Air reactor and chemical looping combustion equipment

Abstract

The invention discloses an air reactor and chemical looping combustion equipment. The air reactor can comprise a first tank body, a reaction space can be defined by the first tank body, and the bottom of the first tank body is provided with a fluidization air inlet used for introducing fluidization air flow. The reaction space comprises a mixing area, a separation area and a heat exchange area which are sequentially arranged from bottom to top in the vertical direction. The mixing zone is configured to provide a space in which the oxygen carrier and the heat carrier are mixed. And the first tank body is provided with a filtering structure in the separation area, and the filtering structure is arranged to filter the heat carrier moving from the separation area to the heat exchange area. The first tank body is provided with a heat exchange structure in the heat exchange area, and the heat exchange structure is arranged to extract heat of the heat carrier. The invention relates to a chemical looping combustion technology, and provides an air reactor and chemical looping combustion equipment, which can effectively separate a heat carrier from an oxygen carrier, effectively extract heat and meet the requirement of the heat carrier as a heat transfer medium.

Description

Technical Field

[0001] This article relates to chemical looping combustion technology, and more particularly to an air reactor and chemical looping combustion equipment. Background Technology

[0002] Chemical looping combustion is a flameless combustion technology and a promising carbon capture technology for addressing climate change and reducing greenhouse gas emissions. Chemical looping combustion technology offers advantages such as low energy consumption, low cost, and high efficiency.

[0003] Chemical looping combustion technology utilizes a solid oxygen carrier (such as a metal oxide) as an oxygen "transporter," breaking down the traditional "one-step" combustion process into a "two-step" reaction. Currently, most chemical looping combustion equipment uses a serial fluidized bed reactor, which consists of a relatively independent air reactor and a fuel reactor. In the air reactor, the oxygen carrier is oxidized by air, releasing heat to produce an oxidized oxygen carrier carrying lattice oxygen and releasing heat. In the fuel reactor, the oxidized oxygen carrier, carrying lattice oxygen, reacts with carbon monoxide, hydrogen, methane, etc., generated from the gasification of fossil fuels such as coal or biomass, releasing lattice oxygen and producing high-concentration carbon dioxide and syngas flue gas without nitrogen, facilitating carbon capture. Currently, the air reactor only contains the oxygen carrier, making it difficult to extract the heat released by the oxygen carrier within the air reactor, and the oxidation process within the air reactor also leads to poor heat recovery. Summary of the Invention

[0004] This application provides an air reactor for chemical looping combustion, including a first tank that encloses a reaction space, and a fluidizing inlet at the bottom of the first tank for introducing a fluidizing gas stream. The reaction space includes a mixing zone, a separation zone, and a heat exchange zone arranged sequentially from bottom to top in the vertical direction; The mixing zone is configured to provide a space for mixing oxygen carrier and heat carrier; The first tank is provided with a filter structure in the separation zone, and the filter structure is configured to filter the heat carrier moving from the separation zone to the heat exchange zone; The first tank is provided with a heat exchange structure in the heat exchange zone, and the heat exchange structure is configured to extract heat from the heat carrier.

[0005] In some exemplary embodiments, a first return feeder is also included, which is connected to the first tank and is configured to transport the heat carrier in the heat exchange zone to the mixing zone.

[0006] In some exemplary embodiments, the first tank is provided with a heat carrier inlet for inputting the heat carrier and a heat carrier outlet for outputting the heat carrier, the heat carrier inlet being provided in the mixing zone and the heat carrier outlet being provided in the heat exchange zone; The first return feeder includes a first separator and a first return body connected to each other; The input end of the first separator is connected to the outlet of the heat carrier, and the first separator is configured to transport the heat carrier in the heat exchange zone to the first return material body. The output end of the first return material body is connected to the inlet of the heat carrier, and the first return material body is configured to transport the heat carrier to the mixing zone.

[0007] In some exemplary embodiments, the output end of the first return material body is connected to the inlet of the heat carrier through a first conveying pipe; The first delivery pipe is equipped with a first valve, which is configured to control the flow rate of the heat carrier flowing to the mixing zone.

[0008] In some exemplary embodiments, the first return material body is provided with an openable and closable control port, the control port is provided with a filter screen, and the control port is configured to add or discharge the heat carrier.

[0009] In some exemplary embodiments, the filter structure includes a screen with a pore size larger than the particle diameter of the heat carrier and smaller than the particle diameter of the oxygen carrier, for filtering the heat carrier and blocking the oxygen carrier; Alternatively, the filter structure may include a partition with at least one through-hole.

[0010] In some exemplary embodiments, the first tank is provided with a supplementary air inlet for providing airflow to the filter structure, the supplementary air inlet being disposed corresponding to the separation zone and located on the lower side of the filter structure.

[0011] In some exemplary embodiments, multiple supplementary air inlets are provided, and the multiple supplementary air inlets are evenly arranged circumferentially around the first tank.

[0012] In some exemplary embodiments, the sidewall of the first tank includes a reaction section, a separation section, and a heat exchange section connected sequentially from bottom to top, wherein the reaction section surrounds the mixing zone, the separation section surrounds the separation zone, and the heat exchange section surrounds the heat exchange zone; The inner wall of the reaction section is covered with a first refractory layer, the material of which includes high-density refractory castable. The inner wall of the separation section is covered with a first lining structure, which includes a heat insulation layer and a second fire-resistant layer stacked in the wall thickness direction of the separation section. The heat exchange structure is disposed on the inner wall of the heat exchange section, and the surface of the heat exchange structure is covered with a wear-resistant and thermally conductive coating.

[0013] In some exemplary embodiments, the first tank is provided with an oxygen carrier inlet for inputting the oxygen carrier and an oxygen carrier outlet for outputting the oxygen carrier; The oxygen carrier inlet is located on the side wall of the first tank. Both the oxygen carrier inlet and the oxygen carrier outlet are provided corresponding to the mixing zone, and the oxygen carrier inlet is located above the oxygen carrier outlet in the vertical direction.

