Circulating fluidized bed reactor provided with solid distribution piece and application of circulating fluidized bed reactor

Abstract

The invention discloses a circulating fluidized bed reactor provided with a solid distribution piece, application of the circulating fluidized bed reactor and a method for producing olefin through methanol conversion. The solid distribution piece prevents solid-phase particle swarms from gathering and falling at the near wall surface, assists each solid-phase material to be further dispersed after entering the reactor, realizes better concentration distribution of a catalyst on different horizontal planes, and realizes more uniform distribution of catalyst carbon deposit. Furthermore, the fluidized bed reactor disclosed by the invention can greatly promote the mixing efficiency between multiple strands of solid-phase materials and between gas and solid phases, reduce the non-uniformity of catalyst distribution on a unit height cross section, remarkably reduce carbon difference distribution on the cross section, strengthen gas-solid contact, promote continuous generation of low-carbon olefins and improve the performance of the reactor; and the production efficiency, the economical efficiency and the environmental protection property of the whole process are further improved.

Description

Technical Field

[0001] The invention relates to the field of fluidized bed reactors, in particular to a circulating fluidized bed reactor provided with a solid distribution piece and application thereof, and a method for producing olefins by converting methanol. Background Art

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

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

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

[0005] CN202208702U discloses a catalyst distributor for promoting uniform distribution of regenerated catalyst in a catalytic cracking regenerator. The distributor is arranged at the center of the device and has distribution arms extending radially. The regenerated catalyst enters the device through small holes and end openings of the distribution arms to improve distribution.

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

[0007] Such prior art solid distributors mainly focus on optimizing gas-solid distribution during catalyst regeneration, and are not specifically designed for reaction processes involving mixing characteristics of multiple solid phase materials (such as the MTO process). The application of these distributors in MTO fast fluidized bed reactors has limitations, and it is difficult to effectively cope with the complex environment of high gas velocity and significant interaction between multiple materials in the fast fluidized bed reactor, resulting in unsatisfactory mixing effect.

[0008] Zhu Liyun, Liu Zetian and others' paper ("Study on the Particle Mixing Characteristics in the Two-stream Catalyst Mixing Pre-lifting Structure of FCC Riser", Journal of Chemical Engineering of Universities, 2014, Issue 03, v.28, pp. 510-517) reported that by adding a concentric central tube at the bottom of the FCC riser, the cavity was divided into the central tube area and the annular gap area, achieving ideal mixing of different solid phase materials at a certain axial height above the central tube. However, the bottom of the MTO fast fluidized bed reactor is the key reaction area, and the addition of a central tube leads to less uniform mixing of different materials in the area near the central tube.

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

[0010] The purpose of the present invention is to overcome the problem that after the existing fast fluidized bed reactor technology is scaled up, there is a problem of poor mixing between multiple catalysts with different temperatures, different carbon deposition degrees, and different particle size distributions in the mixing area of ​​the reaction chamber, as well as between the gas and solid phases, which leads to a decrease in reaction performance. A circulating fluidized bed reactor provided with a solid distribution part and its application and a method for producing olefins by methanol conversion are developed, thereby enabling enhanced mixing of different materials in the mixing area of ​​the reaction chamber of the reactor, especially the circulating fluidized bed reactor, to achieve favorable material distribution and uniformity, thereby improving the performance of the reactor and the production efficiency, economy and environmental protection of the overall process.

[0011] In order to achieve the above-mentioned purpose, the present invention provides, on one hand, a circulating fluidized bed reactor comprising a reaction chamber, wherein a raw gas distributor is arranged at the bottom end of the reaction chamber, and one or more solid-phase feed ports for circulating catalyst feed are opened on the chamber wall located above the raw gas distributor, at least one of the solid-phase feed ports extends into the reaction chamber, and is connected to a solid distribution member toward the center of the reaction chamber; the solid distribution member comprises a bottom plate and at least two side baffles relatively mounted on the bottom plate, wherein the bottom plate and the side baffles together define a flow channel for solids to be distributed therethrough; wherein the flow channel is in the shape of a trapezoid , the upper base of the trapezoidal flow channel is connected to the solid-phase feed port and the bottom plate is tangent to the inner edge of the feed port; the angles between the waist and the lower base of the trapezoid of the flow channel are α1 and α2, and 30°≤α1<90°, preferably 45°≤α1≤75°, 30°≤α2<90°, preferably 45°≤α2≤75°; the length of the upper base of the trapezoid is j, and dg≤j≤2dg, preferably dg≤j≤1.5dg, wherein dg is the equivalent diameter of the solid-phase feed port; the height of the trapezoid is hh, and 0.01D≤hh≤0.2D, preferably 0.05D≤hh≤0.15D, wherein D is the inner diameter of the reaction chamber.

[0012] Another aspect of the present invention provides a circulating fluidized bed reactor comprising a reaction chamber, wherein the reaction chamber is provided with two or more flow-disturbing members arranged along the axial direction of the reactor, the flow-disturbing members conform to the cross-sectional shape of the reaction chamber, and the diameter D1 of the flow-disturbing members is substantially equal to the inner diameter D of the reaction chamber, the flow-disturbing members include a flow-guiding portion and a mixing portion coaxially distributed in the radial direction, wherein the flow-guiding portion includes a flow-guiding plate, and at least three substantially evenly distributed gas-passing holes are provided on the flow-guiding plate, and the opening of the flow-guiding plate is substantially equal to the inner diameter D of the reaction chamber. The total porosity of the pores is 0.2%-6%, preferably 1.5%-4.5%; the mixing portion surrounds the guide portion and includes at least 2 concentrically arranged turbulent body rings, each turbulent body ring is provided with at least 6 uniformly distributed turbulent bodies, the turbulent body surface is non-porous, and the presence of the turbulent body makes the total porosity of the mixing portion 30%-95%, preferably 60%-90%; and the total void area of ​​the mixing portion is 30-500 times, preferably 50-250 times, of the total void area of ​​the guide plate.

[0013] Yet another aspect of the present invention provides a circulating fluidized bed reactor comprising a reaction chamber, wherein a raw gas distributor is provided at the bottom end of the reaction chamber, and a plurality of solid-phase feed ports for circulating catalyst feeding are provided on the chamber wall above the raw gas distributor, wherein the plurality of solid-phase feed ports are respectively used to feed catalysts in the same or different states, including at least one type I solid-phase feed port for a relatively large amount of solid feed, and at least one type II solid-phase feed port for a relatively small amount of solid feed, wherein the geometric center of the type I solid-phase feed port and the geometric center of the type II solid-phase feed port are in a straight line in the vertical direction, or deviate by no more than 5°; the vertical distance between the geometric center of the type II solid-phase feed port and the geometric center of the type I solid-phase feed port is h, 0.5(dc+dz)≤h≤1.5dc, preferably 0.5(dc+dz)≤h≤dc, wherein: dc is the equivalent diameter of the type I solid-phase feed port, and dz is the equivalent diameter of the type II solid-phase feed port.

[0014] The present invention also provides the use of the circulating fluidized bed reactor in methanol conversion to produce olefins, catalytic cracking or fluidized bed propane dehydrogenation.

[0015] The present invention also provides a method for producing olefins by converting methanol. The method uses the reaction equipment described in the present invention, such as a circulating fluidized bed reactor, including feeding methanol raw gas into the feed section of the reaction chamber through a raw gas distributor, and feeding solid-phase catalyst materials, such as regeneration agents, circulating agents, external heat extractors, and other multiple catalyst materials into the feed section of the reaction chamber through one or more solid-phase feed ports and a solid distribution member connected to at least one of the solid-phase feed ports. After the materials enter the equipment, they are carried by the gas phase and flow upward to form contact and react, generating a gas-solid mixture containing low-carbon olefins, and then continue to enter the separation chamber upward for gas-solid separation. The use of a specific solid distribution member connected to the solid-phase feed port prevents the solid-phase particle group from gathering and falling near the wall surface, and assists each solid-phase material to be further dispersed after entering the reactor, so as to achieve a better concentration distribution of the catalyst on different horizontal planes and a more uniform distribution of catalyst carbon deposits.

[0016] Furthermore, the gas-solid mixture is deflected after passing through the guide plate of the flow-disturbing component, flows radially, and continues to pass through the array of flow-disturbing bodies, where a large number of negative-pressure vortices are formed behind each flow-disturbing body. The turbulence intensity is increased, and the nearby catalysts are carried and filled into the large number of vortices behind the flow-disturbing bodies, so that the originally large number of relatively concentrated regeneration agents, circulating agents, external heat-extraction agents, etc. are further dispersed in the cavity under the influence of the airflow, the degree of mixing between multiple streams of catalyst materials is significantly enhanced, the gas-solid contact efficiency is greatly increased, the reaction conditions in different areas of the equipment are close to each other, the occurrence of side reactions is suppressed, and the composition ratio of target low-carbon olefins in the product gas is increased.

[0017] On this basis, the reaction equipment can be further optimized and adjusted from the type II solid phase feed port (e.g., the regeneration agent feed port) for a relatively small amount of solid feed to just above the type I solid phase feed port (e.g., the external heat extraction agent feed port) for a relatively large amount of solid feed, or deviate by no more than 5°. Although the feed amount of the regeneration agent is much smaller than the feed amount of the external heat extraction agent, the regeneration agent has a high temperature and low carbon deposition, and has high reaction activity. It is easy to affect the reaction selectivity due to the excessive local temperature in the reactor. By adjusting the feed to the top of the external heat extraction agent feed port, the fed regeneration agent will flow directly downward for a distance after entering the equipment due to inertia. During the inertial falling process, it can first mix with the external heat extraction agent with a flow rate much larger than its own, merge into the large stream of the external heat extraction agent, and then be carried by the gas phase for flow dispersion, so as to maximize the premixing of part of the catalyst in the equipment, which is beneficial to improve the initial distribution effect of the catalyst particles entering the equipment.

[0018] Through the above technical scheme, the circulating fluidized bed reactor of the present invention can greatly promote the mixing efficiency between multiple solid phase materials and between gas and solid phases, reduce the unevenness of catalyst distribution on the unit height section, significantly reduce the carbon difference distribution on the section, strengthen gas-solid contact, promote the continuous generation of low-carbon olefins, improve the performance of the reactor, and thus improve the production efficiency, economy and environmental protection of the overall process.

[0019] The present invention also discloses the following embodiments:

[0020] Solution 1: A flow-disturbing component for mixing gas-solid two-phases, characterized in that the flow-disturbing component (15) comprises a flow-guiding portion and a mixing portion, wherein:

[0021] The flow guide portion comprises a flow guide plate (20), and the flow guide plate (20) is used to allow the fluid containing gas and solid phases to flow toward the mixing portion;

[0022] The mixing section comprises a plurality of fluid disturbance bodies (21), the plurality of fluid disturbance bodies (21) being used to cause the fluid to form vortices so as to strengthen the interphase disturbance between the gas and solid phases, and the plurality of fluid disturbance bodies (21) are distributed at intervals around the guide plate (20).

[0023] Solution 2: The flow-disturbing component according to Solution 1 is characterized in that the mixing portion comprises a plurality of flow-disturbing body rings which are concentrically arranged around the guide plate (20) and spaced in sequence, and each of the flow-disturbing body rings comprises a plurality of flow-disturbing bodies (21) which are arranged in a ring shape and spaced circumferentially along the guide plate (20); preferably, the flow-disturbing body (21) is arranged as a vertically placed cylinder.

[0024] Solution 3: The flow-disturbing member according to Solution 2 is characterized in that the guide portion further comprises a guide for guiding the airflow at the edge of the mixing portion to the middle portion, preferably the guide is configured as a side ring (22) connected to the largest-sized flow-disturbing body ring, more preferably the side ring (22) has a width of X, X≤D / 16, wherein when the flow-disturbing member (15) is installed in the cavity, the diameter of the cavity is D;

[0025] and / or

[0026] The guide plate (20) is provided with a plurality of air holes. Preferably, the opening rate of the guide plate (20) is less than 6%. More preferably, the cross section of the guide plate (20) is circular, and the diameter of the guide plate (20) is d b , 0.2D≤d b ≤0.6D;

[0027] and / or

[0028] The flow-disturbing body ring with the smallest diameter is embedded and installed on the edge of the guide plate (20).

[0029] 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 has a reaction chamber (6) and a separation chamber (2) connected to each other, wherein the reaction chamber (6) includes a feed section and a spoiler section located above the feed section, and at least one spoiler component (15) described in any one of Schemes 1-3 is installed in the spoiler section, and preferably, a plurality of the spoiler components (15) are installed in the reaction chamber (6) at equal intervals along the axial direction.

[0030] Solution 5. The reaction device according to Solution 4 is characterized in that a raw gas distributor (8) is provided at the bottom end of the feed section, a solid phase feed port is provided on the cavity wall of the feed section above the raw gas distributor (8), and a distribution member (17) is provided in the reaction chamber, and the distribution member (17) is used to disperse the solid phase fed from the solid phase feed port in the feed section;

[0031] Preferably, the distribution member (17) comprises a corrugated plate (18) and side baffles (19) installed on the corrugated plate (18) at intervals;

[0032] More preferably,

[0033] A plurality of distribution holes are opened in the front end area of ​​the corrugated plate (18), and the opening rate of the corrugated plate (18) is 5% to 10%;

[0034] and / or

[0035] The cross section of the corrugated plate (18) is in the shape of an isosceles trapezoid, and the large end of the corrugated plate (18) extends toward the center of the feeding section.

[0036] Solution 6: The reaction device according to Solution 5 is characterized in that 45°≤β≤α≤75°, wherein β is the angle between the side and the bottom of the corrugated plate (18), and α is the angle between the side baffle (19) and the bottom of the corrugated plate (18);

[0037] and / or

[0038] j≥0.5k, wherein the length of the small end of the corrugated plate (18) is k, and the spacing between the side baffles (19) close to the small end of the corrugated plate (18) is j.

[0039] Scheme 7: The reaction device according to Scheme 5 is characterized in that the solid-phase feed port is used to feed the catalyst, and includes an external heat extractor inlet (7) and a circulating agent inlet which are arranged on the cavity wall of the feed section at intervals along the circumferential direction; wherein a regeneration agent inlet (10) is arranged in the cavity wall just above the external heat extractor inlet, and the distance between the regeneration agent inlet (10) and the external heat extractor inlet (7) is h, preferably 0.5 (d c +d z )≤h≤1.5d c , d c is the equivalent diameter of the external heat extractor inlet (7), d z is the equivalent diameter of the regeneration agent inlet (10);

[0040] and / or

[0041] The solid-phase feed port is provided with the distribution member (17), and the side baffle (19) of the distribution member (17) has a height of L, wherein the range of L is 0.2 to 0.5 times the equivalent diameter of the solid-phase feed port;

[0042] Preferably, the external heat extractor inlet (7) is provided with the distribution element (17), 0.2d c ≤L≤0.5d c ;

[0043] and / or

[0044] The distance between the regeneration agent inlet and the flow-disturbing member (15) is 0.3 m to 0.6 m.

[0045] The use of the disruptor component (15) described in any one of Scheme 8, Schemes 1-3, or the reaction equipment described in any one of Schemes 4-7 in methanol conversion to produce olefins, catalytic cracking or fluidized bed propane dehydrogenation.

[0046] Scheme 9, a method for producing olefins by converting methanol, characterized in that the method adopts the reaction equipment described in any one of Schemes 4-7, including feeding methanol raw gas (f) and catalyst into the feed section, allowing the methanol raw gas (f) to contact the catalyst and react to generate a gas flow containing low-carbon olefins, and allowing the gas flow containing low-carbon olefins to pass upward through the disruptor component (15) to form turbulence to enhance the phase disturbance between the gas and solid phases, and then continue to enter the separation chamber (2) upward for gas-solid separation.

[0047] Scheme 10. The method according to Scheme 9, wherein the methanol raw gas (f) is preheated and fed into the feed section through a raw gas distributor (8), wherein the preheating temperature is 150 to 200° C., and the gas superficial velocity u of the methanol raw gas (f) entering the feed section is f 0.8-2.0m / s;

[0048] and / or

[0049] The catalyst includes a catalyst g returned after heat extraction from an external heat extractor inlet feed, a circulating catalyst r fed from a circulating agent inlet feed, and a regenerated catalyst z fed from a regenerated agent inlet feed;

[0050] and / or

[0051] The catalyst enters the feed section through a distribution piece, and preferably the catalyst g returned after heat removal enters the feed section through the distribution piece;

[0052] and / or

[0053] The average concentration of the catalyst in the reaction chamber is 60-120 kg / m 3 , preferably 80-115kg / m 3 ; and / or

[0054] The reaction temperature in the reaction chamber (6) is 450-500°C, and the reaction pressure is 0.01-1 MPa.

[0055] Other features and advantages of the present invention will be described in detail in the following detailed description. BRIEF DESCRIPTION OF THE DRAWINGS

[0056] The accompanying drawings are used to provide a further understanding of the present application and constitute a part of the specification. Together with the following specific embodiments, they are used to explain the present application but do not constitute a limitation to the present application. In the accompanying drawings:

[0057] Figure 1a is a schematic structural diagram of a spoiler component according to a specific embodiment of the present invention;

[0058] Figure 1b yes Figure 1a A partial schematic diagram of the spoiler member shown;

[0059] Figure 2a and 2b They are respectively schematic diagrams of the distribution of the air holes on the guide plate according to some specific embodiments of the present invention;

[0060] Figure 3a -d are schematic structural diagrams of body disruptors with different horizontal cross-sectional shapes according to some specific embodiments of the present invention;

[0061] Figure 4 is a schematic structural diagram of a gas-solid reaction device according to a specific embodiment of the present invention;

[0062] Figure 5 is a schematic structural diagram of a solid distribution member according to a specific embodiment of the present invention;

[0063] Figure 6 is a top view of a solid distribution member according to a specific embodiment of the present invention and a schematic diagram of the distribution of its distribution holes;

[0064] Figure 7 is a side view of a solid distribution member and a solid phase feed port according to a specific embodiment of the present invention;

[0065] Figure 8 It is a structural schematic diagram of the arrangement of a solid phase feed port and a solid distribution member in a feed section of a circulating fluidized bed reactor according to a specific embodiment of the present invention;

[0066] Fig. 9 It is a structural schematic diagram of a MTO continuous reaction regeneration fluidized bed device according to the prior art;

[0067] Fig.10 It is a structural schematic diagram of an inclined baffle type spoiler component according to the prior art;

[0068] Fig.11 It is a structural schematic diagram of a flat baffle type solid distribution member according to the prior art.

[0069] The components in the drawings are not necessarily drawn to scale, emphasis instead being placed on illustrating the principles of the embodiments. In different drawings or views, the same reference numerals refer to the same or corresponding components.

[0070] Description of Reference Numerals

[0071] 1 gas-solid reactor; 2 separation chamber; 3 lifting pipe; 4 external heat extractor; 5 circulating agent feed port; 6 reaction chamber; 7 external heat extractor feed port; 8 raw gas distributor; 9 circulating agent feed port; 10 regeneration agent feed port; 11 fluidizing air distributor; 12 regeneration agent pipe; 13 degassing tank; 14 catalyst regenerator; 15 spoiler component; 16 catalyst fine powder feed port; 17 solid distribution component; 18 bottom plate; 19 side baffle; 20 guide plate; 21 spoiler; 22 side ring; 23 support plate; 24 rib plate; 25 wall surface. DETAILED DESCRIPTION

[0072] The specific implementation of the present application is described in detail below in conjunction with the accompanying drawings. It should be understood that the specific implementation described here is only used to illustrate and explain the present application, and is not used to limit the present application.

[0073] 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 meanings as commonly understood by those of ordinary skill in the art to which the invention belongs. In the event of a conflict, including definitions, the present specification shall prevail.

[0074] When this specification uses "known to those skilled in the art" or "commonly known in the art" or similar terms to describe materials, methods, components, devices or equipment, this term means that this specification includes those commonly used in the art when this application was filed, but also includes those that are not commonly used at present but will become recognized in the art as being suitable for similar purposes.

[0075] The endpoints and any values ​​of the ranges disclosed herein are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoint values ​​of each range, the endpoint values ​​of each range and the individual point values, and the individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed in this article.

[0076] In the present invention, when the technical solution is given in the form of an open-ended limitation such as "comprising" or "including" certain listed elements, those skilled in the art will understand that the implementation method consisting of or substantially consisting of these elements can obviously be used to implement the technical solution. Therefore, those skilled in the art will understand that the technical solution given in the present invention in the form of an open-ended limitation also covers the specific implementation method consisting of or substantially consisting of the listed elements.

[0077] In the present invention, "scope" is provided in the form of a lower limit and an upper limit, for example, one or more lower limits and one or more upper limits. A given range can be limited by selecting a lower limit and an upper limit, and the selected lower limit and upper limit define the boundary of a given range. All scopes limited in this way are inclusive and combinable, i.e., any lower limit can be combined with any upper limit to form a scope. For example, a scope of 60-110 and 80-120 is listed for a particular parameter, and it is also expected to be understood that the scope of 60-120 and 80-110 is also expected. In addition, if the lower limit listed is 1 and 2 and the upper limit listed is 3,4 and 5, then the following scope is all expected: 1-3, 1-4, 1-5, 2-3, 2-4 and 2-5.

[0078] Unless otherwise specified, all percentages, parts, ratios, etc. mentioned in this specification are based on weight; however, when the weight basis does not conform to the common understanding of those skilled in the art, the basis shall be determined by the common understanding of those skilled in the art.

[0079] In the present invention, unless otherwise specified, the directional words used, such as "up, down, top, bottom", are usually used with reference to the directions shown in the drawings or are used to describe the relative positional relationships of the components in the vertical, perpendicular or gravity direction, and "inside" and "outside" usually refer to the radial inside and outside relative to the center of a circle or the inside and outside of a cavity relative to the cavity.

[0080] In the present invention, vortex refers to the phenomenon that the boundary layer near the wall of the disturbing fluid is detached after the airflow passes through the disturbing 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 mass transfer and heat transfer in the reaction process.

[0081] In the present invention, the annular core effect refers to the process in which the gas phase in the fast fluidized bed gradually gathers at the center of the bed while entraining the solid phase and flowing upward, and the particles carrying the accessories move upward, while the catalyst particles in the near-wall area away from the center area are relatively gathered to form a downward movement, thereby forming a circulating flow between the near-center and near-wall areas of the equipment for mass and heat transfer.

[0082] In the present invention, when referring to the "equivalent diameter" of a solid phase feed port, it generally refers to the inner diameter of the solid phase feed port, unless otherwise specified.

[0083] A fluidized bed generally involves at least two phases, gas and solid, and generally involves a mixture of the two phases, and is thus a typical gas-solid reaction device; in this regard, it is easy to understand that in the present invention, when used as a fluidized bed reactor, the fluidized bed generally contains at least one reaction chamber. For the purpose of the present invention, when, in addition to the up and down movement of solids caused by fluidization in the fluidized zone, a special solid circulation channel (generally located outside the fluidized bed) is established to transport (especially, for example, transport in the opposite direction of the movement caused by fluidization) solids (such as catalyst particles), the fluidized bed thus constructed can be referred to as a "circulating fluidized bed" for the purpose of the present invention. For example, for a fluidized bed reactor in the form of a riser, the catalyst particles will be transported upward and concentrated in the upper part of the riser. For this purpose, a circulating (catalyst) agent pipeline that transports the catalyst from the upper part of the riser back to the lower part of the riser can be connected outside the riser, thereby constructing a circulating fluidized bed reactor.

