Device and method for carbon dioxide conversion

Abstract

The application discloses a device and method for converting carbon dioxide into carbon powder, which comprises a CO2 flue gas source, a flow controller, an electric heating furnace, a fluidized bed reactor, a feeding funnel, a pressure reducing valve, a CO2 analyzer, a material collecting tank and an N2 gas tank; the fluidized bed reactor is vertically placed in the electric heating furnace, and the fluidized bed reactor is provided with a liquid alloy; the fluidized bed reactor is connected with the feeding funnel and the CO2 analyzer through a pipeline at the top; the fluidized bed reactor is provided with a wind distribution plate and a conical air distribution funnel at the bottom, and is connected with the material collecting tank, the CO2 flue gas source and the N2 gas tank through a pipeline. The conversion method is that the CO2 flue gas is introduced into the liquid alloy in the fluidized bed reactor, and heated and pressurized, so that carbon powder and metal oxide are generated under the catalysis of the liquid alloy; the conversion method has the advantages of fast reaction rate, short time, high reaction efficiency, large carbon powder generation amount, simple device and suitability for industrialization of carbon dioxide into carbon powder.

Description

Technical Field

[0001] This invention relates to an apparatus and method for converting carbon dioxide into carbon powder, belonging to the field of carbon dioxide utilization technology. Background Technology

[0002] CO2 capture, utilization, and storage (CCUS) technology is currently a major technological means to mitigate climate change, significantly reduce CO2 emissions, and promote sustainable development. It is a highly promising and effective greenhouse gas solution for the coming decades. Converting captured CO2 into high-value-added chemicals and fuels, thereby realizing the resource utilization of CO2, is an important carbon reduction technology that is of great significance for alleviating the energy crisis and achieving carbon neutrality.

[0003] Due to its high thermal stability, CO2 requires extremely high temperatures for dissociation. Current CO2 utilization primarily focuses on absorption from alkanolamine solutions and catalytic reforming of CO2 to methanol. The main drawback of these processes is their long process flow and high energy consumption, from the CO2 treatment source to the final product output. Taking alkanolamine solution absorption as an example, it requires complex absorption and regeneration processes, and the utilization of the captured CO2 remains a significant challenge. Therefore, this invention proposes a method for directly catalytically converting CO2 into carbon powder. Summary of the Invention

[0004] In order to overcome the problems existing in the prior art, the purpose of this invention is to provide an apparatus and method for converting carbon dioxide into toner, which can not only reduce the number of CO2 processing steps, but also directly convert CO2 into high-value-added toner, thus helping to achieve the "dual carbon" goal.

[0005] To achieve the above objectives, the technical solution adopted by the present invention is as follows:

[0006] A device for converting carbon dioxide into carbon powder includes an electric heating furnace 5, a fluidized bed reactor 8 placed vertically inside the electric heating furnace 5, and a liquid alloy 20 contained in the closed fluidized bed reactor 8. A stop valve 11 controls the addition of liquid alloy 20 to the fluidized bed reactor 8 via a feeding funnel 12. Below the fluidized bed reactor 8 are an air distribution plate 16 and a conical air distribution hopper 17, connected to a material collection tank 18 and an N2 gas tank 19 via conduits, using N2 pressurization to isolate air. The conical air distribution hopper 17 is covered with small holes and connected to a CO2 flue gas source 1 via an air inlet pipe 3, which is equipped with a valve 2 and a flow controller 4. A pressure gauge 9 and an intelligent temperature control sensor 10 are connected to the side wall of the fluidized bed reactor 8 via wires. One end of an exhaust pipe 13 extends above the liquid alloy inside the fluidized bed reactor 8, and the other end is connected to a CO2 analyzer 15. The reactants CO2 and the liquid alloy are suspended and flow inside the fluidized bed reactor 8, undergoing thorough mixing and reaction.

[0007] A refractory layer 21 is provided between the outer wall of the fluidized bed reactor 8 and the inner wall of the electric heating furnace 5. The refractory layer 21 can be made of phosphate refractory, silicon carbide refractory, corundum refractory or silicon nitride combined with silicon carbide products, etc.

