WO2009110586A1 - Solution aqueuse et procédé d'absorption et de collecte de dioxyde de carbone dans le gaz de manière efficace - Google Patents

Solution aqueuse et procédé d'absorption et de collecte de dioxyde de carbone dans le gaz de manière efficace Download PDF

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WO2009110586A1
WO2009110586A1 PCT/JP2009/054260 JP2009054260W WO2009110586A1 WO 2009110586 A1 WO2009110586 A1 WO 2009110586A1 JP 2009054260 W JP2009054260 W JP 2009054260W WO 2009110586 A1 WO2009110586 A1 WO 2009110586A1
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carbon dioxide
aqueous solution
group
absorption
reaction
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PCT/JP2009/054260
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English (en)
Japanese (ja)
Inventor
弘道 岡部
フィロツ アラム チョウドリ
信吉 清水
和也 後藤
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財団法人地球環境産業技術研究機構
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Publication of WO2009110586A1 publication Critical patent/WO2009110586A1/fr

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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
    • B01D53/1493—Selection of liquid materials for use as absorbents
    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2

Definitions

  • the present invention absorbs carbon dioxide (CO 2 ) contained in a gas using an aqueous solution for carbon dioxide absorption and recovery, and subsequently desorbs carbon dioxide from the carbon dioxide absorption and recovery aqueous solution in which carbon dioxide is absorbed.
  • the present invention relates to an aqueous solution and a method for recovering separately.
  • Sources of carbon dioxide include coal, heavy oil, natural gas and other thermal power plants, factory boilers or kilns in cement plants, blast furnace blast furnaces that reduce iron oxide with coke, gasoline, heavy oil,
  • transportation equipment such as automobiles, ships, and aircraft that use light oil as fuel. Of these, those other than transportation equipment are fixed facilities, and are expected to be easy to implement measures to reduce carbon dioxide emissions.
  • examples of the alkanolamine include monoethanolamine (hereinafter sometimes referred to as MEA), diethanolamine (hereinafter sometimes referred to as DEA), triethanolamine (hereinafter sometimes referred to as TEA), methyldiethanolamine ( Hereinafter, it may be indicated as MDEA), diisopropanolamine (DIPA), diglycolamine (DGA), etc., but MEA is usually used.
  • MEA monoethanolamine
  • DEA diethanolamine
  • TEA triethanolamine
  • MDEA diisopropanolamine
  • DGA diglycolamine
  • the absorbing solution when an aqueous solution of these alkanolamines is used as the absorbing solution, the corrosiveness of the device material is high, and therefore it is necessary to use expensive corrosion-resistant steel for the device or to reduce the amine concentration in the absorbing solution. Further, since the absorbed carbon dioxide is difficult to desorb, it was necessary to desorb and recover by heating the desorption temperature to a high temperature of 120 ° C. In addition, the energy required for desorbing carbon dioxide from the absorbing solution is also high at 85 kJ / mol CO 2 . For example, in order to collect carbon dioxide at a power plant using this method, extra energy equivalent to 20% of the power generation amount is required. In an era where reduction of carbon dioxide generation, energy saving and resource saving are required, this high energy consumption is a major factor that impedes the practical use of carbon dioxide absorption and recovery equipment.
  • Patent Document 1 a so-called hindered amine aqueous solution having a steric hindrance such as an alkyl group around an amino group is brought into contact with combustion exhaust gas under atmospheric pressure, and carbon dioxide is absorbed in the aqueous solution.
  • a method for removing carbon dioxide is described.
  • Patent Document 1 examples of 2-methylaminoethanol (hereinafter sometimes referred to as MAE) and 2-ethylaminoethanol (hereinafter sometimes referred to as EAE) as hindered amines are described, and MAE and EAE are described. Is described as being preferred for carbon dioxide absorption.
  • MAE 2-methylaminoethanol
  • EAE 2-ethylaminoethanol
  • Patent Document 2 describes a carbon dioxide recovery method including a step of bringing an aqueous amine solution and a mixed gas into contact with each other to absorb carbon dioxide and a step of desorbing carbon dioxide from the aqueous solution.
  • Patent Document 2 discloses, as an aqueous amine solution, a compound containing a secondary amino group bonded to a secondary or tertiary carbon or a primary amino group bonded to a tertiary carbon, such as 2-methylpiperazine (hereinafter referred to as 2MPZ). 2) -amino-2-methyl-1-propanol (hereinafter sometimes referred to as AMP) and the like.
  • 2MPZ 2-methylpiperazine
  • AMP -amino-2-methyl-1-propanol
  • Patent Document 3 exemplifies a mixture of amine compounds having two or more primary, secondary, and tertiary nitrogens in the molecule as components of the absorbing solution.
  • Patent Document 4 proposes secondary cyclic amines substituted with a hydroxyl group or a hydroxyalkyl group as an amine component constituting the absorbing solution.
