WO2022003128A1 - Appareil de séparation de mélange gazeux et procédé pour séparer au moins un fluide principal à partir d'un mélange gazeux - Google Patents

Appareil de séparation de mélange gazeux et procédé pour séparer au moins un fluide principal à partir d'un mélange gazeux Download PDF

Info

Publication number
WO2022003128A1
WO2022003128A1 PCT/EP2021/068242 EP2021068242W WO2022003128A1 WO 2022003128 A1 WO2022003128 A1 WO 2022003128A1 EP 2021068242 W EP2021068242 W EP 2021068242W WO 2022003128 A1 WO2022003128 A1 WO 2022003128A1
Authority
WO
WIPO (PCT)
Prior art keywords
heat exchanger
block
fluid
process fluid
gas mixture
Prior art date
Application number
PCT/EP2021/068242
Other languages
German (de)
English (en)
Inventor
Christian Blank
Original Assignee
Christian Blank
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Christian Blank filed Critical Christian Blank
Priority to EP21740001.9A priority Critical patent/EP4176218A1/fr
Publication of WO2022003128A1 publication Critical patent/WO2022003128A1/fr

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
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/0605—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the feed stream
    • F25J3/0625—H2/CO mixtures, i.e. synthesis gas; Water gas or shifted synthesis gas
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/506—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification at low temperatures
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • 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
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/0635—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • 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
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/0655—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of hydrogen
    • 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
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/066—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation 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
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/0665—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of carbon monoxide
    • 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
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/067—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of carbon dioxide
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/093—Coal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1678—Integration of gasification processes with another plant or parts within the plant with air separation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1846—Partial oxidation, i.e. injection of air or oxygen 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/42—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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/50—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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/30—Compression of the feed 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/02—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams using a pump in general or hydrostatic pressure increase
    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/42—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/80—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being carbon dioxide
    • 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
    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/02—Integration in an installation for exchanging heat, e.g. for waste heat recovery
    • 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
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2

