CN115536151A - Method and device for improving synchronous nitrogen and phosphorus removal of sludge - Google Patents
Method and device for improving synchronous nitrogen and phosphorus removal of sludge Download PDFInfo
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 122
- 239000010802 sludge Substances 0.000 title claims abstract description 103
- 238000000034 method Methods 0.000 title claims abstract description 64
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 61
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 title claims abstract description 38
- 229910052698 phosphorus Inorganic materials 0.000 title claims abstract description 38
- 239000011574 phosphorus Substances 0.000 title claims abstract description 38
- 230000001360 synchronised effect Effects 0.000 title claims abstract description 10
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims abstract description 66
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 54
- 230000001651 autotrophic effect Effects 0.000 claims abstract description 37
- 230000003647 oxidation Effects 0.000 claims abstract description 32
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 32
- 229910052742 iron Inorganic materials 0.000 claims abstract description 30
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 28
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 27
- LELOWRISYMNNSU-UHFFFAOYSA-N hydrogen cyanide Chemical compound N#C LELOWRISYMNNSU-UHFFFAOYSA-N 0.000 claims abstract description 23
- 230000001276 controlling effect Effects 0.000 claims abstract description 19
- 241000894006 Bacteria Species 0.000 claims abstract description 18
- 230000001105 regulatory effect Effects 0.000 claims abstract description 18
- 238000007599 discharging Methods 0.000 claims abstract description 13
- 239000000203 mixture Substances 0.000 claims description 57
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 28
- 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 claims description 17
- JVMRPSJZNHXORP-UHFFFAOYSA-N ON=O.ON=O.ON=O.N Chemical compound ON=O.ON=O.ON=O.N JVMRPSJZNHXORP-UHFFFAOYSA-N 0.000 claims description 16
- 239000010865 sewage Substances 0.000 claims description 16
- 239000000126 substance Substances 0.000 claims description 14
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 11
- 229910052760 oxygen Inorganic materials 0.000 claims description 11
- 239000001301 oxygen Substances 0.000 claims description 11
- 238000005273 aeration Methods 0.000 claims description 10
- 238000003756 stirring Methods 0.000 claims description 10
- 238000006243 chemical reaction Methods 0.000 claims description 6
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 claims description 5
- 239000002351 wastewater Substances 0.000 claims description 5
- 230000033558 biomineral tissue development Effects 0.000 abstract description 11
- 238000000926 separation method Methods 0.000 abstract description 9
- 230000007774 longterm Effects 0.000 abstract description 8
- 230000000694 effects Effects 0.000 description 17
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 7
- 229910052799 carbon Inorganic materials 0.000 description 7
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 6
- 230000000052 comparative effect Effects 0.000 description 6
- 238000005868 electrolysis reaction Methods 0.000 description 6
- 230000001546 nitrifying effect Effects 0.000 description 6
- 229910052717 sulfur Inorganic materials 0.000 description 6
- 239000011593 sulfur Substances 0.000 description 6
- QMQXDJATSGGYDR-UHFFFAOYSA-N methylidyneiron Chemical compound [C].[Fe] QMQXDJATSGGYDR-UHFFFAOYSA-N 0.000 description 5
- 238000002798 spectrophotometry method Methods 0.000 description 4
- 238000010168 coupling process Methods 0.000 description 3
- 239000000945 filler Substances 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000010992 reflux Methods 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 2
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 230000008878 coupling Effects 0.000 description 2
- 238000005859 coupling reaction Methods 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 230000029087 digestion Effects 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 230000003203 everyday effect Effects 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000011159 matrix material Substances 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 2
- KMUONIBRACKNSN-UHFFFAOYSA-N potassium dichromate Chemical compound [K+].[K+].[O-][Cr](=O)(=O)O[Cr]([O-])(=O)=O KMUONIBRACKNSN-UHFFFAOYSA-N 0.000 description 2
- 239000002244 precipitate Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000000758 substrate Substances 0.000 description 2
- JXBUOZMYKQDZFY-UHFFFAOYSA-N 4-hydroxybenzene-1,3-disulfonic acid Chemical compound OC1=CC=C(S(O)(=O)=O)C=C1S(O)(=O)=O JXBUOZMYKQDZFY-UHFFFAOYSA-N 0.000 description 1
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 1
- 241001453382 Nitrosomonadales Species 0.000 description 1
- 229910019142 PO4 Inorganic materials 0.000 description 1
- 238000009825 accumulation Methods 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
