A cyclone-particle loop coupled reactor, fluidized bed and particle loop coupled method

Abstract

The present application relates to a cyclone type particle loop flow coupling reactor, a fluidized bed and a particle loop flow coupling method, the fluidized bed comprising the cyclone type particle loop flow coupling reactor, a gas-solid separation device and a storage tank, a jet pipe group in the cyclone type particle loop flow coupling reactor adopts tangential gas inlet, a plurality of high-speed tangential rotating gas flows are formed in the vicinity of the bottom wall surface area of the loop flow section, the degree of turbulence of the micro-nano particles at the bottom of the loop flow section can be strengthened, the material accumulation is destroyed, thereby the viscous accumulation at the bottom is destroyed, more micro-nano particles participate in the loop flow, the uniformity of the micro-nano particle distribution at the bottom of the loop flow section and the fluidization quality are improved, the problem of the fluidization dead zone of the micro-nano particles at the bottom of the fluidized bed is solved, and the continuous, circulating fluidization and treatment of the micro-nano particles are realized.

Description

TECHNICAL FIELD

[0001] The present application belongs to the technical field of micro-nano particle gas-solid fluidization, and particularly relates to a cyclone type particle loop flow coupling reactor, a fluidized bed and a particle loop flow coupling method, which are used to realize continuous and stable treatment of micron and nano particles. BACKGROUND

[0002] Micro-nano particles generally refer to Geldart C type particles with an average particle size of 1 nm to 1000 um. Compared with general particles, solid particles composed of a small number of atoms or molecules are in a metastable state in thermodynamics. Due to surface effects and volume effects, micro-nano particles exhibit many excellent properties such as magnetism, light absorption, thermal resistance, chemical activity, catalysis and melting point, which are not possessed by millimeter-level materials, while keeping the chemical properties of the original substance. Micro-nano particles are widely used in many fields such as chemical industry, energy storage, medicine, electrocatalysis, environmental protection, agricultural production, information electronics, biological engineering and the like.

[0003] Fluidization technology is a multiphase flow technology for treating mixing, mass transfer, heat transfer and chemical reaction between solid particles and gas-liquid phases in industrial processes, and is an effective means for particle and powder preparation, processing, modification, conveying and improvement of catalytic reaction. The particles are suspended in the fluid and move intensively by using the fluidized bed, so that the particles have a free flow similar to that of a liquid, thereby greatly strengthening the diffusion process of the substance and improving the reaction rate. However, with the decrease of particle size, the interaction between particles increases significantly, and the strong mutual attraction between particles makes micro-nano particles prone to agglomeration and channeling during fluidization, thereby causing the particles to accumulate at the bottom of the fluidized bed, existing a fluidization dead zone, and making it difficult to realize continuous and stable fluidization. SUMMARY

[0004] In view of at least one problem in the prior art, the present application aims to provide a cyclone type particle loop flow coupling reactor, a fluidized bed and a particle loop flow coupling method. The tangential gas inlet mode is introduced into the reactor, and the tangential gas inlet mainly acts on the bottom of the annular gap area. The tangential gas inlet strengthens the turbulent degree of particles at the bottom of the annular gap area, thereby solving the problem of the fluidization dead zone of micro-nano particles at the bottom of the fluidized bed, and realizing continuous and circulating fluidization and treatment of micro-nano particles.

[0005] To achieve the above-mentioned purpose, the present application adopts the following technical solutions:

[0006] A cyclone type particle loop flow coupling reactor comprises:

[0007] A shell comprises a loop flow section, a transition section and a conveying section distributed from bottom to top, the transition section is provided with a feeding port, the loop flow section is provided with a return port, and the top of the conveying section is provided with a discharging port;

[0008] A draft tube is arranged in the loop flow section and connected to the draft tube through a connecting rod; the area between the outer wall of the draft tube and the inner wall of the shell is a annular gap area; the side wall of the loop flow section is tangentially provided with a jet pipe group in the circumferential direction, and the bottom of the shell is provided with a draft tube gas inlet below the draft tube.

