EP3394536A1 - Procédé et dispositif de production d'azote pur et d'oxygène pur par séparation cryogénique d'air - Google Patents

Procédé et dispositif de production d'azote pur et d'oxygène pur par séparation cryogénique d'air

Info

Publication number
EP3394536A1
EP3394536A1 EP16826004.0A EP16826004A EP3394536A1 EP 3394536 A1 EP3394536 A1 EP 3394536A1 EP 16826004 A EP16826004 A EP 16826004A EP 3394536 A1 EP3394536 A1 EP 3394536A1
Authority
EP
European Patent Office
Prior art keywords
pressure
pressure column
low
column
argon
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP16826004.0A
Other languages
German (de)
English (en)
Inventor
Christoph Windmeier
Stefan Dowy
Andreas Obermeier
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Publication of EP3394536A1 publication Critical patent/EP3394536A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—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
    • F25J3/04163—Hot end purification of the feed air
    • F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
    • F25J3/04175—Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/042—Division of the main heat exchange line in consecutive sections having different functions having an intermediate feed connection
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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.
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04381—Details relating to the work expansion, e.g. process parameter etc. using work extraction by mechanical coupling of compression and expansion so-called companders
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04387—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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04418—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 with thermally overlapping high and low pressure columns
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04424—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system without thermally coupled high and low pressure columns, i.e. a so-called split columns
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04624—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 integrated mass and heat exchange, so-called non-adiabatic rectification, e.g. dephlegmator, reflux exchanger
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    • 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
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
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    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
    • F25J3/04878—Side by side arrangement of multiple vessels in a main column system, wherein the vessels are normally mounted one upon the other or forming different sections of the same column
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    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • F25J2200/54—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the low pressure column of a double pressure main column system
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    • 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
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    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/58—Processes or apparatus involving steps for recycling of process streams the recycled stream 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/10—Boiler-condenser with superposed stages

Definitions

  • the invention relates to a process for the production of pure nitrogen and oxygen by cryogenic separation of air according to the preamble of
  • the distillation column system can be designed as a two-column system (for example as a classic Linde double column system), or as a three-column or multi-column system. It may, in addition to the columns for nitrogen-oxygen separation other devices for recovering high purity products and / or other air components, in particular of noble gases, for example, an argon and / or a krypton xenon recovery.
  • nitrogen-oxygen separation other devices for recovering high purity products and / or other air components, in particular of noble gases, for example, an argon and / or a krypton xenon recovery.
  • an “argon discharge column” is meant here a separation column for the argon-oxygen separation, which does not serve to obtain a pure argon product, but rather for the discharge of argon from the air into the high-pressure column and
  • Low pressure column is decomposed. Their circuit differs only slightly from that of a classical crude argon column, which generally has 70 to 180 theoretical plates; however, it contains significantly less theoretical plates, namely less than 40, in particular between 15 and 30.
  • a crude argon column the bottom region of an argon discharge column with an intermediate point of the
  • Cooled overhead condenser on its evaporation side relaxed bottom liquid from the high pressure column or a similar coolant is introduced;
  • Argon discharge column usually has no bottom evaporator.
  • argon column is used here as a generic term for argon discharge columns, full-quality crude argon columns and all transitions in between.
  • a "main heat exchanger” serves for cooling of feed air in indirect
  • Heat exchange with recycle streams from the distillation column system may be formed from a single or a plurality of parallel and / or serially connected and functionally connected heat exchanger sections, for example one or more plate heat exchanger blocks.
  • condenser-evaporator refers to a heat exchanger in which a first condensing fluid stream undergoes indirect heat exchange with a second evaporating fluid stream.
  • Each condenser evaporator has a
  • Condensing passages or evaporation passages exist.
  • the condensation (liquefaction) of the first fluid flow is performed, in the evaporation space the evaporation of the second fluid flow.
  • Evaporation and liquefaction space are formed by groups of passages that are in heat exchange relationship with each other.
  • Evaporation space of a condenser-evaporator may be formed as a bath evaporator, falling film evaporator or forced-flow evaporator.
