EP3193114B1 - Verfahren zur gewinnung eines luftprodukts in einer luftzerlegungsanlage und luftzerlegungsanlage - Google Patents

Verfahren zur gewinnung eines luftprodukts in einer luftzerlegungsanlage und luftzerlegungsanlage Download PDF

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Publication number
EP3193114B1
EP3193114B1 EP17020003.4A EP17020003A EP3193114B1 EP 3193114 B1 EP3193114 B1 EP 3193114B1 EP 17020003 A EP17020003 A EP 17020003A EP 3193114 B1 EP3193114 B1 EP 3193114B1
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Prior art keywords
tank
cryogenic liquid
liquid
period
during
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EP17020003.4A
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German (de)
English (en)
French (fr)
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EP3193114A1 (de
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Stefan Lochner
Ralph Spöri
Christian Zimmermann
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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
    • F25J3/04763—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
    • F25J3/04848—Control strategy, e.g. advanced process control or dynamic modeling
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—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
    • 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
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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
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    • 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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    • F25J3/04078—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
    • F25J3/04096—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 argon or argon enriched stream
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    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04163—Hot end purification of the feed air
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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
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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
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    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
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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
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    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
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    • F25J3/04381—Details relating to the work expansion, e.g. process parameter etc. using work extraction by mechanical coupling of compression and expansion so-called companders
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    • 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
    • F25J3/0489—Modularity and arrangement of parts of the air fractionation unit, in particular of the cold box, e.g. pre-fabrication, assembling and erection, dimensions, horizontal layout "plot"
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    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/30—Processes or apparatus using separation by rectification using a side column in a single pressure column system
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    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
    • F25J2200/94—Details relating to the withdrawal point
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    • 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
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    • F25J2215/42—Nitrogen or special cases, e.g. multiple or low purity N2
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    • F25J2215/52—Oxygen production with multiple purity O2
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    • F25J2215/56—Ultra high purity oxygen, i.e. generally more than 99,9% O2
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    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/58—Argon
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    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/02—Separating impurities in general from the feed stream
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    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/50—Separating low boiling, i.e. more volatile components from oxygen, e.g. N2, Ar
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    • F25J2230/08—Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler
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    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/40—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being air
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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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/50—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being oxygen
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    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
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    • 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
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    • 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
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    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
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    • 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
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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
    • F25J2280/00—Control of the process or apparatus
    • F25J2280/20—Control for stopping, deriming or defrosting after an emergency shut-down of the installation or for back up system
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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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/12—Particular process parameters like pressure, temperature, ratios
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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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/34—Details about subcooling of liquids
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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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/60—Details about pipelines, i.e. network, for feed or product distribution
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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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/62—Details of storing a fluid in a tank

Definitions

  • the invention relates to a method for obtaining an air product in an air separation plant and to an air separation plant configured for carrying out such a method.
  • pressurized oxygen is needed, for the production of which air separation plants with so-called internal compression can be used.
  • air separation plants are also described for example in Häring and explained with reference to the local figure 2.3A.
  • a cryogenic liquid in particular liquid oxygen
  • the internal compression has, among other things, energy advantages compared to a subsequent compression of an already gaseous product.
  • cryogenic liquid is brought from the liquid state into a supercritical state.
  • the term "pseudo-vaporization” or “liquefaction” is used.
  • the high-pressure heat carrier is liquefied (or possibly subjected to a "pseudo-liquefaction" when it is under supercritical pressure).
  • the heat transfer medium is frequently formed by a part of the air supplied to the air separation plant.
  • the present invention proposes a method for obtaining an air product in an air separation plant and an air separation plant equipped for carrying out such a method with the features of the independent patent claims.
  • Preferred embodiments are subject of the dependent claims and the following description.
  • the present application uses the terms "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 losses or expected pressure drops, for example due to cooling effects or Line losses, a.
  • the pressure levels indicated here in bar are absolute pressures.
  • the present invention proposes a method of recovering an air product by means of an air separation plant having a distillation column system and a tank system having a first tank and a second tank.
  • a cryogenic liquid for example pure oxygen or one of the other air products explained above, is removed from the distillation column system and stored at least partly in liquid form in the tank system. After removal from the tank system, the cryogenic liquid may be used as the air product.
