EP3559576A2 - Procédé de séparation cryogénique d'air et système de séparation de l'air - Google Patents

Procédé de séparation cryogénique d'air et système de séparation de l'air

Info

Publication number
EP3559576A2
EP3559576A2 EP17844599.5A EP17844599A EP3559576A2 EP 3559576 A2 EP3559576 A2 EP 3559576A2 EP 17844599 A EP17844599 A EP 17844599A EP 3559576 A2 EP3559576 A2 EP 3559576A2
Authority
EP
European Patent Office
Prior art keywords
gaseous
pressure
column
pressure column
stream
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP17844599.5A
Other languages
German (de)
English (en)
Inventor
Stefan Lochner
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from DE102016015446.2A external-priority patent/DE102016015446A1/de
Application filed by Linde GmbH filed Critical Linde GmbH
Publication of EP3559576A2 publication Critical patent/EP3559576A2/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04163—Hot end purification of the feed air
    • F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
    • F25J3/04175—Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
    • 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
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/10—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream 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
    • 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
    • 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
    • F25J2240/44—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 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being 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
    • 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 for the cryogenic separation of air and an air separation plant according to the preambles of the independent claims.
  • Air separation plants have distillation column systems which can be designed, for example, as two-column systems, in particular as classic Linde double-column systems, but also as three-column or multi-column systems.
  • distillation column systems which can be designed, for example, as two-column systems, in particular as classic Linde double-column systems, but also as three-column or multi-column systems.
  • Distillation columns for the recovery of nitrogen and / or oxygen in the liquid and / or gaseous state ie the distillation columns for nitrogen-oxygen separation, distillation columns for obtaining further air components, in particular the noble gases krypton, xenon and / or argon, can be provided.
  • the distillation columns of said distillation column systems are 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, in particular about 5 bar.
  • the low-pressure column is at a pressure level of, for example, 1, 3 to 1, 7 bar, in particular about 1, 5 bar operated.
  • pressures of 3 to 4 bar can also be used in the low pressure column.
  • the pressures given here and below are absolute pressures at the top of said columns. From EP 0 955 509 A1 a method and a device for air separation are known, which serve for the production of high-purity oxygen. An oxygen-containing liquid fraction is taken from at least one theoretical or practical bottom above the sump of the high pressure column and in the
  • Low pressure column fed Gaseous nitrogen from the low pressure column is at least partially condensed in a top condenser by indirect heat exchange with a vaporizing liquid. At least a portion of the bottom liquid of the high pressure column is passed into the evaporation space of the top condenser of the low pressure column. From the lower part of the low-pressure column, a high-purity oxygen product is taken.
  • DE 25 26 350 A1 discloses a method for air separation with recovery of liquid oxygen and / or nitrogen by the so-called Mehtfachexpansions- method in an air separation plant with a high-pressure column, wherein a task-working pressure of the air to be processed against an operating pressure of
  • High pressure column is increased by several atmospheres.
  • a method described in EP 1 357 342 A1 and a corresponding device are used for air separation of air in a distillation column system for nitrogen-oxygen separation, which comprises a high-pressure column, a low-pressure column and a medium-pressure column and a crude argon column. At least one
  • Feed air stream is fed to the distillation column system.
  • Low pressure column is removed at least one oxygen or nitrogen product stream.
  • At least one first argon-enriched stream becomes the
  • Rohargon yarn is taken from an argon-rich fraction whose argon content is greater than that of the first argon-enriched stream.
  • the first argon-enriched stream is taken from the medium-pressure column.
  • a double column is used, the low-pressure column of which is operated at a pressure which is significantly above atmospheric pressure, in particular of the order of 2 to 5 bar.
  • the high pressure column operated at a corresponding pressure
  • Gaseous oxygen is taken directly from a lower area of the low-pressure column and the apparatus is at least partially kept cold by free expansion of at least one gaseous product leaving the low pressure column.
