CN113209831A - Flat ceramic membrane stack - Google Patents
Flat ceramic membrane stack Download PDFInfo
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- CN113209831A CN113209831A CN202110597280.9A CN202110597280A CN113209831A CN 113209831 A CN113209831 A CN 113209831A CN 202110597280 A CN202110597280 A CN 202110597280A CN 113209831 A CN113209831 A CN 113209831A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
- B01D63/08—Flat membrane modules
- B01D63/082—Flat membrane modules comprising a stack of flat membranes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
- B01D65/02—Membrane cleaning or sterilisation ; Membrane regeneration
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
- B01D2321/18—Use of gases
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Abstract
The invention relates to a flat ceramic membrane stack, which comprises a frame (1) and a membrane stack (2), wherein the periphery of the frame (1) is sealed to form a cylinder, the upper surface and the lower surface of the frame are open, the membrane stack (2) is arranged in the frame (1), an aeration pipe (3) is also arranged on the frame (1), the aeration pipe (3) aerates from the bottom of the frame (1) to the inside of the cylinder frame to enable the inside and the outside of the cylinder frame to form a density difference, external liquid and aerated bubbles enter the membrane stack (2) from the bottom of the frame (1) and flow to the upper part, and after the liquid goes out of the frame (1), the bubbles continuously rise and flow to the lower part along the outer cylinder wall of the frame (1) to form a circulating flow. Compared with the prior art, the invention overcomes the influence of the accumulation of the dead-end filter cake on the surface of the membrane on the filtration flux on the premise of keeping the advantage of high recovery rate of the dead-end filtration.
Description
Technical Field
The invention relates to a filtering device, in particular to a flat ceramic membrane stack.
Background
The separation aperture of the flat ceramic membrane is 50-200 nm, belongs to one of ultrafiltration membranes, and is a special inorganic membrane, the appearance form of the flat ceramic membrane is a flat structure, and a purified water overflowing channel is arranged in the flat ceramic membrane. The membrane support is formed by sintering high-purity alumina powder at a temperature of more than 1000 ℃, and the surface of the membrane support is coated with a functional membrane layer which has certain separation precision and is uniformly distributed. In order to ensure the separation function of the membrane, the two ends of a single membrane sheet of a finished product are sealed and packaged by glue, and engineering plastics with long industrial durability and stable physical and chemical properties are selected for a packaging water collecting end to prepare a single-sheet flat ceramic membrane component.
If the flat ceramic membrane adopts internal pressure type filtration, insoluble substances can block a water production channel, so that external pressure type filtration is adopted in engineering application, namely pollutants are intercepted on the outer surface of the membrane, permeate liquid permeates the membrane layer and is collected in the water production channel, the membrane element is placed in materials or water to be filtered, the materials larger than the micropore diameter of the membrane layer are intercepted on the outer side of the separation layer, clean filtered water permeates the separation layer and the support body under the drive of pressure and enters a water collection channel in the membrane element, and then enters a water production pipeline of the membrane element from an encapsulated water collection end.
The membrane modules with different quantities are connected together to form a membrane stack, two frame forms of vertical installation or horizontal installation can be adopted for the flat ceramic membrane modules according to actual conditions, the flat ceramic membrane modules are installed on the frames in a naked mode, each ceramic membrane module is connected through a pipeline and gathered to a water production main pipe, the water production main pipe is connected with a suction pump, and the pressure difference between the inner side and the outer side of the membrane formed by the negative pressure generated by the suction pump and the atmospheric pressure of the liquid level serves as a filtering driving force.
Because the membrane stack is soaked in liquid, when a suction pump is started, a certain negative pressure is formed between the membrane water collecting channel and the outer surface of the membrane, the liquid penetrates through the separation layer water inlet and water collecting channel, insoluble substances are intercepted on the outer surface of the membrane to form a filter cake, and due to the formation of the filter cake, the filtration resistance is increased, and the filtration flow is gradually attenuated, so that the current flat ceramic membrane stack only can be a typical dead-end filtration mode, and the schematic diagram is shown in fig. 1. Although this filtration method has a high recovery rate, a higher average filtration flow rate can only be obtained by increasing the filtration area to meet the capacity requirement due to the flow rate attenuation.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provide a flat ceramic membrane stack which has high filtration recovery rate and can overcome the influence of filter cake accumulation on filtration flux.
