WO2016015850A1 - Obtention d'un produit pneumatique dans une installation de séparation de l'air équipée d'une unité d'accumulation de froid - Google Patents

Obtention d'un produit pneumatique dans une installation de séparation de l'air équipée d'une unité d'accumulation de froid Download PDF

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Publication number
WO2016015850A1
WO2016015850A1 PCT/EP2015/001519 EP2015001519W WO2016015850A1 WO 2016015850 A1 WO2016015850 A1 WO 2016015850A1 EP 2015001519 W EP2015001519 W EP 2015001519W WO 2016015850 A1 WO2016015850 A1 WO 2016015850A1
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WO
WIPO (PCT)
Prior art keywords
air
amount
liquid
storage unit
cold storage
Prior art date
Application number
PCT/EP2015/001519
Other languages
German (de)
English (en)
Inventor
Alexander Alekseev
Original Assignee
Linde Aktiengesellschaft
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 Aktiengesellschaft filed Critical Linde Aktiengesellschaft
Priority to US15/328,117 priority Critical patent/US20170211882A1/en
Priority to CN201580049839.7A priority patent/CN107076511A/zh
Priority to EP15741735.3A priority patent/EP3175191A1/fr
Publication of WO2016015850A1 publication Critical patent/WO2016015850A1/fr

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
    • F25J3/04224—Cores associated with a liquefaction or refrigeration cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04387—Details relating to the work expansion, e.g. process parameter etc. using liquid or hydraulic turbine expansion
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04472—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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/24—Processes or apparatus using other separation and/or other processing means using regenerators, cold accumulators or reversible heat exchangers
    • 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
    • F25J2210/06—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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/30—Compression of the feed 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
    • 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
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/42—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/02—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams using a pump in general or hydrostatic pressure increase
    • 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
    • F25J2235/42—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • 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
    • F25J2245/40—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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop
    • 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
    • F25J2270/08—Internal refrigeration by flash gas recovery loop
    • 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
    • F25J2280/00—Control of the process or apparatus
    • F25J2280/02—Control in general, load changes, different modes ("runs"), measurements

