EP3247483A1 - Dispositif et procédé de séparation de dioxyde de carbone d'un flux gazeux - Google Patents

Dispositif et procédé de séparation de dioxyde de carbone d'un flux gazeux

Info

Publication number
EP3247483A1
EP3247483A1 EP16706322.1A EP16706322A EP3247483A1 EP 3247483 A1 EP3247483 A1 EP 3247483A1 EP 16706322 A EP16706322 A EP 16706322A EP 3247483 A1 EP3247483 A1 EP 3247483A1
Authority
EP
European Patent Office
Prior art keywords
carbon dioxide
cleaning device
gas stream
unit
oxygen
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Withdrawn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
EP16706322.1A
Other languages
German (de)
English (en)
Inventor
Christian PLEISSNER
Albert Reichl
Henning Schramm
Gerhard Zimmermann
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.)
Siemens AG
Original Assignee
Siemens AG
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 Siemens AG filed Critical Siemens AG
Publication of EP3247483A1 publication Critical patent/EP3247483A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8671—Removing components of defined structure not provided for in B01D53/8603 - B01D53/8668
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1418—Recovery of products
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1425—Regeneration of liquid absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • B01D53/1475—Removing carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/26—Drying gases or vapours
    • B01D53/261—Drying gases or vapours by adsorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/75—Multi-step processes
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C01B32/50—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/20—Reductants
    • B01D2251/202—Hydrogen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/20—Organic absorbents
    • B01D2252/204—Amines
    • B01D2252/20494—Amino acids, their salts or derivatives
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/112—Metals or metal compounds not provided for in B01D2253/104 or B01D2253/106
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/10—Noble metals or compounds thereof
    • B01D2255/102—Platinum group metals
    • B01D2255/1021—Platinum
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/10—Noble metals or compounds thereof
    • B01D2255/102—Platinum group metals
    • B01D2255/1023—Palladium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/20—Metals or compounds thereof
    • B01D2255/207—Transition metals
    • B01D2255/20761—Copper
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/22—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/10—Single element gases other than halogens
    • B01D2257/104—Oxygen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/12—Methods and means for introducing reactants
    • B01D2259/122—Gaseous reactants
    • 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
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
    • 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

