CN101062810A - Biological cycle moving bed sewage treatment system and method thereof - Google Patents
Biological cycle moving bed sewage treatment system and method thereof Download PDFInfo
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- CN101062810A CN101062810A CNA2007102005033A CN200710200503A CN101062810A CN 101062810 A CN101062810 A CN 101062810A CN A2007102005033 A CNA2007102005033 A CN A2007102005033A CN 200710200503 A CN200710200503 A CN 200710200503A CN 101062810 A CN101062810 A CN 101062810A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Abstract
The invention discloses a biological cycle moving bed sewage disposal system and method, which comprises the following steps: entering the raw water into anoxybiotic tank and anaerobic tank with pump from raw water tank; treating; feeding into the cycle moving bed reactor to proceed aeration oxygenation reaction; making the inner section in the tank body of current, inert support filler and bubble be directed with up-and-down cycle splitter, separating splitter and tailboard; forming circulatory flow; reacting the microbe of the current and the inert support filler completely; discharging into desilter; refluxing the depositing sludge in the bottom of the desilter into the anoxia tank; discharging the clear water in the upper of the desilter from the exhaust pipe; refluxing the treated water in the reactor into the anoxia tank through internal reflux pipe. This invention avoids the stratification, which can decrease the operating expense.
Description
(1) technical field
The present invention relates to a kind of sewage disposal system and method thereof, particularly a kind of organism fluidization bed waste water treatment system and method thereof.
(2) background technology
Traditional biological fluid bed sewage disposal system is linked in sequence by former pond, anoxic pond, anaerobic pond, fluidized-bed reactor, sedimentation basin and forms. The loopy moving bed bioreactor is a rectangle form pool body for the sewage reaction, and the pond body is connected with aerator. Following defective is arranged in running: the biomembrane meeting progressive additive in the biological fluidized bed, carrier granular lighten gradually, thereby lamination occurs in fluid bed, need the special device for removing scum of configuration, have so just greatly increased operating cost. What is more, and the conventional flow fluidized bed reactor is after operation a period of time, because blocked up biofilm detachment can cause the interim effluent quality variation of organism fluidization bed waste water treatment system, efficient step-down, the consequence that the fluid mixed performance is bad.
Traditional biological fluid bed sewage disposal system has the variety classeses such as BAF, oxidation ditch.
The characteristics of BAF: need not second pond, the pond body is compact, and the electromechanical equipment amount is large, and automatic instrument(s) is many, take up an area littlely, gross investment is larger, and operating cost is high, the loss of flood peak: about 3～3.5, do not need sludge reflux, aeration rate is larger, and power consumption is larger, and pharmaceutical quantities is slightly little. Sludge output is larger, the mud poor stability, and without sludge bulking: immeasurable variation: be subjected to the impact of the rate of filtration that certain limitation is arranged, reason efficient is high, but regularly backwash meeting causes the treatment effeciency less stable; Filler runs off easily, and wearability is relatively poor, needs in case of necessity to carry out the two stage biological filter tank and processes, and the computer-aided traffic control degree is high, and regular maintenance and tour maintenance workload are larger, make an inspection tour simple overhaul: regularly need overhaul every year, may affect effluent quality.
The oxidation Ditch Technology characteristics are as follows:
1, continuously water-in and water-out can be resisted impact load.
2, denitrification effect is removed, and phosphor-removing effect is poor.
3, disposal ability is low: (its specific area is little: be lower than 100m2/m
3, MLSS concentration is low: 2000～3000mg/L;
4, BOD loading is little: 0.3～0.9Kg/m3.d)
5, return sludge ratio is large: 100%, and the return-flow system investment is large.
6, hydraulic detention time is long: 15.5 hours;
7, adopt surface aeration, be provided with the plate-spinning aerator, the plate-spinning branch is arranged; Energy consumption is higher.
8, power consumption is larger, and operating cost is higher.
(3) summary of the invention
The purpose of this invention is to provide a kind of biological cycle moving bed sewage treatment system and method thereof, solve mainly that the inherent biomembrane of traditional biological fluid bed thickens, carrier granular lamination occurs after lightening, special device for removing scum can significantly increase the problem of operating cost; Blocked up the coming off of biomembrane solve simultaneously the traditional biological fluidized-bed reactor after operation a period of time, owing to can be caused interim effluent quality variation, efficient step-down, the technical problem that the fluid mixed performance is bad.