  • EP 2 801 777 A1 relates to an air separation plant with a
  • a distillation column system comprising at least one high pressure column and a
  • Low pressure column includes and a corresponding method.
  • Main compressor unit is adapted to a total amount of air that the
  • Air separation plant is supplied in total, to compress to a pressure which is at least 4 bar higher than an operating pressure for which the high-pressure column is established.
  • the main compressor unit has a slip-ring rotor motor.
  • the present invention has the particular object of making the creation of air separation plant easier. Disclosure of the invention
  • the present invention proposes a method for
  • Fluids and gases may be rich or poor in one or more components as used herein, with “rich” being for a content of at least 50%, 75%, 90%, 95%, 99%, 99.5%, 99, 9% or 99.99% and “poor” for a content not exceeding 50%, 25%, 10%, 5%, 1%, 0.1% or 0.01% by mol, Weight or volume can stand.
  • the term “predominantly” can correspond to the definition of "rich”.
  • Liquids and gases may also be enriched or depleted in one or more components, which terms refer to a content in a source liquid or gas from which the liquid or gas was recovered.
  • the liquid or gas is "enriched” if it or this is at least 1, 1, 5, 1, 5, 2, 5, 10, 100 or 1, 000 times, and "depleted” if this or this is 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 contains.
  • oxygen or “nitrogen”
  • the present application uses the terms "pressure level” and "temperature level” to characterize pressures and temperatures, thereby indicating that corresponding pressures and temperatures in a given plant need not be used in the form of exact pressure or temperature values to realize the innovative concept. However, such pressures and temperatures typically range in certain ranges, such as ⁇ 1%, 5%, or 10% around an average.
  • pressure levels and temperature levels can be in disjoint areas or in areas that overlap one another.
  • pressure levels include unavoidable or expected pressure drops.
  • temperature levels The same applies to temperature levels.
  • the pressure levels indicated here in bar are absolute pressures.
  • Such nitrogen is nitrogen taken from the air separation plant in the form of a liquid or gaseous nitrogen product (as is typically not the case in the present invention), and the nitrogen which is throttled and discarded as explained below. But this also applies internally compressed nitrogen, ie liquid nitrogen, which is taken from the high-pressure column, pressurized in a pump and evaporated in the main heat exchanger. Internal compaction is also explained, for example, in Häring, section 2.2.5.2, "Internal Compression".
  • An "argon discharge” is here generally understood as a measure in which a fluid is withdrawn from the low-pressure column which is enriched in argon with respect to an oxygen-rich liquid fed from the low-pressure column, in particular the low-pressure column bottoms product, i. For example, has at least twice, five times or ten times the argon content.
  • An argon discharge further comprises, at least a portion of the in one
  • Oxygen in the low-pressure column itself is generally expensive and requires a corresponding "heating" capacity of the main capacitor. If argon is discharged and thus omits the oxygen-argon separation or this is displaced, for example, in a crude argon or Argonausschleuskla, the corresponding amount of argon must not be separated in the oxygen section of the low pressure column and the heating power of the main capacitor can be reduced. Therefore, with the same yield of oxygen, either more air injected into the low-pressure column or more pressure nitrogen from the
  • High-pressure column are removed, which in turn provides energy benefits.
  • an "argon discharge column” can be understood to mean a separation column for argon-oxygen separation which is not suitable for
  • Argon discharge column connected to an intermediate point of the low-pressure column and the argon discharge column is cooled by a top condenser, on its evaporation side typically relaxed bottom liquid from the
  • An argon discharge column typically does not have a bottom evaporator.
  • the present invention is based on the recognition that in one
  • Air separation plant designed primarily for the production of pure oxygen with a content of at least 90% or 95%, in particular from 99 to 99.96%, taken from the high-pressure column nitrogen in a certain amount, an isenthalpic relaxation, i. in particular a throttle relaxation, can be supplied and discarded.
  • an isenthalpic relaxation i. in particular a throttle relaxation
  • a throttle relaxation of other gaseous streams is, as also explained in detail below, advantageous.
