CN115999325A - Ionic liquid phase change absorbent and application thereof - Google Patents
Ionic liquid phase change absorbent and application thereof Download PDFInfo
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Abstract
The invention provides an ionic liquid phase change absorbent and application thereof, wherein the phase change absorbent is a quaternary phase change absorbent composed of primary amine and/or secondary amine, a phase splitting agent, ionic liquid and water. The phase-change absorbent provides a new thought of high efficiency, low energy consumption and low solvent loss for the phase-change absorption process by combining the ionic liquid with the organic amine phase-change system, and solves the problem of CO absorption by a chemical absorption method 2 The problems of high energy consumption and large solvent loss of the absorbent are solved, and the carbon trapping process is realized more effectively.
Description
Technical Field
The invention belongs to the technical field of carbon dioxide trapping, and relates to an absorbent, in particular to an ionic liquid phase change absorbent and application thereof.
Background
Excessive emissions of carbon dioxide are a significant cause of global warming. Carbon Capture and Sequestration (CCS) technology is considered to be implementing CO 2 One of the most effective means of control and abatement. Up to now, the organic amine-based chemisorption method is the most mature and most widely used CO 2 Trapping technology. The chemical absorption method has the advantages of large flue gas treatment capacity and good absorption performance, and is widely applied to industry. However, in the conventional absorption method, monoethanolamine (MEA), methyldiethanolamine (MDEA) and the like are generally used as main absorbents, and high regeneration energy consumption during solvent regeneration becomes a key problem of the method. In addition, due to the high volatility of the amine, the amine absorbent is easy to thermally degrade and evaporate and run off in the recycling process, so that the absorption effect of the absorbent is affected, and particularly when the temperature is high, unavoidable solvent loss is caused in the absorption process and the regeneration process. Therefore, low-energy consumption and low-loss CO is developed 2 The trapping technique is of paramount importance.
The phase change absorbent has excellent application prospect in the aspect of carbon capture. The novel absorbent absorbs CO 2 Or two liquid phases are formed after temperature change, wherein one phase is enriched with CO 2 . Therefore, only the liquid phase is heated during regeneration, thereby reducing the desorption amount and greatly reducing the regeneration heat load. Current phase change absorbers mostly include primary and secondary amines, commonly used as CO 2 Absorbed chemical solvents, and other solvents used for phase separation, such as alcohols, sulfolanes, lipophilic amines, tertiary amines, ethers, and the like. The mixed amine phase change absorbent composed of primary/secondary amine and tertiary amine shows good absorption effect and phase separation characteristic, and the energy consumption level is relatively low, but it is still important to further reduce the energy consumption level.
Disclosure of Invention
In order to solve the technical problems in the prior art, the application provides an ionic liquid phase-change absorbent and application thereof, and the phase-change absorbent combines an ionic liquid phase-change system with an organic amine phase-change system, so that a new thought with high efficiency, low energy consumption and low solvent loss is provided for a phase-change absorption process, and CO absorption by a chemical absorption method is solved 2 The problems of high energy consumption and large solvent loss of the absorbent are solved, and the carbon trapping process is realized more effectively.
In order to achieve the technical effects, the invention provides the following technical scheme:
the invention aims to provide an ionic liquid phase change absorbent, which is a quaternary phase change absorbent composed of primary amine and/or secondary amine, a phase splitting agent, ionic liquid and water.
In the invention, the ionic liquid is combined with the organic amine phase-change system, and the physical trapping effect of the ionic liquid and the chemical effect of the organic amine are utilized to realize dual activation, thereby improving the absorption effect. The characteristics of low specific heat capacity of the ionic liquid are utilized to reduce latent heat, the characteristics of low vapor pressure are utilized to realize low-water regeneration, and the latent heat is further reduced, so that the regeneration energy consumption of the phase change absorbent is reduced on the basis of the phase change absorbent, the industrial application range of the phase change absorbent is improved, and a new idea of high efficiency and low energy consumption is provided for carbon capture.
