Circulating fluidized bed device

Abstract

The invention provides a circulating fluidized bed device which comprises a pre-lifting unit, a main reaction unit, a post-reaction unit and a regeneration unit, the pre-lifting unit, the main reaction unit, the post-reaction unit and the regeneration unit are communicated in sequence, the main reaction unit comprises a lifting pipe reactor, and the post-reaction unit is communicated with the regeneration unit. At least part of the riser reactor is of a sleeve type structure, the sleeve type structure comprises an outer pipe and an inner pipe arranged in the outer pipe in a sleeved mode, an annular space is formed between the outer pipe and the inner pipe, the outer pipe is connected with a plurality of gas conveying pipes, the inner pipe is a first porous medium pipe with a plurality of first via holes, and the inner pipe is a second porous medium pipe with a plurality of second via holes. The inner pipe is internally provided with a reaction cavity, the first via hole is communicated with the annular space and the reaction cavity, and the first porous medium pipe is a metal pipe and is configured to generate heat when being electrified. The technical problems that a circulating fluidized bed catalyst is poor in fluidization performance, the adjustable range of oil agent contact time is narrow, and the experiment effect is affected are solved.

Description

Technical Field

[0001] This invention relates to the field of petrochemical technology, and in particular to a circulating fluidized bed device. Background Technology

[0002] Hot circulating fluidized bed technology is an important technology for evaluating various reaction processes. It has a wide range of reaction adaptability and can be used for fluidized bed reaction evaluation of various reaction processes such as naphtha cracking, propane dehydrogenation, and methanol to olefins, as well as for evaluation of various reaction catalysts, process research and optimization.

[0003] In propane dehydrogenation, the riser in the hot experimental setup is usually quite thin, generally no more than 20 mm. There is a strong wall effect on the inner side of the riser wall, meaning there is a large amount of catalyst near the wall and very little catalyst in the middle, which may even cause catalyst degassing, making it difficult for the catalyst to be in a fluidized state. In contrast, the riser in real industrial applications has a large diameter and a relatively weak wall effect. These differences ultimately lead to significant differences between the hot experimental setup and the real industrial riser in terms of predicted performance such as product yield, affecting the experimental results.

[0004] In propane dehydrogenation, the oil-solid contact time is a critical parameter, and different processes require different contact times. Therefore, matching the oil-solid contact time to the reactor is crucial for improving product conversion and selectivity. Traditional circulating fluidized beds can only change the oil-solid contact time by adjusting the gas velocity, which has a very narrow range of adjustment. Furthermore, turbulent beds have poor gas-solid contact and are prone to backmixing, making it difficult to optimize the oil-solid contact time required for different reactions.

[0005] Chinese patent CN102039107A discloses a parallel-type embedded riser circulating reaction-regeneration device. This device places the riser reactor inside a regenerator and introduces a fuel oil / gas line. The high-temperature atmosphere inside the regenerator provides the heat required for the reaction, achieving a high-temperature reaction. Because of the significant temperature difference between the dense and dilute phase regions of the catalyst in the regenerator, to reduce deformation caused by excessive temperature differences in different parts of the riser, the embedded riser reactor is divided into multiple sections. The section in the dilute phase region has a larger diameter and lower temperature, while the section in the dense phase region has a smaller diameter and higher temperature. However, the embedded riser reactor is located inside the regenerator, with a fixed structure that is difficult to modify later. It is only suitable for high-temperature reactions. At the same time, the operating gas velocity range of the embedded riser reactor is narrow (in a riser reactor with a fixed structure, if the gas velocity is too low, problems such as particle deposition and uneven fluidization will occur in the bed, thereby reducing the mass and heat transfer efficiency; if the gas velocity is too high, the bed density will be very low, resulting in a decrease in the single-pass conversion rate of the reaction). Consequently, the controllable oil-agent contact time range is narrow (in a riser reactor with a fixed structure, the oil-agent contact time can almost only be changed by the gas velocity), making it unsuitable for reaction systems with different oil-agent contact times.

[0006] Therefore, it is urgent to solve the technical problems of poor fluidization of existing circulating fluidized bed catalysts, narrow adjustable range of oil-agent contact time, and their impact on experimental results. Summary of the Invention

[0007] This invention provides a circulating fluidized bed device to solve the technical problems of poor catalyst fluidization, narrow adjustable range of oil-agent contact time, and impact on experimental results in existing circulating fluidized bed reactors. It helps to improve catalyst fluidization, broaden the oil-agent contact time range of fluidized bed reactors, adapt to the reaction environment required by different catalyst systems, and improve experimental results.

[0008] To achieve the above objectives, the present invention provides a circulating fluidized bed device, comprising: a pre-lifting unit, a main reaction unit, a post-reaction unit, and a regeneration unit, wherein the pre-lifting unit, the main reaction unit, the post-reaction unit, and the regeneration unit are sequentially connected, and the regeneration unit is connected to the pre-lifting unit via a regeneration inclined tube; the main reaction unit includes a riser reactor and an adjusting member detachably connected to the riser reactor, wherein the adjusting member is connected between the riser reactor and the post-reaction unit;

[0009] At least part of the riser reactor is a sleeve structure, the sleeve structure including an outer tube and an inner tube sleeved inside the outer tube, an annular space between the outer tube and the inner tube, the outer tube being connected to multiple gas supply pipes, the inner tube being a first porous medium tube having multiple first through holes, the inner tube having a reaction chamber inside, the first through holes connecting the annular space and the reaction chamber, the first porous medium tube being a metal tube and configured to generate heat when energized.

[0010] The circulating fluidized bed device provided by this invention, since at least part of the riser reactor is a sleeve structure, during operation, high-pressure inert gas is continuously injected into the annular space between the outer tube and the inner tube through the gas supply pipe. The high-pressure inert gas continuously passes through multiple first through holes, blowing away or removing the catalyst accumulated on the inner wall of the first porous media tube due to the wall effect, forming a gas-solid flow similar to that of a real industrial riser, thereby improving the fluidization of the catalyst and the accuracy of experimental result prediction.

[0011] Furthermore, since the main reaction unit includes a riser reactor and an adjustable component that is detachably connected to the riser reactor, it can be transformed into a riser or turbulent bed by disassembling and replacing different adjustable components without adjusting the gas velocity over a small range. This makes the modification more convenient, allows for adjustment of the oil-agent contact time, and provides a wide range of oil-agent contact time adjustment. It can precisely match the oil-agent contact time required by different processes, which is more conducive to the adjustment and optimization of the reaction process.

[0012] In one possible implementation, along the axial direction of the regeneration inclined tube, the regeneration inclined tube includes at least one pipe connection unit spaced apart, the pipe connection unit including an outer tube and an inner tube sleeved inside the outer tube, a void cavity being formed between the outer tube and the inner tube, the inner tube having an inner cavity inside, and an outer pipe connected to the sidewall of the outer tube for supplying gas into the void cavity;

[0013] Along the circumference of the inner tube, at least a portion of the sidewall of the inner tube is a second porous medium tube having a plurality of second through holes, the second through holes connecting the inner cavity and the void cavity, the second porous medium tube being a metal tube and configured to generate heat when energized.

[0014] In one possible implementation, the first through-hole includes a first downward-sloping section, the two ends of which penetrate the inner and outer walls of the inner tube, respectively. Along the height direction of the inner tube, the height of the first downward-sloping section at its end on the inner wall is lower than the height of the first downward-sloping section at its end on the outer wall; or,

[0015] The first through hole includes a second downward inclined section and a bent section that are interconnected. One end of the second downward inclined section penetrates the outer wall of the inner tube, and the other end of the second downward inclined section is connected to one end of the bent section. The other end of the bent section penetrates the inner wall of the inner tube.

[0016] In one possible implementation, the opening ratio of the first through hole on the inner tube is 5% to 25%; and / or,

[0017] The diameter of the first via is 3μm to 50μm; and / or,

[0018] The opening ratio of the second through hole on the inner tube is 5% to 25%; and / or,

[0019] The diameter of the second via is 3μm to 50μm; and / or,

[0020] The circulating fluidized bed device also includes a raw material conveying unit, which is connected to the bottom of the pre-lifting unit.