[0084] Accordingly, for the purpose of the present invention, the solid circulation channel can be a simple pipeline or a complex pipeline or system in which other devices are also arranged at appropriate positions. For example, for a fluidized bed, a simple bypass can be set relative to the fluidized bed so that the solid flows in the opposite direction relative to the flow direction of the fluidized bed; this simple bypass is the solid circulation channel described in the present invention. For another example, for an upward fluidized bed, part of the deactivated catalyst can be taken out from the upper part and regenerated in a regenerator, thereby obtaining the "regenerated agent" described in the present invention, and then transported back to the lower part of the fluidized bed; this system with a regenerator can be regarded as the solid circulation channel described in the present invention. For another example, for the purpose of heat exchange (such as heat extraction), part of the catalyst in the fluidized bed reactor is taken out and heat exchanged in a heat exchanger (such as a heat extractor), thereby obtaining the "external heat exchange catalyst (external heat extractor)" described in the present invention, and then transported back to the fluidized bed in the opposite direction of the flow direction of the fluidized bed; this system with a heat exchanger can be regarded as the solid circulation channel described in the present invention. For another example, the gas outlet of the fluidized bed may entrain some solids, and the solids can generally be separated by a separation device (such as a cyclone separator) to obtain the "catalyst fine powder" mentioned in the present invention, and the catalyst fine powder is returned to the fluidized bed; the system with the separation device can be regarded as the solid circulation channel mentioned in the present invention.

[0085] Therefore, as long as the catalyst particles can be transported through an appropriate circulation channel, they can be referred to as "recycled catalyst" in the present invention. For example, the regeneration agent, external heat exchange catalyst (external heat extractor), and catalyst fine powder can be regarded as "recycled catalyst" in the present invention for the fluidized bed. In particular, the catalyst transported through a simple bypass of the fluidized bed is also a "recycled catalyst" and can be referred to as "circulating agent" in the present invention.

[0086] Accordingly, for a fluidized bed, a satisfactory mixing of the gas-solid two-phase is very important, especially when it involves the use of a recycled catalyst. On the one hand, good gas-solid two-phase mixing can ensure that the solid-phase catalyst is fully in contact with the gas-phase reactant, thereby accelerating the reaction rate and improving the overall operating efficiency of the fluidized bed. On the other hand, the uniformity of mixing directly affects the uniformity and quality stability of the product. If the mixing is uneven, it may cause fluctuations in product performance and affect the quality of the final product. On the other hand, the recycling of the catalyst in the fluidized bed is an important embodiment of its economy. Good mixing can reduce the wear and coking of the catalyst, thereby extending its service life. Therefore, for a fluidized bed (especially a circulating fluidized bed), it is often necessary to properly adjust the distribution of solids, gases or both in the fluidized bed (especially for a fluidized bed reactor, the distribution in the reaction chamber). To this end, the present invention provides a fluidized bed with a specific structure. For the purpose of the present invention, for ease of understanding, "solid phase" and "solid" can be used interchangeably, and "gas" and "gas phase" can be used interchangeably.

[0087] In embodiment A of the present invention, the present invention provides, on the one hand, a flow disruptor 15, which includes a flow guide portion and a mixing portion coaxially distributed in the radial direction, or is composed of the flow guide portion and the mixing portion; on the other hand, a fluidized bed reactor is provided, in whose reaction chamber are provided two or more flow disruptor members 15 arranged along the axial direction of the reactor.

[0088] In embodiment B of the present invention, the present invention provides a circulating fluidized bed reactor, wherein a solid distribution member 17 is connected to the solid phase feed port for circulating catalyst, and the solid distribution member 17 includes a bottom plate 18 and at least two side baffles 19 relatively mounted on the bottom plate 18, wherein the bottom plate 18 and the side baffles 19 together define a flow channel for solids to be distributed therethrough, and the flow channel is in a trapezoidal shape.

[0089] In embodiment C of the present invention, the present invention provides a circulating fluidized bed reactor, which includes a plurality of solid-phase feed inlets specifically arranged on the wall of the reaction chamber of the reactor, including at least one Type I solid-phase feed inlet for a relatively large amount of solid feed, and at least one Type II solid-phase feed inlet for a relatively small amount of solid feed, wherein the geometric center of the Type I solid-phase feed inlet is vertically aligned with the geometric center of the Type II solid-phase feed inlet, or deviates by no more than 5°.

[0090] In the present invention, the embodiments A, B and C may be combined with each other to form, for example, embodiment A+B, embodiment A+C, embodiment B+C, and embodiment A+B+C.

[0091] Implementation A

[0092] According to embodiment A, the present invention provides a flow disturbance member 15, which is particularly suitable for a fluidized bed reactor to promote gas-solid two-phase mixing. Figure 1a As shown, the spoiler member 15 includes a flow guiding portion and a mixing portion coaxially distributed in the radial direction, or is composed of the flow guiding portion and the mixing portion.

[0093] In one embodiment, the guide portion of the spoiler member 15 of the present invention includes a guide plate 20, which has at least 3, at least 7, or at least 19 basically evenly distributed air holes, and the total porosity of the openings of the guide plate is 0.2%-6%, preferably 1.5%-4.5%.

[0094] That is to say, one of the specific schemes of the present invention is to set an obstacle for the fluidization direction in the central area of ​​the fluidized bed, so that for the fluidized bed reactor described in the present invention, when the gas flow carrying solids (also referred to as gas-solid mixture in the present invention) moves to the guide plate 20, due to resistance, a large part of the gas flow is adjusted to flow radially into the mixing section; but at the same time, the guide plate 20 is opened with appropriate porosity, so that part of the gas (and even part of the solid) can still pass through the guide plate through the gas holes. It can be understood that such a structure makes the disturbance between the gas and solid phases at the guide plate more conducive to the mixing required by the present invention. Without being limited to any known theory, it is believed that the total porosity of the guide plate is 0.2%-6%, preferably 1.5%-4.5%, which is particularly beneficial for achieving the purpose of the present invention (such as desirable gas-solid two-phase mixing).

[0095] It is understood by those skilled in the art that, for the purpose of the present invention, when referring to objects with relatively regular geometric shapes such as holes, plates, and disrupting bodies, their relative positional relationships (such as arrangement positions) have the usual meaning in the art, for example, they may refer to the relative positional relationship between the geometric centers or centers of gravity (such as the center of a circle) of these objects.

[0096] For the purpose of the present invention, the "substantially uniform" distribution of the air holes has the conventional technical meaning understood by those skilled in the art, such as the centers of the holes are uniformly distributed on the guide plate in the usual sense in the art, such as the distances between adjacent centers are substantially equal and the air holes are uniformly distributed on the entire guide plate, but it does not exclude the situation where the distances between the centers of one or more air holes at the edge of the guide plate and other air holes are close but not equal. It is understood that those skilled in the art can clearly determine whether the distribution of the air holes belongs to the "substantially uniform" distribution conventionally understood in the art based on actual conditions and the general understanding in the art.

[0097] For the purposes of the present invention, the "porosity" of an object refers to the percentage of the area of ​​a cross section of the object that is not occupied by a solid body and thus allows at least gas to pass through, which is a percentage of the total area of ​​the cross section. For example, it is understood that for a perforated plate, the porosity is the percentage of the sum of the areas of all the holes to the total area of ​​the plate.

[0098] In one embodiment, the diameter of the guide plate 20 of the spoiler member 15 of the present invention is d b , 0.2D1≤d b ≤0.6D1, preferably 0.3D1≤d b ≤0.5D1. Preferably, the outer diameter of the mixing portion is D1; ​​that is, preferably, the diameter of the largest flow-disturbing ring of the mixing portion is the outer diameter of the flow-disturbing member 15. Preferably, the inner diameter of the mixing portion is d b ; That is to say, it is preferred that the flow disturbance ring with the smallest size in the mixing section is directly connected to the guide plate 20, and there are no other components between the two. One of the main purposes of the present invention is to improve the mixing between the gas and solid phases. As mentioned above, the arrangement of the guide plate 20 in the central area of ​​the fluidized bed is one of the important technical means, which forms an obstacle to the fluidization direction; however, it is understandable that such an obstacle needs to exist to an appropriate extent, for example, the fluidization state cannot be maintained. Among various factors, the diameter of the guide plate 20 is therefore one of the important parameters. For example, it is obviously not equal to or substantially equal to the inner diameter D of the reaction chamber. Without being limited to any known theory, it is verified through repeated experiments and simulation calculations that the above-mentioned specific diameter d of the guide plate is believed to be b This is particularly advantageous for achieving the purpose of the present invention (eg, desirable gas-solid two-phase mixing).

[0099] In one embodiment, the opening diameter of the air holes on the guide plate 20 of the flow-disturbing member 15 of the present invention is 5-50 mm, preferably 10-40 mm, and preferably 15-20 mm; and preferably, the diameter of each air hole is substantially equal. For the purpose of the present invention, the diameter of the air holes is "substantially equal" means that the diameter difference between each air hole does not exceed 10%, preferably does not exceed 5%, and preferably does not exceed 1%. As mentioned above, the guide plate 20 is properly perforated so that part of the gas (and even part of the solid) can still pass through the guide plate via the air holes. Accordingly, the diameter of the air holes needs to be appropriately adjusted, especially to match the catalyst diameter; without being limited to any known theory, it is believed that the above-mentioned specific air hole diameter of the guide plate is particularly advantageous for achieving the purpose of the present invention (such as desirable gas-solid two-phase mixing) through repeated experiments and simulation calculations. On the other hand, the inventor has found through research that for the fluidized bed of the present invention, the uniformity of the air holes will be conducive to further improving the mixing effect of the gas-solid two-phase. Therefore, it is preferred that the diameters of the various air holes are substantially equal. Similarly, another embodiment of the uniformity of the air holes of the present invention is the regular arrangement of the air holes. Accordingly, in one embodiment, the plurality of air holes on the guide plate 20 of the spoiler member 15 of the present invention are regularly arranged. In one embodiment, as Figure 2a As shown, the air holes are arranged in an equilateral triangle with equal spacing. Figure 2b As shown, the air holes are arranged in an annular array with equal spacing around the center of the guide plate 20. For the purpose of the present invention, there is no particular limitation on the specific spacing between the air holes, as long as the air hole diameter and the total porosity of the guide plate described in the present invention are met. For example, the spacing between the air holes may be 100-800 mm, preferably 200-500 mm.

[0100] In addition, it is particularly understood that for the perforated guide plate 20, the number and diameter of the air holes together lead to the total porosity of the guide plate. Through repeated experiments and simulation calculation verification, the inventor surprisingly found that the diameter of the air holes and the total porosity of the guide plate are relatively important for the purpose of the present invention (such as the desired gas-solid two-phase mixing); in contrast, the number of air holes is not particularly limited, and those skilled in the art can set it appropriately, as long as it meets the conditions of the present invention regarding the diameter of the air holes, the total porosity of the guide plate, and the substantially uniform distribution of the air holes.

