US20140284521A1 - Co2 desorption catalyst - Google Patents

Co2 desorption catalyst Download PDF

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Publication number
US20140284521A1
US20140284521A1 US14/356,074 US201214356074A US2014284521A1 US 20140284521 A1 US20140284521 A1 US 20140284521A1 US 201214356074 A US201214356074 A US 201214356074A US 2014284521 A1 US2014284521 A1 US 2014284521A1
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inorganic powder
catalyst
desorption
surface area
solution
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Hiroshi Deguchi
Tsunenori Watanabe
Yasuyuki Yagi
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Kansai Electric Power Co Inc
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Kansai Electric Power Co Inc
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Assigned to THE KANSAI ELECTRIC POWER CO., INC. reassignment THE KANSAI ELECTRIC POWER CO., INC. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: DEGUCHI, HIROSHI, WATANABE, TSUNENORI, YAGI, YASUYUKI
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    • 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
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Definitions

  • This invention relates to a CO 2 desorption catalyst.
  • Chemical absorption methods are widely known as a method for removing and collecting CO 2 from combustion exhaust gas from thermal power stations and steel works (PTL 1).
  • CO 2 is brought into contact with an aqueous solution mainly containing alkanolamine (hereinafter also referred to as an “absorbing solution”) in an absorption tower, so as to allow the CO 2 to be absorbed into the absorbing solution.
  • the absorbing solution containing the absorbed CO 2 is transferred to a regeneration tower where the transferred solution is heated by heating vapor to cause the absorbed CO 2 to be desorbed (degassed).
  • the desorbed CO 2 is collected, and the absorbing solution from which the CO 2 has been desorbed is transferred back to the absorption tower to be reused.
  • the regeneration tower is filled with metal filler, such as thin stainless-steel plates or mesh balls obtained by wadding stainless steel mesh.
  • metal filler such as thin stainless-steel plates or mesh balls obtained by wadding stainless steel mesh.
  • the contact area of the absorbing solution and heating vapor is increased by allowing the absorbing solution to move through the surface of the filler. In this manner, desorption of CO 2 is promoted.
  • the metal filler heretofore used exerts limited activity on the promotion of desorption. Further, the filler heretofore used generally occupies a large volume of space, and the regeneration tower must therefore be made larger to achieve the desired desorption amount.
  • An object of the invention is to provide a CO 2 desorption catalyst having excellent CO 2 desorption activity.
  • the invention relates to a CO 2 desorption catalyst, a CO 2 desorption device having this catalyst, and a method for desorbing CO 2 by using this catalyst.
  • a CO 2 desorption catalyst comprising an inorganic powder or inorganic powder compact
  • the inorganic powder or inorganic powder compact having a BET specific surface area of 7 m 2 /g or more.
  • a CO 2 desorption device including:
  • a CO 2 absorption tower for absorbing and removing CO 2 from exhaust gas by using an absorbing solution
  • the regeneration tower contains the CO 2 desorption catalyst of any one of Items 1 to 6.
  • the method comprising the step of regenerating an absorbing solution containing absorbed CO 2 ,
  • the CO 2 desorption catalyst of the invention is described below in detail.
  • the invention also encompasses the use of an inorganic powder or inorganic powder compact having a BET specific surface area of 7 m 2 /g or more, as a catalyst for desorbing CO 2 from a CO 2 -containing solution.
  • the invention further encompasses a method for using an inorganic powder or inorganic powder compact having a BET specific surface area of 7 m 2 /g or more, as a catalyst for desorbing CO 2 from a CO 2 -containing solution.
  • the CO 2 desorption catalyst of the invention (hereinafter sometimes simply referred to as “the catalyst of the invention”) comprises an inorganic powder or inorganic powder compact having a BET specific surface area of 7 m 2 /g or more. Since the inorganic powder or inorganic powder compact has a BET specific surface area of 7 m 2 /g or more, the CO 2 desorption catalyst has an excellent activity to desorb CO 2 from a CO 2 -containing absorbing solution.
  • a BET specific surface area is a value obtained by dividing an inorganic powder surface area including the contribution of microscopic unevenness, pores, etc., by the mass of the inorganic powder.
