Coaxial reversal synergistic fluidized bed equipment and fluidization method for C-type particles

Abstract

The invention relates to coaxial reversal synergistic fluidized bed equipment for class-C particles and a fluidization method, and relates to the technical field of gas-solid fluidization reaction. The coaxial reversal synergistic fluidized bed equipment comprises a fluidization chamber and a stirring unit arranged in a fluidized bed body in the fluidization chamber; the stirring unit comprises a first stirring paddle and a second stirring paddle which coaxially rotate in opposite directions; at least one first air supply hole is formed in the first stirring paddle, and / or at least one second air supply hole is formed in the second stirring paddle. According to the equipment provided by the invention, a fluid dynamic field which alternately flows up and down is formed through a coaxial reversal multidirectional stirring mechanism, the particle fluidization state is optimized, and particle deposition and bubble accumulation are avoided; meanwhile, a plurality of air holes are formed in the stirring paddle, so that the precise distribution of gas and the homogenization of bubbles are realized, the surge phenomenon is reduced, the synergism of stirring and fluidization is further improved, the particles can be uniformly distributed in the bed body, the gas-solid contact is more sufficient, and the fluidization effect and the reaction efficiency are obviously improved.

Description

Technical Field

[0001] This invention relates to the field of gas-solid fluidization reaction technology, specifically to a coaxial reverse synergistic fluidized bed device and fluidization method for C-type particles. Background Technology

[0002] Currently, gas-solid fluidized beds, as highly efficient reaction and separation devices, are widely used in chemical, energy, metallurgical, and environmental protection fields. The main advantages of fluidized beds include high mass and heat transfer efficiency, uniform gas-solid contact, and high operational flexibility. However, traditional fluidized bed equipment still faces many challenges in practical applications, especially in the processing of highly viscous solid particles, gas-liquid-solid multiphase systems, and micron-sized particles, where equipment performance, reaction efficiency, and stability are constrained by various factors.

[0003] Especially for Class C particles (<30μm in diameter), the strong electrostatic and van der Waals forces between particles make them prone to agglomeration, leading to phenomena such as choking, embolism, channeling, dead zones, or particle loss during fluidization. Furthermore, gas entering the fluidized bed may form bubbles of varying sizes. These bubbles gradually merge and enlarge during their movement, causing non-uniformity in gas-solid flow, which in turn affects the stability of the fluidization state, hinders separation and reaction efficiency, and reduces product quality.

[0004] To overcome the above problems, existing technologies often introduce external energy such as vibration and magnetic fields, or complex structural designs (such as multi-layer impeller systems) to improve fluidization quality. However, these technologies often face problems such as high energy consumption, high cost, and complex maintenance, making it difficult to meet the economic requirements of industrial production.

[0005] For example, CN118267939A discloses a fluidized bed reactor and system suitable for C-type particles, which integrates pressure regulation, heating, drive shaft and multi-stage stirring functions to solve problems such as particle agglomeration, channeling and uneven reaction in gas-solid fluidization process. It is mainly used in fine chemical, energy and materials fields, especially for the treatment of C-type particles (particle size less than 30μm). However, the design optimization of the impeller and gas distributor is limited, and it does not combine other auxiliary technologies to further improve the mixing efficiency. It has weak adaptability to high viscosity particles or gas-liquid-solid multiphase systems, and is limited to the improvement of single gas-solid systems. Moreover, the system energy consumption control and equipment structure compactness need to be further optimized.

[0006] CN205110110U discloses a stirred air heavy medium fluidized bed separation device, which integrates a blower, a frame-type stirring paddle and a dust removal device for dry separation of particulate materials. Its core is to improve the separation efficiency by breaking up bubbles and suppressing axial back mixing through the stirring paddle. It is suitable for gas-solid two-phase flow separation processes. However, the bubble breaking effect of this scheme is limited by the design of the frame-type stirring paddle, which has limited improvement on the uniformity of particle distribution and is difficult to adapt to highly viscous particles or complex systems.

[0007] CN116367914A discloses a novel stirring mechanism and its manufacturing method, mainly for applications in stirred fluidized beds, solid mixtures, and high-viscosity suspensions. However, in high shear stress or ultra-large-scale industrial reactors, the stability and service life of the connecting elements and blades may be insufficient.

[0008] CN219744819U discloses a coaxial counter-rotating stirred tank for hydrometallurgy. By setting up two coaxial counter-rotating stirring shafts and a venting sleeve, multi-directional flow of liquid is achieved, which improves the stirring uniformity and gas utilization efficiency in the gas-liquid-solid reaction system. However, this solution is limited to a stirred tank reactor, has a relatively limited scope of application, and has limited adaptability to other complex multiphase systems. In addition, the structure is complex and the manufacturing and maintenance costs are high.

[0009] CN212594073U discloses a material mixing uniform distillation kettle, which improves the material mixing uniformity through a coaxial reverse stirring device, thereby optimizing the efficiency of the distillation process. However, this design is mainly for the distillation of liquid materials and is not adaptable to other systems. It has limited effect on improving the mixing efficiency of high-viscosity materials, and its adaptability needs to be further strengthened.

[0010] In summary, existing stirred fluidized beds are relatively few and mostly employ unidirectional stirring methods (such as turbine, anchor, and frame impellers). The stirring direction is singular, the range of fluid disturbance is limited, making it difficult to form multidirectional mixed flow. This easily leads to dead zones of particle accumulation. Especially when processing highly viscous materials or fine particles, as well as gas-liquid-solid three-phase systems, insufficient mixing uniformity becomes a key issue restricting system efficiency. Summary of the Invention

[0011] In view of the problems existing in the prior art, the purpose of the present invention is to provide a coaxial reverse synergistic fluidized bed device and fluidization method for C-type particles, so as to solve the defects of the current fluidized bed for C-type particles. Due to the small particle size and strong viscous effects such as electrostatic force and van der Waals force, the particles are prone to agglomeration. During the fluidization process, phenomena such as stagnation, channeling, uneven bubble and insufficient gas-solid contact or dead zones often occur, resulting in low equipment operating efficiency, thereby affecting the efficiency and uniformity of the reaction.