[0021] In one possible implementation, the regulating element includes a riser replacement section detachably connected between the riser reactor and the subsequent reaction unit; or,

[0022] The regulating component includes a turbulent bed reactor, which is detachably connected between the riser reactor and the post-reaction unit.

[0023] In one possible implementation, the turbulent bed reactor includes a main body, a variable diameter adjustment section, and at least one auxiliary fluidizing nozzle. The variable diameter adjustment section and the main body are detachably connected, and the main body is detachably connected to the downstream reaction unit. The variable diameter adjustment section is detachably connected to the riser reactor, and at least a portion of the inner diameter of the variable diameter adjustment section gradually increases from the riser reactor to the main body.

[0024] The auxiliary fluidizing nozzle extends obliquely from the outside of the variable diameter adjustment section to the inside of the variable diameter adjustment section, and the angle between the central axis of the auxiliary fluidizing nozzle and the central axis of the variable diameter adjustment section is 30° to 60°.

[0025] In one possible implementation, the post-reaction unit includes a stripping settling section, a stripping main section, and a stripping riser connected in sequence. The stripping settling section is connected to the regulating component via a connecting pipe and has a product discharge pipe. The stripping riser is connected to a stripping gas pipe, and a plugging valve is provided at the connection position between the stripping riser and the stripping gas pipe.

[0026] The post-reaction unit further includes a stripping variable diameter section, which is connected between the stripping settling section and the stripping main section, and the inner diameter of at least a portion of the stripping variable diameter section gradually decreases from the stripping settling section to the stripping main section.

[0027] In one possible implementation, the reaction unit, the post-reaction unit, and the regeneration unit are arranged side by side;

[0028] The post-reaction unit and the regeneration unit are connected by a waiting tube and a waiting agent lifting unit connected in sequence.

[0029] In one possible implementation, the regenerator lifting unit includes a regenerator lifting pipe, a regenerator lifting duct, and a regenerator pre-lifter. One end of the regenerator lifting pipe is connected to the regeneration unit, and the regenerator pre-lifter is disposed between the other end of the regenerator lifting pipe and the regenerator lifting duct. The regenerator pipe is connected between the regenerator pre-lifter and the plug valve.

[0030] The acclimation agent riser tube is a sleeve-type structure.

[0031] In one possible implementation, the regeneration unit includes a regeneration settling section, a regeneration main pipe section, and a regeneration riser connected in sequence, the regeneration settling section having a regeneration flue gas pipe, and the regeneration settling section being connected to the regenerating agent riser pipe;

[0032] The regeneration riser is connected to a regeneration air delivery pipe, and a re-plug valve is provided at the connection position between the regeneration riser and the regeneration air delivery pipe. The two ends of the regeneration inclined pipe are respectively connected to the re-plug valve and the pre-lifting unit.

[0033] The regeneration unit further includes a regeneration variable diameter section, which is connected between the regeneration settling section and the regeneration main pipe section, and the inner diameter of at least a portion of the regeneration variable diameter section gradually decreases from the regeneration settling section to the regeneration main pipe section.

[0034] The circulating fluidized bed device provided by this invention is a vertical circulating fluidized bed. Before production, appropriate regulating components can be selected and installed according to the usage requirements. The regulating components can be a riser replacement section or a turbulent bed reactor to complete different types of chemical reactions, thus broadening the application range of the circulating fluidized bed device.

[0035] The circulating fluidized bed device provided by this invention has multiple functions. When the regulating component includes a riser replacement section, it can be used as a single riser reactor for reactions with short gas-solid phase contact time, providing a shorter oil-agent contact time. When the regulating component includes a turbulent bed reactor, it can be used as a turbulent-riser coupled bed, providing a longer oil-agent contact time. Therefore, the gas-solid contact time of the circulating fluidized bed device provided by this invention has a wide adjustable range.

[0036] The circulating fluidized bed device provided by this invention is a vertical circulating fluidized bed, and the flow state is a conveying bed or a turbulent-conveyor coupled bed. The gas-solid contact time can be long or short, and it is applicable to a wide range of reactions. It can effectively increase the adjustable range of oil-agent contact time and can accurately match the oil-agent contact time required by different reaction systems.

[0037] The present invention provides a circulating fluidized bed device in which the riser reactor and the regeneration inclined tube are a sleeve structure. High-pressure inert gas can be delivered into the riser reactor and the regeneration inclined tube to generate disturbance at the bottom of the solid particles, making it difficult for the solid particles to accumulate at the tube wall and to blow the solid particles apart, thereby preventing the accumulation of particulate matter, improving the fluidity of the particulate matter, helping to solve the strong wall effect generated by the laboratory riser reactor, and improving the experimental results.

[0038] In addition to the technical problems solved by the embodiments of the present invention, the technical features constituting the technical solutions, and the beneficial effects brought about by the technical features of these technical solutions described above, other technical problems that can be solved by the circulating fluidized bed device provided by the embodiments of the present invention, other technical features included in the technical solutions, and the beneficial effects brought about by these technical features will be further described in detail in the specific embodiments. Attached Figure Description

[0039] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0040] Figure 1 This is a schematic diagram of the structure of the circulating fluidized bed device provided in an embodiment of the present invention;

[0041] Figure 2 This is a schematic diagram of the structure of another circulating fluidized bed device provided in an embodiment of the present invention;

[0042] Figure 3 A partial cross-sectional view of the riser reactor of the circulating fluidized bed device provided in the embodiments of the present invention, which is a sleeve-type structure;

[0043] Figure 4 for Figure 3 A sectional view of section AA;

[0044] Figure 5 This is a schematic diagram of the structure of the first through-hole of the circulating fluidized bed device provided in an embodiment of the present invention, which is sloping downwards.

[0045] Figure 6 A schematic diagram of the first through-hole of the circulating fluidized bed device provided in an embodiment of the present invention is shown in a bent shape.

[0046] Figure 7 A cross-sectional view of the regeneration inclined tube of the circulating fluidized bed device provided in the embodiment of the present invention, which is a sleeve-type structure;

[0047] Figure 8 for Figure 7 A sectional view of section BB;

[0048] Figure 9 This is a schematic diagram of the structure of the second through-hole of the circulating fluidized bed device provided in an embodiment of the present invention, which is sloping downwards.

[0049] Explanation of reference numerals in the attached figures:

[0050] 10 - Raw material conveying unit;

[0051] 20 - Pre-lifting unit;

[0052] 30 - Main reaction unit;

[0053] 31-Riser reactor;

[0054] 311 - Outer tube;

[0055] 312-Inner tube;

[0056] 313 - Annular space;

[0057] 314 - Gas Pipeline;

[0058] 315 - First via;

[0059] 3151 - First downward slope section;

[0060] 3152 - Second downward slope section;

[0061] 3153-Bent section;

[0062] 316 - Reaction Chamber;

[0063] 317 - First support;

[0064] 32 - Turbulent bed reactor;

[0065] 321-Main body;

[0066] 322 - Variable diameter adjustment section;

[0067] 323 - Auxiliary fluidizing nozzle;

[0068] 33 - Lift pipe replacement section;

[0069] 34 - Flange structure;

[0070] 40-Post-reaction unit;

[0071] 41-Stripping settling section;

[0072] 411 - Product discharge pipe;

[0073] 42-Stripping variable diameter section;

[0074] 43-Stripping main section;

[0075] 44-Stripping riser;

[0076] 45-Stripping pipe;

[0077] 46 - Plug valve;

[0078] 50 - Waiting tube;

[0079] 60 - Reserve agent booster unit;

[0080] 61-Preparation agent riser tube;

[0081] 62-Preparation agent lift duct;

[0082] 63-Preheater for the production of preheating agents;

[0083] 70 - Connecting pipe;

[0084] 80 - Regeneration Unit;

[0085] 81-Regenerated Settlement Section;

[0086] 811-Regenerated Flue Gas Pipe;

[0087] 82-Regeneration variable diameter section;

[0088] 83-Regeneration main pipe section;

[0089] 84-Regenerated riser;

[0090] 85-Re-plug valve;

[0091] 86-Regenerated air delivery pipe;

[0092] 90-Regeneration Inclined Tube;

[0093] 91-Pipe connection unit;

[0094] 911 - Outer tube;

[0095] 912 - Inner tube;

[0096] 9121 - First Half-Tube;

[0097] 9122 - Second Half-Tube;

[0098] 913 - Void cavity;

[0099] 914 - Second via;

[0100] 915 - Inner cavity;

[0101] 916 - Second stent;

[0102] 92-External takeover. Detailed Implementation

[0103] To make the objectives, technical solutions, and advantages of this invention clearer, the technical solutions of this invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some, not all, of the embodiments of this invention. All other embodiments obtained by those skilled in the art based on the embodiments of this invention without creative effort are within the scope of protection of this invention.

