WO2024135202A1 - 一酸化炭素の製造方法及び製造装置 - Google Patents

一酸化炭素の製造方法及び製造装置 Download PDF

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WO2024135202A1
WO2024135202A1 PCT/JP2023/041785 JP2023041785W WO2024135202A1 WO 2024135202 A1 WO2024135202 A1 WO 2024135202A1 JP 2023041785 W JP2023041785 W JP 2023041785W WO 2024135202 A1 WO2024135202 A1 WO 2024135202A1
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carbon dioxide
gas
absorbent
carbon
ionic liquid
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French (fr)
Japanese (ja)
Inventor
慶太 神山
正和 佐々木
拓馬 竹田
章泰 満保
大輔 児玉
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Nihon University
Sanyo Chemical Industries Ltd
Toyo Engineering Corp
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Nihon University
Sanyo Chemical Industries Ltd
Toyo Engineering Corp
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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
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C25B1/01—Products
    • C25B1/23—Carbon monoxide or syngas
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B15/00—Operating or servicing cells
    • C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features

Definitions

  • the present invention relates to a method and apparatus for producing carbon monoxide, which has a simplified device and process, an ionic liquid that is less susceptible to deterioration, and has a relatively low activation overvoltage in the electrolysis step.
  • Exhaust gas generated in a combustion process usually contains a large amount of carbon dioxide gas. Releasing this exhaust gas directly into the atmosphere is undesirable from the viewpoint of preventing global warming. Furthermore, from the viewpoint of preventing global warming, technology to reduce the concentration of carbon dioxide in the atmosphere may be required.
  • a method for separating and recovering carbon dioxide gas from a gas that contains carbon dioxide gas for example, a method using an amine-based solvent is known.
  • a method using an ionic liquid which has excellent stability and absorbency, is also attracting attention. In this method, specifically, the carbon dioxide gas in the gas is absorbed into the ionic liquid, and then the carbon dioxide gas is separated and recovered from the ionic liquid. The ionic liquid after the separation and recovery of the carbon dioxide gas can be used again in the process of absorbing carbon dioxide gas.
  • JP 2018-89569 A describes a carbon dioxide recovery method that uses a composition containing an ionic liquid. It also describes an absorption process in which the carbon dioxide gas in a gas is absorbed into a composition containing an ionic liquid, and a regeneration process in which the composition is heated to separate and recover the carbon dioxide gas. It also explains that the composition after the carbon dioxide gas has been separated and recovered in the regeneration process can be used again in the absorption process.
  • carbon dioxide can be used as a raw material for producing carbon monoxide, for example.
  • carbon monoxide is produced when carbon dioxide is reduced by electrolysis.
  • the carbon monoxide obtained by electrolysis is useful as a raw material for synthesizing various products, such as synthetic fuels and methanol.
  • Figure 2 is a process flow diagram showing the conventional method and device.
  • gas containing carbon dioxide gas (Gas ( CO2 -rich)) is supplied to a pretreatment unit (T1) via a line 200.
  • a pretreatment unit (T1) treated water 50 flows from the top to the bottom, and the treated water 50 at the bottom is returned to the top via a line 201 using a pump 60 for circulation.
  • the gas after pretreatment (Gas ( CO2 -rich)) is supplied from the top of the pretreatment unit (T1) via a line 202 to a carbon dioxide absorption unit ( CO2 -A).
  • a liquid carbon dioxide absorbent containing an ionic liquid is supplied to the carbon dioxide absorption unit (CO 2 -A) in advance.
  • This carbon dioxide absorbent comes into contact with a gas containing carbon dioxide gas (Gas (CO 2 -rich)) supplied via line 202 and absorbs the carbon dioxide gas.
  • the carbon dioxide absorbent (Solvent (CO 2 -rich)) that has absorbed the carbon dioxide gas at the bottom of the carbon dioxide absorption unit (CO 2 -A) is supplied to a carbon dioxide separation unit (CO 2 -D) (corresponding to a unit that performs the regeneration step described in JP 2018-89569 A) using a pump 61 via line 203 and a heat exchanger 70.
  • CO 2 -lean in which the concentration of carbon dioxide has been reduced by the absorption of carbon dioxide in the carbon dioxide absorbent, is recovered or supplied to another system via line 204 from the upper portion of the carbon dioxide absorption unit (CO 2 -A).
