CN110813059A - Method for reducing regeneration energy consumption of carbon dioxide capture solvent - Google Patents

Method for reducing regeneration energy consumption of carbon dioxide capture solvent Download PDF

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Publication number
CN110813059A
CN110813059A CN201810916391.XA CN201810916391A CN110813059A CN 110813059 A CN110813059 A CN 110813059A CN 201810916391 A CN201810916391 A CN 201810916391A CN 110813059 A CN110813059 A CN 110813059A
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carbon dioxide
solution
precipitator
amine
precipitant
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毛松柏
郭本帅
叶宁
汪东
陈曦
季燕
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China Petroleum and Chemical Corp
Research Institute of Sinopec Nanjing Chemical Industry Co Ltd
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China Petroleum and Chemical Corp
Research Institute of Sinopec Nanjing Chemical Industry Co Ltd
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • B01D53/78—Liquid phase processes with gas-liquid contact
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/62—Carbon oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2

Abstract

The invention belongs to the technical field of gas separation, and relates to a method for regenerating a carbon dioxide capture alcohol amine solvent without an external heat source. The method provided by the invention does not need an external heat source in the regeneration process, can obviously reduce the energy consumption required by regeneration, can save the equipment investment and the operation cost of a barren solution pump and a barren solution cooler, and has good application prospect in the field of carbon dioxide capture.

Description

Method for reducing regeneration energy consumption of carbon dioxide capture solvent
Technical Field
The invention belongs to the technical field of gas separation, and particularly relates to a method for regenerating a carbon dioxide capture solvent without an external heat source.
Background
With the increasing demand for fossil energy by humans, large amounts of carbon dioxide are emitted into the atmosphere. Carbon dioxide is one of the most important greenhouse gases, and its large emissions can cause severe disruptions in the earth's climate and ecosystem balance. Thus, carbon dioxide abatement has attracted general attention. An important approach to reducing carbon dioxide emissions is to capture carbon dioxide from the primary emission source. Therefore, the development of advanced carbon dioxide capture technology has become a research hotspot in the field of carbon emission reduction.
Currently, absorption is the most mature and widely used carbon dioxide technology. The alcohol amine is the most common solvent for absorption method, which utilizes the chemical reaction of alcohol amine molecules and carbon dioxide to separate the carbon dioxide in the raw material gas, and then the reaction is reversely carried out by heating, so that the carbon dioxide is separated from the solution, and the alcohol amine solution is regenerated for recycling. Energy consumption is one of main factors for limiting popularization of the carbon dioxide capturing technology by the alcohol amine absorption method, and the key point of developing the advanced carbon dioxide capturing technology by the alcohol amine method is to reduce process energy consumption.
In the alcohol amine method carbon dioxide capture technology, the regeneration energy consumption is the most important part of the energy consumption of the whole process and accounts for about 70 percent of the energy consumption of the process. In order to reduce the energy consumption for regeneration of the carbon dioxide capture solvent, various novel solvents and regeneration methods have been developed.
Patent CN101612509A discloses a composite decarbonization solution for capturing carbon dioxide in mixed gas, which is composed of main absorption components MEA, AEE, absorption-aiding components AHPD, AMP, TEA and MDEA, active components PZ, HEPZ, AEP and DEA, corrosion inhibitor sodium vanadate, antioxidant sodium sulfite and copper acetate, mixed solvents NMP, polyethylene glycol and propylene carbonate and water. The composite decarbonization solution improves the absorption capacity, the purification degree and the desorption rate, enlarges the reaction temperature range and greatly reduces the regeneration energy consumption.
Patent CN101537340 discloses a flue gas CO2The absorbent adopts monoethanolamine as a main component, and contains N-methyldiethanolamine, steric hindrance amine or piperazine to form a mixed solvent. The decarbonization solvent is suitable for decarbonization of flue gas of coal-fired power plant flue gas, industrial kiln gas and the like. The solvent has the following advantages: the method has the advantages of high flue gas purification degree, large absorption capacity, high regeneration desorption degree, low desorption regeneration energy consumption, less solution degradation and consumption, small corrosion to equipment and the like, and can be widely used for carbon dioxide separation of flue gas of coal-fired power plant flue gas, industrial kiln gas and the like.
