CN102502963A - Multi-mode sequencing batch active sludge sewage treatment method and system - Google Patents
Multi-mode sequencing batch active sludge sewage treatment method and system Download PDFInfo
- Publication number
- CN102502963A CN102502963A CN201110344667XA CN201110344667A CN102502963A CN 102502963 A CN102502963 A CN 102502963A CN 201110344667X A CN201110344667X A CN 201110344667XA CN 201110344667 A CN201110344667 A CN 201110344667A CN 102502963 A CN102502963 A CN 102502963A
- Authority
- CN
- China
- Prior art keywords
- pond
- aerobic
- anoxic
- sewage
- anaerobic
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Landscapes
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The invention relates to a multi-mode constant-water-level sequencing batch active sludge sewage treatment method and system, belonging to the technical field of sewage treatment. The system comprises a sludge concentration pre-anoxic pond, an anaerobic pond, an anoxic pond, an aerobic pond, a facultative pond and a sequencing batch pond which are communicated, wherein the facultative pond runs in an aerobic or anoxic way. According to the system, multi-mode sewage treatment ways including an anaerobic-anoxic-aerobic mode, an anoxic-anaerobic-aerobic mode and an anaerobic-anoxic-aerobic-anoxic-aerobic mode can be performed. Due to the adoption of the sewage treatment method, the removing effects of nitrogen, phosphorus and organic matters can be enhanced, and equipment utilization ratio is increased.
Description
Technical field
The present invention relates to a kind of multi-mode constant water level sequencing batch active sludge modified version sewage water treatment method and system thereof, belong to technical field of sewage.
Background technology
At present; Country is to nitrogen, the phosphorus water outlet standard-required increasingly stringent of urban wastewater treatment firm; Many urban wastewater treatment firms require water outlet to reach country's " urban wastewater treatment firm pollutant emission standard " one-level A standard; Therefore a lot of Sewage Plant all are faced with the problem of upgrading, and process for removing nitrogen and phosphor from sewage commonly used is A
2/ O technology and various modified version A
2/ O technology.
1, traditional A
2/ O technology:
Tradition A
2/ O technology is the synchronous dephosphorization and denitrification process that on anaerobism-anoxic process, develops the seventies, and its biological reaction tank is made up of for three sections ANAEROBIC (anaerobism), ANOXIC (anoxic) and OXIC (aerobic), and its typical process flow is seen Fig. 1.This is a kind of Prepositive denitrification type BNR technology of pulling flow type; Be characterized in anaerobism, anoxic, aerobic three sections definite functions; The division is clearly demarcated; Can create and control three sections space-time ratio and operating condition artificially according to water inlet condition and water outlet requirement, as long as carbon source sufficient (TKN/COD≤0.08 or BOD/TKN>=4) just can reach than higher denitrification percent as required.
Conventional biological denitrification phosphorous removal technique is the arrangement form of anaerobism (A1)/anoxic (A2)/aerobic (O).This is arranged in theory based on a kind of like this understanding; That is: gather the phosphorus mikrobe effectively release the phosphorus level whether fully; Dephosphorization ability for improving system has extremely important meaning, anaerobic zone before can make and gather the phosphorus mikrobe and preferentially obtain carbon source and be able to fully release phosphorus.
A
2The shortcoming of/O method mainly is this technology itself.Denitrogenation need keep lower sludge loading; So that fully carry out nitratedly, reach higher denitrification percent, and biological phosphate-eliminating need be kept higher sludge loading; Keep bigger surplus sludge volume; So that reach phosphor-removing effect preferably, therefore in design, also need take required measure to do further to optimize, to relax both contradiction; Simultaneously, mud need be set reflux and internal reflux pump house, independent processing structures such as secondary sedimentation basins, flow process is comparatively complicated, and power consumption is bigger, and management is inconvenient, and always floor space is bigger.
2, constant water level sequencing batch active sludge treatment process
The patent of application number 200610165570.1: method that a kind of constant water level sequencing batch active sludge is disposed of sewage and system thereof, the technology that constant water level sequencing batch active sludge is disposed of sewage is disclosed, be designated hereinafter simply as permanent water level SBR technology.
Permanent water level SBR technology, i.e. water inlet continuously, continuous effluent, permanent water level modified version SBR technology, this technology has improved the plant factor and the reaction tank capacity utilization of SBR technology.Adopt permanent water level operation, avoided becoming the big shortcoming of water level operation head loss.The most important thing is spatially to provide special-purpose anoxic, anaerobic and aerobic pond, kept traditional A
2Each reaction zone definite functions of/O activated sludge process, the advantage that the division is clearly demarcated increase the efficient of biological carbon and phosphorous removal.
Permanent water level SBR technology is that pond body centralized arrangement with the difference in functionality lattice is in a Da Chi.Whole pond body contains middle biological reaction tank lattice and two the permanent water level SBR pond lattice that carry out mud backflow, rhythmic reaction, quiescent setting and replace the symmetric arrangement of water outlet, i.e. first and second sequencing batch ponds of at least one continuous water inlet, continuous effluent, successive reaction, permanent water level.Mud backflow, rhythmic reaction and quiescent setting process (abbreviating the RBS process as) realize (the SBR pond that is in the RBS process is called the RBS pond) in permanent water level SBR pond therein, strain water and then in another permanent water level SBR pond, realize (be in the SBR pond of straining water state be called strain the pond).Two SBR pond cycles hocket RBS with strain the water process.According to dirty wastewater treatment requirement, can before two SBR ponds, adopt the middle biological reaction tank of a plurality of arranged in series, be designed to anoxic pond lattice, anaerobic pond lattice or Aerobic Pond lattice to satisfy different processing (like biological phosphate-eliminating, denitrogenation) requirement.Treat effluent alternately drains by straining hydrophone through permanent water level in two SBR ponds, and excess sludge then discharges by being in the SBR pond of straining water state.
Like the permanent water level SBR of Fig. 2 pond body synoptic diagram, the operation of permanent water level SBR technology is following: sewage is introduced into anoxic pond, and for denitrification reaction provides carbon source, lattice are back to and accomplish denitrogenation processing in the anoxic pond mixed solution from the SBR limit; Then mixed solution then gets into anaerobic pond, carries out anaerobic phosphorus release, and sewage gets into Aerobic Pond then, accomplishes nitratedly, gets into two SBR limit lattice at last.
Operation logic by permanent water level SBR technology can know that permanent water level SBR technology has combined A
2The advantage of/O technology and SBR technology is all having good behaviour aspect denitrogenation dephosphorizing effect and the saving floor space two.