- 235000018660 ammonium molybdate Nutrition 0.000 description 1
- 229940010552 ammonium molybdate Drugs 0.000 description 1
- 239000011609 ammonium molybdate Substances 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000012851 eutrophication Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 229960004887 ferric hydroxide Drugs 0.000 description 1
- 229910001448 ferrous ion Inorganic materials 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 150000002505 iron Chemical class 0.000 description 1
- -1 iron ions Chemical class 0.000 description 1
- IEECXTSVVFWGSE-UHFFFAOYSA-M iron(3+);oxygen(2-);hydroxide Chemical compound [OH-].[O-2].[Fe+3] IEECXTSVVFWGSE-UHFFFAOYSA-M 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 239000010452 phosphate Substances 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
- NIFIFKQPDTWWGU-UHFFFAOYSA-N pyrite Chemical compound [Fe+2].[S-][S-] NIFIFKQPDTWWGU-UHFFFAOYSA-N 0.000 description 1
- 229910052683 pyrite Inorganic materials 0.000 description 1
- 239000011028 pyrite Substances 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 235000017557 sodium bicarbonate Nutrition 0.000 description 1
- 229910000030 sodium bicarbonate Inorganic materials 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000004448 titration Methods 0.000 description 1
Images
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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
-
- 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
- C02F3/28—Anaerobic digestion processes
-
- 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
- C02F3/302—Nitrification and denitrification treatment
-
- 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
- C02F3/302—Nitrification and denitrification treatment
- C02F3/307—Nitrification and denitrification treatment characterised by direct conversion of nitrite to molecular nitrogen, e.g. by using the Anammox process
-
- 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
- C02F2301/00—General aspects of water treatment
- C02F2301/04—Flow arrangements
- C02F2301/046—Recirculation with an external loop
-
- 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
Abstract
The invention relates to a method and a device for improving synchronous nitrogen and phosphorus removal of sludge, which mainly comprise a reactor I and a reactor II which are arranged in series, wherein the reactor I is provided with a first external circulation loop, and the loop is provided with a swirler A; the reactor II is provided with a second external circulation loop, and a cyclone B is arranged on the loop; inoculating shortcut nitrification sludge and anaerobic ammonia oxidation sludge in the reactor I, starting a first external circulation loop when the shortcut nitrification sludge reaches a certain proportion, regulating and controlling the overflow proportion of the cyclone A to be lower than 15%, and discharging the overflow of the cyclone A out of the reactor I; and (3) discharging water from the reactor I into a reactor II, inoculating iron autotrophic denitrification sludge into the reactor II, running until the proportion of iron autotrophic denitrification bacteria reaches a certain proportion, starting a second external circulation loop, regulating and controlling the proportion of underflow of the cyclone B to be lower than 10%, and discharging the underflow out of the reactor II. The invention not only realizes the sludge separation of shortcut nitrification-anaerobic ammonia oxidation and maintains the balanced flora proportion, but also solves the sludge mineralization problem of iron autotrophic denitrification and ensures the long-term stable operation of the device.
Description
Technical Field
The invention belongs to the field of water treatment, and particularly relates to a method and a device for improving synchronous nitrogen and phosphorus removal of sludge.
Background
In order to prevent eutrophication of water bodies, the requirements of China on the discharge amount of nitrogen and phosphorus in sewage are increasingly strict, which provides great challenge for the traditional sewage biological treatment process, adds a plurality of physical and chemical units for meeting the discharge standard of each sewage plant, not only increases the energy consumption and the medicament cost, but also causes secondary pollution. The traditional biological nitrogen and phosphorus removal method mainly has the following problems: the energy consumption for operating aeration is high, the adding cost of the organic carbon source, the alkaline agent and the phosphorus removal agent is high, and the SRT required in the phosphorus removal process and the nitrification process are different, so that the simultaneous obtaining of efficient phosphorus removal and nitrogen removal effects cannot be ensured. Therefore, in order to meet the increasingly strict requirements of sewage discharge indexes, development of a novel, efficient and environment-friendly biological nitrogen and phosphorus removal process is urgently needed.
