CN109954382B - Direct desorption type carbon capture system for solar energy interface evaporation and control method thereof - Google Patents
Direct desorption type carbon capture system for solar energy interface evaporation and control method thereof Download PDFInfo
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- CN109954382B CN109954382B CN201910295506.2A CN201910295506A CN109954382B CN 109954382 B CN109954382 B CN 109954382B CN 201910295506 A CN201910295506 A CN 201910295506A CN 109954382 B CN109954382 B CN 109954382B
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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
- B01D53/46—Removing components of defined structure
- B01D53/62—Carbon oxides
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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
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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
- B01D53/96—Regeneration, reactivation or recycling of reactants
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- 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
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- 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
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- 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 discloses a direct desorption type carbon capture system by solar energy interface evaporation, which mainly comprises a carbon dioxide absorption part, a desorption tower desorption part, a solar energy interface evaporation desorption part and a molecular photo-thermal energy storage part. The invention improves the carbon capture system based on the chemical absorption method, adds a solar energy interface evaporation desorption device to realize the function of a desorption tower-reboiler, and directly desorbs carbon dioxide from an absorbent through the interface evaporation device; the auxiliary heating of the molecular photo-thermal energy storage system is increased, and the energy loss during energy storage of the traditional energy storage device is reduced. A control method of the system is also disclosed. According to the invention, the novel solar energy utilization device couples renewable energy sources into the carbon trapping system, so that the problem of high energy consumption of the traditional carbon trapping system is solved, and the development of the carbon negative emission technology in China is promoted.
Description
Technical Field
The invention relates to the technical field of direct desorption type carbon capture by solar interface evaporation, relates to an absorption method carbon dioxide capture technology, a novel solar interface evaporation technology and a solar molecular photo-thermal energy storage technology, and in particular relates to a direct desorption type carbon capture system by solar interface evaporation and a control method thereof.
Background
The continuous increase in greenhouse gas emissions has led to a growing global warming, which is attracting attention from countries. While in greenhouse gases, CO 2 The greenhouse effect caused by the increase of the concentration is particularly serious. Carbon Capture and Sequestration (CCS) technology is one of the approaches to achieve active carbon abatement. International Energy Agency (IEA) notes that current global energy sector CO is considered 2 Discharge amountThe increasing trend and the continual play of fossil fuels in primary energy consumption have led to an increase in CCS urgency. The importance of carbon capture technology can be seen.
The carbon trapping technology by the chemical absorption method can be directly applied to the existing coal-fired power plants and industrial systems, and the development is the most mature. However, high energy consumption is a critical drawback that has been limiting for its further commercialization, especially the energy consumption required for the absorbent regeneration process, up to 3GJ/t CO 2 . The conventional desorption mode is based on a "stripper-reboiler" structure, and high-temperature steam is supplied by using a reboiler, so that a stripping process is realized in the stripper, thereby resulting in high energy consumption of the reboiler. On one hand, the desorption can be completed by using renewable energy as an auxiliary heat source to assist the desorption tower; on the other hand, the search for new desorption techniques is also an important direction to solve the energy consumption problem.
Solar interfacial evaporation technology was originally used to solve the sea water desalination problem, and interfacial evaporation can achieve higher thermal efficiency and steam rate through thermal localization than traditional bulk heating, and is leading to extensive research due to its technical advantages. With the development of technology, solar energy interface evaporation has been applied in the fields of medical sterilization, sewage treatment, etc., and the realization of carbon capture desorption process by absorption is an innovative application of the technology. The technology realizes a high-temperature environment through absorber heating, realizes a stripping process of a desorption tower through interfacial evaporation, and finally realizes steam-CO by utilizing a gas-liquid separator 2 The separation can replace the traditional desorption mode of a desorption tower-reboiler to a certain extent. The molecular photo-thermal energy storage technology is a novel solar energy utilization and energy storage mode, has the advantages of long energy storage life, high energy storage density and low loss compared with the traditional liquid heat storage, can further reduce energy consumption and simultaneously overcomes the defect of unstable solar energy when being applied to the carbon capture technology.
Disclosure of Invention
Aiming at the defect of high energy consumption of the regeneration of the absorbent by the traditional absorption method carbon capture technology, the invention provides a direct desorption type carbon capture system by solar interface evaporation, which utilizes a solar interface evaporation device to partially replace a desorption tower function to complete the desorption process, thereby effectively reducing the energy consumption required by the regeneration of the absorbent; meanwhile, a molecular photo-thermal energy storage system is added to assist in heating, so that instability of solar energy is compensated.
