Reactor suitable for solid materials

Abstract

The utility model discloses a reactor suitable for solid materials, and belongs to the technical field of chemical engineering, the reactor comprises a tank body used for material mixing, a stirring device is arranged in the tank body, the stirring device comprises a rotating shaft and paddles, the paddles are arranged outside the rotating shaft in a sleeving mode, the rotating shaft extends in the axial direction of the tank body, and the rotating shaft can drive the paddles to rotate; the paddle comprises a central disc which is coaxial with the rotating shaft and a plurality of blades which are arranged on the outer side of the central disc at intervals; the blades are connected with an annular disc, and the annular disc and the central disc are coaxially arranged. The reactor disclosed by the utility model is high in dispersing capacity, suitable for gas dispersion, solid suspension, heat transfer and gas-liquid-solid heterogeneous reaction operations with high strength requirements, and capable of effectively preventing solid materials from depositing at the bottom of the reactor.

Description

Technical Field

[0001] The present disclosure belongs to the technical field of chemical engineering, and particularly relates to a reactor suitable for solid materials. Background Art

[0002] In the process of modern chemical production, most reactions require corresponding catalysts, such as petrochemical, fine chemical, biochemical, environmental protection, etc. Existing reactors using solid catalysts include a tank body and a stirring device arranged in the tank body. The stirring devices mainly include a paddle stirring device and a turbine stirring device. When using solid catalysts (including immobilized biocatalysts, acids, bases, salts and other solid catalysts) as catalysts, there are some deficiencies in simply using traditional reactors. Not only is it extremely inconvenient to recover the catalyst, but also the density of the solid catalyst is greater than that of water, and it is easy to deposit at the bottom of the reactor, resulting in an unsatisfactory longitudinal mass transfer situation of the reaction liquid, insufficient contact between the reaction substrate and the catalyst, and affecting the conversion rate.

[0003] The invention with the publication number CN101927144B relates to a reactor for catalytic production of biodiesel using a solid catalyst. The reactor includes a stirring kettle, a filter, a circulation pump, a methanol storage tank and a discharge pump. The filter is placed at the bottom of the stirring kettle, the outlet of the filter is connected to the inlet of the circulation pump, the outlet of the circulation pump is connected to the feed inlet of the stirring kettle, the discharge pump is connected to the outlet of the circulation pump through a pipeline with a control valve, and the methanol storage tank is directly connected to the feed inlet of the stirring kettle or connected to the inlet of the circulation pump. This invention has the advantages of convenient recovery of solid catalysts, improved service life of catalysts, and reduced costs.

[0004] However, existing reactors using solid catalysts still cannot ensure high-intensity gas dispersion, solid suspension, and have poor heat transfer effect, and have poor mixing effect in gas-liquid-solid heterogeneous reactions, resulting in reduced efficiency of the catalyst and further affecting the reaction efficiency. Summary of the Utility Model

[0005] The purpose of the present disclosure is to provide a reactor suitable for solid materials with a simple structure and easy operation, which is suitable for solid-liquid mixing reactions, has strong dispersion ability, and can also achieve mass transfer of gas, liquid and solid, helping to improve the reaction effect.

[0006] The technical solution adopted by the present disclosure to achieve the above purpose is as follows:

[0007] A reactor applicable to solid materials includes a tank for material mixing. A stirring device is configured inside the tank. The stirring device includes a rotating shaft and blades. The blades are sleeved outside the rotating shaft. The rotating shaft extends along the axial direction of the tank, and the rotating shaft can drive the blades to rotate synchronously. The blades include a central disk coaxially arranged with the rotating shaft and a plurality of blades spaced outside the central disk. And an annular disk is connected to the inner sides of the plurality of blades. The annular disk is coaxially arranged with the central disk.

[0008] Preferably, the annular disk is arranged between the end face of the central disk and the ends of the blades.

[0009] Preferably, a plurality of the annular disks are arranged on the same side of the central disk, and the diameters of the plurality of annular disks arranged in the direction away from the central disk increase in sequence.

[0010] Preferably, the annular disk is of an annular plate-like structure or a trumpet-shaped diffusion structure.

[0011] Preferably, the two ends of the blades are respectively arranged on both sides of the central disk. The blades are of a straight blade type, an inclined blade type or a curved blade type, and the plurality of blades are arranged in a circumferential array.