  • the present invention will be described primarily with reference to the nitrogen taken from the high-pressure column.
  • the standardization of an air separation plant typically includes the
  • the maximum capacity ie the maximum demountable air volume, from the standard dimensions and the
  • Product spectrum (i.e., the respective amounts) of the air products taken from the rectification.
  • the components, in particular the distillation columns, are dimensioned such that no product is discarded. Is the product range outside of the
  • Transport limitations in height (transport height) the capacity can be increased.
  • Drosselentlement to supply to the pressure level of the low pressure column and feed into the low pressure column.
  • packings with different packing densities are used. The packing densities are
  • Has separation capacity In other words, there are overcapacities in the separation performance in the low-pressure column in such areas, which can be used for the air fed in here. In this way, capacity reserves can be used in the context of the present invention.
  • Embodiments of the isenthalp relaxation must be subjected to a sufficient amount of fluid in order to achieve the respective advantageous effects or to show a corresponding effect at all.
  • the respective gaseous material flows be it nitrogen from the high-pressure column or another gaseous one Fluid, are therefore supplied in an appropriate amount of isenthalpic relaxation.
  • a quantity of at least 500 standard cubic meters per hour has been found to be particularly advantageous.
  • an air separation plant in which, for example, about 500,000 standard cubic meters of air per hour used in total, ie compressed in the air separation plant (especially in the main air compressor) and cooled (especially in the main heat exchanger), this corresponds to 0.1% of the amount of air used.
  • the present invention is distinguished in particular from methods in which small amounts of gaseous fluids, for example components which are not condensable in a condensation chamber of a condenser evaporator, are withdrawn and, if appropriate, likewise subjected to isenthalpic expansion.
  • Such non-condensable components are, in particular, helium, neon and hydrogen.
  • atmospheric air is about 0.00052% (helium), about 0.0018% (neon) and about 0.00006% (hydrogen), so their total amount is 0.00238%.
  • significantly lower amounts of substance, if any, would be fed to an isenthalpic expansion, since corresponding components are not available in greater quantities in uncondensed form.
  • the material stream or streams which are provided in gaseous form and subjected to isenthalpentation may also be subjected to expansion in addition to a stream of material optionally also provided in gaseous form and fed to an argon discharge column or crude argon column (see below) can be provided. In this way, the advantages mentioned can be achieved.
  • the material stream (s) provided gaseously and subjected to isenthalpent expansion have an argon content of less than 1.5 mol%, in particular less than 1 mol%.
  • the advantages mentioned can be achieved by using gaseous feed air which has been compressed to the pressure level of the high-pressure column and / or by using a material stream taken off in gaseous form from the high-pressure column. Therefore, the isenthalic relaxation always takes place starting from a corresponding one
  • Pressure level that is at the pressure level of the high pressure column or a pressure level that differs by no more than 1% of this.
  • the gaseous material stream (s) subjected to isenthalpic relaxation are further provided at a temperature level corresponding to at least one temperature level present in the high pressure column. It may in particular be a temperature level at the top of the high-pressure column or at an extraction point of the or one of the isenthalp to relaxing gaseous streams from the
  • Act high-pressure column It can also be a lowest temperature level to which air in the air separation plant is compressed.
  • the gaseous material streams are or are advantageously fed at least at this temperature level to isenthalpic expansion, i. Although heated if necessary, before isenthalpen relaxation, as explained below, but not further cooled.
  • the present invention proposes a process for the cryogenic separation of air using an air separation plant having a distillation column system comprising a high pressure column operating at a first pressure level and a low pressure column operating at a second pressure level below the first pressure level.
  • a high pressure column operating at a first pressure level
  • a low pressure column operating at a second pressure level below the first pressure level.
  • Air separation plant one or more gaseous streams formed and subjected to an isenthalp relaxation, starting from the first pressure level or a pressure level which is not more than 1 bar from the first
  • Pressure level is different, is performed, and in which a pressure difference of 3 to 6 bar is overcome.