Definitions

  • the invention relates to a gas mixture separation system for separating at least one main fluid from a gas mixture.
  • the invention also relates to a method for separating at least one main fluid from a gas mixture.
  • pure hydrogen is mainly produced by steam reforming natural gas, with the harmful gases still remaining in the product gas for a fuel cell, for example carbon monoxide, carbon dioxide and residues of methane, having to be laboriously separated out.
  • the object of the invention is to provide a gas mixture separation plant and a corresponding method with which it is possible to separate a desired fluid from a gas mixture in an energy-efficient manner.
  • the object is achieved according to the invention by a gas mixture separation system for separating at least one main fluid from a gas mixture, the gas mixture separation system comprising an initial block and an end block, which is connected downstream of the initial block.
  • the initial block comprises an inlet for the gas mixture, a compressor connected downstream of the inlet for compressing the gas mixture, a first heat exchanger, a second heat exchanger and an outlet.
  • the end block includes an inlet, a first heat exchanger and an outlet. The inlet of the end block is fluidly connected to the outlet of the header.
  • the gas mixture separation plant has a return line for a main fluid separated in the end block, which is flow-connected to the outlet of the end block.
  • the return line is functionally coupled both to the first heat exchanger of the end block and to the first heat exchanger of the initial block, so that the main fluid present in the return line withdraws heat from a process fluid present in the respective first heat exchanger in order to cool the corresponding process fluid.
  • the second heat exchanger of the header is connected downstream of the first heat exchanger of the header. The second heat exchanger of the initial block liquefies and separates a separation fluid from a process fluid which has been received from the associated first heat exchanger.
  • the second heat exchanger of the header is coupled to a line via which the second heat exchanger of the header receives a cooling fluid that extracts heat from the process fluid present in the second heat exchanger of the header in order to cool the corresponding process fluid.
  • the header has a third heat exchanger that ensures a heat exchange between the respective process fluid that is supplied to the first heat exchanger of the header and the separation fluid that has been separated from the process fluid by means of the second heat exchanger of the header, so that the separation fluid removes heat from the process fluid and evaporates.
  • the third heat exchanger of the initial block is separated from the return line.
  • the object is achieved according to the invention by a method for separating at least one main fluid from a gas mixture, with the following steps:
  • the main fluid can in principle be hydrogen, which is present in as pure as possible is present, since hydrogen as the main gas for a hydrogen economy is to be split off from the gas mixture in as pure a form as possible.
  • a separation fluid has been separated from the gas mixture in the second heat exchanger of the initial block, this being liquefied beforehand.
  • the separation fluid can be a further component of the gas mixture that is to be separated from the gas mixture in order to be able to provide the pure hydrogen.
  • the separation fluid can be carbon monoxide, carbon dioxide or methane.
  • the process fluid in the second heat exchanger of the initial block can be cooled in order to liquefy the separation fluid and thus to separate it in a simple manner from the process fluid present in the second heat exchanger.
  • the cooling fluid is fed to the second heat exchanger, which interacts accordingly with the process gas in the second heat exchanger, whereby the separation fluid can be liquefied in order to be able to separate it accordingly.
  • the cooling fluid can be cooled nitrogen and / or cooled oxygen, the cooling fluid being, for example, at a temperature between 70 and 110 Kelvin, in particular at 95 Kelvin or lower.
  • the gas mixture separation system can comprise at least one cooling fluid line or a line through which the cooling fluid flows.
  • the cooling fluid can have a correspondingly low temperature, for example a temperature between 70 and 110 Kelvin, in particular a temperature of 95 Kelvin or lower, preferably 92 Kelvin or lower.
  • the cooling fluid thermally couples with the respective process fluid in the at least one second heat exchanger, in particular in all existing second heat exchangers, whereby the corresponding separation fluid liquefies and can thus be separated from the respective process fluid.
  • the gas mixture separation system can comprise two cooling fluid lines or two lines through which two different cooling fluids flow separately from one another. In this way, thermal coupling with the two different cooling fluids can take place in the respective second heat exchanger.
  • the at least one cooling fluid can be nitrogen and / or oxygen.
  • the at least one cooling fluid line or the line through which the cooling fluid flows can be part of a further separation system, for example an air separation system, which is thus thermally coupled to the gas mixture separation system.
  • a system can be provided that includes the gas mixture separation system and the further separation system, the gas mixture separation system and the separation system being thermally coupled via the at least one cooling fluid line or the line through which the cooling fluid flows.
  • the further decomposition plant can be part of a system for storing hydrogen obtained from coal.
  • the cooling fluid interacts with the process fluid in the second heat exchanger that has been fed to the second heat exchanger.
  • energy or heat is withdrawn from this process fluid, so that the separation fluid can be liquefied and separated from the process fluid that has been fed to the second heat exchanger.
  • the process fluid fed to the second heat exchanger corresponds to the separation fluid and the process fluid that leaves the second heat exchanger.
  • the cooling fluid removes energy or heat from the separation fluid and the process fluid, which leaves the second heat exchanger.
  • the separation fluid previously liquefied by means of the second heat exchanger of the initial block can be evaporated again, as a result of which it withdraws heat from the process fluid present in the third heat exchanger of the initial block.
  • the energy efficiency of the gas mixture separation system can thus be further improved.
  • the corresponding separation fluid is then in the form of a gas.
  • the third heat exchanger of the initial block is separated from the return line so that the main fluid which flows through the return line does not interact with another fluid in the third heat exchanger. Rather, in the third heat exchanger there is only an exchange of heat between the process fluid that is fed to the first heat exchanger of the initial block and the separation fluid that has been separated from the process fluid that was fed to the second heat exchanger by means of the second heat exchanger of the initial block.
  • the gas mixture which is compressed or compressed in the compressor of the initial block, can be compressed to a pressure ⁇ 5 bar, whereby the boiling point of the individual gases of the gas mixture is increased accordingly.
  • thermal energy is withdrawn from the corresponding process fluid in the respective heat exchangers, as a result of which the process fluid is cooled.
  • the main fluid that is cooled to the maximum is used in particular, which has been split off in the end block in order to cool the process fluid present in the first heat exchanger of the initial block.
  • the energy efficiency of the entire gas mixture separation system can be increased accordingly.
  • the gas mixture separation plant can be used in a system for storing hydrogen obtained from coal, which system has a coal gasification reactor for gasifying coal.
  • the coal gasification reactor requires pure oxygen for the gasification process, which can be provided as the main fluid of the gas mixture separation plant or as a separation fluid for the gas mixture separation plant.
  • the gas mixture separation plant can therefore be integrated in a system for storing hydrogen obtained from coal, which has a coal gasification reactor for gasifying the coal and a steam power plant for producing electricity, which is thermally coupled to the coal gasification reactor.
  • the system can also have a water-gas shift reaction plant which is connected to the coal gasification reactor in order to receive the reaction gases from the coal gasification reactor, a discharge line coupled to an output of the water gas shift reaction system, which is thermally coupled to a feed water line of the steam power plant and a Include gas storage.