[0012] Preferably, a first baffle is symmetrically configured inside the tank. The first baffle is provided with a first hole body, and the first baffle is arranged in contact with the inner wall of the tank.

[0013] Preferably, the length direction of the first baffle extends along the axial direction of the tank. And the width direction of the first baffle extends along the radial direction of the tank or along the tangential direction of the cross-section of the tank.

[0014] Preferably, the tank includes a top plate and a bottom plate, and a feed port is provided on the bottom plate of the tank.

[0015] Preferably, a second baffle is configured at one or both of the top and bottom of the tank. The second baffle is provided with a second hole body, and the outer side of the second baffle is arranged in contact with the inner wall of the tank.

[0016] Preferably, when the first baffle extends along the tangential direction of the cross-section of the tank, the width of the first baffle is 0.5 to 0.75 times the inner diameter of the tank.

[0017] Therefore, the reactor applicable to solid materials of the present disclosure is particularly applicable to heterogeneous reactions, has the characteristic of strong dispersion ability, can realize gas dispersion and solid suspension, and is therefore particularly applicable to solid-liquid mixing reactions, and more particularly applicable to gas-liquid-solid three-phase heterogeneous reactions. Description of the Drawings

[0018] Figure 1 Schematic structural diagram of a reactor applicable to solid materials according to the first embodiment of the present disclosure;

[0019] Figure 2 Schematic structural diagram of a straight - blade impeller according to the first embodiment of the present disclosure;

[0020] Figure 3 Schematic structural diagram of an inclined - blade impeller according to the first embodiment of the present disclosure;

[0021] Figure 4 Schematic structural diagram of an arc - blade impeller according to the first embodiment of the present disclosure;

[0022] Figure 5 Schematic structural diagram of the cooperation between a straight - blade impeller and an annular disc according to the first embodiment of the present disclosure;

[0023] Figure 6 Another schematic structural diagram of the cooperation between a straight - blade impeller and an annular disc according to the first embodiment of the present disclosure;

[0024] Figure 7 Schematic structural diagram of a reactor applicable to solid materials according to the second embodiment of the present disclosure;

[0025] Figure 8 Schematic diagram of the fluid circulation flow direction in the longitudinal sectional view of the reactor according to the second embodiment of the present disclosure;

[0026] Figure 9 Schematic structural diagram of a reactor applicable to solid materials according to the third embodiment of the present disclosure.

[0027] Reference numerals in the drawings: tank body 10; feed inlet 11; rotating shaft 12; impeller 13; central disc 14; blade 15; annular disc 16; first baffle 17; second baffle 18. Detailed implementation manners

[0028] The present disclosure provides a reactor. By arranging a stirring device with blade and disc structures and an optional porous baffle structure in the cavity of the reactor, different fluid flow circulations can be formed in the upper and lower cavities of the stirring blade when stirring the reaction materials, so as to efficiently achieve the full mixing of solid, liquid and gas raw materials.

[0029] The reactor according to the present disclosure includes a tank body, a stirring device disposed inside the tank body, and an optional baffle structure.

[0030] The above - mentioned tank body may include a top plate, a bottom plate and a main body. Preferably, the top plate may have an arc - shaped structure, the bottom plate is a plate - shaped structure, and the main body may be a cylindrical structure. According to one embodiment, the bottom plate may have a feed inlet.

[0031] The above-mentioned stirring device may include a rotating shaft and blades, wherein the blades are sleeved outside the rotating shaft, the rotating shaft extends along the axial direction of the tank body, and the rotating shaft can drive the blades to rotate synchronously. The blades may include a central disk coaxially arranged with the rotating shaft, and a plurality of blades spaced apart on the outer side of the central disk. An annular disk may also be connected to the inner sides of the plurality of blades, and the annular disk is coaxially arranged with the central disk.

[0032] Preferably, in the reactor of the present disclosure, the blades of the stirring device may adopt straight blades or curved disk turbine blades, and may be set as radial flow type blades. In the embodiments of the present disclosure, the two ends of the blade are respectively arranged on both sides in the vertical direction of the central disk, that is, the central disk is located at the middle position in the vertical direction of the blade. Specifically, the blade may be a straight blade type, an inclined blade type, a curved blade type or an arc blade type. The above-mentioned plurality of blades may be arranged in a circumferential array, and adjacent blades are spaced apart along the circumference.