[0014] In some exemplary embodiments, multiple oxygen carrier inlets are provided, and the multiple oxygen carrier inlets are evenly arranged around the circumference of the first tank, and the multiple oxygen carrier inlets are staggered in the vertical direction.

[0015] In some exemplary embodiments, the first tank is provided with an oxygen carrier inlet for inputting the oxygen carrier and an oxygen carrier outlet for outputting the oxygen carrier, wherein the oxygen carrier inlet is located on the bottom wall of the first tank; The oxygen carrier inlet is configured to be connected to a return device for inputting the oxygen carrier, the return device being configured to convey the oxygen carrier into the mixing zone.

[0016] This application also provides a chemical looping combustion device, including the air reactor described above.

[0017] The air reactor of this application embodiment can meet the requirement of the heat carrier as a heat transfer medium, can effectively separate the heat carrier and the oxygen carrier, and can effectively extract heat.

[0018] In the air reactor of this application embodiment, the separated heat carrier can be cooled and then flowed back into the first tank to replenish the heat carrier stock in the first tank, thus forming a recycling of the heat carrier particles.

[0019] The air reactor of this application embodiment has a supplementary air inlet. By introducing airflow through the supplementary air inlet, the flow of the heat carrier is powered, thereby meeting the flow rate requirements of the heat carrier.

[0020] Other features and advantages of this application will be set forth in the following description, and will be apparent in part from the description, or may be learned by practicing the application. Other advantages of this application can be realized and obtained by means of the embodiments described in the description and the accompanying drawings. Attached Figure Description

[0021] The accompanying drawings are used to provide an understanding of the technical solutions of this application and constitute a part of the specification. They are used together with the embodiments of this application to explain the technical solutions of this application and do not constitute a limitation on the technical solutions of this application.

[0022] Figure 1 This is a schematic diagram of the material circulation of a chemical looping combustion device according to an exemplary embodiment of the present invention; Figure 2 This is a schematic diagram of an air reactor according to an exemplary embodiment of the present invention; Figure 3 for Figure 2 A schematic diagram of the material circulation in the air reactor; Figure 4 for Figure 2 A schematic diagram of the first tank in the diagram; Figure 5 for Figure 2 Schematic diagram of the first return feeder in the middle; Figure 6 A schematic diagram of a chemical looping combustion device as an exemplary embodiment of this invention; Figure 7 This is a schematic diagram of a chemical looping combustion material recycling method according to an exemplary embodiment of the present invention; Figure 8 This is a schematic diagram of another chemical looping combustion device for this exemplary embodiment. Detailed Implementation

[0023] This application describes several embodiments, but these descriptions are exemplary and not limiting, and it will be apparent to those skilled in the art that many more embodiments and implementations are possible within the scope of the embodiments described herein. Although many possible combinations of features are shown in the drawings and discussed in the detailed description, many other combinations of the disclosed features are also possible. Unless specifically limited, any feature or element of any embodiment may be used in combination with, or may replace, any feature or element of any other embodiment.

[0024] This application includes and contemplates combinations of features and elements known to those skilled in the art. The embodiments, features, and elements disclosed in this application can also be combined with any conventional features or elements to form unique inventive solutions. Any feature or element of any embodiment can also be combined with features or elements from other inventive solutions to form another unique inventive solution. Therefore, it should be understood that any feature shown and / or discussed in this application can be implemented individually or in any suitable combination. Therefore, the embodiments are not limited except by the limitations imposed by the appended claims and their equivalents. Furthermore, various modifications and changes can be made within the scope of the appended claims.

[0025] Furthermore, in describing representative embodiments, the specification may have presented methods and / or processes as a specific sequence of steps. However, the method or process should not be limited to the specific order of steps described herein, to the extent that it does not depend on such a specific order. As will be understood by those skilled in the art, other sequences of steps are also possible. Therefore, the specific order of steps set forth in the specification should not be construed as a limitation of the claims. Moreover, the claims concerning the method and / or process should not be limited to the steps performed in the written order, and those skilled in the art will readily understand that these orders can be varied and still remain within the spirit and scope of the embodiments of this application.

[0026] Currently, oxygen carriers can undergo oxidation processes in air reactors, which are typically fluidized bed structures. The heat released by the oxygen carrier in these reactors is difficult to extract; that is, the heat in the air reactor cannot be effectively extracted. Furthermore, in high-temperature, high-velocity air reactors, simply arranging the heating surface directly results in low heat extraction efficiency due to heat exchange between the oxygen carrier and the heating surface. Moreover, large oxygen carrier particles can cause severe wear on the heating surface.

[0027] Figure 1 This is a schematic diagram of the material circulation in a chemical looping combustion device according to an exemplary embodiment of the present invention. Figure 2 This is a schematic diagram of an air reactor according to an exemplary embodiment of the present invention. Figure 3 for Figure 2 This exemplary embodiment provides an air reactor that can be applied to chemical looping combustion, such as... Figures 1 to 3As shown, the air reactor 1 may include a first tank 2, which encloses a reaction space 4. The bottom of the first tank 2 is provided with a fluidizing inlet 5 for introducing a fluidizing gas flow. The reaction space 4 includes a mixing zone A1, a separation zone A2, and a heat exchange zone A3 arranged sequentially from bottom to top in the vertical direction. The mixing zone A1 is configured to provide a space for mixing the oxygen carrier 8 and the heat carrier 9. The first tank 2 has a filter structure 6 in the separation zone A2, which is configured to filter the heat carrier 9 moving from the separation zone A2 to the heat exchange zone A3. The first tank 2 has a heat exchange structure 7 in the heat exchange zone A3, which is configured to extract heat from the heat carrier 9. The air reactor 1 of this embodiment can effectively separate the heat carrier 9 and the oxygen carrier 8, and can effectively extract heat, meeting the requirement of the heat carrier 9 as a heat transfer medium.

