Fluidized bed reactor
By designing a distribution plate and a guide tube inside the cylinder, the powder is allowed to circulate autonomously using gas flow. This solves the problems of powder agglomeration and high sealing in silicon-carbon anode fluidized bed reactors, reducing production costs and improving production efficiency and reaction uniformity.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- WANHUA CHEM GRP CO LTD
- Filing Date
- 2024-10-21
- Publication Date
- 2026-04-21
AI Technical Summary
In silicon-carbon anode fluidized bed reactors, powder materials are prone to agglomeration and require high sealing, leading to increased production costs. Mechanical stirring components are also easily damaged, affecting production efficiency.
The design incorporates a distribution plate and a guide tube inside the cylinder, utilizing gas flow to achieve autonomous circulation of the powder, eliminating the need for mechanical stirring components. Gas is blown upwards within the second gap to prevent powder from clumping.
It achieves uniform flow of powder in the circulation chamber, reduces the probability of powder agglomeration, lowers production costs, improves production efficiency and reaction uniformity, and avoids mechanical failures and sealing problems.
Smart Images
Figure CN121892040A_ABST
Abstract
Description
Technical Field
[0001] This invention relates to the field of chemical reaction equipment technology, and more particularly to a fluidized bed reactor. Background Technology
[0002] A fluidized bed reactor is a device in which a chemical reaction takes place in a boiling bed of solid materials or catalysts. It is also known as a "boiling bed reactor." Within a certain flow rate range, the gas intensely agitates the solid particles of catalyst or material piled to a certain thickness (bed), causing them to behave like a boiling liquid and exhibit some of its properties, such as exerting fluid pressure on the vessel walls, overflowing, and having viscosity. This operating condition is called a "fluidized bed."
[0003] Currently, silicon-carbon anode fluidized bed reactors typically include a distributor with an agitator. This agitator stirs the powder to ensure sufficient contact and reaction between the powder and the reacting gas, while also preventing powder agglomeration. However, during long-term operation, the continuous friction between the powder and the agitator can easily lead to agitator malfunction. Furthermore, because the silanes in the silicon-carbon anode fluidized bed reactor readily react with air, the reactor requires high sealing. The introduction of the agitator necessitates an even higher level of sealing at the connection between the agitator and the reactor, significantly increasing production costs.
[0004] Therefore, there is an urgent need to develop a fluidized bed reactor to solve the above-mentioned technical problems. Summary of the Invention
[0005] The purpose of this invention is to provide a fluidized bed reactor that enables powder to circulate autonomously within the circulation chamber and prevents the powder from agglomerating on the inner wall of the cylinder at the second gap.
[0006] To achieve this objective, the present invention adopts the following technical solution:
[0007] Fluidized bed reactor, including:
[0008] The cylindrical body includes a reduced diameter section;
[0009] A distribution plate is disposed inside the cylinder and divides the interior of the cylinder into a first air inlet chamber and a circulation chamber located above the first air inlet chamber. The distribution plate includes a central area and an edge area surrounding the central area. The distribution plate is provided with a first vent hole located in the edge area.
[0010] The guide tube is set inside the circulation chamber. Both ends of the guide tube have openings. One end of the guide tube faces the center area and has a first gap between it and the distribution plate. A second gap is left between the outer wall of the guide tube and the inner wall of the tube body. The small diameter end of the narrowing section is located on the side of the guide tube away from the distribution plate and has a third gap between it and the guide tube. The inner diameter of the small diameter end of the narrowing section is less than or equal to the inner diameter of the guide tube.
[0011] The air source has its outlet end connected to the second gap through the first air inlet chamber and the first vent.
[0012] Optionally, the distribution plate is also provided with a second vent, which is located in the central area. The outlet of the gas source is connected to the circulation chamber through the second vent. The flow rate of the gas through the second vent is less than the flow rate of the gas through the first vent, and / or the gas flow rate through the second vent is less than the gas flow rate through the first vent.
[0013] Optionally, the fluidized bed reactor further includes a partition hood located inside the first air inlet chamber. The partition hood is fastened to the distribution plate, and the inner cavity of the partition hood cooperates with the distribution plate to form a second air inlet chamber. A second vent is located inside the second air inlet chamber, and the outlet end of the gas source is connected to the second vent through the second air inlet chamber.
[0014] Optionally, the guide tube is coaxially arranged with the cylinder body, and the inner diameter of the guide tube is equal to the diameter of the central area.
[0015] Optionally, the first vent is a variable diameter vent, with the larger diameter end of the variable diameter vent facing the circulation chamber.
[0016] Optionally, the fluidized bed reactor further includes a scraper located within a second gap, the scraper being disposed on the inner wall of the cylinder and / or the outer wall of the guide tube.
[0017] Optionally, the scraper extends in a vertical direction.
[0018] Optionally, there are multiple scrapers, which are evenly distributed along the circumference and axial direction of the cylinder.
[0019] Optionally, the fluidized bed reactor also includes a nozzle, which is disposed on the cylinder. The inlet of the nozzle is connected to the outlet of the gas source, and the outlet of the nozzle is located in the circulation chamber and close to the distribution plate.
