Turbulation member, fluidized bed reactor provided with turbulation member and use thereof

Abstract

The application discloses a turbulence member, a fluidized bed reactor provided with the turbulence member, application of the fluidized bed reactor and a method for producing olefins by converting methanol. The turbulence member can strengthen mixing, realize favorable material distribution and uniformity. Further, the fluidized bed reactor can greatly promote mixing efficiency between multiple solid-phase materials and between gas and solid phases, reduce unevenness of catalyst distribution on a unit height cross section, significantly reduce carbon difference distribution on the cross section, strengthen gas-solid contact, promote continuous generation of low-carbon olefins, improve performance of the reactor, and further improve production efficiency, economy and environmental protection of the whole process.

Description

Technical Field

[0001] This invention relates to the field of fluidized bed reactors, and more specifically to turbulence-inducing components, fluidized bed reactors equipped with turbulence-inducing components and their applications, and methods for converting methanol to olefins. Background Technology

[0002] With the continuous growth of global energy demand and the ongoing optimization of the energy structure, the efficient conversion and utilization of coal, as a traditional but abundant fossil energy source, has become an important topic for scientific research and industrial applications. 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 petroleum resources but also provides an effective way to achieve the clean and efficient conversion of coal resources.

[0003] In the MTO process, the fluidized bed reactor, as the core equipment for converting methanol to olefins, directly determines the selectivity, conversion rate, and stability of the reaction due to its internal multiphase flow and mixing effects. Specifically, the mixing zone of the reactor's reaction chamber is a crucial site for key chemical reactions. The rapid and efficient mixing of multiple solid-phase catalyst particles with different temperatures, carbonization levels, and particle size distributions with the gaseous feedstock within this zone is essential for improving the selectivity of low-carbon olefins (such as ethylene and propylene). Moreover, as the scale of the reactor continues to increase, the complexity of the mixing zone in the reaction chamber significantly increases, and undermixing between different materials becomes more pronounced, leading to a decline in reaction performance and consequently affecting the overall economic and environmental performance of the process.

[0004] While some solid distributors have been designed to optimize the uniform distribution of solid particles within the equipment, there is limited research on improving the mixing of multiple different materials in fluidized bed reactors.

[0005] CN202208702U discloses a catalyst distributor for promoting uniform distribution of the spent catalyst in a catalytic cracking regenerator. The distributor is located at the center of the equipment and extends radially with a distribution arm. The spent catalyst enters the equipment through the small holes and end openings of the distribution arm, thereby improving the distribution.

[0006] CN102504861A discloses a novel catalyst distributor for catalytic cracking. The distributor includes multiple distribution grooves and distribution holes, and uses a "cushion" type dense phase fluidization method to deliver the catalyst to different positions of the equipment flow section to achieve gas-solid mixing.

[0007] These existing solid distributors primarily focus on optimizing gas-solid distribution during catalyst regeneration, rather than being specifically designed for reaction processes involving the mixing of multiple solid phases (such as MTO). The application of these distributors in MTO fast fluidized bed reactors is limited; they struggle to effectively handle the complex environment of high gas velocities and significant interactions between multiple material streams, resulting in suboptimal mixing.

[0008] The paper by Zhu Liyun, Liu Zetian, et al. (“Study on particle mixing characteristics in the pre-lifting structure of two catalysts in FCC riser”, Journal of Chemical Engineering of Chinese Universities, 2014, Vol. 28, No. 3, pp. 510-517) reported that by adding a concentric central tube at the bottom of the FCC riser, the cavity is divided into a central tube region and an annular region, achieving ideal mixing of different solid materials 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 adding a central tube results in less uniform mixing of different materials in the vicinity of the central tube.

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

[0010] The purpose of this invention is to overcome the problem of reduced reaction performance caused by insufficient mixing between multiple catalysts and between the gas and solid phases with different temperatures, carbonization levels, and particle size distributions in the mixing region of the reaction chamber after the engineering scale-up of existing fast fluidized bed reactor technology. This invention aims to develop a specific flow-dispersing component and, based on this, to develop a fluidized bed reactor equipped with the flow-dispersing component, its application, and a method for methanol conversion to olefins. This enables enhanced mixing of different materials in the mixing region of the reaction chamber of the reactor, especially the fluidized bed reactor, thereby achieving favorable material distribution and uniformity, and ultimately improving reactor performance as well as the overall process efficiency, economy, and environmental friendliness.

[0011] To achieve the above objectives, the present invention provides a flow-disrupting component comprising a guide portion and a mixing portion coaxially distributed in the radial direction. The guide portion includes a guide plate with at least three substantially uniformly distributed air passages, and the total porosity of the openings in the guide plate is 0.2%-6%, preferably 1.5%-4.5%. The mixing portion surrounds the guide portion and includes at least two concentrically arranged turbulent rings, each turbulent ring having at least six uniformly distributed turbulent fluids. The turbulent fluids have no pores on their surface, and the presence of the turbulent fluids results in a total porosity of 30%-95%, preferably 60%-90%. The total porosity area of ​​the mixing portion is 30-500 times, preferably 50-250 times, the total porosity area of ​​the guide plate.

[0012] Another aspect of the present invention provides a fluidized bed reactor including a reaction chamber, wherein two or more flow-disrupting members are arranged along the reactor axis in the reaction chamber, the flow-disrupting members conform to the cross-sectional shape of the reaction chamber, and the diameter D1 of the flow-disrupting members is substantially equal to the inner diameter D of the reaction chamber, wherein the flow-disrupting members are the flow-disrupting members according to the present invention, and preferably the flow-disrupting members are installed at equal intervals along the axial direction.

[0013] Another aspect of the present invention provides a circulating fluidized bed reactor including a reaction chamber, wherein a feed gas distributor is disposed at the bottom end of the reaction chamber, and one or more solid-phase feed ports for feeding a circulating catalyst are formed on the chamber wall above the feed 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 includes a bottom plate and at least two side baffles mounted opposite each other 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 feed inlet, and the bottom plate is tangent to the inner edge of the feed inlet; the included angles between the waist 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 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.

[0014] In another aspect, the present invention provides a circulating fluidized bed reactor including a reaction chamber, wherein a feed gas distributor is provided at the bottom of the reaction chamber, and multiple solid-phase feed ports for feeding circulating catalyst are provided on the chamber wall above the feed gas distributor. The multiple solid-phase feed ports are respectively used to feed catalyst 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. The geometric center of the type I solid-phase feed port and the geometric center of the type II solid-phase feed port are aligned vertically or deviate from each other 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, where: 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.

[0015] The present invention also provides the application of the aforementioned turbulence-inducing component or the aforementioned fluidized bed reactor in methanol conversion to olefins, catalytic cracking, or fluidized bed propane dehydrogenation.

[0016] This invention also provides a method for methanol-to-olefins conversion. The method employs the reaction equipment described in this invention, such as a fluidized bed reactor. It includes feeding methanol feed gas and multiple catalyst streams containing regenerators, circulating agents, and external heat exchangers into the feed section. Upon entering the equipment, the materials move upwards in parallel under gas-phase carry, forming contact and reacting to generate a gas-solid mixture containing low-carbon olefins. This gas-solid mixture is deflected by the guide plate of the turbulence-inducing component and flows radially. Continuing through an array of turbulent fluids, numerous negative-pressure vortices are formed after each turbulent fluid, increasing turbulence intensity. Nearby catalyst streams are carried and filled into these numerous vortices after the turbulent fluids. This further disperses the previously relatively concentrated regenerators, circulating agents, and external heat exchangers within the chamber due to the airflow, significantly enhancing the mixing degree between the multiple catalyst streams, greatly increasing gas-solid contact efficiency, and making the reaction conditions in different areas of the equipment more uniform. This suppresses side reactions, increases the proportion of target low-carbon olefins in the product gas, and then continues upwards into the separation chamber for gas-solid separation.

[0017] Furthermore, by using a specific solid distribution component connected to the solid feed inlet, the aggregation and falling of solid particles near the wall surface is prevented, and the solid materials are further dispersed after entering the reactor, resulting in a better concentration distribution of the catalyst on different horizontal planes and a more uniform distribution of catalyst coke.

[0018] Based on this, the reaction equipment can be further optimized by adjusting the Type II solid-phase feed inlet (e.g., regenerator feed inlet) for a relatively small amount of solid feed to be directly above the Type I solid-phase feed inlet (e.g., external heat recovery agent feed inlet) for a relatively large amount of solid feed, or by deviating by no more than 5°. Although the feed rate of regenerator is much smaller than that of external heat recovery agent, the regenerator has a high temperature, low carbon deposition, and high reactivity. It is prone to affecting the reaction selectivity due to excessively high local temperatures within the reactor. By adjusting the feed to be above the external heat recovery agent feed inlet, the feed regenerator, due to inertia, will flow directly downwards for a certain distance after entering the equipment. During the inertial descent, it can first mix with the external heat recovery agent, whose flow rate is much larger than its own, and merge into the large flow of external heat recovery agent. Then, it is dispersed by the gas phase flow, maximizing the premixing of the catalyst within the equipment, which is beneficial to improving the initial distribution effect of the catalyst particles entering the equipment.

[0019] Through the above technical solutions, the turbulence-enhancing component of the present invention can strengthen mixing and achieve 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 the gas and solid phases, reduce the non-uniformity of catalyst distribution per unit height cross-section, significantly reduce the carbon difference distribution on the cross-section, strengthen gas-solid contact, promote the continuous generation of low-carbon olefins, improve reactor performance, and thus improve the overall process's production efficiency, economy, and environmental friendliness.

[0020] The present invention also discloses the following embodiments:

[0021] Solution 1: A flow-disrupting component for mixing gas and solid phases, characterized in that the flow-disrupting component (15) comprises a flow-guiding section and a mixing section, wherein,

[0022] The flow guiding section includes a flow guiding plate (20) for causing a fluid containing both gas and solid phases to flow toward the mixing section;

[0023] The mixing section includes a plurality of turbulent fluids (21), which are used to cause the fluid to pass through and form vortices to enhance the interphase disturbance between the gas and solid phases. The plurality of turbulent fluids (21) are distributed at intervals around the guide plate (20).

[0024] Scheme 2, the turbulence component according to Scheme 1, characterized in that the mixing part includes a plurality of turbulence rings arranged concentrically around the guide plate (20) and spaced apart in sequence, each of the turbulence rings including a plurality of turbulence fluids (21) arranged in a ring shape along the circumferential distance of the guide plate (20); preferably the turbulence fluids (21) are set as vertically placed cylinders.

[0025] Scheme 3: According to Scheme 2, the flow-deflecting component is characterized in that the flow-guiding part further includes a guide for guiding the airflow at the edge of the mixing part to the center, preferably the guide is configured as a side ring (22) connected to the largest flow-deflecting ring, more preferably the width of the side ring (22) is X, X≤D / 16, wherein when the flow-deflecting component (15) is installed in the cavity, the diameter of the cavity is D;

[0026] and / or

[0027] The guide plate (20) has multiple air passage holes. Preferably, the opening ratio 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;

[0028] and / or

[0029] The smallest diameter turbulence ring is embedded in the edge of the guide plate (20).

[0030] Scheme 4, a gas-solid reaction device, characterized in that the gas-solid reaction device includes a gas-solid reactor (1), the gas-solid reactor having a connected reaction chamber (6) and a separation chamber (2), wherein the reaction chamber (6) includes a feeding section and a turbulence section located above the feeding section, and at least one turbulence component (15) as described in any one of Schemes 1-3 is installed in the turbulence section, preferably a plurality of the turbulence components (15) are installed at equal intervals along the axial direction in the reaction chamber (6).

[0031] Scheme 5. The reaction equipment according to Scheme 4 is characterized in that a raw material gas distributor (8) is provided at the bottom of the feeding section, a solid phase feed port is provided on the cavity wall of the feeding section above the raw material gas distributor (8), and a distribution member (17) is provided in the reaction chamber, the distribution member (17) being used to disperse the solid phase fed from the solid phase feed port in the feeding section.

[0032] Preferably, the distribution member (17) includes a corrugated plate (18) and side baffles (19) spaced apart on the corrugated plate (18);

[0033] More preferably,

[0034] The front end region of the waveform plate (18) is provided with a plurality of distribution holes, and the opening ratio of the waveform plate (18) is 5% to 10%.

[0035] and / or

[0036] The cross-section of the corrugated plate (18) is an isosceles trapezoid, and the large end of the corrugated plate (18) extends toward the center of the feed section.

[0037] Scheme 6: The reaction apparatus according to Scheme 5 is characterized in that 45°≤β≤α≤75°, where 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).

[0038] and / or

[0039] j≥0.5k, where the length of the small end of the waveform plate (18) is k, and the distance between the side baffles (19) near the small end of the waveform plate (18) is j.