But find that in the process of operation if TN, TP are too high in the water inlet, and water outlet is when having relatively high expectations to denitrogenation dephosphorizing, permanent water level SBR technology also is not very desirable for the treatment effect of denitrogenation dephosphorizing, still need strengthen the denitrogenation dephosphorizing ability.Because this technology has only the not high mud backflow of concentration that is back to anoxic pond from the SBR lattice, and does not have to the high concentration sludge of anaerobic pond to reflux, so phosphor-removing effect has much room for improvement.And the sludge concentration of SBR limit grillages mud is not high.Therefore the improvement carried out with regard to the denitrogenation dephosphorizing function that is aimed at the permanent water level SBR of further raising technology of the present invention.
Summary of the invention
The technical problem that (one) will solve
The objective of the invention is the technology that constant water level sequencing batch active sludge is disposed of sewage is made improvement, strengthen denitrogenation dephosphorizing and removal effect of organic matter, improved plant factor simultaneously to reach.
(2) technical scheme
The present invention proposes the system that a kind of multi-mode sequencing batch activated sludge is disposed of sewage; Comprise that the mud that is communicated with successively concentrates preparatory anoxic pond, first functional pool, second functional pool, first Aerobic Pond, oxygen compatibility pool, second Aerobic Pond, first sequencing batch pond; Said first functional pool and second functional pool are anaerobic pond or anoxic pond, and both are the difference in functionality pond.
Wherein, mud concentrate be provided with in the preparatory anoxic pond with mud be back to first functional pool sludge reflux pump, discharge the sludge pump of excess sludge, with the supernatant reflux pump of supernatant liquid pump to the first Aerobic Pond.
Wherein, be provided with water-in and whisking appliance in first functional pool; Be provided with water-in and whisking appliance in second functional pool; Be provided with whisking appliance, aeration head in the oxygen compatibility pool; First sequencing batch pond is provided with whisking appliance, aeration head, water port, the reflux pump that is connected with anoxic pond and mud is drained into the porous suction pipe that mud concentrates preparatory anoxic pond.
Wherein, Also comprise the 3rd Aerobic Pond and second sequencing batch pond; The 3rd Aerobic Pond is connected with the oxygen compatibility pool and second sequencing batch pond respectively, is provided with whisking appliance, aeration head, water port, the reflux pump that is connected with anoxic pond in second sequencing batch pond and mud is drained into the porous suction pipe that mud concentrates preparatory anoxic pond.
Wherein, said whisking appliance is a diving mixer.
The present invention proposes the method that a kind of sequencing batch activated sludge is disposed of sewage, and the treatment system of using the present invention to propose is handled sewage.
Wherein, oxygen compatibility pool moves by aerobic or anoxic mode.The sewage mixed solution is during according to anaerobic-anoxic-aerobic mode operation, and oxygen compatibility pool moves as aerobic lattice, and first functional pool is an anaerobic pond, and second functional pool is an anoxic pond, and aerobic lattice and first, second, third Aerobic Pond are combined into an Aerobic Pond operation; The sewage mixed solution is during according to anoxic-anaerobic-aerobic mode operation, and oxygen compatibility pool moves as aerobic lattice, and first functional pool is an anoxic pond, and second functional pool is an anaerobic pond, and aerobic lattice and first, second, third Aerobic Pond are combined into an Aerobic Pond operation; The sewage mixed solution is during according to anaerobic-anoxic-aerobic-anaerobic-aerobic mode operation, and oxygen compatibility pool moves as anoxic pond, and first functional pool is an anaerobic pond, and second functional pool is an anoxic pond.
Wherein, said anaerobic-anoxic-aerobic pattern may further comprise the steps:
(1) the aeration head valve open of oxygen compatibility pool, whisking appliance cuts out, as aerobic lattice operation;
(2) make through grid and the pretreated part or all of sewage entering anaerobic pond of settling pit; Be combined into mixed solution with the returned sluge that concentrates preparatory anoxic pond from mud; Make polyP bacteria wherein absorb releases phosphorus by the volatile acid of sewage hydrolyzing acidifying generation; The residence time is 1.0～2.0 hours, and the volume ratio of the total water inlet of sludge back flow quantity and system is that reflux ratio is 0.2～0.6: 1;
(3) the sewage mixed solution gets into anoxic pond through behind the anaerobic pond; Also get into this functional pool through grid and the pretreated part of contaminated water of settling pit; Simultaneously with Aerobic Pond in the mixed solution that refluxes mix; Remove the nitrate salt that brings in the phegma, the volume ratio of the total water inlet of backflow mixed liquor and system is that reflux ratio is 0.5～1.5: 1, and the residence time is 1.0～2.0 hours;
(4) the sewage mixed solution flows in the Aerobic Pond, makes the organic matter degradation in the sewage, removes ammonia nitrogen wherein through nitration reaction, through the biological excessive absorption of polyP bacteria phosphorus wherein.
Wherein, said anoxic-anaerobic-aerobic pattern may further comprise the steps:
(1) the aeration head valve open of oxygen compatibility pool, whisking appliance cuts out, as aerobic lattice operation;
(2) make through grid and the pretreated part of contaminated water entering of settling pit anoxic pond; The mud that concentrates after concentrating in the preparatory anoxic pond with mud mixes; Simultaneously with Aerobic Pond in the mixed-liquor return that refluxes, remove the nitrate salt that brings in the phegma, the volume ratio that sludge back flow quantity and system always intake is that reflux ratio is 0.2～0.6: 1; The volume ratio of the total water inlet of backflow mixed liquor and system is that reflux ratio is 0.5～1.5: 1, and the residence time is 1.0～2.0 hours;
(3) make the sewage mixed solution in the anoxic pond get into anaerobic pond with process grid and the pretreated part of contaminated water of settling pit; Both mix; Make polyP bacteria wherein absorb the releases phosphorus by the volatile acid of sewage hydrolyzing acidifying generation, the residence time is 1.0～2.0 hours.
(4) the sewage mixed solution flows in the Aerobic Pond, makes the organic matter degradation in the sewage, removes ammonia nitrogen wherein through nitration reaction, through the biological excessive absorption of polyP bacteria phosphorus wherein.
Wherein, said anaerobic-anoxic-aerobic-anaerobic-aerobic pattern may further comprise the steps:
(1) the aeration head valve closes of oxygen compatibility pool; Whisking appliance is opened; As anoxic pond operation, subsequent use carbon source is then dropped in (like the biochemical oxygen demand on the 5th of water inlet and ratio BOD5/TKN＜3.5 of kjeldahl nitrogen) in these lattice if when the water-inlet carbon source deficiency can't satisfy higher denitrogenation requirement;
(2) make through grid and the pretreated part or all of sewage entering anaerobic pond of settling pit; Be combined into mixed solution with the returned sluge that concentrates preparatory anoxic pond from mud; Make polyP bacteria wherein absorb releases phosphorus by the volatile acid of sewage hydrolyzing acidifying generation; The residence time is 1.0～2.0 hours, and the volume ratio of the total water inlet of sludge back flow quantity and system is that reflux ratio is 0.2～0.6: 1;
(3) the sewage mixed solution gets into anoxic pond through behind the anaerobic pond; Also can get into this functional pool through grid and the pretreated part of contaminated water of settling pit; Mix through the mixed solution of blowback stream simultaneously with in the Aerobic Pond; Remove the nitrate salt that brings in the phegma, the volume ratio of the total water inlet of backflow mixed liquor and system is that reflux ratio is 0.5～1.5: 1, and the residence time is 1.0～2.0 hours; Get into first Aerobic Pond afterwards, get into anoxic pond then.
