EP3179188A1 - Procédé de décomposition à basse température de l'air et installation de décomposition de l'air - Google Patents

Procédé de décomposition à basse température de l'air et installation de décomposition de l'air Download PDF

Info

Publication number
EP3179188A1
EP3179188A1 EP16020464.0A EP16020464A EP3179188A1 EP 3179188 A1 EP3179188 A1 EP 3179188A1 EP 16020464 A EP16020464 A EP 16020464A EP 3179188 A1 EP3179188 A1 EP 3179188A1
Authority
EP
European Patent Office
Prior art keywords
pressure
air
booster
level
column
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.)
Granted
Application number
EP16020464.0A
Other languages
German (de)
English (en)
Other versions
EP3179188B1 (fr
Inventor
Tobias Lautenschlager
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Publication of EP3179188A1 publication Critical patent/EP3179188A1/fr
Application granted granted Critical
Publication of EP3179188B1 publication Critical patent/EP3179188B1/fr
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—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
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—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
    • F25J3/04793—Rectification, e.g. columns; Reboiler-condenser
    • 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
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
    • F25J2200/06—Processes or apparatus using separation by rectification in a dual pressure main column system in a classical double column flow-sheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/40—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
    • 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

  • the invention relates to a process for the cryogenic separation of air in an air separation plant and to an air separation plant adapted for carrying out such a process according to the preambles of the independent patent claims.
  • gaseous pressure oxygen is needed, for the production of which air separation plants with so-called internal compression can be used.
  • Corresponding air separation plants are also a.a.O. described and explained with reference to the figure 2.3A there.
  • a cryogenic liquid in particular liquid oxygen, is brought to liquid pressure in the cryogenic state, vaporized against a heat carrier, and finally released as a gaseous pressure product.
  • the internal compression has, among other things, energetic advantages compared to a subsequent compression of an already gaseous at low pressure product present.
  • HAP high-air pressure
  • a HAP process is meant an air separation process in which the total amount of air fed into the distillation column system, also referred to herein as "feed air", is first compressed in a main air compressor to a pressure level well above the highest operating pressure in the distillation column system lies.
  • the air is first compressed to a pressure level which is at least 4 to 5 bar and up to 20 bar higher than the highest operating pressure in the distillation column system.
  • the "highest operating pressure” in the distillation column system is the operating pressure of the high-pressure column.
  • Air separation plants for HAP processes can be produced with particularly low investment costs because only one compressor is needed.
  • a so-called inductor current can be used.
  • a throttle flow as it is known in principle, is a partial flow of the compressed feed air, which can be further increased in pressure, is cooled, and a relaxation device, in particular a throttle valve, in the distillation column or its high-pressure column is expanded.
  • such a throttle flow can be further increased in pressure starting from the already high outlet pressure, to which the entire feed air is brought, by means of a hot and a cold booster.
  • a corresponding "warm booster” the air is supplied without or only after relatively little cooling, for example in a water cooler downstream of the main air compressor. An inlet temperature of such a warm booster is therefore well above 0 ° C.
  • a "cold booster” is one Booster, whose inlet temperature is well below 0 ° C by a previously performed cooling of the cold booster air supplied.
  • MAC / BAC Main Air Compressor / Booster Air Compressor
  • MAC / BAC Main Air Compressor / Booster Air Compressor
  • a part of the distillation column system supplied air is compressed only to the highest operating pressure in the distillation column system or at least slightly above, and another part by means of a Nachverêtrs brought to a higher pressure level.
  • Such methods are particularly advantageous if no or only small amounts of a liquid air product, for example liquid oxygen, are to be obtained by means of a corresponding method.
  • a MAC / BAC process using a so-called injection turbine that is a turbine which relaxes compressed air into the low-pressure column of the distillation column system, is particularly suitable.
  • the present invention proposes a method for the cryogenic separation of air in an air separation plant and a Implementation of such a method equipped air separation plant with the features of the independent claims before.
  • Preferred embodiments are subject of the dependent claims and the following description.
  • pressure level and "temperature level” to characterize pressures and temperatures, which is to express that pressures and temperatures in a given equipment need not be used in the form of exact pressure or temperature values to achieve this to realize innovative concept.
  • pressures and temperatures typically range in certain ranges that are, for example, ⁇ 1%, 5%, 10%, 20% or even 50% about an average.
  • Corresponding pressure levels and temperature levels can be in disjoint areas or in areas that overlap one another.
