EP3164654B1 - Procédé et dispositif de fractionnement de l'air à basse température à consommation d'énergie variable - Google Patents

Procédé et dispositif de fractionnement de l'air à basse température à consommation d'énergie variable Download PDF

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Publication number
EP3164654B1
EP3164654B1 EP15735849.0A EP15735849A EP3164654B1 EP 3164654 B1 EP3164654 B1 EP 3164654B1 EP 15735849 A EP15735849 A EP 15735849A EP 3164654 B1 EP3164654 B1 EP 3164654B1
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Prior art keywords
pressure
air
compressed
compressor
flow
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EP15735849.0A
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German (de)
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EP3164654A1 (fr
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Dimitri GOLUBEV
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Linde GmbH
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Linde GmbH
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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
    • F25J3/04012—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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04024—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of purified feed air, so-called boosted air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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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
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    • F25J3/0403—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 nitrogen
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    • 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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    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of nitrogen
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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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    • F25J3/04—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
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    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/042—Division of the main heat exchange line in consecutive sections having different functions having an intermediate feed connection
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    • 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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    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
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    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
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    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
    • F25J2240/42—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval the fluid being air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen

Definitions

  • the invention relates to a method and a device for the variable extraction of a compressed gas product by means of low-temperature separation of air.
  • the distillation column system of such a system can be designed as a two-column system (for example as a classic Linde double-column system), or as a three- or more-column system.
  • it can have further devices for obtaining highly pure products and / or other air components, in particular noble gases, for example argon extraction and / or krypton-xenon extraction.
  • a liquid product stream which is brought under pressure is vaporized against a heat transfer medium and finally obtained as an internally compressed compressed gas product.
  • This method is also known as internal compression. It is used to obtain gaseous printed products.
  • the product stream is then "pseudo-evaporated".
  • the product stream can be, for example, an oxygen product from the low-pressure column of a two-column system or a nitrogen product from the high-pressure column of a two-column system or from the liquefaction chamber of a main condenser, via which the high-pressure column and low-pressure column are in heat-exchanging connection
  • a heat carrier under high pressure is liquefied against the (pseudo) evaporating product stream (or pseudo-liquefied if it is under supercritical pressure).
  • the heat transfer medium is often by part of the Air formed, in the present case from the "second partial flow" of the compressed feed air.
  • DE 102010052545 A1 shows a stationary internal compression process, in which an air flow in the main heat exchanger is warmed up and returned to the main air compressor.
  • the invention relates in particular to systems in which the total feed air is at a pressure which is clearly above the highest distillation pressure which prevails inside the columns of the distillation column system (this is normally the high-pressure column pressure.
  • the "first pressure” is between 17 and 25 bar, for example.
  • the main air compressor is regularly the only machine powered by external energy to compress air.
  • a "single machine” is understood here to mean a single-stage or multi-stage compressor, the stages of which are all connected to the same drive, all stages in are housed in the same housing or connected to the same gearbox.
  • MAC-BAC processes in which the air in the main air compressor is compressed to a relatively low total air pressure, for example to the operating pressure of the high pressure column (plus line losses). Part of the air from the main air compressor is compressed to a higher pressure in a booster air compressor driven by external energy (BAC).
  • BAC external energy
  • This task can be accomplished relatively well with a conventional MAC-BAC method, since both compressors (MAC and BAC) are responsible for functionally separate tasks.
  • the main air compressor only supplies the feed air for disassembly; the air post-compressor supplies energy for internal compression (GOXIV, GANIV) and for liquid production. Both machines can usually be controlled relatively easily between 70% and 100%.
  • the invention is based on the object of specifying a method and a corresponding device which combine the advantages of HAP methods with flexibility such as is known in a similar way to MAC-BAC methods.
  • “Flexibility” is understood here in particular to mean that the system can be operated not only with low energy in a certain production quantity of internally compressed product, but also in a relatively wide load range with approximately constant low specific energy consumption. In particular, the production of other air separation products should remain the same, or at least change less than the product quantity of the internal compression product.
  • part of the quantity of feed air is bypassed the entire distillation column system. This quantity then does not take part in the generation of the first product stream, but can nevertheless be directed through the first turbine in order to produce enough cold or to supply the system with enough energy to be able to maintain or at least reduce the liquid production relatively less than the amount of the first print production.
