Spiral-flow type particle circulation coupling reactor, fluidized bed and particle circulation coupling method

Abstract

The invention relates to a spiral-flow type particle circulation coupling reactor, a fluidized bed and a particle circulation coupling method, the fluidized bed comprises the spiral-flow type particle circulation coupling reactor, a gas-solid separation device and a material storage tank, and a jet pipe group in the spiral-flow type particle circulation coupling reactor adopts tangential gas inlet; a plurality of strands of high-speed tangential rotating airflow are formed in an area near the wall surface of the bottom of the circulation section, so that the turbulence degree of micro-nano particles at the bottom of the circulation section can be enhanced, material accumulation is destroyed, bottom viscous accumulation is destroyed, more micro-nano particles participate in circulation flow, the distribution uniformity and fluidization quality of the micro-nano particles at the bottom of the circulation section are improved, and the fluidization efficiency is improved. The problem that the micro-nano particles have a fluidization dead zone at the bottom of the fluidized bed is solved, and continuous and circulating fluidization and treatment of the micro-nano particles are achieved.

Description

Technical Field

[0001] The present invention belongs to the technical field of gas-solid fluidization of micro-nano particles, and specifically relates to a cyclonic 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 nano particles. Background Art

[0002] Micro-nano particles usually refer to Geldart C particles with an average particle size of 1 nm~1000 um. Compared with general particles, they are solid particles composed of a smaller number of atoms or molecules, and their atoms or molecules are in a metastable state in thermodynamics. Due to surface effects and volume effects, micro-nano particles maintain the chemical properties of the original substance while showing many excellent properties in magnetism, light absorption, thermal resistance, chemical activity, catalysis and melting point that millimeter-scale materials do not have. They are widely used in chemical industry, energy storage, medicine, electrocatalysis, environmental protection, agricultural production, information electronics, bioengineering and many other fields.

[0003] Fluidization technology is a multiphase flow technology that handles the mixing, mass transfer, heat transfer and chemical reactions between solid particles and gas-liquid phases in industrial processes. It is an effective means for the preparation, processing, modification, transportation and improvement of catalytic reactions of particles and powders. The particles are suspended in the fluid by a fluidized bed and made to move violently, so that the particles can produce free flow similar to that of liquid, thereby greatly enhancing the diffusion process of the substance and increasing the reaction rate. However, as the particle size decreases, the interaction force between the particles increases significantly. The strong mutual attraction between the particles makes it easy for micro-nano particles to agglomerate and channel flow during fluidization, which is not an ideal fluidization phenomenon. As a result, the particles accumulate at the bottom of the fluidized bed, and there is a fluidization dead zone, making it difficult to achieve continuous and stable fluidization. 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 cyclonic particle circulation coupling reactor, a fluidized bed and a particle circulation coupling method, wherein a tangential air intake is introduced into the reactor, and the tangential air intake mainly acts on the bottom of the annular gap area; the turbulence of the particles at the bottom of the annular gap area is enhanced by the tangential air intake, thereby solving the problem of the fluidization dead zone of micro-nano particles at the bottom of the fluidized bed, and realizing the continuous and circulating fluidization and processing of micro-nano particles.

[0005] To achieve the above object, the present invention adopts the following technical solutions: A cyclonic particle circulation coupled reactor, comprising: The shell includes a circulation section, a transition section and a conveying section distributed 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 top of the conveying section is provided with a discharge inlet; A flow guide tube is arranged in the circulation section and connected to the flow guide tube through a connecting rod; the area between the outer wall of the flow guide tube and the inner wall of the shell is an annular gap area; a jet tube group is tangentially arranged on the side wall of the circulation section along the circumferential direction, and a flow guide tube air inlet is arranged below the flow guide tube at the bottom of the shell.

[0006] Preferably, the inner diameter of the conveying section is smaller than the inner diameter of the circulation section.

[0007] Preferably, the circulation section is provided with a plurality of groups of the jet tube groups from bottom to top in the height direction.

[0008] Preferably, at least two jet tubes are arranged in each jet tube group, and all the jet tubes are evenly spaced and tangentially arranged on the side wall of the circulation section along the circumferential direction.

