Fluidized bed internal component for strengthening rotational flow mixing and gas-solid fluidized bed

Abstract

The fluidized bed internal component is provided with a conical flow guide side face, a conical top opening of the conical flow guide side face forms a central flow guide area, and a plurality of annular rotational flow areas are formed on the conical flow guide side face at intervals in the generatrix direction of the conical flow guide side face. A plurality of inclined rotational flow guide blades are arranged in each annular rotational flow area, and an annular direct flow area is formed between every two adjacent annular rotational flow areas and on the conical flow guide side face; gas-solid two-phase fluid entering from the cone bottom opening in the axis direction of the conical flow guide side face still flows in the axis direction after passing through the center flow guide area and the annular direct flow area, and flows in the rotational flow direction around the axis of the conical flow guide side face after passing through the annular rotational flow area. The internal component of the fluidized bed can improve flowing and mass transfer of gas-solid two-phase fluid in the fluidized bed and relieve the phenomenon that bed layer particles adhere to the wall.

Description

Technical Field

[0001] The invention relates to the technical field of chemical equipment, in particular to a fluidized bed internal component and a gas-solid fluidized bed for enhancing cyclone mixing. Background Art

[0002] Since its breakthrough application in the catalytic cracking process of petroleum in the 1940s, gas-solid fluidized bed technology has become a key reaction device in the chemical, energy and materials fields, and is widely used in industrial scenarios such as catalytic cracking, coal combustion, gas-solid synthesis and particle drying. Its core advantage lies in the efficient mass and heat transfer achieved through the fluidization of gas-solid two-phase fluids. However, in actual operation, it still faces problems such as uneven bed fluidization caused by bubble merging, significant gas-solid backmixing, and difficulty in controlling the distribution of particle residence time. For example, in the catalytic cracking process, the rapid deactivation of the catalyst is directly related to the decrease in reaction efficiency, and a continuous regeneration system is required to maintain the continuity of the reaction, which places high dynamic stability requirements on the design of internal components.

[0003] Traditional internal components are mainly porous baffles, guide baffles and vertical / horizontal tube bundles, which achieve bubble breakage and flow field regulation through physical barriers. However, this type of structure has significant limitations: mechanical baffles are prone to thermal deformation or clogging due to high temperature and high pressure environments, reducing operational stability; although the tube bundle design can limit the bubble size, it will increase local pressure drop and cause particle wear; static components are difficult to adapt to the differences in fluidization characteristics of particles of different particle sizes and densities, resulting in insufficient flexibility in reactor operation. In addition, traditional internal components have limited effect in suppressing axial backmixing, especially when operating at low material levels, where pressure pulsations are significant, affecting mass transfer efficiency and product selectivity.

[0004] The Chinese invention patent application, publication number CN101172219A, provides an internal component for a gas-solid fluidized bed. By designing at least two layers of horizontal grids, guide vanes arranged in the same direction are provided in each flow area, and the guide vanes in adjacent flow areas are arranged in opposite directions, so that the gas-solid two-phase fluid generates a cross flow, and the guide vanes in the corresponding flow areas of the upper and lower adjacent layers of horizontal grids are arranged in opposite directions. This design not only improves operational stability, but also effectively increases the mass transfer efficiency between the bubble phase and the emulsion phase in the bed, while significantly reducing the axial back-mixing of the gas phase and the particle phase in the bed. However, due to its overly complex structure, this internal component has multiple dead zones, which have an adverse effect on mass transfer and are not easy to install and manufacture.

[0005] Chinese invention patent application publication number CN117920073A discloses a composite internal component for a gas-solid fluidized bed. By employing multiple vertically parallel, spaced-apart, elongated bluff bodies, the structure forces the gas-solid two-phase fluid to form eddies after passing through the flow-disrupting components. These eddies then act synergistically to create turbulent bubbles. This structure effectively breaks up bubbles and particle agglomerates, thereby improving gas-solid transfer efficiency. However, at high catalyst mass flow rates, it can easily lead to problems such as catalyst bridging and poor flow.