  • the substitution position is a carbon atom, Direct substitution compounds on the group are not included.
  • the removal of carbon dioxide from the exhaust gas that is, the absorption process of carbon dioxide into the aqueous solution and the desorption process of carbon dioxide from the aqueous solution that absorbed carbon dioxide are performed with high efficiency.
  • the recovery energy consumed for carbon dioxide recovery is required to be low, and it is important to develop an absorbing solution that can achieve this.
  • the present invention provides an aqueous solution and method for recovering high purity carbon dioxide with low energy consumption in order to efficiently absorb and recover carbon dioxide in gas.
  • an aqueous solution containing at least one tertiary amine compound that has a low heat of reaction between carbon dioxide and an amine and the use of the aqueous solution reduces the overall energy required for carbon dioxide absorption and recovery, resulting in high purity. It aims at providing the method of collect
  • the present inventors have found that the heat of reaction of the tertiary amine compound represented by the general formula [1] with carbon dioxide is lower than that of the conventional tertiary amine. I found.
  • the reaction heat, reaction rate, absorption amount, and desorption performance that characterize the performance of amines used for absorption are in a trade-off relationship.
  • amines with low reaction heat have absorption rates and absorption amounts.
  • the tertiary amine according to the present invention is surprisingly small in performance degradation and has unprecedented characteristics, and is excellent without being bound by the conventional trade-off relationship. It turns out that it has performance.
  • This reduction in the heat of reaction between carbon dioxide and the amine compound results in a reduction in the thermal energy applied during the desorption of carbon dioxide, enabling a reduction in the overall recovery energy in carbon dioxide recovery and solving the problems of the present invention. is there.
  • the aqueous solution containing the amine of the present invention as a part of the aqueous solution has an absorption rate and a desorption rate required for industrially and economically recovering carbon dioxide, and the overall recovery energy is smaller than before. It has been found that it has performance. As a result of further research based on this knowledge, the present invention has been completed.
  • Item 1 An aqueous solution for absorbing and recovering carbon dioxide from a gas containing carbon dioxide, wherein the aqueous solution contains at least one tertiary amine compound represented by the general formula [1].
  • n is selected from 1 or 2
  • R 1 represents an alkyl group or a hydroxyalkyl group
  • R 2 is a 2-position or a 3-position
  • R 2 represents hydrogen, an alkyl group or a hydroxyalkyl group
  • At least one of R 1 and R 2 represents a hydroxyalkyl group.
  • the tertiary amine compound of the general formula [1] is 1-methyl-2-piperidinemethanol, 1-methyl-2-piperidineethanol, 1-methyl-3-piperidinemethanol, 1-ethyl-2-piperidinemethanol, 1- From the group consisting of ethyl-3-piperidinemethanol, 1-ethyl-2-piperidineethanol, 1- (2-hydroxyethyl) pyrrolidine, 1- (2-hydroxyethyl) piperidine and 1- (3-hydroxypropyl) pyrrolidine 2.
  • Item 4. Item 4. The aqueous solution according to any one of Items 1 to 3, further comprising at least one selected from the group consisting of alkanolamines and piperazines.
  • Item 5. Item 5. The aqueous solution according to Item 4, wherein the alkanolamine is at least one selected from the group consisting of 2- (isopropylamino) ethanol, 2- (ethylamino) ethanol, and 2-amino-2-methyl-1-propanol.
  • Item 6. Item 6.
  • Item 7. (1) A step of bringing the aqueous solution into contact with the aqueous solution according to any one of Items 1 to 6 to absorb carbon dioxide, and (2) heating the aqueous solution having absorbed carbon dioxide obtained in (1) above. Desorbing and recovering carbon dioxide, Carbon dioxide absorption and recovery method comprising:
  • the method for separating and recovering carbon dioxide using the carbon dioxide absorbing liquid of the present invention has a high purity by absorbing and desorbing carbon dioxide in the gas with a lower energy consumption compared to known aqueous solutions for absorbing carbon dioxide. Of carbon dioxide can be recovered.
  • the decrease in absorption rate which has been accompanied by the use of a tertiary amine, is small, thereby reducing the overall recovery heat when recovering carbon dioxide and improving the equipment efficiency.
  • it is possible to reduce the recovered energy per unit weight of carbon dioxide which leads to the reduction of the recovery cost that is currently an issue.
  • This also makes it possible to reduce the size of the absorption tower, the desorption tower, and the devices associated therewith for recovering and desorbing carbon dioxide, thereby reducing energy loss and reducing the construction cost.
  • Aqueous solution for absorbing and recovering carbon dioxide is characterized by containing at least one tertiary amine compound represented by the general formula [1].
