EP3640571A1 - Procédé et installation de production d'un produit de l'air riche en oxygène - Google Patents

Procédé et installation de production d'un produit de l'air riche en oxygène Download PDF

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Publication number
EP3640571A1
EP3640571A1 EP18020515.5A EP18020515A EP3640571A1 EP 3640571 A1 EP3640571 A1 EP 3640571A1 EP 18020515 A EP18020515 A EP 18020515A EP 3640571 A1 EP3640571 A1 EP 3640571A1
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Prior art keywords
gas mixture
residual gas
oxygen
air
product
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EP18020515.5A
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German (de)
English (en)
Inventor
Matthias Grahl
Daniel Palaniswamy Otte
Eythymios Kontogeorgopoulos
Xiaohua Fan
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Linde GmbH
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Linde GmbH
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Priority to EP18020515.5A priority Critical patent/EP3640571A1/fr
Publication of EP3640571A1 publication Critical patent/EP3640571A1/fr
Withdrawn legal-status Critical Current

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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
    • F25J3/04048—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
    • 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
    • F25J3/04181—Regenerating the adsorbents
    • 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
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04381—Details relating to the work expansion, e.g. process parameter etc. using work extraction by mechanical coupling of compression and expansion so-called companders
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/044—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 single pressure main column system only
    • 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
    • F25J3/04636—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 hybrid air separation unit, e.g. combined process by cryogenic separation and non-cryogenic separation techniques
    • 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
    • F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead gas
    • 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
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • F25J2205/64—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end by pressure-swing adsorption [PSA] at the hot end
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/52—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being oxygen enriched compared to air, e.g. "crude 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop

Definitions

  • the present invention relates to a method for obtaining an oxygen-rich air product and a corresponding arrangement according to the preambles of the respective independent claims.
  • gaseous oxygen of different purity levels can also be generated from air by means of pressure swing adsorption (PSA), in particular by means of vacuum pressure swing adsorption (VPSA).
  • PSA pressure swing adsorption
  • VPSA vacuum pressure swing adsorption
  • the separation of air using PSA and VPSA is based on the different degrees of adsorption of the air components to an adsorbent.
  • oxygen-rich gas mixtures with, for example, approximately 90 to 95 mole percent oxygen content can be obtained from air using PSA or VPSA.
  • the object of the present invention is to create improved possibilities for obtaining oxygen-rich air products.
  • the residual gas mixture can alternatively or in addition to the vacuum pressure swing adsorption be subjected to a pressure swing adsorption of another type.
  • Rectification columns of rectification column systems which are used for the low-temperature separation of air, can be operated at different pressure levels.
  • Known double-column systems have a so-called high-pressure column (also referred to as a pressure column, medium-pressure column or lower column) and a so-called low-pressure column (also referred to as the upper column).
  • the pressure level of the high-pressure column is, for example, 4 to 6 bar, preferably about 5.5 bar.
  • the low pressure column is operated at a pressure level of, for example, 1.3 to 1.7 bar, preferably approximately 1.4 bar.
  • the pressure levels given here and below are absolute pressures which are present at the top of the columns mentioned. The values mentioned are only examples that can be changed if necessary. In particular for the exclusive extraction of nitrogen-rich air products, air separation plants without a double-column system can also be used, as shown in an example below in Figure 4 illustrated.
  • Adsorption is typically carried out in a PSA or VPSA using porous adsorbents.
  • the proportions of adsorbable components adsorbed in each case depend in particular on the pressure of the gas mixture (feed gas) fed to the PSA or VPSA and on the selectivity of the adsorbent.
  • the adsorbent used in the PSA or VPSA is located in appropriate adsorption containers, whereby two or more adsorption containers are required for continuous production operation. If "PSA” or "VPSA” is used here, this means both a corresponding method or a corresponding method step and a technical device designed to carry out such a method or method step.
  • Each adsorption container in a PSA or VPSA is alternately loaded with the component or components to be adsorbed in one adsorption cycle and regenerated in a desorption or regeneration cycle, whereby additional periods may also exist between these two cycles in which neither a loading nor a Regeneration is carried out and the adsorbent can be flushed, for example, with further gas flows in order to carry out residues of the gas mixture to be separated.
  • this type of rinsing is also a kind of regeneration, it is considered separately below.
  • the adsorption containers of a corresponding arrangement are operated in alternating operation in such a way that at least one of the adsorption containers is always in the adsorption cycle and can therefore deliver a product. In this case too, however, periods can occur in which no product is delivered, for example during pressure equalization or pressure build-up. In this case, product buffers can be used, for example. However, this, and alternating operation in general, is not absolutely necessary.
  • the gas mixture to be processed is passed through the adsorption container under pressure until the adsorbent contained no longer has sufficient absorption capacity for the adsorbed component (s).
  • the supply of the gas mixture to be processed is therefore prevented and a desorption of the adsorbed component (s) is effected by a pressure reduction in the desorption cycle.
  • the VPSA differs from a conventional PSA essentially in the sub-atmospheric pressure level used in the desorption cycle, which is also commonly referred to as "vacuum".
  • the VPSA is distinguished from a conventional PSA in certain cases by increased yields and a lower specific, i.e. product related, energy needs.
  • Oxygen-rich air products occur in PSA or VPSA due to the weaker adsorption of oxygen in the adsorption cycle and are therefore formed under a certain pressure that corresponds to the feed pressure into the PSA or VPSA minus pressure losses.
  • a temperature swing adsorption differs from a PSA or VPSA essentially in that the adsorption and desorption take place at significantly different temperature levels.
  • the air to be processed is typically processed by means of appropriate devices in order to dry it and to remove carbon dioxide and, if appropriate, other components which interfere with the low-temperature separation.
  • the temperature is increased in the desorption cycle in order to reduce the components of the adsorbent, e.g. Mol sieve to desorb.
  • Liquids and gases can, in the language used here, be enriched or depleted in one or more components, these terms relating to a content in a starting liquid or gas from which the liquid or gas under consideration was obtained.
  • the liquid or gas is enriched if it is at least 1.1 times, 1.5 times, 2 times, 5 times, 10 times 100 times or 1,000 times the content, and depleted if this or this contains at most 0.9 times, 0.5 times, 0.1 times, 0.01 times or 0.001 times the content of a corresponding component, based on the starting liquid or the starting gas.
  • oxygen is used here, this should also be understood to mean a liquid or a gas which is or is rich in oxygen, but does not have to consist exclusively of it.
  • pressure level and temperature level to characterize pressures and temperatures, which is intended to express that pressures and temperatures in a corresponding system do not have to be used in the form of exact pressure or temperature values in order to implement the inventive concept .
  • pressures and temperatures are typically in certain ranges, for example ⁇ 1%, 5%, 10% or 20% around an average.
  • Corresponding pressure levels and temperature levels can lie in disjoint areas or in areas that overlap one another.
  • pressure levels include, for example, unavoidable or expected pressure drops.
  • the pressure levels given here in bar are absolute pressures.
  • An air product is understood here to mean a component or a mixture of components in a gaseous or liquid state, which can be formed by processing air (feed air), in particular by low-temperature separation or PSA or VPSA.
  • An air product is therefore characterized in particular by the fact that it has a different composition than atmospheric air, but in particular no additional components compared to atmospheric air.
  • the present invention is based on the knowledge that, to obtain an oxygen-rich air product, the low-temperature separation of air and the VPSA can be combined particularly advantageously and with the generation of corresponding synergy effects.
