EP2118600A2 - Verfahren und vorrichtung zur herstellung von luftgasen in gasförmiger und flüssiger form mit einer hohen flexibilität und durch kryogene destillation - Google Patents

Verfahren und vorrichtung zur herstellung von luftgasen in gasförmiger und flüssiger form mit einer hohen flexibilität und durch kryogene destillation

Info

Publication number
EP2118600A2
EP2118600A2 EP08762155A EP08762155A EP2118600A2 EP 2118600 A2 EP2118600 A2 EP 2118600A2 EP 08762155 A EP08762155 A EP 08762155A EP 08762155 A EP08762155 A EP 08762155A EP 2118600 A2 EP2118600 A2 EP 2118600A2
Authority
EP
European Patent Office
Prior art keywords
pressure
turbine
air flow
main
air
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Withdrawn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
EP08762155A
Other languages
English (en)
French (fr)
Inventor
Alain Guillard
Patrick Le Bot
Xavier Pontone
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.)
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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 Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Publication of EP2118600A2 publication Critical patent/EP2118600A2/de
Withdrawn legal-status Critical Current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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—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
    • F25J3/04248—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.
    • F25J3/04393—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
    • F25J3/04763—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
    • F25J3/04775—Air purification and pre-cooling
    • 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
    • F25J3/04781—Pressure changing devices, e.g. for compression, expansion, liquid pumping
    • 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
    • F25J3/04763—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
    • F25J3/04836—Variable air feed, i.e. "load" or product demand during specified periods, e.g. during periods with high respectively low power costs
    • 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
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04951—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network
    • F25J3/04957—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network and inter-connecting equipments upstream of the fractionation unit (s), i.e. at the "front-end"
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/40—Air or oxygen enriched air, i.e. generally less than 30mol% of O2
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/24—Multiple compressors or compressor stages in parallel
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/04—Multiple expansion turbines in parallel

Definitions

  • a step of compressing the products by means of compressors An independent nitrogen liquefaction cycle making it possible to produce all or part of each of the constituents in liquid form if necessary.
  • the object of this invention is to be able to combine the economic benefits of integrated processes, while retaining the flexibility and flexibility offered by traditional methods.
  • a method for producing at least one air gas by cryogenic distillation in a column system comprising at least one medium pressure column operating at a medium pressure and a low pressure column. operating at a low pressure, thermally connected to each other in which: in a first and a second mode of operation a) the totality of a compressed air flow is brought to a high pressure, at least 5 bars above the pressure the medium pressure column, and purified at this high pressure, called the main pressure; b) this main pressure is possibly variable depending on the productions requested; c) a first portion of the air flow at at least the main pressure is cooled in an exchange line to an intermediate temperature thereof and is expanded in at least a first turbine; d) optionally a second portion of the air flow is expanded in at least a second turbine whose inlet and outlet conditions differ by at most 5 bar and at most 15 ° C or are identical in terms of pressure and temperature to that of the first turbine e) optionally the work provided by the first or third turbine serves at least partially
  • the discharge pressure of the auxiliary turbine is greater than or substantially equal to the atmospheric pressure, preferably substantially equal to the low pressure; m) at least a portion of the air flow expanded in the auxiliary turbine is heated in the exchange line and released to the atmosphere; n) part of the constituents of the air is produced as final product in liquid form, and in the second mode of operation; o) the air flow rate treated in the auxiliary turbine is reduced compared to the flow rate treated in the auxiliary turbine in the first mode, possibly to zero; and p) the production of liquid as final product is decreased relative to the production of liquid as the final product in the first mode, possibly to zero.
  • At least one booster coupled to one of the turbines sucks at room temperature; of all the boosters, only the booster connected mechanically to the first turbine has a suction temperature below -100 0 C; the suction temperature of the first turbine differs by not more than ⁇ 15 ° C from the pseudo vaporization temperature of the oxygen; the main incoming air flow is reduced during the second mode, preferably a flow at least equal to the reduction of the air flow sent to the auxiliary turbine during the second mode;
  • the variation of the main air flow is ensured by the variable vanes of a compressor; the variation of the main air flow is ensured by the starting and / or stopping of an auxiliary air compressor; the main air pressure varies between the first mode and the second mode; the first part of the air is supercharged at a pressure greater than the main pressure upstream of the first turbine so that it enters the first turbine substantially at a pressure greater than the main pressure; the inlet temperature of the auxiliary turbine is at least equal to or even greater than the inlet temperature of the first turbine.
  • This method uses a known distillation system (thermally connected medium pressure and low pressure columns, optionally an intermediate pressure column and / or a mixing column and / or an argon mixture column, etc.) and involves at least one two relaxation turbines.
  • Two flows are at substantially equal pressure if their pressures differ only in the pressure drops.
  • the gaseous fraction of the air flow sucked by the auxiliary turbine is previously relaxed in the first and / or second turbine, possibly sent to the medium pressure column and withdrawn from the medium pressure column before being sent to the auxiliary turbine, after having been reheated in the main exchange line.
  • the production of liquid product, all final products combined constitutes 1%, or 2% or 5% of the air flow sent to the columns (or to the column if only the medium pressure column is supplied with air ).
  • a compressed air flow 1 from a main compressor is supercharged in a booster 3 at a high pressure at least 5 bar abs above the pressure of the medium pressure column, this high pressure being called main pressure.
  • This main pressure may for example be between 10 and 25 bar abs.
  • the flow 5 is then purified with water and carbon dioxide (not shown).
  • the total flow of supercharged and purified air is sent to an exchange line 7 where it cools to a temperature T1.
  • T1 At this temperature, the flow 5 is divided in two to form a flow 9 which liquefies and is sent to the column system and a flow 11.
  • the flow 11 leaves the exchange line 7 at the temperature T1 and is sent to a cold booster 13 to produce a flow 15 at a pressure very substantially greater than the average pressure and possibly greater than the main pressure.
  • the flow rate 15 at a cold booster outlet temperature T2 cools in the exchange line 7 to a temperature T3 higher than T1. At this temperature T3, the flow 15 is divided into two flow rates 17, 19.
  • the flow 17 is expanded in a turbine 21 from the temperature T3 close to the pseudo vaporization temperature of the pressurized oxygen 33.
  • the suction pressure of the turbine 21 is equal to the discharge pressure of the booster 13 thus very substantially greater than the average pressure (greater than 5 bars) and possibly greater than the main pressure and the discharge pressure is higher or equal to the average pressure, preferably substantially equal to the average pressure.
  • the flow expanded to a pressure greater than or equal to the average pressure, preferably substantially equal to the average pressure is divided into two fractions 23, 25.
  • the flow 19 continues cooling in the exchange line and is sent in gaseous form to the column system.
  • the cold booster 13 is driven by the turbine 21.
  • a residual nitrogen flow is heated in the exchange line.
  • a flow of liquid oxygen 35 pressurized in a pump 33 vaporizes in the exchange line 7.
  • a liquid column system other than liquid oxygen, is pressurized, vaporized in the exchange line 7 and then serves as a product under pressure.
  • the fraction 23 is sent to the medium pressure column of the gaseous system while the fraction 25 is returned to the cold end of the exchange line 7.
  • the fraction 25 is sent to a turbine 27 where it expands to a temperature T5 forming an air flow rate 29. This air flow then heats up in the exchange line 7 to be rejected to the atmosphere, so that the distillation is not disturbed.
  • a liquid product is withdrawn from the column system as final product 32.
  • the only liquid product of the apparatus is liquid oxygen but other products can obviously be produced.
  • the air flow 25 treated in the auxiliary turbine 27 is reduced to zero if necessary, the main incoming air flow 1 is reduced by a flow rate at least equal to the reduction of the air flow sent. to the auxiliary turbine 27 and the production of liquid 32 is eventually reduced to zero.
  • the turbine 21 is driven by the booster 13 and the booster 3 drives the auxiliary turbine 27.
  • a compressed air flow 1 from a main compressor is supercharged in two identical boosters in parallel 3A, 3B at a high pressure at least 5 bar abs above the pressure of the medium pressure column, this high pressure being called the main pressure.
  • This main pressure may for example be between 10 and 25 bar abs.
  • the combined flow from both boosters is then purified with water and carbon dioxide (not shown).
  • the total flow of supercharged and purified air 5 from the two boosters is sent to an exchange line 7 where it cools to a temperature T1. At this temperature, the flow 5 is divided in two to form a flow 9 which liquefies and is sent to the column system and a flow 11.
  • the flow 11 leaves the exchange line 7 at the temperature T1 different from at most ⁇ 5 ° C of the vaporization temperature of the pressurized oxygen 33) and is sent to a cold booster 13 to produce a flow 15 at a pressure substantially greater than the average pressure and possibly greater than the main pressure.
  • the flow rate 15 at a cold booster outlet temperature T2 cools in the exchange line 7 to a temperature T3 higher than T1.
  • the flow 15 is divided into two flow rates 17, 19.
  • the flow 17 is again divided in two, each flow being expanded from the discharge pressure of the cold booster 13 in one of two turbines 21 A, 21 B connected in parallel with an inlet temperature T3 close to the pseudo vaporization temperature of the pressurized oxygen 33.
  • the flow 19 continues cooling in the exchange line and is sent in gaseous form to the column system.
  • a residual nitrogen flow is heated in the exchange line.
  • the expanded flows of the two turbines are combined and then divided into two fractions 23, 25.
  • the fraction 23 is sent to the medium pressure column of the gaseous system while the fraction 25 is returned to the end. cold of the exchange line 7.
  • the fraction 25 is sent to a turbine 27 where it expands to a temperature T5 forming an air flow 29 This air flow then warms up in the exchange line 7 to be discharged into the atmosphere, so that the distillation is not disturbed.
  • a liquid product is withdrawn from the column system as final product 32.
  • the only liquid product of the apparatus is liquid oxygen but other products can obviously be produced.
  • the air flow 25 treated in the auxiliary turbine 27 is reduced to zero if necessary, the main airflow incoming 1 is reduced by a flow rate at least equal to the reduction of the air flow sent to the auxiliary turbine 27 and the production of liquid 32 is reduced to zero if necessary.
  • a liquid of the column system for example liquid oxygen, is pressurized, vaporized in the exchange line 7 and then serves as a product under pressure.
  • This variation of the air flow 1 between the two modes of operation is provided by the variable vanes of a compressor and / or by the start and / or stop of an auxiliary air compressor.
  • These two modes of operation may be the only modes of operation of the apparatus or there may be other modes of operation.
  • the turbine 21A is driven by the booster 13.
  • the booster 3A drives the auxiliary turbine 27 and the booster 3B the turbine 21 B. Any other combination can also be considered.

Landscapes

  • 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)
EP08762155A 2007-03-13 2008-02-26 Verfahren und vorrichtung zur herstellung von luftgasen in gasförmiger und flüssiger form mit einer hohen flexibilität und durch kryogene destillation Withdrawn EP2118600A2 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR0753789A FR2913760B1 (fr) 2007-03-13 2007-03-13 Procede et appareil de production de gaz de l'air sous forme gazeuse et liquide a haute flexibilite par distillation cryogenique
PCT/FR2008/050314 WO2008110734A2 (fr) 2007-03-13 2008-02-26 Procédé et appareil de production de gaz de l'air sous forme gazeuse et liquide à haute flexibilité par distillation cryogénique

Publications (1)

Publication Number Publication Date
EP2118600A2 true EP2118600A2 (de) 2009-11-18

Family

ID=38895649

Family Applications (1)

Application Number Title Priority Date Filing Date
EP08762155A Withdrawn EP2118600A2 (de) 2007-03-13 2008-02-26 Verfahren und vorrichtung zur herstellung von luftgasen in gasförmiger und flüssiger form mit einer hohen flexibilität und durch kryogene destillation

Country Status (8)

Country Link
US (1) US8997520B2 (de)
EP (1) EP2118600A2 (de)
JP (1) JP2010530947A (de)
CN (1) CN102016468B (de)
BR (1) BRPI0808719A2 (de)
FR (1) FR2913760B1 (de)
RU (1) RU2009137781A (de)
WO (1) WO2008110734A2 (de)

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7533540B2 (en) * 2006-03-10 2009-05-19 Praxair Technology, Inc. Cryogenic air separation system for enhanced liquid production
FR2928446A1 (fr) * 2008-03-10 2009-09-11 Air Liquide Procede de modification d'un appareil de separation d'air par distillation cryogenique
EP2369281A1 (de) * 2010-03-09 2011-09-28 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
DE102010052545A1 (de) 2010-11-25 2012-05-31 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft
DE102010052544A1 (de) 2010-11-25 2012-05-31 Linde Ag Verfahren zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft
CN105143801A (zh) 2013-03-28 2015-12-09 林德股份公司 以可变能量消耗产生气态压缩氧的方法和设备
JP7379763B2 (ja) * 2019-07-25 2023-11-15 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 ガス液化方法およびガス液化装置
WO2022053173A1 (de) * 2020-09-08 2022-03-17 Linde Gmbh Verfahren und anlage zur tieftemperaturzerlegung von luft

Family Cites Families (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
IT1019710B (it) * 1974-07-12 1977-11-30 Nuovo Pignone Spa Processo ed apparato per la produ zione di elevate percentuali di os sigeno e/o azoto allo stato liquido
DE3012062A1 (de) * 1980-03-28 1981-10-08 Linde Ag, 6200 Wiesbaden Verfahren und vorrichtung zur erzeugung von gasfoermigen sauerstoff
FR2652409A1 (fr) * 1989-09-25 1991-03-29 Air Liquide Procede de production frigorifique, cycle frigorifique correspondant et leur application a la distillation d'air.
GB9008752D0 (en) * 1990-04-18 1990-06-13 Boc Group Plc Air separation
JP2909678B2 (ja) 1991-03-11 1999-06-23 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 圧力下のガス状酸素の製造方法及び製造装置
FR2688052B1 (fr) * 1992-03-02 1994-05-20 Maurice Grenier Procede et installation de production d'oxygene et/ou d'azote gazeux sous pression par distillation d'air.
FR2692664A1 (fr) * 1992-06-23 1993-12-24 Lair Liquide Procédé et installation de production d'oxygène gazeux sous pression.
US5379598A (en) * 1993-08-23 1995-01-10 The Boc Group, Inc. Cryogenic rectification process and apparatus for vaporizing a pumped liquid product
US5475980A (en) * 1993-12-30 1995-12-19 L'air Liquide, Societe Anonyme Pour L'etude L'exploitation Des Procedes Georges Claude Process and installation for production of high pressure gaseous fluid
FR2721383B1 (fr) * 1994-06-20 1996-07-19 Maurice Grenier Procédé et installation de production d'oxygène gazeux sous pression.
CN1153896A (zh) * 1995-08-03 1997-07-09 英国氧气集团有限公司 空气分离方法和设备
GB9515907D0 (en) * 1995-08-03 1995-10-04 Boc Group Plc Air separation
US5758515A (en) * 1997-05-08 1998-06-02 Praxair Technology, Inc. Cryogenic air separation with warm turbine recycle
US5802873A (en) * 1997-05-08 1998-09-08 Praxair Technology, Inc. Cryogenic rectification system with dual feed air turboexpansion
US6808364B2 (en) * 2002-12-17 2004-10-26 General Electric Company Methods and apparatus for sealing gas turbine engine variable vane assemblies
FR2851330B1 (fr) * 2003-02-13 2006-01-06 Air Liquide Procede et installation de production sous forme gazeuse et sous haute pression d'au moins un fluide choisi parmi l'oxygene, l'argon et l'azote par distillation cryogenique de l'air
FR2854683B1 (fr) * 2003-05-05 2006-09-29 Air Liquide Procede et installation de production de gaz de l'air sous pression par distillation cryogenique d'air
FR2854682B1 (fr) * 2003-05-05 2005-06-17 Air Liquide Procede et installation de separation d'air par distillation cryogenique
US7272954B2 (en) * 2004-07-14 2007-09-25 L'air Liquide, Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Proceded Georges Claude Low temperature air separation process for producing pressurized gaseous product
US7437890B2 (en) * 2006-01-12 2008-10-21 Praxair Technology, Inc. Cryogenic air separation system with multi-pressure air liquefaction

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO2008110734A2 *

Also Published As

Publication number Publication date
CN102016468A (zh) 2011-04-13
US20110120186A1 (en) 2011-05-26
BRPI0808719A2 (pt) 2014-08-12
US8997520B2 (en) 2015-04-07
WO2008110734A3 (fr) 2011-07-21
WO2008110734A2 (fr) 2008-09-18
FR2913760A1 (fr) 2008-09-19
JP2010530947A (ja) 2010-09-16
RU2009137781A (ru) 2011-04-20
CN102016468B (zh) 2014-07-30
FR2913760B1 (fr) 2013-08-16

Similar Documents

Publication Publication Date Title
WO2008129198A2 (fr) Procede et appareil de production de gaz de l'air sous forme gazeuse et liquide a haute flexibilite par distillation cryogenique
WO2008110734A2 (fr) Procédé et appareil de production de gaz de l'air sous forme gazeuse et liquide à haute flexibilité par distillation cryogénique
EP1623171B1 (de) Verfahren und vorrichtung zur tieftemperaturzerlegung von luft
CA2828179C (fr) Procede et appareil de liquefaction de co2
EP1014020B1 (de) Kryogenisches Luftzerleggungsverfahren
EP2691718B1 (de) Verfahren zur herstellung eines gases aus druckluft durch kryogene destillation
EP1711765A1 (de) Kryogenes destillationsverfahren und anlage zur lufttrennung
EP3631327A1 (de) Verfahren und vorrichtung zur lufttrennung durch kryogene destillation
EP2788699B1 (de) Verfahren und vorrichtung zum verflüssigen eines co2-reichen gases
EP2457047A2 (de) Verfahren und vorrichtung zur lufttrennung durch kryogene destillation
FR2831249A1 (fr) Procede et installation de separation d'air par distillation cryogenique
FR2946099A1 (fr) Procede de compression d'air humide.
WO2010109149A2 (fr) Appareil et procédé de séparation d'air par distillation cryogénique
EP1409937B1 (de) Verfahren zur dampferzeugung und luftzerlegung
WO2009112744A2 (fr) Appareil de separation d'air par distillation cryogenique
FR2864213A1 (fr) Procede et installation de production sous forme gazeuse et sous haute pression d'au moins un fluide choisi parmi l'oxygene, l'argon et l'azote par distillation cryogenique de l'air
FR2863348A1 (fr) Compresseur de gaz, appareil de separation d'un melange gazeux incorporant un tel compresseur et procede de separation d'un melange gazeux incorporant un tel compresseur
WO2009101329A2 (fr) Procédé et appareil de séparation des gaz de l'air
FR3014181A1 (fr) Procede et appareil de separation d’air par distillation cryogenique

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Kind code of ref document: A2

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MT NL NO PL PT RO SE SI SK TR

RIN1 Information on inventor provided before grant (corrected)

Inventor name: LE BOT, PATRICK

Inventor name: GUILLARD, ALAIN

Inventor name: PONTONE, XAVIER

17P Request for examination filed

Effective date: 20120123

RBV Designated contracting states (corrected)

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MT NL NO PL PT RO SE SI SK TR

DAX Request for extension of the european patent (deleted)
GRAP Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOSNIGR1

INTG Intention to grant announced

Effective date: 20161213

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION HAS BEEN WITHDRAWN

18W Application withdrawn

Effective date: 20170112