  • the gas store can be connected to the water-gas shift reaction system in order to store at least one of the product gases of the water-gas shift reaction system, the steam power plant for Electricity production is thermally coupled with the coal gasification reactor in such a way that the reaction gases of the coal gasification reactor are sufficiently cooled due to the heat dissipated to the feed water of a feed water line of the steam power plant, so that the reaction gases can be processed directly in the water gas shift reaction system without active cooling in between.
  • the gas mixture separation plant can itself provide pure hydrogen, for example as the main fluid, wherein the pure hydrogen can be (temporarily) stored together with the hydrogen obtained from the water-gas shift reaction plant.
  • the gas mixture separation plant can provide pure oxygen, for example as a separation fluid, which is fed to the coal gasification reactor for the gasification process.
  • the gas mixture separation system according to the invention can decompose a gas mixture with a significantly reduced energy requirement compared to the conventional methods, in particular a hydrogen-rich gas mixture. This is because the cooled individual gases that are already present are used exclusively by means of thermal coupling in order to liquefy a separation fluid from the process fluid or process gas, which lowers the temperature of the process fluid.
  • the end block has a second heat exchanger, wherein the second heat exchanger of the end block is connected downstream of the first heat exchanger of the end block, and wherein the second heat exchanger of the end block liquefies a separation fluid of a process fluid obtained from the associated first heat exchanger and separates it from the process fluid.
  • the second heat exchanger of the end block is coupled to the line via which the second heat exchanger of the end block receives the cooling fluid that extracts heat from the process fluid present in the second heat exchanger of the end block in order to cool the corresponding process fluid.
  • the energy efficiency of the gas mixture separation system and of the method can be increased accordingly, since the process fluid is also processed in two different heat exchangers in the end block in order to reduce the temperature of the process fluid accordingly.
  • the process fluid upstream of the second heat exchanger of the initial block also comprises at least one further gas or a further component of the gas mixture than the process fluid that is fed to the second heat exchanger of the end block.
  • the end block has a third heat exchanger which ensures a heat exchange between the respective process fluid that is supplied to the first heat exchanger of the end block and the separation fluid that has been separated from the process fluid by means of the second heat exchanger of the end block, so that the separation fluid removes heat from the process fluid and vaporizes it.
  • the third heat exchanger of the end block is also separated from the return line.
  • the separation fluid previously liquefied by means of the second heat exchanger of the end block can thus be evaporated again, as a result of which it withdraws heat from the process fluid present in the third heat exchanger of the end block.
  • the energy efficiency of the gas mixture separation system can thus be further improved.
  • the corresponding separation fluid is thus in the form of a gas.
  • At least one middle block is provided between the header and the end block, the middle block comprising an inlet, a first heat exchanger and an outlet, the inlet of the middle block with the outlet of the header and the outlet of the middle block with the inlet of the end block are connected, and wherein the return line is also functionally coupled to the first heat exchanger of the central block, so that the main fluid present in the return line withdraws heat from a process fluid present in the first heat exchanger of the central block in order to cool the corresponding process fluid.
  • the Central block comprises a further first heat exchanger which ensures a heat exchange between the main fluid separated in the end block, which is returned via the return line, and the process fluid present in the first heat exchanger of the central block. In this respect, there is a further thermal coupling.
  • every heat exchanger in the entire gas mixture separation system ensures a thermal coupling, via which heat is extracted from the process fluid in order to cool it further.
  • the corresponding heat extraction can take place in the case of the respective second heat exchanger by means of the cooling fluid, in the case of the respective first heat exchanger by means of the main fluid or in the case of the respective third heat exchanger by means of the respective separation fluid.
  • the central block has a second heat exchanger, the second heat exchanger of the central block being connected downstream of the first heat exchanger of the central block, and the second heat exchanger of the central block liquefying a separation fluid of a process fluid obtained from the first heat exchanger of the central block and separating it from the process fluid.
  • the second heat exchanger of the central block is coupled to the line via which the second heat exchanger of the central block receives the cooling fluid that extracts heat from the process fluid present in the second heat exchanger of the central block in order to cool the corresponding process fluid.
  • the process fluid can thus also be cooled several times in the central block by the central block having at least a second heat exchanger which ensures heat exchange between the process fluid and the cooling fluid, via which the corresponding separation fluid can be liquefied and separated.
  • heat can be extracted from the process fluid by the cooling fluid.
  • this ensures that the main fluid obtained from the gas mixture is present in as pure a form as possible, since several separation fluids have been split off from the gas mixture, in particular before they were liquefied.
  • the separation fluid to be separated is basically liquefied in that there is a thermal coupling in the corresponding second heat exchanger of the blocks of the gas mixture separation plant between the process fluid and the cooling fluid.
  • the gas mixture separation plant can comprise a plurality of middle blocks, which are each arranged one after the other between the start block and the end block, the respective middle blocks being coupled to one another. In this way, the purity of the main fluid can be ensured, since several separation fluids have been separated from the gas mixture, in particular one separation fluid per additional central block. In this respect, the number of central blocks determines how many different separation fluids are separated from the gas mixture.
  • the number of middle blocks also ensures how often the process fluid is cooled or how often the main fluid separated in the end block carries out a heat exchange with the process fluid in the corresponding blocks, i.e. the start block, the several middle blocks and the end block.
  • the gas mixture separation system can have a modular structure so that the number of central blocks can be selected to be variable, namely between 0 and a desired number. The higher the number of central blocks, the more different parts of the gas mixture can be separated.
  • a first central block and a second central block are provided between the initial block and the end block, the first central block comprising an inlet, a first heat exchanger and an outlet.
  • the second central block comprises an inlet, a first heat exchanger and an outlet.
  • the input of the first middle block is connected to the output of the header, the output of the first middle block is connected to the input of the second middle block, and the output of the second middle block is connected to the input of the end block.
  • the return line is also functionally coupled to the first heat exchanger of the first central block and to the first heat exchanger of the second central block, so that the main fluid present in the return line extracts heat from a process fluid present in the first heat exchanger of the first central block and from a process fluid present in the first heat exchanger of the second central block to cool the corresponding process fluid.
  • the energy efficiency of the gas mixture separation plant is accordingly increased, since the Main fluid is used several times for cooling the process fluid, namely additionally in the two central blocks.
