CN1587123A - Physiochemical and biochemical interactive city sewage treating method - Google Patents
Physiochemical and biochemical interactive city sewage treating method Download PDFInfo
- Publication number
- CN1587123A CN1587123A CN 200410066451 CN200410066451A CN1587123A CN 1587123 A CN1587123 A CN 1587123A CN 200410066451 CN200410066451 CN 200410066451 CN 200410066451 A CN200410066451 A CN 200410066451A CN 1587123 A CN1587123 A CN 1587123A
- Authority
- CN
- China
- Prior art keywords
- biochemical
- pond
- treatment unit
- sewage
- physiochemical
- 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)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
The present invention belongs to the field of environment protecting technology, and is especially interactive physiochemical and biochemical city sewage treating method. The treating reactor is provided with pre-hypoxia, anaerobic, hypoxia, aerobic and other biochemical treating units and physiochemical treating unit with flocculent thrown. The physiochemical treating unit under different treating mode may be used as biochemical treating unit, and the reaction condition of the reaction units may be altered based on the different quality of inflow water and the different treating requirement. The present invention realizes the serial or parallel connecting of the biochemical treating unit and physiochemical treating unit to make the system always in minimum running cost while eliminating pollutant effectively to ensure drainage quality.
Description
Technical field
The invention belongs to environmental technology field, be specifically related to a kind of Physiochemical and biochemical interactive city sewage treating method.
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 according to the different situations of microbial growth condition and oxygen supply mode.Biological treatment will reach the denitrogenation dephosphorizing purpose just must or create anaerobism, anoxic, zone such as aerobic in the space of reactor on the time, to realize multi-form anaerobic-aerobic dephosphorization, aerobic-the anoxic denitrogenation, required hydraulic detention time is longer, some technology reached more than 12 hours, and capital cost and working cost are all higher.Generally use biological denitrification phosphorous removal technique at present in the world, commonly used has: conventional anaerobic/anoxic/aerobic process (A/A/O technology), Bardenpho, UCT, VIP, SBR, ICEAS, CASS, UNITANK and various oxidation ditch process.Raising along with the wastewater treatment in China emission request, China has also obtained remarkable progress in sewage treatment process research, except using above-mentioned treatment process, domestic inversion A/A/O technology, hydrolysis-anaerobism-little oxygen process integration, high loading activated sludge process, biological aerated filter, efficient compound sewage biological treatment system, the intensification treatment process etc. also researched and developed voluntarily.
The physical chemistry treatment process of water has a variety of, and wherein chemical coagulation is handled the most frequently used, the most representative.Because the municipal effluent water yield is big, dosing coagulant makes working cost higher, and sludge output is big, and therefore, the past adopts the chemical coagulation process Treating Municipal Sewage less separately.In recent years, the continuous release of efficient, cheap medicament adds the requirement of phosphor-removing effect more and more highlyer, and chemical coagulation also begins to come into one's own.Unit such as Tongji University, China Municipal Engineering North China Design And Research Institute has carried out the pilot scale research that the materialization enhanced primary is handled to the Shanghai City combined sewage, in sewage, add iron trichloride, polyaluminium sulfate, ferric sulfate and and the composite use of polyacrylamide (PAM), obtained good effect, particularly the removal effect to total phosphorus is stable.
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, and all the other are then identical with conventional activated sludge process or similar, this class technique denitrification weak effect, main purpose is to help dephosphorization, and sewage disposal running cost is higher.
Several chief cities sewage treatment process is as follows:
(1) A/A/O and improved technology thereof
Along with constantly increasing the weight of of body eutrophication, the nitrogen phosphorus emission standard of effluent of municipal sewage plant is more and more higher, the denitrification dephosphorization technique that is most widely used at present is A/A/O and improved technology thereof, this technology mainly is made up of anaerobic pond, anoxic pond, Aerobic Pond and second pond, better to organic pollution materials and suspended solids removal effect, but have following shortcomings: the 1. removal effect instability of nitrogen and phosphorus; 2. the variation of the influent quality water yield is bigger to the operating performance influence; 3. it is longer to design hydraulic detention time, and working cost is higher.