As a preferred embodiment of the present invention, the total concentration of the amino groups in the phase-change absorbent is 4 to 8mol/L, such as 4mol/L, 4.5mol/L, 5mol/L, 5.5mol/L, 6mol/L, 6.5mol/L, 7mol/L, 7.5mol/L, or 8mol/L, etc., but not limited to the recited values, and other non-recited values within the range of the values are equally applicable.
As a preferable technical scheme of the invention, the ionic liquid comprises imidazole ionic liquid.
Preferably, the imidazole ionic liquid comprises any one or a combination of at least two of 1-butyl-3-methylimidazole hexafluorophosphate, 1-butyl-3-methylimidazole tetrafluoroborate, 1-butyl-3-methylimidazole bromide, 1-butyl-3-methylimidazole hexafluorophosphate, 1-ethyl-3-methylimidazole hexafluorophosphate or 1-ethyl-3-methylimidazole bistrifluoromethylsulfonylimine salt.
Preferably, the mass fraction of the ionic liquid in the phase-change absorbent is 5-30%, such as 5%, 10%, 15%, 20%, 25% or 30%, etc., but is not limited to the recited values, and other non-recited values within the range of values are equally applicable.
As a preferred embodiment of the present invention, the primary and/or secondary amine comprises any one or a combination of at least two of hydroxyethyl ethylenediamine, N-methyl-1, 3-propanediamine, 1, 4-butanediamine, triethylene tetramine or diethylene triamine, and typical but non-limiting examples of such combinations are: a combination of hydroxyethyl ethylenediamine and N-methyl-1, 3-propanediamine, a combination of N-methyl-1, 3-propanediamine and 1, 4-butanediamine, a combination of 1, 4-butanediamine and triethylene tetramine, a combination of triethylene tetramine and diethylenetriamine, a combination of diethylenetriamine and hydroxyethyl ethylenediamine, or a combination of hydroxyethyl ethylenediamine, N-methyl-1, 3-propanediamine and 1, 4-butanediamine, and the like.
Preferably, the mass fraction of the primary amine and/or secondary amine in the phase change absorbent is 10-30%, such as 10%, 12%, 15%, 18%, 20%, 22%, 25%, 28% or 30%, etc., but is not limited to the recited values, and other non-recited values within this range are equally applicable.
As a preferred embodiment of the present invention, the phase-splitting agent comprises a tertiary amine.
Preferably, the tertiary amine comprises any one or a combination of at least two of N, N-diethylaminoethanol, N-dimethylcyclohexylamine, or pentamethyldiethyltriamine, typical but non-limiting examples of such combinations are: a combination of N, N-diethylaminoethanol and N, N-dimethylcyclohexylamine, a combination of N, N-dimethylcyclohexylamine and pentamethyldiethyltriamine, a combination of pentamethyldiethyltriamine and N, N-diethylaminoethanol, or a combination of N, N-diethylaminoethanol, N-dimethylcyclohexylamine and pentamethyldiethyltriamine, or the like.
Preferably, the mass fraction of the phase-splitting agent in the phase-change absorbent is 40-60%, such as 40%, 42%, 45%, 48%, 50%, 52%, 55%, 58% or 60%, etc., but is not limited to the recited values, and other non-recited values within the range of values are equally applicable.
The second object of the present invention is to provide an application of the ionic liquid phase-change absorbent, which is characterized in that the ionic liquid phase-change absorbent is used for absorbing CO in mixed gas 2 。
As a preferable technical scheme of the invention, the ionic liquid phase change absorbent is used for absorbing CO in mixed gas 2 The method of (1) comprises the following steps:
(1) Counter-current absorption of CO in the mixed gas using the ionic liquid phase change absorber 2 Obtaining an absorbed liquid;
(2) Standing and layering the absorbed liquid in the step (1) to obtain a rich liquid and a first lean liquid;
(3) Desorbing the rich liquid in the step (2) to obtain a second lean liquid, and mixing the second lean liquid with the first lean liquid to be used for absorbing CO in the mixed gas in the step (1) 2 。
In the invention, the absorption can be carried out in an absorption tower, and the ionic liquid phase change absorbent is in countercurrent contact with the mixed gas in a spraying mode; the stationary separation may be performed in a separation tank, the desorption may be performed in a desorption column, and the first lean solution and the second lean solution may be combined in a mixing tank.
