CN220165962U - Sewage treatment system with external MBR membrane module of gas stripping circulation - Google Patents
Sewage treatment system with external MBR membrane module of gas stripping circulation Download PDFInfo
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- CN220165962U CN220165962U CN202321551174.8U CN202321551174U CN220165962U CN 220165962 U CN220165962 U CN 220165962U CN 202321551174 U CN202321551174 U CN 202321551174U CN 220165962 U CN220165962 U CN 220165962U
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- biochemical
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- 239000012528 membrane Substances 0.000 title claims abstract description 181
- 239000010865 sewage Substances 0.000 title claims abstract description 45
- 238000011001 backwashing Methods 0.000 claims abstract description 35
- 239000010802 sludge Substances 0.000 claims abstract description 32
- 238000010992 reflux Methods 0.000 claims abstract description 22
- 238000006243 chemical reaction Methods 0.000 claims abstract description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 54
- 239000007788 liquid Substances 0.000 claims description 19
- 238000005276 aerator Methods 0.000 claims description 16
- 230000001105 regulatory effect Effects 0.000 claims description 16
- 238000004519 manufacturing process Methods 0.000 claims description 7
- 239000003899 bactericide agent Substances 0.000 claims description 4
- 238000003860 storage Methods 0.000 claims description 4
- 230000000844 anti-bacterial effect Effects 0.000 claims description 3
- 238000011144 upstream manufacturing Methods 0.000 claims description 3
- 238000000034 method Methods 0.000 abstract description 16
- 238000000926 separation method Methods 0.000 abstract description 10
- 239000011259 mixed solution Substances 0.000 abstract description 7
- 238000005516 engineering process Methods 0.000 abstract description 4
- 238000004062 sedimentation Methods 0.000 abstract description 3
- 238000001471 micro-filtration Methods 0.000 abstract description 2
- 239000000243 solution Substances 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 20
- 238000004140 cleaning Methods 0.000 description 18
- 239000000126 substance Substances 0.000 description 15
- 238000005273 aeration Methods 0.000 description 10
- 238000010586 diagram Methods 0.000 description 7
- 230000008569 process Effects 0.000 description 7
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 description 6
- 238000007599 discharging Methods 0.000 description 6
- 238000005201 scrubbing Methods 0.000 description 6
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 4
- 239000003814 drug Substances 0.000 description 4
- 229910052698 phosphorus Inorganic materials 0.000 description 4
- 239000011574 phosphorus Substances 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 208000034699 Vitreous floaters Diseases 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000003344 environmental pollutant Substances 0.000 description 3
- 239000012510 hollow fiber Substances 0.000 description 3
- 230000014759 maintenance of location Effects 0.000 description 3
- 231100000719 pollutant Toxicity 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 239000005708 Sodium hypochlorite Substances 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000012459 cleaning agent Substances 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000000835 fiber Substances 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 230000004907 flux Effects 0.000 description 2
- 244000005700 microbiome Species 0.000 description 2
- 230000001546 nitrifying effect Effects 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 235000015097 nutrients Nutrition 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 230000001376 precipitating effect Effects 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 238000004220 aggregation Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 239000013043 chemical agent Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000003426 chemical strengthening reaction Methods 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000002791 soaking Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
- 238000001363 water suppression through gradient tailored excitation Methods 0.000 description 1
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- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The utility model discloses a sewage treatment system with an external gas stripping circulation MBR (Membrane biological reactor) membrane assembly, which comprises a sewage pretreatment system, a split membrane bioreactor and a backwashing system; the sewage pretreatment system is communicated with the split type membrane bioreactor, and the split type membrane bioreactor is communicated with the backwashing system; the split membrane bioreactor comprises a biochemical pool and a membrane pool which are communicated with each other, wherein the biochemical pool is communicated with a sewage pretreatment system, and the membrane pool is communicated with a backwashing system; the membrane tank is communicated with the biochemical tank through the gas stripping reflux system and is used for refluxing the mixed solution of the membrane tank to the aerobic section of the biochemical tank through the gas stripping reflux system for denitrification reaction. The utility model greatly strengthens the function of the bioreactor by the membrane separation technology, the membrane bioreactor can improve the activated sludge amount to more than 5000mg/L by the interception function of the microfiltration membrane, the sludge load is improved, the tank solution is smaller than that required by the conventional activated sludge method, and the sedimentation, the filter tank and the like of the traditional biological treatment method are omitted.
