CN212356736U - High-efficiency nitrogen and phosphorus removal domestic sewage treatment equipment for enriching denitrifying phosphorus accumulating bacteria - Google Patents
High-efficiency nitrogen and phosphorus removal domestic sewage treatment equipment for enriching denitrifying phosphorus accumulating bacteria Download PDFInfo
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- CN212356736U CN212356736U CN202020619769.2U CN202020619769U CN212356736U CN 212356736 U CN212356736 U CN 212356736U CN 202020619769 U CN202020619769 U CN 202020619769U CN 212356736 U CN212356736 U CN 212356736U
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 56
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 title claims abstract description 53
- 229910052698 phosphorus Inorganic materials 0.000 title claims abstract description 53
- 239000011574 phosphorus Substances 0.000 title claims abstract description 53
- 241000894006 Bacteria Species 0.000 title claims abstract description 28
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 28
- 239000010865 sewage Substances 0.000 title claims abstract description 27
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 59
- 239000010802 sludge Substances 0.000 claims abstract description 54
- 238000004062 sedimentation Methods 0.000 claims abstract description 30
- 238000001179 sorption measurement Methods 0.000 claims abstract description 30
- 238000000034 method Methods 0.000 claims abstract description 24
- 229910000975 Carbon steel Inorganic materials 0.000 claims abstract description 4
- 239000010962 carbon steel Substances 0.000 claims abstract description 4
- 239000007788 liquid Substances 0.000 claims description 18
- 230000033116 oxidation-reduction process Effects 0.000 claims description 11
- 239000000945 filler Substances 0.000 claims description 10
- 238000005276 aerator Methods 0.000 claims description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 7
- 229910052760 oxygen Inorganic materials 0.000 claims description 7
- 239000001301 oxygen Substances 0.000 claims description 7
- 239000010935 stainless steel Substances 0.000 claims description 5
- 229910001220 stainless steel Inorganic materials 0.000 claims description 5
- 239000002351 wastewater Substances 0.000 claims description 4
- 230000014759 maintenance of location Effects 0.000 claims description 2
- 238000013019 agitation Methods 0.000 claims 1
- 238000004065 wastewater treatment Methods 0.000 claims 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 12
- 229910052799 carbon Inorganic materials 0.000 abstract description 12
- 230000001360 synchronised effect Effects 0.000 abstract description 8
- 230000000694 effects Effects 0.000 abstract description 7
- 230000010354 integration Effects 0.000 abstract description 4
- 238000010992 reflux Methods 0.000 description 16
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 11
- 238000005273 aeration Methods 0.000 description 11
- 230000001276 controlling effect Effects 0.000 description 8
- 229920013639 polyalphaolefin Polymers 0.000 description 6
- 229920001397 Poly-beta-hydroxybutyrate Polymers 0.000 description 4
- 229920000331 Polyhydroxybutyrate Polymers 0.000 description 4
- 238000007790 scraping Methods 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 229910002651 NO3 Inorganic materials 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 2
- 230000001651 autotrophic effect Effects 0.000 description 2
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- 230000001546 nitrifying effect Effects 0.000 description 2
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- PAWQVTBBRAZDMG-UHFFFAOYSA-N 2-(3-bromo-2-fluorophenyl)acetic acid Chemical compound OC(=O)CC1=CC=CC(Br)=C1F PAWQVTBBRAZDMG-UHFFFAOYSA-N 0.000 description 1
- 241000233866 Fungi Species 0.000 description 1
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 210000005056 cell body Anatomy 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000012258 culturing Methods 0.000 description 1
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- 238000012986 modification Methods 0.000 description 1
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- 229910000402 monopotassium phosphate Inorganic materials 0.000 description 1
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- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- PJNZPQUBCPKICU-UHFFFAOYSA-N phosphoric acid;potassium Chemical compound [K].OP(O)(O)=O PJNZPQUBCPKICU-UHFFFAOYSA-N 0.000 description 1
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Abstract
The utility model discloses a high-efficiency denitrification and dephosphorization domestic sewage treatment device for enriching denitrification phosphorus-accumulating bacteria, which comprises a tank body, an anaerobic tank, an adsorption tank, an anoxic tank, a facultative tank, an aerobic tank and a sedimentation tank; the tank body is integrally assembled by rectangular carbon steel open type multi-channel integration; the left side is provided with a sedimentation tank, the right side is provided with a facultative tank, and the middle is provided with an anaerobic tank, an anoxic tank, an aerobic tank and an adsorption tank; a return channel, a water outlet channel, an air inlet pipe, an water inlet pipe, a water outlet pipe and a residual sludge pipe are arranged at the periphery of the sludge tank; by controlling the process and the operating conditions, the DPB in the system dominates, the synchronous nitrogen and phosphorus removal can be realized under the condition of low carbon source, and the 'one carbon dual-purpose' is realized; this novel can induce DPB to become the effect of dominant bacteria group performance denitrification phosphorus removal under the low C/N condition, nitrogen and phosphorus removal is effectual, prevents effectively that mud from expanding, satisfies domestic sewage stable, high-efficient nitrogen and phosphorus removal complete sets demand.
