Stirring type particle circulation coupling reactor, fluidized bed and particle circulation coupling method

Abstract

The invention relates to a stirring type particle circulation coupling reactor, a fluidized bed and a particle circulation coupling method, the fluidized bed comprises a reactor, a solid recovery device and a storage tank, a stirring structure is introduced into the reactor, and horizontal shearing force generated by stirring is used for crushing large-size particle agglomerates to prevent hardening of micro-nano particles; meanwhile, the circular flow of the gas medium provides a vertical acting force for the particles, and the coalescence behavior of the gas phase and the solid phase in the reactor is reduced, so that the problem that the micro-nano particles are blocked in the annular space area of the reactor is solved, the fluidization quality is improved, and the circular continuous treatment of the micro-nano particles is realized; the fluidized bed utilizes the built-in guide cylinder to realize circulation, and the circulation direction can be a central airlift type or a central descending type by adjusting the gas flow rate ratio of the guide cylinder to the annular gap area, so that the circulation flow of particles is enhanced, and the fluidization quality of the particles at the bottom of the circulation section is improved.

Description

Technical Field

[0001] The present invention belongs to the technical field of gas-solid fluidization of ultrafine particles, and specifically relates to a stirring particle circulation coupling reactor, a fluidized bed and a particle circulation coupling method, which are used to realize continuous and stable processing of micron and nanometer particles. Background Art

[0002] Micro-nano particles, especially nanoparticles, usually refer to Geldart C particles with an average particle size of 1 nm~1000 µm, which is between the atomic, molecular and bulk (granular) materials. As the size of the material becomes ultra-fine, its surface molecular arrangement, electron distribution and crystal structure change to a certain extent, so ultra-fine particles derive special properties that are better than conventional coarse particle materials. For example, in the chemical industry, the reduction of catalyst particle size gives it a larger specific surface area, which helps to improve the reaction activity. In the energy field, in order to improve the safety of batteries and the thermal stability of battery components, ceramic powders with good heat resistance are used to prepare separators in lithium batteries and improve the battery charge and discharge cycle performance. In food processing, the extraction rate of bioactive ingredients is increased by micronizing functional products, and the absorption of nutrients such as protein in the human body is promoted. In the pharmaceutical field, ultra-fine amorphous drug particles with high apparent solubility and drug loading are used to deliver drugs with poor water solubility. For water treatment, ultra-fine particles such as metal organic frameworks are used to degrade pollutants in water with their extremely high porosity and specific surface area. In the field of medical testing, strong magnetic ultrafine particles are used as contrast agents for magnetic resonance imaging. In addition, other ultrafine particle-related technologies such as powder metallurgy and ultrafine grinding technology have also been derived.

[0003] The processing and application of micro-nano particles are usually integrated with fluidization technology to achieve efficient large-scale production and processing. Fluidized bed reactors reduce the vertical component of the force on the particles by introducing fluids, so that the particles are suspended in the fluid and have certain fluid properties. Combined with the small particle size and large specific surface area of ​​micro-nano particles, efficient gas-solid contact efficiency and rapid mass transfer and heat transfer performance can be achieved. However, the characteristics of micro-nano particles with large surface energy and high surface activity also make their individual particles often in an unstable state, with a strong tendency to attract each other and form stable agglomerates. This phenomenon makes micro-nano particles prone to abnormal fluidization phenomena such as channeling, slugging and dead zones during the fluidization process, resulting in poor fluidization quality, which is not conducive to the development of micro-nano particle fluidized beds in the industrial field. Summary of the invention

[0004] In view of at least one of the problems in the above-mentioned prior art, the purpose of the present invention is to provide a stirred particle circulation coupling reactor, a fluidized bed and a particle circulation coupling method, wherein a stirring structure is introduced into the reactor, and the horizontal shear force generated by the stirring is used to break up the agglomerations of large-sized particles and prevent the agglomeration of micro-nano particles; at the same time, the circulating flow of the gas medium provides a vertical force for the particles, reducing the aggregation behavior of the gas-solid two phases in the reactor, thereby solving the problem of obstructed flow of micro-nano particles in the annular gap area of ​​the reactor, improving the fluidization quality, and realizing the cyclic continuous processing of micro-nano particles.

[0005] To achieve the above object, the present invention adopts the following technical solutions: A stirred particle circulation coupled reactor, comprising: The shell includes a circulation section, a transition section and a conveying section which are arranged from bottom to top, wherein the transition section is provided with a feed inlet, the circulation section is provided with a return inlet, and the conveying section is provided with a discharge inlet; A guide tube is arranged in the annular flow section; the area between the outer wall of the guide tube and the inner wall of the shell is an annular gap area; an annular gap area air inlet pipe is arranged at the bottom of the annular flow section, and a guide tube gas distributor is arranged below the guide tube; the annular gap area air inlet pipe and the guide tube gas distributor are respectively connected to an external gas source; The stirring blade is arranged in the annular gap area and is driven to rotate by a driving mechanism.

[0006] Preferably, the driving mechanism comprises a motor, the motor is arranged on the housing, the motor is connected to the guide tube via a stirring shaft, the stirring blades are arranged on the outer wall of the guide tube, and the motor is used to drive the guide tube to rotate.