  • the pressure difference is in particular 3 to 5 bar, preferably 3.5 to 4.5 bar, for example about 4 bar.
  • the isenthalpic expansion can be carried out in particular starting from a pressure level which differs by no more than 0.5 bar, 0.2 bar or 0.1 bar from the first pressure level. Further details and the associated advantages have already been explained.
  • the pressure difference may in particular correspond to the difference between the first pressure level, that is to say the operating pressure of the high-pressure column, and a discharge pressure. In the case of isenthalp relaxation, it may in particular be a
  • the gaseous material stream (s) subjected to gaseous expansion comprises or comprise a quantity of fluid of at least 500 standard cubic meters per hour.
  • the measures carried out according to the invention differ from conventional methods in which small amounts are not condensable
  • Components are removed from the condenser evaporator.
  • the latter can be done in the context of the present invention additionally.
  • the gaseous material stream (s) subjected to gaseous expansion has or have an argon content of not more than 1.5% mole percent, in particular not more than 1 mole percent. Therefore, any further streams which are processed in a crude argon column or argon discharge column (see below), as likewise possible in the context of the present invention, are not covered by this or these streams.
  • the gaseous streams which is or are subjected to the isenthalp relaxation is or become at a temperature level
  • Gaseous material streams are or will advantageously be at least at this temperature level of isenthalpy
  • the temperature level at which the gaseous material streams or are formed is or is in particular above -200 ° C, preferably above -150 ° C, and especially below 100 ° C, preferably below 50 ° C. It can also be cooled to a lowest temperature level, to which air in a main heat exchanger of the air separation plant is cooled. Will be inserted as explained below
  • the temperature level of its formation corresponds to that at the sampling point. If, however, a corresponding gaseous stream of compressed and cooled feed air is formed, the temperature level corresponds to its formation of the corresponding
  • the isenthalp relaxation can be carried out at a temperature level of 0 to -200 ° C, in particular a temperature level of -150 to -200 ° C, for example about -170 ° C, i. in particular on the basis of such a temperature level, ie at a typical rectification temperature of air.
  • a corresponding stream of material is typically previously in one
  • the or one of the gaseous streams subjected or to be subjected to isenthalpic expansion, in particular compressed and cooled air may or may be a gaseous nitrogen-rich fluid withdrawn from an upper region of the high-pressure column an atmospheric nitrogen-enriched gaseous fluid from an intermediate region of the high-pressure column.
  • the "upper region” of the high-pressure column is, in particular, a region near or at the top of the high-pressure column which is free of separating internals, the "intermediate region” represents, in particular, an area otherwise provided with separating internals which is arranged between the top and bottom of the high-pressure column.
  • a nitrogen-rich first material stream is formed using a nitrogen-rich first fluid which is taken off in gaseous form from the high-pressure column at the first pressure level.
  • a second fluid which is taken from the low-pressure column in gaseous form at the second pressure level, a second material flow is formed in a further embodiment of the present invention.
  • a "formation" of a material flow "using" a fluid may comprise both that exclusively the fluid mentioned is used for the provision of the material stream, and that the material flow is generated from a plurality of fluids.
  • a "second" stream in the context of the present invention can be formed, for example, exclusively using “impure nitrogen” from the top of the low-pressure column.
  • the nitrogen-rich first stream and, if formed in the further embodiment, the second stream are permanently removed from the distillation column system. This is understood to mean that the said material flows are not in the
  • the nitrogen-rich first stream thus differs from streams, in the form of which, as far as known, for example, pressure nitrogen from the head of the
  • High pressure column deducted and fed into the low pressure column.
  • the nitrogen-rich first stream at least to a portion of the isenthalpen mentioned several times
  • Relaxation in particular a Drosselentschreib, is supplied.
  • the isenthalp or throttle-relieved nitrogen rich first stream or its part is discarded, ie it is not used as a product of the air separation plant.