[0009] Preferably, the inner diameter of the conveying section is smaller than the inner diameter of the loop flow section.

[0010] Preferably, the loop flow section is provided with a plurality of groups of jet pipe groups from bottom to top in the height direction.

[0011] Preferably, at least two jet pipes are arranged in each group of jet pipe groups, and all the jet pipes are uniformly spaced and tangentially arranged on the side wall of the loop flow section in the circumferential direction.

[0012] A cyclone-particle loop flow coupled fluidized bed comprises the cyclone-particle loop flow coupled reactor, the gas-solid separation device and the storage tank according to any one of the above, the gas-solid separation device is arranged at 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 arranged on the discharge inclined pipe.

[0013] Preferably, a solid circulation rate measuring device is arranged between the storage tank and the gas-solid separation device.

[0014] Preferably, the gas-solid separation device comprises a diameter expansion section, a baffle and an exhaust pipe, the diameter expansion section is sleeved at 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 diameter expansion section.

[0015] A particle loop flow coupling method is completed based on the cyclone-particle loop flow coupled fluidized bed according to any one of the above, comprising the following steps:

[0016] Particles are added to the reactor;

[0017] Gas is introduced into the reactor through the draft tube gas inlet and the jet pipe, so that a part of the particles circulate in the annular gap area and the draft tube; another part of the particles enters the gas-solid separation device through the conveying section;

[0018] The gas inlet amount of the jet pipe group is adjusted to form a plurality of tangential rotating gas flows at the bottom area of the loop flow section to break the accumulation and agglomerates of particles at the bottom of the loop flow section;

[0019] The gas-solid separation device separates the gas from the particles, the gas is discharged to the atmosphere, and the particles enter the storage tank;

[0020] The storage tank further sends the particles in it back to the reactor through a discharging inclined pipe to realize external circulation operation.

[0021] Preferably, in the step of adjusting the air intake amount of the jet pipe group, the bottom pressure of the draft tube is less than the bottom pressure of the annular gap area, the particles flow from the bottom of the annular gap area to the bottom of the draft tube in a directional manner, the particles move upward to the top of the draft tube area under the action of the air flow introduced into the draft tube air inlet, and after the particles leave the top of the draft tube, part of the particles flow into the annular gap area and move downward to the bottom of the circulating section to realize continuous central gas-lifting annular flow.

[0022] Preferably, in the step of adjusting the air intake amount of the jet pipe group, the bottom pressure of the draft tube is greater than the bottom pressure of the annular gap area, the particles flow from the bottom of the draft tube to the bottom of the annular gap area in a directional manner, the particles move upward to the top of the annular gap area under the action of the air flow introduced into the jet pipe group, and after the particles leave the top of the annular gap area, part of the particles flow into the draft tube and move downward to the bottom of the circulating section to realize continuous central downward annular flow; the other part of the particles flow into the gas-solid separation device through the conveying section.

[0023] The present application has the following advantages due to the above technical solutions:

[0024] 1. The cyclone type particle circulating coupling reactor provided by the present application adopts tangential air intake of the jet pipe group, a plurality of high-speed tangential rotating air flows are formed near the wall surface area of the bottom of the circulating section, the degree of turbulence of the micro-nano particles at the bottom of the circulating section is strengthened, the material accumulation is destroyed, the bottom viscous accumulation is destroyed, more micro-nano particles participate in the circulating flow, the uniformity of the micro-nano particle distribution at the bottom of the circulating section and the fluidization quality are improved, the problem of the existence of the fluidization dead zone of the micro-nano particles at the bottom of the fluidized bed is solved, and continuous, circulating fluidization and treatment of the micro-nano particles are realized.

[0025] 2. The cyclone type particle circulating coupling fluidized bed and the particle circulating coupling method provided by the present application realize circulating flow by using the built-in draft tube, the direction of the circulating flow can be central gas-lifting type and central downward type by adjusting the gas flow rate of the draft tube and the annular gap area, the particle internal circulation flux and the particle external circulation flux of the circulating coupling reactor can be controlled by adjusting the cyclone air intake amount of the jet pipe group, the distribution ratio of the micro-nano particles in the circulating coupling reactor is controlled, the gas-solid interaction of the micro-nano particles in the circulating coupling reactor is strengthened by the cyclone air intake, the problems of the accumulation of the micro-nano particles at the bottom of the fluidized bed and the distribution of the internal and external circulation amounts of the micro-nano particles are solved, and then the continuous and stable flow of the micro-nano particles in the cyclone-strengthened circulating coupling reactor is realized. BRIEF DESCRIPTION OF DRAWINGS

[0026] Figure 1It is structural schematic diagram of the cyclone type particle loop flow coupled fluidized bed provided by an embodiment of the present application.

[0027] Figure 2 It is cross-sectional structural schematic diagram of the jet pipe group provided by an embodiment of the present application.

[0028] Figure 3 It is flow chart of the particle loop flow coupling method provided by an embodiment of the present application.

[0029] Figure 4 It is central gas-lift type particle loop flow schematic diagram provided by an embodiment of the present application.

[0030] Figure 5 It is central down type particle loop flow schematic diagram provided by an embodiment of the present application.

[0031] Markings in the drawings:

[0032] 1 is the shell, 101 is the loop flow section, 102 is the transition section, 103 is the conveying section, 2 is the draft tube, 3 is the feeding port, 4 is the jet pipe, 5 is the draft tube air inlet, 6 is the gas-solid separation device, 7 is the storage tank, 8 is the discharge inclined pipe, 9 is the discharge pipe, 10 is the solid circulating rate measuring device. DETAILED DESCRIPTION

[0033] In order to make the purpose, technical scheme and advantages of the present application clearer, the technical scheme of the present application will be described clearly and completely below in conjunction with the drawings. Obviously, the described embodiments are some embodiments of the present application, not all embodiments. Based on the embodiments in the present application, all other embodiments obtained by those skilled in the art without creative labor fall within the scope of protection of the present application.

[0034] In the description of the present application, it should be noted that the terms "upper", "lower", "front", "back" and the like indicate the orientation or positional relationship shown in the drawings, and are only for the convenience of describing the present application and simplifying the description, and do not indicate or imply that the systems or elements referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore cannot be understood as a limitation on the present application. The arrows in the drawings represent the flow direction of the material.

[0035] In the description of the present application, it should be noted that unless otherwise explicitly specified and limited, the terms "assembly", "arrangement", "connection" should be understood broadly, for example, it can be fixedly connected, or it can be detachably connected, or integrally connected; it can be mechanically connected, or it can be electrically connected; it can be directly connected, or it can be indirectly connected through an intermediate medium; it can be the communication inside two elements. For those skilled in the art, the specific meaning of the above terms in the present application can be understood according to the specific circumstances.

[0036] The application provides a cyclone type particle loop flow coupling reactor, a fluidized bed and a particle loop flow coupling method.

[0037] In the following, the embodiments of the application are described in detail in combination with the drawings.

[0038] Embodiment 1

[0039] Please refer to Figure 1 The cyclone type particle loop flow coupling reactor provided in the embodiment comprises a shell 1 and a flow guide cylinder 2.

[0040] The shell 1 comprises a loop flow section 101, a transition section 102 and a conveying section 103 distributed from bottom to top, the transition section 102 is provided with a feeding port 3, particles are added into the shell 1 from the feeding port 3, the loop flow section 101 is provided with a back feeding port, and the top of the conveying section 103 is provided with a discharging port.

[0041] The flow guide cylinder 2 is arranged in the loop flow section 101 and is fixedly connected with the inner wall of the flow guide cylinder 2 through connecting rods; the area between the outer wall of the flow guide cylinder 2 and the inner wall of the shell 1 is a loop gap area; the side wall of the loop flow section 101 is provided with a jet pipe group in a tangential direction along the circumferential direction, the bottom of the shell 1 is provided with a flow guide cylinder air inlet 5 below the flow guide cylinder 2, and each jet pipe 4 in the jet pipe group and the flow guide cylinder air inlet 5 are respectively connected with an external air source.

[0042] In a specific application, the flow guide cylinder 2 is a circular tubular structure with openings at the top and bottom, the flow guide cylinder 2 is arranged at the center of the loop flow section 101, and the center lines of the two coincide; the highest point of the flow guide cylinder 2 is lower than the top end of the loop flow section 101, and two connecting rods are connected between the inner walls of the flow guide cylinder 2 and the loop flow section 101, so that the flow guide cylinder 2 is relatively fixed with the loop flow section 101; when the reactor works, part of the particles circulate between the flow guide cylinder 2 and the loop gap area, so as to realize the internal circulation of the particles in the reactor. In addition, the tangential air inlet of the jet pipe group can reduce the accumulation of micro-nano particles at the bottom of the loop flow section 101 and destroy the agglomeration of micro-nano particles, so as to promote the mixing and uniform fluidization of the particles in the shell.

[0043] In the embodiment, the inner diameter of the conveying section 103 is smaller than the inner diameter of the loop flow section 101, the conveying section 103 is a riser with an inner diameter smaller than the loop flow section 101, and the conveying section 103 serves to convey the micro-nano particles fully fluidized in the loop flow section 101 to a gas-solid recovery system, the gas-solid recovery system comprising a gas-solid separation device 6 and a storage tank 7.

[0044] In this embodiment, the circular flow section 101 is provided with multiple groups of jet pipe groups from bottom to top in the height direction, and adjacent two groups of jet pipe groups are parallel, and at least one group of jet pipes in all jet pipe groups is arranged in parallel with the lower end surface of the draft tube 2. Please refer to Figure 2 As shown in the figure, at least two jet pipes 4 are arranged in each group of jet pipe groups, and specifically, four, six or eight jet pipes 4 can be arranged. All jet pipes 4 are uniformly and tangentially arranged on the side wall of the circular flow section 101 in the circumferential direction.

[0045] In specific applications, by arranging a plurality of jet pipes 4 on the outer wall of the circular flow section 101, high-speed auxiliary air is tangentially injected into the circular flow section 101, and multiple high-speed tangential rotating air flows are formed near the bottom wall of the circular flow section 101, and the particle accumulation material layer in the bottom space of the circular flow section 101 is tangentially injected. The cyclone wind has high kinetic energy and can enhance the gas-solid flow characteristics of the micro-nano particles in the circulating coupling reactor from two aspects. On the one hand, the multiple high-speed cyclone winds can make the micro-nano particle material accumulated on the bottom wall of the circular flow section 101 form a whole circumferential movement trend, strengthen the particle turbulence degree, and destroy the material accumulation, thereby destroying the bottom viscous accumulation, so that more micro-nano particles participate in the circulating flow, improve the micro-nano particle distribution uniformity and fluidization quality at the bottom of the circular flow section, solve the problem of fluidization dead zone of micro-nano particles at the bottom of the fluidized bed, and realize continuous, circulating fluidization and treatment of micro-nano particles.

[0046] Embodiment 2

[0047] Please refer to Figure 1 As shown in the figure, the cyclone type particle circulating coupling fluidized bed provided in this embodiment comprises the cyclone type particle circulating coupling reactor in embodiment 1, a gas-solid separation device 6 and a storage tank 7. The gas-solid separation device 6 is arranged at the top of the shell 1 and connected with the discharge port. The storage tank 7 is connected with the gas-solid separation device 6 through a pipeline. The bottom of the storage tank 7 is connected with the return port through a discharge inclined pipe 8. A valve is arranged on the discharge inclined pipe 8.

[0048] In specific applications, the bottom of the storage tank 7 is higher than the return port, which is conducive to the return of particles to the reactor.

[0049] The function of the gas-solid recovery system is to collect particles entrained in the gas 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 are returned to the lower part of the reactor through the discharge inclined pipe 8 at the bottom of the storage tank 7.

[0050] In this embodiment, the gas-solid separation device 6 comprises a diameter expansion section, a baffle and an exhaust pipe. The diameter expansion 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 with the top of the diameter expansion section.

[0051] Specifically, the gas-solid separation device 6 is achieved by setting 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 by a connecting rod, the expansion section is sleeved outside the conveying section 103, and the exhaust pipe is connected with the top of the expansion section. The gas-solid separation is achieved by the baffle plate and the expansion section. The gas-solid two-phase flow is intercepted by the baffle plate and moves to the four directions after leaving the conveying section 103. Since the inner diameter of the expansion section of the gas-solid separation device 6 is larger than that of the conveying section 103, the ratio range is 5:1 to 30:1, and specifically can be 15:1, the gas velocity of the gas-solid two-phase flow decreases significantly after leaving the conveying section 103, which causes 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 the micro-nano particles is very small, the gas-solid separation is difficult, and a small amount of particles are still entrained after passing through the gas-solid separation device 6. Therefore, after the gas-solid two-phase flow passes through the gas-solid separation device 6, the gas is further separated by the filter, and the end of the exhaust pipe can be provided with a filter to reduce the discharge of particles into the atmosphere. In this example, the filter is a tubular container, glass beads are added therein, the gas with a small amount of micro-nano particles entrained is introduced into the tubular container, the interaction between the particles and the glass beads causes the particles to slow down, and the particles are deposited at the bottom of the container, and the gas is discharged from the other end of the tubular container, thereby completing the gas-solid separation.

[0052] In this embodiment, a valve is arranged on the discharge inclined pipe 8. When the fluidized bed is continuously circulated, the valve is opened, and the particles are circulated in the shell 1, the gas-solid separation device 6 and the storage tank 7 to form an external circulation of the particles. The particles enter the annular gap zone from the discharge inclined pipe 8, flow upwards along the annular gap zone to the top of the annular flow section 101 under the carrying action of the inlet gas in the annular gap zone, a part of the particles are carried into the conveying section 103 by the gas, and then enter the storage tank 7 after completing the gas-solid separation by the gas separation device 6, and then enter the annular flow section 101 through the discharge inclined pipe 8 to form a complete annular flow section external circulation process. The fluidized particles are collected in the storage tank 7. The bottom of the storage tank 7 is also provided with a discharge pipe 9, and the discharge of the fluidized particles is completed through the discharge pipe 9.

[0053] In this embodiment, the solid circulation rate measuring device 10 is arranged 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 surface of the solid circulation rate measuring device 10, and a valve is arranged at the bottom. When the fluidized bed is continuously circulated, the particles are discharged from the bottom of the gas-solid separation device 6, pass through the solid circulation rate measuring device 10, and enter the storage tank 7. When the solid circulation rate is measured, the valve at the bottom 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, and when the particles accumulate to a predetermined scale, the timing is stopped, and the time of the solid circulation rate measuring process is obtained. According to the inner diameter of the solid circulation rate measuring device 10 and the particle accumulation height, the particle volume circulating outside during the solid circulation rate measuring process can be calculated, and then combined with the particle bulk density, the particle mass circulating outside can be calculated. Then, the cross-sectional area of the conveying section 103 is obtained according to the inner diameter, and the measurement of the solid circulation rate in the fluidized bed is completed.

[0054] In this embodiment, a flow meter is arranged upstream of the draft tube gas inlet 5, the gas inlet amount is adjusted by controlling the opening degree of the valve on the flow meter, and then the superficial gas velocity in the draft tube zone is controlled, that is, the gas inlet amount of the draft tube 2; a flow meter is also arranged upstream of the jet pipe 4, the gas inlet amount is adjusted by controlling the opening degree of the valve on the flow meter, and then the superficial gas velocity in the conveying section 103 is controlled; the gas inlet amount of the conveying section 103 is equal to the sum of the gas inlet amount of the draft tube 2 and the gas inlet amount of the jet pipe 4.

[0055] Embodiment 3

[0056] Please refer to Figure 3 It is shown that the particle circulating coupling method provided by the embodiment, which is completed based on the cyclone type particle circulating coupling fluidized bed in the embodiment 2, specifically includes the following steps:

[0057] S01, the particles are added into the reactor;

[0058] S02, the gas is introduced into the reactor through the draft tube gas inlet 5 and the jet pipe 4, so that a part of the particles circulate in the annular gap zone and the draft tube 2; and another part of the particles pass through the conveying section and enter the gas-solid separation device 6;

[0059] S03, the gas inlet amount of the jet pipe group is adjusted, so that a plurality of tangential rotating gas flows are formed in the bottom region of the circulating section, for destroying the accumulation and agglomerates of the particles in the bottom region of the circulating section;

[0060] S04, the gas and the particles are separated through the gas-solid separation device 6, the gas is discharged to the atmosphere, and the particles enter the storage tank 7;

[0061] S05, the particles in the storage tank 7 are conveyed into the reactor through the downcomer 8, to realize the external circulation operation.

[0062] Specifically, the particles are added into the reactor through the feeding port 3, the gas is introduced into the loop flow section 101 through the draft tube gas inlet 5 at the bottom of the reactor, and the particles move upward under the carrying of the fluidization wind of the draft tube 2, and most of the particles change the direction of movement after coming out of the top of the draft tube 2 and enter the annular gap region between the draft tube 2 and the loop flow section 101. The particles in the annular gap region move downward, and the particles move radially into the draft tube 2 after moving to the bottom space, completing a loop flow. Another part of the micro-nano particles coming out of the top of the draft tube 2 enters the conveying section 103 and continues to move upward, and after being separated by the gas-solid separation device 6, the micro-nano particles return to the storage tank 9. The micro-nano particles enter the loop flow section 101 through the discharge inclined pipe 8 below the storage tank 9, and complete the entire cycle.

[0063] In the bottom space of the loop flow section 101, high-speed auxiliary wind is introduced tangentially along the inner side of the wall of the loop flow section 101 through the jet pipe group, forming multiple high-speed tangential rotating air flows in the vicinity of the bottom wall of the loop flow section 101. The multiple high-speed rotating air flows can make the micro-nano particle materials accumulated in the bottom wall region of the loop flow section 101 form a whole circumferential movement trend, destroy the material accumulation and agglomeration, thereby destroying the bottom viscous accumulation, allowing more micro-nano particles to participate in the loop flow, improving the uniformity of the micro-nano particle distribution and the fluidization quality at the bottom of the loop flow section 101, and ensuring the normal operation of the loop flow coupling reactor of the micro-nano particles, improving the gas-solid contact efficiency in the fluidized bed, and solving the accumulation problem of the micro-nano particles at the bottom of the fluidized bed.

[0064] In this embodiment, the cyclone gas inlet in the middle region of the loop flow section 101, i.e. the annular gap region, can keep the micro-nano particles accumulated in the annular gap region in a fluidized state and strengthen the circulating flow of the micro-nano particles in the annular gap region. The gas amount of the cyclone gas inlet in the annular gap region is adjusted by adjusting the gas inlet amount of the jet pipe group to adjust the particle concentration in the annular gap region, and the loop flow is realized in a central gas-lifting or central downward mode. The particle internal circulation flux and the external circulation flux of the loop flow coupling reactor can also be adjusted by adjusting the cyclone gas inlet amount, the distribution ratio of the micro-nano particles in the loop flow coupling reactor is adjusted, and the continuous and stable flow of the micro-nano particles in the loop flow coupling reactor with the cyclone strengthened is realized.

[0065] Please refer to Figure 4 As shown in the figure, the central gas-lifting operation is realized in the step of adjusting the gas inlet amount of the jet pipe group, so that the bottom pressure of the draft tube 2 is less than the bottom pressure of the annular gap region, the particles flow from the bottom of the annular gap region into the bottom of the draft tube 2, and the particles move upward to the top of the draft tube region under the action of the gas flow introduced through the draft tube gas inlet 5. After the particles leave the top of the draft tube, a part of the particles flow into the annular gap region, move downward in the annular gap region to the bottom of the loop flow section 101, and realize continuous central gas-lifting loop flow; another part of the particles flow into the conveying section and enter the gas-solid separation device 6.