  • the first central block and the second central block each have a second heat exchanger, wherein the second heat exchanger of the first central block is connected downstream of the first heat exchanger of the first central block, and wherein the second heat exchanger of the first central block liquefies a process fluid contained in the first heat exchanger of the first central block and separated from the process fluid, wherein the second heat exchanger of the first central block is coupled to the line via which the second heat exchanger of the first central block receives the cooling fluid that extracts heat from the process fluid present in the second heat exchanger of the first central block in order to cool the corresponding process fluid, and wherein the second heat exchanger of the second central block is connected downstream of the first heat exchanger of the second central block, and wherein the second heat exchanger of the second central block is a separation fluid of one of the first heat exchanger of the second central block ks contained process fluids liquefied and separated from the process fluid, wherein the second heat exchanger of the second central block is coupled to the line via which the second heat exchanger of the
  • the efficiency is further increased, since a separating fluid is liquefied and separated in the respective second heat exchangers of the two central blocks, in that the cooling fluid is supplied to the respective second heat exchanger, whereby heat is extracted from the corresponding process fluid.
  • the purity of the main fluid can be improved accordingly, since more separation fluids are separated from the process fluid.
  • the second heat exchangers of the different blocks can interact with the cooling fluid, whereby the separation fluid to be separated in the second heat exchanger is liquefied so that the separation fluid can be separated from the process fluid present.
  • the respective middle block can have a third heat exchanger which ensures a heat exchange between the respective process fluid that is supplied to the first heat exchanger and the separation fluid that is generated by means of the respective second heat exchanger has been separated from the process fluid, so that the separation fluid removes heat from the process fluid and evaporates.
  • the middle block can also comprise a third heat exchanger which - in a manner analogous to the start block or the end block - ensures a heat exchange between the respective process fluid that is fed to the first heat exchanger of the middle block and the separation fluid.
  • the separation fluid has been separated from the process fluid in the second heat exchanger by means of the respective second heat exchanger after this has previously been liquefied.
  • the separation fluid removes heat or energy from the process fluid, so that the liquid separation fluid evaporates again. In this respect, the energy efficiency of the gas mixture separation system can be increased further.
  • the second heat exchanger is fluidically coupled to the associated heat exchanger in such a way that the respective separation fluid in the first heat exchanger interacts with the corresponding process fluid in order to extract heat from the process fluid.
  • the energy efficiency of the gas mixture separation system can thus be increased further.
  • At least one storage device is provided for storing the main fluid.
  • the hydrogen in particular pure hydrogen, can at least be temporarily stored in the store for further use.
  • a memory for storing the separation fluid can be provided, which has been separated in the respective second heat exchanger in order to store or temporarily store the separation fluid for later use.
  • the gas mixture separation system has thermal insulation which surrounds and insulates the components of the gas mixture separation system.
  • the respective heat exchangers and the return line are surrounded by the thermal insulation in order to thermally insulate them accordingly.
  • the initial block has a fourth heat exchanger, which is connected upstream of the third heat exchanger, wherein the fourth heat exchanger ensures a heat exchange between the respective process fluid that is fed to the third heat exchanger of the initial block and the separation fluid that has been separated from the process fluid by means of the second heat exchanger of a block directly downstream of the initial block.
  • the efficiency of the gas mixture separation system can thus be increased further.
  • the fluid separated in the second heat exchanger is thermally coupled via the fourth heat exchanger to the compressed gas mixture which is fed to the first heat exchanger of the initial block.
  • the block directly downstream can be the end block if no middle block is provided or the (first) middle block if at least one middle block is provided between the start block and the end block.
  • each block that has a directly downstream block can have a corresponding fourth heat exchanger, that is to say all blocks except the end block, which this has no block directly downstream. This can further increase the efficiency of the entire gas mixture separation plant.
  • the respective fourth heat exchanger is also separated from the return line, i.e. the respective fourth heat exchanger does not receive the main fluid that flows through the main line.
  • the respective third heat exchanger of the corresponding block i.e. that of the start block, the middle block or the end block, is separated from the return line so that the main fluid flowing through the return line does not interact with another fluid in the third heat exchanger.
  • the blocks are graded according to the temperature of the separation fluids to be separated and the temperature point at which the Physical state changes to liquid.
  • the separating fluids to be separated off at high temperatures are thus split off earlier, that is closer to the initial block, whereas the separating fluids still to be separated off at lower temperatures are split off later, i.e. closer to the end block.
  • the cooled separation fluids of the gas mixture separation plant are separated from the respective process fluid and thermally coupled with the last gas mixture by means of a heat exchanger and liquefied by cooling with the cooling fluid, e.g. carbon monoxide.
  • the main fluid which can also be referred to as residual gas, for example hydrogen, can thus be passed in gaseous form to the central or initial block with maximum cooling.
  • the corresponding separation fluid for example liquefied carbon monoxide, cools the process fluid in the supply line from the central or initial block by means of evaporation and expansion including heat transfer.
  • the maximally cooled main fluid that is to say the maximally cooled gaseous hydrogen, can be used to cool the supplied process fluid from the central or initial block.
  • the temperature of the corresponding separation fluid and of the process fluid in the central block is somewhat higher, the temperature of the change in the state of aggregation of the separation fluid in the central block is also higher.
  • Each block can comprise several thermal couplings, namely a heat exchanger between the process fluid and the ultimately separated or remaining main fluid (the respective first heat exchanger), a thermal coupling for cooling the process fluid with the already cooled separation fluids (the respective second heat exchanger) and a thermal coupling of the liquid separated in the respective block, which also cools the process fluid by means of evaporation and normal pressure (the respective third heat exchanger).
  • a heat exchanger between the process fluid and the ultimately separated or remaining main fluid the respective first heat exchanger
  • a thermal coupling for cooling the process fluid with the already cooled separation fluids the respective second heat exchanger
  • a thermal coupling of the liquid separated in the respective block which also cools the process fluid by means of evaporation and normal pressure
  • Figure 1 shows a schematic structure of an inventive
  • Figure 2 shows a schematic structure of an inventive
  • Figure 3 shows a schematic structure of an inventive
  • a gas mixture separation plant 10 which comprises an initial block 12, a middle block 14 downstream of the beginning block 12 and an end block 16 downstream of the middle block 14.
  • the middle block 14 is thus arranged between the start block 12 and the end block 16.
  • the starting block 12 has an inlet 18 in the form of a feed line, via which the gas mixture separation system 10 is supplied with a gas mixture which is to be correspondingly broken down in the gas mixture separation system 10.
  • the gas mixture can comprise hydrogen, carbon dioxide, carbon monoxide and nitrogen.
  • the header 18 comprises a compressor 20, which compresses the gas mixture received via the inlet 18, as a result of which a process fluid is generated.
  • the process fluid can be brought to a pressure of at least 5.2 bar.
  • the process fluid is transported from the compressor 20 to a first heat exchanger 22 in that the process fluid interacts with a main fluid separated in the gas mixture separation system 10 at the temperature T 2.i, for example hydrogen.
  • the main fluid removes heat from the process fluid of the header 12, as will be explained in detail below.
  • the main fluid is conducted via a return line 24 of the gas mixture separation system 10 from the end block 16 via the middle block 14 and the beginning block 12 to a storage unit 26 in which the pure main fluid is stored.