[0104] A fluidized bed is a reactor that uses gas or liquid to suspend solid particles by passing them through a layer of granular solid particles, allowing for gas-solid or liquid-solid phase reactions. Fluidized bed technology can be applied to a variety of fields. The working principle of a fluidized bed is to introduce gas from the bottom, forming a uniform gas-solid two-phase flow state in the solid particles.

[0105] If a fluid, such as gas, passes through, the solid particles do not move; this is the fixed bed stage. When the fluid flows upward through the solid particle layer at a certain velocity, the solid particle layer exhibits a flow phenomenon similar to that of a liquid, known as fluidization. As the fluid velocity increases further, the solid particles separate from each other and move within the fluid. The higher the velocity, the more intense the particle movement, resulting in a large amount of gas-solid two-phase mixed flow within the bed.

[0106] Compared with fixed-bed reactors, circulating fluidized bed reactors facilitate continuous catalyst regeneration and circulation, making them suitable for processes with high catalyst deactivation rates.

[0107] In propane dehydrogenation, laboratory riser reactors exhibit a strong wall effect, resulting in a large amount of catalyst near the wall and very little catalyst in the middle. This is a very inefficient form of gas-solid contact. Furthermore, the oil-catalyst contact time is a critical parameter. Increasing the gas flow rate will result in insufficient contact time and low conversion rate; conversely, decreasing the gas flow rate will result in excessively long contact time, leading to low product selectivity and a small percentage of the target product.

[0108] In propane dehydrogenation reactions conducted in hot experimental setups, riser reactors are typically quite narrow, with diameters usually not exceeding 20 mm. This results in a strong wall effect on the inner wall of the riser, meaning a large amount of catalyst is present near the wall while the central area has very little catalyst, sometimes even leading to catalyst degassing and making it difficult for the catalyst to maintain a fluidized state. This differs significantly from the gas-solid contact observed in actual industrial risers (where the diameter is large and the wall effect is relatively weak), leading to substantial differences in predicted product yields and other performance metrics.

[0109] Different processes require different contact times for the oil agent. Ensuring uniform contact of the oil agent in the reactor, reducing the influence of the wall effect, and matching the required contact time is an important but difficult task. To optimize the contact time of the oil agent required for different reactions, the usual practice is to replace the riser reactor. However, this method is time-consuming, costly, inflexible, and has a limited range of adaptability. It is also not very adaptable to material and process conditions in industrial applications.

[0110] In view of this, the circulating fluidized bed device provided by the present invention can obtain a large range of oil-agent contact time adjustment by detachably setting adjustment components without changing the gas velocity by a small range, accurately matching the oil-agent contact time required by different processes, making the modification of the fluidized bed device more convenient and more conducive to the adjustment and optimization of the reaction process.

[0111] This invention provides a circulating fluidized bed device suitable for the dehydrogenation reaction of propane, butane, or other low-carbon hydrocarbons and the catalyst recycling process. This circulating fluidized bed device can also be used in hot experimental setups.

[0112] The circulating fluidized bed apparatus provided in the embodiments of the present invention is described below with reference to the accompanying drawings.

[0113] refer to Figure 1 and Figure 2 As shown, the present invention provides a circulating fluidized bed device, comprising: a pre-lifting unit 20, a main reaction unit 30, a post-reaction unit 40, and a regeneration unit 80. The pre-lifting unit 20, the main reaction unit 30, the post-reaction unit 40, and the regeneration unit 80 are sequentially connected, and the regeneration unit 80 is connected to the pre-lifting unit 20 through a regeneration inclined tube 90. The main reaction unit 30 includes a riser reactor 31 and an adjusting member detachably connected to the riser reactor 31. The adjusting member is connected between the riser reactor 31 and the post-reaction unit 40.

[0114] refer to Figure 3 and Figure 4 As shown, at least part of the riser reactor 31 has a sleeve-type structure, which includes an outer tube 311 and an inner tube 312 sleeved inside the outer tube 311. An annular space 313 exists between the outer tube 311 and the inner tube 312. Multiple gas delivery pipes 314 are connected to the outer tube 311. (Reference) Figure 5 and Figure 6 As shown, the inner tube 312 is a first porous medium tube with multiple first through holes 315. The inner tube 312 has a reaction chamber 316 inside, and the first through holes 315 connect the annular space 313 and the reaction chamber 316. The reaction chamber 316 enclosed by the tube wall of the inner tube 312 is the lifting area.

[0115] The circulating fluidized bed device provided by the present invention includes a riser reactor 31 and an adjusting component detachably connected to the riser reactor 31 in the main reaction unit 30. By disassembling and replacing different adjusting components, a large range of oil-agent contact time adjustment can be obtained without significantly changing the gas velocity. This allows for precise matching of the oil-agent contact time required by different processes, and is more conducive to the adjustment and optimization of the reaction process.

[0116] In addition, refer to Figure 3 and Figure 4As shown, since at least part of the riser reactor 31 is a sleeve structure, during operation, high-pressure inert gas is continuously injected into the annular space 313 between the outer tube 311 and the inner tube 312 through the gas supply pipe 314. The high-pressure inert gas continuously passes through multiple first through holes 315, blowing away the catalyst accumulated on the inner wall of the first porous media tube due to the wall effect, or blowing it away from the side wall of the first porous media tube, forming a gas-solid flow similar to that of a real industrial riser, thereby improving the fluidization of the catalyst and improving the accuracy of experimental result prediction.

[0117] In one possible implementation, the outer tube 311 and the inner tube 312 are connected by a first support 317, which supports the inner tube 312, improves the stability of the inner tube 312, and avoids resonance. The first support 317 does not block the gas in the annular space 313, allowing the gas to flow axially along the riser reactor 31 within the annular space 313.

[0118] The outer diameter of the inner tube 312 is smaller than the inner diameter of the outer tube 311, thereby forming an annular space 313 between the outer tube 311 and the inner tube 312. The width of the annular space 313 can be 1mm to 4mm, for example, the width of the annular space 313 can be 1mm, 2mm, 2.5mm, 3mm, 3.5mm or 4mm, etc.

[0119] In one possible implementation, the thickness of the first porous dielectric tube is 2 mm to 4 mm, for example, the thickness of the first porous dielectric tube is 2 mm, 2.5 mm, 3 mm, 3.5 mm or 4 mm.

[0120] In one possible implementation, the outer pipe 311 is connected to a plurality of gas supply pipes 314, which include at least two sets of gas supply pipes 314. Each set of gas supply pipes 314 is spaced apart along the axial direction of the outer pipe 311, and the distance between two adjacent sets of gas supply pipes 314 along the axial direction of the outer pipe 311 is 1m to 2m. Each set of gas supply pipes 314 includes 4 to 8 gas supply pipes 314 spaced apart circumferentially along the outer pipe 311.

[0121] In one possible implementation, the inner diameter of the gas supply pipe 314 is 1 mm to 6 mm, for example, the inner diameter of the gas supply pipe 314 is 1 mm, 2 mm, 3 mm, 4 mm, 5 mm or 6 mm.

[0122] To prevent catalyst particles or catalyst debris from falling into the first through hole 315 of the first porous media tube during operation, and to reduce the flow resistance in the riser reactor 31, the first through hole 315 is inclined downward toward the ground.