  • a tank system with a first and a second tank is used, which are charged in alternating operation with the cryogenic liquid.
  • the cryogenic liquid is supplied to the first tank and not to the second tank during a first period and to the second tank and not to the first tank during a second period.
  • the alternate operation further includes taking the cryogenic liquid from the first tank rather than the first tank during the first time period and the first tank and not the second tank during the second time period. It may also be provided to use more than two tanks, which are subjected to a corresponding cycle. However, these always include a first and a second tank and a corresponding supply or withdrawal in a first or second period.
  • the present invention therefore proposes to use as the tank system a tank system with an additional third tank, wherein the cryogenic liquid, which is taken during the first period of the second tank and during the second period of the first tank, at least partially (and in particular at least temporarily) is transferred unheated in the third tank. It may therefore be provided in this context, only a part of the cryogenic liquid, which is taken during the first period of the second tank and during the second period of the first tank unheated transferred to the third tank and another part of the cryogenic liquid directly, as explained below, via a by-pass as an air product or to use in another form.
  • the third tank serves as a template or buffer storage, which is filled with a suitable amount of cryogenic liquid, which is sufficient to bridge the previously explained periods.
  • a transfer to the third tank is "unheated" when the cryogenic liquid, which is taken during the first period of the second tank and during the second period of the first tank, at the removal temperature level of the second or first tank is transferred to the third tank.
  • the cryogenic liquid is not subjected to active temperature-increasing measures or heating.
  • the cryogenic liquid is thus led in particular by no heat exchanger, heater, countercurrent, etc. for heating.
  • temperature level this does not exclude that, due to unavoidable heat inputs, there is a certain, but not active, heating.
  • the term "temperature level” takes this into account, so that the aforementioned removal temperature level can still be within the specified extent below a feed temperature level in the third tank.
  • the unheated transfer to the third tank is therefore particularly to avoid evaporation losses.
  • the cryogenic liquid stored in the first and second tanks is no longer or not exclusively discharged therefrom and used as the air product. Rather, the air product is provided, at least in part, using the cryogenic liquid transferred unheatedly into the third tank, or a portion thereof.
  • cryogenic liquid that has been unheatedly transferred to the third tank is used to provide the air product.
  • Part of the cryogenic liquid transferred unheated into the third tank can be taken out of the third tank and used in a different way. It is also possible that, for example, the portion of the cryogenic liquid evaporated in the respective tanks is not used to provide the air product.
  • cryogenic liquid used to provide the air product is taken from the third tank in liquid state from the third tank, evaporated or transferred from the liquid to the supercritical state and discharged from the air separation plant, and / or that the cryogenic liquid used to provide the air product is taken out of the third tank in the liquid state and stored liquid in a fourth tank in a liquid state.
  • the fourth tank can be part of the tank system with the first to third tank, but it can also be provided separately, for example as part of another tank system.
  • the fourth tank may be located within the air separation plant, for example within a cold box, or within a thermally insulating outer shell which also includes the first to third tanks.
  • the fourth tank can also be arranged outside the air separation plant.
  • the air product may thus be a gaseous or supercritical air product and / or a liquid air product.
  • the gaseous air product can also be stored inside or outside the air separation plant, in particular in a corresponding gas tank.
  • the cryogenic liquid is removed from the distillation column system of the air separation plant at a pressure level on which a corresponding column of the distillation column system, in particular a pure oxygen column, hereinafter also referred to as "second separation column", is operated.
  • the cryogenic liquid is supplied to the first tank and the second tank of the tank system at a pressure level referred to herein as a "first" pressure level.
  • the first pressure level may correspond to the pressure level at which the cryogenic liquid was withdrawn from the distillation column system if no pressure-influencing devices such as pumps are arranged between the separation column and the first and second tanks, respectively. If, for example, a corresponding pump is used, the first pressure level can also be above the pressure level of the separation column.
  • the cryogenic liquid is supplied to the third tank of the tank system at a second, higher pressure level (storage pressure), which can depend in particular on the pressure (product pressure) at which the air product is to be provided.
  • the storage pressure is advantageously slightly above the product pressure, so that a discharge is possible without additional pumps or compressors.