Description
Technical Field
The utility model relates to the field of domestic sewage treatment technical equipment, in particular to a high-efficient nitrogen and phosphorus removal domestic sewage treatment device of enrichment denitrification phosphorus-accumulating bacteria.
Background
With the scientific and technological progress and the development of social economy, the standard of urban domestic sewage treatment is continuously improved; a large amount of nitrogen and phosphorus wastewater in the sewage is directly discharged into a water body without proper treatment, so that the water body environment is seriously polluted, and the human health is seriously harmed. Due to the shortage of water resources in China, the implementation of the strategy of sustainable development is severely restricted. The problem of nitrogen and phosphorus removal in domestic sewage causes difficulty in the standard discharge of urban sewage. The traditional biological nitrogen and phosphorus removal method plays a certain role in sewage treatment, but still has a plurality of defects. If competition of phosphorus-accumulating bacteria and denitrifying bacteria on a carbon source always exists, the sludge ages of the nitrifying bacteria, the denitrifying bacteria and the phosphorus-accumulating bacteria are different, various bacteria are mixed together and are restricted with each other, and the system is difficult to achieve the optimal operation condition; under the condition of low C/N ratio, the aerobic biological phosphorus removal process increases power consumption and generates a large amount of excess sludge; the whole treatment process has the advantages of longer flow, large floor area, high capital investment and the like.
With the continuous and intensive research on sewage treatment, several novel biological nitrogen and phosphorus removal processes have been developed and applied in recent years, mainly including: the novel processes comprise a synchronous nitrification and denitrification process, a short-cut nitrification and denitrification process, an anaerobic ammonia oxidation process, a completely autotrophic nitrogen removal process and a denitrification and phosphorus removal process, and have the advantages of reducing energy consumption, saving carbon sources, reducing sludge yield, occupying small area and the like. Particularly, the Denitrifying phosphorus removal process enables two independent processes of phosphorus removal and denitrification to be simultaneously completed only in an anoxic environment in the presence of Denitrifying phosphorus bacteria DPB (Denitrifying phosphorus culturing bacteria), the combination of the processes of phosphorus absorption and denitrification not only saves the need of a carbon source, but also saves the energy required by aeration by completing the phosphorus absorption in the anoxic environment, and the generated residual sludge amount is greatly reduced. Therefore, the denitrification dephosphorization technology becomes one of the key points and hot spots in the research field of the dephosphorization and denitrification of the sewage at present.
In the prior art, the sewage treatment process can not take nitrogen removal and phosphorus removal into consideration, and the process needs to be improved; the disadvantages of the prior art are represented by: 1. the integration of the equipment is not high enough; 2. the contradiction of sludge age is difficult to solve, wherein the sludge age of autotrophic Nitrite Oxidizing Bacteria (NOB) is long, and the sludge age of DPB and phosphorus accumulating bacteria (PAOs) is short, so that the sludge can not simultaneously exert the maximum efficiency in the same system; 3. carbon source competition: DPB, PAOs and denitrifying bacteria in the sewage with low C/N ratio compete for a carbon source; 4. DO and NO carried in sludge recirculation3 -Inhibit the anaerobic phosphorus release of DPB and PAOs.
SUMMERY OF THE UTILITY MODEL
In order to solve the technical problem, the utility model provides a high-efficiency denitrification and dephosphorization domestic sewage treatment device for enriching denitrification phosphorus-accumulating bacteria, aiming at the defects in the prior art, the device has the advantages of high research and development integration level, low consumption, high efficiency, easy operation and management, stable operation and capability of realizing the rapid enrichment of DPB; the enrichment configuration equipment is optimized, the high-efficiency enrichment of DPB is realized under the low C/N condition, and the requirements of the domestic sewage high-efficiency nitrogen and phosphorus removal complete equipment are met.