Definitions

  • the invention relates to a method for obtaining an air product in one
  • Air separation plant and a corresponding air separation plant according to the independent claims.
  • Air separation plants have distillation column systems, which can be designed, for example, as two-column systems, in particular as classic Linde double-column systems, but also as triple or square column systems.
  • distillation column systems which can be designed, for example, as two-column systems, in particular as classic Linde double-column systems, but also as triple or square column systems.
  • gaseous oxygen GOX
  • liquid nitrogen LIN
  • Nitrogen, GAN ie the distillation columns for nitrogen-oxygen separation
  • distillation columns can be provided for obtaining further air components, in particular the noble gases krypton, xenon and / or argon.
  • DE 31 39 567 A1 and EP 1 989 400 A1 disclose liquid air or liquid nitrogen for regulating the network and for providing
  • the liquid air or the liquid nitrogen is obtained at times of high electricity supply (hereinafter referred to as excess power periods) in an air separation plant with an integrated condenser or in a dedicated liquefaction plant and stored in a tank system with cryogenic tanks.
  • excess power periods high electricity supply
  • power short periods low power supply
  • the liquid air or the liquid nitrogen from taken from the tank system pressure-increased by a pump and heated to about ambient temperature or higher and thus converted into a gaseous or supercritical state.
  • a pressure flow obtained thereby is stored in an energy storage unit in one expansion turbine or more
  • Generators of the power plant unit converted into electrical energy and fed into an electrical grid.
  • the present invention is less concerned with the field of the mere storage of energy, but seeks to provide an air separation plant in which both
  • a "heat exchanger" serves for the indirect transfer of heat between
  • One Heat exchanger may be formed of a single or a plurality of parallel and / or serially connected heat exchanger sections, for example, from one or more plate heat exchanger blocks. For example, it is a
  • Plate heat exchanger (English: Plate Fin Heat Exchanger).
  • Heat exchanger for example, the "main heat exchanger" a
  • Air separation plant by which the majority of the fluids to be cooled or heated to be cooled or heated, has "passages” formed as separate fluid channels with heat exchange surfaces and parallel and separated by other passages to "passages groups"
  • a "cold storage unit” is used to store the thermal energy in the form of cold, ie heat energy withdrawn
  • Cold storage units for use in the context of the present invention may be constructively similar to the regenerators, as they are known in principle from the field of air separation plants.
  • Regenerators are for example available from F.G. Kerry, Industrial Gas Handbook, CRC Press, 2006, especially sections 2.7, “Kapitza Cycle”, and 4.4.3, "Recovery of Krypton and Xenon”.
  • Regenerators have a suitable for cold storage material, in the simplest case
  • regenerator For example, a riprap, which is traversed during the first period of a cold, especially cryogenic, fluid and thereby cools. During the second period, a corresponding regenerator flows through a warm fluid, which cools down due to the cold stored in the regenerator or transfers its heat to the regenerator.
  • Regenerators can also be used in air separation plants for purifying the air used, in particular carbon dioxide and hydrocarbons, which freeze out in the cooled regenerator or liquefy and are vaporized or sublimated during the heating of the regenerator.
  • Regenerators are typically run in alternating mode in air separation plants of a classical type, wherein in each case a first regenerator or a first group of regenerators is regenerated and a second regenerator or a second group of regenerators is available for cooling or cleaning the feed air.
  • cold storage units can be made similar to the regenerators, in terms of process, however, the differences between these processing units are large. These differences are discussed below: 1.
  • a regenerator has primarily a function of a heat exchanger, it is said to serve to transfer the heat from a warmer flow to a colder flow. In an air separation process, therefore, at least two regenerators are always needed: one passes the warmer power and the other the colder power.
  • Such a regenerator pair can procedurally basically by a single
  • a cold accumulator By contrast, the main function of a cold accumulator is to store the cold for a longer time, for example more than 30 minutes.
  • Cold storage can not be replaced by a heat exchanger.
  • the cold storage is used regularly as a single cold storage. If the cold storage is not in operation, the
  • Air separation plant continue to run trouble-free.
  • a regenerator basically has only two operating phases:
  • a cold gas portion is passed through the regenerator and warmed up here (the regenerator cooled), usually less than ten minutes.
  • regenerator is flowed through by the hot gas in the opposite direction, which is thereby cooled (the regenerator warmed), usually less than ten minutes.
  • a cold storage has at least three operating phases:
  • the cold storage is flowed through by a warm gas and warmed (the gas is cooled); It usually takes more than an hour - Thereafter, a rest phase may follow, which may take several hours and in which the cold storage is not flowed through.
  • thermodynamic parameters are different:
  • the average local temperature change in a regenerator is less than 10 K.
  • a cold storage is warmed in the interior on average by about 50 K, at least 30 K or cooled.
  • Cold storage can also include, for example, corrugated aluminum sheets or channeled concrete blocks (in air separation plants unusual, but possible) similar to heat storage.
  • heat storage are extensively described in the relevant literature.
  • storage media are, for example, as mentioned, stone and concrete, but also bricks, cheap produced ceramics or cast iron.
  • earth, gravel, sand and / or gravel are also used.
  • common wave can be coupled to other expansion turbines or energy converters such as oil brakes, generators or compressors is set up to relax a gaseous or at least partially liquid stream.
  • expansion turbines can be used in the present
  • Invention be designed as turboexpander. If a compressor is driven by one or more expansion turbines, but without externally, for example by means of an electric motor, supplied energy, the term “turbine-driven” compressor or alternatively “booster” is used. Arrangements of turbine-driven compressors and expansion turbines are also referred to as “booster turbines”.