[0008] The liquid alloy 20 is made of gallium, gallium-indium alloy, gallium-tin alloy, or gallium-indium-tin alloy.

[0009] The electric heating furnace 5 is equipped with sealing covers 6 and sealing buckles 7 at both ends for sealing the fluidized bed reactor 8.

[0010] The fluidized bed reactor 8 and the sealing cover 6 are both made of stainless steel and are fixed with sealing clips.

[0011] The air distribution plate 16 is circular in shape with a hole in the middle for connection to the conduit; multiple small holes of the same size and evenly distributed are opened around the middle hole of the air distribution plate 16.

[0012] The conical air distribution hopper 17 has 10-20 rows of openings on its side wall; each row has 8-20 openings; and the diameter of each opening is 0.5-1.0 cm.

[0013] The operating method of the carbon dioxide to carbon powder conversion device includes introducing CO2 flue gas into a liquid alloy, and reacting it with heating and pressurization to generate carbon powder and metal oxides. The method is characterized in that: the liquid alloy 20 is introduced into a fluidized bed reactor 8 through a feeding funnel 12, and the addition amount is controlled by a shut-off valve 11; CO2 flue gas from the CO2 flue gas source 1 enters through small holes on a conical gas distribution hopper 17, passes through a gas distribution plate 16, and then enters the fluidized bed reactor 8 to react with the liquid alloy 20, with the CO2 flue gas addition amount controlled by a valve 2 and a flow controller 4; N2 is blown into the fluidized bed reactor 8 from the N2 gas tank 19 through a conduit. The liquid alloy is suspended in the fluidized bed reactor 8, and the reaction is isolated from air. During the reaction, the liquid alloy is heated by an electric heater 5 and pressurized by an N2 gas tank 19. The pressure and temperature are controlled according to the reaction requirements by a pressure gauge 9 and an intelligent temperature control sensor 10. The CO2 gas and liquid alloy in the fluidized bed reactor 8 react under constant temperature and pressure. After the reaction, the remaining CO2 gas flows through an exhaust pipe 13 and a CO2 analyzer 15 to measure the CO2 concentration at the outlet. The products after the reaction are carbon powder and metal oxides. The products after the reaction are collected in a material collection tank 18 for subsequent product separation and characterization analysis.

[0014] The pressure applied is 1-10 MPa, and the heating temperature is 200-400℃.

[0015] The reaction time is 2-4 hours under constant temperature and pressure.

[0016] Compared with existing technologies, this invention has the following advantages and outstanding technical effects: ① This invention uses a fluidized bed reactor as the reactor, which has a large internal capacity, allows for the continuous addition of reactants, and the reactants are suspended and flow inside the fluidized bed reactor, enabling CO2 and liquid alloy to fully mix and react, thus promoting the generation of carbon powder; ② This invention uses N2 pressurization to isolate the air during the reaction, which accelerates the reaction rate, shortens the reaction time, promotes the generation of carbon powder, and increases the amount of carbon powder generated; ③ This invention uses an electric heating furnace to heat the fluidized bed reactor. The electric heating furnace is small in size, flexible in installation, and has high thermal efficiency. When used in conjunction with an intelligent temperature control sensor installed on the side wall of the fluidized bed reactor, it can accurately control the temperature of the reactor. Attached Figure Description

[0017] Figure 1 This is a schematic diagram of the structure of the device of the present invention.

[0018] Figure 2 This is a top view of the air distribution panel.

[0019] Figure 3 This is a schematic diagram of a cone-shaped air distribution hopper structure.

[0020] In the diagram: 1—CO2 flue gas source; 2—valve; 3—inlet pipe; 4—flow controller; 5—electric heating furnace; 6—sealing cover; 7—sealing buckle; 8—fluidized bed reactor; 9—pressure gauge; 10—intelligent temperature control sensor; 11—stop valve; 12—feeding funnel; 13—exhaust pipe; 14—pressure reducing valve; 15—CO2 analyzer; 16—air distribution plate; 17—conical air distribution hopper; 18—material collection tank; 19—N2 gas tank; 20—liquid alloy; 21—refractory layer. Detailed Implementation

[0021] To enable a better understanding of the present invention, the invention will now be described in further detail with reference to the accompanying drawings.