  • R 1 in the general formula [1] includes an alkyl group or a hydroxyalkyl group.
  • R 1 is an alkyl group, it preferably has 1 to 3 carbon atoms, and when it is a hydroxyalkyl group, it has a carbon number. Two or three are preferred. Specific examples include a methyl group, an ethyl group, a propyl group, an isopropyl group, a hydroxyethyl group, a hydroxypropyl group, and the like, and a methyl group, an ethyl group, a hydroxyethyl group, and a hydroxypropyl group are preferably selected.
  • R 2 in the general formula [1] includes hydrogen, an alkyl group, or a hydroxyalkyl group, and the alkyl group and the hydroxyalkyl group preferably have 1 to 3 carbon atoms.
  • Specific examples include hydrogen, methyl group, ethyl group, propyl group, hydroxymethyl group, hydroxyethyl group, hydroxypropyl group, etc., preferably hydrogen, methyl group, ethyl group, hydroxymethyl group, hydroxyethyl group And a hydroxypropyl group are selected.
  • At least one of R 1 and R 2 in the general formula [1] is a hydroxyalkyl group.
  • R 1 and R 2 when R 1 is a hydroxyalkyl group (preferably having 2 or 3 carbon atoms), R 2 is preferably hydrogen or an alkyl group (preferably having 1 to 3 carbon atoms) When 1 is an alkyl group (preferably having 1 to 3 carbon atoms), R 2 is preferably a combination of selecting a hydroxyalkyl group (preferably having 1 to 3 carbon atoms). For the substitution position of R 2 , substitution at the 2- and 3-position is selected.
  • R 1 is an alkyl group
  • 1-methyl-2-piperidinemethanol hereinafter also referred to as M2PPM
  • 1-methyl-2-piperidineethanol hereinafter also referred to as M2PPE
  • E2PPM 1-methyl-3-piperidinemethanol
  • E3PPM 1-ethyl-3-piperidinemethanol
  • R 2 is hydrogen
  • 1- (2 hydroxyethyl) -pyrrolidine hereinafter also referred to as HEPL
  • 1- (2 hydroxyethyl) -piperidine hereinafter also referred to as HEPP
  • 1 -(3-Hydroxypropyl) pyrrolidine and the like are selected.
  • tertiary amine compounds in the present application are known and can be obtained as reagents, but the production methods are described below for typical compounds.
  • R 1 is an alkyl group and R 2 is a hydroxyalkyl group, for example, 1-methyl-piperidinemethanol
  • R 2 is a hydroxyalkyl group
  • 1-methyl-piperidinemethanol it can be obtained by methylating a known 2-piperidinemethanol with methanol (European Journal of Inorganic Chemistry (3), 524-529; 2004).
  • reaction that absorbs carbon dioxide is an exothermic reaction
  • reaction that desorbs the opposite carbon dioxide is an endothermic reaction
  • reaction heat is used as meaning heat generated when absorbing carbon dioxide or heat absorbed from the outside when desorbing carbon dioxide.
  • the aforementioned MEA which is often used for carbon dioxide absorption, is a typical primary amine, and the reaction heat of carbon dioxide is about 85 kJ / mole CO 2 , but it is a typical example of a tertiary amine.
  • the heat of reaction is about 65 kJ / mol CO 2, which is a very low value.
  • the MDEA is as small as 0.2, and as described above, there is a trade-off relationship that a reduction in reaction heat leads to a decrease in reaction rate.
  • the tertiary amine according to the present invention has a characteristic that not only the heat of reaction is lower than that of the normal amine MDEA but also that the accompanying rate decrease is not observed at low heat of reaction. It shows different performance.
  • the absorption rate of MDEA (concentration of 3 ⁇ mol / L) is 0.8 ⁇ g / L / min
  • 1-methyl 2-piperidinemethanol according to the present invention is 2.7 ⁇ g / L / min at the same concentration. showed that. This is also considered to be a manifestation of the steric effect that the compound of the present invention shows in the course of the reaction.
  • the aqueous solution based on the present invention is prepared by mixing the tertiary amine represented by the general formula [1] with at least one selected from the group of alkanolamines and piperazines to adjust the performance of the entire aqueous solution. Also good.
  • the use of the tertiary amine compound represented by the general formula [1] can reduce the heat of reaction as an aqueous solution and improve the reaction rate, and the overall energy associated with the absorption and recovery of carbon dioxide. Consumption will be reduced and economic effects will be exerted.
  • Alkanolamines and piperazines are listed as constituents of the aqueous solution other than the tertiary amine compound represented by the general formula [1].
  • alkanolamines primary, secondary and tertiary amines are selected.
  • 2- (isopropylamino) ethanol hereinafter sometimes referred to as IPAE
  • 2- (ethylamino) ethanol 2-amino-2-methyl-1-propanol are preferably selected.
  • Piperazines include piperazine alone and those having an alkyl substitution in the cyclic part of piperazine, preferably piperazine (hereinafter sometimes referred to as PZ), 2-methylpiperazine, and 2,6- Dimethyl piperazine is selected. These function as a reaction activator upon absorption of carbon dioxide.
