A gas-turbulent viscous ultrafine particle fluidized bed reactor system and method

Abstract

This invention provides a gas-perturbed fluidized bed reactor system and method for viscous ultrafine particles. The system includes a fluidized bed reactor unit, a gas supply unit, a multi-directional gas supply unit, and a gas-solid separation unit. The fluidized bed reactor unit includes a reaction chamber, within which a gaseous zone and a dense phase zone are sequentially arranged along the axial direction. The gas supply unit is connected to the bottom of the reaction chamber and provides primary gas flow to the dense phase zone. The multi-directional gas supply unit includes a gas supply module and several gas supply components. The gas supply module is connected to several gas supply components, and each component is independently connected to the reaction chamber and communicates with the dense phase zone to provide secondary gas flow. The gas-solid separation unit is connected to the gaseous zone. This invention, through the rational configuration and structural arrangement of the multi-directional gas supply unit, achieves uniform flow of materials and efficient gas-solid contact within the fluidized bed reactor, overcoming the problems of particle agglomeration and channeling.

Description

Technical Field

[0001] This invention belongs to the field of gas-solid reaction technology, and relates to a reaction device system and method for achieving stable fluidization of Class C viscous particles by utilizing gas disturbance. Background Technology

[0002] Fluidized bed reactors are widely used in chemical industries, energy production, and materials processing due to their excellent heat and mass transfer efficiency and gas-solid contact efficiency. The working principle of a fluidized bed reactor is to suspend solid particles in gas within the reactor, ensuring sufficient contact between the gas and solid phases, thereby achieving efficient heat and mass transfer. However, in gas-solid fluidization, according to Geldart's particle classification, Class C particles, due to their smaller size, lower density, and stronger surface viscosity, exhibit different fluidization characteristics compared to Class A and Class B particles. Class C particles are ultrafine and highly viscous, with strong electrostatic and van der Waals forces, resulting in high adhesion and agglomeration tendency. These characteristics make it difficult for Class C particles to form a stable fluidized state during fluidization, easily leading to uneven airflow, particle agglomeration, channeling, choking, and gas embolism. This poor fluidization affects the efficiency and uniformity of the gas-solid reaction, limiting the application of Class C particles in fluidized beds.

[0003] Traditional fluidized bed reactors mostly employ unidirectional gas inflow, which fails to achieve uniform disturbance of Class C particles, resulting in low gas-solid contact efficiency. Furthermore, conventional fluidization methods suffer from unstable fluidization states, easily leading to bubble aggregation, particle agglomeration, and other problems such as sludge flow. This results in uneven gas distribution within the reactor and insufficient effective contact area between the gas and solid phases, thereby reducing reaction efficiency and product quality. Particularly for industrial reaction processes requiring stable operation, such fluctuations affect reaction uniformity and product quality, making precise control of reaction conditions difficult and reducing production stability and consistency. In addition, to overcome the agglomeration of Class C particles, traditional fluidized beds often increase the gas flow rate (i.e., aeration rate) to increase the gas impact force and attempt to break up particle agglomerates. However, this method significantly increases energy consumption and, in some cases, still fails to achieve the desired fluidization effect. Simultaneously, excessively high gas flow rates may cause particle dispersion, leading to material loss, increased production costs, and potential environmental pollution. Furthermore, the high aeration rate and strong gas impact force in traditional fluidized beds lead to accelerated equipment wear, especially at the bottom gas distribution plate and fluidized bed sidewalls. For C-type particles with high viscosity, the agglomerated particles will further increase the wear of the equipment during fluidization, resulting in increased maintenance and replacement frequency and significantly increased maintenance costs.

[0004] In recent years, several studies have proposed various improvement methods, such as increasing the structural complexity of the gas distribution plate and introducing external force fields (e.g., stirring, vibration, sound, magnetic fields, bubble breaking) to enhance fluidization. However, traditional stirred fluidized beds still often experience particle adhesion when processing Class C particles, leading to uneven fluidization and even flow loss, resulting in an uneven and unstable reaction process. This phenomenon not only reduces reaction efficiency but also causes a small number of fine particles to be carried by the gas flow to the top of the reactor or the outlet, thus failing to react fully, resulting in "underreaction" of these particles and ultimately a decrease in product yield. While adding a stirring device to the fluidized reactor can improve fluidization quality to some extent, break up the agglomeration of Class C particles, and enhance gas-solid contact, it still has many limitations in practical applications, especially in fine chemical fields such as chemical vapor deposition and carbon material activation. These processes have extremely high requirements for product quality and consistency, particularly the precise control of process parameters such as reaction time, temperature, and pressure. For example, CN118267939A discloses a fluidized bed reactor and reaction system specifically designed for Class C particles. This system includes a fluidizing stirring mechanism, a heating system, and a pressure regulating system to achieve uniform fluidization and meet the reaction conditions of fine chemicals. However, this design relies on the stirring device and multiple precision control systems, increasing equipment complexity and maintenance costs, resulting in high energy consumption, difficult operation, and potentially limiting its applicability to specific high-precision industrial applications. CN205110110U discloses a stirred air-heavy medium fluidized bed separator, introducing a frame-type stirring paddle device to effectively break up large bubbles in the fluidized bed and prevent uneven fluidization caused by bubble coalescence. This design reduces the complexity of vibration and magnetic field-assisted fluidization, but it primarily relies on mechanical stirring to break up bubbles, limiting its applicability. Furthermore, long-term operation of the stirring device may lead to equipment wear and require regular maintenance, increasing operating costs, and it may not achieve optimal results in high-precision separation applications. CN109046187A discloses a gas-solid fluidized bed reactor with a high aeration rate. This reactor achieves efficient gas-solid contact by using "C+ type particles" in the fluidized bed, or by increasing the specific surface area and aeration rate through surface roughening. However, the preparation and fluidization stability of C+ type particles depend on the uniform distribution of nanoparticles, and the operation requires strict control over the fluidized bed gas velocity and pressure, increasing operational complexity. Furthermore, wear of the nanoparticles may lead to particle loss and contamination, and the high aeration rate design carries the risk of increased energy consumption during application. Applying mechanical vibration to the fluidized bed makes C+ type particles easier to disperse under vibration, reducing particle agglomeration. However, the vibration system increases equipment wear and may cause noise and energy consumption problems in large-scale industrial applications.Pulsed airflow devices installed at the bottom or sidewalls of a fluidized bed, applying pulsed airflow periodically or randomly, can break up particle agglomerations. However, this requires high control precision, and the pulse frequency and intensity must be precisely matched to the particle characteristics; otherwise, uneven particle distribution may occur. Introducing sound waves into the fluidized bed to disturb C-type particles can break up particle agglomeration forces, but for large-scale industrial applications, the effect of sound wave disturbance weakens with increasing scale, and the sound wave devices consume a lot of power. Bubble breaking devices can improve fluidization quality to some extent and have a relatively simple structure. However, the mechanical components increase the complexity of the equipment and the difficulty of maintenance, and the effect on smaller C-type particles is limited. It is easy to see that the above methods often increase equipment cost and complexity, and have limited improvement on the fluidization effect of C-type particles.

[0005] Therefore, there is a need to provide a fluidized bed reactor that can ensure the uniformity and stability of particle fluidization while also having a high reaction efficiency. Summary of the Invention

[0006] To address the shortcomings of existing technologies, the present invention aims to provide a gas-disturbance type fluidized bed reactor system and method for viscous ultrafine particles, which has the advantages of high efficiency, flexibility and durability. By continuously supplying gas to the reaction chamber in multiple dimensions and directions, a uniform gas disturbance field is formed, which solves the problems of poor fluidization quality, easy particle agglomeration and channeling of Class C particles in fluidized bed reactors.