In order to solve the technical problems, the technical scheme provided by the invention is that the direct desorption type carbon capture system by solar energy interface evaporation comprises a carbon dioxide absorption part, a desorption tower desorption part, a solar energy interface evaporation desorption part and a molecular photo-thermal energy storage part; the trapping system adopting the chemical absorption method realizes CO by utilizing the solar energy interface evaporation device 2 The desorption process of (2) partially replaces the traditional 'desorption tower-reboiler', solar energy is used as absorbent renewable energy, and the molecular photo-thermal energy storage part is used for auxiliary heating of the absorbent.
The carbon dioxide absorbing part comprises an absorbing tower, a rich liquid pump, a lean/rich liquid heat exchanger and a condenser; the rich liquid outlet at the bottom of the absorption tower is connected to the rich liquid inlet of the lean/rich liquid heat exchanger after passing through the rich liquid pump, the rich liquid outlet of the lean/rich liquid heat exchanger is connected with the heat exchanger, and the lean liquid inlet and the lean liquid outlet of the lean/rich liquid heat exchanger are respectively connected to the lean liquid pump outlet and the lean liquid inlet of the condenser; the condenser outlet is connected to the absorption tower inlet;
the carbon dioxide absorbing part has the function of absorbing CO in the gas to be separated by using an absorbent 2 The method comprises the steps of carrying out a first treatment on the surface of the The gas to be separated enters an absorption tower from the bottom and is absorbed by an absorbent to absorb CO 2 Then the absorbent is discharged from the top to become rich liquid; and the rich liquid is pumped into the lean/rich liquid heat exchanger and the heat exchanger in turn by a rich liquid pump to exchange heat, and the rich liquid enters a desorption tower or an interfacial evaporation desorber after heat exchange, so that the absorption process is completed.
The desorption part of the desorption tower comprises a desorption tower, a first gas-liquid separator, a reboiler, a first control valve, a second control valve and a lean liquid pump; the top rich liquid inlet of the desorption tower is connected to the rich liquid outlet of the heat exchanger through a control valve, the top outlet of the desorption tower is connected to the inlet of the gas-liquid separator I, and the liquid outlet of the gas-liquid separator I is connected to the top inlet of the desorption tower; the outlet and inlet at the bottom of the desorption tower are respectively connected to a reboiler solution inlet and a steam outlet; the lean solution outlet of the reboiler is connected to the lean solution pump inlet through a control valve II;
the desorber has the function of separating CO from the absorbent by the stripping process of the desorber 2 The method comprises the steps of carrying out a first treatment on the surface of the The rich liquid enters a desorption tower from the top after heat exchange, and is fully contacted with steam from bottom to top, CO 2 Enters the vapor phase from the top and enters the gas-liquid separator to be separated, and the separated CO 2 The outflow is collected, and the separated liquid returns to the desorption tower from the top; and the rich liquid is desorbed to form a lean liquid, and the lean liquid flows out of the reboiler and is pumped into a lean/rich liquid heat exchanger by a lean liquid pump to finish desorption.
The solar energy interface evaporation desorption part comprises a glass cover plate, an absorber, a porous medium layer, a cotton core, a heat insulation layer, a gas-liquid separator II, a control valve III and a control valve IV; the glass cover plate, the absorber, the porous medium layer, the cotton core and the heat insulation layer form an interface evaporation desorber; the glass cover plate adopts double-layer heat insulation treatment to achieve the heat preservation function; the absorber is positioned at the uppermost layer in the desorber, is made of a porous material and is made of a carbon-based material or a plasmon material; the porous medium layer is positioned on the lower layer of the absorber; the heat insulation layer is positioned between the porous medium layer and the solution water surface, a solution transportation channel is arranged in the heat insulation layer and is connected with the solution and the porous medium layer, cotton cores are inserted in the channel, and the heat insulation layer is made of foam plastics; the solution inlet and outlet at the bottom of the interface evaporation desorber are respectively connected to the solution outlet of the heat exchanger and the inlet of the lean solution pump through a third control valve and a fourth control valve; the top outlet of the desorber is connected with the inlet of the second gas-liquid separator, and the liquid outlet of the second gas-liquid separator is connected to the inlet of the lean liquid pump through the fourth control valve;
the solar energy interface evaporation desorption part has the function of separating CO in the absorbent by utilizing the interface evaporation principle 2 The method comprises the steps of carrying out a first treatment on the surface of the The absorber absorbs sunlight and then heats up, and the rich liquid entering the interface evaporation desorber is transported to the surface of the absorber through the capillary action of the cotton core and the porous medium layer; due to the porous nature of the absorber, the liquid forms a liquid film to cover the absorber for rapid evaporation, and simultaneously desorbs CO 2 The method comprises the steps of carrying out a first treatment on the surface of the Vaporising gas and CO 2 Separating by gas-liquid separator, collecting the separated liquid into absorbent flowing out of interfacial evaporation desorber, pumping by lean solution pumpAnd (3) entering a lean/rich liquid heat exchanger to finish desorption.