[0040] Scheme 7: The reaction apparatus according to Scheme 5, characterized in that the solid feed inlet is used for feeding the catalyst, including an external heat-extracting agent inlet (7) and a circulating agent inlet spaced circumferentially on the cavity wall of the feed section; wherein, a regenerator inlet (10) is provided in the cavity wall directly above the external heat-extracting agent inlet, and the distance between the regenerator inlet (10) and the external heat-extracting agent inlet (7) is h, preferably 0.5 (d). c +d z )≤h≤1.5d c d c d is the equivalent diameter of the external heat exchanger inlet (7). z The equivalent diameter of the regenerator inlet (10);

[0041] and / or

[0042] The solid feed inlet is provided with the distribution member (17), and the height of the side baffle (19) of the distribution member (17) is L, wherein L is in the range of 0.2 to 0.5 times the equivalent diameter of the solid feed inlet;

[0043] Preferably, the external heat exchanger inlet (7) is provided with the distribution element (17), 0.2d c ≤L≤0.5d c ;

[0044] and / or

[0045] The distance between the regenerant inlet and the turbulence-causing component (15) is 0.3m to 0.6m.

[0046] Application of the turbulence-inducing component (15) described in any one of Schemes 8, Schemes 1-3, or the reaction equipment described in any one of Schemes 4-7 in methanol conversion to olefins, catalytic cracking, or fluidized bed propane dehydrogenation.

[0047] Scheme 9, a method for producing olefins from methanol, characterized in that the method uses the reaction equipment described in any one of Schemes 4-7, including feeding methanol feed gas (f) and catalyst into the feed section, so that the methanol feed gas (f) comes into contact with the catalyst and reacts to generate a gas flow containing low-carbon olefins, and then the gas flow containing low-carbon olefins passes upward through the turbulence member (15) to form turbulence to enhance the interphase disturbance between the gas and solid phases, and then continues to enter the separation chamber (2) for gas-solid separation.

[0048] Scheme 10: According to the method described in Scheme 9, the methanol feed gas (f) is preheated and then fed into the feed section through the feed gas distributor (8), wherein the preheating temperature is 150-200°C, and the apparent velocity u of the methanol feed gas (f) entering the feed section is... f The speed range is 0.8-2.0 m / s.

[0049] and / or

[0050] The catalyst includes catalyst g, which is returned after heat extraction from the external heat extraction agent inlet feed, circulating catalyst r, which is fed from the circulating agent inlet feed, and regenerator z, which is fed from the regenerator inlet feed.

[0051] and / or

[0052] The catalyst enters the feed section through a distributor, preferably the catalyst g that has been heated and returned enters the feed section through the distributor;

[0053] and / or

[0054] The average concentration of the catalyst in the reaction chamber is 60-120 kg / m³. 3 Preferred weight: 80-115 kg / m 3 ; and / or

[0055] The reaction temperature in the reaction chamber (6) is 450-500℃ and the reaction pressure is 0.01-1MPa.

[0056] Other features and advantages of the present invention will be described in detail in the following detailed description section. Attached Figure Description

[0057] The accompanying drawings are provided to further illustrate the present application and form part of the specification. They are used together with the following detailed description to explain the present application, but do not constitute a limitation thereof. In the drawings:

[0058] Figure 1a This is a schematic diagram of the structure of a flow-disrupting component according to a specific embodiment of the present invention;

[0059] Figure 1b yes Figure 1a A partial schematic diagram of the aerodynamic component shown;

[0060] Figure 2a and 2b These are schematic diagrams showing the distribution of air passage holes on the guide plate according to some specific embodiments of the present invention;

[0061] Figure 3a -d are schematic diagrams of the structure of the turbulent fluid with different horizontal cross-sectional shapes according to some specific embodiments of the present invention;

[0062] Figure 4 This is a schematic diagram of a gas-solid reaction apparatus according to a specific embodiment of the present invention;

[0063] Figure 5 This is a schematic diagram of the structure of a solid distribution component according to a specific embodiment of the present invention;

[0064] Figure 6 This is a top view of a solid distribution component according to a specific embodiment of the present invention and a schematic diagram of the distribution holes therein;

[0065] Figure 7 This is a side view of a solid distribution component and a solid feed inlet according to a specific embodiment of the present invention;

[0066] Figure 8 This is a schematic diagram of the solid feed inlet and solid distribution components of the feed section of a circulating fluidized bed reactor according to a specific embodiment of the present invention.

[0067] Figure 9 This is a schematic diagram of the structure of an MTO continuous reaction regeneration fluidized bed device based on existing technology;

[0068] Figure 10 This is a structural schematic diagram of a slanted baffle-type turbulence-disrupting component based on existing technology;

[0069] Figure 11 This is a structural schematic diagram of a flat baffle-type solid distribution component based on existing technology.

[0070] The components in the accompanying drawings are not necessarily drawn to scale; rather, the emphasis is on illustrating the principles of the embodiments. In different drawings or views, the same reference numerals refer to the same or corresponding components.

[0071] Explanation of reference numerals in the attached figures

[0072] 1. Gas-solid reactor; 2. Separation chamber; 3. Riser; 4. External heat exchanger; 5. Circulating agent inlet; 6. Reaction chamber; 7. External heat exchanger inlet; 8. Raw material gas distributor; 9. Circulating agent inlet; 10. Regenerator inlet; 11. Fluidizing air distributor; 12. Regenerator pipe; 13. Degassing tank; 14. Catalyst regenerator; 15. Turbulence component; 16. Catalyst fine powder inlet; 17. Solid distribution component; 18. Bottom plate; 19. Side baffle; 20. Guide plate; 21. Turbulent fluid; 22. Side ring; 23. Support plate; 24. Rib plate; 25. Wall surface. Detailed Implementation

[0073] The specific embodiments of this application will be described in detail below with reference to the accompanying drawings. It should be understood that the specific embodiments described herein are for illustration and explanation only and are not intended to limit this application.

[0074] 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 pertains. In the event of any conflict, including definitions, this specification shall prevail.

[0075] When this specification describes materials, methods, components, apparatus, or devices using terms such as "known to those skilled in the art" or "conventionally known in the art" or similar expressions, such terms mean that this specification includes those conventionally used in the art at the time of filing of this application, but also those that are not currently commonly used, but will become generally accepted in the art for similar purposes.

[0076] The endpoints and any values ​​of the ranges disclosed herein are not limited to the precise ranges or values, and such ranges or values ​​should be understood to include values ​​close to such ranges or values. For numerical ranges, the endpoint values ​​of the various ranges, the endpoint values ​​of the various ranges and individual point values, and individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed herein.

[0077] In this invention, when a technical solution is given in an open-ended form such as "comprising" or "including" certain listed elements, those skilled in the art will understand that embodiments constituted by or substantially constituted by these elements can obviously be used to implement the technical solution. Therefore, those skilled in the art will understand that the technical solutions given in this invention with such open-ended definitions also cover specific embodiments constituted by or substantially constituted by the listed elements.

[0078] In this invention, "range" is given in the form of lower and upper limits, such as one or more lower limits and one or more upper limits. A given range can be defined by selecting a lower limit and an upper limit, which define the boundaries of the given range. All ranges defined in this way are inclusive and composable, meaning that any lower limit can be combined with any upper limit to form a range. For example, if ranges of 60-110 and 80-120 are listed for specific parameters, it is also expected that ranges of 60-120 and 80-110 are also expected. Furthermore, if the listed lower limits are 1 and 2 and the listed upper limits are 3, 4 and 5, then the following ranges are all expected: 1-3, 1-4, 1-5, 2-3, 2-4, and 2-5.

[0079] Unless otherwise specified, all percentages, parts, ratios, etc. mentioned in this specification are based on weight; however, if using weight as a basis does not conform to the conventional understanding of those skilled in the art, the basis shall be determined by the conventional understanding of those skilled in the art.

[0080] In this invention, unless otherwise stated, directional terms such as "upper," "lower," "top," and "bottom" are generally used to describe the relative positions of components in relation to the directions shown in the accompanying drawings or in relation to the vertical, perpendicular, or gravitational directions. "Inner" and "outer" generally refer to radial inward or outward relative to the center of a circle or to the inner or outer part of a cavity relative to the cavity itself.

[0081] In this invention, a vortex refers to the phenomenon where the boundary layer near the wall of the turbulent fluid separates after the airflow passes through the turbulent fluid and forms a negative pressure, causing the nearby fluid to flow back and fill the original space to form a vortex. The vortex is beneficial to the mass and heat transfer in the reaction process.

[0082] In this invention, the ring core effect refers to the process in which the gas phase in the rapid fluidized bed carries the solid phase and flows upward. As the gas phase gradually gathers in the center of the bed, the particles carrying the attachments move upward, while the catalyst particles in the near-wall area far from the center gather relatively and move downward. Thus, the particles form a circulating flow between the near center and near the wall of the equipment for mass and heat transfer.

[0083] In this invention, when referring to the “equivalent diameter” of the solid feed inlet, it generally refers to the inner diameter of the solid feed inlet, unless otherwise stated.

[0084] Fluidized beds generally involve at least two gas-solid phases, and typically involve the mixing of these two phases, thus constituting a typical gas-solid reaction apparatus. It is readily understood that, in this invention, when used as a fluidized bed reactor, the fluidized bed generally contains at least one reaction chamber. For the purposes of this invention, when a dedicated solid circulation channel (generally located outside the fluidized bed) is established in addition to the up-and-down movement of solids in the fluidization zone caused by fluidization to transport (especially, for example, transporting in the opposite direction to the movement caused by fluidization) solids (e.g., catalyst particles), such a fluidized bed can be referred to as a "circulating fluidized bed" for the purposes of this invention. For example, in a riser-type fluidized bed reactor, catalyst particles are transported upwards and concentrated in the upper part of the riser. To address this, a circulating (catalyst) pipeline can be connected outside the riser to return the catalyst from the upper part of the riser to the lower part, thereby constructing a circulating fluidized bed reactor.

[0085] Accordingly, for the purposes of this invention, the solid circulation channel can be a simple pipeline or a complex pipeline or system in which other devices are also provided at appropriate locations. For example, for a fluidized bed, a simple bypass can be provided relative to the fluidized bed, such that the solids flow in the opposite direction to the flow direction of the fluidized bed; this simple bypass is the solid circulation channel described in this invention. As another example, for an upward-flowing fluidized bed, a portion of the deactivated catalyst can be removed from the top and regenerated in a regenerator to obtain the "regenerant" described in this invention, which is then transported back to the bottom of the fluidized bed; this system with a regenerator can be considered as the solid circulation channel described in this invention. Furthermore, for heat exchange (e.g., heat extraction) purposes, a portion of the catalyst in the fluidized bed reactor can be 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 this invention, which is then transported back to the fluidized bed in the opposite direction to the flow direction of the fluidized bed; this system with a heat exchanger can be considered as the solid circulation channel described in this invention. For example, the gas outlet of a fluidized bed may carry some solids, which can generally be separated by a separation device (such as a cyclone separator) to obtain the "catalyst fine powder" described in this invention, and then the catalyst fine powder is sent back to the fluidization; the system with the separation device can be regarded as the solid circulation channel described in this invention.

[0086] Therefore, any catalyst particles that can be transported through a suitable circulation channel can be referred to as a "recirculating catalyst" in this invention. For example, the regenerator, external heat exchange catalyst (external heat extractor), and catalyst powder can all be considered as "recirculating catalysts" in the fluidized bed according to this invention. In particular, catalysts transported through a simple bypass of the fluidized bed are also a type of "recirculating catalyst" and can be referred to as "circulating agents" in this invention.

[0087] Accordingly, satisfactory mixing of the gas and solid phases is crucial for fluidized beds, especially when using recycled catalysts. On one hand, good gas-solid mixing ensures sufficient contact between the solid catalyst and the gaseous 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. Uneven mixing can lead to fluctuations in product performance, affecting the quality of the final product. Furthermore, the recycling of the catalyst in a fluidized bed is a key aspect of its economic efficiency. Good mixing can reduce catalyst wear and coking, thus extending its service life. Therefore, for fluidized beds (especially circulating fluidized beds), it is often necessary to appropriately adjust the distribution of solids, gases, or both within the fluidized bed (especially in the reaction chamber of a fluidized bed reactor). To this end, the present invention provides a fluidized bed with a specific structure. For the purposes of this invention, for ease of understanding, "solid phase" and "solid" are used interchangeably, as are "gas" and "gas phase."

[0088] In embodiment A of the present invention, the present invention provides a flow-disrupting component 15, which includes a flow-guiding section and a mixing section coaxially distributed in the radial direction, or is composed of the flow-guiding section and the mixing section; and provides a fluidized bed reactor in which two or more of the flow-disrupting components 15 are arranged along the reactor axis in the reaction chamber.

[0089] In embodiment B of the present invention, a circulating fluidized bed reactor is provided, wherein a solids distributor 17 is connected to a solids feed inlet for circulating catalyst. The solids distributor 17 includes a bottom plate 18 and at least two side baffles 19 mounted opposite each other on the bottom plate 18, wherein the bottom plate 18 and the side baffles 19 together define a flow channel for solids to be distributed therethrough, the flow channel being trapezoidal in shape.