The shortcut nitrification-anaerobic ammonia oxidation process is one of the biological denitrification processes which are provided in the field of biological denitrification of sewage in recent years, and have the advantages of energy conservation, high efficiency and good application prospect. Through the mode of oxygen limitation, the ammonia nitrogen in the sewage is partially converted into nitrite nitrogen by using short-range nitrifying bacteria, then the nitrite nitrogen and the residual ammonia nitrogen are converted into nitrogen by using anaerobic ammonia oxidizing bacteria according to the degradation proportion of 1.32. However, the process has the defects that the maximum total nitrogen removal rate in the anaerobic ammonia oxidation process is about 89%, and about 11% of total nitrogen of inlet water is converted into nitrate nitrogen in outlet water, so that the total nitrogen of the outlet water is possibly not up to the standard. Meanwhile, the efficient interception of the shortcut nitrifying bacteria and the anaerobic ammonium oxidation bacteria during sludge discharge is also a difficult problem to be overcome to ensure the long-term efficient and stable operation of the system.
Research shows that part of denitrifying bacteria can utilize reducing state matrix of iron, ferrous ion, etc. to reduce nitrate nitrogen into nitrogen. Since no organic carbon source participates in the whole process, the process is called autotrophic denitrification. The price of the reduced substrates such as iron powder or pyrite is much cheaper than that of the organic carbon source, the reduced substrates replace the organic carbon source to participate in the denitrification process, so that the operation cost can be reduced, and meanwhile, the generated iron ions can react with phosphate in water to generate precipitates, so that the effect of chemical phosphorus removal is achieved. However, with the operation of the device, the reaction product of iron can be attached to the surface of zero-valent iron and the surface of microorganisms in the reactor, so that the transfer of matrix and the information exchange among cells are influenced, the denitrification effect is obviously weakened after the operation is approximately 7-10 days, and the total nitrogen of effluent exceeds the standard. The sludge is seriously mineralized and the activity is reduced due to the increase of inorganic substances such as iron salt and the like and the coating of the sludge by the iron oxide. At present, the sludge mineralization problem is mainly solved by adopting a method of frequently discharging sludge, adding a medicament and adjusting a reflux ratio, but the method is not beneficial to enriching the sludge with high activity, and has high operation cost, complex operation and unsatisfactory effect.
CN108264201A discloses a low C/N sewage treatment process for synchronous nitrogen and phosphorus removal, which comprises an anaerobic phosphorus release zone, a sulfur autotrophic denitrification zone, an integrated anaerobic ammonia oxidation zone, an aerobic aeration zone and a sludge settling zone, which are arranged in sequence according to the water flow direction of sewage, wherein the process comprises the following steps: the sewage with low C/N firstly enters an anaerobic phosphorus release area, and the effluent of the anaerobic phosphorus release area is transmitted to a sulfur autotrophic denitrification area; the mixed liquor of the sulfur autotrophic denitrification region is internally circulated to the anaerobic phosphorus release region, the effluent of the sulfur autotrophic denitrification region is transmitted to the integrated anaerobic ammonia oxidation region, and the effluent of the integrated anaerobic ammonia oxidation region is transmitted to the aerobic aeration region; the mixed liquid in the aerobic aeration zone is internally circulated to the sulfur autotrophic denitrification zone, and the effluent of the aerobic aeration zone is transmitted to a sludge settling zone; and part of sludge discharged from the sludge settling zone flows back to the sulfur autotrophic denitrification zone, and the residual sludge in the sludge settling zone is discharged and recycled. The method realizes the coupling process of autotrophic denitrification and anaerobic ammonia oxidation, does not need to additionally add a carbon source, and can realize synchronous nitrogen and phosphorus removal under the condition of low C/N. However, the method has the advantages of longer process flow, more internal reflux pipelines and complex operation, and the phosphorus removal is biological phosphorus removal, so the efficiency is lower than that of the phosphorus removal by a chemical method.
