CN102653434A - Improved oxidation ditch technique of coupled return sludge preconcentration system - Google Patents

Improved oxidation ditch technique of coupled return sludge preconcentration system Download PDF

Info

Publication number
CN102653434A
CN102653434A CN2012101092001A CN201210109200A CN102653434A CN 102653434 A CN102653434 A CN 102653434A CN 2012101092001 A CN2012101092001 A CN 2012101092001A CN 201210109200 A CN201210109200 A CN 201210109200A CN 102653434 A CN102653434 A CN 102653434A
Authority
CN
China
Prior art keywords
pond
concentration
returned sluge
oxidation ditch
mud
Prior art date
Application number
CN2012101092001A
Other languages
Chinese (zh)
Inventor
杨殿海
刘巍
沈昌明
张�浩
徐立
贾川
Original Assignee
同济大学
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by 同济大学 filed Critical 同济大学
Priority to CN2012101092001A priority Critical patent/CN102653434A/en
Publication of CN102653434A publication Critical patent/CN102653434A/en

Links

Abstract

The invention belongs to the technical field of environmental protection, and particularly relates to an improved oxidation ditch technique of a coupled return sludge preconcentration system. A return sludge preconcentration system and a previous oxygen deficiency system are added before a traditional anaerobic-oxidation ditch system, so that the preconcentration system can implement different degrees of concentration of return sludge in an operation mode; the concentrated sludge is subjected to endogenous denitrification reaction in the previous oxygen deficiency system; the supernatant returns to the oxidation ditch to continue the reaction or returns to a secondary settling tank distributing well; the operating conditions of the preconcentration tank are changed according to different qualities and quantities of inflow water, different sludge ages and variable treatment requirements, thereby implementing the regulation and control on the biochemical reactions of the previous oxygen deficiency tank and the anaerobic tank, and optimizing the distribution and utilization of the carbon source; and under the conditions of not adding any external carbon source, polyphosphorus florae are effectively enriched in the biochemical system, thereby effectively stabilizing and reinforcing the dephosphorization performance of the low-carbon-source sewage treatment system, and keeping the denitrification performance of the system at high level.