[0028] In some exemplary embodiments, such as Figures 1 to 3 As shown, oxygen carrier 8 can be a natural oxygen carrier, such as ilmenite, hematite, manganese ore, etc.; oxygen carrier 8 can also be an artificially prepared oxygen carrier, such as nickel-based oxygen carrier, copper-based oxygen carrier, manganese-based oxygen carrier, etc.; but it is not limited to these, oxygen carrier 8 can be other substances with oxygen-carrying capacity. Oxygen carrier 8 has two states, namely oxidized state and reduced state. Oxygen carrier 8 in the reduced state can be oxidized to form oxygen carrier 8 in the oxidized state, and oxygen carrier 8 in the oxidized state carries lattice oxygen; oxygen carrier 8 in the oxidized state can be reduced to form oxygen carrier 8 in the reduced state, releasing lattice oxygen. Oxygen carrier 8 can be particulate, and the particle diameter of oxygen carrier 8 can be 200μm to 600μm, belonging to class B or class D particles. Class B particles and class D particles can be two particle types in the Gerdat particle classification system. The particle diameter of class B particles can be 40μm to 500μm, and the particle diameter of class D particles can be greater than 600μm.

[0029] In some exemplary embodiments, such as Figures 1 to 3 As shown, the heat carrier 9 can be an inert material such as coal ash or quartz sand that hardly reacts with oxygen or the oxygen carrier. The heat carrier 9 possesses high-temperature stability and anti-sintering properties. The particle diameter of the heat carrier 9 can be smaller than that of the oxygen carrier 8, and the particle size of the heat carrier 9 can be 50 μm to 100 μm. The particles of the heat carrier 9 can belong to either type A or type B particles. Type A and type B particles can be two particle types according to the Gerdat particle classification system. The particle diameter of type A particles can be 20 μm to 100 μm, and the particle diameter of type B particles can be 40 μm to 500 μm.

[0030] In some exemplary embodiments, such as Figures 1 to 3As shown, the chemical looping combustion material recycling method can be mainly divided into two parts: one part occurs in air reactor 1, and the other part occurs in fuel reactor 10. In air reactor 1, the reduced oxygen carrier 8 can enter a fluidized state under the action of a fluidizing gas flow (i.e., fluidizing air), which can be an oxidizing gas flow. The fluidized state can refer to a special operating state in which solid particles are suspended by fluid (gas flow) and have fluid characteristics. The oxygen carrier 8 can also react with the fluidizing gas flow entering air reactor 1 to undergo an oxidation reaction and release a large amount of heat. In fuel reactor 10, the oxidized oxygen carrier 8 reacts with fuel to undergo a reduction reaction, generating carbon dioxide and water and absorbing heat. The oxygen carrier 8, as a medium for lattice oxygen transport, circulates between the two reactors, transferring oxygen from air reactor 1 to fuel reactor 10 in the form of lattice oxygen, and transferring heat from air reactor 1 to fuel reactor 10 in the form of sensible heat from oxygen carrier 8, maintaining the temperature of fuel reactor 10, thereby achieving self-heating operation of the device.

[0031] In some exemplary embodiments, such as Figures 1 to 3 As shown, the air reactor 1 also includes a first return feeder 3, which is connected to the first tank 2. The first return feeder 3 can transport the heat carrier 9 in the heat exchange zone A3 to the mixing zone A1. The first return feeder 3 returns the separated heat carrier 9 back into the first tank 2, thereby replenishing the stock of heat carrier 9 in the first tank 2 and forming a recycling of the heat carrier 9 particles.

[0032] Figure 4 for Figure 2 A schematic diagram of the first tank in the diagram. Figure 5 for Figure 2 A schematic diagram of the first return feeder in the diagram, in some exemplary embodiments, such as Figures 2 to 5 As shown, the first tank 2 can be a vertical container, and can be arranged vertically in a vertical direction, with one side being the top and the other the bottom. The top of the first tank 2 can be the upper end in the vertical direction, and the bottom of the first tank 2 can be the lower end in the vertical direction. The side walls of the first tank 2 are cylindrical, and can be the cylindrical body of a vertical container. The side walls of the first tank 2 include a reaction section 40, a separation section 41, and a heat exchange section 42 connected sequentially from bottom to top, all of which are cylindrical. The reaction section 40 can form a mixing zone A1, the separation section 41 can form a separation zone A2, and the heat exchange section 42 can form a heat exchange zone A3. The mixing zone A1, the separation zone A2, and the heat exchange zone A3 are sequentially connected. The top of the first tank 2 can be the end cap of a vertical container, the top of the first tank 2 can be the first end cap 44, the bottom of the first tank 2 can be the end cap of a vertical container, and the bottom of the first tank 2 can be the second end cap 44.

[0033] In some exemplary embodiments, such as Figures 2 to 5 As shown, the inner wall of the reaction section 40 is covered with a first refractory layer (not shown in the figure). The material of the first refractory layer (not shown in the figure) may include high-density refractory castable, and the thickness of the first refractory layer may be 100mm to 150mm. The inner wall of the reaction section 40 may be the surface of the reaction section 40 facing the space it encloses. The refractory properties of the first refractory layer can reduce the heat transfer from the mixing zone A1 to the reaction section 40 and can also improve the refractory performance of the reaction section 40. The inner wall of the separation section 41 is covered with a first lining structure (not shown in the figure). The first lining structure may be a composite structure, that is, the first lining structure may include a thermal insulation layer and a second refractory layer stacked in the wall thickness direction of the separation section 41. The wall thickness direction of the separation section 41 may be the radial direction of the circular structure enclosed by the separation section 41. The second refractory layer may be located on the side of the thermal insulation layer in the wall thickness direction of the separation section 41 closer to the separation zone A2. The insulation layer can be made of lightweight insulation material, the second refractory layer can be a refractory coating, and the thickness of the first inner lining structure is 80mm to 120mm. The insulation layer can prevent heat loss to the outside of the first tank 2, and the second refractory layer can improve the refractory performance of the separation section 41.