[0123] In one possible implementation method, refer to Figure 5As shown, the first through-hole 315 may include a first downwardly inclined section 3151, with both ends of the first downwardly inclined section 3151 penetrating the inner and outer walls of the inner tube 312, respectively. Along the height direction of the inner tube 312, the height of the first downwardly inclined section 3151 at one end on the inner wall of the inner tube 312 is lower than the height of the first downwardly inclined section 3151 at one end on the outer wall of the inner tube 312. That is, the first through-hole 315 is downwardly inclined, which can prevent catalyst particles or catalyst debris from entering the first through-hole 315. In this example, the pore size of the first through-hole 315 is 3μm to 50μm, the angle between the extension direction of the first through-hole 315 and the axial direction of the inner tube 312 is 30° to 60°, and the opening ratio of the first through-hole 315 on the inner tube 312 is 5% to 25%. For example, the diameter of the first through hole 315 is 3μm, 10μm, 20μm, 30μm, 40μm, or 50μm, and the angle between the extension direction of the first through hole 315 and the axial direction of the inner tube 312 is 30°, 40°, 45°, 52°, or 60°. The opening ratio of the first through hole 315 on the inner tube 312 is 5%, 10%, 15%, 15%, 20%, or 25%.

[0124] Among other possible implementation methods, refer to Figure 6 As shown, the first through-hole 315 may include a second downwardly inclined section 3152 and a bent section 3153 that are interconnected. One end of the second downwardly inclined section 3152 penetrates the outer wall of the inner tube 312, and the other end of the second downwardly inclined section 3152 is connected to one end of the bent section 3153. The other end of the bent section 3153 penetrates the inner wall of the inner tube 312. The second downwardly inclined section 3152 is closer to the air inlet side, and the bent section 3153 is closer to the air outlet side. An angle is formed between the second downwardly inclined section 3152 and the bent section 3153. Along the height direction of the inner tube 312: the height of the end of the second downwardly inclined section 3152 away from the angle on the inner tube 312 is higher than the height of the angle on the inner tube 312, and the height of the end of the bent section 3153 away from the angle on the inner tube 312 is higher than the height of the angle on the inner tube 312. That is, the first through-hole 315 is bent, for example, in a "J" shape. In this example, the diameter of the first through-hole 315 is 3μm to 50μm, the angle between the extension direction of the first through-hole 315 and the axial direction of the inner tube 312 is 30° to 60°, the angle between the extension direction of the bent section 3153 and the axial direction of the inner tube 312 is 90°, and the opening ratio of the first through-hole 315 on the inner tube 312 is 5% to 25%. For example, in this example, the diameter of the first through-hole 315 is 3μm, 10μm, 20μm, 30μm, 40μm, or 50μm, and the angle between the extension direction of the first through-hole 315 and the axial direction of the inner tube 312 is 30°, 40°, 45°, 52°, or 60°. The opening ratio of the first through-hole 315 on the inner tube 312 is 5%, 10%, 15%, 15%, 20%, or 25%.

[0125] In one possible implementation, since propane dehydrogenation is an endothermic reaction, and the riser reactor 31 in the laboratory cannot provide heat, it is often necessary to heat the sidewall of the regeneration inclined tube 90 to achieve heat balance. In this application, the first porous media tube is a metal tube and is configured to generate heat when energized. When the first porous media tube is energized, heat can be generated by the resistance of the first porous media tube itself to provide the heat required for the propane dehydrogenation reaction and maintain the heat balance of the reaction. In one possible implementation, the resistance value can be changed by replacing the first porous media tube with one of different metal materials to provide the heat required for different reaction heat effects.

[0126] In one possible implementation method, refer to Figure 1 As shown, the pre-lifting unit 20 includes a pre-lifter, which is used to mix the reaction raw materials and convey them to the main reaction unit 30. The main reaction unit 30 can be used to realize the catalytic dehydrogenation reaction of low-carbon hydrocarbons, including but not limited to the catalytic dehydrogenation reaction of propane, butane or other low-carbon hydrocarbons. The post-reaction unit 40 is used to separate the oil and catalyst phases discharged from the main reaction unit 30, separating the products and raw materials entrained in the catalyst. The regeneration unit 80 is used to regenerate the catalyst by burning coke. The regenerated catalyst enters the pre-lifting unit 20 through the regeneration inclined tube 90 to prepare for the secondary use of the catalyst, enabling continuous production.

[0127] The riser reactor 31 and the regulating component are connected vertically in sequence.

[0128] In one possible implementation method, refer to Figure 1 As shown, the regulating component includes a riser replacement section 33, which is detachably connected between the riser reactor 31 and the downstream reaction unit 40; or, refer to Figure 2 As shown, the regulating component includes a turbulent bed reactor 32, which is detachably connected between the riser reactor 31 and the downstream reaction unit 40.

[0129] refer to Figure 1 As shown, when the riser replacement section 33 is connected between the riser reactor 31 and the downstream reaction unit 40, the material in the riser reactor 31 and the riser replacement section 33 forms a rapid bed or conveying bed, with the material rapidly lifted. The oil-agent contact time between the materials is relatively short, ranging from 0.3 s to 5 s. Under these conditions, the controllable range of propane dehydrogenation conversion is 5% to 35%, and the controllable range of propylene selectivity for propane dehydrogenation is 75% to 95%.

[0130] In one possible implementation method, refer to Figure 2As shown, the turbulent bed reactor 32 and the riser reactor 31 can be connected via a flange structure 34. The flange structure 34 includes flanges; for example, flanges are provided on the outer walls of both ends of the turbulent bed reactor 32, and flanges are provided on the outer wall of the riser reactor 31. The flanges on the outer walls of the turbulent bed reactor 32 and the riser reactor 31 are connected by fasteners such as bolts or screws, achieving a detachable connection between the turbulent bed reactor 32 and the riser reactor 31. The connection and disassembly process is very convenient and requires no major modifications to the overall circulating fluidized bed device. To improve the sealing effect, a sealing ring is provided between the two connected flanges to prevent leakage at the flange location.

[0131] The inner diameter of the turbulent bed reactor 32 is larger than the inner diameter of the riser replacement section 33 and the inner diameter of the riser reactor 31. The ratio of the inner diameter of the turbulent bed reactor 32 to the inner diameter of the riser reactor 31 is 2 to 10, and the ratio of their heights is 0.1 to 1. Therefore, after the material enters the turbulent bed reactor 32 from the riser reactor 31, the change in the flow velocity of the material can prolong the contact time between the oil and the material.

[0132] With the turbulent bed reactor 32 connected between the riser reactor 31 and the downstream reaction unit 40, the material enters the turbulent bed reactor 32, where the material's rise velocity decreases, creating a turbulent bed. The oil-agent contact time between the material and the reactor is relatively long, ranging from 1 s to 8.5 s. Under this condition, the controllable range for propane dehydrogenation conversion is 15%–45%, and the controllable range for propylene selectivity from propane dehydrogenation is 70%–90%.

[0133] The comparison shows that when the turbulent bed reactor 32 is connected between the riser reactor 31 and the post-reaction unit 40, the propane dehydrogenation conversion rate is improved.

[0134] The riser reactor 31 has external heating elements for heat generation, ensuring a suitable internal temperature and maintaining appropriate reaction temperature conditions. The riser replacement section 33 and the turbulent bed reactor 32 also have external heating elements to ensure suitable reaction temperature conditions within the main reaction unit 30. These heating elements can be, for example, electric heating tubes or electric heating jackets, and the reaction temperature within the main reaction unit 30 can be, for example, 550℃~600℃.

[0135] refer to Figure 1 and Figure 2As shown, the circulating fluidized bed device provided by this invention has multiple functions. When the regulating component includes a riser replacement section 33, it can be used as a single riser reactor for reactions with short gas-solid contact times, providing a shorter oil-agent contact time. When the regulating component includes a turbulent bed reactor 32, it can be used as a turbulent-riser coupled bed, providing a longer oil-agent contact time. Simultaneously, the auxiliary fluidizing nozzles 323 of the turbulent bed reactor 32 can introduce fluidizing air with a gas velocity of 20–70 m / s to promote fluidization of the dense phase bed and improve the gas-solid contact effect in the turbulent bed. Therefore, the circulating fluidized bed device provided by this invention has a wide adjustable range for gas-solid contact time and good gas-solid contact effect.