  • An "air product” is any product that can be produced, at least by compressing and cooling air, and in particular, but not necessarily, by subsequent cryogenic rectification.
  • these may be liquid or gaseous oxygen (LOX, GOX), liquid or gaseous nitrogen (LIN, GAN), liquid or gaseous argon (LAR, GAR), liquid or gaseous xenon, liquid or gaseous krypton, liquid or gaseous neon , liquid or gaseous helium, etc., but also for example Liquid air (LAIR).
  • oxygen oxygen
  • nitrogen nitrogen
  • nitrogen also refer in each case to cryogenic liquids or gases which have the respectively-named air component in an amount which is above that atmospheric air. It does not have to be pure liquids or gases with high contents.
  • an "air product” is also understood to mean a corresponding fluid which is finally discharged from the air separation plant, that is no longer for relaxation, evaporation,
  • Liquefaction, compression, etc. is used in the air separation plant or subjected to a corresponding step.
  • an intermediate product is in particular a cryogenic liquid made from air, which is subjected to liquid pressure as part of an internal compaction process and then into a main heat exchanger
  • Air separation plant is heated. Air separation plants can, as mentioned above, with so-called
  • Internal compression can be operated.
  • a liquid supplied to pressure is heated and thereby transferred from the liquid to the gaseous supercritical state, depending on what pressure was applied to the liquid stream.
  • liquefaction is used for the transfer from the liquid to the supercritical or gaseous state.
  • the present invention is based on a method for producing an air product in an air separation plant in which feed air which is compressed in a total of a main air compressor and then to a part in a secondary compressor is recompressed, cooled and then completely or partially in a
  • Main air compressor be compressed feed air, but it may also be provided, only a portion of compressed in the main air compressor feed air in the
  • the method comprises three operating modes, wherein the first operating mode during the above-mentioned power surplus periods, the second operating mode during the periods of normal power consumption and the third operating mode is performed during the above-described power shortage periods.
  • the first operating mode during the above-mentioned power surplus periods
  • the second operating mode during the periods of normal power consumption
  • the third operating mode is performed during the above-described power shortage periods.
  • other modes of operation may be provided as well
  • the liquid intermediate may be, in particular, liquid nitrogen, liquid oxygen and / or liquid argon, ie fluids which can be used, for example, in an internal compression process to provide corresponding gaseous printed products.
  • Intermediate liquid product can also serve liquid air.
  • a corresponding amount can be withdrawn before the distillation system from the so-called throttling flow or removed from the distillation column system at one or more corresponding points of the low-pressure or high-pressure column.
  • a portion of the intermediate quantity is stored liquid in a storage amount in a liquid storage unit, another portion can be delivered as a product to customers, and another portion in a first amount of product in the main heat exchanger can be heated under pressure and provided as the air product to be produced. The heating in the main heat exchanger takes place under pressure thereby advantageously under liquefaction in the context of a
  • the liquid storage unit used advantageously comprises one or more storage tanks for the liquid intermediate (s). It should be emphasized that the method according to the invention is not limited to the production of a single intermediate product, the method may also include the production of several intermediates and their storage and / or provision as air products. The invention will be described below with reference to only one intermediate product or only one corresponding air product.
  • the liquid is stored and stored in the liquid storage unit, basically without changing the liquid level by adding or subtracting liquid intermediate. (By derogation from this principle, at most a part of the stored
  • Liquid can be withdrawn directly as a liquid product, if there is currently a need for this.)
  • the air separation plant runs in normal operation.
  • the cold storage is not flowed through.
  • the feed air is fed in a third Heileinspeisemengege in the distillation column system and in this, again under
  • the liquid storage unit stored in the first operation mode becomes one of the liquid storage unit
  • the total amount forms a third amount of product which is heated in the main heat exchanger under pressure and provided as the air product.
  • Liquid storage unit is removed and first in the column system is returned and there with the third intermediate quantity to one
  • the operating modes 1 and 3 thus differ in particular in that, in the first operating mode, a corresponding liquid intermediate product is stored in the liquid storage unit and this is removed again from the liquid storage unit in the third operating mode. While in the first operating mode, a corresponding liquid intermediate product is stored in the liquid storage unit and this is removed again from the liquid storage unit in the third operating mode. While in the first operating mode, a corresponding liquid intermediate product is stored in the liquid storage unit and this is removed again from the liquid storage unit in the third operating mode. While in the first operating mode, a corresponding liquid intermediate product is stored in the liquid storage unit and this is removed again from the liquid storage unit in the third operating mode. While in the first operating mode, a corresponding liquid intermediate product is stored in the liquid storage unit and this is removed again from the liquid storage unit in the third operating mode. While in the first operating mode, a corresponding liquid intermediate product is stored in the liquid storage unit and this is removed again from the liquid storage unit in the third operating mode. While in the first operating mode, a corresponding liquid intermediate product is stored in the liquid storage
  • Liquid storage unit is balanced. This allows the
  • the inventive method is thus characterized by the fact that the first Lufteinspeisemenge greater than the second Heileinspeisemenge and the second Heileinspeisemenge is greater than the third Heileinspeisemenge.