[0066] Please refer to Figure 5 shown, the center down operation is to make the bottom pressure of the draft tube 2 greater than the bottom pressure of the annular zone in the step of adjusting the gas intake of the jet pipe group, the particles flow from the bottom of the draft tube 2 into the bottom of the annular zone; the particles move upward to the top of the annular zone under the action of the gas flow into the jet pipe group, and after the particles leave the top of the annular zone, a part of the particles flow into the draft tube and move downward to the bottom of the circulating section 101 through the draft tube 2, realizing continuous center down circulating flow; another part of the particles flow into the gas-solid separation device 6 through the conveying section.

[0067] In specific applications, please refer to Figure 1 shown, the height of the conveying section 103 in the fluidized bed is 1600 mm, and the inner diameter of the pipe is 20 mm; the inner diameter of the draft tube 2 is 20 mm, and the height is 300 mm; the inner diameter of the circulating section 101 is 60 mm, and the height is 440 mm. The gas inlet of the jet pipe in the jet pipe group is tangent to the outer diameter of the circulating section 101, and the tangential gas inlet is used to form a cyclone to strengthen the circulation. Please refer to Figure 4 and Figure 5 shown, two layers of gas inlets of the jet pipe group are arranged at the bottom of the circulating section 101, and three layers of gas inlets of the jet pipe group are arranged in the annular zone. Each layer of tangential gas inlet of the jet pipe group is provided with four jet pipes with an inner diameter of 6 mm. The cyclone gas inlet at the bottom of the circulating section 101 can make the particles form a whole circumferential movement, destroy the stable viscous accumulation state of the particles, thereby strengthening the flow of the particles and improving the flow dead zone; the cyclone gas inlet located in the annular zone can not only destroy the particle accumulation in the annular zone and improve the fluidization state of the micro-nano particles, but also can change the operating state of the reactor to center up circulating flow or center down circulating flow by adjusting the cyclone gas intake, thereby further adjusting the particle distribution of the internal circulation of the circulating section and the external circulation of the conveying section, realizing continuous and stable fluidization of the micro-nano particles and being more conducive to process control.

[0068] Taking desulfurization ash particles as an example, the volume average particle size of the solid particles is 10 μm, and the particle density is 1788 kg / m 3 , which belongs to micro-nano particles. The particles are accumulated in the storage tank 7 with a height of 60 cm to provide back pressure for the whole particle circulation system. The shell 1 and the storage tank 7 can be approximately regarded as a communicating vessel. The particles accumulated in the storage tank 7 generate static pressure under the action of gravity, so the particles in the storage tank 7 will spontaneously enter the circulating section 101 through the discharge inclined pipe 8; the opening degree of the control valve on the discharge inclined pipe 8 is set to 100%, which is in a fully open state, and at this time it is the maximum particle circulation rate that the device can reach. The superficial gas velocity in the draft tube 2 is fixed at 2.0 m / s, and the superficial gas velocity in the annular zone is controlled by adjusting the cyclone gas intake, thereby realizing different particle circulation rate operations. It is measured that in this embodiment:

[0069] When the superficial gas velocity of the conveying 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 cyclone-strengthened loop coupled reactor is 7.90 kg / m 2 s, which is increased by 72.5%;

[0070] When the superficial gas velocity of 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 cyclone-strengthened loop coupled reactor is 8.42 kg / m 2 s, which is increased by 33.9%;

[0071] When the superficial gas velocity of 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 cyclone-strengthened loop coupled reactor is 10.20 kg / m 2 s, which is increased by 51.1%.

[0072] It can be shown from the above that, compared with the conventional loop coupled reactor, the cyclone-strengthened loop coupled reactor realizes a higher micro-nano particle circulation rate and a more continuous and stable fluidization effect under the same operating conditions.

[0073] Finally, it should be noted that the above examples are only used to illustrate the technical solutions of the present application, and not to limit them; although the present application has been described in detail with reference to the foregoing examples, those of ordinary skill in the art should understand that they can still modify the technical solutions recorded in the foregoing examples, or make equivalent replacements for some technical features thereof; and these modifications or replacements do not make the essence of the corresponding technical solutions deviate from the spirit and scope of the technical solutions of the embodiments of the present application.

