Moving bed-fluidized bed reaction regeneration coupling device and use method thereof

Abstract

The invention relates to a moving bed-fluidized bed reaction regeneration coupling device and a use method thereof. The device comprises a material heating system; the reaction system comprises a moving bed reactor, and is used for reacting a gas-phase raw material and a solid-phase catalyst and enhancing the axial flow of the solid-phase catalyst; the auxiliary fluidization system is communicated with a spent catalyst outlet of the moving bed reactor, and the auxiliary fluidization system is used for mixing a fluidization aid and a spent catalyst so as to improve the fluidization performance of the spent catalyst; the regeneration system is used for coking the to-be-regenerated catalyst and comprises a fluidized bed regenerator; and the gas-solid separation system is communicated with the outlet of the fluidized bed regenerator, is used for separating the regenerated catalyst and the fluidizing aid, and is used for conveying the regenerated catalyst to the moving bed reactor and conveying the fluidizing aid to the auxiliary fluidizing system. By introducing the auxiliary fluidization system and the gas-solid separation system, the moving bed and the fluidized bed are efficiently coupled, so that the efficient performance of the catalyst in the reaction is ensured, and efficient fluidization coke-burning regeneration is realized.

Description

Technical Field

[0001] The present invention relates to the technical field of gas-solid catalytic reaction regeneration devices, and particularly relates to a moving bed-fluidized bed reaction regeneration coupling device and a using method thereof. Background Art

[0002] As a key basic chemical raw material, the demand for propylene has been increasing year by year. The propane catalytic dehydrogenation process to produce propylene has occupied an important position in the field of propylene production due to its characteristics such as single raw material and high propylene yield, and it is now one of the main methods for propylene production. The reaction regeneration system of propane catalytic dehydrogenation is the core process of the whole propane catalytic dehydrogenation process. The optimized design of the reaction regeneration system can not only improve the conversion rate and selectivity of the reaction process, but also reduce the construction cost and operation cost of the device.

[0003] At present, the commercially available propane catalytic dehydrogenation process mainly adopts the Catofin process or the Oleflex process, and the Cr-based or Pt-based catalysts used both face relatively serious carbon deposition problems. The reactors used in these two processes are fixed bed or moving bed reactors respectively. In these two reactors, the catalyst needs to undergo a long-time catalytic reaction in each regeneration cycle, resulting in serious carbon deposition on the catalyst. Patent ZL202011401309.3 proposes a moving bed reactor for propane dehydrogenation reaction and the regeneration of the spent catalyst obtained after the reaction. Patent ZL202211333011.2 proposes a new type of moving bed regenerator for activating the reduced catalyst. However, in the above-mentioned disclosed patents and existing technologies, since many existing catalysts and new catalysts are difficult to be made into microspheres (Φ60 - 100 μm), because the catalysts formed at this particle size often have poor activity and it is difficult to balance activity, particle size and abrasion resistance, etc. Therefore, many catalysts are difficult to fluidize, and thus cannot be subjected to fluidized bed carbon burning regeneration. So the type of regenerator often has the same form as the reactor type, still adopting a fixed bed or a moving bed. However, the positions of the catalyst particles in the fixed bed or moving bed regenerator are relatively fixed, the catalyst carbon burning is not thorough, the combustion heat is difficult to be removed in time, local hot spots are easily generated, and its combustion mode is not conducive to the regeneration of the catalyst. Moreover, the regeneration equipment is relatively complex and the operation is more cumbersome, which is not conducive to continuous and stable production.

[0004] The reaction environment required for propane catalytic dehydrogenation is characterized by high temperature and short gas-solid contact time, which brings high conversion rate while taking into account high selectivity. Patent ZL202210412935.5 and ZL202210412951.4 both introduce a radial moving bed reactor with downward inlet and upward outlet to overcome the disadvantages such as fluidization of the catalyst bed layer due to the influence of the reaction gas flow in the prior art and to avoid the expensive catalyst being carried out by the reaction medium. However, in the above-mentioned disclosed patents and the existing technologies, the structure of the moving bed reactor is single, mostly single-stage reactors. When the reactors are connected in series or parallel, the structure is complex, and it is difficult to achieve efficient gas-solid contact when matching different catalysts. The overall integration degree is low and the construction cost is high.

[0005] Therefore, based on the experience and practice of being engaged in the relevant industry for many years, the inventor of the present invention proposes a moving bed-fluidized bed reaction regeneration coupling device and its process method to overcome the defects of the prior art. Summary of the Invention

[0006] The purpose of the present invention is to provide a moving bed-fluidized bed reaction regeneration coupling device and its usage method, to solve the technical problems of the complex structure of the existing moving bed supporting regenerator, low heat and mass transfer efficiency, and difficult fluidization of the catalyst. By introducing an auxiliary fluidization system and a gas-solid separation system, the moving bed and the fluidized bed are efficiently coupled, which not only ensures the high efficiency of the catalyst in the propane dehydrogenation reaction, but also realizes efficient fluidized bed coking regeneration.

[0007] The purpose of the present invention is achieved as follows. A moving bed-fluidized bed reaction regeneration coupling device includes:

[0008] A material heating system for exchanging the heat of the gas-phase product and the gas-phase raw material to heat the gas-phase raw material;

[0009] A reaction system including a moving bed reactor communicated with the material heating system, the moving bed reactor being used for the reaction of the gas-phase raw material and the solid-phase catalyst and capable of strengthening the axial flow of the solid-phase catalyst;

[0010] An auxiliary fluidization system communicated with the spent catalyst outlet of the moving bed reactor, the auxiliary fluidization system mixing the fluidization aid and the spent catalyst to improve the fluidization performance of the spent catalyst;

[0011] A regeneration system for coking and regenerating the spent catalyst to form a regenerated catalyst, including a fluidized bed regenerator communicated with the outlet of the auxiliary fluidization system;

[0012] A gas-solid separation system communicated with the outlet of the fluidized bed regenerator, the gas-solid separation system separating the regenerated catalyst and the fluidization aid, and transporting the regenerated catalyst to the moving bed reactor and transporting the fluidization aid to the auxiliary fluidization system.

[0013] In a preferred embodiment of the present invention, the auxiliary fluidization system includes a particle mixer, and a catalyst inlet, a fluidization aid inlet and a mixture outlet are arranged on the particle mixer; the catalyst inlet is communicated with the spent catalyst outlet of the moving bed reactor, and the catalyst inlet is used for conveying the spent catalyst from the moving bed reactor into the particle mixer; the fluidization aid inlet is used for conveying the fluidization aid into the particle mixer; the mixture outlet is communicated with the fluidized bed regenerator;

[0014] The particle density of the fluidization aid is 1000-3000 kg / m 3 , the particle diameter of the fluidization aid is Φ30 μm-Φ1000 μm, and the mixing ratio of the fluidization aid to the spent catalyst is 0.05-1.5:1.

[0015] In a preferred embodiment of the present invention, the moving bed reactor includes a plurality of serially connected conical moving bed reactors. Each conical moving bed reactor includes a first outer shell, and a first inner layer Johnson screen with a diameter gradually decreasing from top to bottom is arranged inside the first outer shell. A first central cavity is formed inside the radial direction of the first inner layer Johnson screen; an upper and lower equal-diameter first outer layer Johnson screen is coaxially sleeved outside the first inner layer Johnson screen, and a first outer ring gap space is formed by a radial interval between the first outer layer Johnson screen and the first outer shell; a first inner ring gap space with a cross-sectional area gradually increasing from top to bottom is formed between the first inner layer Johnson screen and the first outer layer Johnson screen, and solid-phase catalyst is allowed to flow from top to bottom under the action of gravity in the first inner ring gap space;

[0016] A regenerated catalyst inlet is arranged at the top end of the first outer shell, and the spent catalyst outlet is arranged at the bottom end of the first outer shell; a gas-phase raw material inlet is arranged at the lower part of the side wall of the first outer shell, and a gas-phase outlet is arranged at the upper part of the side wall of the first outer shell; the gas-phase raw material enters the first outer shell through the gas-phase raw material inlet and diffuses radially along the first outer shell. The gas-phase raw material is in countercurrent contact with the solid-phase catalyst in the first inner ring gap space and reacts to generate a gas-phase product, and the gas-phase product is output outward through the gas-phase outlet;

[0017] The cone angle range of the first inner layer Johnson screen is 1°-10°.

