CN214781005U - A slot-pulling anaerobic gravity flow dynamic membrane bioreactor device - Google Patents
A slot-pulling anaerobic gravity flow dynamic membrane bioreactor device Download PDFInfo
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- CN214781005U CN214781005U CN202121023107.XU CN202121023107U CN214781005U CN 214781005 U CN214781005 U CN 214781005U CN 202121023107 U CN202121023107 U CN 202121023107U CN 214781005 U CN214781005 U CN 214781005U
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Abstract
The utility model discloses a card groove pull formula anaerobism gravity flows dynamic membrane bioreactor, including reaction tank and the vertical membrane module of locating in the reaction tank, be equipped with water inlet and outlet on the reaction tank, the water inlet is used for introducing sewage, the outlet is used for discharging the water after handling, the reaction tank top surface is equipped with the apron in order to seal the reaction tank, and the reaction tank bottom of the pool is equipped with the draw-in groove that corresponds with the membrane module, the membrane module inlays the card and establishes in the reaction tank to fall into reaction first district and reaction two districts with the reaction tank, the water inlet sets up the reaction tank bottom that corresponds in reaction first district, the outlet sets up on the reaction tank lateral wall upper portion that two districts of reaction correspond, and the sewage of being convenient for relies on gravity to handle the back through the membrane module and discharges from drain outlet department. The reaction device can effectively remove organic pollutants in the wastewater, reduce the turbidity of the wastewater, and has the advantages of low running cost and convenient replacement and cleaning of the dynamic membrane.
Description
Technical Field
The utility model belongs to the technical field of sewage treatment, concretely relates to card groove pull formula anaerobism gravity flow dynamic membrane biological reaction unit.
Background
The Membrane Bioreactor (MBR) is a novel sewage treatment process combining membrane separation with the traditional sewage biological treatment technology, and is mainly characterized in that a membrane component is used for filtering to replace a secondary sedimentation tank in the conventional activated sludge process, so that sludge-water separation and sludge concentration are realized. The membrane bioreactor is divided into an aerobic membrane bioreactor and an anaerobic membrane bioreactor according to whether the aerobic membrane is aerobic or not, and is divided into a split type membrane bioreactor and an integrated type membrane bioreactor according to different arrangement positions of membrane components.
Compared with the traditional activated sludge process, the microfiltration membrane or ultrafiltration membrane in the MBR retains all biomass in the reactor, enriches functional microorganisms, has the advantages of high effluent quality, high organic load bearing capacity, strong impact load resistance, low sludge yield, strong pollutant removal capacity and the like, and is widely applied to the fields of industrial and urban wastewater treatment and reuse water. In view of the fact that most of the existing MBR processes adopt a pump to pump out water, the price of a membrane component is high, and the flux caused by membrane pollution is rapidly reduced, so that the operation cost is high, and the popularization of the MBR technology is limited.
In recent years, the dynamic membrane process adopts cheap large-aperture membrane materials to replace microfiltration/ultrafiltration membranes in the MBR process, and forms a dynamic membrane on the surface of the membrane through sludge or other materials, thereby playing a role in solid-liquid separation. Anaerobic dynamic membrane bioreactors (AnDMBR) are an emerging technology that combines dynamic membrane with anaerobic treatment and applies to activated sludge processes. Compared with the traditional anaerobic process, the anaerobic dynamic membrane bioreactor has unique advantages and characteristics: can generate energy gas, generates less residual sludge, can realize no sludge discharge, has high organic matter removal rate, does not need aeration, has lower energy consumption, and gradually arouses the wide attention of scholars in the field of membrane technology sewage treatment and resource utilization. The formation of the anaerobic dynamic membrane is divided into two stages: the first stage is the formation stage of the anaerobic dynamic membrane, and anaerobic sludge is deposited on the surface of the membrane to form a sludge layer, namely the anaerobic dynamic membrane in the filtering process; the second stage is a stable mature stage of the anaerobic dynamic membrane, good filtering performance can be obtained during stable operation, but finally, a large amount of sludge is deposited and adsorbed on the membrane, so that the dynamic membrane thickness is increased, the pore diameter is reduced, the filtering resistance is increased, and membrane pores are blocked to cause membrane pollution. In general, there are many technical problems to be solved in the anaerobic dynamic membrane bioreactor sewage treatment technology, such as: the occupied area is large, and the operating cost is high; the treatment efficiency is low; the filter membrane is inconvenient to replace and the operation is complex; high difficulty in cleaning the membrane, etc.