The molecular photo-thermal energy storage part comprises a solar energy collector, a first liquid storage tank, a fifth control valve, a sixth control valve, a catalytic reaction cavity, a heat exchanger, a working medium pump and a second liquid storage tank; the outlet of the solar collector is connected to an inlet of the liquid storage tank; the upper outlet and the lower outlet of the liquid storage tank I are respectively connected to the catalytic reaction cavity through a control valve five and a control valve six; the outlet of the catalytic reaction cavity, the working medium inlet and outlet of the heat exchanger, the working medium pump inlet and outlet, the second inlet and outlet of the liquid storage tank and the inlet of the solar collector are sequentially connected; the molecular photothermal energy storage part cycle working medium adopts azobenzene, norbornadiene or ruthenium-rich fulvalene compounds;
the molecular photo-thermal energy storage part has the functions of auxiliary heating and energy storage for a system; the working medium absorbs photons in the solar collector and then undergoes photoisomerization reaction to form photoisomers, and the working medium rich in the photoisomers enters and fills the first liquid storage tank; the working medium flows out of the first liquid storage tank and then enters the catalytic reaction cavity, and is catalyzed to perform reverse reaction to release energy and raise the temperature; and after the higher-temperature working medium heats the rich liquid from the lean/rich liquid heat exchanger through the heat exchanger, the rich liquid is pumped into the second liquid storage tank by the working medium pump, and finally returns to the solar collector to complete circulation.
The second technical scheme of the invention is a control method of a direct desorption type carbon capture system by solar interface evaporation, which comprises four working modes:
mode one: when sunlight is sufficient in daytime, the first control valve and the second control valve are closed, the third control valve and the fourth control valve are opened, the desorption part of the desorption tower stops working, the evaporation and desorption part of the solar interface works normally, and the energy source in the desorption process is solar energy; opening a control valve five, closing a control valve six, enabling the solar collector to work normally, storing the photoisomer working medium in a liquid storage tank I, and normally assisting in heating the whole molecular photothermal energy storage part;
mode two: when sunlight is insufficient in daytime, the first control valve and the second control valve are opened, the third control valve and the fourth control valve are opened, the desorption part of the desorption tower and the evaporation desorption part of the solar interface work normally, and energy sources in the desorption process are solar energy and reboiler energy consumption; opening a control valve five and a control valve six, enabling the solar collector to work normally, and enabling the liquid storage tank I to provide stored photoisomer working medium, so that the whole molecular photothermal energy storage part can be heated normally in an auxiliary mode;
mode three: when the energy storage is sufficient at night, the first control valve and the second control valve are opened, the third control valve and the fourth control valve are closed, the desorption part of the desorption tower normally works, the solar energy interface evaporation desorption part stops working, and the energy source in the desorption process is reboiler energy consumption; closing a control valve five, opening a control valve six, stopping the solar collector, providing the stored photoisomer working medium by a first liquid storage tank, normally assisting in heating the whole molecular photothermal energy storage part, and storing the reacted working medium in a second liquid storage tank;
mode four: when the energy storage is insufficient at night, the first control valve and the second control valve are opened, the third control valve and the fourth control valve are closed, the desorption part of the desorption tower normally works, the solar energy interface evaporation desorption part stops working, and the energy source in the desorption process is reboiler energy consumption; and closing the control valve five and the control valve six, stopping the operation of the whole molecular photo-thermal energy storage part, and maintaining the temperature required by desorption by a reboiler.
Compared with the prior art, the invention has the advantages that:
(1) Realization of CO by solar energy interface evaporation principle 2 The desorption process shares the functions of the traditional desorption tower and reduces the energy consumption required by a reboiler.
