CN114653166B - Carboxylic acid-containing composition, preparation method and application thereof - Google Patents
Carboxylic acid-containing composition, preparation method and application thereof Download PDFInfo
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- CN114653166B CN114653166B CN202011530227.9A CN202011530227A CN114653166B CN 114653166 B CN114653166 B CN 114653166B CN 202011530227 A CN202011530227 A CN 202011530227A CN 114653166 B CN114653166 B CN 114653166B
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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
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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
- B01D53/1418—Recovery of products
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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
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- 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
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- 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
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- 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
Abstract
The invention relates to the field of gas purification treatment, and discloses a composition containing carboxylic acid, a preparation method and application thereof. The composition comprises a hydrogen bond donor and a hydrogen bond acceptor, wherein the hydrogen bond donor is carboxylic acid, and the hydrogen bond acceptor is selected from quaternary ammonium salt and/or quaternary phosphonium salt. Through the synergistic effect of hydrogen bond donor and hydrogen bond acceptor, the composition has the advantages of low saturated vapor pressure, easy recovery, simple synthesis, low price, difficult degradation and environmental friendliness, and is resistant to CO 2 The composition has higher selectivity and dissolution capacity, can be recycled, saves cost and can be industrially applied.
Description
Technical Field
The invention relates to the field of gas purification treatment, in particular to a composition containing carboxylic acid, a preparation method and application thereof.
Background
In recent years, excessive dependence of humans on fossil fuels has led to a large amount of CO 2 Is produced and CO 2 Has a long life cycle, up to 200 years in the atmosphere, which causes a series of environmental problems such as global warming, greenhouse effect, etc. Carbon capture and sequestration technologies (Carbon Capture and Storage, CCS) are aimed at reducing atmospheric CO 2 Concentration, control of globalSpeed of warming.
Currently, CO 2 The trapping technology mainly comprises three types of trapping before combustion, trapping after combustion and oxygen-enriched combustion. The trapping after combustion mainly adopts methods of absorption, adsorption, membrane separation and the like to trap the flue gas (mainly N 2 、CO 2 、H 2 O and O 2 ) CO in (b) 2 And separating and recycling. Due to the advantages of simple operation, flexible running condition, lower energy consumption and the like, the method is used for capturing CO in the flue gas of the power plant at present 2 Is a preferred embodiment of (a). Monoethanolamine (MEA) is the most effective traditional solvent from post-combustion capture technologies, which have been successfully commercialized based on organoamine MEA, and are considered the most mature CO at present 2 Techniques. However, the method has the defects of high energy consumption, solvent corrosion equipment and the like. Therefore, a novel solvent with high selectivity and good dissolution capacity is studied for removing CO in an exhaust gas system 2 Is always a hotspot for the study of students at home and abroad.
CN109432990a discloses a desulfurization decarbonization absorbent comprising complex iron, an organic solvent and an organic base. The organic solvent comprises dimethyl sulfoxide or polyethylene glycol dimethyl ether or a mixture of the two, and the organic base can be dissolved in the organic solvent, and specifically comprises 1-butyl-3-methylimidazole hydroxide. The absorbent has high sulfur content and CO content 2 Has absorption effect. The organic solvent dimethyl sulfone or ethylene glycol dimethyl ether in the solvent has the defects of easy volatilization, high recovery capacity, large loss, environmental pollution and the like. The organic alkali is an ionic liquid solvent, so that the disadvantages of difficult synthesis, high price and the like exist.
CN103007690a discloses a kind of CO 2 The absorbent consists of organic amine and alkaline metal oxide, wherein the mass ratio of the organic amine to the alkaline metal oxide is 0.01-100:1. although the absorbent is capable of absorbing CO 2 However, the organic amine in the solvent has high running cost, and the organic amine is easy to degrade and cause secondary pollution, so that the organic amine needs to be subjected to stabilization treatment.
