WO2024001062A1 - 二氧化碳捕集方法及其装置 - Google Patents

二氧化碳捕集方法及其装置 Download PDF

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WO2024001062A1
WO2024001062A1 PCT/CN2022/138490 CN2022138490W WO2024001062A1 WO 2024001062 A1 WO2024001062 A1 WO 2024001062A1 CN 2022138490 W CN2022138490 W CN 2022138490W WO 2024001062 A1 WO2024001062 A1 WO 2024001062A1
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section
absorption
liquid
carbon dioxide
regeneration
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PCT/CN2022/138490
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English (en)
French (fr)
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赵兴雷
刘双星
薛明
李兴春
杨术刚
张晓飞
陈宏坤
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中国石油天然气集团有限公司
中国石油集团安全环保技术研究院有限公司
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Publication of WO2024001062A1 publication Critical patent/WO2024001062A1/zh

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • 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
    • 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
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • B01D53/79—Injecting reactants
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C01B32/50—Carbon dioxide
    • 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

Definitions

  • This application belongs to the technical field of carbon dioxide capture, and specifically relates to a carbon dioxide capture method and its device.
  • Carbon capture, utilization and storage technology is currently one of the effective means to achieve large-scale carbon neutrality.
  • solvent capture has the advantages of good separation effect, mature and reliable technology.
  • the patent document CN1232500C discloses an application
  • the patent document CN103463955B discloses a process for separating and recovering carbon dioxide from industrial exhaust gas.
  • the absorption tower and the regeneration tower are designed separately, and both construction processes need to be established.
  • Supporting auxiliary facilities, reaction materials need to be returned between reactors, which not only makes the equipment occupy a larger area in actual production, requires higher investment, but also consumes higher energy. Therefore, how to reduce investment and energy consumption is a hot research topic in capture technology.
  • this application provides a carbon dioxide capture method, which can realize the mutual supply of materials in the two reaction processes of absorption and regeneration and reduce energy consumption.
  • This application also provides a carbon dioxide capture device. Using this device to capture carbon dioxide can reduce investment and save equipment space.
  • a carbon dioxide capture method uses a coupling reactor as a reactor.
  • the coupling reactor includes an upper absorption section and a lower regeneration section; the method includes: passing the gas to be treated into the absorption section. , contacts the absorption liquid to obtain rich liquid and residual gas, and the residual gas is discharged from the top of the absorption section; the rich liquid descends in the absorption section, enters the regeneration section, and contacts the vaporizing agent in the regeneration section to obtain carbon dioxide and lean liquid, where, The carbon dioxide is discharged from the top of the regeneration section, and the lean liquid is returned to the absorption section for recycling.
  • the rich liquid flows down in the absorption section, and after being heated by heat exchange, enters the regeneration section.
  • the lean liquid after the lean liquid is cooled by heat exchange, it is returned to the absorption section for recycling.
  • the rich liquid flows down in the absorption section, and is divided into two parts after flowing out from the absorption section.
  • Part of the rich liquid enters the regeneration section from the top of the regeneration section, and the remaining rich liquid passes through heat exchange After the temperature rises, it enters the regeneration section from the middle and upper part of the regeneration section.
  • the volume ratio of the partial rich liquid to the total rich liquid is 5-20%.
  • the reaction temperature is 10°C-60°C.
  • the gas-liquid ratio of the gas to be treated and the absorption liquid is (0.2-0.8) (Nm 3 /h/(L/h)).
  • the absorption liquid includes an alkaline solution.
  • the mass concentration of the absorbent in the absorption liquid is 10wt%-60wt%, and the absorbent includes at least one of alkaline inorganic substances and nitrogen-containing organic substances.
  • the reaction temperature is 100°C-130°C
  • the gas velocity of the vaporizing agent is 0.1m/s-1.5m/s.
  • the device at least includes a coupling reactor, wherein: the coupling reactor includes an upper absorption section and a lower regeneration section; the liquid phase of the absorption section The outlet is connected to the liquid phase inlet of the regeneration section, and the liquid phase outlet of the regeneration section is connected to the liquid phase inlet of the absorption section.
  • the present application also includes a heat exchanger.
  • the heat exchanger is arranged inside the coupling reactor, or the heat exchanger is arranged outside the coupling reactor.
  • the liquid phase outlet of the absorption section passes through the heat exchanger and the regeneration section.
  • the liquid phase inlet is connected, and the liquid phase outlet of the regeneration section is connected to the liquid phase inlet of the absorption section through a heat exchanger.
  • it also includes a heat exchanger, which is arranged inside the coupling reactor, or the heat exchanger is arranged outside the coupling reactor; the liquid in the absorption section
  • the phase outlet is connected to the first liquid phase inlet of the regeneration section through a first pipeline, and the liquid phase outlet of the absorption section is connected to the second liquid phase inlet of the regeneration section through the heat exchanger.
  • the liquid phase outlet of the regeneration section is connected to the liquid phase inlet of the absorption section through the heat exchanger.
  • the carbon dioxide capture method provided by this application couples the two reaction processes of carbon dioxide absorption and regeneration, and realizes the mutual supply of materials for the two reaction processes in the upper absorption section and the lower regeneration section of the coupling reactor, thereby realizing the capture and regeneration of carbon dioxide. regeneration.
  • the method provided by this application can significantly reduce the energy consumption in the carbon dioxide capture process, improve the carbon dioxide capture efficiency and regeneration rate, reduce the difficulty of material circulation operation, and also reduce the footprint of the carbon dioxide capture device and reduce the cost of the carbon dioxide capture device. Equipment investment costs.
  • the carbon dioxide capture device provided by this application can realize the mutual supply of materials in the two reaction processes of carbon dioxide absorption and regeneration, reduce the energy consumption and material circulation operation difficulty in the carbon dioxide capture process, and improve the capture efficiency.
  • the device has a small footprint and low investment costs.
  • Figure 1 is a schematic diagram of a carbon dioxide capture device provided by a specific embodiment of the present application.
  • FIG. 2 is a schematic diagram of a carbon dioxide capture device provided by another specific embodiment of the present application.
  • 100-coupling reactor 110-absorption section; 120-regeneration section; 130-heat exchanger; 140-pump; first pipeline 1.
  • connection can be direct connection, or it can be Indirect connections through intermediaries.
  • connection can be direct connection, or it can be Indirect connections through intermediaries.
  • the present application provides a method for capturing carbon dioxide, which uses a coupling reactor as a reactor.
  • the coupling reactor includes an upper absorption section and a lower regeneration section; the method includes: passing the gas to be treated into the absorption section, and combining it with the absorption section.
  • the liquid contacts to obtain rich liquid and residual gas, and the residual gas is discharged from the top of the absorption section; the rich liquid descends in the absorption section and enters the regeneration section, where it contacts the vaporizer in the regeneration section to obtain carbon dioxide and lean liquid, in which carbon dioxide is self-regenerated
  • the top of the section is discharged, and the lean liquid is returned to the absorption section for recycling.
  • the gas to be treated enters the absorption section at the upper part of the coupling reactor, contacts the absorption liquid and undergoes a chemical reaction, thereby generating residual gas and rich liquid from which carbon dioxide is removed.
  • the rich liquid enters the regeneration section at the lower part of the coupling reactor, causing a gasification reaction between the rich liquid and the vaporization agent introduced into the regeneration section, thereby realizing the regeneration of carbon dioxide and absorbing liquid.
  • the carbon dioxide in the gas to be treated reacts chemically with the absorption liquid.
  • This chemical reaction is an exothermic reaction, and rich liquid and residual gas are obtained.
  • the temperature of the absorption section increases, and we can obtain
  • the rich liquid with increased temperature can provide part of the heat required for the regeneration reaction in the regeneration section.
  • the rich liquid flows downward under the action of gravity and enters the regeneration section from the bottom of the absorption section, which can ensure the rich liquid and vaporization.
  • the agent is fully contacted to improve the carbon dioxide regeneration efficiency.
  • the rich liquid can come into contact with the vaporizing agent whose temperature is raised. After the temperature of the rich liquid is raised to a suitable temperature, the regeneration of carbon dioxide and the regeneration of the absorbing liquid are achieved, and regenerated carbon dioxide and lean liquid are obtained. The regenerated carbon dioxide is obtained from the regeneration section.
  • the lean liquid is discharged from the bottom of the regeneration section and sent into the absorption section as absorption liquid to continue to react with the gas to be treated, thus forming a cycle.
  • the specific ratio of the gas to be treated sent to the absorption section and the lean liquid sent into the absorption section as the absorption liquid can be reasonably determined based on actual needs.
  • this application realizes the mutual supply of materials in the two reaction processes of carbon dioxide absorption and regeneration by integrating the absorption section and the regeneration section in the same coupling reactor. Compared with the current stage where the materials are between the two reactors, The method of intermittent transportation and circulation.
  • the method provided by this application can not only significantly reduce the energy consumption in the carbon dioxide capture process and improve the carbon dioxide capture efficiency, but also solve the problem of high difficulty in material circulation operation at this stage. In addition, it also solves This solves the current problems of large area and high equipment investment for carbon dioxide capture devices.
  • This application does not specifically limit the above-mentioned gas to be treated.
  • it may be flue gas generated after fuel combustion, or it may be air.
  • the method provided by this application has a good treatment effect on the gas to be treated with a carbon dioxide volume content of 1%-50%.
  • the flue gas can be pretreated first.
  • the pretreatment device is located before the coupling reactor. It uses the pretreatment device to remove moisture and particulate matter in the flue gas to avoid affecting the absorption of carbon dioxide in the flue gas by the absorbing liquid, affecting the carbon dioxide capture effect, and ensuring the normal operation of the subsequent coupling reactor. .
  • the above coupling reactor is not particularly limited in this application.
  • it can be a packed tower or a plate tower.
  • the gas to be treated can be introduced from the bottom of the absorption section and contacted with the absorption liquid entering from the top of the absorption section in countercurrent.
  • the carbon dioxide in the gas to be treated is absorbed from the gas phase to the absorption liquid.
  • a rich liquid is formed in the liquid, and the residual gas can be discharged to the environment from the top of the absorption section.
  • heat exchange can be performed first before the lean liquid returns to the absorption section.
  • the lean liquid is cooled by heat exchange, it is returned to the absorption section for recycling, so that the lean liquid provides the parts required for the regeneration reaction in the regeneration section. Heat is beneficial to the regeneration efficiency of carbon dioxide.