[0018] In a preferred embodiment of the present invention, the moving bed reactor includes 4 conical moving bed reactors, which are sequentially set as the fourth conical moving bed reactor, the third conical moving bed reactor, the second conical moving bed reactor, and the first conical moving bed reactor along the gas-phase raw material flow direction;

[0019] The gas-phase raw material inlet of the fourth conical moving bed reactor is communicated with the material heating system. The gas-phase outlet of the fourth conical moving bed reactor is communicated with the gas-phase raw material inlet of the third conical moving bed reactor. The gas-phase outlet of the third conical moving bed reactor is communicated with the gas-phase raw material inlet of the second conical moving bed reactor. The gas-phase outlet of the second conical moving bed reactor is communicated with the gas-phase raw material inlet of the first conical moving bed reactor. The gas-phase outlet of the first conical moving bed reactor is communicated with the material heating system;

[0020] The regenerated catalyst inlet of the first conical moving bed reactor is communicated with the gas-solid separation system; the spent catalyst outlet of the first conical moving bed reactor is communicated with the regenerated catalyst inlet of the second conical moving bed reactor; the spent catalyst outlet of the second conical moving bed reactor is communicated with the regenerated catalyst inlet of the third conical moving bed reactor through an inter-stage riser; the spent catalyst outlet of the third conical moving bed reactor is communicated with the regenerated catalyst inlet of the fourth conical moving bed reactor; the spent catalyst outlet of the fourth conical moving bed reactor is communicated with the auxiliary fluidization system so that the spent catalyst flows to the auxiliary fluidization system.

[0021] In a preferred embodiment of the present invention, the moving bed reactor is a height-increasing multi-stage moving bed reactor, and the height-increasing multi-stage moving bed reactor includes a plurality of single-stage reactors connected in series, and the heights of the plurality of single-stage reactors are sequentially increased along the gas-phase raw material flow direction.

[0022] In a preferred embodiment of the present invention, the single-stage reactors are sequentially connected up and down to form an integrated structure; each single-stage reactor respectively includes a second outer casing, and a second inner layer Johnson screen with equal diameters up and down is arranged in the second outer casing, and a second central cavity is formed inside the second inner layer Johnson screen in the radial direction; a second outer layer Johnson screen with equal diameters up and down is coaxially sleeved outside the second inner layer Johnson screen, and a second outer ring gap space is formed between the second outer layer Johnson screen and the second outer casing at a radial interval; a second inner ring gap space is formed between the second inner layer Johnson screen and the second outer layer Johnson screen, and solid-phase catalyst is allowed to flow from top to bottom under the action of gravity in the second inner ring gap space, and the second inner ring gap spaces at all levels are in a conducting state, the second outer ring gap spaces at all levels are in a sealed state, and the second central cavities at all levels are in a sealed state;

[0023] A regenerated catalyst inlet is provided at the top of the single-stage reactor located at the top, and a spent catalyst outlet is provided at the bottom of the single-stage reactor located at the bottom; gas-phase raw material inlets are respectively provided at the lower parts of the side walls of each second outer casing, and gas-phase outlets are respectively provided at the upper parts of the side walls of each second outer casing;

[0024] Wherein, the regenerated catalyst inlet is communicated with the gas-solid separation system so that the regenerated catalyst separated by the gas-solid separation system flows to the second inner annulus space; the spent catalyst outlet is communicated with the auxiliary fluidization system so that the spent catalyst flows to the auxiliary fluidization system; each gas-phase raw material inlet is respectively communicated with the material heating system so that the preheated gas-phase raw material flows into each second outer annulus space, the gas-phase raw material diffuses radially along the second outer casing, countercurrently contacts the solid-phase catalyst in the second inner annulus space and reacts to generate a gas-phase product, and the gas-phase product is output outward through the gas-phase outlet.

[0025] In a preferred embodiment of the present invention, the material heating system includes a feed and product heat exchanger and a raw material heating part. The feed and product heat exchanger includes a raw material channel and a product channel. The raw material channel is used for transporting the gas-phase raw material, and the product channel is used for transporting the gas-phase product. The gas-phase product in the product channel exchanges heat with the gas-phase raw material in the raw material channel to heat up the gas-phase raw material;

[0026] The raw material heating part includes an integrated heating unit. The integrated heating unit includes a plurality of groups of heating tubes. Each heating tube respectively passes through a combustion furnace. Each heating tube is arranged corresponding to each single-stage reactor. The inlet of the heating tube communicated with the single-stage reactor located at the bottom is communicated with the outlet of the raw material channel. The gas-phase outlets of each single-stage reactor arranged from bottom to top are respectively communicated with the gas-phase raw material inlets of the single-stage reactor at the upper level above it through a heating tube, and the gas-phase outlet of the single-stage reactor located at the top is communicated with the inlet of the product channel; the tube lengths of the heating tubes corresponding to each single-stage reactor arranged from bottom to top are sequentially shortened.

[0027] In a preferred embodiment of the present invention, two adjacent single-stage reactors are connected by a first flange; a first baffle and a second baffle are provided at the connection of two adjacent single-stage reactors to cause the gas phase to flow in a zigzag manner. The first baffle is arranged in the second outer annulus space, and the second baffle is arranged in the second central cavity;

[0028] Each of the single-stage reactors includes at least two sections of single-stage reaction segments, and two adjacent sections of the single-stage reaction segments are connected by a second flange; a third baffle and a fourth baffle are provided at the connection of two adjacent sections of the single-stage reaction segments to cause the gas phase to flow in a zigzag manner. The third baffle is arranged in the second outer annulus space, and the fourth baffle is arranged in the second central cavity; a gas-phase raw material inlet is arranged at the lower part of the side wall of each single-stage reaction segment, and a gas-phase outlet is arranged at the upper part of the side wall of each single-stage reaction segment.

[0029] The gas-phase raw material inlet of the single-stage reaction segment at the bottom end is communicated with the material heating system, and the gas-phase outlet of the single-stage reaction segment below is communicated with the gas-phase raw material inlet of the adjacent single-stage reaction segment above it through an external connection pipe, and the gas-phase outlet of the single-stage reaction segment at the top end is communicated with the material heating system.

[0030] In a preferred embodiment of the present invention, the gas-solid separation system includes a regenerant separator and a fluidizing aid separator. The inlet of the regenerant separator is communicated with the outlet of the fluidized bed regenerator, the regenerant outlet of the regenerant separator is communicated with the moving bed reactor, the gas-phase outlet of the regenerant separator is communicated with the inlet of the fluidizing aid separator, and the outlet of the fluidizing aid separator is communicated with the fluidizing aid inlet of the particle mixer.

[0031] The object of the present invention can also be achieved in the following way. A use method of the aforementioned moving bed-fluidized bed reaction regeneration coupling device includes:

[0032] The gas-phase material is heated by the material heating system and then introduced into the reaction system. The gas-phase raw material and the solid-phase catalyst are in countercurrent contact and react in the reaction system. The spent catalyst after the reaction flows to the auxiliary fluidization system and is mixed with the input fluidizing aid and then introduced into the regeneration system together. The spent catalyst is subjected to coking regeneration to form a regenerated catalyst; the regenerated catalyst enters the gas-solid separation system. Coarser catalyst particles are separated by the gas-solid separation system and then returned to the reaction system. Finer fluidizing aids are separated by the gas-solid separation system and then enter the auxiliary fluidization system, where they are remixed with the spent catalyst and then enter the regeneration system to enter the next regeneration cycle.