[0006] In summary, the internal components of the existing fluidized bed have poor flow and mass transfer effects of the two-phase fluid, which in turn leads to the problem of poor catalyst flow. Summary of the Invention

[0007] The purpose of the present invention is to provide a fluidized bed internal component and a gas-solid fluidized bed with enhanced cyclonic mixing, so as to solve the above-mentioned problems existing in the existing internal components, improve the flow and mass transfer of gas-solid two-phase fluids through the fluidized bed internal component, and alleviate the phenomenon of bed particle adhesion.

[0008] The above technical objectives of the present invention are mainly achieved through the following technical solutions:

[0009] In one aspect, the present invention provides a fluidized bed internal component for enhancing swirl mixing, which is disposed within a fluidized bed to guide the flow of a gas-solid two-phase fluid. The fluidized bed internal component has a conical flow-guiding side surface, wherein the cone top opening of the conical flow-guiding side surface forms a central flow-guiding area. A plurality of annular swirl areas are formed at intervals along the generatrix direction of the conical flow-guiding side surface, each of the annular swirl areas is provided with a plurality of obliquely arranged swirl guide blades. An annular direct flow area is formed on the conical flow-guiding side surface between two adjacent annular swirl areas.

[0010] The gas-solid two-phase fluid entering from the cone bottom opening along the axial direction of the conical guide side surface continues to flow along the axial direction after passing through the central guide area and the annular direct flow area, and flows in the swirl direction around the axis of the conical guide side surface after passing through the annular swirl area.

[0011] In a preferred embodiment of the present invention, the inclination directions of the plurality of swirl guide blades in one annular swirl zone are the same;

[0012] The swirl guide blades in the adjacent annular swirl zones are inclined in opposite directions, so as to form gas-solid two-phase fluids with opposite swirl directions on the inner and outer sides of the annular straight flow zone.

[0013] In a preferred embodiment of the present invention, the fluidized bed internals include:

[0014] A plurality of support beams extending along the generatrix direction of the tapered flow-guiding side surface, wherein the plurality of support beams are spaced apart along the circumferential direction of the tapered flow-guiding side surface;

[0015] A plurality of support rings are provided on the support beam and located within the conical flow-guiding side surface, wherein the plurality of support rings are coaxial and spaced apart along the extension direction of the support beam;

[0016] Among them, a grid plate is installed in the support ring with the smallest diameter to form the central guide area, an annular guide area is formed between the two adjacent support rings, some of the annular guide areas are provided with the swirl guide blades to form the annular swirl area, and the annular guide area without the swirl guide blades forms the annular direct current area.

[0017] In a preferred embodiment of the present invention, both ends of the swirl guide vanes in the annular swirl area are respectively fixed to the support rings on both sides of the swirl area.

[0018] In a preferred embodiment of the present invention, a distance H1 between the support ring with the smallest diameter and the support ring with the largest diameter along the axial direction of the conical flow-guiding side surface is 250 mm to 400 mm.

[0019] In a preferred embodiment of the present invention, the width W1 of the annular swirl zone along the radial direction of the conical guide side is 100mm-250mm, and the width W2 of the annular direct flow zone along the radial direction of the conical guide side is 20mm-50mm.

[0020] In a preferred embodiment of the present invention, the height of the annular swirl zone along the axial direction of the conical guide side is H2, and the height of the annular direct flow zone along the axial direction of the conical guide side is H3, wherein H2=1.1H3~1.6H3.

[0021] In a preferred embodiment of the present invention, the flow area of ​​the central guide zone accounts for 10% to 90% of the cross-sectional flow area of ​​the fluidized bed.

[0022] In a preferred embodiment of the present invention, the angle between the generatrix of the tapered guide side surface and the axis is 30° to 60°.