[0007] To achieve this objective, the present invention adopts the following technical solution:

[0008] In a first aspect, the present invention provides a gas-perturbed fluidized bed reactor system for viscous ultrafine particles. The system includes a fluidized bed reactor unit, a gas supply unit, a multi-directional gas supply unit, and a gas-solid separation unit. The fluidized bed reactor unit includes a reaction chamber, within which a gaseous zone and a dense phase zone are sequentially arranged along the axial direction. The gas supply unit is connected to the bottom of the reaction chamber and provides a primary gas flow to the dense phase zone. The multi-directional gas supply unit includes a gas supply module and several gas supply components. The gas supply module is connected to several gas supply components, and the gas supply components are independently connected to the reaction chamber and communicate with the dense phase zone to provide a secondary gas flow. The gas-solid separation unit is connected to the gaseous zone.

[0009] This invention creates continuous multi-directional disturbances within the fluidized reaction chamber by setting up a multi-directional gas supply unit, which keeps the particulate matter in a suspended state. This effectively breaks the agglomeration and channeling of particulate matter in the dense phase region, resulting in a more uniform distribution of particulate matter and significantly increasing the contact opportunities between gas and particulate matter. This improves the gas-solid reaction efficiency and enhances the uniformity and quality of the product. At the same time, the gas-solid separation unit effectively removes particulate dust from the product, ensuring the purity of the reaction product.

[0010] The gas-turbulent fluidized bed reactor system for viscous ultrafine particles provided by this invention has a wide range of applications and can be used in various gas-solid reactions that require uniform fluidization, improving reaction efficiency and product quality. It is particularly suitable for the processing of C-type particles.

[0011] As a preferred embodiment of the present invention, with the central axis of the reaction chamber as a reference, the gas replenishment component adopts any one or a combination of at least two of the following: tangential setting, radial setting, inclined upward setting, or inclined downward setting, and the setting directions of several gas replenishment components are the same or different.

[0012] It should be noted that, in this invention, "tangential setting" refers to a circumferential setting at a certain angle to the inner wall of the reaction chamber, with the outlet of the gas supply component pointing away from the central axis of the reaction chamber; "radial setting" refers to a circumferential setting perpendicular to the inner wall of the reaction chamber, with the outlet of the gas supply component pointing towards the central axis of the reaction chamber; "inclined upward setting" refers to an axial setting at a certain angle to the inner wall of the reaction chamber, with the outlet of the gas supply component pointing upward; and "inclined downward setting" refers to an axial setting at a certain angle to the inner wall of the reaction chamber, with the outlet of the gas supply component pointing downward. The "circumferential direction" is perpendicular to the "axial direction" of the reaction chamber.

[0013] As a preferred embodiment of the present invention, a plurality of the gas replenishment components are arranged at equal intervals along the axial and / or circumferential directions of the reaction chamber.

[0014] Preferably, the gas replenishment assembly is sealed to the outer peripheral wall of the dense phase region of the reaction chamber.

[0015] Preferably, the distance between the air outlet of the gas replenishment component and the inner wall of the reaction chamber is 2% to 20% of the diameter of the reaction chamber. For example, it can be 2%, 3%, 5%, 8%, 10%, 12%, 15%, 16%, 18% or 20%, but it is not limited to the listed values. Other unlisted values ​​within this range are also applicable.

[0016] Preferably, when the air replenishment component is tangentially arranged, the tilt angle of the air replenishment component is 15° to 45°, for example, it can be 15°, 20°, 25°, 30°, 35°, 40° or 45°, but it is not limited to the listed values. Other unlisted values ​​within this range are also applicable.

[0017] Preferably, when the air replenishment component is inclined upward, the inclination angle of the air replenishment component is 15° to 60°, for example, it can be 15°, 20°, 25°, 30°, 35°, 40°, 45°, 50°, 55° or 60°, but it is not limited to the listed values. Other unlisted values ​​within this range are also applicable.

[0018] Preferably, when the air replenishment component is inclined downward, the inclination angle of the air replenishment component is 15° to 60°, for example, it can be 15°, 20°, 25°, 30°, 35°, 40°, 45°, 50°, 55° or 60°, but it is not limited to the listed values. Other unlisted values ​​within this range are also applicable.

[0019] It should be noted that, in this invention, the tilt angle of the gas replenishment component when it is tangentially arranged refers to the angle between the gas replenishment component and the inner wall of the reaction chamber in the circumferential direction; the tilt angle of the gas replenishment component when it is tilted downward refers to the angle between the gas replenishment component and the inner wall of the reaction chamber in the axial direction; and the tilt angle of the gas replenishment component when it is tilted downward refers to the angle between the gas replenishment component and the inner wall of the reaction chamber in the axial direction.

[0020] As a preferred embodiment of the present invention, the air replenishment module includes an air replenishment fan and a first air storage device connected in sequence, and the outlet end of the first air storage device is respectively connected to a plurality of the air replenishment components.

[0021] Preferably, the first gas storage device is connected to the gas replenishment component through a gas replenishment pipeline, and the gas replenishment pipeline is equipped with a first flow detection component, a first pressure detection component and a first regulating valve.

[0022] As a preferred embodiment of the present invention, a gas distribution plate is provided at the bottom of the inner cavity of the reaction chamber, and the primary gas flow enters the dense phase region through the gas distribution plate.

[0023] Preferably, the gas distribution plate is a tongue-shaped distribution plate.

[0024] This invention utilizes a gas distribution plate to allow the airflow to enter the dense phase region along a tortuous path, reducing the intensity of direct impact on the bed, reducing airflow short-circuiting, avoiding excessively strong or weak local airflow, alleviating channeling and throttling phenomena, reducing dependence on high-velocity or high-pressure airflow, and improving gas-solid contact efficiency.

[0025] Preferably, the reaction chamber has a cylindrical structure.

[0026] Preferably, the volume of the dense phase region is 40% to 70% of the total volume of the reaction chamber, for example, it can be 40%, 45%, 50%, 55%, 60%, 65% or 70%, but it is not limited to the listed values. Other unlisted values ​​within this range are also applicable.

[0027] Preferably, the fluidized reaction unit further includes a feeding device connected to the reaction chamber.

[0028] Preferably, the bottom of the reaction chamber is also provided with a discharge port.

[0029] As a preferred embodiment of the present invention, the gas supply unit includes a gas supply fan and a second gas storage device connected in sequence, and the outlet end of the second gas storage device is connected to the bottom of the reaction chamber.

[0030] Preferably, the second gas storage device is connected to the reaction chamber via a gas supply pipeline, and the gas supply pipeline is equipped with a second flow detection component, a second pressure detection component, and a second regulating valve.

[0031] As a preferred embodiment of the present invention, the gas-solid separation unit includes a cyclone separator connected to the gaseous zone, and the top and bottom of the cyclone separator are respectively provided with an exhaust port and a discharge port.

[0032] This invention uses a cyclone separator to recover particulate matter entrained in the gas during the fluidization start-up phase and during use, thereby reducing losses caused by particulate entrainment and improving product yield.

[0033] Secondly, the present invention provides a gas-perturbed fluidized bed reaction method, wherein the gas-perturbed fluidized bed reaction method employs the gas-perturbed viscous ultrafine particle fluidized bed reaction device system described in the first aspect, and the gas-perturbed fluidized bed reaction method includes:

[0034] (1) Fill the solid raw material into the dense phase region and introduce a gas flow to carry out a gas-solid reaction, so that the solid raw material is in a fluidized state.

[0035] (2) A secondary gas flow is then introduced into the dense phase region to form a multi-directional gas disturbance field, thereby enhancing the fluidization effect and generating a gaseous mixture;

[0036] (3) Separate the gaseous mixture generated by the fluidization reaction into gas and solid.

[0037] This invention first uses a primary airflow to initially fluidize the solid raw material, and then supplements it with a secondary airflow to form a multi-directional disturbance field with intersecting airflow directions, which further breaks up particle agglomeration, enhances fluidization effect, improves gas-solid contact efficiency, improves fluidization uniformity, and reduces problems such as particle agglomeration, channeling and bubble aggregation. While greatly improving the fluidization effect, it also greatly reduces energy consumption.

[0038] As a preferred embodiment of the present invention, the gas disturbance fluidized reaction method further includes: adjusting the injection angle, pressure and velocity of the secondary gas flow to enhance the fluidization state of the solid raw material in the dense phase region.

[0039] This invention achieves multi-dimensional and all-round disturbance of solid raw materials, improves gas-solid contact efficiency, makes the reaction process more stable, and significantly improves fluidization quality.

[0040] As a preferred embodiment of the present invention, the direction of secondary airflow in the multidirectional gas disturbance field includes any one or a combination of at least two of the following: tangential, radial, inclined upward, or inclined downward.

[0041] Preferably, the velocity of the secondary airflow is less than the velocity of the primary airflow.

[0042] Preferably, the pressure of the secondary airflow is lower than the pressure of the primary airflow.

[0043] Preferably, the velocity of the primary airflow is 0.003 to 50 m / s, for example, it can be 0.003 m / s, 0.1 m / s, 0.5 m / s, 1 m / s, 5 m / s, 10 m / s, 15 m / s, 20 m / s, 25 m / s, 30 m / s, 45 m / s, 50 m / s, 55 m / s or 50 m / s, but it is not limited to the listed values, and other unlisted values ​​within this range are also applicable.

[0044] Preferably, the pressure of the primary airflow is 0.1 to 0.5 MPa, for example, it can be 0.1 MPa, 0.15 MPa, 0.2 MPa, 0.25 MPa, 0.3 MPa, 0.35 MPa, 0.4 MPa, 0.45 MPa or 0.5 MPa, but it is not limited to the listed values. Other unlisted values ​​within this range are also applicable.

[0045] The system refers to an equipment system, device system, or production device.

[0046] Compared with the prior art, the beneficial effects of the present invention are as follows:

[0047] (1) The gas disturbance type fluidized reaction device system and method for viscous ultrafine particles provided by the present invention effectively breaks the agglomeration and channeling of particles by forming multi-directional disturbance in the fluidized bed, making the particle distribution more uniform, avoiding the channeling and slugging problems in traditional fluidized beds, improving gas-solid contact efficiency and fluidization uniformity, and solving the problem of poor fluidization effect of traditional fluidized beds for Class C viscous particles.

[0048] (2) By increasing multi-directional gas replenishment disturbance, the present invention significantly increases the contact opportunities between gas and particles, so that the active sites on the particle surface can be fully utilized, thereby improving the gas-solid reaction efficiency and improving the uniformity and quality of the product.

[0049] (3) The present invention adjusts the direction of gas supply and the intensity of air flow according to specific reaction requirements to adapt to different particle characteristics and fluidization requirements, providing continuous and stable air flow disturbance, enhancing the versatility and operability of the system, and is suitable for a variety of industrial application scenarios; at the same time, the multi-directional gas supply method can ensure the continuous suspension of particles in the fluidized bed, which can significantly improve the gas-solid contact efficiency compared with the traditional unidirectional fluidization, so as to achieve a higher reaction rate in a shorter time, and is suitable for the needs of high-efficiency industrial production.

[0050] (4) The present invention provides multi-directional air replenishment disturbance, which helps to prevent particles from depositing and clogging inside the equipment, reduces equipment wear and failure risk, reduces equipment clogging and maintenance frequency, extends equipment service life, and reduces maintenance costs and downtime.

[0051] (5) The present invention optimizes the gas distribution through efficient gas replenishment disturbance, making the fluidization operation more energy-efficient and reducing the energy consumption of the system operation. Compared with traditional fluidized reactors with high gas filling rate or high power vibration device, it saves energy, is environmentally friendly and efficient, and has higher economic benefits.

[0052] (6) The present invention utilizes the integrated design of fluidized reaction unit and gas-solid separation unit to effectively remove particulate dust, ensure the purity of reaction products, improve the cleanliness of reaction device, and further optimize the gas-solid separation effect in conjunction with multi-directional gas replenishment, ensuring the environmental protection and safety of reaction process.

[0053] (7) This invention has a wide range of applications and great potential for industrial applications. It can be widely used in the fluidization reaction of other viscous particles or ultrafine particles. It has a high efficiency and stable fluidization effect, which makes it have significant advantages and market potential in a variety of industrial applications. Attached Figure Description

[0054] Figure 1 This is a schematic diagram of the gas-disturbance viscous ultrafine particle fluidized reaction device system provided in Embodiment 1 of the present invention.

[0055] Figure 2This is a schematic diagram of the tongue-shaped distribution plate provided in Embodiment 1 of the present invention.

[0056] Figure 3 This is a schematic diagram of the air replenishment component provided in Embodiment 1 of the present invention.

[0057] Figure 4 This is a schematic diagram of the air replenishment component provided in Embodiment 2 of the present invention.

[0058] Figure 5 This is a schematic diagram of the air replenishment component provided in Embodiment 3 of the present invention.

[0059] Figure 6 This is a schematic diagram of the air replenishment component provided in Embodiment 4 of the present invention.

[0060] Figure 7 This is a schematic diagram of the air replenishment component provided in Embodiment 5 of the present invention.

[0061] Figure 8 This is a schematic diagram of the air replenishment component provided in Embodiment 6 of the present invention.

[0062] Figure 9 This is a schematic diagram of the air replenishment component provided in Embodiment 7 of the present invention.

[0063] Figure 10 This is a schematic diagram of the air replenishment component provided in Embodiment 8 of the present invention.

[0064] Wherein, 1-reaction chamber; 101-gas zone; 102-dense phase zone; 103-discharge port; 2-feeding device; 3-tongue-shaped distribution plate; 4-air supply fan; 5-second gas storage device; 401-second flow detection component; 402-second pressure detection component; 403-second regulating valve; 6-cyclone separator; 601-exhaust port; 602-discharge port; 7-replenishing fan; 701-first flow detection component; 702-first pressure detection component; 703-first regulating valve; 8-first gas storage device; 9-replenishing component; 901-first gas outlet; 902-second gas outlet; 903-third gas outlet. Detailed Implementation

[0065] It should be understood that in the description of this invention, the terms "center," "longitudinal," "lateral," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," and "outer," etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. These terms are used only for the convenience of describing the invention and for simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on the invention. Furthermore, the terms "first," "second," etc., are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of indicated technical features. Thus, a feature defined with "first," "second," etc., may explicitly or implicitly include one or more of that feature. In the description of this invention, unless otherwise stated, "a plurality of" means two or more.

[0066] It should be noted that, in the description of this invention, unless otherwise explicitly specified and limited, the terms "set," "connected," and "linked" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal connection of two components. Those skilled in the art can understand the specific meaning of the above terms in this invention based on the specific circumstances.

[0067] The technical solution of the present invention will be further described below with reference to the accompanying drawings and specific embodiments.

[0068] In some embodiments, the present invention provides a gas-turbulent fluidized bed reactor system for viscous ultrafine particles, comprising a fluidized bed reactor unit, a gas supply unit, a multi-directional gas replenishment unit, and a gas-solid separation unit. The fluidized bed reactor unit includes a reaction chamber serving as the gas-solid reaction site. A gaseous zone and a dense phase zone are sequentially arranged along the axial direction within the reaction chamber. The dense phase zone is filled with solid material, and the gaseous products generated by the gas-solid reaction enter the gaseous zone. The gas supply unit is connected to the bottom of the reaction chamber and provides a primary gas flow required for basic fluidization to the dense phase zone. This gas serves as the reaction gas and reacts with the solid material in the dense phase zone, causing the solid material to be suspended and achieving initial fluidization. The multi-directional gas replenishment unit includes a gas replenishment module and several gas replenishment components. The gas replenishment module is connected to several gas replenishment components, and each gas replenishment component is independently connected to the reaction chamber and communicates with the dense phase zone. This provides a secondary gas flow to create multi-dimensional, multi-directional airflow turbulence within the reaction chamber, enhancing the stability of the fluidization effect. The gas-solid separation unit is connected to the gaseous zone and is used to effectively intercept and recover rising particulate dust entrained in the gaseous products.

[0069] The gas-perturbed fluidized bed reactor system for viscous ultrafine particles provided by this invention is applicable to various gas-solid reactions requiring uniform fluidization. It can be widely used in the fluidization of viscous or ultrafine particles, including but not limited to chemical vapor deposition, catalytic reactions, material synthesis, adsorption separation, powder mixing, and surface modification. It is particularly suitable for the fluidization treatment of Class C particles. These Class C particles have a particle size ≤20μm and a viscosity of 10–500 mPa·s. Due to their small particle size and high viscosity, they often experience phenomena such as stagnation, uneven bubble distribution, and insufficient gas-solid contact during fluidization, thus affecting the efficiency and uniformity of the reaction. Traditional fluidized bed systems struggle to ensure fluidization uniformity and stability when processing Class C particles, easily leading to low equipment operating efficiency and poor reaction results. This invention, by adding multi-directional gas perturbation, enhances the fluidization effect of Class C particles, avoids particle agglomeration and channeling, and effectively improves fluidization quality.

[0070] With the central axis of the reaction chamber as a reference, the gas replenishment components are arranged tangentially, radially, inclined upwards, or inclined downwards, or a combination of at least two of these arrangements, and the arrangement directions of several gas replenishment components may be the same or different. The gas replenishment components are located in the dense phase region of the lower part of the reaction chamber. The distance from the gas outlet of the gas replenishment component to the inner wall of the reaction chamber is 2% to 20% of the diameter of the reaction chamber. Those skilled in the art can adjust the insertion depth of the gas replenishment components according to actual process conditions. Specifically, when the gas replenishment components are tangentially arranged, the inclination angle of the gas replenishment components is 15° to 45°. When the gas replenishment components are inclined upwards, the inclination angle of the gas replenishment components is 15° to 60°, preferably 30° to 60°. When the gas replenishment components are inclined downwards, the inclination angle of the gas replenishment components is 15° to 60°, preferably 30° to 60°. The present invention provides gas supply components arranged in tangential, radial, upward, downward or multi-directional mixing on the reaction chamber. The direction, angle, flow rate or axial arrangement of the gas supply components can be flexibly adjusted according to process requirements to adapt to the fluidization characteristics of different particles. The components are arranged in an orderly manner inside the fluidization chamber to form multi-dimensional gas disturbance with intersecting airflow directions, thereby improving fluidization uniformity.

[0071] In this invention, there are multiple air-injection components. The setting direction, angle, flow rate, and number of each air-injection component can be adjusted according to process requirements. For example, all air-injection components can be set in the same direction, using any one or at least two combinations of tangential, radial, upward-tilting, or downward-tilting settings. Typical but non-limiting combinations include: tangential and downward-tilting, tangential and downward-tilting, tangential and radial, radial and downward-tilting, radial and downward-tilting, tangential, upward-tilting, and downward-tilting, radial, upward-tilting, and downward-tilting, tangential, radial, and downward-tilting, and so on. Alternatively, at least some air-injection components can have different setting directions. For example, some air-injection components are tangentially set, while others are set in any one or at least two combinations of radial, upward-tilting, or downward-tilting settings. Simultaneously, the angle and flow rate of each air-injection component can be the same or different, and the relevant parameters can be adjusted independently according to actual process requirements.

[0072] Furthermore, several of the gas replenishment components are equidistantly spaced along the axial and / or circumferential direction of the reaction chamber. That is, in this invention, the gas replenishment components can be arranged circumferentially along the reaction chamber, arranged axially along the reaction chamber, or arranged circumferentially and axially simultaneously.

[0073] The gas supply assembly is sealed to the outer peripheral wall of the dense phase region of the reaction chamber. The sealing connection includes, but is not limited to, flange connections, welding, threaded connections, socket connections, compression fittings, or adhesive bonding, as are known to those skilled in the art. The gas supply assembly can be a nozzle or spray nozzle, as are known to those skilled in the art.

[0074] In some embodiments, the gas replenishment module includes a gas replenishment fan and a first gas storage device connected in sequence, with the outlet end of the first gas storage device connected to several gas replenishment components. Further, the first gas storage device is connected to the gas replenishment components via a gas replenishment pipeline, which is equipped with a first flow detection component, a first pressure detection component, and a first regulating valve. In application, the gas replenishment fan is activated to send the secondary gas flow from the first gas storage device into the gas replenishment components on the reaction chamber, causing the secondary gas flow to enter the dense phase region and form a multi-directional airflow disturbance field. The gas velocity and pressure of the secondary gas flow are detected in real time, and the first regulating valve is used to regulate the fluidization state within the reaction chamber to adapt to different reaction conditions and ensure the stability and safety of the reaction operation. The gas replenishment module also necessarily includes necessary pipelines, conventional valves, and general-purpose pumps for achieving complete process operation. Those skilled in the art can add layouts based on the process flow and equipment structure selection; this invention does not impose special requirements or specific limitations in this regard.

[0075] In some embodiments, a gas distribution plate is provided at the bottom of the inner cavity of the reaction chamber, through which the primary gas flow enters the dense phase region. Specifically, the gas distribution plate is a tongue-shaped distribution plate with circumferentially evenly distributed air inlets on its surface. Tongue-shaped guide caps are provided at the air inlets, forming a specific flow channel design that allows the gas to enter the bed along a tortuous path, reducing the intensity of direct impact on the bed and minimizing equipment wear. Compared to traditional planar distribution plates, the tongue-shaped distribution plate used in this invention allows the airflow to be evenly distributed throughout the entire bed area, reducing airflow short-circuiting, avoiding excessively strong or weak local airflow, alleviating channeling and throttling phenomena, reducing dependence on high-velocity or high-pressure airflow, lowering energy consumption, and improving gas-solid contact efficiency. Furthermore, it prevents excessive fine particles from being rapidly entrained to the gaseous zone or the outlet of the reaction chamber, reducing operational difficulty and facilitating control and management. The gas distribution plate provides basic fluidized airflow at the bottom of the reaction chamber, while the multi-directional gas replenishment unit further enhances the fluidization state of the particles, exhibiting a synergistic effect and together forming a highly efficient fluidized gas distribution system, making the gas-solid contact within the entire reaction chamber more complete.