  • the second pressure level can be achieved, in particular, by making a pressure build-up evaporation in the first and / or the second tank.
  • the present invention through the use of the illustrated tank system and pressure increase, combines the advantages of a traditional internal compression process, namely the continuous production of the air product, with the advantages of improved analysis capability. Through this improved analysis option, a high purity of the air product can be guaranteed and documented at any time.
  • evaporation or conversion to the supercritical state can be carried out within the air separation plant used, for example using its main heat exchanger.
  • a backup system with a standby evaporator that does not draw heat of vaporization from the air separation plant can also be used.
  • cryogenic liquid can also be discharged from the third tank (or via the bypass lines from the first and the second tank) in liquid form from the air separation plant, in liquid form, for example in a tank. transported to a consumer and used there in liquid or (after evaporation) gaseous state.
  • the first pressure level ie the pressure level at which the cryogenic liquid is supplied to the first and the second tank, is approximately 1.3 to 4 bar.
  • the second pressure level is, depending on the requirement, at 2 to 100 bar, but above the first pressure level.
  • a particularly flexible pressure increase in time can take place taking into account the pressure requirements of a consumer.
  • the cryogenic liquid may be brought to the first pressure level before being fed to the first tank and the second tank using a pump.
  • the present invention combines the advantages of conventional in this embodiment Internal compression method using appropriate pumps, however, do not allow the implementation of discontinuous analysis methods due to the continuous pressure increase, with processes in which alternately different tanks are charged.
  • the invention develops particular advantages in air separation plants that have very high purity requirements of the respective air product, such as oxygen.
  • conventional fast (routine) analytical methods can approach the detection limit, and more sensitive analytical methods such as gas chromatography must be used.
  • more sensitive analysis methods take much longer to determine the measured value than conventional methods, so that a discontinuous measurement must be carried out.
  • the inventive method also saves energy compared to methods in which an evaporation of a corresponding air product, such as oxygen, takes place only at the consumer. Overall, energy savings of about 1 kW per Nm 3 / h of oxygen can be achieved.
  • the present invention can be used in principle and with particular advantage in corresponding tank systems with pure pressure build-up evaporation. In this way, can be completely dispensed with a pump, which allows a more cost-effective creation of a corresponding air separation plant.
  • the absence of moving or driven parts in a pressure build-up evaporation allows a particularly energy-saving and low-maintenance operation.
  • the evaporation losses which inevitably result in a pressure build-up evaporation do not fall into consideration, in particular, if a gaseous or supercritical air product is to be provided anyway.
  • a combination of an increase in pressure by means of a pump and an additional pressure build-up evaporation is possible.
  • the method according to the invention is particularly suitable for providing highly pure air products, because a discontinuous analysis before heating and delivery to the plant boundary is possible.
  • a purity of the cryogenic liquid which is supplied to the first tank during the first period and to the second tank during the second period is advantageously determined.
  • Conventional methods for purity testing for example spectroscopic methods and / or gas chromatography, can be used for a corresponding analysis.
  • the cryogenic liquid is advantageously transferred from the second tank and into the third tank during the first period and from the first tank during the second period and into the third tank during the second period if its purity corresponds to a preset value.
  • the third tank is thus always filled with cryogenic liquid of defined purity and can be used at any time without additional analysis to provide the air product.
  • the present invention proves by the use of a third tank as particularly advantageous because a corresponding interruption can be compensated by removing the cryogenic liquid from the third tank.
  • an amount of the cryogenic liquid is kept, which is at least as large as a quantity of the cryogenic liquid which can be stored in the first tank and / or in the second tank, or at least as large is that the switching times, during which no liquid can be removed from the first two containers, bridged to allow a continuous withdrawal. In this way, deep cryogenic liquid can be continuously heated and released as an air product, even if the contents of a completely filled first or second tank must be returned or discarded due to a non-default purity in the distillation column system.
  • the present invention is used in air separation plants for the production of pure oxygen.
  • the distillation column system has a first separation column and a second separation column.
  • a fluid stream enriched in a first oxygen content of oxygen is generated using which liquid pure oxygen is generated in the second separation column, which is withdrawn from the second separation column at least in part as the cryogenic liquid.