  • the excess air is not fed into the distillation column system, but is fed back into the heat exchanger immediately after expansion in the turbine and then fed to a suitable point (for example after the second or third stage) of the main air compressor without throttling.
  • a suitable point for example after the second or third stage of the main air compressor without throttling.
  • Another possibility is to guide and separate the excess air into the distillation column system. This other possibility is not part of the invention claimed here.
  • the argon present in this amount of air can be obtained.
  • the excess amount of oxygen can be taken as low-pressure oxygen from the low-pressure column and fed to the UN2 stream. In principle, you only lose the separation work to obtain additional oxygen molecules, but at the same time significantly more argon is produced.
  • an oxygen gas stream can be taken from the lower region of the low-pressure column, mixed with a nitrogen-enriched stream from the upper region of the low-pressure column, and the mixture can be warmed in the main heat exchanger.
  • Electricity from the upper area of the low pressure column is mixed and the mixture is warmed up in the main heat exchanger.
  • a second air turbine can be used, a third partial stream of the feed air compressed in the main air compressor being cooled to an intermediate temperature in a main heat exchanger and relaxed in the second air turbine in a work-performing manner, and at least a first part of the third partial stream being relaxed in the work Distillation column system is initiated.
  • the second partial flow of the feed air compressed in the main air compressor can be cooled to an intermediate temperature in the main heat exchanger, can be post-compressed in a second post-compressor, which is operated as a cold compressor and driven by the second turbine, to a third pressure which is higher than the first pressure.
  • a second post-compressor which is operated as a cold compressor and driven by the second turbine, to a third pressure which is higher than the first pressure.
  • cooled in the main heat exchanger (pseudo) liquefied and then expanded and introduced into the distillation column system.
  • the pressure of the second partial stream can be increased further without using external energy.
  • a correspondingly higher internal compression pressure can be achieved.
  • a fourth partial flow of the air compressed in the main air compressor can be cooled under the first pressure in the main heat exchanger and then expanded and introduced into the distillation column system.
  • the heat exchange process in the main heat exchanger is further optimized by such a second throttle flow.
  • the amount of air used in the cold box is "artificially" increased, which means that more air is driven into the low-temperature part of the system than is necessary to obtain the pressurized oxygen products specified for this operating case. If the feed air is run in "excess", the pressure at the compressor outlet can be reduced, since the energy supply for the (pseudo) evaporation of the GOXIV product is then not with the air pressure, but with the amount of air.
  • the first partial flow of the feed air compressed in the main air compressor is recompressed upstream of its introduction into the main heat exchanger in a first post-compressor which is operated in the warm state and is driven by the first turbine.
  • the inlet pressure of the first turbine is significantly higher than the first pressure to which the total air is compressed.
  • the air for the second turbine for example, is not post-compressed, i.e. its inlet pressure is at the lower level of the first pressure.
  • the second turbine on the other hand, is not recompressed, for example, which means that its inlet pressure is at the lower level of the first pressure.
  • the invention also relates to a device according to claim 8.
  • the device according to the invention can be supplemented by device features which correspond to the features of the dependent method claims.
  • the "means for switching between a first and a second operating mode" are complex regulating and control devices which, in cooperation, enable an at least partially automatic switching between the two operating modes, for example by means of an appropriately programmed operating control system.
  • Atmospheric air is drawn in by a main air compressor 2 via a filter 1.
  • the main air compressor has five stages and compresses the total air flow to a "first pressure" of, for example, 22 bar.
  • the total air flow 3 downstream of the main air compressor 2 is cooled under the first pressure in a pre-cooling 4.
  • the pre-cooled total air flow 5 is cleaned in a cleaning device 6, which is formed in particular by a pair of switchable molecular sieve adsorbers.
  • the cleaned total air flow 7 becomes a first part 8 in a hot air post-compressor 9 with after-cooler 10 to a second pressure of 28 bar, for example, and then divided into a "first partial flow” 11 (first turbine air flow) and a "second partial flow” 12 (first throttle flow).
  • the first partial flow 11 is cooled in a main heat exchanger 13 to a first intermediate temperature.
