CN209797712U - Medium-high concentration comprehensive sewage nitrogen and phosphorus removal treatment system - Google Patents
Medium-high concentration comprehensive sewage nitrogen and phosphorus removal treatment system Download PDFInfo
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- CN209797712U CN209797712U CN201920435520.3U CN201920435520U CN209797712U CN 209797712 U CN209797712 U CN 209797712U CN 201920435520 U CN201920435520 U CN 201920435520U CN 209797712 U CN209797712 U CN 209797712U
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- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 title claims abstract description 32
- 229910052698 phosphorus Inorganic materials 0.000 title claims abstract description 32
- 239000011574 phosphorus Substances 0.000 title claims abstract description 32
- 239000010865 sewage Substances 0.000 title claims abstract description 29
- 238000011282 treatment Methods 0.000 title abstract description 26
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title abstract description 10
- 229910052757 nitrogen Inorganic materials 0.000 title abstract description 5
- 239000010802 sludge Substances 0.000 claims abstract description 58
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 57
- 238000006243 chemical reaction Methods 0.000 claims abstract description 49
- 238000004062 sedimentation Methods 0.000 claims abstract description 33
- 239000004576 sand Substances 0.000 claims abstract description 28
- 239000000126 substance Substances 0.000 claims abstract description 23
- 238000005188 flotation Methods 0.000 claims abstract description 22
- 230000001112 coagulating effect Effects 0.000 claims abstract description 20
- 238000010992 reflux Methods 0.000 claims abstract description 16
- 238000009287 sand filtration Methods 0.000 claims abstract description 13
- 238000011001 backwashing Methods 0.000 claims abstract description 11
- 238000005345 coagulation Methods 0.000 claims description 37
- 230000015271 coagulation Effects 0.000 claims description 37
- 238000005189 flocculation Methods 0.000 claims description 31
- 230000016615 flocculation Effects 0.000 claims description 27
- 239000000945 filler Substances 0.000 claims description 17
- 230000003311 flocculating effect Effects 0.000 claims description 10
- 238000001914 filtration Methods 0.000 claims description 9
- 238000005273 aeration Methods 0.000 claims description 8
- 239000003795 chemical substances by application Substances 0.000 claims description 6
- 238000005276 aerator Methods 0.000 claims description 5
- 239000002131 composite material Substances 0.000 claims description 5
- 239000000470 constituent Substances 0.000 claims description 5
- 239000004519 grease Substances 0.000 claims description 4
- 230000008878 coupling Effects 0.000 claims description 2
- 238000010168 coupling process Methods 0.000 claims description 2
- 238000005859 coupling reaction Methods 0.000 claims description 2
- 238000011010 flushing procedure Methods 0.000 claims description 2
- 239000013049 sediment Substances 0.000 claims description 2
- 239000003344 environmental pollutant Substances 0.000 abstract description 2
- 231100000719 pollutant Toxicity 0.000 abstract description 2
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 abstract 1
- 238000000034 method Methods 0.000 description 23
- 239000002893 slag Substances 0.000 description 10
- 230000000694 effects Effects 0.000 description 5
- 230000003647 oxidation Effects 0.000 description 5
- 238000007254 oxidation reaction Methods 0.000 description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 238000009300 dissolved air flotation Methods 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 230000014759 maintenance of location Effects 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 238000007790 scraping Methods 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 239000006228 supernatant Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 1
- 239000002028 Biomass Substances 0.000 description 1
- 230000032770 biofilm formation Effects 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000011221 initial treatment Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000001546 nitrifying effect Effects 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 238000006213 oxygenation reaction Methods 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000004659 sterilization and disinfection Methods 0.000 description 1
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- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The utility model relates to a middle and high concentration comprehensive sewage denitrification and dephosphorization treatment system. The downstream of the high-efficiency air flotation tank is connected with an anoxic reaction tank, the downstream of the anoxic reaction tank is sequentially connected with an anaerobic reaction tank and an aerobic reaction tank, the downstream of the aerobic reaction tank is connected with a residual sludge sedimentation tank, the residual sludge sedimentation tank is connected to the anoxic reaction tank at the front end through a reflux pump and a reflux pipeline, the downstream of the residual sludge sedimentation tank is connected with a chemical phosphorus removal coagulating sedimentation tank, the downstream of the chemical phosphorus removal coagulating sedimentation tank is connected with a continuous sand filter tank, and the downstream of the continuous sand filter tank is respectively connected with a sand filtration backwashing water return tank and a clear. The utility model discloses processing system not only can effectively remove pollutants such as COD, BOD, ammonia nitrogen, total phosphorus, SS in the sewage, has compact structure simultaneously, and area is little, energy-efficient, a great deal of advantage such as nitrogen and phosphorus removal ability reinforce. Provides a reliable and effective technical approach for the sewage treatment.