Disclosure of Invention
The above-mentioned not enough to prior art exists, the utility model aims at providing a card groove pull formula anaerobism gravity flow dynamic membrane biological reaction device, this reaction device can effectively get rid of the organic pollutant in the waste water, reduces waste water turbidity, and the running cost is low simultaneously, and dynamic membrane is changed, is washd conveniently.
The technical scheme of the utility model is realized like this:
the utility model provides a card groove pull formula anaerobism gravity flows dynamic membrane bioreactor, includes reaction tank and the vertical membrane module of locating in the reaction tank, is equipped with water inlet and outlet on the reaction tank, the water inlet is used for introducing sewage, the outlet is used for the water after the discharge treatment, the reaction tank top surface is equipped with the apron in order to seal the reaction tank, is equipped with the draw-in groove that corresponds with the membrane module at the bottom of the reaction tank, the membrane module inlays to be inserted and blocks and establishes in the reaction tank to fall into reaction first district and reaction second district with the reaction tank, the water inlet sets up the reaction tank bottom that corresponds in reaction first district, the outlet sets up on the reaction tank lateral wall upper portion that corresponds in reaction second district, and the sewage of being convenient for relies on gravity to discharge from drain outlet department after membrane module processing.
Furthermore, the clamping grooves are arranged side by side, so that the membrane component can be conveniently replaced in the sewage treatment process.
Furthermore, the membrane modules are of a plate type structure and are provided with two groups, the two groups of membrane modules are arranged at intervals, and the region between the two groups of membrane modules forms the first reaction region.
Furthermore, the membrane module is composed of a rectangular supporting frame, a nylon gauze layer and a honeycomb-shaped biochemical cotton layer, the nylon gauze layer and the honeycomb-shaped biochemical cotton layer are flatly laid in the supporting frame and isolate two sides of the supporting frame, and meanwhile, the honeycomb-shaped biochemical cotton layer faces to the first reaction area.
Furthermore, a sealing assembly is arranged at the joint of the nylon gauze layer and the honeycomb biochemical cotton layer with the supporting frame, so that the peripheries of the nylon gauze layer and the honeycomb biochemical cotton layer form a sealing structure with the supporting frame, and the sewage in a reaction area is ensured to pass through the honeycomb biochemical cotton layer and the nylon gauze layer in sequence.
Furthermore, a tooth surface type suspension filler is arranged in the first reaction zone; the membrane component cleaning device is characterized by further comprising a stirring unit, wherein the stirring unit comprises a motor, a stirring shaft and blades, the motor is placed on the cover plate, a through hole is formed in the cover plate corresponding to the center of the first reaction region, the stirring shaft is located in the first reaction region and penetrates through the cover plate to be connected with an output shaft of the motor, and the blades are arranged at the lower end of the stirring shaft, so that the motor can be started to drive the blades to stir sewage in the first reaction region to clean the membrane component.
Furthermore, the motor is connected with the control unit, so that the control unit can control the motor to be started and stopped intermittently, and damage caused by overload operation of the motor is avoided.
Furthermore, an exhaust port is arranged on the cover plate, and a gas collection container is arranged at the exhaust port and used for collecting gas generated in the reaction tank.
Furthermore, a sludge discharge pipe is arranged in the reaction tank, one end of the sludge discharge pipe is positioned in the first reaction area, and the other end of the sludge discharge pipe is positioned outside the reaction tank and used for discharging sludge in the first reaction area of the reaction tank.
And furthermore, a biofilm filler is arranged in the second reaction area and is fixedly arranged in the second reaction area.
Compared with the prior art, the utility model discloses following beneficial effect has:
1. the utility model arranges the clamping groove at the bottom of the reaction tank, so that the membrane component can be replaced by drawing, and the installation is convenient; meanwhile, a plurality of clamping grooves are arranged, when the membrane component needs to be replaced, a new membrane component can be inserted into the corresponding clamping groove on the outer side of the membrane component, and then the membrane component needing to be replaced is taken out and cleaned, so that sludge in the first reaction area and untreated sewage can be effectively prevented from entering the second reaction area, and the sewage treatment effect is ensured.