  • pressure levels include unavoidable pressure drops or expected pressure drops, for example, due to cooling effects or line losses.
  • the pressure levels specified here in bar are absolute pressures.
  • turbo compressors are used to compress the air. This applies, for example, to the "main air compressor”, which is characterized in that it compresses the entire quantity of air fed into the distillation column system, that is to say the entire feed air.
  • a “secondary compressor” in which part of the air quantity compressed in the main air compressor is brought to an even higher pressure in MAC / BAC process can also be designed as a turbocompressor.
  • turbocompressors are typically provided, which are also referred to as boosters, but make only a relatively small amount of compaction compared to the main air compressor or the booster compressor.
  • turboexpanders can also be coupled with turbo compressors or boosters and drive them. If one or more turbocompressors without externally supplied energy, ie driven only by one or more turbocompressors, is for such an arrangement and the Term "turbine booster" used. In a turbine booster, the turboexpander and the turbo compressor or booster are mechanically coupled.
  • rotating units for example expansion machines or expansion turbines, compressors or compressor stages, booster turbines or boosters, rotors of electric motors and the like, may be mechanically coupled to one another in a corresponding manner.
  • a "mechanical coupling” is understood to mean in the language used here that a fixed or mechanically adjustable speed relationship between such rotating units can be produced via mechanical elements such as gears, belts, gears and the like.
  • a mechanical coupling may generally be made by two or more elements engaged with each other, for example in form-engagement or frictional engagement, such as belts or traction sheaves with belts, or a non-rotatable connection.
  • a non-rotatable connection can in particular be effected via a common shaft, on which the rotating units are respectively secured against rotation. The rotational speed of the rotating units is the same in this case.
  • corresponding units are "mechanically uncoupled” if there is no fixed or mechanically adjustable speed relationship between corresponding elements.
  • certain speed relationships are given. However, these are not caused by two or more, in each case engaged with each other, for example in the form of engagement or frictional engagement, standing elements or by a rotationally fixed connection.
  • turbocompressors and turboexpanders The mechanical structure of turbocompressors and turboexpanders is known to those skilled in principle.
  • a turbocompressor the air is compressed by means of blades which are arranged on an impeller or directly on a shaft.
  • a turbocompressor forms a structural unit, which, however, can have several "compressor stages".
  • a compressor stage typically includes an impeller or a corresponding array of blades. All of these compressor stages can be driven by a common shaft.
  • a turboexpander is designed basically comparable, with the blades however, be powered by the expanding air. Again, several expansion stages can be provided.
  • Turbo compressor and turboexpander can be designed as radial or axial machines.
  • a “product” leaves the described plant and is stored or consumed, for example, in a tank. So it no longer only participates exclusively in the plant-internal circuits, but can be used accordingly before leaving the plant, for example as a refrigerant in a heat exchanger.
  • the term “product” thus does not include such fractions or streams that remain in the plant itself and are used exclusively there, for example as reflux, coolant or purge gas.
  • the present invention is based on the recognition that the use of serially arranged cold boosters, between which the air to be compressed of the inductor current is not cooled, allows a particularly efficient and at least the exergetic advantages of conventional MAC / BAC processes exhibiting HAP process.
  • the heat exchange profiles in a main heat exchanger which is used in an air separation plant operated according to the invention, prove to be particularly favorable, in particular compared to heat exchange profiles, as obtained in known processes in which an intermediate cooling between cold booster.
  • the present invention is based on the recognition that use of a warm booster upstream of the cold booster offers particular advantages.
  • the three booster compress the multiple explained throttle current, but no further currents. Between the warm booster on the one hand and the serially arranged cold boosters on the other hand and downstream of the cold booster in particular a cooling in the main heat exchanger is made.
  • the present invention proposes a process for the cryogenic separation of air using an air separation plant comprising a distillation column system having a high pressure column operated at a high pressure column pressure level and a low pressure column operating at a low pressure column pressure level having.
  • the high-pressure column pressure level can be, for example, 4 to 7 bar, as is customary in corresponding air separation plants.
  • the low pressure column pressure level is just above the atmospheric pressure, in particular at 1.2 to 1.8 bar, in order to ensure, for example, a good separation efficiency and a discharge in the low-pressure column accumulating air products without additional pumps.
  • the process according to the invention first comprises the step of first compressing the total air fed into the distillation column system to an initial pressure level which is at least 4 and up to 20 bar above the high-pressure column pressure.