(4) the sewage mixed solution flows in the second and the 3rd Aerobic Pond and first sequencing batch pond and carries out aerobic reaction, makes the organic matter degradation in the sewage, removes ammonia nitrogen wherein through nitration reaction, through the biological excessive absorption of polyP bacteria phosphorus wherein.First sequencing batch pond is in mixed-liquor return, rhythmic reaction stage in this half period; Then begin quiescent setting (accomplishing the solid-liquid separation of treat effluent and active sludge); And meanwhile, second sequencing batch pond is in the water stage of straining in this semi-period, and treat effluent is discharged by this pond.
The sewage mixed solution through step (4) afterwards, first sequencing batch pond gets into down half period-strain the water stage, through behind the quiescent setting and water outlet up to standard is discharged; And this moment second sequencing batch pond, begin to go up half period-carry out mixed-liquor return, rhythmic reaction, quiescent setting stage.The volume ratio of the total water inlet of mixed-liquor return amount and system is 0.5～1.5: 1.
Wherein, the mud in first and second sequencing batch ponds concentrates preparatory anoxic pond by porous suction pipe Artesian Drainage to mud, and through 40-60 minute concentrate, sludge concentration reached 20000mg/L, refluxes then and perhaps discharges, and reflux ratio is 0.2～0.6: 1.
(3) beneficial effect
The permanent water level SBR of multi-mode intensified denitrification and dephosphorization of the present invention WWT improved system, with respect to prior art, its advantage comprises:
1, phosphor-removing effect is better: increased mud and concentrated preparatory anoxic pond, when middle reaction tank was set to anaerobic-anoxic-aerobic pattern, the mud that is equivalent to be provided with to anaerobic pond refluxed; And mud is after concentrating; Concentration improves, and flow reduces, and reflux ratio reduces; Therefore sewage mixes the back at the corresponding lengthening of the residence time of anaerobic pond meeting with returned sluge, has improved the effect of anaerobic phosphorus release.
In addition; Returned sluge is the anti-nitration reaction under high sludge concentration condition in mud concentrates preparatory anoxic pond; Getting into anaerobic pond again mixes and carries out anaerobic reaction with water inlet; Reduced the total amount that refluxes to system's anaerobic zone and organic dilution of anterior reaction zone carbon source and control nitrate salt entering anaerobic zone, made the anaerobic phosphorus release better effects if.
The mud enrichment region has concentrated the mud that is back to anaerobic pond, and supernatant is directly got back to back segment Aerobic Pond origin or beginning.The key of biological phosphate-eliminating is the quantity and the remaining oxygen source of the acquisition of VFA (voltaile fatty acid), common heterotrophic bacterium and polyP bacteria.The amount of VFA depends on that VFA and the heterotrophic bacterium in the water of source transforms the VFA that BCOD (biodegradable COD) produces, and VFA is decided by water quality in the water of source, transforms quantity and the hydraulic detention time that VFA then is decided by heterotrophic microorganism by BCOD.The mud quantity of reflux is more little, and the actual hydraulic detention time of anaerobic pond is long more, provides to polyP bacteria and has more utilized VFA to be converted into the PHB chance of (gathering-beta-hydroxy acid), thereby improved the dephosphorization efficiency by using of system.
2, denitrification effect is better: the mud enrichment region has reduced the returned sluge flow that gets into the reaction tank lattice, and the returned sluge total amount does not reduce.After backflow mixed liquor is through mud-water separation (concentrating) district; Anoxic pond is proceeded denitrification to remaining NO3-N (nitric nitrogen) in advance; Anoxic pond relies on the internal carbon source denitrification; Because the MLSS after process mud concentrates can reach 20000mg/L, the endogenous respiration effect of high density MLSS produces great demand to oxygen, thereby has strengthened the denitrification of preparatory anoxic pond and the reduction of NO3-N concentration.Under higher microorganism concn, the degree of endogenous denitrification is very considerable.
After concentrating, reduced returned sluge the flow of total system; Increased the actual residence time of sludge concentration and front end area; Except having strengthened biological phosphate-eliminating and anti-nitration reaction, also increased the reactant concn of the total amount of nitrifier, actual nitration reaction time and front end area.Strengthen nitration reaction, guaranteed system's organonitrogen and ammonia-N removal rate.
3, sludge discharge way is better: increased the mud enriching section, mud is being arranged excess sludge again after concentrating, and sludge concentration can be higher, and row's mud discharge can lack, but the mud total amount can not become.Follow-up like this sludge treatment efficient can be higher, and treatment effect can be better.The residual sludge pump of two SBR limit lattice can reduce by a cover simultaneously, only needs in mud concentrates preparatory anoxic pond, to arrange that a cover residual sludge pump gets final product, and has improved the utilization ratio of residual sludge pump.
4, multi-mode adjustment, flexible operation: can carry out the multi-mode adjustment: like anaerobic-anoxic-aerobic pattern (being beneficial to dephosphorization) according to the influent quality situation; Anoxic-anaerobic-aerobic pattern (being beneficial to denitrogenation); Like anaerobic-anoxic-aerobic-anaerobic-aerobic multistage pattern (being beneficial to dephosphorization denitrogenation).The adjustment of above operation scheme does not need to purchase the mixed-liquor return pump by SBR limit lattice to anoxic pond more, only needs the position of mixed-liquor return pump is adjusted or adjusted through the return flow channel valve, therefore need not increase the equipment purchasing expense.
Description of drawings
Fig. 1 is A in the prior art
2/ O general flow chart.
Fig. 2 is constant water level sequencing batch active sludge technology in the prior art (being permanent water level SBR technology) operational mode figure.
Fig. 3 is anaerobic-anoxic of the present invention-aerobic pattern.
Fig. 4 is anoxic of the present invention-anaerobic-aerobic pattern.
Fig. 5 is anaerobic-anoxic of the present invention-aerobic-anaerobic-aerobic pattern.