  • the content of the tertiary amine represented by the general formula [1] in the aqueous solution of the present invention is usually 5 to 45% by weight, preferably 8 to 40% by weight, more preferably 10 to 35% by weight.
  • the content of alkanolamines in the aqueous solution of the present invention is usually 5 to 50% by weight, preferably 10 to 45% by weight, more preferably 15 to 40% by weight.
  • the content of piperazine in the aqueous solution of the present invention is usually 1 to 15% by weight, preferably 2 to 10% by weight, more preferably 3 to 9% by weight.
  • an optimal composition is selected in consideration of the reaction heat, absorption amount, absorption rate, and desorption performance of each amine.
  • Increasing the composition ratio of the tertiary amine according to the present invention has the effect of reducing the heat of reaction of the entire aqueous solution, but practically performance design including absorption amount, desorption amount, etc. is necessary. Make adjustments and set the ratio of aqueous solution composition.
  • the content of the total amine compound in the aqueous solution according to the present invention is selected to be 20 to 65% by weight, preferably 30 to 60% by weight.
  • the higher the concentration of the amine component the greater the amount of carbon dioxide absorbed, the amount of desorption, and the rate of desorption per unit liquid volume, which is desirable in terms of energy consumption and the size and efficiency of plant equipment. If it exceeds 70%, the amount of carbon dioxide absorbed decreases because the effect of water as an activator decreases. Also, problems such as foaming or emulsification may occur when the amine component is not mixed with water uniformly, the viscosity increases, or when the pH of the liquid is lowered by absorbing carbon dioxide.
  • Carbon dioxide absorption step The carbon dioxide absorption and recovery method of the present invention includes a step of bringing a carbon dioxide-containing gas into contact with the carbon dioxide absorption and recovery aqueous solution to cause the aqueous solution to absorb carbon dioxide.
  • Gases containing carbon dioxide include, for example, thermal power plants fueled with heavy oil, natural gas, etc., kilns at manufacturing plants or kilns at cement plants, blast furnaces at ironworks that reduce iron oxide with coke, carbon in pig iron Exhaust gas from a converter in the same ironworks where the steel is burned to produce steel, and the carbon dioxide concentration in the gas is usually about 5 to 30% by volume, particularly about 10 to 25% by volume. In such a carbon dioxide concentration range, the effects of the present invention are suitably exhibited.
  • the gas containing carbon dioxide may contain gas such as water vapor, CO, H 2 S, and COS in addition to carbon dioxide.
  • the method for bringing a gas containing carbon dioxide into contact with the aqueous solution is not particularly limited.
  • a method of bubbling and absorbing a gas containing carbon dioxide in the aqueous solution a method of dropping the aqueous solution into a gas stream containing carbon dioxide (a spraying or spraying method), or a magnetic or metal mesh
  • the temperature when the aqueous solution of the present invention and a gas containing carbon dioxide are brought into contact with each other to absorb carbon dioxide is preferably in the range of 30 to 70 ° C.
  • the pressure during carbon dioxide absorption is usually about atmospheric pressure. Although it is possible to pressurize to a higher pressure in order to enhance the absorption performance, it is preferable to carry out under atmospheric pressure in order to suppress energy consumption required for compression.
  • Carbon dioxide desorption step The method of the present invention includes a step of heating and recovering the carbon dioxide-absorbed aqueous solution obtained in the carbon dioxide absorption step of (1) above.
  • a method of desorbing carbon dioxide from an aqueous solution that has absorbed carbon dioxide and recovering pure or high-concentration carbon dioxide a method of heating the aqueous solution and removing it by bubbling in a kettle as in distillation, a plate tower, a spray Examples include a method in which a liquid interface is widened and heated in a tower and a desorption tower containing a magnetic or metal mesh filler. Thereby, carbon dioxide is liberated and released from carbamate and bicarbonate.
  • the temperature at the time of desorption of carbon dioxide after absorption is exemplified by a range of 90 to 130 ° C.
  • the pressure during carbon dioxide desorption is usually about atmospheric pressure.
  • the pressure can be reduced to a lower pressure in order to enhance the desorption performance, it is preferably performed under atmospheric pressure in order to suppress energy consumption required for the pressure reduction.
  • the aqueous solution from which carbon dioxide has been desorbed is sent again to the carbon dioxide absorption process and recycled. During this time, the heat applied in the carbon dioxide desorption process is effectively used to increase the temperature of the aqueous solution by heat exchange with the aqueous solution in the circulation process, thereby reducing the energy of the entire recovery process.