In order to achieve the above purpose, the technical scheme of the utility model is as follows: an efficient denitrification and dephosphorization domestic sewage treatment device for enriching denitrification phosphorus-accumulating bacteria, which is called denitrification and dephosphorization device for short; comprises a tank body, an anaerobic tank, an adsorption tank, an anoxic tank, a facultative tank, an aerobic tank and a sedimentation tank; the method is characterized in that:
the nitrogen and phosphorus removal equipment is of a rectangular carbon steel structure, and the tank body is integrally assembled by a plurality of open channels without top covers; the aspect ratio of the channel of the nitrogen and phosphorus removal equipment is 5: 1-10: 1, and the width-depth ratio is 1: 1-2: 1; a sedimentation tank is arranged on the left side of the tank body, a facultative tank is arranged on the right side of the tank body, an anaerobic tank and an anoxic tank are arranged in parallel on the lower middle part, and an aerobic tank is arranged in parallel on the upper middle part; an adsorption tank is arranged above the anaerobic tank; backflow channels are arranged on the left side and the periphery of the upper part of the inner side of the tank body; a water outlet channel is arranged on the right side of the inner side of the tank body; the upper part and the left side of the outer side of the tank body are respectively provided with two groups of air inlet pipes, and the lower part of the outer side of the tank body is respectively provided with a water inlet pipe, a water outlet pipe and a residual sludge pipe; an air ejector is arranged at the upper left corner in the tank body;
water through holes are formed among the anaerobic tank, the adsorption tank, the anoxic tank, the facultative tank, the aerobic tank and the sedimentation tank, and the hydraulic form is plug flow type; the starting end of the anaerobic tank is provided with a water inlet pipe and a submersible plug flow stirrer, and the tail end of the anaerobic tank is provided with an oxidation-reduction potential meter (ORP meter); a submersible stirrer is arranged in the center of the adsorption tank, the submersible stirrer is provided with an upper group of blades and a lower group of blades, and a water passing hole arranged on one side of the adsorption tank, which is close to the sedimentation tank, is used as a sludge return hole; the starting end of the facultative tank is provided with a submersible plug flow stirrer, and the starting end of the facultative tank is communicated with the return channel of the mixed liquid in the aerobic tank through a water through hole; a pipeline leading to the bottom of the anoxic tank is arranged at the bottom of the backflow channel, an ORP (oxidation-reduction potential) instrument and a submersible backflow pump are arranged at the tail end of the backflow channel, and an outlet of the backflow pump is positioned at the starting end of the anaerobic tank and is provided with a flap valve; the facultative tank is respectively provided with two grids which are arranged in series front and back, the starting end of each grid is provided with a submersible plug flow stirrer, the bottom of each grid is provided with an aerator, and the tail end of the second grid of the facultative tank is provided with an ORP instrument and a dissolved oxygen instrument (DO instrument); the aerobic tank is divided into two grids which are arranged in parallel and in series, an aerator is arranged at the bottom of each grid, moving bed fillers are filled in the aerobic tank, a DO instrument and an air lifter are arranged at the tail end of the second grid of the aerobic tank, and the mixed liquor in the aerobic tank flows to a return channel through the air lifter; a stainless steel mesh is arranged between the air lifter and the aerobic tank and is used for preventing the moving bed filler from entering the area of the air lifter; a channel gate is arranged on a return channel of the mixed liquid which is led to the facultative tank and the anoxic tank, and the channel gate is used for adjusting the return flow; the sedimentation tank adopts the form of long-edge water inlet and long-edge water outlet at the outer side, a water distribution hole is arranged below the water inlet channel of the sedimentation tank, a hydraulic baffle is arranged below the water distribution hole, sludge in the sedimentation tank is discharged into a sludge return channel through a travelling type sludge scraping and sucking machine, and the returned sludge flows back through the sludge on the adsorption tankThe holes enter an adsorption tank, and the excess sludge is discharged through an excess sludge pipe at the tail end of the channel; the whole process is controlled by three ORP instruments and two DO instruments to ensure the effluent NH4 +＜3mg/L，TN＜10mg/L，TP＜0.5mg/L。
The hydraulic retention time of the anaerobic tank, the adsorption tank, the anoxic tank, the facultative tank, the aerobic tank and the sedimentation tank is 1.5h, 0.3h, 2h, 6h and 2h respectively; the surface load of the sedimentation tank is 0.8m3/㎡·h—1.2m3Square meter per hour; the ORP control range of the anaerobic tank is-450 mV to-250 mV; the ORP control range of the anoxic tank is-150 mV to 0 mV; the ORP control range of the facultative tank is-100 mV to 50mV, and the DO control range of the facultative tank is less than 0.6 mg/L; the DO control range of the aerobic tank is 1.5 mg/L-2.5 mg/L.