  • the cooled first partial flow 14 is expanded in a first air turbine 15 from the second pressure to about 5.5 bar in a work-performing manner.
  • the first air turbine 15 drives the warm air post-compressor 9.
  • the first partial stream 16, which is relaxed in terms of work, is introduced into a separator (phase separator) 17.
  • the liquid portion 18 is introduced via lines 19 and 20 into the low pressure column 22 of the distillation column system.
  • the distillation column system comprises a high-pressure column 21, the low-pressure column 22 and a main condenser 23 and a conventional argon recovery 24 with crude argon column 25 and pure argon column 26.
  • the main condenser 23 is designed as a condenser-evaporator, in the specific example as a cascade evaporator.
  • the operating pressure at the top of the high pressure column is 5.3 bar in the example, that at the top of the low pressure column is 1.35 bar.
  • the second partial flow 12 of the feed air is cooled in the main heat exchanger 13 to a second intermediate temperature, which is higher than the first intermediate temperature, is fed via line 27 to a cold compressor 28 and there is further compressed to a "third pressure" of approximately 40 bar.
  • the post-compressed second partial flow 29 is introduced again into the main heat exchanger 13 at a third intermediate temperature, which is higher than the second intermediate temperature, and is cooled there to the cold end.
  • the cold second partial stream 30 is expanded in a throttle valve 31 to approximately the operating pressure of the high-pressure column and fed to the high-pressure column 21 via line 32.
  • a part 33 is removed again, cooled in a subcooling countercurrent 34 and fed via lines 35 and 20 into the low-pressure column 22.
  • a "third partial flow" 36 of the feed air is introduced under the first pressure into the main heat exchanger 13 and is cooled there to a fourth intermediate temperature, which in the example is somewhat lower than the first intermediate temperature.
  • the cooled third partial flow 37 is expanded in a second air turbine 38 from the first pressure to approximately high-pressure column pressure while performing work.
  • the second Air turbine 38 drives cold compressor 28.
  • the third partial stream 39 which is relaxed in terms of work, is fed via line 40 to the high-pressure column 21 at the bottom.
  • a "fourth partial flow” 41 (second throttle flow) flows through the main heat exchanger 13 from the warm to the cold end under the first pressure.
  • the cold fourth partial flow 42 is expanded in a throttle valve 43 to approximately the operating pressure of the high-pressure column and fed to the high-pressure column 21 via line 32.
  • the oxygen-enriched bottom liquid of the high-pressure column 21 is cooled in the subcooling countercurrent 34 and introduced into the optional argon recovery 24 via line 45. Vapor 46 generated therefrom and remaining liquid 47 are fed into the low-pressure column 22.
  • a first part 49 of the top nitrogen 48 of the high-pressure column 21 is completely or substantially completely liquefied in the liquefaction chamber of the main condenser 23 against liquid oxygen evaporating in the evaporation chamber from the sump of the low-pressure column.
  • a first part 51 of the liquid nitrogen 50 produced in the process is fed as a return to the high-pressure column 21.
  • a second part 52 is cooled in the subcooling countercurrent 34 and fed into the low-pressure column 22 via line 53. At least a part of the liquid low-pressure nitrogen 53 serves as a return in the low-pressure column 21; another part 54 can be obtained as a liquid nitrogen product (LIN).
  • Gaseous low-pressure nitrogen 55 is drawn off from the top of the low-pressure column 22 and heated in the supercooling countercurrent 34 and in the main heat exchanger 13.
  • the warm low-pressure nitrogen 56 is compressed in a two-section nitrogen product compressor (57, 59) with intermediate and after-cooling (58, 60) to the desired product pressure, which in the example is 12 bar.
  • the first section 57 of the nitrogen product compressor consists, for example, of two or three stages with associated aftercoolers; the second section 59 has at least one stage and is preferably also intercooled and postcooled.
  • Gaseous impure nitrogen 61 is drawn off from an intermediate point of the low-pressure column 22 and in the supercooling counterflow 34 and in the main heat exchanger 13 warmed up.
  • the warm impure nitrogen 62 can be blown off (63) into the atmosphere (ATM) and / or used as regeneration gas 64 for the cleaning device 6.
  • the lines 67 and 68 connect the low-pressure column 22 to the crude argon column 25 of the argon extraction 24.