[0012] To achieve this objective, the present invention adopts the following technical solution:

[0013] In a first aspect, the present invention provides a coaxial inverted synergistic fluidized bed device for C-type particles, the coaxial inverted synergistic fluidized bed device comprising:

[0014] Fluidization chamber, and a stirring unit disposed within the fluidized bed body of the fluidization chamber;

[0015] The stirring unit includes: a first stirring blade and a second stirring blade that rotate in opposite directions on the same axis.

[0016] The first agitator blade is provided with at least one first air inlet hole, and / or the second agitator blade is provided with at least one second air inlet hole.

[0017] The coaxial reverse-flow synergistic fluidized bed device provided by this invention forms a fluid dynamic field with alternating up and down flow through a multi-directional stirring mechanism of coaxial reverse-flow, further optimizing the fluidization state of particles and avoiding particle deposition and bubble accumulation. At the same time, by setting multiple pores on the stirring paddle, the precise distribution of gas and the homogenization of bubbles are achieved, reducing the throttling phenomenon and further improving the synergy between stirring and fluidization. This allows particles to be evenly distributed in the bed, and the gas-solid contact to be more sufficient, thereby significantly improving the fluidization effect and reaction efficiency.

[0018] As a preferred technical solution of the present invention, the first impeller includes one or a combination of at least two of the following: a flat blade impeller, a folding blade impeller, a curved blade impeller, an anchor impeller, a frame impeller, a ribbon impeller, or a screw impeller.

[0019] Preferably, the second impeller includes one or a combination of at least two of the following: a flat-blade impeller, a folding-blade impeller, a curved-blade impeller, an anchor impeller, a frame impeller, a ribbon impeller, or a screw impeller.

[0020] As a preferred embodiment of the present invention, the spacing between adjacent first air inlets gradually decreases along the direction away from the center of the fluidization chamber.

[0021] Preferably, the spacing between adjacent second air inlets gradually decreases in the direction away from the center of the fluidization chamber.

[0022] As a preferred embodiment of the present invention, the angle between the gas injection direction of the first air inlet and the particle trajectory is 30-45°.

[0023] Preferably, the angle between the gas injection direction of the second air inlet and the particle trajectory is 30-45°.

[0024] As a preferred embodiment of the present invention, the diameter of the first air inlet is 0.5-2.5 mm.

[0025] Preferably, the diameter of the second air inlet is 0.5-2.5 mm.

[0026] The second method, according to the present invention, provides a fluidization method for ultrafine viscous particles, the fluidization method comprising:

[0027] Ultrafine viscous particles and gas are fed into the fluidization chamber, while the first and second stirring are carried out simultaneously.

[0028] The first and second stirrs rotate in opposite directions and their axes of rotation are on the same straight line.

[0029] Gas is supplied to the blades of the first stirring paddle through the first air inlet, and / or gas is supplied to the blades of the second stirring paddle through the second air inlet.

[0030] As a preferred embodiment of the present invention, the stirring rate of the first stirring is 20-100 r / min.

[0031] Preferably, the angle between the injection direction of the gas introduced through the first air inlet during the first stirring and the trajectory of the particles is 30-45°.

[0032] As a preferred embodiment of the present invention, the stirring rate of the second stirring is 15-90 r / min.

[0033] Preferably, the angle between the injection direction of the gas introduced through the second air inlet during the second stirring and the trajectory of the particles is 30-45°.

[0034] As a preferred technical solution of the present invention, the gas velocity of the gas fed into the first air inlet during the first stirring is 0.01-0.6 m / s.

[0035] Preferably, the pressure of the gas fed into the first air inlet during the first stirring is 0.01-0.05 MPa.

[0036] As a preferred technical solution of the present invention, the gas velocity of the gas fed into the second air inlet during the second stirring is 0.01-0.2 m / s.

[0037] Preferably, the pressure of the gas fed into the second air inlet during the second stirring is 0.02-0.03 MPa.

[0038] Compared with existing technical solutions, the present invention has the following beneficial effects:

[0039] (1) The fluidization device provided by the present invention can efficiently fluidize particles and mix gas and solid. With the help of the coaxial reverse stirring design, multi-directional flow is increased, which not only breaks up large bubbles, but also enhances the uniformity of particle and gas distribution. It is particularly suitable for the processing of C-type particles and high-viscosity materials, making gas-solid contact more sufficient and greatly improving mass transfer and reaction efficiency.

[0040] (2) The fluidization device provided by the present invention has air holes in the propeller or stirring frame. Through precise gas distribution technology, it further improves the problem of poor fluidization effect in traditional fluidized beds and avoids phenomena such as air embolism, channeling or dead zones.

[0041] (3) The fluidization device provided by this invention has a compact structure and adds a coaxial reverse-stirring propeller transmission mechanism and air supply path. While avoiding the problem of excessive torque of the rotating rod in traditional equipment leading to increased equipment load, it is easy to achieve operation and control, and at the same time reduces operating costs. Optimized in terms of dynamics, the reverse stirring further enhances stirring efficiency through the counter-current effect of the upper and lower fluids, reducing the equipment's demand for high torque and minimizing axial back-mixing of materials. It is suitable for various gas-solid reaction scenarios, including high-efficiency gas-solid reactions in chemical, energy, and fine chemical industries, and performs particularly well in highly viscous particles or difficult-to-disperse materials.