The object of the present invention is achieved like this: this loopy moving bed bioreactor is a rectangle form pool body for the sewage reaction, and the pond body is connected with aerator, and there is a downflow weir outer, body rear wall top, pond, it is characterized in that:
(1), is distributed with the inert carrier filler that supplies attached growth of microorganisms in the body of pond;
(2), the aeration tube end of aerator is connected with aeration head, aeration head places the pond body near the bottom of antetheca;
(3), the middle part is fixed with separately up and down circulation deflector, isolation deflector and backboard successively from A-P in the body of pond, above-mentioned three baffle plates are rectangle, every baffle plate is across the pond body, its two longitudinal edge is separately fixed on the pond body madial wall of two correspondences, middle part in the body of pond is divided into the up-flow district and falls the stream district, wherein:
A, circulate between the top of the upper end of deflector and pond up and down, all leave the circulating water flow passage between at the bottom of lower end and the pond;
B, isolation deflector are longer than the deflector that circulates up and down, also leave the circulating water flow passage between between push up in its upper end and pond, at the bottom of lower end and the pond, narrower than among the above-mentioned a of this circulating water flow passage;
The upper end of c, backboard exceeds the water surface, leaves the circulating water flow passage between at the bottom of lower end and the pond.
Body antetheca upper end, above-mentioned pond is equipped with the anterior angle circulating baffle plate, and there is front fillet the angle between the body antetheca of at the bottom of the pond and pond, and there is rear fillet the angle between the body rear wall of at the bottom of the pond and pond.
Above-mentioned pond body length is 5～8 meters, vertically arranges arbitrarily.
A kind of biological cycle moving bed sewage treatment system of using above-mentioned loopy moving bed bioreactor, it is characterized in that: be linked in sequence and form by former pond, anoxic pond, anaerobic pond, loopy moving bed bioreactor, sedimentation basin, the loopy moving bed bioreactor is connected with aerator, the sedimentation basin bottom connects mud return line, the mud return line outlet is positioned at above the anoxic pond, sedimentation basin top is connected with outlet pipe, return duct in loopy moving bed bioreactor delivery port connects, the delivery port of interior return duct is positioned at above the anoxic pond.
A kind of biological cycle moving bed sewage water treatment method of using above-mentioned biological cycle moving bed sewage treatment system, it is characterized in that flow process is as follows: former water is processed with pump input anoxic pond and anaerobic pond from former pond, then be transfused to the loopy moving bed bioreactor and carry out the aeration aerating reaction, current, inert carrier filler and bubble be subject to respectively in body inside, pond circulating the up and down water conservancy diversion of deflector, isolation deflector, backboard, formation circulates, after the abundant haptoreaction of the microorganism of current and inert carrier filling surface, enter in the sedimentation basin, the precipitating sludge of sedimentation basin bottom is back in the anoxic pond through mud return line, the clear water on sedimentation basin top is discharged from outlet pipe, and a part is back in the anoxic pond through interior return duct through the water of circulated moving bed reactor for treatment.
Above-mentioned inert carrier filler is that diameter is 5～10mm, the particle that is comprised of shoddy, filler, adhesive.
Filler in the above-mentioned inert carrier filler is kaolin, clay or bentonite.
Adhesive in the above-mentioned inert carrier filler is polyurethane, vinylester resin, acrylic or methacrylic acid alkane ester monomer.
The proportioning that above-mentioned inert carrier filler is calculated by weight is as follows:
100 parts of shoddies;
20～30 parts of polyurethane;
10～20 parts of kaolin.
The present invention compared with prior art has following characteristics and beneficial effect:
The present invention is the improvement to the traditional biological fluidized-bed process. New Cycle biological moving bed (be called for short BFMD) is fast at the mass transfer rate that has kept traditional fluidisation bed accessory to have, sludge concentration large, in the organic loading advantages of higher, have following new characteristics:
1), of the present invention rational in infrastructure. Sewage is transfused to from former pond and carries out denitrification the anoxic pond and process, and anaerobic pond provides mud to discharge the condition of phosphorus. The fillet of circulating biological moving bed pond body is configured with and is beneficial to current and carrier filler uniform circulation, prevents the carrier filler deposition.
2), the fluid mixed performance is good, can control biofilm thickness. Circulating biological moving bed pond body is built-in with the deflector that circulates up and down, isolation deflector and backboard, and above-mentioned baffle plate will be divided into the up-flow district and fall the stream district in the body of pond. In the up-flow district, carry out aeration aerating, because disturbance and the up-flow district of air-flow and fall the existence of density contrast between the stream district, so that waste water and carrier filler are in the up-flow district with fall between the stream district and circulate. Carrier granular is subject in the whole circulating biological moving-burden bed reactor shearing and frictional force are more even, can not occur therefore that traditional biological fluid bed internal cause biomembrane thickens, carrier granular lightens and in bed the phenomenon of layering. Owing to hydraulic shear, comparatively violent, the blocked up biomembrane meeting self falling of friction in the circulating biological moving-burden bed reactor, can reach the purpose of control thickness simultaneously, not need special device for removing scum.
3), the backboard in the body of circulating biological moving bed pond and downflow weir can prevent that carrier filler runs off. Growth of microorganism belongs to immobilized microorganism at the filling surface of rough porous, can not run off, so operational management is convenient and simple.
4), the inert carrier filling surface among the present invention has certain roughness, biological stability is good, fluidizing performance is good, tack is good, the surface biological bacterium is many, can increase the quantity of microorganism in the reactive tank, organic removal rate is higher, with low cost. Inert carrier of the present invention is for to form the particle that diameter is 5～10mm by shoddy, filler, adhesive. Its specific area is more much bigger than the specific area of conventional carrier, surpasses 3500m2/m
3, and have good elasticity, wear-resistant and chemical stability, because its density is less, so the energy consumption of circulating biological moving-burden bed reactor is less.
5), circulating biological moving-burden bed reactor treatment effeciency is high, compact conformation, floor space only be 1/4～1/8 of legacy equipment, capital expenditure saving 20%～30%, Enlargement Design is comparatively easy.
6), the transfer efficiency of oxygen is high. The present invention forms adverse current at when operation water inlet current and aeration gas flow in the circulating biological moving-burden bed reactor, increased gas-water contact area; And carrier filler is under the inner because up-flow district of circulating biological moving-burden bed reactor and the effect of falling stream district's density contrast and special fluid bed internal structure in the body of pond, and formation circulates, and coefficient of oxygen utilization is improved 10%～15%, is conducive to the transfer of oxygen.
7), the shock-resistant ability of inert carrier filler among the present invention is strong, without the sludge bulking problem. Compare with general carrier, load impact is had stronger adaptability. The common decomposing pollutant matter of microorganism in the mixed liquor and biofilm microorganisms makes the BOD treating capacity reach 5～16kg/ (m3D), be more than 8 times of Wastewater Treated by Activated Sludge Process amount. Granular inert carrier filler among the present invention has inexpensive, the wear-resisting and resistance to oxidation of light weight and is easy to biofilm and the characteristics of growth of microorganism, in contact oxidation method, moving-burden bed reactor and biological fluidized bed.
8), water treatment efficiency is high. The mutual method of operation of fierce collision of filling carrier has overcome traditional reactor after operation a period of time in the circulating biological moving-burden bed reactor, because the shortcoming of the blocked up interim effluent quality variation that causes of coming off of biomembrane. And the mode of this fierce collision is very beneficial for improving the transfer rate of pollutant on biomembrane in the water body, is conducive to improve treatment effeciency.
9), ammonia nitrogen removal efficient is high. Particulate filler has huge specific area, and the high-activity biological film that the various carbonization bacterium that growing on it, ammonifiers and nitrifier form has the effect of good oxidative degradation and adsorption filtration water pollutant, and larger microorganism living space can be provided. Filling surface provides good set life and the place of breeding for nitrobacteria, this has improved the sludge retention time of nitrobacteria in reaction system on the one hand, on the other hand, because nitrobacteria is easy to anchor at the characteristic of filling surface, also is conducive to improve the nitrobacteria percentage in the whole reaction system. In the general activated sludge process, nitrifier only accounts for 8% of MLVSS, and in inner loop fluidized bed reactor in the activated sludge system, nitrifier can account for 20% of MLVSS. Be greatly improved from this respect ammonia nitrogen removal efficient. Because in the middle of the moving bed biological film system, both can possess the same of higher MLSS value and advance, can effectively possess higher nitrifier concentration again. Therefore, this system's water outlet except the conventional indexs such as COD are low, its water outlet NH3-N concentration can be less than 2mg/L, even less than 1mg/L. That is to say for middle water reuse, adopt the moving bed biological membrane treatment process, can no longer carry out three grades of biological treatments.
The comparison sheet of the present invention and BAF is as follows:
| Project | BAF | The present invention | |
| Investment cost | Civil engineering costs | Need not second pond, the pond body is compact, needs two-stage biofilter | The pond body is compact, arranges simple |
| Investment cost | Electromechanical equipment and instrument | Equipment amount is large, and automatic instrument(s) is many | Equipment investment is general |
| Investment cost | Fees paid for taking rural land | Less | Less |
| Investment cost | Gross investment | Larger | Less |
| Operating cost | The loss of flood peak | About 3～3.5 | About 1～1.5 |
| Operating cost | Sludge reflux | Do not need | Need |
| Operating cost | Aeration rate | Larger | Less |
| Operating cost | Power consumption | Larger | Less |
| Operating cost | Pharmaceutical quantities | Slightly little | Generally |
| Technological effect | Sludge output | Larger, the mud poor stability | Sludge output is few, and mud is stable |
| Technological effect | Have or not sludge bulking | Nothing | Nothing |
| Technological effect | The variation of flow | Be subjected to the impact of the rate of filtration that certain limitation is arranged | Substantially unaffected |
| Technological effect | Treatment effeciency | Height, but regularly backwash meeting causes the treatment effeciency less stable | Height, stable |
| Technological effect | Filter (filling out) material | Run off easily, wearability is relatively poor, and overhaul need to replenish | Be difficult for running off, once add |
| Technological effect | Ammonia nitrogen removal frank | Need to carry out the two stage biological filter tank and process (in case of necessity) | Remove simultaneously COD and ammonia nitrogen in same pond, ammonia nitrogen removal frank is high |
| Operational management | Automaticity | High | Higher |
| Operational management | Regular maintenance and tour | Maintenance workload is larger, makes an inspection tour simple | Maintenance workload is less, makes an inspection tour simple |
| Operational management | Overhaul | Regularly need overhaul every year, may affect effluent quality | Time between overhaul is longer, generally more than 2 years |
The comparison sheet of the present invention and conventional oxidation ditch technology is as follows:
| The comparison of two kinds of operational characteristiies | |
| The present invention | Oxidation ditch |
| Continuously water-in and water-out, the opposing impact load is strong. | Continuously water-in and water-out can be resisted impact load. |
| Ammonia nitrogen removal is effective, and the phosphorus removal effect is better. | Denitrification effect is removed, and phosphor-removing effect is poor. |
| Disposal ability is strong: (its specific area is large: can reach 1500m2/m 3, MLSS concentration is high: can reach 20000mg/L; BOD loading is large: can reach 4.0～20Kg/m3.d) | Disposal ability is low: (its specific area is little: be lower than 100m2/m 3, MLSS concentration is low: 2000～3000mg/L; BOD loading is little: 0.3～0.9Kg/m3.d) |
| Return sludge ratio is little: 50%, and the return-flow system investment is little. | Return sludge ratio is large: 100%, and the return-flow system investment is large. |
| Hydraulic detention time is short: 2 to 3 hours; It is little to process the structures volume. | Hydraulic detention time is long: 15.5 hours; It is large to process the structures volume. |
| Adopt blast aeration, the aerator long service life, dynamic efficiency is high, and energy consumption is lower, and maintenance and maintenance are little. | Adopt surface aeration, be provided with the plate-spinning aerator, the plate-spinning branch is arranged; Energy consumption is higher. |
| Power consumption is less, and operating cost is low. | Power consumption is larger, and operating cost is higher. |
Actual beneficial effect of the present invention is by the compbined test digital proof of following engineering test and operation:
| Stage | Project | Water inlet | Water outlet | Clearance |
| Design objective | COD Cr | 450mg/l | 120mg/l | 75％ |
| Design objective | BOD 5 | 250mg/l | 60mg/l | 76％ |
| Design objective | SS | 200mg/l | 30mg/l | 85％ |
| Design objective | NH 3-N | 45mg/l | 15mg/l | 70％ |
| Design objective | N-P | 4mg/l | 1mg/l | 75％ |
| The integrated operation index | COD Cr | 550mg/l | 60mg/l | 90％ |
| The integrated operation index | BOD 5 | 290mg/l | 30mg/l | 90％ |
| The integrated operation index | SS | 280mg/l | 10mg/l | 96％ |
| The integrated operation index | NH 3-N | 70mg/l | 10mg/l | 86％ |
| The integrated operation index | N-P | 4mg/l | 1mg/l | 75％ |
Adopt the physicochemical property data of carrier filler to see the following form in the benzene invention:
Filler detects data record
| The mensuration project | Data record | Data preparation | ||||||
| Average grain diameter | l 1 | l 2 | l 3 | l 4 | l 5 | l | 7.69 | mm |
| 7.86 | 7.8 | 8.62 | 7.5 | 6.68 | ||||
| d 1 | d 2 | d 3 | d 4 | d 5 | d | 5.51 | ||
| 5.18 | 5.3 | 5.9 | 4.86 | 6.32 | ||||
| Loose volume weight | G 1 | G 2 | γ | 0.35 | g/ml | |||
| 70.5053 | 71.2323 | |||||||
| Real density | G 1 | V 1 | G 2 | V 2 | γ 1 | 1.10 | g/ml | |
| 21.2964 | 19.6 | 21.2964 | 19.6 | |||||
| Voidage | ε | 67.8 | ％ | |||||
| Wet proportion | G 1 | V 1 | G 2 | V 2 | γ 2 | 1.03 | g/ml | |
| 22.3743 | 22 | 21.9182 | 21.05 | |||||
| Wearability | G 1 | G 1′ | G 2 | G 2′ | The pulverizing grinder loss rate | 1.590 | ％ | |
| 50 | 0.7952 | |||||||
| Oxidative resistance | G | V 1 | V 2 | Oxygen consumption dosage | 0.00 | G oxidant/100g filler | ||
| 10.063 | 14.44 | 14.42 | ||||||
| Sinking speed | s | t 1 | t 2 | t 3 | t 4 | u | 6.69 | cm/s |
| 19.9 | 3 | 3.3 | 2.9 | 2.7 | ||||
(4) description of drawings
Fig. 1 is the structural representation of loopy moving bed bioreactor embodiment of the present invention.
Fig. 2 is structure and the schematic flow sheet of biological cycle moving bed sewage treatment system embodiment of the present invention.
Return duct, 7-mud return line, 8-outlet pipe, 9-pump, 10-inert carrier filler, 11-aerator in the former pond of 1-, 2-anoxic pond, 3-anaerobic pond, 4-loopy moving bed bioreactor, 5-sedimentation basin, the 6-.
40-pond body, 41-aeration tube, 42-aeration head, the upper anterior angle circulating baffle plate of 43-, 44-circulate up and down fillet before fillet behind deflector, 45-isolation deflector, 46-backboard, the 47-, the 48-, 49-downflow weir.
(5) specific embodiment
Embodiment is referring to shown in Figure 1, and this loopy moving bed bioreactor is a rectangle form pool body for the sewage reaction, and pond body 40 is connected with aerator 11, and there is a downflow weir 49 outer, body rear wall top, pond, it is characterized in that:
(1), is distributed with the inert carrier filler 10 that supplies attached growth of microorganisms in the pond body 40;
(2), aeration tube 41 ends of aerator are connected with aeration head 42, aeration head places the pond body near the bottom of antetheca;
(3), the middle part is fixed with separately up and down circulation deflector 44, isolation deflector 45 and backboard 46 successively from A-P in the body of pond, above-mentioned three baffle plates are rectangle, every baffle plate is across the pond body, its two longitudinal edge is separately fixed on the pond body madial wall of two correspondences, middle part in the body of pond is divided into the up-flow district and falls the stream district, wherein:
A, circulate between the top of the upper end of deflector 44 and pond up and down, all leave the circulating water flow passage between at the bottom of lower end and the pond;
B, isolation deflector 45 are longer than the deflector that circulates up and down, also leave the circulating water flow passage between between push up in its upper end and pond, at the bottom of lower end and the pond, narrower than among the above-mentioned a of this circulating water flow passage;
The upper end of c, backboard 46 exceeds the water surface, leaves the circulating water flow passage between at the bottom of lower end and the pond.
Body antetheca upper end, above-mentioned pond is equipped with anterior angle circulating baffle plate 43, and there is front fillet 47 angle between the body antetheca of at the bottom of the pond and pond, and there is rear fillet 48 angle between the body rear wall of at the bottom of the pond and pond.
Above-mentioned pond body length is 5～8 meters, vertically arranges arbitrarily.
Referring to Fig. 2, a kind of biological cycle moving bed sewage treatment system of using above-mentioned loopy moving bed bioreactor, it is characterized in that: be linked in sequence and form by former pond 1, anoxic pond 2, anaerobic pond 3, loopy moving bed bioreactor 4, sedimentation basin 5, loopy moving bed bioreactor 4 is connected with aerator 11, the sedimentation basin bottom connects mud return line 7, the mud return line outlet is positioned at above the anoxic pond, sedimentation basin top is connected with outlet pipe 8, return duct 6 in loopy moving bed bioreactor delivery port connects, the delivery port of interior return duct 6 is positioned at above the anoxic pond.
A kind of biological cycle moving bed sewage water treatment method of using above-mentioned biological cycle moving bed sewage treatment system, it is characterized in that flow process is as follows: former water is processed with pump 9 input anoxic pond 2 and anaerobic pond 3 from former pond 1, then be transfused to loopy moving bed bioreactor 4 and carry out the aeration aerating reaction, current, inert carrier filler and bubble be subject to respectively in body inside, pond circulating the up and down water conservancy diversion of deflector 44, isolation deflector 45, backboard 46, formation circulates, after the abundant haptoreaction of the microorganism of current and inert carrier filling surface, enter in the sedimentation basin 5, the precipitating sludge of sedimentation basin bottom is back in the anoxic pond through mud return line 7, the clear water on sedimentation basin top is discharged from outlet pipe 8, and the water that a part is processed through loopy moving bed bioreactor 4 is back in the anoxic pond 2 through interior return duct 6.
Above-mentioned inert carrier filler is that diameter is 5～10mm, the particle that is comprised of shoddy, filler, adhesive. Filler in the inert carrier filler can be selected kaolin, clay or bentonite. Adhesive can be polyurethane, vinylester resin, acrylic or methacrylic acid alkane ester monomer.
The proportioning embodiment one that above-mentioned inert carrier filler is calculated by weight is as follows:
100 parts of shoddies;
20～30 parts of polyurethane;
10～20 parts of kaolin.
The proportioning embodiment two that above-mentioned inert carrier filler is calculated by weight is as follows:
100 parts of shoddies;
25 parts of polyurethane;
15 parts of kaolin.
Claims (9)
1. a loopy moving bed bioreactor is a rectangle form pool body for the sewage reaction, and the pond body is connected with aerator, and there is a downflow weir outer, body rear wall top, pond, it is characterized in that:
(1), is distributed with the inert carrier filler that supplies attached growth of microorganisms in the body of pond;
(2), the aeration tube end of aerator is connected with aeration head, aeration head places the pond body near the bottom of antetheca;
(3), the middle part is fixed with separately up and down circulation deflector, isolation deflector and backboard successively from A-P in the body of pond, above-mentioned three baffle plates are rectangle, every baffle plate is across the pond body, its two longitudinal edge is separately fixed on the pond body madial wall of two correspondences, middle part in the body of pond is divided into the up-flow district and falls the stream district, wherein:
A, circulate between the top of the upper end of deflector and pond up and down, all leave the circulating water flow passage between at the bottom of lower end and the pond;
B, isolation deflector are longer than the deflector that circulates up and down, also leave the circulating water flow passage between between push up in its upper end and pond, at the bottom of lower end and the pond, narrower than among the above-mentioned a of this circulating water flow passage;
The upper end of c, backboard exceeds the water surface, leaves the circulating water flow passage between at the bottom of lower end and the pond.
2. loopy moving bed bioreactor according to claim 1 is characterized in that: body antetheca upper end in above-mentioned pond is equipped with the anterior angle circulating baffle plate, and there is front fillet the angle between the body antetheca of at the bottom of the pond and pond, and there is rear fillet the angle between the body rear wall of at the bottom of the pond and pond.
3. biological cycle moving bed sewage treatment system according to claim 4, it is characterized in that: above-mentioned pond body length is 5～8 meters, vertically arranges arbitrarily.
4. an application rights requires the biological cycle moving bed sewage treatment system of any described loopy moving bed bioreactor of 1-3, it is characterized in that: be linked in sequence and form by former pond, anoxic pond, anaerobic pond, loopy moving bed bioreactor, sedimentation basin, the loopy moving bed bioreactor is connected with aerator, the sedimentation basin bottom connects mud return line, the mud return line outlet is positioned at above the anoxic pond, sedimentation basin top is connected with outlet pipe, return duct in loopy moving bed bioreactor delivery port connects, the delivery port of interior return duct is positioned at above the anoxic pond.
5. an application rights requires the biological cycle moving bed sewage water treatment method of 4 biological cycle moving bed sewage treatment systems, it is characterized in that flow process is as follows: former water is processed with pump input anoxic pond and anaerobic pond from former pond, then be transfused to the loopy moving bed bioreactor and carry out the aeration aerating reaction, current, inert carrier filler and bubble be subject to respectively in body inside, pond circulating the up and down water conservancy diversion of deflector, isolation deflector, backboard, formation circulates, after the abundant haptoreaction of the microorganism of current and inert carrier filling surface, enter in the sedimentation basin, the precipitating sludge of sedimentation basin bottom is back in the anoxic pond through mud return line, the clear water on sedimentation basin top is discharged from outlet pipe, and a part is back in the anoxic pond through interior return duct through the water of circulated moving bed reactor for treatment.
6. biological cycle moving bed sewage treatment system according to claim 5 is characterized in that: above-mentioned inert carrier filler is that diameter is 5～10mm, the particle that is comprised of shoddy, filler, adhesive.
7. biological cycle moving bed sewage treatment system according to claim 6, it is characterized in that: the filler in the above-mentioned inert carrier filler is kaolin, clay or bentonite.
8. biological cycle moving bed sewage treatment system according to claim 6 is characterized in that: the adhesive in the above-mentioned inert carrier filler is polyurethane, vinylester resin, acrylic or methacrylic acid alkane ester monomer.
9. biological cycle moving bed sewage treatment system according to claim 6, it is characterized in that: the proportioning that above-mentioned inert carrier filler is calculated by weight is as follows:
100 parts of shoddies;
20～30 parts of polyurethane;
10～20 parts of kaolin.
