Superfine powder slurry washing device

Abstract

The utility model discloses an ultrafine powder slurry washing device. The ultrafine powder slurry washing device comprises a mixer, a liquid circulation driving part and a membrane type separation assembly which are communicated in sequence, the membrane type separation assembly comprises a separation pipe body and a membrane body structure arranged in the separation pipe body, the interior of the separation pipe body is divided into an ultrafine powder slurry flowing space and a penetrating fluid flowing space by the membrane body structure, and the membrane body structure is an inorganic filtering membrane; the ultrafine powder slurry flowing space is communicated with the liquid circulation driving part and is communicated to a slurry outlet for discharging qualified ultrafine powder slurry; the penetrating fluid flowing space is communicated with the washing water outlet, and the washing water outlet is used for discharging washing water permeating out of the penetrating fluid flowing space. According to the superfine powder slurry washing device, on the basis that the occupied area is reduced and water is saved, the cooling step is not needed, the washing efficiency is improved, and the productivity is improved.

Description

Technical Field

[0001] The utility model relates to the technical field of battery manufacturing auxiliary equipment, and more specifically to an ultra-fine powder slurry washing device. Background Art

[0002] Ferric phosphate is a critical material for the new energy industry. The requirements for controlling impurity levels in ferric phosphate products are extremely high. Most ferric phosphates must contain ions at the ppm level, and some even at the ppb level. When producing ferric phosphate, the reaction system is mixed with various materials, including a large number of soluble impurity ions. However, ferric phosphate has a relatively low solubility in water. Therefore, the washing and purification process of ferric phosphate slurry is based on the different solubilities of different materials in water, using pure water to separate unwanted soluble ions from the materials. This washing process primarily involves dissolution, mass transfer, and solid-liquid separation. First, the impurity ions are transferred from the ferric phosphate slurry into pure water, followed by solid-liquid separation, resulting in a high-purity ferric phosphate slurry.

[0003] In the prior art, tubular membranes can be used to wash ultrafine powder slurries (including but not limited to iron phosphate slurries), such as Figure 1 As shown, Figure 1 The schematic diagram of an existing tubular membrane washing system shows that the tubular membrane washing system includes a circulating washing tank 101, a mortar pump 102, and a membrane 103. The washing water and the emulsified slurry of the ultrafine powder first enter the circulating washing tank 101 for thorough mixing, and then are powered by the mortar pump 102 to pass through a plurality of membranes 103 in sequence. The number of such membranes 103 is not limited to Figure 1 As shown in FIG3 , the number of membranes 103 can be increased or decreased according to production capacity requirements. There is no restriction here. The filtrate passing through each membrane 103 is discharged into the filtrate tank for collection, and the ultrafine powder slurry that cannot pass through the membrane will eventually become a qualified washed slurry and be discharged if the conductivity meets the requirements. If the conductivity does not meet the requirements, it will return to the circulating washing tank 101 as a circulating slurry and continue the washing process until the conductivity meets the requirements and becomes a qualified washed slurry. Finally, this washed slurry will be discharged.

[0004] However, the existing tubular membrane washing system uses an organic membrane, which has strict environmental requirements and requires the operating temperature to be below 50°C. Therefore, the material needs to be cooled in advance before the washing process can be carried out. This requires that the entire system must be equipped with cooling equipment before it can be used. Moreover, since the temperature of the washing water cannot be too high, the entire washing process can only be carried out at low temperatures. As we all know, in this low-temperature washing water environment, the solubility of impurities is not high, so it is very unfavorable for the washing out of impurities, resulting in the entire washing process taking a long time. In this case, in order to remove impurity ions, a large amount of deionized water is often required, which greatly increases the cost of washing consumables. Utility Model Content

[0005] In order to solve the above technical problems, the utility model provides an ultrafine powder slurry washing device, which can reduce the equipment footprint and save water without the need for cooling equipment, thereby improving washing efficiency and increasing production capacity.