(2) The molecular photo-thermal energy storage system is introduced, solar energy is stored into chemical energy by utilizing a photochemical principle, the molecular photo-thermal energy storage system has the characteristics of good stability and long energy storage time, and the desorption process is promoted by auxiliary heating of a heat exchanger.
(3) The novel solar energy utilization technology is adopted, the solar energy utilization form is widened, and the solar energy utilization efficiency is improved.
Drawings
FIG. 1 is a schematic diagram of the principle and structure of a direct desorption type carbon capture system by solar energy interface evaporation;
FIG. 2 is a schematic view of the solar interface evaporation desorber of FIG. 1;
in the figure: the device comprises a 1-absorption tower, a 2-rich liquid pump, a 3-lean/rich liquid heat exchanger, a 4-desorption tower, a 5-gas-liquid separator I, a 6-reboiler, a 7-control valve II, an 8-lean liquid pump, a 9-condenser, a 10-solar collector, a 11-liquid storage tank I, a 12-control valve V, a 13-control valve V, a 14-catalytic reaction cavity, a 15-heat exchanger, a 16-working medium pump, a 17-liquid storage tank II, a 18-control valve III, a 19-control valve I, a 20-glass cover plate, a 21-absorber, a 22-porous medium layer, a 23-cotton core, a 24-heat insulation layer, a 25-gas-liquid separator II and a 26-control valve IV.
Detailed Description
The invention is described in further detail below in connection with specific embodiments. The present embodiment is implemented on the premise of the technical scheme of the present invention, and a detailed implementation manner and a specific operation process are provided, but the protection scope of the present invention is not limited to the following embodiments.
As shown in FIG. 1, the direct desorption type carbon capture system by solar interface evaporation mainly comprises a carbon dioxide absorption part, a desorption tower desorption part, a solar interface evaporation desorption part and a molecular photo-thermal energy storage part; the carbon capture system is suitable for a capture system employing a chemical absorption method.
The components are as follows:
the carbon dioxide absorbing part comprises an absorbing tower 1, a rich liquid pump 2, a lean/rich liquid heat exchanger 3 and a condenser 9;
the desorption part of the desorption tower comprises a desorption tower 4, a first gas-liquid separator 5, a reboiler 6, a first control valve 19, a second control valve 7 and a lean solution pump 8;
the solar energy interface evaporation desorption part comprises a glass cover plate 20, an absorber 21, a porous medium layer 22, a cotton core 23, a heat insulation layer 24, a gas-liquid separator II 25, a control valve III 18 and a control valve IV 26; the glass cover plate 20 adopts double-layer heat insulation treatment to realize the purpose of heat preservation; the absorber 21 is a porous material, and is made of a carbon-based material or a plasmon material; the heat insulation layer 24 is made of foamed plastic;
the molecular photo-thermal energy storage part comprises a solar energy collector 10, a first liquid storage tank 11, a fifth control valve 12, a sixth control valve 13, a catalytic reaction cavity 14, a heat exchanger 15, a working medium pump 16 and a second liquid storage tank 17; the molecular photothermal energy storage part cycle working medium adopts azobenzene, norbornadiene or ruthenium-rich fulvalene compounds.
The connection mode between the main components in each part is as follows:
in the carbon dioxide absorption part, a rich liquid outlet at the bottom of the absorption tower 1 is connected to a rich liquid inlet of a lean/rich liquid heat exchanger 3 after passing through a rich liquid pump 2, the rich liquid outlet of the lean/rich liquid heat exchanger 3 is connected with a rich liquid inlet of a heat exchanger 15, and a lean liquid inlet and a lean liquid outlet of the lean/rich liquid heat exchanger 3 are respectively connected to an outlet of a lean liquid pump 8 and an inlet of a condenser 9; the outlet of the condenser 9 is connected to the top inlet of the absorption tower 1.
In the desorption part of the desorption tower, a rich liquid inlet at the top of the desorption tower 4 is connected to a rich liquid outlet of a heat exchanger 15 through a first control valve 19, the top outlet of the desorption tower 4 is connected to a first inlet 5 of a gas-liquid separator, and a first liquid outlet 5 of the gas-liquid separator is connected to a top inlet of the desorption tower 4; the outlet and inlet at the bottom of the desorption tower 4 are respectively connected to the solution inlet and the steam outlet of the reboiler 6; and the lean solution outlet of the reboiler 6 is connected to the inlet of a lean solution pump 8 through a second control valve 7.