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Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101962252A (en) * | 2010-09-16 | 2011-02-02 | 天津市农业资源与环境研究所 | Local circulating oxygen supply biomembrane reacting device |
| CN102557199A (en) * | 2010-12-14 | 2012-07-11 | 上海洗霸科技股份有限公司 | Micro-electrolytic reactor |
| CN102701444A (en) * | 2012-06-08 | 2012-10-03 | 李卓娅 | Biological fermentation fixed bed reactor, and method for cleaning fixed bed carriers of biological fermentation fixed bed reactor |
| CN102774961A (en) * | 2012-07-11 | 2012-11-14 | 浙江工业大学 | Multistage anaerobic wastewater treatment method and special device |
| CN103073108A (en) * | 2011-10-25 | 2013-05-01 | 苏州嘉净环保科技股份有限公司 | Moving bed type purification tank |
| CN103466787A (en) * | 2013-09-17 | 2013-12-25 | 西安绿标水环境科技有限公司 | Combined aeration moving bed bio-membrane reactor |
| CN103936140A (en) * | 2014-04-15 | 2014-07-23 | 同济大学 | MBBR pretreatment method and system for high-ammonia nitrogen micro-polluted raw water |
| CN106006960A (en) * | 2016-07-18 | 2016-10-12 | 广德清源水处理设备有限公司 | Anoxic baffled reactor and operation method thereof |
| CN107311405A (en) * | 2017-08-18 | 2017-11-03 | 北京博大水务有限公司 | Urban sewage treatment system and technique |
| CN107935171A (en) * | 2018-01-09 | 2018-04-20 | 中冶赛迪工程技术股份有限公司 | Pulling flow type moving bed biofilm reactor |
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| CN108911124A (en) * | 2018-07-18 | 2018-11-30 | 杭州师范大学 | With the integral type self-supported denitrification reactor from retention anaerobic ammonium oxidizing bacteria function |
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2007
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101962252A (en) * | 2010-09-16 | 2011-02-02 | 天津市农业资源与环境研究所 | Local circulating oxygen supply biomembrane reacting device |
| CN101962252B (en) * | 2010-09-16 | 2012-07-11 | 天津市农业资源与环境研究所 | Local circulating oxygen supply biomembrane reacting device |
| CN102557199A (en) * | 2010-12-14 | 2012-07-11 | 上海洗霸科技股份有限公司 | Micro-electrolytic reactor |
| CN103073108A (en) * | 2011-10-25 | 2013-05-01 | 苏州嘉净环保科技股份有限公司 | Moving bed type purification tank |
| CN102701444A (en) * | 2012-06-08 | 2012-10-03 | 李卓娅 | Biological fermentation fixed bed reactor, and method for cleaning fixed bed carriers of biological fermentation fixed bed reactor |
| CN102774961A (en) * | 2012-07-11 | 2012-11-14 | 浙江工业大学 | Multistage anaerobic wastewater treatment method and special device |
| CN102774961B (en) * | 2012-07-11 | 2013-07-31 | 浙江工业大学 | Multistage anaerobic wastewater treatment method and special device |
| CN103466787A (en) * | 2013-09-17 | 2013-12-25 | 西安绿标水环境科技有限公司 | Combined aeration moving bed bio-membrane reactor |
| CN103936140A (en) * | 2014-04-15 | 2014-07-23 | 同济大学 | MBBR pretreatment method and system for high-ammonia nitrogen micro-polluted raw water |
| CN106006960A (en) * | 2016-07-18 | 2016-10-12 | 广德清源水处理设备有限公司 | Anoxic baffled reactor and operation method thereof |
| CN107311405A (en) * | 2017-08-18 | 2017-11-03 | 北京博大水务有限公司 | Urban sewage treatment system and technique |
| CN108178438A (en) * | 2017-12-29 | 2018-06-19 | 冯湛钧 | A kind of rural domestic sewage treatment system and purification method |
| CN107935171A (en) * | 2018-01-09 | 2018-04-20 | 中冶赛迪工程技术股份有限公司 | Pulling flow type moving bed biofilm reactor |
| CN108911124A (en) * | 2018-07-18 | 2018-11-30 | 杭州师范大学 | With the integral type self-supported denitrification reactor from retention anaerobic ammonium oxidizing bacteria function |
| CN108911124B (en) * | 2018-07-18 | 2023-08-18 | 杭州师范大学 | Integrated autotrophic denitrification reactor with self-interception anaerobic ammonia oxidizing bacteria function |
| CN110002688A (en) * | 2019-04-30 | 2019-07-12 | 倍杰特集团股份有限公司 | It is a kind of efficiently to mention mark system |
| CN110002688B (en) * | 2019-04-30 | 2021-11-30 | 倍杰特集团股份有限公司 | Efficient label lifting system |
| CN111995193A (en) * | 2020-09-07 | 2020-11-27 | 贵州省材料产业技术研究院 | Integrated intelligent device and method for advanced treatment of medical wastewater |
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