  • a molecule whose adsorption area has been calculated is allowed to adsorb onto the surface of an inorganic powder at a liquid nitrogen temperature, and based on the adsorbed amount, the BET surface area can be calculated.
  • the upper limit of the BET specific surface area is preferably 500 m 2 /g or less.
  • the inorganic powder or inorganic powder compact has a BET specific surface area of more preferably 50 to 400 M 2 /g, and still more preferably 60 to 250 m 2 /g, in view of the catalytic effect and strength thereof.
  • the BET specific surface area of the inorganic powder or inorganic powder compact can be obtained by measuring the BET specific surface area of the inorganic powder.
  • the inorganic powder compact also has a BET specific surface area of 7 m 2 /g or more.
  • the BET specific surface area of the inorganic powder can be measured using a commercially available measuring instrument.
  • Examples of an instrument for measuring the BET specific surface area include the NOVA-4200e, produced by Quantachrome, and the like.
  • the components of the catalyst of the invention are not limited as long as they are inorganic components.
  • any inorganic components can be used, such as boron nitride (BN), metal oxides, metal nitrides, metal carbides, metal borides, metals (simple substances), intermetallic compounds, and clay minerals.
  • inorganic powders or inorganic powder compacts may be used singly or in a combination of two or more. When two or more types of inorganic powders or inorganic powder compacts are combined for use, the inorganic powders or inorganic powder compacts may be simply mixed, or may be in the form of a solid solution. For example, a solid solution of a plurality of metal oxides may be used as a composite metal oxide.
  • metal oxides include Al 2 O 3 , SiO 2 , TiO 2 , Cr 2 O 3 , MgO, Ga 2 O 3 , CuO, ZnO, and the like.
  • composite metal oxides include Al 2 O 3 —Ga 2 O 3 , CuO—ZnO, Al 2 O 3 —SiO 2 , and SiO 2 —TiO 2 ; and Sr- and Mg-doped lanthanum gallate (LSGM), and Co-doped LSGM (LSGMC), and the like.
  • metal nitrides examples include AlN, SiN, TiN, and the like.
  • metal carbides examples include SiC, TiC, MgC 2 , and the like.
  • metal borides examples include Co 2 B, Fe 2 B, Ni 2 B, PtB, RuB 2 , and the like.
  • metals include Pd, Fe, Co, Ni, Cu, Ru, Ag, Au, Pt, Cr, and the like.
  • intermetallic compounds examples include AlFe, CoPt 3 , CoFe, RuTi, and the like.
  • clay minerals examples include zeolites, talcs, sepiolites, kaolinites, montmorillonites, and the like.
  • the catalyst of the invention is preferably at least one member selected from the group consisting of BN, Ga 2 O 3 , Al 2 O 3 , Pd, Fe, and zeolites.
  • an inorganic powder or inorganic powder compact in which metal is supported on a component mentioned above may be used.
  • the metal supported on the component the same metals given above as examples of metals (Pd, Fe, Co, Ni, Cu, Ru, Ag, Au, Pt, Cr, and the like) may be used.
  • Pd, Fe, Co, Ni, Cu, Ru, Ag, Au, Pt, Cr, and the like the same metals given above as examples of metals (Pd, Fe, Co, Ni, Cu, Ru, Ag, Au, Pt, Cr, and the like) may be used.
  • Al 2 O 3 is used as the catalyst of the invention, at least one member selected from the group consisting of Pd, Fe, Co, Ag, and Ni (in particular, preferably at least one member selected from the group consisting of Pd, Fe, and Ag) is supported on the Al 2 O 3 . In this manner, the CO 2 desorption activity can be improved.
  • the loading of the supported metal is preferably 0.1 to 10 wt %, based on the entire catalyst of the invention.
  • the metal supported on the CO 2 desorption catalyst is in many cases in the so-called oxidation state immediately after the preparation.
  • a reduction treatment may be performed in advance so that the metal in the oxidation state is reduced to the metal state.
  • the catalytic activity of the CO 2 desorption catalyst is thereby further enhanced.