Among Fig. 1～Fig. 5, the 1st, water-in, the 2nd, anaerobic pond, the 3rd, anoxic pond, the 4th, aerobic (nitrated) pond; The 5th, second pond, the 6th, water outlet, the 7th, mixed-liquor return, the 8th, returned sluge, the 9th, excess sludge; The 10th, mud concentrates preparatory anoxic pond, and the 11st, oxygen compatibility pool (good oxygen condition), the 12nd, oxygen compatibility pool (anoxic condition), the 13rd, water port; 14 is first sequencing batch pond (straining the water stage), and 15 is second sequencing batch pond (returned sluge/rhythmic reactions/quiescent setting stage), the 16th, and mixed-liquor return pump, the 17th, supernatant reflux pump; The 18th, sludge reflux pump, the 19th, residual sludge pump, the 20th, diving mixer, the 21st, quiet heavy back mud is collected from perforated tube and is flow to the concentrated preparatory anoxic pond of mud in the sequencing batch reaction tank.
Embodiment
Below in conjunction with accompanying drawing and embodiment, specific embodiments of the invention is done and is described in further detail.Following examples are used to explain the present invention, but are not used for limiting scope of the present invention.
Embodiment 1:
The system that a kind of multi-mode constant water level sequencing batch active sludge modified version that the present invention proposes is disposed of sewage comprises first and second sequencing batch ponds of the permanent water level that is positioned at intermediary continuous pond lattice and two symmetric arrangement.Being positioned at the continuous pond of intermediary lattice comprises: mud concentrates preparatory anoxic pond, anoxic pond, anaerobic pond and first Aerobic Pond, and the first Aerobic Pond back segment is provided with oxygen compatibility pool, is provided with aeration head valve and whisking appliance in the oxygen compatibility pool.Aerobic Pond also comprises the second and the 3rd Aerobic Pond, is communicated with first and second sequencing batch ponds respectively, and the second and the 3rd Aerobic Pond and first and second sequencing batch ponds are arranged symmetrically in lattice both sides, continuous pond, are provided with the porous suction pipe in the sequencing batch pond; Anoxic pond is connected with anaerobic pond, is provided with water-in and whisking appliance in the anoxic pond; Anaerobic pond is connected with first Aerobic Pond, is provided with water-in and whisking appliance in the anaerobic pond; Described first sequencing batch pond and second sequencing batch pond are connected by pump with anoxic pond respectively, are respectively equipped with pump in first sequencing batch pond and second sequencing batch pond, whisking appliance and water port.
Embodiment 2: with anaerobic-anoxic-aerobic mode treatment sewage
The flow process of sewage is: at first make through grid and the pretreated part or all of sewage of settling pit and get into anaerobic pond; Mix with the returned sluge that concentrates preparatory anoxic pond from mud; Make polyP bacteria wherein absorb releases phosphorus by the volatile acid of sewage hydrolyzing acidifying generation; The residence time is 1 hour, and the volume ratio of the total water inlet of sludge back flow quantity and system is that reflux ratio is 0.3: 1; Be anoxic pond behind the anaerobic pond, the sewage in the anoxic pond is mixed with process grid and the pretreated part of contaminated water of settling pit, the mixed solution in the Aerobic Pond flows into anoxic pond through pump simultaneously, removes the nitrate salt that brings in the phegma, and the residence time is 1.0 hours; Sewage continues to flow in Aerobic Pond and first sequencing batch pond (this moment, first sequencing batch pond was in first cycle of mixed-liquor return, reaction, quiescent setting); Make the organic matter degradation in the sewage; Remove the ammonia nitrogen in the sewage through nitration reaction; Through the phosphorus in the biological excessive absorption sewage of polyP bacteria, then begin quiescent setting (accomplishing the solid-liquid separation of treat effluent and active sludge).And meanwhile, second sequencing batch pond is in this semi-period and strains the water stage.
Afterwards, first sequencing batch pond gets into down half period-strain the water stage, through behind the quiescent setting and water outlet up to standard is discharged; And this moment second sequencing batch pond, begin to go up half period-mixed-liquor return, gap reaction, quiescent setting stage.The volume ratio of the total water inlet of mixed-liquor return amount and system is 0.5: 1.
Mud in first and second sequencing batch ponds concentrates preparatory anoxic pond by porous suction pipe Artesian Drainage to mud, and through 40 minutes concentrate, sludge concentration reached 20000mg/L, refluxes then or discharge.
The water quality parameter of embodiment 2 is following:
Influent quality is:
BOD
5＝170mg/L；
CODcr＝350mg/L；
SS＝180mg/L；
TN＝45mg/L；
NH
3-N＝180mg/L；
TP＝5mg/L。
Effluent quality is:
BOD
5≤10mg/L；
CODcr≤45mg/L；
SS≤10mg/L；
TN≤12mg/L；
NH
3-N≤4mg/L；
TP≤0.5mg/L。
Embodiment 3: with anoxic-anaerobic-aerobic mode treatment sewage
The flow process of sewage is: get into anoxic pond through grid and the pretreated part of contaminated water of settling pit; The mud that concentrates after concentrating in the preparatory anoxic pond with mud mixes; Simultaneously with Aerobic Pond in the mixed-liquor return that refluxes, remove the nitrate salt that brings in the phegma, the volume ratio that sludge back flow quantity and system always intake is that reflux ratio is 0.6: 1; The volume ratio of the total water inlet of backflow mixed liquor and system is that reflux ratio is 1: 1, and the residence time is 2.0 hours; Make the sewage in the anoxic pond get into anaerobic pond with process grid and the pretreated part of contaminated water of settling pit, both mix, and make polyP bacteria wherein absorb the releases phosphorus by the volatile acid of sewage hydrolyzing acidifying generation, and the residence time is 2.0 hours; Sewage is flowed in the Aerobic Pond, make the organic matter degradation in the sewage, remove the ammonia nitrogen in the sewage through nitration reaction, through the phosphorus in the biological excessive absorption sewage of polyP bacteria, the reaction times calculates according to Inlet and outlet water water quality and decides; Other is with embodiment 2.
The water quality parameter of embodiment 3 is following:
Influent quality is:
BOD
5＝160mg/L；
CODcr＝300mg/L；
SS＝180mg/L；
TN＝45mg/L；
NH
3-N＝180mg/L；
TP＝4mg/L。
Effluent quality is:
BOD
5≤8mg/L；
CODcr≤45mg/L；
SS≤10mg/L；
TN≤12mg/L；
NH
3-N≤4mg/L；
TP≤0.5mg/L。
Embodiment 4: with anaerobic-anoxic-aerobic-anaerobic-aerobic mode treatment sewage
The sewage flow process is with embodiment 1, and the aeration head by-pass valve control of the oxygen compatibility pool that behind first section aerobic lattice, is provided with is closed, and whisking appliance is opened, and moves by the anoxic mode.If denitrogenation requires when high, can subsequent use carbon source be dropped into these lattice, to strengthen denitrification reaction.