The submerged stirrer in the adsorption tank adopts a low-speed stirrer, and the stirring speed is 40-60 r/min; the unit power of the submersible plug flow stirrer in the anaerobic tank, the anoxic tank and the facultative tank is 2W/m3—4W/m3(wastewater).
The anoxic tank flows back to the anaerobic tank, and the reflux ratio is 100%; the sludge in the sedimentation tank flows back to the adsorption tank, the reflux ratio is 50% -100%, the DPB is alternately enriched in anaerobic/anoxic volume through reflux, and NO is eliminated to the maximum extent through the mode that the mixed liquor in the anoxic tank flows back to the anaerobic tank3 -And DO inhibition of DPB and PAOs.
The facultative tank adopts an intermittent aeration mode, the mixed liquor of the anoxic tank and the mixed liquor of the aerobic tank return flow enter the facultative tank together, DPB is induced to become dominant flora under the condition of low C/N ratio, the synchronous nitrogen and phosphorus removal operation is realized, and the facultative tank has the characteristic of one carbon and two purposes; the synchronous nitrification-denitrification (SND) of facultative denitrifying bacteria is enhanced under low DO conditions.
The control mode of the facultative tank aeration is that when water is discharged NH4 +When the concentration of the oxygen in the aerobic tank is less than or equal to 3mg/L, starting aeration under the following three conditions that DO in the aerobic tank is less than 1.5 mg/L; when ORP of the facultative tank is less than-100 mV; ③ when the OPR of the anoxic pond is less than-150 mV; when water is discharged NH4 +When the concentration is more than 3mg/L, the facultative tank starts aeration,up to water outlet NH4 +Less than or equal to 3 mg/L; when water is discharged NH4 +When the concentration is less than or equal to 3mg/L, the aeration is closed under two conditions that the DO of the facultative tank is more than 0.6 mg/L; ② the ORP of the facultative tank is more than 50 mV.
A moving bed filler is arranged in the aerobic tank, nitrifying bacteria (NOB) with longer sludge age are fixed, and NH is strengthened4 +Removing effect, wherein the filling ratio of the filler is 20% -50%; the reflux of the mixed liquid in the aerobic tank adopts an air stripping pushing mode, so that the energy consumption is reduced, and simultaneously, the large reflux ratio is realized, and the reflux ratio range is 100-400%; the reflux quantity of the mixed liquid in the aerobic tank is realized by controlling the air blower to increase or decrease the air quantity supplied to the air stripping pusher through the frequency converter.
Controlling the reflux amount of the mixed liquid in the aerobic tank, namely when the OPR of the anoxic tank is less than-150 mV, properly increasing the reflux amount to the anoxic tank by increasing the opening of a channel gate; when the ORP of the facultative tank is less than-100 mV, properly increasing the reflux amount to the facultative tank by increasing the opening of a channel gate; when the OPR of the anoxic pond is more than 0mV, properly reducing the reflux amount to the anoxic pond by reducing the opening of the canal gate; when the ORP of the facultative tank is more than 50mV, the return flow to the facultative tank is properly reduced by reducing the opening degree of a channel gate.