  • One relevant method is known from Petras / Mostello, Experience with supplying oxygen to IGCC power plant and evaluation of alternative supply arrangements for future coal gasification facilities, 6th EPRI Coal Gasification Contractors Conference, October 1986, Figure 6-6. It serves to produce 96% oxygen as the main product.
  • the invention has for its object to win in such a method, both oxygen and nitrogen with high purity, that is with a
  • Medium pressure turbine or a turbine used In a specific embodiment, both a medium-pressure turbine and a
  • Relaxation to a second pressure which is higher than the first pressure.
  • an external energy driven booster and / or a turbine driven booster can be used.
  • the method according to the invention can also be operated with internal compression.
  • internal compression a product stream which has been brought to liquid pressure is generally vaporized against a heat carrier and finally recovered as a gaseous pressure product.
  • a supercritical pressure finds no
  • the product flow is then "pseudo-
  • a liquid fraction from the distillation column system is brought to elevated product pressure in the liquid state, warmed under this increased product pressure in the main heat exchanger, and finally withdrawn as a gaseous pressure product, a third substream compressed to the first pressure Feed air is recompressed as a heat carrier to a third pressure, which is higher than the first pressure and in particular higher than the second pressure, and then cooled in the main heat exchanger, the cooled third partial stream is expanded and introduced into the high pressure column and / or the low pressure column third partial flow is in the
  • Main heat exchanger liquefies (or - at supercritical pressure - pseudo-liquefied) and occurs in a substantially liquid state in the separation column (s).
  • the liquid fraction from which the internally compressed product is recovered may be formed according to claim 5 either by oxygen from the low pressure column or by nitrogen from the high pressure column; Furthermore, it is possible to produce both fractions simultaneously as internally compressed products.
  • the (pseudo) liquefied third partial stream of the feed air from the main heat exchanger is preferably used in a liquid expander (dense liquid expander).
  • a fourth partial flow of the feed air in a second expansion machine which is designed as an injection turbine, can be expanded to perform work and then introduced into the low-pressure column.
  • a relatively large proportion of the products can be removed in liquid form.
  • the liquid oxygen-enriched fraction which is introduced into the evaporation space of the high-pressure column overhead condenser can basically originate from an intermediate point of the high-pressure column. In a first variant, it is formed by at least part of the bottom liquid of the high-pressure column. In this case, the high-pressure column head condenser is preferably at the top of the
  • the liquid oxygen-enriched fraction for the high-pressure column top condenser is formed by an intermediate liquid of the low-pressure column.
  • the high-pressure column top condenser can be arranged inside the low-pressure column, separately from the low-pressure column and high-pressure column, or at the top of the high-pressure column.
  • the invention also relates to a device according to claim 15.
  • the device according to the invention can be supplemented by device features which correspond to the characteristics of individual, several or all dependent method claims.
  • FIG. 1 shows a first embodiment of the invention, which is designed as a two-turbine method
  • FIG. 2 shows a second embodiment of the invention, which is designed as a single-turbine method
  • FIG. 3 shows another embodiment of the invention, in which the
  • High-pressure column head condenser is installed in the low-pressure column
  • Figure 4 shows an inventive system with an additional
  • FIG. 5 shows an embodiment of the invention, in which the low-pressure column bottom evaporator is designed as a dephlegmator
  • Figure 6 shows a different turbine configuration of the invention with two serial
  • Figure 7 shows another turbine configuration of the invention with two serial
  • FIG. 8 shows a specific machine configuration of the invention in which both
  • Turbines and a single booster sit on a common shaft
  • Figure 9 shows an embodiment of the invention with a special arrangement of a liquid expander.
  • atmospheric air AIR
  • main air compressor 1 with intermediate and after-cooling 2 to a first pressure of, for example, 4.3 to 5.0 bar, preferably 4.5 to 4.7 bar.
  • the compressed air is further cooled in a pre-cooling 3, for example a direct contact cooler, and supplied to a cleaning device 4, which is replaced by a pair of
  • the purified feed air 5 under the first pressure is branched in the example into a first partial flow 6, a second partial flow 7, a third partial flow 8 and a fourth partial flow 9.