In the said system, be positioned at the intermediary pond and be respectively the concentrated preparatory anoxic pond of mud, anaerobic pond, anoxic pond and first Aerobic Pond.Concrete ordering form is arranged according to above-mentioned three kinds of different operational modes.This technology is identical with former permanent water level SBR technology; The second and the 3rd Aerobic Pond, two sequencing batch ponds (SBR limit lattice) are arranged symmetrically in the both sides in continuous pond; The functional cycle property exchange of sequencing batch pond: when water is being strained during the stage in a pond wherein, another pond is then carried out mixed-liquor return, rhythmic reaction and quiescent setting (accomplishing the solid-liquid separation of treat effluent and active sludge) successively; Vice versa.When sequencing batch pond was strained water, treat effluent was replaced discharge continuously by this pond.Displacement is strained the water time and is generally 2hr; This moment, an other sequencing batch pond then carried out mixed-liquor return, rhythmic reaction and quiescent setting.
Country's " urban wastewater treatment firm pollutant emission standard " is one-level A emission standard (GB18918-2002), and specific targets are following:
Biochemical oxygen demand BOD on the 5th
5≤10mg/L,
Cod codcr≤the 50mg/L that adopts SRM 935a to measure as oxygenant,
Suspension content SS≤10mg/L,
Total nitrogen TN≤15mg/L,
Ammonia-nitrogen content NH
3-N≤5 (8) mg/L,
Total phosphorus TP≤0.5mg/L.
The water quality parameter of embodiment 4 is following:
Influent quality is:
BOD
5＝180mg/L；
CODcr＝350mg/L；
SS＝180mg/L；
TN＝45mg/L；
NH
3-N＝180mg/L；
TP＝4mg/L。
Effluent quality is:
BOD
5≤10mg/L；
CODcr≤45mg/L；
SS≤10mg/L；
TN≤12mg/L；
NH
3-N≤4mg/L；
TP≤0.5mg/L。
Water outlet has reached (GB18918-2002) one-level A emission standard of country's " urban wastewater treatment firm pollutant emission standard ".
Among the embodiment 1-4; Overall yield coefficient: Yt=0.8～1.1kgTSS/kgBOD5, sludge loading: Ls=0.07～0.15kgBOD5/ (kgMLSSd), return sludge ratio: 20～60%; Supernatant reflux ratio: 20～60%; Sludge concentration (MLSS): X=2.5～4.5g/L, sequencing batch pond long-width ratio >=3: 1, the depth of water is between 5～6 meters.
Claims (10)
1. system that the multi-mode sequencing batch activated sludge is disposed of sewage; Comprise that the mud that is communicated with successively concentrates preparatory anoxic pond, first functional pool, second functional pool, first Aerobic Pond, oxygen compatibility pool, second Aerobic Pond, first sequencing batch pond; Said first functional pool and second functional pool are anaerobic pond or anoxic pond, and both are the difference in functionality pond;
Said mud concentrate be provided with in the preparatory anoxic pond with mud be back to first functional pool sludge reflux pump, discharge the sludge pump of excess sludge, with the supernatant reflux pump of supernatant liquid pump to the first Aerobic Pond;
Be provided with water-in and whisking appliance in said first functional pool; Be provided with water-in and whisking appliance in said second functional pool; Be provided with whisking appliance, aeration head in the said oxygen compatibility pool; Said first sequencing batch pond is provided with whisking appliance, aeration head, water port, the reflux pump that is connected with anoxic pond and mud is drained into the porous suction pipe that mud concentrates preparatory anoxic pond.
2. system according to claim 1; It is characterized in that; Also comprise the 3rd Aerobic Pond and second sequencing batch pond; Said the 3rd Aerobic Pond is connected with the oxygen compatibility pool and second sequencing batch pond respectively, is provided with whisking appliance, aeration head, water port, the reflux pump that is connected with anoxic pond in second sequencing batch pond and mud is drained into the porous suction pipe that mud concentrates preparatory anoxic pond.
3. system according to claim 1 and 2 is characterized in that, said whisking appliance is a diving mixer.
4. the method that sequencing batch activated sludge is disposed of sewage is characterized in that, uses claim 1 or 2 described treatment systems that sewage is handled.
5. method according to claim 4 is characterized in that, oxygen compatibility pool moves by aerobic or anoxic mode; The sewage mixed solution is during according to anaerobic-anoxic-aerobic mode operation, and oxygen compatibility pool moves as aerobic lattice, and first functional pool is an anaerobic pond, and second functional pool is an anoxic pond, and aerobic lattice and first, second, third Aerobic Pond are combined into an Aerobic Pond operation; The sewage mixed solution is during according to anoxic-anaerobic-aerobic mode operation, and oxygen compatibility pool moves as aerobic lattice, and first functional pool is an anoxic pond, and second functional pool is an anaerobic pond, and aerobic lattice and first, second, third Aerobic Pond are combined into an Aerobic Pond operation; The sewage mixed solution is during according to anaerobic-anoxic-aerobic-anaerobic-aerobic mode operation, and oxygen compatibility pool moves as anoxic pond, and first functional pool is an anaerobic pond, and second functional pool is an anoxic pond.
6. method of disposing of sewage as claimed in claim 4 is characterized in that, said anaerobic-anoxic-aerobic pattern may further comprise the steps:
(1) the aeration head valve open of oxygen compatibility pool, whisking appliance cuts out, as aerobic lattice operation;
(2) make through grid and the pretreated part or all of sewage entering anaerobic pond of settling pit; Be combined into mixed solution with the returned sluge that concentrates preparatory anoxic pond from mud; Make polyP bacteria wherein absorb releases phosphorus by the volatile acid of sewage hydrolyzing acidifying generation; The residence time is 1.0～2.0 hours, and the volume ratio of the total water inlet of sludge back flow quantity and system is that reflux ratio is 0.2～0.6: 1;
(3) the sewage mixed solution is through getting into anoxic pond behind the anaerobic pond, and mixes through grid and the pretreated part of contaminated water of settling pit, simultaneously with Aerobic Pond in the mixed solution that flows through blowback mix, the nitrate salt that brings in the removal phegma, the residence time is 1.0～2.0 hours;
(4) the sewage mixed solution flows in the Aerobic Pond and first sequencing batch pond, makes the organic matter degradation in the sewage, removes ammonia nitrogen wherein through nitration reaction, through the biological excessive absorption of polyP bacteria phosphorus wherein.
7. method of disposing of sewage as claimed in claim 4 is characterized in that, said anoxic-anaerobic-aerobic pattern may further comprise the steps:
(1) the aeration head valve open of oxygen compatibility pool, whisking appliance cuts out, as aerobic lattice operation;
(2) make through grid and the pretreated part of contaminated water entering of settling pit anoxic pond; The mud that concentrates after concentrating in the preparatory anoxic pond with mud mixes; Simultaneously with Aerobic Pond in the mixed-liquor return that refluxes, remove the nitrate salt that brings in the phegma, the volume ratio that sludge back flow quantity and system always intake is 0.2～0.6: 1; The volume ratio of the total water inlet of backflow mixed liquor and system is 0.5～1.5: 1, and the residence time is 1.0～2.0 hours;
(3) make the sewage mixed solution in the anoxic pond get into anaerobic pond with process grid and the pretreated part of contaminated water of settling pit; Both mix; Make polyP bacteria wherein absorb the releases phosphorus by the volatile acid of sewage hydrolyzing acidifying generation, the residence time is 1.0～2.0 hours;
(4) the sewage mixed solution flows in the Aerobic Pond and first sequencing batch pond, makes the organic matter degradation in the sewage, removes ammonia nitrogen wherein through nitration reaction, through the biological excessive absorption of polyP bacteria phosphorus wherein.
8. method of disposing of sewage as claimed in claim 4 is characterized in that, said anaerobic-anoxic-aerobic-anaerobic-aerobic pattern may further comprise the steps:
(1) the aeration head valve closes of oxygen compatibility pool, whisking appliance is opened, and as anoxic pond operation, if the ratio of biochemical oxygen demand on the 5th of water inlet and kjeldahl nitrogen is less than 3.5, when promptly the water-inlet carbon source deficiency can't satisfy higher denitrogenation requirement, then in these lattice, drops into subsequent use carbon source;
(2) make through grid and the pretreated part or all of sewage entering anaerobic pond of settling pit; Be combined into mixed solution with the returned sluge that concentrates preparatory anoxic pond from mud; Make polyP bacteria wherein absorb releases phosphorus by the volatile acid of sewage hydrolyzing acidifying generation; The residence time is 1.0～2.0 hours, and the volume ratio of the total water inlet of sludge back flow quantity and system is 0.2～0.6: 1;
(3) the sewage mixed solution gets into anoxic pond through behind the anaerobic pond; Also get into this functional pool through grid and the pretreated part of contaminated water of settling pit; Simultaneously with Aerobic Pond in the mixed solution that refluxes mix; Remove the nitrate salt that brings in the phegma, the volume ratio of the total water inlet of backflow mixed liquor and system is 0.5～1.5: 1, and the residence time is 1.0～2.0 hours; Get into first Aerobic Pond afterwards, get into anoxic pond then;
(4) the sewage mixed solution flows in the second and the 3rd Aerobic Pond and first sequencing batch pond and carries out aerobic reaction, makes the organic matter degradation in the sewage, removes ammonia nitrogen wherein through nitration reaction, through the biological excessive absorption of polyP bacteria phosphorus wherein.
9. like any described method among the claim 6-8, it is characterized in that, the sewage mixed solution through step (4) afterwards, first sequencing batch pond gets into the water outlet stage, through mud-water separation behind the quiescent setting and water outlet up to standard is discharged; And this moment, second sequencing batch pond began to get into mixed-liquor return, reaction, quiescent setting stage; The volume ratio of the total water inlet of mixed-liquor return amount and system is 0.5～1.5: 1.
10. method as claimed in claim 9 is characterized in that, the mud in first and second sequencing batch ponds concentrates preparatory anoxic pond by porous suction pipe Artesian Drainage to mud; Through 40-60 minute concentrate; Sludge concentration reaches 20000mg/L, refluxes then or discharge, and reflux ratio is 0.2～0.6: 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110344667 CN102502963B (en) | 2011-11-04 | 2011-11-04 | Multi-mode sequencing batch active sludge sewage treatment method and system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110344667 CN102502963B (en) | 2011-11-04 | 2011-11-04 | Multi-mode sequencing batch active sludge sewage treatment method and system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102502963A true CN102502963A (en) | 2012-06-20 |
| CN102502963B CN102502963B (en) | 2013-07-10 |
Family
ID=46215114
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201110344667 Active CN102502963B (en) | 2011-11-04 | 2011-11-04 | Multi-mode sequencing batch active sludge sewage treatment method and system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102502963B (en) |
Cited By (23)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102745811A (en) * | 2012-07-31 | 2012-10-24 | 浙江商达环保有限公司 | Process control method of modified sequencing batch reactor (MSBR) system |
| CN103214142A (en) * | 2013-03-18 | 2013-07-24 | 国电银河水务股份有限公司 | Efficient synchronized biological nitrogen and phosphorus removal combined treatment device and method |
| CN103739169A (en) * | 2014-01-21 | 2014-04-23 | 中冶华天工程技术有限公司 | Nitrogen and phosphorus removal method for biological sewage treatment |
| CN104291441A (en) * | 2014-09-11 | 2015-01-21 | 浦华环保有限公司 | Biochemical reaction basin for sewage employing multi-scheme biochemical treatment process and operation method of biochemical reaction basin |
| CN105152334A (en) * | 2015-10-13 | 2015-12-16 | 肖白玉 | Textile mill dyeing wastewater treatment method and system |
| CN105217886A (en) * | 2015-10-10 | 2016-01-06 | 上海市政工程设计研究总院（集团）有限公司 | A kind of method using the biological reaction tank of energy switch mode to dispose of sewage |
| CN105601030A (en) * | 2015-12-19 | 2016-05-25 | 湖南科技大学 | Cycle sequencing batch operation sewage treatment plant and technology |
| CN106277329A (en) * | 2016-10-11 | 2017-01-04 | 临邑禹王植物蛋白有限公司 | A kind of method utilizing twin-stage anoxia/aerobic technical finesse protein production waste water |
| CN106396105A (en) * | 2016-11-29 | 2017-02-15 | 中冶华天南京工程技术有限公司 | A multi-mode reaction tank for sewage treatment |
| CN106495324A (en) * | 2016-11-17 | 2017-03-15 | 天津市市政工程设计研究院 | The multistage AO+SBR sewage disposal reaction tanks of high-efficient denitrification and dephosphorization and method |
