CN102718380A - Method and device for reduction treatment of residual sludge - Google Patents
Method and device for reduction treatment of residual sludge Download PDFInfo
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- CN102718380A CN102718380A CN2012102365608A CN201210236560A CN102718380A CN 102718380 A CN102718380 A CN 102718380A CN 2012102365608 A CN2012102365608 A CN 2012102365608A CN 201210236560 A CN201210236560 A CN 201210236560A CN 102718380 A CN102718380 A CN 102718380A
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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
- Y02W10/20—Sludge processing
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Abstract
The invention discloses a method and a device for reduction treatment of residual sludge. After entering an aerobic biochemical reaction basin for aeration and mixing, a mixture of sludge and sewage is led to a settlement basin for settling, and supernate is extracted; the sludge in the settlement basin is periodically drawn into an anaerobic reaction basin for reacting and static settling; equivalent statically-settled supernate in the anaerobic reaction basin is drawn out to flow back to the aerobic biochemical reaction basin; and equivalent sludge in the anaerobic reaction basin is drawn out every three days to flow back to the aerobic biochemical reaction basin, so as to accomplish circulated exchange and flow of the sludge among settlement equipment, anaerobic equipment, aerobic equipment and the settlement equipment. The method of statically settling the supernate in the backflow anaerobic reaction basin is adopted, the concentration of the sludge in the anaerobic reaction basin is increased, the sludge reduction effect is good and stable, and the denitrogenation ability of a process system is improved; in addition, as the concentration of the sludge in the anaerobic reaction basin is increased, and the volume of the anaerobic reaction basin is reduced, constructing and transforming are easy, no reaction devices and equipments are required to be added, the construction cost is low, and the method and the device have a long-term economic benefit.
Description
Technical field
The present invention relates to sewage treatment area, particularly relate to method and device that a kind of excess sludge reduction is handled.
Background technology
Municipal sludge is the sub product that produces in the municipal sewage treatment process, and with regard to the municipal sludge character of China, organic content surpasses 50% in the mud, and contains nutritive substances (wherein N content 1.5%～7.0%, P content 0.8%～3%) such as a large amount of N, P.According to the numeral that China national Environmental Protection Administration provides, Chinese at present annual approximately sewage effluent 40,100,000,000 m
3, seat surplus the municipal sewage plant that has built up running has 400, daily handling ability 2,534 ten thousand m
3Account for 0.3%～0.5% (in the water ratio 97%) of handling the water yield by sludge yield and calculate, the output of Chinese city sewage plant sludge is at 7.602 ten thousand m
3/ d and 12.67 ten thousand m
3Between/the d (in water ratio 97%).Therefore, China will face huge sludge treatment and dispose pressure when the WWT cause constantly makes progress.
If in the mud reflux section, add chemistry (ozone, acid or alkali) or physics (thermal treatment, ultrasonication or treat mechanically) processing unit; Excess sludge can reduce more than 60%; But chemistry or physical treatment is with high costs; Can increase aeration tank organic loading and aeration energy consumption simultaneously, influence the practicality of technology.Other has a kind of method is to add uncoupling agents, and controlling microbial is metabolic, thereby reaches the purpose of excess sludge reduction; Reduction rate is at 50%-80%; And energy consumption level is low, but the uncoupling agents that this method added may cause the over-drastic toxic action to mikrobe, influences the Pollutant Treatment performance of technology itself; Uncoupling agents need be made a big purchase in large quantities in addition, has increased running cost.It is thus clear that the present more problem of mud ubiquity after the chemical physics art breading, not high like reuse difficulty, sludge disintegration rate, produce foul smell, energy consumption is big, running cost is high and equipment corrosion etc.And the reducing biological sludge technology mainly is to realize that through changing mikrobe living environment and the effect of itself mud simplifies; Compare with chemistry, physical technique; It can realize mud under the prerequisite that does not influence effluent quality original position decrement have decrement effect preferably, and working cost is low; Non-secondary pollution is to solve the comparatively ideal approach of mud problem in the sewage biochemical processing process.