[0020] Optionally, the cylinder has a first discharge port and a second discharge port. The first discharge port is connected to the first air inlet chamber and is located near the bottom of the cylinder. The second discharge port is connected to the circulation chamber and is located near the distribution plate.
[0021] The beneficial effects of this invention are:
[0022] The fluidized bed reactor provided by this invention involves gas supplied by a gas source passing sequentially through a first inlet chamber and a first vent, then entering a second gap and flowing upwards to blow up the powder accumulated at the edge of the distribution plate. This causes the powder located at the edge of the distribution plate to flow upwards within the second gap. When the powder reaches the narrowing section, the narrowing section guides the powder, allowing it to flow upwards while simultaneously moving towards the axis of the guide tube. When the powder reaches the edge of the narrowing section's smaller diameter end (i.e., the third gap), it falls back downwards under gravity. Inside the flow tube, the powder falls to the center of the distribution plate. Once a certain thickness of powder accumulates in the center, the powder in the center exerts a compressive force on the powder at the boundary between the center and edge zones, acting in a direction opposite to the axis of the flow tube. This causes the powder at the boundary to enter the edge zone through the first gap. Then, gas blown into the second gap through the first vent blows the powder in the edge zone upwards. This achieves autonomous circulation of the powder within the circulation chamber, allowing for sufficient contact and reaction between the powder and the gas, and reducing the likelihood of powder agglomeration. Secondly, this fluidized bed reactor eliminates the need for mechanical stirring components, thus eliminating the need for sealing at the connection between the mechanical stirring components and the cylinder, which helps reduce production costs. Thirdly, the upward blowing of gas within the second gap causes the powder to flow upwards within the second gap, effectively preventing powder agglomeration on the inner wall of the cylinder at the second gap. Attached Figure Description
[0023] Figure 1 This is a schematic diagram of the structure of the fluidized bed reactor provided in Embodiment 1 of the present invention. Figure 1 ;
[0024] Figure 2 This is a magnified view of a partial structure of the edge region of the distribution plate provided in Embodiment 1 of the present invention;
[0025] Figure 3 This is a schematic diagram of the gas flow path within the fluidized bed reactor provided in Embodiment 1 of the present invention;
[0026] Figure 4 This is a schematic diagram of the powder flow path in the fluidized bed reactor provided in Embodiment 1 of the present invention;
[0027] Figure 5 This is a magnified view of a partial structure of the central area of the distribution plate provided in Embodiment 1 of the present invention;
[0028] Figure 6 This is a schematic diagram of the ring distributor provided in Embodiment 1 of the present invention;
[0029] Figure 7 This is a schematic diagram of the annular tube provided in Embodiment 1 of the present invention.
[0030] In the picture:
[0031] 100. Cylinder body; 111. Reduction section; 112. Expansion section; 121. First air inlet chamber; 122. Circulation chamber; 123. Second air inlet chamber; 131. First discharge port; 132. Second discharge port; 140. Exhaust port; 200. Distribution plate; 210. Central area; 211. Second vent; 220. Edge area; 221. First vent; 300. Guide tube; 410. First gap; 420. Second gap; 430. Third gap; 500. Separator cover; 600. Scraper; 710. Nozzle; 720. Annular pipe; 721. Air inlet; 800. Air inlet pipe; 810. Third discharge port; 900. Annular distributor; 910. Air outlet. Detailed Implementation
[0032] The present invention will now be described in further detail with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and not intended to limit it. Furthermore, it should be noted that, for ease of description, the accompanying drawings show only the parts relevant to the present invention, and not all of the structures.
[0033] In the description of this invention, unless otherwise explicitly specified and limited, the terms "connected," "linked," and "fixed" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral part; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; they can refer to the internal communication of two components or the interaction between two components. Those skilled in the art can understand the specific meaning of the above terms in this invention based on the specific circumstances.
[0034] In this invention, unless otherwise explicitly specified and limited, "above" or "below" the second feature can include direct contact between the first and second features, or contact between the first and second features through another feature between them. Furthermore, "above," "over," and "on top" of the second feature includes the first feature directly above or diagonally above the second feature, or simply indicates that the first feature is at a higher horizontal level than the second feature. "Below," "below," and "under" the second feature includes the first feature directly below or diagonally below the second feature, or simply indicates that the first feature is at a lower horizontal level than the second feature.
[0035] In the description of this embodiment, the terms "upper," "lower," "right," etc., refer to the orientation or positional relationship shown in the accompanying drawings. They are used only for ease of description and simplification of operation, 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. Therefore, they should not be construed as limitations on the present invention. In addition, the terms "first" and "second" are used only for distinction in description and have no special meaning.
[0036] Example 1
[0037] This embodiment provides a fluidized bed reactor that enables powder to circulate autonomously within the circulation chamber and prevents powder from agglomerating on the inner wall of the cylinder at the second gap.