Disclosure of Invention
The invention aims to solve the technical problems of easy volatilization, high recovery capacity, large loss, difficult synthesis, high price, high energy consumption, easy degradation and instability of solvent corrosion equipment and organic amine and environmental pollution in the prior art, and provides a composition containing carboxylic acid, a preparation method and application thereof.
In order to achieve the above object, the present invention provides, in one aspect, a composition containing a carboxylic acid, the composition containing a hydrogen bond donor and a hydrogen bond acceptor, wherein the hydrogen bond donor is a carboxylic acid and the hydrogen bond acceptor is selected from quaternary ammonium salts and/or quaternary phosphonium salts.
The composition containing carboxylic acid provided by the invention contains a hydrogen bond donor, a hydrogen bond acceptor and a solvent, and has the advantages of low saturated vapor pressure, easiness in recovery, simplicity in synthesis, low price, difficulty in degradation and environmental friendliness through the synergistic effect of the hydrogen bond donor and the hydrogen bond acceptor, and is resistant to CO 2 The composition has higher selectivity and dissolution capacity, can be recycled, saves cost and can be industrially applied.
In a second aspect, the present invention provides a process for preparing the above composition, which comprises mixing a hydrogen bond donor, a hydrogen bond acceptor and optionally a solvent under stirring to obtain the composition.
In a third aspect, the invention provides a method for removing CO from exhaust gas 2 In (2) contacting the exhaust gas with an absorbent to obtain a catalyst containing CO 2 Wherein the absorbent is the composition or the composition prepared by the method.
The method for preparing the composition provided by the invention is simple and convenient, is easy to operate and is convenient for industrial application.
The invention provides a method for removing CO in waste gas 2 The composition is used for CO in exhaust gas 2 Is used for removing CO 2 The composition has higher selectivity and dissolution capacity, can be recycled, saves cost and can be industrially applied.
Drawings
FIG. 1 is a schematic diagram of the removal of CO from exhaust gas according to one embodiment of the invention 2 Is a systematic knot of (2)Schematic diagram.
Description of the reference numerals
101 first compressor, 102 second compressor, 103 third compressor, 201 first absorber, 202 second absorber, 301 first mixer, 302 second mixer, 303 third mixer, 401 first flash tank, 402 second flash tank, 500 pump, 600 cooler.
Detailed Description
The endpoints and any values of the ranges disclosed herein are not limited to the precise range or value, and are understood to encompass values approaching those ranges or values. For numerical ranges, one or more new numerical ranges may be found between the endpoints of each range, between the endpoint of each range and the individual point value, and between the individual point value, in combination with each other, and are to be considered as specifically disclosed herein.
In one aspect, the present invention provides a composition comprising a carboxylic acid, the composition comprising a hydrogen bond donor and a hydrogen bond acceptor, wherein the hydrogen bond donor is a carboxylic acid and the hydrogen bond acceptor is selected from quaternary ammonium salts and/or quaternary phosphonium salts.
In some embodiments of the invention, the molar ratio of the hydrogen bond donor to the hydrogen bond acceptor is from 0.2 to 5:1, preferably 0.5-2:1.
in some embodiments of the present invention, the carboxylic acid preferably has a carbon number of 2 to 20, more preferably at least one of a monobasic acid, a dibasic acid and a tribasic acid. Further preferably, the monoacid is selected from at least one of 3, 4-dihydroxycinnamic acid, 4-hydroxycinnamic acid, stearic acid, and linoleic acid. Further preferably, the dibasic acid is selected from at least one of itaconic acid, oxalic acid and glutamic acid. Further preferably, the triacid is selected from at least one of 1,3, 5-pentatricarboxylic acid, 1,2, 4-benzenetricarboxylic acid, and 1,3, 5-benzenetricarboxylic acid.