[0007] Preferably, the side wall of the guide cylinder is connected to the shell through a connecting rod, and the driving mechanism includes a motor, a driving gear, a driven gear and a stirring shaft. The motor is arranged at the bottom of the shell, the output shaft of the motor is connected to the driving gear, the driving gear is meshed with the driven gear, the stirring shaft is connected to the driven gear, and the stirring blade is arranged on the stirring shaft.

[0008] Preferably, the guide tube gas distributor comprises a connected annular tube portion and a straight tube portion, a plurality of gas outlet holes are evenly spaced at the top of the annular tube portion, all of the gas outlet holes are aligned with the guide tube, and the straight tube portion is connected to the external gas source.

[0009] Preferably, the guide tube gas distributor is a conduit, the gas outlet of the conduit is aligned with the guide tube, and the gas inlet of the conduit is connected to the external gas source.

[0010] A stirred particle circulation coupled fluidized bed, comprising a stirred particle circulation coupled reactor as described in any one of the above, a solid recovery device and a storage tank, wherein the solid recovery device is connected to the discharge port through a pipeline, the solid recovery device is connected to the top of the storage tank through a pipeline, and the bottom of the storage tank is connected to the return port through a discharge pipe.

[0011] Preferably, a valve is provided on the feed pipe; and the storage tank is also provided with a discharge pipe.

[0012] A particle circulation coupling method is based on any one of the above-mentioned stirred particle circulation coupling fluidized bed, comprising the following steps: adding particles into a reactor; Start the motor to drive the stirring blade to rotate to break up the agglomerates formed in the annular gap area; Adjust the gas flow rate of the annular gap area air inlet pipe and the guide tube gas distributor to make the bottom pressure of the guide tube and the bottom pressure of the annular gap area different, so that part of the particles circulate in the annular gap area and the guide tube; and another part of the particles enter the solid recovery device through the conveying section; The solid recovery device separates the gas from the particles, the gas is discharged to the atmosphere, and the particles enter the storage tank; The storage tank then transports the particles in the storage tank back to the reactor through the discharge pipe to achieve a circulation operation.

[0013] Preferably, in the step of adjusting the gas flow rate of the air inlet pipe and the guide tube gas distributor in the annular gap area, the bottom pressure of the guide tube is made lower than the bottom pressure of the annular gap area, and the particles flow directionally from the bottom of the annular gap area into the bottom of the guide tube, and the particles move upward to the top of the guide tube area under the action of the airflow introduced by the guide tube gas distributor. After the particles leave the top of the guide tube, some of the particles flow into the annular gap area, and move downward to the bottom of the annular flow section through the annular gap area, thereby realizing continuous central air lift type annular flow; the other part of the particles flow into the solid recovery device through the conveying section.

[0014] Preferably, in the step of adjusting the gas flow rate of the annular gap area air inlet pipe and the guide tube gas distributor, the bottom pressure of the guide tube is made greater than the bottom pressure of the annular gap area, and the particles flow directionally from the bottom of the guide tube into the bottom of the annular gap area; the particles move upward to the top of the annular gap area under the action of the air flow introduced into the annular gap area through the air inlet pipe, and after the particles leave the top of the annular gap area, a part of the particles flow into the guide tube, and move downward to the bottom of the annular flow section through the guide tube, thereby realizing continuous central descending annular flow; the other part of the particles flow into the solid recovery device through the conveying section.

[0015] The present invention adopts the above technical solution, which has the following advantages: 1. The stirred particle circulation coupling reactor provided by the present invention introduces a stirring structure into the reactor, and uses the horizontal shear force generated by stirring to break up the agglomeration of large-sized particles to prevent the compaction of micro-nano particles; at the same time, the circulating flow of the gas medium provides a vertical force for the particles, reducing the aggregation behavior of the gas-solid two phases in the reactor, thereby solving the problem of obstructed flow of micro-nano particles in the annular gap area of ​​the reactor, and strengthening the particle circulation by stirring, thereby improving the fluidization quality and realizing the cyclic continuous processing of micro-nano particles.

[0016] 2. The stirred particle circulation coupled fluidized bed and particle circulation coupling method provided by the present invention utilize a built-in guide tube to realize circulation. By adjusting the ratio of the gas flow rates in the guide tube and the annular gap area, the direction of the circulation can be a center air lift type and a center descending type. The stirring blades arranged on the outer wall of the guide tube directly generate horizontal shear force on the particle agglomerates, thereby effectively promoting the breakup of large-sized agglomerates, avoiding the growth and accumulation of agglomerates at the bottom of the reactor, strengthening the circulation flow of the particles, and improving the fluidization quality of the particles at the bottom of the circulation section.

[0017] 3. The stirred particle circulation coupled fluidized bed and particle circulation coupling method provided by the present invention provide additional kinetic energy for the particles through the energy introduced by stirring. The rotation of the stirring blades weakens the dominant role of the airflow in overcoming the particle gravity and the interaction force between the micro-nano particles. The particle accumulation layer can expand uniformly under lower gas velocity conditions, the gas-solid contact efficiency is improved, the micro-nano particles can reach a better fluidized state, and the cyclic continuous treatment of the micro-nano particles in the stirring-enhanced circulation coupling reactor is realized. BRIEF DESCRIPTION OF THE DRAWINGS

[0018] Figure 1 It is a schematic structural diagram of a stirring particle circulation coupled fluidized bed with a motor placed on top provided in one embodiment of the present invention.