  • According to the invention is also in the first mode of operation of the feed air heat under both
  • the present invention thus provides, the
  • Cold storage unit cooled and cooled in the third mode of operation the cold storage unit by means of excess cold available.
  • the cold is therefore present in excess in the third operating mode, because the air separation plant as a whole advantageously the same or comparable amounts of air products are removed and thus the same or a comparable amount of refrigerant is present.
  • the Lufteinspeisemenge is lower in the third mode of operation.
  • An essential aspect of the invention is that the first and the third product quantities in the first and the third operating mode, although passed through the main heat exchanger, but not through the cold storage unit.
  • inventive method offers the particular advantage of a constant production quantity, but still a targeted adaptation to the current Stromg. Energy tariff allows.
  • the measures according to the invention therefore develop their advantages in particular if the first product quantity does not differ from the third product quantity.
  • the difference existing in the context of the present invention advantageously relates only to the quantities fed in: In the third operating mode, a significantly smaller quantity of air feed into the distillation column system is required and the refrigeration requirement is correspondingly lower. In the first operating mode, the Heileinspeisemenge corresponding larger, so that a correspondingly larger
  • Refrigeration demand is present.
  • the corresponding excess of cold in the third operating mode or the greater refrigeration demand in the first operating mode is compensated by the cold storage unit provided in addition to the main heat exchanger.
  • the extraction of the heat using the cold storage unit in the first mode of operation does not have to be done directly, ie the feed air does not necessarily need by itself Cold storage unit to be performed. Rather, it is also possible to pass other streams through the cold storage unit, transfer their heat to the cold storage unit, and then pass them through the main heat exchanger. Is in the context of this application of a "crowd" the speech, be under
  • the present invention allows the first amount of air feed to be at least 20% greater than the third amount of air feed and the first
  • the first and third product quantities are preferably the same or different by less than 5%.
  • Air product which is composed of the third intermediate amount and the withdrawal amount can transfer.
  • Internal compression method required throttling flow ie a compressed air flow, which is provided at high pressure and performed under at least partial liquefaction by the main heat exchanger to transfer heat to the liquefaction to a correspondingly pressurized liquid stream can be significantly reduced in this way.
  • Liquid storage unit cold is available. In this way, a reduction of a turbine flow, possibly to a minimum value or zero, allows, as also explained in detail in the description of the figures.
  • the present invention in the third mode of operation performed during the low power periods, allows for the turbine flow to be provided
  • a corresponding booster or corresponding stages of such a booster can be operated at minimum speed, which reduces the power consumption.
  • the inductor current can, as also explained in the figures, be reduced accordingly.
  • the amount of throttle flow and the amount of turbine flow after decompression are fed into the distillation column system as part of the air feed rate, but it may also be contemplated to exhaust portions thereof, for example into the atmosphere, for regeneration purposes, etc.
  • the invention can also be used in a process in which part of the feed air that is not compressed in the after-compressor is expanded via an expansion turbine into a low-pressure column of the distillation column system.
  • Methods may include, for example, feed corresponding feed air by means of a so-called injection turbine in the low-pressure column.
  • the cold storage unit used in the context of the present invention comprises at least one cold storage, which is designed as explained above.
  • the context of the invention can also be provided to use a plurality of cold storage, one of which is the actual
  • Main heat exchanger is used, so to compensate for excess or reduced heat or cold amounts and / or to influence the
  • the cooling of the cold storage unit in particular a cold storage unit with at least one cold storage, can in the third operating mode
  • cryogenic gas product in particular so-called impure nitrogen
  • a cryogenic gas product that is not provided in the form of the first or third product, but an additional product.
  • Another portion of the cryogenic gas product can be passed through the main heat exchanger and there cool countercurrently further streams or portions of the feed air. The cryogenic gas product becomes
  • cryogenic gas product which is guided in the third operating mode to a proportion in a low-temperature state for cooling the cold storage unit through the latter, in the first operating mode completely in the
  • Main heat exchanger to be heated, wherein a portion of the heated gas product for heating the cold storage unit is passed through them.
  • This variant of the The process according to the invention can be carried out in particular by forming a
  • Recycled stream are diverted at the warm end of the main heat exchanger of a corresponding heated gas product, through the
  • a corresponding pump or a compressor with an aftercooler can be used.
  • the illustrated variant of the invention can be used.
  • Method has the advantage that both for cooling and for heating the cold storage unit, a medium can be used that on a
  • the feed air in the first operating mode of the feed air to lead a portion for cooling by the cold storage unit and a portion for cooling through at least a portion of the main heat exchanger.
  • Corresponding air is compressed at least to a pressure of a high pressure column of a corresponding distillation column system, which is for example 6 bar.
  • Cold storage unit and the one or more built-in cold storage must therefore be designed for appropriate pressures.
  • Feed air can be diverted, returned through the cold storage unit and passed to the warm end of the main heat exchanger, where it is reunited with the feed air. In this way, a proportion of the cooled feed air is always used for cooling the cold storage unit. Also in this case, a corresponding fan can be used.