In the solar energy interface evaporation desorption part, the glass cover plate 20, the absorber 21, the porous medium layer 22, the cotton core 23 and the heat insulation layer 24 form an interface evaporation desorber; the absorber 21 is positioned at the uppermost layer in the interface evaporation desorber; the porous medium layer 22 is positioned below the absorber 21; the heat insulation layer 24 is positioned between the porous medium layer 22 and the solution water surface, a solution transportation channel is arranged in the heat insulation layer to connect the solution and the porous medium layer 22, and a cotton core 23 is inserted in the channel to transport the solution; the inlet and outlet of the bottom of the interface evaporation desorber are respectively connected to the rich liquid outlet of the heat exchanger 15 and the inlet of the lean liquid pump 8 through a third control valve 18 and a fourth control valve 26; the top outlet of the interfacial evaporation desorber is connected with the inlet of a second gas-liquid separator 25, and the liquid outlet of the second gas-liquid separator 25 is connected to the inlet of a lean liquid pump 8 through a fourth control valve 26.
In the molecular photo-thermal energy storage part, the outlet of the solar collector 10 is connected to the inlet of the first liquid storage tank 11; the upper outlet and the lower outlet of the first liquid storage tank 11 are respectively connected to the inlet of the catalytic reaction cavity 14 through a control valve five 12 and a control valve six 13; the outlet of the catalytic reaction cavity 14, the working medium inlet and outlet of the heat exchanger 15, the working medium pump 16, the inlet and outlet of the liquid storage tank II 17 and the inlet of the solar collector 10 are sequentially connected.
The solar energy interface evaporation direct desorption type carbon capture system has the following operation flow:
the gas to be separated enters the absorption tower 1 from the bottom, and the absorbent sprayed from the top is fully contacted with the gas to absorb CO therein 2 Forming a rich solution; the rich liquid is pumped into the lean/rich liquid heat exchanger 3 and the heat exchanger 15 in turn by the rich liquid pump 2 to exchange heat, and enters the desorption tower 4 or the interfacial evaporation desorber after heat exchange, thereby completing CO 2 And (3) an absorption process.
The rich liquid after heat exchange enters a desorption tower 4 from the top and is fully contacted with steam from a reboiler 6 from bottom to top, and CO 2 The separated CO enters the gas-liquid separator 5 from the top to be separated 2 The outflow is collected, and the separated liquid returns to the desorption tower 4; the rich liquid is desorbed to form a lean liquid, and the lean liquid flows out from the reboiler 6 and is pumped into the lean/rich liquid heat exchanger 3 by the lean liquid pump 8 to complete the desorption process of the desorption tower.
Sunlight irradiates the absorber 21 after passing through the glass cover plate 20, and the absorber 21 heats up; the rich liquid entering the interfacial evaporation desorber is transported to the surface of the absorber 21 by capillary action of the porous medium layer 22 and the cotton core 23, and the liquid adhering surface forms a liquid film due to the porosity of the absorber, so as to evaporate rapidly and simultaneously desorb CO 2 The method comprises the steps of carrying out a first treatment on the surface of the The boil-off gas (containing CO 2 ) CO is separated out by a second gas-liquid separator 25 2 The separated liquid is converged into lean liquid flowing out of the interface evaporation desorber, and is pumped into the lean/rich liquid heat exchanger 3 through the lean liquid pump 8, so that the solar energy interface evaporation desorption process is completed.
The solar energy is irradiated into the solar collector 10, and the internal working medium absorbs photons and then undergoes photoisomerization reaction to form photoisomers; the working medium rich in the photoisomer flows into the first liquid storage tank 11; after the first liquid storage tank 11 is fully loaded, working medium enters the catalytic reaction cavity 14 from the upper or lower outlet through the control valve five 12 and the control valve six 13, and the optical isomer is catalyzed to release energy and raise the temperature; the catalyzed working medium enters a heat exchanger 15 to heat the rich liquid from the lean/rich liquid heat exchanger 3, is pumped into a second liquid storage tank 17 by a working medium pump 16, and finally returns to the solar collector 10 to complete the molecular photo-thermal energy storage cycle.
According to meteorological conditions, day and night conditions and the like, the invention has four working modes, namely the following working modes:
mode one: when sunlight is sufficient in daytime, the first control valve 19 and the second control valve 7 are closed, the third control valve 18 and the fourth control valve 26 are opened, the desorption part of the desorption tower stops working, the evaporation and desorption part of the solar interface works normally, and the energy source in the desorption process is solar energy; and a fifth control valve 12 is opened, a sixth control valve 13 is closed, the solar collector 10 works normally, the first liquid storage tank 11 stores the optical isomer working medium, and the whole molecular photo-thermal energy storage part is heated normally in an auxiliary mode.