[0076] Furthermore, the reaction chamber has a cylindrical structure, and the volume of the dense phase region is 40% to 70% of the total volume of the reaction chamber. This invention does not specifically limit the overall volume of the reaction chamber; those skilled in the art can adjust the volume of the reaction chamber according to actual process conditions and production output. The reaction chamber necessarily includes necessary pipelines, conventional valves, general-purpose pumps, pressure sensors, and safety valves, etc., for achieving complete process operation. Those skilled in the art can add layouts based on process flow and equipment structure selection; this invention does not impose special requirements or specific limitations in this regard.

[0077] In some embodiments, the fluidized bed reaction unit further includes a feeding device connected to the reaction chamber for supplying solid material to the chamber. Specifically, the feeding device is positioned above the dense phase zone, ensuring that the solid material is evenly distributed at the bottom of the reaction chamber. Exemplarily, the feeding device may include a hopper, a feeding mechanism, a conveyor belt, etc., to complete the process. Those skilled in the art can also reasonably add a weighing mechanism according to actual production needs; this invention does not specifically limit this. The bottom of the reaction chamber is also provided with a discharge port for unloading.

[0078] In some embodiments, the gas supply unit includes a gas supply fan and a second gas storage device connected in sequence, with the outlet end of the second gas storage device connected to the bottom of the reaction chamber. Further, the second gas storage device is connected to the reaction chamber via a gas supply pipeline, which is equipped with a second flow detection component, a second pressure detection component, and a second regulating valve. In application, the gas supply fan is activated to send the primary gas flow from the second gas storage device to the bottom of the reaction chamber, allowing it to pass through a gas distribution plate and enter the dense phase region to form an upward airflow. The velocity and pressure of the primary gas flow are monitored in real time, and the second regulating valve is used to adjust the velocity and pressure of the primary gas flow to ensure that the solid material remains in a suspended state, allowing for sufficient contact between the gas and the solid material. The gas supply unit also necessarily includes the necessary pipelines, conventional valves, and general-purpose pumps for achieving complete process operation. Those skilled in the art can add layouts based on the process flow and equipment structure selection; this invention does not impose special requirements or specific limitations in this regard.

[0079] In some embodiments, the gas-solid separation unit includes a cyclone separator connected to the gaseous zone at the top of the reaction chamber. This cyclone separator separates particulate dust generated during the reaction from the gas, ensuring the purity of the reaction products and the cleanliness of the reaction environment. It also works in conjunction with the multi-directional gas supply unit to further improve the overall performance of the reactor, ensuring the high efficiency and continuity of gas-solid separation. The top and bottom of the cyclone separator are respectively equipped with an exhaust port and a discharge port. Fine particulate matter in the gaseous products is trapped and separated in the finished product bin, then discharged through the discharge port. The separated gas is then discharged through the exhaust port to the waste gas treatment system, improving product recovery rate.

[0080] In another specific embodiment, the present invention provides a gas-perturbed fluidized bed reaction method, wherein the gas-perturbed fluidized bed reaction method employs a gas-perturbed viscous ultrafine particle fluidized bed reaction device system as described in a specific embodiment, and the gas-perturbed fluidized bed reaction method includes:

[0081] Step (1) fill the solid raw material into the dense phase region and introduce a gas flow to carry out a gas-solid reaction, so that the solid raw material is in a fluidized state.

[0082] The solid raw material includes any one or a combination of at least two of type A, type B, or type C particulate matter. This invention utilizes a feeding device to deliver the solid raw material into the reaction chamber and distribute it in the bottom region of the chamber. A gas supply fan is activated, causing primary gas to enter the dense phase region from the gas distribution plate at the bottom, gradually increasing the flow velocity to induce fluidization of the solid raw material. Specifically, the primary gas flow velocity is 0.003–50 m / s, and the pressure is 0.1–0.5 MPa.

[0083] Step (2) introduces a secondary gas flow into the dense phase region to form a multi-directional gas disturbance field, thereby enhancing the fluidization effect and generating a gaseous mixture.

[0084] After the solid raw material has undergone initial fluidization, the present invention activates a supplementary air blower to provide a multi-dimensional, multi-directional secondary airflow into the dense phase region of the reaction chamber at a preset angle and flow rate. This creates a uniform multi-directional airflow disturbance within the reaction chamber, breaking up particle agglomerations. During the reaction, the fluidization state of the solid raw material in the dense phase region is controlled by adjusting the injection angle, pressure, and velocity of the secondary airflow to adapt to different reaction conditions. Furthermore, the injection direction of the secondary airflow in the multi-directional gas disturbance field includes any one or a combination of at least two of tangential, radial, upward, or downward tilting directions. The velocity of the secondary airflow is lower than the velocity of the primary airflow, and the pressure of the secondary airflow is lower than the pressure of the primary airflow.

[0085] Step (3) involves gas-solid separation of the gaseous mixture generated by the fluidization reaction.

[0086] The gaseous mixture generated by the reaction of this invention enters the gaseous zone and is discharged from the top of the reaction chamber to the cyclone separator. During the start-up phase or gas volume adjustment process, the fine particles carried upward by the airflow are collected by the cyclone separator, effectively trapping the particulate matter and separating it in the finished product silo. The separated gas is then discharged to the waste gas treatment system.

[0087] Example 1

[0088] This embodiment provides a gas-disturbance-type fluidized bed reactor system for viscous ultrafine particles, including a fluidized bed reactor unit, a gas supply unit, a multi-directional gas replenishment unit, and a gas-solid separation unit. For example... Figure 1 As shown, the fluidized bed reaction unit includes a reaction chamber 1 and a feeding device 2. The reaction chamber 1 has a cylindrical structure, and a gaseous zone 101 and a dense phase zone 102 are sequentially arranged along the axial direction inside the reaction chamber 1. The volume of the dense phase zone 102 is 50% of the total volume of the reaction chamber 1, and a discharge port 103 is provided at the bottom of the reaction chamber 1. The feeding device 2 is connected above the dense phase zone 102 and is used to provide solid raw materials. The bottom of the inner cavity of the reaction chamber 1 is also provided with... Figure 2 The tongue-shaped distribution plate 3 is shown. The air supply unit includes an air supply fan 4 and a second air storage device 5 connected in sequence. The outlet end of the second air storage device 5 is connected to the tongue-shaped distribution plate 3 through an air supply pipe to provide primary airflow. A second flow detection component 401, a second pressure detection component 402, and a second regulating valve 403 are provided on the air supply pipe. The gas-solid separation unit includes a cyclone separator 6, which is connected to the top of the reaction chamber 1 and communicates with the gaseous zone 101. The top and bottom of the cyclone separator 6 are respectively provided with an exhaust port 601 and a discharge port 602. The multi-directional air replenishment unit includes an air replenishment module and multiple air replenishment components 9. Figure 3 As shown, multiple gas supply components 9 are arranged at equal intervals along the circumference of the reaction chamber 1, and each gas supply component 9 is radially arranged and connected to the dense phase region 102 to provide secondary airflow. The gas supply module includes a gas supply fan 7 and a first gas storage device 8 connected in sequence. The outlet end of the first gas storage device 8 is connected to the gas supply component 9 through a gas supply pipe. The gas supply component 9 is welded to the outer wall of the reaction chamber 1, and the distance from the outlet of the gas supply component to the inner wall of the reaction chamber is 2% to 20% of the diameter of the reaction chamber. A first flow detection component 701, a first pressure detection component 702, and a first regulating valve 703 are provided on the gas supply pipe.

