Rotating disc extraction tower

Abstract

The utility model relates to a turntable extraction tower, including tower body, separator plate, stirring shaft, stirrer, the separator plate divides the tower body into a plurality of mixing area in the height direction of tower body, stirring shaft extends along the height direction of tower body and passes through the plurality of mixing area, stirrer is connected on stirring shaft and located in the mixing area, the separator plate is provided with solid phase communication port, and the separator plate is provided with solid phase communication port. The solid-phase communication port is communicated with the stirrer, so that a dispersed phase in the upper-layer mixing area enters the lower-layer mixing area through the solid-phase communication port and the stirrer; a liquid-phase communicating pipe is connected to the partition plate, so that a continuous phase in the lower-layer mixing area enters the upper-layer mixing area through the liquid-phase communicating pipe. A continuous phase from bottom to top and a dispersed phase from top to bottom are subjected to countercurrent washing, in the whole countercurrent process, a solid phase channel and a liquid phase channel are well separated, backmixing is greatly reduced, the tower efficiency is improved, and the device can be used for washing the continuous phase and the dispersed phase and is also suitable for liquid-liquid extraction.

Description

Technical Field

[0001] This utility model relates to the field of chemical separation equipment technology, specifically to a rotary extraction tower. Background Technology

[0002] Rotary disc extractors are liquid-liquid extraction devices widely used in chemical, petroleum, and environmental protection fields. They are popular due to their simple structure, convenient operation, large throughput, and wide applicability.

[0003] The main factors affecting mass transfer in rotary disc extraction columns are the dispersed phase retention fraction and axial backmixing. During industrial scale-up, 75%-90% of the column height is used to compensate for axial backmixing, resulting in a reduction in the mass transfer driving force. Axial backmixing within the continuous phase in the extraction column is considered to be caused by one or more of the following factors: 1) eddy diffusion due to fluid and fluid agitation; 2) radial velocity distribution; 3) entrainment of the continuous phase within the dispersed phase droplet wake; and 4) eddies caused by the flow of dispersed phase droplets.

[0004] Traditional rotary disc extraction columns suffer from significant backmixing and low column efficiency. For an industrial rotary disc extraction column, axial mixing has a substantial impact, and inter-stage backmixing increases significantly with increasing column diameter, reducing the height of the mass transfer unit (H). OXP This increase necessitates the use of taller towers to meet separation requirements. For example... Figure 1 In the conventional rotary disc extraction column shown, the continuous phase is drawn in from the middle when the rotary disc extraction column is working. The dispersed phase at the partition is affected by the suction force of the turbine in zone 2 above the column plate and the downward suction force of the turbine in zone 1 below the column plate. This increases the resistance to the rise of the dispersed phase in zone 1, aggravates backmixing, and affects the column efficiency.

[0005] Currently, improvements to extraction equipment mainly focus on increasing the mass transfer area and enhancing fluid flow within the tower. For example, patent CN204502460U discloses an improved rotary extraction device that uses multiple annular baffles within the extraction tower to create multiple extraction chambers, reducing interstage backmixing and thus improving extraction efficiency. Patent CN216537003U discloses a rotary extraction tower with multiple layers of fixed baffles within the tower. Each pair of adjacent baffles forms a stirring space with the tower wall. The light and heavy phases flow through several stirring spaces, and the raw material undergoes multiple dispersion and polymerization processes, resulting in mass transfer and improved extraction efficiency. However, in the above patents, the baffles all have several circular holes, causing the light and heavy phases to flow within the same channels, leading to significant backmixing of the fluid on both sides of the baffles and low extraction efficiency. Summary of the Invention

[0006] The purpose of this invention is to provide a rotary extraction tower that separates the solid and liquid phases, thereby effectively solving the problem of backmixing between stages and improving extraction efficiency.

[0007] To achieve the above objectives, the technical solution adopted by this utility model is as follows:

[0008] A rotary extraction column includes a column body, a partition plate, a stirring shaft, and a stirrer. The partition plate divides the column body into multiple mixing zones along its height. The stirring shaft extends along the height of the column body and penetrates through the multiple mixing zones. The stirrer is connected to the stirring shaft and located within each mixing zone. A fixed connection port is provided on the partition plate, which communicates with the stirrer, allowing the dispersed phase in the upper mixing zone to enter the lower mixing zone through the fixed connection port and the stirrer. A liquid connection pipe is connected to the partition plate, allowing the continuous phase in the lower mixing zone to enter the upper mixing zone through the liquid connection pipe.