  • the lean liquid after heat exchange can be condensed first and then returned to the absorption section for use.
  • the ratio of the lean liquid drawn from the bottom of the regeneration section to the rich liquid flowing out from the bottom of the absorption section can be reasonably determined according to actual needs to achieve full utilization of heat.
  • the rich liquid flows down in the absorption section and is divided into two parts after flowing out of the absorption section.
  • Part of the rich liquid enters the regeneration section from the top of the regeneration section.
  • the remaining rich liquid is heated by heat exchange and flows from the regeneration section.
  • the middle and upper part enters the regeneration section.
  • This application does not limit the ratio of part of the rich liquid to the remaining rich liquid.
  • the volume ratio of the remaining rich liquid to the total rich liquid is 5-20%.
  • the rich liquid flows down in the absorption section, and after flowing out from the absorption section, a pump can be used to pump it into the heat exchanger.
  • the reaction in the absorption section is usually as follows: the reaction temperature is 10°C-60°C, the reaction pressure is 0.5MPa-2MPa, and the gas velocity of the gas to be treated is 0.1m/s-1.5m/s.
  • the reaction temperature in the absorption section is 20°C-40°C, the reaction pressure is 0.1MPa-1MPa, such as normal pressure, and the gas velocity of the gas to be treated can be 0.2m/s-1m/s, where the gas velocity can be as shown in the table
  • the gas velocity refers to the empty tower flow rate of the gas to be treated entering the absorption section.
  • the diameter of the absorption section can be determined based on the gas velocity, and the reaction time in the absorption section can be determined according to the actual situation.
  • the matching of materials and energy in the carbon dioxide capture process can be further achieved, so that the gas and liquid maintain a stable reaction, ensuring the stability of the entire carbon dioxide capture process, and achieving gas neutralization. Stable and effective capture of carbon dioxide.
  • the gas-liquid ratio of the gas to be treated and the absorption liquid is (0.2-0.8) (Nm 3 /h/(L/h)).
  • the gas flow rate of the gas to be treated can be controlled to 280Nm 3 /h, Then the liquid flow rate of the absorption liquid is 500L/h.
  • This application does not limit the specific type of absorption liquid. It can be a currently commonly used absorption liquid.
  • absorption liquid since carbon dioxide is an acid gas, alkaline or alkaline salt solution can be preferably used as the absorbent aqueous solution. for absorption.
  • the absorbent aqueous solution is an alkaline aqueous solution.
  • the above-mentioned absorption liquid can be obtained by conventional methods.
  • the absorption liquid is prepared by dissolving the absorbent in a solvent.
  • water-soluble absorption liquid is usually used.
  • the absorbent can be dissolved in water first and configured into an absorption liquid.
  • the mass concentration of the absorbent in the absorption liquid is 10wt%-60wt%, such as 10%, 15%, 20%, A range consisting of 25%, 30%, 35%, 40%, 45%, 50%, 55%, 60% or any two thereof.
  • the absorbent includes at least one of alkaline inorganic substances and nitrogen-containing organic substances, preferably a mixture of alkaline inorganic substances and nitrogen-containing organic substances, wherein the alkaline inorganic substances include potassium hydroxide and sodium hydroxide.
  • At least one of the nitrogen-containing organic substances includes at least one of amino acid salts and organic alcohol amines.
  • the absorption liquid may be a monoethanolamine solution or a potassium glycinate solution.
  • This application does not specifically limit the vaporizing agent introduced into the regeneration section.
  • it can be water vapor, or a mixture of water vapor and oxygen-containing gas.
  • the oxygen-containing gas can be, for example, air, oxygen-enriched air, oxygen, etc.
  • the vaporizing agent can be saturated water vapor with a flow rate of 75kg/h and a pressure of 0.3MPa.
  • the reaction temperature in the gasification section is generally controlled at 100°C-130°C
  • the reaction pressure is generally controlled at 0.1MPa-5MPa
  • the gas velocity of the vaporizing agent is generally controlled at 0.1-1.5m/s.
  • the reaction temperature in the gasification section is generally controlled at 100°C-110°C
  • the reaction pressure is generally controlled at 0.1MPa-1MPa
  • the gas velocity of the gasification agent is generally controlled at 0.1-1m/s, where the gas velocity can be:
  • the gas velocity refers to the empty tower flow rate of the vaporizer entering the regeneration section.
  • the diameter of the regeneration section can be determined based on the gas velocity, and the reaction time in the regeneration section can be determined according to the actual situation. Carrying out the regeneration reaction under the above conditions can ensure that the absorbing liquid is fully regenerated and high-quality carbon dioxide product gas can be obtained.
  • This application also provides a carbon dioxide capture device for implementing the above method.
  • the device at least includes a coupling reactor, wherein:
  • the coupling reactor includes an upper absorption section and a lower regeneration section; the liquid phase outlet of the absorption section is connected to the liquid phase inlet of the regeneration section, and the liquid phase outlet of the regeneration section is connected to the liquid phase inlet of the absorption section.
  • the absorption section and the regeneration section may or may not communicate with each other.
  • the above-mentioned coupling reactor can specifically be a packed tower or a plate tower obtained by appropriately modifying and assembling the absorption reactor and regeneration reactor commonly used in this field.
  • the absorption tower and the regeneration tower are preferably coaxially arranged to facilitate the transportation and circulation of materials. , reducing the difficulty of the circulation operation between the two reactors in processes such as carbon dioxide absorption and regeneration, while further reducing the footprint of the device.
  • the liquid phase outlet of the absorption section is generally located at the bottom of the absorption section, used to pass rich liquid into the regeneration section; the gas phase outlet of the absorption section is generally located at the top of the absorption section, used to discharge residual gas.
  • the liquid phase inlet of the regeneration section is generally set at the top of the regeneration section and is connected to the liquid phase outlet of the absorption section; the gas phase inlet of the regeneration section is generally set at the bottom of the regeneration section, which is used to introduce gasification agent into the regeneration section.
  • the gas phase inlet is set at the bottom, and the liquid phase inlet of the regeneration section is set at the top, which can realize countercurrent contact between the gasification agent and the rich liquid, which contributes to the regeneration efficiency.
  • the liquid phase outlet of the regeneration section is generally located at the bottom of the regeneration section, connected to the liquid phase inlet of the absorption section, and is used to introduce lean liquid into the absorption section.
  • the gas phase outlet of the regeneration section is generally located at the top of the regeneration section, and the regenerated carbon dioxide product gas flows out from the gas phase outlet of the regeneration section.
  • a gas storage tank is also included.
  • the gas storage tank is used to temporarily accommodate the regenerated carbon dioxide product.
  • the gas storage tank is connected to the gas phase outlet of the regeneration section.
  • connection in this application can be pipe connection.
  • a heat exchanger may be provided, and the heat exchanger may be provided inside the coupling reactor, or the heat exchanger may be provided outside the coupling reactor.
  • the heat exchanger can be a built-in heat exchanger or an external heat exchanger.
  • the heat exchanger is installed in the coupling reactor, specifically between the absorption section and the regeneration section.
  • the liquid phase outlet of the absorption section is connected to the liquid phase inlet of the regeneration section through a heat exchanger, and the liquid phase outlet of the regeneration section is connected to the liquid phase inlet of the absorption section through a heat exchanger.
  • the liquid phase outlet of the absorption section is connected to the first liquid phase inlet of the regeneration section through a first pipeline, and the liquid phase outlet of the absorption section is connected to the regeneration section through a heat exchanger.
  • the second liquid phase inlet is connected, and the liquid phase outlet of the regeneration section is connected to the liquid phase inlet of the absorption section through a heat exchanger.
  • the first liquid phase inlet is located at the top of the regeneration section, and the second liquid phase inlet is located at the middle and upper part of the regeneration section.
  • the gasification agent can be a high-temperature gasification agent introduced from the gas phase inlet at the bottom of the regeneration section, or a heating section can be provided at the lower part of the regeneration section.
  • the gasification agent can be: the rich liquid flows down in the regeneration section, and reaches the regeneration section. At the bottom of the section, after being heated by the heating section, a mixture of water vapor and carbon dioxide is produced. The water vapor is used as a gasification agent to contact the subsequent descending rich liquid for regeneration.
  • the carbon dioxide capture device of the present application can also include a flow control device.
  • the flow control device includes a gas flow control device and a liquid flow control device.
  • the gas flow control device is located at the front end of the absorption section.
  • the rear end of the flow control device is connected to the gas phase inlet of the absorption unit.
  • valve can be set to adjust and control the flow control device in real time based on the data obtained through monitoring.
  • the carbon dioxide capture device of the present application may also include a gas component analysis device, which is arranged at the gas phase outlet end of the regeneration section and is used to analyze the components of the regeneration gas.
  • pump pressure can be used to allow the gas to be treated and the absorption liquid to enter the absorption section, or pump pressure can be used to allow the lean liquid to enter the absorption section.
  • Step 1 The gas to be treated is sent into the absorption section through the gas phase inlet at the bottom of the absorption section after adjusting the flow rate by the gas flow control device, and the absorption liquid is sent into the absorption section through the liquid phase inlet at the top of the absorption section.
  • the two phases flow in parallel countercurrent.
  • the carbon dioxide is absorbed and treated by contacting in a contact manner. After the absorption treatment, rich liquid and residual gas are obtained;
  • Step 2 The rich liquid obtained after the reaction goes down in the absorption section and flows out from the liquid phase outlet at the bottom of the absorption section; the residual gas after absorption treatment goes up and flows out from the gas phase outlet at the top of the absorption section.
  • the residual gas is analyzed for composition. The gas is discharged into the atmosphere after testing and meeting the standards;
  • Step 3 Make the gasification agent enter the regeneration section from the gas phase inlet of the regeneration section, so that the rich liquid enters the regeneration section and contacts the upward gasification agent to obtain carbon dioxide and lean liquid.
  • the carbon dioxide capture device provided by this application has a simple structure, is convenient and quick to use, can realize the mutual supply of materials and complementary heat in the two reaction processes of carbon dioxide absorption and regeneration, reduces the energy consumption and material circulation operation difficulty of the carbon dioxide capture process, and improves the efficiency of the carbon dioxide capture process. Carbon dioxide capture rate and regeneration rate. In addition, the device has a small footprint and low investment costs.