Description
Technical Field
The utility model relates to a sewage treatment system with an external gas stripping circulation MBR membrane assembly, and belongs to the technical field of sewage treatment.
Background
Conventional MBR process membrane separation includes the following parts: the device comprises a circulating system, a membrane assembly device, a suction system, an aeration cleaning system and a backwashing dosing system. The problems of large occupied area, high running cost and the like exist.
Disclosure of Invention
The utility model aims to provide a sewage treatment system with an external gas stripping circulation MBR membrane component, which can solve the technical problems in the background technology.
In order to solve the technical problems, the utility model adopts the following technical scheme:
a sewage treatment system with an external gas stripping cycle MBR membrane component comprises a sewage pretreatment system, a split membrane bioreactor and a backwashing system; the sewage pretreatment system is communicated with the split type membrane bioreactor, and the split type membrane bioreactor is communicated with the backwashing system; the split membrane bioreactor comprises a biochemical pool and a membrane pool which are communicated with each other, wherein the biochemical pool is communicated with a sewage pretreatment system, and the membrane pool is communicated with a backwashing system; the membrane tank is communicated with the biochemical tank through the gas stripping reflux system and is used for refluxing the mixed solution of the membrane tank to the aerobic section of the biochemical tank through the gas stripping reflux system for denitrification reaction. An aeration device is arranged at the bottom of the membrane component, turbulence is generated by large bubble aeration, the surfaces of the hollow fiber membrane filaments are flushed, and dead angles, which are easy to accumulate mud, among the membrane filaments are eliminated to the greatest extent. The assembly adopts a water collecting mode at two ends, and the membrane area is fully utilized. The system adopts the gas stripping device to replace a mixed liquid reflux pump in a circulating system, and the gas source of the gas stripping device is from scrubbing air of the membrane device without increasing gas quantity, and the residual pressure of the scrubbing air is utilized to enable the gas stripping reflux pipe and the biochemical tank to generate liquid level difference, so that the mixed liquid is refluxed to the biochemical tank.
The external membrane separation system and the gas circulation system are combined, so that the method is a novel membrane bioreactor wastewater treatment technology. It has the following advantages: 1. the active sludge and macromolecular organic substances in the biological reaction tank are intercepted by utilizing the membrane separation component, so that the concentration of the active sludge is improved, and meanwhile, the Hydraulic Retention Time (HRTS) and the Sludge Retention Time (SRT) can be respectively controlled, thereby being beneficial to reducing the difficulty of system control and improving the quality of effluent; 2. the air stripping device is used for replacing a mixed liquid reflux pump, and the air source is from original scrubbing air of the membrane device, so that the whole energy consumption of the system is reduced.
In the sewage treatment system with the air stripping circulation external MBR membrane assembly, the sewage pretreatment system comprises a grating and an adjusting tank, wherein the grating is positioned at the upstream of the adjusting tank, a lifting pump is arranged in the adjusting tank, and the water outlet end of the lifting pump is positioned in the biochemical tank.
In the sewage treatment system with the gas stripping circulation external MBR membrane component, the system also comprises a fan group, an aerator is arranged in an aerobic zone of the biochemical tank, and the fan group is communicated with the aerator in the aerobic zone; an aerator is arranged in the membrane tank, and the fan group is communicated with the aerator in the membrane tank.
In the sewage treatment system with the air stripping circulation external MBR membrane assembly, the bottom of the membrane tank is provided with the sludge discharge pipe, one end of the sludge discharge pipe is positioned in the membrane tank, the other end of the sludge discharge pipe is positioned outside the membrane tank, and the sludge discharge pump is arranged on the sludge discharge pipe positioned outside the membrane tank.
In the sewage treatment system with the air stripping circulation external MBR membrane component, the air stripping device is adopted to replace a mixed liquid reflux pump in the traditional MBR system; the air source of the air stripping device is from scrubbing air of the membrane device; the stripping tube of the stripping device is wrapped outside the membrane device and is immersed below the liquid level together with the membrane device.
In the sewage treatment system with the air stripping circulation external MBR membrane assembly, the backwashing system comprises a water production tank, the bottom of the water production tank is communicated with the outlet end of a membrane device in a membrane pond through a backwashing pipe, and the backwashing pipe is provided with a backwashing pump; the backwashing pipe is communicated with the dosing pipe, the other end of the dosing pipe is communicated with the bactericide storage tank, and the dosing pipe is provided with a metering pump.