[0034] In some exemplary embodiments, such as Figures 2 to 5 As shown, the bottom of the first tank 2 (i.e., the second end cap 43) may be provided with multiple fluidizing inlets 5. Fluidizing inlets 5 can introduce a fluidizing gas stream, which can be an oxidizing gas; in this example, the oxidizing gas can be air. The flow velocity of the fluidizing gas stream can be from 1 m / s to 6 m / s. The fluidizing gas stream can be greater than the minimum fluidizing velocity of the heat carrier 4 and the oxygen carrier 3, and also greater than the terminal velocities of the heat carrier 4 and the oxygen carrier 3. The terminal velocity of the oxygen carrier 3 is greater than the terminal velocity of the heat carrier 4. The minimum fluidizing velocity refers to the minimum empty tower flow velocity required for the solid particle layer in the fixed bed state to begin to transform into a fluidized state. The terminal velocity can refer to the constant maximum velocity that particles can reach in the fluid under the action of gravity. Based on the different particle sizes and types of the heat carrier 4 and the oxygen carrier 3 as stated above, the terminal velocity of the heat carrier 4 is less than the terminal velocity of the oxygen carrier 3. In this example, the flow velocity of the fluidizing gas stream can be 2 m / s.

[0035] In some exemplary embodiments, such as Figures 2 to 5 As shown, the reaction section 40 is equipped with a first air distribution plate 21, which is a flat plate with multiple openings. The first air distribution plate 21 can divide the mixing zone A1 into a fluidized bed air chamber 22 and a fluidized bed furnace 23 arranged in the vertical direction. The fluidized bed air chamber 22 can be connected to the fluidized air inlet 5. The fluidized airflow can enter the fluidized bed air chamber 22 through the fluidized air inlet 5, and then be distributed by the first air distribution plate 21 to enter the fluidized bed furnace 23. The heat carrier 4 and the oxygen carrier 3 can be arranged in the fluidized bed furnace 23 and are fully mixed. They can also enter the fluidized state under the action of the airflow passing through the first air distribution plate 21.

[0036] In some exemplary embodiments, such as Figures 2 to 5 As shown, the first tank 2 is provided with an oxygen carrier inlet 14 for inputting oxygen carrier 8 and an oxygen carrier outlet 13 for outputting oxygen carrier 8. Both the oxygen carrier outlet 13 and the oxygen carrier inlet 14 are located in the reaction section 40, such that both the oxygen carrier inlet 14 and the oxygen carrier outlet 13 are connected to the fluidized bed furnace 23 of the mixing zone A1, forming a configuration where the oxygen carrier inlet 14 and the oxygen carrier outlet 13 correspond to the mixing zone A1. The oxygen carrier inlet 14 is located above the oxygen carrier outlet 13 in the vertical direction, the oxygen carrier outlet 13 is located in the middle of the reaction section 40 in the vertical direction, and the oxygen carrier inlet 14 is located at the top of the reaction section 40 in the vertical direction. In some exemplary embodiments, multiple oxygen carrier inlets 14 are provided, and these multiple oxygen carrier inlets 14 are evenly arranged around the circumference of the first tank 2, while the multiple oxygen carrier inlets 14 are staggered in the vertical direction, meaning that the height positions of the multiple oxygen carrier inlets 14 are different. Multiple oxygen carrier inlets 14 have adjustable opening degrees, and the material distribution ratio of each oxygen carrier inlet 14 can be adjusted according to the oxygen carrier reduction degree to achieve uniform distribution of oxygen carrier in the first tank 2.

[0037] In some exemplary embodiments, such as Figures 2 to 5 As shown, the first tank 2 is provided with a heat carrier inlet 15 for inputting heat carrier 9. The heat carrier inlet 15 can be located in the reaction section 40, so that the heat carrier inlet 15 is connected to the fluidized bed furnace 23 of the mixing zone A1, forming a heat carrier inlet 15 corresponding to the mixing zone A1.

[0038] In some exemplary embodiments, such as Figures 2 to 5 As shown, the filter structure 6 is disposed within the separation section 41. The filter structure 6 may include a screen, which may be a wear-resistant screen with multiple openings and a mesh-like structure. The screen material may be a wear-resistant metal material, and the surface of the screen may be coated with a wear-resistant coating. Applying a wear-resistant coating can reduce damage caused by the heat carrier 9 contacting the screen, improve the durability of the screen, and extend its service life. The pore size of the screen may be larger than the particle diameter of the heat carrier 9 and smaller than the particle diameter of the oxygen carrier 8, so that the screen can only filter through the heat carrier 9 and block the oxygen carrier 8. However, it is not limited to this. For example, the filter structure 6 may include a baffle with through holes, and the number of through holes may be one or more.

[0039] In some exemplary embodiments, such as Figures 2 to 5As shown, the separation section 41 of the first tank 2 may be provided with a supplementary air inlet 16 for providing airflow to the filter structure 6. The supplementary air inlet 16 is connected to the separation zone A2, such that the supplementary air inlet 16 is set corresponding to the separation zone A2. The supplementary air inlet 16 is located on the lower side of the filter structure 6, and the airflow (i.e., the supplementary airflow) entering the supplementary air inlet 16 may be inclined upward and flow towards the supplementary air inlet 16. The supplementary airflow can provide power for the heat carrier 9, causing it to move from the separation zone A2 to the heat exchange zone A3, and can continue to be transported from the heat exchange zone A3 to the first return feeder 3. The gas of the supplementary airflow may be air, and the gas velocity of the supplementary airflow may be greater than the gas velocity of the fluidizing airflow. In this example, the gas velocity of the supplementary airflow may be 3 m / s to 4 m / s. In some exemplary embodiments, such as Figures 2 to 5 As shown, multiple supplementary air inlets 16 can be provided, and these multiple supplementary air inlets 16 can be evenly arranged around the first tank 2 to make the airflow distribution more uniform. At the same time, the airflow velocity of each supplementary air inlet 16 can be controlled separately, that is, the airflow velocity of each supplementary air inlet 16 can be controlled individually.