[0022] like Figure 1As shown, this invention discloses a device for converting carbon dioxide into carbon powder. The device mainly includes a CO2 flue gas source 1, a flow controller 4, an electric heating furnace 5, a fluidized bed reactor 8, a feeding funnel 12, a pressure reducing valve 14, a CO2 analyzer 15, a material collection tank 18, and an N2 gas tank 19. The CO2 flue gas source 1, flow controller 4, feeding funnel 12, pressure reducing valve 14, CO2 analyzer 15, material collection tank 18, and N2 gas tank 19 are respectively connected to the fluidized bed reactor via an inlet pipe 3, an outlet pipe 13, and a conduit. The fluidized bed reactor 8 has a sealing cover 6 and a sealing buckle 7 at both ends of the electric heating furnace 5. The sealing cover at the upper end of the electric heating furnace 5 has two holes, which are respectively connected to the feeding funnel 12 and the CO2 analyzer 15 through conduits. The lower end of the electric heating furnace 5 has one hole, and the lower end of the fluidized bed reactor 8 is fixed to the hole wall. The fluidized bed reactor 8 is placed vertically inside the electric heating furnace 5. There is a refractory layer 21 between the outer wall of the fluidized bed reactor 8 and the inner wall of the electric heating furnace 5. The fluidized bed reactor 8 is filled with liquid alloy 20.

[0023] The fluidized bed reactor 8 is equipped with a pressure gauge 9 and an intelligent temperature control sensor 10 on its side wall, which are connected by wires. The fluidized bed reactor 8 is equipped with an air distribution plate 16 and a conical air distribution hopper 17 at the bottom, which are connected to the material collection tank 18 and the N2 gas tank 19 through a conduit. The conical air distribution hopper 17 is covered with small holes and is connected to the CO2 flue gas source 1 through the air inlet pipe 3.

[0024] The liquid alloy enters the fluidized bed reactor 8 through the feeding funnel 12; the outer wall of the conical gas distribution hopper 17 is covered with an annular rubber tube, and CO2 enters the separation gas chamber through the small hole on the outside of the conical gas distribution hopper 17, and then enters the fluidized bed reactor 8 through the hole on the air distribution plate 16.

[0025] Figure 2 This is a top view of the air distribution plate 16. The air distribution plate 16 is circular in shape with a hole in the middle for connection to the conduit; eight small holes of the same size are evenly distributed around the middle hole of the air distribution plate 16.

[0026] Figure 3 This is a schematic diagram of the conical air distribution hopper 17. The number of rows of openings on the side wall of the conical air distribution hopper 17 is 10-20; the number of openings in each row is 8-20; and the diameter of the openings is 0.5-1.0 cm.

[0027] The specific implementation steps of the working method of the device of the present invention are as follows:

[0028] 1. A certain amount of liquid alloy is added into the fluidized bed reactor 8 through the feeding funnel 12;

[0029] 2. Open the N2 valve to allow N2 in N2 tank 19 to enter the fluidized bed reactor 8 through the conduit at a certain flow rate (greater than the critical fluidization velocity), so that the liquid alloy 20 in the fluidized bed reactor 8 is suspended and flows; according to the pressure gauge 9 on the side wall of the fluidized bed reactor 8, control the pressure in the reactor between 1-10 MPa.

[0030] 3. Turn on the electric heater 5 to raise the temperature inside the fluidized bed reactor 8, and control the temperature between 200-400℃;

[0031] 4. The CO2 flue gas from CO2 flue gas source 1 is introduced into the liquid alloy 20 in the fluidized bed reactor 8 at a certain flow rate;

[0032] 5. React CO2 gas and liquid alloy in fluidized bed reactor 8 under constant temperature and pressure for 2-4 hours to obtain carbon powder and metal oxides;

[0033] 6. After the reaction is completed, the remaining CO2 gas flows through the exhaust pipe 13 and passes through the CO2 analyzer 15 to measure the CO2 concentration at the outlet; the reaction products are passed through the bottom conduit of the fluidized bed reactor 8 into the material collection tank 18 for subsequent product separation and characterization analysis.

Claims

1. A device for converting carbon dioxide into toner, characterized in that: The device includes an electric heating furnace (5), a fluidized bed reactor (8) placed vertically inside the electric heating furnace (5), a closed fluidized bed reactor (8) containing liquid alloy (20), and a feed funnel (12) controlling the addition of liquid alloy (20) to the fluidized bed reactor (8) through a shut-off valve (11); the fluidized bed reactor (8) is provided with an air distribution plate (16) and a conical air distribution hopper (17) below it, which are connected to a material collection tank (18) and an N2 gas tank (19) through conduits, and are isolated from air by N2 pressurization; the conical air distribution hopper (17) is also provided with an air distribution plate (16) below it. The gas distribution hopper (17) is covered with small holes and is connected to the CO2 flue gas source (1) through the air inlet pipe (3). The air inlet pipe (3) is equipped with a valve (2) and a flow controller (4). The side wall of the fluidized bed reactor (8) is connected to a pressure gauge (9) and an intelligent temperature control sensor (10) through wires. One end of the exhaust pipe (13) is connected to the liquid alloy inside the fluidized bed reactor (8), and the other end is connected to a CO2 analyzer (15). The reactants CO2 and liquid alloy are suspended and flow inside the fluidized bed reactor (8) and fully mixed and reacted. A refractory layer (21) is provided between the outer wall of the fluidized bed reactor (8) and the inner wall of the electric heating furnace (5). The electric heating furnace (5) is equipped with sealing caps (6) and sealing buckles (7) at both the top and bottom ends for sealing the fluidized bed reactor (8). The air distribution plate (16) is circular in shape with a hole in the middle, which is connected to the conduit; multiple small holes of the same size and evenly distributed are opened around the middle hole of the air distribution plate (16); The conical air distribution hopper (17) has 10-20 rows of openings on its side wall; each row has 8-20 openings; and the diameter of the openings is 0.5-1.0 cm.

2. The apparatus for converting carbon dioxide to toner according to claim 1, characterized in that: The liquid alloy (20) is made of gallium, gallium-indium alloy, gallium-tin alloy or gallium-indium-tin alloy.

3. The apparatus for converting carbon dioxide to toner according to claim 1, characterized in that: The fluidized bed reactor (8) and the sealing cover (6) are both made of stainless steel and are fixed with sealing buckles.

4. The operating method of the carbon dioxide to carbon powder apparatus according to any one of claims 1 to 3, characterized in that: The method involves introducing CO2 flue gas into a liquid alloy, heating and pressurizing it to react and generate carbon powder and metal oxides. The liquid alloy (20) is introduced into a fluidized bed reactor (8) through a feeding funnel (12), with the amount added controlled by a shut-off valve (11). CO2 flue gas from the CO2 flue gas source (1) enters through small holes in a conical gas distribution hopper (17), passes through a distribution plate (16), and then enters the fluidized bed reactor (8) to react with the liquid alloy (20). The amount of CO2 flue gas added is controlled by a valve (2) and a flow controller (4). N2 is blown in from an N2 gas tank (19) through a conduit from the lower end of the fluidized bed reactor (8), causing the liquid alloy to react with the liquid alloy. The reaction is suspended in the fluidized bed reactor (8) and the reaction is isolated from air. During the reaction, the reaction is heated by an electric heating furnace (5) and N2 is introduced into the N2 gas tank (19) for pressurization. The pressure and temperature are measured by the pressure gauge (9) and the intelligent temperature control sensor (10) according to the reaction pressure and heating control. The CO2 gas and liquid alloy in the fluidized bed reactor (8) react under constant temperature and pressure. After the reaction, the remaining CO2 gas flows through the exhaust pipe (13) and passes through the CO2 analyzer (15) to measure the CO2 concentration at the outlet. The products after the reaction are carbon powder and metal oxide. The products after the reaction are collected in the material collection tank (18) for subsequent product separation and characterization analysis.

5. The working method according to claim 4, characterized in that: The pressure applied is 1-10 MPa, and the heating temperature is 200-400℃.

6. The working method according to claim 4, characterized in that: The reaction time is 2-4 hours under constant temperature and pressure.

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