[0038] Specifically, such as Figures 1 to 4 As shown, the fluidized bed reactor includes a cylindrical body 100, a distribution plate 200, a guide tube 300, and a gas source (not shown). The cylindrical body 100 includes a reduced-diameter section 111. The distribution plate 200 is disposed within the cylindrical body 100 and divides the interior of the cylindrical body 100 into a first air inlet chamber 121 and a circulation chamber 122 located above the first air inlet chamber 121. The distribution plate 200 includes a central region 210 and an edge region 220 surrounding the central region 210. The distribution plate 200 is provided with a first vent 221 located within the edge region 220. The guide tube 300 is disposed within the circulation chamber 122. Inside, both ends of the guide tube 300 are provided with openings. One end of the guide tube 300 is set towards the central area 210 and leaves a first gap 410 between it and the distribution plate 200. A second gap 420 is left between the outer wall of the guide tube 300 and the inner wall of the cylinder 100. The small diameter end of the reduced diameter section 111 is located on the side of the guide tube 300 away from the distribution plate 200 and leaves a third gap 430 between it and the guide tube 300. The inner diameter of the small diameter end of the reduced diameter section 111 is less than or equal to the inner diameter of the guide tube 300. The air outlet end of the air source is connected to the second gap 420 through the first air inlet chamber 121 and the first vent 221.
[0039] Based on the above design, the gas supplied by the gas source passes sequentially through the first air inlet chamber 121 and the first vent 221, then enters the second gap 420 and flows upward. Figure 3In the diagram, the solid arrow points to the flow path of the gas entering the second gap 420 through the first air inlet 121 and the first vent 221, thus blowing up the powder accumulated in the edge area 220 of the distribution plate 200. This causes the powder in the edge area 220 of the distribution plate 200 to flow upward within the second gap 420. When the powder flows to the narrowing section 111, the narrowing section 111 guides the powder, allowing it to flow upward while also moving towards the axis of the guide tube 300. When the powder reaches the edge of the small diameter end of the narrowing section 111 (i.e., at the third gap 430), the powder and the second gap 420 are vertically offset, meaning the powder is subjected to the upward flow of gas. The force of gravity is greatly reduced, causing the powder to fall downwards into the guide cylinder 300 under the action of gravity, until it falls into the central area 210 of the distribution plate 200. When a certain thickness of powder accumulates in the central area 210, the powder in the central area 210 exerts a squeezing force on the powder located at the junction of the central area 210 and the edge area 220, which is opposite to the axis of the guide cylinder 300. This causes the powder located at the junction of the central area 210 and the edge area 220 to enter the edge area 220 through the first gap 410. Then, the gas blown into the second gap 420 from the first vent 221 blows the powder in the edge area 220 up, thereby achieving the effect of autonomous circulation of the powder in the circulation chamber 122. Figure 4 In the diagram, the arrow points to the circulating flow path of the powder, which allows the powder to fully contact and react with the gas, improving the uniformity of the reaction inside the fluidized bed reactor and reducing the probability of powder agglomeration.
[0040] Secondly, this fluidized bed reactor eliminates the need for mechanical stirring components, thereby eliminating the need for a sealing structure at the connection between the mechanical stirring components and the cylinder 100. This not only reduces production costs but also avoids the risk of leakage at the connection between the mechanical stirring components and the cylinder 100. Furthermore, it avoids the problem of downtime for maintenance due to mechanical failure of the mechanical stirring components, significantly improving the production cycle and efficiency of the fluidized bed reactor.
[0041] Furthermore, the gas is blown upward within the second gap 420, causing the powder to flow upward within the second gap 420. This promotes the flow of powder on the inner wall of the cylinder 100 at the second gap 420, and has the effect of preventing the powder from clumping on the inner wall of the cylinder 100 at the second gap 420.
[0042] In this embodiment, the inner diameter of the smaller diameter end of the narrowing section 111 is equal to the inner diameter of the guide tube 300, so as to make the overall structure of the fluidized bed reactor more consistent. Of course, in other embodiments, the inner diameter of the smaller diameter end of the narrowing section 111 can be smaller than the inner diameter of the guide tube 300.
[0043] Furthermore, the guide tube 300 is coaxially arranged with the cylinder 100, and the inner diameter of the guide tube 300 is equal to the diameter of the central area 210, so that the inner cavity of the cylinder 100 is aligned with the central area 210, and the second gap 420 is aligned with the edge area 220. This structure allows as much of the powder flowing through the third gap 430 as possible to fall back into the guide tube 300 and then accumulate in the central area 210 of the distribution plate 200. In addition, this structural design also makes the airflow distribution in the circumferential direction of the cylinder 100 in the circulation chamber 122 more uniform, thereby making the powder in the circulation chamber 122 more uniformly distributed in the circumferential direction of the cylinder 100. This has the effect of improving the uniformity of the internal reaction of the fluidized bed reactor, which is beneficial to the long-term stable operation of the fluidized bed reactor.