Definitions

  • the invention relates to a separator for carbon dioxide from a gas stream, in particular from a flue gas stream ⁇ . Furthermore, the invention relates to a method for the separation of carbon dioxide from a gas stream.
  • the flue gas is brought into contact after the combustion in an absorption unit or an absorber with a suitable wash medium, which is contained in the flue gas, gaseous Kohlendio ⁇ dioxide in the washing medium dissolved or absorbed in a chemical sense.
  • a suitable wash medium which is contained in the flue gas, gaseous Kohlendio ⁇ dioxide in the washing medium dissolved or absorbed in a chemical sense.
  • the exhaust gas freed of carbon dioxide is finally released into the atmosphere.
  • Washing medium becomes a desorption unit or a desorber fed, where the absorbed carbon dioxide from the Waschmedi ⁇ to be released again.
  • the oxygen contained in the gas is then reacted with hydrogen to form water in a reactor connected downstream of the reactor, the purified gas is cooled and condensed water is separated off, the gas purified thereby containing less than 5 parts per million by volume of oxygen remaining water content is between 500 ppmv and 1000 ppmv.
  • the water content can be reduced to a value of less than 1 ppmv.
  • the chemisorption of oxygen contained in the to-clean ⁇ constricting gas is ferutton for example on a copper deposited.
  • the copper contact When the copper contact is loaded, it is regenerated by the addition of hydrogen.
  • the process at a temperature of about 200 ° C is a very high absorption capacity of the copper contact carried out.
  • two reactors must be used in chemisorption.
  • the gas In a reactor, the gas is here purified currency ⁇ rend the other reactor is regenerated simultaneously.
  • the gas is first heated to the required operating temperature, for which purpose usually the heat contained in the already purified gas is used.
  • the gas In flowing through the copper ⁇ contact of the oxygen contained in the gas on the copper ge ⁇ connected is the gas leaves the system free of oxygen.
  • the invention has for a first object of the invention to provide a device by means of an efficient and kos ⁇ -effective purification of carbon dioxide under a
  • the first object of the invention is achieved by a separation device for carbon dioxide from a gas stream, in particular from a flue gas stream, comprising an absorption unit for the separation of carbon dioxide from the gas stream by means of a washing medium, onorungsun connected with the absorption unit desorption unit to release the absorbed carbon dioxide from the washing medium, as well as one of the desorption after the flow downstream compressor unit for the liberated Koh ⁇ lendioxid, wherein the compressor unit is connected upstream of a rotatesvor- direction for carbon dioxide flow.
  • the invention is based on the recognition that the purification of an oxygen-containing carbon dioxide stream can in principle be carried out at different pressures. Due to the decrease in the volume flow at elevated pressures structurally smaller makesappa ⁇ rates are possible at high pressure than at low pressure. Therefore, the cleaning supply of carbon dioxide usually carried out after a compression ⁇ stage.
  • the invention takes into account that the purification of carbon dioxide at high pressure is associated with comparatively high costs.
  • the structural conditions such as the wall thickness of the apparatus and the Zuspeise für of hydrogen, to be adapted to the increased pressure conditions.
  • Next hö ⁇ here demands on the pressure stability and the tightness of the equipment used in each case are provided ,
  • the invention is now still draws against the knowledge of the unwanted se flow augmentation at low pressure into account the possibility to clean Koh ⁇ dioxide at low pressure of oxygen.
  • the invention namely recognizes surprisingly example that a cleaning device can be simpler and less expensive than previously integrated in a prescribed separation device before ⁇ lying in spite of structurally alswoiree- rer apparatus, when the cleaning device for carbon dioxide is carried out at low pressure and thus fluidically a compressor unit for compressing the purified carbon dioxide is connected upstream.
  • the carbon dioxide flowing out of the desorption unit is fed to the cleaning device in uncompressed form. There, the oxygen contained is removed. After purification, the carbon dioxide of the compressor unit is fed and Kompri ⁇ mized.
  • the cleaning device is fluidly ge ⁇ switches between the desorption unit and the compressor unit. This positioning of the cleaning device, which has not been taken into consideration, it is possible that Kom ⁇ complexity of the process and the overall cost of the construction and the subsequent operation of a corresponding cleaning Device to improve over previously common devices.
  • the cleaning device itself must be designed only for low pressures. This allows the use of devices with a small wall thickness, which reduces the cost of materials and thus the cost of materials. Also, no elaborate Safe ⁇ integrated technology necessary as requiring it at high pressures driven costs. In other words, the costs incurred for the use of structurally larger apparatus by the