  • the purity of carbon dioxide recovered in this way is usually extremely high, about 95 to 99.9% by volume.
  • This pure carbon dioxide or high-concentration carbon dioxide is used as a chemical, a raw material for synthesizing a high-molecular substance, or a cooling agent for freezing food.
  • % means “% by weight”.
  • M2PPM, MDEA, IPAE and PZ all use reagents from Tokyo Chemical Industry Co., Ltd., and E3PPM and 1-methyl-4-piperidinemethanol (M4PPM) According to the method described in the examples, the corresponding piperidine methanol was synthesized by ethylation or methylation.
  • the saturated carbon dioxide absorption is a value obtained by measuring the amount of inorganic carbon in the aqueous solution with a gas chromatographic total organic carbon meter, and the carbon dioxide absorption rate is carbon dioxide that is 1/2 of the saturated absorption. It is a value measured using an infrared carbon dioxide meter at the time of absorbing.
  • Example 1 A glass gas absorption bottle is immersed in a constant-temperature water bath set to a temperature of 40 ° C, and 50 ml of an aqueous solution containing 22% by weight of M2PPM, 25% by weight of IPAE and 3% by weight of PZ is placed in this bottle. Filled. A mixed gas containing 20% by volume of carbon dioxide and 80% by volume of N 2 at a pressure of 0.7 L / min is dispersed in a foam form through this glass filter with a coarseness of 100 ⁇ m and a diameter of 13 mm. And absorbed.
  • the carbon dioxide concentration in the gas at the aqueous solution inlet and the aqueous solution outlet is continuously measured with an infrared carbon dioxide meter (HORIBA GAS ANALYZER VA-3000). Was measured. If necessary, the amount of inorganic carbon in the aqueous solution was measured with a gas chromatographic total organic carbon meter (SHIMADZU-TOC-VCSH) and compared with the value calculated from an infrared carbon dioxide meter.
  • the saturated absorption amount was the amount at the time when the carbon dioxide concentration at the outlet of the aqueous solution coincided with the carbon dioxide concentration at the inlet.
  • the absorption rate was compared with the absorption rate at the time when 1/2 of the saturated absorption amount was absorbed.
  • the saturated absorption of carbon dioxide was 148 g / L, and the absorption rate at half absorption of the saturated absorption was 5.0 g / L / min.
  • the liquid temperature was raised to 70 ° C. in several minutes in the same gas stream, and the amount of carbon dioxide desorbed from the liquid was measured. As a result, it was 56 g / L.
  • the reaction heat measured by the method shown in Test Example 1 was 72 kJ / mol CO 2 .
  • Examples 2-6 Using the same apparatus as in Example 1, under the same conditions, heat of reaction, saturated absorption, absorption rate at the time of carbon dioxide absorption using an aqueous solution containing M2PPM, E3PPM, HEPP, HEPL, IPAE, and PZ at the concentrations shown in Table 1 And the amount of carbon dioxide desorption was measured. The obtained results are shown in Table 1.
  • [I] represents the composition of the tertiary amine according to the present invention
  • [II] represents the alkanolamine
  • [III] represents the piperazine composition name and weight%.
  • the tertiary amine according to the present invention has not only the heat of reaction but also the absorption reaction rate and the saturated absorption amount as compared with MDEA, which is a typical tertiary amine conventionally known. The specific high performance of these amines was confirmed.
  • the tertiary amine is an aqueous solution containing the tertiary amine as a component [I], an alkanolamine as a component [II], and a piperazine as a component [III].
  • Comparative Example 3 shows the absorption performance when MDEA, which has been conventionally used industrially as a tertiary amine, is included. If 72 kJ / mol CO 2 of Example 1, are now industrially of MEA used 85 kJ / molCO 2 much lower than, the reduction of energy recovered carbon dioxide is an object of the present invention is made .
  • the rate at the time of carbon dioxide absorption is higher than that of Comparative Example 3 in which Examples 4, 5, and 6 contain MDEA, which is a conventional representative tertiary amine, as a component of [I]. It was confirmed that this is a great advantage.
  • Test example 1 The reaction heat of carbon dioxide absorption was measured using a differential thermal reaction calorimeter (SETARAM, DRC) consisting of a glass reaction tank and a reference tank of the same shape installed in a thermostat. Each of the reaction tank and the reference tank is filled with 150 mL of the aqueous solution of Example 2, and 40 ° C. constant temperature water is circulated in the jacket portion of the tank. In this state, 100% carbon dioxide gas was blown into the reaction vessel aqueous solution at 200 ml / min, and the temperature rise of the liquid was continuously recorded with a temperature recorder until the carbon dioxide absorption was completed, and measured in advance. The reaction heat was calculated using the overall heat transfer coefficient between the reaction tank and the jacket water. Reaction heat resulting carbon dioxide absorption was 58 kJ / molCO 2.

