Circulating type natural graphite purification fluidized bed reactor

Abstract

The utility model discloses a circulating type natural graphite purification fluidized bed reactor. The circulating type natural graphite purification fluidized bed reactor comprises a reactor body, the reactor body is provided with a reaction chamber, a gas inlet structure, a gas outlet structure, a feeding structure, a discharging structure and a first distribution plate structure, the gas inlet structure, the gas outlet structure, the feeding structure, the discharging structure and the first distribution plate structure are communicated with the reaction chamber, and the first distribution plate structure is arranged in the reaction chamber and located between the gas inlet structure and the gas outlet structure; the first distribution plate structure is used for bearing solid materials, and the first distribution plate structure is further provided with a ventilation structure; and the gas-solid separation module is used for separating solid materials in the fluidizing gas or the reaction gas after reacting with the solid materials and conveying the separated solid materials back to the area, close to the first distribution plate structure, of the reaction chamber. The device disclosed by the utility model can be used for further treating the gas participating in the purification reaction and separating solid materials in the gas, so that not only is the yield of the purified solid materials improved, but also the burden of a downstream tail gas treatment system is reduced.

Description

Technical Field

[0001] The utility model particularly relates to a circulating natural graphite purification fluidized bed reactor, belonging to the technical field of material purification. Background Art

[0002] Battery materials have very high requirements for the purity of graphite raw materials, and the Fe impurity content is even required to be below 30ppm. However, natural graphite comes from natural ores, and the impurity composition and structure other than graphite are complex, especially microcrystalline graphite.

[0003] The current industrial treatment methods mainly include: pickling purification and high-temperature evaporation. However, pickling purification generally uses HF acid for purification, and this process will produce a large amount of acid-containing wastewater, causing environmental pollution; high-temperature evaporation requires the use of an intermittent furnace at about 3000°C for purification. This treatment process has a small processing capacity and requires intermittent operation. It has high costs and is difficult to commercialize on a large scale. Utility Model Content

[0004] The main purpose of the utility model is to provide a circulating fluidized bed reactor for purifying natural graphite, which can realize the preparation of high-purity carbon materials (>99.95%) on the one hand; on the other hand, the fluidized bed reactor can also effectively reduce the solid materials being carried out of the fluidized bed reactor with the fluidizing gas or the reaction gas, which not only improves the yield of the purified solid materials, but also reduces the burden on the downstream exhaust gas treatment system.

[0005] In order to achieve the above-mentioned utility model purpose, the technical solution adopted by the utility model includes:

[0006] The utility model embodiment provides a circulating natural graphite purification fluidized bed reactor, which comprises:

[0007] A reactor body, wherein the reactor body comprises a reaction chamber and an air inlet structure, an air outlet structure, a material feed structure, and a material discharge structure connected to the reaction chamber.

[0008] A first distribution plate structure, the first distribution plate structure is arranged in the reaction chamber, the first distribution plate structure is located between the air inlet structure and the air outlet structure, the first distribution plate structure is used to carry solid materials, and the first distribution plate structure also has a permeable structure, the fluidizing gas or reaction gas input from the air inlet structure passes through the permeable structure and contacts and reacts with the solid materials on the first distribution plate structure, and then is discharged from the air outlet structure;

[0009] A gas-solid separation module is used to separate the solid material from the fluidizing gas or reaction gas after reacting with the solid material, and transport the separated solid material back to the reaction chamber near the first distribution plate structure.

[0010] Compared with the prior art, the advantages of the present utility model include: A circulating natural graphite purification fluidized bed reactor provided by an embodiment of the present utility model realizes the preparation of high-purity carbon materials (>99.95%) on the one hand; on the other hand, the circulating natural graphite purification fluidized bed reactor can further treat the gas after the purification reaction and separate the solid materials therein, not only improving the yield of the purified solid materials, but also reducing the burden on the downstream tail gas treatment system. BRIEF DESCRIPTION OF THE DRAWINGS

[0011] In order to more clearly illustrate the technical solutions in the embodiments of the present application or the prior art, the following will briefly introduce the drawings required for use in the description of the embodiments or the prior art. Obviously, the drawings in the following description are only some embodiments recorded in the present application. For those of ordinary skill in the art, without creative efforts, other drawings can also be obtained based on these drawings.