[0042] (4) The fluidization device provided by the present invention does not require the introduction of additional high-energy-consuming equipment compared with traditional stirring, vibration or magnetic field fluidized beds, thus greatly reducing energy consumption. At the same time, the manufacturing and maintenance costs of the equipment are reduced, which improves the economy and scalability of large-scale application. It is suitable for both single gas-solid reactions and gas-liquid-solid three-phase systems. It has broad application potential in chemical, metallurgical, energy and environmental protection fields. For C-type particles and similar high-viscosity materials or micron-sized particle systems, the present invention can significantly improve reaction efficiency and product quality. Attached Figure Description

[0043] Figure 1 This is a schematic diagram of a fluidized reaction apparatus for Class C particles provided in an embodiment of the present invention;

[0044] Figure 2 This is a schematic diagram of the stirring unit in this embodiment of the invention, where the stirring paddle is a paddle type.

[0045] Figure 3 This is a schematic diagram of the stirring blade with air holes in the stirring unit in an embodiment of the present invention;

[0046] Figure 4 This is a schematic diagram showing that the stirring paddle in the stirring unit of this invention is of the anchor type;

[0047] Figure 5 This is a schematic diagram of the stirring paddle in the stirring unit of this invention having an anchor-type air hole.

[0048] Figure 6 This is a schematic diagram of a frame-type stirring paddle in an embodiment of the present invention;

[0049] Figure 7 This is a schematic diagram of a frame-type stirring paddle in an embodiment of the present invention;

[0050] Figure 8 This is a schematic diagram of a frame-shaped stirring paddle in an embodiment of the present invention.

[0051] In the diagram: 100-fluidization chamber, 110-fluidized bed body, 120-stirring unit, 121-first stirring paddle, 122-second stirring paddle, 123-first air inlet, 200-granular silo, 310-gas cylinder, 320-fan, 400-cyclone separator, 500-granular discharge port.

[0052] The present invention will now be described in further detail. However, the examples described below are merely simplified examples of the present invention and do not represent or limit the scope of protection of the present invention. The scope of protection of the present invention is determined by the claims. Detailed Implementation

[0053] To better illustrate the present invention and facilitate understanding of its technical solutions, typical but non-limiting embodiments of the present invention are as follows:

[0054] Currently, when fluidizing C-type particles (particle size <30μm), the strong electrostatic and van der Waals forces between particles cause them to easily agglomerate, leading to phenomena such as choking, embolism, channeling, dead zones, or particle loss during fluidization. Furthermore, gas entering the fluidized bed may form bubbles of varying sizes. These bubbles gradually merge and enlarge during movement, resulting in non-uniform gas-solid flow, which in turn affects the stability of the fluidization state, hinders separation and reaction efficiency, and reduces product quality. Therefore, this invention improves the fluidization effect by designing coaxial stirring units with opposite stirring directions and incorporating air inlets on the stirring paddle, as detailed below:

[0055] I. This embodiment provides a coaxial reverse-flow synergistic fluidized bed device for C-type particles, such as... Figure 1 As shown, the coaxial reverse-rotating fluidized bed device includes:

[0056] Fluidization chamber 100, and stirring unit 120 disposed within fluidized bed body 110 in fluidization chamber 100;

[0057] The stirring unit 120 includes: a first stirring blade 121 and a second stirring blade 122 that are coaxial and rotate in opposite directions;

[0058] The first stirring paddle 121 has at least one first air inlet hole 123 on its blades, and / or the second stirring paddle 122 has at least one second air inlet hole on its blades.

[0059] In this invention, the fluidized reaction equipment is also equipped with a motor, a drive shaft for driving the stirring unit 120 to rotate and stir, and an adjustment device for controlling the stirring rate. The motor controls the speed of the propeller through the speed regulating device to achieve precise control of the stirring intensity. The drive control system can be installed at the bottom or top of the reactor according to the application requirements of different fields.

[0060] In this invention, the stirring unit 120 is also equipped with a gas supply device for supplying gas to the first gas supply hole 123 and / or the second gas supply hole. The gas supply device can adjust the amount of gas replenishment according to the real-time monitored gas flow rate and pressure to ensure gas-solid mixing efficiency and particle distribution uniformity, and form a relatively sufficient disturbance inside the bed in combination with stirring.

[0061] In this invention, coaxial means that the first stirring paddle 121 and the second stirring paddle 122 are located on the same axis, and can choose to share a drive shaft or use their own independent drive shafts.

[0062] In this invention, the stirring shaft of the stirring unit 120 is positioned according to the design requirements of the fluidization equipment, such as being positioned along the axial direction of the fluidization equipment.

[0063] In this invention, the fluidized bed reactor is also equipped with a corresponding granular silo 200 for providing a solid phase to the fluidized bed reactor, and a gas feeder for providing the gas required during the fluidization process, specifically including a gas cylinder 310, a gas supply fan 320, a cyclone separator 400, and a granular discharge port 500.

[0064] In this invention, the gas supplied by the gas feeding device is the main gas supply device in the fluidization process, and the air holes configured on the stirring paddle are additional auxiliary gas supply devices, not the main gas supply end of this invention.

[0065] The first impeller 121 includes one or a combination of at least two of the following: a flat-blade impeller, a folding-blade impeller, a curved-blade impeller, an anchor impeller, a frame impeller, a ribbon impeller, or a screw impeller.

[0066] The second impeller 122 includes one or a combination of at least two of the following: a flat-blade impeller, a folded-blade impeller, a curved-blade impeller, an anchor impeller, a frame impeller, a ribbon impeller, or a screw impeller.

[0067] In this invention, the coaxial design of the first stirring impeller 121 and the second stirring impeller 122 is as follows: Figure 2 and Figure 4 As shown, Figure 3 and Figure 5 The diagrams show the distribution of the first air inlet holes 123 on the first agitator 121. The distribution of the second air inlet holes on the second agitator 122 can be found in the diagrams below. Figure 3 or Figure 5 Make arrangements.