[0033] The above-mentioned annular disk is arranged between the radial outer end face of the central disk and the end of the blade. And the annular disk may be arranged on the upper side of the central disk or dispersedly arranged on the upper and lower sides of the central disk.

[0034] Furthermore, when there are a plurality of annular disks arranged on the same side of the central disk, the diameters of the plurality of annular disks may be the same or may increase sequentially along the axial direction away from the central disk. The annular disk may be an annular plate-like structure or a trumpet-shaped diffused structure.

[0035] According to an embodiment of the present disclosure, the inner wall of the tank body is provided with a first baffle, and the first baffle is provided with a plurality of through holes. And the length direction of the first baffle extends along the axial direction of the tank body, and the width direction of the first baffle extends along the radial direction of the tank body. Furthermore, the radial edge of the first baffle is at a certain distance from the end of the blade.

[0036] According to an embodiment of the present disclosure, the top or bottom of the tank body is provided with a second baffle having a plurality of holes, and the outer edge of the second baffle is attached to the inner wall of the tank body. Furthermore, the second baffle is arranged at a certain distance from the top plate and / or the bottom plate, for example, arranged near the head.

[0037] According to a specific embodiment of the present disclosure, a feed port is provided at the bottom of the tank body for feeding solid materials between the bottom plate and the second baffle. And the second baffle can prevent the solid materials in the tank body from depositing at the bottom during the stirring process.

[0038] The technical solutions of the present disclosure will be further described in detail below in conjunction with specific embodiments and the drawings. It should be understood that the specific embodiments described herein are only used to explain the present disclosure and are not used to limit the present disclosure.

[0039] See Figures 1 to 6, a reactor suitable for solid materials according to the first specific embodiment of the present disclosure includes a tank body 10 for material mixing. For example, the tank body can be cylindrical. The reactor of the present disclosure is particularly suitable for mixing reaction material systems containing solid materials, such as solid catalysts, and is particularly suitable for mixing heterogeneous systems of solid-liquid-gas. The tank body 10 includes a top and a bottom, and a stirring device is provided inside the cavity defined by the tank body 10. A feed inlet 11 for conveying materials into the tank body 10 is provided at the bottom of the tank body 10. According to needs, solid materials, such as solid catalysts, can be filled into the tank body 10 synchronously with the reactants, or can be filled separately. In the tank body 10 of this embodiment, the solid materials can be fed from the bottom, and the gas and / or liquid materials can be fed from the top. Cooperating with the high-speed rotating stirring device, it can promote the floating of the solid materials, promote the full contact of the entire reactant system with the solid catalyst, and help improve the reaction efficiency. According to a preferred embodiment, the feed inlet 11 is concentrically arranged with the tank body 10, and the inner diameter of the feed inlet 11 can be 0.2 to 0.4 times the inner diameter of the tank body 10, for example, 0.3 times.

[0040] Specifically, the above-mentioned stirring device may include a rotating shaft 12 and paddle blades 13. The paddle blades 13 are sleeved outside the rotating shaft 12. One end of the rotating shaft 12 passes through the top plate of the tank body 10 and cooperates with a motor provided outside the tank body 10, preferably a servo motor, and this motor can drive the rotating shaft 12 to rotate. The other end of the rotating shaft 12 extends into the cavity of the tank body 10. The rotating shaft 12 extends along the axial direction of the tank body 10. According to needs, one or a plurality of spaced paddle blades 13 can be provided on the rotating shaft 12, and the rotating shaft 12 can drive the paddle blades 13 to rotate synchronously. The paddle blades 13 can be straight blades or curved disk turbine blades and are set as radial flow type paddle blades 13.

[0041] The above-mentioned stirring device may further include a central disk 14 coaxially arranged with the rotating shaft 12. A plurality of blades 15 are provided on the outside of the central disk 14; the two ends of the blades 15 are respectively arranged on both sides of the central disk 14; the blades 15 are straight blade type, inclined blade type, curved blade type or arc blade type, and a plurality of blades 15 can be arranged in a circumferential array, preferably, these blades are symmetrically arranged, preferably symmetrically arranged along the axis.