[0023] On the other hand, the present invention also provides a gas-solid fluidized bed comprising:

[0024] fluidized bed shell;

[0025] The fluidized bed internal component for enhancing cyclonic mixing is installed in the fluidized bed shell, with an inner flow area formed within the tapered flow-guiding side surface of the fluidized bed internal component and an outer flow area formed between the tapered flow-guiding side surface of the fluidized bed internal component and the fluidized bed shell;

[0026] A distributor is provided below the fluidized bed internal component and is opposite to the cone bottom opening of the conical flow guide side surface of the fluidized bed internal component.

[0027] Compared with the prior art, the technical solution of the present invention has the following characteristics and advantages:

[0028] The fluidized bed internal components for enhanced cyclonic mixing described in the present invention can effectively improve the axial / radial mass transfer efficiency between the bubble phase and the emulsion phase in the bed, alleviate the phenomenon of bed particles adhering to the wall, and at the same time play the role of breaking large bubbles and inhibiting bubble aggregation, thereby strengthening the contact effect between the gas-solid two-phase fluid, and also helping to reduce the backmixing of the gas-solid two-phase fluid, thereby greatly improving the gas-solid mass transfer effect and the operating efficiency of the fluidized bed device.

[0029] The fluidized bed internal component for enhanced cyclonic mixing described in the present invention can be widely used in various fluidized bed industrial devices, especially in continuous devices that require continuous removal of solid particles, and can significantly improve the flow and mass transfer of gas-solid two-phase fluids.

[0030] The gas-solid fluidized bed described in the present invention has a distributor adopting a porous plate or a tubular structure, and its layout design forms a fluidized bed system with two bed densities having a significant difference between the inside and outside of the fluidized bed internals. By introducing a large fluidizing air volume into the bottom of the fluidized bed internals through the distributor, the superficial gas velocity inside the fluidized bed internals (inner flow area) is significantly improved, thereby generating a larger bed gas holdup, corresponding to the formation of a smaller bed density; while the outer area of ​​the fluidized bed internals (outer flow area) has a relatively large bed density due to its relatively small superficial gas velocity, and the static pressure of the fluid in the fluidized bed internals is significantly lower than the static pressure of the external fluid. Under the action of the above-mentioned pressure difference, an orderly and macroscopic radial-axial particle internal circulation path is formed near the fluidized bed internals. This circulating flow mode not only promotes the efficient migration of particles between different areas, but also effectively enhances the mixing mass transfer efficiency between particles through continuous particle replacement and mixing, further optimizes the reaction kinetic conditions of the gas-solid two-phase in the fluidized bed, thereby improving the process performance and reaction efficiency of the entire fluidized bed system. BRIEF DESCRIPTION OF THE DRAWINGS

[0031] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the following briefly introduces the drawings required for the embodiments or the description of the prior art. Obviously, the drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative work. In the drawings:

[0032] The drawings described herein are for illustrative purposes only and are not intended to limit the scope of the present invention in any way. In addition, the shapes and proportional dimensions of the various components in the drawings are merely illustrative and are used to help understand the present invention, and are not intended to specifically limit the shapes and proportional dimensions of the various components of the present invention. Those skilled in the art can select various possible shapes and proportional dimensions to implement the present invention according to specific circumstances under the guidance of the present invention.

[0033] Figure 1 Schematic diagram of the top view of the internal components of the fluidized bed for enhanced cyclonic mixing according to the present invention;

[0034] Figure 2 for Figure 1 Schematic diagram of the cross-sectional structure of AA;

[0035] Figure 3 Schematic diagram of the structure of the gas-solid fluidized bed of the present invention;

[0036] Figure 4 Schematic diagram of the test results of fluid uniformity in the fluidized bed.

[0037] Description of reference numerals:

[0038] 10. Fluidized bed internals; 11. Support beams; 12. Support rings; 13. Grid plates; 14. Swirl guide vanes; 15. Central guide area; 16. Annular guide area; 17. Annular swirl area; 18. Annular direct flow area;

[0039] 20. Fluidized bed shell; 21. Distributor. DETAILED DESCRIPTION

[0040] In order to enable those skilled in the art to better understand the technical solutions of the present invention, the technical solutions in the embodiments of the present invention will be clearly and completely described below in conjunction with the accompanying drawings of the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without making creative efforts should fall within the scope of protection of the present invention.

