatively low, in that despite the high air pressure only a single externally driven compressor is used, namely the main air compressor.
  • one-stage turbine-driven compressors boost are not excluded, which require no external energy, but is driven so to speak with the energy generated in the main air compressor, which is converted into mechanical energy during the work-relaxing relaxation in the turbine.
  • the "first partial flow”, which is expanded to perform work, is formed by the entire remainder of the total air flow, which is not required as a “second partial flow” for internal compression.
  • the "first partial flow” of the air can be before the
  • cooling work to be cooled below ambient temperature, in particular in the main heat exchanger to an intermediate temperature between the temperatures of the hot and the cold end of the main heat exchanger. It then enters the work-performing expansion in the gaseous state and is finally at least partially introduced in the gaseous state into the distillation column system, in particular into the high-pressure column.
  • the gas portion of the first partial flow forms the rising vapor in the lower part of the high-pressure column.
  • High pressure column partially or completely liquefied and fed liquid into the high-pressure column; the rising gas in the lower part of the high-pressure column is then formed by the vapor generated in the high pressure column sump evaporator.
  • High-pressure column head condenser is operated with liquid air only (that is, with a liquid having the same or similar composition as the atmospheric air).
  • the "second part of the feed air” is directly or via a separator (phase separator), which may be arranged in a separate container or installed in the high-pressure column, in the
  • High-pressure column top condenser the two columns can be arranged side by side without the need for process pumps to lift liquids.
  • the system becomes more compact and the columns can be largely prefabricated and then transported to the site.
  • the main air compressor has a single drive unit, which is formed in particular by a gas turbine unit, a steam turbine, a gas engine or a diesel engine.
  • This drive unit then represents the sole source of external energy of the whole system, apart from liquid pumps, which consume much less energy than gas compressors, and the power supply for auxiliary equipment such as control and regulation equipment, lighting, etc. This achieves a very extensive simplification of the compressor drive;
  • a bottom evaporator of the low pressure column can be dispensed by steam generated in the evaporation chamber of the high-pressure column head condenser in the bottom region of the low-pressure column is introduced, said steam forms the entire ascending in the lower portion of the low pressure column gas.
  • a "third partial stream" of the first liquid nitrogen stream is fed as reflux to the low-pressure column, and the internal compression nitrogen stream is formed by a second partial stream of the second liquid nitrogen stream.
  • Liquid nitrogen from the high-pressure column overhead condenser as reflux for the low-pressure column a correspondingly increased proportion of the liquid nitrogen from the low-pressure column top condenser of the internal compression can be supplied.
  • third sub-stream here means that in the process a "second sub-stream" of the first liquid nitrogen stream may or may not exist.
  • the internal compression nitrogen flow is formed by a second partial stream of the first liquid nitrogen stream (from the high pressure column top condenser) and a second partial stream of the second liquid nitrogen stream (from the low pressure column top condenser), these two partial streams being separate on the
  • Embodiment also possible to bring the two second streams to different product pressures or partial streams to the required pressures (after pumping) to relax; the various internal compression nitrogen flows under the different pressures are then separated by the
  • the second partial stream of the second liquid nitrogen stream (from the low-pressure column overhead condenser) is first brought to approximately high-pressure column pressure in the liquid state, and then combined with the second partial stream of the first liquid nitrogen stream (from the high-pressure column top condenser). The mixture then forms the internal compression nitrogen stream and is brought together in a further step from the high pressure column pressure to the product pressure.
  • cold is preferably produced in a single expansion machine, wherein the first partial flow of the high-pressure total air flow is at least partially introduced into the high-pressure column downstream of its work-performing expansion.
  • the expansion machine can be formed for example by an expansion turbine. It may be coupled to a secondary compressor in which the first partial flow of the high-pressure total airflow upstream of its work-performing expansion or the second partial flow of the high-pressure total airflow or the high-pressure total airflow is recompressed to a pressure which is higher than the total air pressure.
  • the process of the invention utilizes two condenser evaporators, the high pressure column top condenser and the low pressure column top condenser.
  • a third condenser-evaporator in the form of a high-pressure column bottom evaporator.
  • bottom liquid of the high-pressure column is evaporated in indirect heat exchange with condensing air, which takes the form of a third part of the
  • High-pressure total air flow is introduced into the liquefaction space of the high-pressure column bottom evaporator.
  • the evaporated bottoms liquid is introduced as ascending gas in the high-pressure column, where it strengthens the
  • the "third part" of the high-pressure total air flow can be formed by the work-performing expanded first partial flow or by a part thereof.
  • energy can be saved by the second partial flow of air in a turbine-driven
  • the booster is preferably used by the Powered relaxation machine, in which the first partial flow of air is released to perform work.
  • Liquid turbine is preferably braked by a generator that generates electrical energy.
  • the energy efficiency can in the inventive method by a boost circuit for the high-pressure column (claim 12) or a
  • the invention also relates to a device according to claim 14.
  • the device according to the invention can be supplemented by device features which correspond to the features of the dependent method claims.