Description

The improved oxidation ditch technology of coupling returned sluge preconcentration technique
Technical field
The invention belongs to environmental protection technical field, be specifically related to a kind of improved oxidation ditch technology of the returned sluge preconcentration technique that is coupled.
Background technology
Sewage disposal technology can be divided into physical treatment technology, physical chemistry treatment technology, biological chemistry treatment technology and chemical treatment method in general, and wherein the biological chemistry treatment technology with sewage is the most commonly used.Biochemical processing also has a variety of, mainly is to classify with the different of oxygen supply mode according to the microbial growth condition.Biological treatment will reach the denitrogenation dephosphorizing purpose just must or create anaerobism, anoxic, zone such as aerobic in the space of reactor drum on the time, to satisfy the environmental requirement of difference in functionality bacterium.The biological denitrification phosphorous removal technique that generally uses in the world at present has: anaerobic/anoxic/aerobic process (A/A/O technology), Bardenpho, UCT, VIP, SBR, ICEAS, CASS, UNITANK and various oxidation ditch process.For making sewage treatment process realize denitrogenation dephosphorizing efficiently, water inlet institute of system carbonaceous sources amount often becomes The key factor.And at China's southern area, Sewage Plant water inlet ubiquity carbon source is less, and C/N ratio is lower, the characteristics that concentration of nitrogen and phosphorus is higher, and sewage treatment process nitrogen phosphorus removal effect receives very big restriction.When water-inlet carbon source is low; The nitrate concentration of water outlet is often more than 12mg/L; The nitrate salt that also contains higher concentration in the returned sluge can destroy the anaerobic environment of system, and the anaerobism carbon source of aggravation polyP bacteria and denitrifying bacteria is competed; And then influence the anaerobic metabolism of polyP bacteria, make the phosphorus removal property of system also receive greatly influence.
Through being set in sewage treatment process, preparatory oxygen depletion system or back oxygen depletion system can remove effectively because the mud backflow gets into the nitrate salt of anaerobic zone.The former carried out hypoxia response earlier before returned sluge gets into Sewage treatment systems, with effective removal nitrate salt; The latter carried out further hypoxia response before reactor drum effluents muddy water mixed solution entering second pond.But,, hope that further removing nitrate salt all needs additional carbon for the system of low-carbon (LC) sewage.And this process has increased the running cost of Sewage treatment systems greatly, all unable its higher expense of bearing of a lot of sewage works.
Adopt materialization and the biochemical sewage treatment process that combines that application is also arranged at present; Its outstanding feature is to add chemical coagulator in the flow process; All the other are then identical with conventional activated sludge process or similar, and main purpose is to help dephosphorization and intensified suspended solid removal effect, but WWT running cost is higher; And can increase surplus sludge volume, increase the subsequent disposal expense.
Several kinds of main low-carbon (LC) urban sewage treatment process are following:
(1) carbon source shunting A/A/O
Along with constantly increasing the weight of of body eutrophication, the nitrogen phosphorus emission standard of effluent of municipal sewage plant is increasingly high, and application at present denitrification dephosphorization technique the most widely is the improved technology of A/A/O, i.e. carbon source shunting A/A/O.This technology mainly is made up of anaerobic pond, anoxic pond, Aerobic Pond and second pond; The separated into two parts of will intaking gets into anaerobic pond and anoxic pond respectively; The further distribution of regulator control system denitrogenation dephosphorizing carbon source; But some shortcomings below existing:, influenced the effect of dephosphorization simultaneously though 1. denitrogenation has been strengthened in the carbon source shunting; 2. the water inlet shunting need be set up corresponding apparatus pipeline and adjustment operating scheme, increases working cost; 3. it is longer to design hydraulic detention time.
(2) segmental influent SBR
Segmental influent SBR realizes anaerobism-aerobic process of multistage anoxic on time series, the water inlet segmentation gets into anaerobism section and multistage anoxic section, thereby reaches the effect that carbon source is distributed; Intensified denitrification and dephosphorization, reaction and precipitation process concentrate in the pond body to be accomplished, and it is few to have processing structures; Take up an area of little; Characteristics such as flexible operation, but it also has some shortcomings: and 1. SBR and modification technology thereof are all used and are strained hydrophone, are strained hydrophone water outlet quantitative limitation; The water yield is handled in single pond can not be very big, so this technology is not suitable for large-scale wastewater treatment plant; 2. the reactor volume utilization ratio is low, and lness ratio of plant is high, and head loss is big; 3. system's operational process is complicated with control, and the water inlet allocation proportion need restudy adjustment; Influenced by the reaction times, can not guarantee anaerobism, anoxic and aerobic reaction conditions fully; 5. water outlet is discontinuous, the subsequent disposal difficulty.
(3) effluent dephosphorization (Phostrip) technology
This technology is that a part of returned sluge is admitted to special reactor drum and releases phosphorus with biological phosphate-eliminating and representative of chemical dephosphorization bonded, then with phosphorus that lime precipitation discharged.Research and engineering practice show that this technology phosphor-removing effect is good, do not receive the influence of influent quality, but there is the following defective: (1) needs to increase special reactor drum and equipment, has increased capital cost; (2) increased the complicacy of operational administrative, technical level of operators has been required high; (3) used lime, the problem of its storage and preparation system is also more; (4) mud increases because of its amount of adding of lime greatly, and processing costs increases.
Summary of the invention
The object of the invention is the processing difficult problem to the ubiquitous low organic concentration of municipal effluent, low ratio of carbon to ammonium, high concentration of nitrogen and phosphorus, proposes a kind of improved oxidation ditch technology of the returned sluge preconcentration technique that is coupled.
The improved oxidation ditch technology of a kind of returned sluge preconcentration technique that is coupled that the present invention proposes; The modified form reactor drum that said improved oxidation ditch process using is made up of biochemical treatment unit and physicochemical treatment unit; Wherein the biochemical treatment unit is made up of preparatory anoxic pond 1, anaerobic pond 2, anaerobic pond 3, oxidation ditch 4; Be connected to form through pipeline and valve successively; Physicochemical treatment unit is made up of second pond 5 and returned sluge pre-concentration pond 6, through pipeline and valve with link to each other, through the variable frequency lift pump dominant discharge.The preparatory anoxic pond 1 in biochemical treatment unit links to each other with concentrated back returned sluge pipeline; Biochemical treatment unit anaerobic pond 2 links to each other with inlet channel; Biochemical treatment unit oxidation ditch 4 and second pond 5 are through linking to each other; Second pond 5 links to each other with returned sluge pre-concentration pond 6, and returned sluge pre-concentration pond 6 links to each other with preparatory anoxic pond 1; Pass through the variable frequency lift pump dominant discharge between second pond 5, returned sluge pre-concentration pond 6 and the preparatory anoxic pond 1; Concrete steps are: municipal effluent gets into anaerobic pond 2, anaerobic pond 3 and oxidation ditch 4 in the biochemical treatment unit after handling through sand setting successively, in the biochemical treatment unit, stops 10-20 hour; Get into