In some embodiments of the invention, preferably, the quaternary ammonium salt has the formula R 1 R 2 R 3 R 4 NX, wherein R 1 、R 2 、R 3 And R is 4 The same or different and are each independently selectedFrom an alkyl group, more preferably an alkyl group having 1 to 6 carbon atoms. X is halogen, more preferably selected from F, cl, br or I. Further preferably, the quaternary ammonium salt is selected from at least one of butyl trimethyl ammonium chloride, tetramethyl ammonium chloride and tetraethyl ammonium chloride.
In some embodiments of the invention, preferably, the quaternary phosphonium salt has the formula R 1 ’R 2 ’R 3 ’R 4 'PX', where R 1 ’、R 2 ’、R 3 ' and R 4 ' are the same or different and are each independently selected from alkyl groups or phenyl groups, more preferably alkyl groups or phenyl groups having 1 to 6 carbon atoms. X' is halogen, more preferably selected from F, cl, br or I; further preferably, the quaternary phosphonium salt is selected from at least one of methyltriphenylphosphine chloride, tetraphenylphosphine bromide, and tributyl methyl phosphine iodide.
In some embodiments of the invention, the composition may further contain a solvent, the molar ratio of the hydrogen bond donor to the solvent preferably being 1-5:1, more preferably 2-4:1.
in some embodiments of the invention, preferably, the solvent is an organic solvent or an inorganic solvent. More preferably, the organic solvent is a C1-C4 saturated monohydric alcohol, more preferably methanol and/or ethanol; the organic solvent is methanol and/or ethanol. More preferably, the inorganic solvent is water, and even more preferably deionized water.
In some embodiments of the invention, preferably, the composition is free of dimethyl sulfoxide, polyethylene glycol dimethyl ether, or an organic amine. In particular, organic amines refer to monoethanolamine and/or diethanolamine.
According to a preferred embodiment of the invention, the composition consists of only the above ingredients.
In a second aspect, the present invention provides a process for preparing the above composition, which comprises mixing a hydrogen bond donor, a hydrogen bond acceptor and optionally a solvent under stirring to obtain the composition.
In some embodiments of the invention, to further facilitate dissolution of the hydrogen bond donor and hydrogen bond acceptor, the temperature of the mixing is preferably 70-130 ℃, more preferably 80-120 ℃.
According to a preferred embodiment of the present invention, the hydrogen bond donor and the hydrogen bond acceptor are mixed under stirring (rotation speed 200-500 rpm) at a temperature preferably 70-130 ℃, more preferably 80-120 ℃, heating is stopped after forming a clear transparent liquid, and stirring is stopped when the temperature is lowered to room temperature (about 10-30 ℃) to obtain the composition.
In a third aspect, the invention provides a method for removing CO from exhaust gas 2 In (2) contacting the exhaust gas with an absorbent to obtain a catalyst containing CO 2 Wherein the absorbent is the composition or the composition prepared by the method.
In the invention, the waste gas is derived from waste gas of a thermal power plant.
In some embodiments of the invention, the ratio of the exhaust gas to the absorbent feed volume is preferably from 5 to 10:1.
in some embodiments of the invention, the feed volumetric flow of the exhaust gas is preferably in the range of 1000 to 5000m 3 /h。
In some embodiments of the invention, the temperature of the contacting is preferably 25-40 ℃. The pressure of the contact is preferably 0.5 to 1.5MPa, more preferably 0.8 to 1.2MPa.
In some embodiments of the invention, to achieve recycling of the absorbent, the method further comprises flashing the mixture to separate the absorbent and CO 2 。
In some embodiments of the invention, the flash vaporization is preferably at a temperature of 40-60 ℃. The pressure of the flash evaporation is preferably 0.05-0.1MPa.