  • the amount of the nitrogen-rich first fluid taken from the high-pressure column is, for example, up to 20%, in particular up to 8%, and more particularly at least 1, 2, 3, 4 or 5% of the total amount of air fed into the distillation column system.
  • a "throttling relaxation" in the parlance of the present invention is a relaxation in which a stream or a corresponding part is passed through one or more throttle valve and thereby undergoes a pressure reduction. In throttle relaxation can, but it must not be the only relaxation, which is subjected to the nitrogen-rich first stream in the present case. Throttling relaxation proves to be extremely cost-effective, especially for smaller amounts of nitrogen.
  • the isenthalpe or throttling release of the first material flow or its isenthalpic or throttling release component is, in particular, brought to a third pressure level, which is in particular greater than or equal to the second pressure level, i. in particular greater than or equal to the pressure level of the second material flow or the low-pressure column, carried out.
  • the third pressure level corresponds to the second pressure level.
  • the first material flow or its portion can be fed to the second flow of material after throttling relaxation.
  • Material stream is provided in the context of another embodiment of the present invention that cooled compressed air provided at the first pressure level and fed to a first portion in the high pressure column and fed to a second portion of the isenthalp relaxation, in particular a Drosselentschreib to the second pressure level and the low pressure column is fed.
  • the provision of the compressed air at the first pressure level comprises that a portion of an amount of feed air compressed in a main air compressor to the first pressure level in a main heat exchanger is brought to a temperature level which is below or close to the liquefaction temperature of air.
  • the nitrogen-rich first fluid is advantageously taken from the high-pressure column at a first temperature level, and the nitrogen-rich first material stream is formed at the first temperature level.
  • This first temperature level thus corresponds to the temperature of the fluid at the removal point from the
  • High-pressure column is removed, which are subjected to isenthalp relaxation and / or a portion of the first stream can be heated from the first to a second temperature level and then subjected to the isenthalp relaxation.
  • Air separation plant and in particular to a lying above 0 ° C (second) temperature level.
  • the first temperature level is in particular from 0 to -200 ° C., in particular from -150 to -200 ° C., for example about -170 ° C.
  • the second temperature level is in particular from 0 to -200 ° C., in particular from -150 to -200 ° C., for example about -170 ° C.
  • Temperature level is in particular at 0 to 100 ° C, in particular 10 to 50 ° C, for example about 20 ° C.
  • the second fluid which is taken from the low-pressure column and used in the formation of the second material flow, may in particular be a nitrogen-rich fluid which is taken from the low-pressure column at the top, and which has a content of 96%. to 99.999 mole percent nitrogen and otherwise predominantly oxygen or argon. If no pure nitrogen from the low-pressure column is required, advantageously only impure nitrogen is taken off at the top. If pure nitrogen is required, the low-pressure column is designed with a further section, as also shown in the figures. In the latter case, advantageously two nitrogen-rich fractions are withdrawn from the low pressure column.
  • the so-called impure nitrogen has a nitrogen content of about 96 to 99.99 mole percent of the so-called impure nitrogen content of at least 99.99% mole percent to 0.1 ppm oxygen.
  • the second fluid can therefore also be a nitrogen-rich fluid which is taken from the low-pressure column at the top, and which has a content of 96%. to 99.999 mole percent nitrogen and otherwise predominantly oxygen or argon. If no
  • enriched fluid which is taken from the low-pressure column via a side draw, and therefore has a correspondingly lower content of nitrogen.
  • Low pressure column is taken in gaseous form, are formed.
  • the additional fluid may be an oxygen-rich fluid, the low pressure column via a
  • the present invention also relates to an air separation plant with a
  • a distillation column system comprising a high pressure column adapted for operation at a first pressure level and a low pressure column adapted for operation at a second pressure level below the first pressure level.
