BR102017023634A2 - FLUIDIZED YIELD REACTOR, REGENERATION REACTION APPARATUS, PROCESS FOR PREPARING OLEFINS AND PROCESS FOR PREPARING AROMATIC HYDROCARBONS - Google Patents

Abstract

fluidized bed reactor, reaction regenerating apparatus, process for preparing olefins and process for preparing aromatic hydrocarbons. The present invention relates to a fluidized bed reactor comprising an input zone at a lower position, an output zone at a higher position and a reaction zone between an input zone and an output zone. a hollow-hole guide plate is arranged in the reaction zone, comprising a dense channel region in an intermediate region thereof and a sparse channel region disposed in a periphery thereof and encompassing the dense channel region. The catalysts in said fluidized bed reactor can be homogeneously distributed in their reaction zone, whereby the reaction efficiency can be improved. a reaction regeneration apparatus comprising said fluidized bed reactor, and a process for preparing olefins from oxygenates and a process for preparing aromatic hydrocarbons from oxygenates using the reaction regeneration apparatus.

Description

FLUIDIZED BED REACTOR, APPARATUS TO REGENERATE REACTION, PROCESS TO PREPARE OLEFINS AND PROCESS TO PREPARE AROMATIC HYDROCARBONS

CROSS REFERENCE WITH RELATED APPLICATION [001] This application claims the benefit of Chinese patent application CN 201410539938.0, entitled Multiregion Coupling Reinforcing Process for Preparing Olefins from Methanol and filed on October 14, 2014, the entire of which is incorporated herein by reference.

FIELD OF TECHNIQUE [002] The present disclosure refers to the field of chemical engineering technique, and in particular, to a fluidized bed reactor. The present disclosure further relates to a reaction regeneration apparatus for use in the fluidized bed reactor, and to a process for preparing olefins and a process for preparing aromatic hydrocarbons.

BACKGROUND OF THE INVENTION [003] In modern petrochemical engineering, ethylene and propylene are the most crucial basic materials. Ethylene can be used in the preparation of downstream products including polyethylene, styrene, vinyl acetate, ethylene oxide and ethylene glycol and so on. Propylene can be used in the preparation of downstream products including polypropylene, acrylonitrile, propylene oxide and isopropyl alcohol and so on. Ethylene and propylene and their downstream products are widely used in the fields of industry and agriculture, transportation and national defense.

[004] In recent years, the demand for ethylene and propylene remains high. Under the circumstance that the oil resource gradually decreases, the short supply of oil in China can be greatly alleviated through the chemical technology of coal, with which ethylene and propylene can be used.

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2/33 prepared from non-oil resources. This is significant in promoting the development of the national heavy chemical industry. Based on the chemical technology of coal, oxygenates can be prepared from coal and then olefins can be prepared from oxygenates.

[005] At the moment, an apparatus for preparing olefins from methanol is similar to a catalytic cracking device, both being of the continuous reaction regeneration type. According to patent literature US166282, a process and a reactor for converting oxides to low carbon olefins are disclosed. A fast fluidized bed reactor is used in a technical solution from the above patent literature. The gas reacts in a reaction zone with low gas velocity and then rises to a rapid separation zone with a rapidly decreasing internal diameter. The catalysts loaded in the product are separated by means of a preliminary cyclone. Because the product and catalysts are separated quickly, the side reaction can be effectively prevented. The reactor used in the above patent literature is a fast upstream fluidized bed reactor with a traditional feed inlet.

[006] Chinese patent literature CN103121901A recites a method for converting oxygenated chemicals to generate low-carbon olefins. According to the method above, the catalysts that will be generated and the regenerated catalysts are premixed in a catalyst mixer and then enter a reactor, so the problems of insufficient catalyst mixing and low production of low-grade olefins carbon in a reaction zone in the prior art can be resolved.

[007] Chinese patent literature CN101164685A refers to a combined rapid fluidized bed reactor for oxygenates or catalytic reaction of dimethyl ether. According to the above patent literature, a separation device in

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3/33 a sedimentation zone is arranged externally, so that the space occupied by the sedimentator can be reduced, thereby the sedimentation speed of the catalysts can be increased and the residence time of the olefins can be reduced. In the meantime, problems of low selectivity and low production of ethylene and propylene can also be solved. When compared to a traditional fast fluidized bed reactor comprising an external sedimentator, the production of ethylene can be increased by 4% and that of propylene can be increased by 3%.

[008] In the prior art, the distribution of the concentration of catalyst particles in the fluidized bed reactor is not uniform, but preferably has characteristics of distribution of diluted concentration at the top of the fluidized bed reactor and dense concentration at the bottom and the diluted concentration in its intermediate region and the dense concentration in its peripheral sections. The distribution characteristics above severely influence the efficiency of the reaction, therefore, urgently require improvements.

SUMMARY OF THE INVENTION [009] Aimed against the above problem, a fluidized bed reactor is provided in accordance with the present disclosure. The catalysts can be distributed homogeneously in a reaction zone of the fluidized bed reactor according to the present disclosure, so that the efficiency of the reaction can be improved. The present disclosure further relates to a reaction regeneration apparatus comprising said fluidized bed reactor, a process for preparing olefins from oxygenates and a process for preparing aromatic hydrocarbons from oxygenates using the reaction regeneration apparatus .

[010] In a first aspect according to the present disclosure, a fluidized bed reactor is provided, comprising an inlet zone in a

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4/33 lowest position, an exit zone in a higher position and a reaction zone between the entry zone and the exit zone. A guide plate is arranged in the reaction zone, comprising a region of dense channel in an intermediate region of its own and a region of sparse channel arranged in its periphery covering the region of dense channel.

[011] In the fluidized bed reactor according to the present disclosure, the dense channel region has a relatively large obstacle for material moving upwards, while the sparse channel region has relatively little obstacle in it. Therefore, especially when the reaction material is gas, in the reaction zone of the fluidized bed reactor, the pressure drop of the gas in an intermediate region is relatively large and that in the surrounding regions is relatively small. Under the guide plate in the fluidized bed reactor, the gas in the intermediate region will be forced into the peripheral regions, so that the speed of the gas flowing through the sparse channel region can be increased. In this case, above the guide plate, the gas velocity of the marginal regions of the circumference of the fluidized bed reactor will be increased, so that catalyst particles in the marginal regions of the circumference can be blown upwards. Under the influence of a fluidized bed reactor wall and the general material flow in the fluidized bed reactor, the catalyst particles blown up flow into the intermediate region of the reaction zone. As a result, the catalyst particles can be distributed homogeneously along the radial direction of the fluidized bed reactor, so the efficiency of the reaction can be improved.

[012] In an embodiment according to the present disclosure, the size of a channel in the dense channel region is smaller than the size of the channel in the sparse channel region. Preferably, the ratio of the channel dimension in the dense channel region to that of the channel in the sparse channel region is in the range of 1: 4 to 2: 3. Preferably, the size of the channel in the dense channel region is

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5/33 a range of 0.01 to 0.08 m. This is because in the fluidized bed reactor, the size of a single bubble can vary according to the diameter of the fluidized bed reactor. Under general conditions, the bubble size is not greater than 0.12 m. In this case, the bubbles of the reaction mass and the catalyst particle aggregates in the fluidized bed reactor will be ruptured. Therefore, the homogeneity of the mixture of the reaction mass and catalysts can be increased and the contact area between the reaction mass and the catalysts can be increased, so that the efficiency of the reaction can be further improved.

[013] In one embodiment, each of the dense channel region and the sparse channel region comprises a circular plate having equally distributed pores, or a plurality of concentric ring-shaped inclined panels or a plurality of straight panels separated in parallel. The guide plate of these types can create the flow of the gas, so that the homogeneity of the distribution of the catalysts in a radial direction can be further improved.

[014] In one embodiment, the dense channel region is round in shape and the sparse channel region is ring-shaped, and the ratio of the diameter of the dense channel region to the width of the sparse channel region is in one range from 2: 1 to 9: 1. In that case, the guide plate can be easily mounted on the fluidized bed reactor.

[015] In one embodiment, a plurality of guide plates are provided distributed along the axial direction of the fluidized bed reactor. By having a plurality of the guide plates, the homogeneity of the distribution of the catalysts in the radial direction of the fluidized bed reactor can be further increased, and the bubbles of the reaction mass and the aggregates of the catalyst particle can be more easily broken. As a result, the efficiency of the reaction can be further improved.

[016] In one mode, the entry for the accelerator gas is arranged in the

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6/33 exit zone of the fluidized bed reactor. Preferably, the inlet for the accelerator gas is configured to extend obliquely from a lower position to a higher position. In this case, the gas, such as nitrogen, inert gas or water vapor, which has a high speed, can be injected into the outlet area of the fluidized bed reactor through the inlet to the accelerator gas, so that the pressure in the fluidized bed can be more uniform and catalysts can be more homogeneously distributed in the fluidized bed reactor. In that case, the defect of the fluidized bed reactor in the prior art is that the density of the catalysts at the top of the fluidized bed reactor is relatively small, while the density of the catalysts at its bottom is relatively large, can be eliminated. Together, by arranging the inlet for the accelerator gas, the catalysts can spread evenly along the axial direction of the fluidized bed reactor, so that the efficiency of the contact of the gas with the solid can be optimized. In the meantime, the rate of circulation of the catalysts throughout the reaction regeneration apparatus can be improved and the yield of the product can be increased.

[017] In one embodiment, the entry for the accelerator gas forms an angle in a range of 5 to 39 degrees in relation to the longitudinal geometric axis of the fluidized bed reactor. In another embodiment, the ratio of the inlet diameter to the accelerator gas to a diameter of the outlet zone of the fluidized bed reactor is in a range of 0.01 to 0.1. In an additional embodiment, the ratio of the length of the part of the outlet zone of the fluidized bed reactor that is above the inlet for the accelerator gas to an overall length of the outlet zone of the fluidized bed reactor is in a range of 0.1 to 0.8.

[018] In a second aspect of the present disclosure, a reaction regeneration apparatus is provided, comprising said fluidized bed reactor and further comprising a separation device and a separation device.

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7/33 regeneration of the catalyst respectively connected with the fluidized bed reactor. The separation device comprises a preliminary gas and solids separator in communication with an outlet zone of the fluidized bed reactor; a vertically arranged draft register, a lower region of the draft register being in communication with a solids outlet of the preliminary gas and solids separator to collect particles from the catalyst and a higher region of the draft register in communication with an outlet of preliminary gas and solids separator gas and a thin gas and solids separator, a gas and solids separator inlet communicating with the highest region of the draft register and its solids outlet communicating with the lowest region circulation record. The catalyst regeneration device comprises a feed zone in a lower position and a discharge zone in a higher position, the feed zone being arranged lower than the lowest region of the draft register and the discharge zone being arranged higher than the inlet area of the fluidized bed reactor. The lower region of the draft register is in communication with the supply zone of the catalyst regeneration device through a second pipe, and the discharge zone of the catalyst regeneration device is in communication with the entrance zone of the reactor. fluidized bed through a third pipe.

[019] The catalysts transported in the fluidized bed reactor product can be separated quickly through the preliminary gas and solids separator and the fine gas and solids separator, so that the secondary reaction of the product under the catalysis of the catalysts that will be regenerated that are still active can be effectively prevented. Production efficiency can also be greatly increased due to rapid separation. In addition, the fluidized bed reactor product generally has a high speed, thereby impacting the device receiving the product at high speed to the extent of intense vibration. How

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8/33 result, the device may even be damaged. According to the present disclosure, a draft register is arranged between the preliminary gas and solids separator and the fine gas and solids separator, so that the impact of the product at high speed can be absorbed by the preliminary gas and solids separator. and the run record together, so that damage to the entire separation device can be prevented. It is unnecessary for the preliminary gas and solids separator and draft register to be made large.

[020] In one embodiment, the diameter of the highest region of the draft register is smaller than that of its lowest region. Preferably, the ratio of the diameter of the highest region to that of the lowest region is in the range of 0.05 to 0.5. The fluctuation caused by the product flowing rapidly from the fluidized bed reactor to the highest region of the draft register can be rapidly reduced by the highest region with the smallest diameter, so that the lowest region of the draft register can remain in a relatively state. placid. As a result, catalysts can be stably accommodated in the lowest region of the draft register and the efficiency of gas and solids separation can be improved.

[021] In one mode, the lowest region of the draft register is configured and arranged, so that it performs a steam removal operation. For example, the steam inlet may be arranged at a lower end of the draft register and the structure or component for use in a steam removal operation may be arranged within the lower region of the draft register. The structure or component is well known to the person skilled in the art. The water vapor is fed to the lowest region of the draft register through its lowest end, so that the product loaded on the catalysts can be separated from the catalysts. The separated product rises with the water vapor to the highest region of the

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9/33 draft and mix with the product in it. In that case, the yield of the product can be greatly increased. In addition, as described above, the draft register is configured, so that severe fluctuation in its lowest region can be prevented, thereby facilitating the steam removal operation.

[022] In one embodiment, the position where the gas outlet of the preliminary gas and solids separator is connected with the draft register is below a position where the inlet of the fine gas and solids separator is connected with the draft register . Based on the above configuration, the catalysts loaded in the product can be precipitated as the product flows upward in the draft register, which further increases the efficiency of separation of gas and solids.

[023] In one embodiment, the preliminary gas and solids separator is a cyclone separator, and the fine gas and solids separator comprises two- or multi-stage cyclone separators. The two- or multi-stage series cyclone separators are configured so that the input of a first stage cyclone separator is in communication with the highest region of the draft register, the product being obtained from a gas outlet. a cyclone separator from the last stage, a gas outlet from an upstream cyclone separator communicates with an input from an adjacent downstream cyclone separator and the solid outlets of all cyclone separators are in communication with the region lowest of the circulation record. In addition, the separation effect of catalysts from the product can be improved by multiple cyclone separators in series connection. As a result, the efficiency of the recovery of the catalyst can be improved and the product obtained can contain less impurities. The cyclone separator can facilitate the quick separation of catalysts from the product and has the advantages of a simple structure and low price. In a preferred embodiment, both the preliminary gas and solids separator and the fine gas and solids separator are

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10/33 cyclone.

[024] In one embodiment, the highest region of the draft register is provided with an inlet port for communication with the gas outlet of the preliminary gas and solids separator and the inlet port configured to be tangent to a side wall of the highest region. The fluidized bed reactor product can be fed into the highest region of the draft register through said entry orifice in a path that is tangent to the side wall of its highest region. As a result, the product's impact on the run register can be reduced, so that the run register vibration can be relieved. In addition, the rotating product can also facilitate the precipitation of catalysts in it, thereby further improving the efficiency of the separation of gas and solids.

[025] In one embodiment, the third pipe is provided with a flow blocking member on top of its inner wall. The flow blocking member is used to block the gas and catalysts flowing backward into the third pipe caused by the strong reaction in the fluidized bed reactor. In that case, the feed rate of the catalyst particles can be effectively increased, so that the circulating rate of the catalysts can be further increased, whereby the product yield can be increased.

[026] In an embodiment according to the present disclosure, the flow blocking member is an inclined deflector for the fluidized bed reactor. In a specific example, the ratio of the deflector area to the cross-sectional area of the third pipe is in the range of 0.1 to 1. The deflector is in the shape of a sector or rectangular. The ratio of the distance between the deflector and the fluidized bed reactor to the length of the third pipe is in the range of 0.01 to 0.5. The angle formed between the deflector and the geometric axis of the third pipe is in a range of 10 to 75 degrees. Preferably, a plurality of deflectors are provided arranged in parallel with respect to each other.

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11/33 [027] In another embodiment, the flow blocking member is a stop tongue projecting radially inward. Preferably, a plurality of stop tabs arranged in a row along the geometric axis of the third pipe are provided. In one embodiment, the ratio of the length of each stop tab to the diameter of the third pipe is in the range of 0.1 to 0.5. Preferably, the cross section of each stop tab is in the shape of a triangle, rectangle or sector.

[028] In one embodiment, the inlet area of the fluidized bed reactor is arranged lower than the lowest region of the draft register and the lowest region of the draft register is in communication with the inlet area of the reactor. fluidized bed through a first pipe. This device can be used to prepare olefins from methanol.

[029] In one embodiment, each of the first pipe, the second pipe and the third pipe is provided with a valve to control the flow of material.

[030] In a third aspect according to the present disclosure, a process for preparing olefins is proposed, using said reaction regeneration apparatus. The entry zone of the fluidized bed reactor is arranged lower than the lowest region of the draft register of a separation device, and the lower region of the draft register is in communication with the entrance zone of the bed reactor fluidized through a first pipe. The process comprises the steps of: reacting the raw material containing oxygenates with catalysts in a reaction zone of the fluidized bed reactor; feeding the product obtained and the catalysts loaded into the separation device through an outlet area of the fluidized bed reactor; separate the product from the loaded catalysts through the separation device, feeding a portion of the catalysts obtained from the separation directly into the inlet area of the fluidized bed reactor and regenerating the

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12/33 remaining catalysts and feeding the regenerated catalysts into the inlet area of the fluidized bed reactor and mixing the unregenerated catalysts and regenerated catalysts into the inlet area of the fluidized bed reactor and then feeding the mixed catalysts into the zone reaction of the fluidized bed reactor.

[031] In an embodiment according to the present disclosure, the weight ratio of the non-regenerated catalysts in relation to the regenerated catalysts is in a range of 0.3 to 1.5.

[032] In one embodiment, the operation of the separation device comprises the following steps. The product of the fluidized bed reactor having catalysts loaded in it is preliminarily separated through a preliminary gas and solids separator. The product obtained from the preliminary separation by loading the remaining catalysts is fed into the highest region of the draft register. The product is then removed from the run register and fed into a fine gas and solids separator for fine separation. Subsequently, the product is obtained from a gas outlet of the fine gas and solids separator and the catalysts of the preliminary gas and solids separator and the fine gas and solids separator are collected in the lowest region of the draft register.

[033] In an embodiment according to the present disclosure, the water vapor is fed into the draft register by its lower end, so that the product loaded in the catalysts can be separated from the catalysts.

[034] In an embodiment according to the present disclosure, the pressure in the fluidized bed reactor by the gauge pressure is in a range of 0 to 0.4 MPa, the average temperature in it is in a range of 380 to 550Ό and the density The average reaction zone is in the range of 40 to 200 kg / m ³ . The catalyst used

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13/33 in it is the SAPO-34, a means of regeneration of the catalyst with the air and the temperature of the regeneration being in a range of 600 to 700 ° C.

[035] In one embodiment, the ratio of the pressure drop generated when the gaseous raw material flows through the dense channel region to that generated when the gaseous raw material flows through the sparse channel region is in a range of 1, 2: 1 to 10: 1.

[036] In one embodiment, the inlet for the accelerator gas is disposed in the outlet zone of the fluidized bed reactor, and the gas flowing into the outlet zone of the fluidized bed reactor through the inlet for the accelerator gas is vapor from water or nitrogen, the linear velocity of the gas staying in a range of 1.0 to 10.0 m / s.

[037] In one embodiment, the oxygenates comprise one or more selected from a group consisting of methanol, ethanol, n-propyl alcohol, isopropyl alcohol, C4-C20 alcohol, ethyl methyl ether, dimethyl ether, diethyl ether, diisopropyl ether, methanal , dimethyl carbonate, acetone and acetic acid and the weight of the oxygenates is responsible for 10 to 100% of the raw material.

[038] In a fourth aspect according to the present disclosure, a process for the preparation of aromatic hydrocarbons is proposed, using the said reaction regeneration apparatus. The process comprises: reacting the raw material containing oxygenates with catalysts in a reaction zone of a fluidized bed reactor; feed the product obtained and the catalysts loaded into a separation device through an outlet zone of the fluidized bed reactor and separate the product from the catalysts loaded therein through the separation device, regenerate the catalysts obtained from the separation and feed the catalysts regenerated into the inlet area of the fluidized bed reactor and into the reaction zone of the fluidized bed reactor.

[039] In one embodiment, the operation of the separation device

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14/33 comprises the following steps. The product of the fluidized bed reactor having the catalysts loaded in it is preliminarily separated through a preliminary gas and solids separator. The producer obtained from the preliminary separation by loading the remaining catalysts is fed into the highest region of the draft register. The product is then removed from the run register and fed into a fine gas and solids separator for fine separation. Subsequently, the product is obtained from a gas outlet of the fine gas and solids separator and the catalysts of the preliminary gas and solids separator and the fine gas and solids separator are collected within the lowest region of the draft register.

[040] In one embodiment, the water vapor is fed into the draft register from its lowest end, so that the product loaded in the catalysts can be separated from the catalysts.

[041] In one embodiment, the pressure in the fluidized bed reactor by the gauge pressure is in a range of 0 to 0.6 MPa, the average temperature in it is in a range of 440 to 550 ° C, the spatial speed in the The reaction is in the range of 0.3 to 5 Ir ¹ and the average density in the reaction zone is in the range of 200 to 450 kg / m ³ . The catalyst used in it is ZSM-5, the catalyst's regeneration medium being air and the regeneration temperature in a range of 550 to 650 ° C.

[042] In one embodiment, the pressure drop generated when the gaseous raw material flows through the dense channel region to that generated when the gaseous raw material flows through the sparse channel region is in the range of 1.2: 1 to 10: 1.

[043] In one embodiment, the inlet for the accelerator gas is arranged in the outlet zone of the fluidized bed reactor, and the gas flowing into the outlet zone of the fluidized bed reactor through the inlet to the accelerator gas is vapor from water or nitrogen, the linear velocity of the gas staying in a range of 1.0 to 10.0

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15/33 m / s.

[044] In one embodiment, the oxygenates comprise one or more selected from a group consisting of methanol, ethanol, n-propyl alcohol, isopropyl alcohol, C4-C20 alcohol, ethyl methyl ether, dimethyl ether, diethyl ether, diisopropyl ether, methanal , dimethyl carbonate, acetone and acetic acid and the weight of the oxygenates is responsible for 10 to 100% of the raw material.

[045] When compared with the prior art, the present disclosure has the following advantages. A guide plate is arranged in the fluidized bed reactor according to the present disclosure, so that the catalysts in it can be distributed homogeneously, so that the efficiency of the reaction can be improved. In addition, the reaction regeneration apparatus according to the present disclosure not only has high reaction efficiency, but also high efficiency of gas and solids separation. As a result, the yield of the product can also be increased.

BRIEF DESCRIPTION OF THE DRAWINGS [046] The present disclosure will be further described in detail based on the examples in view of the accompanying drawings. In the drawings:

[047] Figure 1 schematically shows a structure of a fluidized bed reactor according to an example of the present disclosure, [048] Figure 2 shows a space diagram of a guide plate according to example 1 of the present disclosure , [049] Figure 3 shows a view of the AA section in figure 2, [050] Figure 4 shows a space diagram of a guide plate according to example 2 of the present disclosure, [051] Figure 5 shows a space diagram of a guide plate according to example 3 of the present disclosure, [052] Figure 6 shows schematically a structure of a

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16/33 fluidized bed comprising a plurality of guide plates according to an example of the present disclosure, [053] Figure 7 schematically shows a reaction regeneration apparatus according to example 1 of the present disclosure, [054] Figure 8 schematically shows a separation device for use in the fluidized bed reactor according to example 1 of the present disclosure, [055J figure 9 schematically shows a separation device for use in the fluidized bed reactor according to example 2 of the present disclosure , [056] Figure 10 shows an enlarged view of section A in figure 7 according to an example of the present disclosure, [057] Figure 11 shows an enlarged view of section A in figure 7 according to another example of the present disclosure. and [058] Figure 12 shows schematically a reaction regeneration apparatus according to example 2 of the present disclosure.

[059] In the drawings, the same components are indicated with the same reference sign. Drawings are not drawn at full scale.

DETAILED DESCRIPTION OF THE MODALITIES [060] The present disclosure will be described more in view of the accompanying drawings.

[061] Figure 1 schematically shows a fluidized bed reactor 4 according to an example of the present disclosure. As shown in figure 1, the fluidized bed reactor 4 comprises an inlet zone 70 in a lower position, an outlet zone 42 in a higher position and a reaction zone 41 between inlet zone 70 and the inlet zone. outlet 42. A guide plate 48 is arranged in reaction zone 41.

[062] A plurality of guide plates 48 can be provided distributed along the axial direction of the fluidized bed reactor 4, as shown in figure 6.

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17/33

It should be understood that figure 6 shows merely in a schematic way the reaction zone 41 of the fluidized bed reactor 4 and two guide plates 48 arranged in the reaction zone 41. In fact, the number of guide plates 48 can be one, two or more based on the actual situation.

[063] Guide plate 48 can be used in reaction zone 41 of the fluidized bed reactor, so that the catalyst particles can be distributed more homogeneously in a radial direction. The guide plate 48 comprises a dense channel region 61 arranged in an intermediate region of it and a sparse channel region 62 arranged in a periphery thereof encompassing the dense channel region 61. The dense channel region 61 has a relatively large obstacle to the material moving upwards, while the sparse channel region 62 has a relatively small obstacle for it. Under the guide plate 48 in the fluidized bed reactor 4, the gas in the intermediate region will be forced to flow into the surrounding regions, so that the speed of the gas flowing through the sparse channel region 62 can be increased. In that case, above the guide plate 48, the gas velocity in the marginal regions of the circumference of the fluidized bed reactor 4 will be increased, so that the particles of the catalyst in the marginal regions of the circumference can be blown upwards. Under the influence of a fluidized bed reactor wall 4 and a general material flow in the fluidized bed reactor 4, the blown up catalyst particles flow into an intermediate section of the reaction zone 41 of the fluidized bed reactor 4 (a figure 6 schematically shows the directions of gas flow with arrows). As a result, the particles of the catalyst in the reaction zone 41 of the fluidized bed reactor 4 can be distributed more homogeneously in the radial direction, instead of being diluted in the medium while thick in the surrounding regions.

[064] Guide plate 48 is normally round in shape. The dense channel region 61 is round in shape and the sparse channel region 62 is shaped

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18/33 annular ring. The ratio of the diameter of the dense channel region 61 to the width of the sparse channel region 62 is in a range from 2: 1 to 9: 1, which can facilitate the assembly of the guide plate 48 in the fluidized bed reactor 4. Because it is necessary that the sparse channel region 62 is engaged with a wall of the fluidized bed reactor 4, an appropriate width of the sparse channel region 62 can make the assembly operation easier.

[065] The channel dimension in the dense channel region 61 is smaller than the channel dimension in the sparse channel region 62. For example, the ratio of the channel dimension in the dense channel region 61 to that of the channel in the region of sparse channel 62 is in a range of 1: 4 to 2: 3. Preferably, the channel size in the dense channel region 61 is in the range of 0.01 to 0.08 m. In that case, the bubbles of the reaction mass and the catalyst particle aggregates in the fluidized bed reactor 4 will be ruptured. Therefore, the homogeneity of the mixture between the reaction mass and the catalysts can be increased, and the contact area between the reaction mass and the catalysts can be increased, so the efficiency of the reaction can be further improved.

[066] Figures 2, 3, 4 and 5 respectively show multiple shapes of the guide plate 48. As shown in figures 2 and 3, the dense channel region 61 comprises a plurality of separate concentric ring-shaped plates. The space 66 between adjacent concentric ring-shaped plates 65 forms a channel. The sparse channel region 62 comprises straight panels 67 which are separated and substantially arranged along the radial directions of the guide plate 48 in parallel. The space 68 between adjacent straight panels 67 forms a channel. In one example, each of the plurality of concentric ring-shaped plates 65 is configured to tilt out with respect to a horizontal direction from the center of a circle and each of the plurality of straight panels 67 is configured to tilt with respect to to the horizontal direction. For example, a tilt angle

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19/33 can be in a range of 45 to 85 degrees.

[067] As shown in figure 4, both the channel in the dense channel region 61 and the channel in the sparse channel region 62 are square holes and the dimension of the square hole in the dense channel region 61 is smaller than that of the square hole in the sparse channel region 62. For example, the ratio of the dimension of the square hole in the dense channel region 61 to that of the square hole in the sparse channel region 62 can be in the range of 1: 4 to 2: 3. It should be understood that the shape of the channel is not limited to the square hole, it can also be a round hole, an elliptical hole or a hole of any other type.

[068] As shown in figure 5, the dense channel region 61 comprises a plurality of straight panels 69 separated in parallel and the space 80 between adjacent straight panels forms a channel. The sparse channel region 62 comprises straight panels 81 which are separated and substantially arranged along radial directions of the guide plate 48 in parallel and the space 82 between adjacent straight panels forms a channel. In one example, each of the plurality of straight panels 69 is configured to tilt out with respect to a horizontal direction from a center of a circle, and each of the plurality of straight panels 81 is configured to tilt with respect to the direction horizontal. For example, the tilt angle can be in a range of 45 to 85 degrees.

[069] Inlet 49 for accelerator gas is disposed in outlet zone 42 of the fluidized bed reactor 4. Preferably, inlet 49 for accelerator gas is configured to extend obliquely from a lower position to a position taller. In that case, the gas having high speed can be injected into the outlet zone 42 of the fluidized bed reactor 4 through the inlet 49 to the accelerator gas, so that the pressure in the fluidized bed reactor 4 can be more uniform, and the catalysts can be distributed more evenly in the fluidized bed reactor 4. As a result, product yield can also

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20/33 be higher. Inlet 49 for the accelerator gas forms an angle in a range of 5 to 39 degrees with respect to a vertical direction (that is, the longitudinal geometric axis of the fluidized bed reactor 4), for example, the angle can be 10 or 15 degrees. The diameter of the inlet 49 for the accelerator gas is smaller than that of the outlet zone 42. For example, the ratio of the diameter of the inlet 49 to the accelerator gas for that of the outlet zone 42 can be 0.05 or 0.1 . The ratio of the length L1 of a part of the outlet zone 42 of the fluidized bed reactor 4 which is above the inlet 49 for the accelerator gas to an overall length L2 of the outlet zone 42 of the fluidized bed reactor 4 lies in a range of 0.1 to 0.8. For example, the ratio can be 0.1 or 0.4.

[070] Figure 7 schematically shows a reaction regeneration apparatus 30 according to example 1 of the present disclosure. As shown in figure 7, the reaction regeneration apparatus 30 comprises a separation device 10, the fluidized bed reactor 4 and a catalyst regeneration device 50, as well as pipes for connecting the separation device 10, the bed reactor fluidized fluid 4 and the catalyst regeneration device 50.

[071] The outlet zone 42 of the fluidized bed reactor 4 is in communication with the preliminary gas and solids separator 7 of the separation device 10. The raw material and the catalysts react in the reaction zone 41 and generate the product. The product loads the partial catalysts and leaves the fluidized bed reactor 4 through the outlet zone 42.

[072] The catalyst regeneration device 50 comprises a feed zone 51 in a lower position and a discharge zone 52 in a higher position. The catalyst regeneration device 50 is used to reactivate the catalysts that are spent in the fluidized bed reactor 4 and have lost activity.

[073] As shown in figure 8, the separation device 10 according to

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21/33 with example 1 of the present disclosure is generally used in conjunction with the fluidized bed reactor 4. Specifically, the separation device 10 is configured to receive the product having catalysts loaded in it from an outlet of the product 12 from the fluidized bed reactor 4. After the product flows through the separation device 10, the catalysts loaded on it are separated from it. The separation device 10 will be described in detail.

[074] As shown in figure 8, the separation device 10 comprises a preliminary gas and solids separator 7, a draft register 15 and a fine gas and solids separator 9 arranged in an order according to the flow direction of the product. The preliminary gas and solids separator 7 is directly in communication with the fluidized bed reactor 4 to receive the product from the fluidized bed reactor 4. The draft register 15 is vertically arranged and an inlet hole 16 is arranged in an upper region 8 of the draft register 15. A gas outlet 18 of the preliminary gas and solids separator 7 is in communication with the inlet port 16, and a solids outlet 19 of the preliminary gas and solids separator 7 is in communication with a region lowest 6 of the draft register 15. An outlet orifice 14 is further arranged in the highest region 8 of the draft register 15 in a position offset from the inlet 16. An inlet 20 of the fine gas and solids separator 9 lies in communication with the outlet orifice 14 in the highest region 8 of the draft register 15 and a solids outlet 21 of the fine gas and solids separator 9 is in communication with the lowest region 6 of the circulation record 15.

[075] In an example as shown in figure 8, the preliminary gas and solids separator 7 is a cyclone separator and the fine gas and solids separator 9 can also be a cyclone separator. The cyclone separator 7 and cyclone separator 9 can have the same specification or different specifications. In one example, if the cyclone separator 9 has a different specification than the separator

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22/33 of cyclone 7, cyclone separator 9 can be selected to be able to separate particles of smaller particle size when compared to cyclone separator 7.

[076] During the operation of the separation device 10, the product of the fluidized bed reactor 4 having catalysts loaded in it is fed into the preliminary gas and solids separator 7 first. Most of the catalyst particles are separated from the product in the preliminary gas and solids separator 7 and fed into the lower region 6 of the run register 15. The product transports the remaining small amount of the catalysts into the upper region 8 from the run record 15. The product appropriately slows down in the highest region 8 and enters the fine gas and solids separator 9. The remaining catalysts are separated from the product and fed into the lowest region 6 in the run record 15. The product is obtained from a gas outlet 22 of the fine gas and solids separator 9.

[077] Because both the preliminary gas and solids separator 7 and the fine gas and solids separator 9 can be cyclone separators, the separation rate of the product catalysts can be greatly increased. As a result, the product will not experience a side reaction and the final product may contain very few impurities.

[078] Preferably, the position where the gas outlet 18 of the preliminary gas and solids separator 7 is connected with the draft register 15 is below a position where the inlet 20 of the fine gas and solids separator 9 is connected with the draft register 15. As a set, the preliminary gas and solids separator 7 is disposed in a lower position and the fine gas and solids separator 9 is disposed in a higher position. In this case, the product of the preliminary gas and solids separator 7 can only move upwards in the highest region 8 of the run register 15, in order to leave the run register 15 and enter the

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23/33 fine separator of gas and solids 9. During the movement of the product, the remaining catalysts loaded in it can be precipitated. As a result, the efficiency of the separation of gas and solids can be improved.

[079] Preferably, the inlet hole 16 in the highest region 8 of the draft register 15 is configured to be tangent to a side wall of the highest region 8. In this case, the fluidized bed reactor product 4 can be fed into the highest region 8 on a path that is tangent to the side wall of the highest region 8. As a result, the impact of the product on the run register 15 and the highest region 8 can be reduced, so that the vibration of the run record 15 can be relieved.

[080] The run register 15 can be a container of variable diameter. As shown in figure 8, the diameter of the highest region 8 of the circulation record 15 is smaller than that of its lowest region 6. The ratio of the diameter of the highest region 8 to that of the lowest region 6 is in a range from 0.05 to 0.5. For example, the ratio can be 0.08, 0.1.0.12 or 0.3. As a set, the upper region 8 appears to be a tubular piece vertically arranged in the lower region 6. The reason for configuring the above structure for the run register 15 is that the upper region 8 can actually function as a flow passage of gas rather than a container to accommodate substances, while the lower region 6 can function as a container to accommodate catalysts. A draft register 15 with such a structure can have a settler with a much smaller diameter than a draft register 15 in the prior art, thereby reducing the production cost of the apparatus.

[081] In a preferred example, a steam inlet 5 is arranged at a lower end of the draft register 15 and the structure or component (not shown in the drawings) for use in the steam removal operation can be arranged inside the lowest region 6 of the circulation record 15. The structure

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24/33 or the component is well known to the person skilled in the art, so it will not be described in detail here. In this case, the lower region 6 of the draft register 15 can form an extractor, so that the removal of steam can be performed on the product loaded in the catalysts of the lower region 6 in the process of separating gas and solids, thereby further improving product performance. In a specific example, water vapor can be used to remove steam.

[082] Figure 9 shows a separation device 10 'in accordance with example 2 of the present disclosure. Figure 9 does not show a fluidized bed reactor coordinating with the separation device 10 '. However, it is easy to understand that the connection mode between the separation device 10 'and the fluidized bed reactor is the same as that between the separation device 10 and the fluidized bed reactor as shown in figure 8, which will not be described in detail.

[083] The separation device 10 'is different from the separation device 10 only in its fine separator of gas and solids. In the separation device 10 'as shown in figure 9, a fine gas and solids separator 9' comprises two- or multiple-stage cyclone separators (figure 9 merely shows schematically the two stages 91 'and 92'). These separators can all be cyclone separators or a combination of multiple types of separators.

[084] The two or more stages of the cyclone separators in series connection are configured, so that the input of a cyclone separator of the first stage 91 'is in communication with the highest region 8 of the circulation register 15, the product being obtained from a gas outlet of a second cyclone separator 92 '. In addition, the gas outlet of the cyclone separator of the first stage 91 'is in communication with the input of the cyclone separator of the second stage 92'. The solids outlets of both the first stage 91 'cyclone separator and the second stage 92' cyclone separator are in communication

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25/33 with the lowest region 6 of the draft register 15. It should be noted that the cyclone separator of the first stage 91 'is selected to separate catalysts with relatively large mass and the cyclone separator of the second stage 92' is selected to separate catalysts with relatively small mass. The multiple stages of cyclone separators in series connection are similar in structure to the two stages of cyclone separators in series connection, so they will not be described in detail here.

[085] The catalyst separation effect of the product can be improved through said 9 'fine gas and solids separator, thereby the recovery efficiency of the catalyst can be improved. In the meantime, the product obtained contains less impurities.

[086] In order to save energy, the feed zone 51 of the catalyst regeneration device 50 is arranged lower than the lower region 6 of the draft register 15 and its discharge zone 52 is arranged higher than the inlet zone 70 of the fluidized bed reactor 4, so that gravity can be used to drive the flow of the catalysts between the separating device 10, the fluidized bed reactor 4 and the regenerating device of the catalyst 50. In addition , the lower region 6 of the draft register 15 is in communication with the supply zone 51 of the catalyst regeneration device 50 through a second pipe 43 and the discharge zone 52 of the catalyst regeneration device 50 is in communication with the inlet zone 70 of the fluidized bed reactor 4 through a third pipe 44. In that case, inactive catalysts can enter the regeneration device of catalyst 50 from the re the draft register 15 through the second pipe 43 under gravity and be regenerated therein. The regenerated catalysts automatically enter the fluidized bed reactor 4 from the catalyst regeneration device 50 through the third pipe 44. Throughout the process, the catalysts

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26/33 need to be raised only on the catalyst 50 regeneration device. Since the catalysts are light, a high pressure gas from the bottom of the catalyst 50 regeneration device is merely necessary to elevate the catalysts. Therefore, the power consumption to drive the flow of the catalysts can be greatly reduced and the device can be simplified. Although the second pipe 43 and the third pipe 44 appear to be crossed as shown in figure 7, in the actual apparatus, the second pipe 43 and the third pipe 44 are not crossed, but preferably two straight lines in different planes.

[087] It should be understood that the second pipe 43 is provided with a control valve 46 and the third pipe 44 is provided with a control valve 45, so that the flow of the catalysts can be controlled.

[088] As shown in figure 10 and figure 11, the third pipe 44 is provided with a flow blocking member 47 tilting towards the fluidized bed reactor 4 at the top of its inner wall. Figure 10 shows an example of flow blocking member 47. According to the example as shown in figure 10, flow blocking member 47 is in the form of a deflector 47. Deflector 47 can effectively block gas and catalysts flowing backwards into the third pipe 44 caused by the strong reaction in the fluidized bed reactor 4, so that the circulation rate of the catalysts can be increased, thereby further increasing the product yield. In a specific example, the ratio of the area of the deflector 47 to an area of the cross section of the third pipe 44 is in a range of 0.1 to 1, for example, the ratio can be 0.3, 0.45 or 0, 8. In addition, deflector 47 is sector-shaped or rectangular or even semicircular. The ratio of the distance between the baffle 47 and the fluidized bed reactor 4 to the length of the third pipe 44 is in a range of 0.01 to 0.5, for example, the ratio can be 0.2, 0.3 or 0.4. The angle formed between the deflector 47 and the geometric axis of the third pipe 44 is in a range of 10 to 75 degrees, for example, the

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27/33 angle can be 15 degrees, 10 degrees, 30 degrees or 45 degrees. It should be understood that there may also be a plurality of baffles 47 arranged in parallel as shown by the dashed line in figure 10.

[089] Figure 11 shows a flow blocking member 47 according to another example. As shown in figure 11, the flow blocking member 47 can be configured as a stop latch projecting radially inward from the top of the inner wall of the third pipe 44. There can be a plurality of stop latches 47 arranged in a row along the geometric axis of the third pipe 44. In order to effectively block the gas and catalysts flowing back from the fluidized bed reactor 4 to the third pipe 44, the ratio of the length of each stop tongue 47 to the diameter of the third pipe 44 is configured in a range of 0.1 to 0.5 and the cross section of each of the stop tabs 47 is in the form of a triangle, a rectangle or a sector.

[090] The reaction regeneration apparatus 30 as shown in figure 7 can be used to prepare aromatic hydrocarbons from oxygenates. Because the preparation of aromatic hydrocarbons requires catalysts with high activity, the catalysts fed into the fluidized bed reactor 4 must be completely regenerated. A process for preparing aromatic hydrocarbons from oxygenates using reaction regeneration apparatus 30 will be described in detail.

[091] Figure 12 schematically shows a 30 'reaction regeneration apparatus according to example 2 of the present disclosure. The reaction regeneration apparatus 30 'is similar to the reaction regeneration apparatus 30 as shown in figure 7 in the structure. The difference lies only in that the inlet zone 70 of the fluidized bed reactor 4 is arranged lower than the lower region 6 of the draft register 15 of the separation device 10, and the lower region 6 of the draft register 15 is in communication with entrance zone 70 of the

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28/33 fluidized bed reactor 4 through a first pipe 53. The first pipe 53 is also provided with a control valve 54.

[092] The 30 'reaction regeneration apparatus as shown in figure 12 can be used to prepare olefins from oxygenates. Because the preparation of olefins requires catalysts with moderate activity, the catalysts fed into the fluidized bed reactor 4 must comprise unregenerated catalysts, so that the general activity of the catalysts can be reduced. A process for preparing olefins from methanol using the 30 'reaction regeneration apparatus will be described in detail.

[093] The process for preparing aromatic hydrocarbons will be described based on the reaction regeneration apparatus as shown in figure 7. Aromatic hydrocarbons are generally prepared from raw materials containing oxygenates. For example, oxygenates may comprise one or more selected from a group consisting of methanol, ethanol, n-propyl alcohol, isopropyl alcohol, C4-C20 alcohol, ethyl methyl ether, dimethyl ether, diethyl ether, diisopropyl ether, methanal, dimethyl carbonate , acetone and acetic acid. The weight of oxygenates is responsible for 10 to 100% of the raw material.

[094] The raw material containing oxygenates and catalysts reacts in reaction zone 41 of the fluidized bed reactor 4. In one example, the catalysts are ZSM-

5. The pressure in the fluidized bed reactor 4 indicated by the gauge pressure is in a range from 0 to 0.6 MPa, the average temperature in it is in a range from 440 to 550 ^a C, the spatial speed in the reaction zone is in a range of 0.3 to 5 h ¹ and the average density in the reaction zone is in a range of 200 to 450 kg / m ³ . The ratio of the pressure drop generated when the raw material flows through the dense channel region 61 to that generated when the raw material flows through the sparse channel region 62 is in the range of 1.2: 1 to 10: 1 .

[095] The product obtained and the catalysts loaded in the product are

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29/33 fed into the separation device 10 through outlet zone 42 of the fluidized bed reactor 4. The operation of the separation device 10 comprises the following steps. First, the product from the fluidized bed reactor 4 having the catalysts loaded in it is preliminarily separated via the preliminary gas and solids separator 7. Then, the product obtained from the preliminary separation by loading the remaining catalysts is fed into the upper region 8 from the draft register 15. Subsequently, the product is removed from the draft register 15 and fed into the fine gas and solids separator 9 for fine separation. The product is obtained from the gas outlet of the fine gas and solids separator 9 and the catalysts of the preliminary gas and solids separator 7 and the fine gas and solids separator 9 are collected within the lower region 6 of the circulation register 15.

[096] The catalysts in the lower region 6 of the draft register 15 are fed into the catalyst regeneration device 50 through the second pipe 43 to be regenerated. In one example, a catalyst regeneration medium is air and the regeneration temperature is in the range of 550 to 650 O.

[097] The regenerated catalysts are fed into the inlet zone 70 of the fluidized bed reactor 4 through the third pipe 44. Subsequently, the regenerated catalysts can be pushed by the feed gas, such as methanol, into the reaction zone. 41 of the fluidized bed reactor 4 again for reaction.

[098] In a preferred example, the inlet 49 for the accelerator gas is disposed in the outlet zone 42 of the fluidized bed reactor 4. The gas flowing into the outlet zone 42 of the fluidized bed reactor 4 through the inlet 49 for the accelerator gas is water vapor or nitrogen, the linear velocity of the gas being in a range of 1.0 to 10.0 m / s.

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30/33 [099] In another preferred example, the water vapor is fed into the draft register 15 from its lowest end, so that the product loaded on the catalysts is separated from the catalysts.

[0100] The process for preparing the olefins from methanol will be described based on the reaction regeneration apparatus as shown in figure 12. In the reaction regeneration apparatus as shown in figure 12, the inlet zone 70 of the bed reactor fluidized 4 is disposed lower than the lower region 6 of the draft register 15 and the lower region 6 of the draft register 15 communicates with the inlet zone 70 of the fluidized bed reactor 4 through the first pipe 53.

[0101] Methanol and catalysts react in reaction zone 41 of the fluid bed reactor 4. In one example, the catalysts are of molecular mesh, such as SAPO-34. The pressure in the fluid bed reactor 4 by the gauge pressure is in a range of 0 to 0.4 MPa, the average temperature in it is in the range of 380 to 550 Ό and the average density in the reaction zone is in a range of 40 to 200 kg / m ³ . The ratio of the pressure drop generated when the raw material flows through the dense channel region 61 to that generated when the raw material flows through the sparse channel region 62 is in the range of 1.2: 1 to 10: 1 .

[0102] The product obtained and the catalysts loaded in the product are fed into the separating device 10 through the outlet zone 42 of the fluidized bed reactor 4. An operation of the separating device 10 comprises the following steps. First, the product of the fluidized bed reactor 4 having the catalysts loaded in it is preliminarily separated through the preliminary gas and solids separator 7. Next, the product obtained from the preliminary separation by loading the remaining catalysts is fed into the highest region 8 from the run register 15. Subsequently, the product is removed from the run register 15 and fed into the fine gas and solids separator 9

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31/33 for fine separation. The product is obtained from the gas outlet of the fine gas and solids separator 9, and the catalysts of the preliminary gas and solids separator 7 and the fine gas and solids separator 9 are collected within the lower region 6 of the circulation register 15 .

[0103] A portion of the catalysts in the lower region 6 of the draft register 15 is fed directly into the inlet zone 70 of the fluidized bed reactor 4 through the first pipe 53. The remaining catalysts are fed into the regeneration device of the catalyst 50 through the second pipe 43 to be regenerated. The regenerated catalysts are fed into the inlet zone 70 of the fluidized bed reactor 4 through the third pipe 44 and mixed with the unregenerated catalysts. In one example, a catalyst regeneration medium is air and the regeneration temperature is in the range of 600 to 700 O.

[0104] Subsequently, the catalysts in the inlet zone 70 can be pushed by the feed gas, such as methanol, into the reaction zone 41 of the fluidized bed reactor 4 again for reaction.

[0105] In a preferred example, the inlet 49 for the accelerator gas is arranged in the outlet zone 42 of the fluidized bed reactor 4. The gas flowing into the outlet zone 42 of the fluidized bed reactor 4 through the inlet 49 for the accelerator gas is water vapor or nitrogen, the linear velocity of the gas being in a range of 1.0 to 10.0 m / s.

[0106] In another preferred example, the water vapor is fed into the draft register 15 from its lowest end, so that the product loaded on the catalysts can be separated from the catalysts.

[0107] The inventor carried out the example to prepare aromatic hydrocarbons using the process according to the present disclosure and the reaction regeneration apparatus as shown in figure 12 and made a comparison with

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32/33 process for preparing aromatic hydrocarbons in the prior art. In the examples, the raw materials and catalysts for each experiment are the same and the experiment parameters are conventional parameters for the reaction. The relevant data for the reaction regeneration apparatus and the product yield are shown in table I.

good I

Example s Guide plate types 48 Number turn guide plate 48 Relationship of the channel dimension of the dense channel region to that of the sparse channel region 0 Inlet 49 for gas accelerates pain Deflet or47 Print run 15 Separates preliminary pain from gas and solids 7 Separates fine gas and solids pain 9 Yield 1 Shows owner figure 2 1 2/3 4 Yes Variable diameter Yes Yes 53.8% 2 Shows owner figure 4 3 1/3 4 Yes Variable diameter Yes Yes 56.6% 3 Shows owner figure 5 3 1/4 4 Yes Variable diameter Yes Yes 55.1% Comparison example 1 0 0 No Sediment ador No No 51.2%

[0108] As shown in table I, according to the reaction regeneration apparatus and the process of the present disclosure, the yield of the

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33/33 aromatic hydrocarbons can be increased notably. For example, the yield of aromatic hydrocarbons can be increased by a maximum of 5%, which is a great improvement for chemical enterprises with large production.

[0109] Although the present disclosure has been described in view of preferred embodiments, various modifications and variations to the present disclosure can be made by anyone skilled in the art, without departing from the scope and spirit of the present disclosure. In particular, as long as there is no structural conflict, several modalities, as well as the respective technical aspects mentioned here, can be combined with each other in any way. The present disclosure is not limited to the specific examples disclosed here, but preferably includes all technical solutions that fall within the scope of the claims.

Claims (36)

1. Fluidized bed reactor, comprising an inlet zone in a lower position, an outlet zone in a higher position and a reaction zone between the inlet zone and the outlet zone, CHARACTERIZED by the fact that a plate guide is arranged in the reaction zone, comprising a region of dense channel in an intermediate region of yours and a region of sparse channel arranged in a periphery of yours covering the region of dense channel. 2. Fluidized bed reactor according to claim 1, CHARACTERIZED by the fact that the dimension of a channel in the dense channel region is smaller than that of a channel in the sparse channel region. 3. Fluidized bed reactor, according to claim 2, CHARACTERIZED by the fact that the ratio of the channel dimension in the dense channel region to that of the channel in the sparse channel region is in a range from 1: 4 to 2: 3. 4. Fluidized bed reactor, according to claim 3, CHARACTERIZED by the fact that the channel dimension in the dense channel region is in a range of 0.01 to 0.08 m. Fluidized bed reactor according to any one of claims 1 to 4, CHARACTERIZED by the fact that each of the dense channel and sparse channel region comprises a circular plate having equally distributed pores, or a plurality of panels inclined in a separate concentric ring shape or a plurality of straight panels separated in parallel. 6. Fluidized bed reactor according to any one of claims 1 to 5, CHARACTERIZED by the fact that the dense channel region is round in shape and the sparse channel region is annular ring in shape, and the diameter ratio from the dense channel region to the width of the Petition 870170084340, of 11/01/2017, p. 47/65 2/9 sparse channel is in a range from 2: 1 to 9: 1. Fluidized bed reactor according to any one of claims 1 to 6, characterized by the fact that a plurality of guide plates are provided, which are distributed along the axial direction of the fluidized bed reactor. Fluidized bed reactor according to any one of claims 1 to 7, CHARACTERIZED by the fact that the inlet for the accelerator gas is arranged in the outlet area of the fluidized bed reactor. 9. Fluidized bed reactor according to claim 8, CHARACTERIZED by the fact that the inlet for the accelerator gas is configured to extend obliquely from a lower position to a higher position. 10. Reaction regeneration apparatus, comprising the fluidized bed reactor according to any one of claims 1 to 9 and further comprising a separation device and a catalyst regeneration device respectively connected with the fluidized bed reactor, CHARACTERIZED by the fact that the separation device comprises a preliminary separator of gas and solids in communication with an outlet zone of the fluidized bed reactor; a vertically arranged draft register, a lower region of the draft register being in communication with a solids outlet of the preliminary gas and solids separator to collect particles from the catalyst and a higher region of the draft register in communication with an outlet of preliminary gas and solids separator gas and a thin gas and solids separator, a gas and solids separator inlet communicating with the highest region of the draft register and its solids outlet communicating with the lowest region of the draft register and the regeneration device of the catalyst comprises a zone of Petition 870170084340, of 11/01/2017, p. 48/65 3/9 feed in a lower position and a discharge zone in a higher position, the feed zone being arranged lower than the lower region of the draft register and the discharge zone being arranged higher than the inlet area of the fluidized bed reactor, in which the lower region of the draft register is in communication with the supply zone of the catalyst regeneration device through a second pipe, and the discharge zone of the catalyst regeneration device it is in communication with the entrance area of the fluidized bed reactor through a third pipe. 11. Reaction regeneration apparatus, according to claim 10, CHARACTERIZED by the fact that the diameter of the highest region of the draft register is smaller than that of its lowest region. 12. Reaction regeneration apparatus according to claim 10 or claim 11, CHARACTERIZED by the fact that both the preliminary gas and solids separator and the fine gas and solids separator are cyclone separators. 13. Reaction regeneration apparatus according to claim 10 or claim 11, CHARACTERIZED by the fact that the preliminary gas and solids separator is a cyclone separator, and the fine gas and solids separator comprises cyclone separators of two or multi-stage, in which the two- or multi-stage series cyclone separators are configured, so that the input of a first stage cyclone separator is in communication with the highest region of the draft register, the product of gas being obtained from a gas outlet of a cyclone separator of the last stage, a gas outlet of an upstream cyclone separator communicates with an input of an adjacent downstream cyclone separator and the solids outlets of all cyclone separators are in communication with the Petition 870170084340, of 11/01/2017, p. 49/65 4/9 lowest region of the run record. 14. Reaction regeneration apparatus according to any one of claims 10 to 13, CHARACTERIZED by the fact that the lower region of the draft register is configured and arranged, so that it performs a steam extraction operation. 15. Reaction regeneration apparatus according to claim 10, CHARACTERIZED by the fact that the third pipe is provided with a flow blocking member on top of its internal wall. 16. Reaction regeneration apparatus according to claim 15, CHARACTERIZED by the fact that the flow blocking member is an inclined deflector for the fluidized bed reactor. 17. Reaction regeneration apparatus according to claim 16, CHARACTERIZED by the fact that a plurality of deflectors are provided, which are arranged in parallel with respect to each other. 18. Reaction regeneration apparatus according to claim 15, CHARACTERIZED by the fact that the flow blocking member is a stop latch projecting radially inward. 19. Reaction regeneration apparatus according to claim 18, CHARACTERIZED by the fact that a plurality of stop tabs is provided, which is arranged in a row along the geometric axis of the third pipe. 20. Reaction regeneration apparatus, according to claim 19, CHARACTERIZED by the fact that the ratio of the length of each stop tab to the diameter of the third pipe is in a range of 0.1 to 0.5. 21. Reaction regeneration apparatus according to any one of claims 10 to 20, CHARACTERIZED by the fact that the inlet area of the fluidized bed reactor is arranged lower than the lower region of the register Petition 870170084340, of 11/01/2017, p. 50/65 5/9 draft of the separation device and the lower region of the draft register is in communication with the entrance area of the fluidized bed reactor through a first pipe. 22. Process for preparing olefins, using a reaction regeneration apparatus according to claim 10, wherein the inlet area of the fluidized bed reactor is arranged lower than the lowest region of the draft register of a device of separation, and the lower region of the draft register is in communication with the entrance area of the fluidized bed reactor through a first pipe, CHARACTERIZED by the fact that the process comprises: reacting the gaseous raw material containing oxygenates with catalysts in a reaction zone of the fluidized bed reactor; feeding the product obtained and the catalysts loaded into the separation device through an outlet area of the fluidized bed reactor; separate the product from the loaded catalysts through the separation device, feeding a portion of the catalysts obtained from the separation directly into the fluidized reactor inlet zone, subsequently regenerating the remaining catalysts and feeding the regenerated catalysts into the inlet zone of the fluidized bed reactor and mix the unregenerate catalysts and regenerated catalysts in the fluidized bed reactor inlet area and then feed the mixed catalysts into the fluidized bed reactor reaction zone. 23. Process according to claim 22, CHARACTERIZED by the fact that the weight ratio of non-regenerated catalysts to regenerated catalysts is in the range of 0.3 to 1.5. 24. Process according to claim 22 or claim 23, Petition 870170084340, of 11/01/2017, p. 51/65 6/9 CHARACTERIZED by the fact that the operation of the separation device comprises: preliminarily separate the product from the fluidized bed reactor having catalysts loaded into it through a preliminary gas and solids separator, feed the product obtained from the preliminary separation by loading the remaining catalysts into the highest region of the draft register, taking the gas product out of the draft register and feed it into a fine gas and solids separator for fine separation and obtain the final gas product from a gas outlet of the fine gas and solids separator and collect the catalysts from the preliminary separator of gas and solids and the fine separator of gas and solids into the lower region of the draft register. 25. Process according to claim 24, CHARACTERIZED by the fact that the water vapor is fed into the draft register by its lower end, so that the product loaded in the catalysts is separated from the catalysts. 26. Process according to any of claims 22 to 25, CHARACTERIZED by the fact that the pressure in the fluidized bed reactor by the gauge pressure is in a range of 0 to 0.4 MPa, the average temperature in it is in a range 380 to 550 ° C and the average density in the reaction zone is in a range of 40 to 200 kg / m ³ and the catalyst used in it is SAPO-34, in which a catalyst regeneration medium is air and regeneration temperature is in the range of 600 to 700 ° C. 27. Process according to claim 22, CHARACTERIZED by the fact that the ratio of the pressure drop generated when the gaseous raw material flows through the dense channel region to that generated when the raw material Petition 870170084340, of 11/01/2017, p. 52/65 7/9 gas flows through the sparse channel region in a range of 1.2: 1 to 10: 1. 28. Process according to claim 26 or 27, CHARACTERIZED by the fact that the inlet for the accelerator gas is arranged in the outlet area of the fluidized bed reactor, and the gas flowing into the outlet area of the bed reactor fluidized through the entrance to the accelerator gas is water vapor or nitrogen, the linear velocity of the gas staying in a range of 1.0 to 10.0 m / s. 29. Process according to any of claims 22 to 28, CHARACTERIZED by the fact that the oxygenates comprise one or more selected from a group consisting of methanol, ethanol, n-propyl alcohol, isopropyl alcohol, C4-C20 alcohol, ethyl methyl ether, dimethyl ether, diethyl ether, diisopropyl ether, methanal, dimethyl carbonate, acetone and acetic acid and the weight of the oxygenates is responsible for 10 to 100% of the raw material. 30. Process for the preparation of aromatic hydrocarbons, using a reaction regeneration apparatus according to claim 10, CHARACTERIZED by the fact that the process comprises: reacting the raw material containing oxygenates with catalysts in a reaction zone of a fluidized bed reactor; feed the product obtained and the catalysts loaded in it into a separation device through an exit zone of the fluidized bed reactor and separate the product from the catalysts loaded therein in the separation device, regenerate the catalysts obtained from the separation and feed the catalysts regenerated into the inlet area of the fluidized bed reactor and subsequently into the reaction zone of the fluidized bed reactor. Petition 870170084340, of 11/01/2017, p. 53/65 8/9 31. Process according to claim 30, CHARACTERIZED by the fact that the operation of the separation device comprises: preliminarily separate the product from the fluidized bed reactor having the catalysts loaded in it through a preliminary gas and solids separator, feed the producer obtained from the preliminary separation by loading the remaining catalysts into the highest region of the draft register, take the product to off the run register and feed the product into a fine gas and solids separator for fine separation and obtain the final product from a gas outlet of the fine gas and solids separator and collect the catalysts from the preliminary gas separator and solids and the fine gas and solids separator into the lower region of the draft register. 32. Process according to claim 31, CHARACTERIZED by the fact that the water vapor is fed into the draft register from its lowest end, so that the product loaded in the catalysts is separated from the catalysts. 33. Process according to any one of claims 30 to 32, CHARACTERIZED by the fact that the pressure in the fluidized bed reactor by the gauge pressure is in a range of 0 to 0.6 MPa, the average temperature in it is in a range from 440 to 550 ° C, the spatial velocity in the reaction zone is in a range of 0.3 to 5 ír ¹ and the average density in the reaction zone is in a range of 200 to 450 kg / m ³ and the catalyst used it is ZSM-5, in which the catalyst regeneration medium is air and the regeneration temperature is in the range of 550 to 650 ° C. 34. Process according to claim 30, CHARACTERIZED by the fact that the ratio of the pressure drop generated when the gaseous raw material flows through the dense channel region to that generated when the raw material Petition 870170084340, of 11/01/2017, p. 54/65 Gaseous 9/9 flows through the sparse channel region in a range of 1.2: 1 to 10: 1. 35. Process according to claim 33 or claim 34, CHARACTERIZED by the fact that the inlet for the accelerator gas is arranged in the outlet zone of the fluidized bed reactor, and the gas flowing into the outlet zone of the reactor of fluidized bed through the entrance to the accelerator gas is water vapor or nitrogen, the linear velocity of the gas staying in a range of 1.0 to 10.0 m / s. 36. Process according to any one of claims 30 to 35, CHARACTERIZED by the fact that the oxygenates comprise one or more selected from a group consisting of methanol, ethanol, n-propyl alcohol, isopropyl alcohol, C4-C20 alcohol, ethyl methyl ether, dimethyl ether, diethyl ether, diisopropyl ether, methanal, dimethyl carbonate, acetone and acetic acid and the weight of the oxygenates is responsible for 10 to 100% of the raw material.