  • the method according to the invention makes it possible in the first and in the third Operating mode correspondingly higher compressed air to pass through the cold storage, which in this case only for operation at one, but higher pressure, for example, 6 bar, must be designed.
  • it can also be provided to guide the entire feed air in the third operating mode through at least one section of the main heat exchanger and to cool the cold store with another fluid, as already mentioned.
  • An air separation plant according to the invention for producing an air product is adapted to compress feed air in total in a main air compressor and then recompress to a part in a booster and to cool the feed air and then feed wholly or partly into a distillation column system, means are provided which are set up for it in a first operating mode to feed the feed air in a first Beereinspeisemengege in the distillation column system and in this using the
  • the air separation plant is set up for the first
  • a corresponding air separation plant advantageously comprises means set up for carrying out a method in any of the embodiments of the invention explained above and below.
  • FIG. 1 shows a non-inventive air separation plant in the form of a process flow diagram.
  • FIGS. 2A to 2C show an air separation plant in the form of
  • FIGS. 3A to 3C show an air separation plant according to an embodiment of the invention in the form of process flow diagrams.
  • FIGS. 4A to 4C show an air separation plant according to an embodiment of the invention in the form of process flow diagrams.
  • FIGS. 5A to 5C show an air separation plant according to an embodiment of the invention in the form of process flow diagrams.
  • FIGS. 6A to 6C show an air separation plant according to an embodiment of the invention in the form of process flow diagrams.
  • corresponding elements are given identical reference numerals and will not be explained repeatedly for the sake of clarity. Detailed description of the drawings
  • FIG. 1 shows an air separation plant in the form of a simplified, schematic process flow diagram.
  • the air separation plant includes a
  • feed air in the form of a flow a via a simplified main air compressor 1 1 (English: Main Air
  • Compressor MAC
  • MAC Compressor
  • a partial flow b (FEED) of the compressed, cooled and purified stream a is supplied to a main heat exchanger 14 on the hot side and cold side thereof
  • booster compressor 15 boost air compressor, BAC
  • a partial flow d (JT-AIR, so-called throttle flow) of the partial flow c is recompressed in the after-compressor to a Nachverêtrenddruck warm supplied to the main heat exchanger 14 and this cold side removed.
  • a further partial flow e (TURB, so-called turbine flow) of the partial flow c is, however, the densifier 15 at a Nachverêtr composed horr further compressed in a turbine-driven compressor 6 (booster), warm side fed to the main heat exchanger 14, this taken at an intermediate temperature and in one with the turbine-driven Compressor 16 coupled expansion turbine relaxes.
  • the turbine stream e is in the example with the
  • Partial stream b to a collective flow f (here also referred to as FEED) united.
  • the invention may be used in an air separation plant of the specific embodiment illustrated herein, but it is also suitable
  • Reactor current d correlates, in simplified terms, with the amount of
  • the collecting stream f (FEED) is fed into the lower region of a high-pressure column 21, which is formed as part of a double column and with a low-pressure column 22 via a main condenser 23 in FIG
  • a liquid, oxygen-enriched bottom product is obtained, which withdrawn from the bottom of the high-pressure column 21 as stream g, passed through a supercooling countercurrent 25 and at an appropriate height in the
  • Low pressure column 22 is fed.
  • a gaseous, nitrogen-rich overhead product is obtained which can be withdrawn from the top of the high-pressure column 21 and fed to the plant limit as a gaseous nitrogen pressure product (PGAN).
  • GPN gaseous nitrogen pressure product
  • High-pressure column 21 withdrawn gaseous, nitrogen-rich overhead product is liquefied in the main condenser 23, fed back to the high pressure column 21 in a proportion, passed to the plant boundary as a liquid nitrogen pressure product (PLIN) or stored in liquid form, to a proportion as a stream h passed through the subcooling countercurrent 25 and fed as reflux to the low pressure column 22, and a proportion as a current i by means of a Pump 26 liquid pressure increased (this is the mentioned internal compression).
  • PLIN liquid nitrogen pressure product
  • the current i (ICLIN) is divided into two partial streams in the
  • Main heat exchanger 14 is liquefied and in the form of two gaseous
  • ICGAN1, ICGAN2, here referred to as internal compression products Pressure nitrogen products (ICGAN1, ICGAN2, here referred to as internal compression products) at different pressure levels led to the plant boundary.
  • the division into two partial streams before the liquefaction in the main heat exchanger 14 is not mandatory, it can also only a corresponding
  • a liquid, oxygen-rich bottom product is obtained as an intermediate, which is withdrawn from the bottom of the low-pressure column 22, which also represents the evaporation space of the main condenser 23, as a current m1.
  • a first part thereof is liquid-pressure-increased in the form of a stream m2 by means of a pump 28 (again internal compression).
  • the stream m2 (ICLOX) is in the example shown after division into two streams in the main heat exchanger 14 and liquefied in the form of gaseous pressure oxygen products (HP-GOX, MP-GOX, in turn, internal compaction products) at different pressure levels to the plant boundary. Again, the split is in two
  • Partial streams prior to the desuperheating in the main heat exchanger 14 is not required, it can also be formed only a réelleverdichtungswhichever is not required, it can also be formed only a réelleverdichtungswhichever is not required, it can also be formed only a réelleverdichtungswhichever is not required, it can also be formed only a réelleverdichtungswhichever is not required, it can also be formed only a réelleverdichtungswhichever is not required, it can also be formed only a réelleverdichtungswhichever.
  • a second part of the bottom product m1 is connected via line m3 in a
  • Liquid oxygen tank 27 initiated. It can be wholly or partially liquid
  • Oxygen product (LOX) are led to the plant boundary. The rest is stored in liquid form. If necessary, a portion of the tank contents via pump 121 and line 120 are fed back into the bottom of the low-pressure column 22. In the low-pressure column 22, a gaseous, nitrogen-rich top product is further obtained, which is subtracted in the form of the current n (GAN) from the head of the high-pressure column 22, passed through the subcooling countercurrent 25, in the
