CN203568936U - Oxidation ditch nitrogen and phosphorus removal sewage treatment system - Google Patents
Oxidation ditch nitrogen and phosphorus removal sewage treatment system Download PDFInfo
- Publication number
- CN203568936U CN203568936U CN201320588843.9U CN201320588843U CN203568936U CN 203568936 U CN203568936 U CN 203568936U CN 201320588843 U CN201320588843 U CN 201320588843U CN 203568936 U CN203568936 U CN 203568936U
- Authority
- CN
- China
- Prior art keywords
- oxidation ditch
- pond
- sewage treatment
- communicated
- liquid separation
- 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.)
- Expired - Fee Related
Links
Images
Landscapes
- Activated Sludge Processes (AREA)
- Physical Water Treatments (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The utility model provides an oxidation ditch nitrogen and phosphorus removal sewage treatment system, relates to the technical field of sewage treatment, and aims to solve the problems of facility and equipment waste caused by limited unit-area sewage treatment capability of a conventional oxidation ditch sewage treatment system and low treatment capability caused by difficulty in the maintenance of high concentration of microorganisms in an oxidation ditch due to the facts of low solid-liquid separation efficiency and poor sewage concentration effects when a gravitational settling mode is adopted. The system comprises a nitrogen and phosphorus removal reaction unit and a solid-liquid separation unit, which are communicated with each other, wherein the nitrogen and phosphorus removal reaction unit comprises an anaerobic tank and an oxidation ditch, which are sequentially communicated; the solid-liquid separation unit comprises a secondary settling tank; the output end of the oxidation ditch is communicated with the input end of the secondary settling tank. The system also comprises a dissolved gas deep tank and a floatation tank, which are communicated with each other, wherein the output end of the secondary settling tank is communicated with the input end of the dissolved gas deep tank. The system is particularly applied to reconstruction projects of oxidation ditch sewage treatment plants.
Description
Technical field
The utility model relates to technical field of sewage, particularly a kind of denitrogenation dephosphorizing Sewage treatment systems that the air supporting of dark pond is combined with oxidation ditch.
Background technology
Oxidation ditch (Oxidation Ditch, OD) is circulation mixed aeration tank or claims circulation mixed activated sludge process, is by the APasveer professor utility model of Dutch National Institutes of Health (TND) the earliest.Since 1954 occur, oxidation Ditch Technology has obtained research and development widely at home and abroad.
Yet along with the raising day by day of municipal sewage treatment amount and processing requirements, many oxidation ditches sewage work can not meet the demands because of its water outlet, and faces the awkward situation that needs upgrading.Directly enlarging newly built construction not only needs a large amount of construction investments, but also needs newly-increased construction land, and China is in industrialization, urbanization fast-developing period at present, and it is soaring that Urban Land Price continues, and construction land is very in short supply.Therefore, the take measures potentiality of the existing oxidation ditch sewage treatment facility of deep excavation just seem very necessary.
Long-term Designing Sewage Treatment Plant service experience shows: the usefulness of sewage treatment process and the concentration of active sludge are closely bound up, and the concentration of the active sludge of system is subject to the restriction of mud-water separation effect.But, in actual construction and operational process, existing oxidation ditch sewage work, adopt second pond to carry out mud-water separation, solid-liquid separation efficiency is low, and mud concentrated effect is poor, and the activated sludge concentration that is back to anaerobic pond can only maintain 2000mg/L～3000mg/L, make the microorganism in anaerobic pond and oxidation ditch be difficult to the concentration that remains higher, cause the processing power of oxidation ditch sewage work all the time in lower level; In addition, existing oxidation channel wastewater treatment system, its unit surface sewage treatment capacity is limited, causes the waste of facilities and equipment.Therefore, designing and developing the returned sluge concentration systems of stability and high efficiency is more technical barrier in the urgent need to address.
Summary of the invention
For existing oxidation channel wastewater treatment system, its unit surface sewage treatment capacity is limited, causes the waste of facilities and equipment; Adopt gravitational settling, solid-liquid separation efficiency is low, mud concentrated effect is poor, make the microorganism in oxidation ditch be difficult to the concentration that remains higher, cause the problem that processing power is low, the purpose of this utility model is to provide a kind of oxidation ditch denitrogenation dephosphorizing Sewage treatment systems, its sewage treatment capacity is high, and good effect of separating solid from liquid, is applicable to new construction, the especially improvement project of oxidation ditch sewage work.