  • the carbon dioxide capture device of this embodiment at least includes: a coupling reactor 100 and a heat exchanger 130
  • the coupling reactor 100 includes an upper absorption section 110 and a lower regeneration section 120; the liquid phase outlet of the absorption section 110 is connected to the liquid phase inlet of the regeneration section 120, and the liquid phase outlet of the regeneration section 120 is connected to the liquid phase of the absorption section 110.
  • the entrances are connected;
  • the gas phase inlet of the absorption section 110 is used to introduce the gas to be treated into the absorption section 110
  • the liquid phase inlet of the absorption section 110 is used to introduce absorption liquid or lean liquid into the absorption section 110
  • the liquid phase outlet of the absorption section 110 is used to introduce the gas to be treated.
  • the regeneration section 120 is fed with rich liquid, and the gas phase outlet of the absorption section 110 is used to discharge residual gas.
  • the liquid phase inlet of the regeneration section 120 is connected to the liquid phase outlet of the absorption section 110.
  • the gas phase inlet of the regeneration section 120 is used to introduce gasification agent into the regeneration section 120.
  • the liquid phase outlet of the regeneration section 120 is connected with the liquid phase inlet of the absorption section 110. Connected to pass lean liquid into the absorption section 110;
  • the carbon dioxide capture device of this embodiment also includes a pump 140, and the liquid phase outlet of the regeneration section 120 is connected to the heat exchanger 130 through the pump.
  • the flue gas with a carbon dioxide concentration of 13% is sent into the absorption section through the gas phase inlet at the bottom of the absorption section at a flow rate of 280Nm 3 /h.
  • the mass Potassium glycinate solution with a content of 30% is sent into the absorption section through the liquid inlet at the top of the absorption section.
  • the two phases contact in a parallel counter-current manner to absorb carbon dioxide.
  • rich liquid and residual gas are obtained; where:
  • the residual gas after absorption treatment goes up and flows out from the gas phase outlet at the top of the absorption section.
  • the composition of the residual gas is analyzed.
  • the residual gas is discharged into the atmosphere after being tested to meet the standards;
  • the rich liquid obtained after the reaction flows down in the absorption section, and when it flows out from the liquid phase outlet at the bottom of the absorption section, the temperature of the rich liquid is 65°C; the rich liquid with a temperature of 65°C enters the heat exchanger and is heated to 90°C through heat exchange. Then it enters the regeneration section and makes counter-current contact with saturated water vapor with a gas velocity of 1m/s and a pressure of 0.3MPa (the saturated water vapor enters the regeneration section from the gas phase inlet of the regeneration section), and is collected at the gas phase outlet of the regeneration section.
  • the carbon dioxide product gas with a flow rate of 25.4Nm 3 /h discharges the lean liquid at 101°C from the bottom of the regeneration section.
  • the lean liquid is pumped into the heat exchanger to cool down through pump pressure, and then returns to the absorption section through the liquid phase inlet of the absorption section. ;
  • the carbon dioxide regeneration rate in this embodiment is 69.7%, and the purity (dry basis) of the carbon dioxide product gas can reach more than 99%.
  • the carbon dioxide capture device of this embodiment at least includes: a coupling reactor 100 and a heat exchanger 130
  • the coupling reactor 100 includes an upper absorption section 110 and a lower regeneration section 120; the liquid phase outlet of the absorption section 110 is connected to the liquid phase inlet of the regeneration section 120, and the liquid phase outlet of the regeneration section 120 is connected to the liquid phase of the absorption section 110.
  • the entrances are connected;
  • the gas phase inlet of the absorption section 110 is used to introduce the gas to be treated into the absorption section 110
  • the liquid phase inlet of the absorption section 110 is used to introduce absorption liquid or lean liquid into the absorption section 110
  • the liquid phase outlet of the absorption section 110 is used to introduce the gas to be treated into the absorption section 110
  • the regeneration section 120 is fed with rich liquid, and the gas phase outlet of the absorption section 110 is used to discharge residual gas.
  • the liquid phase inlet of the regeneration section 120 is connected to the liquid phase outlet of the absorption section 110.
  • the gas phase inlet of the regeneration section 120 is used to introduce gasification agent into the regeneration section 120.
  • the liquid phase outlet of the regeneration section 120 is connected with the liquid phase inlet of the absorption section 110. Connected to pass lean liquid into the absorption section 110;
  • the carbon dioxide capture device of this embodiment also includes a pump 140, and the liquid phase outlet of the regeneration section 120 is connected to the heat exchanger 130 through the pump.
  • the flue gas with a carbon dioxide concentration of 13% is sent into the absorption section through the gas phase inlet at the bottom of the absorption section at a flow rate of 280Nm 3 /h.
  • the mass of The monoethanolamine solution with a content of 10% is sent into the absorption section through the liquid inlet at the top of the absorption section.
  • the two phases contact in a parallel counter-current manner to absorb carbon dioxide.
  • rich liquid and residual gas are obtained; where:
  • the residual gas after absorption treatment goes up and flows out from the gas phase outlet at the top of the absorption section.
  • the composition of the residual gas is analyzed.
  • the residual gas is discharged into the atmosphere after being tested to meet the standards;
  • the rich liquid obtained after the reaction flows down in the absorption section, and when it flows out from the liquid phase outlet at the bottom of the absorption section, the temperature of the rich liquid is 65°C; the rich liquid with a temperature of 65°C enters the heat exchanger and is heated to 90°C through heat exchange.
  • the carbon dioxide regeneration rate of this embodiment is 54.8%, and the purity (dry basis) of the carbon dioxide product gas can reach more than 99%.
  • the carbon dioxide capture device of this embodiment at least includes: a coupling reactor 100 and a heat exchanger 130
  • the coupling reactor 100 includes an upper absorption section 110 and a lower regeneration section 120; the liquid phase outlet of the absorption section 110 is connected to the liquid phase inlet of the regeneration section 120, and the liquid phase outlet of the regeneration section 120 is connected to the liquid phase of the absorption section 110.
  • the entrances are connected;
  • the gas phase inlet of the absorption section 110 is used to introduce the gas to be treated into the absorption section 110
  • the liquid phase inlet of the absorption section 110 is used to introduce absorption liquid or lean liquid into the absorption section 110
  • the liquid phase outlet of the absorption section 110 is used to introduce the gas to be treated into the absorption section 110
  • the regeneration section 120 is fed with rich liquid, and the gas phase outlet of the absorption section 110 is used to discharge residual gas.
  • the liquid phase inlet of the regeneration section 120 is connected to the liquid phase outlet of the absorption section 110.
  • the gas phase inlet of the regeneration section 120 is used to introduce gasification agent into the regeneration section 120.
  • the liquid phase outlet of the regeneration section 120 is connected with the liquid phase inlet of the absorption section 110. Connected to pass lean liquid into the absorption section 110;
  • the liquid phase outlet of the absorption section 110 is connected to the liquid phase inlet of the regeneration section 120 through the heat exchanger 130, and the liquid phase outlet of the regeneration section 120 is connected to the liquid phase inlet of the absorption section 110 through the heat exchanger 130;
  • the carbon dioxide capture device of this embodiment also includes a pump 140, and the liquid phase outlet of the regeneration section 120 is connected to the heat exchanger 130 through the pump.
  • the flue gas with a carbon dioxide concentration of 13% is sent into the absorption section through the gas phase inlet at the bottom of the absorption section at a flow rate of 280Nm 3 /h.
  • the mass of The monoethanolamine solution with a content of 60% is sent into the absorption section through the liquid inlet at the top of the absorption section.
  • the two phases contact in a parallel counter-current manner to absorb carbon dioxide.
  • rich liquid and residual gas are obtained; where:
  • the residual gas after absorption treatment goes up and flows out from the gas phase outlet at the top of the absorption section.
  • the composition of the residual gas is analyzed.
  • the residual gas is discharged into the atmosphere after being tested to meet the standards;
  • the rich liquid obtained after the reaction flows down in the absorption section, and when it flows out from the liquid phase outlet at the bottom of the absorption section, the temperature of the rich liquid is 65°C; the rich liquid with a temperature of 65°C enters the heat exchanger and is heated to 90°C through heat exchange.
  • the carbon dioxide regeneration rate in this embodiment is 82.5%, and the purity (dry basis) of the carbon dioxide product gas can reach more than 99%.
  • the carbon dioxide capture device of this embodiment at least includes: a coupling reactor 100 and a heat exchanger 130;
  • the coupling reactor 100 includes an upper absorption section 110 and a lower regeneration section 120; the liquid phase outlet of the absorption section 110 is connected to the liquid phase inlet of the regeneration section 120, and the liquid phase outlet of the regeneration section 120 is connected to the liquid phase of the absorption section 110.
  • the entrances are connected;
  • the gas phase inlet of the absorption section 110 is used to introduce the gas to be treated into the absorption section 110
  • the liquid phase inlet of the absorption section 110 is used to introduce absorption liquid or lean liquid into the absorption section 110
  • the liquid phase outlet of the absorption section 110 is used to introduce the gas to be treated into the absorption section 110 .
  • the regeneration section 120 passes into the rich liquid, and the gas phase outlet of the absorption section 110 is used to discharge the residual gas;
  • the liquid phase inlet of the regeneration section 120 is connected to the liquid phase outlet of the absorption section 110.
  • the gas phase inlet of the regeneration section 120 is used to introduce gasification agent into the regeneration section 120.
  • the liquid phase outlet of the regeneration section 120 is connected with the liquid phase inlet of the absorption section 110. Connected to pass lean liquid into the absorption section 110;
  • the liquid phase outlet of the absorption section is connected to the first liquid phase inlet of the regeneration section through a first pipeline, and the liquid phase outlet of the absorption section is connected to the second liquid phase inlet of the regeneration section through a heat exchanger; the first liquid phase inlet is located at the regeneration section. At the top of the section, the second liquid phase inlet is located in the middle and upper part of the regeneration section;
  • the liquid phase outlet of the regeneration section 120 is connected to the liquid phase inlet of the absorption section 110 through the heat exchanger 130;
  • the carbon dioxide capture device of this embodiment also includes pumps 140 and 150 .