In the invention, the ionic liquidQuaternary system of phase-change absorbent with phase-splitting property for absorbing CO 2 The solution state is homogeneous before absorbing a certain amount of CO 2 The post absorbent is divided into an upper phase and a lower phase, and CO 2 Is concentrated in one phase. Rich liquid phase CO after phase separation 2 The load is 1.5-4 mol/L, and the lean liquid phase CO 2 The load is 0 to 0.6mol/L.
As a preferable technical scheme of the invention, CO in the mixed gas in the step (1) 2 The volume concentration of (a) is 5 to 30%, such as 5%, 10%, 15%, 20%, 25% or 30%, etc., but is not limited to the recited values, and other values not recited in the range of values are equally applicable.
Preferably, the absorption in step (1) is carried out at normal pressure at a temperature of 20 to 60 ℃, such as 20 ℃, 25 ℃, 30 ℃, 35 ℃, 40 ℃, 45 ℃, 50 ℃, 55 ℃, or 60 ℃, etc., but is not limited to the recited values, and other non-recited values within the range of values are equally applicable.
As a preferable technical scheme of the invention, the rich liquid in the step (3) is subjected to heat exchange with the second lean liquid obtained by desorption.
In the present invention, the heat exchange may be performed in a heat exchanger.
Preferably, the absorption in step (1) is carried out at normal pressure at a temperature of 80 to 120 ℃, such as 80 ℃, 85 ℃, 90 ℃, 95 ℃, 100 ℃, 105 ℃, 110 ℃, 115 ℃, or 120 ℃, etc., but is not limited to the recited values, and other non-recited values within the range are equally applicable.
In the present invention, the normal pressure means that the absorption or desorption is performed under the natural pressure of the environment where it is located, that is, the operation of pressurizing or depressurizing is not performed in the absorption or desorption.
As the preferable technical scheme of the invention, the energy consumption for regenerating the ionic liquid phase-change absorbent is 2.05-2.50 GJ/t CO 2 For example 2.05GJ/t CO 2 、2.10GJ/t CO 2 、2.15GJ/t CO 2 、2.20GJ/t CO 2 、2.25GJ/t CO 2 、2.30GJ/t CO 2 、2.35GJ/t CO 2 、2.40GJ/t CO 2 、2.45GJ/t CO 2 Or 2.50GJ/t CO 2 And the like, but are not limited to the recited values, and other non-recited values within the range of values are equally applicable.
In the invention, the energy consumption of regenerating the ionic liquid phase change absorbent is calculated through sensible heat, latent heat and reaction heat, and the calculation method is a common method in the field and is not repeated here.
Preferably, the loss of the ionic liquid phase change absorbent is 1.0-2.2 kg/t CO 2 Such as 1.0kg/tCO 2 、1.1kg/t CO 2 、1.2kg/t CO 2 、1.3kg/t CO 2 、1.4kg/t CO 2 、1.5kg/t CO 2 、1.6kg/tCO 2 、1.7kg/t CO 2 、1.8kg/t CO 2 、1.9kg/t CO 2 、2.0kg/t CO 2 、2.1kg/t CO 2 Or 2.2kg/t CO 2 And the like, but are not limited to the recited values, and other non-recited values within the range of values are equally applicable.
In the invention, the liquid treated by the ionic liquid phase change absorbent enters a cooler for condensation, then enters a gas-liquid separation tank for separation to remove water, and the non-condensable gas enters a subsequent unit, so that the separated liquid can be recycled.