[0044] Furthermore, there are multiple first vent holes 221, which are evenly distributed within the edge region 220. This increases the airflow rate from the first air inlet chamber 121 into the second gap 420 and improves the uniformity of gas flow from the first air inlet chamber 121 into the second gap 420 along the circumference of the cylinder 100. This, in turn, improves the flow rate of the powder in the self-circulating circulation chamber 122 and enhances the uniformity of powder distribution along the circumference of the cylinder 100. It should be noted that the number of first vent holes 221 can be ten, twenty, or thirty-five, depending on the size of the edge region 220.
[0045] Preferably, such as Figures 1 to 4 As shown, the powder accumulation height inside the guide tube 300 is higher than the powder accumulation height inside the second gap 420. Figure 4 The wavy line in the diagram represents the accumulation height of the powder in the guide tube 300 and the second gap 420. The difference between the accumulation height of the powder in the guide tube 300 and the accumulation height of the powder in the second gap 420 is used to promote the flow of the powder in the central area 210 to the edge area 220 through the first gap 410.
[0046] Optionally, such as Figure 3 and Figure 6 As shown, the fluidized bed reactor also includes an annular distributor 900, which is disposed within the first inlet chamber 121. The outlet end of the gas source is connected to the first inlet chamber 121 through the annular distributor 900 to ensure a more uniform distribution of gas entering the first inlet chamber 121. The annular distributor 900 has multiple outlet holes 910, which are evenly distributed along the circumference of the annular distributor 900 and all outlet holes 910 face the distribution plate 200. The diameter of the outlet holes 910 is 1.5mm-4.5mm. For example, the diameter of the outlet holes 910 can be 1.5mm, 2mm, 3mm, 4mm, or 4.5mm, etc. The specific structure and working principle of the annular distributor 900 provided in this embodiment are common technologies in the art and will not be described in detail here.
[0047] Optionally, such as Figures 1 to 5 As shown, the distribution plate 200 is also provided with a second vent 211, which is located in the central area 210. The outlet of the air source is connected to the circulation chamber 122 through the second vent 211. The flow rate of the gas through the second vent 211 is less than that of the gas through the first vent 221, and / or the flow rate of the gas through the second vent 211 is less than that of the gas through the first vent 221. This makes it impossible for the gas through the second vent 211 to blow up the powder in the central area 210, that is, the powder accumulated in the central area 210 cannot flow upward. The gas through the second vent 211 can only slightly disperse the powder in the central area 210, thus loosening the powder in the central area 210. Figure 3 In the diagram, the dashed arrow indicates the flow path of gas entering the circulation chamber 122 through the second vent 211. This design, on the one hand, prevents powder from agglomerating or clumping in the central area 210, and on the other hand, promotes the flow of powder from the central area 210 to the edge area 220, increasing the flow rate of powder flowing from the central area 210 to the edge area 220, thus promoting the self-circulating flow of powder. Furthermore, there are multiple second vents 211, evenly distributed in the central area 210, to increase the airflow rate entering the circulation chamber 122 through the second vents 211, thereby improving the loosening effect on the powder in the central area 210 and achieving a uniform loosening effect. It should be noted that the number of second vents 211 can be ten, twenty, or thirty-five, depending on the size of the central area 210.
[0048] Optionally, the diameter of the second vent 211 is greater than or equal to the diameter of the first vent 221, so as to ensure that the gas passing through the second vent 211 cannot blow up the powder in the central area 210.
[0049] Optionally, such as Figures 1 to 5As shown, the fluidized bed reactor also includes a partition hood 500, which is located inside the first air inlet chamber 121. The partition hood 500 is fastened to the distribution plate 200. The inner cavity of the partition hood 500 and the distribution plate 200 cooperate to form a second air inlet chamber 123. A second vent 211 is located inside the second air inlet chamber 123. The outlet of the gas source is connected to the second vent 211 through the second air inlet chamber 123. This structural design separates the first air inlet chamber 121 and the second air inlet chamber 123, facilitating individual control of the air entering the second air inlet chamber. The flow rate and / or velocity of the gas in the first air inlet chamber 121, and the flow rate and / or velocity of the gas entering the second air inlet chamber 123 are controlled separately to ensure that the gas velocity through the second vent 211 is less than the gas velocity through the first vent 221, and / or to ensure that the gas flow rate through the second vent 211 is less than the gas flow rate through the first vent 221. This ensures that the powder located in the central area 210 cannot flow upward, thereby ensuring that the powder can achieve autonomous circulation.
[0050] Optionally, such as Figures 1 to 4 As shown, the top of the cylinder 100 is provided with an exhaust port 140. Gas entering the second gap 420 through the first vent 221 flows upward and finally exits the cylinder 100 from the exhaust port 140. Figure 3 The solid arrow points to the flow path of the gas entering the second gap 420 through the first intake chamber 121 and the first vent 221; the gas entering the circulation chamber 122 through the second vent 211 flows upward and finally exits the cylinder 100 from the exhaust port 140. Figure 3 The dashed arrow in the middle points to the flow path of the gas entering the circulation chamber 122 through the second vent 211, in order to maintain the stable air pressure inside the cylinder 100 and ensure that the powder flows autonomously within the cylinder 100.
[0051] Optionally, such as Figures 1 to 4 As shown, the cylinder 100 also includes an expansion section 112, which is located on the side of the reduction section 111 away from the distribution plate 200, and the small diameter end of the expansion section 112 faces the small diameter end of the reduction section 111. After passing through the reduction section 111, the gas enters the expansion section 112. The expansion section 112 significantly reduces the gas velocity, thereby preventing the powder from continuing to flow upward with the gas after passing through the reduction section 111. This structural design provides a guarantee for the powder to fall back into the guide cylinder after passing through the reduction section 111, thus ensuring the autonomous circulation of the powder.
[0052] Furthermore, the angle between the sidewall of the expansion section 112 and the horizontal direction is β, where 40° < β < 65°. For example, β can be 40°, 45°, 50°, 60°, or 65°, etc., to improve the reliability of the expansion section 112 in reducing airflow velocity.
[0053] Optionally, such as Figures 1 to 4 As shown, the fluidized bed reactor also includes a scraper 600, which is disposed on the inner wall of the cylinder 100 and located within the second gap 420. Since the powder is prone to agglomeration, when the powder agglomerates to a certain extent, it will form clumps. The scraper 600 can break up the agglomerated powder flowing upward within the second gap 420 in time to avoid powder agglomeration.
[0054] In another embodiment, a scraper 600 is disposed on the outer wall of the guide tube 300 and is located within the second gap 420. In yet another embodiment, scrapers 600 are disposed on both the outer wall of the guide tube 300 and the inner wall of the tube 100, and the scrapers 600 are located within the second gap 420.
[0055] Furthermore, such as Figures 1 to 4 As shown, the scraper 600 extends vertically. Since the flow direction of the powder in the second gap 420 is vertical, setting the scraper 600 to extend vertically can not only reduce the resistance to the upward flow of the powder, but also improve the crushing effect on the agglomerated powder.
[0056] Furthermore, such as Figures 1 to 4 As shown, there are multiple scraper blades 600, which are evenly distributed along the circumference and axial direction of the cylinder 100 to improve the crushing effect on agglomerated powder and at the same time improve the uniformity of the crushing effect on agglomerated powder along the circumference of the cylinder 100.
[0057] Optionally, the number of scraper blades 600 is approximately eight to thirty-five. For example, the number of scraper blades 600 can be eight, ten, twenty-five, thirty, or thirty-five, etc., which can both break up agglomerated powder and reduce the resistance of the scraper blades 600 to the airflow in the second gap 420, ensuring that the powder in the second gap 420 can flow upward.
[0058] Optionally, such as Figures 1 to 4As shown, the first vent 221 is a variable diameter vent, with its larger diameter end facing the circulation chamber 122. This allows the first vent 221 to slow down the gas blown into the second gap 420, preventing excessive upward flow velocity of the powder within the second gap 420 due to excessive gas velocity. It should be noted that if the upward flow velocity of the powder within the second gap 420 is too high, excessive wear of the scraper 600 may occur, affecting the contact reaction between the powder and the gas. Furthermore, if the upward flow velocity of the powder within the second gap 420 is too high, the narrowing section 111 may fail to guide the powder effectively. That is, after passing through the narrowing section 111, the powder will not fall back into the guide tube 300 but will continue to flow upward, preventing the powder's autonomous circulation from functioning properly. It can be seen that the first vent 221 is a variable diameter vent, and the design of the large diameter end of the variable diameter vent facing the circulation chamber 122 can not only prevent the powder from being excessively worn, but also ensure the autonomous circulation of the powder.
[0059] It should be noted that in this embodiment, the diameter of the second vent 211 is greater than or equal to the diameter of the first vent 221. The first vent 221 is a variable diameter vent, that is, the diameter of the second vent 211 is greater than or equal to the diameter of the large diameter end of the first vent 221.
[0060] Optionally, the diameter of the second vent 211 is 0.5mm-6.5mm. For example, the diameter of the second vent 211 can be 0.5mm, 1mm, 3.5mm, 6mm, or 6.5mm, etc. The diameter of the large-diameter end of the first vent 221 is 0.5mm-6.5mm. For example, the diameter of the large-diameter end of the first vent 221 can be 0.5mm, 1mm, 3.5mm, 6mm, or 6.5mm, etc. The diameter of the small-diameter end of the first vent 221 is 0.5mm-6.5mm. For example, the diameter of the small-diameter end of the first vent 221 can be 0.5mm, 1mm, 3.5mm, 6mm, or 6.5mm, etc. It is understandable that although the diameters of the second vent 211, the large diameter end of the first vent 221, and the small diameter end of the first vent 221 are all within the same range, it is sufficient that the diameter of the second vent 211 is greater than or equal to the diameter of the large diameter end of the first vent 221, and the diameter of the large diameter end of the first vent 221 is greater than the diameter of the small diameter end of the first vent 221.