  • the air separation plant according to the invention is characterized by means which are adapted to form one or more gaseous streams using the air in the air separation plant and an isenthalp relaxation from the first pressure level or a pressure level of not more than 1 bar of differs from the first pressure level, and thereby to overcome a pressure difference of 3 to 6 bar, wherein means are provided, which are adapted to the gaseous streams, or which is subjected to gaseous relaxation or in a quantity of fluid of at least 500 standard cubic meters per hour, and means are provided which are adapted to provide the gaseous material streams which are or are subject to gaseous expansion with an argon content of not more than 1.5 mole percent.
  • the air separation plant according to the invention which is advantageously set up for carrying out a method, as explained above, benefits in the same way from the advantages of the method according to the
  • Figure 1 illustrates an air separation plant according to an embodiment of the present invention.
  • FIG. 1 shows an air separation plant which is suitable for operation according to
  • Embodiment of the present invention is arranged.
  • the air separation plant is designated 100 in total.
  • feed air in the form of a stream a (AIR) is sucked by a main air compressor 101 in a feed air through a filter 102, there compressed to a first pressure level and a pre-cooling 103 and a purification 104, respectively.
  • the compressed, precooled and purified feed air is further pressurized in the form of a stream b in a booster 105 with aftercooler 106.
  • the air separation plant 100 may deviate from the illustrated example also be formed with main and Nachverêtr.
  • a first portion of the further pressurized in the booster 105 feed air is in the form of a stream c in a main heat exchanger 107 on a
  • a second portion of the further pressurized feed air in the booster 105 is in the form of a stream d in the
  • Main heat exchanger 107 cooled to a final temperature level and isenthalp relaxed in a throttle valve 109.
  • the relaxed feed air of the streams c and d is combined to form a stream e and partly in the form of a stream f in a High pressure column 1 1 1 and partly in the form of a stream g in one
  • Low-pressure column 112 of a distillation column system 10 which further comprises a
  • an oxygen-enriched liquid in the form of a stream h is withdrawn, passed through a subcooler 15, partly used for cooling in a top condenser of the crude argon column 1 13 and finally fed to the low-pressure column 1 12.
  • a nitrogen-rich fluid in the form of a stream i is withdrawn. This is liquefied in part in the form of a stream k in a main condenser 116, which connects the high-pressure column 11 1 and the low-pressure column 1 12 heat-exchanging. From this, a first portion in the form of a stream I as return to the high-pressure column 1 11 is returned and a second portion in the form of a stream m passed through the subcooler 1 15 and fed to the low-pressure column 112.
  • the not liquefied in the main capacitor 1 16 portion of the stream i is in the example shown to a first portion in the form of a stream n the
  • Main heat exchanger 107 is supplied and heated there and expanded to a second portion in the form of a material flow o isenthalp via a throttle valve 1 17 and fed to a stream p.
  • the stream p is a stream which is formed using impure nitrogen taken from the low pressure column 12 in the form of a stream j and passed through the subcooler 15.
  • the stream p also comprises oxygen-rich fluid which is taken from the low-pressure column 112 in the form of a stream z.
  • a formed in this way collecting stream q is also the
  • Main heat exchanger 107 supplied and heated there.
  • the collecting stream q is then partially blown off in the example shown to the atmosphere (ATM) and used in part in the pre-cooling 103 and the purification 104.
  • ATM atmosphere
  • a portion of the material flow r is branched off, expanded by means of an expansion valve 118 and fed to a stream s.
  • the stream s is a Stream which is formed using further nitrogen-rich fluid taken from the low pressure column 112, passed through the subcooler 15 and heated in the main heat exchanger 107.
  • a collecting stream t formed in this way can be used like the collecting stream q.
  • a portion of the corresponding nitrogen-rich fluid is discarded. Both possibilities can alternatively be used in embodiments of the present invention.
  • a remaining portion of the nitrogen-rich fluid can be used, for example, in the form of a stream of material u as a sealing gas for the compressors used (seal gas).
  • the low pressure column 1 12 oxygen-rich liquid is removed in the form of a stream v and by means of a pump 1 19 liquid pressure increases (internal compression). A portion thereof is heated in the form in the main heat exchanger 107, thereby converted into the gaseous or supercritical state and as gaseous
  • Oxygen pressure product (GOX IC1) provided. Another part is optionally supercooled in the subcooler 1 15 and provided as a liquid oxygen product (GOX).
  • Low pressure column 112 recycled and provided in part in the form of a stream w as a liquid nitrogen product (LIN).
  • Crude argon column 1 13 is liquefied, partly recycled as reflux to the crude argon column 1 13 and partly in the form of a stream of material x to the atmosphere
  • an argon-rich fluid in the form of a stream of material y can also be withdrawn from the crude argon column 1 13 in liquid form and made available as a liquid argon product (LAR).
  • LAR liquid argon product

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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)

Abstract

L'invention concerne un procédé de séparation cryogénique d'air à l'aide d'une installation de séparation d'air (100) comprenant un système de colonne de distillation (10) qui comporte une colonne à haute pression (111) fonctionnant à un premier niveau de pression et une colonne à basse pression (112) fonctionnant à un second niveau de pression inférieur au premier niveau de pression. Il est prévu, à l'aide de l'air dans l'installation de séparation d'air (100), de former au moins un flux gazeux et de soumettre celui-ci à une détente isenthalpique qui est effectuée à partir du premier niveau de pression ou d'un niveau de pression qui ne diffère de pas plus de 1 bar du premier niveau de pression, et pour laquelle une différence de pression de 3 à 6 bars est surmontée. Le ou les flux de gaz qui sont soumis à une détente gazeuse comportent une quantité de fluide supérieure à 500 mètres cubes étalon par heure, et le ou les flux de gaz qui sont soumis à une détente gazeuse ont une teneur en argon non supérieure à 1 % molaire. L'invention concerne également une installation de séparation d'air (100).
EP17844599.5A 2016-12-23 2017-12-20 Procédé de séparation cryogénique d'air et système de séparation de l'air Withdrawn EP3559576A2 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE102016015446.2A DE102016015446A1 (de) 2016-12-23 2016-12-23 Verfahren zur Tieftemperaturzerlegung von Luft und Luftzerlegungsanlage
EP17020072 2017-02-27
PCT/EP2017/025365 WO2018114052A2 (fr) 2016-12-23 2017-12-20 Procédé de séparation cryogénique d'air et système de séparation de l'air

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EP3559576A2 true EP3559576A2 (fr) 2019-10-30

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Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
IT1019710B (it) * 1974-07-12 1977-11-30 Nuovo Pignone Spa Processo ed apparato per la produ zione di elevate percentuali di os sigeno e/o azoto allo stato liquido
JPS5449980A (en) * 1977-09-28 1979-04-19 Hitachi Ltd Air separation plant
FR2699992B1 (fr) 1992-12-30 1995-02-10 Air Liquide Procédé et installation de production d'oxygène gazeux sous pression.
EP0955509B1 (fr) * 1998-04-30 2004-12-22 Linde Aktiengesellschaft Procédé et appareil pour la production d'oxygène à haute pureté
DE10217091A1 (de) * 2002-04-17 2003-11-06 Linde Ag Drei-Säulen-System zur Tieftemperatur-Luftzerlegung mit Argongewinnung
FR2895068B1 (fr) * 2005-12-15 2014-01-31 Air Liquide Procede de separation d'air par distillation cryogenique
EP2313724A2 (fr) * 2008-08-14 2011-04-27 Linde Aktiengesellschaft Procédé et dispositif de séparation de l'air à basse température
EP2801777A1 (fr) * 2013-05-08 2014-11-12 Linde Aktiengesellschaft Installation de décomposition de l'air dotée d'un entraînement de compresseur principal
US9797654B2 (en) * 2013-07-11 2017-10-24 Linde Aktiengesellschaft Method and device for oxygen production by low-temperature separation of air at variable energy consumption

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