Spoiler member, fluidized bed reactor provided with spoiler member, and use thereof

Abstract

A spoiler member (15), a fluidized bed reactor provided with the spoiler member (15), a use thereof, and a method for producing an olefin by methanol conversion. The spoiler member (15) comprises a flow guide part and a mixing part which are coaxially arranged in the radial direction. The flow guide part comprises a flow guide plate (20). At least three gas passing holes basically uniformly distributed are formed in the flow guide plate (20). The total void fraction of the openings of the flow guide plate (20) is 0.2% -6%. The mixing part surrounds the flow guide part and comprises at least two spoiler rings which are concentrically arranged. At least six spoiler bodies (21) which are uniformly distributed are arranged on each spoiler ring. No holes are formed in the surface of each spoiler body (21). The total void fraction of the mixing part is 30% -95% because of the existence of the spoiler bodies (21). The total void area of the mixing part is 30-500 times of the total void area of the flow guide plate. Also provided is a fluidized bed reactor comprising a reaction chamber, and the reaction chamber is provided with two or more spoiler members (15) arranged in the axial direction of the reactor.

Description

Flow-disturbing component, fluidized bed reactor provided with the flow-disturbing component, and application thereof Technical Field

[0001] The present invention relates to the field of fluidized bed reactors, in particular to a flow-disturbing component, a fluidized bed reactor provided with the flow-disturbing component and application thereof, and a method for producing olefins by converting methanol. Background Art

[0002] With the continued growth of global energy demand and the continuous optimization of the energy structure, the efficient conversion and utilization of coal, a traditional but abundant fossil energy source, has become a key topic in scientific research and industrial application. Methanol-to-olefins (MTO) technology, as a key pathway for producing low-carbon olefins from coal or methanol, not only helps alleviate the shortage of oil resources but also provides an effective way to achieve clean and efficient conversion of coal resources. Therefore, it is of extremely important strategic significance. In recent years, with the rapid development of the MTO industry, technological innovation and optimization have become the core driving force for enhancing industrial competitiveness.

[0003] In the MTO process, the fluidized bed reactor is the core equipment for converting methanol into olefins. The internal multiphase flow and mixing effect directly determine the selectivity, conversion rate and stability of the reaction. Specifically, the mixing area of ​​the reactor's reaction chamber is an important place for key chemical reactions to occur. The rapid and efficient mixing of multiple solid-phase catalyst particles with different temperatures, different carbon deposition levels and different particle size distributions with gas-phase raw materials in this area is crucial for improving the selectivity of light-carbon olefins (such as ethylene and propylene). Moreover, as the scale of the reaction unit continues to expand, the complexity of the mixing area of ​​the reaction chamber increases significantly, and the under-mixing phenomenon between the various materials becomes more and more significant, resulting in a decrease in reaction performance, which in turn affects the economy and environmental protection of the overall process.

[0004] In the prior art, although some solid distributors have been designed to optimize the uniform distribution of solid particles within the equipment, there are few studies on improving the mixing of multiple streams of different materials in a fluidized bed reactor.

[0005] CN202208702U discloses a catalyst distributor for promoting uniform distribution of regenerated catalyst in a catalytic cracking regenerator. The distributor is located in the center of the equipment and has distribution arms extending radially. The regenerated catalyst enters the equipment through the small holes and the end opening of the distribution arms, thereby improving distribution.

[0006] CN102504861A discloses a novel catalytic cracking catalyst distributor, which includes multiple distribution slots and distribution holes. It uses an "air cushion" dense phase fluidization method to transport the catalyst to different positions of the equipment flow cross section to achieve gas-solid mixing.

[0007] These existing solid distributors primarily focus on optimizing gas-solid distribution during catalyst regeneration and are not specifically designed for reactions involving the mixing characteristics of multiple solid streams, such as the MTO process. These distributors have limitations in their application to MTO fast fluidized bed reactors, as they struggle to effectively handle the complex environment of high gas velocities and significant interaction between multiple streams, resulting in suboptimal mixing.

[0008] Zhu Liyun, Liu Zetian, et al. ("Study on Particle Mixing Characteristics in a Two-Stream Catalyst Mixing Pre-Lifting Structure in an FCC Riser," Journal of Chemical Engineering of Universities, Vol. 3, 2014, v. 28, pp. 510-517) reported that by adding a concentric central tube to the bottom of the FCC riser, the chamber is divided into a central tube region and an annular region, achieving ideal mixing of different solid phases at a certain axial height above the central tube. However, the bottom of the MTO fast fluidized bed reactor is the critical reaction zone, and the addition of a central tube results in less uniform mixing of different materials in the area near the central tube.

[0009] In summary, in order to address the complex flow and mixing problems existing in the mixing area of ​​the reaction chamber of the fluidized bed reactor in reaction processes involving the mixing characteristics of multiple solid-phase materials (such as the MTO process), the design of new components that can significantly improve the mixing efficiency between multiple solid-phase materials and between the gas and solid phases is of great significance for enhancing the selectivity of low-carbon olefins, improving the performance of the reactor, and promoting the optimization and upgrading of the MTO industry.

[0010] Summary of the Invention

[0011] The purpose of the present invention is to overcome the problem of poor mixing between multiple catalysts with different temperatures, different carbon deposition degrees, and different particle size distributions in the mixing area of ​​the reaction chamber and between the gas and solid phases after the existing fast fluidized bed reactor technology is scaled up, resulting in a decrease in reaction performance. A specific flow disturbance component is developed, and based on this, a fluidized bed reactor equipped with a flow disturbance component and its application and a method for producing olefins from methanol are developed, thereby enabling enhanced mixing of different materials in the mixing area of ​​the reaction chamber of the reactor, especially the fluidized bed reactor, to achieve favorable material distribution and uniformity, thereby improving the performance of the reactor and the production efficiency, economy and environmental protection of the overall process.

[0012] To achieve the above-mentioned object, the present invention provides a flow-disturbing member on one hand, comprising a flow-disturbing portion and a mixing portion coaxially distributed in the radial direction, wherein the flow-disturbing portion comprises a flow-disturbing plate, at least three substantially evenly distributed air holes are provided on the flow-disturbing plate, and the total porosity of the openings of the flow-disturbing plate is 0.2%-6%, preferably 1.5%-4.5%; the mixing portion surrounds the flow-disturbing portion and comprises at least two concentrically arranged flow-disturbing rings, each flow-disturbing ring being provided with at least six evenly distributed flow-disturbing bodies, the flow-disturbing surface being non-porous, and the presence of the flow-disturbing body making the total porosity of the mixing portion be 30%-95%, preferably 60%-90%; and the total void area of ​​the mixing portion is 30-500 times, preferably 50-250 times, of the total void area of ​​the flow-disturbing plate.

[0013] Another aspect of the present invention provides a fluidized bed reactor comprising a reaction chamber, wherein the reaction chamber is provided with two or more flow-disturbing members arranged along the axial direction of the reactor, the flow-disturbing members conform to the cross-sectional shape of the reaction chamber, and the diameter D1 of the flow-disturbing members is substantially equal to the inner diameter D of the reaction chamber, wherein the flow-disturbing members are the flow-disturbing members according to the present invention described above, and the flow-disturbing members are preferably installed at equal intervals along the axial direction.

[0014] Another aspect of the present invention provides a circulating fluidized bed reactor comprising a reaction chamber, wherein a raw gas distributor is provided at the bottom end of the reaction chamber, and one or more solid-phase feed ports for circulating catalyst feed are provided on the chamber wall above the raw gas distributor, at least one of the solid-phase feed ports extends into the reaction chamber and is connected to a solid distribution member toward the center of the reaction chamber; the solid distribution member comprises a bottom plate and at least two side baffles mounted oppositely on the bottom plate, wherein the bottom plate and the side baffles together define a flow channel for solid distribution therethrough; wherein the flow channel is trapezoidal in shape, The upper base of the trapezoidal flow channel is connected to the solid-phase feed port and the bottom plate is tangent to the inner edge of the feed port; the angles between the waist and the lower base of the trapezoid of the flow channel are α1 and α2, and 30°≤α1<90°, preferably 45°≤α1≤75°, 30°≤α2<90°, preferably 45°≤α2≤75°; the length of the upper base of the trapezoid is j, and dg≤j≤2dg, preferably dg≤j≤1.5dg, where dg is the equivalent diameter of the solid-phase feed port; the height of the trapezoid is hh, and 0.01D≤hh≤0.2D, preferably 0.05D≤hh≤0.15D, where D is the inner diameter of the reaction chamber.

[0015] Yet another aspect of the present invention provides a circulating fluidized bed reactor comprising a reaction chamber, wherein a raw gas distributor is provided at the bottom end of the reaction chamber, and a plurality of solid-phase feed ports for circulating catalyst feeding are provided on the chamber wall above the raw gas distributor, wherein the plurality of solid-phase feed ports are respectively used to feed catalysts in the same or different states, including at least one Type I solid-phase feed port for a relatively large amount of solid feed, and at least one Type II solid-phase feed port for a relatively small amount of solid feed, wherein the geometric center of the Type I solid-phase feed port and the geometric center of the Type II solid-phase feed port are in a straight line in the vertical direction, or deviate by no more than 5°; the vertical distance between the geometric center of the Type II solid-phase feed port and the geometric center of the Type I solid-phase feed port is h, 0.5(dc+dz)≤h≤1.5dc, preferably 0.5(dc+dz)≤h≤dc, wherein: dc is the equivalent diameter of the Type I solid-phase feed port, and dz is the equivalent diameter of the Type II solid-phase feed port.

[0016] The present invention also provides the use of the flow-disturbing component or the fluidized bed reactor in methanol conversion to produce olefins, catalytic cracking or fluidized bed propane dehydrogenation.

[0017] The present invention also provides a method for producing olefins by converting methanol. The method adopts the reaction equipment described in the present invention, such as a fluidized bed reactor, and includes feeding methanol raw gas and multiple catalyst materials including a regeneration agent, a circulating agent, and an external heat extractor into the feed section. After the materials enter the equipment, they are carried by the gas phase and flow upward to form contact and react, thereby generating a gas-solid mixture containing light olefins. The gas-solid mixture is deflected after passing through the guide plate of the flow-disturbing component and flows radially. After continuing to pass through the array of disruptive fluids, a large number of negative pressure vortices are formed behind each disruptive fluid, and the turbulence intensity is increased. The nearby catalysts are carried and filled into the large number of vortices behind the disruptive fluids, so that the originally large number of relatively concentrated regeneration agents, circulating agents, external heat extractors, etc. are further dispersed in the cavity under the influence of the gas flow, the mixing degree between the multiple catalyst materials is significantly enhanced, the gas-solid contact efficiency is greatly increased, the reaction conditions in different areas of the equipment are close to each other, the generation of side reactions is suppressed, and the composition ratio of the target light olefins in the product gas is increased. The gas-solid mixture then continues to enter the separation chamber upward for gas-solid separation.

[0018] Furthermore, the use of specific solid distribution parts connected to the solid phase feed port prevents the solid phase particle group from gathering and falling near the wall surface, and helps each stream of solid phase material to be further dispersed after entering the reactor, thereby achieving better concentration distribution of catalyst on different horizontal planes and more uniform distribution of catalyst carbon deposits.

[0019] On this basis, the reaction equipment can be further optimized and adjusted from the Type II solid phase feed port (such as the regeneration agent feed port) for a relatively small amount of solid feed to just above the Type I solid phase feed port (such as the external heat extraction agent feed port) for a relatively large amount of solid feed, or deviate by no more than 5°. Although the feed amount of the regeneration agent is much smaller than the feed amount of the external heat extraction agent, the regeneration agent has a high temperature and low carbon deposition, and has high reaction activity. It is easy for the reaction selectivity to be affected by the excessively high local temperature in the reactor. By adjusting the feed to above the external heat extraction agent feed port, the fed regeneration agent will flow directly downward for a distance after entering the equipment due to inertia. During the inertial falling process, it can first be mixed with the external heat extraction agent with a flow rate much larger than its own, and merge into the large flow of the external heat extraction agent. It is then carried by the gas phase and dispersed, thereby maximizing the premixing of part of the catalyst in the equipment, which is beneficial to improving the initial distribution effect of the catalyst particles entering the equipment.

[0020] Through the above technical solution, the flow-disturbing member of the present invention can enhance mixing, achieving favorable material distribution and uniformity. Furthermore, the fluidized bed reactor of the present invention can significantly improve the mixing efficiency between multiple solid-phase materials and between gas and solid phases, reduce the unevenness of catalyst distribution per unit height cross-section, significantly reduce the carbon difference distribution on the cross-section, enhance gas-solid contact, promote the continuous production of light olefins, enhance the performance of the reactor, and thus improve the production efficiency, economy and environmental protection of the overall process.

[0021] The present invention also discloses the following embodiments:

[0022] Solution 1: A flow-disturbing component for mixing gas-solid two-phases, characterized in that the flow-disturbing component (15) comprises a flow-guiding portion and a mixing portion, wherein:

[0023] The guide portion includes a guide plate (20), and the guide plate (20) is used to allow the fluid containing gas and solid phases to flow toward the mixing portion;

[0024] The mixing section comprises a plurality of turbulent bodies (21), the plurality of turbulent bodies (21) being used to form vortices on the fluid to enhance the interphase disturbance between the gas and solid phases, and the plurality of turbulent bodies (21) being distributed at intervals around the guide plate (20).

[0025] Option 2: The flow-disturbing component according to Option 1 is characterized in that the mixing portion includes a plurality of flow-disturbing rings concentrically arranged around the guide plate (20) and spaced in sequence, each of the flow-disturbing rings including a plurality of flow-disturbing bodies (21) spaced in a ring shape along the circumference of the guide plate (20); preferably, the flow-disturbing body (21) is arranged as a vertically placed cylinder.

[0026] Solution 3: The flow-disturbing member according to Solution 2 is characterized in that the guide portion further comprises a guide for guiding the airflow at the edge of the mixing portion to the middle portion, preferably the guide is configured as an edge ring (22) connected to the largest-sized flow-disturbing ring, more preferably the width of the edge ring (22) is X, X≤D / 16, wherein when the flow-disturbing member (15) is installed in the cavity, the diameter of the cavity is D;

[0027] and / or

[0028] The guide plate (20) is provided with a plurality of air holes. Preferably, the opening rate of the guide plate (20) is less than 6%. More preferably, the cross section of the guide plate (20) is circular, and the diameter of the guide plate (20) is d b , 0.2D≤d b ≤0.6D;

[0029] and / or

[0030] The flow-disturbing ring with the smallest diameter is embedded and installed with the edge of the guide plate (20).

[0031] Option 4, a gas-solid reaction device, characterized in that the gas-solid reaction device includes a gas-solid reactor (1), the gas-solid reactor has a connected reaction chamber (6) and a separation chamber (2), wherein the reaction chamber (6) includes a feed section and a spoiler section located above the feed section, and at least one spoiler component (15) described in any one of Options 1-3 is installed in the spoiler section, and preferably, a plurality of the spoiler components (15) are installed in the reaction chamber (6) at equal intervals along the axial direction.