In the sewage treatment system with the air stripping circulation external MBR membrane assembly, the water outlet end of the membrane device in the membrane tank is communicated with the water producing tank through the self-priming pump; the water outlet end of the membrane device in the membrane tank is positioned at the upper part of the membrane device, the water inlet end of the membrane device in the membrane tank is positioned at the lower part of the membrane device, and the aerator in the membrane tank is positioned below the water inlet end of the membrane device; the stripping reflux system is located above the membrane device.
In the sewage treatment system with the gas stripping circulation external MBR membrane component, the system adopts the following sewage treatment method: the sewage firstly passes through a grid to intercept and remove large particles and floaters, and then enters an adjusting tank; the regulating tank is used for regulating water quantity and balancing water quality, so that the load of the subsequent treatment process is reduced; the regulating tank is provided with a pre-aeration system, fine suspended matters in the regulating tank are prevented from precipitating through pre-aeration, partial COD can be removed, and the load of subsequent aerobic biological treatment is reduced.
In the foregoing sewage treatment system with the air stripping circulation external MBR membrane assembly, the sewage treatment method further includes the following contents: the pretreated effluent enters an anoxic zone of a biological tank through a lifting pump of an adjusting tank, and activated sludge enters an anoxic zone after removing part of organic matters and releasing phosphorus by taking BOD which is easy to degrade in the influent water as a carbon source; the mixed liquid of the aerobic section flows back to the anoxic section for denitrification reaction in a vapor lifting mode, nitrogen nutrients in the effluent are reduced, the effluent of the anoxic tank enters the aerobic tank, and BOD removal, nitrification and phosphorus absorption are completed in the aerobic tank.
Compared with the prior art, the membrane bioreactor process greatly strengthens the functions of the bioreactor through a membrane separation technology, and has the following characteristics compared with the traditional process:
(1) The occupied area is small. The membrane bioreactor can increase the activated sludge amount to more than 5000mg/L through the interception function of the microfiltration membrane, the sludge load is increased, the sludge is less dissolved than the tank required by the conventional activated sludge method, and the sedimentation, the filter tank and the like of the conventional biological treatment method are omitted, so that the occupied area and the civil engineering cost are saved.
(2) The quality of the effluent water is good. The water-through pore of the membrane component is smaller than 0.1 mu m, the solid-liquid separation is efficiently carried out, the separation effect is far better than that of the traditional sedimentation tank, and the effluent suspended matters and turbidity are close to zero.
(3) The management is simple. The high-efficiency interception effect of the membrane ensures that microorganisms are completely intercepted in the reactor, thus realizing the complete separation of the Hydraulic Retention Time (HRT) and sludge age (STR) of the reactor, and the operation control is flexible and stable. Full-automatic control can be realized. The daily operation of the whole system can be operated by observing the filtering pressure, so that the processes of detailed analysis of sludge reflux quantity, sludge property, sludge concentration, water quality components and the like are omitted. The treatment system equipment part consists of a membrane component and a suction pump (which can be omitted when water flows out), and the membrane component is assembled according to the region and can be conveniently removed, replaced or cleaned.
(4) The biochemical effect is good. The reactor runs under high volume load, low sludge load and long sludge age, so that the degradation efficiency of refractory organic matters is greatly improved. Is favorable for interception and propagation of nitrifying bacteria, and has high system nitrifying efficiency. The combination of the operation modes can also have the functions of denitrification and dephosphorization. Due to the synergistic effect of the high sludge concentration and the low sludge load of the biological treatment system and the high-grade filtration realized by the membrane separation, the buffer capacity of the whole system is very strong, and the good water quality can be maintained when the system is impacted.
(5) The operation cost is low. The air stripping device is adopted to replace the traditional mixed liquid reflux pump, so that the investment is reduced, and the operation energy consumption is reduced.
(6) Film self-cleaning function. The fiber membrane continuously swings under the stirring of water flow and aeration, and the automatic cleaning function is realized through the friction action between the fiber membrane and the water flow and the bubbles, so that dirt is difficult to form on the membrane surface. After a period of operation, the membrane hole is partially blocked, and the membrane needs to be cleaned by liquid medicine, so that the single group of membranes can be cleaned by liquid medicine without affecting the normal operation of other membranes.
