Fluidized bed reactor for particle reaction and control method

Abstract

The invention discloses a fluidized bed reactor for particle reaction and a control method.The fluidized bed reactor comprises a reaction unit, a feeding unit and a first cyclone separator, the reaction unit comprises a first shell, and the first shell comprises a first cavity and a second cavity which communicate with each other; the first opening and the second opening are communicated with the first cavity, the third opening is communicated with the second cavity, and the third opening is used for being communicated with an external air source; the feeding unit comprises a first pipeline, the first pipeline extends into the first cavity from the first opening and penetrates through the first cavity to reach the second cavity, and a material conveying opening of the first pipeline is formed in the second cavity; the first cyclone separator is arranged in the first cavity, and an outlet of the first cyclone separator is communicated with the second opening. According to the embodiment provided by the invention, the fluidized bed reactor provided by the invention can improve the treatment efficiency of the to-be-treated particles.

Description

Technical Field

[0001] This application relates to the field of chemical reaction devices, and particularly to a fluidized bed reactor for particle reaction and a control method thereof. Background Art

[0002] When using particulate matter as a raw material for processing and preparation, some unwanted substances carried by the particulate matter will affect the processing and preparation. For example, when the particulate matter is used as a catalyst or a reactant, during its processing and use, the particulate matter will carry some unwanted substances, and the particulate matter can be a carbon-containing substance, such as coke or graphite. These unwanted substances on the particulate matter will affect its participation in processing and preparation as a reactant or a catalyst. In the related art, a gas that does not react with the particle body and reacts with the unwanted substance can be selected as the reaction gas, and the reaction gas reacts with the unwanted substance to remove unwanted substances such as coke on the particles. A fixed bed reactor can be used to provide reaction conditions for the particles to be treated, and the unwanted substances on the particles to be treated will react with the reaction gas to generate a gas that enters the gas phase, so as to reduce the unwanted substances on the particles to be treated, thereby achieving the removal of the unwanted substances on the particles to be treated.

[0003] The particles to be treated located in the fixed bed reactor are closely packed, and the gaps between the fixed bed reactors are small, resulting in low utilization rate of the reaction gas. It takes a long time to remove the carbon-containing substances on the fixed bed reactor to the required level, and the efficiency of treating the carbon-containing substances on the particles to be treated is low. Summary of the Invention

[0004] An embodiment of the present application provides a fluidized bed reactor for particle reaction and a control method thereof, aiming to solve the technical problem of low efficiency in treating carbon-containing substances on particles to be treated.

[0005] An embodiment of the first aspect of the present application provides a fluidized bed reactor for particle reaction and a control method thereof, including:

[0006] A reaction unit, including a first housing, the first housing includes a first chamber and a second chamber that are communicated, as well as a first opening and a second opening that are communicated with the first chamber, and a third opening that is communicated with the second chamber, and the third opening is used to communicate with an external gas source;

[0007] A feeding unit, including a first pipeline, the first pipeline extends into the first chamber from the first opening and passes through the first chamber to reach the second chamber, and the feeding port of the first pipeline is arranged in the second chamber;

[0008] A first cyclone separator is arranged in the first chamber, and the outlet of the first cyclone separator is communicated with the second opening.

[0009] According to any of the foregoing embodiments of the first aspect of the present application, the first chamber includes a sedimentation zone and a first tapered zone. The first cyclone separator is disposed in the sedimentation zone. The tapered zone connects the sedimentation zone and the second chamber, and the diameter of the tapered zone gradually decreases in the direction from the sedimentation zone to the second chamber.

[0010] According to any of the foregoing embodiments of the first aspect of the present application, the second chamber includes a straight pipe zone and a second tapered zone. The straight pipe zone connects the first chamber and the second tapered zone. The diameter of the second tapered zone gradually decreases in the direction from the first chamber to the straight pipe zone. One end of the second tapered zone away from the first chamber communicates with the third opening.

[0011] According to any of the foregoing embodiments of the first aspect of the present application, the reaction unit further includes a heater for heating the second chamber.

[0012] According to any of the foregoing embodiments of the first aspect of the present application, the fluidized bed reactor further includes:

[0013] A discharging unit disposed outside the first housing and communicating with the first pipeline.

[0014] According to any of the foregoing embodiments of the first aspect of the present application, the fluidized bed reactor further includes a filtering unit, and the filtering unit includes:

[0015] A second housing including a third chamber and a fourth chamber. The third chamber communicates with the second opening;

[0016] A filter for isolating the third chamber and the fourth chamber. The filter includes a filter housing disposed in the third chamber;

[0017] A first air pump communicating with the hollow chamber of the filter housing through the fourth chamber.

[0018] According to any of the foregoing embodiments of the first aspect of the present application, the filtering unit further includes:

[0019] An aggregate structure communicating with the third chamber;

[0020] A first valve disposed on the pipeline connecting the third chamber and the aggregate structure.

[0021] According to any of the foregoing embodiments of the first aspect of the present application, the aggregate structure communicates with the first pipeline, and the filtering unit further includes:

[0022] A second valve disposed on the pipeline connecting the aggregate structure and the first pipeline.

[0023] According to any of the foregoing embodiments of the first aspect of the present application, the filtering unit further includes a second pipeline and a third valve. The second pipeline connects the first cyclone separator and the second housing, and the third valve is disposed on the second pipeline;

[0024] The fluidized bed reactor further includes a third pipeline and a fourth pipeline. The third pipeline communicates with the first pipeline and the inlet of the discharging unit, and the fourth pipeline communicates with the inlet of the discharging unit and the second pipeline. The third valve and the discharging unit are in parallel.

[0025] In a second aspect, a control method for a fluidized bed reactor is provided. The method is applied to the fluidized bed reactor as described above, and the method includes:

[0026] Adding the particles to be processed into the second chamber through the first pipeline;

[0027] Introducing the reaction gas into the second chamber through the third opening, so that the unnecessary substances on the particles to be processed react with the reaction gas in the reaction gas;

[0028] Starting the first cyclone separator to switch the particles to be processed to the fluidized state. The particles to be processed move to the first chamber for gas-solid separation, and the separated particles to be processed fall back to the second chamber, and the separated gas is discharged from the second opening out of the first housing.

[0029] According to any of the foregoing embodiments of the second aspect of the present application, when the processing of the particles to be processed is completed, the method includes:

[0030] Closing the third valve, opening the fourth valve, and controlling the first air pump to suck air from the fourth chamber, so that the particles to be processed enter the discharging unit through the first pipeline.

[0031] According to any of the foregoing embodiments of the second aspect of the present application, after starting the first cyclone separator, it includes:

[0032] Opening the first valve to enable the powder intercepted by the filter to enter the aggregate unit;

[0033] Opening the second valve to enable the powder in the aggregate unit to enter the second chamber through the first pipeline.

[0034] In the fluidized bed reactor and control method for particle reaction provided by the embodiments of the present application, by providing that the first housing includes a first chamber and a second chamber that are connected, a first opening connected to the first chamber, and a third opening connected to the second chamber, and providing that a first pipeline extends from the first opening into the first chamber and passes through the first chamber to reach the second chamber, so that the first pipeline can transport the particles to be reacted through the first chamber to the second chamber, which is beneficial to the subsequent treatment of the particles to be reacted; by providing a first cyclone separator in the first chamber, the airflow generated by the first cyclone separator can drive the particles to be reacted and the reaction gas in the second chamber to move to the first chamber, avoiding the accumulation of the particles to be reacted in the second chamber, increasing the contact area between the particles to be reacted and the reaction gas, and increasing the reaction efficiency of the carbon-containing substances on the particles to be reacted and the reaction gas; in the first chamber, the particles to be reacted and the reaction gas are separated, so that the particles to be reacted can return to the second chamber again, so that the carbon-containing substances on the particles to be treated can react with the reaction gas entering from the third opening again to improve the removal effect of the carbon-containing substances on the particles to be treated. BRIEF DESCRIPTION OF THE DRAWINGS

[0035] Other features, objects, and advantages of the present application will become more apparent by reading the following detailed description of non-limiting embodiments with reference to the accompanying drawings, in which the same or similar reference numerals denote the same or similar features, and the drawings are not drawn to actual scale.

[0036] Figure 1 FIG. is a schematic structural diagram of a fluidized bed reactor provided by an embodiment of the first aspect of the present application;

[0037] Figure 2 FIG. is a schematic structural diagram of a fluidized bed reactor provided by an embodiment of the first aspect of the present application.

[0038] DESCRIPTION OF REFERENCE NUMERALS:

[0039] 11. First housing; 111. First chamber; 111a. Settling area; 111b. First tapered area; 112. Second chamber; 112a. Straight pipe area; 112b. Second tapered area; 113. First opening; 114. Second opening; 115. Third opening; 12. Preheater; 13. Heater;

[0040] 2. Feeding unit; 21. First pipeline; 211. Feeding port; V5. Fifth valve;

[0041] 3. First cyclone separator;

[0042] 4. Discharging unit;

[0043] 5. Filter unit; 51. Second housing; 511. Third chamber; 512. Fourth chamber; 52. Filter; 53. First air pump; 54. Aggregate structure; 55. Second pipeline;

[0044] 61. Third pipeline; 62. Fourth pipeline;

[0045] V1. First valve; V2. Second valve; V3. Third valve; V4. Fourth valve;

[0046] X. Vertical direction. Detailed implementation manners

[0047] The features and exemplary embodiments of various aspects of the present application will be described in detail below. For the purpose of making the objectives, technical solutions and advantages of the present application clearer, the present application will be further described in detail below with reference to the accompanying drawings and specific embodiments. It should be understood that the specific embodiments described herein are only configured to explain the present application and are not configured to limit the present application. For those skilled in the art, the present application can be implemented without some of these specific details. The following description of the embodiments is only intended to provide a better understanding of the present application by showing examples of the present application.

[0048] It should be noted that in this article, relational terms such as first and second are only used to distinguish one entity or operation from another entity or operation, and do not necessarily require or imply any actual relationship or order between these entities or operations. Moreover, the terms "include", "comprise" or any other variant thereof are intended to cover non-exclusive inclusion, so that a process, method, article or device including a series of elements not only includes those elements, but also includes other elements not expressly listed, or further includes elements inherent to such process, method, article or device. Without further limitation, the elements defined by the statement "including..." do not exclude the existence of additional identical elements in the process, method, article or device including the elements.

[0049] It should be understood that when describing the structure of a component, when a layer or a region is referred to as being "above" or "over" another layer or another region, it may mean directly above the other layer or another region, or there may be other layers or regions between it and the other layer or another region. And if the component is turned over, this layer or region will be "below" or "beneath" the other layer or region.

[0050] During the processing and use of particles as catalysts or other raw materials, some unwanted substances may be loaded on them. Such substances can be carbon-containing substances, such as coke or graphite. These unwanted substances on the particles to be treated will affect their participation in processing and preparation as reactants or catalysts. In related technologies, a gas that does not react with the particle body but reacts with the unwanted substances can be selected as the reaction gas. Then, the reaction gas can react with the unwanted substances to remove the coke and other unwanted substances on the particles. A fixed-bed reactor can be used to provide reaction conditions for the particles to be treated. The unwanted substances on the particles to be treated will react with the reaction gas to generate a gas that enters the gas phase, so as to reduce the unwanted substances on the particles to be treated, thereby achieving the removal of the unwanted substances on the particles to be treated.

[0051] The particles to be treated located in the fixed-bed reactor are closely packed, and the gaps between the fixed-bed reactors are small, resulting in low utilization rate of the reaction gas. It takes a long time to remove the carbon-containing substances on the fixed-bed reactor to the required level, and the efficiency of treating the carbon-containing substances on the particles to be treated is low.

[0052] Existing solutions cannot well solve the technical problems. To solve the above problems, the embodiments of the present application provide a fluidized-bed reactor. The following will describe the embodiments of the fluidized-bed reactor with reference to the accompanying drawings.

[0053] Please refer to Figure 1 , the fluidized-bed reactor includes a reaction unit, a feeding unit, and a first cyclone separator 3. The reaction unit includes a first housing 11. The first housing 11 includes a first chamber 111 and a second chamber 112 that are connected, as well as a first opening 113 and a second opening 114 that are connected to the first chamber 111, and a third opening 115 that is connected to the second chamber 112. The third opening 115 is used to communicate with an external gas source; the feeding unit includes a first pipeline 21. The first pipeline 21 extends into the first chamber 111 from the first opening 113 and passes through the first chamber 111 to reach the second chamber 112. The feeding port 211 of the first pipeline 21 is arranged in the second chamber 112; the first cyclone separator 3 is arranged in the first chamber 111, and the outlet of the first cyclone separator 3 is connected to the second opening 114.

[0054] The first housing 11 can provide a first chamber 111 and a second chamber 112 for the oxidation reaction of the particles to be processed to remove unwanted substances. One end of the first pipeline 21 can be connected to a container for placing the particles to be processed, and the particles to be processed can be transported to the second chamber 112 through the first pipeline 21. In this application, the first pipeline 21 extends into the first chamber 111 from the first opening 113, passes through the first chamber 111 to reach the second chamber 112, and the particles to be processed located in the first pipeline 21 can be isolated from the first chamber 111 through the first pipeline 21. The first opening 113 and the third opening 115 can be arranged along the vertical direction X, and the first chamber 111 can be located above the second chamber 112. The particles to be processed located in the first pipeline 21 can fall into the second chamber 112 by the action of gravity; they can also be pumped into the second chamber 112 by a transport pump. Optionally, a fifth valve V5 is provided on the first pipeline 21 to control the on-off between the material source and the second chamber 112. The fifth valve V5 can be a two-way ball valve or a gate valve.

[0055] The third opening 115 is in communication with an external gas source, so that the reaction gas provided by the external gas source can enter the second chamber 112 through the third opening 115. The reaction gas can be a mixed gas including reaction gases. For example: a mixed gas of oxygen, air, and nitrogen. The gases in the mixed gas can be mixed in any proportion according to needs. The particles to be processed can include a particle body and unwanted substances. The unwanted substances can be coated on or attached to the particle body and can be embedded in the particle body. Under suitable reaction conditions, the particle body located in the second chamber 112 does not react with the gas entering from the third opening 115, and the unwanted substances and the reaction gas located in the second chamber 112 can undergo a chemical reaction. The unwanted substances can be carbon-containing substances, such as: coke, graphite, etc. Optionally, the gas source includes oxygen, and at a certain temperature, the carbon-containing substances on the particle body react with oxygen.

[0056] The first chamber 111 is in communication with the second chamber 112, so that the particles to be processed and the reaction gas can move from the second chamber 112 to the first chamber 111 together. During the movement of the particles to be processed and the reaction gas, the unwanted substances on the particles to be processed and the reaction gas can continue to undergo an oxidation reaction.

[0057] A cyclone separator is a device used for separating gas-solid systems or liquid-solid systems. The cyclone separator generates a swirling airflow, and solid particles or liquid droplets in the airflow are affected by centrifugal force. The first cyclone separator 3 can be an internal cyclone separator. The first cyclone separator 3 is arranged in the first chamber 111, so that the airflow generated by the first cyclone separator 3 can drive the particles to be processed and the reaction gas in the second chamber 112 to move from the second chamber 112 to the first chamber 111. After the particles to be processed and the reaction gas move to the first chamber 111, the particles to be processed are thrown towards the wall of the first housing 11 under the action of centrifugal force. After the particles to be processed come into contact with the wall of the first housing 11, they lose their inertial force, and the particles to be processed fall along the wall of the first housing 11 towards the second chamber 112 and return to the second chamber 112, so that the unnecessary substances on the particles to be processed can react with the reaction gas entering from the third opening 115 again.

[0058] The first cyclone separator 3 generates a swirling downward outer vortex airflow. During the downward process, the airflow continuously flows into the central part of the separator, forming a centripetal radial airflow, and this part of the airflow constitutes a swirling upward inner vortex flow. Partially broken particles to be processed and unnecessary substances detached from the particles to be processed can be discharged from the first housing 11 through the second opening 114 along with the inner vortex flow, thereby reducing the broken particles to be processed and the unnecessary substances detached from the particles to be processed located in the first housing 11 and improving the quality of the particles to be processed retained in the first housing 11.

[0059] In this embodiment, by providing that the first housing 11 includes a first chamber 111 and a second chamber 112 that are connected, a first opening 113 connected to the first chamber 111, a third opening 115 connected to the second chamber 112, and arranging a first pipeline 21 to extend from the first opening 113 into the first chamber 111 and pass through the first chamber 111 to reach the second chamber 112, so that the first pipeline 21 can transport the particles to be reacted through the first chamber 111 to the second chamber 112; by arranging the first cyclone separator 3 in the first chamber 111, the airflow generated by the first cyclone separator 3 can drive the particles to be reacted and the reaction gas in the second chamber 112 to move to the first chamber 111, avoiding the accumulation of the particles to be reacted in the second chamber 112, increasing the contact area between the particles to be reacted and the reaction gas, and improving the reaction efficiency of the carbon-containing substances on the particles to be reacted and the reaction gas; separating the particles to be reacted and the reaction gas in the first chamber 111, so that the particles to be reacted can return to the second chamber 112 again, so that the unnecessary substances on the particles to be processed can react with the reaction gas entering from the third opening 115 again to improve the removal effect of the carbon-containing substances on the particles to be processed.

[0060] In some embodiments, the fluidized bed reactor further includes a preheater 12, which is used to preheat the gas introduced into the third opening 115.

[0061] The preheater 12 can be of a coil type structure or a packed type structure. It can be arranged outside the pipeline connecting the gas source and the third opening 115, or can be arranged inside the pipeline connecting the gas source and the third opening 115. The preheater 12 can heat the reaction gas to the required temperature to accelerate the reaction between the unnecessary substances and the reaction gas.

[0062] In some embodiments, the first chamber 111 includes a settling zone 111a and a first tapered zone 111b. The first cyclone separator 3 is arranged in the settling zone 111a. The first tapered zone 111b connects the settling zone 111a and the second chamber 112, and the diameter of the first tapered zone 111b gradually decreases in the direction from the settling zone 111a to the second chamber 112.

[0063] By setting the diameter of the first tapered zone 111b to gradually decrease in the direction from the settling zone 111a to the second chamber 112, the gas velocity of the air flow moving to the first chamber 111 decreases in the settling zone 111a, realizing partial gas-solid separation. By setting the diameter of the first tapered zone 111b to gradually decrease in the direction from the settling zone 111a to the second chamber 112, the particles to be processed separated by the air flow generated by the first cyclone separator 3 can contact the wall surface of the first tapered zone 111b and then slide down along the wall surface of the first tapered zone 111b to the second chamber 112.

[0064] In some embodiments, the second chamber 112 includes a straight pipe zone 112a and a second tapered zone 112b. The straight pipe zone 112a connects the first chamber 111 and the second tapered zone 112b. The diameter of the second tapered zone 112b gradually decreases in the direction from the first chamber 111 to the straight pipe zone 112a, and one end of the second tapered zone 112b far from the first chamber 111 is communicated with the third opening 115.

[0065] The diameter of the straight pipe zone 112a can remain unchanged along the gravity direction, so that the particles to be processed can move smoothly in the straight pipe zone 112a. The diameter of the second tapered zone 112b gradually decreases in the direction from the first chamber 111 to the straight pipe zone 112a, and one end of the second tapered zone 112b far from the first chamber 111 is communicated with the third opening 115, so that the third opening 115 can conveniently collect the particles to be processed.

[0066] The material feeding port 211 of the first pipeline 21 can be arranged in the second tapered zone 112b. The sedimentation zone 111a, the first tapered zone 111b, the straight pipe zone 112a and the second tapered zone 112b can be connected in sequence along the gravity direction. The maximum diameter of the sedimentation zone 111a is larger than the minimum diameter of the first tapered zone 111b. The maximum diameter of the first tapered zone 111b is larger than the diameter of the straight pipe zone 112a. The diameter of the straight pipe zone 112a is larger than the minimum diameter of the second tapered zone 112b.

[0067] The dipleg of the first cyclone separator 3 is connected to one end of the straight pipe zone 112a departing from the second tapered zone 112b. The to-be-treated particles separated by the airflow generated by the first cyclone separator 3 slide down to the wall surface of the first tapered zone 111b through the flap valve of the first cyclone separator 3, and then slide down along the wall surface of the first tapered zone 111b to the second chamber 112.

[0068] In some embodiments, the reaction unit further includes a heater 13 for heating the second chamber 112.

[0069] The heater 13 can be arranged in the straight pipe zone 112a which has a uniform diameter to facilitate the arrangement of the heater 13. The heater 13 can also be arranged in the straight pipe zone 112a and the second tapered zone 112b to heat the straight pipe zone 112a and the second tapered zone 112b and increase the area in the second chamber 112 that meets the reaction temperature.

[0070] The wall surface forming the first chamber 111 in the first housing 11 can be directly in contact with the ambient air so that the airflow and the to-be-treated particles heated by the heater 13 can be cooled after entering the first chamber 111, which is beneficial to the sedimentation of the to-be-treated particles in the first chamber 111 to the second chamber 112.

[0071] When the fluidized bed reactor provided in the present application is in the reaction stage, the fifth valve V5 is closed, the concentrations of the components in the gas source and the total flow rate of the gas source are controlled, and the preheater 12 and the heater 13 are turned on so that the temperature of the reaction gas heated by the preheater 12 meets the minimum temperature required for the reaction of the non-desired substances. The heater 13 further heats the reaction gas and the non-desired substances to promote the oxidation reaction between the reaction gas and the non-desired substances and convert the non-desired substances on the particle body into gas.

[0072] The gas will entrain the particles to be processed and move upward, causing the particles to be in a fluidized state. Some of the particles to be processed will enter the enlarged section. Due to the increase in diameter and the decrease in gas velocity, some of the particles to be processed will settle and slide down along the inner wall surface of the first housing 11 to the straight pipe area 112a. Some of the particles to be processed become small particles with a small particle size due to collision and fragmentation or combustion. The small particles enter the first cyclone separator 3 for further gas-solid separation. The separated particles to be processed fall into the dipleg of the first cyclone separator 3. When the amount of particles to be processed in the dipleg is large enough, under the action of gravity, the particles to be processed push open the wing valve and slide down to the wall surface of the first tapered section 111b. Since the gas velocity at the wall surface is small, the particles to be processed return to the straight pipe area 112a again and further react with the reaction gas. The gas then leaves the first housing 11 through the outlet of the first cyclone separator 3.

[0073] In some embodiments, the fluidized bed reactor further includes a discharging unit 4, and the discharging unit 4 is disposed outside the first housing 11 and communicated with the first pipeline 21.

[0074] After the particles to be processed in the first housing 11 are processed, the discharging unit 4 can drive the particles to be processed in the first housing 11 into the feeding port 211, and then transport them to the discharging unit 4 through the first pipeline 21. The discharging unit 4 may include an air pump, a silo, etc. The air pump sucks air from the second chamber 112 through the first pipeline 21 to transport the particles to be processed in the first housing 11 outward through the first pipeline 21.

[0075] The first pipeline 21 can be a tee pipe, that is, one opening is communicated with the material source, one opening is communicated with the discharging unit 4, and the feeding port 211 is communicated with the second chamber 112. The bent part of the first pipeline 21 has a smooth transition to avoid the transportation of solids getting stuck and accumulating at the bent part.

[0076] Please refer to Figure 2 , in some embodiments, the fluidized bed reactor further includes a filtering unit 5. The filtering unit 5 includes a second housing 51, a filter 52, and a first air pump 53. The second housing 51 includes a third chamber 511 and a fourth chamber 512. The third chamber 511 is communicated with the second opening 114; the filter 52 isolates the third chamber 511 and the fourth chamber 512. The filter 52 includes a filter housing disposed in the third chamber 511, and the first air pump 53 is communicated with the hollow chamber of the filter housing through the fourth chamber 512.

[0077] The first housing 11 and the second housing 51 can be arranged at intervals. The first cyclone separator 3 and the third chamber 511 are communicated through the second opening 114. The airflow carrying powder discharged from the first cyclone separator 3 enters the third chamber 511 through the second opening 114. The first air pump 53 sucks air from the third chamber 511. After the airflow carrying powder passes through the filter housing for filtration, it enters the hollow chamber of the filter housing and the fourth chamber 512 and then is discharged outward. The carried powder is intercepted on one side of the filter housing close to the third chamber 511. The powder can be broken particles to be processed, shed unnecessary substances, etc. The filter housing can be a sintered metal tube with a middle cavity. The filter 52 can have a plurality of filter housings. The powder is assembled on the outer surface of the filter 52, and part of the powder can slide down to the bottom of the second housing 51 under the action of gravity.

[0078] By arranging the filtering unit 5, the airflow carrying powder discharged from the first cyclone separator 3 is filtered to avoid polluting the environment by the airflow carrying powder; the powder carried in the airflow contains a particle body, a carbon-containing substance, etc. The powder intercepted on the filter housing is collected for reuse to improve the output rate of the particles to be processed.

[0079] When the fluidized bed reactor provided in this application is in the feeding stage, the first air pump 53 sucks air from the third chamber 511 to make the first chamber 111, the second chamber 112 and the third chamber 511 in a vacuum state; the fifth valve V5 provided on the first pipeline 21 is opened to communicate the second chamber 112 with the material source. Under the action of vacuum, the particles to be processed provided by the material source are sucked into the second chamber 112 through the first pipeline 21. The gas entraining the particles to be processed moves towards the first chamber 111. Since the airflow velocity decreases in the first tapered area 111b and the settling area 111a, the particles to be processed remain in the second chamber 112, while the gas is pumped to pass through the second opening 114, the third chamber 511 and the fourth chamber 512 in sequence and then discharged, thereby realizing feeding into the second chamber 112. Since the inner diameter of the first chamber 111 is larger than the inner diameter of the first pipeline 21, the particles to be processed in the second chamber 112 will not enter the third chamber 511 through the second opening 114.

[0080] When the particles to be processed are in the reaction stage in the fluidized bed reactor, the fifth valve V5 is closed and the first air pump 53 is turned off. The gas source passes the reaction gas into the second chamber 112 through the third opening 115, and the heater 13 is heated up. The carbon-containing substances in the particles to be processed react with oxygen to generate carbon monoxide or carbon dioxide. The gas in the first housing 11 moves upward into the enlarged section and the settling area 111a. There is no heating and heat preservation outside the enlarged section and the settling area 111a. The gas releases heat to the environment through the wall of the reactor, the gas temperature drops, the gas volume decreases, and the viscosity decreases. Some particles settle and return to the straight pipe section of the reactor; the gas enters the inner first cyclone separator 3 for gas-solid separation, and the particles to be processed fall into the second chamber 112; the gas carrying the powder enters the third chamber 511 through the second opening 114, and the powder is intercepted at the filter 52, and the filtered gas is discharged outwards.

[0081] In some embodiments, the filtering unit 5 further includes an aggregate structure 54 and a first valve V1. The aggregate structure 54 is communicated with the third chamber 511; the first valve V1 is arranged on the pipeline communicating the third chamber 511 and the aggregate structure 54.

[0082] When the first valve V1 is closed, the first air pump 53 works, and a negative pressure state can be maintained in the third chamber 511 to drive the gas in the third chamber 511 to be discharged from the filter 52. The powder intercepted by the filter 52 remains in the third chamber 511. When the first valve V1 is opened, the powder intercepted by the filter 52 can be discharged from the third chamber 511 to the aggregate structure 54 under the action of gravity. The aggregate structure 54 can also be communicated with the first air pump 53, and the first air pump 53 can drive the powder in the third chamber 511 into the aggregate structure 54.

[0083] Optionally, the first valve V1 is a three-way valve. The first valve port of the first valve V1 is communicated with the third chamber 511, the second valve port of the first valve V1 is communicated with the aggregate structure 54, and the third valve port of the first valve V1 is communicated with the second air pump.

[0084] In some embodiments, the aggregate structure 54 is communicated with the first pipeline 21, and the filtering unit 5 further includes a second valve V2. The second valve V2 is arranged on the pipeline communicating the aggregate structure 54 and the first pipeline 21.

[0085] The powder collected in the aggregate structure 54 contains the particle body and unnecessary substances. When the second valve V2 is opened, the powder collected in the aggregate structure 54 can be re-transported to the second chamber 112 through the first pipeline 21 for reaction, improving the utilization rate of the particle body.

[0086] The second valve V2 can be a three-way valve. The second valve V2 can include a first valve port, a second valve port, and a third valve port. The first valve port of the second valve V2 communicates with the aggregate structure 54, the second valve port of the second valve V2 communicates with the first pipeline 21, and the third valve port of the second valve V2 communicates with the third air pump.

[0087] When the first valve port, the second valve port, and the third valve port of the second valve V2 are opened, the third air pump can drive the powder in the aggregate structure 54 into the first pipeline 21.

[0088] When the fluidized bed reactor is in the recovery stage of processing the particles to be processed, open the first valve port and the second valve port of the first valve V1, and the powder intercepted by the filter 52 enters the aggregate structure 54;

[0089] Close the first valve port of the first valve V1, open the second valve port and the third valve port of the first valve V1, open the first valve port, the second valve port, and the third valve port of the second valve V2. The third valve port of the first valve V1 communicates with the second air pump, and the third valve port of the second valve V2 communicates with the third air pump respectively. The second air pump and the third air pump blow air to transport the powder in the aggregate structure 54 into the first pipeline 21 and enter the second chamber 112 through the first pipeline 21.

[0090] In some embodiments, the filtering unit 5 further includes a second pipeline 55 and a third valve V3. The second pipeline 55 communicates the second opening 114 and the third chamber 511, and the third valve V3 is arranged on the second pipeline 55;

[0091] The fluidized bed reactor further includes a third pipeline 61, a fourth pipeline 62, and a fourth valve V4. The third pipeline 61 communicates the first pipeline 21 and the inlet of the discharging unit 4. The fourth pipeline 62 communicates the inlet of the discharging unit 4 and the second pipeline 55. The fourth valve V4 is arranged on the fourth pipeline 62. The third valve V3 and the discharging unit 4 are in parallel.

[0092] The third valve V3 can control the on-off between the second opening 114 and the third chamber 511, and the fourth valve V4 can control the on-off between the discharging unit 4 and the third chamber 511. Both the third valve V3 and the fourth valve V4 can be two-way ball valves or two-way gate valves.

[0093] When the fluidized bed reactor is in the discharging stage of processing the particles to be processed, close the third valve V3 and the first valve V1, open the fourth valve V4, and the first air pump 53 sucks air from the third chamber 511. The particles to be processed are sucked into the discharging unit 4 under the action of vacuum. When the vacuum degree suddenly drops, it indicates that the particles to be processed have been completely sucked away. Close the first air pump 53 and open the discharging port of the discharging unit 4, and the particle body that has removed the unnecessary substances flows out from the discharging port.

[0094] The discharging unit 4 can be a second cyclone separator, which can be an external cyclone separator. The particle body is discharged from the discharging port, and the airflow carrying the powder enters the third chamber 511 through the fourth pipeline 62, and is discharged after the powder is filtered by the filter 52.

[0095] In some embodiments, the filtering unit 5 further includes a gas analyzer. The fourth chamber 512 communicates with the hollow cavity of the filter 52 and the gas analyzer. The gas analyzer can be used to analyze the concentrations of carbon monoxide and carbon dioxide in the gas discharged from the fourth chamber 512. According to the amount of oxygen introduced into the second chamber 112 and the concentrations of carbon monoxide and carbon dioxide, the reaction amount of carbon elements can be calculated. When the reaction amount of carbon elements meets the preset requirements, the heater 13 is stopped and the amount of gas introduced into the second chamber 112 is reduced.

[0096] In some embodiments, the fluidized bed reactor further includes a pressure detector for detecting the pressure at the location. The pressure detector P1 can communicate with the first chamber 111 to detect the air pressure in the first chamber 111. The pressure detector P3 can communicate with the fourth chamber 512 to detect the air pressure in the fourth chamber 512. The pressure detector P2 can be arranged on the second pipeline 55 to detect the air pressure in the second pipeline 55. The powder forms a filter layer outside the filter 52, resulting in an increase in the pressure drop before and after the filter 52. By comparing the air pressure in the second pipeline 55 and the air pressure in the fourth chamber 512, the thickness of the filter layer can be analyzed. When the pressure difference between the air pressure in the second pipeline 55 and the air pressure in the fourth chamber 512 is too large, air is blown into the fourth chamber through the first air pump 53, so that the airflow flows from the hollow cavity of the filter 52 into the third chamber 511, and the airflow drives the filter layer to fall to the bottom of the second housing 51.

[0097] The present application also provides a control method for a fluidized bed reactor. The method is applied to the fluidized bed reactor as described above, and the method includes:

[0098] S110, adding the particles to be processed into the second chamber through the first pipeline;

[0099] The fourth valve and the first valve V1 can be opened and closed, the fifth valve V5 and the third valve V3 are opened, and the first air pump 53 sucks air to make the inside of the first housing 11 and the second housing 51 turn to a vacuum state. Under the action of vacuum, the particles to be processed in the material source move through the first pipeline 21 to the second chamber 112.

[0100] S120, introducing the reaction gas into the second chamber through the third opening so that the unnecessary substances on the particles to be processed react with the reaction gas in the reaction gas;

[0101] Close the fifth valve V5, control the concentrations of the components in the gas source and the total flow rate of the gas source, and turn on the preheater 12 and the heater 13 so that the temperature of the reaction gas heated by the preheater 12 meets the minimum temperature required for the reaction of the unwanted substances. The heater 13 further heats the reaction gas and the unwanted substances to promote the oxidation reaction between the reaction gas and the unwanted substances, and convert the unwanted substances on the particle body into gas.

[0102] S130. Start the first cyclone separator to switch the particles to be processed to the fluidized state. The particles to be processed move to the first chamber for gas-solid separation. The separated particles to be processed fall back to the second chamber, and the separated gas is discharged from the second opening out of the first housing.

[0103] The gas separated by the first cyclone separator carries powder. The gas carrying the powder enters the third chamber 511 through the second opening 114. The powder is intercepted at the filter 52, and the filtered gas is discharged outwards through the fourth chamber 512.

[0104] By arranging the first cyclone separator 3 in the first chamber 111, the airflow generated by the first cyclone separator 3 can drive the particles to be reacted and the reaction gas in the second chamber 112 to move to the first chamber 111, avoiding the accumulation of the particles to be reacted in the second chamber 112, increasing the contact area between the particles to be reacted and the reaction gas, and improving the reaction efficiency between the unwanted substances on the particles to be reacted and the reaction gas. In the first chamber 111, the particles to be reacted and the reaction gas are separated, so that the particles to be reacted can return to the second chamber 112 again. Thus, the unwanted substances on the particles to be processed can react with the reaction gas entering from the third opening 115 again to improve the removal effect of the unwanted substances on the particles to be processed.

[0105] In some embodiments, when the treatment of the particles to be processed is completed, the control method includes:

[0106] S140. Close the third valve, open the fourth valve, and control the first air pump to suck air from the fourth chamber so that the particles to be processed enter the discharging unit through the first pipeline.

[0107] The concentration of the components in the gas discharged through the fourth chamber 512 can be detected to determine whether the treatment of the particles to be processed is completed. For example, when the unwanted substance is graphite, the concentrations of carbon monoxide and carbon dioxide in the discharged gas can be analyzed, and the amount of graphite burned can be calculated according to the amount of oxygen introduced. When the amount of graphite burned meets the preset carbon burning requirement, the treatment of the particles to be processed is completed. Then, turn off the heater 13 and the preheater 12, and reduce the amount of gas introduced from the third opening 115.

[0108] The third valve V3 and the first valve V1 can be closed, and the fourth valve is opened. The first air pump 53 sucks air from the third chamber 511. The particulate matter to be processed is carried and sucked into the unloading unit 4 under the action of vacuum. When the vacuum degree suddenly drops, it indicates that the particulate matter to be processed has been completely sucked away. Then, the first air pump 53 is closed, and the unloading port of the unloading unit 4 is opened. The particulate matter with carbonaceous substances removed flows out from the unloading port.

[0109] The unloading unit 4 can be a second cyclone separator. The particulate matter with carbonaceous substances removed is discharged from the unloading port, and the airflow carrying the powder enters the third chamber 511 through the fourth pipeline 62 and is discharged after the powder is filtered by the filter 52.