[0009] Preferably, in the above technical solution, the stirrer includes a lower plate, an upper plate, and blades. The lower plate is connected to the stirring shaft, and the upper plate has a solid phase receiving port opposite to the solid phase communication port. The blades include inner blades connected between the lower plate and the upper plate. Multiple inner blades are provided, and a solid phase channel is formed between two adjacent inner blades. The solid phase channel connects the solid phase receiving port and the mixing area.

[0010] More preferably, the blades further include upper blades and / or lower blades, the upper blades being connected to the upper surface of the upper plate and the lower blades being connected to the lower surface of the lower plate. When the stirrer rotates, the dispersed phase in the continuous phase is washed or extracted by the stirring of the upper and lower blades.

[0011] More preferably, the blades extend from the center of the upper plate or / and lower plate outwards.

[0012] More preferably, the blades are evenly distributed on the lower plate, the upper plate, and between the upper and lower plates.

[0013] More preferably, the stirring shaft passes through the solid connection port and the solid phase receiving port, so that the stirring does not affect the entry of the dispersed phase from the solid connection port into the solid phase receiving port when the stirrer rotates.

[0014] More preferably, the stirring shaft, the solid connection port, and the solid phase receiving port are coaxially arranged.

[0015] More preferably, the solid connection port is connected to a first tube extending toward the solid phase receiving port; and / or the solid phase receiving port is connected to a second tube extending toward the solid connection port, so as to better receive the dispersed phase.

[0016] Preferably, in the above technical solution, the liquid interconnecting pipe includes a straight pipe section and an elbow section. The straight pipe section extends vertically upward, and its lower end is connected to the partition plate. One end of the elbow section is connected to the upper end of the straight pipe section. The elbow section can effectively prevent the dispersed phase thrown out by the agitator from entering the liquid interconnecting pipe, thereby achieving the purpose of separating the flow of the dispersed phase and the continuous phase.

[0017] More preferably, the bending angle of the elbow section is 90°-200°, such as 90°, 120°, 150°, 180°, 200°, etc., with 180° being the optimal angle.

[0018] Preferably, the liquid connecting pipes on the upper and lower partitions are staggered, with an angle of 90°-200°, such as 90°, 120°, 150°, 180°, 200°, etc., with 180° being the optimal angle.

[0019] Preferably, in the above technical solution, the flow rate of the liquid connecting pipe is 0.01 to 0.2 m / s.

[0020] Preferably, in the above technical solution, the diameter of the tower body is 50-4000 mm.

[0021] Preferably, in the above technical solution, the diameter of the agitator is 1 / 3 to 2 / 3 times the diameter of the tower body.

[0022] Preferably, in the above technical solution, the height of the stirrer is 1 / 10 to 1 / 5 of the stirrer diameter.

[0023] Preferably, in the above technical solution, the distance between the upper and lower partitions is 1 / 10 to 2 / 3 times the tower diameter.

[0024] Preferably, in the above technical solution, the diameter of the through-hole of the solid connection is 1 / 8 to 2 / 3 times the diameter of the stirrer.

[0025] Preferably, in the above technical solution, the tower body has an upper clarification section, a mixing section, and a lower clarification section, which are arranged sequentially from top to bottom. The upper clarification section is provided with a liquid phase outlet, the upper part of the mixing section is provided with a solid phase inlet, the lower part of the mixing section is provided with a liquid phase inlet, the mixing area is located in the mixing section between the solid phase inlet and the liquid phase inlet, and the lower clarification section is provided with a solid phase outlet.

[0026] Due to the application of the above technical solution, this utility model has the following advantages compared with the prior art:

[0027] In this invention, the continuous phase from bottom to top and the dispersed phase from top to bottom are washed in a countercurrent manner. During the entire countercurrent process, the solid phase channel and the liquid phase channel are well separated, which greatly reduces backmixing and improves the tower efficiency. It can be used for washing the continuous phase and the dispersed phase, as well as for liquid-liquid extraction. Attached Figure Description

[0028] Appendix Figure 1 This is a partial schematic diagram of a traditional rotary disc extraction column;

[0029] Appendix Figure 2 This is a front view schematic diagram of the rotary extraction tower of this utility model;

[0030] Appendix Figure 3 This is a partial schematic diagram of the mixing section of the rotary extraction tower of this utility model;

[0031] Appendix Figure 4 This is a front view schematic diagram of the stirrer of this utility model;

[0032] Appendix Figure 5 This is a top view of the stirrer of this utility model.

[0033] In the attached diagrams above:

[0034] 1. Tower body; 10. Upper clarification section; 100. Liquid phase outlet; 11. Mixing section; 110. Solid phase inlet; 111. Liquid phase inlet; 112. Mixing zone; 12. Lower clarification section; 120. Solid phase outlet; 13. Interface meter;

[0035] 2. Partition plate; 20. Fixed connection port; 200. First pipe body; 21. Liquid connection pipe; 210. Straight pipe section; 211. Elbow section;

[0036] 3. Stirring shaft; 30. Shaft sleeve;

[0037] 4. Stirrer; 40. Lower plate; 41. Upper plate; 410. Solid phase receiving port; 411. Second tube; 42. Inner blade; 420. Solid phase channel; 43. Upper blade; 44. Lower blade;

[0038] A, Zone 1; B, Zone 2. Detailed Implementation

[0039] The technical solution of this utility model will now be clearly and completely described with reference to the accompanying drawings. Obviously, the described embodiments are only some, not all, of the embodiments of this utility model. Based on the embodiments of this utility model, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of this utility model.

[0040] In the description of this utility model, it should be noted that the terms "center," "upper," "lower," "left," "right," "vertical," "horizontal," "inner," and "outer," etc., indicating the orientation or positional relationship, are based on the orientation or positional relationship shown in the accompanying drawings and are only for the convenience of describing this utility model and 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, and therefore should not be construed as a limitation of this utility model. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and should not be construed as indicating or implying relative importance.

[0041] like Figure 2 , Figure 3 The rotating disc extraction column shown includes a column body 1, a partition plate 2, a stirring shaft 3, and a stirrer 4. Wherein:

[0042] The tower body 1 has an upper clarification section 10, a mixing section 11, and a lower clarification section 12, arranged sequentially from top to bottom. The upper clarification section 10 is provided with a liquid phase outlet 100, the upper part of the mixing section 11 is provided with a solid phase inlet 110, the lower part of the mixing section 11 is provided with a liquid phase inlet 111, and the lower clarification section 12 is provided with a solid phase outlet 120. The diameter of the tower body 1 is 50–4000 mm. In this embodiment, the diameter of the tower body 1 (hereinafter referred to as the tower diameter) specifically refers to the inner diameter of the mixing section 11. Furthermore, the upper clarification section 10 and the lower clarification section 12 may be equipped with an interface meter 13.

[0043] The baffle 2 divides the mixing section 11 into multiple mixing zones 112 along the height of the tower body 1. The solid phase inlet 110 is located on the mixing section 11 of the uppermost mixing zone 112, and the liquid phase inlet 111 is located on the mixing section 11 of the lowermost mixing zone 112. The stirring shaft 3 extends along the height of the tower body 1 and passes through multiple mixing zones 112. In the figure, the stirring shaft 3 is coaxially arranged with the tower body 1. The stirrer 4 is connected to the stirring shaft 3 and located within the mixing zone 112. That is, each mixing zone 112 has a stirrer 4.

[0044] In this embodiment, a solid connection port 20 is provided on the partition 2, and a liquid connection pipe 21 is connected above the partition 2. The solid connection port 20 is connected to the stirrer 4, allowing the dispersed phase in the upper mixing region 112 to enter the stirrer 4 through the solid connection port 20 and then enter the lower mixing region 112 through the stirrer 4. The liquid connection pipe 21 allows the continuous phase in the lower mixing region 112 to enter the upper mixing region 112. Thus, the dispersed phase enters the mixing region 112 through the solid connection port 20 and the stirrer 4, while the continuous phase enters the mixing region 112 through the liquid connection pipe 21. Mass transfer occurs between the two phases in the mixing region 112, and then the dispersed phase enters the lower mixing region 112, and the continuous phase enters the upper mixing region 112, effectively preventing backmixing.

[0045] Specifically:

[0046] The partition plate 2 can be connected to the tower body 1 by fixing holes or welding. The distance between the upper and lower partition plates 2 is 1 / 10 to 2 / 3 times the tower diameter. A hole is formed in the center of the partition plate 2, which serves two purposes: firstly, it allows the stirring shaft 3 to pass through, and secondly, it forms a fixed connection port 20. In this embodiment, the fixed connection port 20 is coaxially arranged with the stirring shaft 3. A first tube 200 of the same diameter is connected to the fixed connection port 20 to collect the settled dispersed phase and feed it into the stirrer 4. The diameter of the fixed connection port 20 is 1 / 8 to 2 / 3 times the stirrer diameter.

[0047] The liquid-connecting pipe 21 can be connected above or below the partition 2; in this embodiment, it is connected above the partition 2. The liquid-connecting pipe 21 includes a straight pipe section 210 and an elbow section 211. The straight pipe section 210 extends vertically upwards, and its lower end connects to the partition 2. One end of the elbow section 211 connects to the upper end of the straight pipe section 210. The elbow section 211 effectively prevents the dispersed phase ejected by the stirrer 4 from entering the liquid-connecting pipe 21, achieving the purpose of separating the dispersed phase from the continuous phase. The liquid-connecting pipes 21 on the upper and lower partitions 2 are staggered by an angle of 90°-200°, as shown in the figure at 180°; the bending angle of the elbow section 211 is also 90°-200°, as shown in the figure at 180°. The diameter of the liquid-connecting pipe 21 is determined according to the continuous phase flow rate, typically 0.01–0.2 m / s.

[0048] The agitator 4 can be a semi-closed turbine agitator, which serves to receive the dispersed phase on one hand and throw the dispersed phase out to the mixing zone 112 on the other. The diameter of the agitator 4 is 1 / 3 to 2 / 3 of the tower diameter; the height of the agitator 4 is 1 / 10 to 1 / 5 of the agitator diameter.

[0049] like Figure 4 , Figure 5As shown: In this embodiment, the stirrer 4 includes a lower plate 40, an upper plate 41, and blades. Specifically:

[0050] Both the lower plate 40 and the upper plate 41 are circular plates. The lower plate 40 is connected to the stirring shaft 3. Specifically, a bushing 30 can be installed on the stirring shaft 3, and the lower plate 40 is connected to the stirring shaft 3 through the bushing 30. The upper plate 41 has a solid phase receiving port 410, which is opposite to the solid connection port 20. The stirring shaft 3 also passes through the solid phase receiving port 410, and the stirring shaft 3 and the solid phase receiving port 410 are coaxially arranged. In this embodiment, a second tube 411 is connected to the solid phase receiving port 410. The first tube 200 of the solid connection port 20 and the second tube 411 of the solid phase receiving port 410 are opposite to each other. In the figure, the first tube 200 extends slightly into the second tube 411 to better receive the dispersed phase. There is no connection between the first tube 200 and the second tube 411. When the stirrer 4 rotates, it does not affect the dispersed phase from the solid phase inlet 20 through the first tube 200, the second tube 411, and the solid phase receiving inlet 410 into the stirrer 4.

[0051] The blades include inner blades 42, upper blades 43, and lower blades 44. The inner blades 42 are connected between the lower plate 40 and the upper plate 41. Multiple inner blades 42 are provided, and a solid-phase channel 420 is formed between adjacent inner blades 42, connecting the solid-phase receiving port 410 and the mixing zone 112. The upper blades 43 are connected to the upper surface of the upper plate 41, and the lower blades 44 are connected to the lower surface of the lower plate 40. Thus, when the stirrer 4 rotates, the dispersed phase enters the solid-phase channel 420 through the solid-phase receiving port 410, and is then ejected into the mixing zone 112. The stirring action of the upper blades 43 and lower blades 44 further agitates the dispersed phase within the continuous phase, achieving washing or extraction. In this embodiment, the multiple inner blades 42, upper blades 43, and lower blades 44 are evenly distributed and extend outwards from the center of the lower plate 40 / upper plate 41, i.e., distributed along the diameter of the circular lower plate 40 / upper plate 41. The inner blade 42, upper blade 43, and lower blade 44 can be straight blades, oblique blades, or arc blades depending on the size of the stirrer 4 and the application. The number of blades is designed to be 3 or more. In the figure, there are 6 inner blades 42 and 6 upper blades 43, and the inner blades 42 and 43 are also staggered.

[0052] The working principle of this embodiment is described in detail below:

[0053] Appendix Figure 3 In the middle: the dots represent solid particles, and the remaining space is filled with liquid.