2. The membrane component of the utility model is made of nylon gauze, honeycomb biochemical cotton and a supporting frame for supporting, thereby effectively reducing the manufacturing cost of the membrane; the structure of the honeycomb biochemical cotton is a three-layer filter cloth structure, the honeycomb biochemical cotton has a pore passage structure with certain thickness and compactness, the dynamic membrane is prevented from being compacted, the service life is prolonged, and meanwhile, the 3D weaving process of the honeycomb biochemical cotton can enhance the attachment of microorganisms in suspended sludge to form a more compact biological membrane. The aperture of the nylon gauze is far smaller than that of the biochemical cotton, so that mud leakage can be prevented, and in addition, a biomembrane can be formed on the surface of the nylon gauze to enhance the filtering effect.
3. The membrane component of the utility model can be cleaned in situ or cleaned in different positions, and the cleaning method is simple and the running cost is low. Adding a tooth-surface type suspended filler into the reaction tank and accelerating the stirring speed to enable the filler to scrape the biological membrane to realize the purpose of in-situ cleaning of the membrane; when the membrane assembly needs to be replaced, a new membrane assembly is inserted into the clamping groove on the outer side of the old membrane assembly, and then the old membrane assembly is taken out to be cleaned in an ex-situ mode.
Drawings
Fig. 1-the structure of the present invention.
FIG. 2 is a graph showing the change of turbidity of sewage treated by membrane modules of 600 meshes and 1000 meshes.
FIG. 3-600 mesh and 1000 mesh membrane modules are used for treating COD change of sewage.
Wherein: 1-a reaction tank; 1 a-reaction zone one; 1 b-reaction zone two; 2-a card slot; 3-a membrane module; 4-a motor; 5-stirring shaft; 6-blade; 7-a control unit; 8-cover plate; 9-an exhaust port; 10-a water inlet; 11-drainage port.
Detailed Description
The present invention will be described in further detail with reference to the accompanying drawings and specific embodiments.
Referring to fig. 1, a trough pull type anaerobic gravity flow dynamic membrane bioreactor comprises a reaction tank 1 and a membrane module 3 arranged in the reaction tank, wherein a water inlet 10 and a water outlet 11 are arranged on the reaction tank 1, the water inlet 10 is used for introducing sewage, the water outlet 11 is used for discharging treated water, a cover plate 8 is arranged on the top surface of the reaction tank 1 to seal the reaction tank 1, a clamping groove 2 corresponding to the membrane module 3 is arranged at the bottom of the reaction tank 1, the membrane module 3 is inserted and clamped in the reaction tank 1 to divide the reaction tank 1 into a first reaction area 1a and a second reaction area 1b, the water inlet 10 is arranged at the bottom of the reaction tank 1 corresponding to the first reaction area 1a, and the water outlet 11 is arranged at the upper part of the side wall of the reaction tank 1 corresponding to the second reaction area 1b to facilitate the discharge of sewage from the water outlet 11 after the sewage is treated by the membrane module 3 by gravity.
The reaction tank can be a rectangular tank or a circular tank, the membrane component can be in a plate type structure or an annular structure, the membrane component in the plate type structure and the membrane component in the annular structure can be arranged in the rectangular tank, the membrane component in the plate type structure and the membrane component in the annular structure can be arranged in the circular tank, and the reaction tank is only required to be divided into a first reaction area and a second reaction area. Therefore, after entering the first reaction area, the sewage enters the second reaction area through the membrane component under the action of gravity and is discharged from a water outlet arranged in the second reaction area. When the membrane module is seriously polluted, the membrane module can be pulled and taken out and replaced by a new membrane module, the operation is convenient, and meanwhile, the taken-out membrane module is also conveniently cleaned in different positions.
During specific implementation, the clamping grooves 2 are arranged side by side, so that a new membrane assembly is inserted and then an old membrane assembly is taken out, and the sewage treatment effect is not influenced.