  • the liquid phase outlet of the regeneration section 120 is connected to the heat exchanger 130 through the pump 140, the rich liquid outlet of the absorption section 110 is connected to the heat exchanger 130 through the pump 150, and the rich liquid inlet at the top of the regeneration section 120.
  • the flue gas with a carbon dioxide concentration of 13% is sent into the absorption section through the gas phase inlet at the bottom of the absorption section at a flow rate of 280Nm 3 /h.
  • the mass of The monoethanolamine solution with a content of 60% is sent into the absorption section through the liquid inlet at the top of the absorption section.
  • the two phases contact in a parallel counter-current manner to absorb carbon dioxide.
  • rich liquid and residual gas are obtained; where:
  • the residual gas after absorption treatment goes up and flows out from the gas phase outlet at the top of the absorption section.
  • the composition of the residual gas is analyzed.
  • the residual gas is discharged into the atmosphere after being tested to meet the standards;
  • the rich liquid obtained after the reaction flows down in the absorption section, and when it flows out from the liquid phase outlet at the bottom of the absorption section, the temperature of the rich liquid is 65°C; the rich liquid enters the regeneration section in two streams, one of which accounts for 5% of the total rich liquid in volume. Directly enters the top of the regeneration section, and the other stream enters the heat exchanger. After being heated to 90°C by heat exchange, it enters the regeneration section and mixes with saturated water vapor with a gas velocity of 1.5m/s and a pressure of 0.3MPa (the saturated water vapor is automatically The gas phase inlet of the regeneration section enters the regeneration section) for counter-current contact.
  • the carbon dioxide product gas with a flow rate of 30.03Nm 3 /h is collected at the gas phase outlet of the regeneration section.
  • the lean liquid at 101°C is discharged from the bottom of the regeneration section through pump pressure. Pump the lean liquid into the heat exchanger to cool down, and then return to the absorption section through the liquid phase inlet of the absorption section;
  • the carbon dioxide regeneration rate in this embodiment is 85.6%, and the purity (dry basis) of the carbon dioxide product gas can reach more than 99%.
  • the carbon dioxide capture device of this embodiment at least includes: a coupling reactor 100, a heat exchanger 130
  • the coupling reactor 100 includes an upper absorption section 110 and a lower regeneration section 120; the liquid phase outlet of the absorption section 110 is connected to the liquid phase inlet of the regeneration section 120, and the liquid phase outlet of the regeneration section 120 is connected to the liquid phase of the absorption section 110.
  • the entrances are connected;
  • the gas phase inlet of the absorption section 110 is used to introduce the gas to be treated into the absorption section 110
  • the liquid phase inlet of the absorption section 110 is used to introduce absorption liquid or lean liquid into the absorption section 110
  • the liquid phase outlet of the absorption section 110 is used to introduce the gas to be treated into the absorption section 110
  • the regeneration section 120 is fed with rich liquid, and the gas phase outlet of the absorption section 110 is used to discharge residual gas.
  • the liquid phase inlet of the regeneration section 120 is connected to the liquid phase outlet of the absorption section 110.
  • the gas phase inlet of the regeneration section 120 is used to introduce gasification agent into the regeneration section 120.
  • the liquid phase outlet of the regeneration section 120 is connected with the liquid phase inlet of the absorption section 110. Connected to pass lean liquid into the absorption section 110;
  • the liquid phase outlet of the absorption section 110 is connected to the liquid phase inlet of the regeneration section 120 through the heat exchanger 130, and the liquid phase outlet of the regeneration section 120 is connected to the liquid phase inlet of the absorption section 110 through the heat exchanger 130;
  • the carbon dioxide capture device of this embodiment also includes pumps 140 and 150 .
  • the liquid phase outlet of the regeneration section 120 is connected to the heat exchanger 130 through the pump 140, the rich liquid outlet of the absorption section 110 is connected to the heat exchanger 130 through the pump 150, and the rich liquid inlet at the top of the regeneration section 120.
  • the flue gas with a carbon dioxide concentration of 13% is sent into the absorption section through the gas phase inlet at the bottom of the absorption section at a flow rate of 280Nm 3 /h.
  • the mass of The monoethanolamine solution with a content of 60% is sent into the absorption section through the liquid inlet at the top of the absorption section.
  • the two phases contact in a parallel counter-current manner to absorb carbon dioxide.
  • rich liquid and residual gas are obtained; where:
  • the residual gas after absorption treatment goes up and flows out from the gas phase outlet at the top of the absorption section.
  • the composition of the residual gas is analyzed.
  • the residual gas is discharged into the atmosphere after being tested to meet the standards;
  • the rich liquid obtained after the reaction flows down in the absorption section, and when it flows out from the liquid phase outlet at the bottom of the absorption section, the temperature of the rich liquid is 65°C; the rich liquid enters the regeneration section in two parts, and part of the rich liquid (volume accounts for 20% of the total rich liquid) %) enters through the first liquid phase inlet at the top of the regeneration section, and the remaining rich liquid enters the heat exchanger. After being heated to 90°C by heat exchange, it enters the regeneration section through the second liquid phase inlet at the middle and lower part of the regeneration section.
  • the gas velocity is Saturated water vapor at 1.5m/s and pressure 0.3MPa (the saturated water vapor enters the regeneration section from the gas phase inlet of the regeneration section) undergoes countercurrent contact, and carbon dioxide with a flow rate of 30.03Nm 3 /h is collected at the gas phase outlet of the regeneration section.
  • the lean liquid at 101°C is discharged from the bottom of the regeneration section, and the lean liquid is pumped into the heat exchanger to cool down through pump pressure, and then returns to the absorption section through the liquid phase inlet of the absorption section;
  • the carbon dioxide regeneration rate in this embodiment is 80.6%, and the purity (dry basis) of the carbon dioxide product gas can reach more than 99%.
  • the carbon dioxide capture device of this embodiment at least includes: a coupling reactor 100, a heat exchanger 130
  • the coupling reactor 100 includes an upper absorption section 110 and a lower regeneration section 120; the liquid phase outlet of the absorption section 110 is connected to the liquid phase inlet of the regeneration section 120, and the liquid phase outlet of the regeneration section 120 is connected to the liquid phase of the absorption section 110.
  • the entrances are connected;
  • the gas phase inlet of the absorption section 110 is used to introduce the gas to be treated into the absorption section 110
  • the liquid phase inlet of the absorption section 110 is used to introduce absorption liquid or lean liquid into the absorption section 110
  • the liquid phase outlet of the absorption section 110 is used to introduce the gas to be treated into the absorption section 110
  • the regeneration section 120 is fed with rich liquid, and the gas phase outlet of the absorption section 110 is used to discharge residual gas.
  • the liquid phase inlet of the regeneration section 120 is connected to the liquid phase outlet of the absorption section 110.
  • the gas phase inlet of the regeneration section 120 is used to introduce gasification agent into the regeneration section 120.
  • the liquid phase outlet of the regeneration section 120 is connected with the liquid phase inlet of the absorption section 110. Connected to pass lean liquid into the absorption section 110;
  • the liquid phase outlet of the absorption section is connected to the first liquid phase inlet of the regeneration section through a first pipeline, and the liquid phase outlet of the absorption section is connected to the second liquid phase inlet of the regeneration section through a heat exchanger; the first liquid phase inlet is located at the regeneration section. At the top of the section, the second liquid phase inlet is located in the middle and upper part of the regeneration section;
  • the liquid phase outlet of the regeneration section 120 is connected to the liquid phase inlet of the absorption section 110 through the heat exchanger 130;
  • the carbon dioxide capture device of this embodiment also includes a pump 140, a pump 150 and a condenser 160.
  • the liquid phase outlet of the regeneration section 120 is connected to the heat exchanger 130 through the pump 140.
  • the rich liquid outlet of the absorption section 110 is connected to the heat exchanger 130 through the pump 150 and the rich liquid inlet at the top of the regeneration section 120.
  • the poor liquid is absorbed from the heat exchanger 130. It is connected to the absorption section 110 through a condenser 160 .
  • the flue gas with a carbon dioxide concentration of 13% is sent into the absorption section through the gas phase inlet at the bottom of the absorption section at a flow rate of 280Nm 3 /h.
  • the mass The monoethanolamine solution with a content of 60% and a temperature of 40°C is fed into the absorption section through the liquid phase inlet at the top of the absorption section.
  • the two phases contact in a parallel counter-current manner to absorb carbon dioxide.
  • rich liquid and Residual gas among them: the residual gas after absorption treatment goes up and flows out from the gas phase outlet at the top of the absorption section.
  • the composition of the residual gas is analyzed.
  • the residual gas is discharged into the atmosphere after being tested to meet the standards;
  • the rich liquid obtained after the reaction flows down in the absorption section, and when it flows out from the liquid phase outlet at the bottom of the absorption section, the temperature of the rich liquid is 65°C; the rich liquid enters the regeneration section in two parts, and part of the rich liquid (volume accounts for 5% of the total rich liquid) %) directly enters the top of the regeneration section through the first liquid phase inlet at the top of the regeneration section, and the remaining rich liquid enters the heat exchanger. After being heated to 90°C through heat exchange, it enters the regeneration section through the second liquid phase inlet of the regeneration section and mixes with the gas.
  • Saturated water vapor with a speed of 1.5m/s and a pressure of 0.3MPa (the saturated water vapor enters the regeneration section from the gas phase inlet of the regeneration section) is in counter-current contact, and a flow rate of 30.03Nm 3 /h is collected at the gas phase outlet of the regeneration section.
  • the carbon dioxide product gas is discharged from the bottom of the regeneration section.
  • the lean liquid is pumped into the heat exchanger to cool down through pump pressure, and then returned to the absorption section through the liquid phase inlet of the absorption section;
  • the carbon dioxide regeneration rate in this embodiment is 87.2%, and the purity (dry basis) of the carbon dioxide product gas can reach more than 99%.
  • the carbon dioxide capture method and device provided by this application integrate the absorption section and the regeneration section in the same coupling reactor, realizing the mutual supply of materials in the two reaction processes of carbon dioxide absorption and regeneration.
  • the method provided by this application can not only significantly reduce the energy consumption in the carbon dioxide capture process and improve the carbon dioxide capture efficiency, but also solve the current problem. It also solves the problem of high difficulty in material circulation operation at each stage. In addition, it also solves the current problems of large area and high equipment investment for carbon dioxide capture devices, which is conducive to large-scale promotion and application.