  • the reduction treatment may be performed, for example, by heat treatment in gas such as H 2 or H 2 —N 2 .
  • the heat treatment is performed at a temperature of preferably 200 to 400° C.
  • the duration of the heat treatment is preferably about 30 minutes to 5 hours.
  • the shape of the inorganic powder is not particularly limited. Examples include a spherical shape, a granular shape, an unfixed shape, a branched shape, a needle shape, a rod shape, a flat shape, and the like.
  • the size of the inorganic powder is not particularly limited.
  • the diameter is preferably about 0.01 to 10 ⁇ m.
  • a compact obtained by shaping the inorganic powder can also be used as the catalyst of the invention.
  • the shape of this compact is not particularly limited. Examples include a spherical shape, a columnar shape, a disk shape, a ring shape, a coating film shape, and the like.
  • the size of the inorganic powder compact is not particularly limited.
  • the diameter is preferably about 1 to 100 mm.
  • the method for producing the inorganic powder compact is not particularly limited.
  • an inorganic powder that can be used in this invention is shaped by a tableting machine, an extruder, or the like.
  • the film thickness is preferably about 0.1 to 0.5 mm.
  • the inorganic powder compact in the shape of a coating film may be produced, for example, in the following manner: organic substances, such as polyethylene glycol and/or ethyl cellulose, are mixed with an inorganic powder to produce a paste composition, the produced paste composition is applied to form a coating film and then calcined to decompose and remove the organic substances.
  • the calcination here is preferably performed at 200° C. or higher.
  • the coating film-shaped compact may be formed on the surface of a metal filler, on the inner surface (wall surface) of a regeneration tower described later, on a narrow tube of a vapor heater, on a plate surface, and the like.
  • the filler can be used to fill a regeneration tower as is conventionally done or can be placed in a CO 2 -containing absorbing solution reservoir at the bottom of a regeneration tower.
  • the coating film-shaped compact may also be formed on the inner surface of a structure in which many flat plates are stacked leaving gaps that serve as flow paths for an absorbing material, or on the inner surface of a honeycomb (monolith) structure with many parallel through-holes. It is also possible to form these structures themselves from the inorganic powder compact.
  • FIG. 1 is a schematic diagram roughly illustrating a CO 2 desorption device according to one embodiment of the invention.
  • FIG. 2 is a schematic diagram roughly illustrating the inside of the regeneration tower of FIG. 1 .
  • the CO 2 desorption device of the invention includes a CO 2 absorption tower for absorbing and removing CO 2 by using an absorbing solution (hereinafter simply referred to as “absorption tower”) and a regeneration tower for regenerating the absorbing solution containing absorbed CO 2 .
  • absorption tower for absorbing and removing CO 2 by using an absorbing solution
  • a regeneration tower for regenerating the absorbing solution containing absorbed CO 2 .
  • an exhaust gas cooling unit and an exhaust gas cooler for cooling exhaust gas, an exhaust gas blower for pressurizing exhaust gas, and the absorption tower filled with the CO 2 absorbing solution for absorbing and removing CO 2 from exhaust gas are arranged.
  • an absorbing solution containing absorbed CO 2 is referred to as a CO 2 -containing absorbing solution (or a CO 2 -containing solution), and an absorbing solution not containing absorbed CO 2 or an absorbing solution regenerated in the regeneration tower is referred to as an unabsorbed solution.
  • the CO 2 -containing absorbing solution and the unabsorbed solution are distinguished from each other.
  • the solution used for absorbing CO 2 is not particularly limited.
  • an aqueous solution of one or more alkanolamines such as monoethanolamine, diethanolamine, triethanolamine, methyldiethanolamine, diisopropanolamine, and diglycolamine, in water is suitably used.
  • alkanolamines may be used singly or in a combination of two or more.
  • the absorption tower and the regeneration tower are connected by a line for supplying the CO 2 -containing absorbing solution to the regeneration tower and a line for supplying the regenerated unabsorbed solution to the absorption tower. These two lines are provided with a heat exchanger for exchanging heat between the CO 2 -containing absorbing solution and the unabsorbed solution. Between the heat exchanger and the absorption tower in the line for supplying the unabsorbed solution to the absorption tower, a cooler for further cooling the unabsorbed solution is provided.