(2) SBR and modification technology thereof
Thereby SBR and modification technology thereof are to realize anaerobism, anoxic and the aerobic denitrogenation dephosphorizing function that reaches on time series, reaction and precipitation process concentrate in the pond body to be finished, it is few to have the structures of processing, 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 head loss is big; 3. the system device utilization ratio is low, and control is complicated; 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) UNITANK technology
UNITANK technology is very similar with three channel type oxidation channel technologies in fact, though can save second pond and mud return-flow system, 1. they exist does not have obviously independently anaerobism, anoxic zones, thereby influences the denitrogenation dephosphorizing effect; 2. sludge concentration imbalance in the reaction tank, in the later stage of reaction time, the influent side sludge concentration is low, precipitation side sludge concentration height, 3. UNITANK processing unit platform tricks is many, and plant factor is low, and control is complicated; 4. effluent weir is fixed, and the initial stage aquifer yield is difficult to determine, and needs reflow treatment.
Summary of the invention
The object of the invention is the processing difficult problem at the ubiquitous low organic concentration of municipal effluent, low ratio of carbon to ammonium, high concentration of nitrogen and phosphorus, proposes a kind of flexible and changeable Physiochemical and biochemical interactive city sewage treating method that can generally adapt to various water quality and processing requirements.
A kind of Physiochemical and biochemical interactive city sewage treating method that the present invention proposes, adopt the biochemical treatment unit, the interactive reactor that physicochemical treatment unit is formed, wherein the biochemical treatment unit is by pre-anoxic pond 1, anaerobic pond 2, anoxic pond 3, Aerobic Pond 4, back aeration tank 5 is connected to form by the water hole of partition wall successively, physicochemical treatment unit is made up of flocculation basin 6, back aeration tank 5 links to each other with flocculation basin 6 with valve by pipeline, the unitary pre-anoxic pond 1 of biochemical treatment links to each other with the returned sluge pipeline, the unitary anaerobic pond 2 of biochemical treatment links to each other with inlet channel, aeration tank 5, the unitary back of biochemical treatment links to each other with settling tank 7, physicochemical treatment unit one end links to each other with water inlet pipe, the other end links to each other with settling tank 7, is connected with valve by pipeline between biochemical treatment unit and the physicochemical treatment unit simultaneously; Municipal effluent enters the Physiochemical and biochemical interactive reactor after handling through sand setting, difference according to the water yield and water quality, select biochemical treatment unit, physicochemical treatment unit series, parallel or while biological nitration denitrification operation scheme, sewage is carried out biochemical treatment, materialization processing, mixed solution in the final reactor enters settling tank and carries out mud-water separation, sedimentary sludge part is back to pre-anoxic pond, and part is as excess sludge discharge, wherein:
(1) when amount of inlet water be design discharge 0.7-1.5 doubly, the influent quality chemical oxygen demand (COD) is 70mg/L-800mg/L, biochemical oxygen demand (BOD) is 30mg/L-400mg/L, suspended solids is 150mg/L-300mg/L, kjeldahl nitrogen is 20mg/L-60mg/L, when total phosphorus is 2mg/L-8mg/L, reactor adopts the series operation mode, pre-anoxic pond (1), anaerobic pond (2) in the reactor, anoxic pond (3), Aerobic Pond (4), aeration tank (5), back, flocculation basin (6), settling tank (7) link to each other successively by pipeline;
(2) when flooding velocity 1.5 times greater than design discharge, the influent quality chemical oxygen demand (COD) is 70mg/L-400mg/L, and biochemical oxygen demand (BOD) is 30mg/L-200mg/L, and suspended solids is 150mg/L-300mg/L, kjeldahl nitrogen is 10mg/L-40mg/L, when total phosphorus is 1mg/L-5mg/L; Reactor adopts the parallel running mode, and the unitary anaerobic pond of reactor state biochemical treatment (2), anoxic pond (3), Aerobic Pond (4) link to each other successively, and in parallel by pipeline with the flocculation basin (6) of physicochemical treatment unit;
(3) when flooding velocity be design discharge 0.7-1.0 doubly, the influent quality chemical oxygen demand (COD) is 100mg/L-300mg/L, biochemical oxygen demand (BOD) is 50mg/L-150mg/L, suspended solids is 150mg/L-300mg/L, kjeldahl nitrogen is 20mg/L-60mg/L, when total phosphorus is 2mg/L-4mg/L, adopt biological nitration denitrification operation scheme simultaneously, anaerobic pond in the reactor (2), aeration tank (5), back, settling tank (7) link to each other successively.