  • the gas stream is flowed into the absorption unit.
  • the contained in the gas stream ⁇ ne carbon dioxide is absorbed within the absorption unit in egg ⁇ nem washing medium.
  • an amino acid salt solution is preferably used as the washing medium.
  • An aqueous amino acid salt solution ⁇ is expedient here.
  • the carbon dioxide-laden washing medium is fed to the desorptive unit.
  • the absorption unit is expediently connected via a discharge line in terms of flow to a supply line of the desorption unit.
  • the desorption unit the carbon dioxide absorbed in the washing medium is released and the scrubbing medium freed from carbon dioxide is returned to the absorption unit, where it is used for re-absorption of carbon dioxide from a flue gas.
  • the desorption unit is preferably fluidly connected via a return line to a supply line of the absorber.
  • the carbon dioxide liberated in the desorption unit is taken off at the desorber head and fed to the cleaning device, where the carbon dioxide is freed from contained oxygen.
  • the oxygen-containing carbon dioxide gas stream advantageously also passes through a condenser in which water contained in the carbon dioxide stream is condensed out.
  • the condenser is fluidically connected between the desorption and the madesvor ⁇ direction.
  • the cleaning device for the catalytic reduction of the oxygen contained in the carbon dioxide is formed. If the kata ⁇ lytic reduction of oxygen by the reaction on the oxygen contained in the carbon dioxide stream with hydrogen over a catalytic surface. It is therefore equally a catalytic oxidation of ⁇ What ser fürs with oxygen.
  • the oxygen-containing carbon dioxide stream is supplied to the cleaning ⁇ device via the flow connection of the desorption unit having the cleaning apparatus. For this purpose, a discharge of the desorption expedient ⁇ ßigerweise is connected to a supply of the cleaning device.
  • the feed line of the cleaning device is expediently connected to a feed line for a hydrogen-containing gas stream.
  • the water ⁇ oxygen content is in this case expediently tailored to the amount of oxygen.
  • the catalytic reaction is preferably carried out in an ent ⁇ speaking apparatus designed for this purpose of the cleaning device.
  • the cleaning device preferably comprises a reactor with a catalytically active material.
  • catalytic active material is preferably a noble metal catalyst, such as a platinum or a palladium catalyst used, at the surface of the catalytic oxidation of the metered hydrogen (or the catalytic reduction of the oxygen fes) takes place to form water.
  • the gas stream is then cooled and thus condensed in the gas stream, formed by the reaction of oxygen with hydrogen water.
  • the cleaning device preferably comprises ⁇ this, a cooler.
  • the cooler is expediently downstream of the reactor of the cleaning device fluidically. The condensed water is then removed.
  • the cleaning device preferably comprises a drying device.
  • the drying device is designed as an adsorption dryer, which extracts the moisture, ie in particular the water, from the carbon dioxide stream using appropriate drying agents.
  • the drying device is expediently connected downstream of the cooler.
  • An alternative embodiment provides a reactor with an integrated drying device so that both a catalyzed reaction of the oxygen with hydrogen and the drying of the carbon dioxide are carried out in a common apparatus.
  • the carbon dioxide stream is supplied only after completion of cleaning, ie after the catalyzed reaction of the oxygen with hydrogen within the reactor, the subsequent cooling and the condensation of the water formed, and the removal of the water by drying the compressor unit ,
  • the cleaning device is expediently over a discharge line fluidly connected to a supply line of the compressor unit.
  • the compressor unit can be designed in one or more stages.
  • the invention provides for use of a cleaning device which is designed to remove oxygen from the gas stream by means of chemisorption.
  • a cleaning device includes dedicated ⁇ advantageously two reactors in which the oxygen from the carbon dioxide is particularly and preferably removed by means of a copper ⁇ contact. The cleaning is preferably carried out via the oxidation of the copper contact. Expediently, such a cleaning device is also fluidically interposed between the desorption unit and the compressor unit.
  • the second object of the invention is achieved by a method for the separation of carbon dioxide from a gas stream, in particular from a flue gas stream, wherein a carbon dioxide-containing gas stream is fed to an absorption unit, wherein contained in the gas stream carbon dioxide is removed by means of a washing medium therefrom, with the Carbon dioxide laden washing medium of a desorption ⁇ unit is supplied, wherein the absorbed in the washing medium carbon dioxide is released from this, and wherein the free ⁇ set carbon dioxide before compression, that is uncompressed, a cleaning device is supplied.