In the reducing biological sludge technology; Aerobic-deposition-anaerobism (OSA) technology is in sewage treatment process, to realize a kind of novel process of sludge reduction simultaneously; Its essence is by a sludge anaerobic pond of the aeration tank in the conventional activated sludge process and settling tank and between insertion and form that the mud of settling tank bottom is extracted out and got in the anaerobic pond, under anaerobic reacts for some time; Then the muddy water mixed solution in the anaerobic pond is mended in the aeration tank, realized aerobic-deposition-anaerobic circulation.This mode; Neither need carry out pre-treatment, also need not add any chemical agent through physics or chemical means, can be under the prerequisite that does not influence effluent quality; Can reduce the 20%-60% of excess sludge production; Improved sludge settling property simultaneously, can transform, made that capital construction and running cost are lower traditional activated sludge process.This has significance for the sludge quantity that solution China increases substantially in the future.
Yet still there is certain defective in OSA technology itself at present.Because the aerobic sludge reflux section that OSA technology is equal at traditional activated sludge process has inserted an anaerobic reation pool; After the mud process anaerobic jar processing that settling tank is discharged, be back to the aeration tank again; Changed the living environment of mikrobe in fact; Also change microbial species group structure and sludge quality in the former aerobic activated sludge to a certain extent, when this brings the sludge reduction effect for system, also influenced the activity of system sludge; Can bring disadvantageous result to WWT; Reduction like sludge yield causes the nitrogen phosphorus element in the mud that reduces part to enter into aqueous phase, has increased the weight of process system nitrogen and phosphorus pollutants burden, thereby makes the water outlet total nitrogen total phosphorus increase.Simultaneously, general traditional OSA technology reflux ratio probably is about 10%, and the volume of anaerobic reation pool is big; Cost is high, difficult management, and OSA technology has big mud decrement potential; Therefore constantly optimize improvement OSA technology; Improve the performance of this technology each side, give full play to OSA sludge reduction effect, the application of popularization OSA and the processing of China's excess sludge are had extremely important meaning.
Summary of the invention
Based on this, be necessary to provide the excess sludge reduction treatment process that a kind of mud decrement effect is obvious, efficiencies of nitrogen removal good, running cost is low.
A kind of excess sludge reduction treatment process may further comprise the steps:
(1) after mud and sewage mixture get into the interior aeration mixing of aerobic biochemical reaction tank, introduces deposition in the settling tank, draw supernatant;
(2) periodicity extracts in the mud entering anaerobic reation pool in the settling tank and reacts, and is quiet heavy; The quiet heavy supernatant of extracting the anaerobic reation pool moderate out is back in the aerobic biochemical reaction tank;
(3) every mud of extracting the anaerobic reation pool moderate at a distance from 3 days out is back in the aerobic biochemical reaction tank, accomplishes the circulation exchange of mud between each equipment of deposition-anaerobic-aerobic-deposition and flows.
Equivalent in the step (2) be meant with get into anaerobic reation pool in the amount that equates of mud.
Mud in the anaerobic reactor is in the state that mixes always, stops in preceding 1 hour stirring mud-water separation, backflow anaerobic sludge supernatant at time mud.Whenever the mixing sludge in 3 days backflow anaerobic reactors; Do not stop to stir before promptly returning mud; Be mixing sludge in the anaerobic reactor, backflow be the mixing sludge of equivalent, the equivalent in the step (3) be meant with settling tank in get into the mud in the anaerobic reation pool amount equate.
Among embodiment, the cycle described in the step (2) is 6 hours therein.
Among embodiment, the quiet heavy time described in the step (2) is 1 hour therein.
Among embodiment, said step (2) is therein: the mud of 2.5% volume ratio gets in the anaerobic reation pool and reacts quiet heavy 1 hour in per 6 hours extraction settling tanks; The quiet heavy supernatant of extracting 2.5% volume ratio in the anaerobic reation pool out is back in the aerobic biochemical reaction tank.
Therein among embodiment, in the step (3) every in 3 days extraction anaerobic reation pools the mud of 5% volume ratio be back in the aerobic biochemical reaction tank.
The present invention also provides a kind of excess sludge reduction treatment unit, comprises aerobic biochemical reaction tank, settling tank and anaerobic reation pool; The outlet of said aerobic biochemical reaction tank connects the inlet of said settling tank, and the outlet of said settling tank connects the inlet of said anaerobic reation pool, and the outlet of said anaerobic reation pool connects the inlet of aerobic biochemical reaction tank.
Among embodiment, said aerobic biochemical reaction tank is provided with aeration head therein.
Among embodiment, said anaerobic reation pool is provided with whipping appts therein.
In the methods of the invention, the phase drains into mud in the anaerobic reation pool weekly, and is every at a distance from three days backflow anaerobic sludges extremely in the aerobic biochemical reaction tank, the quiet heavy supernatant in all the other time backflow anaerobic reation pools.Quiet heavy supernatant is in the cycle in the backflow anaerobic reation pool, and the preceding 1h that refluxes stops the interior magnetic agitation of anaerobic reation pool and treats quiet sinking.And every at a distance from 3 days mud is accomplished digestion reaction in anaerobic reation pool after, not quiet heavy shallow lake is directly in returned sluge to the aerobic biochemical reaction tank.The operation scheme of the quiet heavy supernatant in the backflow anaerobic reation pool is its key link that is different from traditional OSA technology, and it can realize following function:
(1) through adopting the method that leaves standstill supernatant in the backflow anaerobic reation pool, strengthened the sludge concentration of anaerobic reation pool, the mud organic substance of effectively degrading.Through whenever having concentrated the sludge concentration of anaerobic reation pool at a distance from the mode of three days returned sluges, the organism of at every turn entering from the aerobic biochemical reaction tank is decomposed more effectively, increase the labile organic compound in the system, thereby reached the purpose of mud decrement;
(2) sludge reduction is effective and stable, has strengthened the ability of denitrogenating of process system.Reduced impact simultaneously, consolidated the wastewater treatment efficiency of system the aerobic biochemical reaction tank;
(3) adopt the mode of backflow supernatant that sludge concentration is strengthened, thereby reduce the volume of anaerobic reation pool, need not newly-increased reaction unit and equipment, building cost is low, and has long-range economic benefit.
Description of drawings
Fig. 1 is the structural representation of excess sludge reduction treatment unit in the embodiment of the invention 1;
Fig. 2 is the experimental system synoptic diagram of excess sludge reduction treatment unit in the embodiment of the invention 2;
Fig. 3 is that the OSA experimental system sequential of excess sludge reduction treatment process in the embodiment of the invention 2 is set synoptic diagram;
Fig. 4 is the experimental system anaerobism and the aerobic sludge solvability COD ratio relation of excess sludge reduction treatment process in the embodiment of the invention 2;
Fig. 5 is the experimental system anaerobism and the total COD ratio relation of aerobic sludge of excess sludge reduction treatment process in the embodiment of the invention 2.
Reference numeral: 1, sewage; 2, aerobic biochemical reaction tank; 3, the mud mixed liquid that effluents; 4, settling tank; 5, water outlet; 6, the settling tank mud that effluents; 7, anaerobic reation pool; 8, the anaerobic reation pool mud that effluents; 9, aerobic biochemical reaction tank; 10, aerobic biochemical reaction tank; 11, anaerobic reation pool; 12, anaerobic reation pool; 13, intake pump 14, go out water pump; 15, aerobic sludge reflux pump; 16, anaerobic sludge reflux pump; 17, aerobic sludge reflux pump; 18, anaerobic sludge reflux pump; 19, former bucket.
Embodiment
Below in conjunction with accompanying drawing and specific embodiment the present invention is done further elaboration.
As shown in Figure 1; A kind of excess sludge reduction treatment unit; Form by aerobic biochemical reaction tank 2, settling tank 4 and anaerobic reation pool 7; Wherein the outlet of aerobic biochemical reaction tank 2 connects the inlet of settling tank 4, and the outlet of settling tank 4 connects the inlet of anaerobic reation pool 7, and the outlet of anaerobic reation pool 7 connects the inlet of aerobic biochemical reaction tank 2.