  • the invention and further details of the invention are explained in more detail below with reference to exemplary embodiments shown schematically in FIGS. 2 to 12. Hereby show:
  • FIGS. 3 to 5 show three embodiments of the distillation column system of a system according to the invention
  • FIGS 6 and 7 show two embodiments of a cooling and liquefaction unit of a system according to the invention.
  • FIGS 8 and 9 show two embodiments of air pretreatment and cooling
  • Figure 10 shows an embodiment of the method according to the invention in
  • FIG. 2 the part of the air separation plant, which is arranged downstream of the main air compressor 9, only schematically shown as a box 10 (ASU). Inside this box hides an air pre-treatment unit, a cooling and liquefaction unit and a distillation column system.
  • atmospheric air In the main air compressor 9, which has multiple stages with intercooling, atmospheric air (AIR) is compressed to a total air pressure higher than 20 bar and in a concrete numerical example is 37.5 bar.
  • the high-pressure total air flow 1 1 (HP-AIR), which exits the main air compressor 9, is introduced into the air separation plant in the strict sense 10. From there will be one
  • All stages of the main air compressor are driven by a common shaft connected to the shaft of a gas turbine unit 1 comprising a gas turbine compressor 13, a gas turbine combustor 14, a gas turbine expander 15 and, optionally, a steam generator 16 (HRSG - Heat Recovery Steam Generation).
  • a gas turbine unit 1 comprising a gas turbine compressor 13, a gas turbine combustor 14, a gas turbine expander 15 and, optionally, a steam generator 16 (HRSG - Heat Recovery Steam Generation).
  • gas turbine compressor 13 ambient air (amb) is compressed; in the combustion chamber 14 natural gas (NG) is burned with the compressed air.
  • Combustion gas from combustion chamber 14 is deprived of heat in the steam generation; the cooled combustion gas is - possibly after cleaning - blown back into the environment (amb).
  • Figure 3 shows a first embodiment of a distillation column system as used in the invention.
  • the distillation column system has a
  • Head capacitors are designed as a condenser-evaporator.
  • the operating pressures of the columns (at the top of each head) are in the example
  • a "second partial flow” 206 (JT-AIR Joule-Thomson Air) of the high-pressure total air flow is taken from the cooling and liquefaction unit at a pressure of 3.5 bar, in a throttle valve 207
  • High-pressure column pressure is released and introduced via line 208 in a predominantly liquid state into a cup 209, which is arranged within the high-pressure column 202 at an intermediate point.
  • This cup 209 serves as a separator (phase separator).
  • the gaseous portion from line 208 rises within high pressure column 202; the liquid portion is at least partially removed again and introduced via line 210 and throttle valve 21 1 in the evaporation space of the Hochtikcicle Kopfkondensators 204, as well as another liquid air stream 221, which is formed by the small amount of liquid generated during the work expansion relaxation. Steam generated in the vaporization space of the high pressure column top condenser 204 is withdrawn via line 212 and fed to the lower portion of the low pressure column 203 as ascending vapor.
  • Gaseous head nitrogen 213 from the high-pressure column 202 is introduced at least to a first part 214 in the liquefaction space of the high-pressure column top condenser 204 and there at least partially, preferably completely or almost completely liquefied.
  • a "first liquid nitrogen stream" 215 is formed.
  • a first partial flow 216 of the first liquid nitrogen stream 215 is as reflux liquid to the
  • the oxygen-enriched bottom liquid 222 of the high-pressure column 202 is subcooled in the subcooling countercurrent 218 and introduced via throttling valve 223 and line 224 into the evaporation space of the low-pressure column top condenser 205.
  • Another cooling fluid for the low-pressure column headcapacitor 205 becomes formed by the bottom liquid 225 of the low-pressure column 203, which also in the subcooling countercurrent 218 supercooled, throttled (226) and in the
  • Evaporation space of the low-pressure column top condenser 205 introduced (227) is.
  • purge liquid 228 is fed from the high-pressure column top condenser 204 into the evaporation space of the low-pressure column top condenser 205.
  • a rinsing liquid is likewise withdrawn (purge) and discarded or compressed to the supercritical pressure and passed through the main heat exchanger.
  • Low-pressure column 203 at least partially, preferably completely or almost completely liquefied.
  • a second liquid nitrogen stream 232 is formed.
  • a first partial stream 233 of the second liquid nitrogen stream 232 is introduced onto the low-pressure column 203 as further reflux liquid.
  • a second partial stream 234 is supplied to an internal compression and thereby brought in a pump 235 in the liquid state to a product pressure which is between 20 and 100 bar and in the example is about 70 bar.
  • the supercritical nitrogen (ICLIN - Internally Compressed Liquid Nitrogen) is supplied via line 236 of the refrigeration and nitrogen
  • Head nitrogen from the high-pressure column 202 and the low-pressure column 203 are obtained directly as a gaseous pressure product (HPGAN - High Pressure Gaseous Nitrogen / MPGAN - Medium Pressure Gaseous Nitrogen), which is naturally still warmed in the cooling and liquefaction unit to about ambient temperature.
  • a third substream 239 of the second liquid nitrogen stream 232 may also be recovered as liquid nitrogen product (LIN - Liquid Nitrogen).
  • High pressure column 202 a separate separator (phase separator) can be used; the gaseous fraction is then introduced into the high-pressure column, the liquid at least partially into the evaporation space of the high-pressure column top condenser 204th
  • FIG. 4 While only a single internal compression pump 235 is used in FIG. 3, in FIG. 4 the two are used.
  • a first pump 335a brings the second partial stream 334 of the second liquid nitrogen stream 232 as shown in FIG.
  • FIG. 5 differs from FIG. 4 by a third condenser-type evaporator, the high-pressure column bottom evaporator 438.
  • the gaseous air 401 AIR
  • the resulting liquid 442 is additionally introduced into the cup 209.
  • FIGS. 6 and 7 show two embodiments of a cooling
  • Liquefaction unit 50 which may be combined with Figure 2 and each of the distillation column systems of Figures 3 to 6.
  • the total purified high pressure total air flow 81 1 (see FIGS. 8 and 9) under the total air pressure is supplied to the warm end of a main heat exchanger 51, here realized as a single plate heat exchanger block.
  • a first partial flow 56 of the high pressure total air flow 81 1 is removed at a first intermediate temperature from the main heat exchanger and a
  • working air released air 58 is introduced into a separator (phase separator) 59.
  • the largest part of the work-performing expanded first partial flow 58 is introduced in gaseous form via line 201 into the high-pressure column of the distillation column system; the separated liquid 221 is treated as described in FIG.
  • a second partial flow 52 of the high-pressure total air flow 81 1 is removed again at a second, higher intermediate temperature and in the
  • the recompressed second partial flow 55 is again introduced into the warm end of the main heat exchanger 51, where it is fed to the cold end and pseudo-liquefied there.
  • the supercritical second substream 206 is introduced into the distillation column system in the manner shown in Figs.
  • warmed nitrogen streams are delivered as products 61/62 (HPGAN / MPGAN).
  • the warmed residual gas stream is partially blown off via line 63 into the environment (amb) and partially as regeneration in the
  • Cleaning device 802 used for the feed air (see Figures 8 and 9).
  • high-pressure column 202 and low-pressure column 203 are arranged next to one another. If there is very little floor space available, however, it is also possible with the invention to arrange the columns one above the other like a classic Linde double column. In this case, starting from the bottom, the following pieces of equipment are placed in a line one above the other:
  • High-pressure column 202 (in the case of FIG. 5 with high-pressure column bottom evaporator 438 installed in the high-pressure column)
  • FIG. 7 differs from the line 765 of FIG. 6.
  • the second partial flow 752 of the high-pressure total air flow is not precooled in the main heat exchanger, but by admixing a small part 765 of the cold first partial flow 756 before entering the turbine 57
  • FIG. 8 shows, in addition to the cooling and liquefaction unit 50 from FIG. 6, a first embodiment of an air pretreatment unit 799.
  • the compressor stages 804, 806 and 807 and the coolers 805, 808 of the main air compressor 9 are not part of the air pre-treatment unit.
  • the compressed total air 800 is in a pre-cooler 801 at about
  • Total air pressure compressed high pressure total air flow 81 1 is introduced into the cooling and liquefaction unit 50.
  • the air pre-treatment unit 799 can be operated under the total air pressure (see FIG. 10). However, at the high air pressures used here, it is more convenient in most cases to operate the air pretreatment unit as shown in Figure 8 at a lower pressure by placing it between two stages 806 and 807 of the main air compressor. This will be the
  • All three stages 804, 806, 807 of the main air compressor 9 of the embodiment are driven by a single shaft, which is connected to the shaft of a
  • Gas turbine unit a gas engine or another engine is connected.
  • an intercooler 805 is connected, behind the third and last stage an aftercooler 808.
  • FIG. 9 differs from FIG. 8 in that a part 902 of the supercritical high-pressure air 901 is not conducted via line 206 to the distillation column system, but is relaxed in a throttle valve 903 to an intermediate pressure corresponding to the inlet pressure of the last stage 807 of the main air compressor 9 (plus line losses). It is completely warmed up in the main heat exchanger 51 and then fed to the entry of the last stage 807 of the main air compressor 9. As a result, the amount of high-pressure air used to vaporize internal compression nitrogen is increased. This leads to a reduction of the final pressure of the main air compressor and one can reduce the number of compressor stages (cost advantage).
  • FIG. 10 shows an embodiment of the method according to the invention in its entirety.
  • the main air compressor 9 has several stages with intercooling and is formed by a single machine. Its shaft is powered by an electric motor, a steam turbine, a gas turbine unit, a
  • the cooling and liquefaction unit 50 shown in Fig. 10 corresponds to that of Fig. 6, the distillation column system 1000 to that of Fig. 3.
  • the air pretreatment unit 799 and the main air compressor 9 of Fig. 10 may be used with any of the other cooling and liquefaction units described herein and with each other of the distillation column systems shown in this application are combined.
  • the embodiment of Figure 11 is based on Figure 10. It has a
  • Fluid turbine 1107 instead of the throttle valve 207 and is also equipped with a boost circuit.
  • Compressor (booster) 1 173 which is designed as a cold compressor, is compressed from about 3.9 bar to about 6.9 bar.
  • the compressed recycle stream 1 174 is introduced at an intermediate point in the main heat exchanger 51 and cooled there to the cold end.
  • the cooled circulation stream 1 175 is again fed to the high-pressure column 202 at the bottom and intensifies the separation process there. Therefore, the whole thing is called a gain cycle.
  • the work-performing expansion of the first partial flow 56 of the high-pressure total air flow 11 is carried out in two expansion turbines 57a, 57b connected in parallel.
  • the first turbine 57a drives the hot secondary compressor 53 for the first partial flow 752 as before, the second turbine 57b drives the cold compressor 1 173.
  • the two turbines 57a, 57b in the exemplary embodiment have the same inlet and outlet parameters with respect to pressure and temperature (FIG. at others
  • FIG. 12 differs from FIG. 11 in that the boost circuit 1272/1273/1274/1275 does not lead from the evaporation space of the high-pressure column top condenser into the high-pressure column but from the top of the low-pressure column 203 into the liquefaction space of the high-pressure column top condenser 204.
  • gaseous nitrogen product can also be withdrawn directly from the top of the high-pressure column 202 and / or the low-pressure column 203 and heated in the main heat exchanger 51 in the methods of FIGS. 11 and 12.
  • the intensifier circuits shown in FIGS. 11 and 12 can be used with any other of the cooling and liquefaction units described herein as well as with each other of the distillation column systems shown in this application are combined.

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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

L'invention concerne un procédé et un dispositif qui servent à produire de l'azote comprimé par décomposition à basse température de l'air dans un système de colonnes de distillation qui présente une colonne à haute pression (202) et une colonne à basse pression (203) et un condensateur de tête de colonne à haute pression (204) et un condensateur de tête de colonne à basse pression (205). Un compresseur d'air principal (9) constitue le seul compresseur de gaz entraîné par une énergie externe; dans celui-ci, l'air de charge est condensé à une pression d'air totale qui est au moins de 5 bars supérieure à la pression de service de la colonne à haute pression (202). Un premier courant partiel (56) du courant d'air total à haute pression (11, 811) du compresseur d'air principal (9) est détendu avec production de travail à la pression fonctionnelle de la colonne à haute pression ou à une pression supérieure (57) et conduit dans le système de colonnes de distillation (201). Un deuxième courant partiel (52, 55) du courant d'air total à haute pression (11, 811) est refroidi dans un échangeur de chaleur principal (51) et conduit au moins partiellement à l'état fluide dans le système de colonnes de distillation (206, 210). Un courant d'azote de compression interne est formé par un courant partiel (319) du courant d'azote liquide (215) du condensateur de tête de colonne à haute pression (204) et/ou un courant partiel (234, 334) du courant d'azote liquide (232) du condensateur de tête de colonne à basse pression (205); il est porté à l'état liquide à une pression de produit (235, 335a, 335b) qui se situe entre 15 et 100 bars; ensuite il est chauffé dans l'échangeur de chaleur principal (51) et ensuite retiré sous forme de courant de produit d'azote comprimé sous forme gazeuse (60) à la pression de produit.
EP14744775.9A 2013-08-02 2014-07-29 Procédé et dispositif de production d'azote comprimé Withdrawn EP3027988A2 (fr)

Priority Applications (1)

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EP14744775.9A EP3027988A2 (fr) 2013-08-02 2014-07-29 Procédé et dispositif de production d'azote comprimé

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EP13003861 2013-08-02
EP14744775.9A EP3027988A2 (fr) 2013-08-02 2014-07-29 Procédé et dispositif de production d'azote comprimé
PCT/EP2014/002074 WO2015014485A2 (fr) 2013-08-02 2014-07-29 Procédé et dispositif de production d'azote comprimé

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EP (1) EP3027988A2 (fr)
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Publication number Priority date Publication date Assignee Title
EP3059536A1 (fr) * 2015-02-19 2016-08-24 Linde Aktiengesellschaft Procédé et dispositif destinés à la production d'un produit d'azote pressurisé
US20200080773A1 (en) * 2018-09-07 2020-03-12 Zhengrong Xu Cryogenic air separation unit with flexible liquid product make
WO2022179748A1 (fr) * 2021-02-25 2022-09-01 Linde Gmbh Procédé et installation pour fournir de l'azote comprimé

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Publication number Priority date Publication date Assignee Title
US4817394A (en) * 1988-02-02 1989-04-04 Erickson Donald C Optimized intermediate height reflux for multipressure air distillation
US5144808A (en) * 1991-02-12 1992-09-08 Liquid Air Engineering Corporation Cryogenic air separation process and apparatus
DE19735154A1 (de) * 1996-10-30 1998-05-07 Linde Ag Verfahren und Vorrichtung zur Gewinnung von Druckstickstoff
GB9726954D0 (en) * 1997-12-19 1998-02-18 Wickham Michael Air separation
US5906113A (en) * 1998-04-08 1999-05-25 Praxair Technology, Inc. Serial column cryogenic rectification system for producing high purity nitrogen
CN1340687A (zh) * 2000-08-24 2002-03-20 孙克锟 空气分离方法及设备
US7228715B2 (en) * 2003-12-23 2007-06-12 L'air Liquide, Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude Cryogenic air separation process and apparatus
DE102007031759A1 (de) * 2007-07-07 2009-01-08 Linde Ag Verfahren und Vorrichtung zur Erzeugung von gasförmigem Druckprodukt durch Tieftemperaturzerlegung von Luft
FR2949846B1 (fr) * 2009-09-10 2012-02-10 Air Liquide Procede et installation de production d'oxygene par distillation d'air
DE102010056560A1 (de) * 2010-08-13 2012-02-16 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung von Drucksauerstoff und Druckstickstoff durch Tieftemperaturzerlegung von Luft
FR2973487B1 (fr) * 2011-03-31 2018-01-26 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede et appareil de production d'un gaz de l'air sous pression par distillation cryogenique

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MX2016001221A (es) 2016-05-24
WO2015014485A3 (fr) 2015-09-24
US20160161181A1 (en) 2016-06-09

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