WO2017088981A1 - Procédé et dispositif de séparation du dioxyde de carbone à partir d'un gaz de synthèse - Google Patents

Procédé et dispositif de séparation du dioxyde de carbone à partir d'un gaz de synthèse Download PDF

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Publication number
WO2017088981A1
WO2017088981A1 PCT/EP2016/025138 EP2016025138W WO2017088981A1 WO 2017088981 A1 WO2017088981 A1 WO 2017088981A1 EP 2016025138 W EP2016025138 W EP 2016025138W WO 2017088981 A1 WO2017088981 A1 WO 2017088981A1
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WIPO (PCT)
Prior art keywords
gas
carbon dioxide
synthesis
detergent
synthesis gas
Prior art date
Application number
PCT/EP2016/025138
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German (de)
English (en)
Inventor
Peter Riesch
Ulvi Kerestecioglu
Andreas Peschel
Original Assignee
Linde Aktiengesellschaft
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Publication of WO2017088981A1 publication Critical patent/WO2017088981A1/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
    • C10K1/16—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with non-aqueous liquids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D19/00—Degasification of liquids
    • B01D19/0036—Flash degasification
    • 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
    • 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
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/22—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds
    • C01B3/24—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons
    • 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
    • C01B3/52—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with liquids; Regeneration of used liquids
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/002—Removal of contaminants
    • C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
    • C10K1/005—Carbon dioxide
    • 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
    • B01D2252/202—Alcohols or their derivatives
    • 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
    • B01D2252/202—Alcohols or their derivatives
    • B01D2252/2021—Methanol
    • 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
    • B01D2252/205—Other organic compounds not covered by B01D2252/00 - B01D2252/20494
    • 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
    • B01D2256/24—Hydrocarbons
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0415—Purification by absorption in liquids
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0475—Composition of the impurity the impurity being carbon dioxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/06—Integration with other chemical processes
    • C01B2203/061—Methanol production
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/06—Integration with other chemical processes
    • C01B2203/062—Hydrocarbon production, e.g. Fischer-Tropsch process
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/14—Details of the flowsheet
    • C01B2203/148—Details of the flowsheet involving a recycle stream to the feed of the process for making hydrogen or synthesis gas
    • 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
    • C10J2300/0969—Carbon dioxide
    • 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 process for the production and use of a largely consisting of hydrogen and carbon monoxide synthesis gas, wherein a hydrocarbon-containing starting material is converted to a sulfur-free synthesis crude, from the carbon dioxide by means of a physically acting
  • Detergent is separated by a gas scrubbing while the one with
  • Carbon dioxide laden detergent is obtained during its regeneration
  • the invention relates to a device for carrying out the
  • sulfur-free is understood to mean a crude synthesis gas whose content of sulfur components does not exceed a value of 0.1 ppm. A complete absence of sulfur, which can not be achieved with reasonable effort anyway, is not required.
  • a gas mixture should be considered as rich in carbon dioxide, if its
  • Methods and devices of the generic type are used for example in the methanol synthesis, the Fischer-Tropsch synthesis or the hydroformylation of olefins and in particular in the direct synthesis of dimethyl ether.
  • DME Dimethyl ether
  • a combustible substance with a high hydrogen content which is present under normal conditions as a colorless gas.
  • DME has a boiling point of -25.1 ° C at atmospheric pressure and has a vapor pressure of 0.6 MPa at 25 ° C, which is why it is as easy to liquefy and handle as LPG. Because DME without the formation of soot and
  • DME is produced on an industrial scale in two-stage process, being produced in the first stage of a synthesis gas from methanol, which is formed in the second stage by dehydration DME. For some time, however, efforts have been made from different sides
  • direct DME synthesis Compared to the two-stage DME synthesis, direct DME synthesis has significant advantages, resulting in savings in both capital and operating costs. For use in direct DME synthesis
  • the product stream obtained in the direct DME synthesis contains in addition
  • the product stream comprises, in addition to dimethyl ether, at least methanol, water, carbon dioxide, carbon monoxide and hydrogen and, to a lesser extent, methane, ethane, organic acids and higher alcohols.
  • the product stream is cooled, so that water is obtained in the form of a water / methanol mixture, which is subsequently in a
  • Particularly low H 2 / CO ratios in the range of 1.0 can be obtained by the dry reforming of a methane-rich feed such as natural gas.
  • the synthesis crude gas according to the prior art is subjected to either an amine or a methanol wash, but both have specific disadvantages.
  • the separated carbon dioxide falls in an amine scrubbing at a pressure which is only slightly higher than that