  • a first portion 70 of the liquid oxygen 69 from the bottom of the low pressure column 22 is withdrawn as a "first product stream", brought to a "first product pressure” of, for example, 37 bar in an oxygen pump 71 and evaporated under the first product pressure in the main heat exchanger 13 and finally via line 72 as the "first pressurized gas product” (GOX IC - internally compressed gaseous oxygen).
  • a second part 73 of the liquid oxygen 69 from the bottom of the low-pressure column 22 is optionally cooled in the supercooling countercurrent 34 and obtained as a liquid oxygen product (LOX) via line 74.
  • LOX liquid oxygen product
  • a third part 75 of the liquid nitrogen 50 from the high-pressure column 21 or the main condenser 23 is also subjected to an internal compression by bringing it to a second product pressure of, for example, 37 bar in a nitrogen pump 76, under the second product pressure in the main heat exchanger 13 pseudo evaporated and finally obtained via line 77 as an internally compressed gaseous nitrogen pressure product (GAN IC).
  • GAN IC internally compressed gaseous nitrogen pressure product
  • a second part 78 of the gaseous top nitrogen 48 of the high-pressure column 21 is heated in the main heat exchanger and either obtained via line 79 as a gaseous medium-pressure product or - as shown - used as a sealing gas (seal gas) for one or more of the process pumps shown.
  • a lower oxygen production (for example 75%) can then be regarded as a "second operating mode".
  • part of the gaseous portion 17 of the first partial stream 16 relaxed as a "second process stream" via the lines 65, 66 through the main heat exchanger to an intermediate stage of the main air compressor 2.
  • the recycle stream is admixed to the feed air between the second and third stages or between the third and fourth stages of the main air compressor. (This feed air represents the "first process stream”.)
  • the amount of air through the turbine 15 can be kept relatively high and an unchanged - or at least a less reduced - amount of nitrogen and liquid products can be obtained.
  • a 95% mode of operation could just as well be regarded as the "first mode of operation".
  • a "second operating mode” is then achieved, for example, with an oxygen production of 90% of the design value.
  • the return quantity in the table relates to the current air quantity through filter 1. All percentages here and in the rest of the text refer to molar quantities, unless otherwise stated.
  • gaseous oxygen 181 is withdrawn from the low-pressure column and mixed with the gaseous impure nitrogen 61 from the low-pressure column.
  • the mixing takes place downstream of the supercooling counterflow 34 in the example.
  • line 181 is closed, or less gas is conducted via line 181.
  • the corresponding amount of nitrogen 180 from the high pressure column is not condensed in the main condenser 23 and is not introduced into the low pressure column. As a result, it does not take part in the rectification in the low-pressure column (neither indirectly via the evaporation of the bottoms oxygen, nor directly through use as a return liquid) and thereby enables the reduction in oxygen production. At the same time, the same amount of air (or only slightly less) is available for cold production and nitrogen generation.
  • gaseous oxygen 181 is withdrawn from the low-pressure column and mixed with the gaseous impure nitrogen 61 from the low-pressure column.
  • the mixing takes place downstream of the supercooling counterflow 34 in the example.
  • line 181 is closed, or less gas is conducted via line 181.
  • the amount of nitrogen through line 180 relates to the amount of air through filter 1 in the design case.
  • Figure 3 differs from Figure 1 through a third inductor current.
  • the second turbine 38 is operated with a relatively high outlet pressure and a relatively high outlet temperature.
  • Turbine flow 339 which has been relieved of work, then has a pressure which is at least 1 bar, in particular 4 to 11 bar, above the operating pressure of the high-pressure column, and a temperature which is at least 10 K, in particular 20 to 60 K, above the inlet temperature of low-pressure nitrogen flows 55 , 61 is at the cold end of the main heat exchanger.
  • This stream is then further cooled in the cold part of the main heat exchanger.
  • the further cooled third partial flow 340 is expanded as a third throttle flow in a throttle valve 341 to approximately high-pressure column pressure and introduced into the high-pressure column via line 32. This allows the heat exchange process in the main heat exchanger to be further optimized.