  • Main heat exchanger 14 can be heated and fed to the plant boundary. From the head of the low pressure column 22 and from there arranged
  • Liquid retention device may be a liquid, nitrogen-rich stream o
  • An impure nitrogen product (UN2) can be taken as stream p from the
  • REST residual gas
  • a portion 130 of the liquid air in line k is introduced into a liquid-air tank 44.
  • liquid air 134 from the low pressure column 22 may be directed into the liquid air tank 44.
  • the liquid air can be introduced via a pump 131 and line 133 into the low-pressure column 22.
  • the nitrogen-rich liquid of the current i (ICLIN) from the high pressure column 21 or more precisely from the liquefaction space of the main condenser 23 is internally compressed and in the main heat exchanger 14 to the
  • ICGAN1 and ICGAN2 evaporate (degasified).
  • Low-pressure column 22 is internally compressed and vaporized in the main heat exchanger 14 to the internal compression products HP-GOX and MP-GOX. 3.
  • an air separation plant can also produce other liquid intermediates from air, which (in the same way,
  • FIGS. 2A to 2C show an air separation plant in the form of simplified process flow diagrams which show three operating modes.
  • the air separation plant shown in each case comprises the previously explained
  • Rectification unit 20 Both are shown greatly simplified.
  • FIGS. 2A to 2C only show a selection of the currents a to p shown in FIG. 1, namely the partial flow b (FEED), the throttle flow d (JT-AIR), the turbine flow e (TURB, not here with the partial flow b combined to the collection stream f), the internally compressed stream m (ICLOX, here in the
  • Main heat exchanger 14 only to a single internal compaction product, HP-GOX, vaporized) and the current p (UN2, REST).
  • the air separation plant shown in FIGS. 2A to 2C further comprises a cold storage unit 30 with one or more cold storage 31 and a cold storage unit 30
  • Liquid storage unit 40 with one or more storage tanks 41 to 44, for example, a liquid oxygen tank 41, a liquid nitrogen tank 42, a liquid argon tank 43 and / or a liquid air tank 44. Not all of
  • Storage tanks 41 to 44 must be present.
  • Second mode - cold storage is not charged or discharged
  • the operating mode shown in Figure 2A corresponds to the normal operation of a conventional, not according to the invention air separation plant. Regardless of the actual storage operation, the liquid storage unit can be removed in the third (as in any other) operating mode liquid as an end product, if there is a need for it.
  • an air separation plant is designed to handle around 40,000
  • the amount of turbine flow e (TURB), denoted by E in FIG. 2A, can be assumed to be approximately 65,000 standard cubic meters per hour, for example.
  • the air quantity to be fed into the after-compressor 15 (after-compressor amount) of the partial flow c (from which the turbine flow d and the throttle flow e are formed, see FIG. 1) therefore corresponds to D + E in this case, ie amounts to approximately 140,000 Standard cubic meters per hour.
  • the amount B of the stream b depends directly on the amount of air products to be produced and is for example about 60 000 standard cubic meters per hour.
  • the cold storage 31 of the cold storage unit 30 must be in a heated state and in one or more storage tanks 41 to 44 of the
  • Liquid storage unit 40 a liquid intermediate must be stored.
  • the required heating of the cold accumulator 31 of the cold storage unit 30 and the likewise required storage of the liquid intermediate in one or more storage tanks 41 to 44 of the liquid storage unit 40 takes place in the (first) operating mode explained below with reference to FIG.
  • the air separation plant can also be operated using any other liquid intermediates.
  • the air separation plant is operated and supplies corresponding consumers, in addition to the
  • Liquid oxygen tank 41 taken from liquid oxygen in the form of a stream q in a withdrawal amount Q. However, no liquid intermediates are stored anymore.
  • the air separation plant or the rectification unit 20 itself can Amount of liquid oxygen can be reduced as an intermediate to the removal amount Q from the liquid oxygen tank 41. If the withdrawal quantity Q is, for example, 10,000 standard cubic meters per hour, the air separation plant or rectification unit 20 must therefore be during the one shown in FIG. 2B
  • the air of the flow a (AIR) to be compressed by the main air compressor 11 is also reduced by approximately 25%, ie. of about 200 000
  • Standard cubic meters per hour (see explanation for Figure 2A) to about 150 000 standard cubic meters per hour. This reduces the power consumption for the
  • the air to be compressed by the after-compressor 15 of the partial flow c is reduced by approximately 8%, ie by approximately 140,000 standard cubic meters per hour (see FIG Explanatory notes to Figure 2A) to about 128 500 standard cubic meters per hour. This also reduces the power consumption for the booster 15 by about 8%.
  • Cold storage 31 of the cold storage unit 30 are in a cooled state and in one or more storage tanks 41 to 44 of the liquid storage unit 40 must have capacity for storing a corresponding intermediate liquid product.
  • the cooling of the cold storage 31 of the cold storage unit 30 and the removal of a liquid intermediate from one or more storage tanks 41 to 44 of the liquid storage unit 40 has been explained to the third operation mode shown in FIG. 2B in low-power periods.
  • the air separation plant also here continues to provide the same amount M of internal compaction products as in the operating mode according to FIGS. 2A and 2B, for example the approx. 40,000 standard cubic meters per hour mentioned in the above example, but at the same time a storage amount S of, for example, approx. 10 000 standard cubic meters per hour of a generated intermediate product in the form of the current s in the liquid oxygen tank 41 is to be stored, the amount of the intermediate product formed in the air separation plant must be increased accordingly to about 50 000 standard cubic meters per hour. The amount of air fed into the rectification unit or distillation column system increases.
  • the air of the flow a (AIR) to be compressed in this case by the main air compressor 1 increases accordingly, in the example from approximately 200,000 standard cubic meters per hour (see explanations to FIG. 2A) to approximately 250,000 standard cubic meters per hour and thus by about 25%. The same applies to the power consumption.
