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WO2021078405A1 - Procédé et système pour la séparation d'air à basse température - Google Patents

Procédé et système pour la séparation d'air à basse température Download PDF

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Publication number
WO2021078405A1
WO2021078405A1 PCT/EP2020/025456 EP2020025456W WO2021078405A1 WO 2021078405 A1 WO2021078405 A1 WO 2021078405A1 EP 2020025456 W EP2020025456 W EP 2020025456W WO 2021078405 A1 WO2021078405 A1 WO 2021078405A1
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WO
WIPO (PCT)
Prior art keywords
column
pressure column
pressure
evaporation
liquid
Prior art date
Application number
PCT/EP2020/025456
Other languages
German (de)
English (en)
Inventor
Stefan Lochner
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
Publication of WO2021078405A1 publication Critical patent/WO2021078405A1/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
    • F25J3/04151—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
    • F25J3/04006—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
    • F25J3/04078—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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04096—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 argon or argon enriched stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
    • F25J3/04212—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product and simultaneously condensing vapor from a column serving as reflux within the or another 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
    • F25J3/04236—Integration of different exchangers in a single core, so-called integrated cores
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—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
    • F25J3/04333—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
    • 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
    • F25J3/04472—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages
    • F25J3/04496—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist
    • 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
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04709—Producing crude argon in a crude argon column as an auxiliary column system in at least a dual pressure main column system
    • F25J3/04715—The auxiliary column system simultaneously produces oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
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    • F25J3/04721—Producing pure argon, e.g. recovered from a crude argon 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
    • 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
    • F25J3/04763—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
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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
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J2200/00—Processes or apparatus using separation by rectification
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    • F25J2200/00—Processes or apparatus using separation by rectification
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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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
    • F25J2200/94—Details relating to the withdrawal point
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/42—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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F25J2215/56—Ultra high purity oxygen, i.e. generally more than 99,9% O2
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/58—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being argon or crude argon
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop

Definitions

  • the invention relates to a method for the low-temperature decomposition of air and a corresponding system according to the preambles of the independent claims.
  • Air separation plants have rectification column systems which can conventionally be designed, for example, as two-column systems, in particular as classic Linde double-column systems, but also as three- or multi-column systems.
  • rectification columns for obtaining nitrogen and / or oxygen in liquid and / or gaseous state, i.e. the rectification columns for nitrogen-oxygen separation
  • rectification columns can be provided for obtaining further air components, in particular the noble gases krypton, xenon and / or argon.
  • the terms “rectification” and “distillation” as well as “column” and “column” or terms composed of these are often used synonymously.
  • the rectification columns of the rectification column systems mentioned are operated at different pressure levels.
  • Known double column systems have what is known as a high pressure column (also referred to as a pressure column, medium pressure column or lower column) and a so-called low pressure column (also referred to as an upper column).
  • the high pressure column is typically operated at a pressure level of 4 to 7 bar, in particular about 5.3 bar.
  • the low-pressure column is operated at a pressure level of typically 1 to 2 bar, in particular about 1.4 bar. In certain cases, higher pressure levels can also be used in both rectification columns.
  • the pressures specified below are absolute pressures at the top of the columns specified in each case.
  • high pressure column, intermediate pressure column and low pressure column are used for certain columns of an air separation plant as described herein.
  • these terms are not intended to restrict the functions of the respective correspondingly designated columns in accordance with a possibly narrow definition that is used in the specialist literature for the columns of a conventional air separation plant.
  • the meaning of the terms results from the following explanations.
  • the present invention comprises the low-temperature decomposition of air according to the so-called SPECTRA method, as is described, inter alia, in EP 2 789 958 A1 and the other patent literature cited therein.
  • SPECTRA processes enable a high nitrogen yield and were originally developed for the production of gaseous pressurized nitrogen.
  • a return to the (in the simplest case only) column is provided here by condensing top gas from this column, as is still customary in this respect.
  • fluid from the same column is used for cooling in the SPECTRA process.
  • additional columns can be provided to obtain additional air components such as pure or high-purity oxygen and argon.
  • additional columns which, however, usually have in common that overhead gas from one of the columns, as in a classic SPECTRA process, using fluid from the same column, which is evaporated and returned to the column Formation of a liquid reflux is condensed on the column.
  • the column operated in this way can, as is the case according to the invention, be the column with the highest operating pressure in the plant.
  • CN 108036584 A discloses a method for the production of high-purity nitrogen and oxygen as well as liquid oxygen by the low-temperature decomposition of air and a corresponding plant. Various factors are fully taken into account in order to achieve stable, efficient and energy-saving operation of the system.
  • the object of the present invention is to improve the SPECTRA methods mentioned and explained in greater detail below, in particular with regard to energy consumption.
  • the present invention proposes a method for the low-temperature decomposition of air and a corresponding system with the features of the respective independent claims. Refinements are the subject matter of the dependent claims and the following description.
  • Liquids and gases can be rich or poor in one or more components as used here, with “rich” for a content of at least 75%, 90%, 95%, 99%, 99.5%, 99.9% or 99.99% and “poor” can mean a content of no more than 25%, 10%, 5%, 1%, 0.1% or 0.01% on a mole, weight or volume basis.
  • the term “predominantly” can match 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 gas is "enriched” in the sense understood here, if this or this is at least 1, 1-fold, 1, 5-fold, 2-fold, 5-fold, 10-fold 100-fold or 1,000-fold times the content, and "depleted” if this or this is at most 0.9 times, 0.5 times, 0.1 times, 0.01 times or 0.001 times the content of a corresponding component, based on the starting liquid or contains the source gas. If, for example, “oxygen”, “nitrogen” or “argon” is used here, this also includes a liquid or a gas that is rich in oxygen or nitrogen, but does not have to consist exclusively of these.
  • pressure level and "temperature level” to characterize pressures and temperatures, which is intended to express that corresponding pressures and temperatures in a corresponding system do not have to be used in the form of exact pressure or temperature values to realize the inventive concept.
  • pressures and temperatures typically move in certain ranges, for example ⁇ 1%, 5% or 10% around a mean value.
  • Corresponding pressure levels and temperature levels can be in disjoint areas or in areas that overlap one another.
  • pressure levels include, for example, unavoidable or expected pressure losses.
  • the pressure levels specified here in bar are absolute pressures.
  • expansion machines are typically understood to mean known turboexpander. These expansion machines can in particular also be coupled to compressors. These compressors can in particular be turbo compressors. A corresponding combination of turbo expander and turbo compressor is typically also referred to as a "turbine booster". In a turbine booster, the turbo expander and the turbo compressor are mechanically coupled, with the coupling being able to take place at the same speed (for example via a common shaft) or at different speeds (for example via a suitable transmission gear). In general, the term “compressor" is used here.
  • a “cold compressor” here denotes a compressor to which a fluid flow is fed at a temperature level well below 0 ° C, in particular below -50, -75 or -100 ° C and down to -150 or -200 ° C. A the corresponding fluid flow is cooled to a corresponding temperature level in particular by means of the main heat exchanger (see below).
  • the “main air compressor” is characterized by the fact that it compresses all of the air that is fed to the air separation plant and separated there. In contrast, in one or more optionally provided further compressors, for example booster compressors, only a portion of this air that has already been previously compressed in the main air compressor is further compressed.
  • the “main heat exchanger” of an air separation plant represents the heat exchanger in which at least the major part of the air supplied to the air separation plant and broken down there is cooled. This takes place at least partially in countercurrent to the material flows that are discharged from the air separation plant. Substance flows or "products" "diverted” from an air separation plant in this way are, in the language used here, fluids which no longer participate in plant-internal circuits, but are permanently withdrawn from them.
  • a “heat exchanger” for use in the context of the present invention can be designed in a manner customary in the art. It is used for the indirect transfer of heat between at least two fluid flows, for example, which flow countercurrently to one another, for example a warm compressed air flow and one or more cold fluid flows or a cryogenic liquid air product and one or more warm or warmer, but possibly also cryogenic fluid flows.
  • a heat exchanger can be formed from a single or several parallel and / or serially connected heat exchanger sections, e.g. from one or more plate heat exchanger blocks. It is, for example, a plate heat exchanger (Plate Fin Heat Exchanger).
  • Such a heat exchanger has “passages” which are designed as separate fluid channels with heat exchange surfaces and which are connected to form “groups of passages” in parallel and separated by other passages.
  • a heat exchanger is characterized by the fact that heat is exchanged between two mobile media in it at one point in time, namely at least one fluid flow to be cooled and at least one fluid flow to be heated.
  • a "condenser evaporator” is a heat exchanger in which a first, condensing fluid flow is in indirect heat exchange with a second, evaporating fluid flow occurs.
  • Each condenser-evaporator has a liquefaction space and an evaporation space.
  • the liquefaction and evaporation space have liquefaction and evaporation passages.
  • the condensation (liquefaction) of the first fluid flow is carried out in the liquefaction space, and the evaporation of the second fluid flow in the vaporization space.
  • the evaporation and liquefaction spaces are formed by groups of passages which are in a heat exchange relationship with one another.
  • the axes of the two apparatus parts do not have to be exactly perpendicular, but can also be offset from one another, especially if one of the two apparatus parts, for example a column or a column part with a smaller diameter, is to have the same distance from the sheet metal jacket of a coldbox as another with a larger one Diameter.
  • the high pressure column, the low pressure column and the intermediate pressure column in the context of the present invention essentially serve to obtain oxygen and nitrogen-rich air products (top gas of the high pressure column is provided under a corresponding pressure as nitrogen pressure product and bottom liquid can be taken from the low pressure column as pure oxygen product), the Another column used in the present invention for the production of argon and is therefore referred to as an argon column.
  • an argon column Like an argon column in a classic air separation plant, this is fed with a side stream from the low-pressure column.
  • side stream is intended to denote a fluid stream that is taken neither from the sump area nor from the head area, i.e. areas below the lowest or above the uppermost separating device (for example a separating tray or a packing area), but between, ie between two corresponding ones Separation devices.
  • Air separation plants with double column systems and so-called crude and possibly so-called pure argon columns are typically used to extract argon.
  • An example is illustrated by Häring (see above) in Figure 2.3A and described from page 26 in the section "Rectification in the Low-pressure, Crude and Pure Argon Column” and from page 29 in the section "Cryogenic Production of Pure Argon".
  • a pure argon column can also be dispensed with in corresponding plants if the rectification columns in question are designed accordingly. Pure argon can then be withdrawn from the crude argon column or a comparable column typically somewhat further below than the fluid conventionally transferred into the pure argon column, with a separation area located above for separation remaining foreign components is used.
  • the argon column used in the context of the present invention can be operated essentially like a conventional crude argon column known from the prior art (or a correspondingly modified crude argon column). Corresponding argon columns can in particular be formed with a corresponding number of plates.
  • the present invention proposes a method for the low-temperature separation of air, in which an air separation plant is used which has a column system comprising a high pressure column, an intermediate pressure column, a low pressure column and an argon column.
  • the high pressure column used in the context of the present invention is that column which is basically operated like the column used in a conventional SPECTRA process.
  • the high, intermediate and low pressure columns which are used in the context of the present invention are also distinguished by their respective operating pressure levels. Specific values are explained below.
  • the high pressure column is operated at a pressure level which is significantly above the pressure level of a conventional high pressure column.
  • a nitrogen product can be removed from the high pressure column, which nitrogen product can be provided directly at a corresponding pressure level and does not require any subsequent compression in the cold or in the warm.
  • the provision of a corresponding pressurized nitrogen product is therefore significantly simpler in terms of apparatus and, if necessary, in terms of safety technology than in a classic air separation plant.
  • the present invention thus benefits from the advantages of a known SPECTRA method.
  • the present invention also enables the production of an oxygen-rich air product and an argon-rich air product, for which the mentioned further columns are used.
  • the high pressure column in the context of the present invention is operated at a first pressure level
  • the low pressure column at a third pressure level below the first and the second pressure level can also be combined in the manner of a conventional double column of an air separation plant.
  • a heat exchanger used to condense top gas from the intermediate pressure column can also be arranged in the bottom of the low pressure column.
  • the double column system used there consists of a high pressure column and a low pressure column, the high pressure column being arranged below the low pressure column in the sense explained above.
  • This can also be the case for the intermediate pressure column (arrangement below the low pressure column) and the low pressure column (arrangement above the intermediate pressure column) in the context of the present invention.
  • the present invention is limited to such an arrangement in the manner of a double column or double column. Rather, the two columns (intermediate pressure column and low pressure column) can also be designed in the form of two separate columns.
  • the condenser connecting the intermediate pressure column and the low pressure column in a heat-exchanging manner can also be arranged outside the low pressure column.
  • the intermediate pressure column is typically operated at a pressure level which corresponds to a conventional high pressure column of an air separation plant.
  • the operating pressure level of the low pressure column also corresponds to the usual operating pressure level of a classic low pressure column.
  • a condensate is formed from overhead gas of the high pressure column with evaporation or partial evaporation of a first liquid which is taken from the high pressure column and expanded to an evaporation pressure level between the first and the second pressure level .
  • the evaporation pressure level can typically be 3 to 7 bar.
  • the Relaxation thus takes place in the form of partial relaxation to a superatmospheric pressure level, which allows further relaxation to a lower pressure level.
  • the condensate formed is partially or completely fed back into the high pressure column as reflux. Part of a corresponding condensate can also be discharged from a corresponding system as a liquid, nitrogen-rich air product.
  • a first gas is formed which is partially or completely recompressed to the first pressure level and fed back into the high-pressure column. This is an essential feature of a SPECTRA process.
  • the first liquid withdrawn from the high pressure column which is treated accordingly in the context of the present invention, can in particular be a liquid which is withdrawn from the high pressure column a few theoretical or practical trays above the bottom, which In other words, it is carried out in the form of a side stream from the high pressure column.
  • the top condensate is formed from the top gas of the high pressure column with evaporation or partial evaporation of a second liquid which is taken from the intermediate pressure column and compressed to the evaporation pressure level between the first and the second pressure level.
  • a second gas is formed, which is partially or completely expanded to the second pressure level and fed back into the intermediate pressure column.
  • the present invention thus creates two material cycles, namely the material cycle to which the first liquid from the high pressure column is subjected and a second material cycle to which a liquid from the intermediate pressure column is subjected. While the first cycle still corresponds to a typical SPECTRA process, the second cycle, as used according to the invention, is new compared to the prior art.
  • a pump is typically provided which pressurizes the second liquid in the liquid state. While the first liquid from the high pressure column is typically a side stream from the high pressure column, the second liquid from the intermediate pressure column, on the other hand, is formed using bottom liquid.
  • the high pressure column is fed in particular with compressed and cooled feed air. This does not rule out that other columns are also fed with air accordingly; However, this is always provided in the case of the high pressure column used according to the invention.
  • bottom liquid from the high pressure column is expanded from the first to the second pressure level and fed into the intermediate pressure column. This is also typically not the case in conventional SPECTRA processes, even if further columns are used there; a corresponding stream of material, which is formed using bottom liquid, is also used in conventional processes of this kind as a coolant for the condensation of top gas of the corresponding column.
  • a side stream withdrawn from the high-pressure column in the liquid state is also partially or completely expanded from the first to the second pressure level and with the formation of a liquid component and a gas component fed to a phase separation.
  • the liquid fraction can in particular be partially or completely subjected to a separation in the low-pressure column and the gas fraction can be partially or completely subjected to a separation in the intermediate-pressure column.
  • a particular embodiment of such a process comprises feeding the side stream withdrawn from the high pressure column or its component, which has been expanded from the first to the second pressure level, for the phase separation into the intermediate pressure column, where the liquid component is deposited in liquid form, for example in a liquid retention container or on a separation tray, and the gas portion goes directly into the gas phase.
  • the liquid fraction can be partially or completely withdrawn from the intermediate pressure column and fed into the low pressure column, where it is subjected to the separation that takes place there.
  • the gas fraction is left in the intermediate pressure column and is subjected to separation there.
  • the argon column used is operated essentially in the manner of a conventional argon column of an air separation plant.
  • an argon-enriched side stream is withdrawn from the low-pressure column, at least part of the second stream being fed from the low-pressure column into the argon column.
  • the side stream enriched in argon has, in particular, a higher argon content than is present at the top or bottom of the low-pressure column. It is taken from the low-pressure column in an advantageous area known in principle from the area of air separation plants.
  • the argon column is operated using a top condenser.
  • a condensate is formed from the top gas of the argon column with partial evaporation of liquid, which is partially or completely fed back into the argon column.
  • the liquid, with the partial evaporation of which the condensate is formed from the top gas of the argon column, is advantageously removed from the intermediate pressure column within the scope of the present invention, which represents a further fundamental difference compared to known processes.
  • a gas formed in the partial evaporation and / or liquid remaining in the partial evaporation can be fed partially or completely into the low-pressure column.
  • expanders coupled with compressors can be used.
  • a compressor can be used that is mechanically coupled to an expansion machine that is used to depressurize a further portion of the second gas, the is not fed back into the intermediate pressure column is used.
  • the present invention also extends to an air separation plant, for the specific features of which reference is made to the corresponding independent patent claim.
  • an air separation plant is advantageously set up to carry out a method as has been explained above in different configurations.
  • FIG. 1 illustrates an air separation plant according to an embodiment of the present invention in the form of a simplified process flow diagram.
  • FIG. 1 an air separation plant according to a particularly preferred embodiment of the present invention is shown in the form of a greatly simplified, schematic process flow diagram and denoted as a whole by 100.
  • the air separation plant 100 illustrated in FIG. 1 is sucked in air from the atmosphere, here denoted generally by A, via a filter 101 by means of a main air compressor 102, which is in particular multi-stage and with intermediate cooling. After after-cooling in heat exchangers 103 and 104, a feed air stream a formed in this way is cooled in a direct contact cooler 105 operated with water W and then fed to an adsorption device 106.
  • the feed air stream a After the feed air stream a has been dried in this way and essentially freed from carbon dioxide, it is fed to a main heat exchanger 107.
  • the feed air stream a is taken from the main heat exchanger near its cold end and, in the example illustrated here, is essentially fed to the high pressure column 11 of a column system designated overall by 10. A part that is not shown separately can be branched off via a bypass if required.
  • a top stream b of the high pressure column 11 can be discharged from the air separation plant 100 in part in the form of a stream c as a gaseous pressurized nitrogen product.
  • Corresponding pressurized nitrogen products are again labeled C1 and C2.
  • a portion of the top stream b that is not diverted from the air separation plant is fed to a heat exchanger or condenser 108 in the form of a material stream d and is essentially condensed there.
  • a portion of the corresponding condensate can be returned to the high pressure column 11 as a liquid reflux in the form of a stream e. Another portion is withdrawn in the form of a flushing flow P.
  • liquid nitrogen E can also be fed into the system 100 in the manner illustrated here.
  • Another portion can be subcooled in the form of a material flow f in a subcooler 109 and as a liquid nitrogen product F from the system be diverted.
  • a portion that is used for subcooling and is branched off downstream of subcooler 109 is discharged from the system as residual gas, as also explained below with reference to further material flows.
  • an intermediate pressure column 12 of the column system 10 is fed by means of a bottom stream g of the high pressure column 11.
  • this bottom stream g is cooled in the main heat exchanger 107 and then fed into the intermediate pressure column above the bottom or above some separating trays which are above the bottom.
  • the intermediate pressure column is further fed by means of a side stream h from the high pressure column 11, which is depressurized into the intermediate pressure column 12. Gas formed in this way is left in the intermediate pressure column 12; on the other hand, liquid in the form of a stream i is at least partially withdrawn from the intermediate pressure column 12 directly below the feed point and first passed through a subcooler 110 and then fed into a low pressure column 13 of the column system 10.
  • the heat exchanger 108 is initially operated using a side stream k withdrawn from the high pressure column. This is first cooled further in the main heat exchanger 107 and then fed to the heat exchanger 108. Partial relaxation takes place. Downstream of the heat exchanger 108, part of the correspondingly evaporated fluid can be released into atmosphere A. Another part is recompressed, as further illustrated here in the form of a material flow k, possibly after combining with other material flows, in a compressor 111, which is mechanically coupled to an expansion machine 112 and additionally braked by means of a dissipative brake. The stream k can be fed into the high pressure column 11 again in this way. Further cooling capacity for the heat exchanger 108 is provided by a bottom stream I of the intermediate pressure column 12. For this purpose, this is brought to a pressure level required in the heat exchanger 108 by means of a pump 113.
  • the material flow I is heated in the form of a first partial flow m in the main heat exchanger 107 and at least partially expanded in the expansion machine 112. This material flow is then, in particular together with the portion of the overhead stream b used for cooling in the subcooler 109, discharged from the high pressure column from the plant. A further portion n of the bottom stream from the intermediate pressure column 12 evaporated in the heat exchanger 108, on the other hand, is returned to the intermediate pressure column 12.
  • the air separation plant 100 further comprises an argon column 14, which is ultimately fed from the low-pressure column 13 or by means of a side stream o withdrawn from the low-pressure column 13.
  • the side stream o is not transferred directly to the argon column 14, but instead is first transferred to an upper part 15a of an oxygen column designated as a whole by 15.
  • the stream o or the fluid transferred in this way to the upper part 15a is further enriched in argon and depleted in oxygen, so that a corresponding stream p can be transferred from the top of the upper part 15a to the argon column 14 .
  • Bottom liquid from the argon column 14 is returned to the upper part 15a of the oxygen column via a pump, which is not specifically designated here.
  • the oxygen column 15 with the upper part 15a and the lower part 15b is operated with a bottom evaporator 151.
  • This bottom evaporator 151, and a bottom evaporator 131 arranged in the bottom of the low-pressure column 13, are each used to condense top gas from the intermediate pressure column 12, which gas is withdrawn from it in the form of a stream q.
  • a condensed portion is, as not illustrated separately and individually here, essentially used as reflux to the intermediate pressure column 12 and to the low pressure column 13.
  • a stream r is withdrawn from the top of the low-pressure column 13 and blown off in the form of impure oxygen after heating to the atmosphere or used in another way.
  • Oxygen streams s and t are withdrawn from the bottom of the low-pressure column 13, with the oxygen stream s being internally compressed in a pump, which is not specifically designated, and can be used to provide a corresponding internal compression product S.
  • the oxygen flow t can be heated and discharged from the system or released into the atmosphere become.
  • a part can, as illustrated here in the form of a link X, be returned to the low-pressure column 13.
  • the argon column 14 the top of which is cooled by means of a top condenser 141, can be used to provide a liquid argon stream u, which can be provided as an internally compressed argon product U, for example after being temporarily stored in a tank system T. A part of this can also be stored permanently in a storage tank T1 and, for example, can be run out of the system in liquid form.
  • the top condenser 141 of the argon column 14 is cooled using a stream v which is withdrawn in liquid form from the intermediate pressure column 12 a few floors above the sump and fed into an evaporation chamber of the argon condenser 141. Fractions that have evaporated or that have not been evaporated here can be returned to the low-pressure column in the manner illustrated.
  • the upper part 15a and the lower part 15b of the oxygen column 15 are fluidically coupled to one another, as illustrated here in the form of corresponding fluid arrows. Fluid depleted in argon and enriched in oxygen is transferred from the upper part 15a to the lower part 15b, where it is further rectified. In this way, a pure oxygen stream w can be taken from the bottom of the oxygen column 15 or its lower part, which can also be carried out from the air separation plant 100 as a pure oxygen product W in internally compressed form via a corresponding tank system t2 or t3. Further material flows illustrated here and their specific treatment in the air separation plant 100 result directly from the drawing.

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

Abstract

L'invention concerne un procédé de séparation d'air à basse température, dans lequel un système de séparation d'air (100) est utilisé, lequel présente un système de colonnes (10) comprenant une colonne haute pression (11), qui est alimentée en air condensé et refroidi, une colonne à pression intermédiaire (12), une colonne basse pression (13) et une colonne d'argon (14). Un condensat est formé à partir de gaz de tête de la colonne haute pression (11), l'évaporation ou l'évaporation partielle d'un premier liquide prélevé dans la colonne haute pression (11) et détendu à un niveau de pression d'évaporation entre les premier et second niveaux de pression et ledit condensat est renvoyé en partie ou en totalité à la colonne haute pression (11). Lors de l'évaporation du premier liquide, un premier gaz est formé qui est recondensé en partie ou en totalité au premier niveau de pression et renvoyé dans la colonne haute pression (11). Le condensat est en outre formé à partir du gaz de tête de la colonne haute pression (11) selon la présente invention avec évaporation ou évaporation partielle d'un deuxième liquide qui est prélevé à partir de la colonne à pression intermédiaire (12) et condensé au niveau de pression d'évaporation entre les premier et second niveaux de pression, un second gaz étant formé lors de l'évaporation du second liquide, ledit second gaz étant détendu en partie ou en totalité au second niveau de pression et renvoyé dans la colonne à pression intermédiaire (11). L'invention concerne également un système de séparation d'air (100) correspondant.
PCT/EP2020/025456 2019-10-23 2020-10-14 Procédé et système pour la séparation d'air à basse température WO2021078405A1 (fr)

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EP19020595.5 2019-10-23

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP4317877A1 (fr) 2022-08-01 2024-02-07 Air Products and Chemicals, Inc. Procédé et dispositif pour la récupération d'au moins de l'azote et de l'argon
EP4357708A2 (fr) 2022-10-18 2024-04-24 Air Products and Chemicals, Inc. Procédé et dispositif pour la récupération améliorée d'argon

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DE19609490A1 (de) * 1995-03-10 1996-09-12 Linde Ag Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
DE19933558A1 (de) * 1999-07-16 2000-09-28 Linde Tech Gase Gmbh Dreisäulenverfahren und -vorrichtung zur Tieftemperaturzerlegung von Luft
EP2789958A1 (fr) 2013-04-10 2014-10-15 Linde Aktiengesellschaft Procédé de décomposition à basse température de l'air et installation de décomposition de l'air
CN108036584A (zh) 2017-12-28 2018-05-15 乔治洛德方法研究和开发液化空气有限公司 通过低温精馏从空气中生产高纯氮、氧气和液氧的方法及设备
EP3327393A1 (fr) * 2016-11-25 2018-05-30 Linde Aktiengesellschaft Procédé et dispositif de production d'un flux de produit d'oxygène ultrapur par cryogénie de séparation d'air
WO2020083528A1 (fr) * 2018-10-23 2020-04-30 Linde Aktiengesellschaft Procédé et installation de séparation d'air à basse température

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DE19609490A1 (de) * 1995-03-10 1996-09-12 Linde Ag Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
DE19933558A1 (de) * 1999-07-16 2000-09-28 Linde Tech Gase Gmbh Dreisäulenverfahren und -vorrichtung zur Tieftemperaturzerlegung von Luft
EP2789958A1 (fr) 2013-04-10 2014-10-15 Linde Aktiengesellschaft Procédé de décomposition à basse température de l'air et installation de décomposition de l'air
EP3327393A1 (fr) * 2016-11-25 2018-05-30 Linde Aktiengesellschaft Procédé et dispositif de production d'un flux de produit d'oxygène ultrapur par cryogénie de séparation d'air
CN108036584A (zh) 2017-12-28 2018-05-15 乔治洛德方法研究和开发液化空气有限公司 通过低温精馏从空气中生产高纯氮、氧气和液氧的方法及设备
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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP4317877A1 (fr) 2022-08-01 2024-02-07 Air Products and Chemicals, Inc. Procédé et dispositif pour la récupération d'au moins de l'azote et de l'argon
EP4357708A2 (fr) 2022-10-18 2024-04-24 Air Products and Chemicals, Inc. Procédé et dispositif pour la récupération améliorée d'argon

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