Description
Technical Field
The utility model belongs to environmental engineering sewage treatment field relates to a higher comprehensive sewage treatment system of organic matter, total nitrogen, total phosphorus content.
Background
With the progress of industrialization, the comprehensive sewage quality of the original industrial area is more difficult to treat than the general urban domestic sewage quality because the comprehensive sewage quality contains higher concentration of organic matters, total nitrogen and total phosphorus. The national requirements on environmental protection are higher and higher, and the general conventional single sewage treatment process is difficult to meet the standard-reaching requirements of sewage treatment. Several prior art treatments are described and problematic as follows:
First, A2O process
The A2O process is also called as AAO process, an anaerobic tank, an anoxic tank and an aerobic tank are used as a sewage biochemical treatment unit, and then a sedimentation tank is connected to realize sludge-water separation, and the A2O process has good denitrification and dephosphorization effects as a common secondary sewage treatment process.
The A2O process has the following characteristics:
1. The process flow is simple, and the total hydraulic retention time is short.
2. under the condition of anaerobic (anoxic) and aerobic alternate operation, filamentous bacteria cannot propagate in large quantity and sludge filamentous expansion is not easy to occur.
3. No need of dosing in operation, two A sections realize anaerobic (anoxic) treatment by stirring, and the operation cost is low
4. The phosphorus removal effect is difficult to improve, the sludge growth has a certain limit, and especially when the P/BOD value is high.
5. The denitrification effect is difficult to be further improved, and the internal circulation amount is generally limited to 2Q, and is not suitable to be too high.
6. The treated water entering the sedimentation tank needs to keep dissolved oxygen with certain concentration, so that the retention time is reduced, and the phenomena of generating an anaerobic state and releasing phosphorus by sludge are prevented.
Second, contact oxidation
The contact oxidation tank is an immersed aeration biological filter tank, filler is arranged in the tank, and the biofilm hung on the filler is utilized to adsorb and oxidize and decompose organic substances in the wastewater. The oxygen required by the microorganisms is aerated by a fan.
The contact oxidation has the following characteristics:
1. The specific surface area of the filler is large, the oxygenation condition in the tank is good, and the biomass per unit volume in the contact oxidation tank is higher than that in the activated sludge aeration tank and the biological filter, so that the contact oxidation tank can achieve higher volume load.
2. Because the fixation amount in the pool is large and the water flow belongs to a complete mixing type, the water treatment device has stronger adaptability to sudden change of water quality and water quantity.
3. Due to the high sludge concentration, the F/M is maintained at a certain level when the organic load is high, so that the sludge yield can be comparable to or lower than that of the activated sludge process.
4. The SS content in the wastewater subjected to front-end physicochemical treatment is low, and carriers for biofilm fixation are few, so that the specific gravity of the biofilm is small, the biofilm removal is easy to cause, the biofilm formation is unstable, and the SS content of the effluent is easy to exceed the standard.
Third, dissolved air flotation
The dissolved air flotation process utilizes the characteristic that the solubility of water is different under different pressures, and micro bubbles are generated in water under the condition of pressurization or negative pressure, so that the traditional air flotation process for introducing air into water by air introducing equipment is replaced.
The dissolved air flotation has the following characteristics:
1. Solid-liquid, liquid-liquid and tiny suspended matters with specific gravity similar to water are removed.
2. small occupied area and high water yield per unit area.
3. The process flow is simple, the cost is low, and the management and the maintenance are convenient.
4. Because the process mainly takes separation as a main part, the process can be used as primary treatment or advanced pretreatment in the whole sewage treatment process.