  • the total amount of air can be compressed to a pressure level of 10 to 23 bar.
  • the compressed air can be subjected to drying and cleaning, in particular using molecular sieve.
  • a portion of the compressed to the output pressure level and accordingly dried and purified air is then subjected to a first pressure increase to a lying above 0 ° C first temperature level and then two further pressure increases lying below the first temperature level temperature levels.
  • the air subjected to the first pressure increase can be cooled in this case in particular after the first pressure increase in a main heat exchanger of a corresponding air separation plant.
  • the corresponding air is therefore subjected to further pressure increases to correspondingly lower temperature levels.
  • the air subjected to the two further pressure increases is then released into the high-pressure column.
  • a throttle valve is used for relaxation.
  • the air that has been subjected to the two further pressure increases and previously the first pressure increase is therefore a so-called "throttle flow", as it is generally known in the field of air separation.
  • the low-pressure column is removed from a cryogenic, oxygen-rich liquid, subjected to an increase in pressure in the cryogenic state, then heated and evaporated and discharged from the air separation plant as a printed product.
  • the method according to the invention is therefore an air separation process in which a so-called internal compression of oxygen or of a corresponding oxygen-rich printed product takes place.
  • a first booster ie a "warm” booster, as explained several times
  • the first booster is driven using a first expansion machine, in which another part of the compressed to the output pressure level Air is released from the initial pressure level to the second pressure level, which is then fed into the low pressure column.
  • the first expansion machine is thus functionally a so-called “injection turbine” or “Lachmann turbine”, as it is also known from the field of air separation.
  • An appropriate air injection into the low-pressure column improves the energy efficiency.
  • a second booster and a third booster are used, is passed through the air for the two further pressure increases in succession, the air to the third booster at a temperature level is fed on which she leaves the second booster.
  • a second booster and a third booster ie two "cold" booster
  • the air to the third booster at a temperature level is fed on which she leaves the second booster.
  • the total amount of air passed through the first booster, the second booster and the third booster and optionally through the throttle valve according to the invention differ by no more than 10% from each other.
  • these amounts of air may differ by no more than 5%, or be substantially or completely identical.
  • the amounts of air respectively subjected to the first and the two further pressure increases, and optionally also the amount of air expanded in the throttle valve are similar or equal to the extent explained.
  • the present invention unfolds its advantages when the low-pressure column taken, deep cold oxygen-rich liquid is subjected in cryogenic condition of a pressure increase to 6 to 25 bar. A corresponding increase in pressure is therefore provided according to the invention.
  • conventional MAC / BAC processes are conventionally more favorable in such pressure ranges on which an internally compressed oxygen product is provided.
  • the present invention makes it possible to achieve corresponding advantages also in HAP processes by the mentioned use of the serial booster without intermediate cooling.
  • the invention exhibits its advantages when a low liquid production is made, i. Air products in a proportion of at most 1% or 0%, based on the total amount of air fed into the distillation column system, are discharged from the liquid separation plant liquid. This is therefore provided according to the invention. Furthermore, a relatively small amount of nitrogen-rich air products is formed. These nitrogen-rich air products are those which are taken from the high-pressure column of the distillation column system near the head or at the top and are used neither as reflux to the high-pressure column or the low-pressure column.
  • nitrogen-rich air products are taken from the high-pressure column at a fraction of at most 2%, based on the total amount of air fed into the distillation column system, and discharged from the air separation plant in gaseous form.
  • the second booster and the third booster are advantageously each driven by means of expansion machines, in which a further part of the compressed to the output pressure level air is released, which was previously cooled and then, ie after the relaxation in said expansion machines, in the distillation column system is fed.
  • a third expansion machine is used to drive the second booster while a second expansion machine and to drive the third booster.
  • corresponding expansion machines are connected in parallel, ie the air used for the drive of the expansion machines is previously divided into two streams. In this way, the relaxed amount of air in each case the required pressure increase in the corresponding, connected to the relaxation machines cold booster can be adjusted and vice versa.
  • the drive of the cold booster takes place by means of the respective expansion machines via a suitable mechanical coupling.
  • corresponding booster could also drive motor, a drive via corresponding expansion machines, however, is particularly advantageous in terms of investment costs and the heat input into a corresponding system.
  • the relaxation of the air in the expansion machines takes place on the high-pressure column pressure level.
  • a partial liquefaction of the air can take place.
  • a gaseous fraction can be fed directly into the high-pressure column and the liquefied fraction can be expanded into the low-pressure column.
  • the liquefied portion can be used in this way as reflux to the low pressure column and there contributes to improving the separation performance, as explained for example in Kerry in Section 2.6, "Theoretical Analysis of the Claude Cycle".
  • the present invention allows further optimizations.
  • a portion of the air compressed to the outlet pressure level may be cooled and discharged from the outlet pressure level, i. without further pressure increase by boosters and the like, are relaxed in the high-pressure column. This can be done in particular via a further expansion valve.
  • the air that is supplied to the second booster be previously cooled in the main heat exchanger to a temperature level of 130 to 200 K.
  • the air that relaxes in the relaxation machines, the second booster and drive the third booster is particularly previously cooled to a temperature level of 120 to 190 K.
  • the air which is released in the first expansion machine which drives the first booster is in particular previously cooled to a temperature level of 150 to 230 K.
  • the pressure increased in the third booster air is advantageously after the local pressure increase and before its relaxation in the high-pressure column to a temperature level of 97 to 105 K, ie the lowest temperature level, which is provided by means of a corresponding main heat exchanger, cooled.
  • a pressure increase by 10 to 25 bar and by means of the third booster advantageously a pressure increase by 5 to 20 bar causes.
  • the present invention also extends to an air separation plant for cryogenic separation of air comprising a distillation column system having a high pressure column arranged for operation at a high pressure column pressure level and a low pressure column arranged for operation at a low pressure column pressure level.
  • the air separation plant in this case comprises means which are adapted to compress the total, fed into the distillation column system initially to an outlet pressure level which is at least 4 and up to 20 bar above the high pressure column pressure level, a portion of the compressed air to the output pressure level of a first pressure increase at a temperature above 0 ° C first temperature and then subjecting two further pressure increases to lying below the first temperature level temperature levels and then relax using a throttle valve in the high pressure column, and the low pressure column to take a deep cold, oxygen-rich liquid, this in Tiefkaltem state subject to a pressure increase, then to heat and evaporate and out of the air separation plant.
  • a first booster is provided for the first pressure increase, which is mechanically coupled to a first expansion machine, wherein means are provided which are adapted to a further portion of compressed to the output pressure level air in the first expansion machine from the output pressure level to the low pressure column pressure level relax and then feed into the low-pressure column,
  • a second booster and a third booster are provided for the two further pressure increases, and means are provided which are adapted to guide the air for the two further pressure increases successively through the second booster and the third booster and thereby the air to the third Booster at a temperature level on which she leaves the second booster.
  • Means are provided which are adapted to lead in each case by the first booster, the second booster and the third booster in total amounts of air that differ by no more than 10% from each other.
  • means are provided which are adapted to the pressure increase, which is subjected to the low pressure column taken deep cryogenic, oxygen-rich liquid in cryogenic condition, in the form of a pressure increase to 6 to 25 bar.
  • the air separation plant is adapted to provide liquid products in a proportion of at most 1%, based on the total amount of air fed into the distillation column system, liquid and advantageously nitrogen-rich air products in a proportion of at most 2%, based on the total amount of air fed into the distillation column system to remove the high pressure column and provide it in gaseous form.
  • FIG. 1 an air separation plant according to a particularly preferred embodiment of the invention is illustrated in the form of a schematic process flow diagram and denoted overall by 100.
  • the air separation plant 100 is supplied by means of a Lucasverdichtungs- and cleaning unit 1, which comprises a main air compressor and a suitable cleaning system and is shown here very schematically, a compressed air flow a.
  • a compressed air flow a In the FIG. 1 illustrated air separation plant is set up for a so-called HAP process.
  • the compressed air flow a which comprises all the air fed into a distillation column system 10 of the air separation plant 100, is compressed to a pressure level which is at least 4 and up to 20 bar above the pressure level on which a high-pressure column 11 of the distillation column system 10 is operated.
  • the pressure level of the flow a is referred to herein as the "outlet pressure level", the pressure level of the high pressure column 11 as the “high pressure column pressure level”.
  • the outlet pressure level a total of four partial flows are formed from the air of the compressed air flow a, which are designated here by b, c, d and e.
  • the air of the partial flow b is first subjected to an increase in pressure in a booster 2.
  • the pressure increase in the booster 2 which is also referred to here as “first pressure increase”, takes place at well above 0 ° C, which is why the booster 2 is conventionally also referred to as "warm booster".
  • the air of the partial flow b is cooled in an aftercooler 3 and then fed to the hot side a main heat exchanger 4 of the air separation plant 100.
  • the air of the partial flow b is taken from the main heat exchanger 4 (see link A) at an intermediate temperature level which is well below 0 ° C.
  • the corresponding cooled air of the partial flow b is then two more Subjected to pressure increases.
  • the air of the partial flow b is first passed through a booster 5 and then through a booster 6.
  • the booster 5 is referred to here as "second”, the booster 6 as a "third" booster.
  • Both booster 5, 6 are operated at temperature levels well below 0 ° C and in particular at temperature levels below the first temperature level of the booster 2. They are therefore also referred to as "cold booster".
  • the air of the partial flow b is supplied to the third booster 6 at a temperature level at which it leaves the second booster 5. Thus, there is no intermediate cooling between the second booster 5 and the third booster 6. After the pressure increase in the booster 6, the air of the partial flow b at the temperature level at which it leaves the third booster 6, again fed to the main heat exchanger 4 and this cold side taken.
  • the booster 5 and 6 are driven by expansion machines 7 and 8, in which air of the partial flow c, which is divided into sub-streams f and g, is used for this purpose.
  • the air of the partial flow c is in this case first supplied to the main heat exchanger on the warm side and this taken at an intermediate temperature level, before being divided into the mentioned partial flows f and g and the expansion machines 7, 8 is supplied.
  • the air of the partial flow d is supplied to the main heat exchanger 4 on the warm side and removed cold side, the air of the partial flow e is supplied to the main heat exchanger 4 warm side, taken at an intermediate temperature level and used in a relaxation machine 9 for driving the booster 2.
  • the expanded air of the partial flows f and g is transferred to a separation tank 13, in which a liquid phase separates.
  • the liquid phase is expanded (see link B) in the form of a stream h into the low-pressure column 12.
  • the gaseous remaining portion of the air of the currents f and g is fed in the form of a current i in the high-pressure column 11.
  • the air of the partial streams b and d is released via valves 14 and 15 into the high-pressure column 11.
  • an oxygen-enriched, liquid bottom product and a nitrogen-enriched, gaseous top product is formed using air of the streams b, d and i.
  • the oxygen-enriched liquid bottom product of the high pressure column 11 is at least partially removed in the form of a stream k, passed through the subcooling countercurrent 16 and expanded into the low pressure column 12.
  • the nitrogen-enriched, gaseous overhead product is at least partially withdrawn in the form of stream I.
  • a part thereof may be heated in the form of the flow m in the main heat exchanger 4 and executed as a nitrogen-rich pressure product from the air separation plant 100 or used for example as a sealing gas in a main air compressor of the air compression and purification unit 1.
  • a further portion of the current I can be at least partially liquefied in a main capacitor 17 which connects the high-pressure column and the low-pressure column in a heat-exchanging manner.
  • a portion of the corresponding liquefaction product can be returned to the high-pressure column 11 as reflux, another proportion in the form of the current n passed through the supercooling countercurrent 16 and expanded into the low-pressure column 12.
  • an oxygen-rich liquid bottom product and a gaseous top product are formed in the low-pressure column 12.
  • the oxygen-rich liquid bottom product of the low-pressure column 12 can be withdrawn at least partially in the form of the flow o from the high-pressure column 12, increased in pressure by means of a pump 18 in the liquid state, heated in the main heat exchanger 4 and evaporated and executed as internally compressed oxygen pressure product from the air separation plant 100.
  • the gaseous top product of the low-pressure column 12 can be withdrawn at least partially in the form of the stream p as so-called impure nitrogen, passed through the supercooling countercurrent 16, heated in the main heat exchanger 4 and used, for example, as a regeneration gas for adsorbers in the air compression and purification unit 1.
  • FIG. 1 illustrated operation of the air separation plant 100 results in a particularly advantageous heat exchange in the main heat exchanger 4, when the other conditions described above are met. This is based on the in FIGS. 2 and 3 illustrated Q / T diagrams illustrated.
  • FIG. 2 In this case, a corresponding Q / T diagram is shown for the case in which the oxygen-rich fluid of the flow o in the pump 18 of the air separation plant 100 is compressed to a pressure level of approximately 15.0 bar
  • FIG. 3 a corresponding Q / T diagram is illustrated at a pressure of about 10.0 bar.
  • a temperature in K on the abscissa against an enthalpy (sum) of the heat exchanger in MW is plotted on the ordinate.
  • 201 in each case a state change curve or cumulative curve of the warm, with 202 a state change curve or cumulative curve of the cold medium, here to be heated oxygen-rich fluid of the current o, respectively.
  • the state change curves or cumulative curves 201 and 202 are very close to each other due to the operation according to the invention of a corresponding air separation plant.
  • the process in the main heat exchanger is particularly advantageous in the illustrated sense or, in such a case, the entire system can be operated in a particularly energy-optimized manner.

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)
EP16020464.0A 2015-12-07 2016-11-24 Procédé de décomposition à basse température de l'air et installation de décomposition de l'air Active EP3179188B1 (fr)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP15003482.5A EP3179185A1 (fr) 2015-12-07 2015-12-07 Procede de separation cryogenique de l'air et installation de separation d'air

Publications (2)

Publication Number Publication Date
EP3179188A1 true EP3179188A1 (fr) 2017-06-14
EP3179188B1 EP3179188B1 (fr) 2019-01-30

Family

ID=54838146

Family Applications (2)

Application Number Title Priority Date Filing Date
EP15003482.5A Withdrawn EP3179185A1 (fr) 2015-12-07 2015-12-07 Procede de separation cryogenique de l'air et installation de separation d'air
EP16020464.0A Active EP3179188B1 (fr) 2015-12-07 2016-11-24 Procédé de décomposition à basse température de l'air et installation de décomposition de l'air

Family Applications Before (1)

Application Number Title Priority Date Filing Date
EP15003482.5A Withdrawn EP3179185A1 (fr) 2015-12-07 2015-12-07 Procede de separation cryogenique de l'air et installation de separation d'air

Country Status (4)

Country Link
EP (2) EP3179185A1 (fr)
CN (1) CN106931721B (fr)
RU (1) RU2721195C2 (fr)
TR (1) TR201905990T4 (fr)

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
US20050126221A1 (en) * 2003-12-10 2005-06-16 Bao Ha Process and apparatus for the separation of air by cryogenic distillation
DE102007014643A1 (de) * 2007-03-27 2007-09-20 Linde Ag Verfahren und Vorrichtung zur Erzeugung von gasförmigem Druckprodukt durch Tieftemperaturzerlegung von Luft
EP2520886A1 (fr) * 2011-05-05 2012-11-07 Linde AG Procédé et dispositif de production d'un produit comprimé à oxygène gazeux par décomposition à basse température d'air
US20130255313A1 (en) * 2012-03-29 2013-10-03 Bao Ha Process for the separation of air by cryogenic distillation
WO2015082860A2 (fr) * 2013-12-05 2015-06-11 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et appareil de séparation d'air par distillation cryogénique
EP3101374A2 (fr) * 2015-06-03 2016-12-07 Linde Aktiengesellschaft Procede et installation cryogeniques de separation d'air

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2054609C1 (ru) * 1990-12-04 1996-02-20 Балашихинское научно-производственное объединение криогенного машиностроения им.40-летия Октября "Криогенмаш" Способ разделения воздуха
FR2895068B1 (fr) * 2005-12-15 2014-01-31 Air Liquide Procede de separation d'air par distillation cryogenique
DE102006012241A1 (de) * 2006-03-15 2007-09-20 Linde Ag Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
US20050126221A1 (en) * 2003-12-10 2005-06-16 Bao Ha Process and apparatus for the separation of air by cryogenic distillation
DE102007014643A1 (de) * 2007-03-27 2007-09-20 Linde Ag Verfahren und Vorrichtung zur Erzeugung von gasförmigem Druckprodukt durch Tieftemperaturzerlegung von Luft
EP2520886A1 (fr) * 2011-05-05 2012-11-07 Linde AG Procédé et dispositif de production d'un produit comprimé à oxygène gazeux par décomposition à basse température d'air
US20130255313A1 (en) * 2012-03-29 2013-10-03 Bao Ha Process for the separation of air by cryogenic distillation
WO2015082860A2 (fr) * 2013-12-05 2015-06-11 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et appareil de séparation d'air par distillation cryogénique
EP3101374A2 (fr) * 2015-06-03 2016-12-07 Linde Aktiengesellschaft Procede et installation cryogeniques de separation d'air

Non-Patent Citations (3)

* Cited by examiner, † Cited by third party
Title
"Industrial Gases Processing", 2006, WILEY-VCH, article "Cryogenic Rectification"
F.G. KERRY: "Industrial Gas Handbook: Gas Separation and Purification", 2006, CRC PRESS, article "The Lachmann Principle"
KERRY: "Theoretical Analysis of the Claude Cycle", ABSCHNITT

Also Published As

Publication number Publication date
EP3179188B1 (fr) 2019-01-30
TR201905990T4 (tr) 2019-05-21
RU2016147700A3 (fr) 2020-03-05
CN106931721A (zh) 2017-07-07
RU2721195C2 (ru) 2020-05-18
CN106931721B (zh) 2020-12-01
EP3179185A1 (fr) 2017-06-14
RU2016147700A (ru) 2018-06-08

Similar Documents

Publication Publication Date Title
EP3175192A1 (fr) Procédé de séparation cryogénique de l'air et installation de séparation d'air
EP3179187B1 (fr) Procédé de production d'un produit comprime riche en oxygène, gazeux et liquide dans une installation de décomposition de l'air et installation de décomposition de l'air
EP1994344A1 (fr) Procédé et dispositif de décomposition de l'air à basse température
EP3101374A2 (fr) Procede et installation cryogeniques de separation d'air
EP3410050B1 (fr) Procédé de production d'un ou de plusieurs produits pneumatiques et installation de séparation d'air
EP3343158A1 (fr) Procédé de production d'un ou plusieurs produits pneumatiques et unité de fractionnement d'air
EP2963370A1 (fr) Procede et dispositif cryogeniques de separation d'air
EP2835507B1 (fr) Procédé pour la production d'énergie électrique et installation de production d'énergie
EP2963369B1 (fr) Procede et dispositif cryogeniques de separation d'air
EP3019804A2 (fr) Procédé de production d'au moins un produit dérivé de l'air, installation de décomposition d'air, procédé et dispositif de production d'énergie électrique
EP3924677A1 (fr) Procédé et installation pour fournir un ou plusieurs produits présents dans l'air, gazeux et à teneur élevée en oxygène
EP3034974A1 (fr) Procédé et installation de liquéfaction d'air et de stockage et de récupération d'énergie électrique
EP3179188B1 (fr) Procédé de décomposition à basse température de l'air et installation de décomposition de l'air
EP2824407A1 (fr) Procédé de génération d'au moins un produit de l'air, installation de décomposition de l'air, procédé et dispositif de production d'énergie électrique
DE202021002895U1 (de) Anlage zur Tieftemperaturzerlegung von Luft
EP4133227A2 (fr) Procédé de séparation d'air à basse température, installation de séparation d'air et ensemble composé d'au moins deux installations de séparation d'air
WO2019214847A9 (fr) Procédé pour produire un ou plusieurs produit(s) formés à partir d'air et installation de séparation d'air
DE202015004181U1 (de) Luftzerlegungsanlage und Steuereinrichtung für Luftzerlegungsanlage
EP3870916B1 (fr) Procédé de production d'un produit ou d'une pluralité de produits de l'air et installation de séparation de l'air
EP2835506A1 (fr) Procédé pour la production d'énergie électrique et installation de production d'énergie
EP2784420A1 (fr) Procédé de séparation de l'air et installation de séparation de l'air
EP3671085A1 (fr) Dispositif et procédé de récupération de la chaleur de compression à partir de l'air comprimé et traité dans une installation de traitement de l'air
WO2023030689A1 (fr) Procédé pour obtenir un ou plusieurs produits de l'air et installation de séparation d'air
EP3870917B1 (fr) Procédé et installation de séparation cryogénique d'air
EP4127583B1 (fr) Procédé et installation de séparation d'air à basse température

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

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

Free format text: STATUS: THE APPLICATION HAS BEEN PUBLISHED

AK Designated contracting states

Kind code of ref document: A1

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

AX Request for extension of the european patent

Extension state: BA ME

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

Free format text: STATUS: REQUEST FOR EXAMINATION WAS MADE

17P Request for examination filed

Effective date: 20171206

RBV Designated contracting states (corrected)

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

GRAP Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOSNIGR1

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

Free format text: STATUS: GRANT OF PATENT IS INTENDED

INTG Intention to grant announced

Effective date: 20180815

GRAS Grant fee paid

Free format text: ORIGINAL CODE: EPIDOSNIGR3

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

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

Free format text: STATUS: THE PATENT HAS BEEN GRANTED

AK Designated contracting states

Kind code of ref document: B1

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

REG Reference to a national code

Ref country code: GB

Ref legal event code: FG4D

Free format text: NOT ENGLISH

REG Reference to a national code

Ref country code: CH

Ref legal event code: EP

REG Reference to a national code

Ref country code: AT

Ref legal event code: REF

Ref document number: 1093619

Country of ref document: AT

Kind code of ref document: T

Effective date: 20190215

REG Reference to a national code

Ref country code: IE

Ref legal event code: FG4D

Free format text: LANGUAGE OF EP DOCUMENT: GERMAN

REG Reference to a national code

Ref country code: DE

Ref legal event code: R096

Ref document number: 502016003246

Country of ref document: DE

REG Reference to a national code

Ref country code: LT

Ref legal event code: MG4D

REG Reference to a national code

Ref country code: NL

Ref legal event code: MP

Effective date: 20190130

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: FI

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20190130

Ref country code: PT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20190530

Ref country code: NO

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20190430

Ref country code: SE

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20190130

Ref country code: PL

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20190130

Ref country code: LT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20190130

Ref country code: ES

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20190130

Ref country code: NL

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20190130

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: HR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20190130

Ref country code: GR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20190501

Ref country code: LV

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20190130

Ref country code: BG

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20190430

Ref country code: IS

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20190530

Ref country code: RS

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20190130

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20190130

Ref country code: DK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20190130

Ref country code: CZ

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20190130

Ref country code: RO

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20190130

Ref country code: EE

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20190130

Ref country code: IT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20190130

Ref country code: AL

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20190130

REG Reference to a national code

Ref country code: DE

Ref legal event code: R097

Ref document number: 502016003246

Country of ref document: DE

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SM

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20190130

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

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

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

26N No opposition filed

Effective date: 20191031

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SI

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20190130

REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

REG Reference to a national code

Ref country code: DE

Ref legal event code: R081

Ref document number: 502016003246

Country of ref document: DE

Owner name: LINDE GMBH, DE

Free format text: FORMER OWNER: LINDE AKTIENGESELLSCHAFT, 80331 MUENCHEN, DE

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LU

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20191124

Ref country code: LI

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20191130

Ref country code: MC

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20190130

Ref country code: CH

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20191130

REG Reference to a national code

Ref country code: BE

Ref legal event code: MM

Effective date: 20191130

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: IE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20191124

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: BE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20191130

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: TR

Payment date: 20201117

Year of fee payment: 5

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 20201125

Year of fee payment: 5

Ref country code: FR

Payment date: 20201119

Year of fee payment: 5

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: CY

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20190130

GBPC Gb: european patent ceased through non-payment of renewal fee

Effective date: 20201124

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: HU

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT; INVALID AB INITIO

Effective date: 20161124

Ref country code: MT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20190130

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GB

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20201124

REG Reference to a national code

Ref country code: DE

Ref legal event code: R119

Ref document number: 502016003246

Country of ref document: DE

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: MK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20190130

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20220601

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: FR

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20211130

REG Reference to a national code

Ref country code: AT

Ref legal event code: MM01

Ref document number: 1093619

Country of ref document: AT

Kind code of ref document: T

Effective date: 20211124

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: AT

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20211124