Drawings
FIG. 1 is a schematic diagram of the structure of an embodiment of the present utility model;
FIG. 2 is a schematic diagram of a biochemical tank and a membrane tank in a normal operation state;
FIG. 3 is a schematic diagram of a system of biochemical and membrane tanks in a backwashed, chemically enhanced wash state;
FIG. 4 is a schematic diagram of a biochemical tank and a membrane tank system in an in-line chemical cleaning state.
Reference numerals: the sewage treatment system comprises a 1-sewage pretreatment system, a 2-grid, a 3-regulating tank, a 4-biochemical tank, a 5-split membrane bioreactor, a 6-gas stripping reflux system, a 7-gas stripping reflux device, an 8-sludge pump, a 9-backwashing system, a 10-backwashing pump, a 11-water producing tank, a 12-fan set, a 13-metering pump, a 14-bactericide storage tank, a 15-self-priming pump, a 16-membrane tank, a 17-membrane device, an 18-aerator and a 19-lift pump.
The utility model is further described below with reference to the drawings and the detailed description.
Detailed Description
Example 1 of the present utility model: a sewage treatment system with an external MBR membrane component of a gas stripping cycle comprises a sewage pretreatment system 1, a split membrane bioreactor 5 and a backwashing system 9; the sewage pretreatment system 1 is communicated with the split type membrane bioreactor 5, and the split type membrane bioreactor 5 is communicated with the backwashing system 9; the split membrane bioreactor 5 comprises a biochemical tank 4 and a membrane tank 16 which are communicated with each other, the biochemical tank 4 is communicated with the sewage pretreatment system 1, and the membrane tank 16 is communicated with the backwashing system 9; the membrane tank 16 is communicated with the biochemical tank 4 through the gas stripping reflux system 6, and is used for refluxing the mixed solution of the membrane tank 16 to the aerobic section of the biochemical tank 4 through the gas stripping reflux system 6 for denitrification reaction.
The sewage pretreatment system 1 comprises a grating 2 and an adjusting tank 3, wherein the grating 2 is positioned at the upstream of the adjusting tank 3, a lifting pump 19 is arranged in the adjusting tank 3, and the water outlet end of the lifting pump 19 is positioned in the biochemical tank 4. The gap of the grid 2 is 2 mm, and the material is SS304, so that large-size suspended matters and floaters in water can be trapped, the water pump treatment equipment can be prevented from being blocked, and the treatment load of the subsequent treatment process can be reduced. The residence time of the regulating reservoir in the sewage is 6 hours, the effective volume of the regulating reservoir 3 is 120 cubic meters, and the effective depth is 3 meters.
The system also comprises a fan set 12, an aerator 18 is arranged in the aerobic zone of the biochemical tank 4, and the fan set 12 is communicated with the aerator 18 in the aerobic zone; the membrane tank 16 is provided with an aerator 18, and the fan set 12 is communicated with the aerator 18 in the membrane tank 16.
The bottom of the membrane tank 16 is provided with a mud discharging pipe, one end of the mud discharging pipe is positioned in the membrane tank 16, the other end of the mud discharging pipe is positioned outside the membrane tank 16, and a mud discharging pump 8 is arranged on the mud discharging pipe positioned outside the membrane tank 16.
The backwashing system 9 comprises a water production tank 11, wherein the bottom of the water production tank 11 is communicated with the outlet end of a membrane device 17 in a membrane pool 16 through a backwashing pipe, and a backwashing pump 10 is arranged on the backwashing pipe; the backwash pipe is communicated with a dosing pipe, the other end of the dosing pipe is communicated with a bactericide storage tank 14, and a metering pump 13 is arranged on the dosing pipe.
The water outlet end of the membrane device 17 in the membrane pool 16 is communicated with the water producing tank 11 through a self-priming pump 15; the water outlet end of the membrane device 17 in the membrane tank 16 is positioned at the upper part of the membrane tank, the water inlet end of the membrane device 17 in the membrane tank 16 is positioned at the lower part of the membrane tank, and the aerator 18 in the membrane tank 16 is positioned below the water inlet end of the membrane device 17; the stripping reflux unit 7 is located above the membrane unit 17.
The system adopts the following sewage treatment method: the sewage firstly passes through the grid 2, large particles and floaters are intercepted and removed, and then enters the regulating tank 3; the regulating tank 3 is used for regulating water quantity and balancing water quality, so that the load of the subsequent treatment process is reduced; the regulating tank 3 is provided with a pre-aeration system, fine suspended matters in the regulating tank 3 are prevented from precipitating through pre-aeration, partial COD can be removed, and the load of subsequent aerobic biological treatment is reduced.