  • the first partial flow 6 and the third partial flow 8 are jointly (stream 10) in a first after-compressor 1 1 with aftercooler 12 to an intermediate pressure of, for example, 4.3 to 8.0 bar, preferably 4.5 to 6.0 bar nachverêtt and below this intermediate pressure branched from each other.
  • the first partial flow 6 is further compressed under the intermediate pressure in a second after-compressor 13 with aftercooler 14 to a second pressure of, for example, 4.5 to 9.0 bar, preferably 4.7 to 7.0 bar.
  • the first partial flow 15 is then supplied to the main heat exchanger 26 at the warm end at " the second pressure and cooled to a first intermediate temperature.” Under the first intermediate temperature, the first partial flow 16 is fed to a flash machine 17 and performs work thereupon at approximately the operating pressure of a high pressure column (see US Pat
  • the expansion machine 17 is also referred to as a medium-pressure turbine and drives the second secondary compressor 13 via a common shaft 13.
  • the first partial flow 8, which relaxes the work, is sent via line 19 to the high-pressure column 20 supplied, directly above the bottom.
  • the high-pressure column 20 is part of a distillation column system, which also has a low-pressure column 21, an argon column 22 and the associated condenser evaporators, namely a high-pressure column top condenser 23, a low-pressure column bottom evaporator 24 and an argon top condenser 25th
  • the second partial stream is cooled under the first pressure in the main heat exchanger 26 and optionally partially liquefied and at the cold end of the Main heat exchanger 26 taken.
  • the vapor content in the cooled second partial stream 30 is more than 70 mol%, preferably more than 98 mol%.
  • the cooled and mainly gaseous second partial stream 30 is in the
  • Liquefaction space of the low-pressure column sump evaporator 24 introduced. There he flows; preferably from top to bottom, through the liquefaction space and is at least partially, preferably completely or almost completely liquefied in the indirect heat exchange with the partially evaporating bottoms liquid of the low pressure column 21.
  • the vapor content at the outlet from the low-pressure column bottom evaporator 24 is less than 10 mol% ;
  • the second partial stream is completely liquid at this point, but not undercooled.
  • the liquid second substream 31 is then passed into the evaporation space of the argon overhead condenser 25 and previously in an expansion device 32
  • Capacitor 25 vaporized portion 33 of the second partial flow is fed via line 19 into the high-pressure column 20.
  • Evaporation space of the argon top condenser 25 (which acts as a separation stage here) is mixed with the bottom liquid 62 of the high-pressure column 20.
  • the third partial flow 8 is further compressed from the intermediate pressure in a third after-compressor 34 with aftercooler 35 to a third pressure, which is higher than the second pressure.
  • the high pressure air 36 is cooled in the main heat exchanger 26 and liquefied or (if the pressure is supercritical) pseudo-liquefied.
  • the liquid or supercritical cold air is depressurized in a liquid expander 38 to about 7.0 bar, in the lowest case working at about high pressure column pressure.
  • the relaxation of the liquid or supercritical cold air may occur in a Joule-Thomson valve in line 138.
  • the expanded liquid air 39 is to a first part 40 of the high-pressure column 20 at a
  • a second part 41 is cooled in a supercooling countercurrent 42 and after appropriate relaxation 43 in the
  • the fourth partial flow 9 is further compressed in a third after-compressor 44 with aftercooler 45 from the first pressure to about 5.0 to 7.0 bar.
  • the recompressed fourth substream 46 is fed to the main heat exchanger 26 at the warm end and cooled there to a second intermediate temperature, the same or different from the first intermediate temperature can be.
  • the cooled fourth partial flow 47 is fed to a flash-down machine 48 and is expanded to approximately the operating pressure of a high-pressure column (see below).
  • This relaxation machine is also designed as a turboexpander. It is also referred to as injection turbine and drives the third booster 44 via a common shaft.
  • the work-performing relaxed fourth partial stream 49 is supplied to the low-pressure column 21 at an intermediate point.
  • the second relaxation machine is also designed as a turboexpander. It is also referred to as injection turbine and drives the third booster 44 via a common shaft.
  • the work-performing relaxed fourth partial stream 49 is supplied to the low-pressure column 21 at an intermediate point.
  • Intermediate temperature is preferably chosen so that the thermodynamic state of the partial flow 49 sets at most 10 K above its dew point and minimally at 10% molar liquid content.
  • gaseous head stickst off 50 is withdrawn and condensed to a first part 51 in the high-pressure column top condenser 23 substantially completely.
  • the thereby obtained liquid nitrogen 52 is fed to a first part 53 as reflux to the high-pressure column 20.
  • a second part 56 is used as reflux in the low-pressure column 21; a third part 57 can be withdrawn as required as a liquid product (LIN).
  • This nitrogen product has a purity of less than 1000 ppm oxygen, preferably less than 10 ppm oxygen.
  • the second and third parts of the liquid nitrogen 52 become
  • subcooling countercurrent 42 54
  • cooled there and then relaxed in a valve 55 to low pressure column pressure.
  • a fourth part 58 is fed to an internal compression. It is brought in a pump 59 in the liquid state to an elevated first product pressure of typically more than 6 bar.
  • the high-pressure nitrogen 60 is heated under this increased first product pressure in the main heat exchanger 26 and finally as gaseous
  • GAN-IC Printed product deducted.
  • a second portion of the gaseous overhead nitrogen 50 of the high-pressure column 20 is warmed in the main heat exchanger 26 and recovered as gaseous medium pressure product (PGAN).
  • GAN-IC gaseous medium pressure product
  • Relaxation device 64 (for example, a valve) to about
  • the evaporation space of the high-pressure column top condenser 23 is formed in the example as a bath evaporator.
  • the rest 66 flows via line 67 directly into the
  • Low-pressure column 21 The oxygen-enriched fraction 68 evaporated in the high-pressure column overhead condenser 23 is supplied to the low-pressure column 21 (69).
  • Rinsing liquid or non-evaporated oxygen-enriched liquid 69 is introduced via line 67 elsewhere in the low-pressure column 21.
  • an argon-containing oxygen stream 70 is withdrawn from an intermediate point of the low-pressure column 21 and introduced into the argon column 22.
  • the top gas 73 contains more than 50 mol%, preferably more than 70 mol% of argon. It is introduced into the liquefaction space of the argon overhead condenser 25 where it is almost completely condensed.
  • the condensate 74 is returned as reflux into the argon column 22.
  • CGA Crude Gaseous Argon
  • connection either directly or after heating in the main heat exchanger 26 are discarded or fed to a downstream separation step.
  • the return liquid, which arrives in the bottom of the argon column 22, is optionally passed by means of the pump 72, via line 71 back into the low-pressure column 21.
  • liquid oxygen 76 is withdrawn and recovered to a first part 77 as needed as a liquid product (LOX).
  • the remainder 78 is supplied to an internal compression. It is brought in a pump 79 in the liquid state to an elevated second product pressure of typically 6 to 30 bar.
  • the high pressure liquid or supercritical oxygen 80 is heated under this increased second product pressure in the main heat exchanger 26 and finally withdrawn as a gaseous pressure product (GOX-IC).
  • GOX-IC gaseous pressure product
  • Oxygen from the low-pressure column sump is more than 98 mol%
  • gaseous nitrogen 81 is withdrawn, warmed in the subcooling countercurrent 42 and further in the main heat exchanger 26 and recovered as a pressureless nitrogen product (GAN).
  • gaseous impurity nitrogen 82 is withdrawn and also heated in the subcooling countercurrent 42 and the main heat exchanger 26.
  • the warm impure nitrogen (UN2) 83 may be used to a part 84 as a regeneration gas for the cleaning device 4 and to another part 85 as a dry gas for the pre-cooling 3 in an evaporative cooler.
