WO2014104789A1 - Absorbant de dioxyde de carbone ternaire et procédé d'absorption et procédé de séparation de dioxyde de carbone l'utilisant - Google Patents

Absorbant de dioxyde de carbone ternaire et procédé d'absorption et procédé de séparation de dioxyde de carbone l'utilisant Download PDF

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WO2014104789A1
WO2014104789A1 PCT/KR2013/012266 KR2013012266W WO2014104789A1 WO 2014104789 A1 WO2014104789 A1 WO 2014104789A1 KR 2013012266 W KR2013012266 W KR 2013012266W WO 2014104789 A1 WO2014104789 A1 WO 2014104789A1
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ethanol
carbon dioxide
butyl
methyl
butylamino
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Korean (ko)
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김훈식
최영섭
오지영
신승훈
김영진
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Kyung Hee University
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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
    • B01D53/1456—Removing acid components
    • B01D53/1475—Removing carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/22—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising organic material
    • 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
    • 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
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C215/00—Compounds containing amino and hydroxy groups bound to the same carbon skeleton
    • C07C215/02—Compounds containing amino and hydroxy groups bound to the same carbon skeleton having hydroxy groups and amino groups bound to acyclic carbon atoms of the same carbon skeleton
    • C07C215/04—Compounds containing amino and hydroxy groups bound to the same carbon skeleton having hydroxy groups and amino groups bound to acyclic carbon atoms of the same carbon skeleton the carbon skeleton being saturated
    • C07C215/06—Compounds containing amino and hydroxy groups bound to the same carbon skeleton having hydroxy groups and amino groups bound to acyclic carbon atoms of the same carbon skeleton the carbon skeleton being saturated and acyclic
    • C07C215/08—Compounds containing amino and hydroxy groups bound to the same carbon skeleton having hydroxy groups and amino groups bound to acyclic carbon atoms of the same carbon skeleton the carbon skeleton being saturated and acyclic with only one hydroxy group and one amino group bound to the carbon skeleton
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/20—Organic absorbents
    • B01D2252/204—Amines
    • B01D2252/20426—Secondary amines
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/20—Organic absorbents
    • B01D2252/204—Amines
    • B01D2252/20478—Alkanolamines
    • B01D2252/20484—Alkanolamines with one hydroxyl group
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/50—Combinations of absorbents
    • B01D2252/504—Mixtures of two or more absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/60—Additives
    • B01D2252/602—Activators, promoting agents, catalytic agents or enzymes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1425—Regeneration of liquid absorbents
    • 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 method in which three kinds of alkanolamines having different structures are used as a carbon dioxide absorbent, and an aqueous solution of ternary alkanolamine, each of which serves as a main absorbent, a regeneration accelerator, and a rate enhancer.
  • Secondary alkanolamine with steric hindrance and rate enhancer Linear secondary alkanolamine and regeneration accelerator without steric hindrance with low carbon dioxide absorption per mole but fast carbon dioxide absorption rate. Slow absorption but easy regeneration. It relates to a ternary carbon dioxide absorbent containing a class dialkanolamine, a carbon dioxide absorption method, and a separation method using the same.
  • absorption method adsorption method, membrane method, deep cooling method, etc. are used to separate carbon dioxide (CO 2 ) from the exhaust gas and natural gas of chemical plants, power plants, and large boilers.
  • absorption or adsorption methods are often used.
  • the absorption method or the adsorption method has been widely used because it can selectively separate only some of the gas absorbed or adsorbed to the adsorbent or the adsorbent, but has a disadvantage in that the absorbent and the adsorbent are chemically modified during the separation process and require periodic replacement. Therefore, when the solid adsorbent is used, it is advantageous to apply it only when the adsorbent replacement cycle is long due to the small chemical deformation of the adsorbent.