[0040] In some exemplary embodiments, such as Figures 2 to 5 As shown, the heat exchange structure 7 is arranged on the inner wall of the heat exchange section 42. The heat exchange structure 7 can be a zigzag-shaped heat receiving surface. The heat exchange structure 7 can extract heat by contacting the heat carrier 9 and absorbing the ambient temperature within the heat exchange zone A3. The surface of the heat exchange structure 7 is covered with a wear-resistant and thermally conductive coating. Simultaneously, the heat exchange structure 7 can be connected to a heat storage device to store the extracted heat and use it for power generation, etc. In some exemplary embodiments, such as... Figures 2 to 5 As shown, the heat exchange section 42 is provided with a heat carrier outlet 17 for outputting the heat carrier 9. The heat carrier outlet 17 can be connected to the heat exchange zone A3, so that the heat carrier outlet 17 is set to correspond to the heat exchange zone A3.

[0041] In some exemplary embodiments, such as Figures 2 to 5 As shown, the first return feeder 3 includes a first separator 11 and a first return feed body 12 connected to each other. The first separator 11 can be a cyclone separator, with its input end being a first input port 35 and its output end being a first output port 36. The first input port 35 of the first separator 11 can be connected to the heat transfer fluid outlet 17 of the first tank 2, and the first output port 36 of the first separator 11 can be connected to the first return feed body 12. The first separator 11 may have an exhaust port 18.

[0042] In some exemplary embodiments, such as Figures 2 to 5As shown, the first material return body 12 encloses a closed space and has a second input port 37 and a second output port 38. The second input port 37 serves as the input end of the first material return body 12, and the second output port 38 serves as the output end of the first material return body 12. The closed space enclosed by the first material return body 12 can be divided into a main cavity 24 and a wind chamber 25 by a second air distribution plate 30 within it. The cavity wall of the main cavity 24 has the second input port 37 and the second output port 38. The main cavity 24 has a first partition 33, which divides the space within the main cavity 24 into a first flow channel 26 and a second flow channel 27. One end of the first flow channel 26 is connected to the second input port 37, and the other end of the first flow channel 26 is connected to one end of the second flow channel 27. The other end of the second flow channel 27 can be connected to the second output port 38. The first flow channel 26 and the second flow channel 27 formed by the first partition 33 together constitute a layered zigzag flow channel. The bottom of the first return material body 12 has an opening, namely a loosening air guide channel 31 and a fluidizing air guide channel 32, both of which are connected to the return material air chamber 25. The return material air chamber 25 has a second partition 34, which divides the return material air chamber 25 into an independent loosening air chamber 28 and a fluidizing air chamber 29. The loosening air chamber 28 corresponds to the first flow channel 26, and the fluidizing air chamber 29 can correspond to the second flow channel 27. The loosening air guide channel 31 is connected to the loosening air chamber 28, and the fluidizing air guide channel 32 is connected to the fluidizing air chamber 29. Airflow can be introduced into the loosening air guide channel 31 and the fluidizing air guide channel 32 respectively. The airflow can enter the main cavity 24 of the return material through the loosening air chamber 28 and the fluidizing air chamber 29 respectively, so that the heat carrier 9 in the main cavity 24 of the return material is in a fluidized state and can be transported to the second output port 38.

[0043] In some exemplary embodiments, such as Figures 2 to 5 As shown, the first return feeder 3 also includes a first connecting pipe 39 and a first conveying pipe 19. The first output port 36 of the first separator 11 can be connected to the second input port 37 of the first return body 12 through the first connecting pipe 39. The second output port 38 of the first return body 12 can be connected to the heat transfer fluid inlet 15 on the first tank 2 through the first conveying pipe 19. A first valve 20 is provided on the first conveying pipe 19. The first valve 20 is configured to control the flow rate of the heat transfer fluid 9 flowing to the mixing zone A1, and is used to adjust the quantity of heat transfer fluid 9 and the particle concentration distribution in the air reactor 1. For example, the quantity of heat transfer fluid 9 in the first tank 16 can be estimated by measuring the particle flow rate, the temperature in the tank, etc. When the quantity of heat transfer fluid 9 is less than the preset quantity, the flow rate of heat transfer fluid 9 in the first conveying pipe 19 is increased by adjusting the first valve 20 to replenish the heat transfer fluid 9 and maintain the stability of the bed quantity of heat transfer fluid in the system.

[0044] In some exemplary embodiments, the first return material body 12 is provided with an openable and closable control port (not shown in the figure). The control port (not shown in the figure) is configured to add or discharge the heat transfer medium 9. That is, the operator can add or discharge some of the heat transfer medium 9 through the control port (not shown in the figure). For example, when it is necessary to remove all of the heat transfer medium 9, the heat transfer medium 9 can be continuously separated in the air reactor 1 and continuously removed through the control port until all of the heat transfer medium 9 is removed. As another example, when the first return material body 12 collects too much heat transfer medium 9, some of the heat transfer medium 9 can be removed through the control port, thereby reducing the weight of the collected heat transfer medium 9. As yet another example, when it is necessary to replenish the heat transfer medium 9, additional heat transfer medium 9 can be added through the control port. A filter screen can be provided at the control port, equipped with a removable filter screen (pore size can be 80μm) for particle size screening. The filter screen can selectively discharge fine particulate heat transfer medium and ash. The control port can be equipped with a flow regulating valve, which is linked with the online monitoring unit to adjust the discharge of heat carrier in real time and maintain the stability of the heat carrier bed in the system. This can effectively prevent the degradation of heat carrier particle size and ash accumulation, extend the continuous operation cycle of the system, and is suitable for chemical looping combustion equipment for high ash fuels (such as lignite and biomass).