[0009] A cyclonic particle circulation coupled fluidized bed comprises a cyclonic particle circulation coupled reactor as described in any one of the above, a gas-solid separation device and a storage tank, wherein the gas-solid separation device is arranged on the top of the shell and connected to the discharge port, the storage tank is connected to the gas-solid separation device through a pipeline, and the bottom of the storage tank is connected to the return port through a discharge inclined pipe; a valve is provided on the discharge inclined pipe.

[0010] Preferably, a solid circulation rate measuring device is provided between the storage tank and the gas-solid separation device.

[0011] Preferably, the gas-solid separation device comprises an expanded diameter section, a baffle and an exhaust pipe, the expanded diameter section is sleeved on the top of the conveying section 103; the baffle is arranged above the discharge port, and the exhaust pipe is connected to the top of the expanded diameter section.

[0012] A particle circulation coupling method is based on any one of the above-mentioned cyclonic particle circulation coupling fluidized bed, comprising the following steps: adding particles into a reactor; Gas is introduced into the reactor through the air inlet of the guide tube and the jet pipe, so that a part of the particles circulate in the annular gap area and the guide tube; and another part of the particles enters the gas-solid separation device through the conveying section; Adjust the air intake of the jet tube group to form multiple tangential rotating airflows in the bottom area of ​​the annular flow section to destroy the accumulation and agglomeration of particles at the bottom of the annular flow section; The gas-solid separation device separates the gas from the particles, the gas is discharged into 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 inclined pipe to achieve external circulation operation.

[0013] Preferably, in the step of adjusting the air intake volume of the jet tube group, 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 into the air inlet of the guide tube. 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 gas-solid separation device through the conveying section.

[0014] Preferably, in the step of adjusting the air intake volume of the jet tube group, 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 by the jet tube group, 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 gas-solid separation device through the conveying section.

[0015] The present invention adopts the above technical solution, which has the following advantages: 1. In the swirl-type particle circulation coupling reactor provided by the present invention, the jet tube group adopts tangential air intake, and forms multiple high-speed tangential rotating airflows in the area near the bottom wall of the circulation section, which can enhance the turbulence of the micro-nano particles at the bottom of the circulation section, destroy the material accumulation, thereby destroying the bottom viscous accumulation, allowing more micro-nano particles to participate in the circulation flow, improving the distribution uniformity and fluidization quality of the micro-nano particles at the bottom of the circulation section, solving the problem of the existence of fluidization dead zone of micro-nano particles at the bottom of the fluidized bed, and realizing continuous and cyclic fluidization and treatment of micro-nano particles.

[0016] 2. The swirl-type 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 gas flow rate of the guide tube and the annular gap area, the direction of the circulation can be a center gas lift type and a center descending type; by adjusting the swirl air intake of the jet tube group, the internal circulation flux and the external circulation flux of the particles in the circulation coupling reactor can be regulated, thereby realizing the regulation of the distribution ratio of micro-nano particles in the circulation coupling reactor; by strengthening the gas-solid interaction of the micro-nano particles in the circulation coupling reactor through swirl air intake, the accumulation problem of micro-nano particles at the bottom of the fluidized bed and the distribution problem of the internal and external circulation amount of the micro-nano particles are solved, thereby realizing the continuous and stable flow of micro-nano particles in the swirl-enhanced circulation coupling reactor. BRIEF DESCRIPTION OF THE DRAWINGS

[0017] Figure 1 It is a schematic structural diagram of a swirling particle circulation coupled fluidized bed provided in one embodiment of the present invention.

[0018] Figure 2It is a schematic diagram of the cross-sectional structure of a jet tube assembly provided in one embodiment of the present invention.

[0019] Figure 3 It is a flow chart of a particle circulation coupling method provided by one embodiment of the present invention.

[0020] Figure 4 It is a schematic diagram of particle circulation of central airlift type provided by one embodiment of the present invention.

[0021] Figure 5 It is a schematic diagram of a center-down particle circulation provided by an embodiment of the present invention.

[0022] 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 feed port, 4 is a jet pipe, 5 is an air inlet of the guide tube, 6 is a gas-solid separation device, 7 is a storage tank, 8 is a discharge inclined pipe, 9 is a discharge pipe, and 10 is a solid circulation rate measuring device. DETAILED DESCRIPTION

[0023] 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.

[0024] 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.

[0025] 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.

[0026] The present invention provides a swirling particle annular flow coupling reactor, a fluidized bed and a particle annular flow coupling method, wherein a tangential air intake is introduced into the reactor, and the tangential air intake mainly acts on the bottom of the annular gap area; the turbulence of the particles at the bottom of the annular gap area is enhanced by the tangential air intake, thereby solving the problem of a fluidization dead zone of micro-nano particles at the bottom of the fluidized bed, and realizing continuous and cyclic fluidization and treatment of micro-nano particles.

[0027] The embodiments of the present invention are described in detail below with reference to the accompanying drawings.

[0028] Example 1 Please refer to Figure 1 The present embodiment provides a cyclonic particle circulation coupling 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 3, and particles are added into the shell 1 from the feed port 3. The circulation section 101 is provided with a return port, and the top of the conveying section 103 is provided with a discharge port. The guide tube 2 is arranged in the circulation section 101 and is fixedly connected to the inner wall of the guide tube 2 through a connecting rod; the area between the outer wall of the guide tube 2 and the inner wall of the shell 1 is the annular gap area; the side wall of the circulation section 101 is tangentially provided with a jet tube group along the circumferential direction, and a guide tube air inlet 5 is arranged below the guide tube 2 at the bottom of the shell 1, and each jet tube 4 in the jet tube group and the guide tube air inlet 5 are respectively connected to an external air source.

[0029] In specific applications, the guide tube 2 is a circular tubular structure with openings at both the top and the bottom. The guide tube 2 is set at the center of the circulation section 101, and the center lines of the two coincide. The highest point of the guide tube 2 is lower than the top of the circulation section 101. Two connecting rods are connected between the guide tube 2 and the inner wall of the circulation section 101, so that the guide tube 2 and the circulation section 101 are relatively fixed. When the reactor is working, some particles circulate between the guide tube 2 and the annular gap to achieve internal circulation of particles in the reactor. In addition, the jet tube group adopts tangential air intake to reduce the accumulation of micro-nano particles at the bottom of the circulation section 101 and destroy the agglomeration of micro-nano particles, promoting the mixing and uniform fluidization of particles in the shell.

[0030] 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 gas-solid separation device 6 and a storage tank 7.

[0031] In this embodiment, the circulation section 101 is provided with multiple jet tube groups from bottom to top in the height direction, two adjacent jet tube groups are parallel, and at least one jet tube of all the jet tube groups is arranged parallel to the lower end surface of the guide tube 2. Figure 2As shown, each jet tube group is provided with at least two jet tubes 4, specifically four, six or eight jet tubes, and all the jet tubes 4 are evenly spaced and tangentially arranged on the side wall of the circulation section 101 along the circumferential direction.

[0032] In a specific application, by setting a plurality of jet tubes 4 on the outer wall of the circulation section 101, a high-velocity auxiliary wind is introduced tangentially along the inner side of the wall of the circulation section 101, and multiple high-speed tangential rotating airflows are formed in the area near the bottom wall of the circulation section 101, and the particle accumulation material layer in the bottom space of the circulation section 101 is tangentially injected along the inner side of the wall of the circulation section 101. The swirl wind has a high kinetic energy, which can enhance the gas-solid flow characteristics of micro-nano particles in the circulation coupling reactor from two aspects. On the one hand, multiple high-speed swirl winds can make the micro-nano particle materials accumulated in the bottom wall area of ​​the circulation section 101 form an overall circumferential motion trend, strengthen the turbulence of the particles, destroy the accumulation of materials, and thus destroy the bottom viscous accumulation, so that more micro-nano particles participate in the circulation flow, improve the uniformity of the distribution of micro-nano particles at the bottom of the circulation section and the fluidization quality, solve the problem of the existence of a fluidization dead zone of micro-nano particles at the bottom of the fluidized bed, and realize the continuous and cyclic fluidization and treatment of micro-nano particles.

[0033] Example 2 Please refer to Figure 1 As shown, the present embodiment provides a cyclonic particle circulation coupled fluidized bed, comprising the cyclonic particle circulation coupled reactor, the gas-solid separation device 6 and the storage tank 7 in Embodiment 1, the gas-solid separation device 6 is arranged at the top of the shell 1 and connected to the discharge port, the storage tank 7 is connected to the gas-solid separation device 6 through a pipeline, and the bottom of the storage tank 7 is connected to the return port through a discharge inclined pipe 8; a valve is arranged on the discharge inclined pipe 8.

[0034] In a specific application, the bottom of the storage tank 7 is higher than the return port, which is conducive to the particles falling back into the reactor.

[0035] The function of the gas-solid recovery system is to collect particles entrained in the air flow from the conveying section 103. The collected particles enter the storage tank 7 from the lower part of the gas-solid separation device 6, and the gas is discharged from the upper part of the gas-solid separation device 6. The particles then return to the lower part of the flow reactor from the bottom of the storage tank 7 through the discharge inclined pipe 8.

[0036] In this embodiment, the gas-solid separation device 6 includes an expanded diameter section, a baffle and an exhaust pipe. The expanded diameter section is sleeved on the top of the conveying section 103; the baffle is arranged above the discharge port, and the exhaust pipe is connected to the top of the expanded diameter section.

[0037] Specifically, the gas-solid separation device 6 is provided with a baffle plate above the conveying section 103 at the top of the shell 1. The baffle plate can be welded above the discharge port of the conveying section 103 through a connecting rod. The expansion section is sleeved outside the conveying section 103. The exhaust pipe is connected to the top of the expansion section. The gas-solid separation is achieved through the baffle plate and the expansion section. After the gas-solid two-phase flow leaves the conveying section 103, it is intercepted by the baffle plate and moves to the surroundings. Since the inner diameter of the expansion section of the gas-solid separation device 6 is larger than the inner diameter of the conveying section 103, the ratio of the two is in the range of 5:1 to 30:1, and can be specifically 15:1. After the gas-solid two-phase flow leaves the conveying section 103, the gas velocity decreases significantly, causing the drag force on the particles to decrease and then fall to the bottom of the gas-solid separation device 6, and then enter the storage tank 7 through the solid circulation rate measuring device 10; the gas of the gas-solid two-phase flow is discharged through the exhaust pipe of the gas-solid separation device 6. Since the particle size of micro-nano particles is very small, gas-solid separation is difficult. After passing through the gas-solid separation device 6, there are still a small amount of particles entrained. Therefore, after the gas-solid two-phase flow passes through the gas-solid separation device 6, the gas passes through the filter for further gas-solid separation. A filter can be set at the end of the exhaust pipe to reduce the discharge of particles into the atmosphere. In this example, the filter adopts a tubular container, in which glass beads are added, and the gas entrained with a small amount of micro-nano particles is passed into the tubular container. The interaction between the particles and the glass beads causes the particles to slow down, and the particles settle at the bottom of the container. The gas is discharged from the other end of the tubular container, thereby completing the gas-solid separation.

[0038] In this embodiment, a valve is provided on the discharge inclined pipe 8. When the fluidized bed is continuously circulated and fluidized, the valve is opened, and the particles are circulated and fluidized in the shell 1, the gas-solid separation device 6 and the storage tank 7, forming an external circulation of the particles. The particles enter the annular gap area from the discharge inclined pipe 8. Under the carrying effect of the air intake in the annular gap area, the particles flow upward along the annular gap area to the top of the circulation section 101. A part of the particles are carried by the gas into the conveying section 103, and enter the storage tank 7 after completing the gas-solid separation through the gas separation device 6, and then enter the circulation section 101 through the discharge inclined pipe 8, forming a complete external circulation process of the circulation section, and the fluidized particles are collected in the storage tank 7. A discharge pipe 9 is also provided at the bottom of the storage tank 7, and the discharge of the fluidized particles is completed through the discharge pipe 9.

[0039] In this embodiment, a solid circulation rate measuring device 10 is provided between the storage tank 7 and the gas-solid separation device 6. The solid circulation rate measuring device 10 is a prior art. Specifically, a length scale is marked on the outer wall of the solid circulation rate measuring device 10, 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 6 into the solid circulation rate measuring device 10 and enter the storage tank 7. When measuring the solid circulation rate, the bottom valve of the solid circulation rate measuring device 10 is temporarily closed and the timing is started. The particles gradually accumulate in the solid circulation rate measuring device 10. 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 10 and the particle accumulation height, the volume of particles that are externally circulated during the solid circulation rate measurement process can be calculated, and then the mass of particles that are externally circulated can be calculated in combination with the particle accumulation density. Then, according to the inner diameter of the conveying section 103, its cross-sectional area is obtained, and the measurement of the solid circulation rate in the fluidized bed can be completed.

[0040] In this embodiment, a flow meter is provided upstream of the air inlet 5 of the guide tube, and the air intake volume is adjusted by controlling the opening of the valve on the flow meter, thereby controlling the apparent air velocity in the guide tube area, that is, the air intake volume of the guide tube 2; a flow meter is also provided upstream of the jet tube 4, and the air intake volume is adjusted by controlling the opening of the valve on the flow meter, thereby controlling the apparent air velocity of the conveying section 103; the air intake volume of the conveying section 103 is equal to the sum of the air intake volume of the guide tube 2 and the air intake volume of the jet tube 4.

[0041] Example 3 Please refer to Figure 3 As shown, the particle circulation coupling method provided in this embodiment is completed based on the cyclonic particle circulation coupling fluidized bed in Example 2, and specifically includes the following steps: S01, adding particles into a reactor; S02, introducing gas into the reactor through the air inlet 5 of the guide tube and the jet tube 4, so that a part of the particles circulate in the annular gap area and the guide tube 2; and another part of the particles enter the gas-solid separation device 6 through the conveying section; S03, adjusting the air intake of the jet tube group to form multiple tangential rotating airflows in the bottom area of ​​the circulation section to destroy the accumulation and agglomeration of particles at the bottom of the circulation section; S04, separating the gas from the particles through the gas-solid separation device 6, the gas is discharged into the atmosphere, and the particles enter the storage tank 7; S05, the storage tank 7 then transports the particles therein back to the reactor through the discharge inclined pipe 8 to achieve external circulation operation.

[0042] Specifically, the particles are added into the reactor through the feed port 3, and the gas is introduced into the circulation section 101 through the air inlet 5 of the guide tube at the bottom of the reactor. The particles move upward under the fluidizing wind of the guide tube 2. After coming out from the top of the guide tube 2, most of the particles change their movement direction and enter the annular gap area between the guide tube 2 and the circulation section 101. The particles in the annular gap area move downward, and after moving to the bottom space, the particles flow radially into the guide tube 2, completing a circulation flow. Another part of the micro-nano particles coming out from the top of the guide tube 2 enters the conveying section 103 and continues to move upward. After separation by the gas-solid separation device 6, the micro-nano particles return to the storage tank 9, and the micro-nano particles enter the circulation section 101 through the discharge inclined pipe 8 below the storage tank 9, completing the entire cycle.

[0043] In the bottom space of the circulation section 101, high-velocity auxiliary wind is introduced tangentially along the inner side of the wall of the circulation section 101 through the jet tube group, and multiple high-speed tangential rotating airflows are formed in the area near the bottom wall of the circulation section 101, which are tangentially injected into the accumulated material layer in the bottom space of the circulation section 101 along the inner side of the bed wall. The multiple high-speed swirling winds can make the micro-nano particle materials accumulated in the bottom wall area of ​​the circulation section 101 form an overall circumferential movement trend, destroy the material accumulation and agglomeration, thereby destroying the bottom viscous accumulation, allowing more micro-nano particles to participate in the circulation flow, and improving the distribution uniformity and fluidization quality of the micro-nano particles at the bottom of the circulation section 101, thereby ensuring the normal operation of the circulating coupled reactor of micro-nano particles, improving the gas-solid contact efficiency in the fluidized bed, and solving the accumulation problem of micro-nano particles at the bottom of the fluidized bed.

[0044] In this embodiment, the swirl air intake in the middle area of ​​the circulation section 101, i.e., the annular gap area, can keep the micro-nano particles in the annular gap area in a fluidized state, thereby strengthening the circulation flow of the micro-nano particles in the annular gap area. By adjusting the air intake of the jet tube group, the air volume of the swirl air intake in the annular gap area is regulated to adjust the particle concentration in the annular gap area, thereby realizing a central air lift or central descending circulation flow. By adjusting the swirl air intake volume, the particle internal circulation flux and the external circulation flux of the circulating coupling reactor can also be regulated to realize the regulation of the distribution ratio of the micro-nano particles in the circulating coupling reactor, thereby realizing the continuous and stable flow of the micro-nano particles in the swirl-enhanced circulating coupling reactor.