[0006] The utility model provides an ultrafine powder slurry washing device comprising a mixer, a liquid circulation drive component and a membrane separation component which are connected in sequence;

[0007] The membrane separation component includes a separation tube body and a membrane structure arranged inside the separation tube body, wherein the membrane structure divides the interior of the separation tube body into an ultrafine powder slurry flow space and a permeate flow space, and the membrane structure is an inorganic filtration membrane;

[0008] The ultrafine powder slurry flow space is in communication with the liquid circulation drive component and is in communication with a slurry outlet for discharging qualified ultrafine powder slurry;

[0009] The permeate flow space is communicated with a wash water outlet, and the wash water outlet is used to discharge the wash water permeated from the permeate flow space.

[0010] Preferably, in the above-mentioned ultrafine powder slurry washing device, the overall shape of the membrane structure is a circular tube, and the end of the membrane structure is connected to the inner wall of the separation tube body by a seal, and there is a first preset distance between the end of the membrane structure and the corresponding end of the separation tube body.

[0011] Preferably, in the above-mentioned ultrafine powder slurry washing device, the inner diameter of the membrane structure is 90% to 95% of the inner diameter of the separation tube.

[0012] Preferably, in the above-mentioned ultrafine powder slurry washing device, the number of the separation tubes is 2 to 10, and all of the separation tubes are arranged in a direction perpendicular to the ground.

[0013] Preferably, in the above-mentioned ultrafine powder slurry washing device, adjacent separation tubes are connected by U-shaped connecting tubes, and the adjacent U-shaped connecting tubes are located on different sides of the separation tubes.

[0014] Preferably, in the above-mentioned ultrafine powder slurry washing device, the membrane structure is a silicon carbide membrane.

[0015] Preferably, in the above-mentioned ultrafine powder slurry washing device, the diameter of the side membrane pore channel in the membrane structure is 50nm to 200nm.

[0016] Preferably, in the above-mentioned ultrafine powder slurry washing device, the mixer is a pipeline mixer with a spiral channel provided inside.

[0017] Preferably, in the above-mentioned ultrafine powder slurry washing device, the radius of the spiral channel inside the pipeline mixer is different at different positions.

[0018] Preferably, the above-mentioned ultrafine powder slurry washing device further includes a premixer connected to the mixer, and the slurry discharge pipe of the separation tube body is connected to the premixer, and the premixer is also connected to a slurry inlet pipe and a pure water inlet pipe.

[0019] It can be seen from the above technical solution that the above-mentioned ultrafine powder slurry washing device provided by the present invention, since the membrane separation component includes a separation tube body and a membrane structure arranged inside the separation tube body, the membrane structure divides the interior of the separation tube body into an ultrafine powder slurry flow space and a permeate flow space, and the membrane structure is an inorganic filter membrane. This inorganic filter membrane can withstand high temperatures, so there is no need for a cooling step, and washing can be carried out directly, which improves the washing efficiency from the first aspect, and high-temperature washing water itself can promote the improvement of washing efficiency better than cold water, which in turn From the second aspect, the washing efficiency is improved, thereby greatly improving the production capacity. Moreover, since the ultrafine powder slurry flow space is connected with the liquid circulation drive component and is connected to the slurry outlet for discharging qualified ultrafine powder slurry, and the permeate flow space is connected with the washing water outlet, the washing water outlet is used to discharge the washing water that permeates from the permeate flow space. Therefore, the qualified slurry and the permeate can be separated more quickly and effectively. In addition, the mixer is used instead of the large circulation washing tank used in the prior art. Therefore, the footprint of the overall equipment can be reduced, and the manufacturing cost of the overall equipment can also be reduced. BRIEF DESCRIPTION OF THE DRAWINGS

[0020] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the following briefly introduces the drawings required for use in the embodiments or the description of the prior art. Obviously, the drawings described below are merely embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on the provided drawings without paying any creative work.

[0021] Figure 1 is a schematic diagram of an existing tubular membrane washing system;

[0022] Figure 2 This is a schematic diagram of an embodiment of an ultrafine powder slurry washing device provided by the utility model. DETAILED DESCRIPTION

[0023] The core of the utility model is to provide an ultrafine powder slurry washing device, which can reduce the floor space and save water without the need for a cooling step, thereby improving the washing efficiency and increasing the production capacity.

[0024] The following will be combined with the drawings in the embodiments of the present invention to clearly and completely describe the technical solutions in the embodiments of the present invention. Obviously, the embodiments described are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without making creative efforts are within the scope of protection of the present invention.

[0025] The utility model provides an embodiment of an ultrafine powder slurry washing device. Figure 2 As shown, Figure 2 This is a schematic diagram of an embodiment of an ultrafine powder slurry washing device provided by the utility model. The device may include a mixer 1, a liquid circulation drive component 2 and a membrane separation component 3 connected in sequence. The mixer 1 can be used to fully and evenly mix fresh ultrafine powder slurry with pure water, so that the soluble ions mixed in the slurry can be fully dissolved in the pure water to achieve separation from the ultrafine powder, which is convenient for subsequent removal. The liquid circulation drive component 2 is used to provide power for the flow of various substances in the pipeline, so that these substances can continuously enter the membrane separation component 3 from the mixer 1 to achieve separation, such as Figure 2 As shown by the arrows in the figure, the direction of the arrows is the flow direction of various substances in the pipeline;

[0026] The membrane separation component 3 includes a separation tube 31 and a membrane structure 32 (such as Figure 2As shown by the dotted line in the figure, the membrane structure 32 divides the interior of the separation tube 31 into an ultrafine powder slurry flow space 33 (which is equivalent to the internal space of the membrane structure) and a permeate flow space 34 (which is equivalent to the external space of the membrane structure). In other words, this membrane structure 32 can only allow soluble ions to penetrate from the membrane structure to reach the permeate flow space 34, and because the particles of the ultrafine powder slurry itself are larger than the through holes on the surface of the membrane structure 32, they cannot penetrate through and can only remain in the ultrafine powder slurry flow space 33 inside the membrane structure 32. In this way, the soluble ions are separated from the ultrafine powder slurry, and the membrane structure 32 is an inorganic filter membrane, which does not have an organic coating like the prior art. This simple inorganic filter membrane can withstand high temperatures, unlike the organic coating used in the prior art, which can only filter at low temperatures and requires a cooling device to cool the slurry. The solution of this embodiment directly passes the high-temperature slurry into the membrane structure 32, and the high-temperature environment can ensure a faster dissolution rate, and therefore a faster separation rate. This can greatly improve the washing efficiency from two aspects and increase the production capacity of the overall process.

[0027] Moreover, the ultrafine powder slurry flow space 33 is connected to the liquid circulation drive component 2 and is connected to the slurry outlet 4 for discharging qualified ultrafine powder slurry. The power of the liquid circulation drive component 2 can drive the ultrafine powder slurry to continuously move forward in the ultrafine powder slurry flow space 33, and flow out from the slurry outlet 4 after the internal impurity ion content meets the requirements, thereby achieving effective washing;

[0028] Moreover, the above-mentioned permeate flow space 34 can be connected to the washing water outlet 5, and this washing water outlet 5 is used to discharge the washing water that permeates from the permeate flow space 34. In this case, after washing, the washing water contains impurity ions, and this washing water can be discharged, thereby completing the purification process of the ultrafine powder slurry. It should be noted that when the impurity ion concentration in the slurry still does not meet the requirements after one washing, the slurry can be circulated again and washed for the second time until the impurity ion concentration meets the requirements, and then the slurry that meets the requirements can be discharged from the slurry outlet 4. In addition, a detection component 51 can be provided on the pipeline where the washing water outlet 5 is located to detect the concentration of impurity ions, thereby providing a basis for determining whether the slurry is qualified. Specifically, when the impurity ion concentration detected by the detection component 51 is high, it proves that the slurry washing effect is not good enough at this time and another round of washing is required. Therefore, the detection component 51 can transmit this impurity ion concentration information to the control component wirelessly connected to it. After the control component makes a judgment that washing is still needed, it can transmit a control signal to the control valve 41 on the pipeline near the slurry outlet 4 by wireless means, and close the control valve 41 to prevent the slurry from flowing out of the slurry outlet 4 at this time, and continue to circulate the slurry until the control component judges that the slurry is qualified and does not need to be washed again based on the new round of impurity ion concentration information, and then sends an open signal to the control valve 41, so that the qualified slurry flows out from the control valve 41.

[0029] The above-mentioned liquid circulation drive component 2 can preferably be a circulation pump. In this case, the mixer and the membrane structure are combined, and the slurry containing impurities and pure water enter the mixer inlet. After mixing, they are transported into the membrane structure by the circulation pump. The impurity-containing washing water is separated through the microchannel of the membrane structure and enters the washing water collection system, while the slurry continues to circulate in the system, pure water is continuously added, and then the impurity ions are taken away by the membrane structure, and this cycle is repeated to finally achieve the washing of all slurries. The ultrafine powder slurry that can be processed by this device may be, but is not limited to, iron phosphate slurry. Ferric phosphate slurry is obtained through liquid-liquid ion chemical reaction. The particle size of the obtained material is primary particle size, usually between 0.1μm and 10μm. Ionic impurities exist in the liquid phase. With this solution, the mixer processes the original particle size slurry, which has a smaller processed particle size, more uniform distribution, more thorough washing, and less product loss. The particle size distribution of the washed slurry tends to be smoother, and D90 and D99 are smaller, both within 2μm. This mixer has a better effect on washing and removing soluble impurities, such as SO4 2- , K + 、Na + Mg 2+ .

[0030] It can be seen from the above technical solution that in the embodiment of the above-mentioned ultrafine powder slurry washing device provided by the present invention, since the membrane separation component includes a separation tube body and a membrane structure arranged inside the separation tube body, the membrane structure divides the interior of the separation tube body into an ultrafine powder slurry flow space and a permeate flow space, and the membrane structure is an inorganic filter membrane. This inorganic filter membrane can withstand high temperatures, so there is no need for a cooling step, and washing can be carried out directly, which improves the washing efficiency from the first aspect, and high-temperature washing water itself can promote the improvement of washing efficiency better than cold water, which in turn improves the washing efficiency from the second aspect and improves production, and since the ultrafine powder slurry flow space is connected to the liquid circulation drive component and is connected to the slurry outlet for discharging qualified ultrafine powder slurry, and the permeate flow space is connected to the washing water outlet, the washing water outlet is used to discharge the washing water that permeates from the permeate flow space, so the qualified slurry and the permeate can be separated more quickly and effectively, and the mixer is used instead of the large circulation washing tank used in the prior art, so the overall equipment footprint can be reduced, and the overall production cost can also be reduced.

[0031] In a specific embodiment of the ultrafine powder slurry washing device, continue to refer to Figure 2 The overall shape of the membrane structure 32 can be a circular tube, and a seal 36 (ie, Figure 2 The membrane structure 32 is connected to the separation tube 31 (shown by the vertical line in the figure). The sealing member can be, but is not limited to, a sealing strip. Its function is to ensure a sealing effect and prevent the permeate from returning to the ultrafine powder slurry through this portion. A first preset distance L1 is provided between the end of the membrane structure 32 and the corresponding end of the separation tube 31. Generally speaking, the separation tube 31 can preferably be a membrane shell. The membrane structure within this membrane shell is also the membrane element. In this case, the material can pass through the interior of the membrane element, and the liquid flows vertically into the membrane shell and then is discharged.

[0032] Specifically, the ultrafine powder slurry first enters the membrane structure 32 from the end, and at least a part of the impurity ions therein can vertically penetrate the membrane structure 32 and enter the permeate flow space 34, and then the slurry continues to flow forward along the inside of the membrane structure 32. During the flow, some impurity ions still existing in the slurry will also vertically penetrate the membrane structure 32 and enter the permeate flow space 34, and the impurity ions will eventually flow out with the washing water. It can be seen that using this structure can ensure that the contact area and contact time with the membrane structure during the flow of the slurry are larger, so that more impurity ions can pass through the membrane structure to achieve separation, which can achieve separation from the slurry to a greater extent, and make the washing effect better.

[0033] For further reference, Figure 2The inner diameter L2 of the membrane structure 32 can preferably be 90% to 95% of the inner diameter of the separation tube 31. The inner diameter L2 of the membrane structure 32 is the diameter of the channel through which the slurry can pass. For example, when the diameter of the separation tube is 50 mm, L2 is preferably 45 mm to 47.5 mm. Of course, this can be selected based on actual needs and is not limited here. In addition, multiple membrane structures 32 arranged in parallel can be simultaneously installed within each separation tube 31, and the number can be 19, 37, or other numbers, which is not limited here.

[0034] In another specific embodiment of the ultrafine powder slurry washing device, based on the above specific embodiment, the number of separation tubes 31 can be further preferably 2 to 10, and all separation tubes 31 are arranged in a direction perpendicular to the ground. Figure 2 , it can be seen that there are three separation tubes 31, and these three separation tubes 31 are stacked in sequence, which can reduce the floor space and save layout space. Moreover, these separation tubes 31 can be located below the mixer 1, further reducing the occupied area and making the overall layout more compact. When a more thorough separation effect is required, the number of separation tubes can be increased, and when impurity ions are easy to separate, the number of separation tubes can be reduced. This can be selected according to actual needs and is not limited here. In further embodiments, continue to refer to Figure 2 , adjacent separation tube bodies 31 are connected by U-shaped connecting tubes 6, and adjacent U-shaped connecting tubes 6 are located on opposite sides of the separation tube body 31, that is, when a U-shaped connecting tube connects the first separation tube body and the second separation tube body from the left, then another U-shaped connecting tube connects the second separation tube body and the third separation tube body from the right. In this case, the slurry enters the U-shaped connecting tube, the second separation tube body, another U-shaped connecting tube and the third separation tube body from the first separation tube body in turn, achieving maximum contact with the membrane structure and separating more impurity ions. In this way, the overall layout can be more compact and space is not wasted. Of course, other connection methods can be selected according to actual needs, which are not limited here.

[0035] In another specific embodiment of the ultrafine powder slurry washing device, the membrane structure 32 can be preferably a silicon carbide membrane. This silicon carbide membrane has the advantages of high temperature resistance, thermal shock resistance, corrosion resistance, high flux, and long service life. In this case, the powder in the slurry will not be deposited on the surface of the silicon carbide membrane and cause clogging of the washing water channel. The slurry flow rate in the membrane structure during the washing process is preferably 5m / s to 10m / s. Of course, other types of ceramic membranes, such as Al2O3 membranes, can also be selected according to actual needs, and this is not limited here. In a further embodiment, the diameter of the side membrane pore channel in the membrane structure can be preferably 50nm to 200nm. The side membrane pore channel of this diameter can be produced using existing processes, and can be produced by, but not limited to, a pressureless sintering process. Therefore, there is no need to form an organic membrane on its surface as in the prior art. This ensures that water containing impurity ions can pass through smoothly, while the slurry cannot pass through it due to its large particles. It can also withstand high temperatures, so the washing activity is higher at high temperatures, thereby ensuring a better washing effect.