Claims

1. A cyclonic particle loop coupled reactor characterized by, The application relates to a cyclone type particle loop coupling reactor, a gas-solid separation device and a storage tank. The shell comprises a loop flow section, a transition section and a conveying section distributed from bottom to top, the transition section is provided with a feeding port, the loop flow section is provided with a return port, and the top of the conveying section is provided with a discharging port; A guide cylinder is arranged in the loop flow section and is connected with the guide cylinder through a connecting rod; the area between the outer wall of the guide cylinder and the inner wall of the shell is an annular gap area; the side wall of the loop flow section is tangentially provided with a jet pipe group in the circumferential direction; and the bottom of the shell is provided with a guide cylinder air inlet below the guide cylinder.

2. The cyclonic particle loop coupled reactor according to claim 1, wherein, The inner diameter of the conveying section is smaller than the inner diameter of the loop flow section.

3. The cyclonic particle loop coupled reactor according to claim 1, wherein, The loop flow section is provided with a plurality of jet pipe groups in the height direction from bottom to top.

4. The cyclonic particle loop coupled reactor of claim 1, wherein, At least two jet pipes are arranged in each jet pipe group, and all the jet pipes are uniformly and tangentially arranged on the side wall of the loop flow section in the circumferential direction.

5. A cyclone-particle loop-coupled fluidized bed, characterized by, The application further relates to a cyclone type particle loop coupling fluidized bed based on the cyclone type particle loop coupling reactor, the gas-solid separation device and the storage tank.

6. The cyclone-particle loop coupled fluidized bed of claim 5, wherein, The gas-solid separation device comprises a diameter expansion section, a baffle and an exhaust pipe, the diameter expansion section is sleeved on the top of the conveying section, the baffle is arranged above the discharging port, and the exhaust pipe is connected with the top of the diameter expansion section.

7. The cyclone-particle loop coupled fluidized bed according to claim 5, wherein, The cyclone type particle loop coupling fluidized bed based on the cyclone type particle loop coupling reactor, the gas-solid separation device and the storage tank comprises the following steps:

8. A particle circulation coupling method characterized by, Particles are added into the reactor; Gas is introduced into the reactor through the guide cylinder air inlet and the jet pipe, part of the particles flow in the annular gap area and the guide cylinder in a circulating manner, and the other part of the particles enter the gas-solid separation device through the conveying section; The gas inlet amount of the jet pipe group is adjusted, so that a plurality of tangential rotating gas flows are formed at the bottom area of the loop flow section, and the accumulation and agglomerates of the particles at the bottom of the loop flow section are destroyed; 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 particles in the storage tank are conveyed back into the reactor through the discharge inclined pipe, so that external circulation operation is realized. In the step of adjusting the gas inlet amount of the jet pipe group, the bottom pressure of the guide cylinder is less than the bottom pressure of the annular gap area, the particles flow into the bottom of the guide cylinder from the bottom of the annular gap area in a directional manner, the particles move upwards to the top of the guide cylinder area under the action of the gas flow introduced into the guide cylinder air inlet, part of the particles flow into the annular gap area after leaving the top of the guide cylinder, move downwards to the bottom of the loop flow section through the annular gap area, and realize continuous central gas lifting type loop flow; the other part of the particles flow into the gas-solid separation device through the conveying section.

9. The particle circulation coupling method according to claim 8, wherein, ​ 10. The particle circulation coupling method of claim 8, wherein, In the step of adjusting the gas intake of the jet pipe group, the bottom pressure of the draft tube is made greater than the bottom pressure of the annular zone, and the particles flow from the bottom of the draft tube into the bottom of the annular zone in a directional manner; the particles move upward to the top of the annular zone under the action of the gas flow passing through the jet pipe group, and after the particles leave the top of the annular zone, part of the particles flow into the draft tube and move downward to the bottom of the annular zone through the draft tube, so as to realize continuous central descending type annular flow; the other part of the particles flow into the gas-solid separation device through the conveying section.

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