Carbon capture agents, absorbents, devices, capture systems based on organic amines and applications

Abstract

The application provides a kind of carbon capture agent based on organic amine, absorbing liquid, device, capture system and application, the carbon capture agent is used for the absorption and / or capture of carbon dioxide, and organic amine is included in the carbon capture agent.The application can inhibit the energy consumption of carbon dioxide in long-term electrolytic desorption process by using at least one of organic amine, organic amine mixture, organic amine product as carbon capture agent, and the high volatility of carbon capture agent can be avoided;Wherein, the organic amine mixture includes organic amine and complexing agent, the organic amine product includes the product after mixing the organic amine and the complexing agent, and the complexing agent includes amino acid.

Description

Technical Field

[0001] This invention relates to the treatment of carbon dioxide, and more particularly to an organic amine-based carbon capture agent, absorbent, apparatus, capture system, and application. Background Technology

[0002] In recent years, global warming caused by greenhouse gases, especially carbon dioxide, has become a matter of great concern worldwide. However, the environmental problems caused by carbon dioxide remain very prominent. Therefore, how to effectively capture carbon dioxide from flue gas is an urgent problem to be solved.

[0003] To this end, Chinese invention patent CN113578025B (previous research by the inventor of this application) discloses a method and system for capturing carbon dioxide in flue gas, which uses NH3 (inorganic ammonia) as a carbon capture agent to absorb and desorb carbon dioxide, thereby realizing the capture and recovery of carbon dioxide.

[0004] While the aforementioned patents can achieve the absorption and desorption of carbon dioxide in flue gas and reduce the energy consumption of carbon dioxide capture to some extent, the carbon capture agent used in these patents is an inorganic ammonia solution. This results in high volatility, significant losses, unstable operation, and poor circulation performance of the carbon capture agent. Furthermore, inorganic ammonia is toxic and pollutes the environment, and the volatilization recovery system for inorganic ammonia is complex, lengthy, and has high investment costs. In addition, when using inorganic ammonia as a carbon capture agent, the electrolysis energy consumption during the carbon dioxide desorption process will increase significantly with long-term operation of carbon dioxide capture.

[0005] In view of this, it is necessary to provide a carbon capture agent, absorbent, device, capture system and application based on organic amines to solve or at least alleviate the technical defects of the above-mentioned carbon capture agents, which are highly volatile and significantly increase electrolysis energy consumption. Summary of the Invention

[0006] The main objective of this invention is to provide a carbon capture agent, absorbent, device, capture system and application based on organic amines, aiming to solve the technical problems of the high volatility of the aforementioned carbon capture agents and the significant increase in electrolysis energy consumption.

[0007] To achieve the above objectives, the present invention provides an organic amine-based carbon capture agent, characterized in that the carbon capture agent is used for the absorption and / or capture of carbon dioxide, and the carbon capture agent includes at least one of organic amines, mixtures of organic amines, and organic amine products;

[0008] The organic amine mixture includes an organic amine and a compounding agent; the organic amine product includes the product of the organic amine and the compounding agent; the compounding agent includes amino acids.

[0009] Further, the organic amine includes one or more of ethanolamine, aminoethylethanolamine, N-methyldiethanolamine, 2-amino-2-methylpropanol, diethylenetriamine, ethylenediamine, diethylamine, triethylenetetramine, and hydroxyethylethylenediamine;

[0010] And / or, the concentration of the organic amine is 0.2-8 mol / L.

[0011] Furthermore, the molar ratio of the organic amine to the compounding agent is 0.2-8:1.

[0012] Furthermore, the compound agent also includes a regulator, which includes an alkaline hydroxide and / or an alkaline carbonate compound; the molar ratio of the amino acid to the regulator is 0.1-8:1.

[0013] Furthermore, the carbon trapping agent also includes a supporting electrolyte.

[0014] The present invention also provides a method for preparing a carbon capture agent, wherein the carbon capture agent is used for the absorption and / or capture of carbon dioxide;

[0015] The preparation method includes: mixing an organic amine and a compounding agent to obtain the carbon capture agent; wherein the compounding agent includes amino acids.

[0016] The present invention also provides an application of the carbon capture agent as described above, or the carbon capture agent prepared by any of the preparation methods described above, in carbon dioxide capture.

[0017] Furthermore, the carbon dioxide absorption step includes: contacting the carbon scavenger with the carbon dioxide-containing gas to be treated and absorbing it to obtain a carbon dioxide absorption liquid;

[0018] The carbon dioxide capture steps include:

[0019] The carbon capture agent is contacted with and absorbed by the gas to be treated containing carbon dioxide to obtain a carbon dioxide absorbent liquid.

[0020] The carbon dioxide absorbent is electrolyzed to desorb the carbon dioxide in the absorbent, resulting in a desorbed solution and desorbed carbon dioxide.

[0021] Furthermore, the carbon dioxide capture step further includes: electrolyzing the desorption solution to cause the metal ions bound to the carbon capture agent to undergo electrodeposition, thereby obtaining the carbon capture agent separated from the metal ions;

[0022] The desorption solution contains the carbon trapping agent, which is bound to metal ions originating from the electrode.

[0023] The present invention also provides a carbon dioxide absorption device having a carbon trapping agent as described above or prepared by any of the preparation methods described above.

[0024] The present invention also provides a carbon dioxide capture system, which includes a carbon dioxide absorption device and a carbon dioxide desorption device;

[0025] The carbon dioxide absorption device contains a carbon trapping agent as described above or a carbon trapping agent prepared by any of the preparation methods described above;

[0026] The carbon dioxide absorption device and the carbon dioxide desorption device are connected to each other so as to continuously or intermittently transport the carbon dioxide absorbent generated in the carbon dioxide absorption device to the carbon dioxide desorption device, and the carbon dioxide desorption device has an electrolysis mechanism.