Four, continuous sand filtering
The continuous sand filtration process is a three-stage treatment process with simultaneous filtration and backwashing, effectively removes SS in sewage and simultaneously has the functions of micro-flocculation dephosphorization and certain denitrification.
the continuous sand filtration has the following characteristics:
1. The filtration and the back washing are carried out simultaneously, and the continuous operation can be carried out without stopping.
2. The air stripping is utilized to lift the filter sand in the filter tank, and the whole system only has an air compressor without other power equipment.
3. The whole system is a pure pipeline system without a control valve.
4. Compared with the traditional filter tank, the continuous sand filtering system has simpler operation and control.
Therefore, in summary, it is difficult to achieve the treatment standard of the primary A, especially the removal of TN and TP, with the conventional single treatment process for the comprehensive sewage with medium and high concentration (COD concentration: 600 ~ 800 mg/L; BOD concentration: 300 ~ 400 mg/L; TN concentration: 70 ~ 100mg/L; and TP concentration: 8 ~ 20 mg/L).
SUMMERY OF THE UTILITY MODEL
The utility model aims at solving the problem that the traditional single treatment process is difficult to reach the treatment standard of one level A for the comprehensive sewage with medium and high concentration, especially the removal of TN and TP is difficult point, and providing a medium and high concentration comprehensive sewage denitrification and dephosphorization treatment system.
The utility model discloses a realize that the technical scheme that above-mentioned purpose adopted is: a middle-high concentration comprehensive sewage denitrification and dephosphorization treatment system is characterized in that: the utility model provides a sewage denitrogenation dephosphorization processing system is synthesized to well high concentration which characterized in that: the downstream of the high-efficiency air flotation tank is connected with an anoxic reaction tank, the downstream of the anoxic reaction tank is sequentially connected with an anaerobic reaction tank and an aerobic reaction tank, the downstream of the aerobic reaction tank is connected with a residual sludge sedimentation tank, the residual sludge sedimentation tank is connected to the anoxic reaction tank at the front end through a reflux pump and a reflux pipeline, the downstream of the residual sludge sedimentation tank is connected with a chemical phosphorus removal coagulating sedimentation tank, the downstream of the chemical phosphorus removal coagulating sedimentation tank is connected with a continuous sand filter tank, and the downstream of the continuous sand filter tank is respectively connected with a sand filtration backwashing water return tank and a clear.
a coagulation tank and a flocculation tank are arranged in the high-efficiency air floatation tank, and are respectively provided with a coagulation stirrer, the coagulation tank and the flocculation tank are connected through a coagulation-flocculation communicating pipe, the coagulation tank is connected with a PAC dosing device I, and the flocculation tank is connected with a PAM dosing device; the dissolved air pump that sets up in the high-efficient air supporting pond connects sand filtration backwash return water pond and compressed air storage tank respectively, and then connects the air supporting dissolved air tank that the high-efficient air supporting incasement was established, and the air supporting dissolved air tank is connected and is dissolved gas release pipe, dissolves gas release union coupling coagulating basin, flocculation vat, easily floats debris such as dephosphorization flocculating constituent and grease that form in the sewage and form the dross to strike off through connecting in the high-efficient air supporting pond low reaches scraper, scrape the air supporting scum pipe that sediment machine low reaches set up and are used for getting rid of the dross.
And a water level adjusting weir gate for adjusting the water level of the air flotation tank is arranged in the high-efficiency air flotation tank.
The anoxic reaction tank and the anaerobic reaction tank are internally provided with stirrers for creating anoxic and anaerobic environments.
A fixed filler is arranged in the aerobic reaction tank to form a sludge film coexisting state and rich biological phases; and an aeration system consisting of a blower connected with a disc aerator is arranged at the same time.
The excess sludge sedimentation tank is provided with an inclined tube filler for quickly separating mud and water, a mud bucket at the bottom of the tank is respectively connected with a reflux pump and an electric mud valve, the reflux pump is connected into the anoxic reaction tank, the electric mud valve is connected to the outside of the system, and the upper part in the tank is provided with a water collecting tank connected into the chemical phosphorus removal coagulation sedimentation tank.