The purpose of the invention can be realized by the following technical scheme: the utility model provides a dull and stereotyped ceramic membrane stack, includes frame and membrane stack, the frame seal all around and form the tube-shape, upper and lower two sides are open form, the membrane stack install in the frame, the frame on still be equipped with the aeration pipe, the aeration pipe from the frame bottom to the interior aeration of tube-shape frame, make the inside and outside density difference that forms of tube-shape frame, outside liquid gets into the membrane stack and flows toward the upper portion from the frame bottom together with the bubble of aeration, after going out the frame, the bubble continues to rise liquid and then flows toward the lower part along frame urceolus wall, forms a circulation flow.
The membrane stack is provided with at least one layer, each membrane stack comprises a plurality of flat ceramic membranes, and each flat ceramic membrane comprises a separation layer on the side surface and a water collecting channel in the middle.
One end of the water collecting channel is blocked, the other end of the water collecting channel is connected to the clear liquid main pipe, the clear liquid main pipe is connected with the suction pump, pressure difference is formed between the inside and the outside of each flat ceramic membrane through the suction pump, water to be treated penetrates through the separation layer under the driving of the pressure difference and enters the water collecting channel inside the water collecting channel, and materials larger than the micropore diameter of the flat ceramic membrane are intercepted outside the separation layer.
And an aeration pipe is arranged below each membrane stack, and the aeration pipes convey a large amount of bubbles to the space between each flat ceramic membrane and carry out air scrubbing on insoluble substances intercepted on the surface of each flat ceramic membrane.
Aeration is another key factor for enabling filtered liquid to circularly flow due to the difference of internal pressure and external pressure of a membrane stack, and the size of air flow and the rising speed of air bubbles are particularly important for driving the liquid to flow; the aeration rate adopted is not less than 2m per membrane stack3/min。
The film stack is hexahedron, the mounting mode includes horizontal dress or vertical dress, no matter is vertical dress or permanent dress, as long as the surface of film is perpendicular to the horizontal plane can, the hexahedron of film stack four faces perpendicular to the horizontal plane seal with the flat board, the flat board is fixed on the frame, constitutes the confined tube-shape in all around.
The flat plate material used for sealing is determined by the material characteristics of the filtering liquid, the die carriers are the same, and metal materials such as SS304, SS316L, Ti, Al and the like or organic polymer materials such as PVC, CPVC, PP, ABS and the like with certain hardness can be made.
Since the sealed flat plate is less compressed, the thickness of the flat plate is not less than 2mm, preferably 2mm to 5 mm.
The height of the membrane piles is also one of the reasons for influencing the flowing speed of the liquid, and in consideration of the installation density, the height of each membrane pile is not less than 1m, so that bubbles can be ensured to rise, the liquid is driven to reach a certain flowing speed, and meanwhile, insoluble substances intercepted on the surface of the membrane are taken out; the height of each film pile is preferably 1-2.5 m.
The flat ceramic membrane stack is arranged in the filter tank, in order to ensure that liquid can smoothly flow in a circulating manner, the lowest layer of membrane stack cannot be directly placed at the bottom of the membrane tank, a liquid circulating channel needs to be reserved, the height of the channel is not less than 20cm, and preferably, the distance between the bottom of the lowest layer of membrane stack and the bottom of the filter tank is 20 cm-40 cm.
And a mud bucket is arranged at the bottom of the filter tank. Insoluble substances which are separated from the surface of the membrane by the liquid circulating flow formed by scrubbing are deposited in a mud bucket at the bottom of the membrane pool and are periodically discharged, and the sludge is pumped to a sludge dewatering device by a slurry pump in a slurry mode. Pumping the slurry into a sludge dewatering device through a slurry pump for dewatering to obtain a filtrate and a mud cake, and returning the dewatered filtrate to the flat ceramic membrane pool;
the sludge slurry is pumped into sludge dewatering equipment by a slurry pump, the sludge dewatering equipment is a plate and frame filter press, a screw stacking machine, a vacuum filter, a belt filter and the like, and the plate and frame filter press is preferred. The clear filtrate of the filter press returns to the membrane pool.
Compared with the prior art, the invention has the following beneficial effects:
(1) in order to change the dead-end filtration of the flat ceramic membrane into cross-flow filtration, the invention overcomes the influence of the accumulation of a filter cake of the dead-end filtration on the membrane surface on the filtration flux on the premise of keeping the advantage of high recovery rate of the dead-end filtration, seals the four side walls of the hexahedral structure of the membrane stack, and only keeps the top and the bottom to keep the flow of liquid; at bottom aeration, the bubble rises during aeration and drives liquid flow and granule to rise simultaneously, and to the membrane stack top, the bubble continues to rise, and the outside liquid of membrane stack flows down and gets into the membrane stack from the bottom, and when the insoluble substance flows down along with liquid, partial granule participated in the circulation, and partial granule deposit is in the membrane pond bottom. Because the interior liquid upflow of membrane heap, the outer liquid downflow of membrane heap has formed the liquid in the membrane pond and has piled the inside and outside circulation flow of membrane for the direction of filtration is the vertical state with the liquid flow direction, and the insoluble substance that the flowing liquid was held back with the membrane surface takes out the membrane heap, and the liquid that flows down through the outside is accelerated, and the deposit of large granule insoluble substance is in the membrane pond bottom. Can send the mud of bottom to sludge dewatering device through the sediment stuff pump, arrange futilely the sediment outward, strain the clear liquid and return to the membrane tank and continue the membrane filtration.
(2) The traditional flat ceramic membrane stack is generally provided with an air scrubbing device, particles on the surface of the membrane are taken away by aerated bubbles, but the bubbles only rise, so that the circular flow of liquid cannot be formed; in addition, the rising of bubbles also influences the sedimentation of insoluble substances, which increases the difficulty of the subsequent sludge dewatering. The flat ceramic membrane stack with the novel structure can enable liquid inside and outside the membrane stack to circularly flow and cannot influence the sedimentation of insoluble substances.
(3) The invention keeps the characteristic of high recovery rate of the original flat ceramic membrane dead-end filtration, and changes the dead-end filtration mode into the cross-flow filtration mode by changing the structure and function of the flat ceramic membrane stack, thereby having large and stable filtration flow.
(5) The average flux of the new-structure flat ceramic membrane filtration is higher, so that the system investment and the occupied area can be greatly reduced.
(6) Compared with a tubular ceramic membrane in a typical cross-flow filtration mode, the flat ceramic membrane with the novel structure is lower in filtration (transmembrane pressure difference delta P is less than 0.1MPa), so that the advantage of low energy consumption of the flat ceramic membrane is continuously maintained.
Drawings
FIG. 1 is a schematic diagram of a conventional flat filter membrane filtration
FIG. 2 is a schematic structural view of a planar ceramic membrane stack according to the present invention;
FIG. 3 is a top view of a planar ceramic membrane stack according to the present invention;
FIG. 4 is a schematic structural view of the flat ceramic membrane stack of the present invention with the sealing flat removed;
FIG. 5 is a schematic structural view of a flat ceramic membrane stack disposed in a filter according to the present invention;
FIG. 6 is a frame diagram of a flat ceramic membrane stack in a filter according to the present invention;
FIG. 7 is a schematic structural view of a flat filter membrane;
FIG. 8 is a cross-sectional view A-A of FIG. 7;
FIG. 9 is an enlarged view of a portion of FIG. 8;
FIG. 10 is a schematic view of fluid flow between adjacent flat ceramic membrane sheets;
FIG. 11 is a schematic diagram of cross-flow filtration.
Detailed Description
The invention is described in detail below with reference to the figures and specific embodiments.
Example 1
As shown in fig. 2-4, the flat ceramic membrane stack comprises a frame 1, a membrane stack 2, an aeration pipe 3 and a clear liquid header pipe 4.
Wherein, frame 1 including the support frame that is used for installing membrane heap 2 to and set up at support frame dull and stereotyped 11 all around, membrane heap 2 be hexahedron form, the mounting means is including horizontal dress or perpendicular dress, no matter perpendicular dress or permanent dress, as long as the surface perpendicular to horizontal plane of membrane can, four faces of 2 hexahedron perpendicular to horizontal planes of membrane heap are sealed with dull and stereotyped 11, only keep two faces of top surface and bottom surface for open form, make frame 1 be the confined tube-shape all around.
The membrane stack 2 is arranged in the frame 1, at least one layer of membrane stack 2 is arranged, each layer of membrane stack 2 comprises a plurality of flat ceramic membranes, and each flat ceramic membrane comprises a separation layer 21 on the side surface and a water collecting channel 22 in the middle. As shown in fig. 7-9, one end of the water collecting channel 22 is blocked, the other end of the water collecting channel is connected to the clear liquid header pipe 4 through the water producing branch pipe 42, a flange 41 is arranged on the clear liquid header pipe 4 and is used for connecting a suction pump, a pressure difference is formed between the inside and the outside of each flat ceramic membrane through the suction pump, a liquid to be treated S01 penetrates through the separation layer 21 and enters the internal water collecting channel 22 under the driving of the pressure difference, clear liquid S03 enters the clear liquid header pipe 4 through the water producing branch pipe 42 and is pumped out, materials with pore diameters larger than the pore diameters of the flat ceramic membranes are intercepted outside the separation layer 21, as shown in fig. 10, an aeration pipe 3 is arranged below each membrane stack 2, the aeration pipe 3 conveys a large amount of bubbles to the space between the flat ceramic membranes, and gas scrubbing is performed on insoluble substances intercepted on the surfaces of the flat ceramic membranes.
As shown in fig. 5-6, the flat ceramic membrane stack is placed in the filter 5, the frame 1 is cylindrical, the aerator pipe 3 aerates from the bottom of the frame 1 to the cylindrical frame, during aeration, the density of liquid in the cylinder is reduced due to a large amount of bubbles, and the liquid outside the cylinder still keeps the original density, so that an internal and external density difference can be formed, external liquid S01 to be treated and the aerated bubbles enter the membrane stack 2 from the bottom of the frame 1 and flow upwards, and after the liquid goes out of the frame 1, the bubbles continuously rise and flow downwards along the outer cylinder wall of the frame 1, so that a circulating flow is formed.
Aeration is another key factor for enabling filtered liquid to circularly flow due to the difference of internal pressure and external pressure of a membrane stack, and the size of air flow and the rising speed of air bubbles are particularly important for driving the liquid to flow; the aeration rate adopted is not less than 2m per membrane stack 23Min, preferably 2 to 30m3And/min. In this example, the aeration amount was 22m per membrane stack3/min。
The material of the flat plate 11 used for sealing may be determined according to the material characteristics of the filtering liquid, and may be metal material such as SS304, SS316L, Ti, Al, etc., or organic polymer material such as PVC, CPVC, PP, ABS, etc., having a certain hardness. In this embodiment, a PVC material is used.
Because the sealed flat plate is pressed less, the thickness of the flat plate is not less than 2mm, preferably 2 mm-5 mm, the thickness of the flat plate 11 adopted in the embodiment is 2mm, the effect of the flat plate is that on one hand, the flat plate has a sealing effect, on the other hand, the flat plate can be used as a flow guide plate, namely, in the process of circulating flow, a large amount of bubbles are subjected to gas wiping on the surface of the membrane, large granular substances intercepted on the surface of the membrane are taken away, the large granular substances are prevented from being deposited on the surface of the membrane, the large granular substances move upwards along with the bubbles and fluid from bottom to bottom in a sealed cylinder, the large granular substances can sink to the bottom of the filter tank 5 along the flat plate 11 after being discharged from the cylinder, and the flat plate 11 can be used as the flow guide plate to guide slurry.
The height of the membrane piles is also one of the reasons for influencing the flowing speed of the liquid, and in consideration of the installation density, the height of each membrane pile is not less than 1m, so that bubbles can be ensured to rise, the liquid is driven to reach a certain flowing speed, and meanwhile, insoluble substances intercepted on the surface of the membrane are taken out; the height of each film pile is preferably 1-2.5 meters, and the height of the film pile adopted in the embodiment is 1 meter.
As shown in fig. 5-6, the flat ceramic membrane stack is placed in the filter 5, in order to ensure that the liquid can smoothly flow in a circulating manner, the lowest layer of the membrane stack cannot be directly placed at the bottom of the membrane tank, a liquid circulating channel needs to be reserved, the height of the liquid circulating channel is not less than 20cm, preferably, the distance between the bottom of the lowest layer of the membrane stack and the bottom of the filter is 20 cm-40 cm, and the middle distance in this embodiment is 20 cm.
The bottom of the filter 5 is provided with a mud bucket 6. Insoluble substances which are separated from the surface of the membrane by the liquid circulating flow formed by scrubbing are deposited in a mud bucket at the bottom of the membrane pool and are periodically discharged, and the sludge is pumped to a sludge dewatering device by a slurry pump in a slurry mode. Pumping the slurry into a sludge dewatering device through a slurry pump for dewatering to obtain a filtrate and a mud cake, and returning the dewatered filtrate to the flat ceramic membrane pool; the sludge slurry is pumped into sludge dewatering equipment by a slurry pump, the sludge dewatering equipment is a plate and frame filter press, a screw stacking machine, a vacuum filter, a belt filter and the like, and the plate and frame filter press is preferred. The clear filtrate of the filter press returns to the membrane pool.
By adopting the structure, the water inlet direction is vertical to the water production direction, as shown in fig. 11, part of inlet water is discharged as concentrated water with insoluble substances, the surface of the membrane is not easy to generate filter cake accumulation and concentration polarization, the filtering flow is relatively stable, the effective operation period is longer, the filtering flux can be improved, and the filtering recovery rate is high.
Comparative example 1
A commercially available flat ceramic membrane stack.
The two types of flat ceramic membrane stacks of the embodiment 1 and the comparative example 1 are placed in a filter tank, crude brine is filled in the filter tank, negative pressure suction is carried out through a suction pump, the transmembrane pressure difference delta P is less than 0.1MPa, insoluble substances such as calcium carbonate, magnesium hydroxide and silt in the crude brine are intercepted on the surface of the flat ceramic membrane, circulating brine formed by scrubbing with air is carried away from the surface of the flat ceramic membrane, and the brine penetrates through the flat ceramic membrane to obtain refined brine.
The results are shown in table 1 below:
remarking: each backwashing requires removing negative pressure (about 10 seconds) in the membrane module, pumping the filtered liquid into the membrane module in a reverse direction (about 30 seconds) from a clear liquid pipe by using a backwashing pump, and settling time (about 40 seconds) of insoluble substances removed from the surface of the membrane module is about 80 seconds, which is ineffective filtering time. The more frequent the backwashing and the longer the ineffective filtration time, the lower the filtration efficiency.
It can be seen that: under the same material condition, the new structure flat ceramic membrane stack is adopted, the characteristic of high recovery rate of the old structure flat ceramic membrane stack is kept, the filtration flux is larger and stable, the backwashing period can be greatly prolonged, the filtration efficiency is higher, the insoluble substance sedimentation effect is better, and the solid content in the discharged mud is higher.
The transmembrane pressure difference Δ P in the above example was 0.08MPa, and the filtration recovery rates in example 1 and comparative example 1 were both 100% under these conditions, but the filtration fluxes in example 1 and comparative example 1 were greatly different if the suction pressure P was lowered, as shown in Table 2 below:
| transmembrane pressure difference Δ P (MPa) | Example 1 | Comparative example 1 |
| ～0.08 | 0.22～0.16m3/m2.h | 0.2～0.05m3/m2.h |
| 0.06 | 0.22～0.15m3/m2.h | 0.18～0.04m3/m2.h |
| 0.05 | 0.18～0.14m3/m2.h | 0.1～0.01m3/m2.h |
| 0.01 | 0.05～0.02m3/m2.h | 0 |
| 0.001 | 0.02～0.01m3/m2.h | 0 |
It can be seen that the filtration flux of the flat-plate ceramic membrane stack can be maintained at 0.18-0.14 m when the transmembrane pressure difference delta P is reduced to 0.05MPa3/m2H, can still reach 0.05 to 0.02m when the pressure is reduced to 0.01MPa3/m2H, but the filtration flux of the membrane stack of the comparative example 1 is reduced by 50-20% when the transmembrane pressure difference delta P is 0.05MPa, and the filtration task of the comparative example 1 can hardly be completed when the transmembrane pressure difference delta P is reduced to 0.01MPa, which shows that the energy consumption of the flat ceramic membrane stack is lower (the transmembrane pressure difference delta P is lower)<0.1MPa)。
Aeration is another key factor for enabling filtered liquid to circularly flow due to the difference of internal pressure and external pressure of a membrane stack, and the size of air flow and the rising speed of air bubbles are particularly important for driving the liquid to flow; the following filtration results of the membrane stack of the same structure as in example 1 at different aeration rates were measured as shown in Table 3 below
The results are shown in table 1 below:
comparative example 2
The height of the pile, which is also one of the reasons for the influence of the liquid flow rate, was reduced to 0.5 m, and the results of the same test conditions as in example 1 were shown in the following table 4, as in example 1:
from the above, it can be seen that even though the structure is the same as the present invention, the filtering effect is greatly affected if the aeration amount and the membrane stack height are not controlled.