  • the carbon dioxide absorbent is circulated through line 207 and heat exchanger 71 at the bottom of the carbon dioxide separation unit (CO 2 -D) and heated. This heating separates the carbon dioxide gas in the carbon dioxide absorbent.
  • the carbon dioxide absorbent with a reduced carbon dioxide concentration (Solvent (CO 2 -lean)) is supplied to the carbon dioxide absorption unit (CO 2 -A) using pump 63 through line 208, heat exchanger 70 and heat exchanger 72, and is reused.
  • the carbon dioxide gas (CO 2 gas) separated in the carbon dioxide separation unit (CO 2 -D) is supplied from the upper part of the carbon dioxide separation unit (CO 2 -D) via line 209 to the absorbent separation unit (D) after condensing water in a heat exchanger 73. Then, the carbon dioxide gas is recovered.
  • the condensed water (Water), which is a part of the carbon dioxide absorbent (Solvent), is returned to the carbon dioxide absorption unit (CO 2 -D) via line 210.
  • the carbon dioxide gas ( CO2 gas) after the water separation in the absorbent separation unit (D) is supplied to the compression unit (C) via line 211, where the carbon dioxide gas ( CO2 gas) is compressed.
  • the compressed carbon dioxide gas ( CO2 gas) is further supplied to the post-treatment unit (T2) via line 212, where the dehumidification process and the impurity removal process are performed.
  • the post-treated carbon dioxide gas (CO 2 gas) is supplied to a carbon dioxide electrolysis unit (CO 2 -E) via a line 213. Then, in this carbon dioxide electrolysis unit (CO 2 -E), the carbon dioxide gas (CO 2 gas) is electrolyzed to generate carbon monoxide gas (CO gas). The generated carbon monoxide gas (CO gas) is recovered via a line 214.
  • the number of devices is large and the process is complicated.
  • the operating temperature (110°C to 130°C) in the carbon dioxide separation unit (CO 2 -D) is relatively high, so there is a risk that the ionic liquid will deteriorate very gradually during long-term operation.
  • the activation overvoltage in the electrolysis process must be relatively high.
  • the object of the present invention is to provide a carbon monoxide production method and production apparatus that simplifies the device and process, is less susceptible to deterioration of the ionic liquid, and has a relatively low activation overvoltage in the electrolysis process.
  • the present invention relates to a carbon dioxide absorption process (CO 2 -a) in which carbon dioxide gas is absorbed into a carbon dioxide absorbent which contains an imidazolium ionic liquid (A) and water (B), and in which the ratio of the number of moles of water (B) to the number of moles of imidazolium ionic liquid (A) [number of moles of water (B ) ⁇ number of moles of imidazolium ionic liquid (A)] is 0.1 to 50; and a carbon dioxide electrolysis step (CO 2 -e) of generating carbon monoxide gas by electrolyzing the carbon dioxide gas absorbed in the carbon dioxide absorbent, thereby reducing the carbon dioxide concentration in the carbon dioxide absorbent.
  • CO 2 -a carbon dioxide absorption process
  • the present invention further provides a carbon dioxide absorption unit (CO 2 -A) that absorbs carbon dioxide gas into a carbon dioxide absorbent that contains an imidazolium ionic liquid (A) and water (B), in which the ratio of the number of moles of water ( B ) to the number of moles of imidazolium ionic liquid (A) [number of moles of water (B) ⁇ number of moles of imidazolium ionic liquid (A)] is 0.1 to 50; and a carbon dioxide electrolysis unit (CO 2 -E) that electrolyzes the carbon dioxide gas absorbed in the carbon dioxide absorbent to generate carbon monoxide gas and reduce the carbon dioxide concentration in the carbon dioxide absorbent.
  • CO 2 -A carbon dioxide absorption unit
  • CO 2 -E that electrolyzes the carbon dioxide gas absorbed in the carbon dioxide absorbent to generate carbon monoxide gas and reduce the carbon dioxide concentration in the carbon dioxide absorbent.
  • carbon dioxide gas is separated and recovered from the carbon dioxide absorbent, and this separated and recovered carbon dioxide gas is electrolyzed to produce carbon monoxide.
  • the carbon dioxide absorbent after absorbing carbon dioxide gas is used as is in the electrolysis step, and in this electrolysis step, the carbon dioxide gas absorbed in the carbon dioxide absorbent is electrolyzed to generate carbon monoxide and regenerate the carbon dioxide absorbent at the same time.
  • the carbon dioxide separation unit (CO 2 -D) as shown in Fig. 2 is not required, and the number of lines is also reduced. Furthermore, since the carbon dioxide separation unit (CO2-D) with a relatively high operating temperature (110°C to 130°C) is not required, a heat exchanger for heating the components in the device and a heat exchanger in the line for cooling the components when transferring them to another device are also not required. As a result, the device and process are simplified.
  • the ionic liquid is less likely to deteriorate.
  • the specific ionic liquid used in the present invention has excellent stability in the electrolysis process. Therefore, the ionic liquid is less likely to deteriorate in the electrolysis process.
  • the present invention provides a carbon monoxide production method and production device that simplifies the device and process, is less susceptible to deterioration of the ionic liquid, and has a relatively low activation overvoltage in the electrolysis process.
  • FIG. 1 is a process flow diagram illustrating one embodiment of the method and apparatus of the present invention.
  • FIG. 1 is a process flow diagram showing a conventional method and apparatus.
  • the carbon dioxide absorbent used in the present invention contains an imidazolium-based ionic liquid (A) and water (B), and the ratio of the number of moles of water (B) to the number of moles of imidazolium-based ionic liquid (A) [number of moles of water (B) ⁇ number of moles of imidazolium-based ionic liquid (A)] is 0.1 to 50.
  • the imidazolium-based ionic liquid (A) preferably contains a salt of a cation and an anion represented by the following general formula (1):
  • R 1 to R 4 each independently represent a hydrogen atom or an alkyl group having 1 to 6 carbon atoms, and X ⁇ represents an anion of a saturated acyclic monocarboxylic acid having 1 to 6 carbon atoms.
  • the imidazolium-based ionic liquid (A) used in the present invention is not limited to the above salts, and various other types of salts can be used as needed.
  • R 1 to R 4 are each independently a hydrogen atom or a chain alkyl group having 1 to 6 carbon atoms, and examples of the chain alkyl group having 1 to 6 carbon atoms include a methyl group, an ethyl group, an n-propyl group, an n-butyl group, and an n-hexyl group.
  • R 1 to R 4 are preferably a hydrogen atom, a methyl group, an ethyl group, an n-propyl group, and an n-butyl group.
  • R 1 to R 4 may be the same or different, and it is preferable that either R 1 or R 2 is a methyl group, and it is more preferable that either R 1 or R 2 is a methyl group and R 3 and R 4 are hydrogen atoms.
  • Preferred cations constituting the salt represented by general formula (1) include 1-methylimidazolium, 1-ethylimidazolium, 1-propylimidazolium, 1-butylimidazolium, 1,3-dimethyl-imidazolium, 1-ethyl-3-methylimidazolium, 1-propyl-3-methylimidazolium, 1-butyl-3-methylimidazolium, and 1-hexyl-3-methylimidazolium.
  • 1-ethyl-3-methylimidazolium and 1-butyl-3-methylimidazolium are preferred, and 1-ethyl-3-methylimidazolium is even more preferred.
  • X- is an anion of a saturated acyclic monocarboxylic acid having 1 to 6 carbon atoms
  • examples of the saturated acyclic monocarboxylic acid having 1 to 6 carbon atoms include acetic acid, propionic acid, butyric acid, isobutyric acid, valeric acid, pivalic acid, hydroangelic acid, and isovaleric acid.
  • the number of carbon atoms also includes the number of carbon atoms constituting the carboxyl group.
  • these carboxylic acids from the viewpoint of the amount of acidic gas absorption, acetic acid and propionic acid are preferred, and acetic acid is more preferred.
  • acetate and propionate are preferred, and acetate is more preferred.
  • the salt represented by general formula (1) can be produced by reacting a cationic methyl carbonate salt produced by a known method such as that described in JP-A-2001-316372 with a saturated aliphatic carboxylic acid.