The utility model discloses a theory of operation does:
domestic sewage firstly enters an anaerobic tank, phosphorus accumulating bacteria (PAOS) and DPB carry out anaerobic phosphorus release and the COD of the inlet water is utilized to synthesize poly-beta-hydroxybutyrate (PHB), and the process is easy to be subjected to NO3 -And DO, so as to reduce the anaerobic phosphorus release efficiency; therefore, the sludge is returned to the adsorption tank through the sedimentation tank and is fully mixed with the mixed liquid from the anaerobic tank, residual COD is adsorbed to prevent the sludge from expanding, and PHB is synthesized; DPB utilizes PHB as an electron donor, NO3 -Endogenous denitrification as an electron acceptor, which is continued in an anoxic tank with NO at the end3 -And DO content is almost zero, the anoxic mixed liquor flows back to the starting end of the anaerobic tank through a reflux pump, and a good 'suppressing' environment is created for the anaerobic phosphorus release of the DPB; the mixed liquid of the anoxic tank and the mixed liquid returned by the aerobic tank enter a facultative tank together and are implemented under the condition of low DOSynchronous Nitrification and Denitrification (SND) are carried out at present, the nitrification and denitrification are respectively carried out in the aerobic tank and the facultative tank at respective maximum reaction rates, and simultaneously, the DPB carries out denitrification dephosphorization; little COD enters the aerobic tank, the NOB occupies the dominant position in the aerobic tank, and moving bed filler is added into the aerobic tank to fix the NOB with longer sludge age and strengthen the nitrification effect; simultaneously, DPB and PAOS carry out dephosphorization and sludge regeneration, mixed liquid in the aerobic tank flows back to the facultative tank and the anoxic tank, and the purpose of the backflow anoxic tank is to assist backflow sludge to supplement NO to the anoxic tank3 -Satisfies the DPB utilization of NO3 -The derivative is used as an electron acceptor to realize denitrification and induce the enrichment of DPB under the alternate anaerobic/anoxic condition. And (4) discharging water from the aerobic tank to a sedimentation tank, lifting the sludge to a sludge return channel through a travelling type sludge scraping and sucking machine, and then flowing into an adsorption tank.
Through the technical scheme, the utility model discloses technical scheme's beneficial effect is: the novel integrated nitrogen and phosphorus removal device has high integrated degree and good nitrogen and phosphorus removal effect under the condition of low C/N; the nitrogen and phosphorus removal equipment ensures that DPB in the system dominates by controlling the process and the operating conditions, can realize synchronous nitrogen and phosphorus removal under the condition of low carbon source, and realizes 'one carbon dual-purpose'; the mixed liquid in the aerobic pool flows back to the anoxic pool and the facultative pool through the air lifter, and the facultative pool can induce the DPB to become a dominant flora to play a role in denitrifying and phosphorus accumulating under the condition of low C/N by controlling oxidation-reduction potential and dissolved oxygen, and strengthens the synchronous nitrification and denitrification; the sludge in the sedimentation tank flows back to the adsorption tank, and organic matters are quickly adsorbed to prevent the sludge from expanding; NO 3-and DO carried in the sludge flow back to the anaerobic tank after denitrification in the anoxic tank, so that NO is eliminated to the maximum extent3 -And DO inhibits DPB and phosphorus accumulating bacteria PAOs, so as to create a 'depression' environment for DPB anaerobic phosphorus release; the alternative anaerobic/anoxic can enrich DPB, and the process equipment has good nitrogen and phosphorus removal effects under the condition of low C/N.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.
FIG. 1 is a schematic plan view of a high-efficiency denitrification and dephosphorization domestic sewage treatment apparatus for enriching denitrifying phosphorus-accumulating bacteria disclosed in the embodiment of the present invention;
3 FIG. 32 3 is 3 a 3 schematic 3 sectional 3 view 3 of 3 an 3 A 3- 3 A 3 of 3 an 3 apparatus 3 for 3 treating 3 domestic 3 sewage 3 with 3 high 3 efficiency 3 denitrification 3 and 3 dephosphorization 3 by 3 enriching 3 denitrifying 3 phosphorus 3- 3 accumulating 3 bacteria 3 disclosed 3 in 3 the 3 embodiment 3 of 3 the 3 present 3 invention 3; 3
FIG. 3 is a schematic sectional view of a B-B of an efficient denitrification and dephosphorization domestic sewage treatment device for enriching denitrifying phosphorus-accumulating bacteria disclosed in the embodiment of the utility model.
The corresponding part names indicated by the numbers and letters in the drawings:
1. a tank body 2, an anaerobic tank 3, an adsorption tank 4, an anoxic tank
5. Facultative tank 6, aerobic tank 7, dissolved oxygen instrument 8, sedimentation tank water inlet channel
9. Sedimentation tank 10, water outlet channel 11, air lifting and pushing device 12 and return channel
13. Sludge scraping and sucking machine 14, sludge return channel 15, water inlet pipe 16 and water outlet pipe
17. Residual sludge pipe 18, air inlet pipe 19, submersible plug flow stirrer 20 and submersible stirrer
21. Reflux pump 22, aerator 23, canal gate 24 and communicating pipe
25. Electric valve 26, stainless steel net 27, oxidation-reduction potentiometer 28 and water distribution hole
29. Flap valve 30, filler 31, water through hole 32 and hydraulic baffle
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative efforts belong to the protection scope of the present invention.