  • the regeneration tower is provided with a nozzle for downwardly spraying the CO 2 -containing absorbing solution supplied from the line.
  • a filled portion filled with the catalyst of the invention is provided below the nozzle.
  • a heater for heating the CO 2 -containing absorbing solution is provided at the bottom of the regeneration tower.
  • the heater and the regeneration tower are connected by a line so that the CO 2 -containing absorbing solution accumulated in the bottom of the tower is returned to the bottom of the tower after being heated by the heater.
  • a line is provided, in which a cooler for cooling CO 2 gas and a separator for separating moisture from CO 2 gas are sequentially arranged.
  • the separator is provided with a line for resupplying water separated by the separator to the top of the regeneration tower. This line is provided with a nozzle for downwardly spraying this reflux water.
  • CO 2 -containing exhaust gas discharged from a boiler is first transferred to the cooling unit to be cooled with cooling water.
  • the cooled exhaust gas is pressurized by the blower, and then transferred to the absorption tower.
  • exhaust gas is brought into countercurrent contact with an unabsorbed solution mainly containing alkanolamine, and as a result of the chemical reaction, CO 2 in the exhaust gas is absorbed into the unabsorbed solution.
  • the exhaust gas from which CO 2 was removed is discharged out of the system from the top of the tower.
  • the absorbing solution containing absorbed CO 2 is pressurized with a pump, heated by the heat exchanger, and supplied to the regeneration tower via the line from the bottom of the tower.
  • the CO 2 -containing absorbing solution is sprayed from the nozzle and flows down through the surface of the catalyst of the invention. At this time, the absorbing solution is heated by high-temperature water vapor coming upward from below (described later), causing partial desorption of CO 2 .
  • the use of the catalyst of the invention in this desorption reaction better promotes desorption, compared to known metal fillers.
  • the CO 2 -containing absorbing solution that has passed through the filled portion accumulates at the bottom of the tower.
  • the accumulated CO 2 -containing absorbing solution is extracted through the line and heated by the heater, causing partial desorption of CO 2 with the generation of high-temperature water vapor.
  • CO 2 desorption can be promoted with the application of the catalyst of the invention to the surface of the heater.
  • the desorbed CO 2 and the high-temperature water vapor move upward inside the tower while the not evaporated CO 2 -containing absorbing solution moves downward to be accumulated again.
  • the high-temperature water vapor that moves upward inside the tower heats the CO 2 -containing absorbing solution that is flowing down through the surface of the catalyst of the invention.
  • the CO 2 and water vapor discharged from the top of the regeneration tower are cooled by the cooler so that the moisture is condensed.
  • the condensed moisture is separated by the separator and returned to the regeneration tower.
  • the high-purity CO 2 free from moisture is discharged out of this CO 2 desorption device, so as to be effectively used for other purposes.
  • the inorganic powder or inorganic powder compact having a BET specific surface area of 7 m 2 /g or more can efficiently desorb CO 2 from a CO 2 -containing solution.
  • the catalyst of the invention comprises an inorganic powder or inorganic powder compact having a BET specific surface area of 7 m 2 /g or more, and thus has an excellent activity to desorb CO 2 from a CO 2 -containing absorbing solution. Therefore, the inorganic powder or inorganic powder compact can be suitably used as a catalyst for desorbing CO 2 from a CO 2 -containing solution.
  • FIG. 1 is a schematic diagram roughly illustrating a CO 2 desorption device according to one embodiment of the invention.
  • the arrow A in FIG. 1 indicates a movement of exhaust gas free from CO 2 towards a flue.
  • the arrow B in FIG. 1 indicates that CO 2 is separated from the absorbing solution.
  • the arrow C in FIG. 1 indicates that CO 2 is collected.
  • FIG. 2 is a schematic diagram roughly illustrating the inside of the regeneration tower of FIG. 1 .
  • the arrow D in FIG. 2 indicates that a CO 2 -containing absorbing solution is transferred from the absorption tower.