[0089] In this embodiment, multiple gas supply components 9 are arranged on the outer periphery of the dense phase region 102 of the reaction chamber 1, and additional secondary airflow is provided to the dense phase region 102 in the radial direction, thereby forming a uniform radial disturbance. The gas velocity and pressure of the gas supply can be adjusted according to the reaction requirements to ensure the uniformity inside the reaction chamber 1.

[0090] Example 2

[0091] This embodiment provides a gas-disturbance-type fluidized bed reactor system for viscous ultrafine particles. The difference from Embodiment 1 is that the gas supply component 9 adopts a multi-directional mixing arrangement of radial and tangential directions, such as... Figure 4 As shown, each gas supply component 9 consists of a first gas outlet 901, a second gas outlet 902, and a third gas outlet 903. The first gas outlet 901, the second gas outlet 902, and the third gas outlet 903 are all located on the same horizontal plane perpendicular to the axial direction of the reaction chamber 1. The second gas outlet 902 and the third gas outlet 903 are symmetrically arranged with the first gas outlet 901 as the center. The first gas outlet 901 is perpendicular to the inner wall of the reaction chamber 1. The angle between the second gas outlet 902 and the inner wall of the reaction chamber 1 is 30°, and the angle between the third gas outlet 903 and the inner wall of the reaction chamber 1 is 30°. The rest of the structure is exactly the same as in Embodiment 1.

[0092] In this embodiment, multiple gas supply components 9 are arranged on the outer periphery of the dense phase region 102 of the reaction chamber 1. At the same time, additional secondary airflow is provided to the dense phase region 102 in the radial and tangential directions, thereby forming uniform radial disturbance and rotational disturbance. The gas velocity and pressure of the gas supply can be adjusted according to the reaction requirements to ensure the uniformity inside the reaction chamber 1.

[0093] Example 3

[0094] This embodiment provides a gas-disturbance-type fluidized bed reactor system for viscous ultrafine particles. The difference from Embodiment 1 is that each gas supply component 9 is tangentially arranged, such as... Figure 5As shown, multiple gas replenishment components 9 are located on the same horizontal plane perpendicular to the axial direction of the reaction chamber 1, and the angle between each gas replenishment component 9 and the inner wall of the reaction chamber 1 is 45°. The rest of the structure is exactly the same as in Example 1.

[0095] In this embodiment, multiple gas supply components 9 are arranged around the dense phase region 102 of the reaction chamber 1, and additional secondary airflow is provided to the dense phase region 102 in the tangential direction to form a rotational disturbance in the reaction chamber 1, effectively preventing particle aggregation and ensuring thorough mixing of the gas and solid phases. The gas supply speed and pressure can be adjusted according to the reaction requirements to ensure the uniformity inside the reaction chamber 1.

[0096] Example 4

[0097] This embodiment provides a gas-turbulent fluidized bed reactor system for viscous ultrafine particles, which differs from Embodiment 1 in that: Figure 6 As shown, multiple gas replenishment components 9 are arranged circumferentially along the reaction chamber 1 and axially along the reaction chamber 1. The rest of the structure is exactly the same as in Example 1.

[0098] In this embodiment, multiple gas supply components 9 are arranged along the circumference and axial direction of the reaction chamber 1 to form uniform radial disturbance, which enhances the intensity of airflow disturbance and increases the contact rate between gas and solid materials. The gas velocity and pressure of the gas supply can be adjusted according to the reaction requirements to ensure the uniformity inside the reaction chamber 1.

[0099] Example 5

[0100] This embodiment provides a gas-turbulent fluidized bed reactor system for viscous ultrafine particles, which differs from Embodiment 1 in that: Figure 7 As shown, each gas replenishment component 9 is inclined downwards, and the angle between the gas replenishment component 9 and the inner wall of the reaction chamber 1 is 45°. The rest of the structure is exactly the same as in Example 1.

[0101] In this embodiment, the outlet of the gas supply component 9 is tilted downwards, so that the airflow forms a dual effect of downward disturbance and horizontal dispersion in the dense phase region 102, thereby forming a uniform disturbance and avoiding the formation of a dead zone at the bottom of the reaction chamber 1.

[0102] Example 6

[0103] This embodiment provides a gas-turbulent fluidized bed reactor system for viscous ultrafine particles, which differs from Embodiment 1 in that: Figure 8 As shown, each gas replenishment component 9 is inclined upward, and the angle between the gas replenishment component 9 and the inner wall of the reaction chamber 1 is 45°. The rest of the structure is exactly the same as in Example 1.

[0104] In this embodiment, the outlet of the gas supply component 9 is tilted upwards to provide oblique airflow into the reaction chamber 1, so that the airflow forms a dual effect of downward disturbance and horizontal dispersion in the dense phase region 102, thereby forming uniform disturbance, which can break up material agglomeration and promote the solid material to move in an orderly manner along the airflow direction, avoiding the formation of channeling or accumulation.

[0105] Example 7

[0106] This embodiment provides a gas-turbulent fluidized bed reactor system for viscous ultrafine particles, which differs from Embodiment 1 in that: Figure 9 As shown, multiple gas replenishment components 9 are arranged circumferentially along the reaction chamber 1 and also axially along the reaction chamber 1. Each gas replenishment component 9 is inclined downwards, and the angle between the gas replenishment component 9 and the inner wall of the reaction chamber 1 is 45°. The rest of the structure is exactly the same as in Example 1.

[0107] In this embodiment, multiple gas supply components 9 are arranged along the circumference and axial direction of the reaction chamber 1 to provide additional oblique airflow to the reaction chamber 1. This results in a dual effect of downward disturbance and horizontal dispersion of the airflow within the dense phase region 102, thereby creating uniform disturbance, avoiding the formation of dead zones at the bottom of the reaction chamber 1, enhancing the intensity of airflow disturbance, increasing the contact rate between gas and solid materials, and allowing the gas supply velocity and pressure to be adjusted according to reaction requirements to ensure the uniformity inside the reaction chamber 1.

[0108] Example 8

[0109] This embodiment provides a gas-turbulent fluidized bed reactor system for viscous ultrafine particles, which differs from Embodiment 1 in that: Figure 10 As shown, multiple gas supply components 9 are arranged circumferentially along the reaction chamber 1 and also axially along the reaction chamber 1. The gas supply components 9 adopt a multi-directional mixed arrangement of radial, upward and downward tilting. Each gas supply component 9 consists of a first gas outlet 901, a second gas outlet 902 and a third gas outlet 903. The second gas outlet 902 and the third gas outlet 903 are symmetrically arranged with the first gas outlet 901 as the center. The first gas outlet 901 is perpendicular to the inner wall of the reaction chamber 1. The second gas outlet 902 is inclined upward, and the angle between it and the inner wall of the reaction chamber 1 is 30°. The third gas outlet 903 is inclined downward, and the angle between it and the inner wall of the reaction chamber 1 is 30°. The rest of the structure is exactly the same as in Embodiment 1.

[0110] In this embodiment, multiple gas supply components 9 are arranged along the circumference and axial direction of the reaction chamber 1 to provide multi-directional airflow that enters radially, tilts upward, and tilts upward and downward within the reaction chamber 1, thereby achieving a better gas distribution inside and fully disturbing the dense phase region 102 in the flow field. The gas velocity and pressure of the gas supply can be adjusted according to the reaction requirements to ensure the uniformity inside the reaction chamber 1.

[0111] Application Example 1

[0112] This application example uses the gas-turbulent viscous ultrafine particle fluidized reaction device system provided in Example 1 to carry out the gas-solid reaction of Class C particulate matter, specifically including the following steps:

[0113] (1) Use the feeding device 2 to send the C-type particulate matter into the reaction chamber 1 and distribute it in the bottom area of ​​the reaction chamber 1. Start the gas supply fan 4 so that the primary gas enters the dense phase zone 102 from the gas distribution plate at the bottom and gradually increases the flow rate to promote the fluidization of the solid raw material. The gas velocity of the primary gas flow is 25 m / s and the pressure is 0.3 MPa.

[0114] (2) After the solid raw material is initially fluidized, start the air supply fan 7 and then introduce a secondary airflow into the dense phase zone 102 to form a multi-directional gas disturbance field to enhance the fluidization effect, generate a gaseous mixture, and ensure that the gas velocity of the secondary airflow is lower than that of the primary airflow, and that the pressure of the secondary airflow is lower than that of the primary airflow.

[0115] (3) The gaseous mixture generated by the reaction enters the gaseous zone 101 and is discharged from the top of the reaction chamber 1 to the cyclone separator 6. The fine particles carried up by the airflow are collected by the cyclone separator 6, effectively intercepting the particles and separating them in the finished product warehouse. The separated gas is then discharged to the waste gas treatment system for post-treatment.

[0116] Application Example 2

[0117] This application example uses the gas-turbulent viscous ultrafine particle fluidized reaction device system provided in Example 2 to carry out the gas-solid reaction of Class C particles. The difference from Application Example 1 is that the gas velocity of the primary gas flow is 10 m / s and the pressure is 0.15 MPa. The remaining steps are the same as in Application Example 1.

[0118] Application Example 3

[0119] This application example uses the gas-turbulent viscous ultrafine particle fluidized reaction device system provided in Example 3 to carry out the gas-solid reaction of a mixture of type A particles and type C particles. The difference from Application Example 1 is that the gas velocity of the primary gas flow is 40 m / s and the pressure is 0.45 MPa. The remaining steps are the same as in Application Example 1.

[0120] Application Example 4

[0121] This application example uses the gas-turbulent viscous ultrafine particle fluidized reaction device system provided in Example 4 to carry out the gas-solid reaction of Class C particles. The difference from Application Example 1 is that the gas velocity of the primary gas flow is 5 m / s and the pressure is 0.2 MPa. The remaining steps are the same as in Application Example 1.

[0122] Application Example 5

[0123] This application example uses the gas-turbulent viscous ultrafine particle fluidized reaction device system provided in Example 5 to carry out the gas-solid reaction of a mixture of type B particles and type C particles. The difference from Application Example 1 is that the gas velocity of the primary gas flow is 30 m / s and the pressure is 0.25 MPa. The remaining steps are the same as in Application Example 1.

[0124] Application Example 6

[0125] This application example uses the gas-turbulent viscous ultrafine particle fluidized reaction device system provided in Example 6 to carry out the gas-solid reaction of Class C particles. The difference from Application Example 1 is that the gas velocity of the primary gas flow is 45 m / s and the pressure is 0.4 MPa. The remaining steps are the same as in Application Example 1.

[0126] Application Example 7

[0127] This application example uses the gas-turbulent viscous ultrafine particle fluidized reaction device system provided in Example 7 to carry out the gas-solid reaction of Class C particles. The difference from Application Example 1 is that the gas velocity of the primary gas flow is 50 m / s and the pressure is 0.5 MPa. The remaining steps are the same as in Application Example 1.

[0128] Application Example 8

[0129] This application example uses the gas-turbulent viscous ultrafine particle fluidized reaction device system provided in Example 8 to carry out the gas-solid reaction of Class C particles. The difference from Application Example 1 is that the gas velocity of the primary gas flow is 20 m / s and the pressure is 0.3 MPa. The remaining steps are the same as in Application Example 1.

[0130] Comparative Example 1

[0131] This comparative example provides a fluidized reaction device system, which differs from Example 1 in that it does not have a multi-directional gas supply unit, but the rest of the structure is the same as that of Example 1.

[0132] Comparative Example 2

[0133] This comparative example provides a fluidized reaction device system, which differs from Example 1 in that: a stirring device is provided in the reaction chamber 1, but a multi-directional gas supply unit is not provided; the rest of the structure is the same as in Example 1.

[0134] Comparative Example 3

[0135] This comparative example provides a fluidized reaction device system, which differs from Example 1 in that: a circulating airflow device is added and connected to the top and bottom of the reaction chamber 1 respectively, so that some gas flows back to the dense phase region 102 after passing through the reaction chamber 1 to achieve circulating disturbance. A multi-directional gas replenishment unit is not set up, and the rest of the structure is the same as Example 1.

[0136] Comparative Application Example 1

[0137] This comparative application example uses the fluidized bed reactor system provided in Comparative Example 1 to perform a gas-solid reaction of Class C particulate matter. The specific process includes: feeding Class C particulate matter into the reaction chamber 1 using the feeding device 2 and distributing it in the bottom area of ​​the reaction chamber 1; starting the air supply fan 4 to allow primary gas to enter the dense phase zone 102 from the gas distribution plate at the bottom, gradually increasing the flow rate to promote the fluidization of the solid raw material. The primary gas flow velocity is 25 m / s and the pressure is 0.3 MPa. The gaseous mixture generated by the reaction enters the gaseous zone 101 and is discharged from the top of the reaction chamber 1 to the cyclone separator 6. The fine particles carried upward by the airflow are collected by the cyclone separator 6, effectively trapping the particulate matter and separating it in the finished product bin. The separated gas is then discharged to the waste gas treatment system for post-treatment.

[0138] Compared to Application Example 1, which uses unidirectional gas inflow, it is impossible to achieve uniform disturbance of C-type particles, resulting in low gas-solid contact efficiency and insufficient effective contact area between the gas and solid phases, thereby reducing reaction efficiency and product quality.

[0139] Comparative Application Example 2

[0140] This comparative application example uses the fluidized bed reactor system provided in Comparative Example 2 to perform a gas-solid reaction of Class C particulate matter. The specific process includes: feeding Class C particulate matter into the reaction chamber 1 using the feeding device 2 and distributing it in the bottom area of ​​the reaction chamber 1; starting the air supply fan 4 to allow primary gas to enter the dense phase zone 102 from the gas distribution plate at the bottom, gradually increasing the flow rate to promote the fluidization of the solid raw material; the primary gas flow velocity is 25 m / s and the pressure is 0.3 MPa; at the same time, the stirring device is turned on to agitate the material in the reaction chamber 1, and the gaseous mixture generated by the reaction enters the gas zone 101 and is discharged from the top of the reaction chamber 1 to the cyclone separator 6. The fine particles carried upward by the airflow are collected by the cyclone separator 6, effectively trapping the particulate matter and separating it in the finished product bin; the separated gas is then discharged to the waste gas treatment system for post-treatment.

[0141] Compared to Application Example 1, Application Example 2 showed a more significant problem of particle adhesion during the reaction process, leading to uneven fluidization and even loss of flow, resulting in uneven reaction and affecting product quality.

[0142] Comparative Application Example 3

[0143] This comparative application example uses the fluidized bed reactor system provided in Comparative Example 3 to perform a gas-solid reaction of Class C particulate matter. The specific process includes: feeding Class C particulate matter into the reaction chamber 1 using the feeding device 2 and distributing it in the bottom area of ​​the reaction chamber 1; starting the air supply fan 4 to allow primary gas to enter the dense phase zone 102 from the gas distribution plate at the bottom, gradually increasing the flow rate to promote the fluidization of the solid raw material; the primary gas flow velocity is 25 m / s and the pressure is 0.3 MPa; at the same time, some of the gas flows back into the dense phase zone 102 after passing through the reaction chamber 1 to achieve circulation and disturbance; the gaseous mixture generated by the reaction enters the gaseous zone 101 and is discharged from the top of the reaction chamber 1 to the cyclone separator 6; the fine particles carried upward by the airflow are collected by the cyclone separator 6, effectively trapping the particulate matter, and separating it in the finished product bin; the separated gas is then discharged to the waste gas treatment system for post-treatment.

[0144] Compared to Application Example 1, Application Example 3 showed agglomeration and channeling of Class C particles, uneven airflow, and a tendency for air embolism. The contact uniformity between the gas and Class C particles was poor, resulting in too many fine particles being entrained by the gas into the cyclone separator 6.

[0145] This invention, through the design of a multi-directional gas supply unit, allows gas to enter the reaction chamber 1 from multiple directions, creating a uniform fluidization effect within it. This achieves efficient fluidization of solid materials within the fluidized reaction chamber 1, thereby avoiding particle agglomeration and channeling, ensuring sufficient gas-solid contact, and improving reaction efficiency. Simultaneously, the bottom tongue-shaped distribution plate 3, through a specific flow channel design, allows gas to enter along a tortuous path and be evenly distributed throughout the reaction area, reducing airflow short-circuiting and preventing excessive fine particles from being rapidly entrained out of the reaction chamber 1. Furthermore, the invention incorporates a cyclone separator in the top bypass, which can recover fine particles entrained by the airflow during startup or use, reducing losses caused by particle entrainment and improving product yield. The design of this invention effectively improves the fluidization effect of Class C particles. Through the rational configuration and structural arrangement of the multi-directional gas supply system, uniform flow of particles and efficient gas-solid contact in the fluidized bed are achieved, overcoming the problems of particle agglomeration and channeling in traditional fluidized beds. This greatly improves the performance and application range of the reactor, and has higher operational flexibility. The airflow direction and flow rate can be adjusted in real time according to the reaction conditions, making it more adaptable.

[0146] The applicant declares that the above description is only a specific embodiment of the present invention, but the protection scope of the present invention is not limited thereto. Those skilled in the art should understand that any changes or substitutions that can be easily conceived by those skilled in the art within the technical scope disclosed in the present invention fall within the protection and disclosure scope of the present invention.

Claims

1. A gas-turbulent viscous ultrafine particle fluidized bed reactor system, characterized in that, The gas-turbulent viscous ultrafine particle fluidized reaction device system includes a fluidized reaction unit, a gas supply unit, a multi-directional gas replenishment unit, and a gas-solid separation unit; The fluidized bed reaction unit includes a reaction chamber, within which a gaseous zone and a dense phase zone are sequentially arranged along the axial direction. The gas supply unit is connected to the bottom of the reaction chamber and provides a primary gas flow to the dense phase zone. The multi-directional gas replenishment unit includes a gas replenishment module and several gas replenishment components. The gas replenishment module is connected to several gas replenishment components, and the several gas replenishment components are independently connected to the reaction chamber and communicate with the dense phase zone to provide a secondary gas flow. The gas-solid separation unit is connected to the gaseous zone. Several gas replenishment components are equidistantly arranged along the axial and / or circumferential direction of the reaction chamber. With the central axis of the reaction chamber as a reference, the gas replenishment components are arranged in any one or a combination of at least two of the following: tangential arrangement, radial arrangement, inclined upward arrangement, or inclined downward arrangement. The arrangement directions of the several gas replenishment components may be the same or different. When the gas replenishment component is tangentially arranged, the angle between the gas replenishment component and the inner wall of the reaction chamber along the circumferential direction is 15°~45°; when the gas replenishment component is inclined upward, the angle between the gas replenishment component and the inner wall of the reaction chamber along the axial direction is 15°~60°; when the gas replenishment component is inclined downward, the angle between the gas replenishment component and the inner wall of the reaction chamber along the axial direction is 15°~60°.

2. The gas-turbulent viscous ultrafine particle fluidized bed reactor system according to claim 1, characterized in that, The gas replenishment component is sealed to the outer peripheral wall of the dense phase region of the reaction chamber; The distance between the air outlet of the gas replenishment component and the inner wall of the reaction chamber is 2% to 20% of the diameter of the reaction chamber.

3. The gas-turbulent viscous ultrafine particle fluidized bed reactor system according to claim 1, characterized in that, The air replenishment module includes an air replenishment fan and a first air storage device connected in sequence, and the outlet end of the first air storage device is connected to a plurality of the air replenishment components respectively; The first gas storage device is connected to the gas replenishment component through a gas replenishment pipeline, and the gas replenishment pipeline is equipped with a first flow detection component, a first pressure detection component and a first regulating valve.

4. The gas-turbulent viscous ultrafine particle fluidized bed reactor system according to claim 1, characterized in that, A gas distribution plate is provided at the bottom of the inner cavity of the reaction chamber, and the primary gas flow passes through the gas distribution plate and enters the dense phase region. The gas distribution plate is a tongue-shaped distribution plate; The reaction chamber has a cylindrical structure; The volume of the dense phase region is 40% to 70% of the total volume of the reaction chamber; The fluidized reaction unit also includes a feeding device connected to the reaction chamber; The bottom of the reaction chamber is also provided with a discharge port.

5. The gas-disturbance type viscous ultrafine particle fluidized bed reactor system according to claim 1, characterized in that, The gas supply unit includes a gas supply fan and a second gas storage device connected in sequence, and the outlet end of the second gas storage device is connected to the bottom of the reaction chamber. The second gas storage device is connected to the reaction chamber through a gas supply pipeline, and the gas supply pipeline is equipped with a second flow detection component, a second pressure detection component and a second regulating valve.

6. The gas-turbulent viscous ultrafine particle fluidized bed reactor system according to claim 1, characterized in that, The gas-solid separation unit includes a cyclone separator connected to the gaseous zone. The top and bottom of the cyclone separator are respectively provided with an exhaust port and a discharge port.

7. A gas-perturbed fluidized bed reaction method, characterized in that, The gas-perturbed fluidized bed reaction method employs the gas-perturbed viscous ultrafine particle fluidized bed reaction device system according to any one of claims 1-6, and the gas-perturbed fluidized bed reaction method includes: (1) Fill the solid raw material into the dense phase region and introduce a gas flow to carry out a gas-solid reaction, so that the solid raw material is in a fluidized state; (2) A secondary gas flow is then introduced into the dense phase region to form a multi-directional gas disturbance field, thereby enhancing the fluidization effect and generating a gaseous mixture; (3) Perform gas-solid separation on the gaseous mixture generated by the fluidization reaction.

8. The gas-perturbed fluidized bed reaction method according to claim 7, characterized in that, The gas disturbance fluidized reaction method further includes: adjusting the injection angle, pressure and velocity of the secondary gas flow to enhance the fluidization state of the solid raw material in the dense phase region.

9. The gas-perturbed fluidized bed reaction method according to claim 8, characterized in that, The direction of secondary airflow in the multidirectional gas disturbance field includes any one or a combination of at least two of the following: tangential, radial, inclined upward, or inclined downward. The velocity of the secondary airflow is less than the velocity of the primary airflow. The pressure of the secondary airflow is less than the pressure of the primary airflow.

10. The gas-perturbed fluidized bed reaction method according to claim 9, characterized in that, The velocity of the primary airflow is 0.003~50m / s; The pressure of the primary airflow is 0.1~0.5MPa.

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