  • the present invention proposes to use a so-called residual gas mixture in the VPSA that remains during the low-temperature separation of air and can be removed from a corresponding system.
  • the feed air to be processed is typically processed using TSA before it is fed to the cold part.
  • the above-mentioned residual gas mixture is typically used, which remains during the low-temperature decomposition. This is heated, for example, in electric heaters.
  • the oxygen content in a corresponding residual gas mixture can be extremely high, for example around 50 mole percent. To the extent that such a residual gas mixture is not suitable for regeneration in the TSA is used, it is traditionally released into the atmosphere. The same applies to the residual gas mixture after it has been used for regeneration in the TSA. The cleaning and compaction effort invested is therefore lost in conventional processes or systems.
  • a method for obtaining an oxygen-rich air product in order to achieve the advantages mentioned, in which a first residual gas mixture is provided by means of a plant for the low-temperature separation of air, which is enriched with oxygen compared to atmospheric air and also has nitrogen.
  • the first residual gas mixture or part of the first residual gas mixture is fed to a VPSA, by means of which the oxygen-rich air product and a second residual gas mixture depleted in oxygen compared to the first residual gas mixture are provided.
  • the "first residual gas mixture” is not a pure product of a corresponding plant for the low-temperature separation of air. Its oxygen content is therefore limited, as explained below.
  • the present invention enables an oxygen-rich air product to be produced in a particularly advantageous manner, in terms of energy and investment costs, because the residual gas mixture mentioned, the oxygen content of which lies in particular in the areas explained in more detail below, is already provided in a plant for the low-temperature separation of air at a certain pressure level, which a new compression before the feed into the VPSA makes it obsolete or at least significantly reduces the effort required for this.
  • Another advantage arises from the fact that by using the residual gas mixture, which has a higher oxygen content than atmospheric air, the VPSA can be operated more efficiently, since the content of components to be adsorbed is lower relative to the content of the product component not to be adsorbed oxygen.
  • the present invention also makes it possible to use such a residual gas mixture in a sensible manner to obtain valuable products.
  • feed air can be processed in the plant for the low-temperature separation of air by means of a TSA in order to free it from unwanted and disruptive components such as water and Get rid of carbon dioxide.
  • an appropriate residual gas mixture is used in conventional plants for the low-temperature separation of air in a TSA. Since part or all of the residual gas mixture can be fed into the VPSA in the context of the present invention, it may be necessary, ie if the amount of residual gas mixture is insufficient, to take suitable measures here in order to ensure adequate air purification. This can be done, for example, by adapting the air treatment in the plant for the low-temperature separation of air to a smaller amount of residual gas mixture available.
  • a corresponding cooling can in particular include the use of one or more improved evaporative coolers or the use of a cooling device in which a non-aqueous coolant, for example ammonia, is used.
  • the cooling takes place in particular to a temperature level below the customary cooling water temperature, in particular below 15 ° C., below 10 ° C. or below 5 ° C. and above the freezing temperature of water at the respective pressure level.
  • the amount of regeneration gas can also be reduced by increasing the regeneration temperature.
  • a part of the first residual gas mixture can be subjected to vacuum pressure swing adsorption and a further part of the first residual gas mixture can be heated and used as a regeneration gas in the TSA without having previously been subjected to vacuum pressure swing adsorption.
  • the first residual gas mixture can be divided accordingly.
  • the second residual gas mixture or part of the second residual gas mixture is used as regeneration gas in the TSA. This can be done in addition or as an alternative to using the first residual gas mixture.
  • the second residual gas mixture is drawn off from the VPSA by means of a vacuum pump at such a subatmospheric pressure level due to the subatmospheric pressure level during the desorption in the VPSA, but is present downstream of the vacuum pump at a higher pressure level, for example at atmospheric pressure. If necessary, this can either be compressed or the regeneration of the TSA at a correspondingly low level Pressure level. In the latter case, the TSA is operated in a desorption cycle at this low pressure level and the adsorption cycle is carried out at a higher pressure level.
  • the second residual gas mixture or its part can be processed in the TSA by means of a residual gas mixture preparation before being used as regeneration gas, which, depending on the pressure level required, suitably comprises compression and possibly tempering.
  • the present invention can be used in particular when the low-temperature separation of air is carried out according to the so-called SPECTRA method, as is described, inter alia, in US Pat EP 2 789 958 A1 and the other patent literature cited there.
  • the SPECTRA process also cools compressed and pre-cleaned air to a temperature suitable for rectification, which is normally at or near its dew point. This will partially liquefy it.
  • the air is then fed into a rectification column and rectified there.
  • This rectification column can be the only rectification column in a corresponding process, but this is not mandatory.
  • a rectification column is used in the plant for the low-temperature separation of air, in which a gaseous top product enriched with nitrogen from atmospheric air and a liquid bottom product enriched with oxygen from atmospheric air are formed.
  • the rectification column is cryogenic, oxygen-enriched liquid in the form of one or more material streams and at least partially heated in a heat exchanger which is used to cool at least part of the top gas of the rectification column.
  • the liquid enriched with oxygen compared to atmospheric air can be passed through the heat exchanger in the form of a material flow or in the form of several separate material flows. For example, one stream can first be removed from the rectification column and then divided, or two separate streams can already be removed from the rectification column.
  • the oxygen-enriched liquid which is removed from the rectification column in the form of the one or more material streams and heated in the heat exchanger, is expanded to a first part at least in one or more expansion machines and as that or as a part of the residual gas mixture from the plant for the low-temperature separation of air and compressed to a second part at least in one or more compressors, which is coupled to the expansion machine (s), and then fed back into the rectification column.
  • the two portions can be two substreams of a stream withdrawn from the rectification column or it can be oxygen-enriched liquid which has already been discharged from the rectification column in the form of separate streams.
  • a first liquid stream with a first oxygen content and a second liquid stream with a second, different oxygen content can be withdrawn from the rectification column, the first oxygen content being in particular above the second oxygen content.
  • the first stream can be formed in particular using at least part of the liquid bottom product of the rectification column.
  • the second stream of material can be withdrawn from the rectification column from an intermediate plate or from a corresponding liquid retention device.
  • the first and the second material stream are heated at least in part using a heat exchanger, which at the same time serves to cool and at least partially liquefy at least part of the top gas of the rectification column.
  • the first material flow is at least partly further heated, in particular in the main heat exchanger of the system, expanded in a relaxation machine, reheated, in particular in the main heat exchanger, and carried out from the system.
  • This is the residual gas mixture that can be supplied to the VPSA in the context of the present invention.
  • the second material flow is at least partly compressed in a compressor which is coupled to the expansion machine which is used to relax the first material flow or part thereof.
  • the second stream is then at least partially cooled in the main heat exchanger and fed back into the rectification column.
  • one or more Relaxation machines in particular in the form of turbo expanders, and one or more compressors coupled therewith, in particular in the form of corresponding boosters or turbocompressors, are used.
  • the top gas of the rectification column represents, liquefied or non-liquefied, a nitrogen-rich air product which is provided by means of a corresponding process.
  • a nitrogen-rich air product which is provided by means of a corresponding process.
  • Several (liquefied, internally compressed, gaseous, etc.) nitrogen-rich air products can also be provided.
  • An oxygen-containing air product can be produced in the SPECTRA process via another rectification column (high purity).
  • the final pressure of the expansion machine in a SPECTRA process and thus the pressure with which the residual gas mixture is made available, is 1.2 to 1.6 bar, in particular 1.3 to 1.4 bar, and is therefore particularly suitable to feed the residual gas mixture to the VPSA.
  • a corresponding residual gas mixture can be recompressed if necessary and the residual gas pressure in the system can be raised by suitable measures.
  • the pressure level at which the residual gas mixture is fed to the VPSA is 1.2 to 1.6 bar, in particular 1.3 to 1.4 bar
  • the pressure level for the desorption is 0.1 to 0.6 bar. especially at 0.3 to 0.5 bar.
  • higher pressure levels in a SPECTRA process benefit the VPSA, but can be disadvantageous for the SPECTRA process itself.
  • the pressures given therefore represent mutually adjusted values.
  • the first residual gas mixture can have a content of 30 to 70 mol percent, in particular approximately 50 mol percent, of oxygen. In particular, it can have nitrogen in all of the rest, apart from the usual traces of other air components.
  • the nitrogen content in the non-oxygen residue can in particular be more than 90 mole percent or more than 95 mole percent.
  • the second residual gas mixture can have a content of 10 to 30 mol percent, in particular approximately 25 mol percent, of oxygen.
  • the oxygen-rich air product can have a content of 80 to 99 or 80 to 99 mole percent, in particular of about 94 mole percent, of oxygen.
  • the separation of oxygen and argon is typically not possible by adsorption, which is why the maximum oxygen content depends in particular on the argon content in the air.
  • Especially the opposite Atmospheric air possibly significantly increased oxygen content of the first residual gas mixture, leads to a considerable increase in the amount of product or a reduction in the respective need for adsorbent.
  • the present invention further extends to an arrangement which is set up for obtaining an oxygen-rich air product, comprising a plant which is set up for the low-temperature separation of air and for the provision of a first residual gas mixture which is enriched in oxygen with respect to atmospheric air and also has nitrogen.
  • the arrangement comprises a vacuum pressure swing adsorption, which is set up to process the first residual gas mixture or part of the first residual gas mixture and to provide the oxygen-rich air product and a second residual gas mixture that is depleted in oxygen compared to the first residual gas mixture.
  • Figure 1 shows an arrangement according to an embodiment of the invention.
  • the arrangement is designated 100 in total.
  • the arrangement 100 comprises a system, generally designated 10, for the low-temperature separation of air, which comprises a so-called warm part 10a and a so-called cold part 10b.
  • the warm part 10a contains, in particular, the devices for providing the compressed feed air, such as the main air compressor, corresponding filters, and pre-cooling and cleaning devices.
  • a TSA 11 is illustrated by way of example only.
  • the cold part 10b there are the devices for low-temperature rectification, in particular a rectification column system, a main heat exchanger and the like.
  • the relevant specialist literature please refer to the relevant specialist literature.
  • feed air can be processed in a generally known manner.
  • An example can be found in the following Figure 4 .
  • the corresponding feed air A can be processed in the warm part 10a and then transferred to the cold part 10b, where it can be cooled to cryogenic temperatures and rectified.
  • the cold part 10b a plurality of nitrogen-rich air products C, D, E and a residual gas mixture B (referred to here as the "first" residual gas mixture) with a superatmospheric oxygen content are formed.
  • Figure 4 referenced in which corresponding fluids are indicated with identical capital letters.
  • other types of cryogenic air separation than that in Figure 4 shown example are used.
  • the arrangement 100 further comprises a VPSA 20 in the form of one or more corresponding units arranged in parallel or in series. Fluid can be drawn off from the VPSA or from its adsorption containers by means of a vacuum pump 20a for desorption if the latter is or are in a desorption cycle. In this way, a residual gas mixture U (here as a "second" residual gas mixture designated) are formed. In contrast, an oxygen-rich air product V leaves the VPSA or corresponding adsorption container in an adsorption cycle at a typically superatmospheric pressure level.
  • a first residual gas mixture B is thus provided by means of the system 10 for the low-temperature separation of air, which is enriched with oxygen compared to atmospheric air and also has nitrogen.
  • a part B1 of the first residual gas mixture B is subjected to the vacuum pressure swing adsorption 20 in the arrangement 100, by means of which the oxygen-rich air product V and a second residual gas mixture U depleted in oxygen compared to the first residual gas mixture B are provided.
  • feed air is processed by means of the TSA 11, a further part B2 of the first residual gas mixture B (as not specifically illustrated here) being heated and used as a regeneration gas in the TSA 11 without first being subjected to the vacuum pressure swing adsorption 20 to have been.
  • the air separation plant has a capacity of approx. 65,000 Nm 3 / h (standard cubic meters per hour) of air and the VPSA has a product quantity of 3,000 Nm 3 / h of 93% oxygen.
  • the oxygen from the residual gas of the air separation plant has an oxygen content of approx. 50%.
  • a feed amount of approx. 15,000 Nm 3 / h is required.
  • the amount of regeneration gas in the example shown must be reduced by 20%.
  • the outlet pressure of the turbine of the air separation plant could be increased, which leads to an increased energy consumption of the air separation plant, but at the same time to a reduction in the energy consumption in the VPSA.
  • Raising the regeneration gas temperature typically reaches economic limits due to the high oxygen content and the associated costs for valves and the like.
  • Figure 2 shows an arrangement according to a further embodiment of the invention.
  • the arrangement is designated by a total of 200.
  • the first residual gas mixture B is not made available in part to the TSA 11. Rather, the entire first residual gas mixture B is processed in the VPSA. Only during a pressure build-up phase in the VPSA, as illustrated in the form of a flow arrow with a dash-dotted line, is a bypass to a residual gas mixture preparation 21 assigned to the VPSA, which includes heaters, coolers and compressors not specifically identified, since during this phase the VPSA contains the residual gas mixture B can not process anyway. As explained earlier, the second residual gas mixture U is withdrawn from the VPSA 20 by means of the vacuum pump 20a.
  • Figure 3 shows an arrangement according to a further embodiment of the invention.
  • the arrangement is designated by a total of 300.
  • the arrangement 300 differs from the arrangement 200 essentially in that no compression is carried out in the residual gas mixture preparation 21 and the regeneration of the TSA 11 is accordingly carried out at a subatmospheric pressure level.
  • vacuum pump 20a is no longer required.
  • a subatmospheric pressure level can be provided by means of a vacuum pump 11a, by means of which the gas mixture X is carried out from the TSA 11.
  • a corresponding vacuum for example at approx. 0.5 bar (abs.), Prevails in the entire regeneration path of the TSA (heater, adsorber ).
  • a compressor and cooler for removing heat of compression in the residual gas mixture preparation 21 can be dispensed with.
  • FIG 4 illustrates a cryogenic air separation plant that can be used in an arrangement in accordance with an embodiment of the present invention. As before, the system is designated with a total of 10. In the Figure 4 The illustrated system 10 is set up for the low-temperature separation of air according to the SPECTRA method.
  • the system 10 has a main heat exchanger 1 and a rectification column 2.
  • the main heat exchanger 1 can also be composed of several individual heat exchangers or heat exchanger blocks.
  • compressed, pre-cooled and in particular pre-cleaned by means of TSA feed air A is passed in the form of a stream a through the main heat exchanger 1.
  • the feed air A is thereby cooled to a temperature suitable for rectification, which is at or near its dew point. This will partially liquefy it.
  • the air A or the stream a further designated a is fed into the rectification column 2 after cooling and rectified there in the usual way.
  • some practical or theoretical plates are fed in above the bottom of the rectification column 2.
  • the operating pressure of the rectification column 2 is 6 to 20 bar, for example approximately 9 bar.
  • a gaseous top product enriched with nitrogen in relation to atmospheric air and a liquid bottom product enriched in oxygen with respect to atmospheric air are formed.
  • a first liquid stream b with a first oxygen content and a second liquid stream c with a second, different oxygen content are withdrawn from the rectification column 2, the first and the second stream b and c (after supercooling in the main heat exchanger 1) here in each case using a Heat exchanger 3 are heated, which is used for cooling and at least partially liquefying part of the top gas of the rectification column 2.
  • This overhead gas is withdrawn from the top of the rectification column 2 in the form of a stream d and divided into partial streams e and f, the partial stream e being fed into the heat exchanger 3.
  • the aforementioned first material flow b is at least partly further heated, relaxed in a relaxation machine 5, reheated and as part of a material flow g, possibly after combining with further material flows not explained separately here, in the form of the Residual gas mixture B from the system 10 for low-temperature separation of air executed.
  • This residual gas mixture B can be fed to a VPSA.
  • the aforementioned second stream c is then at least partly compressed in a compressor 4, which is coupled to the expansion machine 5, and then cooled and into the rectification column 2 is fed back.
  • a compressor 4 which is coupled to the expansion machine 5, and then cooled and into the rectification column 2 is fed back.
  • it can be combined with other material flows.
  • the expansion machine 5 can be mechanically coupled to the compressor 4 via a braking device which is not specifically designated.
  • the braking device can be designed, for example, as an oil brake.
  • the material flow f already mentioned is heated in the main heat exchanger 1 and can be carried out from the system 10 as a gaseous nitrogen-rich air product C.
  • the stream e on the other hand, after its at least partial liquefaction in the heat exchanger 7, is again divided into the sub-streams g, h and i, the sub-stream g being returned to the rectification column 2 and the sub-stream h being subcooled in a subcooler 9.
  • a subcooled liquid nitrogen-rich air product D can be removed from the system 10.
  • the partial stream i is taken from the system 10 as a further, not supercooled nitrogen-rich air product E.
  • a part of the partial stream h, which is heated in the subcooler 9, is discharged as a further nitrogen-rich air product B.
  • Another air product F can also be provided in the illustrated manner.
  • a liquid nitrogen-rich air product G can be fed into the system.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)
EP18020515.5A 2018-10-18 2018-10-18 Procédé et installation de production d'un produit de l'air riche en oxygène Withdrawn EP3640571A1 (fr)

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EP18020515.5A EP3640571A1 (fr) 2018-10-18 2018-10-18 Procédé et installation de production d'un produit de l'air riche en oxygène

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN115074546A (zh) * 2021-08-12 2022-09-20 昆山易氧空分科技有限公司 一种富氧侧吹炉炼铅的供氧工艺及应用

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS6115068A (ja) * 1984-07-02 1986-01-23 大同酸素株式会社 高純度窒素ガス製造装置
US5421163A (en) * 1991-11-26 1995-06-06 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process for the combined production of nitrogen and oxygen with adjustable flows
EP2789958A1 (fr) 2013-04-10 2014-10-15 Linde Aktiengesellschaft Procédé de décomposition à basse température de l'air et installation de décomposition de l'air

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS6115068A (ja) * 1984-07-02 1986-01-23 大同酸素株式会社 高純度窒素ガス製造装置
US5421163A (en) * 1991-11-26 1995-06-06 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process for the combined production of nitrogen and oxygen with adjustable flows
EP2789958A1 (fr) 2013-04-10 2014-10-15 Linde Aktiengesellschaft Procédé de décomposition à basse température de l'air et installation de décomposition de l'air

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
H.-W. HÄRING (HRSG.: "Industrial Gases Processing", 2006, WILEY-VCH

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN115074546A (zh) * 2021-08-12 2022-09-20 昆山易氧空分科技有限公司 一种富氧侧吹炉炼铅的供氧工艺及应用

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