[0042] According to a specific embodiment, the diameter of the central disk 14 can be 0.2 to 0.5 times the inner diameter of the tank body 10, preferably 0.4 times. The radial width of the blades 15 can be 0.1 to 0.3 times the inner diameter of the tank body 10, preferably 0.2 times. More preferably, the total radial width of the central disk 14 and the blades 15 (that is, the distance between the center axis and the outside of the blades 15) can be 0.5 to 0.75 times the inner diameter of the tank body 10, preferably 0.55 to 0.7 times, for example, 0.6 times.

[0043] During the rotation of the central disk 14 and the rotating shaft 12, a centrifugal force is provided to the surrounding materials, which can drive the surrounding materials to transfer to the side of the tank body 10, thereby expanding the diffusion space of the materials, increasing the contact probability between the materials, especially ensuring the catalytic efficiency of the catalyst, and increasing the reverse rate. The blades 15 provide a high shear force to the materials in the tank body, promoting the uniform mixing of materials in different phases.

[0044] The central disk 14 can effectively prevent the rising bubbles from escaping quickly, playing a role in sealing the large bubbles. During the rotation of the stirring device, the bubbles collide with each other and can achieve the effect of dispersing the materials, that is, it can promote the contact of the materials, thereby promoting the heat transfer between the materials in different states (such as gaseous, liquid and solid), and can also promote the increase of the reaction rate. The multiple blades 15 arranged in a circumferential array can provide sufficient shear force to make the bubbles and the solid and / or liquid materials contact the blades 15, which helps to promote the fragmentation and dispersion of the bubbles, not only promoting the mixing of the materials, but also contributing to the mass transfer between the gas phase, liquid phase and solid phase.

[0045] Further, an annular disk 16 is connected to the inner side of the blade 15, and the annular disk 16 is coaxially arranged with the central disk 14. In the radial direction, the side close to the center axis is the inner side, and the side far from the center axis is the outer side. The annular disk 16 is arranged between the outer end face of the central disk 14 and the inner end of the blade 15. The annular disk 16 can be arranged on one side of the central disk 14 or dispersedly arranged on both sides of the central disk 14. The annular disk 16 is of an annular plate-shaped structure or a trumpet-shaped diffused structure. When multiple annular disks 16 are arranged on the same side of the central disk 14, the diameters of the multiple annular disks 16 increase in sequence along the direction away from the central disk 14.

[0046] The total height of the tank body is the height from the top plate to the bottom plate of the tank body. The distance between the bottom surface of the central disk 14 and the bottom plate of the tank body can be 0.2 - 0.4 times the height of the tank body, preferably 0.3 - 0.4 times, such as 0.35 times. The height of the blade 15 in the vertical direction can be 0.05 - 0.2 times the height of the tank body, preferably 0.08 - 0.15 times, such as 0.1 times. The outer diameter of the annular disk 16 can be less than or equal to the outer diameter of the central disk 14, and the inner diameter of the annular disk 16 can be 200 mm to the inlet diameter. When multiple annular disks 16 are arranged on the same side of the central disk 14, the vertical distance between adjacent annular disks 16 (the distance between the planes where the inner rings of adjacent annular disks 16 are located) can be 0.01 - 0.1 times the height of the tank body, preferably 0.03 - 0.08 times, such as 0.05 times.

[0047] The annular disc 16 cooperates with the blade 15 to provide shear forces at multiple angles for the stirring device, thus helping to improve the mixing effect of bubbles and materials. The annular disc 16 is arranged as a flat annular structure, which can horizontally cut the materials and bubbles during rotation, and the surface of the annular disc 16 can, to a certain extent, guide and change the diffusion directions of the materials and bubbles, helping to promote the mixing of the materials. Moreover, an included angle is formed between the plane where the annular disc 16 is located and the blade 15, so that the materials and bubbles divided and guided by the annular disc 16 are cut, dispersed and guided again, so that the uncontrollability of the flow direction of the materials after leaving the stirring device is enhanced, that is, the diffusion range of the materials can be further expanded, thereby increasing the contact probability between the catalyst and the reactants and improving the catalytic efficiency and reaction rate.