  • the absorbent method uses a liquid absorbent, so it is easy to replace the absorbent and has a larger absorption capacity than the adsorbent. There is an advantage that it is widely used for large-scale exhaust gas purification or gas separation, but there is a disadvantage that the absorbent is chemically or thermally modified.
  • amines such as monoethanolamine (MEA), N-methyldiethanolamine (MDEA), and diethanolamine (DEA) are most widely used. This is because when the alkanolamine absorber reacts with carbon dioxide to form a carbamate compound and heat is applied, the carbamate decomposes, carbon dioxide is removed and recovered, and the alkanolamine absorbent can be regenerated.
  • this process has some serious problems, especially in the generation and decomposition of irreversible amine compounds by impurities such as sulfur dioxide (SO 2 ), oxygen (O 2 ) and nax (NO x ) contained in combustion exhaust gases.
  • organic solvent absorbents are carbon dioxide It is more suitable for high pressure natural gas purification.
  • Ionic liquids which maintain the liquid phase at low temperatures, as absorbents.
  • Ionic liquids are polar salt compounds composed of organic cations and organic or inorganic anions and have properties of dissolving gas molecules such as carbon monoxide, carbon dioxide, sulfur dioxide (SO 2 ), and nitrous oxide (N 2 O).
  • the solubility of the gas absorbed by the ionic liquid depends on the degree of interaction between the gas and the ionic liquid.
  • the polarity, acidity and basicity of the ionic liquid are properly modified by modifying the cations and anions of the ionic liquid.
  • the solubility in a particular gas can be controlled to some extent.
  • these ionic liquid absorbents also have a significantly lower carbon dioxide absorption capacity than the amine absorbents at atmospheric pressure, which is economically problematic for use in the carbon dioxide capture process discharged from power plant combustion gases.
  • borate (BF 4 -) tetrafluoroborate ionic liquid having included a fluorine atom, such as an anion, hexafluorophosphate (PF 6 - -), sulfonimide ((CF 3 SO 2) 2 N) trifluoroacetate
  • PF 6 - - hexafluorophosphate
  • sulfonimide (CF 3 SO 2) 2 N) trifluoroacetate
  • PF 6 - - hexafluorophosphate
  • sulfonimide ((CF 3 SO 2) 2 N) trifluoroacetate has a relatively high solubility in acidic gases such as carbon dioxide and carbon disulfide, but the synthesis of these ionic liquids usually requires two or more complex manufacturing processes, and
  • alkanolamine-based chemical absorbers such as MEA have various disadvantages, particularly excessive renewable energy consumption.
  • attempts have been made to reduce the renewable energy of chemical absorbents by using alkanolamines having steric hindrances around the amine groups of alkanolamines as absorbents.
  • 1-propanol (AMP) When AMP reacts with carbon dioxide, it forms a bicarbonate compound ([AMPH] [HCO 3 ]) that is easier to recycle than carbamate. Therefore, it has 30% lower renewable energy than MEA. It has a disadvantage of less than%.
  • a method of using an alkali carbonate such as sodium carbonate or potassium carbonate as a carbon dioxide absorbent instead of a primary alkanolamine absorbent such as MEA is known, but has a disadvantage of slowing down carbon dioxide absorption.
  • WO 2004-089512 A1 reports that the addition of piperazine or its derivatives to potassium carbonate greatly increases the rate of carbon dioxide absorption of potassium carbonate. The formation problem remains a challenge to be solved.
  • the present invention has been made in order to solve the above problems, the object of the present invention is larger absorption capacity than the existing alkanolamine and alkali carbonate-based absorbents, the absorbent regeneration temperature is low and the regeneration efficiency is required to process In addition to significantly lowering the energy consumption, it is also to provide a ternary carbon dioxide absorbent, carbon dioxide absorption method and separation method using the same that can reduce the corrosion and solvent loss as the regeneration temperature is lowered.