the second pond 5 in the physicochemical treatment unit then; Carry out mud-water separation; ST is 2-4 hour, and precipitating sludge is back to returned sluge pre-concentration pond 6 and carries out the concentrated and screening of mud, and the returned sluge after concentrating then is back to preparatory anoxic pond 1 and removes nitric nitrogen through interior source procedure; Mud after the process anoxic is stable gets into anaerobic pond 2, and part is as excess sludge discharge; According to the difference of the influent quality water yield, the operating parameter in adjustment returned sluge pre-concentration pond, promptly return sludge ratio and returned sluge pre-concentration ratio carry out biochemical treatment to sewage, the phosphorus removal property of stable and consolidation system, wherein:
(1) when the influent quality COD be 70mg/L-130mg/L, biochemical oxygen demand is 30 mg/L-60mg/L, suspended solids is 20 mg/L-40mg/L; Kjeldahl nitrogen is 120 mg/L-130mg/L; When total phosphorus was 1.5mg/L-2.5mg/L, control mud age was 18d-20d, and return sludge ratio is 50%; Adopt the returned sluge pre-concentration than being 50%-55%, controlled oxidation ditch aerobic section DO concentration is 0.6mg/L;
(2) when the influent quality COD be 140 mg/L-180mg/L, biochemical oxygen demand is 70 mg/L-100mg/L, suspended solids is 140 mg/L-160mg/L, kjeldahl nitrogen is 25 mg/L-40mg/L, when total phosphorus is 2mg/L-3mg/L; Control mud age is 18d-20d, and return sludge ratio is 50%, adopts the returned sluge pre-concentration than being 65%-70%, and controlled oxidation ditch aerobic section DO concentration is 1mg/L;
(3) when the influent quality COD be 200 mg/L-250mg/L, biochemical oxygen demand is 100mg/L-130mg/L, suspended solids is 160mg/L-200mg/L; Kjeldahl nitrogen is 25mg/L-40mg/L; When total phosphorus was 2mg/L-4mg/L, control mud age was 15d-17d, and return sludge ratio is 50%; Adopt the returned sluge pre-concentration than being 75%-80%, controlled oxidation ditch aerobic section DO concentration is 2mg/L.
Among the present invention; The influent quality COD is 70mg/L-130mg/L, when biochemical oxygen demand is 30 mg/L-60mg/L, when adopting the short-cut nitrification and denitrification operation scheme; Its control condition is: controlled oxidation ditch dissolved oxygen concentration is 0.6mg/L, and MLSS is 1700-2000mg/L.
Among the present invention; Mud pre-concentration pond concentrates returned sluge; Its control condition is following: through regulating second pond returned sluge flow, make returned sluge get into mud pre-concentration pond, then through regulating the mud lift pump in mud pre-concentration pond; Control mud concentration ratio and the hydraulic detention time of concentrated back mud in preparatory anoxic pond; The supernatant of concentration basin is back to oxidation ditch or directly is back to the second pond distributing well, and the pre-concentration time was controlled at 0.3-0.5 hour according to different operational conditionss, is carrying out endogenous denitrification in the anoxic pond in advance through spissated returned sluge.
Among the present invention; Through the returned sluge preconcentration technique returned sluge is further concentrated; In this process, carry out the screening of mud through short hydraulic detention time (0.3-0.5h); Proportion gentlier is difficult for settled mud flco and is back to oxidation ditch or second pond continuation cycling deposition through supernatant, is back to preparatory anoxic pond after the mud that proportion is heavier concentrates, and progressively improves the settling property and the polyP bacteria concentration of system sludge.Owing to further concentrate, the sludge volume of backflow and nitrate salt total amount significantly reduce simultaneously, and the concentration of returned sluge further improves, and the nitrate salt of anoxic pond mud load decreases in advance, and actual hydraulic detention time prolongs to some extent.Therefore; Being back to the interior concentrating return-flow mud of preparatory anoxic pond can fall remaining nitrate removal through endogenous denitrification in corresponding hydraulic detention time basically; Thereby protected the anaerobic pond anaerobic environment to avoid the influence of returned sluge residue nitrate salt; Keep good anaerobic phosphorus release environment, avoided the anaerobism carbon source competition of denitrifying bacterium and polyP bacteria.Simultaneously, also prolonged the actual hydraulic detention time of anaerobic pond, increased the sludge concentration of anaerobic pond, reduced the organic loading of mud, helped the reinforcement utilization of hydrolysis and the polyP bacteria in particulate organic carbon source carbon source through the returned sluge pre-concentration.Therefore, the returned sluge preconcentration technique can be stablized the effect with the consolidation system dephosphorization, because the actual hydraulic detention time of system prolongs, the nitration denitrification ability is strengthened equally simultaneously.
Among the present invention, the denitrogenation dephosphorizing effect of system that adopted returned sluge pre-concentration process strengthening, its control condition is: sewage is all got into carry out phosphorus from anaerobic pond to discharge; Accomplish anoxic and aerobic reaction through oxidation ditch; Get into settling tank again and carry out mud-water separation, water outlet is directly discharged, after returned sluge entering pre-concentration pond concentrates; Get into preparatory anoxic pond and carry out the endogenous denitrification reaction, get into anaerobic pond then and begin new circulation.The nominal hydraulic detention time of anoxic pond is 0.5h in advance; Anaerobic pond name hydraulic detention time is 2 hours; Oxidation ditch name hydraulic detention time is 14h, and second pond name hydraulic detention time is 4 hours, and returned sluge pre-concentration pond name hydraulic detention time is 0.5h; Return sludge ratio is 50%-100%, and oxidation ditch aerobic section dissolved oxygen is 0.6mg/L--2.0mg/L.
Among the present invention, anoxic pond is used for the anoxic denitrification of returned sluge in advance, and denitrifying carbon source is from mud component; Anaerobic pond is used for when system's biochemistry dephosphorization, carrying out anaerobic phosphorus release; Oxidation ditch is used for that system's organic matter degradation, ammonia nitrogen are nitrated, the aerobic reaction processes such as absorption of denitrification denitrogenation, phosphorus; Second pond is used for mud-water separation; The pre-concentration pond is used for the gravity screening of mud and concentrates.
Characteristics of the present invention are comprehensive and handinesies of reactive system.
The present invention can effectively remove organic pollutant, total Kjeldahl nitrogen, suspended solids and portion phosphate through the Physiochemical and biochemical interactive reaction.After the inventive method is handled, can make water outlet COD≤50 mg/L, biochemical oxygen demand BOD on the 5th 5≤10mg/L, suspended solids SS≤15 mg/L, total nitrogen TN-N≤15 mg/L, NH 3-N≤5 mg/L (Wen Du>12 oC), NH 3-N≤8 mg/L (temperature≤12 oC), indication such as total phosphorus≤1mg/L all can reach or be superior to country's " urban wastewater treatment firm pollutant emission standard " primary standard (B standard) requirement (GB18918-2002).
Description of drawings
Fig. 1 is the modified form anaerobism-oxidation ditch process floor plan synoptic diagram of coupling returned sluge pre-concentration of the present invention.
Label among the figure: 1 is preparatory anoxic pond, and 2 is anaerobic pond, and 3 is anaerobic pond, and 4 is oxidation ditch, and 5 is second pond, and 6 is returned sluge pre-concentration pond, and 7,8 are respectively first variable frequency lift pump and second variable frequency lift pump.
Embodiment
Further specify the present invention through embodiment below.
Embodiment 1:
Less when the influent quality carbon source, when C/N ratio was low, promptly the influent quality COD was 70mg/L-130mg/L; Biochemical oxygen demand is 30 mg/L-60mg/L; Suspended solids is 120 mg/L-140mg/L, and kjeldahl nitrogen is 20 mg/L-30mg/L, when total phosphorus is 1.5mg/L-2.5mg/L; Processing parameter control is adjusted into: control second pond sludge reflux pump makes that average return sludge ratio is 50%; Control pre-concentration pond sludge reflux pump makes average returned sluge concentration ratio 50-55%, and this moment, actual hydraulic detention time was 12.6h, and the control sludge age maintains 18-20d; This moment, the biochemistry pool sludge concentration maintained 1700-2000mg/L, and control plate-spinning rotating speed aerobic section DO maintains 0.6mg/L.Operation process is to steady state with this understanding, continuous monitoring Inlet and outlet water change of water quality.