[0045] Figure 6 This is a schematic diagram of a chemical looping combustion device according to an exemplary embodiment. In some exemplary embodiments, such as Figures 1 to 6 As shown, the chemical looping combustion device includes a fuel reactor 10 and the aforementioned air reactor 1. The fuel reactor 10 may include a second tank 50, which encloses a fluidized bed structure 57. The side wall of the second tank 50 is also provided with an inlet 55 and an outlet 56. The outlet 56 is located at the top of the second tank 50, and the inlet 55 is located above the fluidized bed structure 57 of the second tank 50. The inlet 55 of the second tank 50 can be connected to the oxygen carrier outlet 13 of the first tank 2 via a conveying device 52, which can transport oxygen carrier from the first tank 2 to the second tank 50. The outlet 56 of the second tank 50 can be connected to the oxygen carrier inlet 14 of the first tank 2 via a return device 51, which can transport oxygen carrier from the second tank 50 to the first tank 2. The second tank 50 has a fuel inlet. The fuel is coal / biomass particles that have been crushed and screened to 1mm to 5mm. The fuel can be fed directly into the second tank 50 from the fuel inlet by means of a screw feeder or other means.

[0046] In some exemplary embodiments, such as Figures 1 to 6As shown, recirculated flue gas can be introduced into the bottom of the second tank 17 of the fuel reactor 10. The airflow formed by the recirculated flue gas serves as the fluidizing air for the fluidized bed structure 57 of the fuel reactor 10, thus keeping the material in the fuel reactor 10 in a fluidized state. The flow velocity of the recirculated flue gas introduced into the second tank 17 of the fuel reactor 10 can be from 1 m / s to 3 m / s.

[0047] Figure 7 This is a schematic diagram of a chemical looping combustion material recycling method in an exemplary embodiment. In some exemplary embodiments, such as Figures 1 to 7 As shown, when the air reactor 1 is working, the heat carrier 9 and the oxygen carrier 8 are mixed in the mixing zone A1 of the first tank 2. The oxidizing gas flow introduced through the fluidizing inlet 5 keeps the heat carrier 9 and the oxygen carrier 8 in a fluidized state, and the oxygen in the gas flow also provides raw materials for the oxidation of the oxygen carrier 8. The oxidation process of the oxygen carrier 8 releases a large amount of heat, which the heat carrier 9 can absorb, acting as a heat transfer medium. As shown by the dashed arrow, after passing through the mixing zone A1, the oxidizing gas flow is converted into an oxygen-deficient flow. The oxygen-deficient flow can blow up smaller particles of the heat carrier 9 and a portion of the oxygen carrier 8, causing the heat carrier 9 and a small portion of the oxygen carrier 8 to rise. Most of the oxygen carrier 8 is difficult to blow up due to its physical characteristics (i.e., large particle weight and large particle diameter). The oxidizing gas stream is air before passing through mixing zone A1. However, oxygen is consumed in mixing zone A1, resulting in the gas stream after passing through mixing zone A1 (i.e., the oxygen-deficient stream) being composed of oxygen-deficient air. Oxygen-deficient air refers to a gas with an oxygen concentration lower than normal air (20.9%). Simultaneously, the oxygen carrier 8 can flow out of the first tank 16 of the air reactor 1 from the oxygen carrier outlet 13 of the first tank 16, and simultaneously flow to the fuel reactor 10 by its own gravity and the conveying device 52, entering the second tank 50 of the fuel reactor 10.

[0048] In some exemplary embodiments, such as Figures 1 to 7As shown, the airflow introduced through the supplementary air inlet provides power for the heat carrier 9 to be blown toward the filter structure 6. The heat carrier 9 can continue to move upward through the filter structure 6, that is, the heat carrier 9 can pass through the openings in the screen. The oxygen carrier 8 is blocked by the filter structure 6 and falls down, meaning that the oxygen carrier 8, due to its larger particle diameter, can only fall after impacting the screen. However, it is not limited to this. For example, the oxygen carrier 8 may not be lifted to the height of the supplementary air inlet due to its own gravity. The airflow only lifts the heat carrier 9, allowing it to pass through the filter structure 6, which includes a screen or baffle. The heat carrier 9 passing through the filter structure 6 can contact the heat exchange structure 7, forming direct heat transfer. Combined with non-contact heat transfer, the heat of the heat carrier 9 is transferred to the heat exchange structure 7, and the heat carrier 9 is cooled. At the same time, the particles of the heat carrier 9 are small, so even if they contact the heat exchange structure 7, the wear on the heat exchange structure 7 is relatively small. After passing through the heat exchange structure 7, the temperature of the heat carrier 9 decreases, and as shown by the dashed arrow, it flows with the airflow to the first separator 11 for gas-solid separation. Inside the first separator 11, the heat carrier 9 falls under its own gravity, while the airflow can be discharged through the exhaust port 18.

[0049] In some exemplary embodiments, such as Figures 1 to 7 As shown, the separated heat carrier 9 can fall into the first return material body 12, where it is collected. The first return material body 12 is connected to the first tank 2 via the first conveying pipe 19, which has a first valve 20 to control the flow rate of the heat carrier 9 to the first tank 2. The heat carrier 9 can flow into the mixing zone A1 of the first tank 16 of the air reactor 1 via the first return material body 12. Thus, the heat carrier 9 can be recycled. The circulation path of the heat carrier 9 in the equipment can sequentially pass through the mixing zone A1, separation zone A2, heat exchange zone A3, first separator 11, first flow channel 26, second flow channel 27, first conveying pipe 19, and mixing zone A1 of the first tank 16.