[0068] In this invention, the impeller is an exemplary structure of a frame-type impeller, as shown below. Figure 6 , Figure 7 and Figure 8 As shown.

[0069] In this invention, the first stirring paddle 121 and the second stirring paddle 122 can also be designed as a composite stirring paddle combining multiple single-style stirring paddles, such as a reasonable combination of a flat-blade stirring paddle and a frame stirring paddle.

[0070] In this invention, the first impeller 121 and the second impeller 122 can be selected and preferably both have a propeller-type (e.g., ribbon or screw) structure, with a pitch of 0.8-1.2 times the impeller diameter, to balance axial conveying capacity and particle disturbance effect. When the pitch is small (e.g., less than 0.5D), the impeller propulsion capacity is weak, and solid particles may accumulate at the leading edge of the ribbon, resulting in local accumulation and bubble agglomeration, forming an uneven fluidization zone. When the pitch is too large (e.g., greater than 2D), the helical angle of the impeller tends to be slow, the axial propulsion capacity is enhanced but the radial disturbance is worse, which may form axial channeling. A reasonable pitch design (e.g., 0.8-1.2D) helps to form a stable disturbance flow field in front of the impeller, enhances particle dispersion and renewal frequency, and at the same time, forms an interlaced flow with the difference in stirring direction, optimizes the particle distribution and gas channels in the bed, reduces channeling, dead zones and bubble aggregation problems, thereby improving fluidization uniformity and reaction efficiency.

[0071] The spacing between adjacent first air inlets 123 gradually decreases in the direction away from the center of fluidization chamber 100.

[0072] The spacing between adjacent second air inlets gradually decreases in the direction away from the center of the fluidization chamber 100.

[0073] For example, the first air inlet 123 is adjacent to the stirring shaft. Based on this, the distance between adjacent first air inlets 123 gradually decreases by 1-2 mm. The distance between the first first air inlet 123 and the second first air inlet 123 is 15-20 mm, and so on to achieve the overall design of the first air inlet 123.

[0074] For example, the second air inlet is adjacent to the stirring shaft. Based on this, the distance between adjacent second air inlets gradually decreases by 1-2 mm. The distance between the first and second second air inlets is 15-20 mm, and so on to achieve the overall design of the second air inlets.

[0075] Wherein, the angle between the gas injection direction of the first air inlet 123 and the particle movement trajectory is 30-45°, for example, it can be 30°, 31°, 32°, 33°, 34°, 35°, 36°, 37°, 38°, 39°, 40°, 41°, 42°, 43°, 44° or 45°, but is not limited to the listed values, and other unlisted values ​​within this range also meet the requirements.

[0076] Wherein, the angle between the gas injection direction of the first air inlet 123 and the particle movement trajectory is 30-45°, for example, it can be 30°, 31°, 32°, 33°, 34°, 35°, 36°, 37°, 38°, 39°, 40°, 41°, 42°, 43°, 44° or 45°, but is not limited to the listed values, and other unlisted values ​​within this range also meet the requirements.

[0077] The diameter of the second air inlet is 0.5-2.5mm, for example, it can be 0.5mm, 0.6mm, 0.8mm, 1mm, 1.2mm, 1.4mm, 1.6mm, 1.8mm, 2mm, 2.2mm, 2.4mm or 2.5mm, but is not limited to the listed values. Other unlisted values ​​within this range also meet the requirements.

[0078] The diameter of the second air inlet is 0.5-2.5mm, for example, it can be 0.5mm, 0.6mm, 0.8mm, 1mm, 1.2mm, 1.4mm, 1.6mm, 1.8mm, 2mm, 2.2mm, 2.4mm or 2.5mm, but is not limited to the listed values. Other unlisted values ​​within this range also meet the requirements.

[0079] For example, the process of using a fluidized bed reactor is as follows:

[0080] Gas enters gas cylinder 310 through blower 320, passes through gas supply pipeline, and enters fluidized bed from the bottom after flow meter adjustment;

[0081] Solid material is quantitatively added from the granular silo 200 into the fluidization chamber 100 via a conveying device; gas enters the bed through a distribution plate and comes into contact with the solid particles to form a fluidized state.

[0082] The coaxial reverse propeller stirs the gas-solid mixture in multiple directions. The first impeller 121 breaks down large bubbles downwards, and the second impeller 122 pushes solid particles upwards to achieve uniform gas-solid distribution. A small amount of gas is introduced near the impeller blades through the first air inlet 123 and the second air inlet to further optimize the bubble distribution and prevent channeling or embolism.

[0083] After fluidization, part of the gas-solid mixture is discharged from the top of the fluidized bed and enters the cyclone separator 400. After fine particles are captured, the purified gas is discharged through the exhaust port, and the main reaction material is discharged through the particle discharge port 500 of the reactor.

[0084] In fluidized bed reactors, bed height is a crucial parameter reflecting the uniformity of gas-solid distribution and the degree of particle fluidization. Directional gas supply to the middle and upper parts of the granular material via first and / or second air inlets on the agitator effectively regulates the penetration depth and distribution density of gas within the bed, thereby preventing the formation of large bubbles and localized particle deposition caused by gas concentration at the bed bottom.

[0085] By rationally adjusting the agitator speed and the air supply flow rate, direction, and distribution at the air inlets, the bed height can be maintained within a stable fluctuation range (e.g., within ±5%), improving the overall uniformity and stability of the bed. In particular, when the bed height is within a set operating window (e.g., 50-70% of the reactor volume), the agitation-air supply coupling mechanism of this invention effectively reduces stagnation and collapse phenomena, achieving stable particle dispersion throughout the entire bed height range. Therefore, the synergistic effect of the agitation-air supply unit and the maintenance of bed height are highly coupled, significantly improving the system's fluidization effect.