[0048] The included angle between the annular disc 16 and the blade 15 is defined as the included angle between the vertical axis of the edge of the blade and the tangent line of the inclined plane of the annular disc. This included angle can be below 45°, preferably 5° - 45°, more preferably 15° - 40°, and can be, for example, 20°, 25°, 30°, 35°. Further, the extension line of the edge of the annular disc 16 passes through the midpoint of the connection line of the two vertices of the blade 15, that is, the extension line of the edge of the annular disc 16 intersects the connection line of the two vertices of the blade 15 at the midpoint of the vertex connection line of the blade 15.

[0049] According to an embodiment, the annular disc 16 is arranged in a trumpet shape, thus forming an outward-expanding structure in the outer direction of the central disc 14. In addition to being able to exert and strengthen the cutting, guiding and dispersing effects of the flat annular structure on the materials and bubbles, it also helps to strengthen the suction effect of the stirring device on the materials at the bottom of the tank body 10. Especially when trumpet-shaped annular discs 16 are respectively arranged on the upper and lower sides of the central disc 14, a Venturi tube-like structure is formed inside the stirring device, which helps to suck the materials from the bottom of the tank body 10 during the rotation of the stirring device and spray the part of the materials from the middle of the tank body 10 to the top of the tank body 10. In this way, the materials at the bottom of the tank body 10 float up, which helps the suspension of solid material (such as catalyst) particles, thus avoiding or reducing the deposition of solid materials at the bottom of the tank body 10 and improving the utilization rate of the catalyst.

[0050] When the reactor of this embodiment is used for reactions with solid materials, especially solid particulate catalysts, the stirring intensity of the above-mentioned stirring device is relatively strong, ensuring the breaking and dispersion of bubbles in the reaction system, which is conducive to mass transfer between the gas-liquid-solid phases; it can avoid the problem of solid catalyst accumulation at the bottom during the operation of the reactor, and can expand the diffusion range of the materials, avoiding problems such as poor reaction effects caused by uneven contact between the reactants and the catalyst; and the blades 15, the central disc 14 and the annular disc 16 cooperate to further improve the dispersion ability of the stirring device, being suitable for gas dispersion with high-intensity requirements, and can achieve solid suspension and heat transfer, especially being suitable for gas-liquid-solid heterogeneous reactions.

[0051] Referring to Figure 7 and Figure 8 , the reactor suitable for solid materials according to the second specific embodiment of the present disclosure is different from the first embodiment in that:

[0052] First baffles 17 are symmetrically arranged inside the tank body 10, and the first baffles 17 are provided with hole bodies, and are attached to the inner wall of the tank body 10 and extend radially inward into the tank body.

[0053] Furthermore, the length direction of the first baffle 17 extends along the axial direction of the tank body 10, and the width direction of the first baffle 17 extends along the radial direction inside the tank body 10.

[0054] According to a preferred embodiment, the aperture range of the hole bodies on the first baffle can be 2-20 cm, preferably 5-15 cm, such as 10 cm. The distribution of the hole bodies on the first baffle can be uniform or non-uniform. For example, the distribution density can gradually decrease from the inside to the outside in the radial direction to promote more sufficient flow of the materials in the central region. And, the maximum gap between adjacent hole bodies on the first baffle can be 2-20 cm, preferably 3-12 cm, such as 5-10 cm. The radial extension width of the first baffle can be 0.1-0.3 times the inner diameter of the tank body, such as 0.2 times.

[0055] Second baffles 18 can be respectively arranged or simultaneously arranged at the top and / or bottom of the tank body 10. The second baffles 18 are provided with hole bodies, and the outer sides of the second baffles 18 are attached to the inner wall of the tank body 10.

[0056] Two first baffles 17 can be symmetrically arranged inside the tank body 10. In this way, two upper and lower circulation flows can be formed inside the tank body 10 with the paddle 13 as the boundary, which can promote the flow of the materials, help to accelerate the contact between the reactants and the catalyst, and improve the catalytic efficiency and reaction efficiency.

[0057] During the rotation of the stirring device, when a second baffle 18 is provided at the bottom, it forms a certain interception of the materials in the middle of the tank body 10, which can effectively promote the suspension of solids, avoid the accumulation of solid catalyst particles at the bottom of the tank body 10, and improve the use efficiency of the catalyst. When a second baffle 18 is provided at the top, it can slow down the upward trend of the stirred materials, and at the same time, a feeding method of adding solid materials from the top can also be adopted.