  • the relative height arrangement of the high-pressure column 20, low-pressure column 21 and high-pressure column overhead condenser 23 is selected such that the liquids produced in the condensers, in particular the return liquids 53 and 56, reach their destination with the aid of natural gradients or pressure differences, ie without a pump.
  • the operating pressures are:
  • the high pressure column contains 30 to 60, preferably 40 to 50 theoretical plates; These can be realized for example by sieve plates or ordered packing.
  • the low pressure column contains 90 to 160, preferably 120 to 150 theoretical plates; These can be realized for example by sieve plates or ordered packing.
  • In the argon column are 20 to 200 theoretical plates, preferably in the form of ordered packing.
  • the argon column is designed as Argonausschleusklale, that is, it serves only or mainly for the discharge of argon and thus to increase the
  • Oxygen yield and / or the oxygen purity may be formed with a correspondingly high number of plates, the argon column as a real crude argon column, which produces virtually oxygen-free crude argon and passes, for example, to a pure argon column for argon-nitrogen separation.
  • FIG. 1 Another embodiment, which is not shown in any drawing, is designed as a single-turbine method. It is apparent from Figure 1, by the fourth sub-stream 9, 46, 47, 49, the turbine-recompressor combination 44/48 and the corresponding passage in the main heat exchanger 26 and line 66 are omitted. In this case, the oxygen-enriched stream 63 is completely introduced via line 65 into the top condenser 23 and partially evaporated there. The gas phase 68 and the liquid phase 69 are fed to the low-pressure column, the feed of the gas phase being above that of the liquid phase.
  • FIG. 2 also shows a single-turbine method.
  • the medium-pressure turbine 17 has been omitted from Figure 1, but a Einblaseturbine 248 maintained.
  • the flow 209 forms the "first partial flow” and the injection turbine 248 the "first expansion machine according to claim 1.
  • the description of Figure 1 applies analogously to Figure 2.
  • Feed air in the low-pressure column bottom evaporator 24 preferably completely liquefied. Between the feeds of the currents 67 and 68 in the
  • Low pressure column 21 are here 20 to 60 theoretical plates. Not shown in Figure 2 is a liquid removal at the lowest point of Hochdruckcicle Kopfkondensators 23. Here, a flushing of the bath can be made.
  • FIG. 3 is based on the modified exemplary embodiment of FIG. 1 without
  • the sump liquid 62 of the high-pressure column 20 is not introduced directly into the evaporation space of the high-pressure column top condenser 323, which is arranged as an intermediate evaporator in the interior of the low-pressure column 21. Rather, it is passed via line 367 to an upper intermediate point of the low-pressure column 21 and then, together with the reflux liquid from the upper section of the low-pressure column 21, flows over at least one mass transfer section 387 before flowing into the evaporation space of the high-pressure column top condenser 323.
  • the mass transfer section 387 may also be omitted.
  • FIG. 4 like FIG. 3, is based on the modified exemplary embodiment of FIG. 1 without an injection turbine, and thus again represents a single-turbine method with a medium-pressure turbine 17.
  • the condensation of the second partial stream 30 of the air is distributed over two condensers, the series-side liquefaction side are connected.
  • a low-pressure column intermediate evaporator 488 is additionally used. The substantially gaseous second substream is initially only partially liquefied in the bottom evaporator 424.
  • the two-phase mixture 489 - or after optional phase separation only the gaseous fraction - is then completely or almost completely liquefied in the intermediate evaporator 488 and then passed as usual via line 31 into the evaporation space of the argon top condenser 25.
  • An additional mass transfer section 487 may or may not be installed between the two evaporators 424, 488.
  • the air preferably flows in the direction of gravity through the sump evaporator 424 and the intermediate evaporator 488.
  • a dephlegmator is used as low-pressure column bottom heater 524
  • Oxygen can rise to the top and participate in the mass transfer with the descending oxygen in countercurrent via appropriately designed internals.
  • the air flows in this case preferably against gravity through the liquefaction passages.
  • a greater part of the separation efficiency of the low-pressure column than in a bath evaporator is provided here by the evaporator.