[0136] Meanwhile, the inner tube 312 inside the riser reactor 31 is the first porous medium tube, which can reduce the wall effect of the catalyst during the riser process, make the gas-solid distribution more uniform, improve the gas-solid contact efficiency, and thus improve the reaction yield.

[0137] In one possible implementation method, refer to Figure 2 As shown, the turbulent bed reactor 32 includes a main body 321, a variable diameter adjustment section 322, and at least one auxiliary fluidizing nozzle 323. The variable diameter adjustment section 322 and the main body 321 are detachably connected, and the main body 321 is detachably connected to the downstream reaction unit 40. The variable diameter adjustment section 322 is detachably connected to the riser reactor 31, which facilitates the installation of the turbulent bed reactor 32.

[0138] The inner diameter of at least part of the variable diameter adjustment section 322 gradually increases from the riser reactor 31 to the main body 321. The variable diameter adjustment section 322 is conical in shape, which helps to reduce the accumulation of catalyst particles.

[0139] The inner diameter of the main body 321 is larger than the inner diameter of the riser reactor 31. The ratio of the inner diameter of the main body 321 to that of the riser reactor 31 can be 2, 3, 3, 5, 5.5, 6, 7, 8, 8.3, 9, or 10. Therefore, when using the turbulent bed reactor 32, the gas velocity can be reduced to adjust the oil-agent contact time.

[0140] The height of the turbulent bed reactor 32 is less than or equal to the height of the riser reactor 31. The ratio of the height of the turbulent bed reactor 32 to the height of the riser reactor 31 is 0.1 to 1. For example, the ratio of the height of the turbulent bed reactor 32 to the height of the riser reactor 31 can be 0.1, 0.3, 0.5, 0.8 or 1.

[0141] In one possible implementation, the auxiliary fluidizing nozzle 323 extends obliquely from the outside of the diameter adjustment section 322 to the inside of the diameter adjustment section 322, and the angle between the central axis of the auxiliary fluidizing nozzle 323 and the central axis of the diameter adjustment section 322 is 30° to 60°. The central axis of the auxiliary fluidizing nozzle 323 is referenced. Figure 2 As shown by the slanted dashed line in the figure, the central axis of the variable diameter adjustment section 322 is referenced. Figure 2 The vertical dashed line in the image is shown.

[0142] In one possible implementation, the number of auxiliary fluidizing nozzles 323 can be multiple, such as 2, 3, 4, 5, 6 or 8, etc. The multiple auxiliary fluidizing nozzles 323 are arranged circumferentially along the variable diameter adjustment section 322 and located in the middle and lower part of the variable diameter adjustment section 322. The auxiliary fluidizing nozzles 323 are inserted obliquely upward into the variable diameter adjustment section 322 from the outside of the variable diameter adjustment section 322.

[0143] In one possible implementation, the angle between the central axis of the auxiliary fluidizing nozzle 323 and the central axis of the variable diameter adjustment section 322 can be 30°, 35°, 45°, 50° or 60°, etc.

[0144] In one possible implementation method, refer to Figure 1 and Figure 2 As shown, the post-reaction unit 40 includes a stripping settling section 41, a stripping main section 43, and a stripping riser 44 connected in sequence. The stripping settling section 41 is connected to the regulating component through a connecting pipe 70, and the stripping settling section 41 has a product discharge pipe 411. The stripping riser 44 is connected to a stripping gas pipe 45, and a plugging valve 46 is provided at the connection position between the stripping riser 44 and the stripping gas pipe 45.

[0145] The post-reaction unit 40 directly contacts the stripping gas and the gas-solid mixture in a countercurrent manner, allowing the product gas adsorbed on the catalyst to diffuse into the gas phase, which helps gas-solid separation and improves product yield. When the stripping gas contains feed gas, it can further contact the catalyst to react and improve the reaction yield. The stop valve 46 is used to control the catalyst circulation rate.

[0146] The product discharge pipe 411 can be connected to the top of the stripping settling section 41, and the mixture of the reaction product, nitrogen and material is discharged from the product discharge pipe 411.

[0147] Downstream of the product discharge pipe 411 are sequentially connected a process gas condenser / separator, a tail gas flow meter, a liquid collection and metering device, a solid sampling device, and a process gas analysis device. The product discharged from the product discharge pipe 411 sequentially enters the process gas condenser / separator, the tail gas flow meter, the liquid collection and metering device, the solid sampling device, and the process gas analysis device to achieve gas-liquid separation of the process gas and to sample and analyze the product, while also analyzing the carbon deposition on the catalyst.

[0148] The connecting pipe 70 can be a pipe extending in a horizontal direction. The inlet of the first end of the connecting pipe 70 is connected to the outlet of the regulating element, and the outlet of the second end of the connecting pipe 70 is connected to the stripping and settling section 41 above the post-reaction unit 40, so that the material mixture after the reaction in the main reaction unit 30 is transported to the stripping and settling section 41 through the connecting pipe 70.

[0149] The stripping main section 43 is purged to separate the reaction products from the catalyst.

[0150] In one possible implementation, the post-reaction unit 40 further includes a stripping variable diameter section 42, which connects the stripping settling section 41 and the stripping main section 43, and whose inner diameter gradually decreases from the stripping settling section 41 to the stripping main section 43. The stripping variable diameter section 42 is at least partially conical in shape, which helps to reduce catalyst particle accumulation and improve flowability.

[0151] The stripping settling section 41, the stripping diameter changing section 42, the stripping main section 43, and the stripping riser 44 are connected vertically in sequence. Heating elements are also installed on the outside of the stripping settling section 41, the stripping diameter changing section 42, the stripping main section 43, and the stripping riser 44. These heating elements generate heat to ensure that the operating temperature of the stripping settling section 41, the stripping diameter changing section 42, the stripping main section 43, and the stripping riser 44 is suitable.

[0152] In one possible implementation, the reaction unit 30, the post-reaction unit 40, and the regeneration unit 80 are arranged side by side. The reaction unit 30, the post-reaction unit 40, and the regeneration unit 80 can be arranged side by side in a horizontal direction, which helps to improve the compactness of the circulating fluidized bed device.

[0153] In one possible implementation, the post-reaction unit 40 and the regeneration unit 80 are connected by a pre-generation tube 50 and a pre-generation agent boosting unit 60 connected in sequence.

[0154] In one possible implementation, the regenerator lifting unit 60 includes a regenerator lifting pipe 61, a regenerator lifting air duct 62, and a regenerator pre-lifter 63. One end of the regenerator lifting pipe 61 is connected to the regeneration unit 80, and the regenerator pre-lifter 63 is disposed between the other end of the regenerator lifting pipe 61 and the regenerator lifting air duct 62. The regenerator pipe 50 is connected between the regenerator pre-lifter 63 and the plug valve 46.

[0155] The pre-regeneration unit 60 lifts the pre-regeneration agent from a low position to the inlet of the regeneration unit 80 by lifting air, which increases the driving force for regeneration and enables the catalyst to be successfully circulated.

[0156] In one possible implementation (not shown in the figure), the feedstock riser 61 has a sleeve-type structure. The feedstock riser 61 contains a third porous media tube, which can reduce the wall effect of the dense-phase catalyst during the rise process and prevent catalyst degassing. The third porous media tube contains multiple third through-holes, which can be downwardly inclined or bent. When the third through-hole is downwardly inclined, it prevents the catalyst from entering the through-hole; when the third through-hole is bent, it reduces the flow resistance of the riser gas.

[0157] The inlet of the regeneration tube 50 is connected to the blocking valve 46; the outlet of the regeneration tube 50 is connected to the regeneration agent pre-lifter 63; the inlet of the regeneration agent lift tube 61 is connected to the regeneration agent pre-lifter 63; and the outlet of the regeneration agent lift tube 61 is connected to the inlet at the top of the regeneration unit 80.

[0158] The waiting tube 50 is inclined, and the material is inclined downward from the waiting valve 46 to the waiting agent pre-elevator 63, which helps the material to pass smoothly through the waiting tube 50 and enter the waiting agent pre-elevator 63.

[0159] The catalyst separated in the post-reaction unit 40 enters the pre-regenerator riser 61 through the pre-regenerator tube 50 and finally enters the regeneration unit 80.