Compared with the prior art, the invention has at least the following beneficial effects:
(1) The invention provides an ionic liquid phase-change absorbent and application thereof, wherein the ionic liquid phase-change absorbent contains ionic liquid, and the volatility of the ionic liquid is extremely low, so that the volatility of a system is inhibited, the loss of a solvent is reduced, the cost loss is reduced, and the loss of the solvent can be controlled to be 1.0-2.2 kg/t CO 2 ；
(2) The invention provides an ionic liquid phase-change absorbent and application thereof, wherein the ionic liquid is combined with a phase-change system of organic amine, and double activation is realized by utilizing the physical trapping effect of the ionic liquid and the chemical trapping effect of the organic amine, so that CO is efficiently absorbed 2 The absorption rate in the process is improved, and the reaction process is accelerated;
(3) The invention provides an ionic liquid phase change absorbent and application thereof, wherein the ionic liquid phase change absorbent utilizes the characteristic of low specific heat capacity of ionic liquidThe method can reduce the latent heat to a certain extent, and realize the low-water regeneration in the regeneration stage due to the characteristics of low vapor pressure, so that the latent heat is further reduced; the regeneration energy consumption is further reduced on the basis of the phase change absorbent by reducing the sensible heat and the latent heat, and the regeneration energy consumption is controlled to be 2.05-2.50 GJ/t CO 2 The method comprises the steps of carrying out a first treatment on the surface of the Thereby increasing the industrial application range of the phase-change absorbent and providing a novel method with high efficiency and low energy consumption for carbon capture.
Drawings
FIG. 1 illustrates the phase separation phenomenon of the novel phase change absorber provided by the present invention;
FIG. 2 shows the total CO of the absorbent at different ionic liquid concentrations in an embodiment of the present invention 2 Load changes.
The present invention will be described in further detail below. The following examples are merely illustrative of the present invention and are not intended to represent or limit the scope of the invention as defined in the claims.
Detailed Description
For a better illustration of the present invention, which is convenient for understanding the technical solution of the present invention, exemplary but non-limiting examples of the present invention are as follows:
example 1
The embodiment provides an ionic liquid phase-change absorbent which is a quaternary mixed system composed of imidazole ionic liquid 1-butyl-3-methylimidazole phosphorus hexafluoride salt ([ Bmim ] PF 6), DEEA, MAPA and water. Wherein the mass fraction of DEEA is 60wt%, MAPA is 10wt%, and [ Bmim ] PF6 is 20wt%, with the balance being water. Wherein the proportion of carbon dioxide in the gas is 10%, the absorption temperature is 20 ℃, and the regeneration temperature is 80 ℃.
Example 2
The embodiment provides an ionic liquid phase-change absorbent, which is imidazole ionic liquid 1-butyl-3-methylimidazole phosphorus hexafluoride salt ([ Bmim)]PF 6 ) The quaternary mixed system consists of DEEA, AEEA and water, wherein the mass fraction of DEEA is 40%, the AEEA is 30%, and the [ Bmim ] is formed by mixing the DEEA, the AEEA and the water]PF 6 10% and the balance of water. Wherein the proportion of carbon dioxide in the gas is 30%, the absorption temperature is 60 ℃, and the regeneration is carried outThe temperature was 105 ℃.
Example 3
The low-energy-consumption phase-change absorbent based on the ionic liquid and the application thereof are prepared from imidazole ionic liquid 1-butyl-3-methylimidazole phosphorus hexafluoride salt ([ Bmim)]PF 6 ) A quaternary mixed system consisting of DEEA, TETA and water, wherein the mass fraction of the DEEA is 50%, the mass fraction of the TETA is 15%, and the [ Bmim ] is formed by mixing the DEEA, the TETA and the water]PF 6 5% and the balance of water. Wherein the proportion of carbon dioxide in the gas is 15%, the absorption temperature is 45 ℃, and the regeneration temperature is 95 ℃.
Example 4
The embodiment provides an ionic liquid phase-change absorbent, which is imidazole ionic liquid 1-butyl-3-methylimidazole tetrafluoroborate ([ Bmim)]BF 4 ) A quaternary mixed system consisting of DEEA, BDA and water, wherein the mass fraction of the DEEA is 50wt%, the BDA is 20wt%, and the DEEA is [ Bmim ]]BF 4 5-20wt%. Wherein the proportion of carbon dioxide in the gas is 20%, the absorption temperature is 40 ℃, and the regeneration temperature is 110 ℃.