[0012] Figure 1 It is a schematic diagram of the basic structure of a circulating natural graphite purification fluidized bed continuous purification system provided in a typical embodiment of the present utility model;

[0013] Figure 2 It is a schematic diagram of the basic structure of a circulating natural graphite purification fluidized bed reactor provided in a typical embodiment of the present utility model;

[0014] Figure 3 It is a schematic diagram of a partial structure of a circulating natural graphite purification fluidized bed reactor provided in Embodiment 1 of the present utility model;

[0015] Figure 4 It is a schematic diagram of a partial structure of another circulating natural graphite purification fluidized bed reactor provided in Embodiment 2 of the present utility model. DETAILED DESCRIPTION OF THE EMBODIMENTS

[0016] In view of the deficiencies in the prior art, the inventors of this case have proposed the technical solution of the present utility model through long-term research and a large number of practices. The following will further explain the technical solution, its implementation process, principles, etc.

[0017] An embodiment of the present utility model provides a circulating natural graphite purification fluidized bed reactor, which includes:

[0018] A reactor main body, the reactor main body having a reaction chamber and an intake structure, an outlet structure, a feed structure, and a discharge structure connected to the reaction chamber,

[0019] The first distribution plate structure is arranged in the reaction chamber. The first distribution plate structure is located between the air inlet structure and the air outlet structure. The first distribution plate structure is used to carry solid materials. In addition, the first distribution plate structure also has a breathable structure. The fluidizing gas or reaction gas input from the air inlet structure passes through the breathable structure and contacts and reacts with the solid materials on the first distribution plate structure, and then is led out from the air outlet structure.

[0020] The gas-solid separation module is used to separate the solid materials in the fluidizing gas or reaction gas after reacting with the solid materials, and convey the separated solid materials back to the area of the reaction chamber near the first distribution plate structure.

[0021] Further, the reaction chamber has a gas dispersion zone, a reaction zone and a settling zone that are connected in sequence. The air inlet structure is directly connected to the gas dispersion zone, the air outlet structure is directly connected to the settling zone, the feed structure and the discharge structure are directly connected to the reaction zone. The first distribution plate structure is located between the gas dispersion zone and the reaction zone. Or, the first distribution plate structure is arranged between the gas dispersion zone and the reaction zone and in the dispersion zone. The gas-solid separation module is used to separate and process the gas mixture in the settling zone, convey the separated solid materials back to the reaction zone, and lead out the separated gas from the reaction chamber.

[0022] Further, the area of the radial cross-section of the settling zone is larger than the area of the radial cross-section of the gas dispersion zone.

[0023] Furthermore, the settling zone includes a first settling section and a second settling section arranged in sequence along the direction away from the reaction zone. The area of the radial cross-section of the first settling section gradually increases along the direction away from the reaction zone. The area of the radial cross-section of the second settling section is uniform and the same as the maximum radial cross-section area of the first settling section.

[0024] Further, the air outlet structure is directly connected to the second settling section.

[0025] Further, the reaction zone is a straight cylindrical structure with a uniform radial cross-section area, or the reaction zone is a conical structure with a radial cross-section area gradually increasing along the direction towards the settling zone.

[0026] In a more specific implementation scheme, the gas-solid separation module is arranged inside the reaction chamber. The gas-solid separation module includes a gas-solid separator, an exhaust gas pipeline and a return material pipeline connected to the gas-solid separator. The separator is arranged in the settling zone. The outlet of the exhaust gas pipeline is located outside the reaction chamber. The return material port of the return material pipeline is located in the reaction zone.

[0027] Furthermore, the vertical distance L between the material return port and the bottom of the reaction zone is 0.1H - 1H, preferably 0.2H - 0.8H, and particularly preferably 0.4H - 0.6H, where H is the height of the reaction zone.

[0028] Furthermore, the end section of the material return pipeline is arranged at an angle with the main body section, and the material return port faces the side wall of the reaction zone.

[0029] Furthermore, the angle α formed between the end section and the main body section of the material return pipeline is an obtuse angle.

[0030] Furthermore, the angle α formed between the end section and the main body section of the material return pipeline is 105° - 165°.

[0031] Furthermore, the angle α formed between the end section and the main body section of the material return pipeline is 135° - 150°.

[0032] Furthermore, the minimum distance between the material return port and the side wall of the reaction zone is 0.01D - 0.5D, where D is the inner diameter of the reaction zone.