  • oxygen contained in the carbon dioxide is catalytically reduced in the purifier.
  • a hydrogen-containing gas is expediently metered into the cleaning device.
  • the catalytic reduction of the oxygen or the catalytic oxidation of the added hydrogen takes place by means of a suitable catalytically active material.
  • a noble metal catalyst is used, which is filled in a reactor of the cleaning device.
  • water is formed. The water is preferably condensed out by cooling and removed as far as possible.
  • the oxygen-purified carbon dioxide is then dried so as to reduce the residual moisture.
  • the cooled carbon dioxide is subsequently compressed.
  • FIG. 1 shows a separator for carbon dioxide from egg ⁇ nem flue gas stream with a schematic cleaning device
  • the separation device 1 shows a separator 1 for carbon dioxide from a flue gas stream.
  • the separation device 1 comprises an absorption unit 3 and a desorption unit 5.
  • the flue gas 8 is brought into contact with a scrubbing medium 9 and carbon dioxide absorbed in the flue gas 8 is absorbed by the scrubbing medium 9 via a flue gas line 7.
  • a scrubbing medium 9 As the washing medium 9, an aqueous amino acid salt solution is used.
  • the purified flue gas is discharged via a discharge line 11 at the head 13 of the absorption unit 3 into the atmosphere.
  • the loaded with carbon dioxide washing medium 9 is removed via a 17 connected to the bottom 15 of the absorption unit 3 Abrioslei ⁇ . Via a fluidic coupling or connection of the discharge line 17 with a supply line 19 of the desorption 5, the loaded washing medium 9 of the desorption unit 5 is supplied. In this case, the washing medium 9 passes through a heat exchanger 21.
  • the carbon dioxide is released by thermal desorption again from the washing medium 9.
  • the liberated from carbon dioxide scrubbing medium 9 is returned via the fluidic connection of the desorpti ⁇ onsaku 5 connected discharge line 23 with a feed line 25 of the absorption unit 3 back into this ⁇ and is there for re-absorption of carbon dioxide from a flue gas 8 available.
  • the desorption unit 5 is connected to a reboiler 27 which, as a bottom evaporator, supplies a part of the heat of regeneration for the release of the carbon dioxide absorbed in the washing medium 9.
  • the released within the desorption unit 5 from the washing medium 9 carbon dioxide is withdrawn from the top 29 of the Desorptionsein ⁇ unit 5 via a connected there outlet line 31 therefrom and passes through a condenser 33.
  • the carbon dioxide stream also contains small amounts of oxygen from the gas stream must be removed.
  • the desorption unit 5 is fluidly connected downstream of a cleaning device 35, which is connected via a feed line 37 to the discharge line 31 of the desorption unit 5.
  • the oxygen contained in the carbon dioxide is removed. Only after cleaning, in FIG 2 is described in detail, the carbon dioxide ei ⁇ ner compressor unit 39 is supplied and compressed there.
  • the cleaning device 35 is flow technology between the desorption unit 3 and the
  • Compressor unit 39 is switched, so that the carbon dioxide stream leaving the Desoptions- unit 5 of the cleaning device 35 is supplied uncompressed.
  • the oxygen contained in the carbon dioxide stream is removed. This is done by a catalytic reduction of the oxygen contained in the carbon dioxide stream by means of hydrogen on a catalytically active surface.
  • the oxygen-containing carbon dioxide stream is the cleaning ⁇ device 35 via the fluidic connection of the discharge line 31 of the desorption 5 and the Zunaturallei ⁇ device 37 of the cleaning device 35 is supplied.
  • the feed line 37 of the cleaning device 35 is connected to a supply line 41 for a hydrogen-containing gas.
  • the hydrogen-containing gas flows after passing through a preheater 43 together with the oxygen-containing carbon dioxide stream in the reactor 45, which is downstream of the desorption unit 5 as part of the cleaning device 35 in terms of flow.
  • the reactor 45 is filled with a catalytically active material 47.
  • a catalytically active material 47 In the present case, platinum gratings are used.
  • the upper surface of the grating structure ⁇ provides the catalytically active surface on which the catalytic oxidation is carried out of the What ⁇ serstoffes or the catalytic reduction of oxygen.
  • water forms which, together with the carbon dioxide, flows out of this via a discharge line 49 of the reactor 45.
  • a cooler 51 is arranged, in which the water condenses out and deducted via a corresponding deduction ⁇ line 53.
  • the carbon dioxide starting from the cooler 51, is passed on to a drying device 55, where the water content in the carbon dioxide is reduced to below 1 ppmv by adsorption of the water still contained.
  • the cleaning device 35 is fluidly coupled via a discharge line 57 with a feed line 59 of the compressor unit 39.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Environmental & Geological Engineering (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Carbon And Carbon Compounds (AREA)
  • Treating Waste Gases (AREA)
  • Gas Separation By Absorption (AREA)
  • Catalysts (AREA)

