CN210620522U - Sewage full-flow treatment system based on MBBR and magnetic separation - Google Patents
Sewage full-flow treatment system based on MBBR and magnetic separation Download PDFInfo
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- CN210620522U CN210620522U CN201921134590.1U CN201921134590U CN210620522U CN 210620522 U CN210620522 U CN 210620522U CN 201921134590 U CN201921134590 U CN 201921134590U CN 210620522 U CN210620522 U CN 210620522U
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Abstract
The utility model discloses a sewage full flow processing system based on MBBR and magnetic separation relates to the sewage purification treatment field. The reactor treats sewage in a mode of combining MBBR and magnetic separation and precipitation, and comprises a primary precipitation hydrolysis tank, a first anoxic tank, a second anoxic tank, a first aerobic tank, a second aerobic tank, a third anoxic tank, a third aerobic tank, a dosing mixing tank, a magnetic seed loading tank, a flocculation reaction tank and a final precipitation tank which are sequentially communicated; the device also comprises a magnetic powder separating device and a magnetic powder recovering device, wherein the magnetic powder separating device is connected with a sludge outlet pipe of the final sedimentation tank, the magnetic powder recovering device is respectively connected with the magnetic powder separating device, the magnetic seed loading tank and the primary sedimentation hydrolysis tank, and a nitrifying liquid return pipe is connected between the second aerobic tank and the first anoxic tank. The utility model discloses a combine the two of MBBR and magnetic separation technique, realized the full index high-efficient processing of pollutant, go out water quality of water index and can reach class earth's surface IV class water standard.
Description
Technical Field
The utility model relates to a sewage purification treatment field, concretely relates to sewage full flow processing system based on MBBR and magnetic separation.
Background
With the continuous implementation of the requirements of national environmental protection policies in recent years, the drainage standards of drainage basins and local sewage in various regions are increasingly strict in order to play a good water defense war and promote the continuous improvement of water environment quality. Under the requirement of high discharge standard, the disadvantages of high energy consumption and high resource consumption of the traditional sewage treatment are changed, and the finding of a sewage treatment process which is stable and reaches the standard, high in efficiency and low in consumption, small in occupied area and simple in operation and maintenance is an important development direction in the field of sewage purification treatment.
The sewage full-flow treatment system in the prior art mainly comprises MBR, MBBR and the like, and related research reports in the prior art mainly include:
CN106630393A discloses an unmanned IFAS or MBBR sewage treatment integrated equipment and system, which includes a closed reaction tank, an aeration device and an electrolytic dephosphorization device, the reaction tank is divided into a biochemical reaction tank and a sedimentation tank from one side to the other side in sequence, a suspension carrier is filled in the biochemical reaction tank, sewage enters from a water inlet arranged on the biochemical reaction tank, the biochemical reaction tank and the sedimentation tank as well as the sedimentation tank and a filter tank are communicated, a water inlet pipe of the electrolytic dephosphorization device is communicated with the sedimentation tank, a water outlet pipe is communicated with the biochemical reaction tank, the biochemical reaction tank is divided into an anaerobic tank, an anoxic chamber and an aerobic tank, TN removal depends on backflow and cannot reach more than 80% of total nitrogen removal rate, and the electrolytic dephosphorization device is adopted, so that the sludge yield and the electrode consumption are large, and the operation cost is high.
CN207259318U discloses rural sewage treatment device of integration, including a jar body and the mud room that is located jar body below, wherein, jar body includes from inside to outside in proper order separated thick grid room, thin grid room, MBR membrane treatment room and oxidation chamber, thick grid room of thin grid room parcel, MBR membrane treatment room parcel thin grid room, the indoor sewage of thin grid overflows to MBR membrane treatment indoor through first overflow mouth, oxidation chamber parcel MBR membrane treatment room, the indoor sewage of MBR membrane treatment overflows to the oxidation chamber through the second overflow mouth, the first row mud mouth of thin grid room bottom, the second row mud mouth of MBR membrane treatment room bottom, and the third row mud mouth of oxidation chamber bottom leads to the mud room. The anoxic pond and the aerobic pond are internally provided with the suspension carrier, the MBR is adopted for solid-liquid separation, the suspension carrier is short in service life, needs to be replaced periodically, and is complex in replacement, the MBR is adopted, investment and operation cost are high, and blockage is easy, so that the equipment cannot normally operate, and the overhauling difficulty is low.
CN206901993U discloses integration MBBR sewage treatment device, including anaerobic tank, oxygen deficiency pond good oxygen pond and the sedimentation tank that connects gradually, however, equipment does not set up the advanced treatment unit, and sedimentation tank goes out water direct discharge, goes out water index especially TP, SS and can't reach one-level A standard.
CN109553196A discloses an anaerobic-aerobic composite bed biofilm reactor and a process thereof, which comprises a reactor tank body, wherein the reactor tank body is pre-embedded in backfill soil, the bottom of the reactor tank body is provided with a fine sand foundation layer and a concrete foundation layer, the interior of the reactor tank body is divided into an anoxic zone, an anaerobic zone, an aerobic zone, a settling zone and a filtering and disinfecting zone, an aeration system and an electric control system are arranged in a matching way, MBBR biological suspension carriers with different proportional quantities are added into the anoxic zone, the anaerobic zone and the aerobic zone, the pure membrane MBBR process still needs a settling tank for sludge-water separation, the floor area is increased, a filter tank is adopted as deep treatment, back washing is needed at regular time, and continuous and stable operation of the process is influenced.