[0086] II. This embodiment provides a fluidization method for Class C particles, the fluidization method comprising:

[0087] Type C particles and gas are fed into fluidization chamber 100, while the first and second stirring are performed simultaneously.

[0088] The first and second stirrs rotate in opposite directions and their axes of rotation are on the same straight line.

[0089] Gas is supplied to the blades of the first stirring paddle through the first air inlet 123, and / or gas is supplied to the blades of the second stirring paddle through the second air inlet.

[0090] In this invention, the synergistic optimization of stirring and gas replenishment during fluidization makes the gas-solid fluidization in the fluidized bed more stable, solving the problems of particle loss, deposition and uneven distribution.

[0091] The stirring rate of the first stirring is 20-100 r / min, for example, it can be 20 r / min, 30 r / min, 40 r / min, 50 r / min, 60 r / min, 70 r / min, 80 r / min, 90 r / min or 100 r / min, but is not limited to the listed values. Other unlisted values ​​within this range also meet the requirements.

[0092] Wherein, the angle between the injection direction of the gas introduced by the first air inlet 123 in the first stirring and the trajectory of the particle is 30-45°, for example, it can be 30°, 31°, 32°, 33°, 34°, 35°, 36°, 37°, 38°, 39°, 40°, 41°, 42°, 43°, 44° or 45°, but is not limited to the listed values. Other unlisted values ​​within this range also meet the requirements.

[0093] The stirring rate of the second stirring is 15-90 r / min, for example, it can be 15 r / min, 20 r / min, 30 r / min, 40 r / min, 50 r / min, 60 r / min, 70 r / min, 80 r / min or 90 r / min, but is not limited to the listed values. Other unlisted values ​​within this range are also acceptable.

[0094] In the second stirring process, the angle between the injection direction of the gas introduced through the second air inlet and the trajectory of the particles is 30-45°, for example, it can be 30°, 31°, 32°, 33°, 34°, 35°, 36°, 37°, 38°, 39°, 40°, 41°, 42°, 43°, 44° or 45°, but is not limited to the listed values. Other unlisted values ​​within this range also meet the requirements.

[0095] Wherein, the gas velocity fed into the first air inlet 123 in the first stirring is 0.01-0.6 m / s, for example, it can be 0.01 m / s, 0.02 m / s, 0.04 m / s, 0.06 m / s, 0.08 m / s, 0.1 m / s, 0.15 m / s, 0.2 m / s, 0.25 m / s, 0.3 m / s, 0.35 m / s, 0.4 m / s, 0.45 m / s, 0.5 m / s, 0.55 m / s or 0.6 m / s, but is not limited to the listed values. Other unlisted values ​​within this range also meet the requirements.

[0096] Wherein, the pressure of the gas fed into the first air inlet 123 in the first stirring is 0.01-0.05MPa, for example, it can be 0.01MPa, 0.015MPa, 0.02MPa, 0.025MPa, 0.03MPa, 0.035MPa, 0.04MPa, 0.045MPa or 0.05MPa, but is not limited to the listed values. Other unlisted values ​​within this range also meet the requirements.

[0097] The gas velocity introduced through the second air inlet in the second stirring process is 0.01-0.2 m / s, for example, it can be 0.01 m / s, 0.02 m / s, 0.04 m / s, 0.06 m / s, 0.08 m / s, 0.1 m / s, 0.12 m / s, 0.14 m / s, 0.16 m / s, 0.18 m / s or 0.2 m / s, but is not limited to the listed values. Other unlisted values ​​within this range also meet the requirements.

[0098] The pressure of the gas fed into the second air inlet in the second stirring is 0.02-0.03 MPa, for example, it can be 0.02 MPa, 0.021 MPa, 0.022 MPa, 0.023 MPa, 0.024 MPa, 0.025 MPa, 0.026 MPa, 0.027 MPa, 0.028 MPa, 0.029 MPa or 0.03 MPa, but is not limited to the listed values. Other unlisted values ​​within this range are also acceptable.

[0099] III. To illustrate the fluidization effect achievable by the fluidized reaction apparatus for Class C particles provided by this invention, the following practical example is used for explanation:

[0100] Example 1

[0101] This embodiment provides a coaxial inverted synergistic fluidized bed device for C-type particles, the fluidized bed device comprising:

[0102] Fluidization chamber 100, and stirring unit 120 disposed within fluidized bed body 110 in fluidization chamber 100;

[0103] The stirring unit 120 includes: a first stirring blade 121 and a second stirring blade 122 that are coaxial and rotate in opposite directions;

[0104] The first stirring paddle 121 has ten first air inlets 123 on its blades, and the second stirring paddle 122 has ten second air inlets on its blades.

[0105] The first impeller 121 is a ribbon impeller with a pitch of 0.8 times the impeller diameter; the second impeller 122 is a ribbon impeller with a pitch of 1.2 times the impeller diameter.

[0106] The spacing between adjacent first air inlets 123 gradually decreases in the direction away from the center of fluidization chamber 100; the spacing between adjacent second air inlets gradually decreases in the direction away from the center of fluidization chamber 100; the spacing between adjacent air inlets of the first impeller 121, which are adjacent to the impeller shaft, gradually decreases by 1.5 mm, and the spacing between the first air inlet 123 and the second first air inlet 123 of the first impeller 121 is 18 mm, and so on to achieve the overall design of the first air inlet 123; the spacing between adjacent air inlets of the second impeller 122, which are adjacent to the impeller shaft, gradually decreases by 2.0 mm, and the spacing between the first and second air inlets of the second impeller 122 is 20 mm, and so on to achieve the overall design of the second air inlet.

[0107] The angle between the gas injection direction of the first air inlet 123 and the particle trajectory is 35°; the angle between the gas injection direction of the second air inlet and the particle trajectory is 40°.

[0108] The diameter of the first air inlet 123 is 1 mm; the diameter of the second air inlet is 1 mm.

[0109] Example 2

[0110] This embodiment provides a coaxial inverted synergistic fluidized bed device for C-type particles, the fluidized bed device comprising:

[0111] Fluidization chamber 100, and stirring unit 120 disposed within fluidized bed body 110 in fluidization chamber 100;

[0112] The stirring unit 120 includes: a first stirring blade 121 and a second stirring blade 122 that are coaxial and rotate in opposite directions;

[0113] The first stirring paddle 121 has ten first air inlets 123 on its blades, and the second stirring paddle 122 has ten second air inlets on its blades.

[0114] The first impeller 121 is a curved blade impeller; the second impeller 122 is an anchor impeller.

[0115] The spacing between adjacent first air inlets 123 gradually decreases in the direction away from the center of fluidization chamber 100; the spacing between adjacent second air inlets gradually decreases in the direction away from the center of fluidization chamber 100; taking the first air inlets 123 adjacent to the stirring shaft as a reference, the spacing between adjacent first air inlets 123 gradually decreases by 1mm, and the spacing between the first first air inlet 123 and the second first air inlet 123 is 15mm, and so on to achieve the overall design of the first air inlets 123; taking the second air inlets adjacent to the stirring shaft as a reference, the spacing between adjacent second air inlets gradually decreases by 1mm, and the spacing between the first second air inlet and the second second second air inlet is 15mm, and so on to achieve the overall design of the second air inlets;

[0116] The angle between the gas injection direction of the first air inlet 123 and the particle trajectory is 40°; the angle between the gas injection direction of the second air inlet and the particle trajectory is 35°.

[0117] The diameter of the first air inlet 123 is 2mm; the diameter of the second air inlet is 2mm.

[0118] Example 3

[0119] This embodiment provides a coaxial inverted synergistic fluidized bed device for C-type particles, the fluidized bed device comprising:

[0120] Fluidization chamber 100, and stirring unit 120 disposed within fluidized bed body 110 in fluidization chamber 100;

[0121] The stirring unit 120 includes: a first stirring blade 121 and a second stirring blade 122 that are coaxial and rotate in opposite directions;

[0122] The first stirring paddle 121 has fifteen first air inlets 123 on its blades, and the second stirring paddle 122 has fifteen second air inlets on its blades.

[0123] The first impeller 121 is a frame impeller; the second impeller 122 is a ribbon impeller.

[0124] The spacing between adjacent first air inlets 123 gradually decreases in the direction away from the center of fluidization chamber 100; the spacing between adjacent second air inlets gradually decreases in the direction away from the center of fluidization chamber 100; taking the first air inlets 123 adjacent to the stirring shaft as a reference, the spacing between adjacent first air inlets 123 gradually decreases by 1mm, and the spacing between the first first air inlet 123 and the second first air inlet 123 is 20mm, and so on to achieve the overall design of the first air inlets 123; taking the second air inlets adjacent to the stirring shaft as a reference, the spacing between adjacent second air inlets gradually decreases by 1mm, and the spacing between the first second air inlet and the second second second air inlet is 20mm, and so on to achieve the overall design of the second air inlets.

[0125] The angle between the gas injection direction of the first air inlet 123 and the particle trajectory is 30°; the angle between the gas injection direction of the second air inlet and the particle trajectory is 45°.

[0126] The diameter of the first air inlet 123 is 0.5 mm; the diameter of the second air inlet is 2.5 mm.

[0127] Example 4

[0128] This embodiment provides a coaxial inverted synergistic fluidized bed device for C-type particles, the fluidized bed device comprising:

[0129] Fluidization chamber 100, and stirring unit 120 disposed within fluidized bed body 110 in fluidization chamber 100;

[0130] The stirring unit 120 includes: a first stirring blade 121 and a second stirring blade 122 that are coaxial and rotate in opposite directions;

[0131] The first stirring paddle 121 has sixteen first air inlets 123 on its blades, and the second stirring paddle 122 has ten second air inlets on its blades.

[0132] The first impeller 121 is a flat blade impeller; the second impeller 122 is a screw impeller with a screw pitch equal to 1 times the impeller diameter.

[0133] The spacing between adjacent first air inlets 123 gradually decreases in the direction away from the center of the fluidization chamber 100; the spacing between adjacent second air inlets gradually decreases in the direction away from the center of the fluidization chamber 100; taking the first air inlets 123 adjacent to the stirring shaft as a reference, the spacing between adjacent first air inlets 123 gradually decreases by 1mm, the spacing between the first first air inlet 123 and the second first air inlet 123 is 20mm, and so on to achieve the overall design of the first air inlets 123; taking the second air inlets adjacent to the stirring shaft as a reference, the spacing between adjacent second air inlets gradually decreases by 1mm, the spacing between the first second air inlet and the second second second air inlet is 15mm, and so on to achieve the overall design of the second air inlets;

[0134] The angle between the gas injection direction of the first air inlet 123 and the particle trajectory is 45°; the angle between the gas injection direction of the second air inlet and the particle trajectory is 30°.

[0135] The diameter of the first air inlet 123 is 2.5 mm; the diameter of the second air inlet is 0.5 mm.

[0136] Application Example 1

[0137] This application example uses the fluidized reaction equipment provided in Example 1 to perform a fluidized reaction of gas-solid materials, as detailed below:

[0138] Type C particles and gas are fed into fluidization chamber 100, while the first and second stirring are performed simultaneously.

[0139] The first and second stirrs rotate in opposite directions and their axes of rotation are on the same straight line.