Among the present invention, when adopting the series operation mode, its control condition is as follows: make municipal effluent all enter anaerobic pond 2, anoxic pond 3, Aerobic Pond 4 in the biochemical treatment unit successively, with the chemical agent reaction, stopped 4-8 hour in the biochemical treatment unit; Enter the flocculation basin 6 in the physicochemical treatment unit then,, stopped 0.5-1 hour in physicochemical treatment unit with the flocculation agent thorough mixing; Last mixed solution enters settling tank and carries out mud-water separation, sedimentation time is 2-4 hour, precipitating sludge is back to pre-anoxic pond 1 and carries out endogenous denitrification removal nitric nitrogen, and reflux ratio is 25-100%, and the mud of removing after nitric nitrogen and process anoxic are stablized enters anaerobic pond.
Among the present invention, when adopting the parallel way operation, its control condition is as follows: sewage is divided into 2 strands, one sewage enters anaerobic pond 2, anoxic pond 3, the Aerobic Pond 4 in the biochemical treatment unit, react with chemical agent, flooding velocity is the 50%--80% of total inflow, from Aerobic Pond 4 terminal water outlets, stops 4-6 hour in the biochemical treatment unit; One sewage enters physicochemical treatment unit, and with the flocculation agent thorough mixing, flocculation time is 0.5-1.5 hour, and flooding quantity is the 20%--50% of total inflow; Two strands of sewage are mixed into settling tank after treatment and carry out mud-water separation, and sedimentation time is 1.5-3 hour, and part mud is back to pre-anoxic pond, and return sludge ratio is 25-80%, and partial reflux mud is back to chemical flocculation basin, and return sludge ratio is 0--25%.
Among the present invention, when adopting simultaneously the nitration denitrification operation scheme, its control condition is: sewage is all entered from anaerobic pond 2, through after aeration tank 5 aerations, enter settling tank 7 again and carry out mud-water separation, nitration denitrification is 6-10 working time hour simultaneously, sedimentation time is 3-5 hour, and flocculation basin 6 together carries out aeration as aeration tank 5, back, and mud is back to pre-anoxic pond (1), return sludge ratio is 50%-100%, and dissolved oxygen is 0.6mg/L-1.0mg/L.
Among the present invention, described flocculation agent is a kind of for poly-ferrosilicon, poly-sial etc., and dosage is 20mg/L--80mg/L.
Among the present invention, the Physiochemical and biochemical interactive reactor is made up of pre-anoxic pond, anaerobic pond, anoxic pond, Aerobic Pond, aeration tank, back, flocculation basin and settling tank.Pre-anoxic pond is used for the anoxic denitrification of returned sluge, and denitrifying carbon source is mainly from mud component, or is added by the part municipal effluent; Anaerobic pond is used for carrying out anaerobic phosphorus release when system's biochemistry dephosphorization; Anoxic pond is used for the denitrification denitrogenation of system; Aerobic Pond is used for that system's organic matter degradation, ammonia nitrogen are nitrated, the aerobic reaction processes such as absorption of phosphorus; Back aeration tank is used for the high strength aeration of short period of time when front-end process employing while nitration denitrification technology, promote precipitating action; Flocculation basin is when system's biochemistry materialization series operation, as auxiliary physicochemical treatment unit, the phosphor-removing effect of strengthening system, also can be used as the operation of biochemical unit, strengthen back aeration effect, when system is biochemical materialization parallel running,, bear the materialization Processing tasks of part of contaminated water as independent physicochemical treatment unit.
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 by the Physiochemical and biochemical interactive reaction.After the inventive method is handled, can make water outlet COD≤60mg/L, biochemical oxygen demand (BOD) BOD on the 5th
5≤ 20mg/L, suspended solids SS≤20mg/L, total nitrogen TN-N≤20mg/L, NH
3-N≤8mg/L (temperature＞12 ℃), NH
3Indications such as-N≤15mg/L (temperature≤12 ℃) all can reach or be better than country's " urban wastewater treatment firm pollutant emission standard " primary standard (B standard) requirement (GB18918-2002).
Description of drawings
Fig. 1 is an interactive reactor floor plan synoptic diagram of the present invention.
Number in the figure: 1 is pre-anoxic pond, and 2 is anaerobic pond, and 3 is anoxic pond, and 4 is Aerobic Pond, and 5 is the aeration tank, back, and 6 is flocculation basin, and 7 is settling tank.
Embodiment
Embodiment 1:
Select the series operation mode when normal water quality, the water yield, concrete steps are: the municipal effluent after certain ground warp sand setting is handled is introduced interactive reactor, enters anaerobic pond 2, and the mixed solution in the Aerobic Pond flow to anoxic pond 3 by crossing the blowback of wall plug-flow; Returned sluge enters pre-anoxic pond 1, and sewage flows through anaerobic pond 2, anoxic pond 3, Aerobic Pond 4, aeration tank 5, back successively, from flocculation basin 6 outflow reactors, through settling tank 7 water outlets.22 ℃ of the average water temperatures of intaking, mean ph value is 7.37.The hydraulic detention time of sewage in reactor is 9h, and average return sludge ratio is 100%, and average return current ratio of the mixed liquid is 200%, and sludge concentration maintains about the 3.5g/L, and average sludge age is 10d.
After testing, COD during water inlet
CrMean value is 335mg/L, and mean value is 42mg/L during water outlet, and clearance is 87.5%; SS mean value is 212mg/L during water inlet, and water outlet mean value is 17mg/L, and clearance is 92%; Ammonia nitrogen mean value is 30mg/L during water inlet, and water outlet mean value is 3.4mg/L, and clearance is 88.7%; TN mean value is 35mg/L during water inlet, and mean value is 12mg/L during water outlet, and clearance is 65.7%.TP mean value is 3.89mg/L during water inlet, and when not adding flocculation agent, mean value is 1.1mg/L during water outlet, and clearance is 71.7%; When chemical flocculation basin added poly-ferrosilicon flocculation agent 20mg/L, the TP concentration in the average water outlet was less than 0.5mg/L.
Embodiment 2:
For the combined system sewer line when the heavy rain, the operation materialization pattern in parallel when perhaps the separate system pipeline causes the storm period water yield to increase owing to reasons such as pipeline leakages with biochemical process.Handle the back water outlet to second pond (make biological treatment system maintenance organic loading constant) except sewage by unit anaerobic pond 2, anoxic pond 3, Aerobic Pond 4 (moving by aerobic mode) this moment, the excess load part of contaminated water branches to aeration tank 5, back and flocculation basin 6, merges to enter second pond after the materialization intensive treatment.
Municipal effluent after certain ground warp sand setting processing is introduced interactive reactor, 26.5 ℃ of the average water temperatures of intaking, mean ph value is 7.44.Sewage is 5.6h at the unitary hydraulic detention time of biochemical treatment, and average return sludge ratio is 100%, and average return current ratio of the mixed liquid is 150%, and sludge concentration maintains about 3.0g/L, and average sludge age is 15d.The physicochemical treatment unit hydraulic detention time is 0.4h, and average return sludge ratio is 25%.
After testing, COD during water inlet
CrMean value is 123mg/L, and mean value is 38mg/L during water outlet, and clearance is 69%; SS mean value is 90mg/L during water inlet, and water outlet mean value is 16mg/L, and clearance is 82%; Ammonia nitrogen mean value is 18mg/L during water inlet, and water outlet mean value is 3.9mg/L, and clearance is 78.2%; TN mean value is 21mg/L during water inlet, and mean value is 14.2mg/L during water outlet, and clearance is 32.4%.TP mean value is 2.4mg/L during water inlet, and poly-ferrosilicon flocculant dosage can make TP in the water outlet below 0.6mg/L when 30mg/L.
Embodiment 3:
As water inlet COD with TN concentration is not high or the sewage disposal operation paralleling model of water yield when little.70% of water inlet this moment enters aeration tank 5, back and flocculation basin 6, to make full use of chemical and biological flocculation, in less than 1 hour reaction times, reach the purpose of removing organism and dephosphorization, 30% sewage enters pre-anoxic pond 1, anaerobic pond 2, anoxic pond 3, Aerobic Pond 4 successively, carry out organic matter degradation and denitrogenation, at this moment pre-anoxic pond 1, anaerobic pond 2, anoxic pond 3, Aerobic Pond 4 also can partly move, and the part unit is in holding state.
Municipal effluent after certain ground warp sand setting processing is pumped into interactive reactor, 25 ℃ of the average water temperatures of intaking, mean ph value is 7.32.Sewage is 5.6h at the unitary hydraulic detention time of biochemical treatment, and average return sludge ratio is 100%, and average return current ratio of the mixed liquid is 150%, and sludge concentration maintains about the 3.0g/L, and average sludge age is 20d.The physicochemical treatment unit hydraulic detention time is 0.5h, and average return sludge ratio is 50%.
After testing, COD during water inlet
CrMean value is 90mg/L, and mean value is 28mg/L during water outlet, and clearance is 68.9%; SS mean value is 79mg/L during water inlet, and water outlet mean value is 17mg/L, and clearance is 78.5%; Ammonia nitrogen mean value is 12mg/L during water inlet, and water outlet mean value is 3.6mg/L, and clearance is 71%; TN mean value is 12.7mg/L during water inlet, and mean value is 7.6mg/L during water outlet, and clearance is 12.1%.TP mean value is 1.5mg/L during water inlet, and the polysilicate aluminum sulphate flocculant dosage can make TP in the water outlet below 0.6mg/L when 20mg/L.
Embodiment 4:
In the normal water yield, operation while nitration denitrification pattern when Pollutant levels are low.All by the hypoxemia operation, reach nitration denitrification purpose simultaneously with anaerobic pond 2, anoxic pond 3, Aerobic Pond 4 this moment, and back aeration tank 5 and flocculation basin 6 are by aerobic operation.
Municipal effluent after sand setting is handled pumps into interactive reactor, 22 ℃ of the average water temperatures of intaking, and mean ph value is 7.32.Sewage is 7.6h in the unitary theoretical water power of the biochemical treatment residence time, average return sludge ratio is 100%, need not mixed-liquor return, sludge concentration maintains about 2.5g/L, average sludge age is 18d, the dissolved oxygen concentration of reactor is controlled at 0.6mg/L-1.0mg/L, back aeration tank dissolved oxygen concentration control 3mg/L-4mg/L.
After testing, COD during water inlet
CrMean value is 145mg/L, and mean value is 38mg/L during water outlet, and clearance is 73.8%; SS mean value is 129mg/L during water inlet, and water outlet mean value is 15mg/L, and clearance is 88.4%; Ammonia nitrogen mean value is 18mg/L during water inlet, and water outlet mean value is 2.6mg/L, and clearance is 85%; TN mean value is 22.7mg/L during water inlet, and mean value is 8.4mg/L during water outlet, and clearance is 63%.TP mean value is 1.5mg/L during water inlet, and the TP mean value in the water outlet is below 1.0mg/L.
Claims (5)
1, a kind of Physiochemical and biochemical interactive city sewage treating method, it is characterized in that adopting the biochemical treatment unit, the interactive reactor that physicochemical treatment unit is formed, wherein the biochemical treatment unit is by pre-anoxic pond (1), anaerobic pond (2), anoxic pond (3), Aerobic Pond (4), back aeration tank (5) is connected to form by the water hole of partition wall successively, physicochemical treatment unit is made up of flocculation basin (6), back aeration tank (5) links to each other with flocculation basin (6) with valve by pipeline, the unitary pre-anoxic pond of biochemical treatment (1) links to each other with the returned sluge pipeline, the unitary anaerobic pond of biochemical treatment (2) links to each other with inlet channel, biochemical treatment aeration tank, unitary back (5) links to each other with settling tank (7), physicochemical treatment unit one end links to each other with water inlet pipe, the other end links to each other with settling tank (7), be connected with valve by pipeline between biochemical treatment unit and the physicochemical treatment unit simultaneously, municipal effluent enters the Physiochemical and biochemical interactive reactor after handling through sand setting, difference according to the water yield and water quality, select the biochemical treatment unit, the physicochemical treatment unit series connection, in parallel, or while biological nitration denitrification operation scheme, sewage is carried out biochemical treatment, materialization is handled, mixed solution in the final reactor enters settling tank and carries out mud-water separation, sedimentary sludge part is back to pre-anoxic pond, part is as excess sludge discharge, wherein:
(1) when amount of inlet water be design discharge 0.7-1.5 doubly, the influent quality chemical oxygen demand (COD) is 70mg/L-800mg/L, biochemical oxygen demand (BOD) is 30mg/L-400mg/L, suspended solids is 150mg/L-300mg/L, kjeldahl nitrogen is 20mg/L-60mg/L, when total phosphorus is 2mg/L-8mg/L, reactor adopts the series operation mode, pre-anoxic pond (1), anaerobic pond (2) in the reactor, anoxic pond (3), Aerobic Pond (4), aeration tank (5), back, flocculation basin (6), settling tank (7) link to each other successively by pipeline;
(2) when flooding velocity 1.5 times greater than design discharge, the influent quality chemical oxygen demand (COD) is 70mg/L-400mg/L, and biochemical oxygen demand (BOD) is 30mg/L-200mg/L, and suspended solids is 150mg/L-300mg/L, kjeldahl nitrogen is 10mg/L-40mg/L, when total phosphorus is 1mg/L-5mg/L; Reactor adopts the parallel running mode, and the unitary anaerobic pond of reactor state biochemical treatment (2), anoxic pond (3), Aerobic Pond (4) link to each other successively, and in parallel by pipeline with the flocculation basin (6) of physicochemical treatment unit;
(3) when flooding velocity be design discharge 0.7-1.0 doubly, the influent quality chemical oxygen demand (COD) is 100mg/L-300mg/L, biochemical oxygen demand (BOD) is 50mg/L-150mg/L, suspended solids is 150mg/L-300mg/L, kjeldahl nitrogen is 20mg/L-60mg/L, when total phosphorus is 2mg/L-4mg/L, adopt biological nitration denitrification operation scheme simultaneously, anaerobic pond in the reactor (2), aeration tank (5), back, settling tank (7) link to each other successively.
2, Physiochemical and biochemical interactive city sewage treating method according to claim 1, when it is characterized in that adopting the series operation mode, its control condition is as follows: make municipal effluent all enter anaerobic pond (2), anoxic pond (3), Aerobic Pond (4) in the biochemical treatment unit successively, stopped 4-8 hour in the biochemical treatment unit; Enter the flocculation basin (6) in the physicochemical treatment unit then,, stopped 0.5-1 hour in physicochemical treatment unit with the flocculation agent thorough mixing; Last mixed solution enters settling tank and carries out mud-water separation, sedimentation time is 2-4 hour, precipitating sludge is back to pre-anoxic pond (1) and carries out endogenous denitrification removal nitric nitrogen, and reflux ratio is 25-100%, and the mud of removing after nitric nitrogen and process anoxic are stablized enters anaerobic pond.
3, Physiochemical and biochemical interactive city sewage treating method according to claim 1, when it is characterized in that adopting the parallel way operation, its control condition is as follows: sewage is divided into 2 strands, one sewage enters anaerobic pond (2), anoxic pond (3), the Aerobic Pond (4) in the biochemical treatment unit, flooding velocity is the 50%--80% of total inflow, from the terminal water outlet of Aerobic Pond (4), in the biochemical treatment unit, stopped 4-6 hour; One sewage enters physicochemical treatment unit, and with the flocculation agent thorough mixing, flocculation time is 0.5-1.5 hour, and flooding quantity is the 20%--50% of total inflow; Two strands of sewage are mixed into settling tank after treatment and carry out mud-water separation, and sedimentation time is 1.5-3 hour, and part mud is back to pre-anoxic pond, and return sludge ratio is 25-80%, and partial reflux mud is back to chemical flocculation basin, and return sludge ratio is 0--25%.
4, Physiochemical and biochemical interactive city sewage treating method according to claim 1, when it is characterized in that adopting simultaneously the nitration denitrification operation scheme, its control condition is: sewage is all entered from anaerobic pond (2), through after aeration tank (5) aeration, enter settling tank (7) again and carry out mud-water separation, nitration denitrification is 6-10 working time hour simultaneously, sedimentation time is 3-5 hour, flocculation basin (6) together carries out aeration as aeration tank, back (5), mud is back to pre-anoxic pond (1), return sludge ratio is 50%-100%, and dissolved oxygen is 0.6mg/L--1.0mg/L.
5, the method for Treating Municipal Sewage according to claim 1, its feature also are described flocculation agent for gathering a kind of of ferrosilicon, poly-sial, and dosage is 20mg/L--80mg/L.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100664511A CN100522847C (en) | 2004-09-16 | 2004-09-16 | Physiochemical and biochemical interactive city sewage treating method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100664511A CN100522847C (en) | 2004-09-16 | 2004-09-16 | Physiochemical and biochemical interactive city sewage treating method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1587123A true CN1587123A (en) | 2005-03-02 |
| CN100522847C CN100522847C (en) | 2009-08-05 |
Family
ID=34604010
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2004100664511A Expired - Fee Related CN100522847C (en) | 2004-09-16 | 2004-09-16 | Physiochemical and biochemical interactive city sewage treating method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100522847C (en) |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100376496C (en) * | 2005-04-07 | 2008-03-26 | 同济大学 | Integrated process for treating sewage by suspended bio-carrier |
| CN102295346A (en) * | 2011-06-14 | 2011-12-28 | 江苏龙腾工程设计有限公司 | Adjustable biochemical tank and adjustable AAO process for water treatment |
| WO2011160603A1 (en) * | 2010-06-25 | 2011-12-29 | 可事托环保设备（上海）有限公司 | Multi-stage sewage treatment method and device with biological denitrification and dephosphorization |
| CN101445298B (en) * | 2008-12-23 | 2012-01-25 | 北京桑德环境工程有限公司 | Improved UCT sewage disposal system and method for treating same |
| CN104529081A (en) * | 2014-12-31 | 2015-04-22 | 桂林市世环废气处理设备有限公司 | Treatment process for domestic sewage |
| CN105461061A (en) * | 2015-12-31 | 2016-04-06 | 华南理工大学 | A<2>/O-biology synchronous nitrogen and phosphorus removal device and method for urban sewage |
| 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 |
| CN106865893A (en) * | 2017-03-09 | 2017-06-20 | 杭州职业技术学院 | A kind of domestic sewage treatment process |
| CN108483651A (en) * | 2018-05-28 | 2018-09-04 | 上海市水利工程设计研究院有限公司 | The modified form multi-mode operation A adjusted based on water quality and quantity2O reaction tanks and sewage disposal system |
| 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 |
| 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 |
| 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 |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102586344B (en) * | 2012-03-19 | 2014-12-10 | 同济大学 | Method for producing volatile fatty acid through heating and circular anaerobic fermentation of sludge |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2530949Y (en) * | 2001-10-08 | 2003-01-15 | 张鸿毅 | High-effiicency sewage purifying system |
| SE521571C2 (en) * | 2002-02-07 | 2003-11-11 | Greenfish Ab | Integrated closed recirculation system for wastewater treatment in aquaculture. |
| KR100419431B1 (en) * | 2002-02-28 | 2004-02-18 | 삼성엔지니어링 주식회사 | Wastewater treatment apparatus and method for removing nitrogen and phosphorus |
| CN1408649A (en) * | 2002-04-24 | 2003-04-09 | 陈启松 | Integrated A2/O biochemical system |
| CN1382648A (en) * | 2002-06-17 | 2002-12-04 | 深圳市龙岗区平湖污水处理厂 | Process for treating city sewage by hydrolysis-anaerobic-anoxic-aerobic method |
-
2004
- 2004-09-16 CN CNB2004100664511A patent/CN100522847C/en not_active Expired - Fee Related
Cited By (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100376496C (en) * | 2005-04-07 | 2008-03-26 | 同济大学 | Integrated process for treating sewage by suspended bio-carrier |
| CN101445298B (en) * | 2008-12-23 | 2012-01-25 | 北京桑德环境工程有限公司 | Improved UCT sewage disposal system and method for treating same |
| WO2011160603A1 (en) * | 2010-06-25 | 2011-12-29 | 可事托环保设备（上海）有限公司 | Multi-stage sewage treatment method and device with biological denitrification and dephosphorization |
| CN102295346A (en) * | 2011-06-14 | 2011-12-28 | 江苏龙腾工程设计有限公司 | Adjustable biochemical tank and adjustable AAO process for water treatment |
| CN102295346B (en) * | 2011-06-14 | 2012-12-26 | 江苏龙腾工程设计有限公司 | Adjustable biochemical tank and adjustable AAO process for water treatment |
| CN104529081A (en) * | 2014-12-31 | 2015-04-22 | 桂林市世环废气处理设备有限公司 | Treatment process for domestic sewage |
| CN104529081B (en) * | 2014-12-31 | 2016-01-13 | 桂林市世环废气处理设备有限公司 | The treatment process of one way of life sewage |
| CN105461061A (en) * | 2015-12-31 | 2016-04-06 | 华南理工大学 | A<2>/O-biology synchronous nitrogen and phosphorus removal device and method for urban sewage |
| 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 |
| CN106865893A (en) * | 2017-03-09 | 2017-06-20 | 杭州职业技术学院 | A kind of domestic sewage treatment process |
| CN106865893B (en) * | 2017-03-09 | 2019-06-18 | 杭州职业技术学院 | A kind of domestic sewage treatment process |
| 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 |
| CN108483651A (en) * | 2018-05-28 | 2018-09-04 | 上海市水利工程设计研究院有限公司 | The modified form multi-mode operation A adjusted based on water quality and quantity2O reaction tanks and sewage disposal system |
| 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 |
| 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 |
Also Published As
| Publication number | Publication date |
|---|---|
| CN100522847C (en) | 2009-08-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101503248B (en) | Composite biological film activated sludge denitrification dephosphorization denitrification method and reactor thereof | |
| CN101269882B (en) | Integrated oxidation ditch, construction and operation method | |
| CN1294090C (en) | High efficiency sewage treatment method | |
| CN102126815B (en) | Method for reinforcing nitrogen and phosphorous removal from sewage by utilizing anaerobic environment of pipeline | |
| CN101767910A (en) | Continuous flow sewage hypoxia short distance denitrification treating technique | |
| CN100522847C (en) | Physiochemical and biochemical interactive city sewage treating method | |
| CN114772725B (en) | Device and method for enhancing denitrification and dephosphorization of domestic sewage by coupling sulfur autotrophic short-cut denitrification and anaerobic ammoxidation | |
| CN104724825A (en) | Sewage treatment method | |
| CN102690019A (en) | High-efficiency nitrogen and phosphorus synchronous removal method in treating low concentration wastewater | |
| CN105858886A (en) | Multistage anoxic and oxic coupling MBR sewage treatment technology for enhanced nitrogen and phosphorus removal | |
| CN105753153A (en) | DEAMOX (denitrifying ammonium oxidation) based efficient biological nitrogen and phosphors removal device adopting improved A/O (anoxic/oxic) four-point step-feeding as well as application method | |
| CN1068565C (en) | Improved nitrification and denitrification wastewater treatment process | |
| CN101054249A (en) | Multipoint water feeding sewage treatment process by zeolite and organism united adsorption and regeneration | |
| CN102358663A (en) | Low-DO (dissolved oxygen) rear denitrification sewage treatment plant and technique | |
| CN204727718U (en) | Sewage treatment systems | |
| CN106430575B (en) | A kind of method that oxidation ditch step feed technology realizes short-cut nitrification and denitrification denitrogenation | |
| CN104761100A (en) | Sewage treatment system | |
| CN105254134A (en) | Biological nitrogen removal combination device | |
| CN102653434A (en) | Improved oxidation ditch technique of coupled return sludge preconcentration system | |
| CN110759604B (en) | Two-stage SBR (sequencing batch reactor) series efficient biological denitrification method for low-carbon-source sewage | |
| CN1382648A (en) | Process for treating city sewage by hydrolysis-anaerobic-anoxic-aerobic method | |
| CN105174642A (en) | Efficient biological denitrification method for sewage | |
| CN1706760A (en) | City sewage treating process and system | |
| CN100384758C (en) | Biochemical city sewage denitriding and dephosphorizing method in suspension stuffing bed | |
| CN102010100B (en) | Technology and device for advanced treatment flow of industrially comprehensive wastewater |
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 | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20090805 Termination date: 20130916 |