[0033] Furthermore, the minimum distance between the material return port and the side wall of the reaction zone is 0.05D - 0.4D.

[0034] Furthermore, the minimum distance between the material return port and the side wall of the reaction zone is 0.1D - 0.2D.

[0035] In another more specific embodiment, the gas-solid separation module is arranged outside the reaction chamber. The gas-solid separation module includes a gas-solid separator and is connected to a gas delivery pipe, an exhaust gas pipeline, and a material return pipeline. The gas delivery pipe is communicated with the settling zone, and the material return port of the material return pipeline is communicated with the reaction zone.

[0036] Furthermore, the circulating natural graphite purification fluidized bed reactor further includes: a material return fluidized chamber, which is communicated with the gas-solid separation module and the reaction chamber through the material return pipeline. And a fluidizing gas input port and a second distribution plate structure are provided at the bottom of the material return fluidized chamber. The second distribution plate structure has a breathable structure and covers the fluidizing gas input port. The solid material separated by the gas-solid separation module is first transported into the material return fluidized chamber, reacts with the fluidizing gas, and then is transported back to the reaction zone of the reaction chamber through the material return pipeline.

[0037] Further, the return pipeline includes a first return pipe and a second return pipe. The first return pipe is respectively communicated with the gas-solid separation module and the return fluidization chamber. The second return pipe is respectively communicated with the return fluidization chamber and the reaction zone of the reaction chamber. Wherein, the end section of the first return pipe extends into the interior of the return fluidization chamber, and in the return fluidization chamber, the horizontal height of the position where the end pipe orifice of the first return pipe is located is lower than the horizontal height of the position where the interface between the second return pipe and the return fluidization chamber is located.

[0038] Further, the vertical distance S between the end pipe orifice of the first return pipe and the bottom of the return fluidization chamber is 0.1H′ to 1.0H′, preferably 0.2H′ to 0.8H′, and particularly preferably 0.4H′ to 0.6H′, where H′ is the height of the return fluidization chamber.

[0039] Further, the end section of the first return pipe is arranged at an angle with the main body section, and the end pipe orifice of the first return pipe faces the side wall of the return fluidization chamber.

[0040] Further, the angle β formed by the end section of the first return pipe and the main body section is an obtuse angle.

[0041] Furthermore, the angle β formed by the end section of the first return pipe and the main body section is 105° to 165°.

[0042] Furthermore, the angle β formed by the end section of the first return pipe and the main body section is 135° to 150°.

[0043] Further, the minimum distance R between the end pipe orifice of the first return pipe and the side wall of the return fluidization chamber is 0.01D′ to 0.5D′, where D is the inner diameter of the return fluidization chamber.

[0044] Furthermore, the minimum distance R between the end pipe orifice of the first return pipe and the side wall of the return fluidization chamber is 0.05D′ to 0.4D′.

[0045] Furthermore, the minimum distance R between the end pipe orifice of the first return pipe and the side wall of the return fluidization chamber is 0.1D′ to 0.2D′.

[0046] Further, the second return pipe is integrally arranged obliquely.

[0047] Further, the angle γ between the axis of the second return pipe and the vertical direction is 10° to 90°.

[0048] Furthermore, the angle γ between the axis of the second return pipe and the vertical direction is 15° to 75°.

[0049] Further, the included angle γ between the axial direction of the second return pipe and the vertical direction is 30° to 60°.

[0050] Further, the gas-solid separation module includes a plurality of gas-solid separators, and the plurality of gas-solid separators are connected in series in sequence.

[0051] Further, the gas-solid separator is a cyclone separator.

[0052] The technical solution, its implementation process and principle, etc. will be further explained below in conjunction with the drawings and specific embodiments. Unless otherwise specified, the containers such as the intermediate tank, the feed tank, and the receiving tank, as well as the cooling furnace, the pre-oxidation furnace, the desorption furnace, etc. used in the embodiments of the present invention are all known in the art. The cyclone separator, the metal chloride collector, and the absorption tower used in the embodiments of the present invention are also known in the art. The specific equipment models thereof are not limited herein. The gas supply mechanism and the connection structure between each functional mechanism used in the embodiments of the present invention are all known in the art and are not specifically limited herein.

[0053] Embodiment 1

[0054] Please refer to Figure 1 , a continuous purification system for natural graphite purification fluidized bed, including a reaction unit 200 and a feed unit 100, a receiving unit 300, a gas supply unit, and a tail gas treatment unit 400 that are respectively connected to the reaction unit 200. Among them, the feed unit 100 is used to convey microcrystalline graphite into the reaction unit 200, the gas supply unit is used to input fluidizing gas or reaction gas into the reaction unit 200, the fluidizing gas or reaction gas contacts the microcrystalline graphite in the reaction unit 200, the microcrystalline graphite is purified, and the purified microcrystalline graphite enters the receiving unit 300 for storage. The gas in the reaction unit 200 enters the tail gas treatment unit 400 for purification treatment, and then is discharged or collected.

[0055] Exemplarily, the fluidizing gas or reaction gas may be a mixed gas of inert gases such as nitrogen and argon and halogen gases such as chlorine, hydrogen chloride, and freon. The reaction gas may be halogen gases such as chlorine, hydrogen chloride, and freon. Of course, in addition to natural graphite, the solid material in this embodiment may also be the purification of microcrystalline graphite and its raw materials, as well as other fixed materials, etc. It should be noted that the solid material is in granular form.

[0056] In this embodiment, the reaction unit 200 includes a fluidized bed reactor, and the fluidized bed reactor is used to purify natural graphite (it can be understood that this purification process is realized by the participation of the fluidizing gas or reaction gas provided by the gas supply unit).

[0057] Please refer to together Figure 2In this embodiment, the fluidized bed reactor includes a reactor body and a distribution plate structure. The reactor body has a reaction chamber inside. The reaction chamber has a gas dispersion zone 213, a reaction zone 212 and a settling zone 211 which are connected in sequence. The reactor body is also provided with an air intake structure 214, an air outlet structure 215, a feed structure 216 and a discharge structure 217. The air intake structure 214 is directly connected to the gas dispersion zone 213, the air outlet structure 215 is directly connected to the settling zone 211, the feed structure 216 and the discharge structure 217 are directly connected to the reaction zone 212, and the feed unit 100, the receiving unit 300, the gas supply unit and the tail gas treatment unit 400 are respectively connected to the feed structure 216, the discharge structure 217, the air intake structure 214 and the air outlet structure 215 of the reactor body;

[0058] The distribution plate structure is arranged in the reaction chamber, and the distribution plate structure is located between the gas dispersion zone 213 and the reaction zone 212. The distribution plate structure is at least used to carry fixed materials, and the distribution plate structure also has a breathable structure for gas to pass through. The fluidizing gas or reaction gas input from the air inlet structure passes through the breathable structure and contacts and reacts with the solid material on the distribution plate structure, and then is discharged from the air outlet structure; it should be noted that the air inlet structure 214, the air outlet structure 215, the feed structure 216 and the discharge structure 217 are all equipped with switchable valves. Of course, these valves can also be set on the connecting pipelines between the feed unit 100, the receiving unit 300, the gas supply unit, the tail gas treatment unit 400 and the feed structure 216, the discharge structure 217, the air inlet structure 214, and the air outlet structure 215.

[0059] In this embodiment, the reaction zone 212 is a straight cylindrical structure with a uniform radial cross-sectional area or the reaction zone 212 is a tapered structure with a radial cross-sectional area gradually increasing in the direction of the settling zone 211. The straight cylindrical structure can provide a larger volume of effective reaction zone 212, and the tapered structure can increase the flow rate of the fluidizing gas or the reaction gas in the reaction zone 212, reduce the dead zone, and improve the purification effect. In this embodiment, the settling zone 211 includes a first settling section and a second settling section arranged in sequence away from the reaction zone 212. The area of ​​the radial cross section of the first settling section gradually increases in the direction away from the reaction zone 212. The area of ​​the radial cross section of the second settling section is uniform and is the same as the maximum radial cross-sectional area of ​​the first settling section. Through such a design, the fine powder in the fluidizing gas or the reaction gas after the reaction can be fully settled.