  • AIR air of the flow a
  • FIGS. 2B and 2C Power consumption achieved.
  • a liquid intermediate product is stored which is used in the third operating mode according to FIG. 2B.
  • the operating modes shown in FIGS. 2B and 2C can be realized without providing complicated additional machines, merely by using simple cold storage.
  • Main compressor or the compressor to be compressed air quantities and the amount of turbine flow, which are each expressed in standard cubic meters per hour. The resulting differences between the respective minimum and maximum
  • the cold storage unit 30 used here or the cold storage unit (s) used in the cold storage unit 30 must be operable under the pressure of the throttle flow d.
  • designed for corresponding pressures high pressure vessel must be provided, which may prove to be expensive.
  • FIGS. 3A to 3C show an air separation plant according to an embodiment of the invention in the form of simplified process flow diagrams, again showing the three operating modes.
  • FIG. 3A illustrates normal operation without storage or removal of liquid storage products
  • FIG. 3B a third operation mode performed during power short periods and taking a liquid intermediate from liquid storage unit 40 and liquid tank 41, respectively
  • FIG first mode of operation which is performed during excess flow periods and with storage of a liquid intermediate in the liquid storage unit 40 and the liquid tank 41, respectively.
  • the cold storage unit 30 is illustrated here with two cold storage 33 and 34, which are each charged with partial flows.
  • the cold storage 34 is flowed through with streams which are passed before and then through the main heat exchanger 14.
  • the provision of the cold accumulator 34 serves to balance the
  • the two cold accumulators 33 and 34 are formed according to the one shown in FIG. 3B
  • Operation mode according to Figure 3B additionally available evaporation capacity of the main heat exchanger 14 are used for this purpose.
  • the amount D of the throttle current d (JT-AIR) can be reduced accordingly, for example by about 15,000 Standard cubic meter per hour, when through the cold storage 33 about 12 000 standard cubic meters per hour and through the cold storage 34 about 10 000
  • Liquid tank 41 of the liquid storage unit 40 taken and not in the
  • Rectification unit 20 itself is generated, reduces the amount of the compressed air to be compressed by the main air compressor 2 in the form of the flow a as explained to Figure 2B.
  • the same amount M of internally-compressed liquid intermediate is again provided and vaporized in the main heat exchanger 14 to the corresponding air product.
  • a storage amount S of a liquid intermediate product in the form of the flow s in the liquid tank 41 provided by the rectification unit 20 becomes
  • Liquid storage unit 40 is stored. This means that in the first
  • Evaporation capacity of the main heat exchanger 14 increases accordingly. This required increased evaporation capacity is covered by the provision of a correspondingly increased amount D of the throttle current d (JT-AIR). This also increases the required power of the booster 15 in
  • Figure 3C shown the first mode of operation of the current b with a correspondingly high pressure, namely at the pressure level of the high-pressure column, for example, 6 bar, passed through the cold storage 33 and 34.
  • a correspondingly high pressure namely at the pressure level of the high-pressure column, for example, 6 bar
  • the cold storage 33 and 34 must be designed for the correspondingly higher pressure level, so they are cold storage, which must be set up for both low-level operation and high-level operation.
  • FIGS. 4A to 4C an air separation plant according to an embodiment of the invention is shown in the form of simplified process flow diagrams which again show the three modes of operation mentioned.
  • FIG. 4A illustrates a normal operation without storage or removal of liquid intermediates
  • FIG. 4B a third mode of operation performed during power short periods and taking a liquid intermediate from the liquid storage unit 40 and the liquid tank 41, respectively
  • FIG. 4C first mode of operation, which is performed during excess flow periods and with storage of a liquid intermediate in the liquid storage unit 40 and the liquid tank 41, respectively.
  • the third operating mode shown in FIG. 4B corresponds to that in FIG. 3B
  • a current p (UN2, impure nitrogen) is partially passed through the main heat exchanger 14 and partially through the cold storage 33 and 34 of the cold storage unit 30.
  • the current p (UN2, impure nitrogen) is also used for heating the cold stores 33 and 34 of the cold storage unit 30.
  • the current p is in part compressed by means of a fan unit 35 warm side of the main heat exchanger 14 and passed through the cold storage 33 and 34 of the cold storage unit 30.
  • Correspondingly cooled streams are combined on the cold side of the main heat exchanger 14 with the flow p, so that in total an increased evaporation performance in the
  • Main heat exchanger 14 is required. This is again covered by an increase in the amount D of the throttle current d (JT-AIR).
  • FIGS. 5A to 5C show an air separation plant according to an embodiment of the invention in the form of simplified process flow diagrams which again show the three operating modes in the same arrangement.
  • the amount of recycled through the cold storage 33 and 34 air of the current b is for example about 25 000 standard cubic meters per hour.
  • the production amount of the rectification unit 20 is again due to the removal of the removal amount Q of Stream q of the intermediate liquid reduced, so that a correspondingly smaller amount D of the current d is required.
  • the amount M of the internally compressed intermediate (ICOLX) to be evaporated in the form of the current m remains the same, the required evaporation capacity is replaced by the additional
  • the additional amount of cold to supply the hereby larger quantity B of the flow b from the cold storage 33 and 34 of the cold storage unit 30 is covered.
  • FIGS. 6A to 6C show an air separation plant according to an embodiment of the invention in the form of simplified process flow diagrams which again show the three operating modes in the same arrangement. It differs from the preceding exemplary embodiments essentially in that in the first operating mode (FIG. 6C) gaseous pressure oxygen HP-GOX is cooled in the cold storage 33 and in the third operating mode (FIG. 6B) ICLOX is vaporized and heated in the cold storage 31.