[0019] Figure 2 It is a schematic structural diagram of a stirring particle circulation coupled fluidized bed with a motor placed below provided in one embodiment of the present invention.

[0020] Figure 3 It is a schematic structural diagram of a stirring particle circulation coupled fluidized bed in the form of multiple stirring shafts provided in one embodiment of the present invention.

[0021] Figure 4 It is a schematic diagram of the structural proportions of a reactor provided in one embodiment of the present invention.

[0022] Figure 5 It is a schematic diagram of the structure of a reactor equipped with a coil-type draft tube gas distributor provided by one embodiment of the present invention.

[0023] Figure 6 It is a schematic diagram of the three-dimensional structure of a reactor equipped with a coil-type draft tube gas distributor provided by one embodiment of the present invention.

[0024] Figure 7 It is a schematic diagram of the structure of a coil-type guide tube gas distributor provided by one embodiment of the present invention.

[0025] Figure 8 It is a schematic diagram of the structure of a reactor provided by an embodiment of the present invention, in which a duct-type draft tube gas distributor is installed.

[0026] Fig. 9 It is a flow chart of a particle circulation coupling method provided by one embodiment of the present invention.

[0027] Fig.10 It is a schematic diagram of particle circulation of central airlift type provided by one embodiment of the present invention.

[0028] Fig.11 It is a schematic diagram of a center-down particle circulation provided by an embodiment of the present invention.

[0029] Fig.12 It is a schematic diagram of the structure of a stirring blade in the form of a screw paddle provided in one embodiment of the present invention.

[0030] Fig.13 It is a schematic diagram of the structure of a stirring blade in the form of a propeller provided in one embodiment of the present invention.

[0031] Markings in the accompanying drawings: 1 is a shell, 101 is a circulation section, 102 is a transition section, 103 is a conveying section, 2 is a guide tube, 3 is a motor, 4 is a feed port, 5 is a stirring blade, 6 is an annular gap area, 7 is an air inlet pipe for the annular gap area, 8 is a guide tube gas distributor, 801 is an annular pipe portion, 802 is a straight pipe portion, 9 is a stirring shaft, 10 is a solid recovery device, 11 is a storage tank, 12 is a feed pipe, 13 is a discharge pipe, 14 is a driving gear, 15 is a driven gear, and 16 is a solid circulation rate measuring device. DETAILED DESCRIPTION

[0032] In order to make the purpose, technical solution and advantages of the present invention clearer, the technical solution of the present invention will be clearly and completely described below in conjunction with the accompanying drawings. Obviously, the described embodiments are part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without making creative work are within the scope of protection of the present invention.

[0033] In the description of the present invention, it should be noted that the directions or positional relationships indicated by the terms "upper", "lower", "front", "backward", etc. are based on the directions or positional relationships shown in the accompanying drawings, and are only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the system or element referred to must have a specific direction, be constructed and operated in a specific direction, and therefore cannot be understood as a limitation on the present invention. The arrows in the accompanying drawings represent the flow direction of the substance.

[0034] In the description of the present invention, it should be noted that, unless otherwise clearly specified and limited, the terms "assembly", "setting", and "connection" should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection, or it can be an indirect connection through an intermediate medium, or it can be the internal communication of two components. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood according to specific circumstances.

[0035] The present invention provides a stirring particle circulation coupling reactor, a fluidized bed and a particle circulation coupling method, wherein a stirring structure is introduced into the reactor, and the horizontal shear force generated by the stirring is used to break up the agglomeration of large-sized particles, thereby preventing the agglomeration of micro-nano particles; at the same time, the circulation flow of the gas medium provides a vertical force for the particles, reducing the aggregation behavior of the gas-solid two phases in the reactor, thereby solving the problem of obstruction of the flow of micro-nano particles in the annular gap area of ​​the reactor, improving the fluidization quality, and realizing the cyclic continuous treatment of micro-nano particles.

[0036] The embodiments of the present invention are described in detail below with reference to the accompanying drawings.

[0037] Example 1 Please refer to Figure 1 and Figure 2 The present embodiment provides a stirred particle circulation coupled reactor, comprising a shell 1 and a guide tube 2; The shell 1 includes a circulation section 101, a transition section 102 and a conveying section 103 which are arranged from bottom to top. The transition section 102 is provided with a feed port 4, and particles are added into the shell 1 from the feed port 4. The circulation section 101 is provided with a return port, and the conveying section 103 is provided with a discharge port. The guide tube 2 is arranged in the annular section 101, and the area between the outer wall of the guide tube 2 and the inner wall of the shell 1 is the annular gap area 6; an annular gap area air inlet pipe 7 is arranged at the bottom of the annular section 101, and a guide tube gas distributor 8 is arranged below the guide tube 2; the annular gap area air inlet pipe 7 and the guide tube gas distributor 8 are respectively connected to an external gas source; The stirring blade 5 is arranged in the annular gap area 6 and is driven to rotate by a driving mechanism; the driving mechanism includes a motor 3, and the motor 3 can be arranged on the shell 1 through a bracket. The motor 3 is connected to the guide tube 2 through a stirring shaft 9. The stirring blade 5 is arranged on the outer wall of the guide tube 2, and the motor 3 is used to drive the guide tube 2 to rotate.

[0038] In a specific application, the guide tube 2 is a tubular structure with openings at both the top and the bottom. The guide tube 2 is arranged at the center of the annular section 101, and the center lines of the two coincide. The guide tube 2 and the stirring blades 5 on its outer wall constitute a stirring structure. The stirring blades 5 are located in the annular gap area 6, and the lowest point of the stirring blades 5 is higher than the lower end surface of the guide tube 2. During operation, the guide tube 2 rotates together with the stirring blades 5 to stir and strengthen the flow of particles in the annular gap area 6. The stirring blades 5 can be a blade-type stirring paddle, a screw-type stirring paddle, a propeller-type stirring paddle, a fishbone-type stirring paddle, or a horizontal rod-shaped paddle. The stirring blades 5 on the outer wall of the guide tube 2 can be one group or multiple groups. The multiple groups of stirring blades 5 are evenly distributed around the guide tube 2. When the guide tube 2 rotates, multiple small stirring and fluidizing areas are formed in the annular gap area 6, and at the same time, the particles in the annular gap area 6 are disturbed to strengthen the flow of particles. A multi-stage stirring blade 5 can be set at the same axial height of the guide tube 2 to improve the fluidization quality of the particles in the circulation section. The size of the stirring blade 5 is sufficient to ensure that the stirring blade 5 and the inner wall of the circulation section 101 do not collide or rub during the stirring operation. The number and form of the stirring blade 5 are sufficient to ensure that the normal circulation flow of particles in the annular gap area is not hindered during operation.

[0039] In this embodiment, the guide tube 2 is a single-stage or multi-stage flow guide tube, and its cross-section can be circular or square. The single-stage guide tube 2 is an integral structure, and its advantage is that the structure is simple and easy to control; the multi-stage guide tube is composed of a plurality of short guide tubes connected in series, and each short guide tube is separated by a distance. The guide tube 2 can form an overall annular flow, and each short guide tube can form a local annular flow. Compared with the single-stage guide tube, the multi-stage guide tube has a higher degree of turbulence and a better gas-solid contact effect.

[0040] In this embodiment, the inner diameter of the conveying section 103 is smaller than the inner diameter of the circulation section 101. The conveying section 103 is a lifting pipe with an inner diameter smaller than that of the circulation section 101. Its function is to transport the fully fluidized micro-nano particles in the circulation section 101 to the gas-solid recovery system. The gas-solid recovery system includes a solid recovery device 10 and a storage tank 11.

[0041] Reference Figure 3 In this embodiment, in order to ensure the formation of a stable circulation, D0 is the inner diameter of the circulation section 101, H0 is the height of the circulation section 101, D1 is the inner diameter of the guide tube 2, H1 is the height of the guide tube 2, D2 is the inner diameter of the conveying section 103, and H2 is the height of the conveying section 103.

[0042] The ratio D0 / D1 of the inner diameter D1 of the guide tube 2 to the inner diameter D0 of the circulation section 101 is in the range of 0.4 to 0.8. Preferably, the ratio D1 / D0 of the inner diameter D1 of the guide tube 2 to the inner diameter D0 of the circulation section 101 is in the range of 0.5 to 0.7.

[0043] The ratio H1 / H0 of the height H1 of the guide tube 2 to the height H0 of the circulation section 101 is in the range of 0.4 to 0.7. Preferably, the ratio H1 / H0 of the height H1 of the guide tube 5 to the height H0 of the circulation section 4 is in the range of 0.5 to 0.6.

[0044] The ratio H2 / H0 of the height H2 of the conveying section 103 to the height H0 of the circulation section 101 is in the range of 1 to 5. Preferably, the ratio H2 / H0 of the height H2 of the conveying section 103 to the height H0 of the circulation section 102 is in the range of 2 to 4.

[0045] The ratio D2 / D1 of the inner diameter D2 of the conveying section 103 to the inner diameter D1 of the guide tube 2 is in the range of 0.5 to 3. Preferably, the ratio D2 / D1 of the inner diameter D2 of the conveying section 103 to the inner diameter D1 of the guide tube 2 is in the range of 1 to 2.

[0046] Adjust the gas output of the annular gap area inlet pipe 7 and the guide tube gas distributor 8 so that the gas velocity range of the guide tube 2 is 0.1 to 20 m / s, preferably, the gas velocity range of the guide tube 2 is 0.5 to 10 m / s. The gas velocity range of the conveying section 103 is 1 to 30 m / s, preferably, the gas velocity range of the conveying section is 1.5 to 15 m / s. Specifically, the gas velocity range of the guide tube gas distributor 2 is 5 to 100 m / s, preferably, the gas velocity range of the guide tube gas distributor 2 is 10 to 50 m / s.

[0047] Please refer to Figures 4 to 6 In this embodiment, the draft tube gas distributor 8 is of coil type, including a connected annular tube portion 801 and a straight tube portion 802. The top of the annular tube portion 801 is evenly spaced with a plurality of gas outlets, all of which are aligned with the draft tube 2. The straight tube portion 802 passes through the outer wall of the shell 1 and is connected to the external gas source. The coil type draft tube gas distributor 8 provides a more uniform cross-sectional distribution of the inlet gas.

[0048] Please refer to Figure 7 In other embodiments, the guide tube gas distributor 8 is of a duct type, and the guide tube gas distributor 8 is a duct, which is inserted from the bottom of the shell 1, the gas outlet of the duct is aligned with the guide tube 2, and the gas inlet of the duct is connected to the external gas source. The duct type guide tube gas distributor 8 has a simpler geometric structure and is easier to control the gas inlet direction.

[0049] Please refer to Figure 1 In this embodiment, the annular gap area air inlet pipe 7 can be set to multiple, and is evenly spaced circumferentially at the bottom of the circulation section 101, which can make the particle circulation more uniform and smooth during operation.

[0050] In this embodiment, the motor 3 is installed on the top of the housing 1 and is connected to the top of the guide tube 2 via the stirring shaft 9 to drive the guide tube 2 to rotate.

[0051] Please refer to Figure 2 In other embodiments, the motor 3 is installed at the bottom of the housing 1 and connected to the bottom of the draft tube 2 through the stirring shaft 9 to drive the draft tube 2 to rotate. The stirring shaft 9 passes through the center of the coil-type draft tube gas distributor 8.

[0052] In this embodiment, stirring and strengthening the particle circulation is achieved by the motor 3. The external power supply is powered on to start the motor 3, and the motor 3 drives the guide tube 2 and the stirring blades 5 on the outer wall of the guide tube to rotate continuously through the stirring shaft 9. Under the action of the stirring blades 5, the agglomerates that may be formed in the annular gap area 6 are broken, and the stable and continuous circulation flow of the micro-nano particles in the circulation section 101 is achieved.

[0053] Example 2 Please refer to Figure 3 , similar to Example 1, except that the stirring particle circulation coupling reactor of this embodiment is different, the outer wall of the guide tube 2 is connected to the shell 1 through a connecting rod, the driving mechanism includes a motor 3, a driving gear 14, a driven gear 15 and a stirring shaft 9, the motor 3 can be installed at the bottom of the shell 1 through a motor mounting bracket, the output shaft of the motor 3 is connected to the driving gear 14, the driving gear 14 is meshed with the driven gear 15, the stirring shaft 9 is connected to the driven gear 15, and the stirring blade 5 is arranged on the stirring shaft 9.

[0054] Specifically, the upper and lower ends of the outer wall of the guide tube 2 are connected to the inner wall of the shell 1 through a connecting rod, which is used to fix the guide tube 2. The stirring blade 5 is set in the annular gap area 6 and does not contact the outer wall of the guide tube 2 and the inner wall of the shell 1. When working, the motor 3 first drives the driving gear 14 to rotate, and the driving gear 14 transmits the power to the driven gear 15, thereby driving the stirring shaft 9 connected to the driven gear 15 to rotate, and directly drives the stirring blade 5 on the surface of the stirring shaft to rotate. Under the action of the stirring blade 5, the agglomerates that may be formed in the annular gap area 6 are broken, and the stable and continuous circulation flow of micro-nano particles in the circulation section 101 is realized. The driven gear 15 corresponds to the stirring shaft 7 one by one. Considering the space limitation and the stirring range, multiple driven gears can be set. Generally, the number of groups of driven gears 15 and stirring shafts 9 is 2 to 16. Preferably, the number of groups of driven gears 15 and stirring shafts 9 is 4 to 8.

[0055] Example 3 Please refer to Figure 1 , Figure 2 and Figure 3The present embodiment provides a stirred particle circulation coupled fluidized bed, comprising the stirred particle circulation coupled reactor in embodiment 1, a solid recovery device 10 and a storage tank 11, wherein the solid recovery device 10 and the storage tank 11 constitute a gas-solid recovery system, wherein the solid recovery device 10 is connected to the discharge port of the reactor through a pipeline, the solid recovery device 10 is connected to the top of the storage tank 11 through a pipeline, and the bottom of the storage tank 11 is connected to the return port of the reactor through a feed pipe 12. The storage tank 11 is installed through a bracket, and the bottom of the storage tank 11 is higher than the return port, which is conducive to the particles falling back into the reactor.

[0056] The function of the gas-solid recovery system is to collect particles entrained in the airflow from the conveying section 103. The collected particles enter the storage tank 11 from the lower part of the solid recovery device 10, and the gas is discharged from the solid recovery device 10. The particles are then returned to the lower part of the flow reactor from the bottom of the storage tank 11 through the discharge pipe 12. The solid recovery device 10 is a prior art product. The solid recovery device 10 includes a combination structure of a multi-stage cyclone separator and a bag filter. The multi-stage cyclone separator can specifically be three stages. Among them, the multi-stage cyclone separator can collect most of the particles, and the settled particles enter the storage tank 11 through the lower material legs, and the gas and a small amount of entrained particles enter the bag filter. In the bag filter, the particles are collected in the bags and returned to the storage tank 11 regularly, and the gas is discharged to the atmosphere.