[0041] It should be noted that when an element is referred to as being "disposed on" another element, it may be directly on the other element or there may be an element centered thereon. When an element is referred to as being "connected to" another element, it may be directly connected to the other element or there may be an element centered thereon. The terms "vertical," "horizontal," "left," "right," and similar expressions used herein are for illustrative purposes only and do not represent the only embodiments.

[0042] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by those skilled in the art to which this invention pertains. The terms used herein in the specification of the present invention are for the purpose of describing specific embodiments only and are not intended to limit the present invention. The term "and / or" as used herein includes any and all combinations of one or more of the associated listed items.

[0043] Implementation method one:

[0044] like Figures 1 to 3 As shown, the present invention provides a fluidized bed internal component 10 for enhancing cyclone mixing, which is arranged in the fluidized bed to guide the flow of gas-solid two-phase fluid. The fluidized bed internal component 10 has a conical guide side surface, and the cone top opening of the conical guide side surface forms a central guide area 15. Along the generatrix direction of the conical guide side surface, a plurality of annular cyclone areas 17 are formed on the conical guide side surface at intervals. Each annular cyclone area 17 is provided with a plurality of obliquely arranged cyclone guide blades 14. An annular direct flow area 18 is formed on the conical guide side surface between two adjacent annular cyclone areas 17. The gas-solid two-phase fluid entering from the cone bottom opening along the axial direction of the conical guide side surface continues to flow along the axial direction after passing through the central guide area 15 and the annular direct flow area 18. After passing through the annular cyclone area 17, it flows in the cyclone direction around the axis of the conical guide side surface.

[0045] The fluidized bed internal component 10 for enhanced swirl mixing described in the present invention guides the direct flow and swirl of the gas-solid two-phase fluid (mixed phase) respectively through the alternating direct flow zones and swirl zones on the conical side, which not only helps the particles to effectively break the bubbles and inhibit the aggregation of bubbles, but also improves the mixing effect by enhancing the uniform distribution of particles in the radial direction, effectively improves the axial / radial mass transfer efficiency between the bubble phase and the emulsion phase in the bed, alleviates the phenomenon of bed particles adhering to the wall, but also reduces the axial back mixing of the gas phase and the particle phase in the bed, thereby improving the bed operation stability.

[0046] The fluidized bed internal component 10 for enhanced cyclonic mixing described in the present invention can be widely used in various fluidized bed industrial devices, especially in continuous devices that require continuous removal of solid particles (particle phase or solid phase), and can significantly improve the flow and mass transfer of gas-solid two-phase fluids.

[0047] The specific structure of each part of the fluidized bed internal component 10 for enhancing cyclonic mixing according to the present invention, as well as the position and connection relationship between the parts will be described in detail below.

[0048] like Figure 1 and Figure 2 As shown, the fluidized bed internal component 10 for enhancing cyclonic mixing of the present invention is a conical structure as a whole, with a conical flow-guiding side surface, and a corresponding flow-guiding area is formed by the structural arrangement on the flow-guiding side surface.

[0049] Specifically, the guide side is provided with a plurality of support beams 11 and a plurality of support rings 12. The support beams 11 are long strips, and each support beam 11 extends along the generatrix direction of the tapered guide side. The plurality of support beams 11 are spaced apart along the circumferential direction of the tapered guide side, and the lengths of the support beams 11 are the same; the support rings 12 are circular structures, mounted and fixed on the support beams 11, and the plurality of support rings 12 are coaxially arranged and spaced apart along the length direction of the support beam 11, that is, the diameters of the plurality of support rings 12 gradually increase from top to bottom, the diameter of the uppermost support ring 12 is the smallest and is connected to the top of the support beam 11, and the diameter of the lowermost support ring 12 is the largest and is connected to the bottom of the support beam 11.