  • the starting block 12 comprises a second heat exchanger 28, which is connected downstream of the first heat exchanger 22, so that the second heat exchanger 28 receives the process fluid that is correspondingly cooled in the first heat exchanger 22.
  • the second heat exchanger 28, in particular the process fluid processed by the second heat exchanger 28, also interacts at the temperature T 2. o with at least one cooling fluid 30, for example nitrogen and / or oxygen, which flows via a feed line 31 through a line 32 to a discharge line 33 .
  • the line 32 can accordingly also be referred to as a cooling fluid line through which the cooling fluid 30 flows.
  • the gas mixture separation plant 10 can in principle also comprise two or more lines 30 through which two or more different cooling fluids 30 flow separately from one another, for example nitrogen and oxygen.
  • the at least one cooling fluid 30 can be provided by a separate system, this being provided for storage or further use.
  • the at least one line 30 through which the cooling fluid flows is, for example, part of a further separation plant, in particular an air separation plant. This further decomposition plant is thus thermally coupled to the gas mixture decomposition plant 10.
  • the gas mixture decomposition plant 10 and the further decomposition plant together form a system
  • the further decomposition plant can be part of a system for storing hydrogen obtained from coal.
  • the gas mixture separation system 10 can also be part of the system for storing hydrogen obtained from coal.
  • the cooling fluid 30 flowing in the at least one line 32 couples thermally with the respective process fluid in the second heat exchanger 28.
  • the separation fluid 34 for example carbon dioxide, is liquefied at the temperature T2.0 in that the process fluid is thermally coupled to the at least one cooling fluid at the temperature T1.0.
  • the liquefied separation fluid 34 can then be driven further by means of a pump.
  • the process fluid is passed on from the second heat exchanger 28 to the outlet 36 of the initial block 12, which is in flow connection with the inlet 38 of the subsequent central block 14.
  • the separation fluid 34 separated off in the second heat exchanger 28 of the initial block 12 can flow through a third heat exchanger 40, which is shown in dashed lines in FIG.
  • a heat exchange takes place at the temperature T2.2 between the liquefied separation fluid 34, for example carbon dioxide, and the process fluid present before it is fed to the first heat exchanger 22.
  • the liquefied separation fluid 34 for example carbon dioxide
  • heat can already be extracted from the process fluid, as a result of which the previously liquid separation fluid 34 evaporates again.
  • the separation fluid 34 is present as a gas with the temperature T 2.2 .
  • the process fluid which has been supplied via the inlet 38 of the central block 14, is passed in the central block 14 in an analogous manner to the initial block 12 to a first heat exchanger 42 of the central block 14, in which the process fluid is thermally combined with the main fluid at the temperature T 1 .1 interacts, which has been passed through the return line 24.
  • the process fluid is accordingly cooled via the main fluid in the first heat exchanger 42 of the central block 14.
  • the cooled process fluid leaving the first heat exchanger 42 of the central block 14 is sent to a second heat exchanger 44 of the Central block 14 supplied, which also receives the cooling fluid 30 at the temperature Ti .0 , which flows through the cooling line 32.
  • a further separation fluid 46 of the process fluid which is present in the second heat exchanger 44 of the central block 14, so that the further separation fluid 46 can be separated in the second heat exchanger 44 of the central block 14, as shown by the corresponding arrow in FIG.
  • the further separation fluid 46 is, for example, carbon monoxide. Liquefaction of further Abtrennfluids 46 is carried at the temperature Ti. 0th
  • the remaining process fluid is fed to an input 50 of the end block 16 via an output 48 of the central block 14.
  • the third heat exchanger 52 of the central block 14 enables a heat exchange between the liquid separation fluid 46 and the process fluid which is supplied to the first heat exchanger 42 of the central block 14.
  • the liquid separation fluid can extract heat from the process fluid in that the separation fluid 46 is evaporated. This happens at the temperature Ti. 2 .
  • the process fluid fed to the end block 16 is also fed to a first heat exchanger 54 in the end block 16, which enables a heat exchange between the corresponding process fluid and the main fluid at the temperature T 0.i, the main fluid being fed via the return line 24 from the end block 16 to the reservoir 26 will.
  • the corresponding process fluid can be cooled by the main fluid.
  • the process fluid coming from the first heat exchanger 54 of the end block 16 is fed to a second heat exchanger 56 of the end block 16, in which the process fluid is mixed with the cooling fluid 30 at the temperature To . o interacts so that a further separation fluid 58, for example nitrogen, is liquefied from the present process fluid.
  • the further separation fluid 58 can so in second heat exchanger 56 of the end block 16 are separated, as shown by the corresponding arrow in FIG.
  • the separation fluid 58 is fed to an (optional) third heat exchanger 60 of the end block 16, in particular by means of a pump.
  • the third heat exchanger 60 of the end block 16 also receives the process fluid that is to be supplied to the first heat exchanger 54 of the end block 16. This makes it possible for the further separation fluid 58, which has previously been liquefied, to be evaporated again, as a result of which it withdraws heat from the process fluid. This happens at the temperature T 0.2 .
  • the process fluid leaving the second heat exchanger 56 is fed via an outlet 62 of the end block 16 into the return line 24, which interacts with the respective first heat exchangers 22, 42, 54 of the corresponding blocks 12, 14 and 16 in order to cool the process fluid present there.
  • the process fluid leaving the second heat exchanger 56 thus corresponds to the main fluid, which is present in pure form.
  • a further separation fluid 34, 46, 58 is separated in each block 12 to 16, for example carbon dioxide in the initial block 12, carbon monoxide in the middle block 14 and nitrogen in the end block 16.
  • the separation fluids 34, 46, 58, which are present as gases due to the respective third heat exchangers 40, 52, 60 of the blocks 12-16, can each be at least temporarily stored in a separate memory 64 to 68.
  • the corresponding vaporized separation fluids 34, 46, 58 first interact again with the corresponding process fluid in a fourth heat exchanger or the respective first heat exchanger 22, 42, 54 in order to extract further heat from the process fluid before the corresponding separation fluids 34, 46, 58 are stored in the associated memories 64, 66 and 68.
  • fourth heat exchangers is shown by way of example in FIG. 3, to which reference is made below.
  • the gas mixture separation plant 10 can have further middle blocks 14, which are provided in an analogous manner between the start block 12 and the end block 16.
  • the gas mixture is broken down into three components, namely the main fluid and two separation fluids 34, 58, which were separated from the corresponding process fluid in the respective second heat exchangers 28 and 56 of the starting block 12 and the end block 16, respectively.
  • thermal insulation can be provided which surrounds the components of the gas mixture separation system 10 and thus insulates them.
  • FIG. 3 an embodiment of the gas mixture separation plant 10 is shown, which is based on that of FIG.
  • the embodiment shown in FIG. 3 comprises, in addition to the embodiment according to FIG. 1, a fourth heat exchanger 70 within the initial block 12.
  • the fourth heat exchanger 70 is connected upstream of the third heat exchanger 40 of the corresponding block, that is to say of the initial block 12, so that the fourth heat exchanger 70 receives the process fluid supplied to the third heat exchanger 40 and the separation fluid 46, which by means of the second heat exchanger 44 of the corresponding block, ie the initial block 12, the block directly downstream has been separated from the process fluid, so the middle block 14.
  • the fourth heat exchanger 70 thus provides a heat exchange between the respective process fluid, that is, that which is supplied to the third heat exchanger 40, and the separation fluid 46 which has been separated in the second heat exchanger 44 of the central block 14.
  • the central block 14 can also have a fourth heat exchanger, which is not shown here for reasons of simplicity.
  • the fourth heat exchanger of the middle block 14 would accordingly receive the process fluid fed to the third heat exchanger 52 of the middle block 14 and the separation fluid 58 which has been separated in the second heat exchanger 56 of the end block 16.
  • the efficiency of the entire system can be further increased in this way.