Mode two: when sunlight is insufficient in daytime, the first control valve 19 and the second control valve 7 are opened, the third control valve 18 and the fourth control valve 26 are opened, the desorption part of the desorption tower and the evaporation desorption part of the solar interface work normally, and the energy sources in the desorption process are solar energy and reboiler energy consumption; and a control valve five 12 and a control valve six 13 are opened, the solar collector 10 works normally, the first liquid storage tank 11 provides the stored photoisomer working medium, and the whole molecular photothermal energy storage part is heated normally in an auxiliary mode.
Mode three: when the energy storage is sufficient at night, the first control valve 19 and the second control valve 7 are opened, the third control valve 18 and the fourth control valve 26 are closed, the desorption part of the desorption tower normally works, the solar energy interface evaporation desorption part stops working, and the energy source in the desorption process is reboiler energy consumption; and closing the control valve five 12, opening the control valve six 13, stopping the solar collector 10, providing the stored photoisomer working medium by the first liquid storage tank 11, normally assisting in heating the whole molecular photothermal energy storage part, and storing the reacted working medium in the second liquid storage tank 17.
Mode four: when the energy storage is insufficient at night, the first control valve 19 and the second control valve 7 are opened, the third control valve 18 and the fourth control valve 26 are closed, the desorption part of the desorption tower normally works, the solar energy interface evaporation desorption part stops working, and the energy source in the desorption process is reboiler energy consumption; and closing the control valve five 12 and the control valve six 13, stopping the operation of the whole molecular photo-thermal energy storage part, and maintaining the temperature required by desorption by a reboiler.
In summary, the direct desorption type carbon capture system for solar interface evaporation and the control method thereof realize CO by utilizing the solar interface evaporation device 2 The desorption process of the (2) partially replaces the desorption work of the traditional desorption tower-reboiler, utilizes solar energy as absorbent renewable energy sources, and reduces the energy consumption of the reboiler; the added molecular photo-thermal energy storage part in the system can assist in heating the absorbent, maintain the temperature required by desorption and solve the instability of solar energy. The invention promotes the utilization of solar energy and the development of negative emission technology in China.
Although the invention has been described above with reference to the accompanying drawings, the invention is not limited to the above-described embodiments, which are merely illustrative and not restrictive, and many modifications may be made by those of ordinary skill in the art without departing from the spirit of the invention, which fall within the protection of the invention.
Claims (5)
1. A direct desorption type carbon capture system by solar energy interface evaporation comprises a carbon dioxide absorption part, a desorption tower desorption part, a solar energy interface evaporation desorption part and a molecular photo-thermal energy storage part; the method is characterized in that a carbon trapping system adopting a chemical absorption method uses solar energy as an absorbent renewable energy source, and a molecular photo-thermal energy storage part assists in heating the absorbent;
the carbon dioxide absorption part comprises an absorption tower (1), a rich liquid pump (2), a lean/rich liquid heat exchanger (3) and a condenser (9); the rich liquid outlet at the bottom of the absorption tower (1) is connected to the rich liquid inlet of the lean/rich liquid heat exchanger (3) after passing through the rich liquid pump (2), the rich liquid outlet of the lean/rich liquid heat exchanger (3) is connected with a heat exchanger (15), and the lean liquid inlet and the lean liquid outlet of the lean/rich liquid heat exchanger (3) are respectively connected to the outlet of the lean liquid pump (8) and the solution inlet of the condenser (9); the outlet of the condenser (9) is connected to the top inlet of the absorption tower (1);
the desorption part of the desorption tower comprises a desorption tower (4), a first gas-liquid separator (5), a reboiler (6), a first control valve (19), a second control valve (7) and a lean solution pump (8); the top rich liquid inlet of the desorption tower (4) is connected to the rich liquid outlet of the heat exchanger (15) through the first control valve (19), the top outlet of the desorption tower (4) is connected to the inlet of the first gas-liquid separator (5), and the liquid outlet of the first gas-liquid separator (5) is connected to the top inlet of the desorption tower (4); the outlet and inlet at the bottom of the desorption tower (4) are respectively connected to the solution inlet and the steam outlet of the reboiler (6); the lean solution outlet of the reboiler (6) is connected to the inlet of the lean solution pump (8) through the second control valve (7);