[0140] Gas is supplied to the blades of the first stirring paddle through the first air inlet 123, and / or gas is supplied to the blades of the second stirring paddle through the second air inlet.

[0141] The stirring rate of the first stirrer is 50 r / min; the gas velocity fed into the first air inlet 123 during the first stirrer is 0.2 m / s; the pressure of the gas fed into the first air inlet 123 during the first stirrer is 0.02 MPa.

[0142] The stirring rate of the second stirrer is 40 r / min; the gas velocity of the gas fed into the second air inlet during the second stirrer is 0.1 m / s; and the pressure of the gas fed into the second air inlet during the second stirrer is 0.025 MPa.

[0143] Application Example 2

[0144] This application example uses the fluidized reaction equipment provided in Example 2 to perform a fluidized reaction of gas-solid materials, as detailed below:

[0145] Type C particles and gas are fed into fluidization chamber 100, while the first and second stirring are performed simultaneously.

[0146] The first and second stirrs rotate in opposite directions and their axes of rotation are on the same straight line.

[0147] Gas is supplied to the blades of the first stirring paddle through the first air inlet 123, and / or gas is supplied to the blades of the second stirring paddle through the second air inlet.

[0148] The stirring rate of the first stirrer is 80 r / min; the gas velocity fed into the first air inlet 123 during the first stirrer is 0.4 m / s; the pressure of the gas fed into the first air inlet 123 during the first stirrer is 0.03 MPa.

[0149] The stirring rate of the second stirrer is 60 r / min; the gas velocity of the gas fed into the second air inlet during the second stirrer is 0.15 m / s; and the pressure of the gas fed into the second air inlet during the second stirrer is 0.028 MPa.

[0150] Application Example 3

[0151] This application example uses the fluidized bed reactor provided in Example 3 to perform a fluidized bed reaction of gas-solid materials, as detailed below:

[0152] Type C particles and gas are fed into fluidization chamber 100, while the first and second stirring are performed simultaneously.

[0153] The first and second stirrs rotate in opposite directions and their axes of rotation are on the same straight line.

[0154] Gas is supplied to the blades of the first stirring paddle through the first air inlet 123, and / or gas is supplied to the blades of the second stirring paddle through the second air inlet.

[0155] The stirring rate of the first stirrer is 20 r / min; the gas velocity fed into the first air inlet 123 during the first stirrer is 0.6 m / s; the pressure of the gas fed into the first air inlet 123 during the first stirrer is 0.05 MPa.

[0156] The stirring rate of the second stirrer is 90 r / min; the gas velocity of the gas fed into the second air inlet during the second stirrer is 0.01 m / s; and the pressure of the gas fed into the second air inlet during the second stirrer is 0.02 MPa.

[0157] Application Example 4

[0158] This application example uses the fluidized bed reactor provided in Example 4 to perform a fluidized bed reaction of gas-solid materials, as detailed below:

[0159] Type C particles and gas are fed into fluidization chamber 100, while the first and second stirring are performed simultaneously.

[0160] The first and second stirrs rotate in opposite directions and their axes of rotation are on the same straight line.

[0161] Gas is supplied to the blades of the first stirring paddle through the first air inlet 123, and / or gas is supplied to the blades of the second stirring paddle through the second air inlet.

[0162] The stirring rate of the first stirrer is 100 r / min; the gas velocity of the gas fed into the first air inlet 123 in the first stirrer is 0.01 m / s; the pressure of the gas fed into the first air inlet 123 in the first stirrer is 0.01 MPa.

[0163] The stirring rate of the second stirrer is 15 r / min; the gas velocity of the gas fed into the second air inlet during the second stirrer is 0.2 m / s; and the pressure of the gas fed into the second air inlet during the second stirrer is 0.03 MPa.

[0164] Comparative Application Example 1

[0165] The only difference from Application Example 1 is that the first and second stirrers rotate in the same direction during the fluidization process.

[0166] Comparative Application Example 2

[0167] The only difference from Application Example 1 is that neither the first air inlet 123 nor the second air inlet is supplied with gas during the fluidization process.

[0168] Application Example 5

[0169] The only difference from Application Example 1 is that the angle between the injection direction of the gas supplied by the first gas inlet 123 and the trajectory of the particles during the fluidization process is 20°.

[0170] Application Example 6

[0171] The only difference from Application Example 1 is that the angle between the injection direction of the gas supplied by the second gas inlet during fluidization and the trajectory of the particles is 20°.

[0172] Application Example 7

[0173] The only difference from Application Example 1 is that the angle between the injection direction of the gas fed into the first gas inlet 123 and the trajectory of the particles during the fluidization process is 60°.

[0174] Application Example 8

[0175] The only difference from Application Example 1 is that the angle between the injection direction of the gas supplied by the second gas inlet during fluidization and the trajectory of the particles is 60°.

[0176] Application Example 9

[0177] The only difference from Application Example 1 is that the first air supply holes 123 are evenly spaced during the fluidization process.

[0178] Application Example 10

[0179] The only difference from Application Example 1 is that the second air supply holes are evenly distributed during the fluidization process.

[0180] The above application examples 1-4 were used to fluidize different gas-solid materials to evaluate the performance of the fluidization reaction equipment of the present invention. The relevant parameters of the gas-solid materials used are detailed in Table 1, and the fluidization results are detailed in Table 2.