  • the arrow E in FIG. 2 indicates that the CO 2 -containing absorbing solution transferred from the absorption tower moves down through the surface of the CO 2 desorption catalyst of the invention while allowing desorption of CO 2 under the heat of high-temperature water vapor.
  • the arrows F in FIG. 2 indicate upward movement of the high-temperature water vapor and CO 2 , and downward movement of the not evaporated absorbing solution.
  • the arrow G in FIG. 2 indicates that the absorbing solution is partially extracted to be heated by the heater (high-temperature water vapor is generated when the absorbing solution is heated by the heater).
  • Example 1 15 mg of a BN powder (produced by Sigma-Aldrich) was pressed into a disk shape having a diameter of about 5 mm to produce the inorganic powder compact (catalyst) (metals unsupported) of Example 1. Based on the size of this compact, the external surface area was calculated to be 0.55 cm 2 .
  • this simple external surface area of the external surface of the compact is referred to as the “apparent surface area.”
  • ammonium carbonate (5-fold equivalent) (the “equivalent” as used herein is based on the total molar numbers of Ga ions and Al ions) was added at once to the aqueous solution above, and stirred for 1 hour with a stirrer. The produced precipitate was washed several times with water and collected, followed by calcination at 700° C.
  • Example 2 Inorganic powder compact of Example 2, 15 mg of the EN powder used in Example 1 and 15 mg of this Ga 2 O 3 —Al 2 O 3 were thoroughly mixed and pressed into a disk shape as in Example 1 to thereby produce the inorganic powder compact of Example 2.
  • Each metal salt powder was dissolved in water to produce each metal salt aqueous solution.
  • Each metal salt aqueous solution was impregnated onto an Al 2 O 3 powder (Sumitomo Chemical Co., Ltd., product name: AKP-G05) or onto an SiO 2 powder (Fuji Silysia Chemical Ltd., product name: CARiACT G-10), in such a manner that the weight of each metal after reduction treatment was 2 wt %, followed by drying in air at 100° C. for 6 hours and then calcination in air at 400° C. for 30 minutes to thereby obtain various inorganic powders (produced by an impregnation method).
  • Each metal salt powder used herein is shown below.
  • Pd salt a palladium nitrate n-hydrate (Pd(NO 3 ) 2 .nH 2 O) powder, produced by Kishida Chemical Co., Ltd.)
  • Fe salt an iron nitrate nonahydrate (Fe(NO 3 ) 3 .9H 2 O) powder, produced by Sigma-Aldrich
  • Co salt a cobalt nitrate hexahydrate (Co(NO 3 ) 2 .6H 2 O) powder, produced by Sigma-Aldrich
  • Ag salt a silver nitrate (AgNO 3 ) powder, produced by Sigma-Aldrich
  • Ni salt a nickel nitrate hexahydrate (Ni(NO 3 ) 2 .6H 2 O) powder, produced by Kanto Chemical Co., Inc.
  • Pt salt a diammine dinitro platinum (Pt(NH 3 ) 2 (NO 2 ) 2 ) powder, produced by Kojima Chemicals Co., Ltd.
  • Example 1 15 mg of the EN powder used in Example 1 and 15 mg of each of these various inorganic powders obtained by the impregnation method above were thoroughly mixed, and pressed into a disk shape as in Example 1.
  • a heat treatment was further performed at 300 to 400° C. in 1% H 2 —N 2 gas for 2 hours to thereby produce the inorganic powder compacts of Examples 3 to 14.
  • Solution A 0.15 mol of zinc nitrate, 0.015 mol of aluminum nitrate, 0.012 mol of gallium nitrate, and 0.003 mol of magnesium nitrate were dissolved in 600 mL of water, and kept warm at 60° C.
  • This acidic solution was used as Solution B.
  • 0.3 mol of copper nitrate was dissolved in 300 mL of water and kept warm at 60° C. This acidic solution was used as Solution C.
  • Solution B was uniformly added to Solution A dropwise over 30 minutes while being stirred to obtain a suspension.
  • a portion of Cr-based catalyst (Sud-Chemie Catalyst Co., Ltd., product name: ActiSorb 410RS) was chipped off to give 15 mg of a spherical inorganic powder, which was subjected to heat treatment at 300 to 400° C. in 1% H 2 —N 2 gas for 2 hours to produce the inorganic powder compact of Example 16.