| CN106830321A (en) * | 2017-03-02 | 2017-06-13 | 可事托环保设备（上海）有限公司 | Multiple-unit Improvement type sequencing batch reactor and its application |
| CN106830568A (en) * | 2017-03-30 | 2017-06-13 | 东北师范大学 | A kind of biochemistry pool is aerated the method for the treatment of city waste water and device of intermitten service |
| CN107572737A (en) * | 2017-11-01 | 2018-01-12 | 于萍 | A kind of six sections of biochemical sewage processing methods |
| CN108358314A (en) * | 2018-03-08 | 2018-08-03 | 中国市政工程中南设计研究总院有限公司 | Sludge closes on reflux bioreactor facility in combination and application |
| CN108793409A (en) * | 2018-08-29 | 2018-11-13 | 陕西朗正环保科技有限公司 | A kind of sewage-treatment plant suitable for country sewage changes in flow rate |
| CN108892241A (en) * | 2018-08-29 | 2018-11-27 | 陕西朗正环保科技有限公司 | Integrated rural sewage-treatment plant associated with a kind of AAO and SBR technique |
| CN109205779A (en) * | 2017-06-30 | 2019-01-15 | 广东德嘉电力环保科技有限公司 | A kind of Changeful type sewage disposal system |
| CN109534500A (en) * | 2018-05-03 | 2019-03-29 | 哈尔滨工业大学（威海） | One kind passing through multi-functional A2The method that O technique optimizes denitrogenation dephosphorizing |
| CN109867361A (en) * | 2019-04-19 | 2019-06-11 | 上海市市政规划设计研究院有限公司 | Multi-mode activated sludge process integrated sewage treatment device and sewage water treatment method |
| CN111908608A (en) * | 2020-07-07 | 2020-11-10 | 同济大学 | Multi-section variable membrane bioreactor sewage treatment system and use method thereof |
| CN114920358A (en) * | 2022-05-07 | 2022-08-19 | 北京航天威科环保科技有限公司 | RBS intelligent control method for sewage plant |
| CN115140909A (en) * | 2022-08-15 | 2022-10-04 | 广东北控环保装备有限公司 | Internal and external double-reflux sewage treatment equipment, system and method of coupling regulating tank |
| CN116621331A (en) * | 2023-04-24 | 2023-08-22 | 山东源广环保科技有限公司 | Integrated sewage treatment method |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106865893B (en) * | 2017-03-09 | 2019-06-18 | 杭州职业技术学院 | A kind of domestic sewage treatment process |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6015496A (en) * | 1993-04-12 | 2000-01-18 | Khudenko; Boris M. | In-sewer treatment of wastewater and sludges |
| KR20040079111A (en) * | 2003-03-06 | 2004-09-14 | 한국건설기술연구원 | Device and method for continuous feeding and intermittent discharge in sewage and wastewater treatment plant |
| CN1654357A (en) * | 2005-01-21 | 2005-08-17 | 海宁紫光水务有限责任公司 | Multifunctional sewage treatment reaction tank |
| JP3737288B2 (en) * | 1998-09-22 | 2006-01-18 | 株式会社西原環境テクノロジー | Wastewater treatment system |
| CN1821121A (en) * | 2006-03-09 | 2006-08-23 | 武汉凯迪水务有限公司 | Waste water treating process of circulation sequence batched active sludge and its active sludge reactor |
| CN1986455A (en) * | 2006-12-22 | 2007-06-27 | 浦华控股有限公司 | Constant water level sequencing batch active sludge process and system for treating sewage |
| WO2008141413A1 (en) * | 2007-05-18 | 2008-11-27 | Zenon Technology Partnership | Wastewater treatment with aerobic granules |
| CN101973672A (en) * | 2010-10-18 | 2011-02-16 | 余静 | Zero-energy consumption urban sewage dephosphorization treatment method |
| CN202369444U (en) * | 2011-11-04 | 2012-08-08 | 浦华环保有限公司 | Multi-mode constant water level sequencing batch type activated sludge sewage treatment system |
-
2011
- 2011-11-04 CN CN 201110344667 patent/CN102502963B/en active Active
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6015496A (en) * | 1993-04-12 | 2000-01-18 | Khudenko; Boris M. | In-sewer treatment of wastewater and sludges |
| JP3737288B2 (en) * | 1998-09-22 | 2006-01-18 | 株式会社西原環境テクノロジー | Wastewater treatment system |
| KR20040079111A (en) * | 2003-03-06 | 2004-09-14 | 한국건설기술연구원 | Device and method for continuous feeding and intermittent discharge in sewage and wastewater treatment plant |
| CN1654357A (en) * | 2005-01-21 | 2005-08-17 | 海宁紫光水务有限责任公司 | Multifunctional sewage treatment reaction tank |
| CN1821121A (en) * | 2006-03-09 | 2006-08-23 | 武汉凯迪水务有限公司 | Waste water treating process of circulation sequence batched active sludge and its active sludge reactor |
| CN1986455A (en) * | 2006-12-22 | 2007-06-27 | 浦华控股有限公司 | Constant water level sequencing batch active sludge process and system for treating sewage |
| WO2008141413A1 (en) * | 2007-05-18 | 2008-11-27 | Zenon Technology Partnership | Wastewater treatment with aerobic granules |
| CN101973672A (en) * | 2010-10-18 | 2011-02-16 | 余静 | Zero-energy consumption urban sewage dephosphorization treatment method |
| CN202369444U (en) * | 2011-11-04 | 2012-08-08 | 浦华环保有限公司 | Multi-mode constant water level sequencing batch type activated sludge sewage treatment system |
Cited By (32)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102745811A (en) * | 2012-07-31 | 2012-10-24 | 浙江商达环保有限公司 | Process control method of modified sequencing batch reactor (MSBR) system |
| CN103214142A (en) * | 2013-03-18 | 2013-07-24 | 国电银河水务股份有限公司 | Efficient synchronized biological nitrogen and phosphorus removal combined treatment device and method |
| CN103214142B (en) * | 2013-03-18 | 2016-04-06 | 国电银河水务股份有限公司 | Highly effective synchronous biological denitrogenation dephosphorizing Round Sump treatment unit and method |
| CN103739169A (en) * | 2014-01-21 | 2014-04-23 | 中冶华天工程技术有限公司 | Nitrogen and phosphorus removal method for biological sewage treatment |
| CN104291441A (en) * | 2014-09-11 | 2015-01-21 | 浦华环保有限公司 | Biochemical reaction basin for sewage employing multi-scheme biochemical treatment process and operation method of biochemical reaction basin |
| CN104291441B (en) * | 2014-09-11 | 2016-08-24 | 浦华环保股份有限公司 | The biochemical reaction tank of multi-scheme biochemical processing process sewage and operation method thereof |
| CN105217886A (en) * | 2015-10-10 | 2016-01-06 | 上海市政工程设计研究总院（集团）有限公司 | A kind of method using the biological reaction tank of energy switch mode to dispose of sewage |
| CN105152334A (en) * | 2015-10-13 | 2015-12-16 | 肖白玉 | Textile mill dyeing wastewater treatment method and system |
| CN105601030B (en) * | 2015-12-19 | 2018-09-11 | 湖南科技大学 | A kind of sewage-treatment plant and technique of the operation of cycle sequence batch |
| CN105601030A (en) * | 2015-12-19 | 2016-05-25 | 湖南科技大学 | Cycle sequencing batch operation sewage treatment plant and technology |
| CN106277329B (en) * | 2016-10-11 | 2019-10-18 | 临邑禹王植物蛋白有限公司 | A method of utilizing twin-stage anoxic/aerobic technical treatment protein production waste water |