  • the above object is a steric hindrance represented by the following general formula (3) represented by the following formula (1) to the secondary alkanolamine having a steric hindrance as a main absorbent, secondary alkanolamine without the steric hindrance represented by the following formula (2) as a speed increasing agent, Tertiary dialkanolamine with a regeneration accelerator,
  • R 1 is a C 3 -C 8 alkyl or cycloalkyl group
  • R 2 is a hydrogen or methyl group
  • R 3 is a C 1 -C 8 alkyl group, haloalkyl, or cycloalkyl group
  • R 4 is C 1 -C
  • the linear alkyl group of 6 and R 5 are achieved by a ternary carbon dioxide absorbent characterized by being a hydrogen, methyl or ethyl group.
  • the above object is achieved by a method for absorbing carbon dioxide, characterized in that the above-mentioned ternary carbon dioxide absorbent is dissolved in water to absorb carbon dioxide.
  • the total amount of alkanolamine of the ternary carbon dioxide absorbent is 20 to 100% by weight based on 100% by weight of water.
  • the amount of the main absorbent in the ternary carbon dioxide absorbent is characterized in that 20 to 60% by weight based on 100% by weight of water.
  • the weight increasing agent in the samsung system carbon dioxide absorbent is 15 to 80% by weight based on 100% by weight of the main absorbent and the weight of the regeneration accelerator is 10 to 50% by weight relative to 100% by weight of the main absorbent It is done.
  • the above object the first step of absorbing carbon dioxide from the gas mixture containing carbon dioxide using the above-described samseongdi carbon dioxide absorbent; And a second step of removing the carbon dioxide absorbed from the alkanolamine-based carbon dioxide absorbent.
  • the absorption temperature of the first step is characterized in that the 20 °C to 60 °C.
  • the absorption pressure of the first step is characterized in that the atmospheric pressure to 30 atm.
  • the stripping temperature of the second step is characterized in that 70 °C to 120 °C.
  • the stripping pressure in the second step is characterized in that the atmospheric pressure.
  • the carbon dioxide absorption capacity is high and the absorption rate is fast, but also the regeneration temperature of the absorbent is significantly lower than that of the conventional absorbent, so that the total energy consumption required for the absorption process can be greatly reduced, and the initial absorption capacity is repeated even after repeated absorption and removal.
  • Excellent carbon dioxide It can be used as a separation medium.
  • the present inventors earnestly studied the absorption and regeneration mechanisms to solve the problems of the conventional carbon dioxide absorbents, and found that the regeneration paths proceeded to more complicated mechanisms, not just the reverse of the absorption paths.
  • absorption was found to proceed through the carbamate or bicarbonate route depending on the amine type, but the regeneration process inevitably proceeds through a carbamate compound that is difficult to decompose.
  • the inventors of the primary and secondary amine absorbers and regeneration accelerators The addition of certain linear secondary amines to a mixture of phosphorus tertiary amine compounds led to the discovery that both the rate of absorption and the ease of regeneration could increase at the same time.
  • the ternary carbon dioxide absorbent according to the present invention is a steric hindrance secondary alkanolamine represented by the following formula (1) as a main absorbent, a secondary alkanolamine without steric hindrance represented by the following formula (2) as a speed increasing agent, It is characterized by using a tertiary dialkanolamine having a steric hindrance represented by a regeneration accelerator.
  • R 1 is a C 3 -C 8 alkyl or cycloalkyl group
  • R 2 is a hydrogen or methyl group
  • R 3 is a C 1 -C 8 alkyl group, haloalkyl, or cycloalkyl group
  • R 4 is a C 1 -C 6
  • the linear alkyl group and R 5 are hydrogen, methyl or ethyl group.
  • An alkyl group of C 3 to C 8 represented by R 1 of Formulas 1 and 3 refers to a branched alkyl group having 3 to 8 carbon atoms, for example, isopropyl, isobutyl, t-butyl, i-amyl, 2 -Amyl, t-amyl, 2-hexyl, 2-heptyl, 2-octyl and the like.