Through detecting COD during water inlet CrMV is 105mg/L, and water outlet MV is 25mg/L, and clearance is 76.2 %; SS MV is 130mg/L during water inlet, and water outlet MV is 11mg/L, and clearance is 66%; Ammonia nitrogen MV is 21mg/L during water inlet, and water outlet MV is 1mg/L, and clearance is 95.2%; TN MV is 27mg/L during water inlet, and MV is 11mg/L during water outlet, and clearance is 59.3%.TP MV is 1.9mg/L during water inlet, and MV is 0.8mg/L during water outlet, and clearance is 57.9%.Water outlet COD of system and TN reach (GB18918-2002) one-level A emission standard of country's " urban wastewater treatment firm sewage drainage standard ", and water outlet TP reaches (GB18918-2002) one-level B emission standard of country's " urban wastewater treatment firm sewage drainage standard ".
Embodiment 2:
When the influent quality carbon source increases to some extent, C/N ratio reaches at 4 o'clock, and promptly the influent quality COD is 140 mg/L-180mg/L; Biochemical oxygen demand is 70 mg/L-100mg/L; Suspended solids is 140 mg/L-160mg/L, and kjeldahl nitrogen is 25 mg/L-40mg/L, when total phosphorus is 2mg/L-3mg/L; Processing parameter control is adjusted into: control second pond sludge reflux pump makes that average return sludge ratio is 50%; Control pre-concentration pond concentrating return-flow sludge pump makes average returned sluge concentration ratio 65%-70%, and this moment, actual hydraulic detention time was 11.8h, and the control sludge age maintains 18-20d; This moment, biochemical section sludge concentration was kept 2000-2300mg/L, and control plate-spinning rotating speed aerobic section DO maintains 1mg/L
Through detecting COD during water inlet CrMV is 162mg/L, and MV is 29mg/L during water outlet, and clearance is 82.1%; SS MV is 47mg/L during water inlet, and water outlet MV is 13mg/L, and clearance is 72%; Ammonia nitrogen MV is 27mg/L during water inlet, and water outlet MV is 1mg/L, and clearance is 96.2%; TN MV is 34mg/L during water inlet, and MV is 10mg/L during water outlet, and clearance is 70.6%.TP MV is 2.6mg/L during water inlet, and MV is 0.6mg/L during water outlet, and clearance is 76.9%.Water outlet COD of system and TN reach (GB18918-2002) one-level A emission standard of country's " urban wastewater treatment firm sewage drainage standard ", and the approaching country of water outlet TP " urban wastewater treatment firm sewage drainage standard " is one-level A emission standard (GB18918-2002).
Embodiment 3:
When influent quality carbon source continuation increase, C/N ratio reaches at 6 o'clock, and promptly the influent quality COD is 200 mg/L-250mg/L; Biochemical oxygen demand is 100mg/L-130mg/L; Suspended solids is 160mg/L-200mg/L, and kjeldahl nitrogen is 25mg/L-40mg/L, when total phosphorus is 2mg/L-4mg/L; Processing parameter control is adjusted into: control second pond return sludge pump makes that average return sludge ratio is 50%; Control pre-concentration pond concentrating return-flow sludge pump makes average returned sluge concentration ratio 75%-80%, and this moment, actual hydraulic detention time was 11.4h, and the control sludge age maintains 15-18d; This moment, sludge concentration was kept 2500-2800g/L, and control plate-spinning rotating speed makes aerobic section DO maintain 2mg/L.
Through detecting COD during water inlet CrMV is 234mg/L, and MV is 37mg/L during water outlet, and clearance is 84.2%; SS MV is 110mg/L during water inlet, and water outlet MV is 13mg/L, and clearance is 88%; Ammonia nitrogen MV is 29mg/L during water inlet, and water outlet MV is 1.7mg/L, and clearance is 94%; TN MV is 38mg/L during water inlet, and MV is 12mg/L during water outlet, and clearance is 68%; TP MV is 3.2mg/L during water inlet, can make TP in the water outlet below 0.5mg/L, and clearance is 84.4%.The water outlet COD of system, TN and TP reach (GB18918-2002) one-level A emission standard of country's " urban wastewater treatment firm sewage drainage standard ".

Claims (4)

1. the improved oxidation ditch technology of the returned sluge preconcentration technique that is coupled; It is characterized in that the modified form reactor drum that said improved oxidation ditch process using is made up of biochemical treatment unit and physicochemical treatment unit; Wherein the biochemical treatment unit is made up of preparatory anoxic pond (1), anaerobic pond (2), anaerobic pond (3), oxidation ditch (4); Be connected to form through pipeline and valve successively; Physicochemical treatment unit is made up of second pond (5) and returned sluge pre-concentration pond (6), through pipeline and valve with link to each other, through the variable frequency lift pump dominant discharge; The preparatory anoxic pond in biochemical treatment unit (1) links to each other with concentrated back returned sluge pipeline; Biochemical treatment unit anaerobic pond (2) links to each other with inlet channel; Biochemical treatment unit oxidation ditch (4) and second pond (5) are through linking to each other; Second pond (5) links to each other with returned sluge pre-concentration pond (6), and returned sluge pre-concentration pond (6) links to each other with preparatory anoxic pond (1); Pass through the variable frequency lift pump dominant discharge between second pond (5), returned sluge pre-concentration pond (6) and the preparatory anoxic pond (1); Concrete steps are: municipal effluent gets into anaerobic pond (2), anaerobic pond (3) and oxidation ditch (4) in the biochemical treatment unit after handling through sand setting successively, in the biochemical treatment unit, stops 10-20 hour; Get into the second pond (5) in the physicochemical treatment unit then; Carry out mud-water separation; ST is 2-4 hour, and precipitating sludge is back to returned sluge pre-concentration pond (6) and carries out the concentrated and screening of mud, and the returned sluge after concentrating then is back to preparatory anoxic pond (1) and removes nitric nitrogen through interior source procedure; Mud after the process anoxic is stable gets into anaerobic pond (2), and part is as excess sludge discharge; According to the difference of the influent quality water yield, the operating parameter in adjustment returned sluge pre-concentration pond, promptly return sludge ratio and returned sluge pre-concentration ratio carry out biochemical treatment to sewage, the phosphorus removal property of stable and consolidation system, wherein:
(1) when the influent quality COD be 70mg/L-130mg/L, biochemical oxygen demand is 30 mg/L-60mg/L, suspended solids is 20 mg/L-40mg/L; Kjeldahl nitrogen is 120 mg/L-130mg/L; When total phosphorus was 1.5mg/L-2.5mg/L, control mud age was 18d-20d, and return sludge ratio is 50%; Adopt the returned sluge pre-concentration than being 50%-55%, controlled oxidation ditch aerobic section DO concentration is 0.6mg/L;
(2) when the influent quality COD be 140 mg/L-180mg/L, biochemical oxygen demand is 70 mg/L-100mg/L, suspended solids is 140 mg/L-160mg/L, kjeldahl nitrogen is 25 mg/L-40mg/L, when total phosphorus is 2mg/L-3mg/L; Control mud age is 18d-20d, and return sludge ratio is 50%, adopts the returned sluge pre-concentration than being 65%-70%, and controlled oxidation ditch aerobic section DO concentration is 1mg/L;
(3) when the influent quality COD be 200 mg/L-250mg/L, biochemical oxygen demand is 100mg/L-130mg/L, suspended solids is 160mg/L-200mg/L; Kjeldahl nitrogen is 25mg/L-40mg/L; When total phosphorus was 2mg/L-4mg/L, control mud age was 15d-17d, and return sludge ratio is 50%; Adopt the returned sluge pre-concentration than being 75%-80%, controlled oxidation ditch aerobic section DO concentration is 2mg/L.
2. the improved oxidation ditch technology of coupling returned sluge preconcentration technique according to claim 1 is characterized in that mud pre-concentration pond concentrates returned sluge, and hydraulic detention time is 0.3-0.5 hour.
3. the improved oxidation ditch technology of coupling returned sluge preconcentration technique according to claim 1 is characterized in that in the returned sluge pre-concentration pond mud being screened, and its hydraulic detention time is 0.3-0.5h.
4. the improved oxidation ditch technology of coupling returned sluge preconcentration technique according to claim 1; The denitrogenation dephosphorizing effect of system that it is characterized in that adopting returned sluge pre-concentration process strengthening; Its control condition is: sewage is all got into from anaerobic pond carry out phosphorus release, accomplish anoxic and aerobic reaction through oxidation ditch, get into settling tank again and carry out mud-water separation; Water outlet is directly discharged; After returned sluge entering pre-concentration pond concentrates, get into preparatory anoxic pond and carry out the endogenous denitrification reaction, get into anaerobic pond then and begin new circulation; The nominal hydraulic detention time of anoxic pond is 0.5h in advance; Anaerobic pond name hydraulic detention time is 2 hours; Oxidation ditch name hydraulic detention time is 14h, and second pond name hydraulic detention time is 4 hours, and returned sluge pre-concentration pond name hydraulic detention time is 0.5h; Return sludge ratio is 50%-100%, and oxidation ditch aerobic section dissolved oxygen is 0.6mg/L--2.0mg/L.
CN2012101092001A 2012-04-16 2012-04-16 Improved oxidation ditch technique of coupled return sludge preconcentration system CN102653434A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN2012101092001A CN102653434A (en) 2012-04-16 2012-04-16 Improved oxidation ditch technique of coupled return sludge preconcentration system