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Claims (8)

  1. Procédé pour l'obtention variable d'un produit gazeux sous pression (72 ; 77) au moyen d'un fractionnement de l'air à basse température dans un système de colonnes de distillation, qui présente une colonne haute pression (21) et une colonne basse pression (22), dans lequel
    - la totalité de l'air d'alimentation est comprimée dans un compresseur d'air principal (2) à une première pression, qui est supérieure d'au moins 4 bar à la pression de service de la colonne haute pression (21),
    - un premier flux partiel (8, 11, 14) de l'air d'alimentation (7) comprimé dans le compresseur d'air principal (2) est refroidi à une température intermédiaire dans un échangeur de chaleur principal (13) et détendu avec production de travail dans une première turbine à air (15),
    - au moins une première partie du premier flux partiel (16) détendu avec production de travail est introduite dans le système de colonnes de distillation (40 ; 18, 19, 20),
    - un deuxième flux partiel (12, 27, 29, 30) de l'air d'alimentation comprimé dans le compresseur d'air principal (2) est comprimé ultérieurement dans un premier post-compresseur (9), lequel est opéré à chaud et entraîné par la première turbine (15), à une deuxième pression, qui est supérieure à la première pression, refroidi dans l'échangeur de chaleur principal (13) et ensuite détendu (31) et introduit dans le système de colonnes de distillation,
    - un premier flux de produit (69 ; 75) est prélevé sous forme liquide du système de colonnes de distillation et soumis à une augmentation de pression (71 ; 76) à une première pression de produit,
    - le premier flux de produit à la première pression de produit est évaporé ou pseudo-évaporé et chauffé dans l'échangeur de chaleur principal (13),
    - le premier flux de produit chauffé (72, 77) est obtenu comme premier produit gazeux sous pression (GOX IC ; GAN IC),
    - un premier flux de traitement, qui contient au moins 78 % en mole d'azote, est comprimé dans un compresseur à plusieurs niveaux (2) d'une pression d'entrée à une pression finale,
    - le compresseur à plusieurs niveaux étant formé par le compresseur d'air principal (2) et
    - le premier flux de traitement étant formé par la totalité de l'air d'alimentation.
    - au moins temporairement un deuxième flux de traitement (65), qui contient au moins 78 % en mole d'azote, est mélangé avec le premier flux de traitement en aval du premier niveau du compresseur à plusieurs niveaux (2), le deuxième flux de traitement étant formé par une partie (65) du premier flux partiel (16) de l'air d'alimentation détendu avec production de travail,
    - dans un premier mode de fonctionnement, une première quantité d'un premier produit gazeux sous pression est obtenue,
    - dans un deuxième mode de fonctionnement, une deuxième quantité d'un premier produit gazeux sous pression est obtenue, laquelle est inférieure à la première quantité,
    - dans le premier mode de fonctionnement, une première quantité du deuxième flux de traitement (65), qui peut aussi être nulle, est comprimée dans le compresseur à plusieurs niveaux (2),
    - dans le deuxième mode de fonctionnement, une deuxième quantité du deuxième flux de traitement (65) est comprimée dans le compresseur à plusieurs niveaux (2), laquelle est supérieure à la première quantité du deuxième flux de traitement,
    caractérisé en ce que
    - dans le premier mode de fonctionnement une première quantité de l'air d'alimentation est comprimée dans le compresseur d'air principal (2) et
    - dans le deuxième mode de fonctionnement une deuxième quantité de l'air d'alimentation est comprimée dans le compresseur d'air principal (2), laquelle est inférieure à la première quantité de l'air d'alimentation,
    - le rapport de la deuxième quantité d'air d'alimentation à la première quantité d'air d'alimentation étant supérieur, en particulier de plus de 3 % supérieur, au rapport entre la deuxième quantité du premier produit gazeux sous pression et la première quantité du premier produit gazeux sous pression.
  2. Procédé selon la revendication 1, caractérisé en ce que
    - un troisième flux de traitement est comprimé dans un compresseur de produits azotés d'une pression d'entrée à une pression finale et
    - au moins temporairement un quatrième flux de traitement est mélangé avec le troisième flux de traitement en aval du premier niveau du compresseur de produits azotés,
    - le troisième flux de traitement étant formé par un premier flux d'azote gazeux de la colonne basse pression et
    - le quatrième flux de traitement étant formé par un premier flux d'azote gazeux de la colonne
    haute pression.