[0045] Please refer to Figure 4 As shown, the central air lift operation is to make the bottom pressure of the guide tube 2 less than the bottom pressure of the annular gap area in the step of adjusting the air intake of the jet tube group, and the particles flow directionally from the bottom of the annular gap area into the bottom of the guide tube 2, and the particles move upward to the top of the guide tube area under the action of the air flow introduced into the guide tube air inlet 5. After the particles leave the top of the guide tube, a part of the particles flows into the annular gap area, and moves downward to the bottom of the annular flow section 101 through the annular gap area, realizing continuous central air lift type annular flow; the other part of the particles flows into the gas-solid separation device 6 through the conveying section.

[0046] Please refer to Figure 5 As shown, the center descending operation is to make the bottom pressure of the guide tube 2 greater than the bottom pressure of the annular gap area in the step of adjusting the air intake of the jet tube group, and the particles flow directionally from the bottom of the guide tube 2 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 by the jet tube group, 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 101 through the guide tube 2, realizing continuous center descending annular flow; the other part of the particles flow into the gas-solid separation device 6 through the conveying section.

[0047] For specific applications, please refer to Figure 1 As shown, the height of the conveying section 103 in the fluidized bed is 1600 mm, and the inner diameter of the tube is 20 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 air inlet of the jet tube in the jet tube group is tangent to the outer diameter of the circulation section 101, and a cyclone is formed by using the tangential air inlet to achieve circulation enhancement. Please refer to Figure 4 and Figure 5 As shown, two layers of jet tube group air inlets are arranged at the bottom of the circulation section 101, and three layers of jet tube group air inlets are arranged in the annular gap area. Each layer of jet tube group tangential air inlet is provided with four jet tubes with an inner diameter of 6 mm. The swirl air intake at the bottom of the circulation section 101 can make the particles form an overall circumferential motion, destroy the stable viscous accumulation state of the particles, thereby strengthening the flow of the particles and improving the flow dead zone; the swirl air intake in the annular gap area can, on the one hand, destroy the particle accumulation in the annular gap area and improve the fluidization state of the micro-nano particles. On the other hand, by adjusting the swirl air intake amount, the operating state of the reactor can be changed to a central airlift annular flow or a central descending annular flow, and the particle distribution amount of the inner circulation of the annular section and the outer circulation of the conveying section can be further regulated, so as to achieve continuous and stable fluidization of micro-nano particles and be more conducive to process control.

[0048] Taking desulfurized ash particles as an example, the volume average particle size is 10 μm and the particle density is 1788 kg / m 3 , which are micro-nano particles. Particles piled up to 60 cm high in the storage tank 7 provide back pressure for the entire particle circulation system. The shell 1 and the storage tank 7 can be approximately regarded as a communicating vessel. The particles piled up in the storage tank 7 generate static pressure under the action of gravity, and the particles in the storage tank 7 will spontaneously enter the circulation section 101 through the discharge inclined pipe 8; the control valve opening on the discharge inclined pipe 8 is set to 100%, which is in a fully open state. At this time, it is the maximum particle circulation rate that the device can achieve. The apparent air velocity in the guide tube 2 is fixed at 2.0 m / s. By adjusting the swirl air intake and then controlling the apparent air velocity in the annular gap area, different particle circulation rate operations are achieved. After measurement, in this embodiment: When the superficial gas velocity in the transport section 103 is 2.5 m / s, the particle circulation rate of the conventional loop coupled reactor is 4.58 kg / m 2 s, and the particle circulation rate of the loop coupled reactor under cyclone enhancement is 7.90 kg / m 2 s, an increase of 72.5%; When the superficial gas velocity in the conveying section 103 is 3.5 m / s, the particle circulation rate of the conventional loop coupled reactor is 6.29 kg / m 2 s, and the particle circulation rate of the loop coupled reactor under cyclone enhancement is 8.42 kg / m 2 s, an increase of 33.9%; When the superficial gas velocity in the conveying section 103 is 4.5 m / s, the particle circulation rate of the conventional loop coupled reactor is 6.75 kg / m 2 s, and the particle circulation rate of the loop coupled reactor under cyclone enhancement is 10.20 kg / m 2 s, an increase of 51.1%.