[0060] In a relatively typical embodiment, the distribution plate structure includes m distribution plates having a breathable structure. The m distribution plates are sequentially arranged at intervals along the direction from the gas dispersion zone to the sedimentation zone. The m distribution plates divide the reaction zone into m interconnected reaction spaces. Among them, the first distribution plate is located between the gas dispersion zone and the reaction zone and isolates the gas dispersion zone from the reaction zone. m≥2. Among them, there is a gap between the second to the mth distribution plates and the side wall of the reaction chamber. The adjacent reaction spaces are directly communicated through the gap between the distribution plate and the side wall of the reaction chamber. The gaps between the second to the mth distribution plates and the side wall of the reaction chamber are communicated to form a channel through which both solid materials and gas can pass. Moreover, baffles are provided on the second to the mth distribution plates. The baffles are arranged at an angle with the distribution plates. A receiving space for accommodating solid materials is formed by enclosing between the baffles and the distribution plates. By arranging m distribution plates to divide the reaction zone into multiple receiving spaces, the residence time of the fluidizing gas or reaction gas in the reaction zone can be increased, thereby improving the purification effect. At the same time, the m distribution plates divide the reaction zone into multiple receiving spaces, and the height of each receiving space where the purification reaction can occur is also reduced. The low bed height further improves the stable occurrence of the fluidization reaction. It can be understood that the multiple distribution plates except the first distribution plate are arranged staggered along the direction from the gas dispersion zone to the sedimentation zone.

[0061] In this embodiment, please refer to again Figure 1 , the feeding unit 100 may include at least one intermediate tank 110 and at least one feeding tank 120 connected in series in sequence. The feeding tank 120 is directly connected to the feeding structure 216 of the fluidized bed reactor. The receiving unit 300 includes at least one receiving tank 310. The receiving tank 310 is connected to the discharging structure 217 of the fluidized bed reactor. The gas supply unit may include a fluidizing gas or reaction gas storage tank and a gas pump. The fluidizing gas or reaction gas storage tank is connected to the fluidized bed reactor through the gas pump. The pressure and flow rate of the fluidizing gas or reaction gas can be adjusted through the gas pump.

[0062] In this embodiment, before the purification treatment, the discharge structure 217 of the reactor main body is closed, and the feed structure 216, the gas inlet structure 214, and the gas outlet structure 215 are opened. The fluidizing gas or reaction gas enters the gas dispersion zone 213 of the reactor through the gas inlet structure 214, and the solid material enters the reaction zone 212 of the reactor from the feed unit 100 through the feed structure 216 and presents a fluidized boiling state under the action of the fluidizing gas or reaction gas (if the flow rate of the fluidizing gas or reaction gas is small, the solid material will accumulate on the distribution plate; if the flow rate of the fluidizing gas or reaction gas reaches the predetermined requirement, the solid material will present a fluidized boiling state). After the feeding is completed, the feed structure 216 is closed, and the fluidizing gas or reaction gas contacts the solid material to realize the purification treatment of the solid material. The fluidizing gas or reaction gas participating in the purification treatment will have a reduced flow rate after reaching the settling zone, and is collected by the first cyclone separator 220 for gas-solid separation. The separated solid material will be sent back to the reaction zone again, and the separated gas enters the tail gas treatment unit 400 for purification treatment. The solid material after the purification treatment enters the material receiving unit 300 through the discharge structure 217, thereby completing the purification of the solid material.

[0063] Please refer to Figure 3 , a continuous purification system for natural graphite purification fluidized bed in this embodiment further includes a gas-solid separation module 500. The gas-solid separation module 500 separates and processes the fluidizing gas or reaction gas that has reacted with the solid material in the settling zone 211 inside the reactor main body to separate the solid material therein, and conveys the separated solid material back to the reaction zone 212 of the reaction chamber.

[0064] In this embodiment, please refer to Figure 3 , the gas-solid separation module 500 is arranged inside the reaction chamber. The gas-solid separation module 500 includes two gas-solid separators 510, a exhaust gas pipeline 520, and two return pipelines 530. The two gas-solid separators 510 are arranged in series in the settling zone. The exhaust gas pipeline 520 is connected to one of the gas-solid separators 510, and the outlet of the exhaust gas pipeline 520 is located outside the reaction chamber. Each return pipeline 530 is connected to a gas-solid separator 510. The return pipeline 530 extends vertically as a whole, and the return port at the end of the return pipeline 530 is located in the reaction zone 212.

[0065] In this embodiment, the end section of the return pipeline 530 is arranged at an angle with the main body section to prevent the material in the reaction zone 212 from flowing back along the return pipeline 530. Moreover, the return port faces the side wall of the reaction zone 212. Specifically, the angle α formed between the end section and the main body section of the return pipeline 530 is an obtuse angle, preferably 105° - 165°, and particularly preferably 135° - 150°. If the angle α is too large, the upward airflow in the reaction zone will hinder the feeding of the return pipeline 530, and there is a risk of flowing back into the gas-solid separator. If the angle α is too small, the material in the return pipeline 530 is likely to be blocked at the turning point.