[0090] In embodiment C of the present invention, the present invention provides a circulating fluidized bed reactor, which includes a plurality of solid feed ports specifically arranged on the reaction chamber wall of the reactor, including at least one type I solid feed port for a relatively large amount of solid feed and at least one type II solid feed port for a relatively small amount of solid feed, wherein the geometric center of the type I solid feed port and the geometric center of the type II solid feed port are aligned in the vertical direction or deviate from each other by no more than 5°.

[0091] In this 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.

[0092] Implementation Plan A

[0093] According to embodiment A, one aspect of the present invention provides a flow-disrupting component 15, which is particularly suitable for fluidized bed reactors for promoting gas-solid two-phase mixing. For example... Figure 1a As shown, the turbulence member 15 includes a guide section and a mixing section coaxially distributed in the radial direction, or is composed of the guide section and the mixing section.

[0094] In one embodiment, the flow guiding portion of the turbulence member 15 of the present invention includes a flow guiding plate 20, on which at least 3, at least 7, or at least 19 substantially uniformly distributed air passage holes are opened, and the total void ratio of the openings of the flow guiding plate is 0.2%-6%, preferably 1.5%-4.5%.

[0095] In other words, one specific aspect of the present invention is to create an obstacle in the central region of the fluidized bed that obstructs the fluidization direction. Thus, in the fluidized bed reactor described in this invention, when the gas stream carrying solids (also referred to as a gas-solid mixture in this invention) moves to the baffle plate 20, due to resistance, a large portion of the gas stream is diverted to radial flow into the mixing section. Simultaneously, the baffle plate 20 has openings with an appropriate porosity, allowing some gas (and even some solids) to still pass through the openings. It is understood that this construction makes the disturbance between the gas and solid phases at the baffle plate more favorable for the mixing required by the present invention. Without being limited by any known theory, through repeated experiments and simulations, it is believed that a total porosity of 0.2%-6%, preferably 1.5%-4.5%, in the baffle plate is particularly advantageous for achieving the objectives of the present invention (e.g., desirable gas-solid two-phase mixing).

[0096] Those skilled in the art will understand that, for the purposes of this invention, when referring to objects with relatively regular geometric shapes such as holes, plates, and fluid turbulence, 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., the centers of circles) of these objects.

[0097] For the purposes of this invention, the "substantially uniform" distribution of the air passages has the conventional technical meaning understood by those skilled in the art. For example, the centers of the passages are uniformly distributed on the guide plate in the usual sense in the art; for instance, the distance between adjacent centers is substantially equal, and the air passages are uniformly distributed throughout the guide plate. However, it does not exclude the possibility that one or more air passages at the edge of the guide plate or other locations may have center-to-center distances that are close but not equal to other air passages. It is understood that those skilled in the art can clearly determine whether the distribution of the air passages falls under the conventional understanding of a "substantially uniform" distribution based on actual conditions and general knowledge in the art.

[0098] For the purposes of this 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 solids and thus allows at least gas to pass through. For example, it is understood that for a perforated plate, its porosity is the percentage of the sum of the areas of all the holes to the total area of ​​the plate.

[0099] In one embodiment, the diameter of the guide plate 20 of the turbulence 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 section is D1; ​​that is, preferably, the diameter of the largest turbulent ring in the mixing section is the outer diameter of the turbulent member 15. Preferably, the inner diameter of the mixing section is d. b In other words, preferably, the smallest turbulent ring in the mixing section is directly connected to the guide plate 20, with no other components between them. One of the main objectives of this invention is to improve the mixing between the gas and solid phases. As mentioned earlier, setting a guide plate 20 in the central region of the fluidized bed is one of the important technical means, which forms an obstacle to the fluidization direction; however, it is understood that this obstacle needs to exist to an appropriate degree, for example, not to the point that the fluidization state cannot be maintained. Among various factors, the diameter of the guide plate 20 is therefore an important parameter, for example, it obviously cannot be equal to or substantially equal to the inner diameter D of the reaction chamber. Without being limited by any known theory, through repeated experiments and simulation calculations, it is believed that the aforementioned specific diameter d of the guide plate is suitable. b This is particularly advantageous for achieving the objectives of the present invention (e.g., a desirable gas-solid two-phase mixture).

[0100] In one embodiment, the diameter of the air passage holes on the guide plate 20 of the turbulence member 15 of the present invention is 5-50 mm, preferably 10-40 mm, and even more preferably 15-20 mm; and preferably the diameter of each air passage hole is substantially equal. For the purposes of the present invention, the diameter of the air passage holes being "substantially equal" means that the diameter difference between the individual air passage holes does not exceed 10%, preferably not more than 5%, and even more preferably not more than 1%. As mentioned above, the guide plate 20 is appropriately perforated so that some gas (and even some solid) can still pass through the guide plate through the air passage holes. Accordingly, the diameter of the air passage holes needs to be appropriately adjusted, especially to match the diameter of the catalyst; without being limited by any known theory, through repeated experiments and simulation calculations, it is believed that the above-mentioned specific air passage hole diameter of the guide plate is particularly advantageous for achieving the purposes of the present invention (e.g., desirable gas-solid two-phase mixing). On the other hand, the inventors have found through research that, for the fluidized bed of the present invention, the uniformity of the air passage holes will help to further improve the mixing effect of the gas-solid two-phase. Therefore, it is preferable that the diameters of each air passage are substantially equal. Similarly, another manifestation of the uniformity of the air passages described in this invention is the regular arrangement of the air passages. Accordingly, in one embodiment, the plurality of air passages on the guide plate 20 of the turbulence member 15 of this invention are regularly arranged. In one embodiment, as... Figure 2a As shown, the air vents are arranged in equilateral triangles with equal spacing. In one embodiment, as... Figure 2b As shown, the air passages are arranged in a ring array with equal spacing around the center of the guide plate 20. For the purposes of this invention, the specific spacing of the air passages is not particularly limited, as long as it meets the requirements of the air passage diameter and the total porosity of the guide plate as described in this invention. For example, the spacing between the air passages can be 100-800 mm, preferably 200-500 mm.

[0101] Furthermore, it is particularly noteworthy that those skilled in the art will understand that for the perforated guide plate 20, the number and diameter of its air passages together determine the total porosity of the guide plate. Through repeated experiments and simulation calculations, the inventors surprisingly discovered that the diameter of the air passages and the total porosity of the guide plate are relatively more important to the purpose of this invention (e.g., desirable gas-solid two-phase mixing); in contrast, the number of air passages is not particularly limited, and those skilled in the art can set it appropriately, as long as it meets the conditions of this invention regarding the diameter of the air passages, the total porosity of the guide plate, and the basically uniform distribution of the air passages.

[0102] For the fluidized bed reactor described in this invention, especially the fluidized bed reactor of embodiment A, when the gas flow carrying solids moves to the guide plate 20, due to resistance, a large portion of the gas flow is adjusted to radial flow and enters the mixing section. Therefore, the mixing section needs to be provided with a high porosity to facilitate the continued passage of the gas flow carrying solids in a fluidized state. On the other hand, according to the invention, in the mixing section, the gas flow forms a large number of vortices after passing through the turbulent fluid 21, causing interphase disturbance; when the solid phase (e.g., catalyst particles) passes through the mixing section, the probability of collisions between solid phases and between the solid phase and the turbulent fluid 21 increases significantly, promoting the mixing between different solid phases and between the gas and solid phases. That is to say, it is very advantageous to appropriately provide the turbulent fluid in the mixing section, and its space must be at least partially occupied by the turbulent fluid. Correspondingly, the total porosity of the mixing section cannot be too high. Thus, in one embodiment, the mixing portion of the turbulence member 15 of the present invention surrounds the flow guide portion and includes at least two concentrically arranged turbulence rings, each turbulence ring having at least six uniformly distributed turbulence fluids 21, the surface of the turbulence fluids 21 being non-porous, and the presence of these turbulence fluids making the total porosity of the mixing portion less than 95%, preferably less than 90%, and even more preferably less than 80%; and greater than 30%, preferably greater than 40%, and even more preferably greater than 60%.

[0103] In one embodiment, the mixing section of the present invention includes 2-10, preferably 3-8, turbulent fluid rings concentrically arranged and spaced apart from the guide plate 20. Preferably, the spacing between each of the turbulent fluid rings is equal. As previously mentioned, the mixing section of the present invention is used to allow the airflow carrying solids to continue to pass through in a fluidized state, thereby creating interphase disturbances; therefore, the turbulent fluid rings need to be appropriately distributed. Through repeated experiments and simulation calculations, it is believed that arranging the turbulent fluid rings in the aforementioned number and preferably at equal intervals is advantageous.

[0104] As previously mentioned, in the mixing section, the airflow forms numerous vortices after passing through the turbulent fluid 21, causing interphase disturbances. The inventors have experimentally discovered that appropriate "uniformity" in the turbulent fluid and its distribution is also beneficial to achieving the objectives of this invention (e.g., desirable gas-solid two-phase mixing). Accordingly, in one embodiment, the turbulent fluid 21 of this invention has a uniform shape. According to the invention, the airflow forms numerous vortices after passing through the turbulent fluid 21, causing interphase disturbances; therefore, it is understood that the size and shape of the turbulent fluid 21 itself have an influence on the formation of vortices and the result of interphase disturbances. Accordingly, in one embodiment, the aspect ratio of the turbulent fluid 21 is preferably 3:1-10:1, preferably 4:1-8:1. Preferably, the equivalent diameter of the horizontal cross-section of the turbulent fluid 21 is 10-150 mm, preferably 10-100 mm, and the shape of the horizontal cross-section is selected from rectangles, squares, circles, ellipses, and rhombuses. Figure 3a-d shows schematic diagrams of turbulent fluids with circular, elliptical, square, and rhomboid horizontal cross-sectional shapes, respectively. When the horizontal cross-sectional shape of the turbulent fluid is elliptical, the aspect ratio of the turbulent fluid is the ratio of the height of the turbulent fluid to the minor axis of the ellipse; when the horizontal cross-sectional shape of the turbulent fluid is rectangular, the aspect ratio of the turbulent fluid is the ratio of the height of the turbulent fluid to the short side of the rectangle. Preferably, the turbulent fluid is vertically arranged; correspondingly, the "horizontal cross-section" is a cross-section obtained relative to the length direction of the turbulent fluid.

[0105] As previously mentioned, for gas-solid mixtures fluidized in a fluidized bed, the present invention, through the specific arrangement of the guide plates and turbulent rings in the turbulence-inducing member 15, adjusts the gas-solid mixture, originally flowing in the fluidization direction in the central region of the reactor, to flow radially into the mixing section, thereby creating interphase disturbance. Therefore, the ratio of the total void area of ​​the turbulent rings to that of the guide plates has a further influence on the flow and disturbance of the gas-solid mixture. Without being limited by any known theory, through repeated experiments and simulation calculations, it is believed that, particularly advantageous for achieving the objectives of the present invention (e.g., desirable gas-solid two-phase mixing), the total void area of ​​the mixing section is 30-500 times, preferably 50-250 times, the total void area of ​​the guide plates.

[0106] In one embodiment, the flow guide of the present invention further includes a guide for guiding the material at the edge of the mixing section toward the center. Preferably, the guide is configured as a side ring 22 connected to the largest turbulent flow ring. The width of the side ring 22 is X, preferably D1 / 64≤X≤D1 / 16, more preferably D1 / 50≤X≤D1 / 20.

[0107] According to embodiment A, 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-dispersing members 15 as defined above, arranged along the reactor axial direction. The flow-dispersing members 15 conform to the cross-sectional shape of the reaction chamber, and the diameter D1 of the flow-dispersing members 15 is substantially equal to the inner diameter D of the reaction chamber. For the purposes of this invention, those skilled in the art will understand that "substantially equal to D" means that, for practical installation purposes, the value of D1 is less than, but as close as possible to, D within the limits of the actual process. The specific degree of closeness and difference between the two can be determined by those skilled in the art based on the actual situation and general understanding in the field. For example, D1 may be no more than 1% or 0.5% smaller than D.

[0108] In one embodiment, the two or more flow-disrupting members 15 of the present invention may each have the same or different structures. As previously described, the present invention exerts strong disturbance on the fluidized gas-solid mixture through flow-disrupting members. Similar to the uniformity of the individual components on the flow-disrupting members, the uniformity between the flow-disrupting members also contributes to achieving the desired objectives of the present invention in a predictable manner. Therefore, in one embodiment, the use of multiple identical flow-disrupting members is preferred for the present invention.

[0109] This invention relates to fluidized bed reactors (e.g., embodiment A), and may be, for example, circulating fluidized bed reactors (e.g., embodiments B and C); accordingly, according to the invention, solid-phase feed may be involved in the fluidized bed reactor. Preferably, the reactor has at least one solid-phase feed inlet, and a first, bottom-up, turbulence-inducing member is arranged above all the solid-phase feed inlets, at a distance of 0.2-1.5 m, preferably 0.5-1.2 m, from the geometric center of the uppermost solid-phase feed inlet. As previously stated, the invention exerts strong disturbance on the fluidized gas-solid mixture through the turbulence-inducing member. Accordingly, to enable better interaction between the turbulence-inducing member and the fluidized gas-solid mixture, experimental verification has shown that not only is it necessary to arrange all the turbulence-inducing members above all the solid-phase feed inlets, but also to appropriately set the distance between the first turbulence-inducing member and the uppermost solid-phase feed inlet. Through repeated experiments and simulation calculations, it is believed that the aforementioned specific distance is particularly advantageous for achieving the objectives of the invention (e.g., desirable gas-solid two-phase mixing). Similarly, in order to facilitate the achievement of the objectives of the present invention (e.g., desirable gas-solid two-phase mixing), through repeated experiments and simulation calculations, it is preferred that the two or more flow-disrupting components 15 described in the present invention are installed at equal intervals, and it is even more preferred that the installation interval ΔH satisfies 0.5m≤ΔH≤1.5m.

[0110] When the turbulence-disrupting component 15 is installed in the cavity of the reaction chamber, during the airflow process, there is a situation where the solid phase concentration near the cavity wall is relatively high due to the ring core effect. According to a preferred embodiment of the present invention, in order to guide the near-wall particles to flow towards the center and increase gas-solid contact, the flow guide further includes a guide for guiding the material at the edge of the mixing section towards the center. Preferably, the guide is set as a side ring 22 connected to the largest turbulence-disrupting ring, the width of the side ring 22 being X, preferably D / 64≤X≤D / 16, more preferably D / 50≤X≤D / 20, where D is the inner diameter of the reaction chamber. In one embodiment, the cross-section of the flow guide plate 20 is preferably circular, and the diameter of the flow guide plate 20 is d. b 0.2D≤d b ≤0.6D.

[0111] In one exemplary implementation, such as Figure 1aAs shown, the turbulence-inducing component 15 includes a guide section and a mixing section coaxially distributed in the radial direction. The guide section includes a guide plate 20 and a side ring 22 for guiding material from the edge of the mixing section towards the center. Multiple, substantially uniformly distributed air passages are formed on the guide plate 20. The mixing section surrounds the guide section and includes six turbulence-inducing rings concentrically arranged and spaced apart from each other around the guide plate 20. The smallest diameter turbulence-inducing ring is embedded in the edge of the guide plate 20. Each turbulence-inducing ring includes multiple turbulence-inducing fluids 21 arranged in a ring shape at circumferential intervals along the guide plate 20. The turbulence-inducing fluids 21 are configured as vertically arranged cylinders, so that the airflow forms vortices after passing through the cylindrical arc surface, resulting in more uniform mixing of the gas and solid phases. It is understood that the shape of the turbulence-inducing fluid in this invention is not limited to a cylinder; any shape that allows the airflow to form vortices is acceptable. Figure 1a As shown in -b, the turbulent fluids on the same turbulent fluid ring can be connected by circumferential ribs to provide support for the turbulent fluids and fix their spacing. Similarly, turbulent fluids on different turbulent fluid rings in the same radial direction can be connected by radial ribs to provide support for the turbulent fluid rings and fix their spacing. There is no particular limitation on the number of ribs connecting the turbulent fluids; those skilled in the art can set them appropriately, as long as they meet the conditions of this invention regarding the total porosity and total void area of ​​the mixing section, and fixing the spacing between the turbulent fluids and the turbulent fluid rings to ensure their substantially uniform distribution.

[0112] Based on the aforementioned turbulence-inducing component 15 and fluidized bed reactor according to embodiment A, another aspect of the present invention discloses a gas-solid reaction apparatus. For example... Figure 4 As shown, the gas-solid reaction apparatus includes a gas-solid reactor 1, such as a fluidized bed reactor according to embodiment A, and 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, with a gas phase outlet p at the top of the separation chamber 2. The reaction chamber 6 includes a feed section and a turbulence section located above the feed section, in which multiple turbulence-inducing components 15 are installed at equal intervals along the axial direction.

[0113] The gas-solid reaction apparatus of the present invention, since including the flow-dispersing member 15 of the present invention, also has the aforementioned advantages of the flow-dispersing member.

[0114] Implementation Plan B

[0115] According to embodiment B, one aspect of the present invention provides a solids distributor 17 for a solid feed, which is particularly suitable for a circulating fluidized bed reactor for promoting 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.

[0116] According to embodiment B, another aspect of the present invention provides a circulating fluidized bed reactor, such as... Figure 4As shown, a feed gas distributor 8 is provided at the bottom of the reactor's reaction chamber. One or more solid-phase feed ports, preferably 1-5, are provided on the wall of the feed section above the feed gas distributor 8 for circulating catalyst feeding. At least one of the solid-phase feed ports extends into the reaction chamber and is connected to the solid distribution member 17 towards the center of the reaction chamber. Thus, the gaseous feed gas fed from the bottom contacts the solid phase in a counter-current manner, forming an upward airflow carrying the solid phase. The solid distribution member 17 disperses the solid phase fed from the solid-phase feed port throughout the feed section.

[0117] As previously mentioned, circulating fluidized bed reactors generally involve catalyst recycling. Regardless of the purpose of catalyst recycling, it involves feeding recycled catalyst back into the reactor. Here, we take an ascending fluidized bed as an example. The recycled catalyst is typically taken from the top of the fluidized bed reactor, optionally undergoes intermediate processing, and is then fed back to the feed section at the bottom of the fluidized bed reactor through one or more solid feed ports for the recycled catalyst. Through in-depth research, the inventors have discovered that connecting at least one of these solid feed ports to a specific solid distributor 17, and conveying the recycled catalyst into the reaction chamber through this solid distributor 17, is particularly beneficial for the distribution of the recycled catalyst in the reaction chamber and its mixing with other materials.

[0118] In one implementation scheme, such as Figure 5 As shown, the solid distribution member 17 of the present invention includes a base plate 18 and at least two side baffles 19 mounted opposite each other on the base plate 18, wherein the base plate 18 and the side baffles 19 together define a flow channel for the distribution of solids therethrough; wherein the flow channel is preferably trapezoidal, for example, an isosceles trapezoid, the upper base of which is connected to the solid inlet and the base plate is tangent to the inner edge of the inlet. For the purposes of this invention, when referring to "trapezoidal," and the corresponding terms such as upper base, lower base, and height, they have their conventional geometric meaning.

[0119] To facilitate the distribution of the recycled catalyst in the reaction chamber and its mixing with other materials, the trapezoidal shape described in this invention has a special design, specifically, as follows: Figure 6As shown, the 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 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 inventor 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 inventor found that the specific upper base length j and height hh can be conducive to effectively distributing substantially all of the solid-phase feed via the solid distributor 17, while not having an obvious impact on the fluidization and reaction in the reaction chamber.

[0120] 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 have an impact on the fluidization and reaction in the reaction chamber; while the structure and shape of the side baffle can have an impact on the effective distribution of the solid-phase feed, the fluidization and reaction in the reaction chamber.

[0121] Correspondingly, in one embodiment, as Figure 6 shown, 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 the upper base and lower base of the flow channel, and it has the same symmetry center line as the flow channel; the angles between the waists and the lower base of the trapezoid of this 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 this bottom plate is k, and j < k ≤ 2j, preferably j < k ≤ 1.6j.

[0122] 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 distributor 17 have a relatively stable structure, while not having an obvious impact on the fluidization and reaction in the reaction chamber.

[0123] In one embodiment, as Figure 5As shown, the side baffle 19 of the distribution component 17 can be a rectangular plate with a height of L, where 0.2dg ≤ L ≤ 0.5dg. The rectangular plate has a simple structure and is generally sufficient to meet the needs of this invention in areas such as solid distribution. Through repeated experiments and simulation calculations, the inventors found that when the side baffle 19 has a height L within the specified range, it is sufficiently high to facilitate solid distribution while avoiding material waste. More importantly, it is not too high to significantly affect the fluidization and reaction in the reaction chamber.

[0124] In another embodiment, the side baffle 19 of the distributor 17 can be a right-angled trapezoidal plate with a height L that gradually decreases from the top base, wherein 0.2dg≤L≤0.5dg, and the height of the lower base of the right-angled trapezoid is 0.6-0.8L. Through repeated experiments and simulation calculations, the inventors found that when the side baffle 19 has a right-angled trapezoidal shape within this specific range of lower base height, it is more advantageous in some cases to meet the requirements of not affecting the fluidization and reaction in the reaction chamber, while still basically meeting the requirements of solid distribution.

[0125] It can be understood that, for example Figure 7 As shown, to achieve a more favorable distribution of solids such as the recycled catalyst, the base plate 18 of the distribution member 17 is preferably inclined at a certain angle to the horizontal plane; however, the invention can also be implemented with the base plate placed horizontally. Accordingly, in one embodiment, the base plate 18 forms an angle θ with the horizontal plane, where 0 ≤ θ ≤ 45°, preferably 15° ≤ θ ≤ 30°. The catalyst circulation channel section at the solid feed inlet forms an angle γ with the horizontal plane, where 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 stiffener 24 between the wall of the reaction chamber and the base plate 18.

[0126] The inventors further investigated the cross-sectional shape of the base plate 18. Through repeated experiments and simulation calculations, the inventors discovered that a certain curved surface shape of the base plate is more conducive to the desired distribution of the solid. Unrestricted by any known theory, through numerous experiments, it is believed that the base plate 18 can be a flat plate or a wave plate, preferably a wave plate, wherein the waveform of the wave plate is a cosine wave, a circular wave, or an elliptical wave. For the purposes of this invention, a "circular wave" refers to a waveform formed by the first and last joints of several semicircles of the same radius; while an "elliptical wave" refers to a waveform formed by the first and last joints of several semi-ellipses with the same major and minor axes. It is understood that each of the cosine wave, circular wave, or elliptical wave has a central axis of symmetry; preferably, the waveform height h0 (vertical distance from the crest to the adjacent trough) of the wave plate is 0.1L ≤ h0 ≤ 0.5L. Accordingly, through repeated experiments and simulation calculations, it is preferred that the base plate 18 be a flat plate or a wave plate. Figure 7As shown, the central axis of symmetry of the base plate 18 is directly connected to the lowest point of the inner diameter of the solid feed inlet 7, meaning there is no height difference between them. Furthermore, for cosine, circular, or elliptical waves, the connection point between the base plate and the inner diameter of the solid feed inlet is precisely at the point where the lower half of the wave begins to extend from the central axis of symmetry. For example... Figure 5 and Figure 7 As shown, when using a corrugated plate, there is a gap between the bottom end of the side baffle and the concave corrugations of the corrugated plate that allows solid phase discharge.

[0127] For embodiments B and C of the present invention relating to a circulating fluidized bed reactor, embodiment A relating to a fluidized bed reactor, and combinations thereof, the solid feed inlet originates from 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 an angle with the horizontal plane; for example, the angle 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°.

[0128] In one embodiment, to avoid dead zones in the reaction chamber space below the bottom plate 18 (e.g., a corrugated plate) and achieve better solid concentration distribution, multiple distribution holes are provided on the bottom plate 18 (e.g., a corrugated plate). This allows at least a portion of the solid to pass downwards through these distribution holes as it flows through the channels on the bottom plate 18, thus distributing downwards into the reaction chamber space below the bottom plate 18 (e.g., the corrugated plate). Surprisingly, experimental verification shows that it is not necessary to provide distribution holes throughout the entire bottom plate 18 or the entire flow channel; preferably, multiple distribution holes are only needed in the front-end region of the bottom plate 18 within the flow channel to achieve the aforementioned advantageous "downward distribution" of solids. In other words, no holes are required in the area of ​​the bottom plate 18 outside the flow channel (i.e., outside the side baffles) or in the rear-end region within the flow channel. Through repeated experiments and simulation calculations, in order to achieve the aforementioned "downward distribution" of the advantageous solid, in one embodiment, the front end region where the distribution hole is located can refer to the region on the bottom plate 18 located in the flow channel along the height hh from the top bottom to the bottom bottom, between 45% and 95%, preferably between 65% and 95%.

[0129] Furthermore, through repeated experiments and simulation calculations, in order to achieve the aforementioned "downward distribution" of the advantageous solid, in one embodiment, the total porosity of the bottom plate 18 (e.g., a corrugated plate) is 1%-10%, preferably 4%-8%.

[0130] Similarly, the diameter of the distribution holes needs to be adjusted appropriately, especially to match the diameter of the catalyst. Similar to the factors considered for the gas passage holes, through repeated experiments and simulation calculations, the diameter of the distribution holes can be 2-10 mm, preferably 4-8 mm.

[0131] Similar to venting holes, the distribution holes and their distribution in this invention are preferably uniform. Accordingly, in one embodiment, the diameter of each distribution hole is substantially equal; similarly, for the purposes of this invention, "substantially equal" diameter means that the diameter difference between the individual distribution holes does not exceed 10%, preferably not more than 5%, and even more preferably not more than 1%. Similar to venting holes, in one embodiment, the openings of the distribution holes are arranged in staggered equilateral triangles. In another embodiment, the openings of the distribution holes are arranged in aligned rectangles. Also similar to venting holes, for the purposes of this invention, the specific spacing between the distribution holes is not particularly limited, as long as it satisfies the requirements of the diameter of the distribution holes and the total porosity of the distribution plate as described in this invention. For example, the spacing between the distribution holes can be 20-200 mm, preferably 50-100 mm.