Example 5
The embodiment provides an ionic liquid phase-change absorbent, which is imidazole ionic liquid 1-butyl-3-methylimidazole tetrafluoroborate ([ Bmim)]BF 4 ) The quaternary mixed system consists of DEEA, AEEA and water, wherein the mass fraction of DEEA is 45%, the AEEA is 25%, and the [ Bmim ] is formed by mixing the DEEA, the AEEA and the water]BF 4 10%. The proportion of carbon dioxide in the gas was 12%, the absorption temperature was 50℃and the regeneration temperature was 90 ℃.
Example 6
The embodiment provides an ionic liquid phase-change absorbent which is a quaternary mixed system composed of imidazole ionic liquid 1-butyl-3-methylimidazole bromide ([ Bmim ] Br), DMCA, TETA and water, wherein the mass fraction of the DMCA is 60%, the TETA is 10%, and the [ Bmim ] Br is 10%. Wherein the proportion of carbon dioxide in the gas is 25%, the absorption temperature is 25 ℃, and the regeneration temperature is 80 ℃.
Example 7
The embodiment provides an ionic liquid phase-change absorbent, which is1-ethyl-3-methylimidazole hexafluorophosphate ([ Emim) from imidazole ionic liquid]PF 6 ) The quaternary mixed system consists of DMCA, DETA and water, wherein the mass fraction of the DMCA is 50%, the mass fraction of the DETA is 10%, and the mass fraction of the DETA is [ Emim ]]PF 6 20%. Wherein the proportion of carbon dioxide in the gas is 30%, the absorption temperature is 60 ℃, and the regeneration temperature is 115 ℃.
Example 8
The embodiment provides an ionic liquid phase-change absorbent, which is imidazole ionic liquid 1-butyl-3-methylimidazole phosphorus hexafluoride salt ([ Bmim)]PF 6 ) The quaternary mixed system consists of PMDETA, DETA and water, wherein the mass fraction of the PMDETA is 40%, the mass fraction of the DETA is 10%, and the mass fraction of the PMDETA is [ Bmim ]]PF 6 20%. Wherein the proportion of carbon dioxide in the gas is 10%, the absorption temperature is 50 ℃, and the regeneration temperature is 110 ℃.
Example 9
The embodiment provides an ionic liquid phase-change absorbent, which is imidazole ionic liquid 1-ethyl-3-methylimidazole bis (trifluoromethanesulfonyl) imide salt ([ Emim)]Tf 2 N), DEEA, DETA and water, wherein the mass fraction of DEEA is 60%, the mass fraction of DETA is 30%, and [ Emim ]]Tf 2 N is 5%. Wherein the proportion of carbon dioxide in the gas is 10%, the absorption temperature is 40 ℃, and the regeneration temperature is 120 ℃.
Example 10
The embodiment provides an ionic liquid phase-change absorbent, which is imidazole ionic liquid 1-ethyl-3-methylimidazole bis (trifluoromethanesulfonyl) imide salt ([ Emim)]Tf 2 N), DEEA, AEEA and water, wherein the mass fraction of DEEA is 60%, AEEA is 15% [ Emim ]]Tf 2 N is 5%. Wherein the proportion of carbon dioxide in the gas is 5%, the absorption temperature is 30 ℃, and the regeneration temperature is 95 ℃.
Example 11
The embodiment provides an ionic liquid phase-change absorbent, which is imidazole ionic liquid 1-ethyl-3-methylimidazole hexafluorophosphate ([ Emim ]]PF 6 ) Quaternary mixture of DEEA, MAPA and waterWherein the mass fraction of DEEA is 40%, the mass fraction of MAPA is 20%, and [ Emim ]]PF 6 10%. Wherein the proportion of carbon dioxide in the gas is 10%, the absorption temperature is 50 ℃, and the regeneration temperature is 110 ℃.
Example 12
The embodiment provides an ionic liquid phase-change absorbent, which is imidazole ionic liquid 1-butyl-3-methylimidazole phosphorus hexafluoride salt ([ Bmim)]PF 6 ) The quaternary mixed system consists of DMCA, TETA and water, wherein the mass fraction of the DMCA is 40%, the mass fraction of the TETA is 20%, and the mass fraction of the TETA is [ Bmim ]]PF 6 15%. Wherein the proportion of carbon dioxide in the gas is 20%, the absorption temperature is 40 ℃, and the regeneration temperature is 90 ℃.