According to fig. 1, fig. 2 and fig. 3, the utility model provides a high-efficient nitrogen and phosphorus removal domestic sewage treatment device of enrichment denitrification phosphorus accumulating fungus, including cell body 1, the top cap is not established to rectangle carbon steel structure, and the channel aspect ratio is 5: 1-10: 1, width-depth ratio of 1: 1-2: 1; the tank body comprises an anaerobic tank 2, an adsorption tank 3, an anoxic tank 4, a facultative tank 5, an aerobic tank 6 and a sedimentation tank 9, water passing holes 31 are arranged among the tanks, and the hydraulic form is plug flow type. The starting end of the anaerobic tank 2 is provided with a water inlet pipe 15 and a submersible plug flow stirrer 19, and the tail end is provided with an oxidation-reduction potentiometer 27; the center of the adsorption tank 3 is provided with a submersible stirrer 20, the stirrer is provided with an upper blade and a lower blade, and one side close to the sedimentation tank 9 is provided with a sludge return hole 31; the starting end of the anoxic pond 4 is provided with a diving plug flow stirrer 19 and an aerobic pond mixed liquid return channel 12, the bottom of the return channel 12 is provided with a communicating pipe 24 leading to the bottom of the anoxic pond 4, the tail end of the anoxic pond 4 is provided with an oxidation-reduction potentiometer 27 and a diving return pump 21, the outlet of the return pump is arranged at the starting end of the anaerobic pond 2, and a flap valve 29 is arranged; the facultative tank is divided into 2 lattices, the beginning end of each lattice is provided with a submersible plug flow stirrer 19, the bottom is provided with an aerator 22, and the tail end of the second lattice is provided with an oxidation-reduction potentiometer 27 and a dissolved oxygen instrument 7; the aerobic pool 6 is divided into 2 grids, the bottom of each grid is provided with an aerator 22, moving bed filler 30 is arranged in the pool, the tail end of the pool is provided with a dissolved oxygen instrument 7 and an air lifter 11, mixed liquid passes through the air lifter 11 to a return channel 12, and a stainless steel mesh is arranged between the air lifter and the aerobic pool 6 to prevent the moving bed filler 30 from entering the air lifter; a channel gate 23 is arranged on the mixed liquid return channel 12 leading to the facultative tank 5 and the anoxic tank 4 and is used for adjusting the return flow; the sedimentation tank 9 adopts the form of water inlet from the long edge of the outer side and water outlet from the long edge, a water distribution hole 28 is arranged below the water inlet channel 8, a hydraulic baffle plate 32 is arranged below the water distribution hole 28, sludge is discharged into the sludge return channel 14 through the travelling type sludge scraping and sucking machine 13, returned sludge enters the adsorption tank 3 through a water through hole 31 on the adsorption tank 3, and residual sludge is discharged through a sludge discharge pipe 17 at the tail end of the returned sludge channel 14. The water inlet pipe 15, the water outlet pipe 16, the air inlet pipe 18 and the sludge discharge pipe 17 are respectively provided with an electric valve 25.
The utility model discloses concrete operating procedure does:
1. a starting stage: opening a water inlet valve, injecting domestic sewage, inoculating residual sludge of a domestic sewage plant to the equipment for circulating operation, adding methanol, ammonium nitrate and potassium dihydrogen phosphate, adjusting the concentration of C to N to be (4-5): 1 and the concentration of C to P to be (17-20): 1, so that the concentration of the sludge in the equipment reaches 2000-3000 mg/L, monitoring a water outlet of the equipment, and when the TN removal rate is more than 70 percent and the TP removal rate is more than 50 percent, successfully starting the equipment;
2. and (3) a stabilization stage: continuously feeding water, and regulating and controlling the reflux amount of mixed liquid in the aerobic pool and the aeration time of the facultative pool to control the ORP of the anaerobic pool to be-450 mV to-250 mV, the ORP of the anoxic pool to be-150 mV to 0mV, the ORP of the facultative pool to be-100 mV to 50mV, DO of the facultative pool to be less than 0.6mg/L, and DO of the aerobic pool to be 1.5-2.5 mg/L. Regulating and controlling the return flow of the excess sludge to be changed between 50 and 100 percent, and monitoring the concentration of the pollutants at the water outlet until TP is less than or equal to 0.5mg/L, TN and less than or equal to 10mg/L, NH4 +When the concentration is less than or equal to 3 mg/L;
3. after the debugging, the equipment achieves the stable operation, and the aeration time of the facultative tank and the reflux amount of the mixed liquid are controlled according to the set PLC. The control mode of facultative tank aeration is as follows: when water is discharged NH4 +When the concentration is less than or equal to 3mg/L, aeration is started under the following three conditions: firstly, when DO of an aerobic pool is less than 1.5mg/L, when ORP of a facultative pool is less than-100 mV, and when OPR of an anoxic pool is less than-150 mV; when water is discharged NH4 +When the concentration is more than 3mg/L, the facultative tank is aerated until NH is discharged4 +Less than or equal to 3 mg/L. When water is discharged NH4 +When the concentration is less than or equal to 3mg/L, the aeration is closed under the following two conditions: firstly, when DO in the facultative tank is more than 0.6mg/L, ORP in the facultative tank is more than 50 mV;
when the OPR of the anoxic pond is less than-150 mV, the return flow to the anoxic pond is properly increased by increasing the opening of the canal gate; when the ORP of the facultative tank is less than-100 mV, properly increasing the reflux amount of the facultative tank by increasing the opening of the canal gate; when the OPR of the anoxic pond is more than 0mV, the return flow to the anoxic pond is properly reduced by reducing the opening of the canal gate; when the ORP of the facultative tank is more than 50mV, the return flow to the facultative tank is appropriately reduced by reducing the opening of the channel gate.