The chemical dephosphorization coagulating sedimentation tank is internally provided with a coagulation tank and a flocculation tank and is respectively provided with a coagulation stirrer, the coagulation tank is connected with the flocculation tank through a coagulation flocculation communicating pipe, the coagulation tank is connected with a PAC dosing device II, the flocculation tank is connected with a composite dephosphorization agent dosing device, the flocculation tank is internally connected with an inclined pipe filler for separating dephosphorization sludge, a bottom sludge hopper is connected with an electric sludge discharge valve, and the electric sludge discharge valve is connected to the outside of the system.
And a continuous sand washer which is used for filtering and back flushing is arranged in the continuous sand filter, and the continuous sand washer is connected with a compressed air storage tank.
The utility model has the characteristics that:
1. Compact structure, small occupied area and higher treatment load, and the sludge load can reach 0.06 ~ 0.1.1 KgBOD/KgMLSS.d.
2. the internal reflux design and the backwashing water after continuous filtration are recycled to the air-flotation water-dissolving water, so that the efficiency and the energy are high.
3. The removal rate of higher TN of denitrification can be achieved by controlling the return flow of the nitrifying liquid and the sludge and controlling the dissolved oxygen in the reaction zone.
4. the return sludge and the chemical phosphorus removal sludge are separately designed, so that the influence of dosing on the activated sludge is reduced to the minimum. Meanwhile, the sludge of chemical phosphorus removal can be recycled or specially treated.
Drawings
Fig. 1 is a functional partition diagram of the present invention.
Fig. 2 is a schematic diagram of the equipment layout of the present invention.
Fig. 3 is a schematic view of the pipeline layout of the present invention.
In the figure: the system comprises a T1 high-efficiency air flotation tank, a T2 anoxic reaction tank, a T3 anaerobic reaction tank, a T4 aerobic reaction tank, a T5 residual sludge sedimentation tank, a T6 chemical phosphorus removal coagulating sedimentation tank, a T7 continuous sand filter tank, a T8 sand filter backwashing water return tank and a T9 clear water outlet tank.
The device comprises an E1 coagulation stirrer, an E2 air dissolving pump, an E3 air floating air dissolving tank, an E4 air compressor, an E5 slag scraping machine, an E6 PAC dosing device I, an E7 PAM dosing device, an E8 air blower, an E9 stirrer, an E10 fixed filler, an E11 disc aerator, an E12 reflux pump, an E13 inclined tube filler, an E14 electric mud discharge valve, an E15 water collecting tank, an E16 PAC dosing device II, an E17 composite phosphorus removing agent dosing device, an E18 continuous sand washer, an E19 compressed air storage tank and an E20 water level adjusting weir gate.
The device comprises a G1 process sewage inlet pipe, a G2 air flotation slag discharge pipe, a G3 process clear water outlet pipe, a G4 sludge discharge pipe, a G5 return pipe, a G6 dissolved air release pipe, a G7 air flotation water outlet collection pipe, a G8 coagulation flocculation communicating pipe, a G9 sand filtration water inlet pipe, a G10 sand filtration backwashing pipe, a G11 aeration pipe, a G12 return water dissolved air pipe and a G13 chemical dosing pipe.
Detailed Description
The present invention will be described in detail with reference to the accompanying drawings.
Examples
As shown in the figures 1-3, the downstream of a high-efficiency air flotation tank T1 is connected with an anoxic reaction tank T2, the downstream of an anoxic reaction tank T2 is sequentially connected with an anaerobic reaction tank T3 and an aerobic reaction tank T4, the downstream of an aerobic reaction tank T4 is connected with a residual sludge sedimentation tank T5, the residual sludge sedimentation tank T5 is connected with the anoxic reaction tank T2 at the front end through a reflux pump E12 and a reflux pipeline, the downstream of the residual sludge sedimentation tank T5 is connected with a chemical phosphorus removal coagulation sedimentation tank T6, the downstream of the chemical phosphorus removal coagulation sedimentation tank T6 is connected with a continuous sand filter tank T7, and the downstream of the continuous sand filter T7 is respectively connected with a sand filtration backwashing water return tank T8 and a clear water outlet tank T9.
A coagulation tank and a flocculation tank are arranged in the high-efficiency air flotation tank T1, a coagulation stirrer E1 is respectively arranged in the high-efficiency air flotation tank, the coagulation tank is connected with the flocculation tank through a coagulation-flocculation communicating pipe G8, the coagulation tank is connected with a PAC dosing device E6, and the flocculation tank is connected with a PAM dosing device E7; dissolved air pump E2 that sets up in high-efficient air supporting pond T1 connects sand filtration backwash return water pond T8 and compressed air storage tank E19 respectively, and then connect the air supporting dissolved air tank E3 that sets up in high-efficient air supporting pond T1, air supporting dissolved air tank E3 connects dissolved air release pipe G6, dissolved air release pipe G6 connects the coagulating basin, the flocculating constituent, easy superficial debris such as dephosphorization flocculating constituent and grease that form in the sewage form the dross, and strike off through connecting in high-efficient air supporting pond T1 in the low reaches slag scraper E5, slag scraper E5 low reaches and sets up the air supporting scum pipe G2 that is used for getting rid of the dross.
And a water level adjusting weir gate E20 for adjusting the water level of the air flotation tank is arranged in the high-efficiency air flotation tank T1.
Stirrers E9 are arranged in the anoxic reaction tank T2 and the anaerobic reaction tank T3 and are used for creating an anoxic and anaerobic environment.
A fixed filler E10 is arranged in the aerobic reaction tank T4 to form a mud film coexistence state and rich biological phases; an aeration system consisting of a blower E8 and a disc aerator E11 is also arranged.
The residual sludge settling tank T5 is provided with an inclined tube filler E13 for quickly separating mud and water, a sludge bucket at the bottom of the tank is respectively connected with a reflux pump E12 and an electric sludge discharge valve E14, the reflux pump E12 is connected into the anoxic reaction tank T2, the electric sludge discharge valve E14 is connected outside the system, and the upper part in the tank is provided with a water collecting tank E15 connected into the chemical phosphorus removal coagulation settling tank T6.
The chemical phosphorus removal coagulating sedimentation tank T6 is internally provided with a coagulating tank and a flocculating tank and is respectively provided with a coagulating stirrer E1, the coagulating tank is connected with the flocculating tank through a coagulating and flocculating communicating pipe G8, the coagulating tank is connected with a PAC dosing device II E16, the flocculating tank is connected with a composite phosphorus removal agent dosing device E17, the flocculating tank is internally connected with an inclined pipe filler E13 used for separating phosphorus removal sludge, a bottom sludge hopper is connected with an electric sludge discharge valve E14, and the electric sludge discharge valve E14 is connected to the outside of the system.
A continuous sand washer E18 which can filter and backwash simultaneously is arranged in the continuous sand filter T7, and the continuous sand washer E18 is connected with a compressed air storage tank E19.
Entire system can divide into three processing stage when using:
And in the 1 st stage, high-efficiency air floatation deep pretreatment.
The sewage to be treated continuously enters the system through a process sewage inlet pipe G1, and firstly enters a high-efficiency air flotation tank T1.
The coagulation and flocculation tank of the high-efficiency air flotation tank T1 is respectively provided with a stirrer, and the coagulation tank and the flocculation tank are connected through a coagulation and flocculation communicating pipe G8, so that the coagulation retention time is prolonged. PAC dosing equipment E6 and PAM dosing equipment E7 respectively feed PAC and PAM into the coagulation tank, and the mixture is uniformly mixed through a coagulation stirrer E1. The dissolved air water is taken from a sand filtration backwashing water return tank T8, the dissolved air water is pumped into an air-flotation dissolved air tank E3 through an air-dissolving pump E2, meanwhile, a path of compressed air is provided by a compressed air storage tank E19 and enters the air-flotation dissolved air tank E3, the pressurized dissolved air water is released in an air-dissolving release pipe G6 to form micro-bubbles, the micro-bubbles form floating slag from easy-floating impurities such as phosphorus removal flocculating constituents, grease and the like formed in sewage, the floating slag is scraped through a slag scraper E5, and the floating slag is discharged out of a system through an air-flotation slag discharge pipe G2 and is additionally treated. The water level of the air floatation tank can be adjusted through a water level adjusting weir gate E20 to reach the optimal slag scraping height.