Comparative example 1
The absorbent of the comparative example is a ternary mixed system composed of DEEA, MAPA and water, wherein the mass fraction of DEEA is 60wt% and the mass fraction of MAPA is 10wt%. Wherein the proportion of carbon dioxide in the gas is 20%, the absorption temperature is 35 ℃, and the regeneration temperature is 110 ℃.
Comparative example 2
The absorbent of the comparative example is a ternary mixed system composed of DEEA, AEEA and water, wherein the mass fraction of DEEA is 50% and the mass fraction of AEEA is 20%. Wherein the proportion of carbon dioxide in the gas is 15%, the absorption temperature is 40 ℃, and the regeneration temperature is 105 ℃.
Comparative example 3
The absorbent of the comparative example is a ternary mixed system composed of DEEA, ([ Bmim ] PF 6) and water, wherein the mass fraction of DEEA is 50% and the mass fraction of AEEA is 30%. Wherein the proportion of carbon dioxide in the gas is 10%, the absorption temperature is 40 ℃, and the regeneration temperature is 105 ℃.
Comparative example 4
The absorbent of this comparative example was a catalyst prepared from DEEA, ([ Emim)]Tf 2 N) water, wherein the mass fraction of DEEA is 60%, and the mass fraction of AEEA is 20%. Wherein the proportion of carbon dioxide in the gas is 10%, the absorption temperature is 40 ℃, and the regeneration temperature is 105 ℃.
The phase change absorbents provided in examples 1 to 12 and comparative examples 1 to 4 were tested for absorption efficiency, regeneration energy consumption, and solvent loss, and the results are shown in table 1.
The method for testing the absorption efficiency, the regeneration energy consumption and the solvent loss comprises the following steps: absorption efficiency by CO in gas phase at inlet and outlet of absorption unit 2 And (5) calculating concentration. The regeneration efficiency is achieved by the desorption unit to import and export CO in the liquid phase 2 And (5) calculating a load. The regeneration energy consumption is calculated by three parts of sensible heat, latent heat and reaction heat. The solvent loss is calculated from the composition of the absorbent after cycling through multiple absorption-desorption processes. The calculation methods are all common methods in the art, and are not described herein.
TABLE 1
From the results of the above examples and comparative examples, it is apparent that the addition of the imidazole-based ionic liquid improves the absorption efficiency and the regeneration efficiency, and activates the carbon trapping process. The low specific heat capacity of the ionic liquid is used for reducing the latent heat, the low vapor pressure is used for realizing the regeneration of less water, and the latent heat is reduced, so that the regeneration energy consumption is further reduced on the basis of the phase change absorbent, and the energy consumption can be reduced to 2.05GJ/t CO 2 . Meanwhile, the ionic liquid has extremely low volatility, can inhibit amine volatilization, reduces solvent loss, and can reduce the solvent loss to 1.0kg/t CO 2 . In summary, a low energy consumption phase change absorbent based on ionic liquid is CO after large-scale combustion 2 The trapping field has good application prospect
The applicant states that the detailed structural features of the present invention are described by the above embodiments, but the present invention is not limited to the above detailed structural features, i.e. it does not mean that the present invention must be implemented depending on the above detailed structural features. It should be apparent to those skilled in the art that any modifications of the present invention, equivalent substitutions of selected components of the present invention, addition of auxiliary components, selection of specific modes, etc., are within the scope of the present invention and the scope of the disclosure.
The preferred embodiments of the present invention have been described in detail above, but the present invention is not limited to the specific details of the above embodiments, and various simple modifications can be made to the technical solution of the present invention within the scope of the technical concept of the present invention, and all the simple modifications belong to the protection scope of the present invention.
In addition, the specific features described in the above embodiments may be combined in any suitable manner, and in order to avoid unnecessary repetition, various possible combinations are not described further.
Moreover, any combination of the various embodiments of the invention can be made without departing from the spirit of the invention, which should also be considered as disclosed herein.
Claims (10)
1. The ionic liquid phase change absorbent is characterized by comprising primary amine and/or secondary amine, a phase splitting agent, ionic liquid and water.