  • cycloalkyl groups represented by R 1 of Formulas 1 and 3 include, but are not limited to, cyclopentyl, cyclohexyl, 2-methylcyclohexyl, and the like.
  • alkyl group represented by R 2 of Formulas 1 and 3 is hydrogen or a methyl group.
  • alkyl group of C 1 ⁇ C 8 represented by R 3 in Formula 1 and 3, haloalkyl, or seek to the alkyl groups include methyl, ethyl, propyl, butyl, pentyl, cyclopentyl, cyclohexyl, phenyl, ethyl, chloroethyl, Bromoethyl, cyclohexyl, and the like, but are not limited thereto.
  • C 1 ⁇ C 6 alkyl group represented by R 4 of the formula (2) means a linear alkyl group consisting of 1 to 6 carbon atoms, for example methyl, ethyl, n-propyl, n-butyl, n-pentyl, n -Hexyl, and the like, but not limited thereto.
  • alkyl group represented by R 5 of Formula 2 includes, but is not limited to, hydrogen, methyl or ethyl groups.
  • secondary alkanolamines represented by the general formula (1) are, for example, 2- (isopropylamino) ethanol, 1-methyl-2- (isopropylamino) ethanol, 1,1-dimethyl-2- (Isopropylamino) ethanol, 1-chloromethyl-2- (isopropylamino) ethanol, 1-bromomethyl-2- (isopropylamino) ethanol, 1-ethyl-2- (isopropylamino) ethanol, 1 -Propyl-2- (isopropylamino) ethanol, 1-butyl-2- (isopropylamino) ethanol, 2- (t-butylamino) ethanol, 1-methyl-2- (t-butylamino) ethanol, 1 , 1-dimethyl-2- (t-butylamino) ethanol, 1-chloromethyl-2- (t-butylamino) ethanol, 1-bromomethyl-2- (t-butylamino) ethanol,
  • secondary alkanolamine C a rate enhancer represented by Formula 2
  • tertiary alkanolamine B which is a regeneration accelerator represented by Formula 3, is, for example, N-isopropyl diethanolamine, N-isopropyl di (2-methylethanolamine), N-isopropyl di (2, 2-dimethylethanolamine), N-isopropyl di (2-chloromethylethanolamine), N-isopropyl di (2-bromomethylethanolamine), N-isopropyl di (2-ethylethanolamine), N Isopropyl di (2-propylethanolamine), N-isopropyl di (2-butylethanolamine), Nt-butyl diethanolamine, Nt-butyl di (2-methylethanolamine), Nt-butyl di (2 , 2-dimethylethanolamine), Nt-butyl di (2-chloromethylethanolamine), Nt-butyl di (2-bromomethylethanolamine), Nt-butyl di (2-ethylethanolamine), Nt-butyl Di (2-propyl
  • the ternary carbon dioxide absorbent according to the present invention may be generally used by dissolving in water or an organic solvent, but it is more economical to use the aqueous solution. That is, the ternary carbon dioxide absorbent is most preferably dissolved in water to absorb carbon dioxide.
  • the total amount of alkanolamine of the ternary carbon dioxide absorbent is preferably 10 to 150% by weight, more preferably 20 to 100% by weight based on 100% by weight of water. This is because if the total amount of alkanolamine is less than 20% by weight, the carbon dioxide absorption capacity is significantly lowered. If the total amount of the alkanolamine is less than 20% by weight, the carbon dioxide absorption rate and the amount of absorption are insignificant while the viscosity of the absorbent liquid is too high.
  • the main absorbent represented by the formula (1) is 15 to 80% by weight, preferably 20 to 60% by weight with respect to 100 weight of water. If the amount of the main absorbent is less than 20% by weight, the advantages of the Samsung system absorbent decreases, and if it exceeds 60% by weight, the amount of carbon dioxide absorption per mole increases but the regeneration effect is reduced.
  • the rate increasing agent represented by the formula (2) is 5 to 150% by weight, more preferably 15 to 80% by weight relative to 100 weight of the main absorbent.