[0036] Continue to refer Figure 2 The present application also provides a preferred embodiment, which is based on the various embodiments of the above-mentioned ultrafine powder slurry washing device. The above-mentioned mixer 1 can preferably be a pipeline mixer with a spiral channel 11 inside. Compared with the large equipment used in the prior art, this pipeline mixer greatly reduces the floor space and water consumption. The use of the spiral channel 11 can make the flow path of the slurry and pure water longer, and constantly change direction during the flow process, thereby forming tiny turbulence and achieving repeated mixing in certain parts. In this way, more mixing can be achieved in the same volume, so that a better mixing effect can be achieved using smaller equipment, so that there is sufficient time to release impurity ions, and then realize the stripping of impurity ions in the membrane structure, thereby achieving the purpose of washing. On this basis, another preferred embodiment is provided, in which the spiral channel 11 inside the above-mentioned pipeline mixer has different radii at different positions. This variable diameter design structure is easier to mix the slurry thoroughly than the equal diameter design structure, because during the flow of the slurry, it will collide with spiral parts of different sizes at different times, so the internal turbulence generated is more irregular, resulting in a higher degree of mixing, which can allow the impurity ions in the slurry to be more fully released into the water, thereby achieving better separation. Of course, the specific radius distribution method is not limited, and this can be selected according to actual needs.

[0037] This application also provides another preferred embodiment of the above-mentioned ultrafine powder slurry washing device, and further reference is made to Figure 2, this is based on another preferred embodiment mentioned above, and can also include a premixer 7 connected to the mixer 1, and the slurry discharge pipe 35 of the separation tube body 3 is connected to the premixer 7, and this premixer 7 can also be connected to the slurry inlet pipe 8 and the pure water inlet pipe 9. Specifically, the slurry inlet pipe 8 and the pure water inlet pipe 9 can also be provided with a flow display device, so that the operator can know the flow rate of the incoming liquid in real time. The slurry and pure water coming in from these two pipes can be premixed to form a buffering effect, and then enter the mixer 1 for formal and sufficient mixing, so that the overall mixing effect will be better, and the slurry that has not been washed clean in the slurry discharge pipe 35 can enter the premixer 7 again to achieve re-washing, thereby ensuring that it can be thoroughly washed.

[0038] The washing process of the ultrafine powder slurry washing device is provided below:

[0039] (1) A certain amount of slurry containing impurities is input into the ultrafine powder slurry washing device, and pure water is simultaneously transported into the device;

[0040] (2) The slurry and pure water are fully mixed in the pipeline mixer;

[0041] (3) The mixed material passes through the membrane structure to separate the wash water containing impurities, and the slurry continues to circulate in the device;

[0042] (4) Pure water is continuously added and circulated for washing until the slurry is washed to a qualified level;

[0043] (5) Add fresh slurry and add corresponding pure water in proportion, and circulate the washing. The qualified slurry is discharged after the membrane structure.

[0044] It should also be noted that the removal of qualified slurry can be intermittent or continuous, as follows:

[0045] Intermittent mode: Slurry is first fed into the system, and circulation begins. Liquid permeates the membrane structure and is discharged from the "wash water" position. The slurry concentration increases, becoming concentrated. Pure water is continuously added to the "pure water" position. As pure water is continuously added, it is discharged as wash water. The conductivity (or other impurity ion concentration) in the wash water decreases until it reaches an acceptable level. The addition of pure water is stopped, and the slurry is discharged all at once from the "accepted slurry" position.

[0046] Continuous mode: The device has slurry that has been washed to a qualified level and is in circulation. Fresh slurry and pure water are added from the "fresh slurry" and "pure water" positions respectively, and a suitable circulation ratio is controlled, such as 100:1, that is, the mass of the qualified circulating slurry is 100m3 3 , the fresh slurry added is 1m 3, the added slurry has little effect on the existing qualified slurry. After the pure water and slurry pass through the pipeline mixer, the washing water is discharged through the membrane structure. The slurry has reached the qualified level. Open the "qualified slurry" valve appropriately and continuously discharge the qualified slurry (about 1m 3 ).