[0027] The present invention also provides a carbon dioxide absorbent liquid, which is used for the desorption and / or capture of carbon dioxide;

[0028] The carbon dioxide absorbent contains any of the carbon traps described above or the carbon traps prepared by any of the preparation methods described above, wherein the carbon traps are bound to carbon dioxide.

[0029] The present invention also provides an application of the carbon dioxide absorbent as described above in carbon dioxide desorption and / or carbon dioxide capture.

[0030] Furthermore, the carbon dioxide desorption step includes: electrolyzing the carbon dioxide absorbent to desorb carbon dioxide from the carbon dioxide absorbent;

[0031] The carbon dioxide capture process includes:

[0032] Obtain the carbon dioxide absorbent;

[0033] The carbon dioxide absorbent is electrolyzed to desorb the carbon dioxide from the absorbent.

[0034] The present invention also provides a carbon dioxide desorption device, wherein the anode chamber of the carbon dioxide desorption device contains a carbon dioxide absorbent as described above.

[0035] The present invention also provides a carbon dioxide capture system, which includes a carbon dioxide absorption device and a carbon dioxide desorption device;

[0036] The anode chamber of the carbon dioxide desorption device contains any of the carbon dioxide absorption liquids described above.

[0037] The anode chamber of the carbon dioxide desorption device is connected to the carbon dioxide absorption device to continuously or intermittently receive the carbon dioxide absorbent from the carbon dioxide absorption device.

[0038] Compared with the prior art, the present invention has at least the following advantages:

[0039] This invention proposes an organic amine-based carbon capture agent, which can reduce the volatility of the carbon capture agent by leveraging organic amines and avoid a significant increase in electrolysis energy consumption during carbon dioxide desorption over long-term operation. Moreover, by using organic amines as the carbon capture agent, this invention enables more stable operation of carbon dioxide capture, better cycle performance, lower maintenance costs, and is green, non-toxic, and environmentally friendly. Furthermore, the carbon capture agent provided by this invention, based on organic amines, can be compounded with amino acids, thereby expanding the applicability and compounding diversity of the carbon capture agent and providing a foundation for further optimization of carbon capture agents. Detailed Implementation

[0040] The technical solutions in the embodiments of the present invention will be clearly and completely described below. Obviously, the described embodiments are only a part of the embodiments of the present invention, and not all of them. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0041] Furthermore, the technical solutions of the various embodiments of the present invention can be combined with each other, but only if they are based on the ability of those skilled in the art to implement them. When the combination of technical solutions is contradictory or cannot be implemented, it should be considered that such combination of technical solutions does not exist and is not within the scope of protection claimed by the present invention.

[0042] It should be noted that, taking the inorganic ammonia (NH3) system as an example, the existing technology mainly includes the following four steps (see Figure 1 in Chinese Invention with Authorization Announcement No. CN113578025B for details):

[0043] 1. Desulfurization and deammoniation pretreatment

[0044] The ammonia released from the absorber after the scrubbing water is recovered is used for flue gas desulfurization, achieving the dual functions of desulfurization and ammonia removal. Previous studies have shown that this process has a high ammonia recovery rate (>99%), a low ammonia emission concentration (<25 ppmv), and a high SO2 removal rate (>99%).

[0045] 2. CO2 ammonia absorption (absorption tower)

[0046] The pretreated flue gas enters the CO2 absorption tower and is coupled with the metal ions (Me) after ammonia regeneration by electrodeposition. 2+)-Lean load / CO2-lean load ammonia solution contact decarbonization (reaction formula as follows), after collection Me 2+ -The lean / CO2-rich solution is sent to the anode chamber of the electrolytic cell.

[0047]

[0048] 3. Electrolytically coupled CO2 desorption (anode)

[0049] Metal ions have a significantly stronger coordination ability with ammonia than with CO2. In the anolyte chamber, electrochemically dissolved metal ions compete with CO2 for coordination with the amino group, thereby breaking the NH3-CO2 bond and releasing CO2 (reaction formula below). The desorbed Me... 2+ -The enriched / CO2-lean solution is sent to the cathode chamber of the electrolytic cell.

[0050]

[0051] Me (s) Transition metals such as zinc, copper, and nickel

[0052] 4. Ammonia regeneration coupled by electrodeposition (cathode)

[0053] In the cathode chamber, Me(NH3) n 2+ Electrodeposition is Me (s) (The reaction formula is as follows), which promotes ammonia regeneration. At this time, the solution becomes Me. 2 + -Low-load / CO2-Low-load solution.

[0054]

[0055] After ammonia regeneration, the catholyte returns to the CO2 absorber for the next carbon capture cycle. An anion exchange membrane exists between the catholyte and anolyte; a heat exchanger exists between the absorber and the electrolytic cell; and a flash tank exists in the path from the anolyte to the catholyte for gas-liquid separation. After a certain number of cycles, the anode and cathode exchange fluids, or the flow directions of the anolyte and catholyte alternate periodically, to prevent complete dissolution of the anode metal.

[0056] However, the aforementioned prior art has at least the following drawbacks:

[0057] 1. Inorganic ammonia is highly volatile (high saturated vapor pressure), resulting in significant losses, unstable operation, poor circulation performance, high maintenance costs, and is also toxic, polluting the environment.

[0058] 2. Inorganic ammonia volatilization recovery systems are complex, have lengthy processes, and high investment costs.

[0059] 3. Inorganic ammonia causes the energy consumption of carbon dioxide absorption liquid to increase significantly with long-term operation.

[0060] Based on this, the present invention provides an organic amine-based carbon capture agent for the absorption and / or capture of carbon dioxide. The carbon capture agent includes at least one of organic amines, mixtures of organic amines, and organic amine products.