Patent CN101804287 discloses an absorbent for capturing or separating carbon dioxide from a gas mixture, mainly comprising the following components in percentage by weight: n-ethylethanolamine: 10wt% -50 wt%; sulfolane: 10wt% -40 wt%; water: and (4) the balance. The absorbent uses N-ethylethanolamine as an effective component, and because the N-ethylethanolamine has high solubility to low-pressure carbon dioxide, the desorption effect is good, and meanwhile, the reaction heat of the absorption reaction is low, and the energy consumption for capturing and separating the carbon dioxide is low; meanwhile, sulfolane has the effects of improving desorption effect and reducing volatilization of water, and can further reduce desorption energy consumption. The absorbent can be used to capture or separate carbon dioxide from various gas mixtures, including flue gases, refinery gases, natural gases, synthesis gases, shift gases, and hydrogen production, among others.
In patent CN102049173, a method for deeply removing carbon dioxide from a gas mixture is disclosed, wherein a composite amine aqueous solution is adopted as an absorbent, and the concentration of total amine in the absorbent is 20-50% by weight; the compound amine comprises: the main absorbent is MDEA, and the content of the MDEA accounts for 70-90% of the total amine concentration; the auxiliary absorbent is two of HEP, DMAP and DMAE, and accounts for 10-30% of the total amine concentration. The examples show that the absorbent disclosed in this patent has an absorption performance comparable to that of MEA, but the regeneration energy consumption is reduced by 25%.
Patent CN102553396 discloses a method for capturing carbon dioxide in flue gas of a power station with high efficiency and low energy consumption and equipment thereof, and the method comprises the following steps: 1) taking a composite absorbent aqueous solution consisting of organic amine and functionalized ionic liquid as CO2An absorbent; 2) standing to clarify to form different liquid layers; 3) will be separated to be rich in A.CO2And B. CO2The liquid is heated and analyzed, and high-concentration CO is obtained by regeneration2Gas and composite absorbent aqueous solution; 4) continuously recycling the composite absorbent aqueous solution obtained in the step 3); 5) for high concentration CO2Cooling the gas to condense hot water vapor contained in the gas; 6) for the high concentration CO cooled in the step 5)2Gas is subjected to gas-liquid separation treatment to obtain CO with the purity of more than or equal to 99 percent2A gas; 7) high purity CO2The gas is changed into liquid state, and a high-concentration industrial-grade liquid carbon dioxide finished product is prepared. The examples show that regeneration energy consumption can be reduced by 30% compared with the conventional MEA process by using the method disclosed in the patent.
Patent CN102350180 discloses a regeneration system of a flue gas carbon dioxide capture solution, which comprises a regeneration tower communicated with an absorption tower, a reboiler communicated with the lower part of one side of the regeneration tower, and a gas-liquid separator communicated with the bottom of the regeneration tower, wherein the bottom of the gas-liquid separator is communicated with the absorption tower, the top of the gas-liquid separator is communicated with a gas pump, and the gas pump is communicated with the lower part of the other side of the regeneration tower; the regeneration system can be used in the fields of coal-fired power plant boilers and chemical engineering, has the characteristics of fully utilizing the waste heat of the regeneration solution and utilizing the carbon dioxide to be released more easily under lower pressure, improves the resolution ratio of the carbon dioxide and the regeneration degree of the solution, and reduces the regeneration energy consumption of unit carbon dioxide capture.
Patent CN103638780 discloses a system and method for strengthening regeneration of carbon dioxide capture solution, the system includes a regeneration tower, a reboiler, an ultrasonic generator panel, an ultrasonic controller, a pressure sensor, a liquid level sensor and a temperature sensor, the rich solution from the absorption tower enters from the top of the regeneration tower to flow to the bottom, enters into the reboiler at the lower part to absorb heat and then returns to the regeneration tower, the solution submerges the ultrasonic generator panel, according to the liquid level information detected by the liquid level sensor, a vibrator located below the liquid level of the ultrasonic generator panel is started to work, the escape of carbon dioxide from the liquid phase is promoted through ultrasonic cavitation, the carbon dioxide rises to the upper part of the regeneration tower to form pressure, according to the pressure and temperature values detected by the pressure sensor and the temperature sensor, the ultrasonic controller modulates the output frequency and power of the vibrator on the ultrasonic generator panel, and the method can accelerate the escape of carbon dioxide, the desorption temperature is reduced, the external steam consumption is reduced, the desorption rate of the carbon dioxide and the regeneration degree of the solution are improved, and the energy consumption of the unit carbon dioxide is reduced.
Patent CN105032123 discloses a middle-low temperature regeneration carbon dioxide capture absorbent and a use method thereof, wherein the absorbent comprises the following components: low-temperature amine regeneration: 10-50%, pH regulator: 56-25%, 0-10% of an auxiliary agent, and water: and (4) the balance. When the absorption tower is used, a low-temperature regenerated carbon dioxide absorbent in the absorption tower reacts with a gas containing carbon dioxide to form a rich solution, the absorption temperature is 30-50 ℃, the pressure of the absorption tower is 0.05-6 MPa, the rich solution is preheated by a lean-rich solution heat exchanger, a part of carbon dioxide gas is flashed, the flashed rich solution enters the regeneration tower to be pyrolyzed at a low temperature, the lean solution is regenerated to generate carbon dioxide, the bottom temperature of the regeneration tower is 70-100 ℃, the hot lean solution generated by the regeneration tower is sent to the absorption tower through the heat exchanger to be used for capturing the carbon dioxide, and the whole absorption-regeneration-absorption cycle is completed.
However, whether new solvents are developed or various means are used to enhance the regeneration process, the regeneration reaction is carried out under heated conditions, requiring additional energy input. The invention introduces the precipitator which can carry out mineralization reaction with the carbon dioxide in the alcohol amine rich solution, so that the alcohol amine rich solution is regenerated without an external heating source, thereby obviously reducing the energy consumption required by the regeneration process.
Disclosure of Invention
The invention aims to provide a method for reducing the energy consumption for regenerating a carbon dioxide capture solvent.
The method does not carry out conventional thermal regeneration on the alcohol amine solvent which collects the carbon dioxide in the flue gas, but adds a certain amount of precipitator and auxiliary precipitator into the alcohol amine solvent to carry out mineralization reaction with the carbon dioxide in the alcohol amine rich solution to generate solid precipitate which is separated, so that the rich solution is regenerated without an external heating source, and simultaneously the carbon dioxide is mineralized and fixed.
In the method provided by the invention, the used precipitator contains elements capable of carrying out mineralization reaction with carbon dioxide, including one or two of calcium and magnesium.
In the method provided by the invention, the used precipitator is a compound containing elements capable of generating mineralization reaction with carbon dioxide, and comprises one or two of oxides and hydroxides.
In the method provided by the invention, the phase state of the used precipitating agent can be a solid phase or a solid phase aqueous solution.
In the method provided by the invention, the molar ratio of elements capable of generating mineralization reaction with carbon dioxide in the used precipitator to the carbon dioxide in the pregnant solution is 0.5-0.8.
In the method provided by the invention, the used co-precipitant is Na2CO3、NaHCO3、K2CO3、KHCO3And the like.
In the method provided by the invention, the molar ratio of the used co-precipitant to the precipitant is 0.001-0.01.
In the method provided by the invention, the used carbon dioxide capture solvent is a solvent containing alkylol amine, and comprises an aqueous solution, a non-aqueous solution and a phase-change absorption liquid containing the alkylol amine.
In the method provided by the invention, the alkyl alcohol amine used comprises one or more of Monoethanolamine (MEA), Diethanolamine (DEA), Triethanolamine (TEA), Diisopropanolamine (DIPA), N-Methyldiethanolamine (MDEA) and steric hindered amine.
In the method provided by the invention, substances generated by the mineralization reaction can be separated from the regenerated alcohol amine solution by a filtering mode.
The invention discloses a method for reducing the regeneration energy consumption of a carbon dioxide capture solvent, which comprises the following typical process steps: mixing the alcohol amine-rich solvent absorbing carbon dioxide with a certain amount of precipitator and auxiliary precipitator, pumping the mixture into a regeneration reactor by using a rich solution pump, carrying out mineralization reaction on carbon dioxide in the alcohol amine rich solution and the precipitator under the stirring action, feeding the solution containing solid suspended matters into a plate-frame filter after the reaction, circulating the filtered liquid which is regenerated alcohol amine barren solution to an absorption tower for absorbing carbon dioxide again, and obtaining a filter cake which is mineralized carbon dioxide after the filtration and can be directly sealed or further processed into other products. The plate frame filter can be switched to use by multiple groups, so that the filtering operation is in a continuous state.
In the method provided by the present invention, carbon dioxide can be solidified while the carbon dioxide capturing solvent is regenerated.
In the method provided by the invention, an external heat source is not needed for the regeneration reaction, and the temperature of the regeneration reaction is determined by the reaction heat of the carbon dioxide mineralization reaction and the solution heat of the precipitator and the precipitation aid.
In the method provided by the invention, the regeneration reaction does not need to be carried out under normal pressure or low pressure, and the pressure of the regeneration reaction can be determined by the lift provided by the pregnant solution pump.
Compared with the traditional thermal regeneration process flow, the method provided by the invention needs to consume a certain amount of precipitator and precipitating aid, and needs to be additionally provided with a plate-frame filter, but has the following advantages:
(1) an external heating source is not needed in the regeneration process, the energy consumption required by regeneration can be obviously reduced, and the theoretical regeneration energy consumption is 0;
(2) the regeneration process can be carried out under pressurization, and the circulation of the barren solution can be carried out without a barren solution pump, so that the equipment investment and the pump running cost can be reduced;
(3) the temperature of the regenerated barren solution is lower, and the barren solution does not need to be cooled by a barren solution cooler, so that the equipment investment and the cooling water consumption can be reduced.
Drawings
FIG. 1 is a schematic process flow diagram of a method according to an embodiment of the present invention.
In the figure, 1-a pregnant solution tank, 2-a precipitant and non-precipitant feed ports, 3-a barren solution pump, 4-a regeneration reactor, 5-a filter, and 6-a barren solution tank.
Detailed Description
The invention is further illustrated by the following examples and figures.
The processes in the following examples are shown in FIG. 1. Mixing the alcohol amine-rich solvent absorbing carbon dioxide with a certain amount of precipitator and auxiliary precipitator, pumping the mixture into a regeneration reactor by using a rich solution pump, carrying out mineralization reaction on carbon dioxide in the alcohol amine rich solution and the precipitator under the stirring action, feeding the solution containing solid suspended matters into a plate-frame filter after the reaction, circulating the filtered liquid which is regenerated alcohol amine barren solution to an absorption tower for absorbing carbon dioxide again, and obtaining a filter cake which is mineralized carbon dioxide after the filtration and can be directly sealed or further processed into other products. The plate frame filter can be switched to use by multiple groups, so that the filtering operation is in a continuous state.
Example 1
The method of the embodiment has the following steps:
(1) preparing 30% MEA water solution (MEA: 30w%, water for the rest) by mass fraction, and performing absorption saturation (absorption capacity of 0.54mol CO) by using carbon dioxide2Mol amine) to obtain a rich solution, and placing the rich solution in a rich solution tank;
(2) preparing a certain amount of mixture of a precipitator and a co-precipitator, wherein the precipitator uses calcium hydroxide, the co-precipitator uses sodium bicarbonate, and the molar ratio of the sodium bicarbonate to the calcium hydroxide is 0.003;
(3) mixing a mixture of a precipitator and a co-precipitator with a rich solution, and then sending the rich solution into a regeneration reactor by using a rich solution pump, wherein the molar ratio of the precipitator to carbon dioxide in the rich solution is 0.6;
(3) feeding the solution after reaction into a plate-frame filter;
(4) after a period of operation, formation of a filter cake was observed, and the acid gas loading of the solution obtained after filtration was 0.32mol CO2Per mol of amine.
Example 2
The method of the embodiment has the following steps:
(1) preparing 30% MEA water solution (MEA: 30w%, water for the rest) by mass fraction, and performing absorption saturation (absorption capacity of 0.54mol CO) by using carbon dioxide2Mol amine) to obtain a rich solution, and placing the rich solution in a rich solution tank;
(2) preparing a certain amount of mixture of a precipitator and a co-precipitator, wherein the precipitator uses calcium oxide, the co-precipitator uses potassium bicarbonate, and the molar ratio of the potassium bicarbonate to the calcium oxide is 0.006;
(3) mixing a mixture of a precipitator and a co-precipitator with a rich solution, and then sending the rich solution into a regeneration reactor by using a rich solution pump, wherein the molar ratio of the precipitator to carbon dioxide in the rich solution is 0.8;
(3) feeding the solution after reaction into a plate-frame filter;
(4) after a period of operation, formation of a filter cake was observed, and the acid gas loading of the solution obtained after filtration was 0.26mol CO2Per mol of amine.
Example 3
The method of the embodiment has the following steps:
(1) preparing 30% MEA water solution (MEA: 30w%, water for the rest) by mass fraction, and performing absorption saturation (absorption capacity of 0.54mol CO) by using carbon dioxide2Mol amine) to obtain a rich solution, and placing the rich solution in a rich solution tank;
(2) preparing a certain amount of a mixture of a precipitator and a co-precipitator, wherein the precipitator is a mixture of calcium oxide and magnesium oxide (the molar ratio of calcium oxide to magnesium oxide is 5: 1), the co-precipitator is a mixture of potassium bicarbonate and potassium carbonate (the molar ratio of potassium bicarbonate to potassium carbonate is 4: 1), and the molar ratio of the co-precipitator to the precipitator is 0.001;
(3) mixing a mixture of a precipitator and a co-precipitator with a rich solution, and then sending the rich solution into a regeneration reactor by using a rich solution pump, wherein the molar ratio of the precipitator to carbon dioxide in the rich solution is 0.5;
(3) feeding the solution after reaction into a plate-frame filter;
(4) after a period of operation, formation of a filter cake was observed, and the acid gas loading of the solution obtained after filtration was 0.24mol CO2Per mol of amine.
Example 4
The method of the embodiment has the following steps:
(1) preparing a composite amine aqueous solution (15 w percent of MEA, 10w percent of MDEA, 5w percent of steric hindrance amine and the balance of water) with the mass fraction of 30 percent, and carrying out absorption saturation by using carbon dioxide (the absorption capacity is 0.48mol of CO)2Mol amine) to obtain a rich solution, and placing the rich solution in a rich solution tank;
(2) preparing a certain amount of mixture of a precipitator and a co-precipitator, wherein the precipitator uses calcium oxide, the co-precipitator uses potassium bicarbonate, and the molar ratio of the potassium bicarbonate to the calcium oxide is 0.005;
(3) mixing a mixture of a precipitator and a co-precipitator with a rich solution, and then sending the rich solution into a regeneration reactor by using a rich solution pump, wherein the molar ratio of the precipitator to carbon dioxide in the rich solution is 0.8;
(3) feeding the solution after reaction into a plate-frame filter;
(4) after a period of operation, formation of a filter cake was observed, and the acid gas loading of the solution obtained after filtration was 0.12mol CO2Per mol of amine.
Example 5
The method of the embodiment has the following steps:
(1) preparing a composite amine aqueous solution (MEA 15w%, DIPA 7.5w%, sterically hindered amine 7.5w%, and water in balance) with a mass fraction of 30%, and performing absorption saturation with carbon dioxide (absorption capacity of 0.55mol CO)2Mol amine) to obtain a rich solution, and placing the rich solution in a rich solution tank;
(2) preparing a certain amount of mixture of a precipitator and a co-precipitator, wherein the precipitator uses calcium oxide, the co-precipitator uses sodium bicarbonate, and the molar ratio of the sodium bicarbonate to the calcium oxide is 0.004;
(3) mixing a mixture of a precipitator and a co-precipitator with a rich solution, and then sending the rich solution into a regeneration reactor by using a rich solution pump, wherein the molar ratio of the precipitator to carbon dioxide in the rich solution is 0.7;
(3) feeding the solution after reaction into a plate-frame filter;
(4) after a period of operation, formation of a filter cake was observed, and the acid gas loading of the solution obtained after filtration was 0.21mol CO2Per mol of amine.
Example 6
The method of the embodiment has the following steps:
(1) preparing a composite amine aqueous solution (15 w percent of MEA, 15w percent of steric hindrance amine and the balance of water) with the mass fraction of 30 percent, and absorbing and saturating the composite amine aqueous solution by using carbon dioxide (the absorption capacity is 0.52mol of CO)2Mol amine) to obtain a rich solution, and placing the rich solution in a rich solution tank;
(2) preparing a certain amount of a mixture of a precipitator and a co-precipitator, wherein the precipitator is a mixture of calcium oxide and magnesium oxide (the molar ratio of calcium oxide to magnesium oxide is 4: 1), the co-precipitator is a mixture of potassium bicarbonate and sodium bicarbonate (the molar ratio of potassium bicarbonate to sodium bicarbonate is 1: 1), and the molar ratio of the co-precipitator to the precipitator is 0.006;
(3) mixing a mixture of a precipitator and a co-precipitator with a rich solution, and then sending the rich solution into a regeneration reactor by using a rich solution pump, wherein the molar ratio of the precipitator to carbon dioxide in the rich solution is 0.6;
(3) feeding the solution after reaction into a plate-frame filter;
(4) after a period of operation, formation of a filter cake was observed, and the acid gas loading of the solution obtained after filtration was 0.23mol CO2Per mol of amine.
Example 7
The method of the embodiment has the following steps:
(1) preparing 30% MEA non-aqueous solution (MEA: 30%; the rest is polyethylene glycol) by mass fraction, and performing absorption saturation with carbon dioxide (absorption capacity is 0.52mol CO)2Mol amine) to obtain a rich solution, and placing the rich solution in a rich solution tank;
(2) preparing a certain amount of mixture of a precipitator and a co-precipitator, wherein the precipitator uses calcium oxide, the co-precipitator uses sodium bicarbonate, and the molar ratio of the sodium bicarbonate to the calcium oxide is 0.01;
(3) mixing a mixture of a precipitator and a co-precipitator with a rich solution, and then sending the rich solution into a regeneration reactor by using a rich solution pump, wherein the molar ratio of the precipitator to carbon dioxide in the rich solution is 0.5;
(3) feeding the solution after reaction into a plate-frame filter;
(4) after a period of operation, formation of a filter cake was observed, and the acid gas loading of the solution obtained after filtration was 0.28mol CO2Per mol of amine.
Comparative example 1
The process of the comparative example has the following steps:
(1) preparing 30% MEA water solution (MEA: 30%; the rest is polyethylene glycol) by mass fraction, and performing absorption saturation with carbon dioxide (absorption capacity is 0.54mol CO)2Mol amine) to obtain a rich solution, and placing the rich solution in a rich solution tank;
(2) feeding the rich solution into the regeneration reactor by using a rich solution pump;
(3) feeding the solution after reaction into a plate-frame filter;
(4) after a period of operation, no formation of a filter cake was observed, and the acid gas loading of the solution obtained after filtration was 0.53mol CO2Per mol of amine.

Claims (10)

1. A method for reducing the energy consumption for regenerating the carbon dioxide trapping solvent features that the alcohol amine solvent for trapping carbon dioxide in fume is used to regenerate the rich liquid without external heat source and the carbon dioxide is mineralized and fixed.
2. The method as set forth in claim 1, characterized in that the precipitant used contains an element capable of mineralizing with carbon dioxide, the element being one or both of calcium and magnesium.
3. The method as set forth in claim 2, characterized in that the precipitant used is a compound containing an element capable of undergoing a mineralization reaction with carbon dioxide, said compound being one or both of an oxide and a hydroxide.
4. A process according to claim 2 or 3, characterized in that the precipitant used is in the form of a solid phase or an aqueous solution of a solid phase.
5. The method as claimed in claim 1 or 2, wherein the molar ratio of the element capable of mineralizing with carbon dioxide in the precipitant to carbon dioxide in the pregnant solution is 0.5-0.8.
6. The process as claimed in claim 1, wherein the precipitant aid used is Na2CO3、NaHCO3、K2CO3、KHCO3One or more of (a).
7. The method according to claim 1 or 6, wherein the molar ratio of the co-precipitant to the precipitant is 0.001-0.01.
8. The method according to claim 1, wherein the carbon dioxide capture solvent used is an alkylol amine-containing solvent, and the alkylol amine-containing solvent is an aqueous solution, a non-aqueous solution, or a phase-change absorbent solution containing an alkylol amine.
9. A process according to claim 8, characterized in that the alkanolamines used comprise one or more of Monoethanolamine (MEA), Diethanolamine (DEA), Triethanolamine (TEA), Diisopropanolamine (DIPA), N-Methyldiethanolamine (MDEA), sterically hindered amines.
10. The method as set forth in claim 1, characterized in that the substances produced by the mineralization reaction are separated from the regenerated alcohol amine solution by means of filtration.
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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112892160A (en) * 2021-02-22 2021-06-04 浙江大学 Phase change absorbent and application thereof in carbon dioxide capture
CN114870587A (en) * 2022-05-05 2022-08-09 北京金隅水泥节能科技有限公司 Industrial flue gas carbon dioxide trapping agent and preparation method thereof

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1583570A (en) * 2004-06-14 2005-02-23 上海华明高技术（集团）有限公司 Method for manufacturing super fine calcium carbonate dispersing particles
CN1631789A (en) * 2003-12-24 2005-06-29 上海华明高技术（集团）有限公司 Method for preparing nano calcium carbonate particle
CN101209851A (en) * 2007-12-24 2008-07-02 上海东升新材料有限公司 Method for manufacturing rice-shaped precipitated calcium carbonate
CN101591029A (en) * 2008-05-28 2009-12-02 北京紫光英力化工技术有限公司 Causticizing process prepares the novel process of caustic soda and super fine calcium carbonate
CN101700901A (en) * 2009-11-25 2010-05-05 王冬生 Novel method for producing light calcium carbonate (CaCO3) from white clay generated from alkali recovering in paper-making industry
CN102126736A (en) * 2011-01-19 2011-07-20 刘先黎 Method for preparing nano-calcium carbonate powder by using soluble carbonate
CN103950965A (en) * 2014-04-29 2014-07-30 东华大学 Method for preparing nano-calcium carbonate with different sizes by applying seed crystal method
CN107149851A (en) * 2017-07-18 2017-09-12 华东交通大学 One kind is desorbed and CO in fixed monoethanolamine rich solution2New method

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1631789A (en) * 2003-12-24 2005-06-29 上海华明高技术（集团）有限公司 Method for preparing nano calcium carbonate particle
CN1583570A (en) * 2004-06-14 2005-02-23 上海华明高技术（集团）有限公司 Method for manufacturing super fine calcium carbonate dispersing particles
CN101209851A (en) * 2007-12-24 2008-07-02 上海东升新材料有限公司 Method for manufacturing rice-shaped precipitated calcium carbonate
CN101591029A (en) * 2008-05-28 2009-12-02 北京紫光英力化工技术有限公司 Causticizing process prepares the novel process of caustic soda and super fine calcium carbonate
CN101700901A (en) * 2009-11-25 2010-05-05 王冬生 Novel method for producing light calcium carbonate (CaCO3) from white clay generated from alkali recovering in paper-making industry
CN102126736A (en) * 2011-01-19 2011-07-20 刘先黎 Method for preparing nano-calcium carbonate powder by using soluble carbonate
CN103950965A (en) * 2014-04-29 2014-07-30 东华大学 Method for preparing nano-calcium carbonate with different sizes by applying seed crystal method
CN107149851A (en) * 2017-07-18 2017-09-12 华东交通大学 One kind is desorbed and CO in fixed monoethanolamine rich solution2New method

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112892160A (en) * 2021-02-22 2021-06-04 浙江大学 Phase change absorbent and application thereof in carbon dioxide capture
CN112892160B (en) * 2021-02-22 2022-08-30 浙江大学 Phase change absorbent and application thereof in carbon dioxide capture
CN114870587A (en) * 2022-05-05 2022-08-09 北京金隅水泥节能科技有限公司 Industrial flue gas carbon dioxide trapping agent and preparation method thereof
CN114870587B (en) * 2022-05-05 2023-04-14 北京金隅节能科技有限公司 Industrial flue gas carbon dioxide trapping agent and preparation method thereof

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