[0061] Optionally, the distribution plate 200 is circular, and its diameter is 0.05m-2.5m. For example, the diameter of the distribution plate 200 can be 0.05m, 0.1m, 2m, or 2.5m, etc. The area of the distribution plate 200 is A, the cross-sectional area of the second vent 211 is B, the cross-sectional area of the large-diameter end of the first vent 221 is C, and the opening ratio on the distribution plate 200 is K, where K = (B+C) / A, and A < 12%. For example, A can be 12%, 10%, or 8%, etc., to ensure that the distribution plate 200 has a certain structural strength.
[0062] Optionally, both the cylinder 100 and the guide tube 300 are cylindrical. The height of the guide tube 300 is 0.5m-8.5m. For example, the height of the guide tube 300 can be 0.5m, 1m, 3.5m, 6m, 8m or 8.5m, etc. The inner diameter of the guide tube 300 is D, and the inner diameter of the cylinder 100 is E. M = D / E, 65% < M < 90%. For example, M can be 65%, 70%, 80%, 85% or 90%, etc., to ensure that the second gap 420 has sufficient space in the radial direction of the cylinder 100 so that the powder can maintain a suitable flow rate upward within the second gap 420, and also reduce the probability of powder agglomeration and blockage within the second gap 420.
[0063] Optionally, such as Figures 1 to 4 As shown, the fluidized bed reactor also includes a nozzle 710, which is disposed on the cylinder 100. The air inlet of the nozzle 710 is connected to the air outlet of the gas source, and the air outlet of the nozzle 710 is located in the circulation chamber 122 and close to the distribution plate 200. If there are agglomerated or clumped powders in the edge area 220 of the distribution plate 200, the high-pressure gas ejected from the nozzle 710 can break up the agglomerated and clumped powders.
[0064] Furthermore, there are multiple nozzles 710, and these nozzles 710 are evenly distributed along the circumference of the cylinder 100 to improve the effect of breaking up agglomerated and lumpy powders, and also to improve the uniformity of the breaking effect on agglomerated and lumpy powders along the circumference of the cylinder 100. It is understood that the specific number of nozzles 710 depends on the diameter of the cylinder 100; for the commonly used diameter of the cylinder 100 in fluidized bed reactors, approximately two to six nozzles 710 are sufficient.
[0065] Optionally, in order to avoid interference between the high-pressure gas ejected from the nozzle 710 and the gas entering the second gap 420 through the first vent 221, in this embodiment, the nozzle 710 is opened intermittently, that is, the high-pressure gas is ejected from the nozzle 710 intermittently.
[0066] Optionally, such as Figure 7As shown, the fluidized bed reactor also includes an annular pipe 720, which is wound around the outside of the cylinder 100. The annular pipe 720 has an air inlet 721 connected to the outlet of a gas source. The air inlet of the nozzle 710 is connected to the annular pipe 720, allowing the air inlet of the nozzle 710 to be connected to the outlet of the gas source through the annular pipe 720. The design of the annular pipe 720 buffers the gas entering the nozzle 710, preventing excessively high-pressure gas from being ejected from the nozzle 710 and avoiding the problem of all the powder in the edge zone 220 being blown to the central zone 210. Preferably, the air inlet pressure of the nozzle 710 is 0.15MPa-0.85MPa. For example, the air inlet pressure of the nozzle 710 can be 0.15MPa, 0.2MPa, 0.5MPa, 0.8MPa, or 0.85MPa, etc.
[0067] Furthermore, such as Figure 7 As shown, there are multiple air inlets 721, which are equal in number to the number of nozzles 710. The multiple air inlets 721 are evenly distributed along the circumference of the annular tube 720. In the circumference of the annular tube 720, the air inlets 721 and nozzles 710 are alternately distributed to make the air intake of the multiple nozzles 710 more uniform, thereby improving the uniformity of the crushing effect on agglomerated powder and lumpy powder along the circumference of the cylinder 100.
[0068] Optionally, such as Figures 1 to 4 As shown, the cylinder 100 has a first discharge port 131 and a second discharge port 132. The first discharge port 131 is connected to the first air inlet chamber 121 and is located near the bottom of the cylinder 100. The second discharge port 132 is connected to the circulation chamber 122 and is located near the distribution plate 200. Waste in the first air inlet chamber 121 can be discharged from the cylinder 100 through the first discharge port 131. After the waste in the circulation chamber 122 falls onto the distribution plate 200, it can be discharged from the cylinder 100 through the second discharge port 132. After the nozzle 710 breaks up the powder agglomerated on the distribution plate 200, it can also be discharged from the cylinder 100 through the second discharge port 132. This reduces the probability of residual waste in the cylinder 100 and provides a guarantee for the long-term stability of the fluidized bed reactor. In this embodiment, the first discharge port 131 is coaxial with the cylinder 100, that is, the first discharge port 131 is located at the bottom of the cylinder 100.
[0069] Optionally, such as Figures 1 to 4 As shown, the partition cover 500 is provided with an air inlet pipe 800. The air outlet end of the air source is connected to the second air inlet chamber 123 through the air inlet pipe 800. Furthermore, the air inlet pipe 800 is provided with a third discharge port 810. When the air source stops supplying gas to the second air inlet chamber 123, the third discharge port 810 opens to discharge the waste material in the air inlet pipe 800.
