WO2008129198A2 - Method and apparatus for the production of gas from air in highly flexible gaseous and liquid form by cryogenic distillation - Google Patents
Method and apparatus for the production of gas from air in highly flexible gaseous and liquid form by cryogenic distillation Download PDFInfo
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- WO2008129198A2 WO2008129198A2 PCT/FR2008/050418 FR2008050418W WO2008129198A2 WO 2008129198 A2 WO2008129198 A2 WO 2008129198A2 FR 2008050418 W FR2008050418 W FR 2008050418W WO 2008129198 A2 WO2008129198 A2 WO 2008129198A2
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04109—Arrangements of compressors and /or their drivers
- F25J3/04139—Combination of different types of drivers mechanically coupled to the same compressor, possibly split on multiple compressor casings
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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
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
- F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main feed air
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- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
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- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
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- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—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
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- 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
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- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—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
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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
- F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—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
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- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
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- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
- F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
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- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
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- 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
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
- F25J2240/04—Multiple expansion turbines in parallel
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 pressure of low pressure, thermally interconnected wherein in a first and a second mode of operation a) the entire compressed air flow is brought to a high pressure, at least 5 bar above the pressure of the middle column pressure, 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 (21 B) whose intake and discharge conditions differ by at most 5 bar and at most 15 ° C or are identical in terms of pressure and temperature to those of the first turbine; e) possibly the work provided by the first or third turbine serves at least partially to the work required by
- 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; n) part of the constituents of the air is produced in liquid form as final product; 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 of operation, possibly to zero and p) the production of liquid as product final is reduced, compared to the production of liquid as the final product in the first mode of operation, possibly zero.
- At least one booster coupled to one of the turbines sucks at room temperature
- the suction temperature of the first turbine differs by at most 15 ° C. from the pseudo vaporization temperature of the oxygen; the main incoming air flow rate is reduced, during the second mode, preferably by a flow rate at least equal to the reduction during the second mode of the air flow sent to the auxiliary turbine;
- variable vanes of a compressor 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 suction temperature of the auxiliary turbine is higher than the suction temperature of the first turbine
- the unit may be arranged so that in operation one of the following conditions is met: i) the suction temperature of the auxiliary turbine is higher than the suction temperature of the first turbine ii) the suction temperature of the auxiliary turbine is higher than the suction temperature of the booster iii) the temperature of the booster suction of the booster is lower than the suction temperature of the first turbine iv) the discharge temperature of the booster is higher than the suction temperature of the first turbine v) the discharge temperature of the booster is higher than the discharge temperature of the auxiliary 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 flow rates 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 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.
- T3 the temperature of 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 rate expanded to a pressure greater than or equal to the average pressure, preferably substantially equal to the average pressure, is sent to the column system as the flow rate 25.
- the flow 19 continues cooling in the exchange line and is sent in the form gaseous 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.
- a fraction of air 25 is taken from the purified air 5 at the main pressure and is cooled in 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 is heated in the exchange line.
- a liquid product is withdrawn from the column system as final product 32.
- the only product of the apparatus is liquid oxygen but other products can obviously be produced in liquid form.
- 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 37 is reduced to zero if necessary.
- 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.
- booster 3B There may be a compression step (booster 3B) between the hot booster which brings the air to the main pressure and the cold booster, so that the cold booster is from a pressure above the booster. main pressure.
- the turbine 21 is driven by the booster 13 and the booster 3 drives the auxiliary turbine 27.
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
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- General Engineering & Computer Science (AREA)
- Health & Medical Sciences (AREA)
- Emergency Medicine (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
Description
Procédé et appareil de production de gaz de l'air sous forme gazeuse et liquide à haute flexibilité par distillation cryogénique Method and apparatus for producing highly flexible gaseous and liquid air gases by cryogenic distillation
Les procédés traditionnels de production de gaz de l'air sous forme liquide ou gazeuse présentaient des architectures de procédés distinctes. Ainsi on trouvait :Traditional processes for producing air gases in liquid or gaseous form had distinct process architectures. Thus we found:
• un appareil de séparation de l'air produisant les constituants principaux (O2, N2, Ar), à pression atmosphérique ou légèrement supérieure ;• an air separation unit producing the main components (O2, N2, Ar), at atmospheric or slightly higher pressure;
• une étape de compression des produits au moyen de compresseurs ; • un cycle indépendant de liquéfaction d'azote permettant de produire tout ou partie de chacun des constituants sous forme liquide si nécessaire.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.
