Method for purifying heat-stable salt and recovering amine from decarburized amine solution

Abstract

The invention relates to the technical field of carbon dioxide capture, and discloses a method for purifying heat-stable salt and recovering amine from decarburized amine liquid. The method comprises the following steps: (1) filtering the decarburized amine solution; (2) carrying out ion exchange on the filtered amine liquid and anion exchange resin, and collecting effluent; (3) regenerating the anion exchange resin subjected to saturated adsorption in the ion exchange process in the step (2) by using an alkaline solution, and collecting a regenerated solution; (4) adding acid into the regenerated liquid, and adjusting the pH value to 6-6.5; then alkali is added, and the pH value is adjusted to 8.5-9.5; and (5) performing electrodialysis treatment on the solution of which the pH value is adjusted in the step (4). According to the technical scheme provided by the invention, the decarburized amine liquid is subjected to filtration, ion exchange purification treatment, chemical modulation and electrodialysis treatment, so that purification of the decarburized amine liquid and efficient recovery of amine can be realized.

Description

Technical Field

[0001] The invention relates to the technical field of carbon dioxide capture, and in particular to a method for purifying heat-stable salts and recovering amines using a decarbonized amine liquid. Background Art

[0002] The problem of global warming is becoming increasingly prominent. The large-scale emission of greenhouse gases is one of the main causes of global warming. At present, the problem of industrial carbon emissions with carbon dioxide as the main component has attracted more and more attention. Governments and enterprises are trying to capture, store and utilize carbon dioxide on a large scale. Among the many capture methods, chemical absorption has become the mainstream due to its high efficiency and relatively mature technology. Commonly used chemical absorbents include alcohol amine solutions, such as methyldiethanolamine (MDEA), diethanolamine (DEA) and triethanolamine (TEA). These absorbents can effectively capture and separate carbon dioxide through acid-base reactions, with high absorption capacity and low regeneration energy consumption.

[0003] In the long-term CO2 capture process, the accumulation of heat-stable salts (HSS) in the commonly used absorbent alcohol amine solution is a common problem. These HSS mainly come from impurities in CO2, such as sulfates, sulfides and nitrates. These inorganic salts react with alcohol amines to form salts that are difficult to degrade, resulting in a decrease in the thermal stability of the solution. In addition, high temperature and high pressure operating conditions and the recycling of the solution will also accelerate the generation of HSS, thereby affecting the decarbonization performance of the absorbent and the safety of the equipment.

[0004] A variety of methods have been developed to remove HSS from alcohol amine solutions, including ion exchange, membrane separation technology, electrodialysis and vacuum distillation. Ion exchange uses resin to adsorb HSS in the solution to achieve purification; membrane separation technology uses semi-permeable membranes to screen out HSS; electrodialysis drives ion migration through electric fields to achieve the effect of removing HSS; and vacuum distillation uses the difference in boiling points of different components to achieve separation.

[0005] As an effective carbon dioxide absorbent, the absorption mechanism of alcohol amine solution involves the chemical reaction of primary amine, secondary amine and tertiary amine with carbon dioxide. In the process of absorbing carbon dioxide, primary amine and secondary amine first react with CO2 to form carbamate by acid-base neutralization reaction. Specifically, primary amine (such as MDEA) reacts with CO2 to form primary carbamate; secondary amine (such as DEA) forms secondary carbamate. However, since there is no reactive hydrogen atom on the nitrogen atom of tertiary amine (such as TEA), its reaction with CO2 does not directly form carbamate, but forms bicarbonate intermediate. The formation of these carbamates is reversible, and CO2 can be released under heating or reduced pressure to achieve amine regeneration.

[0006] During the long-term circulation of alcoholamine solution, the accumulation of heat-stable salts (HSS) is inevitable. In order to maintain the absorption efficiency of the solution, these HSS need to be removed regularly. However, existing methods for removing HSS, such as ion exchange, membrane separation and electrodialysis, often not only remove HSS, but also remove carbamates in the solution at the same time. This is because carbamates and HSS have certain similarities in chemical properties, which makes it difficult to completely separate them during the removal process. This non-selective removal process will result in a large amount of amine loss, thereby reducing the absorption capacity and economic benefits of the alcoholamine solution.