[0050] In some exemplary embodiments, such as Figures 1 to 7 As shown, while the heat carrier 9 circulates, recirculated flue gas can be introduced into the bottom of the second tank 50 of the fuel reactor 10 on one side, forming a bubbling bed or turbulent bed. Fuel can be mixed with oxygen carrier 8 in an oxidized state. In the second tank 50, the fuel is pyrolyzed and gasified to produce combustible gases such as carbon monoxide and hydrogen. The oxygen carrier 8 converts the generated combustible gases into carbon dioxide and water. A screw feeder can directly feed fuel into the second tank 50 and continuously supply it, enhancing its pyrolysis and gasification process and promoting the full conversion of fuel. The oxygen carrier 8 is reduced, forming a reduced oxygen carrier 8. The reduced oxygen carrier 8 can be conveyed to the mixing zone A1 of the first tank 2 via the return material device 51. Thus, the circulation path of the oxygen carrier 8 in the equipment sequentially passes through the first tank 2, the conveying device 52, the second tank 50, the return material device 51, and the first tank 2.

[0051] In some exemplary embodiments, a new "heat carrier 9" material circulation is added to the existing oxygen carrier 8 material circulation. The oxygen carrier 8 releases heat through oxidation in the first tank 2 of the air reactor 1, and the heat carrier 9 absorbs the released heat and removes it, thus decoupling the heat release process from the heat transfer process. In this circulation method, the oxygen carrier 8 circulates in the "air reactor-fuel reactor" loop, releasing heat through oxidation in the air reactor 1 and carrying lattice oxygen and sensible heat into the fuel reactor 2, converting combustible gas and maintaining the temperature of the fuel reactor 2, ensuring the self-heating operation of the chemical looping combustion device. The heat carrier 9 circulates in the first tank 2-first return feeder 3 loop, does not participate in the reaction in the air reactor 1, absorbs the heat released by the oxidation of the oxygen carrier 8, and transfers it to the heat exchange structure 7, playing a role in heat extraction and uniform bed temperature.

[0052] Figure 8 This is a schematic diagram of another chemical looping combustion device according to this exemplary embodiment. In some exemplary embodiments, such as Figure 8 As shown, the oxygen carrier inlet 14 on the first tank 2 is located on the bottom wall (i.e., the second end cap 43) of the first tank 2.

[0053] In some exemplary embodiments, such as Figure 8 As shown, the chemical looping combustion device includes a fuel reactor and the aforementioned air reactor. The fuel reactor may include a second tank 50, which encloses a fluidized bed structure 57. The side wall of the second tank 50 is also provided with an inlet 55 and an outlet 56. The inlet 55 is located above the fluidized bed structure 57 of the second tank 50, and the outlet 56 is located between the inlet 55 and the fluidized bed structure 57. The inlet 55 of the second tank 50 can be connected to the oxygen carrier outlet 13 of the first tank 2 via a conveying device 52, which can transport oxygen carrier from the first tank 2 to the second tank 50. The outlet 56 of the second tank 50 can be connected to the first tank 2 via a return device 51. The return device 51 has a riser 53, through which oxygen carrier 8 is conveyed from the second tank 50 to the riser 53. One end of the riser 53 extends into the mixing zone A1 from the oxygen carrier inlet 14. The riser 53 can pass through the first air distribution plate 21. The riser 53 is configured to convey oxygen carrier 8 into the fluidized bed furnace 23 of the mixing zone A1. The fuel reactor also includes a second return feeder 54, which can be connected to the second tank 50. The second return feeder 54 can discharge carbon dioxide and water generated during the reduction process.

[0054] In some exemplary embodiments, such as Figure 8As shown, the oxygen carrier 8 flowing out of the second tank 50 can be pneumatically transferred back to the first tank 16 of the air reactor 1. In this example, the riser 53 extends vertically and is inserted into the first tank 16 from the second end cap 43. Air can be introduced into the bottom of the riser 53 as the driving airflow. The residence time of the oxygen carrier 8 in the riser 53 is very short, and the air velocity in the riser 53 is high. The high-speed airflow can quickly remove heat, resulting in vigorous fluidization and good dispersion of the oxygen carrier 8 particles. After being transported to the first tank 16 of the air reactor, the oxygen carrier 8 disperses and decelerates, eventually falling into the mixing zone A1 at the bottom of the first tank 16. Thus, the oxygen carrier 8 is also recycled. The circulation path of the oxygen carrier 8 can be sequentially the first tank 16 of the air reactor 1, the second tank 17 of the fuel reactor 10, and the first tank 16 of the air reactor. This shortens the return path of the oxygen carrier 8, reduces heat loss, enhances system sealing, and prevents gas backflow. In this example of a chemical looping combustion material recycling method, a dual cycle is formed: the recycling of oxygen carrier 8 and the recycling of heat carrier 9. In some exemplary embodiments, such as Figure 8 As shown, a riser 53 is provided, which can shorten the oxygen carrier return path, reduce heat loss, and enhance system sealing to prevent gas backflow. It is suitable for large-scale industrial-grade chemical loop combustion equipment, especially for coal chemical loop combustion power generation systems, and can be used with a high-pressure return feeder to achieve stable circulation.

[0055] In the description of this application, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", "axial", "radial", "circumferential", etc., indicating the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings, are only for the convenience of describing this application and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of this application.

[0056] Furthermore, the terms "first," "second," etc., are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of technical features indicated. Therefore, a feature defined with "first," "second," etc., may explicitly or implicitly include at least one of those features.

[0057] In the description of this application, "multiple" means at least two, such as two, three, etc., unless otherwise expressly and specifically limited.

[0058] In this application, unless otherwise expressly specified and limited, the terms "installation," "connection," "joining," "fixing," etc., should be interpreted broadly. For example, "connection" can be a fixed connection, a detachable connection, or an integral part; it can be a mechanical connection or an electrical connection; it can be a direct connection or an indirect connection through an intermediate medium; it can be the internal communication of two components or the interaction between two components, unless otherwise expressly limited. Those skilled in the art can understand the specific meaning of the above terms in this application according to the specific circumstances.