According to a preferred embodiment of the invention, the CO in the exhaust gas 2 The removal of (2) is performed using the system shown in figure 1. Specifically, the method comprises the following steps: will contain CO 2 The waste gas of the first absorption tower 201 is compressed by the first compressor 101 and then enters the first absorption tower 201, the absorbent is sprayed from the top of the first absorption tower 201, and the CO in the first absorption tower 201 is contained 2 Is subjected to mass exchange with the absorbent in the first absorption column 201, wherein the absorbent containsCO 2 The feed volume ratio of the exhaust gas of (2) to the absorbent is 5-10:1, contain CO 2 The feed volume flow of the waste gas is 1000-5000m 3 /h, CO-containing 2 The temperature of the contact of the waste gas and the absorbent is 25-40 ℃, the contact pressure is 0.5-1.5MPa, and the preferable pressure is 0.8-1.2MPa, the purified gas is obtained and is discharged after being mixed with the gas discharged from the top of the second absorption tower 202 from the top of the first absorption tower 201 through the first mixer 301, and the CO is obtained at the bottom of the first absorption tower 201 2 Is fed into a first flash tank 401, is fed into a second absorption tower 202 through a second compressor 102 discharged from the top of the first flash tank 401, and contains CO in the second absorption tower 202 2 Is subjected to mass exchange with the absorbent in the first absorption tower 201, wherein the absorbent contains CO 2 The feed volume ratio of the exhaust gas of (2) to the absorbent is 5-10:1, contain CO 2 The feed volume flow of the waste gas is 1000-5000m 3 /h, CO-containing 2 The temperature of contact of the waste gas with the absorbent is 25-40 ℃, the contact pressure is 0.5-1.5MPa, preferably 0.8-1.2MPa, the flash evaporation temperature in the first flash tank 401 is 40-60 ℃, the flash evaporation pressure is 0.05-0.1MPa, the purified gas obtained in the second absorption tower 202 is discharged after passing through the first mixer 301, and the bottom of the first flash tank 401 contains CO 2 And CO-containing with the bottom of the second absorption column 202 2 The absorbent is mixed by the second mixer 302 and then enters a second flash tank 402, the flash evaporation temperature in the second flash tank 402 is 40-60 ℃, the flash evaporation pressure is 0.05-0.1MPa, and the gas obtained at the top of the second flash tank 402 is high-purity CO 2 And is discharged through the third compressor 103. The absorbent recovered at the bottom of the second flash tank 402 is cooled by the pump 500 and the cooler 600 and then enters the third mixer 303, and the absorbent in the third mixer 303 is respectively recycled as the absorbent entering the first absorption tower 201 and the second absorption tower 202, wherein the theoretical plate number of the first absorption tower is 5-10, and the theoretical plate number of the second absorption tower is 5-15.
In the present invention, the pressures refer to gauge pressure.
The present invention will be described in detail by examples. In the examples and comparative examples, the reagents used wereAnalytical pure reagents are commercially available. The waste gas is self-made and contains CO 2 The composition of the simulated flue gas is: CO 2 : 20.25% by volume; o (O) 2 : 8.27% by volume; h 2 O: 10.12% by volume; n (N) 2 : 59.01% by volume; CO: 2.35% by volume; trace sulfide and nitrogen oxides. Room temperature refers to 25 ℃.
Preparation example 1
The hydrogen bond donor linoleic acid and the hydrogen bond acceptor tetramethyl ammonium chloride are weighed, and a small amount of solvent deionized water is added to reduce the viscosity of the compound. Heating a mixture of linoleic acid and tetramethyl ammonium chloride at 80 ℃, stirring while heating, adding a small amount of deionized water, stopping heating after clear and transparent liquid is formed in a container, and stopping stirring when the temperature of the solution in the container is reduced to room temperature to obtain a composition, wherein the molar ratio of a hydrogen bond donor to a hydrogen bond acceptor to a solvent is 2:3:1.
preparation example 2
A composition was prepared according to the method of preparation example 1, except that the hydrogen bond donor was itaconic acid, the hydrogen bond acceptor was tetraethylammonium chloride, and the solvent was methanol, wherein the molar ratio of the hydrogen bond donor, the hydrogen bond acceptor, and the solvent was 4:2:1. the heating temperature was 100 ℃.