[0061] In one instance, the carbon capture agent includes the organic amine, which refers to a class of nitrogen-containing compounds that have an amino group (-NH2, -NH, -N) generated by the chemical reaction of organic substances with ammonia. The organic amine in this invention typically has a pH greater than 7 and does not contain the amino acid.

[0062] In another embodiment, the organic amine mixture comprises the organic amine and a compounding agent, wherein the compounding agent comprises an amino acid. The present invention does not specifically limit the type of amino acid; exemplarily, the amino acid may include one or more of sarcosine, glycine, L-proline, and lysine.

[0063] It should be noted that, since the carbon capture agent is usually liquid, the carbon capture agent provided by the present invention may also contain the solvent, which is capable of dissolving the organic amine. The solvent may include or be water; of course, the organic amine may exist in the form of a solution.

[0064] It should also be noted that, since the organic ammonia and the amino acid can significantly reduce the volatility of the inorganic ammonia and significantly reduce the energy consumption of the inorganic ammonia in the carbon dioxide capture process, the compound agent may also include the inorganic ammonia in addition to the amino acid, thereby reducing the volatility and energy consumption of the inorganic ammonia in the carbon dioxide capture process.

[0065] Since there is a reaction process between the organic amine and the compounding agent, it can also be understood that the organic amine product includes the product after mixing the organic amine and the compounding agent; wherein, the mixing can be carried out in the solvent.

[0066] For example, referring to the following reaction formula, when the organic amine is present, the amino acid will be deprotonated.

[0067]

[0068] Of course, there may be other technical mechanisms in this invention that are not yet fully understood, such as the change process of organic amines and inorganic ammonia, but this does not affect the understanding of the technical solution and technical effect of this invention.

[0069] As a further explanation of the organic amine, the organic amine may, by way of example, include or be one or more of ethanolamine, aminoethylethanolamine, N-methyldiethanolamine, 2-amino-2-methylpropanol, diethylenetriamine, ethylenediamine, diethylamine, triethylenetetramine, and hydroxyethylethylenediamine.

[0070] In this invention, the concentration of the organic amine can be 0.2-8 mol / L, and more specifically 0.5-4 mol / L; that is, the concentration of the organic amine in the carbon scavenger can be 0.2-8 mol / L or 0.5-4 mol / L (the concentration of the organic amine after dissolving in the solvent), or the initial concentration of the organic amine in the carbon scavenger (or, if the compounding agent is present, the concentration before reaction) can be 0.2-8 mol / L or 0.5-4 mol / L.

[0071] When the compounding agent needs to be added to the carbon capture agent, the compounding agent can be mixed into the solution of the organic amine, or both the compounding agent and the organic amine can be mixed into the solvent; the molar ratio of the organic amine and the compounding agent can be 0.2-8:1, and more preferably 0.5-4:1.

[0072] Specifically, the molar ratio of the organic amine to the amino acid can be 0.2-8:1; when the compound agent simultaneously includes or is composed of the amino acid and the inorganic ammonia, the molar ratio of the organic amine to the amino acid can be 0.2-4:1, and the molar ratio of the organic amine to the inorganic ammonia can be 0.2-4:1.

[0073] Since the amino acid can also be deprotonated and activated by alkaline hydroxides and / or alkaline carbonates, when the compounding agent includes the amino acid, the compounding agent may also include a regulator, which may include alkaline hydroxides and / or alkaline carbonates; the molar ratio of the amino acid to the regulator may be 0.1-8:1, and more preferably 0.5-4:1.

[0074] Preferably, the alkaline hydroxide may include or be one or more of sodium hydroxide and potassium hydroxide; the alkaline carbonate compound may include or be an alkaline bicarbonate, specifically, the alkaline carbonate compound may include or be one or more of sodium bicarbonate and potassium bicarbonate.

[0075] Since the carbon dioxide capture involved in this invention involves carbon dioxide absorption and electrodesorption, in order to ensure the electrodesorption process, the carbon capture agent may also include a supporting electrolyte, such as potassium chloride.

[0076] The present invention also provides a method for preparing a carbon capture agent as described above, wherein the carbon capture agent is used for the absorption and / or capture of carbon dioxide. The preparation method comprises: mixing the organic amine and the compounding agent to obtain the carbon capture agent; the compounding agent includes the amino acid.

[0077] The carbon scavenger may be liquid, and the mixing may be carried out in the solvent, which typically includes or is water. In the embodiments and comparative examples of this invention, water is used as the solvent. Exemplarily, the organic amine may exist in solution form, i.e., the organic amine is dissolved in the solvent, and then the organic amine solution is mixed with the compounding agent to obtain the carbon scavenger.

[0078] The present invention also provides the application of the carbon capture agent as described in any of the above claims in carbon dioxide absorption and / or carbon dioxide capture.

[0079] It should be noted that the carbon dioxide absorption refers to the use of a carbon capture agent to absorb carbon dioxide gas into a carbon absorption liquid, thereby separating the carbon dioxide gas from other gases or substances in the gas to be treated.

[0080] The carbon dioxide capture refers to the following steps: first, carbon dioxide gas is absorbed into a carbon absorbent using a carbon capture agent; then, carbon dioxide is released by carbon dioxide desorption (e.g., electrodesorption), thereby completing the capture and recovery of carbon dioxide and obtaining carbon dioxide products.

[0081] For example, the carbon dioxide absorption step may include:

[0082] The carbon capture agent is contacted with the gas to be treated containing carbon dioxide (e.g., flue gas containing carbon dioxide) and absorbed to obtain a carbon dioxide absorbent liquid after carbon dioxide absorption.

[0083] Specifically, the process of contacting the carbon capture agent with the carbon dioxide-containing gas to be treated can be carried out in a carbon dioxide absorption device, specifically in a carbon absorption tower.

[0084] The carbon dioxide capture steps may include:

[0085] The carbon scavenger is contacted with and absorbed by the carbon dioxide-containing gas to obtain a carbon dioxide absorbent; then, the carbon dioxide absorbent is electrolyzed to desorb the carbon dioxide in the absorbent, resulting in an desorbed liquid and desorbed carbon dioxide; wherein the desorbed liquid contains the carbon scavenger, and the carbon scavenger in the desorbed liquid is bound with metal ions originating from the electrode.

[0086] Specifically, the process of contacting the carbon capture agent with the carbon dioxide-containing gas to be treated can be carried out in a carbon dioxide absorption device to generate a carbon dioxide absorbent liquid after absorbing carbon dioxide; then, the carbon dioxide absorbent liquid is transported to a carbon dioxide desorption device to release the carbon dioxide bound to the carbon capture agent by electrolysis, thereby realizing the capture and recovery of carbon dioxide.

[0087] As a further explanation of the carbon dioxide capture, the carbon dioxide capture step may further include: electrolyzing the desorption solution to cause the metal ions bound to the carbon capture agent to undergo electrodeposition, thereby obtaining the carbon capture agent separated from the metal ions.

[0088] It is important to understand that carbon dioxide release typically occurs in the anode chamber of a carbon dioxide desorption device. That is, the electrodes in the anode chamber undergo electrodissolution, then combine with the carbon scavenger in the carbon dioxide absorbent, thereby separating the carbon dioxide from the carbon scavenger, completing the release of carbon dioxide, and obtaining the desorbed liquid. This can be accomplished using an external gas-liquid separation device, or the gas-liquid separation of carbon dioxide and the desorbed liquid can be directly completed in the anode chamber.

[0089] Electrolysis of the desorption solution is usually carried out in the cathode chamber of a carbon dioxide desorption device; that is, electrodeposition of the desorption solution occurs in the cathode chamber, thereby depositing metal ions in the desorption solution onto the electrodes of the cathode chamber, completing the separation of the carbon scavenger and the metal ions; the separated carbon scavenger can be reused for carbon dioxide absorption, thereby reforming the carbon dioxide absorbent.

[0090] The present invention also provides a carbon dioxide absorption device, wherein the carbon dioxide absorption device includes a carbon scavenger as described in any of the above claims. The carbon scavenger may be pre-placed in the absorption chamber of the carbon dioxide absorption device; alternatively, the carbon scavenger may be supplied to the carbon dioxide absorption device from the outside during the carbon dioxide absorption process.

[0091] The present invention also provides a carbon dioxide capture system, which includes a carbon dioxide absorption device and a carbon dioxide desorption device.

[0092] The carbon dioxide absorption device includes a carbon capture agent as described in any of the above descriptions; the carbon dioxide absorption device and the carbon dioxide desorption device are connected to each other so as to continuously or intermittently transport the carbon dioxide absorbent generated in the carbon dioxide absorption device to the carbon dioxide desorption device, and the carbon dioxide desorption device has an electrolysis mechanism.

[0093] It should be noted that, since the carbon dioxide desorption device is an electrodesorption device, the anode chamber and cathode chamber contained therein can be interchanged due to the influence of electrical properties. Therefore, the carbon dioxide absorption device can be connected to the anode chamber of the carbon dioxide desorption device, or it can be connected to the cathode chamber of the carbon dioxide desorption device at the same time, in order to adapt to the electrodesorption of carbon dioxide after the electrical properties are converted.

[0094] It should also be noted that, since the desorbed liquid needs to be electrolyzed in the cathode chamber after being generated in the anode chamber of the carbon dioxide desorption device, the anode chamber and cathode chamber of the carbon dioxide desorption device can be connected to each other to facilitate the transport of the desorbed liquid.

[0095] The present invention also provides a carbon dioxide absorbent for desorption and / or capture of carbon dioxide; the carbon dioxide absorbent contains a carbon capture agent as described in any of the above claims, the carbon capture agent in the carbon dioxide absorbent is bound to carbon dioxide, and is typically obtained by the carbon capture agent absorbing carbon dioxide.

[0096] The present invention also provides an application of the carbon dioxide absorbent as described in any one of the above claims in carbon dioxide desorption and / or carbon dioxide capture. It should be understood that, during the desorption process of the carbon dioxide absorbent, the volatilization rate of the carbon capture agent can be significantly reduced, and the electrolysis energy consumption during the desorption process can be reduced.

[0097] For example, the carbon dioxide desorption step may include:

[0098] Electrolysis is performed on the carbon dioxide absorbent as described in any of the above claims to desorb carbon dioxide from the absorbent, thereby obtaining carbon dioxide gas and a desorbent, wherein the carbon scavenger in the desorbent contains metal ions.

[0099] During the electrolysis process, the carbon dioxide absorbent can be placed in the anode chamber of the carbon dioxide desorption device, and the previously desorbed solution can be placed in the cathode chamber of the same device. This allows for simultaneous desorption of carbon dioxide in the anode chamber and electrodeposition of metal ions in the cathode chamber, while also enabling the re-acquisition of the carbon capture agent. The electrolysis current density can be 1 A / m³. 2 -400A / m 2 .

[0100] The carbon dioxide capture process may include:

[0101] Obtain a carbon dioxide absorbent as described in any of the above descriptions; the carbon dioxide absorbent may be derived from a carbon dioxide absorption device.

[0102] The carbon dioxide absorbent is subjected to any of the electrolysis methods described above to desorb the carbon dioxide from the absorbent.

[0103] The present invention also provides a carbon dioxide desorption device, wherein the anode chamber of the carbon dioxide desorption device contains the carbon dioxide absorbent as described. The carbon dioxide absorbent in the anode chamber can be supplied continuously from an external source or intermittently from an external source. When the carbon dioxide absorbent is continuously supplied to the anode chamber, the supply of the carbon dioxide absorbent and the electrolysis of the carbon dioxide absorbent can be performed simultaneously; when the carbon dioxide absorbent is intermittently supplied to the anode chamber, the carbon dioxide absorbent can be supplied to the anode chamber first, and then the carbon dioxide absorbent can be electrolyzed.

[0104] As a further description of the carbon dioxide desorption device, the carbon dioxide desorption device is typically an electrodesorption device, having an anode chamber and a cathode chamber separated by an anion exchange membrane. The electrodes in the anode chamber and the cathode chamber may contain transition metals (such as Zn, Cu, Ni, etc.). The electrodes in the anode chamber and the cathode chamber are electrically electrolyzed with an external power source. A cover may also be provided above the anode chamber and the cathode chamber to prevent gas escape. The anode chamber and the cathode chamber may also have channels for liquid and / or gas transport, as well as corresponding valves.

[0105] The present invention also provides a carbon dioxide capture system, comprising a carbon dioxide absorption device and a carbon dioxide desorption device; the anode chamber of the carbon dioxide desorption device contains a carbon dioxide absorbent as described above; the anode chamber of the carbon dioxide desorption device and the carbon absorbent outlet of the carbon dioxide absorption device are connected to each other to continuously or intermittently receive the carbon dioxide absorbent from the carbon dioxide absorption device. Wherein, when the anode chamber of the carbon dioxide desorption device is adjusted, the adjusted anode chamber can also be directly connected to the carbon absorbent outlet of the carbon dioxide absorption device.

[0106] The following are specific examples of the present invention:

[0107] Comparative Example 1: Inorganic Ammonia (NH3) System

[0108] 1. Simulation device for carbon dioxide desorption:

[0109] The simulation device includes a first electrolysis chamber and a second electrolysis chamber. The first electrolysis chamber contains a first electrode, and the second electrolysis chamber contains a second electrode. Both the first and second electrodes are 7 cm long. 2The zinc plate has an electrode spacing of 2cm. Both the first and second electrodes are electrically connected to an external power source. When one electrolysis chamber is used as the anode chamber, the other electrolysis chamber is used as the cathode chamber. The first and second electrolysis chambers are separated by an anion exchange membrane, and the upper openings of both the first and second electrolysis chambers are sealed with the cover. Both the first and second electrolysis chambers are provided with carbon dioxide exhaust channels and electrolyte inlet and outlet channels.

[0110] 2. Preparation of anolyte and catholyte (M represents mol / L):

[0111] The anolyte in the anode chamber is a CO2-rich and zinc-poor solution (17.5 mL);

[0112] Anode solution composition: 0.2M Zn 2+ +1.2M CO2 + 2M ammonia + 2M potassium chloride.

[0113] The catholy solution located in the cathode chamber is a CO2-poor, zinc-rich solution (17.5 mL);

[0114] Cathodic solution composition: 0.7M Zn 2+ +0.5M CO2 + 2M ammonia + 2M potassium chloride.

[0115] 3. Simulation of electrolytic adsorption:

[0116] The prepared anolyte was used as the first electrolyte, and the prepared catholyte was used as the second electrolyte. Using the aforementioned simulation apparatus, the electrolyte was tested at 60°C and 100 A / m. 2 Constant current cyclic electrolysis is performed at a current density; the cyclic electrolysis is measured by the completion of the electrolysis of the first electrolyte in the cathode chamber.

[0117] The specific process of one cycle of electrolysis is as follows:

[0118] The first electrolyte was placed in the anode chamber, and the second electrolyte was placed in the cathode chamber. The mixture was subjected to an atmosphere of 60°C and 100 A / m. 2 The first electrolysis is carried out at a certain current density, thereby releasing carbon dioxide from the first electrolyte and causing zinc ions in the second electrolyte to electrodeposit. When the amount of CO2 discharged from the anode chamber reaches about 90% (at this time the carbon content of the solution is about 10% of the initial amount), the first electrolysis ends. After the first electrolysis is completed, the second electrolyte is used to absorb carbon dioxide until the carbon dioxide concentration reaches saturation (based on pH stability).

[0119] The second electrolyte was placed in the anode chamber, and the first electrolyte was placed in the cathode chamber, at 60°C and 100 A / m. 2The second electrolysis is carried out at a certain current density, thereby releasing carbon dioxide from the second electrolyte and causing zinc ions in the first electrolyte to electrodeposit. When the amount of CO2 discharged from the anode chamber reaches about 90% (at this time the carbon content of the solution is about 10% of the initial amount), the second electrolysis is ended. The first electrolyte is then subjected to carbon dioxide absorption until the carbon dioxide concentration reaches saturation (based on pH stability).

[0120] Then, subsequent cycles of electrolysis are performed.

[0121] The experimental results of this comparative example are as follows:

[0122] First cycle electrolysis: ammonia loss 5%, energy consumption 26kJ / molCO2;

[0123] Fifth cycle electrolysis: ammonia loss 28%, energy consumption 78kJ / molCO2;

[0124] The tenth cycle of electrolysis resulted in a 48% loss of ammonia and an energy consumption of 113 kJ / mol CO2.

[0125] Note: "Loss" refers to the amount of a corresponding component in the first electrolyte that is lost after electrolysis in the cathode chamber during this cycle of electrolysis, compared to its initial formulation (before the cycle of electrolysis).

[0126] "Energy consumption" refers to the power consumption generated by the first electrolyte in a single electrolysis in the cathode chamber during this electrolysis cycle.

[0127] Example 1: Ethanolamine

[0128] Compared to Comparative Example 1, this comparative example only replaced 2M ammonia in the anolyte with 2M ethanolamine and replaced 2M ammonia in the catholyte with 2M ethanolamine, while keeping other conditions unchanged.

[0129] Right now:

[0130] Anode solution composition: 0.2M Zn 2+ +1.2M CO2 + 2M ethanolamine + 2M potassium chloride;

[0131] Cathodic solution composition: 0.7M Zn 2+ +0.5M CO2 + 2M ethanolamine + 2M potassium chloride.

[0132] The experimental results of this embodiment are as follows:

[0133] First cycle electrolysis: ethanolamine loss 0.2%, energy consumption 42kJ / molCO2;

[0134] Fifth cycle electrolysis: ethanolamine loss 1.1%, energy consumption 45 kJ / mol CO2;

[0135] The tenth cycle of electrolysis resulted in a 2.3% loss of ethanolamine and an energy consumption of 47 kJ / mol CO2.

[0136] Example 2: Aminoethylethanolamine

[0137] Compared to Comparative Example 1, this embodiment only replaces 2M ammonia in the anolyte with 2M aminoethylethanolamine and 2M ammonia in the catholyte with 2M aminoethylethanolamine, while keeping other conditions unchanged.

[0138] Right now:

[0139] Anode solution composition: 0.2M Zn 2+ +1.2M CO2 + 2M aminoethylethanolamine + 2M potassium chloride;

[0140] Cathodic solution composition: 0.7M Zn 2+ +0.5M CO2 + 2M aminoethylethanolamine + 2M potassium chloride.

[0141] The experimental results of this embodiment are as follows:

[0142] First cycle electrolysis: loss of aminoethylethanolamine 0.001%, energy consumption 46 kJ / mol CO2;

[0143] Fifth cycle electrolysis: loss of aminoethylethanolamine 0.003%, energy consumption 48kJ / molCO2;

[0144] The tenth cycle of electrolysis resulted in a loss of 0.004% of aminoethylethanolamine and an energy consumption of 51 kJ / mol CO2.

[0145] Example 3: Diethylamine

[0146] Compared to Comparative Example 1, this embodiment only replaces 2M ammonia in the anolyte with 2M diethylamine and 2M ammonia in the catholyte with 2M diethylamine, while keeping other conditions unchanged.

[0147] Right now:

[0148] Anode solution composition: 0.2M Zn 2+ +1.2M CO2 + 2M diethylamine + 2M potassium chloride;

[0149] Cathodic solution composition: 0.7M Zn 2+ +0.5M CO2 + 2M diethylamine + 2M potassium chloride.

[0150] The experimental results of this embodiment are as follows:

[0151] First cycle electrolysis: Diethylamine loss 0.1%, energy consumption 68 kJ / mol CO2;

[0152] Fifth cycle electrolysis: Diethylamine loss 0.5%, energy consumption 72kJ / molCO2;

[0153] The tenth cycle of electrolysis resulted in a 0.9% loss of diethylamine and an energy consumption of 71 kJ / mol CO2.

[0154] Example 4: N-Methyldiethanolamine

[0155] Compared to Comparative Example 1, this embodiment only replaces 2M ammonia in the anolyte with 2M N-methyldiethanolamine and 2M ammonia in the catholyte with 2M N-methyldiethanolamine, while keeping other conditions unchanged.

[0156] Right now:

[0157] Anode solution composition: 0.2M Zn 2+ +1.2M CO2 + 2M N-methyldiethanolamine + 2M potassium chloride;

[0158] Cathodic solution composition: 0.7M Zn 2+ +0.5M CO2 + 2M N-methyldiethanolamine + 2M potassium chloride.

[0159] The experimental results of this embodiment are as follows:

[0160] First cycle electrolysis: N-methyldiethanolamine loss 0.001%, energy consumption 49 kJ / mol CO2;

[0161] Fifth cycle electrolysis: N-methyldiethanolamine loss 0.003%, energy consumption 52kJ / molCO2;

[0162] The tenth cycle of electrolysis resulted in a 0.005% loss of N-methyldiethanolamine and an energy consumption of 53 kJ / mol CO2.

[0163] Example 5: 2-Amino-2-methyl-propanol

[0164] Compared to Comparative Example 1, this embodiment only replaces 2M ammonia in the anolyte with 2M 2-amino-2-methyl-propanol and 2M ammonia in the catholyte with 2M 2-amino-2-methyl-propanol, while keeping other conditions unchanged.

[0165] Right now:

[0166] Anode solution composition: 0.2M Zn 2+ +1.2M CO2 + 2M 2-amino-2-methyl-propanol + 2M potassium chloride;

[0167] Cathodic solution composition: 0.7M Zn 2++0.5M CO2 + 2M 2-amino-2-methyl-propanol + 2M potassium chloride.

[0168] The experimental results of this embodiment are as follows:

[0169] First cycle electrolysis: 2-amino-2-methyl-propanol loss 0.001%, energy consumption 53 kJ / mol CO2;

[0170] Fifth cycle electrolysis: 2-amino-2-methyl-propanol loss 0.002%, energy consumption 57 kJ / mol CO2;

[0171] The tenth cycle of electrolysis resulted in a 0.005% loss of 2-amino-2-methyl-propanol and an energy consumption of 59 kJ / mol CO2.

[0172] Example 6: Aminethylethanolamine + sarcosine

[0173] Compared to Comparative Example 1, this embodiment only replaces the 2M ammonia in the anolyte with 1M aminoethylethanolamine + 1M sarcosine; and replaces the 2M ammonia in the catholyte with 1M aminoethylethanolamine + 1M sarcosine, while keeping other conditions unchanged.

[0174] Right now:

[0175] Anode solution composition: 0.2M Zn 2+ +1.2M CO2 + 1M aminoethylethanolamine + 1M sarcosine + 2M potassium chloride;

[0176] Cathodic solution composition: 0.7M Zn 2+ +0.5M CO2 +1M aminoethylethanolamine +1M sarcosine +2M potassium chloride.

[0177] The experimental results of this embodiment are as follows:

[0178] First cycle electrolysis: aminoethylethanolamine + sarcosine loss 0.002%, energy consumption 29kJ / molCO2;

[0179] Fifth cycle electrolysis: aminoethylethanolamine + sarcosine loss 0.008%, energy consumption 31kJ / molCO2;

[0180] The tenth cycle of electrolysis: aminoethylethanolamine + sarcosine resulted in a loss of 0.025% and an energy consumption of 29 kJ / mol CO2.

[0181] Example 7: Diethylamine + Sarcosine

[0182] Compared to Comparative Example 1, this embodiment only replaces the 2M ammonia in the anolyte with 2M diethylamine + 2M sarcosine; and replaces the 2M ammonia in the catholyte with 2M diethylamine + 2M sarcosine, while keeping other conditions unchanged.

[0183] Right now:

[0184] Anode solution composition: 0.2M Zn 2+ +1.2M CO2 + 2M diethylamine + 2M sarcosine + 2M potassium chloride;

[0185] Cathodic solution composition: 0.7M Zn 2+ +0.5M CO2 + 2M diethylamine + 2M sarcosine + 2M potassium chloride.

[0186] The experimental results of this embodiment are as follows:

[0187] First cycle electrolysis: Diethylamine + sarcosine loss 0.002%, energy consumption 31kJ / molCO2;

[0188] Fifth cycle electrolysis: Diethylamine + sarcosine loss 0.01%, energy consumption 32kJ / molCO2;

[0189] The tenth cycle of electrolysis resulted in a 0.03% loss of diethylamine and sarcosine, with an energy consumption of 29 kJ / mol CO2.

[0190] Example 8: Aminethylethanolamine + Glycine

[0191] Compared to Comparative Example 1, this embodiment only replaces 2M ammonia in the anolyte with 2M aminoethylethanolamine + 2M glycine; and replaces 2M ammonia in the catholyte with 2M aminoethylethanolamine + 2M glycine, while keeping other conditions unchanged.

[0192] Right now:

[0193] Anode solution composition: 0.2M Zn 2+ +1.2M CO2 + 2M aminoethylethanolamine + 2M glycine + 2M potassium chloride;

[0194] Cathodic solution composition: 0.7M Zn 2+ +0.5M CO2 + 2M aminoethylethanolamine + 2M glycine + 2M potassium chloride.

[0195] The experimental results of this embodiment are as follows:

[0196] First cycle electrolysis: aminoethylethanolamine + glycine loss 0.001%, energy consumption 41kJ / molCO2;

[0197] Fifth cycle electrolysis: aminoethylethanolamine + glycine loss 0.003%, energy consumption 44kJ / molCO2;

[0198] The tenth cycle of electrolysis: aminoethylethanolamine + glycine lost 0.005%, and the energy consumption was 43 kJ / mol CO2.

[0199] Example 9: Diethylamine + Glycine + Inorganic Ammonia

[0200] Compared to Comparative Example 1, this embodiment only replaces the 2M ammonia in the anolyte with 1M diethylamine + 1M glycine + 1M inorganic ammonia; and replaces the 2M ammonia in the catholyte with 1M diethylamine + 1M glycine + 1M inorganic ammonia, while keeping other conditions unchanged.

[0201] Anode solution composition: 0.2M Zn 2+ +1.2M CO2 + 1M diethylamine + 1M glycine + 1M inorganic ammonia + 2M potassium chloride;

[0202] Cathodic solution composition: 0.7M Zn 2+ +0.5M CO2 + 1M diethylamine + 1M glycine + 1M inorganic ammonia + 2M potassium chloride.

[0203] The experimental results of this embodiment are as follows:

[0204] First cycle electrolysis: diethylamine + glycine + inorganic ammonia loss 0.6%, energy consumption 37kJ / molCO2;

[0205] Fifth cycle electrolysis: diethylamine + glycine + inorganic ammonia, 3% loss, energy consumption 41kJ / molCO2;

[0206] The tenth cycle of electrolysis: diethylamine + glycine + inorganic ammonia resulted in a 5% loss and an energy consumption of 40 kJ / mol CO2.

[0207] Example 10: Aminoethylethanolamine + Glycine + Inorganic Ammonia

[0208] Compared to Comparative Example 1, this embodiment only replaces the 2M ammonia in the anolyte with 1M aminoethylethanolamine + 1M glycine + 1M inorganic ammonia; and replaces the 2M ammonia in the catholyte with 1M aminoethylethanolamine + 1M glycine + 1M inorganic ammonia, while keeping other conditions unchanged.

[0209] Anode solution composition: 0.2M Zn 2+ +1.2M CO2 + 1M aminoethylethanolamine + 1M glycine + 1M inorganic ammonia + 2M potassium chloride;

[0210] Cathodic solution composition: 0.7M Zn 2+ +0.5M CO2 + 1M aminoethylethanolamine + 1M glycine + 1M inorganic ammonia + 2M potassium chloride.

[0211] The experimental results of this embodiment are as follows:

[0212] First cycle electrolysis: aminoethylethanolamine + glycine + inorganic ammonia loss 0.5%, energy consumption 32kJ / molCO2;

[0213] Fifth cycle electrolysis: aminoethylethanolamine + glycine + inorganic ammonia, 2% loss, energy consumption 34kJ / molCO2;

[0214] The tenth cycle of electrolysis: aminoethylethanolamine + glycine + inorganic ammonia resulted in a 4% loss and an energy consumption of 41 kJ / mol CO2.