| CN106277329A (en) * | 2016-10-11 | 2017-01-04 | 临邑禹王植物蛋白有限公司 | A kind of method utilizing twin-stage anoxia/aerobic technical finesse protein production waste water |
| CN106495324B (en) * | 2016-11-17 | 2019-08-16 | 天津市市政工程设计研究院 | High-efficient denitrification and dephosphorization multistage AO+SBR sewage disposal reaction tank and method |
| CN106495324A (en) * | 2016-11-17 | 2017-03-15 | 天津市市政工程设计研究院 | The multistage AO+SBR sewage disposal reaction tanks of high-efficient denitrification and dephosphorization and method |
| CN106396105A (en) * | 2016-11-29 | 2017-02-15 | 中冶华天南京工程技术有限公司 | A multi-mode reaction tank for sewage treatment |
| CN106830321A (en) * | 2017-03-02 | 2017-06-13 | 可事托环保设备（上海）有限公司 | Multiple-unit Improvement type sequencing batch reactor and its application |
| CN106830321B (en) * | 2017-03-02 | 2017-12-01 | 可事托环保设备（上海）有限公司 | Multiple-unit Improvement type sequencing batch reactor and its application |
| CN106830568A (en) * | 2017-03-30 | 2017-06-13 | 东北师范大学 | A kind of biochemistry pool is aerated the method for the treatment of city waste water and device of intermitten service |
| CN109205779A (en) * | 2017-06-30 | 2019-01-15 | 广东德嘉电力环保科技有限公司 | A kind of Changeful type sewage disposal system |
| CN107572737A (en) * | 2017-11-01 | 2018-01-12 | 于萍 | A kind of six sections of biochemical sewage processing methods |
| CN108358314A (en) * | 2018-03-08 | 2018-08-03 | 中国市政工程中南设计研究总院有限公司 | Sludge closes on reflux bioreactor facility in combination and application |
| CN108358314B (en) * | 2018-03-08 | 2023-05-05 | 中国市政工程中南设计研究总院有限公司 | Sludge near reflux bioreactor, combined facility and application thereof |
| CN109534500A (en) * | 2018-05-03 | 2019-03-29 | 哈尔滨工业大学（威海） | One kind passing through multi-functional A2The method that O technique optimizes denitrogenation dephosphorizing |
| CN108892241A (en) * | 2018-08-29 | 2018-11-27 | 陕西朗正环保科技有限公司 | Integrated rural sewage-treatment plant associated with a kind of AAO and SBR technique |
| CN108793409A (en) * | 2018-08-29 | 2018-11-13 | 陕西朗正环保科技有限公司 | A kind of sewage-treatment plant suitable for country sewage changes in flow rate |
| CN108793409B (en) * | 2018-08-29 | 2023-12-29 | 中化学朗正环保科技有限公司 | Sewage treatment device suitable for rural sewage flow change |
| CN109867361A (en) * | 2019-04-19 | 2019-06-11 | 上海市市政规划设计研究院有限公司 | Multi-mode activated sludge process integrated sewage treatment device and sewage water treatment method |
| CN109867361B (en) * | 2019-04-19 | 2024-04-16 | 上海市市政规划设计研究院有限公司 | Multi-mode activated sludge process sewage treatment integrated device and sewage treatment method |
| CN111908608A (en) * | 2020-07-07 | 2020-11-10 | 同济大学 | Multi-section variable membrane bioreactor sewage treatment system and use method thereof |
| CN114920358A (en) * | 2022-05-07 | 2022-08-19 | 北京航天威科环保科技有限公司 | RBS intelligent control method for sewage plant |
| CN115140909A (en) * | 2022-08-15 | 2022-10-04 | 广东北控环保装备有限公司 | Internal and external double-reflux sewage treatment equipment, system and method of coupling regulating tank |
| CN116621331A (en) * | 2023-04-24 | 2023-08-22 | 山东源广环保科技有限公司 | Integrated sewage treatment method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102502963B (en) | 2013-07-10 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102502963B (en) | Multi-mode sequencing batch active sludge sewage treatment method and system | |
| CN202369444U (en) | Multi-mode constant water level sequencing batch type activated sludge sewage treatment system | |
| CN109160670B (en) | Denitrification method of municipal sewage denitrification filter based on short-cut denitrification and anaerobic ammonia oxidation | |
| CN102101746B (en) | Low-carbon urban sewage biological phosphorus removal and autotrophic biological nitrogen removal device and method | |
| CN101503248B (en) | Composite biological film activated sludge denitrification dephosphorization denitrification method and reactor thereof | |
| CN105461061A (en) | A<2>/O-biology synchronous nitrogen and phosphorus removal device and method for urban sewage | |
| CN102583743B (en) | Dual-sludge denitrification dephosphorizing and denitrifying A/A-O device and method | |
| CN101519266B (en) | High-efficient denitrification and dephosphorization MBR process and device | |
| CN102126811B (en) | Double-anoxic denitrification method and equipment for enhanced denitrification of sewage | |
| CN101817621B (en) | Semi-denitrification-based wastewater treatment technology | |
| CN102153236A (en) | Rear denitrifying sewage treatment device and process | |
| CN110092536A (en) | A kind of kitchen anaerobic digestion biogas slurry combined treatment process | |
| CN102690019A (en) | High-efficiency nitrogen and phosphorus synchronous removal method in treating low concentration wastewater | |
| CN103121754A (en) | Denitrification and dephosphorization technique | |
| CN112299560A (en) | Continuous flow denitrification dephosphorization series anaerobic ammonia oxidation coupling endogenous denitrification sewage treatment system and method | |
| CN101823814B (en) | Method and system of integrated denitrifying phosphorus and nitrogen removal | |
| CN109368928A (en) | A kind of dephosphorization denitrogenation devices and methods therefor based on short-cut denitrification reaction | |
| CN108046518A (en) | A kind of apparatus and method of the intensified denitrification and dephosphorization of low-carbon-source sewage | |
| CN112142262A (en) | Low CN municipal sewage advanced treatment system and method based on multistage AO side-stream phosphorus removal technology | |
| CN104230110A (en) | Nitrogen and phosphorus removal system and method for treating low-carbon-nitrogen-ratio domestic wastewater by A2O-MBBR (anaerobic-anoxic-oxic-moving bed biofilm reactor) combined chemical process | |
| CN102674548B (en) | Sequencing batch A2O sewage treatment method | |
| CN205442793U (en) | Biological simultaneous nitrogen and phosphorus removal device of municipal sewage A2O - | |
| CN112456641B (en) | Device and method for realizing continuous flow synchronous short-cut nitrification and denitrification dephosphorization based on sludge side treatment | |
| CN103183454A (en) | Coupling type biological denitrification method and system thereof | |
| CN102730833B (en) | Constant water level sequencing batch type activated sludge treatment sewage system with characteristic of multi-stage A-O reinforced denitrogenation and phosphorus removing, and method thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |