A flow control device for a reactor

Abstract

The present invention belongs to the technical field of reactors, and discloses a reactor flow control device, including a baffle, a guide tube and an agitator; the baffle is a triangular prism-shaped angular baffle; the number of baffles is at least one, and the baffle is evenly arranged vertically on the inner wall of the reactor; the angle γ of the baffle facing the middle of the reactor is 30° to 90°; the guide tube is vertically suspended and arranged in the middle of the reactor, and the guide tube is connected to the inner wall of the reactor through a connecting rod; the agitator is vertically located in the guide tube, and the bottom end of the agitator extends out of the guide tube. Because the baffle is a triangular prism-shaped angular baffle, the circumferential flow of the material in the reactor is suppressed, and the vertical collision speed of the frontal surface is reduced, and the kinetic energy loss of the material is reduced; and because γ is 30° to 90°, the viscous resistance of the baffle to the frontal material is reduced, thereby reducing the possibility of reverse vortex formation on the back surface of the baffle, and the axial circulation of the material is further strengthened in combination with the axial flow agitator and the guide tube, thereby improving the material mixing effect.

Description

Technical Field

[0001] The invention belongs to the technical field of reactors, and in particular relates to a flow control device for a reactor. Background Art

[0002] In chemical production, stirring is an important process that is widely used in material mixing, dispersion, extraction and crystallization. In current precipitation crystallization reactors, anchor, paddle and folding blade turbine agitators are widely used. The axial flow generated during the stirring process can promote the mixing and reaction of suspended materials, but the circumferential flow (circumferential flow) generated during the stirring process affects the mixing degree of the materials. In order to weaken the circumferential flow during the stirring process, baffles are usually set on the inner wall of the reactor. The baffles can inhibit the circumferential flow, that is, the circumferential flow. However, the baffles currently used have a large load and high energy consumption, and the materials inside the reactor will form a reverse vortex on the back surface of the baffle after hitting the upstream surface of the baffle. This phenomenon is not conducive to material mixing and crystallization reaction. Summary of the invention

[0003] In view of this, the present invention provides a reactor flow control device, which can suppress the circumferential flow of materials in the reactor, eliminate the reverse vortex of the baffle, reduce the loss of kinetic energy of the materials, and promote uniform mixing of the materials.

[0004] In order to achieve the above-mentioned purpose, the following provides a reactor flow control device, which is used in the reactor, including a baffle, a guide tube and an agitator; the baffle is a triangular prism-shaped angular baffle; the number of baffles is at least one, and the baffle is vertically arranged on the inner wall of the reactor; the angle γ of the baffle toward the middle of the reactor is 30° to 90°; the guide tube is vertically suspended and arranged in the middle of the reactor, and the guide tube is connected to the inner wall of the reactor through a connecting rod; the agitator is vertically located in the guide tube, and the bottom end of the agitator extends out of the guide tube.

[0005] Preferably, the angle α between the back flow surface of the baffle and the inner diameter of the reactor is 20° to 60°.

[0006] Preferably, the angle β between the flow-facing surface of the baffle and the inner diameter of the reactor is 10° to 30°.

[0007] Preferably, the distance L between one end of the baffle plate adjacent to the inner wall of the reactor and the angle toward the middle of the reactor satisfies: 1 / 20×r≤L≤3 / 10×r, wherein r is the inner diameter of the reactor.

[0008] Preferably, the height H' of the guide tube satisfies: 0.3h≤H'≤0.6h, wherein h is the height of the reactor.

[0009] Preferably, the agitator comprises a stirring shaft and a stirring paddle; the stirring paddles are arranged on the stirring shaft at intervals, and the stirring paddles are located outside the guide tube.

[0010] Preferably, the stirring paddle includes a blade, and a stirring diameter φ' of the blade satisfies: 0.3r≤φ'≤0.5r, wherein r is the inner diameter of the reactor.

[0011] Preferably, the diameter φ of the guide tube satisfies: 0.4r≤φ≤0.7r, and φ≥φ', wherein r is the inner diameter of the reactor, and φ' is the stirring diameter of the blade.

[0012] Preferably, the distance H'' between the bottom end of the guide tube and the stirring paddle closest to the guide tube satisfies: 0.1r''<H''<0.3r'', wherein r'' is the stirring diameter of the stirring paddle.

[0013] Preferably, the number of stirring paddles is at least one, and one stirring paddle is located at the bottom end of the stirring shaft. Compared with the prior art, the beneficial effects of the present invention using the above scheme are:

[0014] The agitator is used to stir the materials in the reactor, and the guide tube is used to guide the flow. During the stirring process, the materials will inevitably collide with the baffle arranged on the inner wall of the reactor. The baffle of the present invention is a triangular prism-shaped angular baffle, which can suppress the circumferential flow of the materials to a large extent. In addition, because the angle γ of the baffle of the present invention toward the middle of the reactor chamber is 30°~90°, the viscous resistance of the baffle to the oncoming material is reduced, thereby reducing the possibility of reverse vortex formation on the back flow surface of the baffle. The combination of the axial flow agitator and the guide tube further strengthens the axial circulation of the material and improves the material mixing rate. BRIEF DESCRIPTION OF THE DRAWINGS

[0015] Figure 1 It is a structural schematic diagram of a reaction kettle provided by an embodiment of the present invention;

[0016] Figure 2 yes Figure 1 Schematic diagram of the structure of the AA section;

[0017] Figure 3 yes Figure 1 Schematic diagram of top view;

[0018] In the figure: 1, reactor; 2, baffle; 3, guide tube; 4, agitator; 41, agitator shaft; 42, agitator paddle. DETAILED DESCRIPTION

[0019] In order to make the purpose, technical solution and advantages of the present invention more clearly understood, the present invention is further described in detail below in conjunction with specific embodiments. It should be understood that the specific embodiments described herein are only used to explain the present invention and are not used to limit the present invention.

[0020] This embodiment provides a reaction kettle, such as Figure 1-Figure 3 As shown, it is used in a reactor 1, and includes a baffle 2, a guide tube 3 and an agitator 4; the baffle 2 is a triangular prism-shaped angular baffle; the number of the baffles 2 is at least one, and the baffle 2 is vertically arranged on the inner wall of the reactor 1; the angle γ of the baffle 2 facing the middle of the chamber of the reactor 1 is 30° to 90°; the guide tube 3 is vertically suspended and arranged in the middle of the reactor 1, and the guide tube 3 is connected to the inner wall of the reactor 1 through a connecting rod; the agitator 4 is vertically located in the guide tube 3, and the bottom end of the agitator 4 extends out of the guide tube 3.

[0021] The agitator 4 of this embodiment is perpendicular to the bottom of the reactor 1, so the agitator 4 is an axial flow agitator, that is, the material is made to flow axially during stirring. The agitator 4 is used to axially stir the material in the reactor, and the guide tube 3 is used for diversion. During the stirring process, the material will inevitably collide with the baffle 2 set on the inner wall of the reactor 1. The baffle 2 of this embodiment is a triangular prism-shaped angular baffle, which can not only further increase the shear force of the material flowing through it, but also inhibit the circumferential flow of the material to a large extent; in addition, because the angle γ of the baffle 2 of the baffle 2 facing the middle of the chamber of the reactor 1 in this embodiment is 30°~90°, this reduces the viscous resistance of the baffle to the incoming material, thereby reducing the possibility of reverse vortex formation on the back surface of the baffle, and the combination of the axial flow agitator and the guide tube further strengthens the axial circulation of the material and improves the material mixing effect.

[0022] In this embodiment, the baffle 2 is a hollow structure, which is to reduce the weight of the reactor on the one hand, and save raw materials and reduce costs on the other hand. In addition, in order to prevent materials from entering the hollow baffle 2, the bottom end of the baffle 2 is fixedly connected to the bottom surface of the chamber of the reactor 1, and the upper end of the baffle 2 is closed.

[0023] In this embodiment, the bottom surface and the top surface of the baffle 2 may be parallel to each other, and the number of the baffles 2 is 2 to 6, preferably 4.

[0024] Because the baffle 2 is a triangular prism structure, one side surface thereof is connected to the inner wall of the reactor 1, and one of the other two side surfaces is a back-flow surface and the other is a front-flow surface.

[0025] The upstream surface is the side opposite to the circumferential flow direction of the material, and the side opposite to the circumferential flow direction of the material is the downstream surface. Therefore, the upstream surface and the downstream surface are related to the circumferential flow direction of the material.

[0026] For example, when the circumferential flow direction of the logistics is clockwise, the upstream surface is side A, and the downstream surface is side B; when the circumferential flow direction of the material is counterclockwise, the upstream surface is side B, and the downstream surface is side A.

[0027] In a specific embodiment, the angle α between the back flow surface of the baffle 2 and the inner diameter of the reactor 1 is 20° to 60°. On the premise of ensuring that the baffle 2 can increase the shear force on the material flowing through it, the contact area between the back flow surface of the baffle 2 and the material flowing through the baffle 2 is increased, thereby effectively avoiding the occurrence of reverse vortex.

[0028] For example, if α is less than 20°, the reverse vortex suppression effect is small or even has no effect; and if α is greater than 60°, the reverse vortex suppression effect will not increase significantly with the increase of α, and the material used will increase, thereby increasing the cost.

[0029] In a specific embodiment, the angle β between the frontal surface of the baffle 2 and the inner diameter of the reactor 1 is 10° to 30°; this reduces the kinetic energy loss of the material by changing the impact angle with the material, and increases the shearing effect of the baffle 2 on the material flowing through it, thereby more effectively suppressing the circumferential flow of the material.

[0030] For example, if β is greater than 30°, not only will materials be wasted and costs increased, but most importantly, the effect of the baffle 2 in suppressing the circumferential flow of materials will be reduced.

[0031] In this embodiment, γ=α+β.

[0032] In a specific embodiment, the horizontal distance L between one end of the baffle plate 2 adjacent to the inner wall of the reactor 1 and the angle of the same baffle plate 2 toward the middle of the reactor 1 satisfies: 1 / 20×r≤L≤3 / 10×r, where r is the inner diameter of the reactor 1.

[0033] If L>3 / 10×r, although it can better suppress the circumferential flow of materials, it also provides greater resistance to the flow of materials. Then the agitator used to stir the materials needs to provide greater force for the materials, which will result in higher energy consumption during the material stirring process.

[0034] If L < 1 / 20 × r, the effect of suppressing the circumferential flow of the material will be poor. In this embodiment, L is preferably 1 / 10 × r.

[0035] In a specific embodiment, the connecting rod used to connect the guide tube 3 to the inner wall of the reactor 1 can be a cross welding frame, and the cross welding frame and the guide tube 3 can be welded or threadedly connected by nuts and screws. The cross welding frame and the inner wall of the reactor 1 can be welded or threadedly connected by nuts and screws.

[0036] When the material is stirred in the reactor 1, the existence of the guide tube 3 can further enhance the axial flow circulation effect of the material and reduce the kinetic energy loss of the circumferentially flowing material when it hits the baffle.

[0037] In a specific embodiment, the height H' of the guide tube 3 satisfies: 0.3h≤H'≤0.6h, where h is the height of the reactor 1, in order to ensure that the axial flow content of the material is better increased.

[0038] In a specific embodiment, the stirrer 4 is used to stir the materials in the reactor 1. The stirrer 4 can be connected to the motor through a coupling, or can be driven manually.

[0039] In a specific embodiment, the stirrer 4 includes a stirring shaft 41 and a stirring paddle 42 ; the stirring paddle 42 is arranged on the stirring shaft 41 at intervals, and the stirring paddle 42 is located outside the guide tube 3 .

[0040] The blades of the stirring paddle 42 of the present embodiment may be one of axial flow stirring paddles such as a folding blade type, a propulsion type, and a turbine type.

[0041] The stirring shaft 41 can be connected to the motor via a coupling.

[0042] In a specific embodiment, the stirring paddle 42 includes a blade, and a stirring diameter φ' of the blade satisfies: 0.3r≤φ'≤0.5r, wherein r is the inner diameter of the reactor 1, which can achieve a better stirring effect.

[0043] In this specific embodiment, the guide tube 3 is located directly above the stirring paddle 42, and the distance H'' between the bottom end of the guide tube 3 and the stirring paddle 42 closest to the guide tube 3 satisfies: 0.1r''<H''<0.3r'', where r'' is the stirring diameter of the stirring paddle 42. In this way, the guide tube 3 can be ensured to have the function of guiding flow, that is, the amount of raw materials used in the manufacture of the guide tube 3 can be reduced without affecting the guiding effect of the guide tube 3, thereby reducing the cost.

[0044] In a specific embodiment, the diameter φ of the guide tube 3 satisfies: 0.4r≤φ≤0.7r, and φ≥φ', wherein r is the inner diameter of the reactor 1, and φ' is the stirring diameter of the blade.

[0045] Preferably, φ=0.7r, φ'=0.4r, and the guide tube 3 can be a cylindrical structure or a conical structure. For example, when the guide tube 3 is a conical structure, the diameter of its upper end is greater than the diameter of its lower end, for example, the upper end diameter of the conical guide tube 3 is φ=0.7r, and the lower end diameter is φ=0.5r, which can reduce the material used in the production of the guide tube and reduce the production cost.

[0046] In a specific embodiment, the number of the stirring paddle 42 is at least one, and one of the stirring paddles 42 is located at the bottom end of the stirring shaft 41, so as to avoid the formation of vortices in the middle of the material and destroy the circumferential flow of the material.

[0047] When the number of stirring paddles 42 is greater than one, the distance H''' between each two stirring paddles 42 satisfies: 0.1r''<H'''<0.2r'', where r'' is the stirring diameter of the stirring paddle 42, which effectively avoids the circumferential flow of the material. A keyway is provided on the stirring shaft 41, and the stirring paddle 42 is detachably connected to the stirring shaft 41 through the keyway.

[0048] Working process:

[0049] The stirring shaft 41 rotates in the guide tube 3, driving the stirring paddle 42 to rotate directly below the guide tube 3, thereby realizing axial stirring of the material. Due to the presence of the guide tube 3, the axial circulation of the material can be further enhanced. In addition, because the inner wall of the reactor 1 is also provided with a triangular prism-shaped angular baffle 2, and the angle β between the frontal surface of the baffle 2 and the inner diameter of the reactor 1 is 10°~30°, the circumferential flow of the material can be suppressed, and the kinetic energy loss caused by the material hitting the baffle can be reduced. At the same time, the angle α between the back surface of the baffle 2 and the inner diameter of the reactor 1 is 20°~60°, which can eliminate the phenomenon of reverse vortex of the baffle, further enhance the axial flow circulation effect, reduce the kinetic energy lost when the circumferential flow of the material hits the baffle, and at the same time, the axial flow agitator and the guide tube are combined to further enhance the axial circulation of the material and improve the material mixing effect. The reactor flow control device of this embodiment is reasonably designed and has strong versatility.

[0050] The above is only a preferred specific embodiment of the present invention, but the protection scope of the present invention is not limited thereto. Any changes or substitutions that can be easily thought of by a person skilled in the art within the technical scope disclosed by the present invention should be included in the protection scope of the present invention. Therefore, the protection scope of the present invention should be based on the protection scope of the claims.

Claims

1. A reactor flow control device, used in a reactor (1), characterized in that: The invention comprises a baffle (2), a flow guide tube (3) and an agitator (4); the baffle (2) is a triangular prism-shaped angular baffle; the number of the baffle (2) is at least one, and the baffle (2) is vertically arranged on the inner side wall of the reactor (1); the angle γ of the baffle (2) facing the middle of the reactor (1) is 30° to 90°; the flow guide tube (3) is vertically suspended and arranged in the middle of the reactor (1), and the flow guide tube (3) is connected to the inner side wall of the reactor (1) through a connecting rod; the agitator (4) is vertically located in the flow guide tube (3), and the bottom end of the agitator (4) protrudes from the flow guide tube (3); The angle α between the back flow surface of the baffle (2) and the inner diameter of the reactor (1) is 20° to 60°; The angle β between the flow-facing surface of the baffle (2) and the inner diameter of the reactor (1) is 10° to 30°; The distance L between one end of the baffle plate (2) adjacent to the inner wall of the reactor (1) and the angle toward the middle of the reactor (1) satisfies: 1 / 20×r≤L≤3 / 10×r, where r is the inner diameter of the reactor (1).

2. The reactor flow control device according to claim 1, characterized in that: The height H' of the guide tube (3) satisfies: 0.3h≤H'≤0.6h, where h is the height of the reaction kettle (1).

3. The reactor flow control device according to claim 1, characterized in that: The stirrer (4) comprises a stirring shaft (41) and a stirring paddle (42); the stirring shaft (41) is provided with stirring paddles (42) at intervals, and the stirring paddles (42) are located outside the guide tube (3).

4. The reactor flow control device according to claim 3, characterized in that: The stirring paddle (42) comprises a blade, and a stirring diameter φ' of the blade satisfies: 0.3r≤φ'≤0.5r, wherein r is the inner diameter of the reaction kettle (1).

5. The reactor flow control device according to claim 4, characterized in that: The diameter φ of the guide tube (3) satisfies: 0.4r≤φ≤0.7r, and φ≥φ', wherein r is the inner diameter of the reaction kettle (1), and φ' is the stirring diameter of the blade.

6. The reactor flow control device according to claim 4, characterized in that: The distance H'' between the bottom end of the guide tube (3) and the stirring paddle (42) closest to the guide tube (3) satisfies: 0.1r''<H''<0.3r'', wherein r'' is the stirring diameter of the stirring paddle (42).

7. The reactor flow control device according to claim 4, characterized in that: The number of the stirring paddle (42) is at least one, and one of the stirring paddles (42) is located at the bottom end of the stirring shaft (41).

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