[0050] Among them, such as Figures 1 to 3 As shown, a grid plate 13 is installed in the support ring 12 with the smallest diameter (the uppermost support ring 12) to form a central guide area 15. The central guide area 15 is formed by the cone top opening of the cone guide side, which is a circular area, and the grid plate 13 is set in the circular area to divide the central guide area 15 into a large number of direct current channels; the gas-solid two-phase fluid enters from the cone bottom opening along the axial direction of the cone guide side and flows upward, and still flows upward along the axial direction after passing through the central guide area 15. The setting of the grid plate 13 can effectively break up bubbles, inhibit the aggregation of bubbles, and improve the mixing effect.

[0051] Among them, such as Figures 1 to 3As shown, an annular guide area 16 is formed between two adjacent support rings 12. The annular guide area 16 is a section of an annular conical surface on the conical guide side surface, and the annular conical surface is defined between two adjacent support rings 12. A plurality of swirl guide blades 14 are provided within a portion of the annular guide area 16 to form an annular swirl area 17. The multiple swirl guide blades 14 within the same annular swirl area 17 face the same direction, and the ends of the swirl guide blades 14 are respectively fixed to the support rings 12 on both sides of the swirl area. The gas-solid two-phase fluid that enters from the cone bottom opening and flows upward along the axis of the conical guide side surface, after passing through the annular swirl area 17, flows around the axis of the conical guide side surface in the swirl direction. The swirl direction refers to the direction of the spiral line. The swirl described in the present invention is a fluid that flows upward along the spiral line direction. The annular guide area 16, which is not provided with swirl guide vanes 14, forms an annular direct flow area 18. No flow guide components are installed in the annular direct flow area 18. The gas-solid two-phase fluid that enters from the cone bottom opening and flows upward along the axis of the conical guide side surface continues to flow upward along the axis after passing through the annular direct flow area 18. The annular swirl areas 17 and the annular direct flow areas 18 are alternately arranged along the generatrix of the conical guide side surface. In this embodiment, three annular swirl areas 17 are formed on the conical guide side surface, with two annular direct flow areas 18 formed between the three annular swirl areas 17.

[0052] The fluidized bed internal component 10 adopts a conical tapered structure to alleviate the phenomenon of bed particles adhering to the wall, while playing the role of breaking large bubbles and inhibiting bubble aggregation, thereby enhancing the contact effect between the gas-solid two-phase fluid; the alternating annular swirl zone 17 and annular direct flow zone 18 guide the gas-solid two-phase fluid to form alternating swirl and direct flow, which helps the particles to effectively break the bubbles, inhibit the aggregation of bubbles, and effectively improve the axial / radial mass transfer efficiency between the bubble phase and the emulsion phase in the bed. At the same time, it can also reduce the axial back mixing of the gas phase and the particle phase in the bed, thereby improving the bed operation stability.

[0053] The structure and technical effects of the preferred embodiment of the fluidized bed internal component 10 for enhancing cyclonic mixing according to the present invention will be further described below.

[0054] According to one embodiment of the present invention, the swirl guide vanes 14 in adjacent annular swirl zones 17 are inclined in opposite directions to form gas-solid two-phase fluids with opposite swirl directions on the inner and outer sides of the annular straight flow zone 18 .

[0055] Specifically, the swirl guide blades 14 in the annular swirl zone 17 adjacent to the inner side of the annular direct current zone 18 are tilted along the first direction to form a two-phase flow flowing along the first swirl direction (clockwise) in this area, and the swirl guide blades 14 in the annular swirl zone 17 adjacent to the outer side of the annular direct current zone 18 are tilted along the second direction to form a two-phase flow flowing along the second swirl direction (counterclockwise) in this area, thereby causing the gas-solid two-phase fluid to produce an interlaced spiral flow, which can effectively improve the radial mass transfer efficiency between the bubble phase and the emulsion phase in the bed and alleviate the phenomenon of bed particles adhering to the wall.