[0033] As described above, the moving bed-fluidized bed reaction regeneration coupling device and its use method of the present invention have the following beneficial effects:

[0034] The present invention solves the problems of conventional reaction regeneration devices, such as difficulty in matching the reaction regeneration requirements of special catalysts, low coking regeneration and gas-solid contact efficiency, complex series-parallel types of reactors, low integration, and high construction costs.

[0035] In the moving bed-fluidized bed reaction regeneration coupling device of the present invention, the reaction system and the regeneration system are efficiently coupled through the auxiliary fluidization system and the gas-solid separation system. The fluidizing agent is mixed with the catalyst to be regenerated that is not easy to fluidize through the auxiliary fluidization system to improve the fluidization performance of the catalyst to be regenerated, so as to achieve efficient fluidized char regeneration of the catalyst, which not only ensures the efficient performance of the catalyst in the propane dehydrogenation reaction, but also achieves efficient fluidized char regeneration; the two types of particles after regeneration are efficiently separated in turn through the gas-solid separation system to avoid the influence of the fluidizing agent on the catalytic reaction process.

[0036] The conical moving bed reactor of the present invention can avoid the phenomenon of solid-phase materials adhering to the wall and blocking holes on the outside of the first inner layer of the Johnson net, or avoid the phenomenon of air pockets, cavities and other unfavorable fluidization phenomena on the inside of the first outer layer of the Johnson net, strengthen the axial flow of the catalyst in the bed, promote the contact between the gas and the catalyst, and improve the reaction efficiency of the catalytic dehydrogenation of propane.

[0037] The highly incremental multi-stage moving bed reactor of the present invention utilizes the characteristics of short gas-solid contact time and low backmixing required in the propane catalytic dehydrogenation process. By setting a baffle, the diffusion reaction time of the gas phase in the solid phase material under the same processing capacity is shortened, and the backmixing is reduced, so that the gas-solid contact is more uniform, and the occurrence of subsequent side reactions is reduced, which is beneficial to improving the selectivity and yield of the product; a highly integrated structure is adopted, and the moving bed reactors of each stage are efficiently connected in series through a special sealing flange. The structure of the bed layer directly connected can reduce the space occupied by the reaction system, and effectively reduce the construction and use costs of the moving bed propane dehydrogenation process.

[0038] The integrated heating unit of the present invention utilizes serpentine heating tubes of different lengths to supplement the different heat required for raw materials in different reaction stages, and more accurately matches the temperature required for the reaction to improve the selectivity and yield of the product.

[0039] The present invention can provide the optimal reaction environment required for propane dehydrogenation under existing or new catalysts, ensure efficient and stable reaction, realize efficient and continuous fluidized coke regeneration, and can effectively reduce the construction and use costs of the process, achieve the purpose of energy saving and consumption reduction, and has a high prospect for industrial promotion. BRIEF DESCRIPTION OF THE DRAWINGS

[0040] The following drawings are only intended to illustrate and explain the present invention, and are not intended to limit the scope of the present invention.

[0041] in:

[0042] Figure 1 It is a schematic diagram of Example 1 of the moving bed-fluidized bed reaction regeneration coupling device of the present invention.

[0043] Figure 2Schematic diagram of Embodiment 2 of the moving bed-fluidized bed reaction regeneration coupling device of the present invention.

[0044] Figure 3 Schematic diagram of the conical moving bed reactor of the present invention.

[0045] Figure 4 Schematic diagram of the single-stage reactor of the present invention.

[0046] In the figure:

[0047] 1. Material heating system; 11. Feed and discharge heat exchanger; 121. First heater; 122. Second heater; 123. Third heater; 124. Fourth heater; 13. Integrated heating unit; 131. First heating tube; 132. Second heating tube; 133. Third heating tube; 134. Fourth heating tube;

[0048] 2. Reaction system;

[0049] 201. Spent catalyst outlet; 202. First central cavity; 203. First outer annulus space; 204. First inner annulus space; 205. Regenerated catalyst inlet; 206. Gas-phase raw material inlet; 207. Gas-phase outlet; 208. Second central cavity; 209. Second outer annulus space; 210. Second inner annulus space;

[0050] 21. Conical moving bed reactor; 2101. First outer shell; 2102. First inner layer Johnson screen; 2103. First outer layer Johnson screen; 211. First conical moving bed reactor; 212. Second conical moving bed reactor; 213. Third conical moving bed reactor; 214. Fourth conical moving bed reactor; 215. Inter-stage riser; 216. Catalyst buffer; 217. Delivery air duct;

[0051] 22. Height-increasing multi-stage moving bed reactor; 220. Single-stage reactor; 2201. Second outer shell; 2202. Second inner layer Johnson screen; 2203. Second outer layer Johnson screen; 2204. Single-stage reaction section; 2205. Second flange; 2206. Third baffle; 2207. Fourth baffle; 2208. Outer connection pipe; 2209. Fifth baffle; 221. First single-stage reactor; 222. Second single-stage reactor; 223. Third single-stage reactor; 224. Fourth single-stage reactor; 225. First flange; 226. First baffle; 227. Second baffle;

[0052] 23. Catalyst feed pipe;

[0053] 3. Auxiliary fluidization system; 31. Particle mixer; 32. Catalyst inlet; 33. Auxiliary fluidizing agent inlet; 34. Mixture outlet; 35. Mixture feed pipe;

[0054] 4. Regeneration system; 40. Fluidized bed regenerator; 41. Main air duct for regeneration; 42. Main air distributor; 43. Loop pipe distributor; 44. Draft tube; 45. Inner circulation pipe for regenerant; 46. Large pore distributor plate; 47. Outlet pipe for regenerant; 48. Flue gas outlet; 49. Combined cyclone separator;

[0055] 5. Gas-solid separation system; 51. Regenerant separator; 52. Fluidizing aid separator;

[0056] 6. Riser. Detailed implementation manners

[0057] For a clearer understanding of the technical features, objectives, and effects of the present invention, the detailed implementation manners of the present invention will now be described with reference to the accompanying drawings.

[0058] The detailed implementation manners of the present invention described herein are only for the purpose of explaining the present invention and should not be construed in any way as a limitation of the present invention. Under the teaching of the present invention, those skilled in the art can conceive any possible variations based on the present invention, and these should all be regarded as belonging to the scope of the present invention. It should be noted that when an element is referred to as being "disposed on" another element, it can be directly on the other element or there can also be an intermediate element. When an element is considered to be "connected" to another element, it can be directly connected to the other element or there may be an intermediate element at the same time. The terms "mounted", "connected", and "coupled" should be understood in a broad sense. For example, it can be a mechanical connection or an electrical connection, or it can be the communication inside two elements. It can be directly connected or indirectly connected through an intermediate medium. For those of ordinary skill in the art, the specific meanings of the above terms can be understood according to specific circumstances. The terms "vertical", "horizontal", "upper", "lower", "left", "right", and similar expressions used herein are only for the purpose of illustration and do not represent the only implementation manner.

[0059] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by those skilled in the technical field to which this application belongs. The terms used herein in the specification of this application are only for the purpose of describing specific implementation manners and are not intended to limit this application. The term "and / or" used herein includes any and all combinations of one or more of the related listed items.

[0060] For catalysts with significant coke formation during the reaction process, which require timely regeneration but are difficult to form into microsphere particles, a reaction-regeneration device that matches them needs to be designed. This device should be able to adapt to the reaction environments required by various catalysts, enabling the catalyst after the moving bed reaction to be efficiently coked and regenerated, achieving continuous and stable production. At the same time, a highly integrated moving bed reaction system is needed to achieve efficient gas-solid contact and effectively reduce construction costs.

[0061] As Figures 1 to 4 shown, the present invention provides a moving bed-fluidized bed reaction-regeneration coupling device, comprising:

[0062] A material heating system 1, which is used to exchange the heat of the gas-phase product and the gas-phase raw material to heat the gas-phase raw material; the material heating system 1 is used to exchange the heat of the gas-phase product and the gas-phase raw material, achieving the effect of cooling the product while heating the raw material, and heating the gas-phase raw material to the temperature required by the reaction system 2.