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Inorganic Chemistry (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

L'invention concerne un appareil de séparation de mélange gazeux pour séparer un fluide principal, ayant un bloc de départ (12) et un bloc final (16). Le bloc de départ (12) comporte un premier échangeur de chaleur (22) et un deuxième échangeur de chaleur (28). En outre, une conduite de retour (24) est prévue pour le fluide principal séparé dans le bloc final (16), et est couplée de manière fonctionnelle au premier échangeur de chaleur (54) du bloc final (16) et au premier échangeur de chaleur (22) du bloc de départ (12), de telle sorte que le fluide principal aspire de la chaleur à partir d'un fluide de traitement présent dans le premier échangeur de chaleur (22, 54) pour refroidir le fluide de traitement. Le deuxième échangeur de chaleur (28) est couplé à une conduite (32) à travers laquelle il reçoit un fluide de refroidissement. Le deuxième échangeur de chaleur (28) condense un fluide de séparation d'un fluide de traitement et sépare le fluide de séparation. Un troisième échangeur de chaleur (40), séparé de la conduite de retour, assure un échange de chaleur entre le fluide de traitement acheminé dans le premier échangeur de chaleur (22) du bloc de départ (12) et le fluide de séparation. En outre, il est décrit un procédé pour séparer au moins un fluide principal à partir d'un mélange gazeux.
PCT/EP2021/068242 2020-07-02 2021-07-01 Appareil de séparation de mélange gazeux et procédé pour séparer au moins un fluide principal à partir d'un mélange gazeux WO2022003128A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP21740001.9A EP4176218A1 (fr) 2020-07-02 2021-07-01 Appareil de séparation de mélange gazeux et procédé pour séparer au moins un fluide principal à partir d'un mélange gazeux