Preparation example 3
A composition was prepared according to the method of preparation example 1, except that the hydrogen bond donor was oxalic acid, the hydrogen bond acceptor was tetraphenylphosphine bromide, and the hydrogen bond acceptor was tetraethylammonium chloride, wherein the molar ratio of the hydrogen bond donor, the hydrogen bond acceptor and the solvent was 3:3:1. the heating temperature was 120 ℃.
Preparation example 4
A composition was prepared as in preparation example 1, except that the hydrogen bond donor was 1,3, 5-pentanetricarboxylic acid and the hydrogen bond acceptor was butyltrimethylammonium chloride. Wherein the molar ratio of hydrogen bond donor, hydrogen bond acceptor and solvent is 1:5:1.
preparation example 5
A composition was prepared as in preparation example 1, except that the hydrogen bond donor was 3, 4-dihydroxycinnamic acid and the hydrogen bond acceptor was tetraethylammonium chloride. Wherein the molar ratio of hydrogen bond donor, hydrogen bond acceptor and solvent is 5:1:1.
example 1
As in FIG. 1, will contain CO 2 Is compressed by the first compressor 101 and then enters the first absorption tower 201, the absorbent is sprayed from the top of the first absorption tower 201, wherein the absorbent is the composition obtained in the preparation example 1, and the absorbent contains CO in the first absorption tower 201 2 The waste gas and the absorbent are subjected to material exchange in the first absorption tower 201, the purified gas is obtained and is mixed with the gas discharged from the top of the second absorption tower 202 through the first mixer 301 from the top of the first absorption tower 201 and is discharged, and the CO-containing gas is obtained from the bottom of the first absorption tower 201 2 Is fed into a first flash tank 401, is fed into a second absorption tower 202 through a second compressor 102 discharged from the top of the first flash tank 401, and contains CO in the second absorption tower 202 2 The waste gas and the absorbent are subjected to substance exchange in the first absorption tower 201, the purified gas obtained in the second absorption tower 202 is discharged through the first mixer 301, and the bottom of the first flash tank 401 contains CO 2 And CO-containing with the bottom of the second absorption column 202 2 The absorbent is mixed by the second mixer 302 and then enters the second flash tank 402, and the gas obtained at the top of the second flash tank 402 is high-purity CO 2 And discharged through the third compressor 103, the absorbent recovered at the bottom of the second flash tank 402 is cooled by the pump 500 and the cooler 600 and then enters the third mixer 303, and the absorbent in the third mixer 303 is respectively recycled as the absorbent entering the first absorption tower 201 and the second absorption tower 202 respectively, and the purified gas is collected. The specific operating parameters of each device are shown in table 1:
TABLE 1
Example 2
CO in the exhaust gas was carried out as in example 1 2 Except that the absorbent was the composition obtained in preparation 2, and the specific operating parameters of each device are shown in table 2:
TABLE 2
Example 3
CO in the exhaust gas was carried out as in example 1 2 Except that the absorbent was the composition obtained in preparation 3, and the specific operating parameters of each device are shown in table 3:
TABLE 3 Table 3
Example 4
CO in the exhaust gas was carried out as in example 1 2 Except that the absorbent was the composition obtained in preparation example 4.
Example 5
CO in the exhaust gas was carried out as in example 1 2 Except that the absorbent was the composition obtained in preparation 5.
Example 6
The separation of the azeotropic mixture was performed as in example 1, except that the molar ratio of hydrogen bond donor, hydrogen bond acceptor and solvent was 6:1:1.
comparative example 1
CO in the exhaust gas was carried out as in example 1 2 Except that the absorbent used was a composition of urea and choline chloride in a molar ratio of 1:2.
Comparative example 2
The separation of the azeotropic mixture was performed as in example 1, except that the hydrogen bond donor used was ethylene glycol.
Comparative example 3
The separation of the azeotropic mixture was performed as in example 1, except that the hydrogen bond acceptor used was betaine.
Test example 1
CO in the purified gases obtained in examples and comparative examples 2 The content of (2) was measured using a test instrument of refinery gas system, agilent 7890B, 4-valve 6-column system, hayesep-Q molecular sieve column as column type, column box temperature using temperature programming, initial temperature 60 ℃, constant temperature 1min, post temperature programming, temperature rate 20 ℃/min, temperature rising to 150 ℃ and retention 5min, inspector TCD, temperature 250 ℃, injector temperature 70 ℃, and the obtained test results are shown in Table 4.
CO 2 Removal rate/% = (CO in the exhaust gas before purification) 2 Content of (2) purified gas CO 2 Content of (2)/CO in the exhaust gas before purification 2 The content of (2) is multiplied by 100%.
TABLE 4 Table 4
As can be seen from Table 4, the compositions obtained in examples 1 to 6 and comparative examples 1 to 3 were used for removing CO from exhaust gas 2 CO in the purified gas of examples 1 to 6 2 Is low in CO 2 The removal rate of CO in the purified gas of comparative examples 1 to 3 was 99.9 vol% or more 2 Higher content of CO 2 The removal rate of (C) was lower than 99.9 vol%, indicating that CO was contained in the exhaust gas by using the composition of the present invention 2 Has better effect and is beneficial to industrialized application.
The preferred embodiments of the present invention have been described in detail above, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, a number of simple variants of the technical solution of the invention are possible, including combinations of the individual technical features in any other suitable way, which simple variants and combinations should likewise be regarded as being disclosed by the invention, all falling within the scope of protection of the invention.
Claims (13)
1. CO in waste gas is got rid of 2 Is characterized in that the exhaust gas is contacted with an absorbent to obtain a catalyst containing CO 2 Wherein the absorbent contains a hydrogen bond donor and a hydrogen bond acceptor, wherein the hydrogen bond donor is a carboxylic acid and the hydrogen bond acceptor is selected from quaternary ammonium salts and/or quaternary phosphonium salts;
wherein the carboxylic acid is at least one of linoleic acid, itaconic acid and oxalic acid, the quaternary ammonium salt is at least one of tetramethyl ammonium chloride and tetraethyl ammonium chloride, and the quaternary phosphonium salt is tetraphenyl phosphine bromide;
the absorbent further comprises a solvent, the molar ratio of the hydrogen bond donor to the solvent being 2-4:1, the solvent is used for reducing the viscosity of a hydrogen bond donor and a hydrogen bond acceptor;
wherein the feeding volume ratio of the waste gas to the absorbent is 5-10:1, a step of;
wherein the feeding volume flow of the waste gas is 1000-5000m 3 /h。
2. The process of claim 1, wherein the contacting is at a temperature of 25-40 ℃ and a pressure of 0.5-1.5MPa.
3. The method of claim 2, wherein the contacting is at a pressure of 0.8-1.2MPa.
4. A process according to any one of claims 1 to 3, wherein the process further comprises flashing the mixture to separate the absorbent and CO 2 。
5. The process of claim 4, wherein the flash evaporation is at a temperature of 40-60 ℃ and a pressure of 0.05-0.1MPa.
6. The method of claim 1, wherein the molar ratio of the hydrogen bond donor to the hydrogen bond acceptor is from 0.2 to 5:1.
7. the method of claim 1, wherein the molar ratio of the hydrogen bond donor to the hydrogen bond acceptor is from 0.5 to 2:1.
8. the method of claim 1, wherein the solvent is an organic solvent or an inorganic solvent.
9. The method of claim 8, wherein the organic solvent is a C1-C4 saturated monohydric alcohol.
10. The method of claim 9, wherein the organic solvent is methanol and/or ethanol.
11. The method of claim 8, wherein the inorganic solvent is water.
12. The method of claim 8, wherein the inorganic solvent is deionized water.
13. The method of claim 1, wherein the absorbent is free of dimethyl sulfoxide, polyethylene glycol dimethyl ether, or an organic amine.
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