[0181] Table 1

[0182] solid particles gas Application Example 1 Resin-based carbon microspheres <![CDATA[CO2 / Ar]]> Application Example 2 Petroleum coke-based carbon materials <![CDATA[CO2 / Ar]]> Application Example 3 Biomass-based carbon materials <![CDATA[CO2 / Ar]]> Application Example 4 Resin-based porous carbon Silane / Acetylene

[0183] Table 2

[0184] Fluidization results Application Example 1 A stable expanded bed with good uniformity is formed. Application Example 2 The bed expands well, the disturbance is enhanced, and the suspension is good. Application Example 3 The bed expansion effect is good, and the particle agglomeration is fully dispersed. Application Example 4 The bed expands sufficiently, with minimal pressure drop fluctuations and good uniformity. Comparative Application Example 1 Severe sedimentation at the bottom, large pressure drop fluctuations, and difficulty in fluidization. Comparative Application Example 2 Large pressure drop, severe aggregation Application Example 5 The bed expansion effect was slightly poor, and a minor dead zone appeared. Application Example 6 The bed expansion effect was slightly poor, and some particles were retained at the edges. Application Example 7 Fluidization hysteresis, low expansion rate Application Example 8 Apparent fluidization, but large pressure drop fluctuations. Application Example 9 It easily forms agglomeration channels and gullies. Application Example 10 Fluidization Unstable

[0185] As shown in Table 1, Application Examples 1-4 of the present invention demonstrate that the multi-directional stirring mechanism with coaxial reversal creates an alternating fluid dynamic field, optimizing the fluidization state of particles and preventing particle deposition and bubble accumulation. Simultaneously, by setting multiple vents on the stirring paddle, precise gas distribution and bubble homogenization are achieved, reducing slugging and further enhancing the synergy between stirring and fluidization. This allows particles to be evenly distributed within the bed, resulting in more thorough gas-solid contact and significantly improving fluidization effect and reaction efficiency. Application Examples 5-10 show that changing the jet angle or eliminating the gradual gas supply design significantly reduces the fluidization state. Comparative Examples 1-2 show that removing key designs (such as reverse stirring and stirring gas supply) leads to large pressure drop fluctuations, small bed expansion, and near-complete fluidization failure or severe particle agglomeration.

[0186] The preferred embodiments of the present invention have been described in detail above. However, the present invention is not limited to the specific details in the above embodiments. Within the scope of the technical concept of the present invention, various simple modifications can be made to the technical solution of the present invention, and these simple modifications all fall within the protection scope of the present invention.

[0187] It should also be noted that the various specific technical features described in the above specific embodiments can be combined in any suitable manner without contradiction. In order to avoid unnecessary repetition, the present invention will not describe the various possible combinations separately.

[0188] Furthermore, various different embodiments of the present invention can be combined in any way, as long as they do not violate the spirit of the present invention, they should also be regarded as the content disclosed by the present invention.

Claims

1. A coaxial reverse-rotation synergistic fluidized bed device for C-type particles, characterized in that, The coaxial reversing synergistic fluidized bed device includes: Fluidization chamber, and a stirring unit disposed within the fluidized bed body of the fluidization chamber; The stirring unit includes: a first stirring blade and a second stirring blade that rotate in opposite directions on the same axis. The first agitator blade is provided with at least one first air inlet hole, and / or the second agitator blade is provided with at least one second air inlet hole.

2. The coaxial reverse-rotating synergistic fluidized bed device as described in claim 1, characterized in that, The first impeller includes one or a combination of at least two of the following: a flat blade impeller, a folding blade impeller, a curved blade impeller, an anchor impeller, a frame impeller, a ribbon impeller, or a screw impeller. Preferably, the second impeller includes one or a combination of at least two of the following: a flat-blade impeller, a folding-blade impeller, a curved-blade impeller, an anchor impeller, a frame impeller, a ribbon impeller, or a screw impeller.

3. The coaxial reverse-rotating synergistic fluidized bed device as described in claim 1 or 2, characterized in that, The spacing between adjacent first air inlets gradually decreases in the direction away from the center of the fluidization chamber; Preferably, the spacing between adjacent second air inlets gradually decreases in the direction away from the center of the fluidization chamber.

4. The coaxial reverse-rotating synergistic fluidized bed device as described in any one of claims 1-3, characterized in that, The angle between the gas injection direction of the first air inlet and the particle trajectory is 30-45°. Preferably, the angle between the gas injection direction of the second air inlet and the particle trajectory is 30-45°.

5. The coaxial reverse-rotating synergistic fluidized bed device as described in any one of claims 1-4, characterized in that, The diameter of the first air inlet is 0.5-2.5 mm; Preferably, the diameter of the second air inlet is 0.5-2.5 mm.

6. A fluidization method for C-type particles, characterized in that, The fluidization method includes: Type C particles and gas are fed into the fluidization chamber while the first and second stirring are performed simultaneously. The first and second stirrs rotate in opposite directions and their axes of rotation are on the same straight line. Gas is supplied to the blades of the first stirring paddle through the first air inlet, and / or gas is supplied to the blades of the second stirring paddle through the second air inlet.

7. The fluidization method as described in claim 6, characterized in that, The stirring rate of the first stirrer is 20-100 r / min; Preferably, the angle between the injection direction of the gas introduced through the first air inlet during the first stirring and the trajectory of the particles is 30-45°.

8. The fluidization method as described in claim 6 or 7, characterized in that, The stirring rate of the second stirrer is 15-90 r / min; Preferably, the angle between the injection direction of the gas introduced through the second air inlet during the second stirring and the trajectory of the particles is 30-45°.

9. The fluidization method according to any one of claims 6-8, characterized in that, In the first stirring process, the gas velocity fed into the first air inlet is 0.01-0.6 m / s; Preferably, the pressure of the gas fed into the first air inlet during the first stirring is 0.01-0.05 MPa.

10. The fluidization method according to any one of claims 6-9, characterized in that, In the second stirring process, the gas velocity fed into the second air inlet is 0.01-0.2 m / s; Preferably, the pressure of the gas fed into the second air inlet during the second stirring is 0.02-0.03 MPa.

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