  • the amount of the rate enhancer is less than 15% by weight relative to the main absorbent, the increase in carbon dioxide absorption rate is insignificant, and when it exceeds 80% by weight, the increase in carbon dioxide absorption is insignificant but energy consumption is increased during regeneration.
  • the regeneration accelerator represented by Chemical Formula 3 is 5 to 80% by weight, more preferably 10 to 50% by weight based on 100 parts by weight of the main absorbent. If the amount of the regeneration accelerator is less than 10% by weight relative to the main absorbent, the absorbent regeneration effect is insignificant. If the regeneration accelerator exceeds 50% by weight, the regeneration effect of the carbon dioxide absorbent increases, but the absorption rate is significantly lowered.
  • the rate enhancer which is a secondary amine without steric hindrance among the components of the ternary carbon dioxide absorbent according to the present invention, has a high thermal stability and difficult to regenerate when reacted with carbon dioxide as shown in Scheme 1 below.
  • a regeneration accelerator when used in combination with a regeneration accelerator, it forms a bicarbonate that is easily regenerated. This is because the regeneration accelerator rapidly reacts with the carbamate formed from the rate enhancer and converts it into bicarbonate.
  • the absorbent of the present invention when used, the amount of carbamate produced is not large even after carbon dioxide absorption, so that the absorbent can be regenerated even at a low temperature, and thus, the energy of the overall absorption process can be saved, and the corrosion and absorbent loss problems derived from the high regeneration temperature can be reduced. Etc. can be greatly reduced.
  • the method for separating carbon dioxide from the gas mixture containing carbon dioxide by using the above-described samsung system carbon dioxide absorbent according to another aspect of the present invention, carbon dioxide in an aqueous solution in which the above-described samsung system carbon dioxide absorbent is dissolved in water And a second step of absorbing the carbon dioxide absorbed from the carbon dioxide absorbent.
  • Examples of the gas mixture containing carbon dioxide include exhaust gas and natural gas emitted from chemical plants, power plants, and large boilers.
  • a preferable temperature is in the range of 0 ° C to 80 ° C, more preferably in the range of 20 ° C to 60 ° C, and the preferred pressure is in the range of atmospheric pressure to 50 atmospheres, more preferably in the range of atmospheric pressure to 30 atmospheres. to be. If the absorption temperature exceeds 60 °C desorption proceeds at the same time because the amount of carbon dioxide absorption is reduced, if the absorption temperature is less than 20 °C because the need for additional refrigeration equipment to lower the temperature there is a problem in economic efficiency. .
  • the preferred temperature is in the range of 60 °C to 140 °C, more preferably in the range of 70 °C to 120 °C
  • the pressure is preferably at atmospheric pressure. This is because when the stripping temperature is less than 70 ° C., the stripping does not proceed, and when the stripping temperature is higher than 120 ° C., it becomes the same as the case where the absorbent of MEA is used.
  • the removal is difficult to proceed at a high pressure, because it is necessary to increase the vapor pressure of the water in order to maintain such a high pressure because the high temperature is required, there is a problem in economic efficiency. Therefore, stripping is desirable at normal pressure.
  • atmospheric pressure means 1 atmosphere.
  • FIG. 1 is a schematic diagram of an absorption and stripping experiment apparatus.
  • the device of FIG. 1 is a 60 mL stainless steel absorption reactor (R1) with a thermometer (T2) attached, a pressure transducer (P1) for high pressure (0 to 70 atmospheres), 75 mL with a thermometer (T1) attached. It consists of a carbon dioxide storage cylinder (S2) and the stirrer (1), it is installed in a thermostat to measure the carbon dioxide absorption capacity at a certain temperature. In addition, a carbon dioxide supply container (S1) and a pressure gauge (P2) were installed outside the thermostat.