  • the present invention allows continuous supply of high purity oxygen through the use of the third tank.
  • Such a method comprises, using the first separation column, further generating a fluid stream enriched in a second oxygen content of oxygen and a fluid stream enriched in a third oxygen content of oxygen.
  • the fluid stream enriched in oxygen at the second oxygen content is advantageously taken from the first separation column below the fluid stream enriched in oxygen at the first oxygen content. He therefore has a higher oxygen content.
  • the fluid stream enriched in the third oxygen content of oxygen is advantageously taken from the bottom of the first separation column.
  • the two fluid streams are then in particular in one Head condenser of the first separation column and heated in a main heat exchanger to different temperatures, wherein the oxygen enriched to the second oxygen content, heated fluid stream is at least partially compressed in a compressor coupled with a relaxation machine, cooled and recycled to the first separation column.
  • part of the fluid stream enriched in the third oxygen content of oxygen is used to drive the expansion machine.
  • a main heat exchanger of the air separation plant is used for heating the cryogenic liquid which is subsequently provided as the air product.
  • a separate evaporator may also be used.
  • a corresponding evaporator can also be used in particular if a capacity of the main heat exchanger of the air separation plant is insufficient and / or if additional amounts of air products are to be provided than it is able to provide a corresponding main heat exchanger (also temporary).
  • the present invention also extends to an air separation plant adapted to recover an air product.
  • the air separation plant comprises a distillation column system and a tank system with a first tank and a second tank and has features as indicated in the corresponding device claim.
  • a corresponding air separation plant is set up for carrying out a method, as has been explained in detail above. Reference should therefore be made to the relevant features and advantages at this point.
  • FIGS. 2 and 3 each show tank systems, as in an air separation plant according to FIG. 1 or a deviating trained air separation plant may be involved.
  • the integration of the tank system results from the also in FIG. 1 specified elements.
  • FIG. 1 an air separation plant according to an embodiment of the present invention is shown schematically in the form of an installation diagram.
  • the air separation plant is designated 100 in total.
  • Atmospheric air 1 is sucked in via a filter 2 from an air compressor 3 and compressed there to an absolute pressure of 6 to 20 bar, preferably about 9 bar.
  • the compressed air 6 is cleaned in a cleaning device 7 which has a pair of containers filled with adsorption material, preferably molecular sieve.
  • the purified air 8 is cooled in a main heat exchanger 9 to about dew point and partially liquefied.
  • a first part 11 of the cooled air 10 is introduced via a throttle valve 51 into a first separation column 12, which is designed as a single column.
  • the feed is preferably some practical or theoretical soils above the sump.
  • the operating pressure of the first separation column 12 is at the top 6 to 20 bar, preferably about 9 bar.
  • Your top condenser 13 is cooled with a fluid stream 18 and a fluid stream 14.
  • the fluid stream 18 is from an intermediate point some practical or theoretical plates above the air supply or at the same level as this, the fluid stream 14 withdrawn from the bottom of the first separation column 12.
  • the fluid stream 18 has been referred to in the above discussion as a "second oxygen oxygenated fluid stream" and the fluid stream 14 is referred to as a "third oxygen oxygenated fluid stream.”
  • gaseous nitrogen 15, 16 is withdrawn at the top of the first separation column 12, heated in the main heat exchanger 9 to about ambient temperature and finally withdrawn via line 17 as gaseous pressure product (PGAN). Additional gaseous nitrogen is passed through the top condenser 13. A part 53 of the condensate 52 obtained in the top condenser 13 may be recovered as liquid nitrogen product (PLIN); the rest 54 is given up as reflux to the top of the separation column 12.
  • PLIN liquid nitrogen product
  • the fluid flow 14 is in the top condenser 13 under a pressure of 2 to 9 bar, preferably about 4 bar, evaporated and then flows in gaseous form via a line 19 to the cold end of the main heat exchanger 9. From this it is taken at an intermediate temperature in the form of the stream 20 and in a relaxation machine 21, which is designed in the example shown as a turboexpander, work-performing expanded to about 300 mbar above atmospheric pressure.
  • the expansion machine 21 is mechanically coupled to a (cold) compressor 30 and a braking device 22, which is formed in the illustrated example by an oil brake.