[0058] In addition, both the first baffle 17 and the second baffle 18 are provided with holes, which form a filtering and screening effect on the contacted materials and bubbles, and realize the cutting and crushing of large-particle materials during this process. Specifically, under the action of this stirring device, the materials have a certain impact force when contacting the first baffle 17 and / or the second baffle 18, so that the cutting effect of the first baffle 17 and the second baffle 18 on the materials and bubbles is enhanced. That is to say, the probability of breaking large-particle agglomerates in the materials increases, which helps to improve the mixing uniformity of the materials. Especially the first baffle 17 erected on the side of the tank body 10, due to the centrifugal action of the stirring device on the materials, when the materials contact the first baffle 17, an angle is formed between its flow direction and the first baffle 17, thereby improving the interception and crushing effect of the first baffle 17 on the materials.

[0059] According to a preferred embodiment, the aperture range of the holes on the second baffle can be 10 - 30 mm, preferably 15 - 25 mm, such as 20 mm. The distribution of the holes on the second baffle can be uniform or non-uniform. For example, the distribution density can gradually decrease from the central area to the edge area in the radial direction to promote more sufficient flow of the materials near the central area. Preferably, the hole distribution density on the second baffle can be 50 - 200 holes per square meter, preferably 80 - 160 holes per square meter, such as 100 holes per square meter.

[0060] Preferably, a plurality of first baffles 17 can be arranged at intervals, especially a plurality of first baffles 17 are symmetrically arranged, preferably a plurality of first baffles 17 are radially symmetrically arranged. When the second baffle 18 is provided, preferably the second baffle 18 is at a certain distance from the top plate and / or the bottom plate of the tank body 10. According to a specific embodiment, the distance between the second baffle and the bottom plate of the tank body or the top plate of the tank body can be 0.05 - 0.2 times the height of the tank body, preferably 0.1 - 0.15 times. Such a distance is beneficial to the addition, mixing and prevention of deposition of solid materials.

[0061] Refer to Figure 9 According to the reactor for solid materials of the third specific embodiment of the present disclosure, which is different from the second embodiment in that the width direction of the first baffle 17 extends along the tangential direction of the chord of the cross-section of the tank body 10. Preferably, two first baffles 17 are symmetrically arranged along the plane where the central axis of the tank body is located.

[0062] Compared with conventional reaction devices, in the reaction device of the present disclosure, due to the baffle structure provided along the side of the tank body, the radial widths of the central disc and the blades of the stirring device of the present disclosure are relatively small, thereby guiding the stirred material to form two up-and-down circulation flows in the tank body, avoiding the formation of regular vortex flows in the tank body, and thus ensuring that heterogeneous materials including solids, liquids, and / or gases can be effectively stirred and dispersed, while preventing the deposition of solid materials.

[0063] According to a preferred embodiment, the aperture range of the holes in the first baffle can be 2 - 20 cm, preferably 5 - 15 cm, such as 10 cm. The distribution of the holes on the first baffle can be uniform or non-uniform. For example, the distribution density can gradually decrease from the central region to the edge region in the radial direction to promote more sufficient flow of the material near the central region. Preferably, the maximum gap between adjacent holes on the first baffle can be 2 - 20 cm, preferably 3 - 12 cm, such as 5 - 10 cm. The width of the first baffle can be 0.5 - 0.75 times the inner diameter of the tank body, such as 0.6 times.

[0064] The conventional operations in the operation steps of the reactor of the present disclosure are well-known to those skilled in the art and will not be elaborated herein.