Through the above-mentioned specific embodiment, the beneficial effects of the utility model are that: this novel an organic wholeThe integration degree is high, and the nitrogen and phosphorus removal effect is good under the condition of low C/N; the nitrogen and phosphorus removal equipment ensures that DPB in the system dominates by controlling the process and the operating conditions, can realize synchronous nitrogen and phosphorus removal under the condition of low carbon source, and realizes 'one carbon dual-purpose'; the mixed liquid in the aerobic pool flows back to the anoxic pool and the facultative pool through the air lifter, and the facultative pool can induce the DPB to become a dominant flora to play a role in denitrifying and phosphorus accumulating under the condition of low C/N through controlling the oxidation-reduction potential and strengthen the synchronous nitrification and denitrification; the sludge in the sedimentation tank flows back to the adsorption tank, and organic matters are quickly adsorbed to prevent the sludge from expanding; NO carried in sludge3 -The wastewater flows back to the anaerobic tank after being subjected to denitrification in the anoxic tank, so that the inhibition of NO 3-and DO on DPB and phosphorus accumulating bacteria PAOs is eliminated to the maximum extent, and a 'depression' environment is created for the anaerobic phosphorus release of the DPB; the alternative anaerobic/anoxic can enrich DPB, and the process equipment has good nitrogen and phosphorus removal effects under the condition of low C/N.
The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the invention. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (5)
1. An efficient denitrification and dephosphorization domestic sewage treatment device for enriching denitrification phosphorus-accumulating bacteria, which is called denitrification and dephosphorization device for short; it is characterized by comprising a tank body, an anaerobic tank, an adsorption tank, an anoxic tank, a facultative tank, an aerobic tank and a sedimentation tank; the nitrogen and phosphorus removal equipment is of a rectangular carbon steel structure, and the tank body is integrally assembled by a plurality of open channels without top covers; the aspect ratio of the channel of the nitrogen and phosphorus removal equipment is 5: 1-10: 1, and the width-depth ratio is 1: 1-2: 1; a sedimentation tank is arranged on the left side of the tank body, a facultative tank is arranged on the right side of the tank body, an anaerobic tank and an anoxic tank are arranged in parallel on the lower middle part, and an aerobic tank is arranged in parallel on the upper middle part; an adsorption tank is arranged above the anaerobic tank; backflow channels are arranged on the left side and the periphery of the upper part of the inner side of the tank body; a water outlet channel is arranged on the right side of the inner side of the tank body; the upper part and the left side of the outer side of the tank body are respectively provided with two groups of air inlet pipes, and the lower part of the outer side of the tank body is respectively provided with a water inlet pipe, a water outlet pipe and a residual sludge pipe; an air ejector is arranged at the upper left corner in the tank body;
water through holes are formed among the anaerobic tank, the adsorption tank, the anoxic tank, the facultative tank, the aerobic tank and the sedimentation tank, and the hydraulic form is plug flow type; the starting end of the anaerobic tank is provided with a water inlet pipe and a submersible plug flow stirrer, and the tail end of the anaerobic tank is provided with an oxidation-reduction potentiometer; a submersible stirrer is arranged in the center of the adsorption tank, the submersible stirrer is provided with an upper group of blades and a lower group of blades, and a water passing hole arranged on one side of the adsorption tank, which is close to the sedimentation tank, is used as a sludge return hole; the starting end of the facultative tank is provided with a submersible plug flow stirrer, and the starting end of the facultative tank is communicated with the return channel of the mixed liquid in the aerobic tank through a water through hole; a pipeline leading to the bottom of the anoxic tank is