  • the expanded fluid stream 23 is heated in the main heat exchanger 9 to approximately ambient temperature.
  • the warm fluid stream 24 is blown off into the atmosphere (ATM) as fluid flow 25 and / or used as regeneration gas 26, 27, optionally after heating in the heating device 28.
  • ATM atmosphere
  • the fluid stream 18 is vaporized in the top condenser 13 under a pressure of 2 to 9 bar, preferably about 4 bar, and flows in gaseous form via a line 29 to the compressor 30, in which it is recompressed to approximately the operating pressure of the first separation column 12.
  • the recompressed fluid stream 31 is cooled again in the main heat exchanger 9 to column temperature and finally fed via line 32 of the first separation column 12 at the bottom again.
  • the explained treatment of the fluid streams 14 and 18 corresponds to the already mentioned, so-called SPECTRA method.
  • a fluid stream 36 is withdrawn from an intermediate location of the separation column 12 in the liquid state, leaving 5 to 25 theoretical or practical levels above the air supply is arranged.
  • the fluid stream 36 is optionally subcooled in a sump evaporator 37 of a second separation column 38, which is designed as a pure oxygen column, and then fed via a line 39 and a throttle valve 40 to the top of the second separation column 38.
  • the operating pressure of the second separation column 38 (at the top) is 1.3 to 4 bar, preferably about 2.5 bar.
  • the sump evaporator 37 of the second separation column 38 is also operated by means of a second part 42 of the cooled feed air 10.
  • the feed air stream 42 is thereby at least partially, for example completely, condensed and flows via a line 43 to the first separation column 12, where it is introduced approximately at the level of feeding the remaining feed air 11 or into the column bottom.
  • cryogenic liquid 41 From the bottom of the second separation column 38 pure oxygen is removed as cryogenic liquid 41, optionally brought by a pump 55 to an elevated pressure of 2 to 100 bar, preferably about 12 bar, and in a tank assembly 70, which in the following FIGS. 2 and 3 is fed. After an intermediate storage in the tank assembly 70, the cryogenic liquid is passed via a line 56 to the cold end of the main heat exchanger 9, evaporated there under the increased pressure and warmed to about ambient temperature and finally recovered via line 57 as a gaseous product (GOX-IC).
  • GOX-IC gaseous product
  • a top gas 58 of the second separation column 38 is admixed with the above-explained expanded second fluid stream 23 (see link A). If necessary, part of the feed air for pump prevention of the cold compressor 30 is led to its inlet via a bypass line 59 (so-called anti-surge control).
  • liquid separation plant 100 upstream of and / or downstream of the pump 55 liquid oxygen can be removed as a liquid fraction (in the drawing with LOX).
  • an external liquid such as liquid argon, liquid nitrogen or liquid oxygen, even from a liquid tank, in the main heat exchanger 9 are evaporated in indirect heat exchange with the feed air (not shown in the drawing).
  • FIG. 2 is a tank system according to an embodiment of the invention, which in an air separation plant 100, as shown in FIG. 1 is illustrated, illustrated in the form of a schematic system diagram and designated overall by 70.
  • the cryogenic liquid of the fluid flow 41 is brought from a first pressure level to a second pressure level.
  • the first pressure level may in particular correspond to a pressure level at which a second separation column 38 (pure oxygen column) of an air separation plant 100, as described in US Pat FIG. 1 is shown, can be operated.
  • the second pressure level is for example 2 to 100 bar.
  • the pressure-increased fluid flow 41 is supplied to a first tank 71 or a second tank 72.
  • the tanks 71 and 72 are alternatively charged with the cryogenic liquid of the fluid flow 41, i.e., with each other. during a first period, the cryogenic liquid of the fluid stream 41 is supplied to the first tank 71 and not to the second tank 72 and to the second tank 72 and not the first tank 71 for a second period.
  • a tank controller 80 may be provided, for example.
  • a third tank 73 As already explained, it can also be provided, for example, when the third tank 73 is completely filled, as illustrated here by means of a line 74, to forward corresponding fluid directly and to supply it to a heating.