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

Abstract

L'invention concerne un procédé servant à produire un produit pneumatique dans une installation de séparation de l'air. Ledit procédé consiste à refroidir au moins dans un compresseur d'air principal (2) de l'air de charge et à l'injecter dans un système de colonnes de distillation (21, 22). Une unité d'accumulation de liquide (40) et un accumulateur de froid (31 - 33) sont utilisés. Dans un premier mode de fonctionnement, le liquide est injecté dans l'unité d'accumulation de liquide (40), et l'accumulateur de froid est réchauffé. Dans un troisième mode de fonctionnement, le liquide est évacué, et l'accumulateur de froid est refroidi. Dans un deuxième mode de fonctionnement, le liquide n'est ni injecté ni évacué.
PCT/EP2015/001519 2014-07-31 2015-07-23 Obtention d'un produit pneumatique dans une installation de séparation de l'air équipée d'une unité d'accumulation de froid WO2016015850A1 (fr)

Priority Applications (3)

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US15/328,117 US20170211882A1 (en) 2014-07-31 2015-07-23 Production of an air product in an air separation plant with cold storage unit
CN201580049839.7A CN107076511A (zh) 2014-07-31 2015-07-23 在具有冷存储单元的空气分离设备中生产空气产物
EP15741735.3A EP3175191A1 (fr) 2014-07-31 2015-07-23 Obtention d'un produit pneumatique dans une installation de séparation de l'air équipée d'une unité d'accumulation de froid

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EP14002684.0 2014-07-31
EP14002684 2014-07-31

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EP3293475A1 (fr) * 2016-09-07 2018-03-14 Linde Aktiengesellschaft Procédé et appareil de stockage et de récupération d'énergie
EP3312533A1 (fr) 2016-10-18 2018-04-25 Linde Aktiengesellschaft Procédé de séparation de l'air et installation de séparation de l'air
DE102016014945A1 (de) 2016-12-14 2018-06-14 Linde Aktiengesellschaft Sauerstoffversorgungsverfahren und Sauerstoffversorgungssystem für Stahlwerk
DE102016015292A1 (de) 2016-12-22 2018-06-28 Linde Aktiengesellschaft Verfahren zur Bereitstellung eines oder mehrerer Luftprodukte mit einer Luftzerlegungsanlage
KR20190041511A (ko) * 2016-08-30 2019-04-22 8 리버스 캐피탈, 엘엘씨 고압의 산소를 생성하기 위한 극저온 공기 분리 방법

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FR3084736B1 (fr) * 2018-08-01 2022-04-15 Air Liquide Procede et appareil de production d'argon par distillation cryogenique de l'air
CN114383384B (zh) * 2021-12-30 2022-09-16 北京科技大学 一种空气液化与深冷空分工艺集成方法

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KR20190041511A (ko) * 2016-08-30 2019-04-22 8 리버스 캐피탈, 엘엘씨 고압의 산소를 생성하기 위한 극저온 공기 분리 방법
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EP3293475A1 (fr) * 2016-09-07 2018-03-14 Linde Aktiengesellschaft Procédé et appareil de stockage et de récupération d'énergie
EP3312533A1 (fr) 2016-10-18 2018-04-25 Linde Aktiengesellschaft Procédé de séparation de l'air et installation de séparation de l'air
DE102016014945A1 (de) 2016-12-14 2018-06-14 Linde Aktiengesellschaft Sauerstoffversorgungsverfahren und Sauerstoffversorgungssystem für Stahlwerk
DE102016015292A1 (de) 2016-12-22 2018-06-28 Linde Aktiengesellschaft Verfahren zur Bereitstellung eines oder mehrerer Luftprodukte mit einer Luftzerlegungsanlage

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