2. The phase-change absorbent according to claim 1, wherein the total concentration of amino groups in the phase-change absorbent is 4 to 8mol/L.
3. The phase change absorbent according to claim 1 or 2, wherein the ionic liquid comprises an imidazole-based ionic liquid;
preferably, the imidazole ionic liquid comprises any one or a combination of at least two of 1-butyl-3-methylimidazole hexafluorophosphate, 1-butyl-3-methylimidazole tetrafluoroborate, 1-butyl-3-methylimidazole bromide, 1-butyl-3-methylimidazole hexafluorophosphate, 1-ethyl-3-methylimidazole hexafluorophosphate or 1-ethyl-3-methylimidazole bistrifluoromethylsulfonylimine salt;
preferably, the mass fraction of the ionic liquid in the phase-change absorbent is 5-30%.
4. A phase change absorbent according to any one of claims 1-3, wherein the primary and/or secondary amine comprises any one or a combination of at least two of hydroxyethylethylene diamine, N-methyl-1, 3-propanediamine, 1, 4-butanediamine, triethylenetetramine or diethylenetriamine;
preferably, the mass fraction of the primary amine and/or secondary amine in the phase-change absorbent is 10-30%.
5. The phase change absorbent according to any one of claims 1-4, wherein the phase-splitting agent comprises a tertiary amine;
preferably, the tertiary amine comprises any one or a combination of at least two of N, N-diethylaminoethanol, N-dimethylcyclohexylamine or pentamethyldiethyltriamine;
preferably, the mass fraction of the phase-splitting agent in the phase-change absorbent is 40-60%.
6. Use of an ionic liquid phase change absorber according to any one of claims 1-5 for absorbing CO in a mixed gas 2 。
7. The use according to claim 6, wherein the ionic liquid phase change absorber is used for absorbing CO in a mixed gas 2 The method of (1) comprises the following steps:
(1) Counter-current absorption of CO in the mixed gas using the ionic liquid phase change absorber 2 Obtaining an absorbed liquid;
(2) Standing and layering the absorbed liquid in the step (1) to obtain a rich liquid and a first lean liquid;
(3) Desorbing the rich liquid in the step (2) to obtain a second lean liquid, and mixing the second lean liquid with the first lean liquid to be used for absorbing CO in the mixed gas in the step (1) 2 。
8. The use according to claim 7, wherein the CO in the mixed gas of step (1) 2 The volume concentration of (2) is 5-30%;
preferably, the absorption in step (1) is carried out at normal pressure and at a temperature of 20 to 60 ℃.
9. The use according to claim 7, wherein the rich liquid of step (3) is heat exchanged with the desorbed second lean liquid;
preferably, the absorption in step (1) is carried out at normal pressure and at a temperature of 80 to 120 ℃.
10. The use according to claim 7, characterized in that the energy consumption for regenerating the ionic liquid phase-change absorbent is 2.05-2.50 GJ/t CO 2 ；
Preferably, the loss of the ionic liquid phase change absorbent is 1.0-2.2 kg/t CO 2 。
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117101347A (en) * | 2023-08-15 | 2023-11-24 | 中国矿业大学 | For CO 2 Trapped ionic liquid-based phase change absorber |
| CN117959916A (en) * | 2024-03-28 | 2024-05-03 | 深碳科技(深圳)有限公司 | Liquid-liquid two-phase absorbent and preparation method and application thereof |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117101347A (en) * | 2023-08-15 | 2023-11-24 | 中国矿业大学 | For CO 2 Trapped ionic liquid-based phase change absorber |
| CN117101347B (en) * | 2023-08-15 | 2024-03-29 | 中国矿业大学 | For CO 2 Trapped ionic liquid-based phase change absorber |
| CN117959916A (en) * | 2024-03-28 | 2024-05-03 | 深碳科技(深圳)有限公司 | Liquid-liquid two-phase absorbent and preparation method and application thereof |
| CN117959916B (en) * | 2024-03-28 | 2024-06-07 | 深碳科技(深圳)有限公司 | Liquid-liquid two-phase absorbent and preparation method and application thereof |
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