[0059] In this application, unless otherwise expressly specified and limited, "above" or "below" the second feature can mean that the first and second features are in direct contact, or that the first and second features are in indirect contact through an intermediate medium. Furthermore, "above," "over," and "on top" of the second feature can mean that the first feature is directly above or diagonally above the second feature, or simply that the first feature is at a higher horizontal level than the second feature. "Below," "below," and "under" the second feature can mean that the first feature is directly below or diagonally below the second feature, or simply that the first feature is at a lower horizontal level than the second feature.

[0060] In the description of this specification, the references to terms such as "one embodiment," "some embodiments," "example," "specific example," or "some examples," etc., indicate that a specific feature, structure, material, or characteristic described in connection with that embodiment or example is included in at least one embodiment or example of this application. In this specification, the illustrative expressions of the above terms do not necessarily refer to the same embodiment or example. Furthermore, the specific features, structures, materials, or characteristics described may be combined in any suitable manner in one or more embodiments or examples. Moreover, without contradiction, those skilled in the art can combine and integrate the different embodiments or examples described in this specification, as well as the features of different embodiments or examples.

[0061] Although embodiments of this application have been shown and described above, it is understood that the above embodiments are exemplary and should not be construed as limiting this application. Those skilled in the art can make changes, modifications, substitutions and variations to the above embodiments within the scope of this application.

Claims

1. An air reactor for use in chemical looping combustion, characterized in that, It includes a first tank body, which encloses a reaction space, and the bottom of the first tank body is provided with a fluidizing inlet for introducing fluidizing gas flow; The reaction space includes a mixing zone, a separation zone, and a heat exchange zone arranged sequentially from bottom to top in the vertical direction; The mixing zone is configured to provide a space for mixing oxygen carrier and heat carrier; The first tank is provided with a filter structure in the separation zone, and the filter structure is configured to filter the heat carrier moving from the separation zone to the heat exchange zone; The first tank is provided with a heat exchange structure in the heat exchange zone, and the heat exchange structure is configured to extract heat from the heat carrier.

2. The air reactor according to claim 1, characterized in that, It also includes a first return feeder, which is connected to the first tank and is configured to transport the heat carrier in the heat exchange zone to the mixing zone.

3. The air reactor according to claim 2, characterized in that, The first tank is provided with a heat carrier inlet for inputting the heat carrier and a heat carrier outlet for outputting the heat carrier. The heat carrier inlet is provided in the mixing zone and the heat carrier outlet is provided in the heat exchange zone. The first return feeder includes a first separator and a first return body connected to each other; The input end of the first separator is connected to the outlet of the heat carrier, and the first separator is configured to transport the heat carrier in the heat exchange zone to the first return material body. The output end of the first return material body is connected to the inlet of the heat carrier, and the first return material body is configured to transport the heat carrier to the mixing zone.

4. The air reactor according to claim 3, characterized in that, The output end of the first return material body is connected to the inlet of the heat carrier through the first conveying pipe; The first delivery pipe is equipped with a first valve, which is configured to control the flow rate of the heat carrier flowing to the mixing zone.

5. The air reactor according to claim 3, characterized in that, The first return material body is provided with an openable and closable control port, the control port is provided with a filter screen, and the control port is configured to add or discharge the heat carrier.

6. The air reactor according to claim 1, characterized in that, The filter structure includes a screen, the pore size of which is larger than the particle diameter of the heat carrier and smaller than the particle diameter of the oxygen carrier, so as to filter the heat carrier and prevent the oxygen carrier from passing through. Alternatively, the filter structure may include a partition with at least one through-hole.

7. The air reactor according to claim 1, characterized in that, The first tank is provided with a supplementary air inlet for providing airflow to the filter structure. The supplementary air inlet is located corresponding to the separation zone and is situated on the lower side of the filter structure.

8. The air reactor according to claim 7, characterized in that, The supplementary air inlet is provided in multiple ways, and the multiple supplementary air inlets are evenly arranged around the circumference of the first tank.

9. The air reactor according to claim 1, characterized in that, The sidewall of the first tank includes a reaction section, a separation section, and a heat exchange section connected sequentially from bottom to top. The reaction section encloses the mixing zone, the separation section encloses the separation zone, and the heat exchange section encloses the heat exchange zone. The inner wall of the reaction section is covered with a first refractory layer, the material of which includes high-density refractory castable. The inner wall of the separation section is covered with a first lining structure, which includes a heat insulation layer and a second fire-resistant layer stacked in the wall thickness direction of the separation section. The heat exchange structure is disposed on the inner wall of the heat exchange section, and the surface of the heat exchange structure is covered with a wear-resistant and thermally conductive coating.

10. The air reactor according to claim 1, characterized in that, The first tank is provided with an oxygen carrier inlet for inputting the oxygen carrier and an oxygen carrier outlet for outputting the oxygen carrier; The oxygen carrier inlet is located on the side wall of the first tank. Both the oxygen carrier inlet and the oxygen carrier outlet are provided corresponding to the mixing zone, and the oxygen carrier inlet is located above the oxygen carrier outlet in the vertical direction.

11. The air reactor according to claim 10, characterized in that, The oxygen carrier inlet is provided in multiple ways, and the multiple oxygen carrier inlets are evenly arranged around the circumference of the first tank body, and the multiple oxygen carrier inlets are staggered in the vertical direction.

12. The air reactor according to claim 1, characterized in that, The first tank is provided with an oxygen carrier inlet for inputting the oxygen carrier and an oxygen carrier outlet for outputting the oxygen carrier, and the oxygen carrier inlet is located on the bottom wall of the first tank. The oxygen carrier inlet is configured to be connected to a return device for inputting the oxygen carrier, the return device being configured to convey the oxygen carrier into the mixing zone.

13. A chemical looping combustion device, characterized in that, Includes the air reactor as described in any one of claims 1 to 12.

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