[0066] In this embodiment, the minimum distance between the return port and the side wall of the reaction zone 212 close to it is 0.01D - 0.5D, preferably 0.05D - 0.4D, and particularly preferably 0.1D - 0.2D, where D is the inner diameter of the reaction zone. Based on such a design, it can not only prevent the central upward airflow and material in the reaction chamber from hindering the feeding of the return pipeline 530 and flowing back into the gas-solid separator, but also avoid the material returned by the return pipeline 530 from hitting the inner wall.

[0067] In this embodiment, the distance L between the return port of the return pipeline 530 and the bottom of the reaction zone 212 is 0.1H - 1.0H, preferably 0.2H - 0.8H, and more preferably 0.4H - 0.6H, where H is the height of the reaction zone. Due to such a design, it can prevent the solid material returned from the return pipeline 530 from being blown away by the airflow and being secondarily entrained into the settling zone, and avoid the solid material returned from the return pipeline 530 being affected by the fluctuations of the bed material and the airflow, thereby improving the discharging smoothness of the return pipeline.

[0068] It should be noted that the structures and structural parameters set in the two return pipelines 530 in the embodiments of the present invention can be the same, and the structures of the two gas-solid separators can also be the same.

[0069] Embodiment 2

[0070] The structure of the main part of a natural graphite purification fluidized bed continuous purification system in this embodiment is basically the same as that in Embodiment 1, and the same parts of the two will not be elaborated here.

[0071] In this embodiment, please refer to Figure 4, the gas-solid separation module is arranged outside the reaction chamber. The gas-solid separation module includes two gas-solid separators 510, a gas delivery pipe 550, an exhaust gas pipeline 520, two return pipelines 530, and a return material fluidization chamber 540. The gas delivery pipe 550 is communicated with the settling zone 211. The return pipeline 530 is connected to the reaction zone 212 through the return material fluidization chamber 540. The solid material obtained by separation in the gas-solid separator 510 first enters the return material fluidization chamber 540, and after being re-reacted with the fluidizing gas in the return material fluidization chamber 540, it returns to the settling zone 211.

[0072] In this embodiment, a fluidizing gas inlet and a distribution plate structure are further arranged at the bottom of the return material fluidization chamber. The distribution plate structure has a breathable structure, and the distribution plate structure covers the fluidizing gas inlet. The solid material separated by the gas-solid separation module is first transported into the return material fluidization chamber, reacts with the fluidizing gas, and then is transported back to the reaction zone of the reaction chamber through the return pipeline. The distribution plate structure can be the same as the distribution plate structure in the reaction chamber, and will not be elaborated here.

[0073] In this embodiment, please further refer to Figure 4 , the return pipeline 530 includes a first return pipe 531 and a second return pipe 532. The first return pipe 531 is respectively connected to the gas-solid separator 510 and the return material fluidization chamber 540. The second return pipe 532 is respectively connected to the return material fluidization chamber 540 and the reaction zone 212 of the reaction chamber. Among them, the end section of the first return pipe 531 extends into the interior of the return material fluidization chamber 540, and in the return material fluidization chamber 540, the horizontal height of the end pipe orifice of the first return pipe 531 is lower than the horizontal height of the interface between the second return pipe 532 and the return material fluidization chamber 540.

[0074] In this embodiment, the vertical distance S between the end pipe orifice of the first return pipe 531 and the bottom of the return material fluidization chamber is 0.1H' to 1.0H', preferably 0.2H' to 0.8H', and particularly preferably 0.4H' to 0.6H', where H' is the height of the return material fluidization chamber. By such design, it can be avoided that the solid material output from the first return pipe 531 is blown away by the air flow and returns to the gas-solid separator 510, and it can be avoided that the solid material output from the first return pipe 531 is affected by the fluctuations of the bed material and the air flow, thereby improving the discharging smoothness of the solid material output from the first return pipe 531.

[0075] In this embodiment, the end section of the first return pipe 531 is arranged at an angle with the main body section, and the end opening of the first return pipe 531 faces the side wall of the return fluidization chamber 540. The angle β between the end section and the main body section of the first return pipe 531 is an obtuse angle, preferably 105° to 165°, and particularly preferably 135° to 150°. Based on such a setting, it is possible to avoid the upward airflow in the return fluidization chamber 540 from hindering the feeding of the first return pipe 531, avoid the risk of the material flowing back into the gas-solid separator 510, and at the same time, avoid the blockage of the material in the first return pipe 531.

[0076] In this embodiment, the minimum distance R between the end opening of the first return pipe 531 and the side wall of the return fluidization chamber 540 is 0.01D' to 0.5D′, preferably 0.05D' to 0.4D′, and particularly preferably 0.1D′ to 0.2D′, where D′ is the inner diameter of the return fluidization chamber 540. Based on such a design, it is possible to avoid the central upward airflow and the material in the return fluidization chamber 540 from hindering the feeding of the first return pipe 531 and the risk of the upward airflow and the material flowing back into the gas-solid separator, and at the same time, avoid the material returned by the first return pipe 531 from hitting the inner wall.

[0077] In this embodiment, the second return pipe 532 is integrally inclined, and the angle γ between the axial direction of the second return pipe 532 and the vertical direction is 10° to 90°, preferably 15° to 75°, and particularly preferably 30° to 60°. Based on such a design, it is possible to avoid the deposition of the material in the second return pipe 532 and blockage of the second return pipe 532, and ensure the stable discharging of the second return pipe 532.

[0078] A cyclic natural graphite purification fluidized bed reactor provided by an embodiment of the present invention can further process the gas after the purification reaction and separate the solid material therein, which not only improves the yield of the purified solid material but also reduces the burden on the downstream tail gas treatment system.

[0079] It should be understood that the above embodiments are only used to illustrate the technical concept and characteristics of the present invention, and their purpose is to enable those skilled in the art to understand the content of the present invention and implement it accordingly, and cannot be used to limit the protection scope of the present invention. Any equivalent changes or modifications made according to the spirit of the present invention should be covered within the protection scope of the present invention.

Claims

1. A cyclic natural graphite purification fluidized bed reactor, characterized in that, Comprising: A reactor main body having a reaction chamber, and an intake structure, an outlet structure, a feed structure, and a discharge structure that communicate with the reaction chamber; A first distribution plate structure disposed in the reaction chamber, between the intake structure and the outlet structure, for carrying solid materials, and having a gas-permeable structure through which fluidizing gas or reaction gas input from the intake structure passes and contacts the solid materials on the first distribution plate structure for reaction, and then is discharged from the outlet structure; A gas-solid separation module for separating solid materials from the fluidizing gas or reaction gas after reaction with the solid materials and conveying the separated solid materials back to the area of the reaction chamber near the first distribution plate structure.

2. The circulating natural graphite purification fluidized bed reactor according to claim 1, wherein: The reaction chamber has a gas dispersion zone, a reaction zone, and a settling zone that are sequentially connected. The intake structure is directly connected to the gas dispersion zone, the outlet structure is directly connected to the settling zone, the feed structure and the discharge structure are directly connected to the reaction zone, the first distribution plate structure is located between the gas dispersion zone and the reaction zone, or the first distribution plate structure is disposed between the gas dispersion zone and the reaction zone and in the dispersion zone. The gas-solid separation module is used to separate and process the gas mixture in the settling zone, convey the separated solid materials back to the reaction zone, and discharge the separated gas from the reaction chamber.

3. The circulating natural graphite purification fluidized bed reactor according to claim 2, wherein: The gas-solid separation module is disposed inside the reaction chamber and includes a gas-solid separator, an exhaust gas pipeline, and a return material pipeline connected to the gas-solid separator. The separator is disposed in the settling zone, the outlet of the exhaust gas pipeline is located outside the reaction chamber, and the return material port of the return material pipeline is located in the reaction zone.

4. The circulating natural graphite purification fluidized bed reactor according to claim 3, characterized in that: The vertical distance L between the return material port and the bottom of the reaction zone is 0.1H - 1.0H, where H is the height of the reaction zone; And / or, the vertical distance L between the return material port and the bottom of the reaction zone is 0.2H - 0.8H; And / or, the vertical distance L between the return material port and the bottom of the reaction zone is 0.4H - 0.6H.