[0056] According to one embodiment of the present invention, Figure 2 and Figure 3 As shown, the distance H1 between the support ring 12 with the smallest diameter and the support ring 12 with the largest diameter along the axial direction of the conical flow-guiding side surface is 250 mm to 400 mm, that is, the height of the entire fluidized bed internal component 10 is 250 mm to 400 mm.

[0057] According to one embodiment of the present invention, Figure 2 As shown, the width W1 of the annular swirl zone 17 along the radial direction of the conical guide side surface is 100 mm to 250 mm, and the width W2 of the annular straight flow zone 18 along the radial direction of the conical guide side surface is 20 mm to 50 mm.

[0058] According to one embodiment of the present invention, the height of the annular swirl zone 17 along the axial direction of the conical guide side is H2, and the height of the annular straight flow zone 18 along the axial direction of the conical guide side is H3, wherein H2=1.1H3~1.6H3.

[0059] According to one embodiment of the present invention, the flow area of ​​the central guide zone 15 accounts for 10% to 90% of the cross-sectional flow area of ​​the fluidized bed; preferably, the flow area of ​​the central guide zone 15 accounts for 60% to 90% of the cross-sectional flow area of ​​the fluidized bed.

[0060] According to one embodiment of the present invention, the angle between the generatrix of the conical guide side and the axis is 30° to 60°. Figure 2 As shown, the angle γ between the generatrix of the conical guide side and the horizontal plane is 30° to 60°.

[0061] Implementation method 2:

[0062] like Figure 3As shown, the present invention also provides a gas-solid fluidized bed, which includes: a fluidized bed shell 20; a fluidized bed internal component 10 for enhanced cyclone mixing as described in embodiment one, the fluidized bed internal component 10 is installed in the fluidized bed shell 20, an inner flow area is formed in the conical guide side of the fluidized bed internal component 10, and an outer flow area is formed between the conical guide side of the fluidized bed internal component 10 and the fluidized bed shell 20; a distributor 21, the distributor 21 is arranged below the fluidized bed internal component 10, and is opposite to the conical bottom opening of the conical guide side of the fluidized bed internal component 10.

[0063] Specifically, such as Figure 3 As shown, the fluidized bed shell 20 has a cylindrical structure, and the fluidized bed internal component 10 is installed in the fluidized bed shell 20 through a bracket and the two are coaxially arranged. A distributor 21 is also provided in the fluidized bed shell 20, and the fluidized bed internal component 10 and the distributor 21 are arranged opposite to each other up and down. The gas phase generated by the distributor 21 can flow upward and mix with the particle phase and pass through the fluidized bed internal component 10, so that large bubbles are broken, the contact between the gas and solid phases is improved, the back mixing is reduced, and the reaction effect is improved.

[0064] In the present invention, the distributor 21 adopts a porous plate or tubular structure, and its layout design forms a fluidized bed system with two bed densities with significant differences inside and outside the fluidized bed internals 10. By introducing a large fluidizing air volume into the bottom of the fluidized bed internals 10 through the distributor 21, the superficial gas velocity inside the fluidized bed internals 10 (inner circulation area) is significantly improved, thereby generating a larger bed gas content, corresponding to the formation of a smaller bed density; while the outer area of ​​the fluidized bed internals 10 (outer circulation area) has a relatively small superficial gas velocity, and its bed density is relatively large. Based on the principle of fluid statics, it can be seen that the static pressure of the fluid in the fluidized bed internals 10 is significantly less than the static pressure of the external fluid, and this pressure difference becomes the core power source for driving the particle circulation. Under the action of the above-mentioned pressure difference, an orderly and macroscopic radial-axial particle internal circulation path is formed near the fluidized bed internals 10. This circulating flow mode not only promotes efficient migration of particles between different areas, but also effectively enhances the mixing and mass transfer efficiency between particles through continuous particle replacement and mixing, further optimizes the reaction kinetic conditions of the gas-solid two phases in the fluidized bed, thereby improving the process performance and reaction efficiency of the entire fluidized bed system.

[0065] The characteristics of the gas-solid fluidized bed of the present invention will be described below in combination with specific experimental test results.

[0066] According to the characteristics of different solid content in the fluidized bed along the axial and radial directions, it can be seen that the solid content is mainly affected by the following factors: the superficial gas velocity U g , mass flow rate G s, the diameter D of the fluidized bed shell, the radius ratio r / R, r is the distance from a radial position of the horizontal section of the fluidized bed to the center, R is the radius of the fluidized bed shell, the axial height H, the average particle size d p , the true density of particles ρ p , gas kinematic viscosity μ, gas density ρ g , the acceleration due to gravity g, that is,

[0067]

[0068] Further through fitting, the axial / radial distribution expression of the fluidized bed solid content using the fluidized bed internals 10 described in the first embodiment can be obtained:

[0069]

[0070] Among them, Fr is the Froude number,

[0071] Based on this, it can be seen that the fluid uniformity test within the gas-solid fluidized bed described in the present invention requires a comprehensive assessment of the fluid state at different heights and radial positions within the fluidized bed. Specifically, it requires precise pressure measurements at different locations within the fluidized bed to calculate and evaluate the heterogeneity index. In the actual experimental measurement process, multiple pressure sensors were installed at different heights and radial positions within the fluidized bed to collect pressure data in real time. This data was then processed to ultimately determine the heterogeneity index of the fluidized bed.

[0072] Two control groups were set up at the same time. One of the control groups had no internal components in the fluidized bed, and the other control group had flat internal components in the prior art (such as the horizontal grid internal components provided in the background art publication number CN101172219A). Except for the difference in internal components, the other experimental test conditions of the two control groups were the same as those of the gas-solid fluidized bed in the present invention.

[0073]

[0074] Among them, γ a is the heterogeneity index in the fluidized bed, n is the number of pressure sensors set at different positions during the test, P i is the airflow pressure measured by the i-th pressure sensor, A i is the flow area of ​​the fluid at the position of the i-th pressure sensor, is the average pressure.

[0075] In a specific test process, the test data and analysis calculation results are as follows: Figure 4As shown, Tables 1-3 are the pressure data of three groups of experiments at different radial test points at different gas velocities, and Table 4 is based on the first three tables and the above-mentioned inhomogeneity index γ a The heterogeneity index at different gas velocities obtained by the calculation formula can be seen from the comparison that the heterogeneity index of the fluid in the gas-solid fluidized bed of the present invention is significantly enhanced when the gas velocity is relatively high.

[0076] Therefore, when the gas-solid fluidized bed in the present invention is used for catalytic reactions of high-speed gas-solid two-phase fluids, due to the relatively high heterogeneity index within the bed layer, there is sufficient pressure difference in the radial direction, thereby enhancing the efficient migration of particles between different areas. Through continuous particle replacement and mixing, the mixing and mass transfer efficiency between particles is effectively enhanced.

[0077] The specific embodiments described above further illustrate the objectives, technical solutions and beneficial effects of the present invention in detail. It should be understood that the above description is only a specific embodiment of the present invention and is not intended to limit the scope of protection of the present invention. Any modifications, equivalent substitutions, improvements, etc. made within the spirit and principles of the present invention should be included in the scope of protection of the present invention.

Claims

1. A fluidized bed internal component for enhancing cyclonic mixing, arranged in a fluidized bed to guide the flow of gas-solid two-phase fluid, characterized in that: The fluidized bed internal component (10) has a conical flow-guiding side surface, a cone top opening of the conical flow-guiding side surface forms a central flow-guiding area (15), a plurality of annular swirl areas (17) are formed on the conical flow-guiding side surface along the generatrix direction of the conical flow-guiding side surface, each of the annular swirl areas (17) is provided with a plurality of swirl guide blades (14) arranged obliquely, and an annular direct flow area (18) is formed on the conical flow-guiding side surface between two adjacent annular swirl areas (17); The gas-solid two-phase fluid entering from the cone bottom opening along the axial direction of the conical guide side surface continues to flow along the axial direction after passing through the central guide area (15) and the annular direct flow area (18), and flows in the swirling direction around the axis of the conical guide side surface after passing through the annular swirling area (17).