A kind of excess sludge reduction treatment process of the present invention may further comprise the steps:
(1) after sewage 1 got into and carries out sufficient aeration mixing in the aerobic biochemical reaction tank 2, the mud mixed liquid 3 that effluents of aerobic biochemical reaction tank 2 was introduced deposition in the settling tanks 4, and supernatant is drawn as water outlet 5;
(2) periodically extract quantitative settling tank in the settling tank 4 mud 6 that effluents and get in the anaerobic reation pools 7, under anaerobic react, reaction quiet heavy 1 hour of the back that finishes; The quiet heavy supernatant of extracting anaerobic reation pool 7 moderates out is back in the aerobic biochemical reaction tank 2;
(3) every anaerobic reation pool of extracting anaerobic reation pool 7 moderates at a distance from 3 days out mud 8 that effluents is back in the aerobic biochemical reaction tank 2, accomplishes the circulation of mud between each equipment of deposition-anaerobic-aerobic-deposition and exchanges mobile.
The effect research of the excess sludge reduction treatment process of embodiment 2 embodiment 1
This embodiment further specifies the effect of the inventive method through the contrast experiment.
Excess sludge reduction treatment process of the present invention is the basis with SBR-OSA (sequence intermittent activated sludge process-aerobic-deposition-anaerobism) technology; On the basis that does not increase any device; With backflow anaerobic reation pool 7 quiet heavy supernatants; Whenever the operation scheme that replaces traditional backflow mixing sludge at a distance from the operation scheme of three days backflow anaerobic reation pool 7 mixing sludges; Form novel SBR-OSA technology,, improve raising system WWT performance in the hope of reducing the impact that refluxes to aerobic biochemical reaction tank 2 through the quiet heavy supernatant that refluxes; Simultaneously also hope further to strengthen OSA (aerobic-deposition-anaerobism) system sludge minimizing usefulness, reduce the anaerobic reation pool volume, reduce cost through this improvement operation scheme.
This experiment has made up traditional SBR-OSA and improvement SBR-OSA (the present invention) two cover process systems compare research.
Fig. 2 is the synoptic diagram of experimental system; Wherein in former bucket 19, dispose synthetic sewage; Fig. 2 lower right is the SBR-OSA novel process model system of modified form of the present invention, and the phase is regularly carried out the quiet heavy supernatant or the mud exchange of SBR (sequence intermittent activated sludge process) aerobic biochemical reaction tank 11, anaerobic reation pool 13 weekly.Quiet heavy supernatant/mud exchange essence is that the quiet heavy mud of SBR is introduced in the anaerobic reation pool 13, and the quiet heavy supernatant/mud in back that stays for some time is got back in the aerobic reaction pond 11 and continued biochemical treatment sewage.
The used equipment of each structural unit is seen table 1 in the system.
The used equipment of table 1 experimental system
In the two cover SBR-OSA experimental installations, a cover serves as that anaerobic reation pool is inserted on the basis with the SBR system, forms traditional SBR-OSA technology through peristaltic pump and time automatic control equipment, and as control experiment group (shown in Fig. 2 upper right side).Another set of system on traditional SBR-OSA technology basis, changes operation scheme, and is promptly from anaerobic reation pool alternately reflux anaerobic sludge and supernatant, every at a distance from 3 days backflow anaerobic sludges (shown in Fig. 2 lower right).Be convenient narration; With traditional SBR-OSA technology code name is " OSA-1 "; Technology code name after the improvement of the present invention is " OSA-2 ", and wherein the aerobic biochemical reaction tank is designated as " O-1 " respectively and " O-2 ", anaerobic reation pool are designated as " A-1 ", " A-2 " respectively.
It is the plastic measuring glass of 5L that aerobic biochemical reaction tank 9,10 all adopts useful volume, height * mouth diameter * end diameter=540mm * 350mm * 250mm, available depth 450mm.The aeration head of packing in the aerobic biochemical reaction tank is regulated aeration rate, and being controlled at the aeration phase dissolved oxygen is 2mg/L～3mg/L, and makes through mixing agitator that mud is in the thorough mixing state in the reactor drum.