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102020117503 2020-07-02
DE102020117503.5 2020-07-02

Publications (1)

Publication Number Publication Date
WO2022003128A1 true WO2022003128A1 (fr) 2022-01-06

Family

ID=76859609

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2021/068242 WO2022003128A1 (fr) 2020-07-02 2021-07-01 Appareil de séparation de mélange gazeux et procédé pour séparer au moins un fluide principal à partir d'un mélange gazeux

Country Status (3)

Country Link
EP (1) EP4176218A1 (fr)
DE (1) DE102021117030B4 (fr)
WO (1) WO2022003128A1 (fr)

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3614872A (en) * 1967-12-22 1971-10-26 Texaco Inc Synthesis gas separation process
US20070221541A1 (en) * 2006-03-21 2007-09-27 Tennessee Valley Authority Multi-stage cryogenic acid gas removal
US20090145167A1 (en) * 2007-12-06 2009-06-11 Battelle Energy Alliance, Llc Methods, apparatuses and systems for processing fluid streams having multiple constituents
US20100126215A1 (en) * 2007-04-13 2010-05-27 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method For Cooling A Cryogenic Exchange Line
EP2196251A1 (fr) * 2008-12-04 2010-06-16 Siemens Aktiengesellschaft Installation de séparation de dioxyde de carbone et procédé de fonctionnement d'une telle installation
WO2011026170A1 (fr) * 2009-09-01 2011-03-10 Cool Energy Limited Procédé et appareil de réduction de concentration d'espèce acide dans un gaz acide
US20120167620A1 (en) * 2009-05-15 2012-07-05 Eva Marfilia Van Dorst Method and system for separating co2 from synthesis gas or flue gas