And 2, anaerobic and aerobic biochemical pond treatment and sludge-water separation.
The pollutants discharged by the air floatation water enter an anoxic reaction tank T2 after deep pretreatment, the discharged water of the anoxic reaction tank T2 enters an anaerobic reaction tank T3, E9 stirrers are respectively arranged in the anoxic reaction tank T2 and the anaerobic reaction tank T3, anoxic and anaerobic environments are created by ceaseless stirring, and the denitrification treatment effect is enhanced. The effluent of the anaerobic reaction tank T3 enters an aerobic reaction tank T4. The aerobic reaction tank T4 is provided with a fixed filler E10 to form a sludge film coexistence state and rich biological phases. The aeration system consists of a blower E8 and a disc aerator E11, and the continuous low dissolved oxygen aeration achieves the best aerobic treatment effect. The residual sludge settling tank T5 makes mud and water quickly separated through an inclined tube filler E13, the sludge falls into a sludge bucket at the bottom of the tank, one part of the sludge flows back to the anoxic reaction tank T2 through a return pump E12, and one part of the residual sludge can be discharged out of the system through an electric sludge discharge valve E14.
And 3, two-stage chemical phosphorus removal, continuous sand filtration and water discharge.
The supernatant is collected by a water collecting tank E15 and enters a chemical phosphorus removal coagulating sedimentation tank T6, and a coagulation and flocculation tank and a stirrer are also arranged in the chemical phosphorus removal coagulating sedimentation tank T6. And a PAC dosing device II E16 and a composite phosphorus removing agent dosing device E17 respectively dose phosphorus removing agents into the coagulation and flocculation tanks to further remove TP in the water to reach the standard. Dephosphorization sludge formed by adding the chemicals is separated through an inclined tube filler E13, the sludge falls into a bottom hopper, the sludge is discharged out of a system through an electric sludge discharge valve E14, supernatant enters a continuous sand filter T7, the continuous sand filter T7 performs backwashing while filtering, the whole process is completed by a continuous sand washer E18, and compressed air required by the continuous sand washer E18 is provided by another air source pipeline of a compressed air storage tank E19 (wherein one air source pipeline is used for floating). After continuous filtration by the continuous sand filter T7, the effluent SS reaches the standard, clean water enters the clear water outlet pool T9, and the effluent of the clear water outlet pool T9 can reach the standard after being sterilized by ultraviolet disinfection externally connected with the system and then be discharged.
Claims (8)
1. The utility model provides a sewage denitrogenation dephosphorization processing system is synthesized to well high concentration which characterized in that: the downstream of the high-efficiency air flotation tank is connected with an anoxic reaction tank, the downstream of the anoxic reaction tank is sequentially connected with an anaerobic reaction tank and an aerobic reaction tank, the downstream of the aerobic reaction tank is connected with a residual sludge sedimentation tank, the residual sludge sedimentation tank is connected to the anoxic reaction tank at the front end through a reflux pump and a reflux pipeline, the downstream of the residual sludge sedimentation tank is connected with a chemical phosphorus removal coagulating sedimentation tank, the downstream of the chemical phosphorus removal coagulating sedimentation tank is connected with a continuous sand filter tank, and the downstream of the continuous sand filter tank is respectively connected with a sand filtration backwashing water return tank and a clear.
2. The system of claim 1, wherein the system comprises: a coagulation tank and a flocculation tank are arranged in the high-efficiency air floatation tank, and are respectively provided with a coagulation stirrer, the coagulation tank and the flocculation tank are connected through a coagulation-flocculation communicating pipe, the coagulation tank is connected with a PAC dosing device I, and the flocculation tank is connected with a PAM dosing device; the dissolved air pump that sets up in the high-efficient air supporting pond connects sand filtration backwash return water pond and compressed air storage tank respectively, and then connects the air supporting dissolved air tank that the high-efficient air supporting incasement was established, and the air supporting dissolved air tank is connected and is dissolved gas release pipe, dissolves gas release union coupling coagulating basin, flocculation vat, easily floats debris such as dephosphorization flocculating constituent and grease that form in the sewage and form the dross to strike off through connecting in the high-efficient air supporting pond low reaches scraper, scrape the air supporting scum pipe that sediment machine low reaches set up and are used for getting rid of the dross.
3. the system of claim 2, wherein the system comprises: and a water level adjusting weir gate for adjusting the water level of the air flotation tank is arranged in the high-efficiency air flotation tank.
4. The system of claim 1, wherein the system comprises: the anoxic reaction tank and the anaerobic reaction tank are internally provided with stirrers for creating anoxic and anaerobic environments.
5. The system of claim 1, wherein the system comprises: a fixed filler is arranged in the aerobic reaction tank to form a sludge film coexisting state and rich biological phases; and an aeration system consisting of a blower connected with a disc aerator is arranged at the same time.
6. The system of claim 1, wherein the system comprises: the excess sludge sedimentation tank is provided with an inclined tube filler for quickly separating mud and water, a mud bucket at the bottom of the tank is respectively connected with a reflux pump and an electric mud valve, the reflux pump is connected into the anoxic reaction tank, the electric mud valve is connected to the outside of the system, and the upper part in the tank is provided with a water collecting tank connected into the chemical phosphorus removal coagulation sedimentation tank.
7. The system of claim 1, wherein the system comprises: the chemical dephosphorization coagulating sedimentation tank is internally provided with a coagulation tank and a flocculation tank and is respectively provided with a coagulation stirrer, the coagulation tank is connected with the flocculation tank through a coagulation flocculation communicating pipe, the coagulation tank is connected with a PAC dosing device II, the flocculation tank is connected with a composite dephosphorization agent dosing device, the flocculation tank is internally connected with an inclined pipe filler for separating dephosphorization sludge, a bottom sludge hopper is connected with an electric sludge discharge valve, and the electric sludge discharge valve is connected to the outside of the system.
8. The system of claim 1, wherein the system comprises: and a continuous sand washer which is used for filtering and back flushing is arranged in the continuous sand filter, and the continuous sand washer is connected with a compressed air storage tank.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920435520.3U CN209797712U (en) | 2019-04-02 | 2019-04-02 | Medium-high concentration comprehensive sewage nitrogen and phosphorus removal treatment system |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201920435520.3U CN209797712U (en) | 2019-04-02 | 2019-04-02 | Medium-high concentration comprehensive sewage nitrogen and phosphorus removal treatment system |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109809653A (en) * | 2019-04-02 | 2019-05-28 | 大连迈克环境科技工程有限公司 | A kind of middle and high concentration composite wastewater denitrogenation dephosphorizing treatment process |
| CN113772900A (en) * | 2021-10-19 | 2021-12-10 | 交通运输部天津水运工程科学研究所 | Efficient nitrogen and phosphorus removal process system for mariculture tail water treatment |
| CN115072941A (en) * | 2022-07-21 | 2022-09-20 | 深圳永清水务有限责任公司北京分公司 | Biological electrochemical device for treating high-salinity wastewater |
-
2019
- 2019-04-02 CN CN201920435520.3U patent/CN209797712U/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109809653A (en) * | 2019-04-02 | 2019-05-28 | 大连迈克环境科技工程有限公司 | A kind of middle and high concentration composite wastewater denitrogenation dephosphorizing treatment process |
| CN113772900A (en) * | 2021-10-19 | 2021-12-10 | 交通运输部天津水运工程科学研究所 | Efficient nitrogen and phosphorus removal process system for mariculture tail water treatment |
| WO2023065653A1 (en) * | 2021-10-19 | 2023-04-27 | 交通运输部天津水运工程科学研究所 | High-efficiency denitrification and dephosphorization process system for mariculture tail water treatment |
| CN115072941A (en) * | 2022-07-21 | 2022-09-20 | 深圳永清水务有限责任公司北京分公司 | Biological electrochemical device for treating high-salinity wastewater |
| CN115072941B (en) * | 2022-07-21 | 2024-06-07 | 深圳永清水务有限责任公司 | Bioelectrochemical device for treating high-salt wastewater |
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