[0070] It should be noted that the air source connected to the first air inlet chamber 121, the air source connected to the second air inlet chamber 123, and the air source connected to the nozzle 710 can be the same air source or different air sources. When the air source connected to the first air inlet chamber 121, the air source connected to the second air inlet chamber 123, and the air source connected to the nozzle 710 are the same air source, a first valve is installed on the air inlet pipe of the annular distributor. By controlling the opening of the first valve, the gas velocity and flow rate of the gas entering the first air inlet chamber 121 can be controlled. A second valve is installed on the air inlet pipe 800 connected to the second air inlet chamber 123. By controlling the opening of the second valve, the gas velocity and flow rate of the gas entering the second air inlet chamber 123 can be controlled. A third valve is installed on the air inlet pipe connected to the air inlet hole of the annular pipe 720. By controlling the opening of the third valve, the gas pressure entering the nozzle 710 can be controlled. Of course, the control of the gas flow rate and volume of the gas entering the first intake chamber 121, the control of the gas flow rate and volume of the gas entering the second intake chamber 123, and the control of the gas pressure entering the nozzle 710 can also be achieved through other methods common in the art, which will not be elaborated here. When the gas source connected to the first intake chamber 121, the gas source connected to the second intake chamber 123, and the gas source connected to the nozzle 710 are not the same gas source, that is, the gas source includes a first gas source, a second gas source, and a third gas source, wherein the first gas source is connected to the first intake chamber 121, the second gas source is connected to the second intake chamber 123, and the third gas source is connected to the air inlet of the nozzle 710, then controlling the first gas source, the second gas source, and the third gas source individually can achieve the control of the gas flow rate and volume of the gas entering the first intake chamber 121, the control of the gas flow rate and volume of the gas entering the second intake chamber 123, and the control of the gas pressure entering the nozzle 710.
[0071] In this embodiment, the opening ratio K on the distribution plate 200 is 2%, the diameter of the distribution plate 200 is 0.1m, the diameter of the large diameter end of the first vent 221 is 2mm, the diameter of the small diameter end of the first vent 221 is 1mm, the diameter of the second vent 211 is 2mm, the inner diameter D of the guide tube 300 is 0.07m, the height of the guide tube 300 is 1.5m, the angle β between the sidewall of the expansion section 112 and the horizontal direction is 45°, the number of scrapers 600 is twelve, the length of the scrapers 600 is 100mm, the diameter of the air outlet 910 of the annular distributor 900 is 2mm, the number of air outlets 910 of the annular distributor 900 is ten, the number of nozzles 710 is two, and the air inlet pressure of the nozzles 710 is 0.2MPa.
[0072] Example 2
[0073] This embodiment provides a fluidized bed reactor, which differs from the fluidized bed reactor provided in Embodiment 1 in that:
[0074] In this embodiment, the opening ratio K on the distribution plate 200 is 5%, the diameter of the distribution plate 200 is 0.2m, the diameter of the large diameter end of the first vent 221 is 3mm, the diameter of the small diameter end of the first vent 221 is 2mm, the diameter of the second vent 211 is 3mm, the inner diameter D of the guide tube 300 is 0.16m, the height of the guide tube 300 is 2m, the angle β between the side wall of the expansion section 112 and the horizontal direction is 45°, the number of scrapers 600 is twelve, the length of the scrapers 600 is 200mm, the diameter of the air outlet 910 of the annular distributor 900 is 2mm, the number of air outlets 910 of the annular distributor 900 is fifteen, the number of nozzles 710 is two, and the air inlet pressure of the nozzles 710 is 0.2MPa.
[0075] The remaining structure of the fluidized bed reactor provided in this embodiment is the same as that in Embodiment 1, and will not be described again.
[0076] Example 3
[0077] This embodiment provides a fluidized bed reactor, which differs from the fluidized bed reactor provided in Embodiment 1 in that:
[0078] In this embodiment, the opening ratio K on the distribution plate 200 is 5%, the diameter of the distribution plate 200 is 1m, the diameter of the large diameter end of the first vent 221 is 6mm, the diameter of the small diameter end of the first vent 221 is 3mm, the diameter of the second vent 211 is 6mm, the inner diameter D of the guide tube 300 is 0.7m, the height of the guide tube 300 is 4m, the angle β between the side wall of the expansion section 112 and the horizontal direction is 60°, the number of scrapers 600 is twenty, the length of the scrapers 600 is 300mm, the diameter of the air outlet 910 of the annular distributor 900 is 4mm, the number of air outlets 910 of the annular distributor 900 is fifty, the number of nozzles 710 is four, and the air inlet pressure of the nozzles 710 is 0.5MPa.
[0079] The remaining structure of the fluidized bed reactor provided in this embodiment is the same as that in Embodiment 1, and will not be described again.