The utility model solves the technical scheme that its technical problem adopts: it comprises denitrogenation dephosphorizing reaction member and the solid-liquid separation unit being connected, described denitrogenation dephosphorizing reaction member comprises anaerobic pond and the oxidation ditch being communicated with successively, described solid-liquid separation unit comprises second pond, the output terminal of described oxidation ditch is communicated with the input terminus of described second pond, described solid-liquid separation unit also comprises the dark pond of molten gas and the air flotation pool being connected, and the output terminal of described second pond is communicated with the input terminus in the dark pond of described molten gas.
Further, the degree of depth in the dark pond of described molten gas is 30m～100m.
Further, the dark tank depth of described molten gas is 40m～50m.
Described air flotation pool is communicated with the input terminus of described anaerobic pond by pipeline.
Effect of the present utility model is: oxidation ditch denitrogenation dephosphorizing Sewage treatment systems of the present utility model is provided with the dark pond of molten gas and the air flotation pool of series connection, to realize efficient solid-liquid separation after traditional gravity settling basin.The dark pond of molten gas utilizes water column static pressure to increase the air dissolves amount in mud mixture, and above-mentioned mud mixture enters air flotation pool again to carry out solid-liquid separation and obtain concentrated active sludge.Compare with existing oxidation channel wastewater treatment system, in the situation that floor space is identical, adopt the pneumatically supported oxidation channel wastewater treatment system in the dark pond of the utility model, its sewage load increases by 20%, has effectively improved the sewage treatment capacity for the treatment of system unit surface.
In addition, the mud of process pressure air-dissolving enters air flotation pool and carries out solid-liquid separation, and in air flotation pool, can form concentration is the concentrated active sludge of 20000mg/L～40000mg/L, has increased the concentration of returned sluge.Compare the treatment system that independent employing air flotation pool carries out solid-liquid separation, treatment system of the present utility model increases air solubleness in mud mixture, has guaranteed air flotation effect.Make to enter more than concentrated activated sludge concentration in denitrogenation dephosphorizing reaction member can reach 5000mg/L, greatly improved the concentration of active sludge, can give full play to the processing potentiality of Sewage treatment systems, significantly promote the removal efficiency of pollutent.
Accompanying drawing explanation
Fig. 1 is the structural representation of the oxidation ditch denitrogenation dephosphorizing Sewage treatment systems of embodiment mono-of the present utility model.
Embodiment
Below in conjunction with the drawings and specific embodiments to the oxidation ditch denitrogenation dephosphorizing sewage disposal the utility model proposes
System is described in further detail.According to the following describes and claims, advantage of the present utility model and feature will be clearer.It should be noted that, accompanying drawing all adopts very the form of simplifying and all uses non-ratio accurately, only in order to convenient, the object of aid illustration the utility model embodiment lucidly.
Sewage denitrification and dephosphorization (AAO) principle is as follows: bio-denitrifying sewage is mainly realized by nitration denitrification process, is divided into two stages of nitrification and denitrification.Under aerobic condition, utilize the nitrobacteria in sewage that nitride is converted into nitrate, then under anoxia condition (dissolved oxygen concentration < 0.5mg/L), utilizes the denitrifying bacterium in sewage that nitrate reduction is become to gaseous nitrogen.
Biological removal of phosphorus in wastewater is mainly taken the photograph phosphorus and mud discharging is realized by polyP bacteria is excessive, and its reaction process is mainly that anaerobic phosphorus release and aerobic (anoxic) are inhaled two processes of phosphorus.That is: under anaerobic, polyphosphate particle (poly-P) generate energy in polyP bacteria degraded body, discharges phosphoric acid salt, absorbs the organism in water simultaneously, and is translated into poly-beta-hydroxy alkanoate (PHA) and is stored in cell; Under aerobic or anoxia condition, the PHA in polyP bacteria oxygenolysis body, glycogen biosynthesis, the Ruminants animal poly-phosphate in excessive absorption water of while, thus reach the object of removing phosphorus in water.
The oxidation ditch denitrogenation dephosphorizing Sewage treatment systems of the present embodiment is described below in conjunction with Fig. 1, it comprises denitrogenation dephosphorizing reaction member 10 and the solid-liquid separation unit 20 being connected, denitrogenation dephosphorizing reaction member 10 comprises anaerobic pond 101 and the oxidation ditch 102 being communicated with successively, solid-liquid separation unit 20 comprises the dark pond 202 of second pond 201, molten gas and the air flotation pool 203 being communicated with successively, and the output terminal of oxidation ditch 102 is communicated with the input terminus of second pond 201.
Further, air flotation pool 203 is communicated with the input terminus of anaerobic pond 101 by pipeline.
In denitrogenation dephosphorizing reaction member 10, the input terminus of anaerobic pond 101 is communicated with sewage inlet A, sewage mixes at anaerobic pond 101 with the concentrated active sludge of coming from air flotation pool 203 backflows by pipeline, the reaction of generation anaerobic phosphorus release, polyphosphate particle (poly-P) generate energy in polyP bacteria degraded body in concentrated active sludge, discharge phosphoric acid salt, simultaneously, the short chain fatty acid that polyP bacteria absorbs in sewage forms PHB(poly-β-hydroxybutyric acid poly-β-hydroxybutyrate, and PHB is a kind of of PHA) and be stored in cell paste.
The output terminal of anaerobic pond 101 is communicated with the input terminus of oxidation ditch 102, oxidation ditch 102 utilizes continuous ring type reaction tank (Cintinuous Loop Reator, abbreviation CLR) make biological reaction tank, the water outlet of anaerobic pond 101 enters in oxidation ditch 102 pond bodies, and rely on the thrust of submersible water impeller to flow in oxidation ditch 102 pond body-internal-circulations, can be for the sewage oxygenation in the body of pond be with microbial consumption in supplying water during rotary aeration disc work, when rotary aeration disc quits work, sewage in the body of pond is just in anoxic condition, sewage in the body of pond is under the plug-flow effect of submersible water impeller, formation aerobic-anaerobic circulates, can effectively remove organism, pass through nitration denitrification denitrogenation simultaneously, and remove phosphorus, finally by the sewage of processing, by the output terminal of oxidation ditch 102, enter second pond 201.
In the oxidation ditch denitrogenation dephosphorizing Sewage treatment systems of the present embodiment, the output terminal of oxidation ditch 102 is communicated with the second pond 201 of solid-liquid separation unit 20, carrying out mud-water separation in the reacted mud mixture input of denitrogenation dephosphorizing second pond 201, the water outlet of second pond 201 is through water outlet B output system and enter subsequent disposal unit, and pressure air-dissolving is carried out in the sludge reflux of second pond 201 bottoms to the dark pond 202 of molten gas.The diameter in the dark pond 202 of molten gas is about 1.0m～6.0m, and the degree of depth is about 30m～100m, and bottom, pond is provided with aerating apparatus, the dark pond 202 of molten gas utilizes water column static pressure, gas-liquid two-phase is mixed, and bubble and liquid are long duration of contact, can significantly improve the gas content in mud mixture.Preferably, the dark pond of molten gas 202 degree of depth are 40m～50m, and now, the dark pond of molten gas 202 water colunm pressures are moderate.The main suspended state that relies on blast aeration to maintain active sludge in the dark pond 202 of molten gas.
The output terminal in the dark pond 202 of molten gas is communicated with the input terminus of air flotation pool 203, will complete the mud mixture input air flotation pool 203 of molten gas, and mud mixture discharges microbubble under negative pressure, for air supporting.Air supporting is the micro-bubble that height of formation disperses in water, and micro-bubble sticks on the solid or liquid particle of hydrophobic group in sewage, forms apparent density and is less than the flco of water and floats to the water surface, thereby realize the process of solid-liquid separation.Mud mixture is by the solid-liquid separation of air flotation pool 203, can form concentration is the concentrated active sludge of 20000mg/L～40000mg/L, the concentrated activity sludge reflux on air flotation pool 203 tops is to anaerobic pond 101, the clear liquid on air flotation pool 203 tops is delivered to the end of denitrogenation dephosphorizing reaction member 10, clear liquid enters second pond 201 after mixing with the water outlet of oxidation ditch 102, or flows directly into second pond 201.The excess sludge that contains phosphorus is discharged system by the mud relief outlet C of air flotation pool 203 bottoms, thereby reaches the object of removing phosphorus in water.
In the present embodiment, utilize original second pond 201 in Sewage treatment systems to carry out mud-water separation, mud after separation enters pressure air-dissolving in the dark pond 202 of molten gas again, and form high-concentration activated sludge in air flotation pool 203, by refluxing to improve the concentration of active sludge in denitrogenation dephosphorizing reaction member 10, thereby improve the treatment efficiency of whole Sewage treatment systems.Adopt the oxidation ditch denitrogenation dephosphorizing Sewage treatment systems in the dark pond 202 of molten gas to compare with conventional processing system, sewage load increases by 20%, has effectively improved the sewage treatment capacity for the treatment of system unit surface.
In above-described embodiment, material used, reagent etc., if no special instructions, all can obtain from commercial channels.
The treating processes of the present embodiment is described below in conjunction with Fig. 1:
One, anaerobic phosphorus release reaction: first sewage enter anaerobic zone 101, and treatment sewage mixes with the thickened sludge that air flotation pool 203 is back to anaerobic zone 101,, there is anaerobic phosphorus release reaction in hydraulic detention time 1.5h; Polyphosphate particle (poly-P) generate energy in polyP bacteria degraded body in active sludge, discharges phosphoric acid salt, and meanwhile, the short chain fatty acid that polyP bacteria absorbs in sewage forms PHB and is stored in cell paste.
Two, nitration denitrification reaction: the water outlet of anaerobic pond 101 enters the oxygen-starved area of oxidation ditch 102, denitrifying bacteria utilizes the carbon source in the water inlet of oxidation ditch 102 to carry out anti-nitration reaction and realizes denitrogenation, sewage enters the aerobic zone of oxidation ditch 102 under angle of rake effect, in aerobic zone, realize the removal of COD, ammonia nitrogen and total phosphorus, the residence time of sewage in oxidation ditch 102 is 10.0h;
Three, mud-water separation: the water outlet of oxidation ditch 102 enters in second pond 201 carries out mud-water separation, and the surface load of second pond 201 is 0.9m
3/ (m
2h), hydraulic detention time is 2.5～4.0h, and the water outlet after mud-water separation is through water outlet B output system and enter subsequent disposal unit, and pressure air-dissolving is carried out in the sludge reflux of second pond 201 bottoms to the dark pond 202 of molten gas.
Four, the molten gas in dark pond: the returned sluge of second pond 201 enters the dark pond 202 of molten gas, the degree of depth in the dark pond 202 of molten gas is 50m, the supply position of air compressor is apart from liquid level 40m, and in the dark pond 201 of molten gas, hydraulic detention time is 1～2min, and gas-solid ratio is controlled at 0.005～0.006; In the dark pond 202 of molten gas, utilize water column static pressure to complete the molten gas process of mud.
Five, solid-liquid separation: the mud of process pressure air-dissolving enters air flotation pool 203 and carries out solid-liquid separation, in air flotation pool 203, active sludge is because the buoyancy of bubble forms the thickened sludge that concentration is 20000mg/L～40000mg/L on surface, concentrated active sludge is delivered to anaerobic pond 101 by sludge reflux pump, the conveying ratio of concentrated active sludge accounts for 40% of returned sluge total amount in step 4,4%～10% the excess sludge that contains polyP bacteria is discharged to system by mud relief outlet C simultaneously, when guaranteeing sludge activity, realize biological phosphate-eliminating.The clear liquid on air flotation pool 203 tops is delivered to the end of denitrogenation dephosphorizing reaction member 10, and clear liquid enters second pond 201 after mixing with the water outlet of oxidation ditch 102, or flows directly into second pond 201, to avoid the active sludge in clear liquid dilution oxidation ditch 102.
When the conveying ratio of concentrated active sludge account for returned sluge total amount 30%～60% time, concentrated activated sludge concentration in denitrogenation dephosphorizing reaction member 10 enters more than can reach 5000mg/L, the activated sludge concentration of comparing after traditional gravity settling basin solid-liquid separation can only maintain 2000mg/L～3000mg/L, Sewage treatment systems of the present utility model has greatly improved the concentration of active sludge concentrated in denitrogenation dephosphorizing reaction member 10, can give full play to the processing potentiality of Sewage treatment systems, significantly promote the removal efficiency of pollutent.
Foregoing description is only the description to the utility model preferred embodiment; the not any restriction to the utility model scope; any change, modification that the those of ordinary skill in the utility model field is done according to above-mentioned disclosure, all belong to the protection domain of claims.
Claims (4)
1. oxidation ditch denitrogenation dephosphorizing Sewage treatment systems, comprise the denitrogenation dephosphorizing reaction member and the solid-liquid separation unit that are connected, described denitrogenation dephosphorizing reaction member comprises anaerobic pond and the oxidation ditch being communicated with successively, described solid-liquid separation unit comprises second pond, the output terminal of described oxidation ditch is communicated with the input terminus of described second pond, it is characterized in that: described solid-liquid separation unit also comprises the dark pond of molten gas and the air flotation pool being connected, and the output terminal of described second pond is communicated with the input terminus in the dark pond of described molten gas.
2. oxidation ditch denitrogenation dephosphorizing Sewage treatment systems according to claim 1, is characterized in that: the degree of depth in the dark pond of described molten gas is 30m～100m.
3. oxidation ditch denitrogenation dephosphorizing Sewage treatment systems according to claim 2, is characterized in that: the dark tank depth of described molten gas is 40m～50m.
4. oxidation ditch denitrogenation dephosphorizing Sewage treatment systems according to claim 1, is characterized in that: described air flotation pool is communicated with the input terminus of described anaerobic pond by pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320588843.9U CN203568936U (en) | 2013-09-24 | 2013-09-24 | Oxidation ditch nitrogen and phosphorus removal sewage treatment system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320588843.9U CN203568936U (en) | 2013-09-24 | 2013-09-24 | Oxidation ditch nitrogen and phosphorus removal sewage treatment system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203568936U true CN203568936U (en) | 2014-04-30 |
Family
ID=50536680
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201320588843.9U Expired - Fee Related CN203568936U (en) | 2013-09-24 | 2013-09-24 | Oxidation ditch nitrogen and phosphorus removal sewage treatment system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203568936U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103508633A (en) * | 2013-09-24 | 2014-01-15 | 上海市政工程设计研究总院（集团）有限公司 | Oxidation ditch nitrogen and phosphorus removal sewage treatment system and technology thereof |
-
2013
- 2013-09-24 CN CN201320588843.9U patent/CN203568936U/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103508633A (en) * | 2013-09-24 | 2014-01-15 | 上海市政工程设计研究总院（集团）有限公司 | Oxidation ditch nitrogen and phosphorus removal sewage treatment system and technology thereof |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103880248B (en) | A kind of coking wastewater processing system and treatment process | |
| CN101519266B (en) | High-efficient denitrification and dephosphorization MBR process and device | |
| CN205258127U (en) | Circulatory flow loop type multistage sludge -biofilm intergrowth combined type bioreactor | |
| CN104150716A (en) | Biology processing apparatus capable of processing sewage at low-temperature with low carbon-nitrogen-ratio in cold region and method for processing sewage at low-temperature with low carbon-nitrogen-ratio in cold region | |
| CN106565017A (en) | Bicirculating nitrogen and phosphorus removal wastewater treatment system and method | |
| CN101633531A (en) | Sewage treatment reactor for alternately operating intermittent flow and continuous flow | |
| CN112979065A (en) | Garbage transfer station leachate full-treatment system | |
| CN102786184A (en) | Two-stage A / O-MBR denitrification and dephosphorization apparatus | |
| CN105923771B (en) | A kind of self-loopa biological denitrification reactor | |
| CN104512963A (en) | Integral multistage simultaneous nitrification and denitrification biological membrane system denitrification method and device | |
| CN105967435A (en) | Double-circulation nitrogen and phosphorus removal wastewater treatment system and process | |
| CN103508635A (en) | Efficient nitrogen and phosphorus removal wastewater treatment system and process | |
| CN201458900U (en) | Improved segmentation water inlet depth nitrogen and phosphorus removing device | |
| CN103183454B (en) | Coupling type biological denitrification method and system thereof | |
| CN204185292U (en) | Three-dimensional tapered aeration sewage disposal aerobic reactor | |
| CN201614333U (en) | Decentralized sewage treatment device | |
| CN108996687A (en) | A kind of short distance backflow intensifying anoxic/aerobic reactor nitrogen rejection facility and method | |
| CN203238141U (en) | Sewage biological treatment membrane filtration system | |
| CN201914974U (en) | Dual-circular groove membrane bioreactor (MBR) waste water treatment system | |
| CN102010062A (en) | MBR wastewater treating system with double circular grooves | |
| CN219689523U (en) | Treatment device for aged leachate of household garbage landfill | |
| CN104828942B (en) | A kind of new municipal sewage denitrogenation dephosphorizing handling process | |
| CN203568935U (en) | Efficient denitrifying and dephosphorizing sewage treatment system | |
| CN203768185U (en) | Coking wastewater treatment system | |
| CN203568934U (en) | Sewage treatment system capable of improving concentration of activated sludge |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20140430 Termination date: 20210924 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |