CN114426332B - Method for rapidly starting SBR system to realize denitrification and dephosphorization - Google Patents
Method for rapidly starting SBR system to realize denitrification and dephosphorization Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 87
- 238000006243 chemical reaction Methods 0.000 claims abstract description 86
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 80
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 79
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims abstract description 77
- 229910052698 phosphorus Inorganic materials 0.000 claims abstract description 75
- 239000011574 phosphorus Substances 0.000 claims abstract description 75
- 241000894006 Bacteria Species 0.000 claims abstract description 50
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 40
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims abstract description 26
- 239000010802 sludge Substances 0.000 claims abstract description 24
- 239000002351 wastewater Substances 0.000 claims abstract description 24
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 23
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 23
- 239000001301 oxygen Substances 0.000 claims abstract description 23
- 230000001546 nitrifying effect Effects 0.000 claims abstract description 21
- DCXYFEDJOCDNAF-UHFFFAOYSA-N Asparagine Natural products OC(=O)C(N)CC(N)=O DCXYFEDJOCDNAF-UHFFFAOYSA-N 0.000 claims abstract description 14
- DCXYFEDJOCDNAF-REOHCLBHSA-N L-asparagine Chemical compound OC(=O)[C@@H](N)CC(N)=O DCXYFEDJOCDNAF-REOHCLBHSA-N 0.000 claims abstract description 14
- 229960001230 asparagine Drugs 0.000 claims abstract description 14
- 235000009582 asparagine Nutrition 0.000 claims abstract description 14
- 150000002148 esters Chemical class 0.000 claims abstract description 13
- 125000001453 quaternary ammonium group Chemical group 0.000 claims abstract description 13
- 239000000126 substance Substances 0.000 claims abstract description 12
- 238000005273 aeration Methods 0.000 claims description 61
- 238000003756 stirring Methods 0.000 claims description 48
- 238000004062 sedimentation Methods 0.000 claims description 12
- 238000013019 agitation Methods 0.000 claims description 11
- YHHSONZFOIEMCP-UHFFFAOYSA-O phosphocholine Chemical compound C[N+](C)(C)CCOP(O)(O)=O YHHSONZFOIEMCP-UHFFFAOYSA-O 0.000 claims description 10
- 229950004354 phosphorylcholine Drugs 0.000 claims description 10
- 239000010865 sewage Substances 0.000 claims description 10
- -1 trehalose ester Chemical class 0.000 claims description 9
- KWIUHFFTVRNATP-UHFFFAOYSA-N Betaine Natural products C[N+](C)(C)CC([O-])=O KWIUHFFTVRNATP-UHFFFAOYSA-N 0.000 claims description 5
- KWIUHFFTVRNATP-UHFFFAOYSA-O N,N,N-trimethylglycinium Chemical compound C[N+](C)(C)CC(O)=O KWIUHFFTVRNATP-UHFFFAOYSA-O 0.000 claims description 5
- 229960003237 betaine Drugs 0.000 claims description 5
- HDTRYLNUVZCQOY-UHFFFAOYSA-N α-D-glucopyranosyl-α-D-glucopyranoside Natural products OC1C(O)C(O)C(CO)OC1OC1C(O)C(O)C(O)C(CO)O1 HDTRYLNUVZCQOY-UHFFFAOYSA-N 0.000 claims description 4
- HDTRYLNUVZCQOY-WSWWMNSNSA-N Trehalose Natural products O[C@@H]1[C@@H](O)[C@@H](O)[C@@H](CO)O[C@@H]1O[C@@H]1[C@H](O)[C@@H](O)[C@@H](O)[C@@H](CO)O1 HDTRYLNUVZCQOY-WSWWMNSNSA-N 0.000 claims description 4
- WGTYBPLFGIVFAS-UHFFFAOYSA-M tetramethylammonium hydroxide Chemical compound [OH-].C[N+](C)(C)C WGTYBPLFGIVFAS-UHFFFAOYSA-M 0.000 claims description 4
- 238000011081 inoculation Methods 0.000 claims description 3
- 238000004904 shortening Methods 0.000 claims description 3
- ZTOKUMPYMPKCFX-CZNUEWPDSA-N (E)-17-[(2R,3R,4S,5S,6R)-6-(acetyloxymethyl)-3-[(2S,3R,4S,5S,6R)-6-(acetyloxymethyl)-3,4,5-trihydroxyoxan-2-yl]oxy-4,5-dihydroxyoxan-2-yl]oxyoctadec-9-enoic acid Chemical compound OC(=O)CCCCCCC/C=C/CCCCCCC(C)O[C@@H]1O[C@H](COC(C)=O)[C@@H](O)[C@H](O)[C@H]1O[C@H]1[C@H](O)[C@@H](O)[C@H](O)[C@@H](COC(C)=O)O1 ZTOKUMPYMPKCFX-CZNUEWPDSA-N 0.000 claims description 2
- 229930006000 Sucrose Natural products 0.000 claims description 2
- 239000005720 sucrose Substances 0.000 claims description 2
- 230000035484 reaction time Effects 0.000 claims 1
- 230000000694 effects Effects 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- 244000005700 microbiome Species 0.000 description 4
- SHZGCJCMOBCMKK-UHFFFAOYSA-N D-mannomethylose Natural products CC1OC(O)C(O)C(O)C1O SHZGCJCMOBCMKK-UHFFFAOYSA-N 0.000 description 3
- PNNNRSAQSRJVSB-UHFFFAOYSA-N L-rhamnose Natural products CC(O)C(O)C(O)C(O)C=O PNNNRSAQSRJVSB-UHFFFAOYSA-N 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 238000012258 culturing Methods 0.000 description 3
- 239000011521 glass Substances 0.000 description 3
- 230000001105 regulatory effect Effects 0.000 description 3
- 229910002651 NO3 Inorganic materials 0.000 description 2
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 2
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 238000002798 spectrophotometry method Methods 0.000 description 2
- 230000001360 synchronised effect Effects 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 1
- 108090000913 Nitrate Reductases Proteins 0.000 description 1
- 229910019142 PO4 Inorganic materials 0.000 description 1
- 241000589651 Zoogloea Species 0.000 description 1
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 description 1
- APUPEJJSWDHEBO-UHFFFAOYSA-P ammonium molybdate Chemical compound [NH4+].[NH4+].[O-][Mo]([O-])(=O)=O APUPEJJSWDHEBO-UHFFFAOYSA-P 0.000 description 1
- 229940010552 ammonium molybdate Drugs 0.000 description 1
- 235000018660 ammonium molybdate Nutrition 0.000 description 1
- 239000011609 ammonium molybdate Substances 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 230000001651 autotrophic effect Effects 0.000 description 1
- 230000001580 bacterial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000029087 digestion Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 150000004676 glycans Chemical class 0.000 description 1
- 230000003834 intracellular effect Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000002068 microbial inoculum Substances 0.000 description 1
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 1
- 239000010452 phosphate Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 229920002627 poly(phosphazenes) Polymers 0.000 description 1
- USHAGKDGDHPEEY-UHFFFAOYSA-L potassium persulfate Chemical compound [K+].[K+].[O-]S(=O)(=O)OOS([O-])(=O)=O USHAGKDGDHPEEY-UHFFFAOYSA-L 0.000 description 1
- 230000035755 proliferation Effects 0.000 description 1
- 238000012163 sequencing technique Methods 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 238000004448 titration Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/301—Aerobic and anaerobic treatment in the same reactor
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/308—Biological phosphorus removal
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2203/00—Apparatus and plants for the biological treatment of water, waste water or sewage
- C02F2203/004—Apparatus and plants for the biological treatment of water, waste water or sewage comprising a selector reactor for promoting floc-forming or other bacteria
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/14—NH3-N
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/16—Total nitrogen (tkN-N)
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/22—O2
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
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- Biodiversity & Conservation Biology (AREA)
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- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Molecular Biology (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The invention discloses a method for rapidly starting an SBR system to realize denitrification and dephosphorization. The method comprises the following steps: s1: inoculating activated sludge, S2: setting an operation period, and adopting an operation mode of gradually increasing the water inlet volume load in the starting process; s3: the method comprises the steps that nitrogen and phosphorus-containing wastewater to be treated enters an SBR reactor to start a starting process, wherein asparagine is added into the wastewater in an aerobic reaction stage, sugar ester substances are added into the wastewater in an anoxic reaction stage, and quaternary ammonium base is added after dissolved oxygen is reduced to be less than 0.1 mg/L; s4: and completing the starting process of the SBR system until the water inlet volume load reaches the designed water inlet volume load, the ammonia nitrogen removal rate reaches more than 90%, and the total nitrogen and total phosphorus removal rates reach more than 85%. The method can realize the rapid enrichment culture of nitrifying bacteria and denitrifying phosphorus accumulating bacteria in a short time, and further rapidly start the denitrification and dephosphorization functions of the SBR system.
Description
Technical Field
The invention belongs to the technical field of biological wastewater treatment, and particularly relates to a method for rapidly starting an SBR system to realize denitrification and dephosphorization.
Background
SBR (sequencing batch reactor activated sludge process) is a biological denitrification and dephosphorization process with wide application, carbon, nitrogen and phosphorus pollutants in sewage can be removed in the same reactor, and nitrifying bacteria, denitrifying bacteria, phosphorus accumulating bacteria and the like with different functions are required to play respective roles under different conditions. Wherein nitrifying bacteria belong to aerobic autotrophic microorganisms, grow slowly and have long generation time, and are not easy to culture quickly; denitrifying bacteria are mostly heterotrophic facultative bacteria that convert nitrate and/or nitrite to nitrogen; the phosphorus accumulating bacteria are heterotrophic microorganisms, phosphorus in sewage is sucked into bacteria mainly by virtue of the fact that the aerobic phosphorus uptake amount is larger than the anaerobic phosphorus release amount during growth and proliferation, phosphorus removal is achieved by discharging surplus sludge, the quantity of nitrifying bacteria is reduced while sludge is discharged, and the nitrification effect is poor, so that the risk that ammonia nitrogen in effluent does not reach standards exists while phosphorus removal, and competition for carbon sources exists between denitrifying bacteria and phosphorus accumulating bacteria, so that the denitrification and phosphorus removal effect is not ideal.
With the continuous and intensive research on sewage treatment, novel denitrification and dephosphorization processes and related microorganisms are developed and applied. In particular, the denitrification dephosphorization process ensures that two independent processes of dephosphorization and denitrification can be completed simultaneously only in an anoxic environment under the participation of denitrification dephosphorization bacteria (DPB), the combination of the phosphorus absorption and denitrification processes not only saves the requirement on a carbon source, but also can save the energy source required by aeration when the phosphorus absorption is completed in the anoxic environment, and greatly reduces the amount of residual sludge.
CN200810105508. X discloses a method for rapidly starting a continuous flow double sludge denitrification dephosphorization process by using SBR. The method comprises the steps of firstly intermittently and independently culturing denitrification phosphorus accumulating sludge and a biological film in a nitrifying pond in two reactors, and then placing the denitrification phosphorus accumulating sludge and the aerobic nitrifying biological film into a continuous flow double-sludge system; wherein the culture of the denitrification phosphorus accumulating sludge is sequentially carried out in two stages in the SBR reactor, the aerobic phosphorus accumulating bacteria are cultured in the 1 st stage, and the denitrification phosphorus accumulating bacteria are cultured in the 2 nd stage. CN201310509936.2 discloses a rapid start-up method of SBR for synchronous denitrification and dephosphorization, which uses batch reactors with intermittent water inflow arranged in time sequence, and comprises the following steps: (1) Operating the SBR system under anaerobic/aerobic alternate conditions, domesticating phosphorus-enriched bacteria, making the phosphorus-enriched bacteria aerobically absorb phosphorus, anaerobically releasing phosphorus, and removing phosphate in water by sludge discharge; (2) And (3) changing the operation mode of the system, and enriching the denitrifying phosphorus accumulating bacteria. The anoxic section is increased, the aeration time is shortened, and denitrifying phosphorus accumulating bacteria utilize an intracellular carbon source and take nitrate nitrogen/nitrite nitrogen as an electron acceptor to absorb phosphorus; (3) The composite microbial inoculum is added into the reactor, so that the bio-enhancement and the anaerobic/aerobic/anoxic/aerobic are repeatedly coupled, DPB is effectively proliferated, glycan bacteria are restrained, the starting time of the reactor is shortened, the water outlet effect is improved, the starting mode is operated for about 50d, and compared with the anaerobic/aerobic/anoxic starting method, the aeration time is saved by about 30 percent. In the prior art, the system is regulated and controlled in the aspect of technology, and quick start is difficult to realize through regulating and controlling parameters due to the difference between microorganisms, particularly in the starting process.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides a method for rapidly starting an SBR system to realize denitrification and dephosphorization. The method can realize the rapid enrichment culture of nitrifying bacteria and denitrifying phosphorus accumulating bacteria in a short time, and further rapidly start the denitrification and dephosphorization functions of the SBR system.
The invention provides a method for rapidly starting an SBR system to realize denitrification and dephosphorization, which comprises the following steps:
s1: inoculating activated sludge containing nitrifying bacteria and denitrifying phosphorus accumulating bacteria into an SBR reactor,
s2: setting an operation period in the starting process of the SBR system, wherein each period operates according to the time sequence of water inlet and reaction-sedimentation-drainage-idling, and the reaction is divided into an aerobic reaction and an anoxic reaction, and the two reactions alternately operate; an operation mode of gradually increasing the water inlet volume load is adopted in the starting process;
s3: the method comprises the steps that nitrogen and phosphorus-containing wastewater to be treated enters an SBR reactor to start a starting process, wherein asparagine is added into the wastewater in an aerobic reaction stage, sugar ester substances are added into the wastewater in an anoxic reaction stage, and quaternary ammonium base is added after dissolved oxygen is reduced to be less than 0.1 mg/L;
s4: and completing the starting process of the SBR system until the water inlet volume load reaches the designed water inlet volume load, the ammonia nitrogen removal rate reaches more than 90%, and the total nitrogen and total phosphorus removal rates reach more than 85%.
In the technical scheme, in the step S1, the activated sludge containing nitrifying bacteria and denitrifying phosphorus accumulating bacteria can be obtained from the residual activated sludge in a secondary sedimentation tank of a sewage treatment plant for treating nitrogen and phosphorus, and the inoculation amount is 2000-5000mg/L. Under general conditions, the residual activated sludge can be adapted to the wastewater to be treated through domestication, and the removal rate of nitrogen and phosphorus in the initial inoculation stage is less than 50%.
In the above technical scheme, the wastewater containing nitrogen and phosphorus to be treated can be derived from wastewater polluted by nitrogen and phosphorus in industry and life. In the nitrogen and phosphorus containing wastewater, the ammonia nitrogen concentration is 100-300mg/L, the total nitrogen concentration is 100-400mg/L, the COD concentration is 300-600mg/L, and the total phosphorus concentration is 5-20mg/L.
In the above technical scheme, in step S2, the operation period in the starting process of the SBR system may be set by a method commonly used in the art, and the period may be 6 to 24 hours, and each period may be operated according to the time sequence of water inlet and reaction-sedimentation-drainage-idling, where the reaction period may be more than 50% and may be 60 to 80%. The water inlet and the reaction can be carried out after the water is ended, and the reaction can be started at the same time of water inlet.
In the above technical scheme, in step S2, the aerobic reaction and the anoxic reaction alternately run, where the aerobic reaction may be performed in an aeration mode, and the anoxic reaction may be performed in a non-aeration and only stirring mode. In practice, the first start-up may be an aerobic reaction or an anoxic reaction, and the present invention is not particularly limited. For example, it may be a first aeration-first agitation, a first agitation-first aeration-second agitation, a first aeration-first agitation-second aeration-second agitation, or a first agitation-first aeration-second agitation-second aeration, or the like.
In the above technical solution, in step S2, the initial intake volume load is 50% or less of the designed intake volume load, and may be 10% -50%. When the total nitrogen and total phosphorus removal rate of the inlet water reaches more than 60%, preferably 70% -80%, the next inlet water volume load is increased by 10-20% each time (the volume fraction of the next inlet water volume load to the designed inlet water volume load is increased compared with the volume fraction of the next inlet water volume load to the designed inlet water volume load).
In the above technical scheme, in step S2, the ratio of the aerobic aeration time to the anoxic stirring time in the first operation period is 10:1-3:1. Preferably, an operation mode of gradually shortening the aerobic aeration time and correspondingly increasing the anoxic stirring time is adopted. When the ammonia nitrogen removal rate of the inflowing water reaches more than 70%, preferably 80% -90%, the aerobic aeration time in the next operation period is shortened, and the anoxic stirring time is correspondingly increased (namely, the shortened aerobic aeration time is used for increasing the anoxic stirring time), and the time of each change is 3% -15% of the aerobic aeration time in the current operation period. In the invention, the first aerobic aeration time in the next operation period can be shortened, and the first anoxic stirring time can be increased. The ratio of aerobic aeration time to anoxic agitation time in the last operating cycle at the end of the start-up process is generally 10:1 to 1:1, preferably 5:1 to 2:1.
In the above technical solution, asparagine is added to the wastewater in the aerobic reaction stage, preferably in the first aerobic reaction stage. Sugar esters are added into the wastewater in the anoxic reaction stage firstly, and after the dissolved oxygen is reduced to less than 0.1mg/L, quaternary ammonium base is added, preferably sugar esters are added into the wastewater in the first anoxic reaction stage firstly, and after the dissolved oxygen is reduced to less than 0.1mg/L, quaternary ammonium base is added.
In the above technical scheme, the dosage of the asparagine is 0.001-1.0mg/L, preferably 0.01-0.10mg/L.
In the above technical scheme, the sugar ester substance comprises at least one of mouse Li Tangzhi, trehalose ester, sophorolipid, sucrose ester and the like, preferably rhamnose ester. The quaternary ammonium base is at least one of phosphorylcholine, betaine, tetramethylammonium hydroxide and the like, and preferably phosphorylcholine. The sugar esters are used in an amount of 0.001-1.0mg/L, preferably 0.01-0.10mg/L. The amount of the quaternary ammonium base is 0.001-1.0mg/L, preferably 0.01-0.10mg/L.
In the technical scheme, the operation conditions of the SBR reactor are as follows: the dissolved oxygen is controlled to be 0.5-5.0mg/L (preferably 1.0-5.0 mg/L) during aeration reaction, 0-1.0mg/L (preferably 0-0.5 mg/L) during stirring reaction, the pH value of the whole reaction stage is 6-9, and the temperature is 25-40 ℃.
In the above technical solution, the SBR system may include a plurality of SBR reactors so that wastewater continuously enters the SBR system.
The method of the invention has the following advantages:
(1) In the nitrifying bacteria culturing process, asparagine can accelerate zoogloea formation, provide carriers for nitrifying bacteria enrichment, reduce nitrifying bacteria loss and improve ammonia nitrogen removal effect. Meanwhile, the competition of phosphorus accumulating bacteria and nitrifying bacteria to dissolved oxygen can be reduced, and the aerobic phosphorus absorbing capacity of the phosphorus accumulating bacteria is improved.
(2) In the process of culturing denitrifying phosphorus accumulating bacteria, sugar ester substances and quaternary ammonium base are added in a step-by-step mode, so that the activity of nitrate reductase can be improved, the utilization of the electron acceptor of nitrate by denitrifying bacteria is enhanced, and simultaneous denitrification and excessive phosphorus uptake are realized.
(3) Specific substances are added according to different culture stages, so that the synergistic growth of multiple bacterial groups can be promoted, and the common enrichment of nitrifying bacteria and denitrifying phosphorus accumulating bacteria is realized.
(4) According to the invention, through adopting an operation mode of gradually increasing the water inlet volume load, preferably gradually shortening the aerobic aeration time and correspondingly increasing the anoxic stirring time, nitrifying bacteria which are difficult to culture can be cultured first, and then denitrifying bacteria and dephosphorizing bacteria are cultured, so that synchronous removal of total nitrogen and total phosphorus is realized rapidly.
Detailed Description
The technical scheme of the invention is further described in detail below with reference to examples. The embodiments and specific operation procedures are given on the premise of the technical scheme of the invention, but the protection scope of the invention is not limited to the following embodiments.
The experimental methods in the following examples, unless otherwise specified, are all conventional in the art. The experimental materials used in the examples described below were purchased from biochemical reagent stores unless otherwise specified.
In the method, the COD concentration is measured by GB11914-89 'determination of water quality chemical oxygen demand-dichromate method'; the ammonia nitrogen concentration is measured by using GB7478-87 method for measuring ammonium in water-distillation and titration, the total nitrogen concentration adopts GB 11894-89 water quality-total nitrogen determination-alkaline potassium persulfate digestion ultraviolet spectrophotometry, and the total phosphorus concentration adopts GB11893-89 ammonium molybdate spectrophotometry. The relative abundance at the nitrifying and denitrifying polyphosphazenes levels can be determined using high throughput sequencer analysis.
Example 1
A set of SBR system is built in a laboratory, and comprises 3 organic glass reactors with effective volumes of 5L, wherein the concentration of ammonia nitrogen is 200mg/L, the concentration of total nitrogen is 230mg/L, the concentration of COD is 500mg/L, and the concentration of total phosphorus is 15 mg/L.
Firstly, inoculating residual activated sludge containing nitrifying bacteria and denitrifying phosphorus accumulating bacteria in a secondary sedimentation tank of a sewage field according to the sludge concentration of 3000mg/L, and setting an operation period of each reactor to be 8 hours, wherein water is fed and the reaction is carried out at the same time. The single SBR reactor is carried out according to the procedures of first aeration reaction, first stirring reaction, second aeration reaction, sedimentation and drainage. Each run cycle was performed by adding asparagine at 0.01mg/L at the initial stage of the first aeration reaction, adding mouse Li Tangzhi at 0.01mg/L at the first agitation reaction stage, and adding phosphorylcholine at 0.10mg/L when the dissolved oxygen was reduced to less than 0.1 mg/L.
The initial water inlet volume load is 30% of the designed water inlet volume load, and the first operation period is operated according to the first aeration reaction (240 min), the first stirring reaction (30 min), the second aeration reaction (60 min), the sedimentation (60 min) and the drainage (90 min). When the ammonia nitrogen removal rate of the inflow water reaches more than 80%, the first aeration time in the next operation period is shortened by 30min, and the first anoxic stirring time is increased by 30min. When the total nitrogen and total phosphorus removal rate of the inlet water reaches more than 70%, the inlet water volume load of the next operation period is increased by 10 percent.
The operating conditions of the SBR reactor were: the dissolved oxygen is controlled at 2.5mg/L during aeration reaction, the dissolved oxygen is less than 0.5mg/L during stirring reaction, the pH value of the whole reaction stage is 7.5-7.8, and the temperature is 32 ℃.
The aeration time and the stirring time are gradually adjusted by the control method, the load is gradually increased until the water inlet volume load reaches the designed water inlet volume load, the starting process of the SBR system is completed, the ratio of the aeration time to the stirring time in the last operation period is 3:1, the ammonia nitrogen removal rate of the water inlet reaches 95.3%, and the total nitrogen removal rate and the total phosphorus removal rate reach 87.5% and 88.1%, respectively, and the starting period is 40 days.
Comparative example 1
In comparison with example 1, the difference is that: in each operation cycle, phosphorylcholine is added according to 0.01mg/L in the initial stage of the first aeration reaction, asparagine is firstly added according to 0.01mg/L in the first stirring reaction stage, and rhamnose ester is added according to 0.10mg/L when dissolved oxygen is reduced to less than 0.1 mg/L.
When the system is started for 40 days, the ratio of aeration time to stirring time in the last operation period is 4:1, the ammonia nitrogen removal rate of the inlet water is 92.2%, the total nitrogen removal rate is 77.3%, the total phosphorus removal rate is 75.9%, the inlet water volume load is 70%, and the rapid start of the system is not realized.
Comparative example 2
In comparison with example 1, the difference is that: during the anoxic stirring phase, while rhamnose ester is added, phosphorylcholine is added.
When the system is started for 40 days, the ratio of aeration time to stirring time in the last operation period is 3:1, the ammonia nitrogen removal rate of the inlet water is 91.3%, the total nitrogen removal rate is 85.5%, the total phosphorus removal rate is 78.1%, the inlet water volume load is 80%, and the rapid starting of the system is not realized.
Comparative example 3
Compared to example 1, the difference was that no mouse Li Tangzhi and no phosphorylcholine were added during the anoxic agitation phase.
When the system is started for 40 days, the ratio of aeration time to stirring time in the last operation period is 3:1, the ammonia nitrogen removal rate of the inlet water is 92.7%, the total nitrogen removal rate is 74.5%, the total phosphorus removal rate is 75.3%, the inlet water volume load is 60%, and the rapid starting of the system is not realized.
Example 2
The reactor and start-up procedure and conditions were the same as in example 1, except that: in the stirring reaction stage, betaine is added to replace the equal mass of phosphorylcholine according to the concentration of 0.1mg/L after the dissolved oxygen is reduced to less than 0.1 mg/L.
After the SBR system is started, the ratio of the aeration time to the stirring time in the last operation period is 3:1, and when the ammonia nitrogen removal rate of the inlet water reaches 94.4 percent and the total nitrogen and total phosphorus removal rates reach 85.1 percent and 86.2 percent respectively, the starting period is 42 days.
Example 3
The reactor and start-up procedure and conditions were the same as in example 1, except that: in the stirring reaction stage, trehalose ester is used for replacing equal mass of mouse Li Tangzhi, and betaine is used for replacing equal mass of phosphorylcholine.
After the start of the SBR system is completed, the ratio of the aeration time to the stirring time in the last operation period is 3:1, and when the ammonia nitrogen removal rate of the inlet water reaches 94.1%, and the total nitrogen removal rate and the total phosphorus removal rate reach 84.8% and 85.3% respectively, the start period is 43 days.
Example 4
A set of SBR system is built in a laboratory, and comprises 2 organic glass reactors with effective volumes of 5L, and is used for treating sewage with ammonia nitrogen concentration of 260mg/L, total nitrogen concentration of 290mg/L, COD concentration of 600mg/L and total phosphorus concentration of 18 mg/L.
Firstly, inoculating residual activated sludge containing nitrifying bacteria and denitrifying phosphorus accumulating bacteria of a secondary sedimentation tank of a sewage field according to the sludge concentration of 4000mg/L, and setting an operation period of each reactor to be 12 hours, wherein the reaction is started while water is fed. The single SBR reactor is carried out according to the procedures of first aeration reaction, first stirring reaction, second aeration reaction, second stirring reaction, sedimentation and drainage. Asparagine was added at 0.1mg/L in the first aeration reaction stage, and mouse Li Tangzhi was added at 0.01mg/L in the first agitation reaction stage, and betaine was added at 0.01mg/L when the dissolved oxygen was reduced to less than 0.1 mg/L.
The initial water inlet volume load is 20% of the designed water inlet volume load, and the water inlet volume load is operated according to the first aeration reaction (360 min), the first stirring reaction (60 min), the second aeration reaction (90 min), the second stirring reaction (30 min), the sedimentation (60 min) and the drainage (120 min) in the first operation period. When the ammonia nitrogen removal rate of the inflow water reaches more than 80%, the first aeration time in the next operation period is shortened by 30min, and the first stirring time is increased by 30min. When the total nitrogen and total phosphorus removal rate of the inlet water reaches more than 70%, the inlet water volume load of the next operation period is increased by 20 percent.
The operating conditions of the SBR reactor were: the dissolved oxygen is controlled at 4.5mg/L in aeration reaction, the dissolved oxygen is less than 0.5mg/L in stirring reaction, the pH value in the whole reaction stage is 7.8-8.0, and the temperature is 35 ℃.
The aeration time and the stirring time are gradually adjusted by the control method, the load is gradually increased until the water inlet volume load reaches the designed water inlet volume load, the starting process of the SBR system is completed, the ratio of the aeration time to the stirring time in the last operation period is 2:1, the ammonia nitrogen removal rate of the water inlet reaches 93.2%, and the total nitrogen and total phosphorus removal rates reach 85.6% and 86.2%, respectively, and the starting period is 41 days.
Example 5
The reactor and the treated wastewater and culture conditions were the same as in example 4, and the start-up process was different from example 4. The initial inlet volume load of the starting method is 20% of the designed inlet volume load, and the method operates according to the first aeration reaction (330 min), the first stirring reaction (110 min), the second aeration reaction (90 min), the second stirring reaction (30 min), the sedimentation (60 min) and the drainage (100 min) in the first operation period. When the total nitrogen and total phosphorus removal rate of the inlet water reaches more than 70%, the inlet water volume load of the next operation period is increased by 20 percent.
By setting the time ratio of aeration to stirring to be 3:1 at the initial stage of starting, the aeration time and stirring time are not regulated in the starting process, the load is gradually increased until the water inlet volume load reaches the designed water inlet volume load, the starting process of the SBR system is completed, and the starting period is 42 days when the ammonia nitrogen removal rate reaches 92.3% and the total nitrogen and total phosphorus removal rates reach 84.1% and 85.4% respectively in the last operation period.
Example 6
A set of SBR system is built in a laboratory, and comprises 4 organic glass reactors with effective volumes of 5L, and sewage with ammonia nitrogen concentration of 150mg/L, total nitrogen concentration of 200mg/L, COD concentration of 400mg/L and total phosphorus concentration of 12mg/L is treated.
Firstly, inoculating residual activated sludge containing nitrifying bacteria and denitrifying phosphorus accumulating bacteria in a secondary sedimentation tank of a sewage field according to the sludge concentration of 2500mg/L, and setting an operation period of each reactor to be 6 hours, wherein water is fed and the reaction is carried out at the same time. The single SBR reactor is carried out according to the procedures of first aeration reaction, first stirring reaction, second aeration reaction, sedimentation and drainage. Asparagine was added at 0.05mg/L in the first aeration reaction stage, trehalose ester was added at 0.05mg/L in the first agitation reaction stage, and phosphorylcholine was added at 0.05mg/L when the dissolved oxygen was reduced to less than 0.1 mg/L.
The initial water inlet volume load is 40% of the designed water inlet volume load, and the first operation period is operated according to the first aeration reaction (200 min), the first stirring reaction (40 min), the second aeration reaction (40 min), the sedimentation (40 min) and the drainage (40 min). When the ammonia nitrogen removal rate of the inflow water reaches more than 80%, the first aeration time in the next operation period is shortened by 10min, and the first stirring time is increased by 10min. When the total nitrogen and total phosphorus removal rate of the inlet water reaches more than 70%, the inlet water volume load of the next operation period is increased by 15 percent.
The operating conditions of the SBR reactor were: the dissolved oxygen is controlled at 1.5mg/L during aeration reaction, the dissolved oxygen is less than 0.3mg/L during stirring reaction, the pH value of the whole reaction stage is 7.4-7.7, and the temperature is 30 ℃.
The aeration time and the stirring time are gradually adjusted by the control method, the load is gradually increased until the water inlet volume load reaches the designed water inlet volume load, the starting process of the SBR system is completed, the ratio of the aeration time to the stirring time in the last operation period is 3:1, the ammonia nitrogen removal rate of the water inlet reaches 93.7%, and the total nitrogen and total phosphorus removal rates reach 84.6% and 85.3%, respectively, and the starting period is 41 days.
Claims (23)
1. A method for rapidly starting an SBR system to realize denitrification and dephosphorization comprises the following steps:
s1: inoculating activated sludge containing nitrifying bacteria and denitrifying phosphorus accumulating bacteria into an SBR reactor,
s2: setting an operation period in the starting process of the SBR system, wherein each period operates according to the time sequence of water inlet and reaction-sedimentation-drainage-idling, and the reaction is divided into an aerobic reaction and an anoxic reaction, and the two reactions alternately operate; an operation mode of gradually increasing the water inlet volume load is adopted in the starting process;
s3: the method comprises the steps that nitrogen and phosphorus-containing wastewater to be treated enters an SBR reactor to start a starting process, wherein asparagine is added into the wastewater in an aerobic reaction stage, sugar ester substances are added into the wastewater in an anoxic reaction stage, and quaternary ammonium base is added after dissolved oxygen is reduced to be less than 0.1 mg/L;
s4: and completing the starting process of the SBR system until the water inlet volume load reaches the designed water inlet volume load, the ammonia nitrogen removal rate reaches more than 90%, and the total nitrogen and total phosphorus removal rates reach more than 85%.
2. A method according to claim 1, characterized in that: in the step S1, the activated sludge containing nitrifying bacteria and denitrifying phosphorus accumulating bacteria is taken from the residual activated sludge in a secondary sedimentation tank of a sewage treatment plant for treating nitrogen and phosphorus, and the inoculation amount is 2000-5000mg/L.
3. A method according to claim 1, characterized in that: in the nitrogen and phosphorus containing wastewater to be treated, the ammonia nitrogen concentration is 100-300mg/L, the total nitrogen concentration is 100-400mg/L, the COD concentration is 300-600mg/L, and the total phosphorus concentration is 5-20mg/L.
4. A method according to claim 1, characterized in that: in step S2, setting an operation period in the starting process of the SBR system, wherein the period duration is 6-24 hours, and each period operates according to the time sequence of water inlet and reaction-sedimentation-drainage-idling, wherein the reaction duration is more than 50%.
5. The method of claim 4, wherein: the reaction time is 60% -80%.
6. A method according to claim 1, characterized in that: in the step S2, the aerobic reaction and the anoxic reaction alternately run.
7. The method of claim 6, wherein: in step S2, the two alternate operations specifically include: first aeration-first agitation, first agitation-first aeration-second agitation, first aeration-first agitation-second aeration-second agitation, or first agitation-first aeration-second agitation-second aeration.
8. A method according to claim 1, characterized in that: in the step S2, the initial water inlet volume load is less than 50% of the designed water inlet volume load; and/or when the total nitrogen and total phosphorus removal rate of the inlet water reaches more than 60%, the next inlet water volume load is improved, and the improvement amplitude is 10-20 percent each time.
9. The method according to claim 8, wherein: in the step S2, the initial water inlet volume load is 10% -50% of the designed water inlet volume load; and/or when the total nitrogen and total phosphorus removal rate of the inlet water reaches 70% -80%, the volume load of the inlet water of the next time is improved.
10. A method according to claim 1, characterized in that: in the step S2, the ratio of the aerobic aeration time to the anoxic stirring time in the first operation period is 10:1-5:1.
11. A method according to claim 1, characterized in that: an operation mode of gradually shortening the aerobic aeration time and correspondingly increasing the anoxic stirring time is adopted.
12. The method of claim 11, wherein: when the ammonia nitrogen removal rate of the inflowing water reaches more than 70%, the aerobic aeration time in the next operation period is shortened, the anoxic stirring time is correspondingly increased, and the time of each change is 3-15% of the aerobic aeration time in the current operation period.
13. The method of claim 12, wherein: when the ammonia nitrogen removal rate of the inflow water reaches 80% -90%, the aerobic aeration time in the next operation period is shortened, and the anoxic stirring time is correspondingly increased.
14. A method according to claim 1 or 10, characterized in that: the ratio of the aerobic aeration time to the anoxic stirring time in the last operation period at the end of the starting process is 10:1-1:1.
15. The method of claim 14, wherein: the ratio of the aerobic aeration time to the anoxic stirring time in the last operation period at the end of the starting process is 5:1-2:1.
16. A method according to claim 1, characterized in that: adding asparagine to the wastewater in the aerobic reaction stage, wherein asparagine is added to the wastewater in the first aerobic reaction stage; and/or adding sugar ester substances into the wastewater in the anoxic reaction stage, wherein after the dissolved oxygen is reduced to less than 0.1mg/L, quaternary ammonium base is added, and in the first anoxic reaction stage, sugar ester substances are added into the wastewater, and after the dissolved oxygen is reduced to less than 0.1mg/L, quaternary ammonium base is added.
17. A method according to claim 1, characterized in that: the dosage of the asparagine is 0.001-1.0mg/L.
18. The method of claim 17, wherein: the dosage of the asparagine is 0.01-0.10mg/L.
19. A method according to claim 1, characterized in that: the sugar ester substance comprises at least one of mouse Li Tangzhi, trehalose ester, sophorolipid and sucrose ester; the quaternary ammonium base is at least one of phosphorylcholine, betaine and tetramethylammonium hydroxide.
20. A method according to claim 1 or 19, characterized in that: the dosage of the sugar ester substance is 0.001-1.0mg/L; the dosage of the quaternary ammonium base is 0.001-1.0mg/L.
21. The method of claim 20, wherein: the dosage of the sugar ester substance is 0.01-0.10mg/L; the dosage of the quaternary ammonium base is 0.01-0.10mg/L.
22. A method according to claim 1, characterized in that: the operation conditions of the SBR reactor are as follows: the dissolved oxygen is controlled to be 0.5-5.0mg/L in the aeration reaction, the dissolved oxygen is 0-1.0mg/L in the stirring reaction, the pH value in the whole reaction stage is 6-9, and the temperature is 25-40 ℃.
23. A method according to claim 1, characterized in that: the SBR system includes a plurality of SBR reactors to allow wastewater to continuously enter the SBR system.
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| US20180148681A1 (en) * | 2016-11-29 | 2018-05-31 | China Petroleum & Chemical Corporation | Composition capable of promoting the growth of denitrifying microorganisms and uses thereof |
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| CN104445612A (en) * | 2013-09-16 | 2015-03-25 | 中国石油化工股份有限公司 | Method for rapidly starting denitrification-nitrification biochemical treatment system |
| CN103588300A (en) * | 2013-10-25 | 2014-02-19 | 沈阳建筑大学 | Quick starting method of SBR (Sequencing Batch Reactor) for synchronously denitrifying and removing phosphor |
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Effective date of registration: 20231215 Address after: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee after: CHINA PETROLEUM & CHEMICAL Corp. Patentee after: Sinopec (Dalian) Petrochemical Research Institute Co.,Ltd. Address before: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee before: CHINA PETROLEUM & CHEMICAL Corp. Patentee before: DALIAN RESEARCH INSTITUTE OF PETROLEUM AND PETROCHEMICALS, SINOPEC Corp. |