[0063] A reaction system 2, including a moving bed reactor connected to the material heating system 1. The moving bed reactor is used for the reaction of the gas-phase raw material and the solid-phase catalyst (the gas-phase raw material and the solid-phase catalyst are in countercurrent contact and react), and can strengthen the axial flow of the solid-phase catalyst, having high catalytic reaction performance; the catalyst can be a molecular sieve catalyst, which is composed of a carrier zeolite molecular sieve and an active component metal oxide. The metal oxide can include oxides of a series of metals such as Zn, Co, V, etc.

[0064] An auxiliary fluidization system 3, which is connected to the spent catalyst outlet 201 of the moving bed reactor. The auxiliary fluidization system 3 mixes the fluidization aid and the spent catalyst to improve the fluidization performance of the spent catalyst; the fluidization aid can be quartz sand, which is essentially silicon dioxide and has no reaction activity.

[0065] A regeneration system 4, which is used to carry out coking regeneration on the spent catalyst to form a regenerated catalyst, including a fluidized bed regenerator 40 connected to the outlet of the auxiliary fluidization system 3.

[0066] A gas-solid separation system 5, which is connected to the outlet of the fluidized bed regenerator 40. The gas-solid separation system 5 separates the regenerated catalyst and the fluidization aid, and transports the regenerated catalyst to the moving bed reactor and the fluidization aid to the auxiliary fluidization system 3.

[0067] The reaction system 2 and the regeneration system 4 are arranged in parallel, and the reaction system 2 (moving bed reactor) and the regeneration system 4 (fluidized bed regenerator 40) are efficiently coupled through the auxiliary fluidization system 3 and the gas-solid separation system 5.

[0068] The catalyst after reaction (spent catalyst) is mixed with the auxiliary fluidizing agent in the auxiliary fluidization system 3 to improve the fluidization performance of the spent catalyst. The mixture of the spent catalyst and the auxiliary fluidizing agent is fed into the regeneration system 4 together, and the spent catalyst is coked and regenerated in the regeneration system 4.

[0069] The two kinds of particles after regeneration are efficiently separated in sequence through the gas-solid separation system 5 to avoid the influence of the auxiliary fluidizing agent on the catalytic reaction process.

[0070] The coarser solid-phase catalyst returns to the moving bed reactor after separation, and the finer auxiliary fluidizing agent enters the auxiliary fluidization system 3 after separation, is remixed with the spent catalyst, and then enters the fluidized bed regenerator 40 to achieve circulating flow.

[0071] The present invention solves the problems that the conventional reaction regeneration device is difficult to match the reaction regeneration requirements of the special catalyst, the coking regeneration and the gas-solid contact efficiency are low, the series-parallel type of the reactor is complex, the integration degree is low, and the construction cost is relatively high.

[0072] In the moving bed-fluidized bed reaction regeneration coupling device of the present invention, the reaction system and the regeneration system are efficiently coupled through the auxiliary fluidization system and the gas-solid separation system. The auxiliary fluidizing agent is mixed with the spent catalyst that is not easy to fluidize through the auxiliary fluidization system to improve the fluidization performance of the spent catalyst, so as to achieve efficient fluidized coking regeneration of the catalyst, which not only ensures the high efficiency of the catalyst in the propane dehydrogenation reaction, but also realizes efficient fluidized coking regeneration; the two kinds of particles after regeneration are efficiently separated in sequence through the gas-solid separation system to avoid the influence of the auxiliary fluidizing agent on the catalytic reaction process;

[0073] The present invention can provide the best reaction environment required for propane dehydrogenation under the existing or new catalyst, ensure efficient and stable reaction, while realizing efficient and continuous fluidized coking regeneration, and can effectively reduce the construction and use costs of this process, achieving the purpose of energy conservation and consumption reduction, and having a high industrial promotion prospect.

[0074] Further, as Figure 1 、 Figure 2 shown, the auxiliary fluidization system 3 includes a particle mixer 31. A catalyst inlet 32, an auxiliary fluidizing agent inlet 33 and a mixture outlet 34 are arranged on the particle mixer 31; the catalyst inlet 32 is communicated with the spent catalyst outlet 201 of the moving bed reactor, and the catalyst inlet 32 is used to transport the spent catalyst from the moving bed reactor into the particle mixer 31; the auxiliary fluidizing agent inlet 33 is used to transport the auxiliary fluidizing agent into the particle mixer 31; the mixture outlet 34 is communicated with the fluidized bed regenerator 40 through a mixture discharge pipe 35;

[0075] The particle density of the auxiliary fluidizing agent is 1000 - 3000 kg / m 3, the particle diameter of the fluidization aid is Φ30μm to Φ1000μm, and the mixing ratio of the fluidization aid to the spent catalyst is 0.05 to 1.5:1.

[0076] A fluidization aid with a suitable particle size is input into the particle mixer 31, and the fluidization aid and the spent catalyst are fully mixed, enhancing the fluidization performance of the spent catalyst and achieving efficient fluidization of the spent catalyst.

[0077] Furthermore, as Figure 1 , Figure 2 shown, the gas-solid separation system 5 includes a regenerant separator 51 and a fluidization aid separator 52. The inlet of the regenerant separator 51 is communicated with the outlet of the fluidized bed regenerator 40. The regenerant outlet of the regenerant separator 51 is communicated with the moving bed reactor. The gas phase outlet of the regenerant separator 51 is communicated with the inlet of the fluidization aid separator 52. The outlet of the fluidization aid separator 52 is communicated with the fluidization aid inlet 33 of the particle mixer 31.

[0078] Furthermore, as Figure 1 , Figure 2 shown, the outlet of the fluidized bed regenerator 40 is communicated with the inlet of the regenerant separator 51 through a riser 6.

[0079] Example 1

[0080] As Figure 1 , Figure 3 shown, the moving bed reactor includes a plurality of conical moving bed reactors 21 connected in series. Each conical moving bed reactor 21 includes a first outer shell 2101. A first inner layer Johnson screen 2102 with a diameter gradually decreasing from top to bottom is provided inside the first outer shell 2101. A first central cavity 202 is formed inside the first inner layer Johnson screen 2102 in the radial direction. A first outer layer Johnson screen 2103 with the same diameter up and down is coaxially sleeved outside the first inner layer Johnson screen 2102. A first outer ring gap space 203 is formed between the first outer layer Johnson screen 2103 and the first outer shell 2101 at a radial interval. A first inner ring gap space 204 with a cross-sectional area gradually increasing from top to bottom is formed between the first inner layer Johnson screen 2102 and the first outer layer Johnson screen 2103. The first inner ring gap space 204 allows the solid-phase catalyst to flow from top to bottom under the action of gravity;

[0081] At the top of the first outer shell 2101, a regenerated catalyst inlet 205 is provided, and at the bottom of the first outer shell 2101, a spent catalyst outlet 201 is provided; at the lower part of the side wall of the first outer shell 2101, a gas-phase raw material inlet 206 is provided, and at the upper part of the side wall of the first outer shell 2101, a gas-phase outlet 207 is provided; the gas-phase raw material enters the first outer shell 2101 through the gas-phase raw material inlet 206 and diffuses radially along the first outer shell 2101. The gas-phase raw material contacts the solid-phase catalyst in the first inner annulus space 204 in a countercurrent manner and reacts to produce a gas-phase product, and the gas-phase product is output outward through the gas-phase outlet 207.

[0082] The conical moving bed reactor 21 of the present invention can avoid the phenomenon of wall sticking and hole blocking of the solid-phase material outside the first inner layer Johnson screen 2102, or avoid the phenomena such as gas cavities and cavities that are not conducive to fluidization inside the first outer layer Johnson screen 2103, strengthen the axial flow of the catalyst in the bed layer, promote the contact between the gas and the catalyst, and improve the reaction efficiency of propane catalytic dehydrogenation.

[0083] Furthermore, the cone angle range of the first inner layer Johnson screen 2102 is 1° to 10°. The inner layer Johnson screen (the first inner layer Johnson screen 2102) of the conical moving bed reactor 21 can improve the problems of gas cavities or wall sticking in the solid-phase material bed layer.