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AU2011274797B2 (en) 2010-07-09 2015-05-21 Arnold Keller Carbon dioxide capture and liquefaction
DE202017006193U1 (de) 2017-11-29 2018-01-25 Hans-Joachim Huf Vorrichtung zur Zerlegung von Luft

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3614872A (en) * 1967-12-22 1971-10-26 Texaco Inc Synthesis gas separation process
US20070221541A1 (en) * 2006-03-21 2007-09-27 Tennessee Valley Authority Multi-stage cryogenic acid gas removal
US20100126215A1 (en) * 2007-04-13 2010-05-27 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method For Cooling A Cryogenic Exchange Line
US20090145167A1 (en) * 2007-12-06 2009-06-11 Battelle Energy Alliance, Llc Methods, apparatuses and systems for processing fluid streams having multiple constituents
EP2196251A1 (fr) * 2008-12-04 2010-06-16 Siemens Aktiengesellschaft Installation de séparation de dioxyde de carbone et procédé de fonctionnement d'une telle installation
US20120167620A1 (en) * 2009-05-15 2012-07-05 Eva Marfilia Van Dorst Method and system for separating co2 from synthesis gas or flue gas
WO2011026170A1 (fr) * 2009-09-01 2011-03-10 Cool Energy Limited Procédé et appareil de réduction de concentration d'espèce acide dans un gaz acide

Also Published As

Publication number Publication date
DE102021117030B4 (de) 2023-09-21
DE102021117030A1 (de) 2022-01-05
EP4176218A1 (fr) 2023-05-10

Similar Documents

Publication Publication Date Title
EP0093448B1 (fr) Procédé et dispositif pour obtenir de l'oxygène gazeux sous pression élevée
EP2980514A1 (fr) Procédé de séparation cryogénique de l'air et installation de séparation d'air
EP1067345B1 (fr) Procédé et dispositif pour la séparation cryogénique des constituants de l'air
EP0895045B1 (fr) Procédé de séparation d'air
WO1997004279A1 (fr) Procede et dispositif de production variable d'un produit gazeux comprime
EP3205963A1 (fr) Procédé de production d'un produit pneumatique et installation de décomposition d'air
EP4018143A1 (fr) Procédé de fonctionnement d'un échangeur de chaleur, agencement doté d'un échangeur de chaleur et système doté d'un agencement correspondant
DE60018083T2 (de) Verfahren und Vorrichtung zur Abtrennung von Kohlenmonoxid und Wasserstoff aus einem Gasgemisch
DE102021117030B4 (de) Gasgemisch-Zerlegungsanlage sowie Verfahren zum Abtrennen von wenigstens einem Hauptfluid aus einem Gasgemisch
EP3322947B1 (fr) Procédé de refroidissement d'un flux de traitement
EP2770286B1 (fr) Procédé et dispositif de collecte d'oxygène et d'azote sous haute pression
EP0081849B1 (fr) Procédé et dispositif de séparation d'un gaz d'échappement de synthèse
DE102012006746A1 (de) Verfahren und Vorrichtung zur Erzeugung elektrischer Energie
DE3035844A1 (de) Verfahren und vorrichtung zur gewinnung von sauerstoff mittlerer reinheit
EP3293475A1 (fr) Procédé et appareil de stockage et de récupération d'énergie
DE10045128A1 (de) Verfahren und Vorrichtung zur Erzeugung hoch reinen Stickstoffs durch Tieftemperatur-Luftzerlegung
DE102015007529A1 (de) Verfahren und Anlage zur Abtrennung von Methan aus einem methanhaltigen Synthesegasstrom
DE2518557C3 (de) Verfahren zur Luftzerlegung mit Flüssigkeitserzeugung durch Tieftemperaturrektifikation
DE102004036708A1 (de) Verfahren zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes
EP2976511A1 (fr) Procédé et dispositif pour produire de l'énergie électrique
EP3948124B1 (fr) Procédé de fonctionnement d'un échangeur de chaleur, dispositif doté d'un échangeur de chaleur et installation dotée du dispositif correspondant
DE3403647A1 (de) Verfahren und vorrichtung zum kuehlen eines gasstromes vor und/oder bei seiner verdichtung
WO2023030689A1 (fr) Procédé pour obtenir un ou plusieurs produits de l'air et installation de séparation d'air
WO2023274574A1 (fr) Procédé et installation permettant de fournir un produit à base d'azote, un produit à base d'oxygène et un produit à base d'hydrogène
DE102013019504A1 (de) Verfahren zur Gewinnung eines flüssigen Stickstoffprodukts durch Tieftemperaturzerlegung von Luft und Luftzerlegungsanlage

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 21740001

Country of ref document: EP

Kind code of ref document: A1

WWE Wipo information: entry into national phase

Ref document number: 2021740001

Country of ref document: EP

ENP Entry into the national phase

Ref document number: 2021740001

Country of ref document: EP

Effective date: 20230202

NENP Non-entry into the national phase

Ref country code: DE