The pretreated effluent enters an anoxic zone of a biological tank through a lifting pump 19 of the regulating tank 3, and activated sludge enters an anoxic zone after removing part of organic matters and releasing phosphorus by using BOD which is easy to degrade in the influent water as a carbon source; the mixed liquid of the aerobic section flows back to the anoxic section for denitrification reaction in a vapor lifting mode, nitrogen nutrients in the effluent are reduced, the effluent of the anoxic tank enters the aerobic tank, and BOD removal, nitrification and phosphorus absorption are completed in the aerobic tank.
The water from the biochemical tank 4 enters from a gate of the membrane tank 16, each group of membrane tank 16 is provided with two membrane devices 17, membrane components in the membrane devices 17 are arranged in a layer, a self-contained aeration system is connected with a membrane scrubbing air pipe, a water collecting port is connected to a self-sucking pump inlet corresponding to the system, water in the membrane tank is sucked into the center of each hollow fiber membrane through a filter membrane wall by virtue of vacuum suction force generated by a water pump, and the collected water is discharged into a filtered water main pipe.
When the membrane works, the membrane is automatically stopped or backwashed, so that the service life of the membrane is prolonged, the stable water outlet flow is ensured, and the backwashed water adopts filtered water. Turbulence is generated by adopting large bubble aeration at the bottom of the membrane device 17, so that the surfaces of the hollow fibers are washed, the aggregation of pollutants on the surfaces of the membranes is reduced, and the times of chemical cleaning are reduced.
After continuous operation for several days, the suction negative pressure is gradually increased, the system is subjected to chemical dosing backwashing, namely, a cleaning agent is injected into a backwashing pipeline through a metering pump 13 when the chemical agent is usually citric acid, sodium hypochlorite and the like for backwashing, so that the membrane is cleaned, pollutants attached to the surface of the membrane are removed better, and the membrane flux is recovered.
When the transmembrane pressure difference is 20kPa higher when the membrane surface is clogged than that in the initial stable operation, and when the transmembrane pressure difference cannot be recovered by backwashing or chemical dosing backwashing, chemical recovery cleaning or cleaning is required every half year to one year.
The membrane component chemical recovery cleaning can realize online cleaning without hanging off a membrane pool. Closing a water gate of a membrane tank to be cleaned, discharging sludge in the tank into a regulating tank, performing reverse water pumping for cleaning, then configuring a chemical reagent with higher concentration for soaking and gas scrubbing, and recovering the membrane flux. The chemical cleaning agent can be selected to be alkaline-washed or acid-washed according to different pollutants, and sodium hypochlorite, sodium hydroxide, citric acid and the like are generally adopted.
As shown in FIG. 2, the system schematic diagram of the biochemical tank and the membrane tank in the normal operation state is shown, in this state, N1/N2/N5/N6 is opened, N3/N4/N7 is closed, the water flow direction is that the mixed solution is sucked by N1, and the mixed solution is lifted by the air introduced by N5 and flows back to the biochemical tank from N2. Meanwhile, the membrane component is matched with a suction pump to carry out solid-liquid separation and is discharged from N6.
FIG. 3 is a schematic diagram of a biochemical tank and a membrane tank in a backwash and chemical enhanced washing state, in which N1/N2/N5/N7 is opened and N3/N4/N6 is closed, the water flow direction is that mixed liquid is sucked by N1, and the mixed liquid is lifted by air introduced by N5 and flows back to the biochemical tank from N2. Meanwhile, the membrane component is backwashed by matching with a backwashed pump. The backwash liquid adopts a membrane component to produce water, and the chemical strengthening washing is realized by adding a medicament into the backwash liquid by using a metering pump. The circulation between the membrane module and the biochemical tank is still kept open during the chemical enhanced washing. Preventing local medicine accumulation from damaging the living environment of microorganisms.