[0054] Within the mixing zone 112, solid particles are the dispersed phase (assuming a heavy phase) and move downwards, while the liquid is the continuous phase and moves upwards. Solid particles enter the mixing zone 112 through the solid phase inlet 110 and are dispersed within the mixing zone 112 by the action of the upper blade 43 and lower blade 44 of the rotating stirrer 4. Under gravity, the solid particles sink to the partition 2 and enter the first pipe 200 connected to the partition 2, forming a solid particle enrichment zone. Solid particles flow from the enrichment zone through the solid phase receiving port 410 into the solid phase channel 420 within the stirrer 4. Under the centrifugal force of the rotating stirrer 4, the solid particles are thrown out and continuously dispersed and mixed by the upper blade 43 and lower blade 44, thus washing the solid particles. Liquid enters the mixing zone 112 through the liquid phase inlet 111 and flows into the upper mixing zone 112 through the liquid connection pipe 21, where it washes the solid particles under the rotation of the stirrer 4. In this way, the liquid flows from bottom to top and washes against the solid particles flowing from top to bottom in a countercurrent manner. The solid particles at the bottom are washed clean and discharged from the tower body 1 through the solid phase outlet 120, while the liquid at the top has the highest solute content and overflows from the tower body 1 through the liquid phase outlet 100. Throughout the countercurrent process, the solid phase channel and the liquid phase channel are well separated, greatly reducing backmixing and improving tower efficiency.

[0055] Example:

[0056] The rotating disc extraction tower of this embodiment was used for the extraction of polyphenylene sulfide (PPS) slurry. The same PPS slurry was used in the embodiment and the comparative example.

[0057] In each mixing zone, PPS slurry and acetone are mixed while being stirred. The PPS particles in the slurry are washed in a countercurrent contact with acetone at a certain flow rate. The N-methyl-2-pyridinyl ketone (NMP) content in the inlet slurry is C0, and the NMP content at the bottom of the tower is C1. The washing efficiency β = 1 - C1 / C0.

[0058] Example 1:

[0059] In this embodiment, the rotary extraction column has a column diameter of 300 mm, a bushing outer diameter of 45 mm, a stirrer speed of 60 r / min, and five mixing zones inside the column. The diameter of the through-hole at the connection between the baffle and the stirrer is 80 mm, and the diameter of the opening at the connection between the baffle and the liquid-liquid connecting pipe is 60 mm. The two-phase flow area ratio is approximately 8.86% ((80^2-45^2+60^2) / 300^2*100%=8.86%).

[0060] Acetone washing solution was fed into the rotary extractor at a flow rate of 200 L / h from the liquid phase inlet, filling the entire rotary extractor. Then, the PPS slurry to be washed was fed into the rotary extractor at a flow rate of 80 L / h from the solid phase inlet. The concentration of solvent NMP in the PPS particles before washing was 3%, and the concentration of solvent NMP in the PPS particles after washing was 0.01%. The washing efficiency was calculated to be 99.7%.

[0061] Comparative Example 1:

[0062] Using the rotary disc extraction tower and the first type of partition structure disclosed in CN216537003U, the diameter of the rotary disc extraction tower is 300 mm, the stirring speed is 60 r / min, 5 mixing zones are set inside the tower, the sieve aperture is 15 mm, there are 48 sieve holes, and the two-phase flow area ratio is 12% (15^2*48 / 300^2*100%=12%). The PPS slurry was washed under the same operating conditions as in Example 1. The concentration of solvent NMP in the PPS particles before washing was 3% (the same value as in Example 1), and the concentration of solvent NMP in the PPS particles after washing was 0.2%. The washing efficiency was calculated to be 93.3%.

[0063] Comparative Example 2:

[0064] Using the rotary disc extraction column and the second type of baffle structure disclosed in CN216537003U, the rotary disc extraction column has a column diameter of 300 mm, an agitator speed of 60 r / min, 5 mixing zones inside the column, an inner diameter of 160 mm for the ring plate, and a two-phase flow area ratio of 28.4% (160^2 / 300^2*100%=28.4%). The PPS slurry was washed under the same operating conditions as in Example 1. Before washing, the concentration of solvent NMP in the PPS particles was 3% (the same value as in Example 1), and after washing, the concentration of solvent NMP in the PPS particles was 0.5%. The washing efficiency was calculated to be 83.3%.

[0065] It is evident that the washing efficiency of the rotary extractor in this embodiment (99.7%) is higher than that of the rotary extractor using CN216537003U in Comparative Example 1 (93.3%), and far higher than that of the rotary extractor using CN216537003U in Comparative Example 2 (83.3%).

[0066] The above embodiments are only for illustrating the technical concept and features of this utility model, and are intended to enable those skilled in the art to understand the content of this utility model and implement it accordingly. They should not be construed as limiting the scope of protection of this utility model. All equivalent changes or modifications made in accordance with the spirit and essence of this utility model should be included within the scope of protection of this utility model.

Claims

1. A rotating disc extraction column, comprising a column body (1), a partition (2), a stirring shaft (3), and a stirrer (4), wherein the partition (2) divides the column body (1) into multiple mixing zones (112) along its height direction, the stirring shaft (3) extends along the height direction of the column body (1) and penetrates the multiple mixing zones (112), and the stirrer (4) is connected to the stirring shaft (3) and located within the mixing zones (112), characterized in that: The partition (2) is provided with a solid connection port (20), which is connected to the stirrer (4) so ​​that the dispersed phase in the upper mixing region (112) can enter the lower mixing region (112) through the stirrer (4) via the solid connection port (20); the partition (2) is connected with a liquid connection pipe (21) so that the continuous phase in the lower mixing region (112) can enter the upper mixing region (112) via the liquid connection pipe (21).

2. The rotating disc extraction tower according to claim 1, characterized in that: The stirrer (4) includes a lower plate (40), an upper plate (41), and blades. The lower plate (40) is connected to the stirring shaft (3). The upper plate (41) has a solid phase receiving port (410) which is opposite to the solid phase connecting port (20). The blades include inner blades (42), which are connected between the lower plate (40) and the upper plate (41). Multiple inner blades (42) are provided, and a solid phase channel (420) is formed between two adjacent inner blades (42). The solid phase channel (420) connects the solid phase receiving port (410) and the mixing area (112).

3. The rotating disc extraction tower according to claim 2, characterized in that: The blade also includes an upper blade (43) and / or a lower blade (44), the upper blade (43) being connected to the upper surface of the upper plate (41) and the lower blade (44) being connected to the lower surface of the lower plate (40).

4. The rotating disc extraction tower according to claim 2 or 3, characterized in that: The blades extend outwards from the center of the upper plate (41) or / lower plate (40); and / or The blades are evenly arranged on the upper plate (41) / lower plate (40).

5. The rotating disc extraction tower according to claim 2, characterized in that: The stirring shaft (3) passes through the solid connection port (20) and the solid phase receiving port (410); The stirring shaft (3), the solid connection port (20), and the solid phase receiving port (410) are coaxially arranged.

6. The rotating disc extraction tower according to claim 2, characterized in that: The solid connection port (20) is connected to a first tube (200) extending toward the solid phase receiving port (410); and / or the solid phase receiving port (410) is connected to a second tube (411) extending toward the solid connection port (20).

7. The rotating disc extraction column according to claim 1, characterized in that: The liquid connection pipe (21) includes a straight pipe section (210) and an elbow section (211). The straight pipe section (210) extends vertically upward. The lower end of the straight pipe section (210) is connected to the partition plate (2). One end of the elbow section (211) is connected to the upper end of the straight pipe section (210). The bending angle of the elbow section (211) is 90°-200°.

8. The rotating disc extraction column according to claim 1, characterized in that: The liquid connecting pipes (21) on the upper and lower partitions (2) are staggered, with an angle of 90°-200°; and / or The flow rate of the liquid connection pipe (21) is 0.01 to 0.2 m / s.

9. The rotating disc extraction tower according to claim 1, characterized in that: The diameter of the tower body (1) is 50–4000 mm; and / or The diameter of the stirrer (4) is 1 / 3 to 2 / 3 times the diameter of the tower body; and / or The height of the stirrer (4) is 1 / 10 to 1 / 5 of the stirrer diameter; and / or The spacing between the upper and lower partitions (2) is 1 / 10 to 2 / 3 times the tower diameter; and / or The diameter of the fixed connection port (20) is 1 / 8 to 2 / 3 times the diameter of the stirrer.

10. The rotating disc extraction column according to claim 1, characterized in that: The tower body (1) has an upper clarification section (10), a mixing section (11), and a lower clarification section (12), which are arranged sequentially from top to bottom. The upper clarification section (10) is provided with a liquid phase outlet (100). The upper part of the mixing section (11) is provided with a solid phase inlet (110), and the lower part of the mixing section (11) is provided with a liquid phase inlet (111). The mixing area (112) is located in the mixing section (11) between the solid phase inlet (110) and the liquid phase inlet (111). The lower clarification section (12) is provided with a solid phase outlet (120).

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