Take advantage of dress human configuration sewage with plastic tank, whisking appliance is set regulates rotating speed and make the SS in the former water (suspended solid) can't sedimentation.Install between each unit Flow of Goods and Materials and carry through peristaltic pump and accomplish, regulate rotating speed required flow is set.Insert time control switch and realize the sequential setting of OSA system.
In this research, two cover system synchronous operations are provided with time-program(me) through the time automatic control equipment, and realization system Inlet and outlet water, blast aeration, stirring, deposition, robotization idle and the mud exchange are controlled.
This institute takes from Guangzhou with mud and hunts moral sewage work.
Experiment water quality adopts the sewage of human configuration, and its composition has: peptone, glucose, CH
3COONa, NH
4Cl, KH
2PO
4, KHSO
4, NaHCO
3Deng.Artificial sewage's water-quality guideline is seen table 2.
Table 2 experiment artificial sewage water quality
Annotate: COD:chemical oxygen demand (COD); TN:total nitrogen (the inorganic total amount with organonitrogen of various forms in the water); TP:total phosphorus (total content of phosphoric in the water body); SS:suspended solids (suspended solid).
The measuring method of the main monitoring index in the experimentation is seen table 3.
Table 3 monitoring index and measuring method
1. system operational parameters and mode
Adopt 24 hours continuous dynamic operation methods.The water inlet of two cover process systems, quiet heavy, water outlet, mud each cycle of exchange are 6h, in 1 day 4 cycle, adopt identical sequential setting (like Fig. 3).
The phase flooding time is 25min weekly, flooding quantity 500mL, flow 20mL/min.The two cover process systems total amount of intaking every day is 8L, and the configuration in per two days of former water once guarantees that human configuration sewage does not have higher degradation rate.Water outlet time phase is 20min weekly, aquifer yield 500mL, flow 25mL/min.
Aerobic biochemical reaction tank 9,10 useful volumes are 4L, and hydraulic detention time (HRT) is 2d.
Anaerobic reation pool 11 (A-1) and 12 (A-2) useful volume are 750mL, and sludge retention time (SRT) is 5 days.In the OSA-1 system, the phase drains in the anaerobic reation pool A-1 through the mud in quiet heavy latter stage of peristaltic pump with aerobic biochemical reaction tank 2.5% volume ratio weekly, and 5% mud among the A-1 is back to aerobic reactor.In the OSA-2 system, the phase drains into the mud in quiet heavy latter stage of 2.5% volume ratio among the O-2 in the A-2 weekly, every at a distance from three days backflow 5% anaerobic sludges to O-2, the quiet heavy supernatant of all the other time backflow A-2.The quiet heavy supernatant of backflow A-2 is in the cycle, and the preceding 1h that refluxes stops the interior magnetic agitation of A-2 and treats quiet sinking.
Along with the carrying out of experiment, quiet heavy sludge volume can change, and therefore need guarantee that sludge retention time can not produce too great fluctuation process in mud exchange capacity and the anaerobic reation pool according to practical situation trace adjustment mud exchange capacity.
2. experimental result
2.1 mud decrement effectiveness analysis
Investigating the mud actual yield needs the cumulative amount of water outlet SS (suspended solid) and the sludge quantity of experiment sampling loss are all counted in the actual output of mud, i.e. mud actual output=apparent output+water outlet SS semi-invariant+experiment waste.So mud actual yield Y
aCan represent by 2-1:
Wherein, MLSS
D0With MLSS
D200Day and the 200th day sludge concentration (mg/L) for system's startup;
W
SampleBe experiment sampling integration loss amount (mg);
V
aBe aerobic reactor useful volume (4L);
COD
iWith COD
eBe Inlet and outlet water COD MV (mg/L);
Q
dBe phase water consumption (2L/d) around every day;
T
iBe experiment total time in later stage (200d).
System sludge actual yield result sees table 4.
Table 4 system sludge actual yield
Consider water outlet SS integration loss amount, the actual yield 0.1026mgMLSS/mgCOD of mud in the OSA-1 system, the actual yield of mud is 0.0899mgMLSS/mgCOD in the OSA-2 system, OSA-2 is than the actual decrement 11.8% of OSA-1 mud.The more apparent decrement effect of actual decrement has descended 34.5 percentage points, mainly is because higher at the OSA-2 in operation early stage of system water outlet SS, and SS reaches time of tending towards stability than OSA-1 system head.But can see that in Fig. 5 behind d150, the water outlet SS of two systems is very approaching, is about 4mg/L.If consider to begin to calculate mud decrement from d150, OSA-2 will be remarkable than the decrement effect of OSA-1 many, much larger than 11.8%.
2.2 carbon element equilibrium analysis
Further analyze the ratio relation of anaerobic sludge COD and aerobic sludge COD, can estimate organism palliating degradation degree under the anaerobic reaction condition roughly, like Fig. 4 and Fig. 5.
As shown in Figure 4, to sCOD, OSA-1 system and OSA-2 system anaerobic sludge and aerobic sludge average of relatives are 1.28 and 1.17.Get into the interior sCOD of anaerobic reation pool and be lower than the sCOD that refluxes from anaerobic reation pool, explain that sCOD increases to some extent in anaerobic reation pool, and then have intracellular matter after dissolving born of the same parents, to discharge in the mixed solution under the explanation anaerobic reaction condition.
As can beappreciated from fig. 5, to tCOD, A-1/O-1 MV is 0.66, and A-2/O-2 MV is 0.64.Less than 1, explain that COD is cleared up from the ratio of anaerobism mud tCOD that refluxes and the mud tCOD that gets into anaerobic reation pool under anaerobic environment.Can estimate roughly that A-1 has 34% mud tCOD under anaerobism, to obtain cutting down; A-2 has 36% mud tCOD under anaerobism, to obtain degraded.The reduction of tCOD can cause the decline of sludge yield, thereby realizes the effect of sludge reduction.
Can know from above conclusion; OSA-2 is more abundant than the molten born of the same parents of bacterium in the anaerobic reation pool of OSA-1, to the reduction better effects if of active sludge, and combines Fig. 5 two systems can know the reduction analysis of tCOD; The tCOD degradation effect of OSA-2 is better, explains that OSA-2 has better sludge reduction effect.
The above embodiment has only expressed one embodiment of the present invention, and it describes comparatively concrete and detailed, but can not therefore be interpreted as the restriction to claim of the present invention.Should be pointed out that for the person of ordinary skill of the art under the prerequisite that does not break away from the present invention's design, can also make some distortion and improvement, these all belong to protection scope of the present invention.Therefore, the protection domain of patent of the present invention should be as the criterion with accompanying claims.
Claims (8)
1. an excess sludge reduction treatment process is characterized in that, may further comprise the steps:
(1) after mud and sewage mixture get into the interior aeration mixing of aerobic biochemical reaction tank, introduces deposition in the settling tank, draw supernatant;
(2) periodicity extracts in the mud entering anaerobic reation pool in the settling tank and reacts, and is quiet heavy; The quiet heavy supernatant of extracting the anaerobic reation pool moderate out is back in the aerobic biochemical reaction tank;
(3) every mud of extracting the anaerobic reation pool moderate at a distance from 3 days out is back in the aerobic biochemical reaction tank, accomplishes the circulation exchange of mud between each equipment of deposition-anaerobic-aerobic-deposition and flows.
2. excess sludge reduction treatment process according to claim 1 is characterized in that, the cycle described in the step (2) is 6 hours.
3. excess sludge reduction treatment process according to claim 1 is characterized in that, the quiet heavy time described in the step (2) is 1 hour.
4. according to each described excess sludge reduction treatment process of claim 1-3, it is characterized in that said step (2) is: the mud of 2.5% volume ratio gets in the anaerobic reation pool and reacts in per 6 hours extraction settling tanks, quiet heavy 1 hour; The quiet heavy supernatant of extracting 2.5% volume ratio in the anaerobic reation pool out is back in the aerobic biochemical reaction tank.
5. excess sludge reduction treatment process according to claim 1 is characterized in that, the mud of whenever extracting 5% volume ratio in the anaerobic reation pool in the step (3) at a distance from 3 days out is back in the aerobic biochemical reaction tank.
6. an excess sludge reduction treatment unit is characterized in that, comprises aerobic biochemical reaction tank, settling tank and anaerobic reation pool; The outlet of said aerobic biochemical reaction tank connects the inlet of said settling tank, and the outlet of said settling tank connects the inlet of said anaerobic reation pool, and the outlet of said anaerobic reation pool connects the inlet of aerobic biochemical reaction tank.
7. excess sludge reduction treatment unit according to claim 6 is characterized in that, said aerobic biochemical reaction tank is provided with aeration head.
8. excess sludge reduction treatment unit according to claim 6 is characterized in that said anaerobic reation pool is provided with whipping appts.
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103058472A (en) * | 2012-10-30 | 2013-04-24 | 天津城市建设学院 | Chemical conditioning method for improving dehydration property of surplus sludge |
| CN104817237A (en) * | 2015-05-15 | 2015-08-05 | 重庆交通大学 | Biological sludge zero-discharge sewage treatment plant and method |
| CN109160701A (en) * | 2018-09-27 | 2019-01-08 | 中山大学 | A method of optimization excess sludge problem |
| CN112624497A (en) * | 2020-12-02 | 2021-04-09 | 香港科技大学深圳研究院 | Sludge reduction promotion method based on sulfate reduction and electrochemical pretreatment |
| CN112759083A (en) * | 2021-01-12 | 2021-05-07 | 中山大学 | Sludge source reduction device and sludge source reduction process |
| CN117843135A (en) * | 2023-11-28 | 2024-04-09 | 嘉兴市洪合环境工程有限公司 | SBR sewage treatment system and method thereof |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003117595A (en) * | 2001-10-10 | 2003-04-22 | Kyodo Shoji:Kk | Treating method and treating equipment for solid-liquid mixture |
| CN101935131A (en) * | 2010-06-25 | 2011-01-05 | 余静 | Municipal sewage treatment method with zero energy consumption low sludge yield |
| CN102167480A (en) * | 2011-03-23 | 2011-08-31 | 中山大学 | Excess sludge decrement treatment method and device |
| CN202226756U (en) * | 2011-10-19 | 2012-05-23 | 东北石油大学 | Enhanced treatment device for sludge digestion supernatant |
-
2012
- 2012-07-09 CN CN201210236560.8A patent/CN102718380B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003117595A (en) * | 2001-10-10 | 2003-04-22 | Kyodo Shoji:Kk | Treating method and treating equipment for solid-liquid mixture |
| CN101935131A (en) * | 2010-06-25 | 2011-01-05 | 余静 | Municipal sewage treatment method with zero energy consumption low sludge yield |
| CN102167480A (en) * | 2011-03-23 | 2011-08-31 | 中山大学 | Excess sludge decrement treatment method and device |
| CN202226756U (en) * | 2011-10-19 | 2012-05-23 | 东北石油大学 | Enhanced treatment device for sludge digestion supernatant |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103058472A (en) * | 2012-10-30 | 2013-04-24 | 天津城市建设学院 | Chemical conditioning method for improving dehydration property of surplus sludge |
| CN104817237A (en) * | 2015-05-15 | 2015-08-05 | 重庆交通大学 | Biological sludge zero-discharge sewage treatment plant and method |
| CN109160701A (en) * | 2018-09-27 | 2019-01-08 | 中山大学 | A method of optimization excess sludge problem |
| CN112624497A (en) * | 2020-12-02 | 2021-04-09 | 香港科技大学深圳研究院 | Sludge reduction promotion method based on sulfate reduction and electrochemical pretreatment |
| CN112759083A (en) * | 2021-01-12 | 2021-05-07 | 中山大学 | Sludge source reduction device and sludge source reduction process |
| CN117843135A (en) * | 2023-11-28 | 2024-04-09 | 嘉兴市洪合环境工程有限公司 | SBR sewage treatment system and method thereof |
| CN117843135B (en) * | 2023-11-28 | 2024-08-02 | 嘉兴市洪合环境工程有限公司 | SBR sewage treatment system and method thereof |
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