[0047] In addition, to prevent clogging of the membrane structure, a cross-flow process can be used to reduce contamination and blockage, slow flux decay, and maintain a relatively stable flux. When using a cross-flow process, the membrane surface is flushed at a higher flow rate, preventing trapped impurities from accumulating and clogging the membrane surface, maintaining a good membrane flux. This can extend the membrane cleaning cycle and reduce the cleaning frequency. Moreover, controlling the flow rate across the membrane surface is also the key to ensuring sufficient mixing and preventing material deposition on the membrane component surface.

[0048] In order to delay the service life of the membrane structure, a backflush process can also be used, that is, after a period of operation, compressed air is used to pressurize and backflush from the washing water outlet into the device, so that the washing water flows in reverse. The advantage is that the powder material attached to the membrane surface can be blown off to ensure the flux of the membrane. For example, the flux can be backflushed when it drops to a certain value: when the device starts to operate, its washing water flux can reach 10m 3 / h. After running for two hours, some membrane channels may be blocked and powder may adhere to the membrane, and the membrane flux is reduced to 6m 3 / h, then online backflushing is required at this time, or it can be backflushing at a fixed time, such as backflushing for 5 minutes when the system runs for 2 hours.

[0049] The above description of the disclosed embodiments will enable one skilled in the art to implement or use the present invention. Various modifications to these embodiments will be readily apparent to one skilled in the art, and the general principles defined herein may be implemented in other embodiments without departing from the spirit or scope of the present invention. Therefore, the present invention is not limited to the embodiments shown herein but is intended to conform to the widest scope consistent with the principles and novel features disclosed herein.

Claims

1. An ultrafine powder slurry washing device, characterized in that: It includes a mixer, a liquid circulation driving component and a membrane separation component which are connected in sequence; The membrane separation component includes a separation tube body and a membrane structure arranged inside the separation tube body, wherein the membrane structure divides the interior of the separation tube body into an ultrafine powder slurry flow space and a permeate flow space, and the membrane structure is an inorganic filtration membrane; The ultrafine powder slurry flow space is in communication with the liquid circulation drive component and is in communication with a slurry outlet for discharging qualified ultrafine powder slurry; The permeate flow space is communicated with a wash water outlet, and the wash water outlet is used to discharge the wash water permeated from the permeate flow space.

2. The ultrafine powder slurry washing device according to claim 1, characterized in that: The overall shape of the membrane structure is a circular tube, and the end of the membrane structure is connected to the inner wall of the separation tube body by a seal, and there is a first preset distance between the end of the membrane structure and the corresponding end of the separation tube body.

3. The ultrafine powder slurry washing device according to claim 2, characterized in that: The inner diameter of the membrane structure is 90% to 95% of the inner diameter of the separation tube.

4. The ultrafine powder slurry washing device according to claim 3, characterized in that: The number of the separation tube bodies is 2 to 10, and all the separation tube bodies are arranged in a direction perpendicular to the ground.

5. The ultrafine powder slurry washing device according to claim 4, characterized in that: Adjacent separation tube bodies are connected by U-shaped connecting tubes, and the adjacent U-shaped connecting tubes are located on different sides of the separation tube bodies.

6. The ultrafine powder slurry washing device according to claim 1, characterized in that: The film structure is a silicon carbide film.

7. The ultrafine powder slurry washing device according to claim 6, characterized in that: The diameter of the side membrane pore channels in the membrane structure is 50 nm to 200 nm.

8. The ultrafine powder slurry washing device according to any one of claims 1 to 7, characterized in that: The mixer is a pipeline mixer with a spiral channel arranged inside.

9. The ultrafine powder slurry washing device according to claim 8, characterized in that: The spiral channel inside the pipeline mixer has different radii at different positions.

10. The ultrafine powder slurry washing device according to claim 9, characterized in that: It also includes a premixer communicated with the mixer, and the slurry discharge pipe of the separation tube body is communicated with the premixer, and the premixer is also connected with a slurry inlet pipe and a pure water inlet pipe.

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