2. The fluidized bed internal component for enhancing cyclonic mixing according to claim 1, characterized in that: The inclination directions of the plurality of swirl guide blades (14) in one annular swirl zone (17) are the same; The swirl guide blades (14) in the adjacent annular swirl zones (17) are inclined in opposite directions, so as to form gas-solid two-phase fluids with opposite swirl directions on the inner and outer sides of the annular direct flow zone (18).

3. The fluidized bed internal component for enhancing cyclonic mixing according to claim 1, characterized in that: The fluidized bed internals (10) include: A plurality of support beams (11) extending along the generatrix direction of the tapered flow-guiding side surface, wherein the plurality of support beams (11) are spaced apart along the circumferential direction of the tapered flow-guiding side surface; A plurality of support rings (12) are provided on the support beam (11) and located within the conical flow-guiding side surface, wherein the plurality of support rings (12) are coaxial and spaced apart along the extension direction of the support beam (11), and the diameter of each support ring (12) gradually decreases from the top to the bottom of the conical flow-guiding side surface; A grid plate (13) is installed in the support ring (12) with the smallest diameter to form the central guide area (15), an annular guide area (16) is formed between two adjacent support rings (12), some of the annular guide areas (16) are provided with the swirl guide blades (14) to form the annular swirl area (17), and the annular guide areas (16) not provided with the swirl guide blades (14) form the annular direct current area (18).

4. The fluidized bed internal component for enhancing cyclonic mixing according to claim 3, characterized in that: Both ends of the swirl guide blade (14) in the annular swirl area (17) are respectively fixed on the support rings (12) on both sides of the swirl area.

5. The fluidized bed internal component for enhancing cyclonic mixing according to claim 3, characterized in that: A distance H1 between the support ring (12) with the smallest diameter and the support ring (12) with the largest diameter along the axial direction of the conical flow-guiding side surface is 250 mm to 400 mm.

6. The fluidized bed internal component for enhancing cyclonic mixing according to claim 3, characterized in that: The width W1 of the annular swirl zone (17) along the radial direction of the conical guide side surface is 100 mm to 250 mm, and the width W2 of the annular direct flow zone (18) along the radial direction of the conical guide side surface is 20 mm to 50 mm.

7. The fluidized bed internal component for enhancing cyclonic mixing according to claim 3, characterized in that: The height of the annular swirl zone (17) along the axial direction of the conical guide side surface is H2, and the height of the annular direct flow zone (18) along the axial direction of the conical guide side surface is H3, wherein H2=1.1H3~1.6H3.

8. The fluidized bed internal component for enhancing cyclonic mixing according to claim 1, characterized in that: The flow area of ​​the central guide zone (15) accounts for 10% to 90% of the cross-sectional flow area of ​​the fluidized bed.

9. The fluidized bed internal component for enhancing cyclonic mixing according to claim 1, characterized in that: The angle between the generatrix of the conical guide side surface and the axis is 30° to 60°.

10. A gas-solid fluidized bed, characterized in that: include: a fluidized bed shell (20); The fluidized bed internal component (10) for enhancing cyclonic mixing according to any one of claims 1 to 9, wherein the fluidized bed internal component (10) is installed in the fluidized bed shell (20), an inner flow area is formed in the conical flow-guiding side surface of the fluidized bed internal component (10), and an outer flow area is formed between the conical flow-guiding side surface of the fluidized bed internal component (10) and the fluidized bed shell (20); A distributor (21) is provided below the fluidized bed internal component (10) and is opposite to the cone bottom opening of the conical flow guide side surface of the fluidized bed internal component (10).

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