  • Object of the present invention is therefore to provide a method and an apparatus of the generic type, which allow the cost of the
  • This object is achieved procedurally according to the invention that carbon dioxide is separated from the loaded detergent only by lowering the pressure and subsequent warm expulsion.
  • the regeneration of the loaded detergent according to the invention is significantly simplified and can therefore be carried out at significantly lower costs.
  • carbon dioxide is only incompletely removed from the detergent and recovered with low purity.
  • the regenerated detergent is therefore recycled to the gas scrubber with a significantly increased carbon dioxide partial pressure over the prior art. Since this partial pressure determines the minimum achievable in the gas scrubbing carbon dioxide concentration in the scrubbed gas, a synthesis gas is obtained with a relatively high carbon dioxide content.
  • the carbon dioxide is separated from the loaded detergent only to the extent that the carbon dioxide content in the synthesis gas reaches a maximum value determined by its intended use or does not fall below by more than 0.1 mol%.
  • the synthesis gas is to be used in direct DME synthesis, it is preferably produced according to the invention with a carbon dioxide content lying between 0.1 and 10 mol%.
  • the simplified detergent regeneration causes that in comparison to the prior art, an increased amount of detergent enters the carbon dioxide-rich gas stream, which is recycled and used in the synthesis of the synthesis gas. As long as the increased amount of detergent does not lead to an unfavorable composition of the raw synthesis gas and / or disturbs its production process, but it is not critical. First and foremost, the proportion of detergent in the
  • methanol is used as a detergent because it can be easily converted to synthesis gas and replaced at low cost.
  • ethanol, acetone, ethyl acetate, DME or a mixture of at least one of these substances and also methanol or of at least two of these substances as detergents.
  • both the process for producing the synthesis gas and the process in which the synthesis gas produced is converted into a product include one or more process steps in which the same or very similar
  • Material streams are subjected to the same treatment. For example, falls during the detergent regeneration for carbon dioxide removal from the
  • Methanol used in synthesis crude gas to a predominantly consisting of water and methanol mixture is separated from the water in a separation step to obtain a water content reduced methanol fraction, which can be used again as a detergent in the gas scrubbing.
  • a same separation step is, as described above, also required in the direct DME synthesis. Appropriately, to carry out such
  • Process step used the same device and simultaneously used both in the production, as well as the use of the synthesis gas.
  • a methanol / water mixture obtained in methanol scrubbing in the production of a synthesis gas as an insert for a direct DME synthesis and a direct DME synthesis are treated together in a separator to separate water and methanol from each other.
  • a variant of the method according to the invention provides to carry out the warm expulsion in several successive steps in order to obtain a partially regenerated detergent stream and to use it approximately for the separation of a generated during the use of the synthesis gas stream.
  • This process variant is preferably used when carbon dioxide is washed out of the synthesis crude gas by methanol and the resulting synthesis gas is used in the direct DME synthesis.
  • a further variant of the method according to the invention provides that a material stream containing, when using the synthesis gas, unreacted components of the synthesis gas and carbon dioxide-containing material stream for producing the
  • the invention relates to a device for the production and use of a largely consisting of hydrogen and carbon monoxide synthesis gas, with a gas generator in which a sulfur-containing synthesis crude can be obtained from a hydrocarbon-containing starting material, a gas scrubber with an absorber for the separation of carbon dioxide from the syngas with the help a physically acting detergent and a regeneration part for the regeneration of the absorbent laden with separated substances in the absorber, wherein the regeneration part is connected to the gas generator so that a in the
  • Detergent regeneration occurring carbon dioxide-rich gas stream can be attributed as an insert into the gas generator, and a production facility in which the synthesis gas is converted into a product.
  • the object is achieved device-side according to the invention that the regeneration part for the separation of carbon dioxide from the loaded detergent only a relaxation device and a downstream of the
  • Relaxing device arranged means for warm expulsion.
  • both the expansion device and the device for warm expulsion via a line connected to the gas generator in order to perform this carbon dioxide as an insert can. It is also possible that only the device for warm expulsion is connected to the gas generator, while the Relaxation device with the absorber or the production device is in fluid communication to supply these separated carbon dioxide.
  • the expansion device comprises a throttle body and a separator, wherein in the absorber with carbon dioxide laden detergent via the throttle body is depressurized to produce a two-phase mixture, which can be separated in the separator in a carbon dioxide-rich gas and a depleted in the carbon dioxide liquid phase.
  • the device for hot expulsion preferably comprises a column
  • Head cooler and a reboiler wherein both the head cooler and the reboiler can be arranged outside the column or integrated into the column. Further preferably, the column is preceded by a heat exchanger for heating the detergent to be regenerated. Most preferably, the column has less
  • a variant of the device according to the invention provides that at least one part of the plant can be used simultaneously for the generation and the use of the synthesis gas.
  • the jointly usable part of the plant is a water separation device in which water can be separated from the detergent loaded in the gas scrubbing detergent before the detergent regenerated is returned to the absorber.
  • a device for direct DME synthesis in which the synthesis gas generated is convertible to dimethyl ether, is the
  • the device according to the invention comprises, in particular in this case, a bypass line via which part of the methanol scrubbed in the gas scrubber branches off upstream of the direct DME synthesis device and without further treatment from the direct DME synthesis water scavenger to the absorber recycled methanol stream can be mixed. Further developing the device according to the invention, it is proposed to arrange a separator between the column of the warm expelling device and the upstream of the column heat exchanger, in which the heated in the heat exchanger detergent can be separated into a gas and a liquid phase.
  • the separator is connected both to the column and to the production device, so that both the gas phase and a first part of the liquid phase of the column and a second part of the liquid phase of the production device can be supplied, where it is used, for example, for product processing. It is particularly preferred to use this device variant if the production device is a device for direct DME synthesis and gas scrubbing is a methanol wash.
  • Figures 1 and 2 each show means for generating a synthesis gas and its use for the production of DME, wherein the synthesis gas is recovered according to preferred variants of the invention.
  • a hydrocarbon-containing starting material is the
  • Gas generator G supplied where it is converted into a sulfur-free synthesis gas 2.
  • a sulfur-free synthesis gas 2 For the separation of carbon dioxide, consisting mainly of hydrogen, carbon monoxide and carbon dioxide synthesis gas 2 in the
  • Absorber column A is initiated, where it flows at a pressure of typically 20 to 80 bar up and in intensive contact with an overhead of the
  • Absorber column A supplied methanol detergent 3 is brought.
  • Methanol detergent 3 which may already be preloaded with its supply with carbon dioxide, absorbs only a portion of the synthesis gas 2 contained in the synthesis
  • Dimethyl ether 5 is reacted.
  • the methanol washing agent 6 loaded with substances separated from the synthesis gas 2 is depressurized in a first step via the throttle body a to a pressure of about 3 to 40 bar, absorbed substances passing into the gas phase, so that a two-phase mixture 7 enters the separator D1 passes and there in a first carbon dioxide-rich, hydrogen and carbon monoxide-containing gas phase 8 and a reduced carbon dioxide content methanol detergent 9 is separated.
  • the reduced only in carbon dioxide content methanol detergent 9 is continued in the device for hot expulsion W, where it is first warmed in the heat exchanger E1 against regenerated methanol detergent 3 and subsequently introduced into the middle part of the column K to further carbon dioxide through
  • the column K which is supplied via the reboiler E2 heat and having fewer exchange trays, as known from the prior art for the same purpose column is equipped with a head cooler E3, with the help of which especially water and methanol from the Head withdrawn, consisting primarily of carbon dioxide gas phase 1 1
  • the resulting two-phase mixture 12 is separated in the separator D2 in a second carbon dioxide-rich gas phase 13 and a largely consisting of water, methanol and carbon dioxide second liquid phase 14, which is recycled as reflux to the top of the column K.
  • a synthesis gas 4 with an advantageous for direct DME synthesis H 2 / CO ratio in the vicinity of 1, 0, at least the second carbon dioxide-rich gas phase 13 to
  • Gas generator G returned.
  • the first carbon dioxide-rich gas phase 8 is also introduced into the gas separator G as stream 8 ', recycled as stream 8 " into the absorber column A or used as stream 8 "' in the DME synthesis device M.
  • Both the reboiler E2 and the head cooler E3 are operated with comparatively low power, so that the liquid fraction 16 withdrawn from the bottom of the column K and consisting predominantly of water and methanol has a relatively high carbon dioxide concentration of between 0.01 and 3 mol%.
  • the liquid fraction 16 in the DME synthesis device M arranged methanol / water separator T supplied, which is used at the same time for the separation of a resulting in the direct DME synthesis methanol / water mixture.
  • Via line 3 regenerated methanol detergent, which is largely anhydrous, but still contains carbon dioxide, returned to the absorber column A.
  • the liquid fraction 16 may also be split so that only a portion is passed to the separation unit T to remove the water from the methanol stream while the remainder 17 is regenerated
  • FIG. 2 shows a variant of the device from FIG. 1 with a modified one
  • regenerated methanol detergent 21 from which a part 22 is forwarded to the further regeneration in the column W, while another part 23 of the DME synthesis device M is fed and used there for the product separation, after which he prepared in particular by water separation and shared with the regenerated methanol detergent 3 is returned to the absorber column A.
  • the carbon dioxide-rich gas phase 24 produced in the separator D3 is likewise introduced into the column W.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Analytical Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Gas Separation By Absorption (AREA)

Abstract

L'invention concerne un procédé ainsi qu'un dispositif pour produire et utiliser un gaz de synthèse (4) constitué en grande partie d'hydrogène et de monoxyde de carbone, en faisant réagir un produit de départ (1) hydrocarboné pour donner un gaz de synthèse brut (2) sans soufre à partir duquel le dioxyde de carbone est séparé par épuration des gaz par voie humide (A) à l'aide d'un détergent (3) physiquement actif, épuration au cours de laquelle on obtient un détergent (6) chargé en dioxyde de carbone au cours de la régénération duquel on obtient un flux gazeux (13) riche en dioxyde de carbone à utiliser pour produire le gaz de synthèse brut (2) ainsi qu'un détergent (3) régénéré à réutiliser pour l'épuration des gaz par voie humide (A) et le gaz de synthèse (4) produit étant transformé en un produit (5). L'invention est caractérisée en ce que le dioxyde de carbone est séparé du détergent chargé simplement par réduction de la pression (a) puis expulsion de chaleur (W).
PCT/EP2016/025138 2015-11-26 2016-11-08 Procédé et dispositif de séparation du dioxyde de carbone à partir d'un gaz de synthèse WO2017088981A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102015015310.2A DE102015015310A1 (de) 2015-11-26 2015-11-26 Verfahren und Vorrichtung zur Kohlendioxidabtrennung aus Synthesegas
DE102015015310.2 2015-11-26

Publications (1)

Publication Number Publication Date
WO2017088981A1 true WO2017088981A1 (fr) 2017-06-01

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CN (1) CN106800953A (fr)
DE (1) DE102015015310A1 (fr)
WO (1) WO2017088981A1 (fr)

Cited By (2)

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Publication number Priority date Publication date Assignee Title
EP3666364A1 (fr) * 2018-12-14 2020-06-17 L'air Liquide, Société Anonyme Pour L'Étude Et L'exploitation Des Procédés Georges Claude Procédé et dispositif de régénération du détergent chargé à partir d'un lavage à gaz
WO2022106051A1 (fr) * 2020-11-18 2022-05-27 Linde Gmbh Méthode et dispositif pour générer un gaz de synthèse tout en faisant recirculer du dioxyde de carbone

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DE102018000817A1 (de) * 2018-02-01 2019-08-01 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Übertragung von Wärme auf einen zweiphasigen Stoffstrom
DE102019001557A1 (de) * 2019-03-06 2020-09-10 Linde Gmbh Verfahren und Vorrichtung zur Synthesegaserzeugung mit Kohlendioxidrückführung

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EP2767324A1 (fr) * 2013-02-14 2014-08-20 Linde Aktiengesellschaft Procédé de fonctionnement d'un lavage physique de gaz utilisant du méthanol
US20140357736A1 (en) * 2012-01-04 2014-12-04 Haldor Topsøe A/S Co-production of methanol and urea
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US20140357736A1 (en) * 2012-01-04 2014-12-04 Haldor Topsøe A/S Co-production of methanol and urea
US20150197422A1 (en) * 2012-04-10 2015-07-16 Total Raffinage Chimie Method for processing a gas stream by absorption
EP2767324A1 (fr) * 2013-02-14 2014-08-20 Linde Aktiengesellschaft Procédé de fonctionnement d'un lavage physique de gaz utilisant du méthanol
US20150139879A1 (en) * 2013-11-19 2015-05-21 IFP Energies Nouvelles Method and plant for removing acid compounds from gaseous effluents of different origins

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3666364A1 (fr) * 2018-12-14 2020-06-17 L'air Liquide, Société Anonyme Pour L'Étude Et L'exploitation Des Procédés Georges Claude Procédé et dispositif de régénération du détergent chargé à partir d'un lavage à gaz
WO2022106051A1 (fr) * 2020-11-18 2022-05-27 Linde Gmbh Méthode et dispositif pour générer un gaz de synthèse tout en faisant recirculer du dioxyde de carbone

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