[0080] Example 4
[0081] This embodiment provides a fluidized bed reactor, which differs from the fluidized bed reactor provided in Embodiment 1 in that:
[0082] In this embodiment, the opening ratio K on the distribution plate 200 is 4%, the diameter of the distribution plate 200 is 2m, the diameter of the large diameter end of the first vent 221 is 6mm, the diameter of the small diameter end of the first vent 221 is 4mm, the diameter of the second vent 211 is 6mm, the inner diameter D of the guide tube 300 is 1.6m, the height of the guide tube 300 is 5m, the angle β between the side wall of the expansion section 112 and the horizontal direction is 60°, the number of scrapers 600 is thirty, the length of the scrapers 600 is 300mm, the diameter of the air outlet 910 of the annular distributor 900 is 4mm, the number of air outlets 910 of the annular distributor 900 is sixty, the number of nozzles 710 is six, and the air inlet pressure of the nozzles 710 is 0.5MPa.
[0083] The remaining structure of the fluidized bed reactor provided in this embodiment is the same as that in Embodiment 1, and will not be described again.
[0084] Obviously, the above embodiments of the present invention are merely examples for clearly illustrating the present invention, and are not intended to limit the implementation of the present invention. Those skilled in the art will be able to make various obvious changes, readjustments, and substitutions without departing from the scope of protection of the present invention. It is neither necessary nor possible to exhaustively describe all embodiments here. Any modifications, equivalent substitutions, and improvements made within the spirit and principles of the present invention should be included within the scope of protection of the claims of the present invention.
Claims
1. A fluidized bed reactor, characterized in that, include: A cylindrical body (100), the cylindrical body (100) including a reduced diameter section (111); A distribution plate (200) is disposed inside the cylinder (100) and divides the interior of the cylinder (100) into a first air inlet chamber (121) and a circulation chamber (122) located above the first air inlet chamber (121). The distribution plate (200) includes a central area (210) and an edge area (220) surrounding the central area (210). The distribution plate (200) is provided with a first vent (221) located within the edge area (220). A flow guide tube (300) is disposed in the circulation chamber (122). Both ends of the flow guide tube (300) are provided with openings. One end of the flow guide tube (300) is disposed facing the central area (210) and has a first gap (410) between it and the distribution plate (200). A second gap (420) is left between the outer wall of the flow guide tube (300) and the inner wall of the cylinder (100). The small diameter end of the reduced diameter section (111) is located on the side of the flow guide tube (300) away from the distribution plate (200) and has a third gap (430) between it and the flow guide tube (300). The inner diameter of the small diameter end of the reduced diameter section (111) is less than or equal to the inner diameter of the flow guide tube (300). The air source has its outlet end connected to the second gap (420) through the first air inlet chamber (121) and the first vent (221).
2. The fluidized bed reactor according to claim 1, characterized in that, The distribution plate (200) is also provided with a second vent (211), which is located in the central area (210). The outlet of the gas source is connected to the circulation chamber (122) through the second vent (211). The flow rate of the gas through the second vent (211) is less than the flow rate of the gas through the first vent (221), and / or the flow rate of the gas through the second vent (211) is less than the flow rate of the gas through the first vent (221).
3. The fluidized bed reactor according to claim 2, characterized in that, The fluidized bed reactor further includes a partition cover (500), which is located inside the first air inlet chamber (121). The partition cover (500) is fastened to the distribution plate (200). The inner cavity of the partition cover (500) cooperates with the distribution plate (200) to form a second air inlet chamber (123). The second vent (211) is located inside the second air inlet chamber (123). The outlet of the gas source is connected to the second vent (211) through the second air inlet chamber (123).
4. The fluidized bed reactor according to any one of claims 1-3, characterized in that, The guide tube (300) is coaxially arranged with the cylinder (100), and the inner diameter of the guide tube (300) is equal to the diameter of the central region (210).
5. The fluidized bed reactor according to any one of claims 1-3, characterized in that, The first vent (221) is a variable diameter vent, with the larger diameter end of the variable diameter vent facing the circulation chamber (122).
6. The fluidized bed reactor according to any one of claims 1-3, characterized in that, The fluidized bed reactor further includes a scraper (600) located within the second gap (420), and the scraper (600) is disposed on the inner wall of the cylinder (100) and / or the outer wall of the guide tube (300).
7. The fluidized bed reactor according to claim 6, characterized in that, The scraper (600) extends in a vertical direction.
8. The fluidized bed reactor according to claim 6, characterized in that, The number of scraper blades (600) is multiple, and the multiple scraper blades (600) are evenly distributed along the circumference and axial direction of the cylinder (100).
9. The fluidized bed reactor according to any one of claims 1-3, characterized in that, The fluidized bed reactor further includes a nozzle (710), which is disposed on the cylinder (100). The air inlet of the nozzle (710) is connected to the air outlet of the gas source, and the air outlet of the nozzle (710) is located in the circulation chamber (122) and close to the distribution plate (200).
10. The fluidized bed reactor according to any one of claims 1-3, characterized in that, The cylinder (100) has a first discharge port (131) and a second discharge port (132). The first discharge port (131) is connected to the first air inlet chamber (121) and is located near the bottom of the cylinder (100). The second discharge port (132) is connected to the circulation chamber (122) and is located near the distribution plate (200).