[0049] The above shows that, compared with the conventional circulating coupled reactor, the cyclone-enhanced circulating coupled reactor achieves a higher micro-nano particle circulation rate and a more continuous and stable fluidization effect under the same operating conditions.

[0050] 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 cyclonic particle circulation coupled reactor, characterized in that: include: The shell includes a circulation section, a transition section and a conveying section distributed 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 top of the conveying section is provided with a discharge inlet; A flow guide tube is arranged in the circulation section and connected to the flow guide tube through a connecting rod; the area between the outer wall of the flow guide tube and the inner wall of the shell is an annular gap area; a jet tube group is tangentially arranged on the side wall of the circulation section along the circumferential direction, and a flow guide tube air inlet is arranged below the flow guide tube at the bottom of the shell.

2. The cyclonic particle circulation coupled reactor according to claim 1, characterized in that: The inner diameter of the conveying section is smaller than the inner diameter of the circulation section.

3. The cyclonic particle circulation coupled reactor according to claim 1, characterized in that: The circulation section is provided with a plurality of groups of the jet tube groups from bottom to top in the height direction.

4. The cyclonic particle circulation coupled reactor according to claim 1, characterized in that: At least two jet tubes are arranged in each jet tube group, and all the jet tubes are evenly spaced and tangentially arranged on the side wall of the circulation section along the circumferential direction.

5. A cyclonic particle circulation coupled fluidized bed, characterized in that: It comprises the cyclonic particle circulation coupling reactor, gas-solid separation device and storage tank as described in any one of claims 1 to 4, the gas-solid separation device is arranged on the top of the shell and connected to the discharge port, the storage tank is connected to the gas-solid separation device through a pipeline, and the bottom of the storage tank is connected to the return port through a discharge inclined pipe; a valve is provided on the discharge inclined pipe.

6. The cyclonic particle circulation coupled fluidized bed according to claim 5, characterized in that: A solid circulation rate measuring device is provided between the storage tank and the gas-solid separation device.

7. The cyclonic particle circulation coupled fluidized bed according to claim 5, characterized in that: The gas-solid separation device includes an expanded diameter section, a baffle and an exhaust pipe. The expanded diameter section is sleeved on the top of the conveying section 103; the baffle is arranged above the discharge port, and the exhaust pipe is connected to the top of the expanded diameter section.

8. A particle circulation coupling method, characterized in that: The cyclonic particle annular flow coupled fluidized bed according to any one of claims 5 to 7 is completed, comprising the following steps: adding particles into a reactor; Gas is introduced into the reactor through the air inlet of the guide tube and the jet pipe, so that a part of the particles circulate in the annular gap area and the guide tube; and another part of the particles enters the gas-solid separation device through the conveying section; Adjust the air intake of the jet tube group to form multiple tangential rotating airflows in the bottom area of ​​the annular flow section to destroy the accumulation and agglomeration of particles at the bottom of the annular flow section; The gas-solid separation device separates the gas from the particles, the gas is discharged into 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 inclined pipe to achieve external circulation operation.

9. The particle circulation coupling method according to claim 8, characterized in that: In the step of adjusting the air intake volume of the jet tube group, 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. Under the action of the airflow introduced into the air inlet of the guide tube, the particles move upward to the top of the guide tube area. After the particles leave the top of the guide tube, a part of the particles flows into the annular gap area, and moves downward to the bottom of the annular flow section through the annular gap area, realizing continuous central air lift type annular flow; the other part of the particles flows into the gas-solid separation device through the conveying section.

10. The particle circulation coupling method according to claim 8, characterized in that: In the step of adjusting the air intake volume of the jet tube group, 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 by the jet tube group, and after the particles leave the top of the annular gap area, a part of the particles flows into the guide tube, and moves downward to the bottom of the annular flow section through the guide tube, realizing continuous central descending annular flow; the other part of the particles flows into the gas-solid separation device through the conveying section.

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