  • the heating of the fluid can, as also mentioned, for example, in a main heat exchanger 9 of a corresponding air separation plant, for example, the air separation plant 100 according to FIG. 1 , and / or take place in an additional evaporator 90.
  • FIG. 3 illustrates a tank system according to another embodiment of the invention in the form of a schematic diagram of the system.
  • the tank system of FIG. 3 is designated 70.
  • the tank system 70 which in FIG. 3 is equipped with a pressure build-up evaporator 75.
  • a pump 55 as in the tank system 70 according to FIG. 2 or in the air separation plant 100 according to FIG. 1 is optional here.
  • a corresponding pump 55 is regularly omitted and the cryogenic liquid of the stream 41 is fed to the tanks 71 and 72 at the distillation pressure in the pure oxygen column 38, which here corresponds to the "first pressure level".
  • the pressure build-up evaporator 75 a portion of the cryogenic liquid of the stream 41 removed in liquid form from the tanks 71 and 72 is vaporized.
  • the vaporized and pressurized gas is supplied to a head space of the tanks 71 and 72, respectively. In this way, the pump 55 can be saved and it can only be a pressure build-up evaporation used.
  • the cryogenic liquid used to provide the liquid air product may be removed from the third tank 73 in the liquid state and vaporized in the main heat exchanger 9 and / or in the additional evaporator 90 or transferred from the liquid to the supercritical state and discharged from the air separation plant become.
  • the cryogenic liquid used to provide the liquid air product can also be removed from the third tank 73 in the liquid state and stored in a fourth tank 76 until it is liquid. Details have already been explained. Further withdrawals upstream and / or downstream of the third tank 73 are possible.

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  • 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)
EP17020003.4A 2016-01-14 2017-01-02 Verfahren zur gewinnung eines luftprodukts in einer luftzerlegungsanlage und luftzerlegungsanlage Active EP3193114B1 (de)

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US (1) US10209004B2 (zh)
EP (1) EP3193114B1 (zh)
KR (1) KR20170085449A (zh)
CN (1) CN107238255B (zh)
TW (1) TWI712770B (zh)

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JP6900241B2 (ja) * 2017-05-31 2021-07-07 レール・リキード−ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード ガス製造システム
WO2021129948A1 (de) 2019-12-23 2021-07-01 Linde Gmbh Verfahren und anlage zur bereitstellung eines sauerstoffprodukts
CN111273570B (zh) * 2020-02-19 2021-07-06 北京天拓集智科技有限公司 一种空气分离设备的控制方法
KR20230069966A (ko) 2020-09-17 2023-05-19 린데 게엠베하 혼합 가스 터빈을 이용한 공기의 극저온 분리를 위한 공정 및 장치

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DE676616C (de) 1936-09-04 1939-06-08 Messer & Co Gmbh Verfahren zur Erzeugung von unter Druck stehendem gasfoermigem Sauerstoff
US5148680A (en) * 1990-06-27 1992-09-22 Union Carbide Industrial Gases Technology Corporation Cryogenic air separation system with dual product side condenser
US6295840B1 (en) 2000-11-15 2001-10-02 Air Products And Chemicals, Inc. Pressurized liquid cryogen process
DE102007051184A1 (de) 2007-10-25 2009-04-30 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Tieftemperatur-Luftzerlegung
CN103092339B (zh) * 2012-12-13 2015-10-07 鸿富锦精密工业（深圳）有限公司 电子装置及其页面演示方法
EP2979051B1 (de) * 2013-03-28 2019-07-17 Linde Aktiengesellschaft Verfahren und vorrichtung zur erzeugung von gasförmigem drucksauerstoff mit variablem energieverbrauch
WO2014173496A2 (de) * 2013-04-25 2014-10-30 Linde Aktiengesellschaft Verfahren zur gewinnung eines luftprodukts in einer luftzerlegungsanlage mit zwischenspeicherung und luftzerlegungsanlage

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EP3193114A1 (de) 2017-07-19
TW201730493A (zh) 2017-09-01
KR20170085449A (ko) 2017-07-24
CN107238255B (zh) 2021-03-16
CN107238255A (zh) 2017-10-10
US20170205142A1 (en) 2017-07-20
US10209004B2 (en) 2019-02-19

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