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  • Analytical Chemistry (AREA)
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Abstract

L'invention porte sur une solution aqueuse pour absorber et collecter du dioxyde de carbone à partir d'un gaz contenant du dioxyde de carbone. La solution aqueuse est caractérisée en ce qu'elle contient au moins un composé amine tertiaire représenté par la formule générale (1) [dans laquelle n est un nombre choisi parmi 1 et 2; R1 représente un groupe alkyle ou un groupe hydroxyalkyle; et R2 est dans la position 2 ou 3 et représente un hydrogène, un groupe alkyle ou un groupe hydroxyalkyle, à la condition qu'au moins l'un parmi R1 et R2 représente un groupe hydroxyalkyle].
PCT/JP2009/054260 2008-03-07 2009-03-06 Solution aqueuse et procédé d'absorption et de collecte de dioxyde de carbone dans le gaz de manière efficace WO2009110586A1 (fr)

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JP2008058181A JP5557426B2 (ja) 2008-03-07 2008-03-07 ガス中の二酸化炭素を効率的に吸収及び回収する水溶液及び方法
JP2008-058181 2008-03-07

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US9409119B2 (en) 2010-12-22 2016-08-09 Kabushiki Kaisha Toshiba Acid gas absorbent, acid gas removal method, and acid gas removal device

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AU2010209661B2 (en) * 2009-02-02 2015-09-17 Basf Se Absorbent containing cyclic amines for removing acid gases
EP3653584A1 (fr) 2010-02-10 2020-05-20 Queen's University At Kingston Eau présentant une force ionique commutable
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JP5659084B2 (ja) * 2011-05-30 2015-01-28 株式会社東芝 酸性ガス吸収剤、酸性ガス除去方法および酸性ガス除去装置
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KR101861780B1 (ko) 2014-12-31 2018-05-28 서울대학교산학협력단 온도 응답성 물질을 이용한 이산화탄소 흡수 및 방출 조절 시스템 및 이에 따른 삼투압 조절, 이를 이용한 담수화 및 정수화 방법
JP6860147B2 (ja) * 2016-09-08 2021-04-14 株式会社Ihi 置換ピペラジン化合物及び酸性ガス用の吸収剤、吸収液

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