WO2018100566A1 - Composition de récupération de dioxyde de carbone et système de récupération de dioxyde de carbone - Google Patents

Composition de récupération de dioxyde de carbone et système de récupération de dioxyde de carbone Download PDF

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Publication number
WO2018100566A1
WO2018100566A1 PCT/IB2018/000031 IB2018000031W WO2018100566A1 WO 2018100566 A1 WO2018100566 A1 WO 2018100566A1 IB 2018000031 W IB2018000031 W IB 2018000031W WO 2018100566 A1 WO2018100566 A1 WO 2018100566A1
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carbon dioxide
ionic liquid
absorption
melting point
temperature
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PCT/IB2018/000031
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English (en)
Japanese (ja)
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健太郎 植田
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大阪瓦斯株式会社
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    • 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
    • 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
    • B01D53/46—Removing components of defined structure
    • B01D53/62—Carbon oxides
    • 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
    • B01D53/77—Liquid phase processes
    • B01D53/78—Liquid phase processes with gas-liquid contact
    • 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
    • B01D53/81—Solid phase processes
    • 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
    • B01D53/81—Solid phase processes
    • B01D53/82—Solid phase processes with stationary reactants
    • 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
    • B01D53/96—Regeneration, reactivation or recycling of reactants
    • 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
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C211/00—Compounds containing amino groups bound to a carbon skeleton
    • C07C211/62—Quaternary ammonium compounds
    • C07C211/63—Quaternary ammonium compounds having quaternised nitrogen atoms bound to acyclic carbon atoms
    • 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 present invention relates to a carbon dioxide recovery composition containing an ionic liquid, and a carbon dioxide recovery method using the carbon dioxide recovery composition.
  • Patent Document 1 proposes a carbon dioxide separation and recovery method in which CO 2 is separated and recovered from a multicomponent mixed gas by a physical absorption method using an ionic liquid absorbing liquid.
  • absorption of carbon dioxide into an ionic liquid is an exothermic reaction.
  • the temperature of the ionic liquid is increased due to heat generation, the absorption rate of carbon dioxide is not preferable.
  • the present invention has been made in view of the above-described problems, and an object of the present invention is to provide a carbon dioxide recovery composition and a carbon dioxide recovery method that are advantageous in terms of heat balance when recovering carbon dioxide.
  • the characteristic configuration of the carbon dioxide recovery composition for achieving the above object is a carbon dioxide recovery composition containing an ionic liquid, which is an absorption state that is a melting point of the ionic liquid in a state of absorbing carbon dioxide
  • the melting point is 50 ° C. or more and 110 ° C. or less, and the melting point or decomposition temperature of the ionic liquid in a state where carbon dioxide is desorbed is higher than the absorption state melting point.
  • Carbon dioxide recovery is performed on exhaust gas (hereinafter referred to as processing gas) from engines and boilers in factories and power plants.
  • the temperature of these processing gases is generally about 60 ° C to 120 ° C.
  • the inventors have conceived to mitigate the adverse effects of heat generation due to absorption of carbon dioxide in this temperature range by utilizing heat generation and heat absorption associated with phase transition of the ionic liquid. And measure the melting point of the ionic liquid in the state of absorbing carbon dioxide of some ionic liquids, confirm that these ionic liquids cause a phase transition in the temperature range of general processing gas, carbon dioxide recovery As a result, the present invention was completed.
  • the absorption state melting point which is the melting point of the ionic liquid in the state of absorbing carbon dioxide
  • the carbon dioxide recovery composition containing the ionic liquid can be suitably used for carbon dioxide recovery.
  • Another characteristic configuration of the carbon dioxide recovery composition according to the present invention is that the ionic liquid contains tetraethylammonium benzimidazolide.
  • the absorption state melting point of tetraethylammonium benzimidazolide (hereinafter sometimes referred to as “N2Bn”) measured by the inventors is 55 ° C.
  • N2Bn tetraethylammonium benzimidazolide
  • Another characteristic configuration of the carbon dioxide recovery composition according to the present invention is that the ionic liquid contains tetraethylammonium imidazolide.
  • the absorption melting point of tetraethylammonium imidazolide (hereinafter sometimes referred to as “N2Im”) measured by the inventor is 70 ° C.
  • N2Im tetraethylammonium imidazolide
  • the carbon dioxide recovery composition can be suitably used for recovering carbon dioxide from a processing gas having a temperature higher than 70 ° C.
  • Another characteristic configuration of the carbon dioxide recovery composition according to the present invention is that the ionic liquid contains tetrabutylammonium carbazolide.
  • the absorption melting point of tetrabutylammonium carbazolide (hereinafter sometimes referred to as “N4Cz”) measured by the inventor is 100 ° C.
  • N4Cz tetrabutylammonium carbazolide
  • the characteristic configuration of the carbon dioxide recovery method for achieving the above object is a carbon dioxide recovery method having an absorption step
  • the absorption step is a step in which a treatment gas containing carbon dioxide is brought into contact with a carbon dioxide recovery composition containing an ionic liquid to absorb carbon dioxide into the ionic liquid;
  • the absorption state melting point which is the melting point of the ionic liquid in a state of absorbing carbon dioxide, is 50 ° C. or more and 110 ° C. or less, and the melting point or decomposition temperature of the ionic liquid in the state of removing carbon dioxide is the absorption state melting point.
  • Higher than The absorption process temperature at which the absorption process is performed is higher than the absorption state melting point.
  • Carbon dioxide recovery is performed on exhaust gas (hereinafter referred to as processing gas) from engines and boilers in factories and power plants.
  • the temperature of these processing gases is generally about 60 ° C to 120 ° C.
  • the inventors have conceived to mitigate the adverse effects of heat generation due to absorption of carbon dioxide in this temperature range by utilizing heat generation and heat absorption associated with phase transition of the ionic liquid. And measure the melting point of the ionic liquid in the state of absorbing carbon dioxide of some ionic liquids, confirm that these ionic liquids cause a phase transition in the temperature range of general processing gas, carbon dioxide recovery As a result, the present invention was completed.
  • the absorption state melting point of the ionic liquid in the state of absorbing carbon dioxide is 50 ° C. or higher and 110 ° C. or lower, and the melting point or decomposition temperature of the ionic liquid in the state of desorbing carbon dioxide is higher than the absorption state melting point.
  • the absorption process is performed using the carbon dioxide recovery composition containing the ionic liquid, and the absorption process temperature at which the absorption process is performed is higher than the absorption state melting point.
  • the carbon dioxide can be recovered in an advantageous state.
  • the regeneration step is a step of heating the carbon dioxide recovery composition to desorb carbon dioxide, and is performed after the absorption step,
  • the regeneration process temperature at which the regeneration process is performed is higher than the absorption process temperature and lower than the melting point and decomposition temperature of the ionic liquid.
  • FIG. 1 is a schematic configuration diagram of a temperature swing adsorption device in which a carbon dioxide recovery method using a carbon dioxide recovery composition is performed.
  • An ionic liquid is an organic salt that is melted without crystallization even at room temperature.
  • the composition for carbon dioxide recovery according to this embodiment is configured to contain the above-described ionic liquid.
  • the ionic liquid according to the present embodiment has an absorption state melting point that is a melting point of the ionic liquid in a state where carbon dioxide is absorbed is 50 ° C. or higher and 110 ° C. or lower, and a melting point of the ionic liquid in a state where carbon dioxide is desorbed or A decomposition temperature higher than the absorption state melting point is used.
  • Examples of the ionic liquid having such characteristics include tetraethylammonium benzimidazolide (N2Bn), tetraethylammonium imidazolide (N2Im), and tetrabutylammonium carbazolide (N4Cz).
  • N2Bn tetraethylammonium benzimidazolide
  • N2Im tetraethylammonium imidazolide
  • N4Cz tetrabutylammonium carbazolide
  • Tetraethylammonium benzimidazolide (tetraethyl ammoniumbenzimidazolide, N2Bn) is cationic: tetraethylammonium (tetraethylammonium, N 2222) and an anion: A benzimidazole (benzimidazole, BnIm) and salts, ionic liquids represented by the following formula 1 It is.
  • N2Bn can be synthesized by reacting tetraethylammonium hydroxide and benzimidazole. Specifically, it can be synthesized by the following procedure.
  • the absorption state melting point (Tmad) of N2Bn and the melting point or decomposition temperature (Tmde) of the ionic liquid in a state where carbon dioxide was desorbed were measured as follows.
  • Tmad About 1 g of N2Bn was put into the flask, the inside of the flask was evacuated to 0.1 kPa or less, and then the flask was heated from room temperature to 150 ° C. at a rate of 0.5 ° C./min with 14 kPa of carbon dioxide gas supplied. The temperature was raised. N2Bn was visually observed, and the temperature at which N2Bn was liquefied and about half was transparent was defined as Tmad. The Tmad of N2Bn was measured to be 55 ° C.
  • Tetraethylammonium imidazolide (tetraethylammoniumimidazolide, N2Im) is cationic: tetraethylammonium (tetraethylammonium, N 2222) and an anion: a salt with imidazole (imidazole, Im), it is an ionic liquid represented by the following Formula 2.
  • N2Im can be synthesized by reacting tetraethylammonium hydroxide and imidazole. Specifically, it can be synthesized by the following procedure.
  • a 100 ml three-necked reactor equipped with a dropping funnel and a three-way cock is charged with 0.82 g of imidazole (because it is a 98% product, 0.80 g, 11.8 mmol) and 4.0 ml of methanol, and stirred at room temperature. 4.94 g of 35% tetraethylammonium hydroxide solution (1.73 g, 11.8 mmol because it is a 35% product) is dropped from the dropping funnel. Thereafter, the dropping funnel is washed with methanol (2.0 ml), and the methanol solution is also dropped into the reaction system. After stirring at room temperature for 1 day, the solvent of this reaction mixture is distilled off and dried under reduced pressure (60 ° C. 17 hr) to obtain 1.45 g of a white solid.
  • the absorption melting point (Tmad) of N2Im and the melting point or decomposition temperature (Tmde) of the ionic liquid in a state where carbon dioxide was desorbed were measured as follows, similarly to N2Bn.
  • Tmad About 1 g of N2Im was put into the flask, the inside of the flask was evacuated to 0.1 kPa or less, and then the flask was supplied at a rate of 0.5 ° C./min from room temperature to 150 ° C. while supplying 14 kPa of carbon dioxide gas. The temperature was raised. N2Im was visually observed, and the temperature at the time when N2Im liquefied and about half of the amount became transparent was defined as Tmad. The Tmad of N2Im was measured as 70 ° C.
  • Tmde Treatment temperature
  • Tetrabutylammonium carbazolyl de (tetrabuthylammoniumcarbazolide, N4Cz) is cationic: tetrabutylammonium (tetrabuthylammonium, N 4444) and an anion: carbazole (carbazole, Cz) is a salt with an ionic liquid represented by the following Formula 3 It is.
  • N4Cz can be synthesized by reacting tetrabutylammonium hydroxide with carbazole. Specifically, it can be synthesized by the following procedure.
  • a 100 ml three-necked reactor equipped with a dropping funnel and a three-way cock is charged with 0.67 g of carbazole (because it is a 96% product, 0.64 g, 3.85 mmol) and 5.0 ml of THF, and stirred at room temperature.
  • a dropping funnel 10.00 g of a 10% tetrabutylammonium hydroxide methanol solution (1.00 g, 3.85 mmol because it is a 10% product) is dropped.
  • the dropping funnel is washed with THF (2.0 ml), and the THF solution is also dropped into the reaction system.
  • the solvent of this reaction mixture is distilled off and dried under reduced pressure (60 ° C., 17 hr) to obtain 1.26 g of a yellow solid.
  • the absorption melting point (Tmad) of N4Cz and the melting point or decomposition temperature (Tmde) of the ionic liquid in a state where carbon dioxide was desorbed were measured as follows in the same manner as N2Bn.
  • Tmad About 1 g of N4Cz was put into the flask, the inside of the flask was evacuated to 0.1 kPa or less, and then the flask was supplied at a rate of 0.5 ° C./min from room temperature to 150 ° C. while supplying 14 kPa of carbon dioxide gas. The temperature was raised. N4Cz was visually observed, and the temperature at which N4Cz was liquefied and about half was transparent was defined as Tmad. The N4Cz Tmad was measured at 100 ° C.
  • Tmde melting temperature
  • composition for recovering carbon dioxide containing an ionic liquid can be used for recovering carbon dioxide in a liquid state. Further, it is more preferable to use a carbon dioxide recovery composition containing an ionic liquid for carbon dioxide recovery in a state of being supported on a carrier.
  • Examples of applicable carriers include capsules and porous inorganic particles.
  • the capsule for example, a core-shell type capsule or a sea-island structure type capsule that is configured so that the gas absorbing material is not exposed to the surface is preferable. That is, the gas absorbing material is disposed on the inner side, and the outer side of the gas absorbing material is covered with a film or an outer shell.
  • the porous inorganic particles are preferably those that penetrate to the surface but do not elute even when the gas absorbing material is liquefied because the pore diameter is small.
  • Examples of inorganic substances forming the porous inorganic particles include silicates, phosphates, oxides, and the like.
  • Examples of the silicate include calcium silicate, barium silicate, magnesium silicate, and zeolite.
  • Examples of the phosphate include calcium phosphate, barium phosphate, magnesium phosphate, zirconium phosphate, and apatite.
  • Examples of the oxide include silicon oxide such as silicon dioxide and silicon monoxide, and alumina. Preferred is an oxide, more preferred is silicon oxide, and even more preferred is silicon dioxide.
  • the temperature swing adsorption device 1 in this embodiment includes a first absorption tank 2, a second absorption tank 3, a steam supply line 4, a process gas supply line 5, a carbon dioxide recovery line 6, an exhaust line 7, and a blower 8.
  • the gas absorbing material 9 is filled in each of the first absorption tank 2 and the second absorption tank 3.
  • the gas absorbent 9 is obtained by supporting the above-described carbon dioxide recovery composition on a carrier.
  • processing gas applicable to the temperature swing adsorption device 1 for example, industrial processing gas discharged from a thermal power plant, a steelworks blast furnace, an automobile and the like can be mentioned.
  • the processing gas is supplied to the first absorption tank 2 through the processing gas supply line 5 for a predetermined time, and the gas absorbent 9 absorbs carbon dioxide contained in the processing gas (absorption process).
  • the remaining gas components are discharged via the exhaust line 7.
  • the processing gas supply line 5 is switched to supply the processing gas to the second absorption tank 3 for a predetermined time, and high-temperature steam is supplied to the first absorption tank 2 through the vapor supply line 4 for a predetermined time. Then, carbon dioxide is desorbed to regenerate the gas absorbent 9 (regeneration step). The desorbed carbon dioxide is recovered via the carbon dioxide recovery line 6.
  • the processing gas supply line 5 is switched to supply the processing gas to the first absorption tank 2 again for a predetermined time, and the steam supply line 4 is switched to supply steam to the second absorption tank 3 for a predetermined time. And heated to desorb carbon dioxide to regenerate the gas absorbent 9.
  • an absorption process is performed in which the gas absorbent 9 is brought into contact with the processing gas and carbon dioxide is absorbed.
  • the carbon dioxide is removed by heating.
  • the regeneration step of regenerating the gas absorbing material 9 is operated, and is configured to switch every predetermined time. Therefore, carbon dioxide in the processing gas can be continuously separated and recovered.
  • phase change of the ionic liquid in the absorption process and the regeneration process described above will be described by taking as an example the case of using tetraethylammonium benzimidazolide (N2Bn) as the ionic liquid.
  • the regeneration step of the present embodiment is a step of heating the carbon dioxide recovery composition to desorb carbon dioxide.
  • N2Im tetraethylammonium imidazolide
  • the above-described temperature swing adsorption device 1 may further include a condenser. Since the recovered carbon dioxide contains moisture, only the carbon dioxide can be separated and recovered by removing the moisture with a condenser. The removed water can be reused as steam.
  • the above-described temperature swing adsorption device may be combined with a pressure swing method as necessary, or only the pressure swing method may be adopted instead of the temperature swing method.
  • the pressure swing method during the regeneration process, the carbon dioxide recovery line is pulled by a pump to make the inside of the absorption tank have a reduced pressure, so that regeneration of the gas absorbent can be promoted.
  • the gas absorbent 9 is filled in the first absorbent tank 2 and the second absorbent tank 3, and carbon dioxide is recovered without the gas absorbent 9 moving. And in the 1st absorption tank 2 and the 2nd absorption tank 3, an absorption process and a regeneration process are performed by turns.
  • the absorption process is performed in one tank (absorption tower), the regeneration process is performed in the other tank (regeneration tower), and the gas absorbent 9 (carrier carrying ionic liquid) is put into two tanks. It may be circulated. Specifically, the gas absorbent 9 comes into contact with the processing gas in the absorption tower, and the ionic liquid absorbs carbon dioxide and melts.
  • the gas absorbent 9 is transferred to the regeneration tower and heated by high-temperature steam, and the ionic liquid releases carbon dioxide and solidifies. And the gas absorption material 9 is moved to an absorption tower again.
  • the pressure swing method may be combined with the temperature swing method, or only the pressure swing method may be adopted instead of the temperature swing method.
  • the gas absorbent material 9 in a liquid state may be configured as follows. Then, the gas absorbent 9 in the liquid state may be circulated to the absorption tower / regeneration tower described above.

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  • Environmental & Geological Engineering (AREA)
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Abstract

L'invention concerne une composition de récupération de dioxyde de carbone et un procédé de récupération de dioxyde de carbone, qui sont avantageux en termes d'équilibre thermique pendant la récupération de dioxyde de carbone. Une composition pour la récupération de dioxyde de carbone, ladite composition contenant un liquide ionique, un point de fusion à l'état d'absorption, qui est le point de fusion du liquide ionique avec du dioxyde de carbone absorbé à l'intérieur de celui-ci étant compris entre 50 et 110 °C inclus, et la température de décomposition ou le point de fusion du liquide ionique avec le dioxyde de carbone désorbé de celui-ci est supérieur au point de fusion à l'état d'absorption.
PCT/IB2018/000031 2016-12-01 2018-01-25 Composition de récupération de dioxyde de carbone et système de récupération de dioxyde de carbone WO2018100566A1 (fr)

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JP2016234543A JP6815177B2 (ja) 2016-12-01 2016-12-01 二酸化炭素回収用組成物および二酸化炭素回収方法
JP2016-234543 2016-12-01

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JP7442137B2 (ja) * 2020-05-11 2024-03-04 株式会社タクマ ガス回収装置、及びガス回収方法

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20120222557A1 (en) * 2009-11-03 2012-09-06 University Of Notre Dame Du Lac Ionic liquids comprising heteraromatic anions
WO2015069799A1 (fr) * 2013-11-05 2015-05-14 University Of Notre Dame Du Lac Capture de dioxyde de carbone au moyen de liquides ioniques à changement de phase
US20150196895A1 (en) * 2012-07-13 2015-07-16 Danmarks Tekniske Universitet Co2 sorption by supported amino acid ionic liquids
WO2017163944A1 (fr) * 2016-03-24 2017-09-28 大阪瓦斯株式会社 Absorbeur de dioxyde de carbone et procédé de production d'un absorbeur de dioxyde de carbone
WO2017169669A1 (fr) * 2016-03-30 2017-10-05 大阪瓦斯株式会社 Matériau d'absorption de gaz, système de séparation et de récupération de dioxyde de carbone, et procédé de separation et de récupération de dioxyde de carbone

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20120222557A1 (en) * 2009-11-03 2012-09-06 University Of Notre Dame Du Lac Ionic liquids comprising heteraromatic anions
US20150196895A1 (en) * 2012-07-13 2015-07-16 Danmarks Tekniske Universitet Co2 sorption by supported amino acid ionic liquids
WO2015069799A1 (fr) * 2013-11-05 2015-05-14 University Of Notre Dame Du Lac Capture de dioxyde de carbone au moyen de liquides ioniques à changement de phase
WO2017163944A1 (fr) * 2016-03-24 2017-09-28 大阪瓦斯株式会社 Absorbeur de dioxyde de carbone et procédé de production d'un absorbeur de dioxyde de carbone
WO2017169669A1 (fr) * 2016-03-30 2017-10-05 大阪瓦斯株式会社 Matériau d'absorption de gaz, système de séparation et de récupération de dioxyde de carbone, et procédé de separation et de récupération de dioxyde de carbone

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