FIG. 4 is a schematic diagram of the system of the biochemical tank and the membrane tank in the on-line chemical cleaning state, in which N3/N4/N5 is opened and N1/N2/N6/N7 is closed, the water flow direction is that the mixed solution is sucked by N3, and the mixed solution is lifted by the air introduced by N5 and flows back to the chemical cleaning tank from N4. The chemical in the chemical backwashing tank is prepared in advance, and after the cleaning is finished, N3/N4 is closed and the cleaning waste liquid is discharged. The cleaning box can be removed, so that the occupied area is saved. The cleaning speed of the method is far faster than that of the traditional off-line cleaning mode, and one membrane component can be cleaned independently, and a plurality of membrane components can be cleaned on line simultaneously. The traditional MBR technology is difficult to realize on-line chemical cleaning.
Claims (6)
1. The sewage treatment system with the air stripping circulation external MBR membrane component is characterized by comprising a sewage pretreatment system (1), a split membrane bioreactor (5) and a backwashing system (9); the sewage pretreatment system (1) is communicated with the split type membrane bioreactor (5), and the split type membrane bioreactor (5) is communicated with the backwashing system (9); the split membrane bioreactor (5) comprises a biochemical tank (4) and a membrane tank (16) which are communicated with each other, the biochemical tank (4) is communicated with the sewage pretreatment system (1), and the membrane tank (16) is communicated with the backwashing system (9); the membrane tank (16) is communicated with the biochemical tank (4) through the gas stripping reflux system (6), and is used for carrying out denitrification reaction on the mixed liquid of the membrane tank (16) to the aerobic section of the biochemical tank (4) through the gas stripping reflux system (6).
2. The sewage treatment system with the air stripping circulation external MBR membrane assembly according to claim 1, wherein the sewage pretreatment system (1) comprises a grating (2) and a regulating tank (3), the grating (2) is positioned at the upstream of the regulating tank (3), a lifting pump (19) is arranged in the regulating tank (3), and the water outlet end of the lifting pump (19) is positioned in the biochemical tank (4).
3. The sewage treatment system with the gas stripping cycle external MBR membrane assembly according to claim 1, wherein the system further comprises a fan set (12), an aerator (18) is arranged in an aerobic zone of the biochemical tank (4), and the fan set (12) is communicated with the aerator (18) in the aerobic zone; an aerator (18) is arranged in the membrane tank (16), and the fan group (12) is communicated with the aerator (18) in the membrane tank (16).
4. The sewage treatment system with the air stripping circulation external MBR membrane assembly according to claim 1, wherein a sludge discharge pipe is arranged at the bottom of the membrane tank (16), one end of the sludge discharge pipe is positioned in the membrane tank (16), the other end of the sludge discharge pipe is positioned outside the membrane tank (16), and a sludge discharge pump (8) is arranged on the sludge discharge pipe positioned outside the membrane tank (16).
5. The sewage treatment system with the gas stripping cycle external MBR membrane assembly according to claim 1, wherein the backwashing system (9) comprises a water production tank (11), the bottom of the water production tank (11) is communicated with the outlet end of a membrane device (17) in a membrane pond (16) through a backwashing pipe, and a backwashing pump (10) is arranged on the backwashing pipe; the backwashing pipe is communicated with the dosing pipe, the other end of the dosing pipe is communicated with the bactericide storage tank (14), and the dosing pipe is provided with a metering pump (13).
6. The sewage treatment system with the gas stripping cycle external MBR membrane assembly according to claim 1, wherein the water outlet end of the membrane device (17) in the membrane tank (16) is communicated with the water production tank (11) through a self-priming pump (15); the water outlet end of the inner membrane device (17) of the membrane tank (16) is positioned at the upper part of the inner membrane device, the water inlet end of the inner membrane device (17) of the membrane tank (16) is positioned at the lower part of the inner membrane device, and the aerator (18) in the membrane tank (16) is positioned below the water inlet end of the membrane device (17); the stripping reflux device (7) is integrated in the membrane device (17).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321551174.8U CN220165962U (en) | 2023-06-16 | 2023-06-16 | Sewage treatment system with external MBR membrane module of gas stripping circulation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321551174.8U CN220165962U (en) | 2023-06-16 | 2023-06-16 | Sewage treatment system with external MBR membrane module of gas stripping circulation |
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| Publication Number | Publication Date |
|---|---|
| CN220165962U true CN220165962U (en) | 2023-12-12 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202321551174.8U Active CN220165962U (en) | 2023-06-16 | 2023-06-16 | Sewage treatment system with external MBR membrane module of gas stripping circulation |
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| Country | Link |
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| CN (1) | CN220165962U (en) |
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2023
- 2023-06-16 CN CN202321551174.8U patent/CN220165962U/en active Active
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