arranged at the bottom of the backflow channel, an ORP (oxidation-reduction potential) instrument and a submersible backflow pump are arranged at the tail end of the backflow channel, and an outlet of the backflow pump is positioned at the starting end of the anaerobic tank and is provided with a flap valve; the facultative tank is respectively provided with two grids which are arranged in series front and back, the starting end of each grid is provided with a submersible plug flow stirrer, the bottom of each grid is provided with an aerator, and the tail end of the second grid of the facultative tank is provided with an ORP (oxidation-reduction potential) instrument and a dissolved oxygen instrument; the aerobic tank is divided into two grids which are arranged in parallel and in series, an aerator is arranged at the bottom of each grid, moving bed fillers are filled in the aerobic tank, a DO instrument and an air lifter are arranged at the tail end of the second grid of the aerobic tank, and the mixed liquor in the aerobic tank flows to a return channel through the air lifter; a stainless steel mesh is arranged between the air lifter and the aerobic tank, and the stainless steel mesh prevents the moving bed filler from entering the area of the air lifter; a channel gate is arranged on a return channel of the mixed liquid which is led to the facultative tank and the anoxic tank, and the channel gate adjusts the return flow; the sedimentation tank adopts the form of outside long-edge water inlet and long-edge water outlet, a water distribution hole is arranged below the water inlet channel of the sedimentation tank, a hydraulic baffle is arranged below the water distribution hole, and sludge in the sedimentation tank is scraped and sucked through a traveling vehicleThe mud machine is discharged into a mud return channel, returned mud enters the adsorption tank through a mud return hole on the adsorption tank, and excess mud is discharged through an excess mud pipe at the tail end of the channel; the whole process is controlled by three ORP instruments and two DO instruments, and the total effluent quality index NH4 +＜3mg/L，TN＜10mg/L，TP＜0.5mg/L。
2. The apparatus of claim 1, wherein the hydraulic retention time of the anaerobic tank, the adsorption tank, the anoxic tank, the facultative tank, the aerobic tank and the sedimentation tank is 1.5h, 0.3h, 2h, 6h and 2h respectively.
3. The apparatus of claim 1, wherein the sedimentation tank has a surface load of 0.8m3/㎡·h—1.2m3/㎡·h。
4. The apparatus for high-efficiency denitrification and dephosphorization domestic sewage treatment equipment of claim 1, wherein the ORP control range of the anaerobic tank is-450 mV to-250 mV; the ORP control range of the anoxic tank is-150 mV to 0 mV; the ORP control range of the facultative tank is-100 mV to 50mV, and the DO control range of the facultative tank is less than 0.6 mg/L; the DO control range of the aerobic tank is 1.5 mg/L-2.5 mg/L.
5. The apparatus for high efficiency denitrification and dephosphorization wastewater treatment based on the enrichment of denitrifying phosphorus accumulating bacteria as claimed in claim 1, wherein the submerged agitator in the adsorption tank adopts a low speed agitator, and the agitation speed is 40r/min to 60 r/min; the unit power of the submersible plug flow stirrer in the anaerobic tank, the anoxic tank and the facultative tank is 2W/m3—4W/m3(wastewater).
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111499005A (en) * | 2020-04-22 | 2020-08-07 | 江苏博尔清源环境技术有限公司 | A high-efficiency denitrification and phosphorus removal domestic sewage treatment equipment for enriching denitrifying phosphorus accumulating bacteria |
| CN115367877A (en) * | 2022-08-24 | 2022-11-22 | 上海禾元环保集团有限公司 | Continuous circulating flow biological nitrogen and phosphorus removal reactor and method |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111499005A (en) * | 2020-04-22 | 2020-08-07 | 江苏博尔清源环境技术有限公司 | A high-efficiency denitrification and phosphorus removal domestic sewage treatment equipment for enriching denitrifying phosphorus accumulating bacteria |
| CN115367877A (en) * | 2022-08-24 | 2022-11-22 | 上海禾元环保集团有限公司 | Continuous circulating flow biological nitrogen and phosphorus removal reactor and method |
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