[0084] Furthermore, as Figure 1 、 Figure 3 shown, the moving bed reactor includes 4 conical moving bed reactors 21, which are sequentially set as the fourth conical moving bed reactor 214, the third conical moving bed reactor 213, the second conical moving bed reactor 212, and the first conical moving bed reactor 211 along the gas-phase raw material flow direction;

[0085] The gas-phase raw material inlet 206 of the fourth conical moving bed reactor 214 is connected to the material heating system 1, the gas-phase outlet 207 of the fourth conical moving bed reactor 214 is connected to the gas-phase raw material inlet 206 of the third conical moving bed reactor 213, the gas-phase outlet 207 of the third conical moving bed reactor 213 is connected to the gas-phase raw material inlet 206 of the second conical moving bed reactor 212, the gas-phase outlet 207 of the second conical moving bed reactor 212 is connected to the gas-phase raw material inlet 206 of the first conical moving bed reactor 211, and the gas-phase outlet 207 of the first conical moving bed reactor 211 is connected to the material heating system 1; the feeding and discharging methods of the gas-phase materials of each conical moving bed reactor 21 are both from the outside at the bottom and from the center at the top.

[0086] The regeneration catalyst inlet 205 of the first conical moving bed reactor 211 is connected to the gas-solid separation system 5, and the spent catalyst outlet 201 of the first conical moving bed reactor 211 is connected to the regeneration catalyst inlet 205 of the second conical moving bed reactor 212, and a control valve is provided therebetween; the spent catalyst outlet 201 of the second conical moving bed reactor 212 is connected to the regeneration catalyst inlet 205 of the third conical moving bed reactor 213 through an inter-stage riser 215. A catalyst buffer 216 is provided at the highest point of the inter-stage riser 215, and a conveying air pipe 217 is provided at the lowest point of the inter-stage riser 215; the spent catalyst outlet 201 of the third conical moving bed reactor 213 is connected to the regeneration catalyst inlet 205 of the fourth conical moving bed reactor 214, and a control valve is provided therebetween; the spent catalyst outlet 201 of the fourth conical moving bed reactor 214 is connected to the auxiliary fluidization system 3 through a catalyst downcomer 23 to enable the spent catalyst to flow to the auxiliary fluidization system 3.

[0087] Further, as Figure 1 , Figure 3 shown, the material heating system 1 includes an inlet-outlet heat exchanger 11 and a raw material heating section. The inlet-outlet heat exchanger 11 includes a raw material passage and a product passage. The raw material passage is used for conveying a gaseous raw material, and the product passage is used for conveying a gaseous product. The gaseous product in the product passage exchanges heat with the gaseous raw material in the raw material passage to heat up the gaseous raw material; the raw material heating section includes a plurality of heaters corresponding to each conical moving bed reactor 21 one by one. The gaseous raw material is heated to a set temperature by the corresponding heater before entering each conical moving bed reactor 21.

[0088] Corresponding to the structure in which the aforementioned moving bed reactor includes 4 conical moving bed reactors 21, the raw material heating section includes a first heater 121, a second heater 122, a third heater 123, and a fourth heater 124 for heating the raw material to an expected reaction temperature. Since the reaction is endothermic, the material temperature decreases as the reaction proceeds. Therefore, heat needs to be supplemented through the heaters between the reactors to stabilize the material temperature to the expected reaction temperature.

[0089] A third heater 123 is provided between the gas outlet 207 of the fourth conical moving bed reactor 214 and the gaseous raw material inlet 206 of the third conical moving bed reactor 213. A second heater 122 is provided between the gas outlet 207 of the third conical moving bed reactor 213 and the gaseous raw material inlet 206 of the second conical moving bed reactor 212. A first heater 121 is provided between the gas outlet 207 of the second conical moving bed reactor 212 and the gaseous raw material inlet 206 of the first conical moving bed reactor 211. The gaseous raw material inlet 206 of the fourth conical moving bed reactor 214 is connected to the raw material passage through a fourth heater 124.

[0090] Further, as shown in Figure 1 and Figure 3 , the regeneration system 4 includes a fluidized bed regenerator 40, which includes a main air duct 41 for regeneration, a main air distributor 42, an annular duct distributor 43, a draft tube 44, a regenerant internal circulation pipe 45, a large pore distributor plate 46, a regenerant outlet pipe 47, a flue gas outlet 48, and a combined cyclone separator 49. The regenerant outlet pipe 47 is connected to the inlet of the regenerant separator 51 through a riser 6.

[0091] In the moving bed-fluidized bed reaction regeneration coupling device with the above-mentioned moving bed reactors in which a plurality of conical moving bed reactors 21 are connected in series, the connection relationships of each system are as follows: the outlet of the fourth heater 124 of the material heating system 1 is connected to the gas-phase raw material inlet 206 of the fourth conical moving bed reactor 214; the reaction system 2 is connected to the catalyst inlet 32 of the auxiliary fluidization system 3 through a catalyst downcomer 23; the mixed agent outlet 34 of the auxiliary fluidization system 3 is connected to the inlet of the fluidized bed regenerator 40; the regenerant outlet pipe 47 of the regeneration system 4 is connected to the gas-solid separation system 5 through a riser 6; the regenerated catalyst outlet of the gas-solid separation system 5 is connected to the regenerated catalyst inlet 205 of the reaction system 2; and the auxiliary fluidization agent outlet of the gas-solid separation system 5 is connected to the auxiliary fluidization agent inlet 33 of the auxiliary fluidization system 3.

[0092] Example 2

[0093] As shown in Figure 2 and Figure 4 , the moving bed reactor is a height-increasing multi-stage moving bed reactor 22, which includes a plurality of single-stage reactors 220 connected in series. Preferably, the number of series stages is 4 to 6; the heights of the plurality of single-stage reactors 220 are sequentially increased along the gas-phase raw material flow direction.

[0094] Further, as shown in Figure 2 and Figure 4As shown, each single-stage reactor 220 is connected in sequence up and down to form an integrated structure; each single-stage reactor 220 respectively includes a second outer casing 2201, and a second inner Johnson screen 2202 with equal diameters up and down is arranged inside the second outer casing 2201. A second central cavity 208 is formed inside the second inner Johnson screen 2202 in the radial direction; a second outer Johnson screen 2203 with equal diameters up and down is coaxially sleeved outside the second inner Johnson screen 2202, and a second outer annulus space 209 is formed by arranging a radial interval between the second outer Johnson screen 2203 and the second outer casing 2201; a second inner annulus space 210 is formed between the second inner Johnson screen 2202 and the second outer Johnson screen 2203. The second inner annulus space 210 allows the solid-phase catalyst to flow from top to bottom under the action of gravity. The second inner annulus spaces 210 at all levels are arranged in a conductive manner, the second outer annulus spaces 209 at all levels are arranged in a sealed manner, and the second central cavities 208 at all levels are arranged in a sealed manner;

[0095] A regenerated catalyst inlet 205 is arranged at the top of the single-stage reactor 220 at the top, and a spent catalyst outlet 201 is arranged at the bottom of the single-stage reactor 220 at the bottom; gas-phase raw material inlets 206 are respectively arranged at the lower parts of the side walls of each second outer casing 2201, and gas-phase outlets 207 are respectively arranged at the upper parts of the side walls of each second outer casing 2201;

[0096] Among them, the regenerated catalyst inlet 205 is connected to the gas-solid separation system 5 so that the regenerated catalyst separated by the gas-solid separation system 5 flows into the second inner annulus space 210; the spent catalyst outlet 201 is connected to the auxiliary fluidization system 3 so that the spent catalyst flows into the auxiliary fluidization system 3; each gas-phase raw material inlet 206 is respectively connected to the material heating system 1 so that the preheated gas-phase raw material flows into each second outer annulus space 209. The gas-phase raw material diffuses radially along the second outer casing 2201, countercurrently contacts the solid-phase catalyst in the second inner annulus space 210 and reacts to generate a gas-phase product, and the gas-phase product is output outward through the gas-phase outlet 207.

[0097] Furthermore, as Figure 2 、 Figure 4 shown, the material heating system 1 includes an inlet-outlet heat exchanger 11 and a raw material heating part. The inlet-outlet heat exchanger 11 includes a raw material channel and a product channel. The raw material channel is used to convey the gas-phase raw material, and the product channel is used to convey the gas-phase product. The gas-phase product in the product channel exchanges heat with the gas-phase raw material in the raw material channel to heat up the gas-phase raw material; the inlet-outlet heat exchanger 11 can make full use of the waste heat of the product to achieve the purpose of heating the raw material while achieving the effect of cooling the product;

[0098] The raw material heating section includes an integrated heating unit 13, and the integrated heating unit 13 can meet the different heat requirements among the single-stage reactors 220 at all levels; the integrated heating unit 13 includes multiple groups of heating tubes, each heating tube passes through the combustion furnace respectively, and each heating tube is arranged corresponding to each single-stage reactor 220 one by one. The inlet of the heating tube connected to the single-stage reactor 220 at the bottom is communicated with the outlet of the raw material passage. The gas-phase outlets 207 of the single-stage reactors 220 arranged successively from bottom to top are respectively communicated with the gas-phase raw material inlets 206 of the single-stage reactor 220 at the upper level through a heating tube, and the gas-phase outlet 207 of the single-stage reactor 220 at the top is communicated with the inlet of the product passage; the tube lengths of the heating tubes corresponding to the single-stage reactors 220 arranged successively from bottom to top are shortened successively.

[0099] Specifically, the height-increasing multi-stage moving bed reactor 22 includes 4 single-stage reactors 220, which are respectively set as the first single-stage reactor 221, the second single-stage reactor 222, the third single-stage reactor 223 and the fourth single-stage reactor 224 from bottom to top; the length of the first single-stage reactor 221 is 1000 mm to 5000 mm, the length of the second single-stage reactor 222 is 1200 mm to 6000 mm, the length of the third single-stage reactor 223 is 1400 mm to 7200 mm, and the length of the fourth single-stage reactor 224 is 1600 mm to 8600 mm.

[0100] Correspondingly, the integrated heating unit 13 includes 4 groups of heating tubes, namely the first heating tube 131, the second heating tube 132, the third heating tube 133, and the fourth heating tube 134. The outlet of the raw material passage is communicated with the gas-phase raw material inlet 206 of the first single-stage reactor 221 through the first heating tube 131. The gas-phase outlet 207 of the first single-stage reactor 221 is communicated with the gas-phase raw material inlet 206 of the second single-stage reactor 222 through the second heating tube 132. The gas-phase outlet 207 of the second single-stage reactor 222 is communicated with the gas-phase raw material inlet 206 of the third single-stage reactor 223 through the third heating tube 133. The gas-phase outlet 207 of the third single-stage reactor 223 is communicated with the gas-phase raw material inlet 206 of the fourth single-stage reactor 224 through the fourth heating tube 134. The gas-phase outlet 207 of the fourth single-stage reactor 224 is communicated with the product passage. Each heating tube is a heating coil tube, and the tube lengths of the first heating tube 131, the second heating tube 132, the third heating tube 133, and the fourth heating tube 134 are shortened successively to reduce the heating time of the medium and match the different heat requirements of each single-stage reactor 220.

[0101] The integrated heating unit 13 uses serpentine heating tubes with different lengths to supplement the different heat required for the raw materials in different reaction stages, more precisely matching the temperature required for the reaction to improve the selectivity and yield of the product.

[0102] Further, asFigure 2 , Figure 4 As shown in Figure 4 , two adjacent single-stage reactors 220 are connected by a first flange 225; a first baffle 226 and a second baffle 227 are provided at the connection of two adjacent single-stage reactors 220 to cause the gas phase to flow in a zigzag manner. The first baffle 226 is disposed in the second outer annulus space 209, and the second baffle 227 is disposed in the second central cavity 208. The first flange 225, the first baffle 226, and the second baffle 227 may be integrally formed.

[0103] Compared with the existing moving bed reactor, baffles (the first baffle 226 and the second baffle 227) are added to achieve the zigzag flow of the gas phase, and flanges (the first flange 225) are connected to highly integrate the moving bed reactor.

[0104] Furthermore, as shown in Figure 4 Figure 4 , each single-stage reactor 220 includes at least two single-stage reaction sections 2204. Two adjacent single-stage reaction sections are connected by a second flange 2205; a third baffle 2206 and a fourth baffle 2207 are provided at the connection of two adjacent single-stage reaction sections 2204 to cause the gas phase to flow in a zigzag manner. The third baffle 2206 is disposed in the second outer annulus space 209, and the fourth baffle 2207 is disposed in the second central cavity 208. The second flange 2205, the third baffle 2206, and the fourth baffle 2207 may be integrally formed. A fifth baffle 2209 is further disposed in the second outer annulus space 209 of the single-stage reaction section 2204; a gas-phase raw material inlet 206 is provided at the lower part of the side wall of each single-stage reaction section 2204, and a gas-phase outlet 207 is provided at the upper part of the side wall of each single-stage reaction section 2204;

[0105] The gas-phase raw material inlet 206 of the single-stage reaction section 2204 at the bottom end is communicated with the material heating system 1. The gas-phase outlet 207 of the single-stage reaction section 2204 below is communicated with the gas-phase raw material inlet 206 of the adjacent single-stage reaction section 2204 above it through an external connection pipe 2208, and the gas-phase outlet 207 of the single-stage reaction section 2204 at the top end is communicated with the material heating system 1.

[0106] Among them, each single-stage reaction section 2204 is a cylindrical shape with equal diameters up and down, the length is 10000 mm to 30000 mm, the diameter of the second inner Johnson screen 2202 is Φ1800 mm to Φ5400 mm, the diameter of the second outer Johnson screen 2203 is Φ3400 mm to Φ10200 mm, and the diameter of the second outer shell 2201 is Φ5000 mm to Φ15000 mm.

[0107] Both ends of each single-stage reaction section 2204 are the second flanges 2205. Among them, there is an annular gap vacancy on the second flange 2205, and the size and position are the same as those of the second inner annular gap space 210, meeting the requirements of the second inner annular gap space 210 being unobstructed and the second central cavity 208 and the second outer annular gap space 209 being sealed off; each single-stage reaction section 2204 is connected through the second flange 2205, and at the same time, the outside is connected through the outer connection pipe 2208.

[0108] The feeding and discharging method of the gas-phase material in each single-stage reaction section 2204 is that the gas-phase material enters from the outside and exits from the outside, and the solid-phase material flows in the second inner annular gap space 210.

[0109] After the gas-phase material enters the second outer annular gap space 209 from the gas-phase raw material inlet 206, it diffuses into the interior of the second inner layer Johnson screen 2202; after the gas-phase material enters the second central cavity 208, it diffuses upward. After diffusing to the height where the baffle is located, it diffuses to the outside of the second outer layer Johnson screen 2203 and diffuses to leave from the gas-phase outlet 207; the solid-phase material flows in the second inner annular gap space 210.

[0110] The height-increasing multi-stage moving bed reactor 22 utilizes the characteristics of the propane catalytic dehydrogenation process that require short gas-solid contact time and low backmixing. By setting baffles, the diffusion reaction time of the gas phase in the solid-phase material under the same throughput is shortened, and at the same time, the backmixing is reduced, making the gas-solid contact more uniform, reducing the occurrence of subsequent side reactions, and being beneficial to improving the selectivity and yield of the product.

[0111] The height-increasing multi-stage moving bed reactor 22 adopts a highly integrated structure. Through special sealing flanges, each single-stage reactor 220 is efficiently connected in series. The structure with directly connected bed layers can reduce the space occupied by the reaction system and effectively reduce the construction and use costs of the moving bed propane dehydrogenation process.