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Abstract

一种二氧化碳捕集方法及其装置。方法利用耦合反应器（100）作为反应器，耦合反应器（100）包括上部的吸收段（110）和下部的再生段（120）。方法包括：将待处理气体通入吸收段（110）内，与吸收液接触，得到富液和残余气，残余气从吸收段（110）顶部排出；富液在吸收段（110）内下行，进入再生段（120）内，在再生段（120）与汽化剂接触，得到二氧化碳和贫液。二氧化碳从再生段（120）顶部排出，贫液返回吸收段（110）内循环使用。该方法实现吸收和再生两个反应过程的物料互供。

Description

二氧化碳捕集方法及其装置
本申请要求于2022年07月01日提交中国专利局、申请号为202210764733.7、申请名称为“二氧化碳捕集方法及其装置”的中国专利申请的优先权，其全部内容通过引用结合在本申请中。
技术领域
本申请属于二氧化碳捕集技术领域，具体涉及一种二氧化碳捕集方法及其装置。
背景技术
碳捕集利用与封存技术(CCUS)是目前实现大规模碳中和的有效手段之一，其中，溶剂法捕集具有分离效果好、技术成熟可靠等优势，例如专利文献CN1232500C公开了一种应用于化学吸收液再生的再生塔热量回收方法，专利文献CN103463955B公开了一种从工业尾气中分离回收二氧化碳的工艺，但是上述工艺方法中，吸收塔和再生塔单独设计，施工过程两者均需要建立配套的辅助设施，反应物料需要在反应器之间返料操作，不仅使实际生产中设备的占地面积较大，投资较高，而且能耗较高。因此，如何降低投资及能耗是捕集技术的研究热点。
发明内容
针对上述缺陷，本申请提供一种二氧化碳捕集方法，能够实现吸收和再生两个反应过程的物料互供，降低能耗。
本申请还提供一种二氧化碳捕集装置，采用该装置对二氧化碳进行捕集，能够降低投资并节约设备占地面积。
本申请的一方面，提供一种二氧化碳捕集方法，该方法利用耦合反应器作为反应器，耦合反应器包括上部的吸收段和下部的再生段；方法包括：将待处理气体通入吸收段内，与吸收液接触，得到富液和残余气，残余气从吸收段顶部排出；富液在吸收段内下行，进入再生段内，在再生段与汽化剂接 触，得到二氧化碳和贫液，其中，二氧化碳自再生段顶部排出，贫液返回吸收段内循环使用。
根据本申请的一实施方式，富液在吸收段内下行，经换热升温后，进入再生段内。根据本申请的一实施方式，贫液经换热降温后，返回吸收段内循环使用。
根据本申请的一实施方式，所述富液在所述吸收段内下行，从吸收段流出后分为两部分，部分富液从再生段的顶部进入所述再生段，剩余富液经换热升温后，从再生段的中上部进入所述再生段内。
根据本申请的一实施方式，所述部分富液占总富液的体积比为5-20％。
根据本申请的一实施方式，在吸收段内，反应温度为10℃-60℃。
根据本申请的一实施方式，待处理气体与吸收液的气液比为(0.2-0.8)(Nm 3/h/(L/h))。
根据本申请的一实施方式，吸收液包括碱性溶液。
根据本申请的一实施方式，吸收液中吸收剂的质量浓度为10wt％-60wt％，吸收剂包括碱性无机物、含氮有机物中的至少一种。
根据本申请的一实施方式，在再生段内，反应温度为100℃-130℃，汽化剂的气速为0.1m/s-1.5m/s。
本申请的另一方面，提供一种二氧化碳捕集装置，用于实现上述的方法，装置至少包括耦合反应器，其中：耦合反应器包括上部的吸收段和下部的再生段；吸收段的液相出口与再生段的液相入口相连，再生段的液相出口与吸收段的液相入口相连。
根据本申请的一实施方式，还包括换热器，换热器设置在耦合反应器内，或者，换热器设置在耦合反应器外；吸收段的液相出口通过换热器与再生段的液相入口连接，再生段的液相出口通过换热器与吸收段的液相入口连接。
根据本申请的一实施方式，还包括换热器，所述换热器设置在所述耦合反应器内，或者，所述换热器设置在所述耦合反应器外；所述吸收段的液相出口通过第一管路与所述再生段的第一液相入口连接，且所述吸收段的液相出口通过所述换热器与所述再生段的第二液相入口连接，所述再生段的液相出口通过所述换热器与所述吸收段的液相入口连接。
本申请的实施，至少具有以下有益效果：
本申请提供的二氧化碳捕集方法，通过耦合二氧化碳吸收与再生两个反应过程，在耦合反应器上部的吸收段和下部的再生段内实现两个反应过程的物料互供，实现二氧化碳的捕集和再生。本申请提供的方法，能够显著降低二氧化碳捕集过程中的能耗、提高二氧化碳捕集效率和再生率、降低了物料循环操作难度，而且还减小了二氧化碳捕集装置的占地面积，降低了设备投资成本。
本申请提供的二氧化碳捕集装置，能够实现二氧化碳吸收与再生两个反应过程中的物料互供，降低了二氧化碳捕集过程中的能耗和物料循环操作难度，提高了捕集效率。此外该装置还具有较小的占地面积和较低的投资成本。
附图说明
图1是本申请一具体实施例所提供的二氧化碳捕集装置的示意图；
图2本申请另一具体实施例所提供的二氧化碳捕集装置的示意图
附图标记说明：
100-耦合反应器；110-吸收段；120-再生段；130-换热器；140-泵；第一管路1。
具体实施方式
以下所列举具体实施方式只是对本申请的原理和特征进行描述，所举实例仅用于解释本申请，并非限定本申请的范围。基于本申请实施例，本领域普通技术人员在没有做出创造性劳动前提下所获得的所有其他实施方式，都属于本申请保护的范围。
需要说明的是，在本申请的描述中，除非另有明确的规定和限定，术语“设置”、“连通”、“相连”等应做广义理解，例如，连通可以是直接连通，也可以是通过中间媒介间接连通。对于本领域的普通技术人员而言，可以具体情况理解上述属于在本申请中的具体含义。
本申请提供一种二氧化碳捕集方法，该方法利用耦合反应器作为反应器，耦合反应器包括上部的吸收段和下部的再生段；该方法包括：将待处理气体通入吸收段内，与吸收液接触，得到富液和残余气，残余气从吸收段顶部排 出；富液在吸收段内下行，进入再生段内，在再生段与汽化剂接触，得到二氧化碳和贫液，其中，二氧化碳自再生段顶部排出，贫液返回吸收段内循环使用。
本申请提供的二氧化碳捕集方法，待处理气体进入耦合反应器上部的吸收段内，与吸收液接触而发生化学反应，从而生成脱除二氧化碳的残余气和富液。富液进入耦合反应器下部的再生段，使富液与通入再生段内的汽化剂发生气化反应，同时实现了二氧化碳和吸收液的再生。
在吸收段内，待处理气体中的二氧化碳与吸收液接触发生化学反应，该化学反应为放热反应，得到富液和残余气，由于吸收段发生放热反应，吸收段温度升高，可以得到温度升高的富液，温度升高的富液可以为再生段提供再生反应所需的部分热量，富液在重力作用下向下流动，自吸收段底部进入再生段，能够保证富液与汽化剂充分接触，提高二氧化碳再生效率。
在再生段内，富液可与温度提升的汽化剂接触，使富液的温度升高至适宜温度后，实现二氧化碳的再生和吸收液的再生，得到再生二氧化碳和贫液，再生二氧化碳从再生段的顶部排出，贫液从再生段的底部排出，送入吸收段内作为吸收液与待处理气体继续反应，从而形成循环。
本申请中，具体送入吸收段的待处理气体与送入吸收段内的贫液作为吸收液的比例可根据实际需求合理确定。
由此可见，本申请通过将吸收段和再生段集成在同一个耦合反应器中，实现了二氧化碳吸收和再生两个反应过程中的物料互供，相较于现阶段物料在两个反应器之间输运和循环的方法，本申请提供的方法，不仅能够显著降低二氧化碳捕集过程中的能耗、提高二氧化碳捕集效率，而且还解决了现阶段物料循环操作难度高的问题，此外还解决了当前二氧化碳捕集装置占地面积大、设备投资高的问题。
本申请对上述待处理气体不做特别限定，比如可以是燃料燃烧后产生的烟气，也可以是空气。
本申请提供的方法，对于二氧化碳的体积含量为1％-50％的待处理气体具有很好的处理效果。
在本申请的具体实施过程中，可以先对烟气进行预处理。预处理装置位于耦合反应器之前，利用预处理装置除去烟气中的水分和颗粒物，避免影响 吸收液对烟气中二氧化碳的吸收，影响二氧化碳的捕集效果，保证后续的耦合反应器的正常运行。
本申请对上述耦合反应器不做特别限定，比如可以是填料塔，也可以是板式塔。
为了确保吸收段内待处理气体与吸收液充分接触，可以将待处理气体从吸收段底部通入，与自吸收段顶部进入的吸收液逆流接触，待处理气体中的二氧化碳从气相被吸收到吸收液中形成富液，残余气可以从吸收段的顶部排放至环境中。
本申请中，富液进入再生段之前可首先进行热交换，在一种实施方式中，富液在吸收段内下行，经换热升温后，进入再生段内，使富液为再生段提供再生反应所需的部分热量，有利于二氧化碳的再生效率。
本申请中，贫液返回吸收段之前可首先进行热交换，在一些实施例中，贫液经换热降温后，返回吸收段内循环使用，使贫液为再生段提供再生反应所需的部分热量，有利于二氧化碳的再生效率。
进一步地，换热后的贫液可先进行冷凝处理后，再返回吸收段使用。
为了实现二氧化碳吸收和再生两个反应过程的热量互补，可以使自再生段底部引出的贫液与自吸收段底部流出的富液进行换热，此外贫液可以为富液在再生段提供部分所需热量。
在上述实施例中，换热过程中，自再生段底部引出的贫液与自吸收段底部流出的富液的比例可根据实际需求合理确定，以实现热量充分利用为宜。
本申请中，通过耦合二氧化碳吸收与再生两个反应过程，在上部的吸收段和下部的再生段内实现两个反应过程的物料互供、热量互补，实现了二氧化碳的吸收和再生。
在另一种实施方式中，富液在吸收段内下行，从吸收段流出后分为两部分，部分富液从再生段的顶部进入再生段，剩余富液经换热升温后，从再生段的中上部进入再生段内。这样，既能够实现两个反应过程的物料互供、热量互补，保证吸收段和再生段的连续进行，还能够降低能耗。
本申请对部分富液与剩余富液的比例不作限定，例如剩余富液占总富液的体积比为5-20％。
在上述实施例中，进一步地，富液在吸收段内下行，从吸收段流出后， 可采用泵将其泵入换热器内。
在本申请具体实施过程中，吸收段内反应通常为：反应温度为10℃-60℃，反应压力0.5MPa-2MPa，待处理气体的气速为0.1m/s-1.5m/s。优选地，吸收段内反应温度为20℃-40℃，反应压力为0.1MPa-1MPa，例如常压，待处理气体的气速可以为0.2m/s-1m/s，其中气速可以是表观气速，指的是待处理气体进入吸收段的空塔流速，根据气速可以确定吸收段的直径，吸收段内反应时间可以根据实际情况来定。
通过调节待处理气体、吸收液的流量等条件，还可进一步实现二氧化碳捕集过程中物料与能量的匹配，使得气体和液体维持稳定反应，确保整个二氧化碳捕集过程中的稳定性，实现气体中二氧化碳的稳定有效的捕集。在一些实施例中，待处理气体与吸收液的气液比为(0.2-0.8)(Nm 3/h/(L/h))。在本申请的具体实施过程中，当待处理气体与吸收液的气液比为0.56(Nm 3/h/(L/h))时，可以控制待处理气体的气体流量为280Nm 3/h，则吸收液的液体流量为500L/h。
本申请对吸收液的具体种类不作限定，可以是目前常用的吸收液，示例性地，在一些实施例中，由于二氧化碳为酸性气体，可以优先选用碱性或碱性盐溶液等作为吸收剂水溶液进行吸收。为了确保吸收液与二氧化碳具有较强的反应性，能够高选择性地吸收二氧化碳，在一些实施例中，吸收剂水溶液为碱性水溶液。
上述吸收液可以采用常规方法获得，例如将吸收剂溶于溶剂中制得吸收液，为进一步增强吸收液对二氧化碳的吸收能力，确保后续再生回收二氧化碳的稳定性，通常选用可溶于水的吸收剂，在本申请的具体实施过程中，可以先将吸收剂溶解在水中，配置成吸收液，吸收液中吸收剂的质量浓度为10wt％-60wt％，例如10％、15％、20％、25％、30％、35％、40％、45％、50％、55％、60％或其中的任意两者组成的范围。
在上述实施例中，吸收剂包括碱性无机物、含氮有机物中的至少一种，优选为碱性无机物、含氮有机物的混合物，其中碱性无机物包括氢氧化钾、氢氧化钠中的至少一种，含氮有机物包括氨基酸盐、有机醇胺中的至少一种。例如吸收液可以是单乙醇胺溶液，也可以是甘氨酸钾溶液。
本申请对于通入再生段内的汽化剂不做特别限定，比如可以是水蒸气， 还可以是水蒸气与含氧气体的混合气。其中含氧气体比如可以是空气、富氧空气、氧气等。在本申请的具体实施过程中，汽化剂可以是流量为75kg/h、压力为0.3MPa的饱和水蒸气。
在本申请的具体实施过程中，气化段内的反应温度一般控制在100℃-130℃，反应压力一般控制在0.1MPa-5MPa，汽化剂的气速一般控制在0.1-1.5m/s。优选地，气化段内的反应温度一般控制在100℃-110℃，反应压力一般控制在0.1MPa-1MPa，气化剂的气速一般控制在0.1-1m/s，其中气速可以是表观气速，指的是汽化剂进入再生段的空塔流速，根据气速可以确定再生段的直径，再生段内反应时间可以根据实际情况来定。在上述条件下进行再生反应，能够确保吸收液充分实现再生，并得到高品质的二氧化碳产品气。
本申请还提供一种二氧化碳捕集装置，用于实现上述的方法，该装置至少包括耦合反应器，其中：
耦合反应器包括上部的吸收段和下部的再生段；吸收段的液相出口与再生段的液相入口相连，再生段的液相出口与吸收段的液相入口相连。
在耦合反应器中，吸收段和再生段之间可以相互贯通，也可以不相互贯通。
上述耦合反应器具体可以是由本领域常用的吸收反应器和再生反应器经适当改造和组装得到的填料塔或板式塔，吸收塔和再生塔最好同轴设置，以方便物料的输运和循环，降低二氧化碳吸收和再生等工艺过程中两个反应器之间的循环操作难度，同时进一步减少装置的占地面积。
吸收段的气相入口一般设置在吸收段底部，用于向吸收段通入待处理气体；吸收段的液相入口一般设置在吸收段的顶部，用于向吸收段内通入吸收液或者贫液。通过将吸收段的气相入口设置在底部，将吸收段的液相入口设置顶部，可以实现待处理气体与吸收液或贫液逆流接触，有助于二氧化碳的捕集效率。
吸收段的液相出口一般设置在吸收段底部，用于向再生段通入富液；吸收段的气相出口一般设置在吸收段的顶部，用于将残余气排出。
再生段的液相入口一般设置在再生段顶部，与吸收段的液相出口相连；再生段的气相入口一般设置在再生段底部，用于向再生段通入气化剂，通过将再生段的气相入口设置在底部，将再生段的液相入口设置顶部，可以 实现气化剂与富液逆流接触，有助于再生效率。
再生段的液相出口一般设置在再生段底部，与吸收段的液相入口相连，用于向吸收段通入贫液。再生段的气相出口一般设置在再生段的顶部，再生的二氧化碳产品气从再生段的气相出口流出。
在上述实施例中，还包括储气罐，储气罐用于临时容置再生的二氧化碳产品，储气罐与再生段的气相出口相连。
需要说明的是，本申请的连通、相连可以管道连通。
在一种实施方式中，为了实现吸收段和再生段热量互补，可以设置换热器，换热器设置在耦合反应器内，或者，换热器设置在耦合反应器外。
本申请中，换热器可以是内置式换热器或外置式换热器。对于内置式换热器，即换热器设置在耦合反应器内，具体可以设置在吸收段和再生段之间。
吸收段的液相出口通过换热器与再生段的液相入口连接，再生段的液相出口通过换热器与吸收段的液相入口连接。
在另一种实施方式中，为了进一步降低能耗，吸收段的液相出口通过第一管路与再生段的第一液相入口连接，且吸收段的液相出口通过换热器与再生段的第二液相入口连接，再生段的液相出口通过换热器与吸收段的液相入口连接。其中，第一液相入口位于再生段的顶部，第二液相入口位于再生段的中上部。
本申请中，气化剂可以是自再生段底部的气相入口通入的高温气化剂，也可以在再生段内的下部设置加热段，具体可以是：富液在再生段内下行，至再生段底部，经加热段加热后，产生水蒸气和二氧化碳混合物，水蒸气作为气化剂与后续下行的富液接触进行再生。
为了实现对气体流量和液体流量的控制，本申请的二氧化碳捕集装置还可以包括流量控制装置，流量控制装置包括气体流量控制装置和液体流量控制装置，其中气体流量控制装置位于吸收段前端，气体流量控制装置后端与吸收单元的气相入口相连。
在上述实施例中，可以设置阀门根据监测获得的数据对流量控制装置进行实时调节控制。
本申请的二氧化碳捕集装置还可以包括气体成分分析装置，设置在再 生段的气相出口端，用于对再生气进行成分分析。
本申请中，可以采取泵压的方式使待处理气体、吸收液进入吸收段内，也可以采取泵压的方式使贫液进入吸收段内。
本申请中，采用上述二氧化碳捕集装置实施二氧化碳捕集方法，具体工艺步骤如下：
步骤一：使待处理气体经气体流量控制装置调节流量后经吸收段底部的气相入口送入吸收段内，使吸收液经吸收段顶部的液相入口送入吸收段内，两相以平行逆流的方式接触进行二氧化碳的吸收处理，经吸收处理后，得到富液和残余气；
步骤二：反应后得到的富液在吸收段内下行，由吸收段底部的液相出口流出；吸收处理后的残余气上行，由吸收段顶部的气相出口流出，对残余气进行成分分析，残余气经检测达标后排入大气；
步骤三：使气化剂自再生段的气相入口进入再生段，使富液进入再生段内与上行的气化剂接触，得到二氧化碳和贫液。
本申请提供的二氧化碳捕集装置结构简单，使用方便快捷，能够实现二氧化碳吸收和再生两个反应过程中的物料互供和热量互补，降低了二氧化碳捕集过程的能耗和物料循环操作难度，提高了二氧化碳捕集率和再生率。此外该装置还具有较小的占地面积和较低的投资成本。
为使本申请的目的、技术方案和优点更加清楚，下面将结合本申请的实施例，对本申请实施例中的技术方案进行清楚、完整地描述，显然，所描述的实施例是本申请一部分实施例，而不是全部的实施例。基于本申请中的实施例，本领域普通技术人员在没有做出创造性劳动前提下所获得的所有其他实施例，都属于本申请保护的范围。
实施例1
如图1所示，本实施例的二氧化碳捕集装置至少包括：耦合反应器100、换热器130
其中：耦合反应器100包括上部的吸收段110和下部的再生段120；吸收段110的液相出口与再生段120的液相入口相连，再生段120的液相出口与吸收段110的液相入口相连；
吸收段110的气相入口用于向吸收段110通入待处理气体，吸收段110 的液相入口用于向吸收段110内通入吸收液或者贫液，吸收段110的液相出口用于向再生段120通入富液，吸收段110的气相出口用于将残余气排出。
再生段120的液相入口与吸收段110的液相出口相连，再生段120的气相入口用于向再生段120通入气化剂，再生段120的液相出口与吸收段110的液相入口相连，用于向吸收段110通入贫液；
吸收段110的液相出口通过换热器130与再生段120的液相入口连接，再生段120的液相出口通过换热器130与吸收段110的液相入口连接；
本实施例的二氧化碳捕集装置还包括泵140，再生段120的液相出口通过泵与换热器130连接。
本实施例的二氧化碳捕集方法在上述装置中进行，包括如下的工艺步骤：
使二氧化碳浓度为13％的烟气以流量为280Nm 3/h经吸收段底部的气相入口送入吸收段内，按照气液比为0.56(Nm 3/h/(L/h))，使质量含量为30％的甘氨酸钾溶液经吸收段顶部的液相入口送入吸收段内，两相以平行逆流的方式接触进行二氧化碳的吸收处理，经吸收处理后，得到富液和残余气；其中：吸收处理后的残余气上行，由吸收段顶部的气相出口流出，对残余气进行成分分析，残余气经检测达标后排入大气；
反应后得到的富液在吸收段内下行，由吸收段底部的液相出口流出时，富液温度为65℃；使温度为65℃的富液进入换热器，经换热升温至90℃后进入再生段内，与气速为1m/s、压力为0.3MPa的饱和水蒸气(其中饱和水蒸气自再生段的气相入口进入再生段内)进行逆流接触，在再生段的气相出口收集到流量为25.4Nm 3/h的二氧化碳产品气，将101℃的贫液从再生段底部排出，通过泵压方式将贫液泵入换热器中降温，然后经吸收段的液相入口返回吸收段；
经计算，本实施例二氧化碳再生率为69.7％，且二氧化碳产品气的纯度(干基)可达99％以上。
实施例2
如图1所示，本实施例的二氧化碳捕集装置至少包括：耦合反应器100、换热器130
其中：耦合反应器100包括上部的吸收段110和下部的再生段120；吸收段110的液相出口与再生段120的液相入口相连，再生段120的液相出口与吸收段110的液相入口相连；
吸收段110的气相入口用于向吸收段110通入待处理气体，吸收段110的液相入口用于向吸收段110内通入吸收液或者贫液，吸收段110的液相出口用于向再生段120通入富液，吸收段110的气相出口用于将残余气排出。
再生段120的液相入口与吸收段110的液相出口相连，再生段120的气相入口用于向再生段120通入气化剂，再生段120的液相出口与吸收段110的液相入口相连，用于向吸收段110通入贫液；
吸收段110的液相出口通过换热器130与再生段120的液相入口连接，再生段120的液相出口通过换热器130与吸收段110的液相入口连接；
本实施例的二氧化碳捕集装置还包括泵140，再生段120的液相出口通过泵与换热器130连接。
本实施例的二氧化碳捕集方法在上述装置中进行，包括如下的工艺步骤：
使二氧化碳浓度为13％的烟气以流量为280Nm 3/h经吸收段底部的气相入口送入吸收段内，按照气液比为0.2(Nm 3/h/(L/h))，使质量含量为10％的单乙醇胺溶液经吸收段顶部的液相入口送入吸收段内，两相以平行逆流的方式接触进行二氧化碳的吸收处理，经吸收处理后，得到富液和残余气；其中：吸收处理后的残余气上行，由吸收段顶部的气相出口流出，对残余气进行成分分析，残余气经检测达标后排入大气；
反应后得到的富液在吸收段内下行，由吸收段底部的液相出口流出时，富液温度为65℃；使温度为65℃的富液进入换热器，经换热升温至90℃后进入再生段内，与气速为0.1m/s、压力为0.3MPa的饱和水蒸气(其中饱和水蒸气自再生段的气相入口进入再生段内)进行逆流接触，在再生段的气相出口收集到流量为19.95Nm 3/h的二氧化碳产品气，将101℃的贫液从再生段底部排出，通过泵压方式将贫液泵入换热器中降温，然后经吸收段的液相入口返回吸收段；
经计算，本实施例二氧化碳再生率为54.8％，且二氧化碳产品气的纯度 (干基)可达99％以上。
实施例3
如图1所示，本实施例的二氧化碳捕集装置至少包括：耦合反应器100、换热器130
其中：耦合反应器100包括上部的吸收段110和下部的再生段120；吸收段110的液相出口与再生段120的液相入口相连，再生段120的液相出口与吸收段110的液相入口相连；
吸收段110的气相入口用于向吸收段110通入待处理气体，吸收段110的液相入口用于向吸收段110内通入吸收液或者贫液，吸收段110的液相出口用于向再生段120通入富液，吸收段110的气相出口用于将残余气排出。
再生段120的液相入口与吸收段110的液相出口相连，再生段120的气相入口用于向再生段120通入气化剂，再生段120的液相出口与吸收段110的液相入口相连，用于向吸收段110通入贫液；
吸收段110的液相出口通过换热器130与再生段120的液相入口连接，再生段120的液相出口通过换热器130与吸收段110的液相入口连接；
本实施例的二氧化碳捕集装置还包括泵140，再生段120的液相出口通过泵与换热器130连接。
本实施例的二氧化碳捕集方法在上述装置中进行，包括如下的工艺步骤：
使二氧化碳浓度为13％的烟气以流量为280Nm 3/h经吸收段底部的气相入口送入吸收段内，按照气液比为0.8(Nm 3/h/(L/h))，使质量含量为60％的单乙醇胺溶液经吸收段顶部的液相入口送入吸收段内，两相以平行逆流的方式接触进行二氧化碳的吸收处理，经吸收处理后，得到富液和残余气；其中：吸收处理后的残余气上行，由吸收段顶部的气相出口流出，对残余气进行成分分析，残余气经检测达标后排入大气；
反应后得到的富液在吸收段内下行，由吸收段底部的液相出口流出时，富液温度为65℃；使温度为65℃的富液进入换热器，经换热升温至90℃后进入再生段内，与气速为1.5m/s、压力为0.3MPa的饱和水蒸气(其中饱和水蒸气自再生段的气相入口进入再生段内)进行逆流接触，在再生段的气相出 口收集到流量为30.03Nm 3/h的二氧化碳产品气，将101℃的贫液从再生段底部排出，通过泵压方式将贫液泵入换热器中降温，然后经吸收段的液相入口返回吸收段；
经计算，本实施例二氧化碳再生率为82.5％，且二氧化碳产品气的纯度(干基)可达99％以上。
实施例4
如图2所示，本实施例的二氧化碳捕集装置至少包括：耦合反应器100、换热器130；
其中：耦合反应器100包括上部的吸收段110和下部的再生段120；吸收段110的液相出口与再生段120的液相入口相连，再生段120的液相出口与吸收段110的液相入口相连；
吸收段110的气相入口用于向吸收段110通入待处理气体，吸收段110的液相入口用于向吸收段110内通入吸收液或者贫液，吸收段110的液相出口用于向再生段120通入富液，吸收段110的气相出口用于将残余气排出；
再生段120的液相入口与吸收段110的液相出口相连，再生段120的气相入口用于向再生段120通入气化剂，再生段120的液相出口与吸收段110的液相入口相连，用于向吸收段110通入贫液；
吸收段的液相出口通过第一管路与再生段的第一液相入口连接，吸收段的液相出口通过换热器与再生段的第二液相入口连接；第一液相入口位于再生段的顶部，第二液相入口位于再生段的中上部；
再生段120的液相出口通过换热器130与吸收段110的液相入口连接；
本实施例的二氧化碳捕集装置还包括泵140、泵150。再生段120的液相出口通过泵140与换热器130连接，吸收段110的富液出口通过泵150与换热器130及再生段120顶部富液入口。
本实施例的二氧化碳捕集方法在上述装置中进行，包括如下的工艺步骤：
使二氧化碳浓度为13％的烟气以流量为280Nm 3/h经吸收段底部的气相入口送入吸收段内，按照气液比为0.8(Nm 3/h/(L/h))，使质量含量为60％的单乙醇胺溶液经吸收段顶部的液相入口送入吸收段内，两相以平行逆流的方式 接触进行二氧化碳的吸收处理，经吸收处理后，得到富液和残余气；其中：吸收处理后的残余气上行，由吸收段顶部的气相出口流出，对残余气进行成分分析，残余气经检测达标后排入大气；
反应后得到的富液在吸收段内下行，由吸收段底部的液相出口流出时，富液温度为65℃；富液分两股进入再生段，一股是体积占总富液的5％直接进入再生段顶部，另一股进入换热器，经换热升温至90℃后进入再生段内，与气速为1.5m/s、压力为0.3MPa的饱和水蒸气(其中饱和水蒸气自再生段的气相入口进入再生段内)进行逆流接触，在再生段的气相出口收集到流量为30.03Nm 3/h的二氧化碳产品气，将101℃的贫液从再生段底部排出，通过泵压方式将贫液泵入换热器中降温，然后经吸收段的液相入口返回吸收段；
经计算，本实施例二氧化碳再生率为85.6％，且二氧化碳产品气的纯度(干基)可达99％以上。
实施例5
如图2所示，本实施例的二氧化碳捕集装置至少包括：耦合反应器100、换热器130
其中：耦合反应器100包括上部的吸收段110和下部的再生段120；吸收段110的液相出口与再生段120的液相入口相连，再生段120的液相出口与吸收段110的液相入口相连；
吸收段110的气相入口用于向吸收段110通入待处理气体，吸收段110的液相入口用于向吸收段110内通入吸收液或者贫液，吸收段110的液相出口用于向再生段120通入富液，吸收段110的气相出口用于将残余气排出。
再生段120的液相入口与吸收段110的液相出口相连，再生段120的气相入口用于向再生段120通入气化剂，再生段120的液相出口与吸收段110的液相入口相连，用于向吸收段110通入贫液；
吸收段110的液相出口通过换热器130与再生段120的液相入口连接，再生段120的液相出口通过换热器130与吸收段110的液相入口连接；
本实施例的二氧化碳捕集装置还包括泵140、泵150。再生段120的液相出口通过泵140与换热器130连接，吸收段110的富液出口通过泵150与换热器130及再生段120顶部富液入口。
本实施例的二氧化碳捕集方法在上述装置中进行，包括如下的工艺步骤：
使二氧化碳浓度为13％的烟气以流量为280Nm 3/h经吸收段底部的气相入口送入吸收段内，按照气液比为0.8(Nm 3/h/(L/h))，使质量含量为60％的单乙醇胺溶液经吸收段顶部的液相入口送入吸收段内，两相以平行逆流的方式接触进行二氧化碳的吸收处理，经吸收处理后，得到富液和残余气；其中：吸收处理后的残余气上行，由吸收段顶部的气相出口流出，对残余气进行成分分析，残余气经检测达标后排入大气；
反应后得到的富液在吸收段内下行，由吸收段底部的液相出口流出时，富液温度为65℃；富液分两部分进入再生段，部分富液(体积占总富液的20％)通过再生段顶部的第一液相入口进入，剩余富液进入换热器，经换热升温至90℃后通过再生段中下部的第二液相入口进入再生段内，与气速为1.5m/s、压力为0.3MPa的饱和水蒸气(其中饱和水蒸气自再生段的气相入口进入再生段内)进行逆流接触，在再生段的气相出口收集到流量为30.03Nm 3/h的二氧化碳产品气，将101℃的贫液从再生段底部排出，通过泵压方式将贫液泵入换热器中降温，然后经吸收段的液相入口返回吸收段；
经计算，本实施例二氧化碳再生率为80.6％，且二氧化碳产品气的纯度(干基)可达99％以上。
实施例6
如图2所示，本实施例的二氧化碳捕集装置至少包括：耦合反应器100、换热器130
其中：耦合反应器100包括上部的吸收段110和下部的再生段120；吸收段110的液相出口与再生段120的液相入口相连，再生段120的液相出口与吸收段110的液相入口相连；
吸收段110的气相入口用于向吸收段110通入待处理气体，吸收段110的液相入口用于向吸收段110内通入吸收液或者贫液，吸收段110的液相出口用于向再生段120通入富液，吸收段110的气相出口用于将残余气排出。
再生段120的液相入口与吸收段110的液相出口相连，再生段120的气相入口用于向再生段120通入气化剂，再生段120的液相出口与吸收段 110的液相入口相连，用于向吸收段110通入贫液；
吸收段的液相出口通过第一管路与再生段的第一液相入口连接，吸收段的液相出口通过换热器与再生段的第二液相入口连接；第一液相入口位于再生段的顶部，第二液相入口位于再生段的中上部；
再生段120的液相出口通过换热器130与吸收段110的液相入口连接；
本实施例的二氧化碳捕集装置还包括泵140、泵150及冷凝器160。再生段120的液相出口通过泵140与换热器130连接，吸收段110的富液出口通过泵150与换热器130及再生段120顶部富液入口，换热器130来的吸收贫液通过冷凝器160与吸收段110连接。
本实施例的二氧化碳捕集方法在上述装置中进行，包括如下的工艺步骤：
使二氧化碳浓度为13％的烟气以流量为280Nm 3/h经吸收段底部的气相入口送入吸收段内，按照气液比为0.8(Nm 3/h/(L/h))，使质量含量为60％、温度为40℃的单乙醇胺溶液经吸收段顶部的液相入口送入吸收段内，两相以平行逆流的方式接触进行二氧化碳的吸收处理，经吸收处理后，得到富液和残余气；其中：吸收处理后的残余气上行，由吸收段顶部的气相出口流出，对残余气进行成分分析，残余气经检测达标后排入大气；
反应后得到的富液在吸收段内下行，由吸收段底部的液相出口流出时，富液温度为65℃；富液分两部分进入再生段，部分富液(体积占总富液的5％)通过再生段顶部的第一液相入口直接进入再生段顶部，剩余富液进入换热器，经换热升温至90℃后通过再生段的第二液相入口进入再生段内，与气速为1.5m/s、压力为0.3MPa的饱和水蒸气(其中饱和水蒸气自再生段的气相入口进入再生段内)进行逆流接触，在再生段的气相出口收集到流量为30.03Nm 3/h的二氧化碳产品气，将101℃的贫液从再生段底部排出，通过泵压方式将贫液泵入换热器中降温，然后经吸收段的液相入口返回吸收段；
经计算，本实施例二氧化碳再生率为87.2％，且二氧化碳产品气的纯度(干基)可达99％以上。
本申请提供的二氧化碳捕集方法和装置，该装置将吸收段和再生段集成在同一个耦合反应器中，实现了二氧化碳吸收和再生两个反应过程中的物料互供，相较于现阶段二氧化碳捕集技术，物料在两个反应器之间输运 和循环的工艺方法，本申请提供的方法，不仅能够显著降低二氧化碳捕集过程中的能耗、提高二氧化碳捕集效率，而且还解决了现阶段物料循环操作难度高的问题，此外还解决了当前二氧化碳捕集装置占地面积大、设备投资高的问题，有利于实现大规模推广应用。
以上详细描述了本申请的较佳具体实施例以及试验验证。应当理解，本领域的普通技术无需创造性劳动就可以根据本申请的构思作出诸多修改和变化。因此，凡本技术领域中技术人员依本申请的构思在现有技术的基础上通过逻辑分析、推理或者有限的实验可以得到的技术方案，皆应在由权利要求书所确定的保护范围内。

Claims (13)

  1. 一种二氧化碳捕集方法，其中，该方法利用耦合反应器作为反应器，所述耦合反应器包括上部的吸收段和下部的再生段；
    所述方法包括：将待处理气体通入所述吸收段内，与吸收液接触，得到富液和残余气，所述残余气从所述吸收段顶部排出；
    所述富液在所述吸收段内下行，进入所述再生段内，在所述再生段与汽化剂接触，得到二氧化碳和贫液，其中，所述二氧化碳自再生段顶部排出，所述贫液返回吸收段内循环使用。
  2. 根据权利要求1所述的二氧化碳捕集方法，其中，所述富液在所述吸收段内下行，经换热升温后，进入所述再生段内。
  3. 根据权利要求1所述的二氧化碳捕集方法，其中，所述富液在所述吸收段内下行，从吸收段流出后分为两部分，部分富液从再生段的顶部进入所述再生段，剩余富液经换热升温后，从再生段的中上部进入所述再生段内。
  4. 根据权利要求3所述的二氧化碳捕集方法，其中，所述部分富液占总富液的体积比为5-20％。
  5. 根据权利要求1-4任一项所述的二氧化碳捕集方法，所述贫液经换热降温后，返回吸收段内循环使用。
  6. 根据权利要求1-5任一项所述的二氧化碳捕集方法，其中，在所述吸收段内，反应温度为10℃-60℃。
  7. 根据权利要求1-6任一项所述的二氧化碳捕集方法，其中，所述待处理气体与所述吸收液的气液比为(0.2-0.8)(Nm 3/h/(L/h))。
  8. 根据权利要求1-7任一项所述的二氧化碳捕集方法，其中，所述吸收液包括碱性溶液。
  9. 根据权利要求1-8任一项所述的二氧化碳捕集方法，其中，所述吸收液中吸收剂的质量浓度为10wt％-60wt％，所述吸收剂包括碱性无机物、含氮有机物中的至少一种。
  10. 根据权利要求1-9任一项所述的二氧化碳捕集方法，其中，在所述再生段内，反应温度为100℃-130℃，所述汽化剂的气速为0.1m/s-1.5m/s。
  11. 一种二氧化碳捕集装置，其中，用于实现权利要求1-10任一项所述的 方法，其中，所述装置至少包括耦合反应器，其中：
    所述耦合反应器包括上部的吸收段和下部的再生段；所述吸收段的液相出口与所述再生段的液相入口相连，所述再生段的液相出口与所述吸收段的液相入口相连。
  12. 根据权利要求11所述的二氧化碳捕集装置，其中，还包括换热器，所述换热器设置在所述耦合反应器内，或者，所述换热器设置在所述耦合反应器外；所述吸收段的液相出口通过所述换热器与所述再生段的液相入口连接，所述再生段的液相出口通过所述换热器与所述吸收段的液相入口连接。
  13. 根据权利要求11所述的二氧化碳捕集装置,其中，还包括换热器，所述换热器设置在所述耦合反应器内，或者，所述换热器设置在所述耦合反应器外；
    所述吸收段的液相出口通过第一管路与所述再生段的第一液相入口连接，且所述所述吸收段的液相出口通过所述换热器与所述再生段的第二液相入口连接，所述再生段的液相出口通过所述换热器与所述吸收段的液相入口连接。
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Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20090293722A1 (en) * 2005-06-28 2009-12-03 Svendsen Hallvard F Method and Apparatus for Energy Reduction In Acid Gas Capture
CN201940151U (zh) * 2010-10-14 2011-08-24 中国石油化工股份有限公司 一种油气吸收及吸收剂再生耦合装置
CN202605989U (zh) * 2012-06-07 2012-12-19 中国华能集团清洁能源技术研究院有限公司 一种二氧化碳捕集再生装置
CN103097000A (zh) * 2010-07-20 2013-05-08 鲍尔斯潘公司 用于从气流洗涤co2的吸收介质和使用所述介质的方法
CN205868002U (zh) * 2016-08-01 2017-01-11 江苏揽山环境科技股份有限公司 脱硫反应塔
CN208493731U (zh) * 2018-01-12 2019-02-15 杭州中环化工设备有限公司 有机胺负压循环脱硫系统
CN110115913A (zh) * 2019-06-20 2019-08-13 中国华能集团清洁能源技术研究院有限公司 一种抑制吸收剂挥发的二氧化碳捕集系统及方法
US20210291108A1 (en) * 2020-03-18 2021-09-23 Kabushiki Kaisha Toshiba Acidic gas absorbent, acidic gas removal method and acidic gas removal apparatus

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20090293722A1 (en) * 2005-06-28 2009-12-03 Svendsen Hallvard F Method and Apparatus for Energy Reduction In Acid Gas Capture
CN103097000A (zh) * 2010-07-20 2013-05-08 鲍尔斯潘公司 用于从气流洗涤co2的吸收介质和使用所述介质的方法
CN201940151U (zh) * 2010-10-14 2011-08-24 中国石油化工股份有限公司 一种油气吸收及吸收剂再生耦合装置
CN202605989U (zh) * 2012-06-07 2012-12-19 中国华能集团清洁能源技术研究院有限公司 一种二氧化碳捕集再生装置
CN205868002U (zh) * 2016-08-01 2017-01-11 江苏揽山环境科技股份有限公司 脱硫反应塔
CN208493731U (zh) * 2018-01-12 2019-02-15 杭州中环化工设备有限公司 有机胺负压循环脱硫系统
CN110115913A (zh) * 2019-06-20 2019-08-13 中国华能集团清洁能源技术研究院有限公司 一种抑制吸收剂挥发的二氧化碳捕集系统及方法
US20210291108A1 (en) * 2020-03-18 2021-09-23 Kabushiki Kaisha Toshiba Acidic gas absorbent, acidic gas removal method and acidic gas removal apparatus

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