[0132] Thus, as Figure 5 As shown, in the embodiment where the base plate 18 is a corrugated plate, the solid phase flowing through the corrugated plate can achieve a wide range of solid phase particle concentration distribution in both sides (arrow a), in front (arrow c), in front and below (arrow b), and through the distribution holes (arrow d).

[0133] Implementation Plan C

[0134] According to embodiment C, the present invention provides a circulating fluidized bed reactor, such as... Figure 4 and Figure 8 As shown, a feed gas distributor 8 is provided at the bottom of the reactor's reaction chamber, and multiple solid-phase feed ports, preferably 2-6, are provided on the chamber wall above the feed gas distributor 8 for feeding the circulating catalyst. These multiple solid-phase feed ports are 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. The geometric center of the type I solid-phase feed port and the geometric center of the type II solid-phase feed port are aligned vertically, or deviate by no more than 5°. The geometric center of the feed port is the center point of its cross-section. In this invention, as long as the amounts of the two solid feed streams are not completely equal, they can be referred to as a relatively large amount and a relatively small amount of solid feed, respectively. For the purposes of this invention, the positional relationship between the type II solid-phase feed port and the type I solid-phase feed port can be referred to as a "vertical arrangement."

[0135] As mentioned earlier, circulating fluidized bed reactors may involve various recirculating catalysts, such as regenerators, regenerators, and externally heated agents. Even conventional fluidized bed reactors may contain the recirculating catalyst described in this invention, for example, fine catalyst powder separated by separation equipment (e.g., a cyclone separator) and returned to the fluidized bed. Accordingly, when a fluidized bed reactor involves two or more different recirculating catalysts, they can be fed separately through the Type I solid-phase feed inlet and the Type II solid-phase feed inlet described in this invention, according to their amounts. Even if a fluidized bed reactor involves only one recirculating catalyst, it can be divided into two streams of material with different amounts, and fed separately through the Type I solid-phase feed inlet and the Type II solid-phase feed inlet described in this invention.

[0136] With the vertical arrangement of the Type I and Type II solid feed ports of the present invention, a relatively small amount of solid feed enters the fluidized bed through the Type II solid feed port located above, and can quickly merge into the relatively large amount of solid feed fed through the Type I solid feed port and flow together, which helps to improve the uniformity of gas-solid and solid-solid (e.g. external heat recovery agent and regenerator) distribution of the small amount of solid feed in the reactor.

[0137] Accordingly, to promote the uniform distribution, the vertical arrangement of the Type I and Type II solid phase feed inlets requires that they have an appropriate distance in the vertical direction. In one embodiment, such as Figure 8 As shown, the vertical distance between the geometric center of the type II solid phase inlet and the geometric center of the type I solid phase inlet is h, preferably 0.5(dc+dz)≤h≤1.5dc, and preferably 0.5(dc+dz)≤h≤dc, where: dc is the equivalent diameter of the type I solid phase inlet, and dz is the equivalent diameter of the type II solid phase inlet.

[0138] In particular, such as Figure 8 As shown, for the circulating fluidized bed reactor of embodiment C, in order to further facilitate the gas-solid and solid-solid uniform distribution, the aforementioned solid distribution member 17 according to embodiment B can be connected to one or more solid feed inlets.

[0139] In one implementation scheme, such as Figure 8As shown, the plurality of solid feed ports further includes at least one additional solid feed port, which is also used for feeding a relatively large amount of solids and is located at least 120°, preferably at least 150°, circumferentially from the geometric center of the type I solid feed port; wherein, preferably, no solid distributor 17 is connected to the additional solid feed port. Preferably, the additional solid feed port has the same equivalent diameter as the type I solid feed port. In this case, the additional solid feed port is relatively far from the type I solid feed port, which reduces the impact of mixing and distribution between the solids fed through the type I and type II solid feed ports respectively. Therefore, this embodiment is suitable when mixing and distribution between the solids fed through the type I and type II solid feed ports is a major consideration. Accordingly, the inventors determined the interval of at least 120°, preferably at least 150°, through repeated experiments and simulation calculations.

[0140] In another embodiment, the plurality of solid feed ports includes one or more additional solid feed ports, the geometric centers of which are symmetrically distributed circumferentially with respect to the type I solid feed port; preferably, one or more, preferably all, of the additional solid feed ports also have the solid distribution element 17 arranged towards the center of the reaction chamber. Preferably, the additional solid feed ports have the same equivalent diameter as the type I solid feed port. It is understood that this embodiment is suitable when the distribution of solids fed through the additional solid feed ports is also a significant consideration. Accordingly, the two or more solid distribution elements 17 used have the same or different dimensions. For different operating conditions and different feeds, it is believed that as long as the two or more solid distribution elements 17 used have the same dimensions, various conditions can be basically met without having to set solid distribution elements 17 of different sizes at the type I solid feed port and the multiple additional solid feed ports; thus avoiding greater fluctuations under different conditions, and even the need to replace solid distribution elements of different sizes under different conditions.

[0141] 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 inlet and the geometric center of the additional solid phase inlet are on the same horizontal line, or the vertical deviation does not exceed 5°.

[0142] The vertical arrangement of the Type I and Type II solid-phase feed inlets of this invention is to promote the mixing and distribution of solids fed through these two inlets. Accordingly, through experimental studies, the inventors have found it advantageous that the Type II solid-phase feed inlet also extends into the reaction chamber, and preferably its extension distance is greater than that of the Type I solid-phase feed inlet. This allows a relatively small amount of solid feed to better merge into a relatively large amount of solid feed below. On the other hand, experimental studies have shown that, also for the purpose of better mixing, it is also preferable that the further extension distance of the Type II solid-phase feed inlet relative to the Type I solid-phase feed inlet does not exceed 1 / 2 of the height hh of the trapezoid of the base plate 18.

[0143] It is understandable that the diameter of the inlet of the pipeline and connecting pipelines affects factors such as the amount and speed of transport. Based on a comprehensive consideration of multiple factors, and through repeated experiments and simulation calculations, it is believed that the preferred ratio of the equivalent diameter of the Type I solid-phase inlet to the Type II solid-phase inlet is 2:1-10:1, preferably 3:1-5:1. Under these conditions, the circulating fluidized bed of the present invention can have greater operational flexibility and is widely applicable to the separate feeding of relatively large and relatively small amounts of recycled catalyst under various conditions.

[0144] Similarly, fluidized bed reactors are generally vertically arranged, and correspondingly, the section of the catalyst circulation channel connecting to the reactor wall often has a certain angle with the horizontal plane, which also affects parameters such as the conveying speed. Through repeated experiments and simulation calculations, it is advantageous that the angle between the catalyst circulation channel section at the Type I solid inlet and the horizontal plane is γ, where 0°≤γ≤60°, preferably 0°≤γ≤45°. Similarly, the angle between the catalyst circulation channel section at the Type II solid inlet and the horizontal plane is δ, where 0°≤δ≤60°, preferably 0°≤δ≤45°. It is particularly advantageous that the γ is equal to or appropriately greater than the δ, for example, 0°≤(γ-δ)≤15°.

[0145] The circulating fluidized bed described in this invention may involve various recirculating catalysts, especially in cases such as methanol conversion to olefins, catalytic cracking, or fluidized bed propane dehydrogenation, which may involve external heat recovery agents, circulating agents, regenerators, and catalyst fines. In such cases, the Type I solid-phase feed inlet is used for feeding external heat recovery agents or circulating agents, and the Type II solid-phase feed inlet is used for feeding regenerators or catalyst fines. Preferably, the Type I solid-phase feed inlet is used for feeding external heat recovery agents, and the Type II solid-phase feed inlet is used for feeding regenerators.

[0146] In this invention, such as Figure 8As shown, the solid feed inlet is used to feed the catalyst, including an external heat recovery agent inlet 7, a circulating agent inlet 5 and 9, and a catalyst fine powder inlet 16 (the catalyst fine powder can be, for example, catalyst fine powder separated from the gas phase containing low-carbon olefins discharged from the gas phase outlet and returned to the feed section) opened circumferentially on the cavity wall of the feed section; wherein, a regenerator inlet 10 is opened in the cavity wall directly above the external heat recovery agent inlet 7, and the vertical distance between the geometric center of the regenerator inlet 10 and the geometric center of the external heat recovery agent inlet 7 is h, 0.5(dc+dz)≤h≤1.5dc, preferably 0.5(dc+dz)≤h≤dc.

[0147] In some embodiments, one or more solid feed inlets are provided with solid distributors 17, for example, such as... Figure 4 , Figure 8 Solid distributors 17 are provided at the circulating agent inlet 5 or 9, the regenerator inlet 10, or the external heat exchanger inlet 7. The side baffle 19 of the solid distributor 17 has a height of L, where L ranges from 0.2 to 0.5 times the equivalent diameter of the corresponding solid inlet. Preferably, the solid distributor 17 is provided at the external heat exchanger inlet 7, where 0.2dc ≤ L ≤ 0.5dc, where L is the height of the side baffle 19 and dc is the equivalent diameter of the external heat exchanger inlet. This allows the regenerator z returned after the regeneration of the catalyst to be generated to quickly flow into the catalyst g returned by the external heat exchanger pipe, which helps to improve the uniformity of the gas-solid and solid-solid (e.g., external heat exchanger, circulating agent, and regenerator) distribution of the regenerator particles in the reactor. If the distance between the pipe openings is too far, the regenerator will detach from the main distribution of the external heat exchanger, resulting in uneven distribution.

[0148] In some implementations, the circulating agent inlets 5 and 9, the catalyst powder inlet 16, and the external heat exchanger inlet 7 are at the same horizontal level, and the regenerator inlet 10 is vertically above the external heat exchanger inlet 7.

[0149] In some embodiments, the regenerant inlet 10 is the uppermost solid phase inlet in the feed section of the reaction chamber, and the distance between the geometric center of the regenerant inlet 10 and the first turbulence member 15 from bottom to top in the reactor is 0.2-1.5m, preferably 0.5-1.2m.

[0150] It should be noted that in some embodiments of the present invention, such as Figure 4As shown, the gas-solid reaction equipment also includes some conventional settings found in existing gas-solid reaction equipment, such as a catalyst regenerator 14 and a degassing tank 13. The top of the reaction chamber 6 is configured as an upwardly tapering outlet, and the top of the tapering outlet extends into the separation chamber 2 to form a riser pipe 3. The separation chamber 2 is equipped with a fluidizing air distributor 11 for feeding fluidizing air q into the separation chamber 2. At least one catalyst circulation pipe and an external heat exchanger pipe with an external heat exchanger 4 are connected between the separation chamber 2 and the feeding section. The separation chamber 2 is connected to the inlet of the catalyst regenerator 14 through a regenerator pipe 12. The outlet of the catalyst regenerator 14 is connected to the feeding section through a regenerator pipe with a degassing tank 13, etc. The configuration can be adjusted according to actual production needs, and will not be described in detail here.

[0151] The gas-solid reaction apparatus of the present invention, under the action of the turbulence member 15, the solid distribution member 17 and / or the relative position adjustment of the solid feed inlet according to the present invention, ensures that the standard deviation σ1 of the concentration ratio of solid particles at different positions in the total solid particles in the height region above the uppermost solid feed inlet of the reaction chamber 6 is less than 1.5, preferably less than 0.8; the standard deviation σ2 of the concentration ratio of solid particles at different positions in the height region above the uppermost solid feed inlet of the reaction chamber 6 is less than 1.5, preferably less than 0.8; and the standard deviation (uniformity) σ of the total concentration difference of solid particles (e.g., recirculated catalyst, including circulating agent, regenerator and external heat recovery agent) at different positions in the height region above the uppermost solid feed inlet of the reaction chamber 6 is less than 1.5. p The standard deviation should be less than 1.5, preferably less than 1.2; the above standard deviations are calculated according to the following formula:

[0152]

[0153] Where σ is the standard deviation, representing the dispersion (uniformity) of samples taken from different locations in reaction chamber 6. A larger value indicates a more uneven distribution of the sample within the total quantity. 1i x represents the concentration percentage of solid particles (e.g., regenerant) at a specific sampling point within the cavity relative to the total solid particles. 2i x represents the concentration percentage of solid particles (e.g., regenerant) at a sampling point within the cavity in the total gas-solid content. pi This represents the concentration ratio of the total amount of solid particles (e.g., recirculated catalyst) at a specific sampling point within the cavity to the total gas-solid content. denoted as the average concentration of samples under the corresponding conditions within the region, and n is the number of sampling points within the region, where n ≥ 10.