[0007] In summary, the development of a method that can effectively remove HSS and efficiently recover amines is of great significance for improving the recycling efficiency of alcohol amine solutions and reducing operating costs. Summary of the invention

[0008] The purpose of the present invention is to overcome the problem in the prior art that, due to the similarity in chemical structure between heat-stable salt and carbamate, carbamate is removed while removing the heat-stable salt accumulated in the recycling process of alcohol amine solution, thereby causing the loss of amine, and to provide a method for purifying heat-stable salt from decarbonized amine solution and recovering amine. The method for purifying heat-stable salt from decarbonized amine solution and recovering amine of the present invention can achieve the removal of heat-stable salt from decarbonized amine solution and the efficient recovery of amine.

[0009] In order to achieve the above object, the present invention provides a method for purifying heat-stable salts and recovering amines from a decarbonized amine solution, the method comprising the following steps: (1) Filtering the decarbonized amine liquid; (2) performing ion exchange on the amine solution obtained after filtration with an anion exchange resin, and collecting the effluent; (3) regenerating the anion exchange resin saturated with adsorption during the ion exchange process in step (2) using an alkaline solution, and collecting the regenerated solution; (4) adding acid to the regeneration solution and adjusting the pH value to 6-6.5; then adding alkali and adjusting the pH value to 8.5-9.5; (5) The solution after adjusting the pH value in step (4) is subjected to electrodialysis.

[0010] Preferably, the decarbonation amine solution is an alcohol amine solution containing a heat-stable salt.

[0011] Preferably, in step (1), the filtering process is carried out in a bag filter or a pressure filter, and the pore size of the filter is 1-100 μm.

[0012] Preferably, in step (2), the ion exchange process comprises: passing the amine solution obtained after filtration through an anion exchange resin bed in an ion exchange device, and the flow rate of the amine solution obtained after filtration is 0.1-10 L / min.

[0013] Preferably, the anion exchange resin is at least one of a strong alkaline ion exchange resin, a weak alkaline ion exchange resin and a strong and weak alkaline mixed ion exchange resin.

[0014] Preferably, in step (3), the regeneration process comprises: passing the alkaline solution through the anion exchange resin bed in the ion exchange device, and the flow rate of the alkaline solution is 5-20 mL / min, and the contact time between the alkaline solution and the saturated adsorption anion exchange resin is 5-10 min.

[0015] Preferably, the alkaline solution is a sodium hydroxide solution and / or a potassium hydroxide solution.

[0016] Preferably, in step (4), the acid is at least one of sulfuric acid, hydrochloric acid and nitric acid.

[0017] Preferably, in step (4), the base is at least one of sodium hydroxide, potassium hydroxide and aqueous ammonia.

[0018] Preferably, in step (5), the conditions of the electrodialysis treatment include: voltage of 15-20 V, current of 0.1-0.8 A, and flow rate of 10-20 mL / min.

[0019] Preferably, the method further comprises returning the effluent obtained in step (2) to the carbon capture system for reuse.

[0020] According to the method for purifying heat-stable salts and recovering amines from decarbonized amine liquid of the present invention, the decarbonized amine liquid is filtered, purified by ion exchange, chemically modulated and electrodialyzed, so that the decarbonized amine liquid can effectively remove heat-stable salts and efficiently recover amines. DETAILED DESCRIPTION

[0021] The specific embodiments of the present invention are described in detail below. It should be understood that the specific embodiments described herein are only used to illustrate and explain the present invention, and are not used to limit the present invention.

[0022] The endpoints and any values ​​of the ranges disclosed in this article are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoint values ​​of each range, the endpoint values ​​of each range and the individual point values, and the individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed in this article.

[0023] The method for purifying heat-stable salts and recovering amines from decarbonized amine liquid of the present invention comprises the following steps: (1) Filtering the decarbonized amine liquid; (2) performing ion exchange on the amine solution obtained after filtration with an anion exchange resin, and collecting the effluent; (3) regenerating the anion exchange resin saturated with adsorption during the ion exchange process in step (2) using an alkaline solution, and collecting the regenerated solution; (4) adding acid to the regeneration solution and adjusting the pH value to 6-6.5; then adding alkali and adjusting the pH value to 8.5-9.5; (5) The solution after adjusting the pH value in step (4) is subjected to electrodialysis.

[0024] In the method of the present invention, the decarbonized amine solution may be an alcohol amine solution containing a heat-stable salt. The heat-stable salt may be at least one of hydrochloride, sulfate, formates, acetates, oxalates, thiocyanates and thiosulfinates. The alcohol amine solution may include at least one of a primary amine (MDEA), a secondary amine (DEA) and a tertiary amine (TEA). The product of the reaction of the alcohol amine solution with carbon dioxide may be a carbamate. Specifically, the reaction product of the primary amine (MDEA) and carbon dioxide is a primary carbamate, the reaction product of the secondary amine (DEA) and carbon dioxide is a secondary carbamate, and the reaction product of the tertiary amine and carbon dioxide is a bicarbonate intermediate. The reaction of the alcohol amine solution with carbon dioxide is reversible, and under the conditions of heating and / or decompression, carbon dioxide gas can be released to achieve amine regeneration.