  3. Procédé selon l'une quelconque des revendications 1 à 2, caractérisé en ce que dans le deuxième mode de fonctionnement, un flux d'oxygène gazeux (181), prélevé de la zone inférieure de la colonne basse pression (22), est mélangé avec un flux (61) enrichi en azote de la zone supérieure de la colonne basse pression (22) et le mélange est chauffé dans l'échangeur de chaleur principal (13).
  4. Procédé selon l'une quelconque des revendications 1 à 3, caractérisé en ce que
    - un troisième flux partiel (36, 37) de l'air d'alimentation (7) comprimé dans le compresseur d'air principal (2) est refroidi à une température intermédiaire dans l'échangeur de chaleur principal (13) et détendu avec production de travail dans une deuxième turbine à air (38) et
    - au moins une première partie du troisième flux partiel (39) détendu avec production de travail est introduite dans le système de colonnes de distillation (40),
    - la pression à l'entrée de turbine de la deuxième turbine à air étant en particulier égale à la première pression.
  5. Procédé selon la revendication 4, caractérisé en ce que
    - le deuxième flux partiel (12, 27, 29, 30) de l'air d'alimentation (7) comprimé dans le compresseur d'air principal (2) est refroidi à une température intermédiaire dans l'échangeur de chaleur principal (13) en aval du premier post-compresseur (9), est comprimé ultérieurement dans un deuxième post-compresseur (28), lequel est opéré comme un compresseur à froid et entraîné par la deuxième turbine (38), à une troisième pression, qui est supérieure à la première pression, refroidi dans l'échangeur de chaleur principal (13) et ensuite détendu (31) et introduit (32) dans le système de colonnes de distillation.
  6. Procédé selon l'une quelconque des revendications 1 à 5, caractérisé en ce qu'un quatrième flux partiel (41, 42) de l'air (7) comprimé dans le compresseur d'air principal (2) est refroidi sous la première pression dans l'échangeur de chaleur principal (13) et ensuite détendu (43) et introduit dans le système de colonnes de distillation.
  7. Procédé selon la revendication 4 ou 5 ou selon la revendication 6 se référant à l'une quelconque des revendications 4 ou 5, caractérisé en ce que
    - le troisième flux partiel (37, 339) est détendu dans la deuxième turbine à air (38) à une pression, qui est supérieure d'au moins 1 bar à la pression de service de la colonne haute pression (21) et
    - le troisième flux partiel (339) détendu avec production de travail est refroidi encore dans l'échangeur de chaleur principal (13) et ensuite détendu (341) et introduit dans le système de colonnes de distillation.
  8. Dispositif pour l'obtention variable d'un produit gazeux sous pression (72 ; 73) au moyen d'un fractionnement de l'air à basse température comprenant
    - un système de colonnes de distillation qui comprend une colonne haute pression (21) et une colonne basse pression (22),
    - un compresseur d'air principal (2) pour la compression de la totalité de l'air d'alimentation à une première pression qui est supérieure d'au moins 4 bar à la pression de service de la colonne haute pression (21),
    - des moyens pour le refroidissement d'un premier flux partiel (8, 11, 14) de l'air d'alimentation (7) comprimé dans le compresseur d'air principal (2) à une température intermédiaire dans un échangeur de chaleur principal (13),
    - une première turbine à air (15) pour la détente avec production de travail du premier flux partiel refroidi,
    - des moyens pour l'introduction (40 ; 18, 19, 20) du premier flux partiel (16) détendu avec production de travail dans le système de colonnes de distillations,
    - un premier post-compresseur (9) pour la compression ultérieure d'un deuxième flux partiel (12, 27, 29, 30) de l'air d'alimentation comprimé dans le compresseur d'air principal (2) à une deuxième pression, qui est supérieure à la première pression, le post-compresseur (9) pouvant être opéré à chaud et étant entraîné par la première turbine (15), - des moyens pour le refroidissement du deuxième flux partiel comprimé ultérieurement dans l'échanger de chaleur principal (13),
    - des moyens pour la détente (31) et l'introduction dans le système de colonnes de distillation du deuxième flux partiel refroidi,
    - des moyens pour le prélèvement sous forme liquide d'un premier flux de produit (69 ; 75) du système de colonnes de distillation et pour l'augmentation de la pression (71 ; 76) du premier flux de produit liquide à une première pression de produit,
    - des moyens pour l'évaporation ou la pseudo-évaporation et le chauffage du premier flux de produit sous la première pression de produit dans l'échangeur de chaleur principal (13),
    - des moyens pour l'obtention du premier flux de produit (72 ; 77) chauffé comme premier produit gazeux sous pression (GOX IC ; GAN IC),
    - un compresseur à plusieurs niveaux (2) pour la compression d'un premier flux de traitement, qui contient au moins 78 % en mole d'azote, d'une pression d'entrée à une pression finale,
    - le compresseur à plusieurs niveaux étant formé par le compresseur d'air principal (2) et
    - le premier flux de traitement étant formé par la totalité de l'air d'alimentation,
    - des moyens pour le mélange d'un deuxième flux de traitement (65), lequel contient au moins 78 % en mole d'azote, avec le premier flux de traitement en aval du premier niveau du compresseur à plusieurs niveaux (2 ; 57/59), le deuxième flux de traitement (180) étant formé par une partie (65) du premier flux partiel (16) de l'air d'alimentation détendu avec production de travail,
    - des moyens pour la commutation entre un premier et un deuxième mode de fonctionnement,
    - dans le premier mode de fonctionnement, une première quantité du premier produit gazeux sous pression étant obtenue,
    - dans un deuxième mode de fonctionnement, une deuxième quantité d'un premier produit gazeux sous pression étant obtenue, laquelle est inférieure à la première quantité et
    - les moyens pour la commutation entre le premier et le deuxième mode de fonctionnement étant conçus de telle façon que
    - dans le premier mode de fonctionnement, une première quantité du deuxième flux de traitement (65), qui peut aussi être nulle, est comprimée dans le compresseur à plusieurs niveaux (2) d'une pression d'entrée à une pression finale,
    - dans le deuxième mode de fonctionnement, une deuxième quantité du deuxième flux de traitement (65 ; 180) est comprimée dans le compresseur à plusieurs niveaux (2 ; 57/59), laquelle est supérieure à la première quantité du deuxième flux de traitement,
    caractérisé en ce que les moyens pour la commutation entre le premier et le deuxième mode de fonctionnement sont conçus de telle façon que
    - dans le premier mode de fonctionnement une première quantité de l'air d'alimentation est comprimée dans le compresseur d'air principal (2) et
    - dans le deuxième mode de fonctionnement une deuxième quantité de l'air d'alimentation est comprimée dans le compresseur d'air principal (2), laquelle est inférieure à la première quantité de l'air d'alimentation,
    - le rapport de la deuxième quantité d'air d'alimentation à la première quantité d'air d'alimentation étant supérieur, en particulier de plus de 3 % supérieur, au rapport entre la deuxième quantité du premier produit gazeux sous pression et la première quantité du premier produit gazeux sous pression.
EP15735849.0A 2014-07-05 2015-06-25 Procédé et dispositif de fractionnement de l'air à basse température à consommation d'énergie variable Active EP3164654B1 (fr)

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PCT/EP2015/001284 WO2016005030A1 (fr) 2014-07-05 2015-06-25 Procédé et dispositif de fractionnement de l'air à basse température à consommation d'énergie variable

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TW201607599A (zh) 2016-03-01
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RU2691210C2 (ru) 2019-06-11
EP2963367A1 (fr) 2016-01-06
US10458702B2 (en) 2019-10-29
EP3164653A1 (fr) 2017-05-10
TW201607598A (zh) 2016-03-01
RU2690550C2 (ru) 2019-06-04
US20170131028A1 (en) 2017-05-11
CN106489059A (zh) 2017-03-08
WO2016005030A1 (fr) 2016-01-14
CN106662394A (zh) 2017-05-10
EP3164654A1 (fr) 2017-05-10
RU2017103309A3 (fr) 2018-12-18
RU2017103309A (ru) 2018-08-06
US20170153058A1 (en) 2017-06-01
CN106662394B (zh) 2019-11-05
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RU2017103099A (ru) 2018-08-06
US10215489B2 (en) 2019-02-26

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