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN2012101092001A CN102653434A (en) 2012-04-16 2012-04-16 Improved oxidation ditch technique of coupled return sludge preconcentration system

Publications (1)

Publication Number Publication Date
CN102653434A true CN102653434A (en) 2012-09-05

Family

ID=46729185

Family Applications (1)

Application Number Title Priority Date Filing Date
CN2012101092001A CN102653434A (en) 2012-04-16 2012-04-16 Improved oxidation ditch technique of coupled return sludge preconcentration system

Country Status (1)

Country Link
CN (1) CN102653434A (en)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103964633A (en) * 2014-04-21 2014-08-06 河海大学 Integrated efficient biological reactor and reaction process thereof
CN104355499A (en) * 2014-11-12 2015-02-18 浦华环保有限公司 Side flow denitrification tank and side flow denitrification method
CN106186570A (en) * 2016-08-29 2016-12-07 合肥合意环保科技工程有限公司 One way of life sewage treatment process and equipment

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102344222A (en) * 2010-07-29 2012-02-08 上海市政工程设计研究总院 Oxidation ditch process with functions of preventing and controlling activated sludge bulking

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102344222A (en) * 2010-07-29 2012-02-08 上海市政工程设计研究总院 Oxidation ditch process with functions of preventing and controlling activated sludge bulking

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103964633A (en) * 2014-04-21 2014-08-06 河海大学 Integrated efficient biological reactor and reaction process thereof
CN103964633B (en) * 2014-04-21 2015-10-07 河海大学 Integrated bioreactor and reaction process thereof
CN104355499A (en) * 2014-11-12 2015-02-18 浦华环保有限公司 Side flow denitrification tank and side flow denitrification method
CN104355499B (en) * 2014-11-12 2016-07-06 浦华环保股份有限公司 A kind of effluent denitrification process
CN106186570A (en) * 2016-08-29 2016-12-07 合肥合意环保科技工程有限公司 One way of life sewage treatment process and equipment

Similar Documents

Publication Publication Date Title
JP5899373B2 (en) Process comprising an ANAMOX microorganism on a biofilm carrier for removing ammonium from a wastewater stream
CN104556376B (en) The municipal sewage biological phosphate-eliminating autotrophic denitrification method of nitrite is provided based on short-cut denitrification
US6946073B2 (en) Method for treating wastewater in a membrane bioreactor to produce a low phosphorus effluent
Collivignarelli et al. Simultaneous nitrification-denitrification processes in activated sludge plants: Performance and applicability
EP1259465B1 (en) Method and system for sustainable treatment of municipal and industrial wastewater
CN100417608C (en) Multi-phase dual cycle influent process
US6406629B1 (en) Biological process for removing phosphorous involving a membrane filter
US6485645B1 (en) Biological process for removing phosphorus involving a membrane filter
CN100360439C (en) Combined activated sludge-biofilm sequencing batch reactor and process
AU656814B2 (en) Method and system for biologically removing nitrogen from wastewater
CN1294090C (en) High efficiency sewage treatment method
Vaiopoulou et al. An activated sludge treatment plant for integrated removal of carbon, nitrogen and phosphorus
CN101519265B (en) Sewage treatment process and system
US6830689B2 (en) Process for removing phosphorus from wastewater utilizing a triple basin wastewater treatment system
CN101381185B (en) Denitrification processing method of coking wastewater and processing arrangement
US4867883A (en) High-rate biological waste water treatment process using activated sludge recycle
CN101386460B (en) Multi-stage composite processing technology of high-concentration organic sewage
CN105585122B (en) A kind of high-ammonia nitrogen low C/N is than waste water treatment system and treatment process
CN104556572B (en) A kind of method of waste water high-efficiency biochemical denitrification dephosphorization
CN202054705U (en) Magnetic loading A2/O sewage treatment device
CN101244883B (en) High-efficiency low-consumption retexture method for urban sewage
CN103482820B (en) AAO-biological contact oxidation strengthened nitrogen and phosphorus removal integrated device and method
CN100528777C (en) Organic waste water processing method
EP2539286A2 (en) Hybrid aerobic and anaerobic wastewater and sludge treatment systems and methods
US6982036B2 (en) Chemically enhanced primary sludge fermentation method

Legal Events

Date Code Title Description
PB01 Publication
C06 Publication
SE01 Entry into force of request for substantive examination
C10 Entry into substantive examination
WD01 Invention patent application deemed withdrawn after publication

Application publication date: 20120905

C02 Deemed withdrawal of patent application after publication (patent law 2001)