[0101] For the fluidized bed reactor described in the present invention, especially the fluidized bed reactor of embodiment A, when the airflow carrying solids moves to the guide plate 20, due to resistance, a large part of the airflow is adjusted to flow radially into the mixing section. Therefore, the mixing section needs to be set with a higher void ratio to facilitate the airflow carrying solids to continue to pass in a fluidized state. On the other hand, according to the present invention, in the mixing section, a large number of vortices are formed after the airflow passes through the disturbing fluid 21, causing interphase disturbance; when the solid phase (such as catalyst particles) passes through the mixing section, the collision probability between the solid phases and between the solid phase and the disturbing fluid 21 is greatly increased, which promotes the mixing between different solid phases and between the gas and solid phases. In other words, it is very advantageous to properly set the disturbing fluid in the mixing section, and its space must be at least partially occupied by the disturbing fluid. Accordingly, the total void ratio of the mixing section cannot be too high. Thus, in one embodiment, the mixing portion of the flow-disturbing member 15 of the present invention surrounds the flow-guiding portion and includes at least 2 concentrically arranged flow-disturbing fluid rings, each flow-disturbing fluid ring is provided with at least 6 uniformly distributed flow-disturbing fluids 21, the flow-disturbing fluid 21 surface is non-porous, and the presence of these flow-disturbing fluids makes the total porosity of the mixing portion less than 95%, preferably less than 90%, and also preferably less than 80%; and greater than 30%, preferably greater than 40%, and also preferably greater than 60%.

[0102] In one embodiment, the mixing section of the present invention includes 2-10 fluid-disturbing rings, preferably 3-8, concentrically arranged around the guide plate 20 and spaced in sequence. Preferably, the spacing between each of the fluid-disturbing rings is equal. As mentioned above, the mixing section of the present invention is used to allow the airflow carrying solids to continue to pass in a fluidized state and cause phase disturbances therein; therefore, the fluid-disturbing rings need to be appropriately distributed. It is believed that it is advantageous to arrange the fluid-disturbing rings in the above-mentioned number and preferably at equal spacing through repeated experiments and simulation calculations.

[0103] As mentioned above, in the mixing section, a large number of vortices are formed after the airflow passes through the disrupting body 21, causing phase disturbance. In this regard, the inventors have found through experiments that the disrupting body and its distribution have appropriate "uniformity" which is also conducive to the realization of the purpose of the present invention (such as the desired gas-solid two-phase mixing). Accordingly, in one embodiment, the disrupting body 21 of the present invention has the same shape. According to the present invention, a large number of vortices are formed after the airflow passes through the disrupting body 21, causing phase disturbance; therefore, it can be understood that the size and shape of the disrupting body 21 itself have an effect on the formation of the vortex and the result of the phase disturbance. Accordingly, in one embodiment, the aspect ratio of the disrupting body 21 is preferably 3: 1-10: 1, preferably 4: 1-8: 1. Preferably, the equivalent diameter of the horizontal cross section of the disrupting body 21 is 10-150mm, preferably 10-100mm, and the shape of the horizontal cross section is selected from rectangle, square, circle, ellipse and rhombus. Figure 3a-d show schematic diagrams of structures of the disrupting bodies with circular, elliptical, square and diamond horizontal cross-sectional shapes, respectively. When the horizontal cross-sectional shape of the disrupting body is an ellipse, the aspect ratio of the disrupting body is the height of the disrupting body to the short axis of the ellipse; when the horizontal cross-sectional shape of the disrupting body is a rectangle, the aspect ratio of the disrupting body is the height of the disrupting body to the short side of the rectangle. Preferably, the disrupting body is arranged vertically; accordingly, the "horizontal cross section" is a cross section obtained relative to the length direction of the disrupting body.

[0104] As mentioned above, for the fluidized gas-solid mixture in the fluidized bed, the present invention uses the specific arrangement of the guide plate and the flow-disturbing fluid ring in the flow-disturbing member 15, so that the gas-solid mixture originally in the fluidizing direction in the central area of ​​the reactor is adjusted to flow radially into the mixing section, and causes phase disturbances therein. Therefore, the ratio of the total void area of ​​the flow-disturbing fluid ring to the guide plate has a further influence on the flow and disturbance of the gas-solid mixture. Without being limited to any known theory, it is believed that it is particularly advantageous to achieve the purpose of the present invention (e.g., desirable gas-solid two-phase mixing) that the total void area of ​​the mixing section of the present invention is 30-500 times, preferably 50-250 times, of the total void area of ​​the guide plate.

[0105] In one embodiment, the guide portion of the present invention also includes a guide member for guiding the material at the edge of the mixing portion to the middle portion, and the guide member is preferably configured as an edge ring 22 connected to the largest size of the fluid disruptor ring, and the width of the edge ring 22 is X, preferably D1 / 64≤X≤D1 / 16, and more preferably D1 / 50≤X≤D1 / 20.

[0106] According to embodiment A, the present invention provides a fluidized bed reactor comprising a reaction chamber, wherein the reaction chamber is provided with two or more flow-disturbing members 15 as defined above arranged along the axial direction of the reactor, the flow-disturbing member 15 conforms to the cross-sectional shape of the reaction chamber, and the diameter D1 of the flow-disturbing member 15 is substantially equal to the inner diameter D of the reaction chamber; wherein, for the purpose of the present invention, it is understood by those skilled in the art that the D1 is substantially equal to the D, which means that for the purpose of being able to carry out actual installation, the value of the D1 is less than but as close to the D as possible under the condition that the actual process allows, and the specific degree of proximity and difference between the two can be determined by those skilled in the art according to the actual situation and based on the general understanding of the art. For example, the D1 can be less than D by no more than 1%, or no more than 0.5%.

[0107] In one embodiment, the structures of the two or more spoiler members 15 of the present invention are identical or different. As previously mentioned, the present invention applies strong disturbance to the gas-solid mixture of fluidized state by the spoiler member, which is similar to the uniformity of each component on the spoiler member, and the uniformity between the spoiler members is also conducive to achieving the desired purpose of the present invention in a predictable manner to a certain extent. Therefore, in one embodiment, it is preferred for the present invention to use a plurality of identical spoilers.

[0108] The present invention relates to a fluidized bed reactor (such as embodiment A), and may be, for example, a circulating fluidized bed reactor (such as embodiments B and C); accordingly, according to the present invention, a solid phase feed may be involved in a fluidized bed reactor. Preferably, the reactor has at least one solid phase feed port, and the first flow disturbance member from bottom to top in the reactor is arranged above all solid phase feed ports, 0.2-1.5m from the geometric center of the top solid phase feed port, preferably 0.5-1.2m. As mentioned above, the present invention applies strong disturbance to the gas-solid mixture in the fluidized state by the flow disturbance member. Accordingly, in order to make the flow disturbance member and the fluidized gas-solid mixture act better, after experimental verification, it is necessary not only to arrange all the flow disturbance members above all solid phase feed ports, but also to appropriately set the distance between the first flow disturbance member and the top solid phase feed port. It is verified by repeated experiments and simulation calculations that it is believed that the above-mentioned specific distance is particularly advantageous for achieving the purpose of the present invention (such as desirable gas-solid two-phase mixing). Similarly, in order to facilitate the purpose of the present invention (such as satisfactory gas-solid two-phase mixing), it is verified through repeated experiments and simulation calculations that the two or more spoiler components 15 of the present invention are preferably installed at equal intervals, and the installation interval ΔH is also preferably 0.5m≤ΔH≤1.5m.

[0109] When the flow-disturbing member 15 is installed in the cavity of the reaction chamber, during the movement of the airflow, there is a situation where the solid phase concentration near the cavity wall is higher due to the ring-core effect. According to a preferred embodiment of the present invention, in order to guide the particles near the wall to flow toward the center and increase the gas-solid contact, the flow guide portion also includes a guide for guiding the material at the edge of the mixing portion to the middle, and the guide is preferably set as an edge ring 22 connected to the largest flow-disturbing ring, and the width of the edge ring 22 is X, preferably D / 64≤X≤D / 16, more preferably D / 50≤X≤D / 20, wherein D is the inner diameter of the reaction chamber. In one embodiment, the cross-section of the guide plate 20 is preferably circular, and the diameter of the guide plate 20 is d b , 0.2D≤d b ≤0.6D.

[0110] In an exemplary embodiment, Figure 1aAs shown, the flow-disturbing member 15 includes a flow-disturbing portion and a mixing portion coaxially distributed in the radial direction. The flow-disturbing portion includes a flow-disturbing plate 20 and a side ring 22 for guiding the material at the edge of the mixing portion to the middle. The flow-disturbing plate 20 is provided with a plurality of substantially evenly distributed air holes. The mixing portion surrounds the flow-disturbing portion and includes six flow-disturbing body rings that are concentrically arranged around the flow-disturbing plate 20 and spaced in sequence. Among them, the flow-disturbing body ring with the smallest diameter is embedded and installed with the edge of the flow-disturbing plate 20. Each flow-disturbing body ring includes a plurality of flow-disturbing bodies 21 that are arranged in a ring shape and spaced circumferentially along the flow-disturbing plate 20. The flow-disturbing body 21 is configured as a vertically disposed cylinder, so that a vortex is formed after the airflow passes through the cylindrical arc surface, so that the mixing of the gas-solid two-phase is more uniform. It can be understood that the shape of the flow-disturbing body of the present invention is not limited to a cylinder, and any shape that can form a vortex in the airflow is acceptable. As shown in FIG. Figure 1a -b, the fluid disturbance bodies on the same fluid disturbance body ring can be connected by circumferential ribs to provide support for the fluid disturbance body and fix the spacing thereof, and the fluid disturbance bodies in the same radial direction on different fluid disturbance body rings can be connected by radial ribs to provide support for the fluid disturbance body ring and fix the spacing thereof. There is no particular restriction on the number of ribs connecting the fluid disturbance bodies, and those skilled in the art can set them appropriately, as long as they meet the conditions of the present invention regarding the total void ratio and total void area of ​​the mixing portion, fixing the spacing between the fluid disturbance body and the fluid disturbance body ring to make their distribution substantially uniform, etc.

[0111] Based on the above-mentioned flow disturbance member 15 and fluidized bed reactor according to embodiment A, the present invention discloses a gas-solid reaction device. Figure 4 As shown, the gas-solid reaction device includes a gas-solid reactor 1, such as a fluidized bed reactor according to embodiment A, a circulating fluidized bed reactor according to embodiments B and C. The gas-solid reactor 1 has a connected reaction chamber 6 and a separation chamber 2 located above the reaction chamber 6, and a gas phase outlet p is opened at the top of the separation chamber 2. The reaction chamber 6 includes a feed section and a flow disturbance section located above the feed section, and a plurality of flow disturbance components 15 are installed in the flow disturbance section at equal intervals along the axial direction.

[0112] Since the gas-solid reaction device of the present invention includes the flow-disturbing member 15 of the present invention, it also has the above-mentioned advantages of the flow-disturbing member.

[0113] Implementation Plan B

[0114] According to embodiment B, the present invention provides, on the one hand, a solid distribution member 17 for solid feed, which is particularly suitable for a circulating fluidized bed reactor to promote the distribution of the solid feed, the mixing of the solid feed with (if any) other solid feeds, and the mixing of the solid feed with the fluidizing medium.

[0115] According to embodiment B, the present invention provides a circulating fluidized bed reactor, such as Figure 4As shown, a raw gas distributor 8 is provided at the bottom end of the reaction chamber of the reactor, and one or more solid phase feed ports, preferably 1-5 solid phase feed ports, for circulating catalyst feed are provided on the chamber wall of the feed section above the raw gas distributor 8. At least one of the solid phase feed ports extends into the reaction chamber, and is connected to the solid distribution member 17 toward the center of the reaction chamber. In this way, the gaseous raw material fed from the bottom end contacts the solid phase in reverse, and forms an airflow carrying the solid phase upward, and the solid distribution member 17 is used to disperse the solid phase fed from the solid phase feed port in the feed section.

[0116] As mentioned above, for a circulating fluidized bed reactor, it generally involves the recycling of the catalyst. Regardless of the purpose for which the catalyst is recycled, the feeding of the recycled catalyst back to the reactor is involved. Here, an upward fluidized bed is taken as an example. The recycled catalyst is generally taken out from the upper part of the fluidized bed reactor, and after optional intermediate treatment, it is returned to the feed section at the lower part of the fluidized bed reactor through one or more solid-phase feed ports for feeding the circulating catalyst. To this end, after in-depth research, the inventors found that at least one of the solid-phase feed ports is connected to a specific solid distribution member 17, and the recycled catalyst is transported to the reaction chamber through the solid distribution member 17, which will be particularly beneficial to the distribution of the recycled catalyst in the reaction chamber and its mixing with other materials.

[0117] In one embodiment, if Figure 5 As shown, the solid distribution member 17 of the present invention comprises a bottom plate 18 and at least two side baffles 19 mounted oppositely 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; wherein the flow channel is preferably in the shape of a trapezoid, such as an isosceles trapezoid, the upper base of the trapezoidal flow channel is connected to the solid phase feed port and the bottom plate is tangent to the inner edge of the feed port. For the purpose of the present invention, when referring to "trapezoidal", and the corresponding terms such as upper base, lower base, height, etc., have their conventional geometric meanings.

[0118] In order to facilitate the distribution of the recycled catalyst in the reaction chamber and its mixing with other materials, the trapezoidal shape of the present invention has a special design. Specifically, Figure 6As shown, the angles between the waists and the lower base of the trapezoidal flow channel are α1 and α2, where 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, where dg ≤ j ≤ 2dg, preferably dg ≤ j ≤ 1.5dg, and dg is the equivalent diameter of the solid feed inlet; the height of the trapezoid is hh, where 0.01D ≤ hh ≤ 0.2D, preferably 0.05D ≤ hh ≤ 0.15D, and D is the inner diameter of the reaction chamber. Through repeated experiments and simulation calculations for verification, the inventors found that the specific α1 and α2 angles enable the solid feed to be more dispersedly distributed in the reaction chamber; and at the same time, it does not waste the space of the trapezoidal flow channel and does not significantly affect the fluidization and reaction in the reaction chamber. Similarly, through repeated experiments and simulation calculations for verification, the inventors found that the specific upper base length j and height hh are conducive to effectively distributing substantially all of the solid feed via the solid distributor 17, while not significantly affecting the fluidization and reaction in the reaction chamber.

[0119] As described above, the trapezoidal flow channel of the present invention is defined by the bottom plate 18 and the side baffle 19 together. Therefore, the structure and shape of the bottom plate 18 can also affect the fluidization and reaction in the reaction chamber; while the structure and shape of the side baffle can affect the effective distribution of the solid feed, as well as the fluidization and reaction in the reaction chamber.

[0120] Accordingly, 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, where j < k ≤ 2j, preferably j < k ≤ 1.6j.

[0121] 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 significantly affecting the fluidization and reaction in the reaction chamber.

[0122] In one embodiment, as Figure 5As shown, the side baffle 19 of the distribution member 17 can be a rectangular plate with a height of L, wherein 0.2dg≤L≤0.5dg. The rectangular plate has a simple structure and is basically sufficient to meet the requirements of the present invention in terms of, for example, solid distribution. Through repeated experiments and simulation calculation verification, the inventors found that when the side baffle 19 has a height L in the specific range, on the one hand, it is high enough to facilitate solid distribution; on the other hand, it does not cause waste of materials, and more importantly, it is not too high to significantly affect the fluidization and reaction in the reaction chamber.

[0123] In another embodiment, the side baffle 19 of the distribution member 17 may be a right-angled trapezoidal plate with a height L gradually decreasing from the upper bottom, wherein 0.2dg≤L≤0.5dg, and the height of the lower bottom of the right-angled trapezoid is 0.6-0.8L. Through repeated experiments and simulation calculation verification, the inventors found that when the side baffle 19 has a right-angled trapezoidal shape with a specific lower bottom height range, while still being able to basically meet the requirements of solid distribution, in some cases it is more conducive to meeting the requirements of not affecting the fluidization and reaction in the reaction chamber.

[0124] It is understandable that if Figure 7 As shown, in order to satisfy a more favorable distribution of solids such as recycled catalysts, the bottom plate 18 of the distribution member 17 is preferably inclined at a certain angle to the horizontal plane; however, the present invention can also be implemented when the bottom plate is placed horizontally. Accordingly, in one embodiment, the bottom plate 18 is at an angle θ with the horizontal plane, wherein 0≤θ≤45°, preferably 15°≤θ≤30°. The angle between the catalyst circulation channel section at the solid phase feed port and the horizontal plane is γ, 0°≤│γ-θ│≤15°. In one embodiment, arranging the distribution member 17 at a certain angle to the horizontal plane can be achieved by providing a support plate 23 and / or a rib plate 24 between the wall of the reaction chamber and the bottom plate 18.

[0125] The inventors further studied the cross-sectional shape of the bottom plate 18. Through repeated experiments and simulation calculation verification, the inventors found that forming a certain curved surface form of the bottom plate can be more conducive to the satisfactory distribution of solids. Without being limited to any known theory, through a large number of experiments, it is believed that the bottom plate 18 can be a flat plate or a corrugated plate, preferably a corrugated plate, and the waveform of the corrugated plate is a cosine wave, a circular wave or an elliptical wave. For the purpose of the present invention, "circular wave" refers to a waveform formed by connecting several semicircles with the same radius in the first place; and "elliptical wave" refers to a waveform formed by connecting several semi-ellipses with the same major and minor axes in the first place. It can be understood that for cosine waves, circular waves or elliptical waves, each has a central symmetry axis; preferably, the waveform height h0 of the corrugated plate (the vertical distance from the crest to the adjacent trough) is 0.1L≤h0≤0.5L. Accordingly, through repeated experiments and simulation calculation verification, it is preferred as Figure 7As shown, the central symmetry axis of the bottom plate 18 is directly connected to the lowest point of the inner diameter of the solid phase feed port 7, that is, there is no height difference between the two. In addition, for a cosine wave, a circular wave or an elliptical wave, the connection point between the bottom plate and the inner diameter of the solid phase feed port is exactly at the point extending from the central symmetry axis to the lower half of the wave for the waveform. Figure 5 and Figure 7 As shown, when a corrugated plate is used, there is a gap between the bottom end of the side baffle and the concave corrugations of the corrugated plate to allow solid phase discharge.

[0126] For embodiments B and C of the present invention involving a circulating fluidized bed reactor, embodiment A involving a fluidized bed reactor, and combinations thereof, the solid phase feed port is 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 present a certain angle with the horizontal plane, for example, the angle between the pipe section at the connection between the catalyst circulation channel and the reactor wall and the horizontal plane is γ0, which is, for example, 30°<γ0<70°.

[0127] In one embodiment, in order to avoid the formation of a dead zone in the reaction chamber space below the bottom plate 18 (e.g., a corrugated plate) in the reactor and to achieve a better solid phase concentration distribution, a plurality of distribution holes are provided on the bottom plate 18 (e.g., a corrugated plate), so that when the solid is transported through the flow channel on the bottom plate 18, at least a portion of the solid will pass downward through these distribution holes, thereby being distributed downward to the reaction chamber space below the bottom plate 18 (e.g., a corrugated plate). Through experimental verification, surprisingly, it is not necessary to provide distribution holes in the entire bottom plate 18 or the entire flow channel; preferably, it is only necessary to provide a plurality of distribution holes in the front end area of ​​the bottom plate 18 in the flow channel to achieve the above-mentioned "downward distribution" of the favorable solid. In other words, the area outside the flow channel (i.e., outside the side baffle) and the rear end area in the flow channel on the bottom plate 18 do not need to be punched. It has been verified through repeated experiments and simulation calculations that in order to achieve the above-mentioned "downward distribution" of favorable solids, in one embodiment, the front end area where the distribution holes are arranged here may refer to the area on the bottom plate 18 that is in the flow channel from the upper bottom to the lower bottom along the height hh of 45%-95%, preferably between 65%-95%.

[0128] Further, through repeated experiments and simulation calculations, it is verified that in order to achieve the above-mentioned "downward distribution" of favorable solids, in one embodiment, the total open hole porosity of the bottom plate 18 (such as a corrugated plate) is 1%-10%, preferably 4%-8%.

[0129] Similarly, the diameter of the distribution holes needs to be adjusted appropriately, especially to match the catalyst diameter. Similar to the various factors considered for the gas holes, through repeated experiments and simulation calculations, the diameter of the distribution holes can be 2-10 mm, preferably 4-8 mm.

[0130] Similar to the through-holes, the distribution holes and their distribution of the present invention are preferably uniform. Accordingly, in one embodiment, the diameter of each distribution hole is substantially equal; similarly, for the purpose of the present invention, the diameter of the distribution holes is "substantially equal" means that the diameter difference between the distribution holes does not exceed 10%, preferably does not exceed 5%, and preferably does not exceed 1%. Similar to the through-holes, in one embodiment, the opening distribution of the distribution holes is an equilateral triangle distribution with staggered front and back rows. In another embodiment, the opening distribution of the distribution holes is a rectangular distribution aligned front and back. Also similar to the through-holes, for the purpose of the present invention, there is no special restriction on the specific spacing between the distribution holes, as long as it can meet the distribution hole diameter and the total porosity of the distribution plate described in the present invention. For example, the spacing between the distribution holes can be 20-200mm, preferably 50-100mm.

[0131] So, like Figure 5 As shown, for the implementation scheme in which the bottom plate 18 is a corrugated plate, the solid phase flowing through the corrugated plate can achieve a large range of solid phase particle concentration distribution on both sides of the corrugated plate (arrow a), in front (arrow c), in front and below (arrow b) and through the distribution holes (arrow d).

[0132] Implementation Plan C

[0133] According to embodiment C, the present invention provides a circulating fluidized bed reactor such as Figure 4 and Figure 8 As shown, a raw gas distributor 8 is provided at the bottom end of the reaction chamber of the reactor, and a plurality of solid-phase feed ports for circulating catalyst feed are provided on the chamber wall above the raw gas distributor 8, preferably 2-6 solid-phase feed ports, and the plurality of solid-phase feed ports are used to feed catalysts in the same or different states, respectively, including at least one type I solid-phase feed port for a relatively large amount of solid feed, and at least one type II solid-phase feed port for a relatively small amount of solid feed, wherein the geometric center of the type I solid-phase feed port and the geometric center of the type II solid-phase feed port are in a straight line in the vertical direction, or deviate by no more than 5°, and the geometric center of the feed port is the center point of the feed port cross section. In the present invention, as long as the amounts of the two solid feeds are not completely equal, they can be referred to as relatively large amounts and relatively small amounts of solid feeds, respectively. For the purpose of the present invention, the positional relationship between such type II solid-phase feed ports and type I solid-phase feed ports can be referred to as "vertical arrangement".

[0134] As mentioned above, a circulating fluidized bed reactor may involve a variety of recycled catalysts, such as a circulating agent, a regenerating agent, an external heat extractor, etc.; and even a conventional fluidized bed reactor may also contain the recycled catalyst described in the present invention, such as a catalyst fine powder separated by a separation device (such as a cyclone separator) and sent back to the fluidized bed. Accordingly, when the fluidized bed reactor involves two or more different recycled catalysts, they can be fed according to their amounts through the Type I solid phase feed port and the Type II solid phase feed port described in the present invention. Even if the fluidized bed reactor only involves one recycled catalyst, it can be divided into two streams of materials with different amounts as appropriate, and fed through the Type I solid phase feed port and the Type II solid phase feed port described in the present invention, respectively.

[0135] Through the vertical arrangement of the Type I and Type II solid phase feed ports of the present invention, a relatively small amount of solid feed can quickly merge into a relatively large amount of solid feed fed through the Type I solid phase feed port and flow together after entering the fluidized bed through the Type II solid phase feed port located above, thereby helping to improve the gas-solid and solid-solid (such as external heat extraction agent and regeneration agent) uniformity of the smaller amount of solid feed in the reactor.

[0136] Accordingly, in order to promote the uniform distribution, the vertical arrangement of the type I and type II solid phase feed ports requires that the two should have an appropriate spacing in the vertical direction. Figure 8 As shown, the vertical distance between the geometric center of the Type II solid phase feed port and the geometric center of the Type I solid phase feed port is h, preferably 0.5(dc+dz)≤h≤1.5dc, preferably 0.5(dc+dz)≤h≤dc, wherein: dc is the equivalent diameter of the Type I solid phase feed port, and dz is the equivalent diameter of the Type II solid phase feed port.

[0137] In particular, if Figure 8 As shown, for the circulating fluidized bed reactor of embodiment C, in order to be more conducive to the uniform distribution of gas-solid and solid-solid, the solid distribution element 17 according to embodiment B can be connected to one or more solid phase feed ports.

[0138] In one embodiment, if Figure 8As shown, the multiple solid-phase feed ports also include at least one additional solid-phase feed port, which is also used for relatively large amounts of solid feed and is at least 120°, preferably at least 150°, circumferentially away from the geometric center of the type I solid-phase feed port; wherein, preferably, the additional solid-phase feed port is not connected to the solid distribution member 17. Preferably, the additional solid-phase feed port has the same equivalent diameter as the type I solid-phase feed port. In this case, the additional solid-phase feed port is relatively far away from the type I solid-phase feed port, which will reduce the effect of mixing and distribution between the solids fed through the type I and type II solid-phase feed ports, respectively. Therefore, when mixing and distribution between the solids fed through the type I and type II solid-phase feed ports, respectively, is the main consideration, this embodiment is suitable. Accordingly, the inventors determined the interval of at least 120°, preferably at least 150°, through repeated experiments and simulation calculations.

[0139] In another embodiment, the plurality of solid-phase feed ports include one or more additional solid-phase feed ports, and the geometric centers of the one or more additional solid-phase feed ports and the I-type solid-phase feed ports are all symmetrically distributed on the circumference; wherein, preferably, one or more of the additional solid-phase feed ports, preferably all, are also provided with the solid distribution member 17 in the direction toward the center of the reaction chamber. Preferably, the additional solid-phase feed port has the same equivalent diameter as the I-type solid-phase feed port. It can be understood that this embodiment is suitable when the distribution of solids fed through the additional solid-phase feed port is also a more important consideration. Accordingly, the two or more solid distribution members 17 used have the same or different sizes. For different working conditions and different feeds, it is believed that as long as the two or more solid distribution members 17 used have the same size, various conditions can be basically met without having to set solid distribution members 17 of different sizes at the I-type solid-phase feed port and multiple additional solid-phase feed ports; thereby avoiding greater fluctuations under different conditions, and even different sizes of solid distribution members may need to be replaced under different conditions.

[0140] For the sake of uniformity and controllability, through repeated experiments and simulation calculations, it is preferred that the geometric center of the type I solid phase feed port and the geometric center of the additional solid phase feed port are on the same horizontal line, or the upper and lower deviations do not exceed 5°.

[0141] The vertical arrangement of the Type I and Type II solid-phase feed ports of the present invention is to promote the mixing and distribution of the solids fed through the two feed ports; accordingly, through experimental research, the inventors found that it is advantageous that the Type II solid-phase feed port also extends into the reaction chamber, and preferably the distance it extends is greater than the distance the Type I solid-phase feed port extends, which allows a relatively small amount of solid feed to be better merged into a relatively large amount of solid feed below. On the other hand, experimental research shows that, for the purpose of better mixing, it is also preferred that the distance that the Type II solid-phase feed port further extends relative to the Type I solid-phase feed port does not exceed 1 / 2 of the height hh of the trapezoid of the bottom plate 18.

[0142] It is understandable that the diameter of the feed port of the pipeline and the connecting pipeline affects the amount, speed and other factors of the conveying. Based on the comprehensive investigation of multiple factors, through repeated experiments and simulation calculation verification, it is believed that the ratio of the equivalent diameter of the type I solid phase feed port to the type II solid phase feed port is preferably 2:1-10:1, preferably 3:1-5:1. In this case, the circulating fluidized bed of the present invention can have greater operational flexibility and is more widely applicable to the feeding of relatively large amounts and relatively small amounts of recycled catalysts under various conditions.

[0143] It is also understood that the fluidized bed reactor is generally arranged vertically, and accordingly, the pipe section at the connection between the catalyst circulation channel and the reactor wall also often has a certain angle with the horizontal plane, and this angle also affects parameters such as the conveying speed. Through repeated experiments and simulation calculation verification, it is advantageous that the angle between the catalyst circulation channel pipe section at the type I solid phase feed port and the horizontal plane is γ, wherein 0°≤γ≤60°, preferably 0°≤γ≤45°. Similarly, the angle between the catalyst circulation channel pipe section at the type II solid phase feed port and the horizontal plane is δ, wherein 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°.

[0144] The circulating fluidized bed of the present invention may involve a variety of recycling catalysts, especially when, for example, methanol conversion to produce olefins, catalytic cracking or fluidized bed propane dehydrogenation, it may involve an external heat extractor, a circulating agent, a regenerating agent and catalyst fine powder. The type I solid phase feed port is a solid phase feed port for feeding an external heat extractor or a circulating agent, and the type II solid phase feed port is a solid phase feed port for feeding a regenerating agent or catalyst fine powder; preferably, the type I solid phase feed port is a solid phase feed port for feeding an external heat extractor, and the type II solid phase feed port is a solid phase feed port for feeding a regenerating agent.

[0145] In the present invention, Figure 8As shown, the solid phase feed port is used to feed the catalyst, including an external heat extractor feed port 7, circulating agent feed ports 5 and 9, and a catalyst fine powder feed port 16 which are circumferentially spaced apart on the cavity wall of the feed section (the catalyst fine powder, for example, can be the catalyst fine powder separated from the gas phase containing low-carbon olefins discharged from the gas phase outlet by a cyclone separator and refluxed into the feed section); wherein, a regeneration agent feed port 10 is provided in the cavity wall just above the external heat extractor feed port 7, and the vertical distance between the geometric center of the regeneration agent feed port 10 and the geometric center of the external heat extractor feed port 7 is h, 0.5(dc+dz)≤h≤1.5dc, preferably 0.5(dc+dz)≤h≤dc.

[0146] In some embodiments, one or more of the solid phase feed ports are provided with a solid distribution member 17, for example, Figure 4 , Figure 8 The solid distribution member 17 is provided at the circulating agent feed port 5 or 9, the regeneration agent feed port 10 or the external heat extraction agent feed port 7 shown. The side baffle 19 of the solid distribution member 17 has a height of L, wherein L is in the range of 0.2-0.5 times the equivalent diameter of the corresponding solid phase feed port; preferably, the solid distribution member 17 is provided at the external heat extraction agent feed port 7, 0.2dc≤L≤0.5dc, wherein L is the height of the side baffle 19, and dc is the equivalent diameter of the external heat extraction agent feed port; in this way, the regeneration agent z returned by the catalyst to be regenerated after the regeneration treatment can be quickly merged into the catalyst g returned by the external heat extraction pipe and flow together, which is helpful to improve the uniform distribution of the regeneration agent particles in the reactor, such as the external heat extraction agent, the circulating agent and the regeneration agent. If the distance between the pipe ports is too far, the regeneration agent will be separated from the main distribution of the external heat extraction agent, resulting in uneven distribution.

[0147] In some embodiments, the circulating agent feed ports 5 and 9 , the catalyst fine powder feed port 16 , and the external heat extraction agent feed port 7 are at the same horizontal height, and the regeneration agent feed port 10 is vertically above the external heat extraction agent feed port 7 .

[0148] In some embodiments, the regeneration agent feed port 10 is the uppermost solid phase feed port in the reaction chamber feed section, and the distance between the geometric center of the regeneration agent feed port 10 and the first flow disturbance member 15 from bottom to top in the reactor is 0.2-1.5 m, preferably 0.5-1.2 m.

[0149] It should be noted that in some embodiments of the present invention, Figure 4As shown, the gas-solid reaction equipment also includes some conventional settings in the gas-solid reaction equipment in the prior art, such as a catalyst regenerator 14 and a degassing tank 13, wherein the top of the reaction chamber 6 is arranged as an upwardly tapered discharge port, the top of the tapered discharge port extends into the separation chamber 2 to form a lifting pipe 3, and the separation chamber 2 is provided with a fluidizing air distributor 11 for feeding fluidizing air q into the separation chamber 2, 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 feed section, the separation chamber 2 is connected to the feed port of the catalyst regenerator 14 through the regeneration agent pipe 12, and the discharge port of the catalyst regenerator 14 is connected to the feed section through the regeneration agent pipe provided with the degassing tank 13, etc., which can be configured and adjusted according to actual production needs, and the present invention will not be repeated here.

[0150] The gas-solid reaction device of the present invention, under the action of the relative position adjustment of the flow disturbance member 15, the solid distribution member 17 and / or the solid phase feed port according to the present invention, makes the standard deviation σ1 of the change in the concentration ratio of the solid phase particles in the total amount of the solid phase particles at different positions in the height area above the top solid phase feed port in the reaction chamber 6 less than 1.2, preferably less than 0.8, makes the standard deviation σ2 of the change in the concentration ratio of the solid phase particles in the total amount of the gas-solid material at different positions in the height area above the top solid phase feed port in the reaction chamber 6 less than 1.5, preferably less than 0.8, makes the standard deviation (unevenness) σ of the total concentration difference of the solid phase particles (for example, the recycled catalyst, including the circulating agent, the regenerating agent and the external heat extracting agent) at different positions in the height area above the top solid phase feed port in the reaction chamber 6 p Less than 1.7, preferably less than 1.2; the above standard deviation is calculated according to the following formula:

[0151]

[0152] Where σ is the standard deviation, representing the discreteness (unevenness) of the samples taken at different positions in the reaction chamber 6. The larger the value, the more uneven the distribution of the samples in the total amount. 1i is the concentration ratio of solid particles (such as regenerant) at a sampling point in the cavity to the total amount of solid particles, x 2i is the concentration ratio of solid particles (such as regenerant) in the total gas-solid volume at a sampling point in the cavity, x pi is the concentration ratio of the total amount of solid particles (such as recycled catalyst) at a sampling point in the cavity to the total amount of gas and solid, x is the average concentration of samples under the corresponding conditions in the area, n is the number of sampling points in the area, and n≥10.

[0153] The present invention greatly promotes the mixing of multiple streams of different solid-phase particle materials, strengthens gas-solid contact, reduces the uneven distribution of solid-phase particles (such as regeneration agent) on a unit height cross section, significantly reduces the carbon difference distribution on the cross section, promotes the continuous generation of low-carbon olefins, and improves the performance of the reactor by arranging a turbulent component in the turbulent section cavity of the fluidized bed reactor equipment, adjusts the relative positions of type I solid-phase feed inlets (such as external heat extraction agent feed inlets) and type II solid-phase feed inlets (such as regeneration agent feed inlets) in the feed section, and / or arranges solid distribution components at one or more solid-phase feed inlets.

[0154] On the other hand, the present invention provides the use of the disruptor member 15 or fluidized bed reactor according to embodiment A of the present invention, the solid distribution member 17 or circulating fluidized bed reactor according to embodiment B of the present invention, the circulating fluidized bed reactor according to embodiment C of the present invention, or a combination thereof in methanol conversion to produce olefins, catalytic cracking, or fluidized bed propane dehydrogenation.

[0155] On the other hand, the present invention provides a method for producing olefins by converting methanol, which adopts the reaction equipment according to the present invention (such as a circulating fluidized bed reactor with a solid distribution member, a fluidized bed reactor with a flow disturbance member, a circulating fluidized bed reactor with a specific solid phase feed port position, or a combination thereof), comprising feeding methanol raw gas f into the feed section through a raw gas distributor, feeding catalyst (such as a recycled catalyst, such as an external heat extractor g, a regeneration agent z, circulating agents r1 and r2, etc.) into the feed section through one or more solid phase feed ports and a solid distribution member 17 connected to at least one of the solid phase feed ports, so that the methanol raw gas f contacts the catalyst and reacts to generate a gas-solid mixture containing light olefins; the gas-solid mixture containing light olefins is allowed to enter the separation chamber 2 upward for gas-solid separation, and the separated gas phase containing light olefins is discharged from the gas phase outlet p at the top of the separation chamber.

[0156] In some embodiments, the external heat extraction agent g returned after heat extraction is dispersed into the feed section through a solid distribution member 17 connected to the external heat extraction agent feed port 7 .

[0157] In some embodiments, the regenerated agent z returned after regeneration is dispersed into the feed section through a solid distribution member 17 connected to the regenerated agent feed port 10 .

[0158] In some embodiments, the gas-solid mixture containing light olefins forms a vortex in the flow disturbance section through the flow disturbance member 15 to enhance the phase disturbance between the gas and solid phases.

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

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

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

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

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

[0164] Example

[0165] The present application is further described below by way of examples, but they do not constitute a limitation of the present application.

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

[0167] The following example is a method for producing olefins by methanol conversion, which includes allowing methanol raw gas f to enter the reaction chamber 6 through the raw gas distributor 8 at the bottom of the reaction chamber 6 after preheating, and mixing, contacting and reacting with the regeneration agent z returned from the catalyst regenerator 14, the external heat extractor g returned after heat extraction, the circulating agents r1 and r2, and the recovered catalyst fine powder. After the reaction, the catalyst is entrained by the gas and quickly passes through the riser 3, and is separated from the gas phase body through the quick separation component at its outlet, and falls downward into the lower part of the separation chamber 2 under the influence of gravity. Part of the accumulated catalyst is directly circulated back to the feed section of the reaction chamber 6 as circulating agents r1 and r2, part of it is passed through an external heat exchanger to extract heat, and after cooling, it is returned to the feed section as an external heat exchanger g, and another part is sent to the catalyst regenerator 14 through the regenerated agent pipe 12 as a regenerated agent for regeneration. After removing the carbon deposits on the catalyst, it is returned to the feed section through the regenerated agent pipe as a regenerated agent z, and multiple streams of different catalyst materials are remixed to contact and react with the raw gas; and the gas phase containing low-carbon olefins carrying a small amount of catalyst fine powder after the reaction leaves the separation chamber 2 through the gas phase outlet p at the top of the separation chamber 2, and is further removed by gas-solid separation. The catalyst fine powder is sent to the subsequent unit for treatment, and the catalyst fine powder is returned to the feed section of the reaction chamber 6 through the catalyst fine powder feed port 16.

[0168] In the following examples, the amount of carbon deposit on the catalyst (or the average amount of carbon deposit) is calculated by dividing the mass of carbon deposit on the catalyst by the mass of the catalyst. The method for determining the mass of carbon deposit on the catalyst is as follows: weigh 0.1-1 gram of carbon-bearing catalyst and place it in a high-temperature carbon analyzer (Wuxi High Speed ​​Analytical Instrument Co., Ltd., high-frequency infrared sulfur-carbon analyzer HIR-944) for combustion, and measure the mass of carbon dioxide generated by combustion by infrared to obtain the mass of carbon deposit on the catalyst. In order to determine the amount of carbon deposit on the catalyst in the reaction zone, an equal amount of small portions of catalyst can be continuously or periodically drawn out or directly taken out from various positions in the reaction zone.

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

[0170] In the following embodiments, by directly sampling the sampling point, the carbon deposit amount Ci of the solid phase particles (including regeneration agent, circulating agent, external heat extractor, etc.) in the area of ​​the sampling point at a certain time can be measured by the high temperature carbon analyzer. Since the circulating agent, external heat extractor and other materials are all derived from the catalyst that has not been regenerated after the reaction, the carbon deposit amount of this part of the catalyst is measured as Cx. If it is assumed that the density of the carbon-containing catalyst that has not been regenerated, such as the circulating agent, the external heat extractor and other recycled catalysts, is approximately the same as the density of the regenerated non-carbon deposited catalyst, then the concentration of the solid phase particles (such as the regeneration agent) at a certain sampling point in the cavity accounts for x in the total amount of the solid phase particles. 1i =(1-Ci / Cx);

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

[0172] Example 1

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

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

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

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

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

[0178] Example 2

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

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

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

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

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

[0184] Example 3

[0185] The reaction chamber 6 of the circulating fluidized bed reactor is provided with 5 circular flow-disturbing members 15 arranged along the axial direction of the reactor and conforming to the cross-sectional shape of the reaction chamber, with an installation spacing ΔH=0.8m; the diameter D1 of the flow-disturbing member 15 is substantially equal to the inner diameter D of the reaction chamber, and includes a flow-guiding portion and a mixing portion coaxially distributed in the radial direction; wherein the flow-guiding portion includes a flow-guiding plate 20, on which a plurality of equilateral triangular evenly distributed gas-passing holes are provided, with a hole diameter of Φ15mm and a total hole porosity of 2%; the mixing portion includes 6 concentrically arranged flow-guiding portions surrounding the flow-guiding portion. The fluid-disturbing ring is provided, each fluid-disturbing ring is provided with a plurality of identical cylindrical fluid-disturbing bodies 21 which are evenly distributed and have no holes on the surface, the fluid-disturbing bodies 21 are vertically arranged, the fluid-disturbing body 21 in the fluid-disturbing ring with the smallest size is embedded and installed with the edge of the guide plate 20, the horizontal cross-section of the fluid-disturbing body 21 is circular, the aspect ratio is 3.5:1, the equivalent diameter of the horizontal cross-section is 85 mm, the total void ratio of the mixing part is 86%, and the ratio of the total void area of ​​the mixing part to the total void area of ​​the guide plate is 176; the diameter of the guide plate 20 is d b =0.2D1, a side ring 22 connected to the largest fluid disturbance ring is provided on the cavity wall close to the reaction cavity, and the width X of the side ring 22 is D1 / 30.

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

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

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

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

[0190] Example 4

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

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

[0193] Example 5

[0194] The circulating fluidized bed reactor is set up according to Example 3, except that no flow disturbance member 15 is provided in the reaction chamber 6.

[0195] The standard deviation of the change in the concentration ratio of the regenerant in the total solid particles in the reaction chamber is σ1, and the standard deviation of the change in the concentration ratio of the regenerant in the total gas-solid material is σ2. The carbon deposition of the feed regenerant is 0.03wt%, and the carbon deposition of the remaining circulating agent, external heat extractor and returned catalyst fine powder is 3.2wt%. The difference in the average carbon deposition per unit area of ​​the horizontal section at a height of 2m above the raw gas distributor is less than 0.80wt%. The unevenness of the catalyst concentration distribution in the chamber above the regenerant feed port is σ p It is 1.49.

[0196] Example 6

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

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

[0199] Example 7

[0200] The bottom end of the reaction chamber 6 of the circulating fluidized bed reactor is located on the chamber wall above the raw gas distributor 8, and four solid-phase feed ports for circulating catalyst feed are provided, including an external heat extraction agent feed port 7, two circulating agent feed ports 5, 9 and a regeneration agent feed port 10, wherein the regeneration agent feed port 10 extends into the reactor chamber wall and is connected to a solid distribution member 17 toward the center of the reaction chamber. The distribution member includes a bottom plate 18 and two side baffles 19 relatively mounted on the bottom plate, defining an isosceles trapezoidal flow channel, the upper bottom of which is connected to the regeneration agent feed port 10 and is tangent to the inner edge of the feed port, and the waist of the trapezoid is tangent to the lower The bottom angles α1 and α2 are both 60°, the upper bottom length j of the trapezoidal flow channel is equal to the regeneration agent feed port diameter dg, and the height hh of the trapezoid is 0.1 times the inner diameter D of the reaction chamber; the bottom plate of the distribution member is a flat plate with an isosceles trapezoidal shape, and the angles β1 and β2 between its bottom side and waist are both 48°, and the upper bottom length k of the trapezoidal bottom plate is 1.4dg; the side baffle of the distribution member is rectangular, and its height L = 0.2dg, and a plurality of distribution holes are opened in the front end area of ​​the distribution member, with a total porosity of 5% and a hole diameter of Φ6mm, which are distributed in a front-to-back aligned rectangular array, and the bottom plate forms an angle θ with the horizontal plane, θ = 22°.

[0201] The gas superficial velocity uf of the methanol raw gas f entering the reaction chamber is 1.2 m / s, the preheating temperature is 180°C, the catalyst is selected from the SAPO34 molecular sieve catalyst of the methanol to olefins process, and the average concentration of the catalyst in the reaction chamber is 81 kg / m 3 , reaction temperature 480℃, reaction pressure 0.11MPa.

[0202] The standard deviation of the concentration ratio of the regenerant in the total solid particles in the reaction chamber σ1 is 1.16, the standard deviation of the concentration ratio of the regenerant in the total gas-solid material σ2 is 1.38, the carbon deposition of the feed regenerant is 0.03wt%, the carbon deposition of the remaining circulating agent, external heat extractor and returned catalyst fine powder is 3.2wt%, the difference of the average carbon deposition per unit area of ​​the horizontal section at a height of 2m above the raw gas distributor is less than 1.13wt%, and the unevenness of the catalyst concentration distribution in the chamber above the regenerant feed port σ p It is 1.69.

[0203] Example 8

[0204] The bottom end of the reaction chamber 6 of the circulating fluidized bed reactor is located on the chamber wall above the raw gas distributor 8 and is provided with four solid-phase feed ports for circulating catalyst feed, including an external heat extractor feed port 7, two circulating agent feed ports 5, 9 and a regeneration agent feed port 10, wherein the regeneration agent feed port 10 extends into the reactor chamber wall and is connected to a solid distribution member 17 toward the center of the reaction chamber. The distribution member includes a bottom plate 18 and two side baffles 19 relatively mounted on the bottom plate, defining an isosceles trapezoidal flow channel, the upper bottom of which is connected to the regeneration agent feed port 10 and is tangent to the inner edge of the feed port, and the angles α1 and α2 between the waist of the trapezoid and the lower bottom are both The upper base length j of the trapezoidal flow channel is equal to the diameter dg of the regeneration agent feed port, and the height hh of the trapezoid is 0.1 times the inner diameter D of the reaction chamber; the bottom plate of the distribution member is a corrugated plate with an isosceles trapezoidal shape, and the angles β1 and β2 between its bottom and waist are both 50°, and the upper bottom length k of the trapezoidal bottom plate is 1.4dg; the side baffle of the distribution member is a right-angled trapezoidal plate, and the upper bottom height is 0.3dg and the lower bottom height is 0.2dg; a plurality of distribution holes are opened in the front end area of ​​the distribution member, and the total porosity of the openings is 7%, the opening diameter is Φ6mm, and they are distributed in the form of equilateral triangles staggered in front and back rows, and the bottom plate forms an angle θ with the horizontal plane, θ=22°.

[0205] The gas superficial velocity uf of the methanol raw gas f entering the reaction chamber is 1.2 m / s, the preheating temperature is 180°C, the catalyst is selected from the SAPO34 molecular sieve catalyst of the methanol to olefins process, and the average concentration of the catalyst in the reaction chamber is 82 kg / m 3 , reaction temperature 480℃, reaction pressure 0.11MPa.

[0206] The standard deviation of the concentration ratio of the regenerant in the total solid particles in the reaction chamber σ1 is 1.08, the standard deviation of the concentration ratio of the regenerant in the total gas-solid material σ2 is 1.29, the carbon deposition of the feed regenerant is 0.03wt%, the carbon deposition of the remaining circulating agent, external heat extractor and returned catalyst fine powder is 3.2wt%, the difference of the average carbon deposition per unit area of ​​the horizontal section at a height of 2m above the raw gas distributor is less than 0.91wt%, and the unevenness of the catalyst concentration distribution in the chamber above the regenerant feed port σ p is 1.60.

[0207] Comparative Example 1

[0208] Use Fig. 9 In the MTO continuous reaction regeneration fluidized bed reactor shown, no flow disturbance components and solid distribution components are arranged in the reaction chamber 6, and the regeneration agent returns to the reactor through the regeneration agent feed port 10. Two circulating agent feed ports, an external heat extraction agent feed port and a catalyst fine powder feed port are also distributed on the circumference at the same horizontal height.

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

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

[0211] Comparative Example 2

[0212] The circulating fluidized bed reactor is set up according to Comparative Example 1, except that the regeneration agent feed port 10 in the reaction chamber 6 is connected to a flat baffle-type solid distribution member (a) having a trapezoidal shape and a horizontal plate in the direction of the center of the reaction chamber. Fig.11 ).

[0213] The standard deviation of the concentration ratio of the regenerant in the total solid particles in the reaction chamber σ1 is 1.27, the standard deviation of the concentration ratio of the regenerant in the total gas-solid material σ2 is 1.43, the carbon deposition of the feed regenerant is 0.03wt%, the carbon deposition of the remaining circulating agent, external heat extractor and returned catalyst fine powder is 3.2wt%, the difference of the average carbon deposition per unit area of ​​the horizontal section at a height of 2m above the raw gas distributor is less than 1.67wt%, and the unevenness of the catalyst concentration distribution in the chamber above the regenerant feed port σ p It is 2.39.

[0214] Comparative Example 3

[0215] A circulating fluidized bed reactor is set up according to Comparative Example 1, except that three flow-disturbing components are arranged axially at equal intervals in the reaction chamber 6, with an installation interval ΔH=0.8m, and the structure of the flow-disturbing component is an inclined baffle-type internal component according to the prior art ( Fig.10 ), the angle between the baffle and the horizontal plane is 45°, the distance between the regeneration agent feed port 10 and the first flow disturbance member from bottom to top in the reactor is 0.5m; the regeneration agent feed port 10 in the reaction chamber 6 is connected to a flat baffle-type solid distribution member (which is a trapezoidal flat plate and is a horizontal plate) toward the center of the reaction chamber. Fig.11 ).

[0216] The standard deviation of the concentration ratio of the regenerant in the total solid particles in the reaction chamber σ1 is 1.22, the standard deviation of the concentration ratio of the regenerant in the total gas-solid material σ2 is 1.31, the carbon deposition of the feed regenerant is 0.03wt%, the carbon deposition of the remaining circulating agent, external heat extractor and returned catalyst fine powder is 3.2wt%, the difference of the average carbon deposition per unit area of ​​the horizontal section at a height of 2m above the raw gas distributor is less than 1.08wt%, and the unevenness of the catalyst concentration distribution in the chamber above the regenerant feed port σ p is 1.40.

[0217] The preferred embodiments of the present invention are described in detail above, but the present invention is not limited thereto. Within the technical concept of the present invention, the technical solution of the present invention can be subjected to a variety of simple modifications, including the combination of various technical features in any other suitable manner, and these simple modifications and combinations should also be regarded as the contents disclosed by the present invention and belong to the protection scope of the present invention.

Claims

1. A circulating fluidized bed reactor, characterized in that: The reactor includes a reaction chamber, at the bottom end of which there is a raw gas distributor (8), and on the chamber wall above the raw gas distributor (8), one or more solid-phase feed ports for circulating catalyst feed are provided. At least one of the solid-phase feed ports extends into the reaction chamber and is connected with a solid distributor (17) in the direction towards the center of the reaction chamber; the solid distributor (17) includes a bottom plate (18) and at least two side baffles (19) oppositely installed on the bottom plate (18), and a flow channel for solid distribution is defined by the bottom plate (18) and the side baffles (19) together; wherein the flow channel is in a trapezoidal shape, the upper base of the trapezoidal flow channel is connected to the solid-phase feed port and the bottom plate (18) is tangent to the inner edge of the feed port; 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 port; The height of the trapezoid is hh, and 0.01D ≤ hh ≤ 0.2D, preferably 0.05D ≤ hh ≤ 0.15D, where D is the inner diameter of the reaction chamber; 2. The reactor according to claim 1, characterized in that The bottom plate (18) is also in a trapezoidal shape, its upper base is collinear with the upper base of the flow channel, and the lengths of its upper base and lower base are respectively greater than those of the upper base and lower base of the flow channel, and it has the same symmetry center line as the flow channel; wherein: The angles between the waists and the lower base of the trapezoid of the bottom plate (18) are β1 and β2, 30° ≤ β1 < 90°, preferably 45° ≤ β1 ≤ 75° and β1 ≤ α1, 30° ≤ β2 < 90°, preferably 45° ≤ β2 ≤ 75° and β2 ≤ α2; and The length of the upper base of the trapezoid of the bottom plate (18) is k, and j < k ≤ 2j, preferably j < k ≤ 1.6j; 3. The reactor according to claim 1, characterized in that The side baffle (19) of the distributor (17) is a rectangular plate with a height of L or a right trapezoidal plate with a height gradually decreasing from the upper base L, wherein, 0.2dg ≤ L ≤ 0.5dg, and the height of the lower base is 0.6 - 0.8L; 4. The reactor according to claim 1, characterized in that A plurality of distribution holes are provided in the front-end area of the bottom plate (18), and the total porosity of the holes on the bottom plate (18) is 1% - 10%, preferably 4% - 8%; 5. The reactor according to claim 4, characterized in that The front-end area where the distribution holes are provided is the area on the bottom plate within the flow channel, which is between 45% - 95%, preferably 65% - 95% of the height hh in the direction from the upper base to the lower base; 6. The reactor according to claim 4, characterized in that The diameter of the distribution holes is 2 - 10 mm, preferably 4 - 8 mm. Preferably, the diameters of each distribution hole are substantially equal; Preferably, the opening distribution of at least part of the distribution holes is an equilateral triangle distribution with front and rear rows staggered, or a rectangular distribution with front and rear alignment; 7. The reactor according to claim 1, characterized in that The bottom plate (18) is a flat plate or a corrugated plate, preferably the corrugation of the corrugated plate is a cosine wave, a circular wave or an elliptical wave; 8. The reactor according to claim 1, characterized in that The bottom plate (18) forms an angle θ with the horizontal plane, where 0° ≤ θ ≤ 45°, preferably 15° ≤ θ ≤ 30°.

9. The reactor according to claim 1, characterized in that The reaction chamber is provided with two or more flow-disturbing members (15) arranged along the axial direction of the reactor, the flow-disturbing members (15) conform to the cross-sectional shape of the reaction chamber, and have a diameter D1 substantially equal to the inner diameter D of the reaction chamber, the flow-disturbing members include a flow-guiding portion and a mixing portion coaxially distributed in the radial direction, or consist of the flow-guiding portion and the mixing portion, wherein: The guide portion comprises a guide plate (20), the guide plate (20) is provided with at least three substantially evenly distributed air holes, and the total porosity of the openings of the guide plate is 0.2%-6%, preferably 1.5%-4.5%; The mixing portion surrounds the flow guide portion and comprises at least two concentrically arranged fluid-disturbing rings, each fluid-disturbing ring being provided with at least six fluid-disturbing bodies (21) distributed evenly, the surface of the fluid-disturbing bodies (21) being non-porous, and the presence of the fluid-disturbing bodies (21) making the total porosity of the mixing portion 30%-95%, preferably 60%-90%; and The total void area of ​​the mixing portion is 30-500 times, preferably 50-250 times, the total void area of ​​the guide plate.

10. The reactor according to claim 9, characterized in that The diameter of the guide plate (20) is d b , 0.2D1≤d b ≤0.6D1; preferably, the outer diameter of the mixing part is D1 and the inner diameter is d b ; and / or The opening diameter of the air holes on the guide plate (20) is 5-50 mm, preferably 5-20 mm, and the diameter of each air hole is substantially equal; and / or The air holes on the guide plate (20) are arranged regularly, and the air holes are arranged in an equilateral triangle with equal spacing between each other, or in a circular array with equal spacing with the center of the guide plate (20) as the center of the circle.

11. The reactor according to claim 9, characterized in that The mixing section comprises 2 to 10 fluid-turbulating body rings which are concentrically arranged around the guide plate (20) and spaced in sequence, and the spacing between the fluid-turbulating body rings is equal; and / or The disrupting bodies (21) have the same shape, with an aspect ratio of 3:1-10:1, an equivalent diameter of a horizontal cross section of the disrupting bodies (21) of 10-150 mm, preferably 10-100 mm, and a shape of the horizontal cross section selected from a rectangle, a square, a circle, an ellipse and a rhombus; wherein the disrupting bodies are arranged vertically.

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

13. The reactor according to claim 1 or 9, characterized in that A plurality of solid-phase feed ports for circulating catalyst feed are provided on the cavity wall above the raw gas distributor (8), wherein the plurality of solid-phase feed ports are respectively used to feed catalysts in the same or different states, and include at least one type I solid-phase feed port for a relatively large amount of solid feed, and at least one type II solid-phase feed port for a relatively small amount of solid feed, wherein the geometric center of the type I solid-phase feed port and the geometric center of the type II solid-phase feed port are in a straight line in the vertical direction, or the deviation does not exceed 5°; The vertical distance between the geometric center of the type II solid phase feed port and the geometric center of the type I solid phase feed port is h, 0.5(dc+dz)≤h≤1.5dc, preferably 0.5(dc+dz)≤h≤dc, wherein: dc is the equivalent diameter of the Type I solid phase feed port, and dz is the equivalent diameter of the type II solid phase feed port; At least the type I solid phase feed port extends into the reaction chamber and is connected to a solid distribution member (17) toward the center of the reaction chamber.

14. The reactor according to claim 13, characterized in that The multiple solid-phase feed ports also include at least one additional solid-phase feed port, which is also used for relatively large amounts of solid feed and is circumferentially at least 120°, preferably at least 150°, away from the geometric center of the type I solid-phase feed port; wherein the additional solid-phase feed port is preferably not connected to a solid distribution piece (17).

15. The reactor according to claim 13, characterized in that The multiple solid-phase feed ports include one or more additional solid-phase feed ports, and the geometric centers of the one or more additional solid-phase feed ports and the type-I solid-phase feed ports are all symmetrically distributed on the circumference; wherein, preferably, one or more, preferably all, of the additional solid-phase feed ports are also provided with the solid distribution member (17) in the direction toward the center of the reaction chamber.

Images