  • the second partial flow 30/31 flows unchanged from bottom to top through the liquefaction passages of the low-pressure column bottom evaporator 524. Liquid and any remaining gas leave the heat exchanger both at the top.
  • Such an embodiment of the method allows a lowering of the outlet pressure of the main air compressor of typically 50 to 150 mbar compared to the
  • FIG. 6 also dispenses with an injection turbine and is otherwise largely identical to FIG. 1.
  • the exemplary embodiment differs only in the execution of the work-performing expansion of the first partial flow 15.
  • the work-performing expansion from the second pressure to the high pressure column pressure takes place in two stages in two serial turbines 617a, 617b performed.
  • the first, warm turbine 617a relaxes to an intermediate pressure.
  • the resulting air flow 618 in the main heat exchanger 26 from a higher to a lower
  • FIG. 7 differs from FIG. 6 in that between the two turbines 617 a, 617 b no intermediate cooling, but an intermediate heating
  • the stream 618 is warmed in the main heat exchanger 26 before being introduced into the cold turbine 617b via line 616. This arrangement allows a further energetic optimization of the process over the
  • FIG. 8 is procedurally identical to FIG.
  • Injection turbine in turn, thus represents a single-turbine method with a medium-pressure turbine 17.
  • the liquid expander 938 downstream of the subcooling countercurrent 42 is arranged. This allows the existing
  • the second partial flow 37 is expanded only via a liquid expander 38; this one is between

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  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

L'invention concerne un procédé et un dispositif servant à produire de l'azote pur et de l'oxygène pur par séparation cryogénique d'air. Un système de distillation comprend une colonne haute pression (20), une colonne basse pression (21) et une colonne d'argon (22), ainsi qu'un condenseur de tête de colonne haute pression (23), un évaporateur de bas de colonne basse pression (24) et un condenseur de tête d'argon (25). La totalité de l'air d'alimentation est comprimée à une première pression dans un compresseur d'air principal (1). Un premier flux partiel (10, 6, 15, 16) de l'air comprimé à la première pression est refroidi dans un échangeur de chaleur principal (26) et amené (18) au moins en partie au système de colonnes de distillation. Un second flux partiel (7) de l'air comprimé à la première pression est refroidi dans l'échangeur de chaleur principal (26), puis au moins partiellement liquéfié dans l'évaporateur de bas de colonne basse pression (24). Le second flux partiel au moins partiellement liquéfié (31, 33, 19) est introduit au moins en partie dans le système de colonnes de distillation. Une fraction liquide enrichie en oxygène (62, 86) est introduite (63, 64, 65) dans la chambre d'évaporation du condenseur de tête de colonne haute pression (23). Un flux d'oxygène (70) contenant de l'argon provenant d'une zone intermédiaire de la colonne basse pression (21) est introduit dans la colonne d'argon (22). Le second flux partiel (31) est au moins partiellement introduit en aval de l'évaporateur de bas de colonne basse pression (24) dans le condenseur de tête d'argon (25), où il est au moins partiellement évaporé. Le second flux partiel (33) est au moins partiellement introduit en aval du condenseur de tête d'argon (25) dans la colonne haute pression (20) et/ou dans la colonne basse pression (21)
EP16826004.0A 2015-12-23 2016-12-22 Procédé et dispositif de production d'azote pur et d'oxygène pur par séparation cryogénique d'air Withdrawn EP3394536A1 (fr)

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PCT/EP2016/002162 WO2017108187A1 (fr) 2015-12-23 2016-12-22 Procédé et dispositif de production d'azote pur et d'oxygène pur par séparation cryogénique d'air

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JP6351895B1 (ja) * 2018-03-20 2018-07-04 レール・リキード−ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード 窒素製造方法および窒素製造装置
CN109186179B (zh) * 2018-09-30 2023-09-19 苏州制氧机股份有限公司 全精馏提氩富氧空分装置及工艺
WO2022263013A1 (fr) * 2021-06-17 2022-12-22 Linde Gmbh Procédé et installation permettant de fournir un produit à base d'air gazeux sous pression riche en oxygène

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