CN106348528A discloses a magnetic loading sedimentation and biological aerated filter composite sewage treatment system, which comprises a magnetic loading sedimentation unit and a biological aerated filter unit, and has the working principle that a coagulant, a flocculant and magnetic powder are respectively added into a magnetic coagulation reactor by a dosing tank and a magnetic separator, sewage to be treated enters the magnetic coagulation reactor through a water inlet to destabilize and flocculate, then enters an inclined tube sedimentation tank to complete primary treatment, most of phosphorus, suspended matters and part of organic matters are removed, and then enters the biological aerated filter to remove ammonia nitrogen and part of organic matters, so that secondary treatment of the sewage is realized. The system design does not allow for removal of total nitrogen and does not meet existing emission standard requirements.
The biochemical treatment is carried out by adopting an activated sludge method, the wastewater is difficult to reach the standard and be discharged under the unfavorable conditions of water inlet impact, low temperature in winter and the like, the system load is low, and the occupied area is large; MBR process membrane modules need to be cleaned on line at regular time and backwashed regularly, have the defects of high manufacturing cost, high energy consumption, special maintenance and the like, and are in urgent need of improvement; the MBBR process needs to be matched with advanced treatment processes such as a high-efficiency sedimentation tank and a filter tank, has the defects of long process flow, large occupied area and the like, and is not favorable for high integration of the process.
In order to improve the water environment quality, realize stable standard reaching of effluent and high-efficiency low-consumption simple operation of equipment, the improvement of the existing sewage full-flow treatment system is urgently needed.
SUMMERY OF THE UTILITY MODEL
Based on the defect that exists among the above-mentioned prior art, the utility model provides a sewage full flow processing system based on MBBR and magnetic separation can ensure that the full index of core index of sewage is up to standard.
The utility model discloses the technical solution who adopts is:
a sewage full-flow treatment system based on MBBR and magnetic separation comprises a reactor, wherein the reactor treats sewage in a mode of combining MBBR and magnetic separation precipitation, the reactor comprises a primary sedimentation hydrolysis tank, a first anoxic tank, a second anoxic tank, a first aerobic tank, a second aerobic tank, a third anoxic tank, a third aerobic tank, a dosing mixing tank, a magnetic seed loading tank, a flocculation reaction tank and a final sedimentation tank which are sequentially communicated, and adjacent tank bodies are communicated;
the device also comprises a magnetic powder separation device and a magnetic powder recovery device, wherein the magnetic powder separation device is connected with the sludge outlet pipe of the final sedimentation tank, and the magnetic powder recovery device is respectively connected with the magnetic powder separation device, the magnetic seed loading tank and the primary sedimentation hydrolysis tank;
suspension carriers are added into the first anoxic tank, the second anoxic tank, the first aerobic tank, the second aerobic tank, the third anoxic tank and the third aerobic tank,
a first stirrer special for a suspension carrier is arranged in the first anoxic tank, the second anoxic tank and the third anoxic tank; the first aerobic tank, the second aerobic tank and the third aerobic tank are internally provided with perforated pipe aerators, and the dosing mixing tank, the magnetic seed loading tank and the flocculation reaction tank are internally provided with a second stirrer, a third stirrer and a fourth stirrer in sequence;
the primary sedimentation hydrolysis tank is connected with a water inlet pipe and a sludge discharge pipe, and the final sedimentation tank is connected with a water outlet pipe;
a nitrifying liquid return pipe is connected between the second aerobic tank and the first anoxic tank, one end of the second aerobic tank is used as a water inlet, and one end of the first anoxic tank is used as a water outlet.
As an optimized proposal of the utility model, the adjacent cell bodies are separated by the clapboard, the clapboard is provided with a water passing hole for keeping the adjacent cell bodies communicated, the water passing hole comprises a primary sedimentation hydrolysis pool water passing hole positioned on the clapboard between the primary sedimentation hydrolysis pool and the first anoxic pool, a first anoxic pool water passing hole positioned on the clapboard between the first anoxic pool and the second anoxic pool, a second anoxic pool water passing hole positioned on the clapboard between the second anoxic pool and the first aerobic pool, a first aerobic pool water passing hole positioned on the clapboard between the first aerobic pool and the second aerobic pool, a second aerobic pool water passing hole positioned on the clapboard between the second aerobic pool and the third anoxic pool, a third anoxic pool water passing hole positioned on the clapboard between the third anoxic pool and the third aerobic pool, a third aerobic pool water passing hole positioned on the clapboard between the third aerobic pool and the magnetic loading pool, a chemical adding mixing pool positioned on the clapboard between the chemical adding mixing pool and the magnetic loading pool, A magnetic seed loading pool water passing opening on a partition plate between the magnetic seed loading pool and the flocculation reaction pool and a flocculation reaction pool water passing opening on a partition plate between the flocculation reaction pool and the final sedimentation pool.
Preferably, an oxygen-poor intercepting screen is arranged in front of the first oxygen-poor pool water passing port, in front of the second oxygen-poor pool water passing port and in front of the third oxygen-poor pool water passing port, the oxygen-poor intercepting screen is a flat screen, the upper edge of the oxygen-poor intercepting screen is 30cm below the operating water level, the lower edge of the oxygen-poor intercepting screen is higher than half of the operating water level, and the operating water level is the same as the mounting height of the lower edge of the water outlet pipe.
Preferably, an aerobic interception screen is arranged in front of the first aerobic tank water passing port, in front of the second aerobic tank water passing port and in front of the third aerobic tank water passing port, the aerobic interception screen is a drum screen, the upper edge of the aerobic interception screen is below 65% of the operating water level, the lower edge of the aerobic interception screen is higher than 35% of the operating water level, and the operating water level is the same as the mounting height of the lower edge of the water outlet pipe.
Preferably, the magnetic powder separation device is connected with the magnetic powder recovery device through a sludge inlet pipe, the magnetic powder recovery device is connected with the magnetic seed loading tank through a magnetic seed return pipe, and the magnetic powder recovery device is connected with the primary sedimentation hydrolysis tank through a sludge return pipe.
Preferably, the density of the above-mentioned suspension carrier is 0.95 to 1.04g/cm3The porosity is more than 90 percent; the density of the suspension carrier in the first anoxic tank, the second anoxic tank and the third anoxic tank is 1.02-1.04g/cm3The effective specific surface area of the suspension carrier is 300-620m2/m3(ii) a Preferably, the density of the suspended carrier in the first aerobic tank is 0.95-0.97g/cm3The density of the suspended carrier in the second aerobic tank and the third aerobic tank is 0.97-0.99g/cm3The effective specific surface area of the suspension carriers in the first aerobic tank and the third aerobic tank is 450-800m2/m3The effective specific surface area of the suspension carrier in the second aerobic tank is 620-1200m2/m3。
Preferably, a nitrifying liquid reflux intercepting screen is arranged at the water inlet of the nitrifying liquid reflux pipe, the nitrifying liquid reflux intercepting screen is a flat screen, the opening direction of the perforated pipe aerator is downward, the opening aperture is 4-6mm, and the installation height is 30cm above the bottom of the tank.
Preferably, the upper edges of the chemical feeding mixing tank water gap and the flocculation reaction tank water gap are 30cm below the operating water level, and the lower edge of the magnetic seed loading tank water gap is level with the bottom of the magnetic seed loading tank.
The utility model discloses the theory of operation does: the advantages of high load and good effect of the pure membrane MBBR process are utilized to treat ammonia nitrogen, total nitrogen and organic matters in the sewage; by utilizing the characteristics that the magnetic separation load is high and the inlet water SS can bear 500mg/L, a mud-water separation system of a pure membrane process is omitted, and the mud-water separation and the advanced treatment of the traditional technology can be realized through magnetic separation, so that the SS and the TP reach the standard; the sludge separated in the magnetic separation process is refluxed to the primary sedimentation hydrolysis tank to reinforce the hydrolysis and recover the carbon source, so that the problem of low utilization efficiency of the pure membrane MBBR process on the carbon source in the form of particle colloid is solved. The sewage enters a primary sedimentation hydrolysis tank Z1 through a water inlet pipe, enters a first anoxic tank Z2 after partial SS removal is finished, is mixed with nitrifying liquid flowing back through a nitrifying liquid return pipe P3, is subjected to denitrification reaction in a first anoxic tank Z2 and a second anoxic tank Z3, then enters a first aerobic tank Z4 and a second aerobic tank Z5 to respectively remove organic matters and ammonia nitrogen, the effluent of the second aerobic tank Z5 enters a third anoxic tank Z6 to perform deep denitrification by utilizing an externally-fed carbon source, then enters a third aerobic tank Z7 to ensure that organic matters in a biochemical section are removed, the effluent of the third aerobic tank Z7 enters a dosing mixing tank Z8, is dosed with PAC, flows into a magnetic seed loading tank Z9, is dosed with magnetic powder, then enters a flocculation reaction tank Z10, after PAM is fully reacted, suspended matters in the water and a flocculating agent form magnetic floc, the magnetic floc, enters a final sedimentation tank Z11 to be precipitated, and the treated water is discharged through a water outlet pipe. Magnetic flocs precipitated at the bottom of the sedimentation tank enter a magnetic powder separation system M1, magnetic seeds and the flocs are separated through shearing force, the magnetic seeds are recovered by a magnetic powder recovery device M2 and returned to a magnetic seed loading tank Z9 for recycling, the flocs flow back to a primary sedimentation hydrolysis tank Z1 to be in contact with inlet water for flocculation and hydrolysis, and residual sludge is discharged through a sludge discharge pipe P2.
Compared with the prior art, the utility model discloses following beneficial technological effect has:
1) the treatment effect is good: the ammonia nitrogen of the effluent of the system is less than 1.5mg/L, TN is less than 5mg/L, TP is less than 0.1mg/L, SS is less than 6mg/L, and the ammonia nitrogen is far higher than the first-class A standard, so that the ammonia nitrogen can stably reach the quasi-IV standard;
2) high load and small occupied area: the equipment is added with an active polymer suspension carrier, the removal load of pollutants is 2-3 times of that of the traditional activated sludge, the magnetic seed addition enhances the floc settling velocity, and the surface load is more than 2 times of that of the high-efficiency sedimentation tank; the MBBR pure membrane process does not need a traditional secondary sedimentation tank, and the magnetic separation does not need a subsequent filter tank; the occupied area can be reduced by 50% compared with the traditional technology on the whole;
3) strong impact load resistance: no matter MBBR or magnetic separation, the water quality and water quantity impact with 100-200% of design load in a short time can be borne;
4) the operation cost is low: the residual sludge flows back to the primary sedimentation hydrolysis tank, and the concentration of the available carbon source is increased by hydrolyzing the sludge; the magnetic separation medicament has high use efficiency, reduces the medicament adding amount by 10-40%, has the magnetic powder recovery rate over 99.5% and has low operation cost;
5) the operation and maintenance are simple: the MBBR pure membrane process is adopted, sludge backflow and back washing are not required, the sludge yield is low, the operation is simple, and meanwhile, due to the absence of activated sludge, the sludge bulking is not required to be worried about; the suspended carrier, the perforated pipe aeration and the interception screen have the service life of more than 15 years, are free from damage and aging, operate and maintenance, and can be widely applied to sewage treatment plants or integrated equipment.
Drawings
The present invention will be further explained with reference to the accompanying drawings:
FIG. 1 is a front view of a sewage full-flow treatment system based on MBBR and magnetic separation.
In the figure: a primary sedimentation hydrolysis tank-Z1, a first anoxic tank-Z2, a second anoxic tank-Z3, a first aerobic tank-Z4, a second aerobic tank-Z5, a third anoxic tank-Z6, a third aerobic tank-Z7, a dosing mixing tank-Z8, a magnetic seed loading tank-Z9, a flocculation reaction tank-Z10, a final sedimentation tank-Z11, a water inlet pipe-P1, a sludge discharge pipe-P2, a nitrified liquid return pipe-P3, a water outlet pipe-P4, a sludge outlet pipe-P5, a sludge inlet pipe-P6, a magnetic seed return pipe-P7, a sludge return pipe-P8, a suspension carrier-S1, a perforated pipe aerator-S2, a first stirrer-S3, an anoxic interception screen-S4, an aerobic interception screen-S5, a nitrified liquid return pipe-S6, a second stirrer-S7 and a third stirrer-S8, a fourth stirrer-S9, a magnetic powder separating device-M1, a magnetic powder recovering device-M2; a primary sedimentation hydrolysis tank water gap-W1, a first anoxic tank water gap-W2, a second anoxic tank water gap-W3, a first aerobic tank water gap-W4, a second aerobic tank water gap-W5, a third anoxic tank water gap-W6, a third aerobic tank water gap-W7, a dosing mixing tank water gap-W8, a magnetic seed loading tank water gap-W9 and a flocculation reaction tank water gap-W10.
Detailed Description
The utility model provides a sewage full flow processing system based on MBBR and magnetic separation, in order to make the utility model discloses an advantage, technical scheme are clearer and more clear, and will combine specific embodiment below, right the utility model discloses further detailed description.
As shown in figure 1, the utility model relates to a sewage full flow processing system based on MBBR and magnetic separation can solve the unstable, too much inconvenient maintenance scheduling problem of equipment of prior art treatment effect.
The utility model discloses sewage full-flow processing system based on MBBR and magnetic separation, it includes the reactor, the reactor is handled sewage through the mode that MBBR and magnetic separation deposit the two combination, this reactor includes many cell bodies, it is first heavy hydrolysis tank Z1, first oxygen deficiency pond Z2, second oxygen deficiency pond Z3 preferably from left to right in proper order, first good oxygen pond Z4, second good oxygen pond Z5, third oxygen deficiency pond Z6, third good oxygen pond Z7, add medicine mixed pool Z8, magnetism kind loading pond Z9, flocculation reaction pond Z10 and final sedimentation pond Z11, in addition still include relevant technology pipeline, technology pipe fitting and suspension carrier S1;
the process pipeline comprises a water inlet pipe P1, a sludge discharge pipe P2, a nitrified liquid return pipe P3, a water outlet pipe P4, a sludge outlet pipe P5, a sludge inlet pipe P6, a magnetic seed return pipe P7 and a sludge return pipe P8;
the process pipe fitting comprises a perforated pipe aerator S2, a first stirrer S3, an anoxic interception screen mesh S4, an aerobic interception screen mesh S5, a nitrified liquid reflux interception screen mesh S6, a second stirrer S7, a third stirrer S8, a fourth stirrer S9, a magnetic powder separation device M1 and a magnetic powder recovery device M2;
suspension carriers S1 are added into the first anoxic tank Z2, the second anoxic tank Z3, the first aerobic tank Z4, the second aerobic tank Z5, the third anoxic tank Z6 and the third aerobic tank Z7; a first stirrer S3 special for suspension carriers is arranged in the first anoxic tank Z2, the second anoxic tank Z3 and the third anoxic tank Z6; perforated pipe aerators S2 are arranged in the first aerobic tank Z4, the second aerobic tank Z5 and the third aerobic tank Z7, and a second stirrer S7, a third stirrer S8 and a fourth stirrer S9 are sequentially arranged in the dosing mixing tank Z8, the magnetic seed loading tank Z9 and the flocculation reaction tank Z10;
the water inlet pipe P1 is communicated with the upper part of the primary sedimentation hydrolysis tank Z1; the sludge discharge pipe P2 is communicated with the bottom of the primary sedimentation hydrolysis tank Z1; one end of a nitrifying liquid return pipe P3 is communicated with the second aerobic tank Z5, and the other end is communicated with the first anoxic tank Z2; a water outlet pipe P4 is communicated with the upper part of the final sedimentation tank Z11; one end of a sludge outlet pipe P5 is communicated with the bottom of the final sedimentation tank Z11, and the other end is communicated with a magnetic powder separation device M1; one end of the sludge inlet pipe P6 is communicated with the magnetic powder separating device M1, and the other end is communicated with the magnetic powder separating device M2; one end of a magnetic seed return pipe P7 is communicated with the magnetic powder separating device M2, and the other end is communicated with a magnetic seed loading pool Z9; one end of a sludge return pipe P8 is communicated with the magnetic powder separating device M2, and the other end is communicated with the upper part of the primary sedimentation hydrolysis tank Z1;
adjacent tank bodies are separated by partition plates, water passing ports for keeping the adjacent tank bodies communicated are arranged on the partition plates, and the primary sedimentation hydrolysis tank Z1 is communicated with the first anoxic tank Z2 by a primary sedimentation hydrolysis tank water passing port W1; the first anoxic tank Z2 is communicated with the second anoxic tank Z3 through an anoxic interception screen S4 and a first anoxic tank water-passing opening W2; the second anoxic tank Z3 is communicated with the first aerobic tank Z4 through an anoxic interception screen S4 and a second anoxic tank water-passing opening W3; the first aerobic tank Z4 is communicated with the second aerobic tank Z5 through an aerobic interception screen S5 and a first aerobic tank water gap W4; the second aerobic tank Z5 is communicated with the third anoxic tank Z6 through an aerobic interception screen S5 and a second aerobic tank water gap W5; a nitrifying liquid reflux intercepting screen S6 is arranged at the bottom of the second aerobic tank; the third anoxic tank Z6 is communicated with the third aerobic tank Z7 through an anoxic interception screen S4 and a third anoxic tank water-passing opening W6; the third aerobic tank Z7 is communicated with the dosing mixing tank Z8 through an aerobic interception screen S5 and a third aerobic tank water gap W7; the dosing mixing tank Z8 is communicated with the magnetic seed loading tank through a water gap W8 of the dosing mixing tank Z9; the magnetic seed loading pool Z9 is communicated with the flocculation reaction pool Z10 through a water outlet W9 of the magnetic seed loading pool; the flocculation reaction tank Z10 is communicated with the final sedimentation tank Z11 through a flocculation reaction tank water gap W10;
the oxygen-poor intercepting screen S4 is preferably a flat screen, the upper edge of the oxygen-poor intercepting screen S4 is 30cm below the operating water level, and the lower edge is higher than half of the operating water level; the aerobic interception screen S5 is preferably a roller screen, the upper edge is below 65% of the operation water level, and the lower edge is higher than 35% of the operation water level; the utility model discloses preferred nitration liquid backward flow interception screen cloth S6 is the flat screen cloth.
The preferred density of the suspension carrier S1 of the utility model is 0.95-1.04g/cm3The porosity is more than 90%. The density of the suspension carrier S1 of the utility model which is preferably arranged in the first anoxic tank Z2, the second anoxic tank Z3 and the third anoxic tank Z6 is 1.02-1.04g/cm3The effective specific surface area of the suspension carrier S1 is 300-620m2/m3. The utility model preferably selects the suspension carrier S1 with the density of 0.95-0.97g/cm which is positioned in the first aerobic tank Z43The density of the suspension carrier S1 in the second aerobic tank Z5 and the third aerobic tank Z8 is 0.97-0.99g/cm3The effective specific surface area of the suspension carrier S1 in the first aerobic tank Z4 and the third aerobic tank Z8 is 450-2/m3The effective specific surface area of the suspension carrier S1 in the second aerobic tank Z5 is 620-1200m2/m3。
The preferred perforated pipe aerator S2 of the utility model has a downward opening direction, an opening aperture of 4-6mm and an installation height of 30cm above the pool bottom.
The utility model discloses the preferred medicine that adds mixes the pond and crosses mouth of a river W10 of crossing of mouth of a river W8, flocculation reaction pond and goes up along 30cm below the operation water level, magnetism kind loading pond cross mouth of a river W9 down along with magnetism kind loading pond Z9's bottom of a pool keep level.
The utility model preferably selects the hydraulic retention time of the primary sedimentation hydrolysis tank to be 3-4h, and the sludge concentration of the mud-water mixing area is 3000-5000 mg/L; the sludge concentration of the first anoxic tank, the second anoxic tank, the first aerobic tank, the second aerobic tank, the third anoxic tank and the third aerobic tank is less than 500 mg/L; the filling rate of the suspension carriers in the first anoxic tank, the second anoxic tank and the third anoxic tank is10-50% and DO less than 0.4 mg/L; the filling rate of the suspended carriers in the first aerobic tank, the second aerobic tank and the third aerobic tank is 30-66%, and the DO is 2-6 mg/L; the hydraulic retention time of the third aerobic tank is 15-30 min; the hydraulic retention time of the chemical adding mixing tank is 1.5-2min, the hydraulic retention time of the magnetic seed loading tank is 1.5-2min, the hydraulic retention time of the flocculation reaction tank is 2-3min, the retention time of the final settling tank is 20-30min, and the surface load is 15-30m3/m2·h。
The utility model selects the MBBR pure membrane form, the biochemical section does not need the sludge reflux, the microorganism mainly grows on the suspension carrier in the form of the biomembrane, the concentration of the suspended sludge in the reactor is less than 500mg/L, the sludge expansion does not occur, and the backwashing is not needed; compared with an activated sludge-biofilm composite process, the nitrification load can be directly increased by increasing the DO in the aerobic zone without worrying about breaking sludge flocs through high aeration, the impact resistance effect is more stable, and the regulation and control are more flexible; the pure membrane process has higher volume load and more comprehensive occupied area.
The utility model discloses select the magnetic separation technique, easy operation need not newly-increased filter unit, and surface load 15 ~ 40m3/m2H, remarkable phosphorus removal advantages, high medicament use efficiency, 10-40% reduction of dosage, land occupation saving and low operation cost.
The utility model selects the suspension carriers with different densities and effective specific surface areas, and the density of the suspension carriers in the first anoxic tank, the second anoxic tank and the third anoxic tank is 1.02-1.04g/cm3Slightly larger than water, so as to avoid the denitrification to generate nitrogen to push the carrier to float and accumulate; the microorganisms attached to the suspension carriers in the first anoxic tank, the second anoxic tank and the third anoxic tank are mainly anoxic heterotrophic bacteria, have sufficient organic matters and thicker biological membrane, and have the effective specific surface area of 300-620m2/m3The internal water passing channel of the suspended carrier is relatively wide, so that good mass transfer of a biological membrane can be guaranteed; the organic load of the first aerobic pool is far higher than that of the second aerobic pool and the third aerobic pool, the biomass and the thickness of the biological membrane are relatively highest, so the density is selected to be 0.95-0.97g/cm3Effective specific surface area of 450-2/m3After the suspended carrier is filmed, the density of the suspended carrier is close to that of water, and the flow channel is wider, so that mass transfer and oxygen transfer are ensured; the second aerobic tankThe organic load of the third aerobic tank is relatively low, the biomass is relatively reduced, and the selected density is 0.97-0.99g/cm3The whole density of the suspended carrier after film forming is similar to that of water, and the fluidization of the carrier can be realized only through aeration disturbance; compared with the third aerobic tank, the second aerobic tank mainly bears the nitrification load, the biofilm with slow growth of nitrifying bacteria is relatively thin, and a suspension method carrier with relatively narrow flow channel and larger effective specific surface area can be selected on the basis of ensuring good mass transfer of the biofilm, so that the second aerobic tank selects the 1200 m-class suspension carrier with the effective specific surface area of 6202/m3The third aerobic tank selects 450-800m2/m3The suspension carrier of (1).
The utility model has the main innovation that the MBBR and the magnetic separation technology are combined, the traditional secondary sedimentation tank is not needed, and the effluent of the biological section can directly enter the deep treatment; the advanced treatment and the backflow to the primary sedimentation hydrolysis tank strengthen the removal of the SS of the inlet water, and simultaneously, the sludge hydrolysis increases the concentration of the available carbon source.
The MBBR pure film form means that the removal of pollutants in the biological section is completed by a biological film on a suspension carrier, the sludge concentration in the reactor is less than 500mg/L, active substances in the sludge are mainly fallen biological films, and the process does not set sludge backflow.
The void fraction of the above-mentioned suspension vehicle means the percentage of the void volume per unit of the suspension vehicle to the total volume.
The effective specific surface area of the suspension carrier refers to the protected surface area of the suspension carrier which can realize good mass and oxygen transfer per unit volume and can grow effective microorganisms.
The filling rate of the suspension carrier refers to the ratio of the volume of the suspension carrier to the volume of the added reaction tank.
The magnetic powder separation device is a device which breaks magnetic powder and residual sludge in floccules through the action of shearing force generated by high-speed rotation on the floccules.
The magnetic powder recovery device is a device for realizing magnetic powder recovery and non-magnetic substance separation under the action of a magnetic field.
As is well known to those skilled in the art, the magnetic powder separation device can be a high shear dispersion emulsifier, which is a standard device; the magnetic powder recovery device is a magnetic separator which is standard equipment, and the type is reasonably selected according to the magnetic powder and the water inlet condition.
The reactor can be a box structure, and if the reactor is the box structure, the main body material can be various materials such as stainless steel, carbon steel, glass fiber reinforced plastics or engineering plastics, and the like, and the technical personnel in the field can select the reactor according to the use requirement.
As is well known to those skilled in the art, the tank capacity and the addition amount of the suspension carrier in each area of the system are determined according to the water quantity, the water quality and the treatment standard; the nitrification liquid reflux ratio, the sludge reflux ratio and the aerobic tank DO meet the basic requirements of the system on sewage treatment.
On the basis of understanding the structure and innovation points of the sewage full-flow treatment system based on MBBR and magnetic separation, the working method is explained in detail.
Example 1:
a sewage full-flow treatment method based on MBBR and magnetic separation comprises the following steps:
a. the sewage to be treated firstly enters a primary sedimentation hydrolysis tank, contacts with return sludge for flocculation, and removes partial colloid and particle pollutants, the sludge is hydrolyzed in the primary sedimentation hydrolysis tank to increase the concentration of soluble organic matters, and the residual sludge is discharged through a sludge discharge pipe;
b. the effluent of the primary sedimentation hydrolysis tank sequentially flows through the first anoxic tank and the second anoxic tank, nitrate carried by the return nitrification liquid is removed through denitrifying bacteria attached and grown on the suspension carriers, and part of organic matters in the raw water are consumed;
c. the effluent of the second anoxic tank enters a first aerobic tank, and the removal of organic matters in raw water is completed through aerobic heterotrophic bacteria attached to and grown on the suspended carriers, wherein the ammonia nitrogen oxidation rate of the effluent of the first aerobic tank is less than 10 percent compared with that of the effluent of the first aerobic tank;
d. the effluent of the first aerobic tank enters a second aerobic tank, the ammonia nitrogen in the raw water is removed through nitrobacteria attached and grown on the suspended carriers, and the ammonia nitrogen in the effluent of the second aerobic tank is less than 1.5 mg/L;
e. the effluent of the second aerobic tank enters a third anoxic tank, deep total nitrogen removal is completed through denitrifying bacteria attached and grown on the suspended carriers, and organic matters required by denitrification can be supplemented by an externally-added carbon source;
f. the effluent of the third anoxic tank enters a third aerobic tank, and the guarantee effect of effluent organic matters is realized through aerobic heterotrophic bacteria attached and grown on the suspension carrier;
g. the effluent of the third aerobic tank sequentially passes through a dosing mixing tank, a magnetic seed loading tank and a flocculation reaction tank, and magnetic seeds and a flocculating agent are respectively added into the magnetic seed loading tank and the flocculation reaction tank, so that granular and colloidal organic matters in the sewage are coagulated into flocs taking the magnetic seeds as 'nuclei';
h. the effluent of the flocculation reaction tank enters a final sedimentation tank to complete sludge-water separation, and the supernatant reaches the discharge standard of sewage and is discharged by a water outlet pipe of the flocculation reaction tank;
i. magnetic floccules at the bottom of the final settling tank enter a magnetic powder separation device, and are scattered through shearing force to form a magnetic powder-floccule mixed solution;
j. the mixed liquid of the water discharged from the magnetic powder separation device enters a magnetic powder recovery device, the recovery of magnetic powder and the separation of non-magnetic flocs are completed under the action of a magnetic field, the recovered magnetic powder flows back to a magnetic seed loading pool to realize the recycling of magnetic seeds, and the residual sludge enters a primary sedimentation hydrolysis pool to be hydrolyzed.
In this embodiment, the process parameters are set as follows:
designed water volume of 30000m for certain municipal sewage plant3D, COD, BOD of the influent water5、NH3The design values of TN, TP and SS are 630, 300, 55, 70, 10 and 450mg/L respectively, and the total hydraulic retention time is 14.2 h; the hydraulic retention time of the primary sedimentation hydrolysis tank is 3h, and the sludge concentration of the mud-water mixing area is 4500-5000 mg/L; the sludge concentration of the first anoxic tank, the second anoxic tank, the first aerobic tank, the second aerobic tank, the third anoxic tank and the third aerobic tank is less than 500 mg/L; the filling rates of the suspended carriers in the first anoxic tank, the second anoxic tank and the third anoxic tank are respectively 50%, 45% and 50%, and DO is less than 0.4 mg/L; the filling rates of the suspended carriers of the first aerobic tank, the second aerobic tank and the third aerobic tank are respectively 50%, 55% and 30%, and DO is 2-6 mg/L; the hydraulic retention time of the third aerobic tank is 20min, and the chemical adding mixing tankThe hydraulic retention time of the flocculation reaction tank is 1.5min, the hydraulic retention time of the magnetic seed loading tank is 1.5min, the hydraulic retention time of the flocculation reaction tank is 2min, the retention time of the final sedimentation tank is 20min, and the surface load is 15m3/m2H, COD, BOD of effluent5、NH3The average values of TN, TP and SS are 14.5, 3.2, 0.34, 4.65, 0.08 and 4.6mg/L respectively.
Example 2:
the difference from the embodiment 1 is that:
the process parameters are set as follows:
the design water quantity of certain integrated equipment is 200m3D, COD, BOD of the influent water5、NH3TN, TP and SS design values are 270, 135, 35, 40, 4.5 and 220mg/L respectively, and the total hydraulic retention time is 8.3 h; the hydraulic retention time of the primary sedimentation hydrolysis tank is 4h, and the sludge concentration of the mud-water mixing area is 3500 and 4000 mg/L; the sludge concentration of the first anoxic tank, the second anoxic tank, the first aerobic tank, the second aerobic tank, the third anoxic tank and the third aerobic tank is less than 500 mg/L; the filling rates of the suspended carriers in the first anoxic tank, the second anoxic tank and the third anoxic tank are respectively 40%, 40% and 40%, and DO is less than 0.4 mg/L; the filling rates of the suspended carriers of the first aerobic tank, the second aerobic tank and the third aerobic tank are respectively 45%, 50% and 35%, and DO is 2-6 mg/L; the hydraulic retention time of the third aerobic tank is 20min, the hydraulic retention time of the chemical adding mixing tank is 2min, the hydraulic retention time of the magnetic seed loading tank is 2min, the hydraulic retention time of the flocculation reaction tank is 3min, the retention time of the final sedimentation tank is 30min, and the surface load is 30m3/m2H, COD, BOD of effluent5、NH3The average values of TN, TP and SS are respectively 13.8, 2.1, 0.28, 4.39, 0.09 and 4.3 mg/L.
Example 3:
the difference from the embodiment 1 is that:
the process parameters are set as follows:
design water volume of 1000m for certain integrated equipment3D, COD, BOD of the influent water5、NH3TN, TP and SS design values are respectively 350, 140, 25, 40, 3 and 200mg/L, and the total hydraulic retention time is 8.0 h; of primary sedimentation hydrolysis tankThe hydraulic retention time is 3.5h, and the sludge concentration of the mud-water mixing area is 4000-; the sludge concentration of the first anoxic tank, the second anoxic tank, the first aerobic tank, the second aerobic tank, the third anoxic tank and the third aerobic tank is less than 500 mg/L; the filling rates of the suspended carriers in the first anoxic tank, the second anoxic tank and the third anoxic tank are respectively 45%, 35% and 45%, and DO is less than 0.4 mg/L; the hydraulic retention time of the third aerobic tank is 25min, the filling rates of the suspended carriers of the first aerobic tank, the second aerobic tank and the third aerobic tank are respectively 50%, 35% and 30%, and DO is 2-6 mg/L; the hydraulic retention time of the chemical adding mixing tank is 2min, the hydraulic retention time of the magnetic seed loading tank is 1.5min, the hydraulic retention time of the flocculation reaction tank is 3min, the retention time of the final settling tank is 25min, and the surface load is 25m3/m2H, COD, BOD of effluent5、NH3The average values of TN, TP and SS are respectively 15.2, 3.6, 0.39, 3.98, 0.08 and 4.5 mg/L.
The above-mentioned non-listed parts can be obviously realized under the guidance of the above-mentioned examples 1-3.
In the description of the present invention, it is to be understood that the terms "center", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are merely for convenience of description and for simplicity of description, and do not indicate or imply that the device or element referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore, should not be construed as limiting the present invention.
The specific embodiments described herein are merely illustrative of the spirit of the invention. Various modifications, additions and substitutions for the specific embodiments described herein may be made by those skilled in the art without departing from the spirit of the invention or exceeding the scope of the invention as defined in the accompanying claims.
Claims (10)
1. The utility model provides a sewage full flow processing system based on MBBR and magnetic separation, its includes the reactor, its characterized in that: the reactor treats sewage in a mode of combining MBBR and magnetic separation and precipitation, and comprises a primary precipitation hydrolysis tank, a first anoxic tank, a second anoxic tank, a first aerobic tank, a second aerobic tank, a third anoxic tank, a third aerobic tank, a dosing mixing tank, a magnetic seed loading tank, a flocculation reaction tank and a final precipitation tank which are sequentially communicated;
the device also comprises a magnetic powder separation device and a magnetic powder recovery device, wherein the magnetic powder separation device is connected with the sludge outlet pipe of the final sedimentation tank, and the magnetic powder recovery device is respectively connected with the magnetic powder separation device, the magnetic seed loading tank and the primary sedimentation hydrolysis tank;
suspension carriers are added into the first anoxic tank, the second anoxic tank, the first aerobic tank, the second aerobic tank, the third anoxic tank and the third aerobic tank;
a first stirrer special for a suspension carrier is arranged in the first anoxic tank, the second anoxic tank and the third anoxic tank; the first aerobic tank, the second aerobic tank and the third aerobic tank are internally provided with perforated pipe aerators, and the dosing mixing tank, the magnetic seed loading tank and the flocculation reaction tank are internally provided with a second stirrer, a third stirrer and a fourth stirrer in sequence;
the primary sedimentation hydrolysis tank is connected with a water inlet pipe and a sludge discharge pipe, and the final sedimentation tank is connected with a water outlet pipe;
a nitrifying liquid return pipe is connected between the second aerobic tank and the first anoxic tank, one end of the second aerobic tank is used as a water inlet, and one end of the first anoxic tank is used as a water outlet.
2. The MBBR and magnetic separation based sewage full-flow treatment system according to claim 1, wherein: the adjacent tank bodies are separated by a partition plate, the partition plate is provided with water passing ports for keeping the adjacent tank bodies communicated, and the water passing ports comprise a primary sedimentation hydrolysis tank water passing port positioned on the partition plate between the primary sedimentation hydrolysis tank and the first anoxic tank, a first anoxic tank water passing port positioned on the partition plate between the first anoxic tank and the second anoxic tank, a second anoxic tank water passing port positioned on the partition plate between the second anoxic tank and the first aerobic tank, a first aerobic tank water passing port positioned on the partition plate between the first aerobic tank and the second aerobic tank, a second aerobic tank water passing port positioned on the partition plate between the second aerobic tank and the third anoxic tank, a third anoxic tank water passing port positioned on the partition plate between the third anoxic tank and the third aerobic tank, a third aerobic tank water passing port positioned on the partition plate between the third aerobic tank and the dosing mixing tank, and a dosing mixing tank water passing port positioned on the partition plate between the dosing mixing tank and the magnetic seed loading tank, A magnetic seed loading pool water passing opening on a partition plate between the magnetic seed loading pool and the flocculation reaction pool and a flocculation reaction pool water passing opening on a partition plate between the flocculation reaction pool and the final sedimentation pool.
3. The MBBR and magnetic separation based sewage full-flow treatment system according to claim 2, wherein: and an oxygen-poor intercepting screen is arranged in front of the water outlet of the first oxygen-poor pool, in front of the water outlet of the second oxygen-poor pool and in front of the water outlet of the third oxygen-poor pool, the oxygen-poor intercepting screen is a flat screen, the upper edge of the oxygen-poor intercepting screen is 30cm below the operating water level, the lower edge of the oxygen-poor intercepting screen is higher than half of the operating water level, and the operating water level is as high as the lower edge of the water outlet pipe.
4. The MBBR and magnetic separation based sewage full-flow treatment system according to claim 2, wherein: and aerobic intercepting screens are arranged in front of the water passing port of the first aerobic tank, in front of the water passing port of the second aerobic tank and in front of the water passing port of the third aerobic tank, the aerobic intercepting screens are drum screens, the upper edge of each aerobic intercepting screen is below 65% of the operating water level, the lower edge of each aerobic intercepting screen is higher than 35% of the operating water level, and the operating water level is as high as the lower edge of the water outlet pipe.
5. The MBBR and magnetic separation based sewage full-flow treatment system according to claim 1, wherein: the magnetic powder separating device is connected with the magnetic powder recovering device through a sludge inlet pipe, the magnetic powder recovering device is connected with the magnetic seed loading pool through a magnetic seed return pipe, and the magnetic powder recovering device is connected with the primary sedimentation hydrolysis pool through a sludge return pipe.
6. The MBBR and magnetic separation based sewage full-flow treatment system according to claim 1, wherein: the density of the suspension carrier is 0.95-1.04g/cm3The porosity is more than 90%.
7. The MBBR and magnetic separation based sewage full-flow treatment system according to claim 1, wherein: the water inlet of the nitrifying liquid return pipe is provided with a nitrifying liquid return intercepting screen, the nitrifying liquid return intercepting screen is a flat screen, the opening direction of the perforated pipe aerator is downward, the opening aperture is 4-6mm, and the installation height is 30cm above the bottom of the tank.
8. The MBBR and magnetic separation based sewage full-flow treatment system according to claim 1, wherein: the density of the suspension carrier in the first anoxic tank, the second anoxic tank and the third anoxic tank is 1.02-1.04g/cm3The effective specific surface area of the suspension carrier is 300-620m2/m3。
9. The MBBR and magnetic separation based sewage full-flow treatment system according to claim 1, wherein: the density of the suspension carrier in the first aerobic tank is 0.95-0.97g/cm3The density of the suspended carrier in the second aerobic tank and the third aerobic tank is 0.97-0.99g/cm3。
10. The MBBR and magnetic separation based sewage full-flow treatment system according to claim 1, wherein: the effective specific surface area of the suspension carrier in the first aerobic tank and the third aerobic tank is 450-800m2/m3The effective specific surface area of the suspension carrier in the second aerobic tank is 620-1200m2/m3。
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| CN110386724A (en) * | 2019-07-19 | 2019-10-29 | 青岛思普润水处理股份有限公司 | A kind of sewage whole process processing system and method based on MBBR and Magneto separate |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110386724A (en) * | 2019-07-19 | 2019-10-29 | 青岛思普润水处理股份有限公司 | A kind of sewage whole process processing system and method based on MBBR and Magneto separate |
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