  • Zeolite produced by Tosoh Corporation, product name: HSZ-640 HOD1A; BET specific surface area catalog value: 400 m 2 /g; diameter: about 1.5 mm; length: about 6 ⁇ m; extruded shape
  • metal filler 100 mg was prepared. Specifically, one metal filler (100 mg) was prepared by wadding a stainless steel mesh with a width of 6 mm and a length of 30 mm into a ball having a diameter of 6 mm.
  • metal filler (660 mg) was prepared. Specifically, seven fillers in total were prepared: six metal fillers (100 mg each) used in Comparative Example 1; and one metal filler (60 mg) obtained by wadding a stainless steel mesh with a width of 6 mm and a length of 18 mm into a ball having a diameter of 6 mm.
  • the apparent surface area was calculated based on the size and shape of each catalyst.
  • the apparent surface area of each metal filler of Comparative Examples 1 and 2 was calculated based on the diameter, length, and number of stainless steel wires used to form the mesh.
  • the BET specific surface area was obtained using the NOVA-4200e produced by Quantachrome. Tables 1 and 2 below show the measurement results.
  • aqueous monoethanolamine (MEA) solution 50 mL containing absorbed CO 2 (123.4 or 127.1 g-CO 2 /L) was placed into a volumetric flask, to which one of each of the catalysts obtained in Examples 1 to 16 and Comparative Example 1 was added.
  • the aqueous MEA solution was then heated. The heating was performed using a silicone oil bath. The temperature was increased at a rate of 1.4° C./min. After the temperature of the aqueous MEA solution reached 104° C. and was maintained at 104° C. for 30 minutes, a small amount of the aqueous MEA solution was sampled to measure the amount of residual CO 2 .
  • MEA monoethanolamine
  • the CO 2 desorption amount per apparent surface area was obtained by subtracting the amount of residual CO 2 after the temperature reached 104° C. and was maintained at this temperature for 30 minutes from the CO 2 amount before the test, and dividing the result by the apparent surface area. Table 1 shows the test results.
  • aqueous amine solution 150 mL containing absorbed CO 2 (151.6 g-CO 2 /L) was placed into a flask, to which one of each of the catalysts obtained in Examples 17 and 18 and Comparative Example 2 was added.
  • This absorbing solution was heated to 75° C. The heating was performed by immersing the flask in a silicone oil bath heated to 120° C.
  • the flow rate of desorbed CO 2 when the absorbing solution had a temperature of 75° C. was measured using a mass flow meter (Azbil Corporation, MQV0002). Table 2 shows the test results.

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Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20130174673A1 (en) * 2010-06-14 2013-07-11 Stichting Energiconderzoek Centrum Nederland Gas sampling for co2 assay
US20160115034A1 (en) * 2013-05-28 2016-04-28 The Kansai Electric Power Co., Inc. Co2 recovery apparatus and co2 recovery method
US9579602B2 (en) 2015-02-26 2017-02-28 University Of Wyoming Catalytic CO2 desorption for ethanolamine based CO2 capture technologies
CN113996331A (zh) * 2021-11-17 2022-02-01 国家电投集团远达环保催化剂有限公司 一种富co2胺溶液解吸整体式蜂窝催化剂及其制备方法
US11285431B2 (en) 2020-03-09 2022-03-29 Kabushiki Kaisha Toshiba Acid gas removal apparatus and method
CN114699883A (zh) * 2022-04-22 2022-07-05 浙江大学 催化剂协同外场强化二氧化碳低能耗解吸系统及方法
WO2023087066A1 (en) * 2021-11-19 2023-05-25 The University Of Melbourne Co2 capture and desorption using core-shell catalysts
CN116550117A (zh) * 2023-07-07 2023-08-08 山西大地生态环境技术研究院有限公司 一种二氧化碳的捕集及联产有机弱酸盐的装置及其方法

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110536736A (zh) * 2017-08-25 2019-12-03 韩国电力公社 酸性气体捕集装置
KR102096862B1 (ko) * 2018-01-18 2020-04-03 한국에너지기술연구원 전이금속 산화물 촉매를 이용한 산성가스 제거용 흡수제의 재생방법
JP7102376B2 (ja) * 2019-02-07 2022-07-19 株式会社東芝 酸性ガス除去装置及び酸性ガス除去方法

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20030136708A1 (en) * 2002-01-14 2003-07-24 Crane Robert A. Reforming catalyst and process

Family Cites Families (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3851041A (en) * 1966-02-01 1974-11-26 A Eickmeyer Method for removing acid gases from gaseous mixtures
JPH0779950B2 (ja) 1989-12-25 1995-08-30 三菱重工業株式会社 燃焼排ガス中のｃｏ▲下２▼の除去方法
JP3462604B2 (ja) * 1994-12-26 2003-11-05 日本パイオニクス株式会社 不活性ガスの精製方法および装置
JP3749391B2 (ja) * 1998-03-04 2006-02-22 トヨタ自動車株式会社 排ガス浄化用触媒及びその製造方法
JP2004244265A (ja) * 2003-02-13 2004-09-02 Hitachi Metals Ltd 窒化ほう素粉末の製造方法、および窒化ほう素粉末
MY136774A (en) * 2003-02-28 2008-11-28 Shell Int Research Method of improving the operation of a manufacturing process
JP2007314745A (ja) * 2006-04-27 2007-12-06 Tokyo Electric Power Co Inc:The エタノール発酵工程で発生した二酸化炭素から燃料を製造する方法
US20090155889A1 (en) * 2007-12-13 2009-06-18 Alstom Technology Ltd System and method for regeneration of an absorbent solution
US8414853B2 (en) * 2008-03-21 2013-04-09 Alstom Technology Ltd System and method for enhanced removal of CO2 from a mixed gas stream via use of a catalyst
JP5232686B2 (ja) * 2009-02-24 2013-07-10 大陽日酸株式会社 ガスの精製方法および精製装置
EP2552573B1 (de) * 2010-03-30 2019-10-02 University of Regina Katalytisches verfahren und vorrichtung zur abtrennung von säuregasen aus einem gasstrom
DE102011013318A1 (de) * 2011-03-07 2012-09-13 Hochschule Heilbronn Verfahren zur Regeneration von mit CO2 beladenen aminhaltigen Waschlösungen bei der Sauergaswäsche

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20030136708A1 (en) * 2002-01-14 2003-07-24 Crane Robert A. Reforming catalyst and process

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20130174673A1 (en) * 2010-06-14 2013-07-11 Stichting Energiconderzoek Centrum Nederland Gas sampling for co2 assay
US9080930B2 (en) * 2010-06-14 2015-07-14 Stichting Energieonderzoek Centrum Nederland Gas sampling for CO2 assay
US20160115034A1 (en) * 2013-05-28 2016-04-28 The Kansai Electric Power Co., Inc. Co2 recovery apparatus and co2 recovery method
US10000383B2 (en) * 2013-05-28 2018-06-19 The Kansai Electric Power Co., Inc. CO2 recovery apparatus and CO2 recovery method
US9579602B2 (en) 2015-02-26 2017-02-28 University Of Wyoming Catalytic CO2 desorption for ethanolamine based CO2 capture technologies
US11285431B2 (en) 2020-03-09 2022-03-29 Kabushiki Kaisha Toshiba Acid gas removal apparatus and method
CN113996331A (zh) * 2021-11-17 2022-02-01 国家电投集团远达环保催化剂有限公司 一种富co2胺溶液解吸整体式蜂窝催化剂及其制备方法
WO2023087066A1 (en) * 2021-11-19 2023-05-25 The University Of Melbourne Co2 capture and desorption using core-shell catalysts
CN114699883A (zh) * 2022-04-22 2022-07-05 浙江大学 催化剂协同外场强化二氧化碳低能耗解吸系统及方法
CN116550117A (zh) * 2023-07-07 2023-08-08 山西大地生态环境技术研究院有限公司 一种二氧化碳的捕集及联产有机弱酸盐的装置及其方法

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