5. The circulating natural graphite purification fluidized bed reactor according to claim 3 or 4, characterized in that: The end section of the return material pipeline is arranged at an angle with the main section, and the return material port faces the side wall of the reaction zone; And / or, the angle α formed by the end section and the main section of the return material pipeline is an obtuse angle; And / or, the angle α formed by the end section and the main section of the return material pipeline is 105° - 165°; And / or, the angle α formed by the end section and the main section of the return material pipeline is 135° - 150°; And / or, the minimum distance between the return material port and the side wall of the reaction zone is 0.01D - 0.5D, where D is the inner diameter of the reaction zone; And / or, the minimum distance between the return material port and the side wall of the reaction zone is 0.05D - 0.4D; And / or, the minimum distance between the return material port and the side wall of the reaction zone is 0.1D - 0.2D.

6. The circulating natural graphite purification fluidized bed reactor according to claim 2, characterized in that: The gas-solid separation module is arranged outside the reaction chamber. The gas-solid separation module includes a gas-solid separator, and is connected to a gas delivery pipe, an exhaust pipe, and a return pipe. The gas delivery pipe communicates with the settling zone, and the return port of the return pipe communicates with the reaction zone of the reaction chamber.

7. The cyclic natural graphite purification fluidized bed reactor according to claim 6, characterized in that, It further includes: A return material fluidization chamber, which is communicated with the gas-solid separation module and the reaction chamber through the return pipe. Moreover, a fluidizing gas inlet and a second distribution plate structure are provided at the bottom of the return material fluidization chamber. The second distribution plate structure has a breathable structure, and the second distribution plate structure covers the fluidizing gas inlet. The solid material separated by the gas-solid separation module is first transported into the return material fluidization chamber, reacts with the fluidizing gas, and then is transported back to the reaction zone of the reaction chamber through the return pipe.

8. The circulating natural graphite purification fluidized bed reactor according to claim 7, characterized in that: The return pipe includes a first return pipe and a second return pipe. The first return pipe is respectively communicated with the gas-solid separation module and the return material fluidization chamber. The second return pipe is respectively connected to the return material fluidization chamber and the reaction zone of the reaction chamber. Among them, the end section of the first return pipe extends into the interior of the return material fluidization chamber, and in the return material fluidization chamber, the horizontal height of the end pipe orifice of the first return pipe is lower than the horizontal height of the interface between the second return pipe and the return material fluidization chamber. And / or, the vertical distance S between the end pipe orifice of the first return pipe and the bottom of the return material fluidization chamber is 0.1H′ to 1.0H′, where H′ is the height of the return material fluidization chamber. And / or, the vertical distance S between the end pipe orifice of the first return pipe and the bottom of the return material fluidization chamber is 0.2H′ to 0.8H′. And / or, the vertical distance S between the end pipe orifice of the first return pipe and the bottom of the return material fluidization chamber is 0.4H′ to 0.6H′.

9. The circulating natural graphite purification fluidized bed reactor according to claim 8, characterized in that: The end section of the first return pipe is arranged at an angle with the main body section, and the end pipe orifice of the first return pipe faces the side wall of the return material fluidization chamber. And / or, the angle β formed by the end section of the first return pipe and the main body section is an obtuse angle. And / or, the angle β formed by the end section of the first return pipe and the main body section is 105° to 165°. And / or, the angle β formed by the end section of the first return pipe and the main body section is 135° to 150°. And / or, the minimum distance R between the end pipe orifice of the first return pipe and the side wall of the return material fluidization chamber is 0.01D′ to 0.5D′, where D is the inner diameter of the return material fluidization chamber. And / or, the minimum distance R between the end pipe orifice of the first return pipe and the side wall of the return material fluidization chamber is 0.05D′ to 0.4D′. And / or, the minimum distance R between the end pipe orifice of the first return pipe and the side wall of the return material fluidization chamber is 0.1D'N0.2D′. And / or, the second return pipe is integrally inclined. And / or, the angle γ between the axis of the second return pipe and the vertical direction is 10° to 90°. And / or, the included angle γ between the axial direction of the second return pipe and the vertical direction is 15° to 75°; And / or, the included angle γ between the axial direction of the second return pipe and the vertical direction is 30° to 60°.

10. The circulating natural graphite purification fluidized bed reactor according to claim 3 or 4 or 6 or 7 or 8 or 9, characterized in that: The gas-solid separation module includes a plurality of gas-solid separators, and the plurality of gas-solid separators are connected in series in sequence; And / or, the gas-solid separator is a cyclone separator.

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