[0154] This invention significantly promotes the mixing of multiple streams of different solid particles by setting up turbulence components in the turbulence section cavity of the fluidized bed reactor equipment, adjusting the relative positions of Type I solid feed inlets (e.g., external heat recovery agent feed inlets) and Type II solid feed inlets (e.g., regenerator feed inlets) in the feed section, and / or setting up solid distribution components at one or more solid feed inlets. This enhances gas-solid contact, reduces the non-uniformity of solid particle (e.g., regenerator) distribution per 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.

[0155] Another aspect of the present invention provides the application of the turbulence-dispersing component 15 or fluidized bed reactor according to embodiment A of the present invention, the solid distribution component 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 combinations thereof, in methanol conversion to olefins, catalytic cracking, or fluidized bed propane dehydrogenation.

[0156] Another aspect of the present invention provides a method for methanol conversion to produce olefins. This method employs a reaction apparatus according to the present invention (e.g., a fluidized bed reactor with a turbulence-inducing component, a circulating fluidized bed reactor with a solid distribution component, a circulating fluidized bed reactor with a specific solid inlet location, or a combination thereof). The method includes feeding methanol feed gas f and a catalyst (e.g., a recirculating catalyst, such as an external heat exchanger g, a regenerator z, and circulating agents r1 and r2) into a feed section, allowing the methanol feed gas f to contact the catalyst and react to generate a gas-solid mixture containing low-carbon olefins. The gas-solid mixture containing low-carbon olefins is then passed upwards through a turbulence-inducing section to form a vortex, thereby enhancing the interphase disturbance between the gas and solid phases and further reacting. Afterwards, it continues upwards into a separation chamber 2 for gas-solid separation, with the separated gas phase containing low-carbon olefins exiting from the gas phase outlet p at the top of the separation chamber.

[0157] In some embodiments, the gas-solid mixture containing low-carbon olefins forms a vortex in the turbulence section through the turbulence member 15.

[0158] In some embodiments, the catalyst enters the feed section through a solid distributor 17 connected to a solid feed inlet. In some embodiments, the external heat recovery agent g, after heat recovery, is dispersed into the feed section through a solid distributor 17 connected to an external heat recovery agent inlet 7. In some embodiments, the regenerated agent z, after regeneration, is dispersed into the feed section through a solid distributor 17 connected to a regenerator inlet 10.

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

[0160] In some embodiments, the recirculated catalyst includes externally extracted heat agent g fed from externally extracted heat agent inlet 7 after heat recovery, the temperature of externally extracted heat agent g being 300-400°C; regenerator z fed from regenerator inlet 10, the temperature of regenerator z being 600-700°C; regenerator r1 and r2 fed from regenerator inlets 5 and 9 respectively, the temperatures of regenerator r1 and r2 being 450-500°C; and catalyst fine powder fed from catalyst fine powder inlet 16.

[0161] In some embodiments, the average concentration of catalyst in reaction chamber 6 is 60-150 kg / m³. 3 Preferred weight: 80-115 kg / m 3 .

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

[0163] To facilitate understanding of the present invention, the following embodiments are provided. However, these embodiments are only for the purpose of helping to understand the present invention and should not be regarded as specific limitations of the present invention.

[0164] Example

[0165] The present application will be further illustrated by the following examples, but these examples do not constitute a limitation thereof.

[0166] The following examples were carried out in a gas-solid reaction apparatus, such as... Figure 4 and Figure 9As shown, the gas-solid reaction equipment may include a gas-solid reactor 1 (e.g., a fluidized bed reactor according to embodiment A, or 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 connected to each other, the bottom end of the reaction chamber 6 is provided with a feed gas distributor 8, the reaction chamber 6 includes a feed section and a turbulence section located above the feed section, the top end of the reaction chamber 6 is provided with an upwardly tapering discharge port, the top end of the tapering discharge port extends into the separation chamber 2 to form a riser 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 top end of the separation chamber 2 has a gas phase outlet p; the gas-solid reactor 1 is also provided with a gas phase outlet p for feeding fluidizing air q into the reaction chamber 6. At least one catalyst circulation pipe and an external heat exchanger pipe equipped with an external heat exchanger 4 are connected to the feed section and the separation chamber 2. The catalyst circulation pipe is connected to the circulating agent inlets 5 and 9 to return the circulating agent to the feed section of the reaction chamber 6. The external heat exchanger pipe is connected to the external heat exchanger inlet 7 to return the external heat exchanger to the feed section of the reaction chamber 6. The feed section of the reaction chamber 6 is also equipped with a catalyst fine powder inlet 16 to return the separated catalyst fine powder to the reaction chamber 6. The separation chamber 2 is connected to the inlet of the catalyst regenerator 14 through the regenerator pipe 12. The outlet of the catalyst regenerator 14 is connected to the reaction chamber 6 through a regenerator pipe equipped with a degassing tank 13. The regenerator pipe is connected to the regenerator inlet 10 to return the regenerator to the feed section of the reaction chamber 6. Unless otherwise specified, the positions of the components (e.g., turbulence components, solid distribution components) and solid phase inlets in the reaction chamber 6 are in accordance with the prior art (e.g., Figure 9 Configure it.

[0167] The following examples illustrate a method for producing olefins from methanol. This method involves preheating methanol feed gas f and then introducing it into the reaction chamber 6 via a feed gas distributor 8 at the bottom. The methanol feed gas f is mixed, contacted, and reacted with regenerator z returned from catalyst regenerator 14, external heat recovery agent g returned after heat extraction, circulating agents r1 and r2, and recovered catalyst powder. After the reaction, the catalyst is rapidly carried by the gas through riser 3 and detached from the main gas phase via a fast separation component at its outlet, falling downwards into the lower part of separation chamber 2 under gravity. The accumulated catalyst is partially recycled back to the feed section of reaction chamber 6 as circulating agents r1 and r2, partially heated by an external heat exchanger and returned to the feed section as external heat exchanger g after cooling, and partially sent to the catalyst regenerator 14 as a regenerator through the regenerator pipe 12 for regeneration. After removing the carbon deposits on the catalyst, it is returned to the feed section as regenerator z through the regenerator pipe. Multiple different catalyst materials are remixed and reacted with the raw gas. The gas phase containing low-carbon olefins and 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. After further gas-solid separation to remove the catalyst fine powder, it is sent to the subsequent unit for processing. The catalyst fine powder is returned to the feed section of reaction chamber 6 through the catalyst fine powder inlet 16.

[0168] In the following embodiments, the amount of catalyst coking (or average amount of coking) is calculated by dividing the mass of coking on the catalyst by the mass of the catalyst. The method for determining the mass of coking on the catalyst is 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-Carbon Analyzer HIR-944) for combustion. The mass of carbon dioxide generated during combustion is measured by infrared spectroscopy, thereby obtaining the mass of coking on the catalyst. To determine the amount of catalyst coking in the reaction zone, equal amounts of small portions of catalyst can be continuously or periodically extracted or directly taken from various locations within the reaction zone.

[0169] In the following embodiments, x represents the concentration percentage of the total solid particles (e.g., catalyst) in the total gas-solid mixture. pi The determination method is as follows: A high-precision differential pressure analyzer (its high-tech, multi-point high-precision differential pressure analyzer MC-32) is used to measure the sampling area to obtain the pressure difference change ΔPi. The average density of this sampling area is then ρi = ΔPi / (9.8 × hp), where hp is the distance between the measured pressure difference points, is a constant, and the particle density of the catalyst is ρc. Therefore, x pi =ρi / ρc=ΔPi / (9.8×hp×ρc);

[0170] In the following embodiments, by directly sampling at the sampling point, the amount of carbon deposit Ci of the solid particles (including regenerator, circulating agent, external heat recovery agent, etc.) in the sampling point area at a certain moment can be measured by a high-temperature carbon analyzer. Since the circulating agent, external heat recovery agent, etc. are all derived from the catalyst that has not been regenerated after the reaction, the amount of carbon deposit of this part of the catalyst is measured as Cx. If it is assumed that the density of the carbon-containing catalyst that has not been regenerated, such as the circulating agent, external heat recovery agent, etc., is approximately the same as the density of the regenerated carbon-free catalyst, then the concentration ratio x of the solid particles (e.g., regenerator) at a certain sampling point in the chamber in the total amount of solid particles is... 1i = (1-Ci / Cx);

[0171] In the following embodiments, x represents the concentration percentage of solid particles (e.g., regenerant) at a sampling point within the cavity in the total gas-solid phase. 2i The calculation method is as follows: x 2i =x pi ·x 1i The number of sampling points in the region is n, where n≥10.

[0172] Example 1

[0173] The reaction chamber 6 of the circulating fluidized bed reactor is equipped with three circular flow-disrupting components 15 arranged axially along the reactor, conforming to the cross-sectional shape of the reaction chamber, with an installation spacing ΔH = 0.8m. The diameter D1 of the flow-disrupting components 15 is approximately equal to the inner diameter D of the reaction chamber, and includes a guide section and a mixing section coaxially distributed in the radial direction. The guide section includes a guide plate 20, on which multiple equilateral triangularly evenly distributed air passage holes are opened, with an opening diameter Φ15mm and a total porosity of 3%. The mixing section surrounds the guide section and includes six concentrically arranged... A series of turbulent rings are arranged, each with multiple identical cylindrical turbulent fluids 21 evenly distributed and without pores. The turbulent fluids 21 are vertically arranged, with the smallest turbulent fluid ring having its turbulent fluid 21 embedded in the edge of the guide plate 20. The horizontal cross-sectional shape of the turbulent fluid 21 is circular with a length-to-diameter ratio of 3.5:1, and its equivalent diameter is 85 mm. The total porosity of the mixing section is 86%, and the ratio of the total porosity area of ​​the mixing section to the total porosity area of ​​the guide plate is 176. The diameter of the guide plate 20 is d. b =0.35D1, and a side ring 22 is provided on the cavity wall near the reaction chamber, which is connected to the largest turbulent fluid ring. The width X of the side ring 22 is D1 / 25.

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

[0175] The external heat recovery agent inlet 7 has the same equivalent diameter as the circulating agent inlets 5 and 9. The three inlets are evenly distributed around the reaction chamber on the same horizontal plane. The equivalent diameter dz of the regenerator inlet 10 is 1 / 4 of the equivalent diameter dc of the external heat recovery agent inlet 7, and it is located directly above the external heat recovery agent inlet 7. The pipe section at the external heat recovery agent inlet 7 extends into the reaction chamber at an angle γ of 30° with the horizontal plane. The regenerator inlet 10 extends into the reaction chamber at an angle δ of 22° with the horizontal plane. The horizontal extension distance relative to the external heat recovery agent inlet 7 is 1 / 4 of the height hh of the bottom plate 18 of the solid distribution component 17. The distance h between the regenerator inlet 10 and the external heat recovery agent inlet 7 is 0.5(dc+dz). The distance between the regenerator inlet 10 and the first turbulence member 15 from bottom to top in the reactor is 0.5m.

[0176] The apparent velocity of the methanol feed gas f entering the feed section is 1.2 m / s, the preheating temperature is 180℃, the catalyst is selected from SAPO 34 molecular sieve catalyst for methanol-to-olefins process, and the average concentration of catalyst in the reaction chamber is 85 kg / m³. 3 The reaction temperature was 480℃ and the reaction pressure was 0.11MPa.

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

[0178] Example 2

[0179] The reaction chamber 6 of the circulating fluidized bed reactor is equipped with four circular flow-disrupting components 15 arranged axially along the reactor, conforming to the cross-sectional shape of the reaction chamber, with an installation spacing ΔH = 0.8m. The diameter D1 of the flow-disrupting components 15 is approximately equal to the inner diameter D of the reaction chamber, and includes a guide section and a mixing section coaxially distributed in the radial direction. The guide section includes a guide plate 20, on which multiple equilateral triangularly evenly distributed air passage holes are opened, with an opening diameter Φ15mm and a total porosity of 6%. The mixing section surrounds the guide section and includes six concentrically arranged... A series of turbulent rings are arranged, each with multiple identical cylindrical turbulent fluids 21 evenly distributed and without pores. The turbulent fluids 21 are vertically arranged, with the smallest turbulent fluid ring having its turbulent fluid 21 embedded in the edge of the guide plate 20. The horizontal cross-sectional shape of the turbulent fluid 21 is circular with a length-to-diameter ratio of 3.5:1, and its equivalent diameter is 85 mm. The total porosity of the mixing section is 86%, and the ratio of the total porosity area of ​​the mixing section to the total porosity area of ​​the guide plate is 176. The diameter of the guide plate 20 is d. b =0.6D1, and a side ring 22 is provided on the cavity wall near the reaction chamber, which is connected to the largest turbulent fluid ring. The width X of the side ring 22 is D1 / 16.

[0180] The bottom of the reaction chamber 6, located above the raw material gas distributor 8, has four solid-phase feed ports on its wall for feeding the circulating catalyst. These include one external heat-extracting agent feed port 7, two circulating agent feed ports 5 and 9, and one regenerator feed port 10. The external heat-extracting agent feed port 7 extends into the reaction chamber and is connected to a solid distribution member 17 towards the center of the reaction chamber. This distribution member includes a corrugated bottom plate 18 and two side baffles 19 mounted opposite each other on the bottom plate, defining an isosceles trapezoidal flow channel. The upper bottom of this channel is connected to the external heat-extracting agent feed port 7 and is tangent to the inner edge of the feed port. The waist of the trapezoid is tangent to the lower bottom. The included angles α1 and α2 are both 75°. The length j of the upper base of the trapezoid is equal to the diameter dg of the regenerant inlet. The height hh of the trapezoid is 0.1 times the inner diameter D of the reaction chamber. The bottom plate of the distributor is a corrugated plate with an isosceles trapezoidal shape. The included angles β1 and β2 between its base and waist are both 45°. The length k of the upper base of the trapezoidal bottom plate is 2dg. The side baffle of the distributor is rectangular with a height L = 0.5dg. The front end area of ​​the distributor has multiple distribution holes with a total porosity of 10% and a hole diameter of Φ6mm. The holes are distributed in a rectangular array aligned front and back. The bottom plate forms an angle θ with the horizontal plane, where θ = 22°.

[0181] The external heat recovery agent inlet 7 has the same equivalent diameter as the circulating agent inlets 5 and 9. The three inlets are evenly distributed around the reaction chamber on the same horizontal plane. The equivalent diameter dz of the regenerator inlet 10 is 1 / 4 of the equivalent diameter dc of the external heat recovery agent inlet 7, and it is located directly above the external heat recovery agent inlet 7. The pipe section at the external heat recovery agent inlet 7 extends into the reaction chamber at an angle γ of 30° with the horizontal plane. The regenerator inlet 10 extends into the reaction chamber at an angle δ of 22° with the horizontal plane. The horizontal extension distance relative to the external heat recovery agent inlet 7 is 1 / 4 of the height hh of the bottom plate 18 of the solid distribution component 17. The distance h between the regenerator inlet 10 and the external heat recovery agent inlet 7 is 1.5dc. The distance between the regenerator inlet 10 and the first turbulence member 15 from bottom to top in the reactor is 0.6m.

[0182] The apparent velocity of the methanol feed gas f entering the feed section is 1.0 m / s, the preheating temperature is 180℃, the catalyst is selected from SAPO 34 molecular sieve catalyst for methanol-to-olefins process, and the average concentration of catalyst in the reaction chamber is 115 kg / m³. 3 The reaction temperature was 480℃ and the reaction pressure was 0.11MPa.

[0183] The standard deviation σ1 of the change in the concentration ratio of regenerant in the total solid particles in the reaction chamber is 0.49, and the standard deviation σ2 of the change in the concentration ratio of regenerant in the total gas-solid material is 0.58. The carbon deposition of the feed regenerant is 0.03 wt%, and the carbon deposition of the remaining circulating agent, external heat recovery agent, and returned catalyst fine powder is 3.2 wt%. The difference in the average carbon deposition per unit area of ​​the horizontal cross-section 2 m above the feed gas distributor is less than 0.32 wt%. The non-uniformity of catalyst concentration distribution in the chamber above the regenerant inlet is σ. p It is 1.02.

[0184] Example 3

[0185] The reaction chamber 6 of the circulating fluidized bed reactor is equipped with five circular flow-disrupting components 15 arranged axially along the reactor, conforming to the cross-sectional shape of the reaction chamber, with an installation spacing ΔH = 0.8m. The diameter D1 of the flow-disrupting components 15 is approximately equal to the inner diameter D of the reaction chamber, and includes a guide section and a mixing section coaxially distributed in the radial direction. The guide section includes a guide plate 20, on which multiple equilateral triangularly evenly distributed air passage holes are opened, with an opening diameter Φ15mm and a total porosity of 2%. The mixing section surrounds the guide section and includes six concentrically arranged... A series of turbulent rings are arranged, each with multiple identical cylindrical turbulent fluids 21 evenly distributed and without pores. The turbulent fluids 21 are vertically arranged, with the smallest turbulent fluid ring having its turbulent fluid 21 embedded in the edge of the guide plate 20. The horizontal cross-sectional shape of the turbulent fluid 21 is circular with a length-to-diameter ratio of 3.5:1, and its equivalent diameter is 85 mm. The total porosity of the mixing section is 86%, and the ratio of the total porosity area of ​​the mixing section to the total porosity area of ​​the guide plate is 176. The diameter of the guide plate 20 is d. b =0.2D1, a side ring 22 is provided on the cavity wall near the reaction chamber, which is connected to the largest turbulent fluid ring. The width X of the side ring 22 is D1 / 30.

[0186] The bottom of the reaction chamber 6, located above the raw material gas distributor 8, has four solid-phase feed ports for circulating catalyst feeding. These include an external heat-extracting agent feed port 7, two circulating agent feed ports 5 and 9, and a regenerator feed port 10. The external heat-extracting agent feed port 7 extends into the reaction chamber and is connected to a solid distribution member 17 towards the center of the reaction chamber. This distribution member includes a corrugated bottom plate 18 and two side baffles 19 mounted opposite each other on the bottom plate, defining an isosceles trapezoidal flow channel. The upper bottom of the channel is connected to the external heat-extracting agent feed port 7 and is tangent to the inner edge of the feed port. The waist of the trapezoid and the lower bottom are intersected. 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 regenerant inlet. The height hh of the trapezoid is 0.1 times the inner diameter D of the reaction chamber. The bottom plate of the distributor is a corrugated plate with an isosceles trapezoidal shape. The angles β1 and β2 between its base and waist are both 48°. The length k of the upper base of the trapezoidal bottom plate is 1.4dg. The side baffle of the distributor is rectangular with a height L = 0.2dg. The front end area of ​​the distributor has multiple distribution holes with a total porosity of 5% and a hole diameter of Φ6mm. The holes are distributed in a rectangular array aligned front and back. The bottom plate forms an angle θ with the horizontal plane, where θ = 22°.

[0187] The external heat recovery agent inlet 7 has the same equivalent diameter as the circulating agent inlets 5 and 9. The three inlets are evenly distributed around the reaction chamber on the same horizontal plane. The equivalent diameter dz of the regenerator inlet 10 is 1 / 4 of the equivalent diameter dc of the external heat recovery agent inlet 7, and it is located directly above the external heat recovery agent inlet 7. The pipe section at the external heat recovery agent inlet 7 extends into the reaction chamber at an angle γ of 30° with the horizontal plane. The regenerator inlet 10 extends into the reaction chamber at an angle δ of 22° with the horizontal plane. The horizontal extension distance relative to the external heat recovery agent inlet 7 is 1 / 4 of the height hh of the bottom plate 18 of the solid distribution component 17. The distance h between the regenerator inlet 10 and the external heat recovery agent inlet 7 is 0.5(dc+dz). The distance between the regenerator inlet 10 and the first turbulence member 15 from bottom to top in the reactor is 0.4m.

[0188] The apparent velocity of the methanol feed gas f entering the feed section is 1.2 m / s, the preheating temperature is 180℃, the catalyst is selected from SAPO 34 molecular sieve catalyst for methanol-to-olefins process, and the average concentration of catalyst in the reaction chamber is 85 kg / m³. 3 The reaction temperature was 450℃ and the reaction pressure was 0.11MPa.

[0189] The standard deviation σ1 of the change in the concentration ratio of regenerator in the total solid particles in the reaction chamber is 0.41, and the standard deviation σ2 of the change in the concentration ratio of regenerator in the total gas-solid material is 0.47. The carbon deposition of the feed regenerator is 0.03 wt%, and the carbon deposition of the remaining circulating agent, external heat recovery agent, and returned catalyst fine powder is 3.2 wt%. The difference in the average carbon deposition per unit area of ​​the horizontal cross-section 2 m above the feed gas distributor is less than 0.30 wt%. The non-uniformity of catalyst concentration distribution in the chamber above the regenerator inlet is σ. p It is 0.94.

[0190] Example 4

[0191] The circulating fluidized bed reactor is configured according to Example 3, except that two turbulence-inducing components 15 are axially spaced at equal intervals in the reaction chamber 6, the width X of the side ring 22 is D1 / 64, the total porosity 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 regenerator inlet 10 and the external heat recovery agent inlet 7 is 1.5dc;

[0192] The standard deviation σ1 of the change in the concentration ratio of regenerator in the total solid particles in the reaction chamber is 0.56, and the standard deviation σ2 of the change in the concentration ratio of regenerator in the total gas-solid material is 0.69. The carbon deposition of the feed regenerator is 0.03 wt%, and the carbon deposition of the remaining circulating agent, external heat recovery agent, and returned catalyst fine powder is 3.2 wt%. The difference in the average carbon deposition per unit area of ​​the horizontal cross-section 2 m above the feed gas distributor is less than 0.39 wt%. The non-uniformity of catalyst concentration distribution in the chamber above the regenerator inlet is σ. p It is 1.05.

[0193] Example 5

[0194] The circulating fluidized bed reactor was set up according to Example 3, except that the external heat exchanger inlet 7 in the reaction chamber 6 was not equipped with a solid distribution component 17, and the catalyst directly entered the reactor chamber.

[0195] The standard deviation σ1 of the change in the concentration ratio of regenerant in the total solid particles in the reaction chamber is 0.92, and the standard deviation σ2 of the change in the concentration ratio of regenerant in the total gas-solid material is 1.11. The carbon deposition of the feed regenerant is 0.03 wt%, and the carbon deposition of the remaining circulating agent, external heat recovery agent, and returned catalyst fine powder is 3.2 wt%. The difference in the average carbon deposition per unit area of ​​the horizontal cross-section 2 m above the feed gas distributor is less than 1.17 wt%. The non-uniformity of catalyst concentration distribution in the chamber above the regenerant inlet is σ. p It is 1.13.

[0196] Example 6

[0197] The circulating fluidized bed reactor is set up according to Example 3, except that three turbulence-inducing components 15 are axially and equally spaced in the reaction chamber 6. The regenerator inlet 10 and the external heat exchanger inlet 7 are at the same horizontal height of the reactor but located at different positions on the circumference of the reactor. The regenerator inlet 10 is closer to the side of the external heat exchanger inlet 7. The regenerator inlet 10 in the reaction chamber 6 is connected to a solid distribution component 17 facing the center of the reaction chamber.

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

[0199] Example 7

[0200] The reaction chamber 6 of the circulating fluidized bed reactor is equipped with three circular flow-disrupting components 15 arranged axially along the reactor, conforming to the cross-sectional shape of the reaction chamber, with an installation spacing ΔH = 0.8 m. The diameter D1 of the flow-disrupting components 15 is approximately equal to the inner diameter D of the reaction chamber, and includes a guide section and a mixing section coaxially distributed in the radial direction. The guide section includes a guide plate 20, on which multiple equilateral triangles are evenly distributed (e.g., ...). Figure 2a The air passage (shown) has an opening diameter of Φ15mm and a total porosity of 3%. The mixing section surrounding the guide section includes six concentrically arranged turbulent rings. Each turbulent ring has multiple identical cylindrical turbulent fluids 21 evenly distributed and without pores. The horizontal cross-sectional shape of the turbulent fluid 21 is circular with a length-to-diameter ratio of 3.5:1, and its equivalent diameter is 85mm. The total porosity of the mixing section is 86%, and the ratio of the total porosity area of ​​the mixing section to the total porosity area of ​​the guide plate is 176. The diameter of the guide plate 20 is d. b =0.35D1, and a side ring 22 is provided on the cavity wall near the reaction chamber, which is connected to the largest turbulent fluid ring. The width X of the side ring 22 is D1 / 25.

[0201] The apparent velocity of the methanol feed gas f entering the reaction chamber is 1.2 m / s, the preheating temperature is 180℃, the catalyst is selected from SAPO 34 molecular sieve catalyst for methanol-to-olefins process, and the average concentration of catalyst in the reaction chamber is 85 kg / m³. 3 The reaction temperature was 480℃ and the reaction pressure was 0.11MPa.

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

[0203] Example 8

[0204] The reaction chamber 6 of the circulating fluidized bed reactor is equipped with five circular flow-disrupting components 15 arranged axially along the reactor, conforming to the cross-sectional shape of the reaction chamber, with an installation spacing ΔH = 0.8 m. The diameter D1 of the flow-disrupting components 15 is approximately equal to the inner diameter D of the reaction chamber, and includes a guide section and a mixing section coaxially distributed in the radial direction. The guide section includes a guide plate 20, on which multiple concentric annular arrays are uniformly distributed (e.g., ...). Figure 2b The air passage (shown) has an opening diameter of Φ15mm and a total porosity of 2%. The mixing section surrounding the guide section includes six concentrically arranged turbulent rings. Each turbulent ring has multiple identical cylindrical turbulent fluids 21 evenly distributed and without pores. The horizontal cross-section of the turbulent fluid 21 is circular with a length-to-diameter ratio of 3.5:1, and its equivalent diameter is 85mm. The total porosity of the mixing section is 86%, and the ratio of the total porosity area of ​​the mixing section to the total porosity area of ​​the guide plate is 176. The diameter of the guide plate 20 is d. b =0.2D1, a side ring 22 is provided on the cavity wall near the reaction chamber, which is connected to the largest turbulent fluid ring. The width X of the side ring 22 is D1 / 30.

[0205] The apparent velocity of the methanol feed gas f entering the reaction chamber is 1.2 m / s, the preheating temperature is 180℃, and the catalyst is selected from SAPO 34 molecular sieve catalyst used in methanol-to-olefins processes. The average concentration of the catalyst in the reaction chamber is 90 kg / m³. 3 The reaction temperature was 480℃ and the reaction pressure was 0.11MPa.

[0206] The standard deviation σ1 of the change in the concentration ratio of regenerator in the total solid particles in reaction chamber 6 is 1.16, and the standard deviation σ2 of the change in the concentration ratio of regenerator in the total gas-solid material is 1.23. The carbon deposition of the feed regenerator is 0.03 wt%, and the carbon deposition of the remaining circulating agent, external heat recovery agent, and returned catalyst fine powder is 3.2 wt%. The difference in the average carbon deposition per unit area of ​​the horizontal cross-section 2 m above the feed gas distributor is less than 1.22 wt%. The non-uniformity of catalyst concentration distribution in the chamber above the regenerator inlet is σ pIt is 1.36.

[0207] Comparative Example 1

[0208] Adopting such Figure 9 The MTO continuous reaction regeneration fluidized bed reactor shown has no turbulence components or solid distribution components in the reaction chamber 6. The regenerator is returned to the reactor through the regenerator inlet 10. There are also two circulating agent inlets, one external heat recovery agent inlet and one catalyst fine powder inlet distributed on the circumference at the same horizontal level.

[0209] The apparent velocity of the methanol feed gas f entering the feed section is 1.2 m / s, the preheating temperature is 180℃, the catalyst is selected from SAPO 34 molecular sieve catalyst for methanol-to-olefins process, and the average concentration of catalyst in the reaction chamber is 85 kg / m³. 3 The reaction temperature was 480℃ and the reaction pressure was 0.11MPa.

[0210] The standard deviation σ1 of the change in the concentration ratio of regenerant in the total solid particles in the reaction chamber is 1.97, and the standard deviation σ2 of the change in the concentration ratio of regenerant in the total gas-solid material is 2.56. The carbon deposition of the feed regenerant is 0.03 wt%, and the carbon deposition of the remaining circulating agent, external heat recovery agent, and returned catalyst fine powder is 3.2 wt%. The difference in the average carbon deposition per unit area of ​​the horizontal cross-section 2 m above the feed gas distributor is less than 1.85 wt%. The non-uniformity of catalyst concentration distribution in the chamber above the regenerant inlet is σ. p It is 2.78.

[0211] Comparative Example 2

[0212] The circulating fluidized bed reactor was set up according to Comparative Example 1, except that three axially spaced turbulence-inducing components were arranged in the reaction chamber 6 at equal intervals, with an installation spacing ΔH = 0.8m. The structure of the turbulence-inducing components was a sloping baffle-type internal component based on existing technology. Figure 10 The angle between the baffle and the horizontal plane is 45°, and the distance between the regenerant inlet 10 and the first turbulence-causing component from bottom to top in the reactor is 0.5m.

[0213] The standard deviation σ1 of the change in the concentration ratio of regenerator in the total solid particles in the reaction chamber is 1.72, and the standard deviation σ2 of the change in the concentration ratio of regenerator in the total gas-solid material is 1.92. The carbon deposition of the feed regenerator is 0.03 wt%, and the carbon deposition of the remaining circulating agent, external heat recovery agent, and returned catalyst fine powder is 3.2 wt%. The difference in the average carbon deposition per unit area of ​​the horizontal cross-section 2 m above the feed gas distributor is less than 1.67 wt%. The non-uniformity of catalyst concentration distribution in the chamber above the regenerator inlet is σ. p It is 1.57.

[0214] Comparative Example 3

[0215] The circulating fluidized bed reactor was set up according to Comparative Example 1, except that three axially spaced turbulence-inducing components were arranged in the reaction chamber 6 at equal intervals, with an installation spacing ΔH = 0.8m. The structure of the turbulence-inducing components was a sloping baffle-type internal component based on existing technology. Figure 10 The angle between the baffle and the horizontal plane is 45°, and the distance between the regenerant inlet 10 and the first turbulence-causing component from bottom to top in the reactor is 0.5m; in the reaction chamber 6, the regenerant inlet 10 is connected to a trapezoidal, horizontally oriented flat baffle-type solid distribution component (…). Figure 11 ).

[0216] The standard deviation σ1 of the change in the concentration ratio of regenerator in the total solid particles in the reaction chamber is 1.22, and the standard deviation σ2 of the change in the concentration ratio of regenerator in the total gas-solid material is 1.31. The carbon deposition of the feed regenerator is 0.03 wt%, and the carbon deposition of the remaining circulating agent, external heat recovery agent, and returned catalyst fine powder is 3.2 wt%. The difference in the average carbon deposition per unit area of ​​the horizontal cross-section 2 m above the feed gas distributor is less than 1.08 wt%. The non-uniformity of catalyst concentration distribution in the chamber above the regenerator inlet is σ. p It is 1.40.

[0217] The preferred embodiments of the present invention have been described in detail above; however, the present invention is not limited thereto. Within the scope of the inventive concept, various simple modifications can be made to the technical solutions of the present invention, including combining the various technical features in any other suitable manner. These simple modifications and combinations should also be considered as the content disclosed in the present invention and are all within the protection scope of the present invention.

Claims

1. A flow-turbing component (15) for a fluidized bed reactor, characterized in that, The turbulence-inducing component includes a guide section and a mixing section coaxially distributed in the radial direction, wherein, The flow guide includes a flow guide plate (20), on which at least three evenly distributed air passage holes are opened, and the total porosity of the openings of the flow guide plate is 0.2%-6%. The mixing section surrounds the guide section and includes at least two concentrically arranged turbulent rings. Each turbulent ring has at least six uniformly distributed turbulent fluids (21). The turbulent fluids (21) have non-porous surfaces, and the presence of the turbulent fluids (21) results in a total porosity of 30%-95% for the mixing section. The total void area of ​​the mixing section is 30-500 times the total void area of ​​the guide plate. The aspect ratio of the turbulent fluid (21) is 3:1-10:1, the equivalent diameter of the horizontal cross section of the turbulent fluid (21) is 10-150mm, and the shape of the horizontal cross section is selected from rectangle, square, circle, ellipse and rhombus.

2. The flow-disrupting component according to claim 1, characterized in that, The diameter of the turbulence-inducing component (15) is D1, and the diameter of the guide plate (20) is d. b , 0.2D1≤d b ≤0.6D1; the outer diameter of the mixing section is D1, and the inner diameter is d. b .

3. The flow-disrupting component according to claim 1, characterized in that, The diameter of the air passage holes on the guide plate (20) is 5-50mm, and the diameter difference between each air passage hole does not exceed 10%.

4. The turbulence-disrupting component according to claim 1, characterized in that, The air passages on the guide plate (20) are arranged regularly, with the air passages arranged in equilateral triangles with equal spacing between them, or in a ring array with equal spacing around the center of the guide plate (20).

5. The turbulence-disrupting component according to claim 1, characterized in that, The mixing section includes 2-10 turbulent rings arranged concentrically around the guide plate (20) and spaced apart sequentially, with equal spacing between each turbulent ring.

6. The turbulence-disrupting component according to claim 1, characterized in that, The turbulent fluids (21) have the same shape; wherein the turbulent fluids are arranged vertically.

7. The flow-disrupting component according to claim 1, characterized in that, The flow guide also includes a guide for guiding material from the edge of the mixing section toward the center.

8. The turbulence-disrupting component according to claim 1, characterized in that, The total porosity of the openings in the guide plate is 1.5%-4.5%; and / or The presence of the turbulent fluid (21) results in a total porosity of 60%-90% in the mixing section; and / or The total void area of ​​the mixing section is 50-250 times the total void area of ​​the guide plate.

9. The turbulence-disrupting component according to claim 7, characterized in that, The guide is configured as a side ring (22) connected to the largest turbulent ring, the width of which is X, D1 / 64≤X≤D1 / 16.

10. A fluidized bed reactor comprising a reaction chamber, characterized in that, The reaction chamber is provided with two or more flow-disrupting components (15) arranged along the reactor axis. The flow-disrupting components (15) conform to the cross-sectional shape of the reaction chamber, and the diameter D1 of the flow-disrupting components (15) is equal to the inner diameter D of the reaction chamber. The flow-disrupting components (15) are flow-disrupting components according to any one of claims 1-9.

11. The reactor according to claim 10, characterized in that, The two or more turbulence-disrupting components (15) may each have the same or different structures; the reactor has at least one solid inlet, and the first turbulence-disrupting component in the reactor is arranged above all the solid inlets, 0.2-1.5m away from the geometric center of the uppermost solid inlet.

12. The reactor according to claim 10, characterized in that, The two or more turbulence-disrupting components (15) are installed at equal intervals, with an installation spacing ΔH of 0.5m ≤ ΔH ≤ 1.5m.

13. The reactor according to claim 10, wherein it is a circulating fluidized bed reactor, characterized in that, The reactor is provided with a raw material gas distributor (8) at the bottom of the reaction chamber, and one or more solid feed ports for circulating catalyst feeding are provided on the chamber wall above the raw material gas distributor (8). At least one of the solid feed ports extends into the reaction chamber and is connected to a solid distribution member (17) in the direction of the center of the reaction chamber. The solid distribution member (17) includes a base plate (18) and at least two side baffles (19) mounted opposite to each other on the base plate, wherein the base plate (18) and the side baffles (19) together define a flow channel for solid distribution therethrough; wherein the flow channel is trapezoidal in shape, the upper bottom of the flow channel is connected to the solid feed port and the base plate is tangent to the inner edge of the feed port; The trapezoidal waist and lower base of the flow channel have angles α1 and α2, and 30°≤α1<90°, 30°≤α2<90°; The length of the upper base of the trapezoid is j, and dg≤j≤2dg, where dg is the equivalent diameter of the solid feed inlet; The height of the trapezoid is hh, and 0.01D≤hh≤0.2D, where D is the inner diameter of the reaction chamber.

14. The reactor according to claim 13, characterized in that, The base plate (18) is also trapezoidal in shape, with its upper base collinear with the upper base of the flow channel, and the lengths of its upper and lower bases being greater than the upper and lower bases of the flow channel, respectively, and having the same center line of symmetry as the flow channel; wherein: The trapezoidal legs of the base plate (18) form angles β1 and β2 with respect to the lower base, where 30° ≤ β1 < 90° and β1 ≤ α1, and 30° ≤ β2 < 90° and β2 ≤ α2; and The upper base of the trapezoid of the base plate (18) has a length of k, and j <k≤2j。 15. The reactor according to claim 13, characterized in that, The front end region of the base plate (18) is provided with a plurality of distribution holes, and the total void ratio of the openings of the base plate (18) is 1%-10%; the front end region where the distribution holes are provided is the region on the base plate located in the flow channel along the height hh from the top bottom to the bottom bottom; the diameter of the distribution holes is 2-10mm, and the diameter difference between each distribution hole does not exceed 10%; at least some of the distribution holes are distributed in an equilateral triangle distribution with staggered front and back rows, or in a rectangular distribution with front and back aligned.

16. The reactor according to claim 13, characterized in that, The base plate is a flat plate or a wave plate, and the waveform of the wave plate is a cosine wave, a circular wave or an elliptical wave; the base plate (18) forms an angle θ with the horizontal plane, where 0°≤θ≤45°.

17. The reactor according to claim 10 or 13, wherein it is a circulating fluidized bed reactor, characterized in that, The reactor is provided with a raw material gas distributor (8) at the bottom 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 material gas distributor (8). 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. The geometric center of the type I solid phase feed port and the geometric center of the type II solid phase feed port are on the same straight line in the vertical direction, or deviate from each other by no more than 5°. The vertical distance between the geometric center of the type II solid feed inlet and the geometric center of the type I solid feed inlet is h, where 0.5(dc+dz)≤h≤1.5dc, and: dc is the equivalent diameter of the type I solid feed inlet, and dz is the equivalent diameter of the Type II solid feed inlet; At least one of the type I solid feed ports extends into the reaction chamber and is connected to a solid distribution member (17) in the direction of the center of the reaction chamber.

18. The reactor according to claim 17, characterized in that, The plurality of solid feed ports also include at least one additional solid feed port, which is also used for a relatively large amount of solid feed and is located at least 120° circumferentially from the geometric center of the type I solid feed port; wherein, no solid distribution element (17) is connected to the additional solid feed port.

19. The reactor according to claim 17, characterized in that, The plurality of solid feed ports include one or more additional solid feed ports, the geometric centers of the one or more additional solid feed ports and the type I solid feed port are all symmetrically distributed on the circumference; wherein, one or more of the additional solid feed ports are also provided with the solid distribution element (17) in the direction towards the center of the reaction chamber.

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