[0032] Solution 5. The reaction equipment according to Solution 4 is characterized in that a raw gas distributor (8) is provided at the bottom end of the feed section, a solid phase feed port is provided on the cavity wall of the feed section above the raw gas distributor (8), and a distribution member (17) is provided in the reaction chamber, and the distribution member (17) is used to disperse the solid phase fed from the solid phase feed port in the feed section;

[0033] Preferably, the distribution member (17) includes a corrugated plate (18) and side baffles (19) installed on the corrugated plate (18) at intervals;

[0034] More preferably,

[0035] The front end area of ​​the corrugated plate (18) is provided with a plurality of distribution holes, and the opening rate of the corrugated plate (18) is 5% to 10%;

[0036] and / or

[0037] The cross section of the corrugated plate (18) is in the shape of an isosceles trapezoid, and the large end of the corrugated plate (18) extends toward the center of the feeding section.

[0038] Solution 6: The reaction equipment according to Solution 5, characterized in that 45°≤β≤α≤75°, wherein β is the angle between the side and bottom of the corrugated plate (18), and α is the angle between the side baffle (19) and the bottom of the corrugated plate (18);

[0039] and / or

[0040] j≥0.5k, wherein the length of the small end of the corrugated plate (18) is k, and the spacing between the side baffles (19) close to the small end of the corrugated plate (18) is j.

[0041] Scheme 7. The reaction equipment according to Scheme 5 is characterized in that the solid-phase feed port is used to feed the catalyst, and includes an external heat-extraction agent inlet (7) and a circulating agent inlet spaced apart along the circumferential direction on the cavity wall of the feed section; wherein a regeneration agent inlet (10) is provided in the cavity wall just above the external heat-extraction agent inlet, and the distance between the regeneration agent inlet (10) and the external heat-extraction agent inlet (7) is h, preferably 0.5 (d c +d z )≤h≤1.5d c , d c is the equivalent diameter of the external heat extractor inlet (7), d z is the equivalent diameter of the regenerant inlet (10);

[0042] and / or

[0043] The solid-phase feed port is provided with the distribution member (17), and the side baffle (19) of the distribution member (17) has a height of L, wherein the range of L is 0.2 to 0.5 times the equivalent diameter of the solid-phase feed port;

[0044] Preferably, the external heat extracting agent inlet (7) is provided with the distribution member (17), 0.2d c ≤L≤0.5d c ;

[0045] and / or

[0046] The distance between the regeneration agent inlet and the flow-disturbing component (15) is 0.3m to 0.6m.

[0047] Application of the flow-disturbing component (15) described in any one of Scheme 8, Schemes 1-3, or the reaction equipment described in any one of Schemes 4-7 in methanol conversion to produce olefins, catalytic cracking, or fluidized bed propane dehydrogenation.

[0048] Scheme 9, a method for producing olefins by converting methanol, characterized in that the method adopts the reaction equipment described in any one of Schemes 4-7, including feeding methanol raw gas (f) and catalyst into the feed section, allowing the methanol raw gas (f) to contact the catalyst and react to generate a gas flow containing low-carbon olefins, and allowing the gas flow containing low-carbon olefins to pass upward through the disrupting component (15) to form turbulence to enhance the phase disturbance between the gas and solid phases, and then continue to enter the separation chamber (2) upward for gas-solid separation.

[0049] Scheme 10: The method according to Scheme 9, wherein the methanol raw gas (f) is preheated and fed into the feed section through a raw gas distributor (8), wherein the preheating temperature is 150-200°C, and the gas superficial velocity u of the methanol raw gas (f) entering the feed section is f 0.8-2.0m / s;

[0050] and / or

[0051] The catalyst includes a catalyst g returned after heat extraction from an external heat extractor inlet, a circulating catalyst r fed from a circulating agent inlet, and a regenerated catalyst z fed from a regenerated agent inlet;

[0052] and / or

[0053] The catalyst enters the feed section through a distribution piece, and preferably the catalyst g returned after heat removal enters the feed section through the distribution piece;

[0054] and / or

[0055] The average concentration of the catalyst in the reaction chamber is 60-120 kg / m 3 , preferably 80-115kg / m 3 and / or

[0056] The reaction temperature in the reaction chamber (6) is 450-500° C., and the reaction pressure is 0.01-1 MPa.

[0057] Other features and advantages of the present invention will be described in detail in the following detailed description. BRIEF DESCRIPTION OF THE DRAWINGS

[0058] The accompanying drawings are used to provide a further understanding of the present application and constitute a part of the specification. Together with the following detailed description, they are used to explain the present application but do not constitute a limitation of the present application. In the accompanying drawings:

[0059] FIG1a is a schematic structural diagram of a spoiler according to a specific embodiment of the present invention;

[0060] FIG1b is a partial schematic diagram of the spoiler member shown in FIG1a;

[0061] 2a and 2b are schematic diagrams of the distribution of air holes on a guide plate according to some specific embodiments of the present invention;

[0062] 3a-d are schematic structural diagrams of body disruptors with different horizontal cross-sectional shapes according to some specific embodiments of the present invention;

[0063] FIG4 is a schematic structural diagram of a gas-solid reaction device according to a specific embodiment of the present invention;

[0064] FIG5 is a schematic structural diagram of a solid distribution member according to a specific embodiment of the present invention;

[0065] 6 is a top view of a solid distribution member and a schematic diagram of the distribution of distribution holes thereof according to a specific embodiment of the present invention;

[0066] 7 is a side view of a solid distribution member and a solid phase feed port according to a specific embodiment of the present invention;

[0067] 8 is a schematic structural diagram of the arrangement of a solid phase feed port and a solid distribution member in a feeding section of a circulating fluidized bed reactor according to a specific embodiment of the present invention;

[0068] FIG9 is a schematic structural diagram of an MTO continuous reaction regeneration fluidized bed device according to the prior art;

[0069] FIG10 is a schematic structural diagram of an oblique baffle-type spoiler component according to the prior art;

[0070] FIG11 is a schematic structural diagram of a flat baffle-type solid distribution member according to the prior art.

[0071] The components in the drawings are not necessarily drawn to scale, emphasis instead being placed on illustrating the principles of the embodiments. In different drawings or views, the same reference numerals designate the same or corresponding components.

[0072] Description of Reference Numerals

[0073] 1. Gas-solid reactor; 2. Separation chamber; 3. Riser; 4. External heat exchanger; 5. Circulating agent feed port; 6. Reaction chamber; 7. External heat exchanger feed port; 8. Raw gas distributor; 9. Circulating agent feed port; 10. Regeneration agent feed port; 11. Fluidising air distributor; 12. Regeneration agent pipe; 13. Degassing tank; 14. Catalyst regenerator; 15. Flow disruptor; 16. Catalyst fine powder feed port; 17. Solid distribution member; 18. Bottom plate; 19. Side baffle; 20. Guide plate; 21. Flow disruptor; 22. Side ring; 23. Support plate; 24. Rib plate; 25. Wall surface. DETAILED DESCRIPTION

[0074] The following describes the specific embodiments of the present application in detail with reference to the accompanying drawings. It should be understood that the specific embodiments described herein are only used to illustrate and explain the present application and are not intended to limit the present application.

[0075] All publications, patent applications, patents, and other references mentioned in this specification are incorporated herein by reference. Unless otherwise defined, all technical and scientific terms used in this specification have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. In the event of conflict, the present specification, including definitions, will control.

[0076] When this specification uses the words "known to those skilled in the art" or "commonly known in the art" or similar terms to describe materials, methods, components, devices or equipment, this term means that this specification includes those commonly used in the art at the time this application was filed, but also includes those that are not commonly used at present but will become recognized in the art as being suitable for similar purposes.

[0077] The endpoints of the ranges and any values ​​disclosed herein are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoints of each range, the endpoints of each range and individual point values, and the individual point values ​​can be combined with each other to obtain one or more new numerical ranges, and these numerical ranges should be considered to be specifically disclosed herein.

[0078] In the present invention, when a technical solution is presented in the form of an open-ended limitation such as "comprising" or "including" certain listed elements, those skilled in the art will understand that an embodiment consisting of or consisting essentially of these elements can obviously be used to implement the technical solution. Therefore, those skilled in the art will understand that the technical solution presented in the present invention in the form of an open-ended limitation also covers a specific embodiment consisting of or consisting essentially of the listed elements.

[0079] In the present invention, " scope " is provided in the form of lower limit and upper limit, for example one or more lower limits and one or more upper limits.Given range can be limited by selecting a lower limit and an upper limit, and selected lower limit and upper limit define the boundary of given range.All scopes limited in this way are included and combinable, and promptly any lower limit can form a scope with any upper limit combination.For example, the scope of 60-110 and 80-120 is listed for specific parameters, and it is also expected to be understood that the scope of 60-120 and 80-110.In addition, if the lower limit listed is 1 and 2 and the upper limit listed is 3,4 and 5, then the following scope is all expected to be: 1-3, 1-4, 1-5, 2-3, 2-4 and 2-5.

[0080] Unless otherwise specified, all percentages, parts, ratios, etc. mentioned in this specification are based on weight; however, if the weight basis does not conform to the common knowledge of those skilled in the art, the basis shall be determined by the common knowledge of those skilled in the art.

[0081] In the present invention, unless otherwise specified, the directional words used, such as "up, down, top, bottom", are usually used with reference to the directions shown in the drawings or are used to describe the relative positional relationships of the components in the vertical, perpendicular or gravity directions. "Inside" and "outside" usually refer to the radial inside and outside relative to the center of a circle or the inside and outside of a cavity relative to the cavity.

[0082] In the present invention, vortex refers to the phenomenon that the boundary layer near the wall of the disturbing fluid separates after the air flow passes through the disturbing fluid and forms a negative pressure, causing the nearby fluid to flow back to fill the original space to form a vortex. The vortex is beneficial to the mass transfer and heat transfer of the reaction process.

[0083] In the present invention, the annular core effect refers to the process in which the gas phase in the fast fluidized bed gradually gathers at the center of the bed while entraining the solid phase and flowing upward, and the particles carrying the accessories move upward, while the catalyst particles in the near-wall area away from the center area are relatively gathered to form a downward movement, thereby forming a circulating flow between the near-center and near-wall surfaces of the equipment for mass and heat transfer.

[0084] In the present invention, when referring to the "equivalent diameter" of a solid phase feed port, it generally refers to the inner diameter of the solid phase feed port, unless otherwise specified.

[0085] A fluidized bed generally involves at least two phases, gas and solid, and generally involves mixing of the two phases, and is therefore a typical gas-solid reaction device. It will be readily understood that, in the present invention, when used as a fluidized bed reactor, the fluidized bed generally contains at least one reaction chamber. For the purposes of the present invention, when, in addition to the upward and downward movement of solids in the fluidized zone due to fluidization, a dedicated solid circulation channel (generally located outside the fluidized bed) is established to transport solids (e.g., catalyst particles) (especially, for example, in the direction opposite to the movement caused by fluidization), the fluidized bed thus constructed may be referred to as a "circulating fluidized bed" for the purposes of the present invention. For example, in a fluidized bed reactor in the form of a riser, catalyst particles are transported upward and concentrated in the upper portion of the riser. To this end, a circulating (catalyst) agent pipeline can be connected to the outside of the riser to transport catalyst from the upper portion of the riser back to the lower portion of the riser, thereby constructing a circulating fluidized bed reactor.

[0086] Accordingly, for the purposes of the present invention, the solid circulation channel can be a simple pipeline or a complex pipeline or system with other devices installed at appropriate locations. For example, for a fluidized bed, a simple bypass can be provided relative to the fluidized bed so that solids flow in the opposite direction relative to the flow direction of the fluidized bed; this simple bypass is the solid circulation channel described in the present invention. For another example, for an ascending fluidized bed, a portion of the deactivated catalyst can be removed from the upper portion and regenerated in a regenerator to obtain the "regenerated agent" described in the present invention, which is then transported back to the lower portion of the fluidized bed; this system with a regenerator can be considered as the solid circulation channel described in the present invention. For another example, for the purpose of heat exchange (e.g., heat extraction), a portion of the catalyst in the fluidized bed reactor is removed and heat exchanged in a heat exchanger (e.g., a heat extractor) to obtain the "external heat exchange catalyst (external heat extractor)" described in the present invention, which is then transported back to the fluidized bed in the opposite direction of the flow direction of the fluidized bed; this system with a heat exchanger can be considered as the solid circulation channel described in the present invention. For example, the gas outlet of the fluidized bed may entrain some solids, and the solids can generally be separated by a separation device (such as a cyclone separator) to obtain the "catalyst fine powder" described in the present invention, and the catalyst fine powder is returned to the fluidization; the system with the separation device can be regarded as the solid circulation channel described in the present invention.

[0087] Therefore, any catalyst particles that can be transported through an appropriate circulation channel can be referred to as "recycled catalyst" in the present invention. For example, the regeneration agent, external heat exchange catalyst (external heat extraction agent), and catalyst fines can all be considered "recycled catalyst" for the fluidized bed as described herein. In particular, catalyst transported through a simple bypass of the fluidized bed is also a "recycled catalyst" and can be referred to as "circulating agent" in the present invention.

[0088] Accordingly, for a fluidized bed, satisfactory mixing of the gas-solid phase is very important, especially when using a recycled catalyst. On the one hand, good gas-solid mixing can ensure that the solid-phase catalyst is in full contact with the gas-phase reactants, thereby accelerating the reaction rate and improving the overall operating efficiency of the fluidized bed. On the other hand, mixing uniformity directly affects the uniformity and quality stability of the product. If the mixing is uneven, it may cause fluctuations in product performance, affecting the quality of the final product. On the other hand, the recycling of the catalyst in the fluidized bed is an important embodiment of its economic efficiency. Good mixing can reduce catalyst wear and coking, thereby extending its service life. Therefore, for a fluidized bed (especially a circulating fluidized bed), it is often necessary to appropriately adjust the distribution of solids, gases, or both in the fluidized bed (especially for a fluidized bed reactor, the distribution in the reaction chamber). To this end, the present invention provides a fluidized bed with a specific structure. For the purposes of the present invention, for ease of understanding, "solid phase" and "solid" are used interchangeably, and "gas" and "gas phase" are used interchangeably.

[0089] In embodiment A of the present invention, the present invention provides, on the one hand, a flow-disturbing member 15, which includes a flow-guiding portion and a mixing portion coaxially distributed in the radial direction, or is composed of the flow-guiding portion and the mixing portion; on the other hand, a fluidized bed reactor is provided, in which a reaction chamber is provided with two or more flow-disturbing members 15 arranged along the axial direction of the reactor.

[0090] In embodiment B of the present invention, the present invention provides a circulating fluidized bed reactor, wherein a solid distribution member 17 is connected to the solid phase feed port for circulating catalyst, and the solid distribution member 17 includes a bottom plate 18 and at least two side baffles 19 relatively mounted on the bottom plate 18, wherein the bottom plate 18 and the side baffles 19 together define a flow channel for solid distribution therethrough, and the flow channel is trapezoidal in shape.

[0091] In embodiment C of the present invention, the present invention provides a circulating fluidized bed reactor, which includes a plurality of solid-phase feed inlets specifically arranged on the wall of the reaction chamber of the reactor, including at least one Type I solid-phase feed inlet for a relatively large amount of solid feed, and at least one Type II solid-phase feed inlet for a relatively small amount of solid feed, wherein the geometric center of the Type I solid-phase feed inlet and the geometric center of the Type II solid-phase feed inlet are vertically aligned, or deviate by no more than 5°.

[0092] In the present invention, the embodiments A, B and C can be combined with each other to form, for example, embodiment A+B, embodiment A+C, embodiment B+C, and embodiment A+B+C.

[0093] Implementation Plan A

[0094] According to embodiment A, the present invention provides a flow-disturbing member 15, which is particularly suitable for a fluidized bed reactor to promote gas-solid two-phase mixing. As shown in Figure 1a, the flow-disturbing member 15 includes a flow-guiding portion and a mixing portion coaxially distributed in the radial direction, or is composed of the flow-guiding portion and the mixing portion.

[0095] In one embodiment, the guide portion of the spoiler member 15 of the present invention includes a guide plate 20, which has at least 3, at least 7, or at least 19 basically evenly distributed air holes, and the total porosity of the openings of the guide plate is 0.2%-6%, preferably 1.5%-4.5%.

[0096] That is, one of the specific solutions of the present invention is to set an obstacle to the fluidization direction in the central area of ​​the fluidized bed. Therefore, for the fluidized bed reactor described in the present invention, when the solid-carrying gas flow (also referred to as gas-solid mixture in the present invention) moves to the guide plate 20, due to resistance, a large part of the gas flow is adjusted to flow radially into the mixing section; but at the same time, the guide plate 20 is opened with holes with an appropriate porosity, so that part of the gas (and even part of the solid) can still pass through the guide plate through the air holes. It can be understood that such a structure makes the disturbance between the gas and solid phases at the guide plate more conducive to the mixing required by the present invention. Without being limited to any known theory, through repeated experiments and simulation calculations, it is believed that the total porosity of the guide plate is 0.2%-6%, preferably 1.5%-4.5%, which is particularly advantageous for achieving the purpose of the present invention (such as satisfactory gas-solid two-phase mixing).

[0097] It is understood by those skilled in the art that, for the purposes of the present invention, when referring to objects with relatively regular geometric shapes such as holes, plates, and disrupting bodies, their relative positional relationships (e.g., arrangement positions) have the usual meaning in the art, for example, they may refer to the relative positional relationships between the geometric centers or centers of gravity (e.g., centers of circles) of these objects.

[0098] For the purposes of the present invention, the term "substantially uniform" distribution of the air holes has the conventional technical meaning as understood by those skilled in the art, such as the centers of the holes being uniformly distributed on the guide plate in the conventional sense in the art, such as the distances between adjacent centers being substantially equal and the air holes being uniformly distributed across the entire guide plate. However, this does not exclude the possibility that one or more air holes at, for example, the edge of the guide plate may be spaced at similar, but not equal, distances between the centers of the other air holes. It is understood that those skilled in the art can clearly determine whether the distribution of the air holes is "substantially uniform" as conventionally understood in the art based on actual circumstances and general knowledge in the art.

[0099] For the purposes of the present invention, the "porosity" of an object refers to the percentage of the total area of ​​a cross-section of the object that is not occupied by a solid object, thereby allowing at least gas to pass through. For example, it is understood that for a plate with holes, the porosity is the percentage of the sum of the areas of all holes to the total area of ​​the plate.

[0100] In one embodiment, the diameter of the guide plate 20 of the spoiler member 15 of the present invention is d b , 0.2D1≤d b ≤0.6D1, preferably 0.3D1≤d b ≤0.5D1. Preferably, the outer diameter of the mixing portion is D1; ​​that is, preferably, the diameter of the largest flow-disturbing ring of the mixing portion is the outer diameter of the flow-disturbing member 15. Preferably, the inner diameter of the mixing portion is d b; That is to say, it is preferred that the turbulent flow ring with the smallest size in the mixing section is directly connected to the guide plate 20, and there are no other components between the two. One of the main purposes of the present invention is to improve the mixing between the gas and solid phases. As mentioned above, arranging the guide plate 20 in the central area of ​​the fluidized bed is one of the important technical means, which forms an obstacle to the fluidization direction; however, it is understandable that such an obstacle needs to exist to an appropriate extent, for example, it cannot make the fluidization state unable to be maintained. Among various factors, the diameter of the guide plate 20 is therefore one of the important parameters. For example, it is obviously not equal to or substantially equal to the inner diameter D of the reaction chamber. Without being limited to any known theory, it is believed that the above-mentioned specific diameter d of the guide plate is verified by repeated experiments and simulation calculations. b This is particularly advantageous for achieving the objectives of the present invention (eg, desirable gas-solid two-phase mixing).

[0101] In one embodiment, the diameter of the openings of the air holes on the guide plate 20 of the flow-disturbing member 15 of the present invention is 5-50 mm, preferably 10-40 mm, and more preferably 15-20 mm; and preferably, the diameters of each air hole are substantially equal. For the purposes of the present invention, the diameters of the air holes are "substantially equal" means that the diameters of the air holes differ by no more than 10%, preferably no more than 5%, and more preferably no more than 1%. As previously mentioned, the air holes in the guide plate 20 are appropriately opened so that some gas (and even some solids) can still pass through the guide plate via the air holes. Accordingly, the diameter of the air holes needs to be appropriately adjusted, in particular to match the catalyst diameter. Without being limited by any known theory, through repeated experiments and simulation calculations, it is believed that the above-mentioned specific air hole diameters of the guide plate are particularly advantageous for achieving the objectives of the present invention (e.g., satisfactory gas-solid two-phase mixing). On the other hand, the inventors have found that, for the fluidized bed of the present invention, uniformity of the air holes will further improve the mixing effect of the gas-solid two-phase. Therefore, it is preferred that the diameters of the various air holes are substantially equal. Similarly, another embodiment of the uniformity of the air holes of the present invention is the regular arrangement of the air holes. Accordingly, in one embodiment, the multiple air holes on the guide plate 20 of the spoiler member 15 of the present invention are regularly arranged. In one embodiment, as shown in FIG2a , the air holes are arranged in an equilateral triangle with equal spacing between each other. In one embodiment, as shown in FIG2b , the air holes are arranged in an equidistant annular array with the center of the guide plate 20 as the center of the circle. For the purpose of the present invention, there is no particular limitation on the specific spacing between the air holes, as long as the air hole diameter and the total porosity of the guide plate described in the present invention can be met. For example, the spacing between the air holes can be 100-800 mm, preferably 200-500 mm.

[0102] Furthermore, those skilled in the art will appreciate that, for a perforated deflector plate 20, the number and diameter of its pores contribute to the deflector plate's total porosity. Through repeated experiments and simulations, the inventors surprisingly discovered that the pore diameter and the deflector plate's total porosity are relatively important for the objectives of the present invention (e.g., achieving satisfactory gas-solid two-phase mixing). In contrast, the number of pores is not particularly limited and can be appropriately adjusted by those skilled in the art, as long as it meets the requirements of the present invention regarding pore diameter, total deflector plate porosity, and substantially uniform pore distribution.

[0103] For the fluidized bed reactor described in the present invention, especially the fluidized bed reactor of embodiment A, when the airflow carrying solids moves to the guide plate 20, due to resistance, a large part of the airflow is adjusted to flow radially into the mixing section. Therefore, the mixing section needs to be provided with a higher void ratio to facilitate the airflow carrying solids to continue to pass in a fluidized state. On the other hand, according to the present invention, in the mixing section, a large number of vortices are formed after the airflow passes through the disturbing fluid 21, causing interphase disturbance; when the solid phase (such as catalyst particles) passes through the mixing section, the probability of collision between the solid phases and between the solid phase and the disturbing fluid 21 is greatly increased, which promotes mixing between different solid phases and between gas and solid phases. In other words, it is very advantageous to properly arrange a disturbing fluid in the mixing section, and its space must be at least partially occupied by the disturbing fluid. Accordingly, the total void ratio of the mixing section cannot be too high. Thus, in one embodiment, the mixing portion of the flow-disturbing member 15 of the present invention surrounds the flow-guiding portion and includes at least two concentrically arranged flow-disturbing rings, each of which is provided with at least six evenly distributed flow-disturbing bodies 21, the flow-disturbing bodies 21 having non-porous surfaces, and the presence of these flow-disturbing bodies makes the total porosity of the mixing portion less than 95%, preferably less than 90%, and also preferably less than 80%; and greater than 30%, preferably greater than 40%, and also preferably greater than 60%.

[0104] In one embodiment, the mixing section of the present invention includes 2-10 fluid turbulence rings, preferably 3-8, concentrically arranged and spaced apart from each other around the guide plate 20. Preferably, the spacing between the fluid turbulence rings is equal. As previously mentioned, the mixing section of the present invention is used to allow the solids-laden airflow to continue to pass through in a fluidized state and cause phase disturbances therein; therefore, the fluid turbulence rings need to be appropriately distributed. Through repeated experiments and simulation calculations, it is believed that the fluid turbulence rings are advantageously arranged in the aforementioned number and preferably at equal spacing.

[0105] As mentioned above, in the mixing section, a large number of vortices are formed after the airflow passes through the disrupting fluid 21, causing phase disturbance. In this regard, the inventors have found through experiments that the disrupting fluid and its distribution have appropriate "uniformity" which is also conducive to the realization of the purpose of the present invention (such as satisfactory gas-solid two-phase mixing). Accordingly, in one embodiment, the disrupting fluid 21 of the present invention has the same shape. According to the present invention, a large number of vortices are formed after the airflow passes through the disrupting fluid 21, causing phase disturbance; therefore, it can be understood that the size and shape of the disrupting fluid 21 itself have an influence on the formation of vortices and the result of phase disturbance. Accordingly, in one embodiment, the aspect ratio of the disrupting fluid 21 is preferably 3:1-10:1, preferably 4:1-8:1. Preferably, the equivalent diameter of the horizontal cross section of the disrupting fluid 21 is 10-150mm, preferably 10-100mm, and the shape of the horizontal cross section is selected from rectangle, square, circle, ellipse and rhombus. Figures 3a-d show schematic structural diagrams of disrupting fluids with circular, elliptical, square and rhombus horizontal cross-sectional shapes, respectively. When the horizontal cross-section of the disruptor is elliptical, the aspect ratio of the disruptor is the ratio of the height of the disruptor to the minor axis of the ellipse. When the horizontal cross-section of the disruptor is rectangular, the aspect ratio of the disruptor is the ratio of the height of the disruptor to the minor side of the rectangle. Preferably, the disruptor is arranged vertically; accordingly, the "horizontal cross-section" refers to a cross-section taken along the length of the disruptor.

[0106] As previously mentioned, for the gas-solid mixture fluidized in the fluidized bed, the present invention is through the specific arrangement of the guide plate and the fluid-disturbing ring in the flow-disturbing member 15, so that the gas-solid mixture originally in the fluidized direction in the central area of ​​the reactor is adjusted to flow radially into the mixing section, and causes interphase disturbance here. Therefore, the ratio of the total void area of ​​the fluid-disturbing ring to the guide plate has a further impact on the flow and disturbance of the gas-solid mixture. Not being limited to any known theory, through repeated experiments and simulation calculation verification, it is believed that for achieving the purpose of the present invention (such as desirable gas-solid two-phase mixing) it is particularly advantageous that the total void area of ​​the mixing section described in the present invention is 30-500 times, preferably 50-250 times, of the total void area of ​​the guide plate.

[0107] In one embodiment, the guide portion of the present invention further includes a guide member for guiding the material at the edge of the mixing portion to the middle portion, and the guide member is preferably configured as an edge ring 22 connected to the largest size of the fluid-disturbing ring, and the width of the edge ring 22 is X, preferably D1 / 64 ≤ X ≤ D1 / 16, more preferably D1 / 50 ≤ X ≤ D1 / 20.

[0108] According to embodiment A, the present invention provides a fluidized bed reactor comprising a reaction chamber, wherein the reaction chamber is provided with two or more flow-disrupting members 15 as defined above arranged along the axial direction of the reactor, the flow-disrupting members 15 conforming to the cross-sectional shape of the reaction chamber, and the diameter D1 of the flow-disrupting members 15 is substantially equal to the inner diameter D of the reaction chamber; wherein, for the purposes of the present invention, it is understood by those skilled in the art that the D1 is substantially equal to the D, meaning that for the purpose of enabling actual installation, the value of the D1 is less than but as close to the D as possible when the actual process permits, and the specific degree of closeness and difference between the two can be determined by those skilled in the art according to actual conditions and based on the general understanding of the art. For example, the D1 can be no less than 1% or no more than 0.5% smaller than the D.

[0109] In one embodiment, the structures of the two or more flow-disturbing members 15 of the present invention are the same or different. As previously mentioned, the present invention applies a strong disturbance to the gas-solid mixture in the fluidized state by the flow-disturbing member. Similar to the uniformity of the various components on the flow-disturbing member, the uniformity between the flow-disturbing members is also conducive to achieving the desired purpose of the present invention in a predictable manner to a certain extent. Therefore, in one embodiment, it is preferred for the present invention to use multiple identical flow-disturbing members.

[0110] The present invention relates to a fluidized bed reactor (such as embodiment A), and can be, for example, a circulating fluidized bed reactor (such as embodiments B and C); Accordingly, according to the present invention, a solid phase feed can be involved in a fluidized bed reactor. Preferably, the reactor has at least one solid phase feed port, and the first flow disruptor from bottom to top in the reactor is arranged above all solid phase feed ports, 0.2-1.5m from the geometric center of the topmost solid phase feed port, preferably 0.5-1.2m. As previously mentioned, the present invention applies strong disturbance to the gas-solid mixture of fluidized state by the flow disruptor. Accordingly, in order to better act between the flow disruptor and the fluidized gas-solid mixture, after experimental verification, it is not only necessary to arrange all flow disruptors above all solid phase feed ports, but also to appropriately set the distance between the first flow disruptor and the topmost solid phase feed port. Verified by repeated experiments and simulation calculations, it is believed that the above-mentioned specific distance is particularly advantageous for achieving the purpose of the present invention (such as desirable gas-solid two-phase mixing). Similarly, in order to facilitate the purpose of the present invention (such as satisfactory gas-solid two-phase mixing), it has been verified through repeated experiments and simulation calculations that the two or more spoiler members 15 of the present invention are preferably installed at equal intervals, and the installation spacing ΔH is also preferably 0.5m≤ΔH≤1.5m.

[0111] When the flow-disturbing member 15 is installed in the cavity of the reaction chamber, during the movement of the airflow, there is a situation where the solid phase concentration near the cavity wall is higher due to the ring-core effect. According to a preferred embodiment of the present invention, in order to guide the particles near the wall to flow toward the center and increase the gas-solid contact, the guide portion also includes a guide for guiding the material at the edge of the mixing portion to the middle, and the guide is preferably set as an edge ring 22 connected to the largest flow-disturbing ring, and the width of the edge ring 22 is X, preferably D / 64≤X≤D / 16, more preferably D / 50≤X≤D / 20, wherein D is the inner diameter of the reaction chamber. In one embodiment, the cross section of the guide plate 20 is preferably circular, and the diameter of the guide plate 20 is d b , 0.2D≤d b ≤0.6D.

[0112] In an exemplary embodiment, as shown in FIG1a, the flow-disturbing member 15 includes a flow-disturbing portion and a mixing portion coaxially distributed in the radial direction. The flow-disturbing portion includes a flow-disturbing plate 20 and a side ring 22 for guiding the material at the edge of the mixing portion to the middle. The flow-disturbing plate 20 is provided with a plurality of substantially evenly distributed air holes. The mixing portion surrounds the flow-disturbing portion and includes six flow-disturbing rings concentrically arranged around the flow-disturbing plate 20 and spaced in sequence. Among them, the flow-disturbing ring with the smallest diameter is embedded and installed with the edge of the flow-disturbing plate 20. Each flow-disturbing ring includes a plurality of flow-disturbing bodies 21 arranged in an annular shape at intervals along the circumference of the flow-disturbing plate 20. The flow-disturbing body 21 is configured as a vertically arranged cylinder so that the airflow forms a vortex after passing through the cylindrical arc surface, making the gas-solid two-phase mixing more uniform. It is understandable that the shape of the flow-disturbing body of the present invention is not limited to a cylinder, and any shape that can form a vortex in the airflow is acceptable. As shown in Figures 1a-b, the fluid-disturbing bodies on the same fluid-disturbing body ring can be connected by circumferential ribs to provide support for the fluid-disturbing body and fix their spacing, and the fluid-disturbing bodies in the same radial direction on different fluid-disturbing body rings can be connected by radial ribs to provide support for the fluid-disturbing body ring and fix their spacing. There is no particular restriction on the number of ribs connecting the fluid-disturbing bodies, and those skilled in the art can set them appropriately as long as they meet the conditions of the present invention regarding the total porosity and total void area of ​​the mixing portion, the spacing between the fluid-disturbing body and the fluid-disturbing body ring is fixed so that their distribution is substantially uniform, etc.

[0113] On the basis of the aforementioned flow-disturbing member 15 and the fluidized bed reactor according to embodiment A, the present invention discloses a gas-solid reaction device on the other hand. As shown in Figure 4, the gas-solid reaction device includes a gas-solid reactor 1, for example, a fluidized bed reactor according to embodiment A, a circulating fluidized bed reactor according to embodiments B and C. The gas-solid reactor 1 has a connected reaction chamber 6 and a separation chamber 2 located above the reaction chamber 6, and a gas phase outlet p is opened at the top of the separation chamber 2. Wherein, the reaction chamber 6 includes a feed section and a flow-disturbing section located above the feed section, and a plurality of flow-disturbing members 15 are installed in the flow-disturbing section at equal intervals along the axial direction.

[0114] Since the gas-solid reaction device of the present invention includes the flow-disturbing member 15 of the present invention, it also has the above-mentioned advantages of the flow-disturbing member.

[0115] Implementation Plan B

[0116] According to embodiment B, the present invention provides, on the one hand, a solid distribution member 17 for solid feed, which is particularly suitable for a circulating fluidized bed reactor to promote the distribution of the solid feed, the mixing of the solid feed with (if any) other solid feeds, and the mixing of the solid feed with the fluidizing medium.

[0117] According to embodiment B, another aspect of the present invention provides a circulating fluidized bed reactor, as shown in FIG4 . A raw gas distributor 8 is provided at the bottom end of the reactor's reaction chamber. One or more solid-phase feed ports, preferably 1-5 solid-phase feed ports, are provided on the chamber wall of the feed section above the raw gas distributor 8 for feeding circulating catalyst. At least one of the solid-phase feed ports extends into the reaction chamber and is connected to the solid distribution member 17 toward the center of the reaction chamber. In this way, the gaseous raw material fed from the bottom contacts the solid phase in a reverse direction, forming an airflow carrying the solid phase upward. The solid distribution member 17 is used to disperse the solid phase fed from the solid-phase feed port in the feed section.

[0118] As mentioned above, for a circulating fluidized bed reactor, it generally involves the recycling of the catalyst. Regardless of the purpose for which the catalyst is recycled, the feeding of the recycled catalyst back to the reactor is involved. Here, an upward fluidized bed is taken as an example. The recycled catalyst is generally taken out from the upper part of the fluidized bed reactor, and after optional intermediate treatment, it is returned to the feed section of the lower part of the fluidized bed reactor through one or more solid-phase feed ports for feeding the circulating catalyst. To this end, after in-depth research, the inventors found that at least one of the solid-phase feed ports is connected to a specific solid distribution member 17, and the recycled catalyst is transported to the reaction chamber through the solid distribution member 17, which will be particularly beneficial to the distribution of the recycled catalyst in the reaction chamber and its mixing with other materials.

[0119] In one embodiment, as shown in FIG5 , the solids distribution member 17 of the present invention comprises a bottom plate 18 and at least two side baffles 19 mounted oppositely to the bottom plate 18, wherein the bottom plate 18 and the side baffles 19 together define a flow channel for solids distribution therethrough; wherein the flow channel is preferably in the shape of a trapezoid, such as an isosceles trapezoid, wherein the upper base of the trapezoidal flow channel is connected to the solids feed port and the bottom plate is tangent to the inner edge of the feed port. For the purposes of the present invention, when referring to a "trapezoid," and corresponding terms such as upper base, lower base, and height, they have their conventional geometric meanings.

[0120] To facilitate the distribution of the recycled catalyst in the reaction chamber and its mixing with other materials, the trapezoid in the present invention has a special design. Specifically, as shown in Figure 6, the angles between the waist and the lower base of the trapezoid of the flow channel are α1 and α2, and 30° ≤ α1 < 90°, preferably 45° ≤ α1 ≤ 75°, 30° ≤ α2 < 90°, preferably 45° ≤ α2 ≤ 75°; the length of the upper base of the trapezoid is j, and dg ≤ j ≤ 2dg, preferably dg ≤ j ≤ 1.5dg, where dg is the equivalent diameter of the solid-phase feed inlet; the height of the trapezoid is hh, and 0.01D ≤ hh ≤ 0.2D, preferably 0.05D ≤ hh ≤ 0.15D, where D is the inner diameter of the reaction chamber. Through repeated experiments and simulation calculations for verification, the inventors found that the specific α1 and α2 angles can make the solid-phase feed more dispersedly distributed in the reaction chamber; and at the same time, it will not waste the space of the trapezoidal flow channel and will not have an obvious impact on the fluidization and reaction in the reaction chamber. Similarly, through repeated experiments and simulation calculations for verification, the inventors found that the specific upper base length j and height hh can facilitate the effective distribution of substantially all the solid-phase feed via the solid distribution member (17), and at the same time will not have an obvious impact on the fluidization and reaction in the reaction chamber.

[0121] As described above, the trapezoidal flow channel of the present invention is defined by the bottom plate (18) and the side baffle (19) together. Therefore, the structure and shape of the bottom plate (18) can also affect the fluidization and reaction in the reaction chamber; while the structure and shape of the side baffle can affect the effective distribution of the solid-phase feed, the fluidization and reaction in the reaction chamber.

[0122] Correspondingly, in one embodiment, as shown in Figure 6, the bottom plate (18) is also trapezoidal, for example, in the shape of an isosceles trapezoid, its upper base is collinear with the upper base of the flow channel, and the lengths of its upper base and lower base are respectively greater than those of the upper base and lower base of the flow channel, and it has the same symmetry center line as the flow channel; where the angles between the waist and the lower base of the trapezoid of the bottom plate are β1 and β2, 30° ≤ β1 < 90°, preferably 45° ≤ β1 ≤ 75° and β1 ≤ α1, 30° ≤ β2 < 90°, preferably 45° ≤ β2 ≤ 75° and β2 ≤ α2; and the length of the upper base of the trapezoid of the bottom plate is k, and j < k ≤ 2j, preferably j < k ≤ 1.6j.

[0123] Without being limited to any known theory, through repeated experiments and simulation calculations for verification, it is believed that the β1 and β2 angles equal to or slightly smaller than the α1 and α2 angles, and the specific range of the upper base of the bottom plate relative to the upper base of the flow channel, make the entire solid distribution member (17) have a relatively stable structure, and at the same time will not have an obvious impact on the fluidization and reaction in the reaction chamber.

[0124] In one embodiment, as shown in Figure 5 , the side baffles 19 of the distribution member 17 can be rectangular plates with a height L, where 0.2dg ≤ L ≤ 0.5dg. Rectangular plates have a simple structure and are generally sufficient to meet the requirements of the present invention, such as solids distribution. Through repeated experiments and simulations, the inventors have found that when the side baffles 19 have a height L within the specified range, they are sufficiently high to facilitate solids distribution, while also minimizing material waste and, more importantly, not so high as to significantly affect fluidization and reaction within the reaction chamber.

[0125] In another embodiment, the side baffles 19 of the distribution member 17 may be rectangular trapezoidal plates with a height L gradually decreasing from the upper base, wherein 0.2dg ≤ L ≤ 0.5dg, and the height of the lower base of the rectangular trapezoid is 0.6-0.8L. Through repeated experiments and simulation calculations, the inventors have found that when the side baffles 19 have a rectangular trapezoidal shape within this specific lower base height range, while still substantially meeting the requirements for solid distribution, in some cases, they are more conducive to meeting the requirements of not affecting fluidization and reaction in the reaction chamber.

[0126] It can be understood that, as shown in Figure 7, in order to meet a more favorable distribution of solids such as recycled catalysts, the bottom plate 18 of the distribution member 17 is preferably inclined at a certain angle to the horizontal plane; however, the present invention can also be implemented when the bottom plate is placed horizontally. Accordingly, in one embodiment, the bottom plate 18 is at an angle θ with the horizontal plane, where 0≤θ≤45°, preferably 15°≤θ≤30°. The angle between the catalyst circulation channel section at the solid phase feed port and the horizontal plane is γ, 0°≤│γ-θ│≤15°. In one embodiment, arranging the distribution member 17 at a certain angle to the horizontal plane can be achieved by providing a support plate 23 and / or a rib plate 24 between the wall of the reaction chamber and the bottom plate 18.

[0127] The inventors further studied the cross-sectional shape of the bottom plate 18. Through repeated experiments and simulation calculations, the inventors found that forming a certain curved surface of the bottom plate can be more conducive to the desired distribution of solids. Without being limited to any known theory, through a large number of experiments, it is believed that the bottom plate 18 can be a flat plate or a corrugated plate, preferably a corrugated plate, and the waveform of the corrugated plate is a cosine wave, a circular wave or an elliptical wave. For the purpose of the present invention, "circular wave" refers to a waveform formed by connecting several semicircles with the same radius at the first position; and "elliptical wave" refers to a waveform formed by connecting several semi-ellipses with the same major and minor axes at the first position. It can be understood that for cosine waves, circular waves or elliptical waves, each has a central symmetry axis; preferably, the waveform height h0 of the corrugated plate (the vertical distance from the peak to the adjacent trough) is 0.1L≤h0≤0.5L. Accordingly, through repeated experiments and simulation calculations, it is preferred that the central symmetry axis of the bottom plate 18 is directly connected to the lowest point of the inner diameter of the solid phase feed port 7 as shown in Figure 7, that is, there is no height difference between the two. Furthermore, for a cosine wave, circular wave, or elliptical wave, the connection point between the bottom plate and the inner diameter of the solid phase feed port is located exactly at the point extending from the central symmetry axis toward the lower half of the wave for that waveform. As shown in Figures 5 and 7, when a corrugated plate is used, there is a gap between the bottom end of the side baffle and the concave corrugation of the corrugated plate to allow solid phase discharge.

[0128] For Embodiments B and C of the present invention involving a circulating fluidized bed reactor, Embodiment A involving a fluidized bed reactor, and combinations thereof, the solid-phase feed port is located at the connection between the catalyst circulation channel and the fluidized bed reactor. Accordingly, when the catalyst circulation channel is connected to the reactor wall, it may also form a certain angle with the horizontal plane. For example, the angle γ0 between the section of the catalyst circulation channel at the connection with the reactor wall and the horizontal plane is γ0, which is, for example, 30°<γ0<70°.

[0129] In one embodiment, to avoid the formation of dead zones in the reaction chamber space below the bottom plate 18 (e.g., a corrugated plate) in the reactor and to achieve better solid concentration distribution, a plurality of distribution holes are provided on the bottom plate 18 (e.g., a corrugated plate). When solids are transported through the flow channel on the bottom plate 18, at least a portion of the solids will pass downward through these distribution holes, thereby being distributed downward into the reaction chamber space below the bottom plate 18 (e.g., a corrugated plate). Experimental verification has surprisingly shown that distribution holes do not need to be provided throughout the entire bottom plate 18 or the entire flow channel; preferably, the aforementioned advantageous "downward distribution" of solids can be achieved by simply providing a plurality of distribution holes in the front end region of the bottom plate 18 within the flow channel. In other words, the area of ​​the bottom plate 18 outside the flow channel (i.e., outside the side baffles) and the rear end region within the flow channel do not need to be perforated. Through repeated experiments and simulation calculations, it has been verified that in order to achieve the above-mentioned "downward distribution" of favorable solids, in one embodiment, the front end area where the distribution holes are set here can refer to the area on the bottom plate 18 in the flow channel from the upper bottom to the lower bottom along the height hh between 45% and 95%, preferably between 65% and 95%.

[0130] Furthermore, repeated experiments and simulation calculations have shown that, in order to achieve the above-mentioned "downward distribution" of favorable solids, in one embodiment, the total porosity of the bottom plate 18 (eg, a corrugated plate) is 1%-10%, preferably 4%-8%.

[0131] Similarly, the diameter of the distribution holes needs to be adjusted appropriately, especially to match the catalyst diameter. Similar to the various factors considered for the gas holes, through repeated experiments and simulation calculations, the diameter of the distribution holes can be 2-10 mm, preferably 4-8 mm.

[0132] Similar to the air holes, the distribution holes and their distribution described in the present invention are preferably uniform. Accordingly, in one embodiment, the diameter of each distribution hole is substantially equal; similarly, for the purposes of the present invention, the diameter of the distribution holes is "substantially equal" means that the diameter difference between the distribution holes does not exceed 10%, preferably does not exceed 5%, and more preferably does not exceed 1%. Similar to the air holes, in one embodiment, the opening distribution of the distribution holes is an equilateral triangle distribution with staggered rows in the front and back. In another embodiment, the opening distribution of the distribution holes is a rectangular distribution with aligned rows in the front and back. Also similar to the air holes, for the purposes of the present invention, the specific spacing between the distribution holes is not particularly limited, as long as it can meet the distribution hole diameter and the total porosity of the distribution plate described in the present invention. For example, the spacing between the distribution holes can be 20-200 mm, preferably 50-100 mm.

[0133] In this way, as shown in Figure 5, for the implementation scheme in which the bottom plate 18 is a corrugated plate, the solid phase flowing through the corrugated plate can achieve a large range of solid phase particle concentration distribution on both sides of the corrugated plate (arrow a), in front (arrow c), in front and below (arrow b) and through the distribution holes (arrow d).

[0134] Implementation Plan C

[0135] According to embodiment C, the present invention provides a circulating fluidized bed reactor, as shown in Figures 4 and 8, wherein a raw gas distributor 8 is provided at the bottom end of the reaction chamber of the reactor, and a plurality of solid-phase feed ports for circulating catalyst feed are provided on the chamber wall above the raw gas distributor 8, preferably 2-6 solid-phase feed ports, wherein the plurality of solid-phase feed ports are respectively used to feed catalysts in the same or different states, including at least one type I solid-phase feed port for a relatively large amount of solid feed, and at least one type II solid-phase feed port for a relatively small amount of solid feed, wherein the geometric center of the type I solid-phase feed port and the geometric center of the type II solid-phase feed port are in a straight line in the vertical direction, or deviate by no more than 5°, and the geometric center of the feed port is the center point of the feed port cross section. In the present invention, as long as the amounts of the two solid feeds are not completely equal, they can be referred to as relatively large and relatively small amounts of solid feed, respectively. For the purposes of the present invention, the positional relationship between such a type II solid-phase feed port and a type I solid-phase feed port can be referred to as a "vertical arrangement".

[0136] As mentioned above, a circulating fluidized bed reactor may involve a variety of recycled catalysts, such as a circulating agent, a regenerating agent, an external heat extractor, etc.; and even a conventional fluidized bed reactor may also contain the recycled catalyst described in the present invention, such as a catalyst fine powder separated by a separation device (such as a cyclone separator) and returned to the fluidized bed. Accordingly, when the fluidized bed reactor involves two or more different recycled catalysts, they can be fed respectively according to their amounts through the Type I solid phase feed port and the Type II solid phase feed port described in the present invention. Even if the fluidized bed reactor only involves one recycled catalyst, it can be divided into two streams of materials with different amounts, and fed respectively through the Type I solid phase feed port and the Type II solid phase feed port described in the present invention.

[0137] Through the vertical arrangement of the Type I and Type II solid phase feed ports of the present invention, a relatively small amount of solid feed can quickly merge into the relatively large amount of solid feed fed through the Type I solid phase feed port and flow together after entering the fluidized bed through the Type II solid phase feed port located above, which helps to improve the gas-solid and solid-solid (such as external heat extraction agent and regeneration agent) uniformity of the smaller amount of solid feed in the reactor.

[0138] Accordingly, in order to promote the uniform distribution, the vertical arrangement of the type I and type II solid phase feed ports requires that the two should have an appropriate spacing in the vertical direction. In one embodiment, as shown in Figure 8, the vertical distance between the geometric center of the type II solid phase feed port and the geometric center of the type I solid phase feed port is h, preferably 0.5(dc+dz)≤h≤1.5dc, preferably 0.5(dc+dz)≤h≤dc, wherein: dc is the equivalent diameter of the type I solid phase feed port, and dz is the equivalent diameter of the type II solid phase feed port.

[0139] In particular, as shown in FIG8 , for the circulating fluidized bed reactor of embodiment C, in order to further facilitate the uniform distribution of gas-solid and solid-solid, the solid distribution member 17 according to embodiment B may be connected to one or more solid phase feed ports.

[0140] In one embodiment, as shown in FIG8 , the plurality of solid-phase feed ports further include at least one additional solid-phase feed port, which is also used for feeding a relatively large amount of solids and is circumferentially at least 120°, preferably at least 150°, from the geometric center of the Type I solid-phase feed port; wherein, preferably, the additional solid-phase feed port is not connected to the solid distribution member 17. Preferably, the additional solid-phase feed port has the same equivalent diameter as the Type I solid-phase feed port. In this case, the additional solid-phase feed port is relatively far away from the Type I solid-phase feed port, which will reduce the effect of mixing and distribution between the solids fed through the Type I and Type II solid-phase feed ports. Therefore, when mixing and distribution between the solids fed through the Type I and Type II solid-phase feed ports is the main consideration, this embodiment is suitable. Accordingly, the inventors determined the spacing of at least 120°, preferably at least 150°, through repeated experiments and simulation calculations.

[0141] In another embodiment, the multiple solid-phase feed inlets include one or more additional solid-phase feed inlets, and the geometric centers of the one or more additional solid-phase feed inlets and the I-type solid-phase feed inlet are all symmetrically distributed about the circumference. Preferably, one or more, and preferably all, of the additional solid-phase feed inlets are also provided with the solid distribution member 17 toward the center of the reaction chamber. Preferably, the additional solid-phase feed inlets have the same equivalent diameter as the I-type solid-phase feed inlet. It is understood that this embodiment is suitable when the distribution of solids fed through the additional solid-phase feed inlets is a significant consideration. Accordingly, the two or more solid distribution members 17 used can have the same or different sizes. For different operating conditions and different feeds, it is believed that as long as the two or more solid distribution members 17 used have the same size, various conditions can be generally met, eliminating the need to provide solid distribution members 17 of different sizes at the I-type solid-phase feed inlet and the multiple additional solid-phase feed inlets. This avoids greater fluctuations under different conditions, and may even require the replacement of solid distribution members of different sizes under different conditions.

[0142] For the sake of uniformity and controllability, through repeated experiments and simulation calculations, it is preferred that the geometric center of the type I solid phase feed port and the geometric center of the additional solid phase feed port are on the same horizontal line, or the upper and lower deviations do not exceed 5°.

[0143] The vertical arrangement of the Type I and Type II solid-phase feed ports of the present invention is intended to promote mixing and distribution between the solids fed through these two feed ports; accordingly, through experimental research, the inventors have found that it is advantageous for the Type II solid-phase feed port to also extend into the reaction chamber, and preferably, the distance it extends is greater than the distance the Type I solid-phase feed port extends, which allows a relatively small amount of solid feed to better merge into the relatively large amount of solid feed below. On the other hand, experimental research shows that, also for the purpose of better mixing, it is also preferred that the distance the Type II solid-phase feed port extends further relative to the Type I solid-phase feed port does not exceed 1 / 2 of the height hh of the trapezoid of the bottom plate 18.

[0144] It is understood that the diameter of the feed ports of the pipeline and the connecting pipeline affects factors such as the amount and speed of conveyance. Based on a comprehensive examination of multiple factors, verified by repeated experiments and simulation calculations, it is believed that the preferred ratio of the equivalent diameters of the Type I solid-phase feed port to the Type II solid-phase feed port is 2:1-10:1, preferably 3:1-5:1. In this case, the circulating fluidized bed of the present invention can have greater operational flexibility and is more widely applicable to the separate feeding of relatively large and relatively small amounts of recycled catalyst under various conditions.

[0145] It is also understood that the fluidized bed reactor is generally arranged vertically, and accordingly the pipe section at the junction of its catalyst circulation channel and the reactor wall also tends to have a certain angle with the horizontal plane, and this angle also affects parameters such as conveying speed. Verified by repeated experiments and simulation calculations, it is advantageous that the angle between the catalyst circulation channel pipe section at type I solid-phase feed port and the horizontal plane is γ, wherein 0°≤γ≤60°, preferably 0°≤γ≤45°. Similarly, the angle between the catalyst circulation channel pipe section at type II solid-phase feed port and the horizontal plane is δ, wherein 0°≤δ≤60°, preferably 0°≤δ≤45°. Particularly advantageously, the γ is equal to or appropriately greater than the δ, such as 0°≤(γ-δ)≤15°.

[0146] The circulating fluidized bed of the present invention may involve a variety of recycling catalysts, especially when it is used to produce olefins through methanol conversion, catalytic cracking or fluidized bed propane dehydrogenation, it may involve an external heat extractor, a circulating agent, a regeneration agent and catalyst powder. Then the type I solid phase feed port is a solid phase feed port for feeding an external heat extractor or a circulating agent, and the type II solid phase feed port is a solid phase feed port for feeding a regeneration agent or catalyst powder; preferably, the type I solid phase feed port is a solid phase feed port for feeding an external heat extractor, and the type II solid phase feed port is a solid phase feed port for feeding a regeneration agent.

[0147] In the present invention, as shown in Figure 8, the solid phase feed port is used to feed the catalyst, including an external heat extraction agent feed port 7, a circulating agent feed port 5 and 9, and a catalyst powder feed port 16 which are circumferentially spaced apart on the cavity wall of the feed section (the catalyst powder can, for example, come from the gas phase containing light olefins discharged from the gas phase outlet, and the catalyst powder separated by a cyclone separator is refluxed into the feed section); wherein, a regeneration agent feed port 10 is provided in the cavity wall just above the external heat extraction agent feed port 7, and the vertical distance between the geometric center of the regeneration agent feed port 10 and the geometric center of the external heat extraction agent feed port 7 is h, 0.5(dc+dz)≤h≤1.5dc, preferably 0.5(dc+dz)≤h≤dc.

[0148] In some embodiments, one or more of the solid-phase feed ports are provided with a solid distribution member 17. For example, a solid distribution member 17 may be provided at the circulating agent feed port 5 or 9, the regenerant feed port 10, or the external heat extraction agent feed port 7 as shown in FIG4 or FIG8. The side baffle 19 of the solid distribution member 17 has a height of L, wherein L is in the range of 0.2-0.5 times the equivalent diameter of the corresponding solid-phase feed port; preferably, the solid distribution member 17 is provided at the external heat extraction agent feed port 7, 0.2dc≤L≤0.5dc, wherein L is the height of the side baffle 19, and dc is the equivalent diameter of the external heat extraction agent feed port; in this way, the regenerant z returned from the regenerated catalyst after regeneration can be quickly merged into the catalyst g returned from the external heat extraction pipe and flow together, which helps to improve the uniform distribution of the regenerant particles in the gas-solid and solid-solid (e.g., external heat extraction agent, circulating agent, and regenerant) in the reactor. If the distance between the pipe ports is too far, the regenerant will be separated from the main distribution of the external heat extraction agent, resulting in uneven distribution.

[0149] In some embodiments, the circulating agent feed ports 5 and 9 , the catalyst fine powder feed port 16 and the external heat extractor feed port 7 are at the same level, and the regeneration agent feed port 10 is vertically above the external heat extractor feed port 7 .

[0150] In some embodiments, the regenerant feed port 10 is the uppermost solid phase feed port in the feed section of the reaction chamber, and the distance between the geometric center of the regenerant feed port 10 and the first flow disruptor 15 from bottom to top in the reactor is 0.2-1.5 m, preferably 0.5-1.2 m.

[0151] It should be noted that, in some embodiments of the present invention, as shown in Figure 4, the gas-solid reaction equipment also includes some conventional settings in the gas-solid reaction equipment in the prior art, such as a catalyst regenerator 14 and a degassing tank 13, wherein the top of the reaction chamber 6 is set as an upwardly tapering discharge port, and the top of the tapered discharge port extends into the separation chamber 2 to form a lifting pipe 3, and the separation chamber 2 is provided with a fluidizing air distributor 11 for feeding fluidizing air q into the separation chamber 2, and the separation chamber 2 and the feed section are connected by at least one catalyst circulation pipe and an external heat exchanger pipe with an external heat exchanger 4, the separation chamber 2 is connected to the feed port of the catalyst regenerator 14 through the regeneration agent pipe 12, and the discharge port of the catalyst regenerator 14 is connected to the feed section through the regeneration agent pipe provided with the degassing tank 13, etc., which can be configured and adjusted according to actual production needs, and the present invention will not be repeated here.

[0152] The gas-solid reaction apparatus of the present invention, under the action of the relative position adjustment of the flow-disturbing member 15, the solid distribution member 17 and / or the solid-phase feed port according to the present invention, makes the standard deviation σ1 of the change in the concentration ratio of the solid-phase particles in the total amount of the solid-phase particles at different positions in the height area above the top solid-phase feed port in the reaction chamber 6 less than 1.5, preferably less than 0.8, makes the standard deviation σ2 of the change in the concentration ratio of the solid-phase particles in the total amount of the gas-solid material at different positions in the height area above the top solid-phase feed port in the reaction chamber 6 less than 1.5, preferably less than 0.8, makes the standard deviation (unevenness) σ of the total concentration difference of the solid-phase particles (for example, the recycled catalyst, including the circulating agent, the regenerating agent and the external heat extracting agent) at different positions in the height area above the top solid-phase feed port in the reaction chamber 6 less than 1.5, preferably less than 0.8 p Less than 1.5, preferably less than 1.2; the above standard deviation is calculated according to the following formula:

[0153] Where σ is the standard deviation, representing the discreteness (unevenness) of the samples at different positions in the reaction chamber 6. The larger the value, the more uneven the distribution of the samples in the total amount. 1i is the concentration ratio of solid particles (such as regenerant) at a certain sampling point in the cavity to the total amount of solid particles, x 2i is the concentration ratio of solid particles (such as regenerant) in the total gas-solid volume at a certain sampling point in the cavity, x pi is the concentration ratio of the total amount of solid particles (such as recycled catalyst) at a certain sampling point in the cavity to the total amount of gas and solid. is the average concentration of samples in the area under the corresponding conditions, n is the number of sampling points in the area, and n≥10.

[0154] The present invention greatly promotes the mixing between multiple streams of different solid-phase particulate materials, strengthens gas-solid contact, reduces the uneven distribution of solid-phase particles (such as regenerants) on a unit height cross-section, significantly reduces the carbon difference distribution on the cross-section, promotes the continuous generation of low-carbon olefins, and improves the performance of the reactor by arranging a flow disturbance component in the flow disturbance section cavity of the fluidized bed reactor equipment, adjusts the relative positions of type I solid-phase feed inlets (such as external heat extraction agent feed inlets) and type II solid-phase feed inlets (such as regenerant feed inlets) in the feed section, and / or arranges solid distribution components at one or more solid-phase feed inlets.

[0155] On the other hand, the present invention provides the use of the disruptor member 15 or fluidized bed reactor according to embodiment A of the present invention, the solid distribution member 17 or circulating fluidized bed reactor according to embodiment B of the present invention, the circulating fluidized bed reactor according to embodiment C of the present invention, or a combination thereof in methanol conversion to produce olefins, catalytic cracking, or fluidized bed propane dehydrogenation.

[0156] On the other hand, the present invention provides a method for producing olefins by converting methanol. The method adopts the reaction equipment according to the present invention (such as a fluidized bed reactor with a flow disturbance component, a circulating fluidized bed reactor with a solid distribution component, a circulating fluidized bed reactor with a specific solid phase feed port position, or a combination thereof), comprising feeding methanol raw gas f and a catalyst (such as a recycled catalyst, such as an external heat extractor g, a regeneration agent z, circulating agents r1 and r2, etc.) into the feed section, so that the methanol raw gas f contacts the catalyst and reacts to generate a gas-solid mixture containing light olefins; the gas-solid mixture containing light olefins is passed upward through the flow disturbance section to form a vortex to enhance the phase disturbance between the gas and solid phases and further react, and then continues to enter the separation chamber 2 upward for gas-solid separation, and the separated gas phase containing light olefins is discharged from the gas phase outlet p at the top of the separation chamber.

[0157] In some embodiments, the gas-solid mixture containing light olefins forms a vortex in the flow-disturbing section through the flow-disturbing member 15 .

[0158] In some embodiments, the catalyst enters the feed section through a solid distribution member 17 connected to the solid phase feed port. In some embodiments, the external heat extractor g returned after heat extraction is dispersed into the feed section through a solid distribution member 17 connected to the external heat extractor feed port 7. In some embodiments, the regenerated agent z returned after regeneration is dispersed into the feed section through a solid distribution member 17 connected to the regenerated agent feed port 10.

[0159] In some embodiments, the methanol raw gas f is preheated and fed into the feed section through the raw gas distributor 8, wherein the preheating temperature is 150-200°C, and the gas superficial velocity ug of the methanol raw gas f entering the feed section is 0.8-2.0 m / s.

[0160] In some embodiments, the recycled catalyst includes the external heat extraction agent g fed from the external heat extraction agent feed port 7 and returned after heat extraction, the temperature of the external heat extraction agent g is 300-400°C; the regeneration agent z fed from the regeneration agent feed port 10, the temperature of the regeneration agent z is 600-700°C; the circulating agents r1 and r2 fed from the circulating agent feed ports 5 and 9 respectively, the temperature of the circulating agents r1 and r2 is 450-500°C; and the catalyst fine powder fed from the catalyst fine powder feed port 16.

[0161] In some embodiments, the average concentration of the catalyst in the reaction chamber 6 is 60-150 kg / m 3 , preferably 80-115kg / m 3 .

[0162] In some embodiments, the reaction temperature in the reaction chamber 6 is 450-500° C., and the reaction pressure is 0.01-1 MPa.

[0163] In order to facilitate the understanding of the present invention, the present invention lists the following embodiments, but the embodiments are only used to help understand the present invention and should not be regarded as specific limitations of the present invention.

[0164] Example

[0165] The present application is further described below with reference to examples, which however do not constitute a limitation of the present application.

[0166] The following embodiments are carried out in a gas-solid reaction device, as shown in Figures 4 and 9, which may include a gas-solid reactor 1 (for example, a fluidized bed reactor according to embodiment A, a circulating fluidized bed reactor according to embodiments B and C), a degassing tank 13 and a catalyst regenerator 14; wherein the gas-solid reactor 1 may include a reaction chamber 6 and a separation chamber 2 that are connected to each other, a raw gas distributor 8 is provided at the bottom end of the reaction chamber 6, the reaction chamber 6 includes a feed section and a turbulent flow section located above the feed section, the top end of the reaction chamber 6 is provided as an upwardly tapered discharge port, the top end of the tapered discharge port extends into the separation chamber 2 to form a riser 3, and a fluidized air distributor 11 for feeding fluidized air q into the separation chamber 2 is provided in the separation chamber 2, and a gas phase outlet p is opened at the top end of the separation chamber 2; the gas-solid reactor 1 is also provided with at least one catalyst circulation pipe connecting the feed section of the reaction chamber 6 and the separation chamber 2, and an external heat exchanger pipe provided with an external heat exchanger 4. The catalyst circulation pipe is connected to the circulating agent feed ports 5 and 9, respectively, for returning the circulating agent to the feed section of the reaction chamber 6. The external heat exchanger pipe is connected to the external heat exchanger feed port 7 for returning the external heat exchanger to the feed section of the reaction chamber 6. The feed section of the reaction chamber 6 is also provided with a catalyst fine powder feed port 16 for returning the separated catalyst fine powder to the reaction chamber 6. The separation chamber 2 is connected to the feed port of the catalyst regenerator 14 via a spent catalyst pipe 12. The discharge port of the catalyst regenerator 14 is connected to the reaction chamber 6 via a regeneration agent pipe provided with a degassing tank 13. The regeneration agent pipe is connected to the regeneration agent feed port 10 for returning the regeneration agent to the feed section of the reaction chamber 6. Unless otherwise specified, the positions of the components (e.g., the flow disturbance member and the solid distribution member) and the solid phase feed port in the reaction chamber 6 are arranged according to the prior art (e.g., FIG. 9 ).

[0167] The following examples illustrate a method for producing olefins from methanol conversion. The method involves allowing preheated methanol feed gas f to enter the reaction chamber 6 through a feed gas distributor 8 at the bottom of the reaction chamber 6. The preheated methanol feed gas f then mixes, contacts, and reacts with a regeneration agent z returned from a catalyst regenerator 14, an external heat extractor g returned after heat extraction, circulating agents r1 and r2, and recovered catalyst fines. Following the reaction, the catalyst, entrained by the gas, rapidly passes through a riser 3, where it is separated from the main gas phase by a rapid separation mechanism at its outlet and falls under the influence of gravity into the lower portion of a separation chamber 2. Part of the accumulated catalyst is directly circulated back to the feed section of the reaction chamber 6 as circulating agents r1 and r2, part of it is passed through an external heat exchanger to obtain heat, and after cooling, it is returned to the feed section as an external heat exchanger g, and another part is sent to the catalyst regenerator 14 through the regenerated agent pipe 12 as a regenerated agent for regeneration. After removing the carbon deposits on the catalyst, it is returned to the feed section through the regenerated agent pipe as a regenerated agent z. Multiple streams of different catalyst materials are remixed, contacted with the raw gas and reacted; and the gas phase containing light olefins with a small amount of catalyst fine powder after the reaction leaves the separation chamber 2 through the gas phase outlet p at the top of the separation chamber 2, and is further removed by gas-solid separation to be sent to the subsequent unit for treatment. The catalyst fine powder is returned to the feed section of the reaction chamber 6 through the catalyst fine powder feed port 16.

[0168] In the following examples, the amount of catalyst carbon deposit (or average carbon deposit) is calculated by dividing the mass of carbon deposit on the catalyst by the mass of the catalyst. The mass of catalyst carbon deposit is determined as follows: 0.1-1 gram of carbonized catalyst is weighed and placed in a high-temperature carbon analyzer (Wuxi High-Speed ​​Analytical Instrument Co., Ltd., High-Frequency Infrared Sulfur and Carbon Analyzer HIR-944). The mass of carbon dioxide generated by combustion is measured by infrared spectroscopy to obtain the mass of catalyst carbon deposit. To determine the amount of catalyst carbon deposit within the reaction zone, small aliquots of catalyst can be continuously or periodically withdrawn or directly removed from various locations within the reaction zone.

[0169] In the following examples, the concentration ratio of the total amount of solid particles (such as catalyst) in the total amount of gas and solid is x pi The determination method is as follows: Use a high-precision differential pressure analyzer (its high-tech, multi-point high-precision differential pressure analyzer MC-32) to measure the sampling point area, and the pressure difference change ΔPi can be obtained. Then the average density of the sampling point area ρi=ΔPi / (9.8×hp), where hp is the distance between the measured pressure difference points, which is a constant value. The particle density of the catalyst is ρc, so x pi =ρi / ρc=ΔPi / (9.8×hp×ρc);

[0170] In the following embodiments, by directly sampling the sampling point, the carbon deposit amount Ci of the solid phase particles (including regeneration agent, circulation agent, external heat extraction agent, etc.) in the area of ​​the sampling point at a certain moment can be measured by a high-temperature carbon analyzer. Since the circulation agent, external heat extraction agent and other materials are all introduced from the catalyst that has not been regenerated after the reaction, the carbon deposit amount of this part of the catalyst is measured as Cx. If it is assumed that the density of the recycled catalyst containing carbon that has not been regenerated, such as the circulation agent, external heat extraction agent, etc., is approximately the same as the density of the regenerated catalyst without carbon deposits, then the concentration ratio of the solid phase particles (such as the regeneration agent) at a certain sampling point in the cavity to the total amount of solid phase particles is x. 1i =(1-Ci / Cx);

[0171] In the following examples, the concentration of solid particles (such as regenerant) at a sampling point in the chamber accounts for x of the total gas-solid phase. 2i The calculation method is, x 2i =x pi ·x 1i , the number of sampling points in the area is n, n≥10.

[0172] Example 1

[0173] The reaction chamber 6 of the circulating fluidized bed reactor is provided with three circular flow-disturbing members 15 arranged along the axial direction of the reactor and conforming to the cross-sectional shape of the reaction chamber, with an installation spacing ΔH = 0.8m; the diameter D1 of the flow-disturbing member 15 is substantially equal to the inner diameter D of the reaction chamber, and includes a flow-guiding portion and a mixing portion coaxially distributed in the radial direction; wherein the flow-guiding portion includes a flow-guiding plate 20, on which a plurality of equilateral triangular evenly distributed gas holes are provided, with a hole diameter of Φ15mm and a total hole porosity of 3%; the mixing portion includes six concentrically arranged flow-guiding portions surrounding the flow-guiding portion. The fluid-disturbing ring is provided, and each fluid-disturbing ring is provided with a plurality of identical cylindrical fluid-disturbing bodies 21 that are evenly distributed and have no holes on the surface. The fluid-disturbing bodies 21 are arranged vertically, and the fluid-disturbing body 21 in the fluid-disturbing ring with the smallest size is embedded in the edge of the guide plate 20. The horizontal cross-section of the fluid-disturbing body 21 is circular, with an aspect ratio of 3.5:1, an equivalent diameter of the horizontal cross-section of 85 mm, a total void ratio of 86% in the mixing portion, and a ratio of the total void area of ​​the mixing portion to the total void area of ​​the guide plate of 176; the diameter of the guide plate 20 is d b =0.35D1, a side ring 22 connected to the largest fluid-disturbing ring is provided near the cavity wall of the reaction cavity, and the width X of the side ring 22 is D1 / 25.

[0174] The bottom end of the reaction chamber 6 is located on the chamber wall above the raw gas distributor 8 and is provided with four solid phase feed ports for circulating catalyst feed, including an external heat extractor feed port 7, two circulating agent feed ports 5, 9 and a regeneration agent feed port 10. The external heat extractor feed port 7 extends into the reaction chamber and is connected to a solid distribution member 17 toward the center of the reaction chamber. The distribution member includes a corrugated plate bottom plate 18 and two side baffles 19 relatively mounted on the bottom plate, defining an isosceles trapezoidal flow channel, the upper bottom of which is connected to the external heat extractor feed port 7 and is tangent to the inner edge of the feed port. The angle between the waist of the trapezoid and the lower bottom is α1 and α2 are both 55°, the upper base length j of the trapezoid is equal to the regeneration agent feed port diameter dg, and the height hh of the trapezoid is 0.1 times the inner diameter D of the reaction chamber; the bottom plate of the distribution member is a corrugated plate with an isosceles trapezoidal shape, and the angles β1 and β2 between its base and waist are both 50°, and the upper bottom length k of the trapezoidal bottom plate is 1.4dg; the side baffle of the distribution member is rectangular, and its height L = 0.3dg, and a plurality of distribution holes are opened in the front end area of ​​the distribution member, with a total porosity of 6.5% and a hole diameter of Φ6mm. They are distributed in a front-to-back aligned rectangular array, and the bottom plate forms an angle θ with the horizontal plane, θ = 22°.

[0175] The external heat extractor feed port 7 has the same equivalent diameter as the circulating agent feed ports 5 and 9. The three feed ports are evenly distributed along the circumference of the reaction chamber on the same horizontal plane. The equivalent diameter dz of the regenerative agent feed port 10 is 1 / 4 of the equivalent diameter dc of the external heat extractor feed port 7 and is arranged directly above the external heat extractor feed port 7; the pipe section at the external heat extractor feed port 7 extends appropriately into the reaction chamber toward the center at an angle γ of 30° to the horizontal plane; the regenerative agent feed port 10 extends into the reaction chamber at an angle δ of 22° to the horizontal plane, and the horizontal extension distance relative to the external heat extractor feed port 7 is 1 / 4 of the height hh of the bottom plate 18 of the solid distribution member 17. The distance h between the regenerative agent feed port 10 and the external heat extractor feed port 7 is 0.5(dc+dz), and the distance between the regenerative agent feed port 10 and the first flow disruptor member 15 from bottom to top in the reactor is 0.5m.

[0176] The gas superficial velocity uf of the methanol raw gas f entering the feed section is 1.2m / s, the preheating temperature is 180℃, the catalyst is selected from the SAPO34 molecular sieve catalyst of the methanol to olefins process, and the average concentration of the catalyst in the reaction chamber is 85kg / m 3 , reaction temperature 480℃, reaction pressure 0.11MPa.

[0177] The standard deviation σ1 of the change in the concentration ratio of the regenerant in the total amount of solid particles in the reaction chamber is 0.32, and the standard deviation σ2 of the change in the concentration ratio of the regenerant in the total amount of gas-solid materials is 0.46. The carbon deposition of the fed regenerant is 0.03wt%, and the carbon deposition of the remaining circulating agent, external heat agent, and returned catalyst fine powder is 3.2wt%. The difference in the average carbon deposition per unit area of ​​the horizontal section at a height of 2m above the raw gas distributor is less than 0.21wt%. The unevenness of the catalyst concentration distribution in the chamber above the regenerant feed port is σ p It is 0.89.

[0178] Example 2

[0179] The reaction chamber 6 of the circulating fluidized bed reactor is provided with four circular flow-disturbing members 15 arranged along the axial direction of the reactor and conforming to the cross-sectional shape of the reaction chamber, with an installation spacing ΔH = 0.8m; the diameter D1 of the flow-disturbing member 15 is substantially equal to the inner diameter D of the reaction chamber, and includes a guide portion and a mixing portion coaxially distributed in the radial direction; wherein the guide portion includes a guide plate 20, on which a plurality of equilateral triangular evenly distributed gas holes are provided, with a hole diameter of Φ15mm and a total hole porosity of 6%; the mixing portion includes six concentrically arranged gas holes surrounding the guide portion. The fluid-disturbing ring is provided, and each fluid-disturbing ring is provided with a plurality of identical cylindrical fluid-disturbing bodies 21 that are evenly distributed and have no holes on the surface. The fluid-disturbing bodies 21 are arranged vertically, and the fluid-disturbing body 21 in the fluid-disturbing ring with the smallest size is embedded in the edge of the guide plate 20. The horizontal cross-section of the fluid-disturbing body 21 is circular, with an aspect ratio of 3.5:1, an equivalent diameter of the horizontal cross-section of 85 mm, a total void ratio of 86% in the mixing portion, and a ratio of the total void area of ​​the mixing portion to the total void area of ​​the guide plate of 176; the diameter of the guide plate 20 is d b =0.6D1, a side ring 22 connected to the largest fluid-disturbing ring is provided near the cavity wall of the reaction cavity, and the width X of the side ring 22 is D1 / 16.

[0180] The bottom end of the reaction chamber 6 is located on the chamber wall above the raw gas distributor 8 and is provided with four solid phase feed ports for circulating catalyst feed, including an external heat extractor feed port 7, two circulating agent feed ports 5, 9 and a regeneration agent feed port 10, wherein the external heat extractor feed port 7 extends into the reaction chamber and is connected to a solid distribution member 17 toward the center of the reaction chamber. The distribution member includes a corrugated plate bottom plate 18 and two side baffles 19 relatively mounted on the bottom plate, defining an isosceles trapezoidal flow channel, the upper bottom of which is connected to the external heat extractor feed port 7 and is tangent to the inner edge of the feed port, and the waist of the trapezoid is tangent to the lower bottom. The angles α1 and α2 are both 75°, the upper base length j of the trapezoid is equal to the diameter dg of the regeneration agent feed port, and the height hh of the trapezoid is 0.1 times the inner diameter D of the reaction chamber; the bottom plate of the distribution member is a corrugated plate with an isosceles trapezoidal shape, and the angles β1 and β2 between its base and waist are both 45°, and the upper bottom length k of the trapezoidal bottom plate is 2dg; the side baffle of the distribution member is rectangular, and its height L = 0.5dg, and a plurality of distribution holes are opened in the front end area of ​​the distribution member, with a total porosity of 10% and a hole diameter of Φ6mm. They are distributed in a front-to-back aligned rectangular array, and the bottom plate forms an angle θ with the horizontal plane, θ = 22°.

[0181] The external heat extractor feed port 7 has the same equivalent diameter as the circulating agent feed ports 5 and 9. The three feed ports are evenly distributed along the circumference of the reaction chamber on the same horizontal plane. The equivalent diameter dz of the regenerative agent feed port 10 is 1 / 4 of the equivalent diameter dc of the external heat extractor feed port 7 and is arranged directly above the external heat extractor feed port 7; the pipe section at the external heat extractor feed port 7 extends appropriately into the reaction chamber toward the center at an angle γ of 30° to the horizontal plane; the regenerative agent feed port 10 extends into the reaction chamber at an angle δ of 22° to the horizontal plane, and the horizontal extension distance relative to the external heat extractor feed port 7 is 1 / 4 of the height hh of the bottom plate 18 of the solid distribution member 17. The distance h between the regenerative agent feed port 10 and the external heat extractor feed port 7 is 1.5dc, and the distance between the regenerative agent feed port 10 and the first flow disruptor component 15 from bottom to top in the reactor is 0.6m.

[0182] The gas superficial velocity uf of the methanol raw gas f entering the feed section is 1.0 m / s, the preheating temperature is 180°C, the catalyst is selected from the SAPO34 molecular sieve catalyst of the methanol to olefins process, and the average concentration of the catalyst in the reaction chamber is 115 kg / m 3 , reaction temperature 480℃, reaction pressure 0.11MPa.

[0183] The standard deviation of the change in the concentration ratio of the regenerant in the total solid particles in the reaction chamber is σ1, and the standard deviation of the change in the concentration ratio of the regenerant in the total gas-solid material is σ2. The carbon deposition of the feed regenerant is 0.03wt%, and the carbon deposition of the remaining circulating agent, external heat agent, and returned catalyst fine powder is 3.2wt%. The difference in the average carbon deposition per unit area of ​​the horizontal section at a height of 2m above the raw gas distributor is less than 0.32wt%. The unevenness of the catalyst concentration distribution in the chamber above the regenerant feed port is σ p is 1.02.

[0184] Example 3

[0185] The reaction chamber 6 of the circulating fluidized bed reactor is provided with five circular flow-disturbing members 15 arranged along the axial direction of the reactor and conforming to the cross-sectional shape of the reaction chamber, with an installation spacing ΔH = 0.8m; the diameter D1 of the flow-disturbing member 15 is substantially equal to the inner diameter D of the reaction chamber, and includes a flow-guiding portion and a mixing portion coaxially distributed in the radial direction; wherein the flow-guiding portion includes a flow-guiding plate 20, on which a plurality of equilateral triangular gas holes are evenly distributed, with an opening diameter of Φ15mm and a total opening porosity of 2%; the mixing portion includes six concentrically arranged flow-disturbing rings surrounding the flow-guiding portion, each flow-disturbing ring being provided with a plurality of identical cylindrical flow-disturbing bodies 21 evenly distributed and having no holes on the surface, and the flow-disturbing bodies 21 The turbulent body 21 in the smallest turbulent body ring is embedded in the edge of the guide plate 20. The horizontal cross-section of the turbulent body 21 is circular with an aspect ratio of 3.5:1. The equivalent diameter of the horizontal cross-section is 85 mm. The total void ratio of the mixing part is 86%, and the ratio of the total void area of ​​the mixing part to the total void area of ​​the guide plate is 176. The diameter of the guide plate 20 is d b =0.2D1, a side ring 22 connected to the largest fluid-disturbing ring is provided near the cavity wall of the reaction cavity, and the width X of the side ring 22 is D1 / 30.

[0186] The bottom of the reaction chamber 6 is located on the chamber wall above the raw gas distributor 8 and is provided with four solid phase feed ports for circulating catalyst feed, including an external heat extractor feed port 7, two circulating agent feed ports 5, 9 and a regeneration agent feed port 10. The external heat extractor feed port 7 extends into the reaction chamber and is connected to a solid distribution member 17 toward the center of the reaction chamber. The distribution member includes a corrugated plate bottom plate 18 and two side baffles 19 relatively mounted on the bottom plate, defining an isosceles trapezoidal flow channel, the upper bottom of which is connected to the external heat extractor feed port 7 and is tangent to the inner edge of the feed port. The waist of the trapezoid is sandwiched between the lower bottom and the bottom. The angles α1 and α2 are both 60°, the length j of the upper base of the trapezoid is equal to the diameter dg of the regeneration agent feed port, and the height hh of the trapezoid is 0.1 times the inner diameter D of the reaction chamber; the bottom plate of the distribution member is a corrugated plate with an isosceles trapezoidal shape, and the angles β1 and β2 between its base and waist are both 48°, and the length k of the upper base of the trapezoidal bottom plate is 1.4dg; the side baffle of the distribution member is rectangular, and its height L = 0.2dg, and a plurality of distribution holes are opened in the front end area of ​​the distribution member, with a total porosity of 5% and a hole diameter of Φ6mm. They are distributed in a front-to-back aligned rectangular array, and the bottom plate forms an angle θ with the horizontal plane, θ = 22°.

[0187] The external heat extractor feed port 7 has the same equivalent diameter as the circulating agent feed ports 5 and 9. The three feed ports are evenly distributed along the circumference of the reaction chamber on the same horizontal plane. The equivalent diameter dz of the regenerative agent feed port 10 is 1 / 4 of the equivalent diameter dc of the external heat extractor feed port 7 and is arranged directly above the external heat extractor feed port 7; the pipe section at the external heat extractor feed port 7 extends appropriately into the reaction chamber toward the center at an angle γ of 30° to the horizontal plane; the regenerative agent feed port 10 extends into the reaction chamber at an angle δ of 22° to the horizontal plane, and the horizontal extension distance relative to the external heat extractor feed port 7 is 1 / 4 of the height hh of the bottom plate 18 of the solid distribution member 17. The distance h between the regenerative agent feed port 10 and the external heat extractor feed port 7 is 0.5(dc+dz), and the distance between the regenerative agent feed port 10 and the first flow disruptor member 15 from bottom to top in the reactor is 0.4m.

[0188] The gas superficial velocity uf of the methanol raw gas f entering the feed section is 1.2m / s, the preheating temperature is 180℃, the catalyst is selected from the SAPO34 molecular sieve catalyst of the methanol to olefins process, and the average concentration of the catalyst in the reaction chamber is 85kg / m 3 , reaction temperature 450℃, reaction pressure 0.11MPa.

[0189] The standard deviation of the change in the concentration ratio of the regenerant in the total solid phase particles in the reaction chamber is σ1, and the standard deviation of the change in the concentration ratio of the regenerant in the total gas-solid material is σ2. The carbon deposition of the feed regenerant is 0.03wt%, and the carbon deposition of the remaining circulating agent, external heat agent, and returned catalyst fine powder is 3.2wt%. The difference in the average carbon deposition per unit area of ​​the horizontal section at a height of 2m above the raw gas distributor is less than 0.30wt%. The unevenness of the catalyst concentration distribution in the cavity above the regenerant feed port is σ p It is 0.94.

[0190] Example 4

[0191] The circulating fluidized bed reactor is set up according to Example 3, except that two flow-disturbing members 15 are axially and evenly spaced in the reaction chamber 6, the width of the side ring 22 is X=D1 / 64, the total porosity of the opening of the guide plate 20 is 6%, and the diameter d of the guide plate 20 is b =0.6D1, the distance h between the regeneration agent feed port 10 and the external heat extraction agent feed port 7 is 1.5dc;

[0192] The standard deviation of the change in the concentration ratio of the regenerant in the total solid particles in the reaction chamber is σ1, and the standard deviation of the change in the concentration ratio of the regenerant in the total gas-solid material is σ2. The carbon deposition of the feed regenerant is 0.03wt%, and the carbon deposition of the remaining circulating agent, external heat agent, and returned catalyst fine powder is 3.2wt%. The difference in the average carbon deposition per unit area of ​​the horizontal section at a height of 2m above the raw gas distributor is less than 0.39wt%. The unevenness of the catalyst concentration distribution in the cavity above the regenerant feed port is σ p is 1.05.

[0193] Example 5

[0194] A circulating fluidized bed reactor is set up according to Example 3, except that the external heat extractor feed port 7 in the reaction chamber 6 is not provided with a solid distribution member 17, and the catalyst directly enters the reactor cavity.

[0195] The standard deviation of the change in the concentration ratio of the regenerant in the total solid particles in the reaction chamber is σ1, and the standard deviation of the change in the concentration ratio of the regenerant in the total gas-solid material is σ2. The carbon deposition of the feed regenerant is 0.03wt%, and the carbon deposition of the remaining circulating agent, external heat agent, and returned catalyst fine powder is 3.2wt%. The difference in the average carbon deposition per unit area of ​​the horizontal section at a height of 2m above the feed gas distributor is less than 1.17wt%. The unevenness of the catalyst concentration distribution in the chamber above the regenerant feed port is σ p It is 1.13.

[0196] Example 6

[0197] A circulating fluidized bed reactor is set up according to Example 3, except that three flow-disturbing components 15 are axially evenly spaced in the reaction chamber 6, the regeneration agent feed port 10 and the external heat extraction agent feed port 7 are at the same horizontal height of the reactor and are located at different positions around the reactor, the regeneration agent feed port 10 is close to one side of the external heat extraction agent feed port 7, and the regeneration agent feed port 10 in the reaction chamber 6 is connected to a solid distribution member 17 toward the center of the reaction chamber.

[0198] The standard deviation of the change in the concentration ratio of the regenerant in the total solid phase particles in the reaction chamber σ1 is 1.03, the standard deviation of the change in the concentration ratio of the regenerant in the total gas-solid material σ2 is 1.19, the carbon deposition of the feed regenerant is 0.03wt%, and the carbon deposition of the remaining circulating agent, external heat agent and returned catalyst fine powder is 3.2wt%. The difference in the average carbon deposition per unit area of ​​the horizontal section at a height of 2m above the raw gas distributor is less than 0.89wt%. The unevenness of the catalyst concentration distribution in the chamber above the regenerant feed port σ p It is 1.23.

[0199] Example 7

[0200] The reaction chamber 6 of the circulating fluidized bed reactor is provided with three circular flow-disturbing members 15 arranged along the axial direction of the reactor and conforming to the cross-sectional shape of the reaction chamber, with an installation spacing ΔH=0.8m; the diameter D1 of the flow-disturbing member 15 is substantially equal to the inner diameter D of the reaction chamber, and includes a guide portion and a mixing portion coaxially distributed in the radial direction; wherein the flow-disturbing member includes a guide plate 20, on which a plurality of equilateral triangle-shaped gas holes (as shown in FIG2a) are uniformly distributed, with an opening diameter of Φ15mm and a total porosity of 3%; the mixing portion includes six concentrically arranged flow-disturbing rings surrounding the flow-disturbing member, each of which is provided with a plurality of identical cylindrical flow-disturbing bodies 21 uniformly distributed and having no holes on the surface, the horizontal cross-sectional shape of the flow-disturbing body 21 being circular with an aspect ratio of 3.5:1, the equivalent diameter of its horizontal cross-sectional area being 85mm, the total porosity of the mixing portion being 86%, and the ratio of the total void area of ​​the mixing portion to the total void area of ​​the flow-disturbing plate being 176; the diameter of the flow-disturbing plate 20 is d b =0.35D1, a side ring 22 connected to the largest fluid-disturbing ring is provided near the cavity wall of the reaction cavity, and the width X of the side ring 22 is D1 / 25.

[0201] The gas superficial velocity uf of the methanol feed gas f entering the reaction chamber is 1.2m / s, the preheating temperature is 180℃, the catalyst is selected from the SAPO34 molecular sieve catalyst of the methanol to olefins process, and the average concentration of the catalyst in the reaction chamber is 85kg / m 3 , reaction temperature 480℃, reaction pressure 0.11MPa.

[0202] The standard deviation σ1 of the change in the concentration ratio of the regenerant in the total amount of solid particles in the reaction chamber 6 is 1.31, and the standard deviation σ2 of the change in the concentration ratio of the regenerant in the total amount of gas-solid materials is 1.48. The carbon deposition of the feed regenerant is 0.03wt%, and the carbon deposition of the remaining circulating agent, external heat agent, and returned catalyst fine powder is 3.2wt%. The difference in the average carbon deposition per unit area of ​​the horizontal section at a height of 2m above the raw gas distributor is less than 1.21wt%. The unevenness of the catalyst concentration distribution in the chamber above the regenerant feed port is σ p It is 1.39.

[0203] Example 8

[0204] The reaction chamber 6 of the circulating fluidized bed reactor is provided with five circular flow-disturbing members 15 arranged along the axial direction of the reactor and conforming to the cross-sectional shape of the reaction chamber, with an installation spacing ΔH=0.8m; the diameter D1 of the flow-disturbing member 15 is substantially equal to the inner diameter D of the reaction chamber, and includes a guide portion and a mixing portion coaxially distributed in the radial direction; wherein the guide portion includes a guide plate 20, on which a plurality of concentric annular arrays of gas holes are uniformly distributed (as shown in FIG2b), with a hole diameter of Φ15mm and a total porosity of 2%; the mixing portion includes six concentrically arranged flow-disturbing rings surrounding the flow-disturbing portion, each of which is provided with a plurality of identical cylindrical flow-disturbing bodies 21 uniformly distributed and without holes on the surface, the horizontal cross-section of the flow-disturbing body 21 is circular with an aspect ratio of 3.5:1, an equivalent diameter of the horizontal cross-section of the flow-disturbing body 21 of 85mm, a total porosity of the mixing portion of 86%, and a ratio of the total void area of ​​the mixing portion to the total void area of ​​the flow-disturbing plate of 176; the diameter of the flow-disturbing plate 20 is d b =0.2D1, a side ring 22 connected to the largest fluid-disturbing ring is provided near the cavity wall of the reaction cavity, and the width X of the side ring 22 is D1 / 30.

[0205] The gas superficial velocity uf of the methanol feed gas f entering the reaction chamber is 1.2m / s, the preheating temperature is 180℃, the catalyst is selected from the SAPO34 molecular sieve catalyst of the methanol to olefins process, and the average concentration of the catalyst in the reaction chamber is 90kg / m 3 , reaction temperature 480℃, reaction pressure 0.11MPa.

[0206] The standard deviation σ1 of the change in the concentration ratio of the regenerant in the total amount of solid particles in the reaction chamber 6 is 1.16, and the standard deviation σ2 of the change in the concentration ratio of the regenerant in the total amount of gas-solid materials is 1.23. The carbon deposition of the feed regenerant is 0.03wt%, and the carbon deposition of the remaining circulating agent, external heat agent, and returned catalyst fine powder is 3.2wt%. The difference in the average carbon deposition per unit area of ​​the horizontal section at a height of 2m above the raw gas distributor is less than 1.22wt%. The unevenness of the catalyst concentration distribution in the chamber above the regenerant feed port is σ p is 1.36.

[0207] Comparative Example 1

[0208] The MTO continuous reaction regeneration fluidized bed reactor shown in FIG9 is used, wherein no flow disturbance components and solid distribution components are provided in the reaction chamber 6, and the regeneration agent returns to the reactor through the regeneration agent feed port 10. Two circulating agent feed ports, an external heat extraction agent feed port and a catalyst fine powder feed port are also distributed on the circumference at the same horizontal height.

[0209] The gas superficial velocity uf of the methanol raw gas f entering the feed section is 1.2m / s, the preheating temperature is 180℃, the catalyst is selected from the SAPO34 molecular sieve catalyst of the methanol to olefins process, and the average concentration of the catalyst in the reaction chamber is 85kg / m 3 , reaction temperature 480℃, reaction pressure 0.11MPa.

[0210] The standard deviation of the change in the concentration ratio of the regenerant in the total solid particles in the reaction chamber is σ1, and the standard deviation of the change in the concentration ratio of the regenerant in the total gas-solid material is σ2.56. The carbon deposition of the feed regenerant is 0.03wt%, and the carbon deposition of the remaining circulating agent, external heat agent, and returned catalyst fine powder is 3.2wt%. The difference in the average carbon deposition per unit area of ​​the horizontal section at a height of 2m above the raw gas distributor is less than 1.85wt%. The unevenness of the catalyst concentration distribution in the chamber above the regenerant feed port is σ p It is 2.78.

[0211] Comparative Example 2

[0212] A circulating fluidized bed reactor was set up according to Comparative Example 1, except that three flow-disrupting members were equidistantly spaced axially in the reaction chamber 6, with an installation spacing ΔH = 0.8 m. The structure of the flow-disrupting member was an inclined baffle-type internal member according to the prior art ( FIG. 10 ), and the angle between the baffle and the horizontal plane was 45°. The distance between the regeneration agent feed port 10 and the first flow-disrupting member from bottom to top in the reactor was 0.5 m.

[0213] The standard deviation of the change in the concentration ratio of the regenerant in the total solid particles in the reaction chamber is σ1, and the standard deviation of the change in the concentration ratio of the regenerant in the total gas-solid material is σ2. The carbon deposition of the feed regenerant is 0.03wt%, and the carbon deposition of the remaining circulating agent, external heat agent, and returned catalyst fine powder is 3.2wt%. The difference in the average carbon deposition per unit area of ​​the horizontal section at a height of 2m above the raw gas distributor is less than 1.67wt%. The unevenness of the catalyst concentration distribution in the chamber above the regenerant feed port is σ p It is 1.57.

[0214] Comparative Example 3

[0215] A circulating fluidized bed reactor was set up according to Comparative Example 1, except that three flow-disrupting members were equidistantly arranged axially in the reaction chamber 6, with an installation spacing ΔH = 0.8 m. The structure of the flow-disrupting member was an inclined baffle-type internal member according to the prior art ( FIG. 10 ), the angle between the baffle and the horizontal plane was 45°, and the distance between the regeneration agent feed port 10 and the first flow-disrupting member from bottom to top in the reactor was 0.5 m; the regeneration agent feed port 10 in the reaction chamber 6 was connected to a flat baffle-type solid distribution member ( FIG. 11 ) having a trapezoidal shape and a horizontal plate as a whole, toward the center of the reaction chamber.

[0216] The standard deviation of the change in the concentration ratio of the regenerant in the total solid particles in the reaction chamber is σ1, and the standard deviation of the change in the concentration ratio of the regenerant in the total gas-solid material is σ2. The carbon deposition of the feed regenerant is 0.03wt%, and the carbon deposition of the remaining circulating agent, external heat agent, and returned catalyst fine powder is 3.2wt%. The difference in the average carbon deposition per unit area of ​​the horizontal section at a height of 2m above the raw gas distributor is less than 1.08wt%. The unevenness of the catalyst concentration distribution in the chamber above the regenerant feed port is σ p is 1.40.

[0217] The preferred embodiments of the present invention are described in detail above, but the present invention is not limited thereto. Within the technical concept of the present invention, various simple variations of the technical solution of the present invention may be made, including combining the various technical features in any other appropriate manner. These simple variations and combinations should also be regarded as the contents disclosed by the present invention and fall within the scope of protection of the present invention.

Claims

1. A spoiler component (15), characterized in that: The flow-disturbing member includes a flow-guiding portion and a mixing portion coaxially distributed in the radial direction, wherein: The guide portion comprises a guide plate (20), the guide plate (20) is provided with at least three substantially evenly distributed air holes, and the total porosity of the openings of the guide plate is 0.2%-6%, preferably 1.5%-4.5%; The mixing portion surrounds the flow guide portion and comprises at least two concentrically arranged fluid-disturbing rings, each fluid-disturbing ring being provided with at least six fluid-disturbing bodies (21) distributed evenly, the surface of the fluid-disturbing bodies (21) being non-porous, and the presence of the fluid-disturbing bodies (21) making the total porosity of the mixing portion 30%-95%, preferably 60%-90%; and The total void area of ​​the mixing portion is 30-500 times, preferably 50-250 times, the total void area of ​​the guide plate.

2. The spoiler member according to claim 1, characterized in that: The diameter of the spoiler member (15) is D1, and the diameter of the guide plate (20) is d b , 0.2D1≤d b ≤0.6D1; preferably, the outer diameter of the mixing part is D1 and the inner diameter is d b .

3. The spoiler member according to claim 1 or 2, characterized in that: The opening diameter of the air holes on the guide plate (20) is 5-50 mm, preferably 5-20 mm, and the diameter of each air hole is substantially equal.

4. A spoiler member according to any one of the preceding claims, characterized in that The air holes on the guide plate (20) are arranged regularly, and the air holes are arranged in an equilateral triangle with equal spacing between each other, or in a circular array with equal spacing with the center of the guide plate (20) as the center of the circle.

5. A spoiler member according to any one of the preceding claims, characterized in that The mixing section comprises 2 to 10 fluid-disturbing rings which are concentrically arranged around the guide plate (20) and spaced in sequence, and the spacing between the fluid-disturbing rings is equal.

6. A spoiler member according to any one of the preceding claims, characterized in that The disrupting bodies (21) have the same shape, with an aspect ratio of 3:1-10:1, an equivalent diameter of a horizontal cross section of the disrupting bodies (21) of 10-150 mm, preferably 10-100 mm, and a shape of the horizontal cross section selected from a rectangle, a square, a circle, an ellipse and a rhombus; wherein the disrupting bodies are arranged vertically.

7. A spoiler member according to any one of the preceding claims, characterized in that The guide part also includes a guide member for guiding the material at the edge of the mixing part to the middle part. Preferably, the guide member is configured as a side ring (22) connected to the largest size of the fluid-disturbing ring. The width of the side ring (22) is X, preferably D1 / 64≤X≤D1 / 16, more preferably D1 / 50≤X≤D1 / 20.

8. A fluidized bed reactor comprising a reaction chamber, characterized in that: The reaction chamber is provided with two or more flow-disturbing members (15) arranged along the axial direction of the reactor, the flow-disturbing members (15) conform to the cross-sectional shape of the reaction chamber, and the diameter D1 of the flow-disturbing members (15) is substantially equal to the inner diameter D of the reaction chamber, wherein the flow-disturbing members (15) are the flow-disturbing members according to any one of claims 1 to 7.

9. The reactor according to claim 8, characterized in that The structures of the two or more spoiler members (15) are the same or different, preferably the same; the reactor has at least one solid-phase feed port, and the first spoiler member from bottom to top in the reactor is arranged above all the solid-phase feed ports, 0.2-1.5 m, preferably 0.5-1.2 m away from the geometric center of the top solid-phase feed port.

10. The reactor according to claim 8 or 9, characterized in that The two or more spoiler members (15) are installed at equal intervals, with an installation interval ΔH of 0.5m≤ΔH≤1.5m.

11. The reactor according to any one of claims 8 to 10, which is a circulating fluidized bed reactor, characterized in that: A raw material gas distributor (8) is provided at the bottom end of the reaction chamber of the reactor, and one or more solid-phase feed ports for circulating catalyst feed are provided on the chamber wall above the raw material gas distributor (8). At least one of the solid-phase feed ports extends into the reaction chamber and is connected with a solid distribution member (17) in the direction towards the center of the reaction chamber; The solid distribution member (17) includes a bottom plate (18) and at least two side baffles (19) oppositely installed on the bottom plate. A flow channel for solid distribution is defined by the bottom plate (18) and the side baffles (19) together. The flow channel is trapezoidal in shape, the upper base of the trapezoidal flow channel is connected to the solid-phase feed port, and the bottom plate is tangent to the inner edge of the feed port; The included angles between the waists and the lower base of the trapezoidal flow channel are α1 and α2, and 30° ≤ α1 < 90°, preferably 45° ≤ α1 ≤ 75°, 30° ≤ α2 < 90°, preferably 45° ≤ α2 ≤ 75°; The length of the upper base of the trapezoid is j, and dg ≤ j ≤ 2dg, preferably dg ≤ j ≤ 1.5dg, where dg is the equivalent diameter of the solid-phase feed port; The height of the trapezoid is hh, and 0.01D ≤ hh ≤ 0.2D, preferably 0.05D ≤ hh ≤ 0.15D, where D is the inner diameter of the reaction chamber.

12. The reactor according to claim 11, characterized in that The bottom plate (18) is also trapezoidal in shape, its upper base is collinear with the upper base of the flow channel, and the lengths of its upper base and lower base are respectively greater than those of the upper base and lower base of the flow channel, and it has the same symmetry center line as the flow channel. Among them: The included angles between the waists and the lower base of the trapezoidal bottom plate (18) are β1 and β2, 30° ≤ β1 < 90°, preferably 45° ≤ β1 ≤ 75° and β1 ≤ α1, 30° ≤ β2 < 90°, preferably 45° ≤ β2 ≤ 75° and β2 ≤ α2; and The length of the upper base of the trapezoidal bottom plate (18) is k, and j < k ≤ 2j, preferably j < k ≤ 1.6j.

13. The reactor according to claim 11 or 12, characterized in that A plurality of distribution holes are provided in the front-end area of the bottom plate (18). The total void ratio of the holes on the bottom plate (18) is 1% - 10%, preferably 4% - 8%. Preferably, the front-end area where the distribution holes are provided is the area between 45% - 95%, preferably 65% - 95% of the height hh in the direction from the upper base to the lower base within the flow channel on the bottom plate. Preferably, the diameter of the distribution holes is 2 - 10 mm, preferably 4 - 8 mm. Preferably, the diameters of each distribution hole are substantially equal. Preferably, the opening distribution of at least part of the distribution holes is an equilateral triangle distribution with front and rear rows staggered, or a rectangular distribution with front and rear alignment.

14. The reactor according to any one of claims 11 to 13, characterized in that The bottom plate is a flat plate or a corrugated plate. Preferably, the corrugation of the corrugated plate is a cosine wave, a circular wave or an elliptical wave. Preferably, the bottom plate (18) forms an angle θ with the horizontal plane, where 0° ≤ θ ≤ 45°, preferably 15° ≤ θ ≤ 30°.

15. The reactor according to any one of claims 8 to 14, which is a circulating fluidized bed reactor, characterized in that: A raw gas distributor (8) is provided at the bottom end of the reaction chamber of the reactor, and a plurality of solid-phase feed ports for circulating catalyst feed are provided on the chamber wall above the raw gas distributor (8), wherein the plurality of solid-phase feed ports are respectively used to feed catalysts in the same or different states, and include at least one type I solid-phase feed port for a relatively large amount of solid feed, and at least one type II solid-phase feed port for a relatively small amount of solid feed, wherein the geometric center of the type I solid-phase feed port and the geometric center of the type II solid-phase feed port are in a straight line in the vertical direction, or the deviation does not exceed 5°; The vertical distance between the geometric center of the type II solid phase feed port and the geometric center of the type I solid phase feed port is h, 0.5(dc+dz)≤h≤1.5dc, preferably 0.5(dc+dz)≤h≤dc, wherein: dc is the equivalent diameter of the Type I solid phase feed port, and dz is the equivalent diameter of the type II solid phase feed port; At least the type I solid phase feed port extends into the reaction chamber and is connected to a solid distribution member (17) toward the center of the reaction chamber.

16. The reactor according to claim 15, characterized in that The multiple solid-phase feed ports also include at least one additional solid-phase feed port, which is also used for relatively large amounts of solid feed and is circumferentially at least 120°, preferably at least 150°, away from the geometric center of the type I solid-phase feed port; wherein the additional solid-phase feed port is preferably not connected to a solid distribution piece (17).

17. The reactor according to claim 15 or 16, characterized in that The multiple solid-phase feed ports include one or more additional solid-phase feed ports, and the geometric centers of the one or more additional solid-phase feed ports and the type-I solid-phase feed ports are all symmetrically distributed on the circumference; wherein, preferably, one or more, preferably all, of the additional solid-phase feed ports are also provided with the solid distribution member (17) in the direction toward the center of the reaction chamber.

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