[0025] In step (1), the filtering process can be implemented in a bag filter or a pressure filter, and the pore size of the filter can be 1-100 μm. The bag filter can be at least one of a single bag filter, a multi-bag filter, a rocker bag filter and a high-precision bag filter. The pressure filter can be at least one of a quartz sand filter, an activated carbon filter and a manganese sand filter. In a more preferred case, the filtering process can be implemented in a pressure filter. The material of the filter medium of the filter can be at least one of stainless steel, activated carbon, fiber material and glass fiber (PTFE). In the most preferred embodiment, the material of the filter medium of the filter is stainless steel. The filter medium of the filter is replaced in time when the filter is overloaded.

[0026] In step (2), the ion exchange process may include: passing the amine solution obtained after filtration through an anion exchange resin bed in an ion exchange device, and the flow rate of the amine solution obtained after filtration may be 0.1-10 L / min. In a more preferred case, the flow rate of the amine solution obtained after filtration is 1-8 L / min. The ion exchange process may be implemented in various conventional ion exchange devices in the art.

[0027] In step (2), the anion exchange resin may be at least one of a strong basic ion exchange resin, a weak basic ion exchange resin, and a strong and weak basic mixed ion exchange resin. In the most preferred embodiment, the anion exchange resin is a weak basic anion exchange resin, such as a weak basic anion exchange resin with a product model of ‌D301 purchased from Langfang Aoguang Energy Saving Technology Co., Ltd.

[0028] In step (3), the regeneration process may include: passing the alkaline solution through the anion exchange resin bed in the ion exchange device, and the flow rate of the alkaline solution may be 5-20 mL / min, and the contact time between the alkaline solution and the saturated adsorption anion exchange resin may be 5-10 min. In a more preferred case, the flow rate of the alkaline solution is 8-18 mL / min, and the contact time between the alkaline solution and the saturated adsorption anion exchange resin is 6-8 min.

[0029] In the method of the present invention, the alkaline solution can be a sodium hydroxide solution and / or a potassium hydroxide solution. In the most preferred embodiment, the alkaline solution is a sodium hydroxide solution. The concentration of the alkaline solution can be 2-6wt%, preferably 3-5wt%, specifically, for example, 3wt%, 3.2wt%, 3.5wt%, 3.7wt%, 4wt%, 4.2wt%, 4.5wt%, 4.7wt% or 5wt%.

[0030] In step (4), acid is added to the regeneration liquid and the pH value is adjusted to 6-6.5. In a more preferred case, acid is added to the regeneration liquid and the pH value is adjusted to 6.2-6.4. When the pH value of the regeneration liquid is adjusted to the above preferred range, NH4 + Forms and maintains heat-stable salt ionic form for better amine recovery.

[0031] In step (4), alkali is added to the regeneration liquid and the pH value is adjusted to 8.5-9.5. In a more preferred case, alkali is added to the regeneration liquid and the pH value is adjusted to 8.8-9.3. When the pH value of the regeneration liquid is adjusted to the above preferred range, the carbamate can be converted into a neutral form, thereby obtaining a better amine recovery effect.

[0032] In step (4), the acid may be at least one of sulfuric acid, hydrochloric acid and nitric acid. In the most preferred embodiment, the acid is hydrochloric acid. The acid is used in the form of an aqueous solution. The concentration of the acid may be 0.5-5wt%, preferably 0.5-2wt%, specifically, for example, 0.5wt%, 0.8wt%, 1.2wt%, 1.5wt%, or 2wt%.

[0033] In step (4), the alkali may be at least one of sodium hydroxide, potassium hydroxide and ammonia water. In the most preferred embodiment, the alkali is sodium hydroxide. The alkali is used in the form of an aqueous solution. The concentration of the alkali may be 0.5-5wt%, preferably 1-3wt%, specifically, for example, 1wt%, 1.2wt%, 1.5wt%, 1.8wt%, 2wt%, 2.2wt%, 2.5wt%, 2.8wt% or 3wt%.

[0034] In step (5), the conditions of the electrodialysis treatment may include: voltage of 15-20V, current of 0.1-0.8A, and flow rate of 10-20mL / min. In a more preferred case, the conditions of the electrodialysis treatment include: voltage of 16-18V, current of 0.2-0.6A, and flow rate of 12-18mL / min. The electrodialysis treatment process may be implemented in various conventional electrodialysis devices in the art. According to this preferred embodiment, better thermal stability salt purification and amine recovery effects can be obtained.

[0035] In the present invention, the method further comprises returning the effluent obtained in step (2) to the carbon capture system for reuse. The carbon capture system comprises a flue gas pretreatment system, an absorption system, a regeneration system, a compression drying system and a refrigeration liquefaction system. The carbon capture system is used to absorb carbon dioxide gas from industrial waste gas.

[0036] The following examples further illustrate the method for purifying heat-stable salts and recovering amines from decarbonized amine liquid of the present invention. The examples are implemented based on the technical solution of the present invention, and detailed implementation methods and specific operation processes are given, but the protection scope of the present invention is not limited to the following examples.

[0037] The experimental methods in the following examples, unless otherwise specified, are all conventional methods in the art. The experimental materials used in the following examples, unless otherwise specified, are all commercially available.

[0038] In the following examples and comparative examples, the test method for the concentration of the heat-stable salt and the concentration of the amine in the sample was carried out in the following manner.

[0039] Thermal stability salt concentration test: Take 50mL of sample, heat, and reflux for 5 minutes to remove residual CO2 and H2S. After heating, cover the sample with a quartz glass cover and cool it in a dark place. Use deionized water to compensate for the difference to ensure that the final sample volume is consistent with the initial volume. Weigh 2-3g of sample and place it in a 100mL plastic cup. The sample weight is recorded as W . Pour the sample into the resin column and rinse the plastic cup with deionized water several times. The washing solution is also poured into the resin column and then rinsed with deionized water. Use a 250mL beaker to collect the solution flowing out of the resin column. Use pH test paper to test the effluent from the resin column until it is neutral (pH=7) or equal to the pH value of the rinse water. Add 2-3 drops of phenolphthalein indicator with a concentration of 5g / L to the beaker, titrate with 0.1mol / L sodium hydroxide solution until it turns pink, and record the consumption of sodium hydroxide solution (V). The calculation formula for the mass concentration Wt% of thermally stable salt is as follows: Wt%=

[0040] Amine concentration test: Use GC-MS to test the amine concentration of the sample. Preheat the chromatograph for 30 minutes, take 20 μL of sample and dilute it into 50 g of deionized water. After injection, perform baseline correction, peak identification and quantitative analysis on the chromatogram to determine the amine concentration of the sample.

[0041] Example 1 (1) An amine solution containing a high concentration of heat-stable salt that has been in operation for a long time in a field project was used as the initial sample. The sample was pumped into a filter device for filtration. The pore size of the filter was 50 μm.

[0042] (2) The amine solution obtained after filtration was pumped into an ion exchange device containing a weakly alkaline anion exchange resin (purchased from Langfang Aoguang Energy Saving Technology Co., Ltd., product model D301) for ion exchange. The flow rate of the amine solution was controlled to 5 L / min to obtain the effluent A1 after ion exchange purification.

[0043] (3) Pump a 4 wt% sodium hydroxide solution into the ion exchange device to regenerate the anion exchange resin that was saturated with adsorption during the ion exchange process. Control the flow rate of the sodium hydroxide solution to 15 mL / min and the contact time to 7 min, and collect the regenerated liquid.

[0044] (4) The regeneration liquid obtained in step (3) is added to a hydrochloric acid solution having a concentration of 1.5 wt %, and the solution is continuously stirred during the addition process, and the pH value of the solution is detected by a pH meter until the pH value of the solution is 6.4; then, a sodium hydroxide solution having a concentration of 1.8 wt % is added to the regeneration liquid, and the solution is continuously stirred during the addition process, and the pH value of the solution is detected by a pH meter until the pH value of the solution is 9.1, thereby obtaining a solution after adjusting the pH value.

[0045] (5) The pH-adjusted solution obtained in step (4) was pumped into an electrodialysis device. The voltage of the electrodialysis device was controlled to be 18 V, the current to be 0.5 A, and the flow rate of the solution to be 15 mL / min. The effluent B1 was collected.

[0046] The initial sample, the collected effluent A1 and the effluent B1 were tested for thermal stability salt concentration and amine concentration, respectively. The test results are as follows: The initial sample had a thermally stable salt concentration of 2.95 wt % and an amine concentration of 30.2 wt %; The concentration of heat-stable salt in effluent A1 was 1.32 wt %, and the concentration of amine was 25.3 wt %; The concentration of the heat-stable salt in the effluent B1 was 0.65 wt %, and the concentration of the amine was 4.2 wt %.

[0047] Example 2 (1) An amine solution containing a high concentration of heat-stable salt that has been in operation for a long time in a field project was used as the initial sample. The sample was pumped into a filter device for filtration. The pore size of the filter was 50 μm.

[0048] (2) The amine solution obtained after filtration was pumped into an ion exchange device containing a weakly alkaline anion exchange resin (purchased from Langfang Aoguang Energy Saving Technology Co., Ltd., product model D301) for ion exchange. The flow rate of the amine solution was controlled to 8 L / min to obtain the effluent A2 after ion exchange purification.

[0049] (3) Pump a 5 wt% sodium hydroxide solution into the ion exchange device to regenerate the anion exchange resin that was saturated with adsorption during the ion exchange process. Control the flow rate of the sodium hydroxide solution to 18 mL / min and the contact time to 6 min, and collect the regenerated liquid.

[0050] (4) The regeneration liquid obtained in step (3) is added to a 5 wt% hydrochloric acid solution, stirring continuously during the addition process, and detecting with a pH meter until the pH value of the solution is 6.3; then, a 1.8 wt% sodium hydroxide solution is added to the regeneration liquid, stirring continuously during the addition process, and detecting with a pH meter until the pH value of the solution is 9.0, thereby obtaining a solution after adjusting the pH value.

[0051] (5) The pH-adjusted solution obtained in step (4) was pumped into an electrodialysis device. The voltage of the electrodialysis device was controlled to be 17 V, the current to be 0.6 A, and the flow rate of the solution to be 18 mL / min. The effluent B2 was collected.

[0052] The initial sample, the collected effluent A2 and the effluent B2 were tested for thermal stability salt concentration and amine concentration, respectively. The test results are as follows: The initial sample had a thermally stable salt concentration of 2.95 wt % and an amine concentration of 30.2 wt %; The concentration of heat-stable salt in effluent A2 was 1.25 wt %, and the concentration of amine was 24.6 wt %; The concentration of the heat-stable salt in the effluent B2 was 0.64 wt %, and the concentration of the amine was 4.3 wt %.

[0053] Example 3 (1) An amine solution containing a high concentration of heat-stable salt that has been in operation for a long time in a field project was used as the initial sample. The sample was pumped into a filter device for filtration. The pore size of the filter was 50 μm.

[0054] (2) The amine solution obtained after filtration was pumped into an ion exchange device containing a weakly alkaline anion exchange resin (purchased from Langfang Aoguang Energy Saving Technology Co., Ltd., product model D301) for ion exchange. The flow rate of the amine solution was controlled to be 5 L / min to obtain the effluent A3 after ion exchange purification.

[0055] (3) Pump a 4 wt% sodium hydroxide solution into the ion exchange device to regenerate the anion exchange resin that was saturated with adsorption during the ion exchange process. Control the flow rate of the sodium hydroxide solution to 15 mL / min and the contact time to 7 min, and collect the regenerated liquid.

[0056] (4) The regeneration liquid obtained in step (3) is added to a 2 wt% hydrochloric acid solution, stirring continuously during the addition process, and detecting with a pH meter until the pH value of the solution is 6.2; then, a 3 wt% sodium hydroxide solution is added to the regeneration liquid, stirring continuously during the addition process, and detecting with a pH meter until the pH value of the solution is 9.2, thereby obtaining a solution after adjusting the pH value.

[0057] (5) The pH-adjusted solution obtained in step (4) was pumped into an electrodialysis device. The voltage of the electrodialysis device was controlled to be 16 V, the current to be 0.2 A, and the flow rate of the solution to be 12 mL / min. The effluent B3 was collected.

[0058] The initial sample, the collected effluent A3 and the effluent B3 were tested for thermal stability salt concentration and amine concentration, respectively. The test results are as follows: The initial sample had a thermally stable salt concentration of 2.95 wt % and an amine concentration of 30.2 wt %; The concentration of heat-stable salt in effluent A3 was 1.27 wt %, and the concentration of amine was 24.7 wt %; The concentration of the heat-stable salt in the effluent B3 was 0.61 wt %, and the concentration of the amine was 4.2 wt %.

[0059] Example 4 The method of Example 1 was used to purify the heat-stable salt and recover the amine from the alcohol amine solution containing high concentration of heat-stable salt in a long-term operation of a field project. The difference was that in step (5), the voltage of the electrodialysis device was adjusted to 15 V, the current was adjusted to 0.1 A, and the flow rate was adjusted to 10 mL / min, and finally the collected liquid A4 and the collected liquid B4 were obtained.

[0060] The initial sample, the collected effluent A4 and the effluent B4 were tested for thermal stability salt concentration and amine concentration, respectively. The test results are as follows: The initial sample had a thermally stable salt concentration of 2.95 wt % and an amine concentration of 30.2 wt %; The concentration of heat-stable salt in effluent A4 was 1.32 wt %, and the concentration of amine was 25.3 wt %; The concentration of the heat-stable salt in the effluent B4 was 0.69 wt %, and the concentration of the amine was 3.6 wt %.

[0061] Comparative Example 1 The alcohol amine solution containing a high concentration of heat-stable salt that has been in long-term operation in the field engineering demonstration was treated according to the method of Example 1, except that the electrodialysis treatment process in step (5) was not performed, and the solution after pH adjustment in step (4) was directly used as the effluent D1. The initial sample and the collected effluent D1 were tested for heat-stable salt concentration and amine concentration. The test results are as follows: The initial sample had a thermally stable salt concentration of 2.95 wt % and an amine concentration of 30.2 wt %; The concentration of the heat-stable salt in the effluent D1 was 0.92 wt %, and the concentration of the amine was 2.2 wt %.

[0062] From the comparison of the data of Examples 1-4 and Comparative Example 1, it can be seen that the method for purifying heat-stable salts and recovering amines using the decarbonized amine liquid of the present invention can effectively remove heat-stable salts while achieving efficient recovery of amines.

[0063] The preferred embodiments of the present invention are described in detail above, but the present invention is not limited thereto. Within the technical concept of the present invention, the technical solution of the present invention can be subjected to a variety of simple modifications, including the combination of various technical features in any other suitable manner, and these simple modifications and combinations should also be regarded as the contents disclosed by the present invention and belong to the protection scope of the present invention.

Claims

1. A method for purifying heat-stable salts and recovering amines from a decarbonized amine solution, characterized in that: The method comprises the following steps: (1) Filtering the decarbonized amine liquid; (2) performing ion exchange on the amine solution obtained after filtration with an anion exchange resin, and collecting the effluent; (3) regenerating the anion exchange resin saturated with adsorption during the ion exchange process in step (2) using an alkaline solution, and collecting the regenerated solution; (4) adding acid to the regeneration solution and adjusting the pH value to 6-6.5; then adding alkali and adjusting the pH value to 8.5-9.5; (5) The solution after adjusting the pH value in step (4) is subjected to electrodialysis.

2. The method according to claim 1, characterized in that: The decarbonation amine solution is an alcohol amine solution containing a heat-stable salt.

3. The method according to claim 1, characterized in that: In step (1), the filtering process is carried out in a bag filter or a pressure filter, and the pore size of the filter is 1-100 μm.

4. The method according to claim 1, characterized in that: In step (2), the ion exchange process includes: passing the amine solution obtained after filtration through an anion exchange resin bed in an ion exchange device, and the flow rate of the amine solution obtained after filtration is 0.1-10 L / min.

5. The method according to claim 1 or 4, characterized in that: The anion exchange resin is at least one of a strong alkaline ion exchange resin, a weak alkaline ion exchange resin and a strong and weak alkaline mixed ion exchange resin.

6. The method according to claim 1, characterized in that In step (3), the regeneration process includes: passing the alkaline solution through the anion exchange resin bed in the ion exchange device, and the flow rate of the alkaline solution is 5-20 mL / min, and the contact time between the alkaline solution and the saturated adsorption anion exchange resin is 5-10 min.

7. The method according to claim 1 or 6, characterized in that: The alkaline solution is a sodium hydroxide solution and / or a potassium hydroxide solution.

8. The method according to claim 1, characterized in that In step (4), the acid is at least one of sulfuric acid, hydrochloric acid and nitric acid; and / or The alkali is at least one of sodium hydroxide, potassium hydroxide and ammonia water.

9. The method according to claim 1, characterized in that: In step (5), the conditions of the electrodialysis treatment include: voltage of 15-20 V, current of 0.1-0.8 A, and flow rate of 10-20 mL / min.

10. The method according to any one of claims 1 to 9, characterized in that: The method further comprises returning the effluent obtained in step (2) to the carbon capture system for reuse.