[0057] In this embodiment, a solid circulation rate measuring device 16 is provided between the storage tank 11 and the solid recovery device 10. The solid circulation rate measuring device 16 is a prior art. Specifically, a length scale is marked on the outer wall of the solid circulation rate measuring device 16, and a valve is provided at the bottom. When the fluidized bed is continuously circulated and fluidized, particles are discharged from the bottom of the gas-solid separation device 10 into the solid circulation rate measuring device 16 and enter the storage tank 11. When measuring the solid circulation rate, the bottom valve of the solid circulation rate measuring device 16 is temporarily closed and timing is started. The particles gradually accumulate in the solid circulation rate measuring device 16. When the particles accumulate to a predetermined scale, the timing is ended to obtain the time of the solid circulation rate measurement process. According to the inner diameter of the solid circulation rate measuring device 16 and the particle accumulation height, the volume of the externally circulated particles in the solid circulation rate measurement process can be calculated, and the mass of the externally circulated particles can be calculated according to the particle accumulation density. Then, the cross-sectional area of ​​the conveying section 103 is obtained according to the inner diameter of the conveying section 103, and the measurement of the solid circulation rate in the fluidized bed can be completed.

[0058] In this embodiment, a valve is provided on the feed pipe 12. When the fluidized bed is continuously circulated and fluidized, the valve is opened, and the particle circulation rate can be controlled by adjusting the valve opening, and the fluidized particles are collected in the storage tank 11. The storage tank 11 is also provided with a discharge pipe 13, through which the fluidized particles are discharged.

[0059] In this embodiment, flow meters are provided at the front end of the guide tube gas distributor 8 and the front end of the annular gap area air inlet pipe 7; the superficial gas velocity in the guide tube 2 = the gas flow rate in the guide tube 2 / the cross-sectional area of ​​the guide tube 2, the gas flow rate is measured by the flow meter at the front end of the guide tube gas distributor 8, and the cross-sectional area of ​​the guide tube 2 is obtained according to the inner diameter of the guide tube 2; the superficial gas velocity in the conveying section 103 = the gas flow rate in the conveying section 103 / the cross-sectional area of ​​the conveying section 103. The gas flow rate in the conveying section 103 = the gas flow rate in the guide tube 2 + the gas flow rate in the annular gap area 6, and the cross-sectional area of ​​the conveying section 103 is obtained according to the inner diameter of the conveying section 103.

[0060] Example 4 Please refer to Figure 8 The particle circulation coupling method provided in this embodiment is based on the stirred particle circulation coupling fluidized bed in Example 2, and specifically includes the following steps: S01, adding particles into a reactor; S02, starting the motor 3 to drive the stirring blade 5 to rotate, so as to break up the agglomerates formed in the annular gap area 6; S03, adjusting the gas flow rate of the annular gap area air inlet pipe 7 and the guide tube gas distributor 8, so that the bottom pressure of the guide tube 2 and the bottom pressure of the annular gap area 6 are not equal, so that part of the particles circulate in the annular gap area 6 and the guide tube 2; and the other part of the particles enter the solid recovery device 10 through the conveying section 103; S04, the solid recovery device 10 separates the gas from the particles, the gas is discharged into the atmosphere, and the particles enter the storage tank 11; S05, the storage tank 11 then transports the particles therein back to the reactor through the discharge pipe 12 to achieve a cyclic operation.

[0061] In this embodiment, compressed air enters the reactor through the annular gap area air inlet pipe 7 and the guide tube gas distributor 8, and the airflow introduced by the guide tube gas distributor 8 ventilates the micro-nano particles in the guide tube 2, and the airflow introduced by the annular gap area air inlet pipe 7 ventilates the micro-nano particles in the annular gap area 6. The ratio of the gas flow rates of the guide tube 2 and the annular gap area 6 is adjusted by adjusting the air intake amount of the annular gap area air inlet pipe 7 and the guide tube gas distributor 8, and the direction of the circulation can be a center air lift type and a center drop type.

[0062] Please refer to Fig. 9In this embodiment, in step S02, the gas flow rate of the annular gap area air inlet pipe and the guide tube gas distributor is adjusted. When the central air lift operation is adopted, the bottom pressure of the guide tube 2 is made less than the bottom pressure of the annular gap area 6. The particles flow from the bottom of the annular gap area 6 to the bottom of the guide tube 2 in a directional manner. Under the action of the air flow introduced by the guide tube gas distributor 8, the particles move upward to the top of the guide tube 2 area. After the particles leave the top of the guide tube 2, a part of the particles flow into the annular gap area 6, and move downward to the bottom of the circulation section 101 through the annular gap area 6, realizing continuous central air lift circulation flow; another part of the particles flow into the conveying section 103, and the particles in the conveying section 103 are in a pneumatic conveying state, which can ensure that the particles are taken out of the reactor system in time to realize external circulation. The gas-solid two-phase flow in the conveying section 103 passes through the solid recovery device 10 to separate the particles from the gas, and the gas is discharged to the atmosphere. The particles enter the storage tank 12 and finally return to the circulation section 101 in the reactor through the discharge pipe 12 to realize the circulation operation.

[0063] Please refer to Fig.10 When the center descending operation is adopted, in the step of adjusting the gas flow rate of the annular gap area inlet pipe and the gas distributor of the guide tube, the bottom pressure of the guide tube is made greater than the bottom pressure of the annular gap area, and the particles flow directionally from the bottom of the guide tube into the bottom of the annular gap area; the particles move upward to the top of the annular gap area under the action of the airflow introduced into the annular gap area inlet pipe, and after the particles leave the top of the annular gap area, a part of the particles flow into the guide tube, and move downward to the bottom of the annular flow section through the guide tube, realizing continuous center descending annular flow; the other part of the particles flow into the conveying section 103, and the particles in the conveying section 103 are in a pneumatic conveying state, which can ensure that the particles are taken out of the reactor system in time to realize circulation. The gas-solid two-phase flow in the conveying section 103 passes through the solid recovery device 10 to separate the particles from the gas, the gas is discharged to the atmosphere, the particles enter the storage tank 12, and finally return to the annular flow section 101 in the reactor through the discharge pipe 12 to realize the circulation operation.

[0064] In a specific application, the reactor in the fluidized bed adopts an arrangement in which the motor 3 is placed at the bottom of the shell 1 as an example. The inner diameter of the conveying section 103 is 20 mm and the height is 1600 mm; the inner diameter of the guide tube 2 is 20 mm and the height is 300 mm; the inner diameter of the circulation section 101 is 60 mm and the height is 440 mm. The ratio D1 / D0 of the inner diameter D1 of the guide tube 2 to the inner diameter D0 of the circulation section 101 is 0.33; the ratio H1 / H0 of the height H1 of the guide tube 2 to the height H0 of the circulation section 101 is 0.68; the ratio H2 / H0 of the height H2 of the conveying section 103 to the height H0 of the circulation section 101 is 3.64; the ratio D2 / D1 of the inner diameter D2 of the conveying section 103 to the inner diameter D1 of the guide tube 2 is 1.0; the apparent gas velocity range of the guide tube 2 is 0.5 to 1.5 m / s; the apparent gas velocity range of the conveying section 103 is 1.5 to 4.5 m / s; the guide tube gas distributor 8 adopts a coil air intake method with a gas velocity of 20 m / s. The particles are desulfurized ash particles with a volume average particle size of 10μm and a particle density of 1788 kg / m3, which are micro-nano particles. Particles 60 cm high are piled up in the storage tank 11 to provide back pressure for the entire fluidized bed particle circulation. The shell 1 and the storage tank 11 can be approximately regarded as communicating vessels. The particles are piled up in the storage tank 11, and static pressure is generated under the action of gravity. Then the particles in the storage tank 11 will spontaneously enter the circulation section 101 through the discharge inclined pipe 12; the valve opening on the discharge pipe 12 is set to 100%, which is in a fully open state. At this time, the fluidized bed can achieve the maximum particle circulation rate. When the apparent gas velocity of the conveying section 103 is fixed at 4.5 m / s, the rotation speed of the guide tube 2 and the gas velocity of the guide tube 2 are adjusted by the motor 3. Please refer to Fig.12 The stirring blades 5 on the outer wall of the guide tube 2 are in the form of screw paddles for stirring enhancement, and the particle stable circulation processing capabilities of the conventional circulating coupled reactor and the stirring enhanced circulating coupled reactor are compared.

[0065] After measurement, in this embodiment: When the superficial gas velocity of the draft tube 2 is 0.5 m / s, the particle circulation rate of the conventional loop coupled reactor is 1.97 kg / m 2 s, and the particle circulation rate of the loop coupled reactor under stirring enhancement is 3.81 kg / m 2 s, an increase of 93.4%; When the superficial gas velocity of the draft tube 2 is 1.0 m / s, the particle circulation rate of the conventional loop coupled reactor is 3.17 kg / m 2 s, and the particle circulation rate of the loop coupled reactor under stirring enhancement is 6.20 kg / m 2 s, an increase of 95.6%; When the superficial gas velocity of the draft tube 2 is 1.5 m / s, the particle circulation rate of the conventional loop coupled reactor is 6.12 kg / m 2 s, and the particle circulation rate of the loop coupled reactor under stirring enhancement is 6.75 kg / m 2 s, an increase of 10.3% compared with the previous day.

[0066] Please refer to Fig.13 The stirring blades 5 on the outer wall of the guide tube 2 are in the form of propellers for stirring enhancement, and the particle stable circulation processing capabilities of the conventional circulating coupled reactor and the stirring enhanced circulating coupled reactor are compared.

[0067] After measurement, in this embodiment: When the superficial gas velocity of the draft tube 2 is 0.5 m / s, the particle circulation rate of the conventional loop coupled reactor is 1.97 kg / m 2 s, and the particle circulation rate of the loop coupled reactor under stirring enhancement is 4.72 kg / m2 s, an increase of 139.6%; When the superficial gas velocity of the draft tube 2 is 1.0 m / s, the particle circulation rate of the conventional loop coupled reactor is 3.17 kg / m 2 s, and the particle circulation rate of the loop coupled reactor under stirring enhancement is 6.40 kg / m 2 s, an increase of 101.9%; When the superficial gas velocity of the draft tube 2 is 1.5 m / s, the particle circulation rate of the conventional loop coupled reactor is 6.12 kg / m 2 s, and the particle circulation rate of the loop coupled reactor under stirring enhancement is 6.70 kg / m 2 s, an increase of 9.5% compared to the previous day.

[0068] The stirred particle circulating coupled fluidized bed of this embodiment provides additional kinetic energy to the particles through the energy introduced by stirring. The rotation of the stirring blades weakens the dominant role of the airflow in overcoming the particle gravity and the interaction force between the micro-nano particles. The particle accumulation layer can expand evenly under low gas velocity conditions, the gas-solid contact efficiency is improved, and the micro-nano particles can achieve a better fluidized state. Compared with the existing circulating coupled reactor, the circulating coupled reactor enhanced by stirring achieves a higher micro-nano particle circulation rate under the same operating conditions, with better fluidization effect and more stable circulation.

[0069] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, rather than to limit it. Although the present invention has been described in detail with reference to the aforementioned embodiments, those skilled in the art should understand that they can still modify the technical solutions described in the aforementioned embodiments, or make equivalent replacements for some of the technical features therein. However, these modifications or replacements do not deviate the essence of the corresponding technical solutions from the spirit and scope of the technical solutions of the embodiments of the present invention.

Claims

1. A stirred particle circulation coupled reactor, characterized in that: include: The shell includes a circulation section, a transition section and a conveying section which are arranged from bottom to top, wherein the transition section is provided with a feed inlet, the circulation section is provided with a return inlet, and the conveying section is provided with a discharge inlet; A guide tube is arranged in the annular flow section; the area between the outer wall of the guide tube and the inner wall of the shell is an annular gap area; an annular gap area air inlet pipe is arranged at the bottom of the annular flow section, and a guide tube gas distributor is arranged below the guide tube; the annular gap area air inlet pipe and the guide tube gas distributor are respectively connected to an external gas source; The stirring blade is arranged in the annular gap area and is driven to rotate by a driving mechanism.

2. The stirred particle circulation coupled reactor according to claim 1, characterized in that: The driving mechanism comprises a motor, the motor is arranged on the shell, the motor is connected to the guide tube via a stirring shaft, the stirring blade is arranged on the outer wall of the guide tube, and the motor is used to drive the guide tube to rotate.

3. The stirred particle circulation coupled reactor according to claim 1, characterized in that: The side wall of the guide cylinder is connected to the shell through a connecting rod. The driving mechanism includes a motor, a driving gear, a driven gear and a stirring shaft. The motor is arranged at the bottom of the shell. The output shaft of the motor is connected to the driving gear, the driving gear is meshed with the driven gear, the stirring shaft is connected to the driven gear, and the stirring blade is arranged on the stirring shaft.

4. The stirred particle circulation coupled reactor according to claim 1, characterized in that: The guide tube gas distributor comprises a connected annular tube portion and a straight tube portion, a plurality of gas outlet holes are evenly spaced at the top of the annular tube portion, all of the gas outlet holes are aligned with the guide tube, and the straight tube portion is connected to the external gas source.

5. The stirred particle circulation coupled reactor according to claim 1, characterized in that: The guide tube gas distributor is a conduit, the gas outlet of the conduit is aligned with the guide tube, and the gas inlet of the conduit is connected to the external gas source.

6. A stirred particle circulation coupled fluidized bed, characterized in that: It comprises a stirred particle circulation coupled reactor, a solid recovery device and a storage tank as described in any one of claims 1 to 5, wherein the solid recovery device is connected to the discharge port through a pipeline, the solid recovery device is connected to the top of the storage tank through a pipeline, and the bottom of the storage tank is connected to the return port through a discharge pipe.

7. The stirred particle circulation coupled fluidized bed according to claim 5, characterized in that: The feed pipe is provided with a valve; the storage tank is also provided with a discharge pipe.

8. A particle circulation coupling method, characterized in that: The stirring particle circulation coupled fluidized bed according to any one of claims 6 to 7 is completed, comprising the following steps: adding particles into a reactor; Start the motor to drive the stirring blade to rotate to break up the agglomerates formed in the annular gap area; Adjust the gas flow rate of the annular gap area air inlet pipe and the guide tube gas distributor to make the bottom pressure of the guide tube and the bottom pressure of the annular gap area different, so that part of the particles circulate in the annular gap area and the guide tube; and another part of the particles enter the solid recovery device through the conveying section; The solid recovery device separates the gas from the particles, the gas is discharged to the atmosphere, and the particles enter the storage tank; The storage tank then transports the particles in the storage tank back to the reactor through the discharge pipe to achieve a circulation operation.

9. The particle circulation coupling method according to claim 8, characterized in that: In the step of adjusting the gas flow rate of the air inlet pipe and the guide tube gas distributor in the annular gap area, the bottom pressure of the guide tube is made lower than the bottom pressure of the annular gap area, and the particles flow directionally from the bottom of the annular gap area into the bottom of the guide tube, and the particles move upward to the top of the guide tube area under the action of the air flow introduced by the guide tube gas distributor. After the particles leave the top of the guide tube, some of the particles flow into the annular gap area, and move downward to the bottom of the annular flow section through the annular gap area, realizing continuous central air lift annular flow; the other part of the particles flow into the solid recovery device through the conveying section.

10. The particle circulation coupling method according to claim 8, characterized in that: In the step of adjusting the gas flow rate of the air inlet pipe and the gas distributor of the guide tube in the annular gap area, the bottom pressure of the guide tube is made greater than the bottom pressure of the annular gap area, and the particles flow directionally from the bottom of the guide tube into the bottom of the annular gap area; the particles move upward to the top of the annular gap area under the action of the air flow introduced into the annular gap area through the air inlet pipe, and after the particles leave the top of the annular gap area, a part of the particles flow into the guide tube, and move downward to the bottom of the annular flow section through the guide tube, thereby realizing continuous central descending annular flow; the other part of the particles flow into the solid recovery device through the conveying section.

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