  • valve V4 In the case of the stripping experiment, the valve V4 is closed, the temperature of the absorption reactor R1 is raised to 60 to 120 ° C, the valve V4, the valve V5 and the valve V6 are opened, and 20 mL / min of nitrogen is removed. The carbon dioxide was removed while feeding to the absorption reactor (R1) and the temperature was lowered to room temperature and the weight change before and after stripping was measured.
  • Example 2 Using the same ternary absorbent as in Example 1, the carbon dioxide absorption experiment was carried out in the same manner as in Example 1 while changing the absorption temperature while fixing the carbon dioxide pressure to 1 atm, and the results are shown in Table 2 below.
  • Example 3 Using the absorbent of Example 1, the carbon dioxide absorption experiment was carried out in the same manner as in Example 1 while changing the absorption pressure in a fixed temperature of 40 °C, the results are shown in Table 3 below.
  • Example 4 A carbon dioxide absorption experiment was conducted in the same manner as in Example 1 while using the absorbent of Example 1, with the temperature at 40 ° C. and the pressure fixed at 1 atm, changing the total amount of ternary absorbent to water. It is shown in Table 4 below. The larger the amount of amine, the smaller the amount of carbon dioxide absorption per mole of amine. It is thought that the higher the amount of amine, the greater the viscosity of the absorbing solution, resulting in restricted mass transfer.
  • Example 1 and the composition of the main absorbent A, the speed enhancer B, the regeneration accelerator C while varying the composition (weight%) using the ternary system absorbent used in Example 1, the absorption temperature is fixed to 40 °C, the absorption pressure to 1 atm.
  • Carbon dioxide absorption experiment was carried out in the same manner, and the results are shown in Table 5 below.
  • the absorption temperature was fixed at 40 ° C., the absorption pressure was set to 1 atm, and the carbon dioxide absorption experiment was carried out in the same manner as in Example 1 while changing the composition of the ternary absorbent used in Example 1, and then the absorption was measured at normal pressure. After lowering, stripping experiments were performed while flowing nitrogen at a rate of 15 mL / min. Absorption and stripping of the first carbon dioxide is completed, the absorption and stripping is repeated five times under the same conditions again, and compared to the initial carbon dioxide absorption and the fifth carbon dioxide absorption amount is shown in Table 6 below.

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Abstract

La présente invention concerne un absorbant de dioxyde de carbone ternaire et un procédé d'absorption et un procédé de séparation de dioxyde de carbone l'utilisant, l'absorbant comprenant des alcanolamines ternaires ayant différentes structures, à savoir, une alcanolamine secondaire qui est un absorbant primaire et a un encombrement stérique, une alcanolamine secondaire qui est un agent améliorant la vitesse et n'a pas d'encombrement stérique, et une dialcanolamine tertiaire qui est un promoteur de régénération et a un encombrement stérique. La présente invention a non seulement une excellente capacité d'absorption de dioxyde de carbone et une vitesse d'absorption de dioxyde de carbone rapide, mais a également une température de régénération d'absorbant remarquablement faible par comparaison avec un absorbant à base d'alcanolamine classique et donc peut réduire de façon significative la consommation d'énergie globale requise pour un procédé d'absorption, et peut également empêcher le dioxyde de carbone récupéré d'être contaminé par de l'humidité et de la vapeur d'absorbant, dû à la faible température de régénération.
PCT/KR2013/012266 2012-12-31 2013-12-27 Absorbant de dioxyde de carbone ternaire et procédé d'absorption et procédé de séparation de dioxyde de carbone l'utilisant Ceased WO2014104789A1 (fr)

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Cited By (3)

* Cited by examiner, † Cited by third party
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EP4703026A1 (fr) * 2024-08-26 2026-03-04 Københavns Universitet Procédé de capture de dioxyde de carbone

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EP3078409A1 (fr) * 2015-04-09 2016-10-12 Kabushiki Kaisha Toshiba Agent d'absorption de gaz acides, procédé et appareil d'élimination de gaz acides
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