the solar energy interface evaporation desorption part comprises a glass cover plate (20), an absorber (21), a porous medium layer (22), a cotton core (23), a heat insulation layer (24), a second gas-liquid separator (25), a third control valve (18) and a fourth control valve (26); the glass cover plate (20), the absorber (21), the porous medium layer (22), the cotton core (23) and the heat insulation layer (24) form an interface evaporation desorber; the glass cover plate (20) adopts double-layer heat insulation treatment; the absorber (21) is positioned at the uppermost layer in the interface evaporation desorber; the porous medium layer (22) is positioned below the absorber (21); the heat insulation layer (24) is positioned between the porous medium layer (22) and the solution water surface, a solution transportation channel is arranged in the heat insulation layer and is connected with the solution and the porous medium layer (22), and a cotton core (23) is inserted in the channel; the solution inlet and outlet at the bottom of the interfacial evaporation desorber are respectively connected to the solution outlet of the heat exchanger (15) and the inlet of the lean solution pump (8) through the third control valve (18) and the fourth control valve (26); the top outlet of the interface evaporation desorber is connected with the inlet of a second gas-liquid separator (25), and the liquid outlet of the second gas-liquid separator (25) is connected to the inlet of the lean liquid pump (8) through a fourth control valve (26);
the molecular photo-thermal energy storage part comprises a solar energy collector (10), a first liquid storage tank (11), a fifth control valve (12), a sixth control valve (13), a catalytic reaction cavity (14), a heat exchanger (15), a working medium pump (16) and a second liquid storage tank (17); the outlet of the solar collector (10) is connected to the inlet of the first liquid storage tank (11); the upper outlet and the lower outlet of the first liquid storage tank (11) are respectively connected to the inlet of the catalytic reaction cavity (14) through the fifth control valve (12) and the sixth control valve (13); the outlet of the catalytic reaction cavity (14), the working medium inlet and outlet of the heat exchanger (15), the inlet and outlet of the working medium pump (16), the inlet and outlet of the liquid storage tank II (17) and the inlet of the solar collector (10) are sequentially connected;
the gas to be separated enters the absorption tower (1) from the bottom, the absorbent absorbs carbon dioxide in the gas to form rich liquid, the rich liquid is pumped into the lean/rich liquid heat exchanger (3) and the heat exchanger (15) in sequence by the rich liquid pump (2) to exchange heat, and the rich liquid enters the desorption tower (4) and/or the interfacial evaporation desorber after heat exchange;
the rich liquid entering the interface evaporation desorber is conveyed to the surface of the absorber (21) by the cotton core (23) and the porous medium layer (22) to be evaporated, and carbon dioxide is desorbed at the same time; the carbon dioxide-containing gas flowing out of the interfacial evaporation desorber enters the gas-liquid separator II (25), the separated liquid is converged into lean liquid flowing out of the bottom of the desorber, the lean liquid is pumped into the lean/rich liquid heat exchanger (3) by the lean liquid pump (8), and finally enters the absorption tower (1) after passing through the condenser (9) to complete circulation;
in the molecular photo-thermal energy storage part, working medium reacts after photon absorption in the solar collector (10), the working medium rich in reactant flows into the catalytic reaction cavity (14) after filling the first liquid storage tank (11), and the reactant in the working medium is catalyzed by the catalytic reaction cavity (14) to release energy and heat; after higher-temperature working medium flows into the heat exchanger (15) to heat rich liquid from the lean/rich liquid heat exchanger (3), the working medium is pumped into the second liquid storage tank (17) by the working medium pump (16), and finally returns to the solar collector (10) to complete circulation; the absorber (21) is a porous material.
2. A solar interface evaporation direct desorption type carbon capture system according to claim 1, wherein the absorber (21) is a carbon-based material or a plasmon material.
3. A solar interface evaporation direct desorption type carbon capture system as claimed in claim 1, wherein said thermal insulation layer (24) is made of foam plastic.
4. The direct desorption type carbon capture system for solar energy interface evaporation according to claim 1, wherein the circulating working medium of the molecular photo-thermal energy storage part adopts azobenzene, norbornadiene or ruthenium-rich fulvalene compounds.
5. A control method of a solar energy interface evaporation direct desorption type carbon capturing system according to any one of claims 1 to 4, comprising four operation modes:
mode one: when sunlight is sufficient in daytime, the first control valve (19) and the second control valve (7) are closed, the third control valve (18) and the fourth control valve (26) are opened, the desorption part of the desorption tower stops working, the evaporation and desorption part of the solar interface works normally, and the energy source in the desorption process is solar energy; opening a control valve five (12), closing a control valve six (13), and normally operating the solar collector (10), wherein the first liquid storage tank (11) stores the photoisomer working medium, and the whole molecular photothermal energy storage part is normally heated in an auxiliary mode;
mode two: when sunlight is insufficient in daytime, the first control valve (19) and the second control valve (7) are opened, the third control valve (18) and the fourth control valve (26) are opened, the desorption part of the desorption tower and the evaporation desorption part of the solar interface work normally, and the energy sources in the desorption process are solar energy and reboiler energy consumption; opening a control valve five (12) and a control valve six (13), enabling the solar collector (10) to work normally, and enabling the first liquid storage tank (11) to provide stored photoisomer working medium, so that the whole molecular photothermal energy storage part can be heated normally in an auxiliary mode;
mode three: when the energy storage is sufficient at night, a first control valve (19) and a second control valve (7) are opened, a third control valve (18) and a fourth control valve (26) are closed, the desorption part of the desorption tower works normally, the solar energy interface evaporation desorption part stops working, and the energy source in the desorption process is reboiler energy consumption; closing a control valve five (12), opening a control valve six (13), stopping the solar collector (10), providing the stored photoisomerization working medium by a liquid storage tank one (11), normally assisting in heating the whole molecular photothermal energy storage part, and storing the reacted working medium in a liquid storage tank two (17);
mode four: when the energy storage is insufficient at night, a first control valve (19) and a second control valve (7) are opened, a third control valve (18) and a fourth control valve (26) are closed, the desorption part of the desorption tower works normally, the evaporation and desorption part of the solar interface stops working, and the energy source in the desorption process is reboiler energy consumption; and closing a control valve five (12) and a control valve six (13), stopping the operation of the whole molecular photo-thermal energy storage part, and maintaining the temperature required by desorption by a reboiler.
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201828081U (en) * | 2010-09-13 | 2011-05-11 | 海宁伊满阁太阳能科技有限公司 | Glass shell absorption and adsorption type refrigerating system |
| CN202052455U (en) * | 2011-04-26 | 2011-11-30 | 华北电力大学 | Solar auxiliary extraction flue gas decarburization and refrigeration combination system with liquid absorbent |
| CN103752142A (en) * | 2014-01-26 | 2014-04-30 | 天津大学 | Solar aided carbon dioxide trapping integrated system |
| CN104174273A (en) * | 2014-08-12 | 2014-12-03 | 天津大学 | Direct solar driven carbon dioxide flash evaporation and desorption integrated system and method |
| CN105251316A (en) * | 2015-10-26 | 2016-01-20 | 天津大学 | Independent solar direct thermal-driven system capable of removing CO2 by means of mixed working media |
| CN106345222A (en) * | 2016-09-29 | 2017-01-25 | 天津大学 | Solar thermal assisted temperature swing adsorption carbon trapping system |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9919259B2 (en) * | 2010-07-09 | 2018-03-20 | Carbon Capture Scientific, Llc | Gas pressurized separation column and process to generate a high pressure product gas |
-
2019
- 2019-04-12 CN CN201910295506.2A patent/CN109954382B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201828081U (en) * | 2010-09-13 | 2011-05-11 | 海宁伊满阁太阳能科技有限公司 | Glass shell absorption and adsorption type refrigerating system |
| CN202052455U (en) * | 2011-04-26 | 2011-11-30 | 华北电力大学 | Solar auxiliary extraction flue gas decarburization and refrigeration combination system with liquid absorbent |
| CN103752142A (en) * | 2014-01-26 | 2014-04-30 | 天津大学 | Solar aided carbon dioxide trapping integrated system |
| CN104174273A (en) * | 2014-08-12 | 2014-12-03 | 天津大学 | Direct solar driven carbon dioxide flash evaporation and desorption integrated system and method |
| CN105251316A (en) * | 2015-10-26 | 2016-01-20 | 天津大学 | Independent solar direct thermal-driven system capable of removing CO2 by means of mixed working media |
| CN106345222A (en) * | 2016-09-29 | 2017-01-25 | 天津大学 | Solar thermal assisted temperature swing adsorption carbon trapping system |
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