Abstract

L'invention concerne un dispositif de séparation (1) de dioxyde de carbone d'un flux gazeux, notamment d'un flux de gaz de fumée, comprenant une unité d'absorption (3) pour séparer le dioxyde de carbone du flux gazeux à l'aide d'un milieu de lavage (9), une unité de désorption (5) reliée fluidiquement à l'unité d'absorption (3) pour libérer le dioxyde de carbone absorbé par le milieu de lavage (9), et une unité compresseur (39) raccordée fluidiquement en aval de l'unité de désorption (5) pour comprimer le dioxyde de carbone libéré, un un dispositif de nettoyage (35) destiné au dioxyde de carbone étant raccordé fluidiquement à l'unité compresseur (39) en amont de cette dernière. L'invention concerne également un procédé de séparation de dioxyde de carbone d'un flux gazeux, notamment d'un flux de gaz de fumée.
EP16706322.1A 2015-04-02 2016-02-10 Dispositif et procédé de séparation de dioxyde de carbone d'un flux gazeux Withdrawn EP3247483A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102015206050 2015-04-02
PCT/EP2016/052775 WO2016155929A1 (fr) 2015-04-02 2016-02-10 Dispositif et procédé de séparation de dioxyde de carbone d'un flux gazeux

Publications (1)

Publication Number Publication Date
EP3247483A1 true EP3247483A1 (fr) 2017-11-29

Family

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EP16706322.1A Withdrawn EP3247483A1 (fr) 2015-04-02 2016-02-10 Dispositif et procédé de séparation de dioxyde de carbone d'un flux gazeux

Country Status (7)

Country Link
US (1) US20180117530A1 (fr)
EP (1) EP3247483A1 (fr)
JP (1) JP2018515327A (fr)
CN (1) CN107427760A (fr)
AU (1) AU2016239468A1 (fr)
CA (1) CA2981366A1 (fr)
WO (1) WO2016155929A1 (fr)

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GB2607400A (en) * 2021-04-02 2022-12-07 Toshiba Kk Gas processing equipment and gas processing method, and carbon dioxide capture system and carbon dioxide capture method

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JP2010253370A (ja) * 2009-04-23 2010-11-11 Mitsubishi Heavy Ind Ltd Ｃｏ２回収装置及びｃｏ２回収方法
EP2598230A1 (fr) * 2010-07-28 2013-06-05 Sargas AS Turboréacteur à capture de carbone
JP6016513B2 (ja) * 2012-08-09 2016-10-26 三菱重工業株式会社 Ｃｏ２回収装置およびｃｏ２回収方法
FR2997311B1 (fr) * 2012-10-25 2015-12-11 Air Liquide Procede et installation pour eliminer l'oxygene d'un flux gazeux comprenant du co2
WO2014175478A1 (fr) * 2013-04-24 2014-10-30 한국에너지기술연구원 Appareillage pour séparer et collecter le co2 comportant un appareil de désoxydation
WO2014191160A1 (fr) * 2013-05-28 2014-12-04 Siemens Aktiengesellschaft Dispositif et procédé de séparation de dioxyde de carbone d'avec un courant gazeux
US10213728B2 (en) * 2013-06-21 2019-02-26 Siemens Aktiengesellschaft Method for separating carbon dioxide from a gas flow, in particular from a flue gas flow, and separating device for separating carbon dioxide from a gas flow, in particular from a flue gas flow
CN103539083B (zh) * 2013-10-17 2015-12-09 潘庆光 采用燃氢烟气制备工业氮气的方法

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JP2018515327A (ja) 2018-06-14
CA2981366A1 (fr) 2016-10-06
WO2016155929A1 (fr) 2016-10-06
CN107427760A (zh) 2017-12-01
AU2016239468A1 (en) 2017-09-07

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