Cette configuration permettait une grande souplesse d'utilisation car chacune des trois « fonctions » mises en œuvre (séparation, compression, liquéfaction) pouvait être opérée ou stoppée de façon indépendante sans affecter le fonctionnement des deux autres.This configuration allowed a great flexibility of use because each of the three "functions" implemented (separation, compression, liquefaction) could be operated or stopped independently without affecting the operation of the other two.
Néanmoins, cette configuration souffre d'un manque de compétitivité important, compte tenu du coût très élevé de cette architecture, qui réclame un appareil par fonction.Nevertheless, this configuration suffers from a significant lack of competitiveness, given the very high cost of this architecture, which requires a device by function.
Les procédés plus récents de production de gaz de l'air, que nous appelons procédés intégrés, présentent l'avantage de pouvoir combiner dans un seul équipement ces trois fonctions. Les appareils dits « à pompe », incluant des cycles de détente d'air ou éventuellement d'azote, permettent de produire à partir du même équipement les constituants de l'air sous forme gazeuse sous pression et liquide. Parmi ceux-ci, les procédé à paliers de vaporisation décalés pour délivrer des produits sous pression, tels que décrits dans le brevet EP-A-0504029 ou encore FR-A-2688052, sont particulièrement intéressants puisqu'ils permettent la combinaison de ces fonctions à partir d'un unique compresseur d'air, à haute pression. L'efficacité énergétique de l'ensemble est comparable au procédé traditionnel et l'investissement est grandement diminué.The more recent processes for producing air gases, which we call integrated processes, have the advantage of being able to combine these three functions in a single equipment. The so-called "pump" devices, including cycles of expansion of air or possibly nitrogen, make it possible to produce from the same equipment the constituents of the air in gaseous form under pressure and liquid. Among these, the offset vaporization step processes for delivering products under pressure, as described in patent EP-A-0504029 or FR-A-2688052, are particularly interesting since they allow the combination of these functions. from a single air compressor, at high pressure. The energy efficiency of the whole is comparable to the traditional process and the investment is greatly diminished.
Par contre la souplesse de production est affectée par la combinaison « 3 en 1 » des fonctions, et on pourra plus difficilement opérer ou arrêter une fonction sans affecter l'ensemble. Le but de cette invention est de pouvoir combiner les avantages économiques des procédés intégrés, tout en conservant la souplesse et la flexibilité offerte par les procédés traditionnels.On the other hand, the flexibility of production is affected by the combination "3 in 1" functions, and it will be more difficult to operate or stop a function without affecting the whole. 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.