[0065] Compared with the prior art, the reactor of the present disclosure has the following beneficial effects:

[0066] 1. The stirring device uses a turbine blade, which is a paddle type with a relatively strong stirring intensity in medium- and high-speed stirring devices. The central disc can effectively prevent the rising bubbles from quickly escaping, playing a role in sealing large bubbles. The high-speed rotating blades provide a large shear force, ensuring the breaking and dispersion of bubbles, which is beneficial to the mass transfer between gas-liquid-solid phases;

[0067] 2. The cooperation between the blades and the annular disc further improves the dispersion ability of the stirring device, is suitable for gas dispersion with high-intensity requirements, and can achieve solid suspension, heat transfer, and is particularly suitable for gas-liquid-solid heterogeneous reactions;

[0068] 3. The annular discs can be arranged in parallel or in a trumpet-shaped diffusion. During the rotation of the blades, the annular discs can push the material to spread around, and at the same time, they can also suck in and eject the material between the annular rings, thereby expanding the diffusion range of the material, improving the mixing uniformity of the material, and reducing the probability of material deposition at the bottom of the tank body;

[0069] 4. The arrangement of the trumpet-shaped diffused annular disc also helps to form the structure of a Venturi tube inside the stirring device. As the blades and the central disc rotate, it can increase the flow rate of the inhaled material, thereby expanding the diffusion range of this part of the material, contributing to improving the material exchange between different regions inside the tank body, thus enhancing the mixing degree of the catalyst and the material and improving the reaction efficiency;

[0070] 5. The arrangement of the first baffle and / or the second baffle can promote the suspension of solids during the rotation of the stirring device, effectively prevent the deposition of the catalyst at the bottom of the reactor, and improve the utilization rate; the holes provided on the first baffle and the second baffle also contribute to the material mixing and increase the contact probability between the catalyst and the material.

[0071] The above-described embodiments have elaborated on the technical solutions of the present disclosure. It should be understood that the above are only specific embodiments of the present disclosure and do not limit the present disclosure. Any modifications, supplements, or substitutions in a similar manner made within the scope of the principles of the present disclosure shall be included within the protection scope of the present disclosure.

Claims

1. A reactor applicable to solid materials, comprising a tank for mixing materials, wherein a stirring device is arranged inside the tank, the stirring device includes a rotating shaft and blades, the blades are sleeved outside the rotating shaft, the rotating shaft extends along the axial direction of the tank, and the rotating shaft can drive the blades to rotate; characterized in that, the blades include a central disc coaxially arranged with the rotating shaft and a plurality of blades spaced outside the central disc; and an annular disc is connected to the inner sides of the plurality of blades, and the annular disc is coaxially arranged with the central disc.

2. The reactor applicable to solid materials according to claim 1, characterized in that, the annular disc is arranged between the end face of the central disc and the ends of the blades.

3. The reactor applicable to solid materials according to claim 1 or 2, characterized in that, a plurality of the annular discs are arranged on the same side of the central disc, and the diameters of the plurality of annular discs arranged in the direction away from the central disc increase in sequence.

4. The reactor applicable to solid materials according to claim 1 or 2, characterized in that, the annular disc is of an annular plate-like structure or a trumpet-shaped diffused structure.

5. The reactor applicable to solid materials according to claim 1, characterized in that, the two ends of the blades are respectively arranged on both sides of the central disc; the blades are of a straight blade type, an inclined blade type or a curved blade type, and the plurality of blades are arranged in a circumferential array.

6. The reactor applicable to solid materials according to claim 1, characterized in that, a first baffle is symmetrically arranged inside the tank, the first baffle is provided with a first hole body, and the first baffle is arranged in contact with the inner wall of the tank.

7. The reactor applicable to solid materials according to claim 6, characterized in that, the length direction of the first baffle extends along the axial direction of the tank; and the width direction of the first baffle extends along the radial direction of the tank or along the tangential direction of the cross section of the tank.

8. The reactor applicable to solid materials according to claim 1, characterized in that, the tank includes a top plate and a bottom plate, and a feed port is provided on the bottom plate of the tank.

9. The reactor applicable to solid materials according to claim 8, characterized in that, One or both of the top and bottom of the tank are provided with a second baffle, the second baffle is provided with a second hole body, and the outer edge of the second baffle is arranged in contact with the inner wall of the tank.

10. The reactor applicable to solid materials according to claim 7, characterized in that, when the first baffle extends along the tangential direction of the cross section of the tank, the width of the first baffle is 0.5 to 0.75 times the inner diameter of the tank.

11. The reactor applicable to solid materials according to claim 6, characterized in that, The aperture range of the first hole body is 2 cm to 20 cm.

12. The reactor applicable to solid materials according to claim 9, wherein The aperture range of the second hole body is 10 mm to 30 mm.

Images