  • 1-ethyl-3-methylimidazolium acetate, 1-ethyl-3-methylimidazolium propionate, and 1-butyl-3-methylimidazolium acetate are preferred, with 1-ethyl-3-methylimidazolium acetate and 1-ethyl-3-methylimidazolium propionate being even more preferred.
  • the weight of the imidazolium ionic liquid (A) contained in the carbon dioxide absorbent is preferably 75% by weight or more and 99% by weight or less, and more preferably 86% by weight or more and 95% by weight or less, based on the weight of the carbon dioxide absorbent. If the weight of the imidazolium ionic liquid (A) is not set to 100% by weight as in the above range, but a certain amount of water (B) is contained, the activation overvoltage during the electrolytic reduction of carbon dioxide can be further reduced, and carbon monoxide can be produced more efficiently.
  • the carbon dioxide absorbent used in the present invention contains water (B).
  • the weight of water (B) contained in the carbon dioxide absorbent is preferably 1% by weight or more and 25% by weight or less, and more preferably 5% by weight or more and 14% by weight or less, relative to the weight of the carbon dioxide absorbent.
  • the ratio of the number of moles of water (B) to the number of moles of imidazolium ionic liquid (A) is 0.1 to 50. If the ratio of the number of moles of water (B) to the number of moles of imidazolium ionic liquid (A) is within the above range, it is possible to both dissolve carbon dioxide and increase the efficiency of electrolysis.
  • the ratio of the number of moles of water (B) to the number of moles of imidazolium ionic liquid (A) [number of moles of water (B) ⁇ number of moles of imidazolium ionic liquid (A)] is 0.1 to 1.
  • the carbon dioxide absorbent used in the present invention may contain other components (also referred to as other components) other than the imidazolium ionic liquid (A) and water (B).
  • aprotic organic solvents include aprotic organic solvents [ester solvents (such as gamma-butyrolactone), nitrile solvents (such as acetonitrile), and ethers (such as diethylene glycol dimethyl ether and triethylene glycol dimethyl ether)], and protic organic solvents [alcohol solvents (such as methanol, ethanol, and propanol)].
  • FIG. 1 is a process flow diagram showing one embodiment of the method and apparatus of the present invention. The present invention will be described in detail below with reference to FIG. 1.
  • the method of the present invention has a carbon dioxide absorption step (CO 2 -a) in which carbon dioxide gas is absorbed in the carbon dioxide absorbent described above.
  • the apparatus of the present invention also has a carbon dioxide absorption unit (CO 2 -A) for carrying out this carbon dioxide absorption step (CO 2 -a).
  • a gas containing carbon dioxide gas is used. That is, the gas containing carbon dioxide gas is brought into contact with a carbon dioxide absorbent, thereby allowing the carbon dioxide gas to be absorbed in the carbon dioxide absorbent.
  • the type of gas containing carbon dioxide is not particularly limited.
  • exhaust gas generated in the combustion process of facilities such as factories and power plants usually contains a large amount of carbon dioxide. It is not preferable from the viewpoint of environmental protection to release this exhaust gas directly into the atmosphere. Therefore, in the present invention, it is a preferred embodiment to separate and recover carbon dioxide from such exhaust gas. However, the present invention is not limited thereto. If necessary, other gases (for example, air) may be used as the gas containing carbon dioxide gas.
  • the temperature when the carbon dioxide absorption step (CO 2 -a) is carried out is preferably 30° C. to 60° C.
  • the pressure is preferably 0 to 30 kPaG. Carbon dioxide is more easily absorbed at low temperatures and high pressures, but from the viewpoint of economy, the above-mentioned operating conditions are often adopted.
  • the gas containing carbon dioxide mentioned above may be pretreated as necessary.
  • This pretreatment may include, for example, a cleaning process to remove impurities contained in the gas.
  • gas containing carbon dioxide gas (Gas ( CO2 -rich)) is supplied to a pretreatment unit (T1) via a line 100.
  • gas containing carbon dioxide gas (Gas ( CO2 -rich)
  • pretreatment unit (T1) treated water 50 flows from the top to the bottom, and the treated water 50 at the bottom is returned to the top via a line 101 using a pump 60 for circulation.
  • the gas after pretreatment (Gas ( CO2 -rich)) is supplied from the top of the pretreatment unit (T1) via a line 102 to a carbon dioxide absorption unit ( CO2 -A).
  • a liquid carbon dioxide absorbent is supplied in advance to the carbon dioxide absorption unit (CO 2 -A) in Fig. 1.
  • This carbon dioxide absorbent comes into contact with a gas containing carbon dioxide gas (Gas (CO 2 -rich)) supplied via a line 102, and absorbs the carbon dioxide gas.
  • the carbon dioxide absorbent (Solvent (CO 2 -rich)) that has absorbed the carbon dioxide gas at the bottom of the carbon dioxide absorption unit (CO 2 -A) is supplied to the carbon dioxide electrolysis unit (CO 2 -E) via a line 103 using a pump 61.
  • gas whose carbon dioxide concentration has been reduced by the absorption of the carbon dioxide gas into the carbon dioxide absorbent may be subjected to other treatments (e.g., cleaning treatment) as necessary.
  • the gas after cleaning may be subjected to further treatments.
  • the gas after cleaning, or the gas that has not been cleaned may be released directly into the atmosphere.
  • gas (CO 2 -lean) in which the carbon dioxide concentration has been reduced by the carbon dioxide being absorbed by the carbon dioxide absorbent is recovered via line 104 from the top of the carbon dioxide absorption unit (CO 2 -A), or is supplied to another system, or is released into the atmosphere.
  • the method of the present invention has a carbon dioxide electrolysis step (CO 2 -e) in which carbon dioxide gas absorbed in the carbon dioxide absorbent described above is electrolyzed to generate carbon monoxide gas.
  • the device of the present invention also has a carbon dioxide electrolysis unit (CO 2 -E) for carrying out this carbon dioxide electrolysis step (CO 2 -e ).
  • This electrolysis causes a reduction reaction of carbon dioxide to generate carbon monoxide gas. As a result, the carbon dioxide gas is consumed and the carbon dioxide concentration in the carbon dioxide absorbent is reduced.
  • the temperature when performing the carbon dioxide electrolysis step is preferably 20°C to 80°C, more preferably 20°C to 60°C. This temperature can be lower than the temperature required for the conventional carbon dioxide separation step (corresponding to the regeneration step described in JP 2018-89569 A).
  • the pressure is approximately 20 to 100 kPaG, but may be higher if the specifications of the electrolysis device allow.
  • the voltage depends on the specifications of the electrolysis device and the type of ionic liquid, but since it is believed that the activation overvoltage required for electrolysis of carbon dioxide is reduced due to the effect of the ionic liquid, it may be possible to lower the voltage than that required for the conventional electrolysis step.
  • the apparatus used in the carbon dioxide electrolysis step (CO 2 -e) may be, for example, that described in JP 2018-154901 A. However, the present invention is not limited thereto, and various other known apparatuses may be used.
  • the carbon dioxide concentration in the carbon dioxide absorbent is reduced by electrolysis in the carbon dioxide electrolysis step (CO 2 -e).
  • the carbon dioxide absorbent after electrolysis of carbon dioxide gas can be reused in the carbon dioxide absorption step (CO 2 -a). That is, in the method of the present invention, it is preferable to reuse the carbon dioxide absorbent after electrolysis of carbon dioxide gas in the carbon dioxide electrolysis step (CO 2 -e) in the carbon dioxide absorption step (CO 2 -a). In addition, it is preferable for the device of the present invention to reuse the carbon dioxide absorbent after electrolysis of carbon dioxide gas in the carbon dioxide electrolysis unit (CO 2 -E) in the carbon dioxide absorption unit (CO 2 -A).
  • the carbon dioxide absorbent (Solvent (CO 2 -rich)) that has absorbed carbon dioxide in the carbon dioxide absorption unit (CO 2 -A) is supplied to the carbon dioxide electrolysis unit (CO 2 -E) via line 103. Then, in this carbon dioxide electrolysis unit (CO 2 -E), the carbon dioxide absorbed in the carbon dioxide absorbent (Solvent (CO 2 -rich)) is electrolyzed to generate carbon monoxide gas.
  • the carbon dioxide absorbent (Solvent (CO 2 -lean)) with a reduced carbon dioxide concentration is supplied to the carbon dioxide absorption unit (CO 2 -A) via line 107 using pump 63 and is used again.
  • carbon monoxide gas is generated by electrolysis in the carbon dioxide electrolysis step (CO 2 -e).
  • the carbon dioxide absorbent used in the present invention has a high solubility of carbon dioxide but a very low solubility of carbon monoxide. Therefore, the generated carbon monoxide gas can be easily recovered from the carbon dioxide absorbent.
  • the method of the present invention preferably further comprises an absorbent separation step (d) for separating the carbon dioxide absorbent remaining in the recovered carbon monoxide gas.
  • the apparatus of the present invention preferably further comprises an absorbent separation unit (D) for carrying out the absorbent separation step (d). This is because there may be cases where the absorbent remains in the carbon monoxide gas in the form of vapor.
  • carbon monoxide gas produced in the carbon dioxide electrolysis unit (CO 2 -E) is supplied from the top of the carbon dioxide electrolysis unit (CO 2 -E) via line 108 to the absorbent separation unit (D) to perform the absorbent separation step (d).
  • the absorbent (solvent) separated in the absorbent separation unit (D) is returned via line 109 to the carbon dioxide electrolysis unit (CO 2 -E) together with the absorbent (solvent (CO 2 -rich)) supplied from line 103.
  • the recovered carbon monoxide gas may be subjected to a compression process and other post-treatment processes (e.g., a dehumidification process, an impurity removal process) as necessary.
  • carbon monoxide gas (CO gas) after the absorbent is separated in the absorbent separation unit (D) is supplied to the compression unit (C) via line 110, and the carbon monoxide gas (CO gas) is compressed in the compression process (d).
  • the compressed carbon monoxide gas (CO gas) is further supplied to the post-treatment unit (T2) via line 111, where the dehumidification process and impurity removal process are carried out.
  • the carbon monoxide gas (CO gas) after post-treatment is then recovered via line 112.
  • the carbon monoxide produced can be used as a raw material for various products, such as synthetic fuels and methanol.
  • products such as synthetic fuels and methanol.
  • a two-necked recovery flask containing 10 g of a carbon dioxide absorbent was adjusted to 40° C. under atmospheric pressure.
  • a gas collection balloon containing carbon dioxide was attached to the two-necked recovery flask (5), and carbon dioxide was blown into the two-necked recovery flask from the gas collection balloon, and then the flask was sealed with a rubber stopper.
  • the weight of the two-neck flask was measured.
  • Carbon dioxide was blown into the container again using the method described in (6), and the container was then sealed with a rubber stopper. The container was then subjected to vibration for 3 minutes and its weight was measured.
  • the carbon dioxide used was produced by Iwatani Corporation.
  • 1-ethyl-3-methylimidazolium acetate was a reagent manufactured by Tokyo Chemical Industry Co., Ltd.
  • the effects of the present invention are not limited to the simplification of the carbon monoxide production equipment and process by making it possible to omit the carbon dioxide separation step (a regeneration step with a relatively high operating temperature) in conventional methods, and the prevention of deterioration of the ionic liquid.
  • the improvement in the efficiency of carbon monoxide production by, for example, lowering the activation overvoltage, as demonstrated by the results of Examples 1 to 4, is also one of the effects of the present invention.
  • the present invention is highly useful as a method and apparatus for separating carbon dioxide gas from a gas (eg, exhaust gas), and as a method and apparatus for producing carbon monoxide.

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PCT/JP2023/041785 2022-12-22 2023-11-21 一酸化炭素の製造方法及び製造装置 Ceased WO2024135202A1 (ja)

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WO2012077198A1 (ja) * 2010-12-08 2012-06-14 トヨタ自動車株式会社 燃料製造システム
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HAILU AMANUEL, SHAW SCOTT K.: "Efficient Electrocatalytic Reduction of Carbon Dioxide in 1-Ethyl-3-methylimidazolium Trifluoromethanesulfonate and Water Mixtures", ENERGY & FUELS, AMERICAN CHEMICAL SOCIETY, WASHINGTON, DC, US., vol. 32, no. 12, 20 December 2018 (2018-12-20), WASHINGTON, DC, US. , pages 12695 - 12702, XP055957751, ISSN: 0887-0624, DOI: 10.1021/acs.energyfuels.8b02750 *

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