When the membrane module is replaced, if the membrane module is directly taken out, sludge in the first reaction area and untreated sewage directly enter the second reaction area, and the sewage treatment effect is affected. A plurality of clamping grooves are arranged, so that a new membrane assembly can be inserted into the clamping groove on the inner side or the outer side of the membrane assembly for replacement before the membrane assembly needing replacement is taken down, and the sewage treatment effect cannot be influenced. Here, the number of the clamping grooves is two or more, and when two clamping grooves are arranged, the membrane modules can be alternately inserted into the two clamping grooves, so that the replacement of new and old membrane modules is realized, and the operation is simple and convenient.
Meanwhile, if a new membrane module is inserted into the clamping groove in the first reaction zone as a replacement, a small amount of sewage and sludge between the old membrane module and the new membrane module can directly enter the second reaction zone, so that in order to prevent the sewage in the first reaction zone from entering the second reaction zone without being treated by the membrane module, in the sewage treatment process, the membrane module is inserted into the first clamping groove in the first reaction zone in advance, then the new membrane module is gradually inserted into the clamping groove close to the first reaction zone for replacement in the subsequent replacement process, the clamping grooves can be arranged into a plurality of clamping grooves, the quantity of the clamping grooves meeting the sequential operation period is preferably estimated, and when the membrane module on the clamping groove on the outermost side needs to be replaced, the sludge is regularly cleaned, so that the sewage treatment effect is ensured.
Certainly, what number of clamping grooves are specifically arranged can be determined according to actual needs, sewage treatment effects and the like.
In specific implementation, the membrane modules 3 are of a plate type structure and have two groups, the two groups of membrane modules 3 are arranged at intervals, and the region between the two groups of membrane modules 3 forms the first reaction region 1 a. Therefore, the reaction tank is divided into a first reaction area and two second reaction areas, and the treated water body can be discharged from the water outlets corresponding to the two second reaction areas.
When the membrane assembly is specifically implemented, the membrane assembly 3 is composed of a rectangular supporting frame, a nylon gauze layer and a honeycomb-shaped biochemical cotton layer, the nylon gauze layer and the honeycomb-shaped biochemical cotton layer are flatly laid in the supporting frame and isolate two sides of the supporting frame, and meanwhile, the honeycomb-shaped biochemical cotton layer faces to a reaction first area. The honeycomb biochemical cotton layer can provide a carrier for the attachment growth of microorganisms, the structure of the honeycomb biochemical cotton is a three-layer filter cloth structure, the honeycomb biochemical cotton has a pore structure with a certain thickness and compactness, the membrane assembly can be effectively relieved from being compacted, the service life is prolonged, and the 3D stereo weaving process can enhance the attachment of the microorganisms in the suspended sludge to form a more compact biological membrane. In the sewage treatment process, anaerobic microorganisms are accumulated in the 3D mesh structure of the honeycomb biochemical cotton and secrete microorganism Extracellular Polymers (EPS) to gradually form a layer of biological membrane, so that the biodegradation performance is enhanced. Meanwhile, the honeycomb biochemical cotton also plays a role in membrane filtration, a thicker biological membrane is formed on the outer surface of the honeycomb biochemical cotton, the interception performance of the honeycomb biochemical cotton is improved, and the honeycomb biochemical cotton has a filtration function. However, because the suspended sludge particles have smaller diameters and are easy to run off through the honeycomb-shaped biochemical cotton, and the turbidity of the effluent is increased, a layer of nylon gauze with smaller pore diameters is added on the outer side of the honeycomb-shaped biochemical cotton. In the using process, a layer of dynamic membrane is also generated on the surface of the nylon net, and the dynamic membrane further removes soluble organic matters in water through the interception function of membrane pores and the adsorption function of membrane surfaces and the membrane pores, so that the filtering function is enhanced.
When the device is specifically implemented, the sealing assembly is arranged at the joint of the nylon gauze layer and the honeycomb biochemical cotton layer with the supporting frame, so that the peripheries of the nylon gauze layer and the honeycomb biochemical cotton layer form a sealing structure with the supporting frame, and the sewage in a reaction area is ensured to sequentially pass through the honeycomb biochemical cotton layer and the nylon gauze layer.
In specific implementation, a tooth-surface type suspension filler is arranged in the first reaction zone 1 a; still include the stirring unit, the stirring unit includes motor 4, (mixing) shaft 5 and blade 6, motor 4 places on apron 8 to be equipped with the through-hole on the apron 8 that the center of reaction district 1a corresponds, the (mixing) shaft 5 is located reaction district 1a and passes apron 8 and motor 4 output shaft, blade 6 sets up at (mixing) shaft 5 lower extreme, is convenient for starter motor 4 to drive blade 6 and rotates in order to implement the stirring in order to wash the membrane module to the sewage in reaction district 1 a.
The tooth surface type suspension filler is cylindrical, the polyethylene plastic is used as a main material, the appearance is in an outer ratchet shape, and the inner wall of the filler is provided with a cross rib reinforcing structure. The tooth-surface type filler accelerates the stirring speed at a certain adding ratio, so that the tooth-surface type filler fully flows along with water in the reaction tank, and the attachment on the surface of the membrane is cleaned by scrubbing with the honeycomb biochemical cotton, so that the membrane pollution is effectively reduced, and the service life of the membrane is prolonged. Meanwhile, an attachment place is provided for microorganisms in the anaerobic membrane separation device, the biomass is improved, and the degradation performance of pollutants is enhanced.
Meanwhile, a sealing washer can be sleeved on the stirring shaft for sealing in consideration of the sealing effect of the through hole of the cover plate.
During specific implementation, the motor 4 is connected with the control unit 7, so that the control unit 7 can control the motor 4 to be intermittently started and stopped, and damage caused by overload operation of the motor 4 is avoided.
During specific implementation, the cover plate 8 is provided with an exhaust port 9, and a gas collection container is arranged at the exhaust port 9 and used for collecting gas generated in the reaction tank. Methane gas can be generated by anaerobic reaction in the reaction tank, and can be recycled after being collected by the gas collection container.
During specific implementation, a sludge discharge pipe is arranged in the reaction tank 1, one end of the sludge discharge pipe is positioned in the first reaction area, and the other end of the sludge discharge pipe is positioned outside the reaction tank and used for discharging sludge in the first reaction area of the reaction tank.
In specific implementation, the second reaction zone 1b is provided with a biofilm filler, and the biofilm filler is fixedly arranged in the second reaction zone 1 b.
The biofilm filler is fixedly arranged in the reaction zone II, when the membrane component is replaced, the biofilm filler cannot enter the reaction zone I, and meanwhile, the biofilm filler is arranged in the reaction zone II to carry out deep treatment on a water body entering the reaction zone II, so that the removal effect of pollutants is enhanced.
Examples
The internal length x internal width x internal height of the reaction cell is: 20 cm is multiplied by 30 cm is multiplied by 50 cm, the effective volume is 30L, and the glass is made of organic glass. Two plate-type membrane assemblies are symmetrically arranged in the reactor, membrane substrates are made of honeycomb biochemical cotton and nylon gauze, the membrane assemblies are 36 cm in length and 16 cm in width, and the total area of effective filtration membranes is 0.1152 m2. The height of the membrane module is 40 cm, and the volume in the membrane is 9.6L. Water is continuously fed, and the flow rate is 0.8L/h. Setting the hydraulic retention time to be 12 h, regularly recording the water outlet flux and the liquid level change height at two sides every day, and avoiding the sewage and sludge in the first reaction zone from overflowing from the upper part of the membrane component to enter the second reaction zone; collecting water inflow, sludge supernatant and water outflow samples at regular intervals, determining COD, polysaccharide and protein in various water samples, and determining the sludge concentration at regular intervals; when the film is seriously polluted, the film is cleaned by adding the tooth surface type suspension filler and accelerating the stirring speed. The running effect of the reactor is evaluated by the quality of inlet and outlet water.
The film forming components are made of 600-mesh nylon gauze and 1000-mesh nylon gauze and honeycomb biochemical cotton in sequence for experiments, and are respectively referred to as 600-mesh film components and 1000-mesh film components hereinafter.
The inlet water is simulated domestic wastewater, CODCrThe content is 300-500 mg/L, the polysaccharide content is 300-350 mg/L, and the protein content is 40-50 mg/L.
When the device is started, anaerobic flocculent sludge is inoculated, and the sludge concentration (TSS) is 5.5 g/L.
In the operation process, the change situation of the effluent turbidity and the change situation of the effluent COD are respectively shown in fig. 2 and fig. 3, and as can be seen from fig. 2, the effluent turbidity after the domestic wastewater is treated is in a descending trend along with the extension of the operation time, which shows that the activated sludge and the membrane component in the reactor have good removal effect on the turbidity of the domestic wastewater, and the 600-mesh membrane component has better treatment effect than the 1000-mesh membrane component; as can be seen from FIG. 3, the COD of the treated domestic wastewater is in a whole descending trend along with the prolonging of the operation time, which shows that the organic pollutants in the domestic wastewater are degraded by the activated sludge in the mixed liquid and are intensively removed by the dynamic membrane, and after the domestic wastewater is operated for a period of time, the COD removal effect of the 1000-mesh membrane module is better than that of the 600-mesh membrane module. The results of measuring polysaccharide, protein and COD in the inlet water, the outlet water and the sludge supernatant are shown in tables 1 and 2 respectively.
TABLE 1.600 mesh measurement results of wastewater treatment
| Polysaccharide (mg/L) | Protein (mg/L) | COD（mg/L） | |
| Inflow water | 353.52 | 45.60 | 439.59 |
| Supernatant fluid | 36.84 | 40.43 | 179.95 |
| Discharging water | 6.46 | 11.21 | 80.23 |
| Dynamic biofilm rejection rate | 82.46% | 72.27% | 55.42% |
| Reaction apparatus removal rate | 98.17% | 75.42% | 81.75% |
TABLE 2.1000 mesh measurement results of wastewater treatment
| Polysaccharide (mg/L) | Protein (mg/L) | COD（mg/L） | |
| Inflow water | 337.36 | 50.77 | 430.38 |
| Supernatant fluid | 21.43 | 33.10 | 158.42 |
| Discharging water | 3.04 | 8.92 | 65.56 |
| Dynamic biofilm rejection rate | 85.81% | 73.05% | 58.62% |
| Reaction apparatus removal rate | 99.10% | 82.42% | 84.77% |
Experimental results show that after most pollutants in domestic sewage are degraded by activated sludge in the mixed liquor, the residual pollutants are further removed by the dynamic membrane in an enhanced manner, and the enhanced removal effect comprises the effects of on-membrane microbial degradation and membrane interception.
In addition, in the experimental process, the membrane pollution speed is 0.026 cm/h by adopting a 600-mesh membrane component; the membrane pollution speed is 0.053 cm/h by adopting a 1000-mesh membrane component. Therefore, compared with the 1000-mesh membrane module, the 600-mesh membrane module is slower in blockage and longer in operation period. Comparing table 1 and table 2, it can be seen that, because the pore diameter of the 1000-mesh membrane module is smaller, the microorganisms in the activated sludge form a more compact biological membrane on the membrane surface, the retention rate of the dynamic biological membrane is slightly higher than that of the 600-mesh membrane module, but the overall removal effect is not very different.
Under the stirring state, after running for 30 min, a 600-mesh membrane component is adopted, and the membrane pollution speed is 0.978 cm/h; a1000-mesh membrane component is adopted, and the membrane pollution speed is 1.059 cm/h. Adding a tooth-surface type suspension filler, accelerating the stirring speed and running for 30 min, and then adopting a 600-mesh membrane component, wherein the membrane pollution speed is 0.259 cm/h; the membrane pollution speed is 0.191 cm/h by adopting a 1000-mesh membrane component. Therefore, when the film is seriously polluted, the tooth-surface type suspension filler can be added and the stirring speed is increased, so that the purpose of cleaning the film can be achieved.
Finally, it should be noted that the above-mentioned embodiments of the present invention are only examples for illustrating the present invention, and are not limitations to the embodiments of the present invention. Variations and modifications in other variations will occur to those skilled in the art upon reading the foregoing description. Not all embodiments are exhaustive. All obvious changes or variations which are introduced by the technical solution of the present invention are still within the scope of the present invention.
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| CN113149205A (en) * | 2021-05-13 | 2021-07-23 | 西南大学 | Draw-in groove pull type anaerobic gravity flow dynamic membrane biological reaction device |
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| CN113149205A (en) * | 2021-05-13 | 2021-07-23 | 西南大学 | Draw-in groove pull type anaerobic gravity flow dynamic membrane biological reaction device |
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