Claims (10)
1. The utility model provides a dull and stereotyped ceramic membrane stack, characterized in that includes frame (1) and membrane stack (2), frame (1) seal all around and form the tube-shape, the upper and lower two sides are open form, membrane stack (2) install in frame (1), frame (1) on still be equipped with aeration pipe (3), aeration pipe (3) from frame (1) bottom to tube-shape frame in the aeration, make the tube-shape frame inside and outside form density difference, outside liquid and the bubble of aeration get into membrane stack (2) and flow towards the upper portion from frame (1) bottom together, go out frame (1) back, the bubble continues to rise liquid and then flows along frame (1) outer tube wall down, forms a circulation flow.
2. A flat ceramic membrane stack according to claim 1, wherein the membrane stack (2) comprises at least one layer, each membrane stack (2) comprising a plurality of flat ceramic membranes, each flat ceramic membrane comprising lateral separation layers (21) and intermediate water collection channels (22).
3. The membrane stack according to claim 2, wherein the water collecting channels (22) are plugged at one end and connected at the other end to the clean liquid header pipe (4), the clean liquid header pipe (4) is connected to a suction pump, a pressure difference is formed between the inside and the outside of each flat ceramic membrane by the suction pump, water to be treated penetrates through the separation layer (21) under the driving of the pressure difference and enters the water collecting channels (22) inside the water collecting channels, and materials with pore diameters larger than the pore diameters of the micro-pores of the flat ceramic membranes are trapped outside the separation layer (21).
4. The flat ceramic membrane stack according to claim 2, wherein an aeration pipe (3) is provided under each membrane stack (2), and the aeration pipe (3) supplies a large amount of bubbles to the space between each flat ceramic membrane, thereby scrubbing the insoluble substances trapped on the surface of each flat ceramic membrane.
5. A flat ceramic membrane stack according to claim 1, wherein the aeration rate used is not less than 2m per membrane stack (2)3/min。
6. A planar ceramic membrane stack according to claim 1, wherein the membrane stack (2) is hexahedral and is mounted in a horizontal or vertical manner to ensure that the outer surface of each membrane in the stack is perpendicular to the horizontal plane.
7. The ceramic membrane stack according to claim 1 or 6, wherein the hexahedral four faces of the membrane stack (2) perpendicular to the horizontal plane are sealed with flat plates fixed to a frame to form a cylindrical shape with closed periphery.
8. The planar ceramic membrane stack of claim 7, wherein each membrane stack has a height of 1-2.5 m and a planar thickness of 2-5 mm.
9. A flat ceramic membrane stack according to claim 1, wherein the flat ceramic membrane stack is placed in the filter tank (5), and the distance between the bottom of the lowest layer of the membrane stack and the bottom of the filter tank is 20cm to 40 cm.
10. A ceramic membrane stack according to claim 9, wherein a hopper (6) is provided at the bottom of the filter tank (5).
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| CN202110597280.9A CN113209831A (en) | 2021-05-31 | 2021-05-31 | Flat ceramic membrane stack |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114797482A (en) * | 2022-05-13 | 2022-07-29 | 新宇达环保科技有限公司 | Cleaning process for online automatic back-cleaning film |
| CN114906903A (en) * | 2022-05-24 | 2022-08-16 | 扬州大学 | Space-saving flat ceramic membrane water purifying device with lateral intensive aeration generation |
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2021
- 2021-05-31 CN CN202110597280.9A patent/CN113209831A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114797482A (en) * | 2022-05-13 | 2022-07-29 | 新宇达环保科技有限公司 | Cleaning process for online automatic back-cleaning film |
| CN114906903A (en) * | 2022-05-24 | 2022-08-16 | 扬州大学 | Space-saving flat ceramic membrane water purifying device with lateral intensive aeration generation |
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Inventor after: Cheng Xiong Inventor after: Li Jun Inventor after: Liu Lihua Inventor before: Cheng Xiong |