[0110] In some embodiments, after starting the first cyclone separator, it includes:

[0111] S150, open the first valve to enable the powder intercepted by the filter to enter the aggregate unit;

[0112] S160, open the second valve to enable the powder in the aggregate unit to enter the second chamber through the first pipeline.

[0113] Optionally, open the first valve port and the second valve port of the first valve V1, and the powder intercepted by the filter 52 enters the aggregate structure 54; close the first valve port of the first valve V1, open the second valve port and the third valve port of the first valve V1, open the first valve port, the second valve port and the third valve port of the second valve V2. The third valve port of the first valve V1 is connected to the second air pump, and the third valve port of the second valve V2 is connected to the third air pump. The second air pump and the third air pump blow air to transport the powder in the aggregate structure 54 into the first pipeline 21 and enter the second chamber 112 through the first pipeline 21.

[0114] Exemplarily, the control method of the fluidized bed reactor provided by the present application includes the following stages;

[0115] Feeding stage: Close the fourth valve and the first valve V1, open the fifth valve V5 and the third valve V3. The first air pump 53 is switched to the vacuum state, and the inside of the first housing 11 and the second housing 51 is in a vacuum state. The particulate matter to be processed in the material source is transported to the second chamber 112 through the first pipeline 21.

[0116] Reaction stage: Close the fifth valve V5, and turn the first air pump 53 to the venting state. The gas source supplies the reaction gas, which is heated to 550 °C by the preheater 12. The heater 13 heats the second chamber 112 to 700 °C. The graphite in the particles to be treated reacts with oxygen to generate carbon monoxide or carbon dioxide. The gas in the second chamber 112 moves into the expansion section and the settling zone 111a. There is no heating and insulation outside the expansion section and the settling zone 111a. The gas releases heat to the environment through the wall of the first housing 11. The gas temperature drops, the gas volume decreases, and the viscosity decreases. Some of the particles to be treated settle back to the straight pipe section 112a of the second chamber 112. The gas enters the first cyclone separator 3 inside for gas-solid separation again. The particles to be treated sink into the dipleg and then return to the straight pipe section 112a of the second chamber 112. The gas enters the third chamber 511 through the second opening 114, is filtered by the filter 52, and then discharged through the fourth chamber 512.

[0117] The powder separated by the filter 52 slides to the bottom of the second housing 51. Open the first valve V1, and the powder falls to the aggregate structure 54. Close the first valve port of the first valve V1, open the second valve V2, the third valve port of the first valve V1, and the 112 of the second valve V2.

[0118] Discharging stage: Close the third valve V3 and the first valve V1, open the fourth valve V4, and turn the first air pump 53 to the vacuum state. Under the action of vacuum, the particles to be treated are sucked into the outer second cyclone separator 4. The particles to be treated enter the bin of the second cyclone separator 4. When the vacuum suddenly drops, it indicates that the particles to be treated have been completely sucked away. Close the first air pump 53 and open the discharge port of the outer second cyclone separator 4 to discharge the particle body.

[0119] The effects of the present application are described below with Experimental Example 1, Experimental Example 2, Comparative Example 1, and Comparative Example 2.

[0120] Comparative Example 1:

[0121] The particles to be treated are catalytic cracking coked catalysts with an average particle size of 83 μm. The unnecessary substance is coke, and the coke mass fraction is 7%. For 1000 g of catalyst, the coke on the catalyst must be reduced to 0.5% to restore its activity.

[0122] A fixed fluidized bed reactor is used to treat the particles to be treated. A filter is provided at the top outlet of the fixed fluidized bed reactor to ensure that the subsequent gas meets the emission requirements. The catalyst is added from the top with a funnel and discharged from the bottom.

[0123] The fixed fluidized bed reactor has a diameter of 80 mm and a height of 1000 mm. The height of the first tapered zone is 400 mm. The diameter of the settling zone is 400 mm and the height is 500 mm. The gas flow rate of the reaction gas is 24 SLPM. First, nitrogen is introduced to heat up to 600 °C, and then it is switched to air with the same gas flow rate. The regeneration duration is 30 min, and the carbon deposition amount on the catalyst is 1%. The oxygen utilization rate is 0.74. The pressure drop of the filter is 20 KPa.

[0124] Experimental Example 1:

[0125] The particles to be treated are coked catalysts for fluid catalytic cracking, with an average particle size of 83 μm. The unwanted substance is carbon deposition, and the mass fraction of carbon deposition is 7%. For 1000 g of catalyst, the carbon deposition on the catalyst must be reduced to 0.5% to restore its activity.

[0126] The fluidized bed reactor proposed in this application is used to treat the particles to be treated. The particles are added to the reactor by means of vacuum pumping, and there is no dust during the feeding process. The diameter of the first shell is 80 mm and the height is 1000 mm. The height of the first tapered zone is 400 mm. The diameter of the settling zone is 400 mm and the height is 500 mm. The gas flow rate of the reaction gas is 24 SLPM. First, nitrogen is introduced to heat up to 600 °C, and then it is switched to air with the same gas flow rate. The regeneration duration is 30 min, and the carbon deposition amount on the catalyst is 0.5%. The oxygen utilization rate is 1.2. The pressure drop of the filter used is 5 KPa, and there are 10 g of fine particles at the bottom of the filter, with an average particle size of 7 μm, indicating that the fluidized bed reactor of this application has a good gas-solid separation effect.

[0127] Comparative Example 2:

[0128] The particles to be treated are radioactive particles, with an average particle size of 110 μm and a particle bulk density of 4800 kg / m 3 , and the unwanted substance is graphite, with a mass fraction of graphite of 10%. For 1000 g of particles, the graphite on the particles must be reduced to 0.5% to restore its activity.

[0129] A fixed fluidized bed reactor is used to treat the particles to be treated. A filter is set at the top outlet of the fixed fluidized bed reactor to ensure that the subsequent gas meets the emission requirements. The catalyst is added from the top with a funnel and discharged from the bottom.

[0130] The fixed fluidized bed reactor has a diameter of 80 mm and a height of 1000 mm. The height of the first tapered zone is 400 mm. The diameter of the settling zone is 400 mm and the height is 500 mm. The gas flow rate of the reaction gas is 24 SLPM. First, nitrogen is introduced to heat up to 650 °C, and then it is switched to air with the same gas flow rate. The regeneration duration is 40 min, and the carbon deposition amount on the catalyst is 2%. The oxygen utilization rate is 0.74. The pressure drop of the filter is 23 KPa.

[0131] Experimental Example 2:

[0132] The particles to be treated are radioactive particles with an average particle size of 110 μm and a particle bulk density of 4800 kg / m 3 , and the unwanted substance is graphite with a mass fraction of 10%. For 1000 g of particles, the graphite on the particles must be reduced to 0.5% to restore their activity.

[0133] The fluidized bed reactor proposed in this application is used to treat the particles to be treated. The particles are added to the reactor by means of vacuum pumping, and there is no dust generation during the feeding process.

[0134] The diameter of the first shell is 80 mm and the height is 500 mm. The height of the first tapered zone is 400 mm. The diameter of the settling zone is 400 mm and the height is 400 mm. The gas flow rate of the reaction gas is 24 SLPM. First, nitrogen is introduced to heat up to 650 °C, and then it is switched to air with the same gas flow rate. The regeneration duration is 40 min, and the carbon deposition amount on the particles is 0.5%. The oxygen utilization rate is 0.92. The pressure drop of the filter is 5 KPa. The external cyclone separator and vacuum pumping are used for discharging, and there is no dust generation during the discharging process.

[0135] Comparing Comparative Example 1 with Experimental Example 1 and Comparative Example 2 with Experimental Example 2, it can be seen that using the fluidized bed reactor provided in this application can improve the utilization rate of the reaction gas and the treatment efficiency of the object to be treated. Among them, the oxygen utilization rate is greater than 1 because some carbon-containing substances react with oxygen to generate carbon monoxide.

[0136] According to the embodiments of the present application as described above, these embodiments do not describe all the details in detail, nor do they limit the invention to only the specific embodiments. Obviously, many modifications and variations can be made according to the above description. These embodiments are selected and specifically described in this specification to better explain the principle and practical application of the present application, so that those skilled in the art can make good use of the present application and its modifications based on the present application. The present application is only limited by the claims and their full scope and equivalents.

Claims

1. A fluidized bed reactor for particle reaction, characterized in that, the fluidized bed reactor comprises: a reaction unit including a first housing, the first housing including a first chamber and a second chamber that are in communication, as well as a first opening and a second opening that are in communication with the first chamber, and a third opening that is in communication with the second chamber, the third opening being for communicating with an external gas source; a feeding unit including a first pipeline, the first pipeline extending into the first chamber from the first opening and passing through the first chamber to reach the second chamber, and a material feeding port of the first pipeline being provided in the second chamber; a first cyclone separator provided in the first chamber, an outlet of the first cyclone separator being in communication with the second opening.

2. The fluidized bed reactor for particle reaction according to claim 1, characterized in that, the first chamber includes a settling zone and a first tapered zone, the first cyclone separator is provided in the settling zone, the tapered zone connects the settling zone and the second chamber, and a diameter of the tapered zone gradually decreases in a direction from the settling zone to the second chamber.

3. The fluidized bed reactor for particle reaction according to claim 1, characterized in that, the second chamber includes a straight pipe zone and a second tapered zone, the straight pipe zone connects the first chamber and the second tapered zone, a diameter of the second tapered zone gradually decreases in a direction from the first chamber to the straight pipe zone, and one end of the second tapered zone remote from the first chamber is in communication with the third opening.

4. The fluidized bed reactor for particle reaction according to claim 1, characterized in that, the reaction unit further includes a heater for heating the second chamber.

5. The fluidized bed reactor for particle reaction according to claim 1, characterized in that, the fluidized bed reactor further comprises: a discharging unit provided outside the first housing and in communication with the first pipeline.

6. The fluidized bed reactor for particle reaction according to claim 5, characterized in that, the fluidized bed reactor further includes a filtering unit, and the filtering unit includes: a second housing including a third chamber and a fourth chamber, the third chamber being in communication with the second opening; a filter for isolating the third chamber and the fourth chamber, the filter including a filter housing provided in the third chamber; a first air pump in communication with a hollow chamber of the filter housing through the fourth chamber.

7. The fluidized bed reactor for particle reaction according to claim 6, characterized in that, the filtering unit further includes: an aggregate structure in communication with the third chamber; a first valve provided on a pipeline connecting the third chamber and the aggregate structure.

8. The fluidized bed reactor according to claim 7, characterized in that, the aggregate structure is in communication with the first pipeline, and the filtering unit further includes: a second valve provided on a pipeline connecting the aggregate structure and the first pipeline.

9. The fluidized bed reactor for particle reaction according to claim 6, characterized in that, The filtering unit further includes a second pipeline and a third valve. The second pipeline communicates with the first cyclone separator and the second housing, and the third valve is disposed on the second pipeline. The fluidized bed reactor further includes a third pipeline, a fourth pipeline, and a fourth valve. The third pipeline communicates with the first pipeline and the inlet of the discharging unit. The fourth pipeline communicates with the inlet of the discharging unit and the second pipeline. The fourth valve is disposed on the fourth pipeline, and the third valve is in parallel with the discharging unit.

10. A control method for a fluidized bed reactor Characterized in that The method is applied to the fluidized bed reactor for particle reaction according to any one of claims 1 to 9, and the method includes: Adding the particles to be processed into the second chamber through the first pipeline; Introducing the reaction gas into the second chamber through the third opening, so that the unnecessary substances on the particles to be processed react with the reaction gas in the reaction gas; Starting the first cyclone separator to switch the particles to be processed to the fluidized state. The particles to be processed move to the first chamber for gas-solid separation, and the separated particles to be processed fall back to the second chamber, and the separated gas is discharged from the first housing through the second opening.

11. The control method for the fluidized bed reactor according to claim 10 Characterized in that When the processing of the particles to be processed is completed, the method includes: Closing the third valve, opening the fourth valve, and controlling the first air pump to suck air from the fourth chamber, so that the particles to be processed enter the discharging unit through the first pipeline.

12. The control method for the fluidized bed reactor according to claim 10 Characterized in that After starting the first cyclone separator, it includes: Opening the first valve to enable the powder intercepted by the filter to enter the aggregate unit; Opening the second valve to enable the powder in the aggregate unit to enter the second chamber through the first pipeline.

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