[0215] Example 11: Aminoethylethanolamine + L-proline + NaOH

[0216] Compared to Comparative Example 1, this embodiment only replaces the 2M ammonia in the anolyte with 2M aminoethylethanolamine + 2M L-proline + 2M sodium hydroxide; and replaces the 2M ammonia in the catholyte with 2M aminoethylethanolamine + 2M L-proline + 2M sodium hydroxide, while keeping other conditions unchanged.

[0217] Right now:

[0218] Anode solution composition: 0.2M Zn 2+ +1.2M CO2 + 2M aminoethylethanolamine + 2M L-proline + 2M sodium hydroxide + 2M potassium chloride;

[0219] Cathodic solution composition: 0.7M Zn 2+ +0.5M CO2 + 2M aminoethylethanolamine + 2M L-proline + 2M sodium hydroxide + 2M potassium chloride.

[0220] The experimental results of this embodiment are as follows:

[0221] First cycle electrolysis: aminoethylethanolamine + L-proline loss 0.005%, energy consumption 43kJ / molCO2;

[0222] Fifth cycle electrolysis: aminoethylethanolamine + L-proline loss 0.011%, energy consumption 46kJ / molCO2;

[0223] The tenth cycle of electrolysis resulted in a loss of 0.019% for aminoethylethanolamine and L-proline, with an energy consumption of 48 kJ / mol CO2.

[0224] Example 12: Aminethylethanolamine + Glycine + Lysine

[0225] Compared to Comparative Example 1, this embodiment only replaces the 2M ammonia in the anolyte with 1M aminoethylethanolamine + 1M glycine + 1M lysine; and replaces the 2M ammonia in the catholyte with 1M aminoethylethanolamine + 1M glycine + 1M lysine, while keeping other conditions unchanged.

[0226] Anode solution composition: 0.2M Zn 2+ +1.2M CO2 + 1M aminoethylethanolamine + 1M glycine + 1M lysine + 2M potassium chloride;

[0227] Cathodic solution composition: 0.7M Zn 2+ +0.5M CO2 +1M aminoethylethanolamine +1M glycine +1M lysine +2M potassium chloride.

[0228] The experimental results of this embodiment are as follows:

[0229] First cycle electrolysis: aminoethylethanolamine + glycine + lysine loss 0.003%, energy consumption 33kJ / molCO2;

[0230] Fifth cycle electrolysis: aminoethylethanolamine + glycine + lysine loss 0.006%, energy consumption 36kJ / molCO2;

[0231] The tenth cycle of electrolysis resulted in a loss of 0.012% for aminoethylethanolamine + glycine + lysine, with an energy consumption of 37 kJ / mol CO2.

[0232] The above technical solutions of the present invention are merely preferred embodiments of the present invention and do not limit the patent scope of the present invention. All equivalent structural transformations made using the present invention specification under the technical concept of the present invention, or direct / indirect applications in other related technical fields, are included in the patent protection scope of the present invention.

Claims

1. An application of a carbon scavenger in carbon dioxide capture, characterized in that, The carbon dioxide capture step includes: contacting the carbon capture agent with the gas to be treated containing carbon dioxide and absorbing it to obtain a carbon dioxide absorption liquid; The carbon dioxide absorbent is electrolyzed to desorb the carbon dioxide in the absorbent, resulting in an desorbed solution and desorbed carbon dioxide. The desorbed solution contains the carbon scavenger, which is bound to metal ions from the electrode. The desorbed solution is then electrolyzed to cause the metal ions bound to the carbon scavenger to undergo electrodeposition, resulting in the carbon scavenger separated from the metal ions. The method for preparing the carbon capture agent includes: The carbon capture agent is obtained by mixing an organic amine and a compounding agent; wherein the compounding agent includes amino acids; The organic amine includes at least one of aminoethylethanolamine and diethylamine; the amino acid includes at least one of sarcosine, glycine, L-proline, and lysine.

2. The application according to claim 1, characterized in that, The concentration of the organic amine is 0.2-8 mol / L.

3. The application according to claim 1, characterized in that, The molar ratio of the organic amine to the compounding agent is 0.2-8:

1.

4. The application according to claim 1, characterized in that, The compound agent also includes a regulator, which includes an alkaline hydroxide and / or an alkaline carbonate compound; the molar ratio of the amino acid to the regulator is 0.1-8:

1.

5. The application according to any one of claims 1-4, characterized in that, The carbon capture agent also includes a supporting electrolyte.

6. The application of a carbon dioxide absorbent in carbon dioxide desorption, characterized in that, The carbon dioxide absorbent contains a carbon trapping agent, and the carbon trapping agent is bound to carbon dioxide; The carbon dioxide desorption includes: electrolyzing the carbon dioxide absorbent to desorb carbon dioxide from the absorbent, obtaining a desorbed solution and desorbed carbon dioxide, wherein the desorbed solution contains the carbon scavenger, and the carbon scavenger is bound with metal ions from the electrode; electrolyzing the desorbed solution to cause the metal ions bound with the carbon scavenger to undergo electrodeposition, thereby obtaining the carbon scavenger separated from the metal ions; The method for preparing the carbon capture agent includes: The carbon capture agent is obtained by mixing an organic amine and a compounding agent; wherein the compounding agent includes amino acids; The organic amine includes at least one of aminoethylethanolamine and diethylamine; the amino acid includes at least one of sarcosine, glycine, L-proline, and lysine.

7. The application according to claim 6, characterized in that, The concentration of the organic amine is 0.2-8 mol / L.

8. The application according to claim 6, characterized in that, The molar ratio of the organic amine to the compounding agent is 0.2-8:

1.

9. The application according to claim 6, characterized in that, The compound agent also includes a regulator, which includes an alkaline hydroxide and / or an alkaline carbonate compound; the molar ratio of the amino acid to the regulator is 0.1-8:

1.

10. The application according to any one of claims 6-9, characterized in that, The carbon capture agent also includes a supporting electrolyte.

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