[0160] In one possible implementation, the regeneration unit 80 includes a regeneration settling section 81, a regeneration main pipe section 83, and a regeneration riser 84 connected in sequence. The regeneration settling section 81 has a regeneration flue gas pipe 811 and is connected to the regenerator riser pipe 61.

[0161] The regeneration riser 84 is connected to the regeneration air supply pipe 86, and a re-plug valve 85 is installed at the connection point between the regeneration riser 84 and the regeneration air supply pipe 86. The two ends of the regeneration inclined pipe 90 are connected to the re-plug valve 85 and the pre-lift unit 20, respectively. The re-plug valve 85 is used to control the flow rate of the catalyst entering the regeneration inclined pipe 90 for secondary circulation.

[0162] The inlet at one end of the regeneration inclined tube 90 is connected to the re-plug valve 85, and the outlet at the other end of the regeneration inclined tube 90 is connected to the pre-lifting unit 20.

[0163] The regeneration flue gas pipe 811 can be connected to the top of the regeneration settling section 81, and the regeneration flue gas pipe 811 is used to discharge flue gas.

[0164] Downstream of the regenerated flue gas pipe 811 are sequentially connected a flue gas condenser separator, a tail gas flow meter, a liquid collection and metering device, a solid sampling device, and a flue gas analysis device. After leaving the regenerated flue gas pipe 811, the flue gas sequentially enters the flue gas condenser separator, the tail gas flow meter, the liquid collection and metering device, the solid sampling device, and the flue gas analysis device to achieve gas-liquid separation of the flue gas and to sample and analyze the flue gas, while also analyzing the carbon deposition of the catalyst. The material balance can be calculated based on the composition and flow rate of the process gas, liquid, and flue gas.

[0165] The regeneration inclined tube 90 is inclined, and from the re-plug valve 85 to the pre-lifting unit 20, the regeneration inclined tube 90 is inclined downward, which helps the material to smoothly enter the pre-lifting unit 20 through the regeneration inclined tube 90.

[0166] Considering that the catalyst surface used in the circulating fluidized bed device is prone to coking and its activity decreases rapidly, it is necessary to continuously regenerate the catalyst by burning coke. Therefore, this application sets up a regeneration unit 80 to regenerate the catalyst by burning coke, so that the catalyst can be restored to its activity, realize the recycling of the catalyst, and ensure the continuous progress of the catalytic dehydrogenation reaction.

[0167] In one possible implementation, the regeneration unit 80 further includes a regeneration variable diameter section 82 connected between the regeneration settling section 81 and the regeneration main pipe section 83. From the regeneration settling section 81 to the regeneration main pipe section 83, the inner diameter of at least a portion of the regeneration variable diameter section 82 gradually decreases, and at least a portion of the regeneration variable diameter section 82 is conical in shape, which helps to facilitate a smooth transition between high and low gas velocities, avoids catalyst particle accumulation and dead zones, and improves flowability.

[0168] The regenerated settlement section 81, the regenerated variable diameter section 82, the regenerated main pipe section 83, and the regenerated riser 84 are connected vertically in sequence.

[0169] The regeneration settling section 81, the regeneration variable diameter section 82, the regeneration main pipe section 83, and the regeneration riser 84 are all equipped with heating elements on their exteriors. These heating elements are used to generate heat, ensuring that the temperature of the catalyst coking regeneration is suitable and providing heat for the catalyst coking regeneration.

[0170] The regeneration unit 80 can also perform gas stripping on the catalyst, replacing the oxygen or water vapor trapped in the catalyst voids and channels to meet the special requirements of some reactions for oxygen and water content.

[0171] In one possible implementation, the circulating fluidized bed apparatus provided by the present invention further includes a raw material conveying unit 10, which is connected to the bottom of the pre-lifting unit 20. The raw material conveying unit 10 is used to convey reaction raw materials to the pre-lifting unit 20.

[0172] In one possible implementation method, refer to Figure 7 and Figure 8 As shown, along the axial direction of the regeneration inclined tube 90, the regeneration inclined tube 90 includes at least one pipe connection unit 91 arranged at intervals. The pipe connection unit 91 includes an outer tube 911 and an inner tube 912 sleeved inside the outer tube 911. That is, the pipe connection unit 91 has a sleeve structure, and the cavity inside the inner tube 912 is the catalyst flow region.

[0173] In one possible implementation, the regeneration inclined tube 90 includes two or more pipe connection units 91 connected in sequence, the number of which is not specifically limited here.

[0174] A cavity 913 is formed between the outer tube 911 and the inner tube 912. The inner tube 912 has an inner cavity 915. The sidewall of the outer tube 911 is connected to a plurality of outer tubes 92. The outer tubes 92 are used to deliver gas into the cavity 913. Along the circumference of the inner tube 912, at least a portion of the sidewall of the inner tube 912 is a second porous medium tube with a plurality of second through holes 914. The second through holes 914 connect the inner cavity 915 and the cavity 913.

[0175] The external pipe 92 can be used to introduce high-pressure inert gas into the cavity 913. The inert gas entering the cavity 913 enters the inner cavity 915 through the second through hole 914.

[0176] In one possible implementation, the outer tube 911 and the inner tube 912 are connected by a second support 916, which supports the inner tube 912, improves the stability of the inner tube 912, and avoids resonance. The second support 916 does not block the gas in the cavity 913, allowing the gas to flow axially along the pipe connection unit 91 within the cavity 913.

[0177] In one possible implementation, a pipe connection unit 91 is installed every 2m to 3m along the axial direction of the regeneration inclined tube 90, and the length of the pipe connection unit 91 can be 100mm to 500mm. For example, a pipe connection unit 91 can be installed every 2m, 2.5m or 3m along the axial direction of the regeneration inclined tube 90, and the length of the pipe connection unit 91 can be 100mm, 200mm, 280mm, 300mm, 400mm or 500mm.

[0178] In one possible implementation, since the solids or particles within the regeneration inclined tube 90 mostly flow through a semi-tube, the sidewall of a portion of the inner tube 912 can be a second porous media tube with multiple second through-holes 914. (Reference) Figure 8As shown, in this example, the inner tube 912 includes a first half tube 9121 and a second half tube 9122. The first half tube 9121 and the second half tube 9122 are spliced ​​together along the circumference of the inner tube 912. The first half tube 9121 is a second porous medium tube with multiple second through holes 914. The first half tube 9121 is located on the side closer to the ground. The tube wall of the second half tube 9122 is a solid tube wall. The second half tube 9122 is located on the side away from the ground.

[0179] Since the solids or particles inside the regeneration inclined tube 90 mostly flow through a half-tube, the outer tube 92 can be provided only on the side wall of the outer tube 911 facing the first half-tube 9121. Of course, the outer tube 92 can also be provided on the side wall of the outer tube 911 facing the second half-tube 9122, which helps to improve the airflow circulation effect in the cavitation cavity 913.

[0180] In another possible implementation, the entire sidewall of the inner tube 912 is a second porous media tube with multiple second through holes 914. The inner tube 912 is a complete porous media tube.

[0181] In another possible implementation, the inner diameter of the outer tube 911 is 1 mm to 6 mm, for example, the inner diameter of the outer tube 911 is 1 mm, 2 mm, 3 mm, 4 mm, 5 mm or 6 mm.

[0182] Along the axial direction of the outer tube 911, multiple sets of outer tubes 92 are connected at intervals to the sidewalls of the outer tube 911. Each set of outer tubes 92 includes 3 to 6 outer tubes 92 arranged circumferentially along the outer tube 911. The number of outer tubes 92 in each set can be the same or different. This structure helps to improve the uniformity of the gas blown into the second porous medium tube through the outer tubes 92 and improves the flowability of solid particles in the inner tube 912.

[0183] In one possible implementation, the second via 914 is sloping downwards. The two ends of the second via 914 penetrate the inner wall surface and the outer wall surface of the inner tube 912, respectively.

[0184] In one possible implementation, the diameter of the second via 914 is 3μm to 50μm, the angle between the extension direction of the second via 914 and the axial direction of the inner tube 912 is 30° to 60°, and the opening ratio of the second via 914 on the inner tube 912 is 5% to 25%.

[0185] In this application, references Figure 9 As shown, part of the sidewall of the inner tube 912 is a second porous medium tube with multiple second through holes 914. When the second porous medium tube is inclined downward, the catalyst can be prevented from entering the second through holes 914.

[0186] In one possible implementation, since propane dehydrogenation is an endothermic reaction, and the regeneration inclined tube 90 in the laboratory cannot provide heat, it is often necessary to heat the sidewalls of the regeneration inclined tube 90 to achieve heat balance. In this application, the second porous media tube is a metal tube and is configured to generate heat when energized. When the second porous media tube is energized, heat can be generated by the resistance of the second porous media tube itself to provide the heat required for the propane dehydrogenation reaction and maintain the heat balance of the reaction. In one possible implementation, the resistance value can be changed by replacing the second porous media tube with one of different metal materials to provide the heat required for different reaction heat effects and to maintain the temperature of the regenerated catalyst.

[0187] In one possible implementation, the riser reactor 31 or the feedstock riser 61 is a sleeve structure. The sleeve structure of the feedstock riser 61 is consistent with the sleeve structure of the riser reactor 31, but the pipe diameter is different, which will not be described in detail here.

[0188] refer to Figure 2 and Figure 7 As shown, this application considers the poor catalyst flow within the regenerated inclined tube 90. When the regenerated inclined tube 90 is too thick, the catalyst flows in a semi-pipe manner, which easily leads to accumulation. In hot experimental setups, the inner diameter of the regenerated inclined tube 90 is often too small, resulting in low delivery rates and making it impossible to add loosening points. Therefore, this application improves the catalyst flow within the regenerated inclined tube 90 by providing at least one pipe connection unit 91 at intervals on the regenerated inclined tube 90. The pipe connection unit 91 includes an outer tube 911 and an inner tube 912 sleeved inside the outer tube 911. Along the circumference of the inner tube 912, at least a portion of the sidewall of the inner tube 912 is a second porous medium tube with multiple second through holes 914. This improves the catalyst flow within the regenerated inclined tube 90, reduces problems such as catalyst adhesion and accumulation within the regenerated inclined tube 90, and ensures experimental results.

[0189] In this application, part of the sidewall of the inner tube 912 inside the regenerated inclined tube 90 is a second porous medium tube with multiple second through holes 914. The high-pressure inert gas delivered to the cavity 913 through the outer tube 92 can cause disturbance at the bottom of the catalyst inside the inner tube 912 after the second through holes 914 are opened on the inner tube 912. This makes it difficult for the catalyst flowing in the half-tube to accumulate on the inner wall of the inner tube 912, and it can also blow away the catalyst particles to prevent the accumulation of particulate matter and promote the flow of particulate matter inside the inner tube 912.

[0190] The aforementioned detachable connection can be made via flange structure 34.

[0191] The aforementioned waiting agent is the waiting catalyst.

[0192] This invention provides a circulating fluidized bed device in which material moves from the inlet of the riser reactor 31 to the inlet of the post-reaction unit 40, i.e., the material enters the stripping and settling section 41. The oil-agent contact time between the material and the material can be controlled within the range of 0.3s to 8.5s, which can effectively increase the adjustable range of the oil-agent contact time. Overall, the controllable range of propane dehydrogenation conversion rate is 5% to 45%, and the controllable range of propylene selectivity is 70% to 95%.

[0193] The raw material conveying unit 10 includes a raw material conveying pipe that passes through the inlet of the pre-lifting unit 20 from bottom to top and extends into the interior of the pre-lifting unit 20; the outlet of the pre-lifting unit 20 is connected to the inlet of the riser reactor 31; the outlet of the riser reactor 31 is detachably connected to the inlet of the riser replacement section 33, or the outlet of the riser reactor 31 is connected to the inlet of the turbulent bed reactor 32.

[0194] During operation, the catalyst enters the pre-lifting unit 20 through the regeneration inclined tube 90. Simultaneously, the material conveyed from the raw material conveying unit 10 reacts after contacting the catalyst in the riser reactor 31. The mixture of reaction products, materials, and catalyst enters the stripping settling section 41 through the connecting pipe 70 for gas-solid separation. The gaseous products and materials after the reaction are discharged through the product discharge pipe 411, while the solid catalyst falls downward into the stripping main section 43. In the stripping main section 43, it encounters the gaseous medium (such as nitrogen or air) simultaneously conveyed upward from the stripping gas pipe 45 to the stripping riser 44, achieving purging separation. The catalyst finally moves downward, passing through the stripping riser 44 and the waiting tube 50 into the waiting agent pre-lifter 63. When the pre-lifter 63 is activated, the catalyst is blown through the pre-lifter pipe 61 to the regeneration settling section 81 for gas-solid separation. At the same time, the regeneration air delivery pipe 86 delivers regeneration air (such as carbon dioxide, water vapor, etc.) upward. The nozzles in the regeneration riser 84 spray oil droplets into the regeneration riser 84. Under the action of the regeneration air, the oil droplets are fluidized and move upward in the opposite direction to contact the catalyst, thereby realizing the coking regeneration of the catalyst. The coking flue gas carries a small amount of catalyst upward into the regeneration settling section 81 for gas-solid separation. The flue gas is discharged from the regeneration flue gas pipe 811. The regenerated catalyst after coking flows downward and is delivered to the pre-lifter unit 20 through the regeneration inclined pipe 90. This realizes continuous catalyst regeneration and long-cycle operation, which is suitable for continuous production.

[0195] When the regulating component includes the riser replacement section 33, the circulating fluidized bed device provided by the present invention can be used alone as a single riser reactor. When used alone as a single riser reactor, the controllable range of propane dehydrogenation conversion rate is 5% to 35%, and the controllable range of propylene selectivity generated from propane dehydrogenation is 75% to 95%.

[0196] When the regulating component includes a turbulent bed reactor 32, the circulating fluidized bed device provided by the present invention can be used as a turbulent-riseer coupled bed. When used as a riser-turbulent bed coupled reactor, the controllable range of propane dehydrogenation conversion is 15% to 45%, and the controllable range of propylene selectivity generated from propane dehydrogenation is 70% to 90%. Compared to using it alone as a single riser reactor, the propane dehydrogenation conversion is improved, and the propylene selectivity is reduced.

[0197] Therefore, this application allows for flexible selection of adjustment components according to production needs, enabling it to be used as a single riser reactor to achieve a high controllable range of propylene selectivity; it also enables it to be used as a turbulent-riser coupled bed, thereby improving propane dehydrogenation conversion.

[0198] The circulating fluidized bed device provided by this invention is a vertical circulating fluidized bed. Before production, appropriate adjustment components can be selected and installed according to the usage requirements. The adjustment components can be the riser replacement section 33 or the turbulent bed reactor 32 to complete different types of chemical reactions, thus broadening the application range of the circulating fluidized bed device.

[0199] The circulating fluidized bed device provided by this invention is a vertical circulating fluidized bed, and the flow state is a conveying bed or a turbulent-conveyor coupled bed. The gas-solid contact time can be long or short, and it is applicable to a wide range of reactions. It can effectively increase the adjustable range of oil-agent contact time and accurately match the oil-agent contact time required by different reaction systems.

[0200] The circulating fluidized bed device provided by this invention effectively solves the technical defects of existing circulating fluidized bed reactors, such as strong wall effect, poor flow in inclined tubes, narrow operating gas velocity range, and poor gas-solid contact effect in turbulent beds. It accurately reproduces the gas-solid flow of industrial fluidized bed reactors and can significantly broaden the oil-agent contact time range of fluidized bed reactors to adapt to the reaction environment required by different catalyst systems. At the same time, it has the advantages of low modification and operating costs.

[0201] In the description of this invention, it should be understood that the terms "center," "length," "width," "thickness," "top," "bottom," "upper," "lower," "left," "right," "front," "rear," "vertical," "horizontal," "inner," "outer," "axial," and "circumferential," etc., used to indicate orientation or positional relationships are based on the orientation or positional relationships shown in the accompanying drawings and are only for the convenience of describing this invention and simplifying the description, and are not intended to indicate or imply that the indicated position or component must have a specific orientation, or a specific structure and operation, and therefore should not be construed as a limitation of this invention.

[0202] Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of this invention, "a plurality of" means at least two, such as two, three, etc., unless otherwise explicitly specified.

[0203] In this invention, unless otherwise explicitly specified and limited, the terms "installation," "connection," "linking," and "fixing," etc., should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral part; they can refer to a mechanical connection, an electrical connection, or a connection that allows communication between them; they can refer to a direct connection or an indirect connection through an intermediate medium; they can refer to the internal communication of two components or the interaction between two components. Those skilled in the art can understand the specific meaning of the above terms in this invention according to the specific circumstances.

[0204] In this invention, unless otherwise explicitly specified and limited, "above" or "below" the second feature can include direct contact between the first and second features, or contact between the first and second features through another feature between them. Furthermore, "above," "over," and "on top" of the second feature includes the first feature directly above or diagonally above the second feature, or simply indicates that the first feature is at a higher horizontal level than the second feature. "Below," "below," and "under" the second feature includes the first feature directly below or diagonally below the second feature, or simply indicates that the first feature is at a lower horizontal level than the second feature.

[0205] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, and not to limit them; although the present invention has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some or all of the technical features; and these modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of the present invention.

Claims

1. A circulating fluidized bed device, characterized in that, include: The pre-lifting unit (20), the main reaction unit (30), the post-reaction unit (40), and the regeneration unit (80) are connected in sequence, and the regeneration unit (80) is connected to the pre-lifting unit (20) through a regeneration inclined tube (90). The main reaction unit (30) includes a riser reactor (31) and an adjusting member detachably connected to the riser reactor (31). The adjusting member is connected between the riser reactor (31) and the post-reaction unit (40). At least part of the riser reactor (31) is a sleeve structure, which includes an outer tube (311) and an inner tube (312) sleeved inside the outer tube (311). There is an annular space (313) between the outer tube (311) and the inner tube (312). The outer tube (311) is connected to a plurality of gas supply pipes (314). The inner tube (312) is a first porous medium tube with a plurality of first through holes (315). The inner tube (312) has a reaction chamber (316) inside. The first through holes (315) connect the annular space (313) and the reaction chamber (316). The first porous medium tube is a metal tube and is configured to generate heat when energized.

2. The circulating fluidized bed device according to claim 1, characterized in that, Along the axial direction of the regeneration inclined tube (90), the regeneration inclined tube (90) includes at least one pipe connection unit (91) spaced apart. The pipe connection unit (91) includes an outer tube (911) and an inner tube (912) sleeved inside the outer tube (911). A void cavity (913) is formed between the outer tube (911) and the inner tube (912). The inner tube (912) has an inner cavity (915). An outer pipe (92) is connected to the side wall of the outer tube (911). The outer pipe (92) is used to deliver gas into the void cavity (913). Along the circumference of the inner tube (912), at least a portion of the sidewall of the inner tube (912) is a second porous medium tube having a plurality of second through holes (914), the second through holes (914) connecting the inner cavity (915) and the void cavity (913), the second porous medium tube being a metal tube and configured to generate heat when energized.

3. The circulating fluidized bed device according to claim 1, characterized in that, The first through hole (315) includes a first downward inclined section (3151), the two ends of which penetrate the inner wall and outer wall of the inner tube (312), respectively. Along the height direction of the inner tube (312), the height of the first downward inclined section (3151) at one end on the inner wall of the inner tube (312) is lower than the height of the first downward inclined section (3151) at one end on the outer wall of the inner tube (312); or, The first through hole (315) includes a second downward inclined section (3152) and a bent section (3153) that are interconnected. One end of the second downward inclined section (3152) penetrates the outer wall of the inner tube (312), and the other end of the second downward inclined section (3152) is connected to one end of the bent section (3153). The other end of the bent section (3153) penetrates the inner wall of the inner tube (312).

4. The circulating fluidized bed device according to claim 2, characterized in that, The opening ratio of the first through hole (315) opened on the inner tube (312) is 5% to 25%; and / or, The aperture of the first via (315) is 3μm to 50μm; and / or, The opening ratio of the second through hole (914) opened on the inner tube (912) is 5% to 25%; and / or, The aperture of the second via (914) is 3μm to 50μm; and / or, The circulating fluidized bed device also includes a raw material conveying unit (10), which is connected to the bottom of the pre-lifting unit (20).

5. The circulating fluidized bed apparatus according to any one of claims 1-4, characterized in that, The regulating component includes a riser replacement section (33), which is detachably connected between the riser reactor (31) and the post-reaction unit (40); or, The regulating component includes a turbulent bed reactor (32), which is detachably connected between the riser reactor (31) and the post-reaction unit (40).

6. The circulating fluidized bed apparatus according to claim 5, characterized in that, The turbulent bed reactor (32) includes a main body (321), a variable diameter adjustment section (322), and at least one auxiliary fluidizing nozzle (323). The variable diameter adjustment section (322) and the main body (321) are detachably connected, and the main body (321) is detachably connected to the post-reaction unit (40). The variable diameter adjustment section (322) is detachably connected to the riser reactor (31). The inner diameter of at least a portion of the variable diameter adjustment section (322) gradually increases from the riser reactor (31) to the main body (321). The auxiliary fluidizing nozzle (323) extends obliquely from the outside of the variable diameter adjustment section (322) to the inside of the variable diameter adjustment section (322), and the angle between the central axis of the auxiliary fluidizing nozzle (323) and the central axis of the variable diameter adjustment section (322) is 30° to 60°.

7. The circulating fluidized bed apparatus according to claim 5, characterized in that, The post-reaction unit (40) includes a stripping settling section (41), a stripping main section (43), and a stripping riser (44) connected in sequence. The stripping settling section (41) is connected to the regulating component through a connecting pipe (70), and the stripping settling section (41) has a product discharge pipe (411). The stripping riser (44) is connected to a stripping gas pipe (45), and a plugging valve (46) is provided at the connection position between the stripping riser (44) and the stripping gas pipe (45). The post-reaction unit (40) further includes a stripping variable diameter section (42), which is connected between the stripping settling section (41) and the stripping main section (43), and the inner diameter of at least part of the stripping variable diameter section (42) gradually decreases from the stripping settling section (41) to the stripping main section (43).

8. The circulating fluidized bed apparatus according to claim 7, characterized in that, The reaction unit (30), the post-reaction unit (40), and the regeneration unit (80) are arranged side by side; The post-reaction unit (40) and the regeneration unit (80) are connected by a pre-generation tube (50) and a pre-generation agent boosting unit (60) connected in sequence.

9. The circulating fluidized bed apparatus according to claim 8, characterized in that, The regenerator lifting unit (60) includes a regenerator lifting pipe (61), a regenerator lifting air duct (62), and a regenerator pre-lifter (63). One end of the regenerator lifting pipe (61) is connected to the regeneration unit (80). The regenerator pre-lifter (63) is disposed between the other end of the regenerator lifting pipe (61) and the regenerator lifting air duct (62). The regenerator pipe (50) is connected between the regenerator pre-lifter (63) and the plug valve (46). The acclimation agent riser tube (61) is a sleeve-type structure.

10. The circulating fluidized bed apparatus according to claim 9, characterized in that, The regeneration unit (80) includes a regeneration settling section (81), a regeneration main pipe section (83) and a regeneration riser (84) connected in sequence. The regeneration settling section (81) has a regeneration flue gas pipe (811) and is connected to the regenerator riser pipe (61). The regeneration riser (84) is connected to the regeneration air delivery pipe (86), and a re-plug valve (85) is provided at the connection position between the regeneration riser (84) and the regeneration air delivery pipe (86). The two ends of the regeneration inclined pipe (90) are respectively connected to the re-plug valve (85) and the pre-lifting unit (20). The regeneration unit (80) further includes a regeneration variable diameter section (82), which is connected between the regeneration settling section (81) and the regeneration main pipe section (83), and the inner diameter of at least a portion of the regeneration variable diameter section (82) gradually decreases from the regeneration settling section (81) to the regeneration main pipe section (83).

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