Selon l'invention, il est prévu un procédé de production d'au moins un gaz de l'air par distillation cryogénique dans un système de colonnes comprenant au moins une colonne moyenne pression opérant à une moyenne pression et une colonne basse pression opérant à une basse pression, thermiquement reliées entre elles dans lequel dans un premier et un deuxième mode de fonctionnement a) la totalité d'un débit d'air comprimé est portée à une haute pression, au moins 5 bars au dessus de la pression de la colonne moyenne pression, et épurée à cette haute pression, appelée pression principale ; b) cette pression principale est éventuellement variable en fonction des productions demandées ; c) une première partie du débit d'air à au moins la pression principale est refroidie dans une ligne d'échange jusqu'à une température intermédiaire de celle-ci et est détendue dans au moins une première turbine ; d) éventuellement une seconde partie du débit d'air est détendue dans au moins une seconde turbine (21 B) dont les conditions d'admission et de refoulement diffèrent d'au plus 5 bars et d'au plus 15°C ou sont identiques en termes de pression et de température à celles de la première turbine ; e) éventuellement le travail fourni par la première ou une troisième turbine sert au moins partiellement au travail requis par un surpresseur ; f) la pression d'admission de la première turbine est très sensiblement supérieure à la moyenne pression et éventuellement supérieure à la pression principale ; g) la pression de refoulement de la première turbine est supérieure ou égale à la moyenne pression, préférablement sensiblement égale à la moyenne pression ; h) un/le surpresseur comprime au moins une fraction du débit d'air à une haute pression, supérieure ou égale à la pression d'air principale refroidie dans la ligne d'échange jusqu'à une température cryogénique (<-100°C), et renvoie le débit surpressé dans la ligne d'échange, où au moins une partie se liquéfie au bout froid puis est envoyée dans le système de colonnes après détente ; i) un produit liquide sous pression du système de colonnes se vaporise dans la ligne d'échange ; et dans le premier mode de fonctionnement, j) une turbine auxiliaire aspire une fraction gazeuse du débit d'air ayant été refroidie dans la ligne d'échange principale ; k) la pression d'aspiration de la turbine auxiliaire est supérieure ou substantiellement égale à la pression principale, préférablement supérieure d'au moins 2 bars abs ou substantiellement égale à la pression principale ;According to the invention, there is provided 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 pressure of low pressure, thermally interconnected wherein in a first and a second mode of operation a) the entire compressed air flow is brought to a high pressure, at least 5 bar above the pressure of the middle column pressure, 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 (21 B) whose intake and discharge conditions differ by at most 5 bar and at most 15 ° C or are identical in terms of pressure and temperature to those of the first turbine; e) possibly the work provided by the first or third turbine serves at least partially to the work required by a booster; f) the inlet pressure of the first turbine is very substantially greater than the average pressure and possibly greater than the main pressure; g) the discharge pressure of the first turbine is greater than or equal to the average pressure, preferably substantially equal to the average pressure; h) a booster compresses at least a fraction of the air flow at a high pressure, greater than or equal to the main air pressure cooled in the exchange line to a cryogenic temperature (<-100 ° C) ), and returns the depressed flow in the exchange line, where at least some liquefies at the cold end then is sent into the column system after relaxation; i) a liquid product under pressure of the column system vaporizes in the exchange line; and in the first mode of operation, j) an auxiliary turbine sucks a gaseous fraction of the air flow having been cooled in the main exchange line; k) the suction pressure of the auxiliary turbine is greater than or substantially equal to the main pressure, preferably greater than at least 2 bar abs or substantially equal to the main pressure;
I) la pression de refoulement de la turbine auxiliaire est supérieure ou substantiellement égale à la pression atmosphérique, préférablement substantiellement égale à la basse pression ; m) au moins une partie du débit d'air détendu dans la turbine auxiliaire est réchauffée dans la ligne d'échange; n) une partie des constituants de l'air est produite sous forme liquide comme produit final ; et dans le deuxième mode de fonctionnement, o) le débit d'air traité dans la turbine auxiliaire est réduit par rapport au débit traité dans la turbine auxiliaire dans le premier mode de fonctionnement, éventuellement à zéro et p) la production de liquide comme produit final est diminuée, par rapport à la production de liquide comme produit final dans le premier mode de fonctionnement, éventuellement à zéro. Selon d'autres aspects facultatifs :I) 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; n) part of the constituents of the air is produced in liquid form as final product; 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 of operation, possibly to zero and p) the production of liquid as product final is reduced, compared to the production of liquid as the final product in the first mode of operation, possibly zero. According to other optional aspects:
- toutes les turbines sont freinées par un surpresseur d'air ;- all turbines are braked by an air booster;
- au moins un surpresseur couplé à une des turbines aspire à température ambiante ;at least one booster coupled to one of the turbines sucks at room temperature;
- de tous les surpresseurs, seul le surpresseur relié mécaniquement à la première turbine a une température d'aspiration en dessous de -1000C ;- Of all the boosters, only the booster connected mechanically to the first turbine has a suction temperature below -100 0 C;
- la température d'aspiration de la première turbine diffère d'au plus 15°C, de la température de pseudo vaporisation de l'oxygène ; - le débit d'air principal entrant est réduit, pendant le deuxième mode, de préférence d'un débit au moins égal à la réduction pendant le deuxième mode du débit d'air envoyé à la turbine auxiliaire ;the suction temperature of the first turbine differs by at most 15 ° C. from the pseudo vaporization temperature of the oxygen; the main incoming air flow rate is reduced, during the second mode, preferably by a flow rate at least equal to the reduction during the second mode of the air flow sent to the auxiliary turbine;
- la variation du débit d'air principal est assurée par les aubages variables d'un compresseur ;the variation of the main air flow is ensured by the variable vanes of a compressor;
- la variation de débit d'air principal est assurée par la mise en route et/ou l'arrêt d'un compresseur d'air auxiliaire ;the variation of the main air flow is ensured by the starting and / or stopping of an auxiliary air compressor;
- la pression d'air principale varie entre le premier mode et le deuxième mode ; - la première partie de l'air est surpressée à une pression supérieure à la pression principale en amont de la première turbine de sorte qu'elle rentre dans la première turbine substantiellement à une pression supérieure à la pression principale ;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;
- la température d'aspiration de la turbine auxiliaire est plus élevée que la température d'aspiration de la première turbine ;the suction temperature of the auxiliary turbine is higher than the suction temperature of the first turbine;
- l'air détendu dans la turbine auxiliaire est rejeté à l'atmosphère.- the air expanded in the auxiliary turbine is released to the atmosphere.
Selon un autre aspect de l'invention, il est prévu une unité de refroidissement et de réchauffage de débits destinés à et provenant d'un système de colonnes de séparation d'air comprenant une ligne d'échange, une première turbine, une turbine auxiliaire, un surpresseur, la ligne d'échange comprenant : i) au moins un passage pour recevoir un premier débit d'air épuré, l'au moins un passage pour recevoir un premier débit d'air épuré étant relié au surpresseur, ii) au moins un passage relié au refoulement du surpresseur, l'au moins un passage relié au surpresseur étant relié à la première turbine, iii) au moins deux passages pour recevoir au moins deux fluides (35,37) qui se réchauffent, iv) au moins un passage pour recevoir un deuxième débit d'air épuré, l'au moins un passage pour recevoir le deuxième débit d'air épuré étant relié à l'aspiration de la turbine auxiliaire et le refoulement de la turbine auxiliaire étant relié à au moins un passage d'air à réchauffer.According to another aspect of the invention, there is provided a flow cooling and heating unit for and coming from a system of air separation columns comprising an exchange line, a first turbine, an auxiliary turbine a booster, the exchange line comprising: i) at least one passage for receiving a first stream of purified air, the at least one passage for receiving a first stream of purified air being connected to the booster, ii) the at least one passage connected to the discharge of the booster, the at least one passage connected to the booster being connected to the first turbine, iii) at least two passages to receive at least two fluids (35,37) which are heated, iv) at least a passage for receiving a second flow of purified air, the at least one passage for receiving the second flow of purified air being connected to the suction of the auxiliary turbine and the discharge of the auxiliary turbine being connected to at least one passage of air to warm up.
L'unité peut être disposée de sorte qu'en opération, une des conditions suivantes est remplie : i) la température d'aspiration de la turbine auxiliaire est supérieure à la température d'aspiration de la première turbine ii) la température d'aspiration de la turbine auxiliaire est supérieure à la température d'aspiration du surpresseur iii) la température d'aspiration du surpresseur est inférieure à la température d'aspiration de la première turbine iv) la température de refoulement du surpresseur est supérieure à la température d'aspiration de la première turbine v) la température de refoulement du surpresseur est supérieure à la température de refoulement de la turbine auxiliaire.The unit may be arranged so that in operation one of the following conditions is met: i) the suction temperature of the auxiliary turbine is higher than the suction temperature of the first turbine ii) the suction temperature of the auxiliary turbine is higher than the suction temperature of the booster iii) the temperature of the booster suction of the booster is lower than the suction temperature of the first turbine iv) the discharge temperature of the booster is higher than the suction temperature of the first turbine v) the discharge temperature of the booster is higher than the discharge temperature of the auxiliary turbine.
On se propose ici d'améliorer la flexibilité de production des procédés de type mono-machines tels que décrits précédemment :It is proposed here to improve the production flexibility of single-machine type processes as described above:
• soit en offrant la possibilité de réduire voire annuler la production de liquide des unités utilisant un procédé tel que décrit dans EP-A-0504029 ; • soit en offrant la possibilité de produire de façon efficace des liquides avec des procédés tels que décrits dans FR-A-2688052 ;Or by offering the possibility of reducing or even canceling the production of liquid from the units using a process as described in EP-A-0504029; Or by providing the possibility of efficiently producing liquids with processes as described in FR-A-2688052;
• et en offrant la possibilité de faire l'un ou l'autre de façon réversible, et énergétiquement efficace dans les deux cas.• and offering the possibility to do one or the other reversibly, and energetically effective in both cases.
Ce procédé utilise un système de distillation connu (colonnes moyenne pression et basse pression thermiquement reliées, éventuellement une colonne à pression intermédiaire et/ou une colonne de mélange et/ou une colonne de mixture argon, etc..) et met en jeu au moins deux turbines de détente.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.
Deux débits sont à pression substantiellement égale si leurs pressions ne différent que par les pertes de charge. La fraction gazeuse du débit d'air aspiré par la turbine auxiliaire est préalablement détendue dans la première et/ou la seconde turbine, éventuellement envoyé à la colonne moyenne pression et soutiré de la colonne moyenne pression avant être envoyé à la turbine auxiliaire, après avoir été réchauffée dans la ligne d'échange principale. En premier mode de fonctionnement, la production de produit liquide, tous produits finaux confondus, constitue 1 %, ou 2% ou 5% du débit d'air envoyé aux colonnes (ou à la colonne si seule la colonne moyenne pression est alimentée en air). L'invention sera décrite en plus de détail en se référant aux figures, qui montrent des installations de séparation d'air capables de fonctionner selon le procédé de l'invention.Two flow rates 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. In the first mode of operation, 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 ). The invention will be described in more detail with reference to the figures, which show air separation plants capable of operating according to the method of the invention.
Dans la Figure 1 , un débit d'air comprimé 1 provenant d'un compresseur principal est surpressé dans un surpresseur 3 à une haute pression au moins 5 bar abs au-dessus de la pression de la colonne moyenne pression, cette haute pression étant appelée pression principale. Cette pression principale peut par exemple être entre 10 et 25 bars abs. A cette pression principale le débit 5 est ensuite épuré en eau et dioxyde de carbone (non-illustré). Le débit total d'air surpressé et épuré 5 est envoyé à une ligne d'échange 7 où il se refroidit jusqu'à une température T1. A cette température, le débit 5 est divisé en deux pour former un débit 9 qui se liquéfie et est envoyé au système de colonnes et un débit 11. Le débit 11 quitte la ligne d'échange 7 à la température T1 différent d'au plus ±5°C de la température de vaporisation de l'oxygène pressurisé 33 et est envoyé à un surpresseur froid 13 pour produire un débit 15 à une pression très sensiblement supérieure à la moyenne pression et éventuellement supérieure à la pression principale. Le débit 15 à une température T2 de sortie de surpresseur froid se refroidit dans la ligne d'échange 7 jusqu'à une température T3 plus élevée que T1. A cette température T3, le débit 15 est divisé en deux débits 17, 19. Le débit 17 est détendu dans une turbine 21 à partir de la température T3 proche de la température de pseudo vaporisation de l'oxygène pressurisé 33.In Figure 1, 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. At this main pressure 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. 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. 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.
La pression d'aspiration de la turbine 21 est égale à la pression de refoulement du surpresseur 13 donc très sensiblement supérieure à la moyenne pression (supérieure d'au moins 5 bars) et éventuellement supérieure à la pression principale et la pression de refoulement est supérieure ou égale à la moyenne pression, préférablement sensiblement égale à la moyenne pression. Le débit détendu jusqu'à une pression supérieure ou égale à la moyenne pression, préférablement sensiblement égale à la moyenne pression est envoyé au système de colonne comme débit 25. Le débit 19 poursuit son refroidissement dans la ligne d'échange et est envoyé sous forme gazeuse au système de colonnes.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 rate expanded to a pressure greater than or equal to the average pressure, preferably substantially equal to the average pressure, is sent to the column system as the flow rate 25. The flow 19 continues cooling in the exchange line and is sent in the form gaseous to the column system.
Le surpresseur froid 13 est entraîné par la turbine 21.The cold booster 13 is driven by the turbine 21.
Un débit d'azote résiduaire se réchauffe dans la ligne d'échange. Un débit d'oxygène liquide 35 pressurisé dans une pompe 33 se vaporise dans la ligne d'échange 7.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.
Optionnellement un liquide du système de colonnes, autre que l'oxygène liquide, est pressurisé, vaporisé dans la ligne d'échange 7 et sert ensuite de produit sous pression.Optionally a liquid column system, other than liquid oxygen, is pressurized, vaporized in the exchange line 7 and then serves as a product under pressure.
Selon un premier mode de fonctionnement, une fraction d'air 25 est prélevé dans l'air épuré 5 à la pression principale et est refroidi dans la ligne d'échange 7. A une température T4 inférieure à -10O0C et supérieure à T2, la fraction 25 est envoyée à une turbine 27 où elle se détend jusqu'à une température T5 formant un débit d'air 29. Ce débit d'air se réchauffe dans la ligne d'échange.According to a first mode of operation, a fraction of air 25 is taken from the purified air 5 at the main pressure and is cooled in the exchange line 7. At a temperature T4 lower than -10O 0 C and greater than T2 the fraction 25 is sent to a turbine 27 where it expands to a temperature T5 forming an air flow 29. This air flow is heated in the exchange line.
Un produit liquide est soutiré du système de colonnes comme produit final 32. Dans l'exemple le seul produit de l'appareil est de l'oxygène liquide mais d'autres produits peuvent évidemment être produits sous forme liquide. Selon un deuxième mode de fonctionnement le débit d'air 25 traité dans la turbine auxiliaire 27 est réduit éventuellement à zéro, le débit d'air principal entrant 1 est réduit d'un débit au moins égal à la réduction du débit d'air envoyée à la turbine auxiliaire 27 et la production de liquide 37 est diminuée éventuellement à zéro. Cette variation du débit d'air 1 entre les deux modes de fonctionnement est assurée par les aubages variables d'un compresseur et/ou par la mise en route et/ou l'arrêt d'un compresseur d'air auxiliaire.A liquid product is withdrawn from the column system as final product 32. In the example the only product of the apparatus is liquid oxygen but other products can obviously be produced in liquid form. According to a second mode of operation, 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 37 is reduced to zero if necessary. 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.
Ces deux modes de fonctionnement peuvent constituer les seuls modes de fonctionnement de l'appareil ou bien il peut y avoir d'autres modes de fonctionnement.These two modes of operation may be the only modes of operation of the apparatus or there may be other modes of operation.
Il peut y avoir une étape de compression (surpresseur 3B) entre la surpression chaude qui amène l'air à la pression principale et la surpression froide, de sorte que la surpression froide s'effectue à partir d'une pression au- dessus de la pression principale. De préférence, la turbine 21 est entraînée par le surpresseur 13 et le surpresseur 3 entraîne la turbine auxiliaire 27. There may be a compression step (booster 3B) between the hot booster which brings the air to the main pressure and the cold booster, so that the cold booster is from a pressure above the booster. main pressure. Preferably, the turbine 21 is driven by the booster 13 and the booster 3 drives the auxiliary turbine 27.
Claims
Priority Applications (6)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2009553189A JP5032596B2 (en) | 2007-03-13 | 2008-03-12 | Method and apparatus for producing gas from air in the form of gases and liquids with high flexibility by cryogenic distillation |
| US12/530,826 US20110011130A1 (en) | 2007-03-13 | 2008-03-12 | Method And Apparatus For The Production Of Gas From Air In Highly Flexible Gaseous And Liquid Form By Cryogenic Distillation |
| EP08775715.9A EP2118601B1 (en) | 2007-03-13 | 2008-03-12 | Method and apparatus for the production of gas from air in highly flexible gaseous and liquid form by cryogenic distillation |
| CN2008800071781A CN101883963B (en) | 2007-03-13 | 2008-03-12 | Method and apparatus for the production of gas from air in highly flexible gaseous and liquid form by cryogenic distillation |
| BRPI0808718-0A BRPI0808718B1 (en) | 2007-03-13 | 2008-03-12 | COOLING AND HEATING FLOW UNIT |
| RU2009137758/06A RU2479806C2 (en) | 2007-03-13 | 2008-03-12 | Method and machine for generating gas from air in gaseous and liquid form of high flexibility by method of cryogenic distillation |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR0753788A FR2913759B1 (en) | 2007-03-13 | 2007-03-13 | METHOD AND APPARATUS FOR GENERATING GAS AIR FROM THE AIR IN A GAS FORM AND LIQUID WITH HIGH FLEXIBILITY BY CRYOGENIC DISTILLATION |
| FR0753788 | 2007-03-13 |
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| WO2008129198A2 true WO2008129198A2 (en) | 2008-10-30 |
| WO2008129198A3 WO2008129198A3 (en) | 2011-07-07 |
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| PCT/FR2008/050418 Ceased WO2008129198A2 (en) | 2007-03-13 | 2008-03-12 | Method and apparatus for the production of gas from air in highly flexible gaseous and liquid form by cryogenic distillation |
Country Status (8)
| Country | Link |
|---|---|
| US (1) | US20110011130A1 (en) |
| EP (1) | EP2118601B1 (en) |
| JP (1) | JP5032596B2 (en) |
| CN (1) | CN101883963B (en) |
| BR (1) | BRPI0808718B1 (en) |
| FR (1) | FR2913759B1 (en) |
| RU (1) | RU2479806C2 (en) |
| WO (1) | WO2008129198A2 (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| JP2010536004A (en) * | 2007-08-10 | 2010-11-25 | 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 | Method and apparatus for separating air by cryogenic distillation |
| JP2010536003A (en) * | 2007-08-10 | 2010-11-25 | 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 | Method and apparatus for separating air by cryogenic distillation |
| FR2985305A1 (en) * | 2012-01-03 | 2013-07-05 | Air Liquide | Method for separation of air by cryogenic distillation for production of gas, involves pressurizing and vaporizing liquid flow in one of two exchange lines, and coupling cold booster with driving mechanism e.g. electrical motor |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2948184B1 (en) | 2009-07-20 | 2016-04-15 | Air Liquide | METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION |
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- 2008-03-12 CN CN2008800071781A patent/CN101883963B/en not_active Expired - Fee Related
- 2008-03-12 BR BRPI0808718-0A patent/BRPI0808718B1/en not_active IP Right Cessation
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| JP2010536003A (en) * | 2007-08-10 | 2010-11-25 | 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 | Method and apparatus for separating air by cryogenic distillation |
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Also Published As
| Publication number | Publication date |
|---|---|
| CN101883963A (en) | 2010-11-10 |
| EP2118601B1 (en) | 2017-12-20 |
| BRPI0808718A2 (en) | 2014-08-12 |
| WO2008129198A3 (en) | 2011-07-07 |
| EP2118601A2 (en) | 2009-11-18 |
| CN101883963B (en) | 2013-09-18 |
| JP5032596B2 (en) | 2012-09-26 |
| JP2010531424A (en) | 2010-09-24 |
| US20110011130A1 (en) | 2011-01-20 |
| BRPI0808718B1 (en) | 2019-09-24 |
| RU2479806C2 (en) | 2013-04-20 |
| FR2913759A1 (en) | 2008-09-19 |
| RU2009137758A (en) | 2011-04-20 |
| FR2913759B1 (en) | 2013-08-16 |
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