[0112] In the moving bed-fluidized bed reaction-regeneration coupling device adopting the above-mentioned height-increasing multi-stage moving bed, the connection relationship of each system is as follows: the outlet of the first heating pipe 131 of the material heating system 1 is connected to the gas-phase raw material inlet 206 of the first single-stage reactor 221, the reaction system 2 is connected to the catalyst inlet 32 of the auxiliary fluidization system 3 through the catalyst feeding pipe 23, the mixture outlet 34 of the auxiliary fluidization system 3 is connected to the inlet of the fluidized bed regenerator 40, the regenerant outlet pipe 47 of the regeneration system 4 is connected to the gas-solid separation system 5 through the riser 6, the regenerated catalyst outlet of the gas-solid separation system 5 is connected to the regenerated catalyst inlet 205 of the reaction system 2, and the auxiliary fluidization agent outlet of the gas-solid separation system 5 is connected to the auxiliary fluidization agent inlet 33 of the auxiliary fluidization system 3.

[0113] Example 3

[0114] The using method of the moving bed-fluidized bed reaction-regeneration coupling device of the present invention includes:

[0115] The gaseous material is heated by the material heating system 1 and then introduced into the reaction system 2. The gaseous raw material and the solid-phase catalyst are in countercurrent contact and react in the reaction system 2. The reacted catalyst (spent catalyst) flows to the auxiliary fluidization system 3 and is mixed with the input fluidization aid and then introduced into the regeneration system 4 together. Specifically, a fluidization aid with a suitable particle size is input into the particle mixer 31. The fluidization aid is fully mixed with the spent catalyst, enhancing the fluidization performance of the spent catalyst and achieving efficient fluidization of the spent catalyst.

[0116] The spent catalyst undergoes coke burning regeneration to form a regenerated catalyst. The regenerated catalyst enters the gas-solid separation system 5 through the riser 6. Coarser catalyst particles are separated by the regenerant separator 51 of the gas-solid separation system 5 and then returned to the reaction system 2. Finer fluidization aids are separated by the fluidization aid separator 52 of the gas-solid separation system 5 and then enter the auxiliary fluidization system 3, where they are remixed with the spent catalyst and then enter the regeneration system 4 for the next regeneration cycle.

[0117] As described above, the moving bed-fluidized bed reaction-regeneration coupling device and its use method of the present invention have the following beneficial effects:

[0118] The present invention solves the problems of conventional reaction-regeneration devices, such as difficulty in matching the reaction-regeneration requirements of special catalysts, low coke burning regeneration and gas-solid contact efficiency, complex series-parallel types of reactors, low integration, and high construction costs.

[0119] In the moving bed-fluidized bed reaction-regeneration coupling device of the present invention, the reaction system and the regeneration system are efficiently coupled through the auxiliary fluidization system and the gas-solid separation system. The fluidization aid is mixed with the poorly fluidizable spent catalyst through the auxiliary fluidization system to improve the fluidization performance of the spent catalyst, so as to achieve efficient fluidization and coke burning regeneration of the catalyst, ensuring both the high efficiency of the catalyst in the propane dehydrogenation reaction and the efficient fluidization and coke burning regeneration. The two types of particles after regeneration are efficiently separated in sequence through the gas-solid separation system to avoid the influence of the fluidization aid on the catalytic reaction process.

[0120] The conical moving bed reactor of the present invention can avoid the phenomenon of solid-phase material sticking to the wall and blocking holes outside the first inner layer Johnson screen, or avoid the phenomena of cavitation and cavity inside the first outer layer Johnson screen, which are unfavorable for fluidization, strengthen the axial flow of the catalyst in the bed layer, promote the contact between gas and catalyst, and improve the reaction efficiency of propane catalytic dehydrogenation.

[0121] The highly incremental multi-stage moving bed reactor of the present invention utilizes the characteristics of short gas-solid contact time and low backmixing required in the propane catalytic dehydrogenation process. By setting a baffle, the diffusion reaction time of the gas phase in the solid phase material under the same processing capacity is shortened, and the backmixing is reduced, so that the gas-solid contact is more uniform, and the occurrence of subsequent side reactions is reduced, which is beneficial to improving the selectivity and yield of the product; a highly integrated structure is adopted, and the moving bed reactors of each stage are efficiently connected in series through a special sealing flange. The structure of the bed layer directly connected can reduce the space occupied by the reaction system, and effectively reduce the construction and use costs of the moving bed propane dehydrogenation process.

[0122] The integrated heating unit of the present invention utilizes serpentine heating tubes of different lengths to supplement the different heat required for raw materials in different reaction stages, and more accurately matches the temperature required for the reaction to improve the selectivity and yield of the product.

[0123] The present invention can provide the optimal reaction environment required for propane dehydrogenation under existing or new catalysts, ensure efficient and stable reaction, realize efficient and continuous fluidized coke regeneration, and can effectively reduce the construction and use costs of the process, achieve the purpose of energy saving and consumption reduction, and has a high prospect for industrial promotion.

[0124] The above description is only an illustrative embodiment of the present invention and is not intended to limit the scope of the present invention. Any equivalent changes and modifications made by any person skilled in the art without departing from the concept and principle of the present invention shall fall within the scope of protection of the present invention.

Claims

1. A moving bed-fluidized bed reaction regeneration coupling device, characterized in that: include: A material heating system, used to exchange heat between the gas phase product and the gas phase raw material to heat the gas phase raw material; A reaction system, comprising a moving bed reactor connected to the material heating system, wherein the moving bed reactor is used for the reaction of the gas-phase raw material and the solid-phase catalyst and can enhance the axial flow of the solid-phase catalyst; An auxiliary fluidization system is connected to the outlet of the catalyst to be regenerated of the moving bed reactor, and the auxiliary fluidization system mixes a fluidizing agent and the catalyst to be regenerated to improve the fluidization performance of the catalyst to be regenerated; A regeneration system, used for coking and regenerating the spent catalyst to form a regenerated catalyst, comprising a fluidized bed regenerator connected to the outlet of the auxiliary fluidized system; A gas-solid separation system is connected to the outlet of the fluidized bed regenerator, and the gas-solid separation system separates the regenerated catalyst and the fluidizing agent, and transports the regenerated catalyst to the moving bed reactor and the fluidizing agent to the auxiliary fluidization system.

2. The moving bed-fluidized bed reaction regeneration coupling device according to claim 1, characterized in that: The auxiliary fluidization system comprises a particle mixer, on which a catalyst inlet, a fluidizing agent inlet and a mixing agent outlet are arranged; the catalyst inlet is communicated with the catalyst outlet to be regenerated of the moving bed reactor, and the catalyst inlet is used to transport the catalyst to be regenerated from the moving bed reactor into the particle mixer; the fluidizing agent inlet is used to transport the fluidizing agent into the particle mixer; the mixing agent outlet is communicated with the fluidized bed regenerator; The particle density of the fluidizing agent is 1000-3000 kg / m 3 The particle diameter of the fluidizing agent is Φ30 μm to Φ1000 μm, and the mixing ratio of the fluidizing agent to the catalyst to be generated is 0.05 to 1.5:

1.

3. The moving bed-fluidized bed reaction regeneration coupling device according to claim 2, characterized in that: The moving bed reactor comprises a plurality of conical moving bed reactors connected in series, each of the conical moving bed reactors comprises a first outer shell, a first inner layer Johnson net with a diameter gradually decreasing from top to bottom is arranged in the first outer shell, and a first central cavity is formed on the radial inner side of the first inner layer Johnson net; a first outer layer Johnson net with equal diameters is coaxially sleeved on the outer side of the first inner layer Johnson net, and the first outer layer Johnson net and the first outer shell are radially spaced to form a first outer annular space; a first inner annular space with a cross-sectional area gradually increasing from top to bottom is formed between the first inner layer Johnson net and the first outer layer Johnson net, and a solid phase catalyst is allowed to flow from top to bottom under the action of gravity in the first inner annular space; The top of the first outer shell is provided with a regenerated catalyst inlet, and the bottom of the first outer shell is provided with the catalyst outlet to be regenerated; the lower part of the side wall of the first outer shell is provided with a gaseous raw material inlet, and the upper part of the side wall of the first outer shell is provided with a gaseous phase outlet; the gaseous raw material enters the first outer shell through the gaseous raw material inlet and diffuses radially along the first outer shell, the gaseous raw material countercurrently contacts with the solid-phase catalyst in the first inner annular space and reacts to produce a gaseous phase product, and the gaseous phase product is output outward through the gaseous phase outlet; The cone angle of the first inner layer Johnson mesh ranges from 1° to 10°.

4. The moving bed-fluidized bed reaction regeneration coupling device according to claim 3, characterized in that: The moving bed reactor comprises four conical moving bed reactors, which are sequentially arranged along the flow direction of the gas-phase raw material as a fourth conical moving bed reactor, a third conical moving bed reactor, a second conical moving bed reactor, and a first conical moving bed reactor; The gas-phase raw material inlet of the fourth conical moving bed reactor is connected to the material heating system, the gas-phase outlet of the fourth conical moving bed reactor is connected to the gas-phase raw material inlet of the third conical moving bed reactor, the gas-phase outlet of the third conical moving bed reactor is connected to the gas-phase raw material inlet of the second conical moving bed reactor, the gas-phase outlet of the second conical moving bed reactor is connected to the gas-phase raw material inlet of the first conical moving bed reactor, and the gas-phase outlet of the first conical moving bed reactor is connected to the material heating system; The regenerated catalyst inlet of the first conical moving bed reactor is connected to the gas-solid separation system; the regenerated catalyst outlet of the first conical moving bed reactor is connected to the regenerated catalyst inlet of the second conical moving bed reactor; the regenerated catalyst outlet of the second conical moving bed reactor is connected to the regenerated catalyst inlet of the third conical moving bed reactor through an interstage riser; The regenerated catalyst outlet of the third conical moving bed reactor is connected to the regenerated catalyst inlet of the fourth conical moving bed reactor; the regenerated catalyst outlet of the fourth conical moving bed reactor is connected to the auxiliary fluidized system so that the regenerated catalyst flows to the auxiliary fluidized system.

5. The moving bed-fluidized bed reaction regeneration coupling device according to claim 2, characterized in that: The moving bed reactor is a multi-stage moving bed reactor with increasing height, which comprises a plurality of single-stage reactors connected in series, and the heights of the plurality of single-stage reactors are arranged to increase in sequence along the flow direction of the gas-phase raw material.

6. The moving bed-fluidized bed reaction regeneration coupling device according to claim 5, characterized in that: Each of the single-stage reactors is sequentially connected up and down to form an integrated structure; each of the single-stage reactors comprises a second outer shell, a second inner layer Johnson net with equal diameters is arranged in the second outer shell, and a second central cavity is formed on the radial inner side of the second inner layer Johnson net; a second outer layer Johnson net with equal diameters is coaxially sleeved on the outer side of the second inner layer Johnson net, and the second outer layer Johnson net and the second outer shell are radially spaced to form a second outer annular space; a second inner annular space is formed between the second inner layer Johnson net and the second outer layer Johnson net, and the solid-phase catalyst is allowed to flow from top to bottom under the action of gravity in the second inner annular space, the second inner annular space of each stage is in a conducting arrangement, the second outer annular space of each stage is in a sealed arrangement, and the second central cavity of each stage is in a sealed arrangement; The top of the single-stage reactor at the top is provided with a regenerated catalyst inlet, and the bottom of the single-stage reactor at the bottom is provided with the catalyst outlet to be regenerated; the lower part of the side wall of each stage of the second outer shell is provided with a gas phase raw material inlet, and the upper part of the side wall of each stage of the second outer shell is provided with a gas phase outlet; Among them, the regenerated catalyst inlet is connected with the gas-solid separation system so that the regenerated catalyst separated by the gas-solid separation system flows to the second inner annular gap space; the regenerated catalyst outlet is connected with the auxiliary fluidization system so that the regenerated catalyst flows to the auxiliary fluidization system; the gas-phase raw material inlets of each stage are respectively connected with the material heating system so that the preheated gas-phase raw material flows into the second outer annular gap space of each stage, the gas-phase raw material diffuses radially along the second outer shell, countercurrently contacts with the solid-phase catalyst in the second inner annular gap space and reacts to produce gas-phase products, and the gas-phase products are output outward through the gas-phase outlet.

7. The moving bed-fluidized bed reaction regeneration coupling device according to claim 6, characterized in that: The material heating system includes an inlet and outlet heat exchanger and a raw material heating part. The inlet and outlet heat exchanger includes a raw material channel and a product channel. The raw material channel is used to transport gaseous raw materials, and the product channel is used to transport gaseous products. The gaseous products in the product channel exchange heat with the gaseous raw materials in the raw material channel to increase the temperature of the gaseous raw materials. The raw material heating part includes an integrated heating unit, which includes multiple groups of heating tubes, each of which passes through the combustion furnace respectively. Each of the heating tubes is arranged one by one corresponding to each of the single-stage reactors. The inlet of the heating tube connected to the single-stage reactor located at the bottom is connected to the outlet of the raw material channel. The gas phase outlet of each of the single-stage reactors arranged sequentially from bottom to top is connected to the gas phase raw material inlet of the single-stage reactor above it through a heating tube, and the gas phase outlet of the single-stage reactor located at the top is connected to the inlet of the product channel; the length of each of the heating tubes corresponding to each of the single-stage reactors arranged sequentially from bottom to top is shortened in sequence.

8. The moving bed-fluidized bed reaction regeneration coupling device according to claim 6, characterized in that: Two adjacent single-stage reactors are connected by a first flange; a first baffle and a second baffle are provided at the connection between the two adjacent single-stage reactors to deflect the gas phase, the first baffle is arranged in the second outer annular space, and the second baffle is arranged in the second central cavity; Each of the single-stage reactors comprises at least two single-stage reaction sections, and the two adjacent single-stage reaction sections are connected by a second flange; a third baffle and a fourth baffle are provided at the connection between the two adjacent single-stage reaction sections to deflect the gas phase, the third baffle is arranged in the second outer annular space, and the fourth baffle is arranged in the second central cavity; a gas phase raw material inlet is arranged at the lower part of the side wall of each of the single-stage reaction sections, and a gas phase outlet is arranged at the upper part of the side wall of each of the single-stage reaction sections; The gas-phase raw material inlet of the single-stage reaction section located at the bottom is connected to the material heating system, the gas-phase outlet of the single-stage reaction section located below is connected to the gas-phase raw material inlet of the single-stage reaction section adjacent to it above through an external pipe, and the gas-phase outlet of the single-stage reaction section located at the top is connected to the material heating system.

9. The moving bed-fluidized bed reaction regeneration coupling device according to claim 2, characterized in that: The gas-solid separation system includes a regeneration agent separator and a fluidizing agent separator, wherein the inlet of the regeneration agent separator is connected to the outlet of the fluidized bed regenerator, the regeneration agent outlet of the regeneration agent separator is connected to the moving bed reactor, the gas phase outlet of the regeneration agent separator is connected to the inlet of the fluidizing agent separator, and the outlet of the fluidizing agent separator is connected to the fluidizing agent inlet of the particle mixer.

10. A method for using the moving bed-fluidized bed reaction regeneration coupling device according to any one of claims 1 to 9, characterized in that: include: The gaseous material is heated by the material heating system and then passed into the reaction system. The gaseous raw material and the solid-phase catalyst are countercurrently contacted and reacted in the reaction system. The catalyst to be regenerated after the reaction flows to the auxiliary fluidization system and is mixed with the input fluidizing agent and then passed into the regeneration system. The catalyst to be regenerated is burned and regenerated to form a regenerated catalyst; the regenerated catalyst enters the gas-solid separation system, the coarser catalyst particles are separated by the gas-solid separation system and then returned to the reaction system, the finer fluidizing agent is separated by the gas-solid separation system and then enters the auxiliary fluidization system, and is remixed with the catalyst to be regenerated and then enters the regeneration system to enter the next regeneration cycle.

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