CN110228911A discloses a multistage tandem type autotrophic-heterotrophic denitrification coupling nitrogen and phosphorus removal method and a device, comprising the following steps: the method comprises the following steps of preparing an iron-carbon micro-electrolysis filler, preparing and pretreating solid carbon source particles, domesticating the solid carbon source particle filler by using activated sludge to inoculate and form a film, inoculating and form a film of the iron-carbon micro-electrolysis filler, and treating sewage. The method adopts a nitrogen removal technology coupling three modes of iron-carbon micro-electrolysis, autotrophic denitrification and heterotrophic denitrification, improves the effect of nitrogen and phosphorus removal of the system, reduces the accumulation of nitrite nitrogen, and ensures the quality of effluent water. However, in the operation process, the iron-carbon micro-electrolysis material can be gradually utilized by autotrophic denitrifying bacteria, so that the iron-carbon micro-electrolysis effect is weakened, and the micro-electrolysis material needs to be replaced regularly to ensure long-term stable operation. Meanwhile, inorganic substances in the sludge can be gradually accumulated in the reactor after long-term operation, so that the sludge is seriously mineralized.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides a method and a device for improving synchronous nitrogen and phosphorus removal of sludge. According to the invention, the shortcut nitrification-anaerobic ammonia oxidation and the iron autotrophic denitrification are coupled, and a specific cyclone separation mode is combined, so that the sludge separation of the shortcut nitrification-anaerobic ammonia oxidation is realized, the proportion of flora is maintained to be balanced, the sludge mineralization problem of the iron autotrophic denitrification is solved, and the long-term stable operation of the device is ensured.
The invention provides a method for improving synchronous nitrogen and phosphorus removal of sludge, which mainly comprises the following steps: the reactor I and the reactor II are arranged in series, the reactor I is provided with a first external circulation loop, and the loop is provided with a cyclone A; the reactor II is provided with a second external circulation loop, and a cyclone B is arranged on the loop; inoculating shortcut nitrification sludge and anaerobic ammonium oxidation sludge in the reactor I, starting and running until the proportion of shortcut nitrification bacteria reaches 30-40%, starting a first external circulation loop, regulating and controlling the proportion of overflow substances of the cyclone A to be lower than 15%, discharging the overflow substances out of the reactor I, and circulating underflow substances to the reactor I; and (3) discharging water from the reactor I into a reactor II, inoculating iron autotrophic denitrification sludge into the reactor II, operating until the ratio of iron autotrophic denitrifying bacteria reaches 30-40%, starting a second external circulation loop, regulating and controlling the ratio of bottom flow of the cyclone B to be lower than 10%, discharging the bottom flow out of the reactor II, and circulating overflow back to the reactor II.
In the present invention, the reactor I and the reactor II may be any of various stirring type reactors conventionally used in the art, wherein the reactor I has an aeration system and a stirring system, and the reactor II has a stirring system.
In the invention, a first external circulation loop is arranged outside a reactor I, namely, a circulation discharge port is arranged at the upper part of the reactor I and is lower than a water discharge port at the upper part, and a circulation return port is arranged at the lower part of the reactor I, so that the external circulation loop from the upper part to the lower part of the reactor I is constructed. And (3) conveying the mixture discharged from the circulating discharge port to the cyclone A through a circulating pump, controlling the volume of the mixture discharged from the reactor I to be not more than 40 percent of the effective volume of the reactor I, preferably 20-30 percent, treating the mixture by the cyclone A, controlling the overflow to be less than 15 percent of the volume of the mixture entering the cyclone A, preferably 1-10 percent, and returning the rest mixture into the reactor I from the bottom of the cyclone A through a circulating return port.
In the invention, a second external circulation loop is arranged outside the reactor II, namely a circulation discharge hole is arranged at the lower part of the reactor II and close to the bottom, a circulation feed back hole is arranged in the middle of the reactor, and the external circulation loop from the lower part to the middle of the reactor II is constructed. And (3) conveying the mixture discharged from the circulating discharge hole to the cyclone B through a circulating pump, controlling the volume of the mixture discharged from the reactor II not to exceed 40 percent of the effective volume of the reactor II, preferably 20 to 30 percent, treating the mixture by the cyclone B, regulating and controlling the underflow to account for less than 10 percent of the volume of the mixture entering the cyclone B, preferably 1 to 5 percent, and returning the rest mixture to the reactor II through an overflow hole and a circulating return hole.
In the invention, the sludge concentration of the inoculated shortcut nitrification sludge in the reactor I is 2000-3000 mg/L, and the sludge concentration of the inoculated anaerobic ammonia oxidation sludge is 3000-4000mg/L. The short-cut nitrified sludge is flocculent sludge, the anaerobic ammonium oxidation sludge is granular sludge, and the two types of sludge with different properties are matched for use, so that the mass transfer effect is good, and the sludge loss is less.
In the invention, the operation conditions of the reactor I are as follows: the reaction temperature is 25-35 ℃, the pH value is 7.0-8.0, and the dissolved oxygen concentration is below 1.0mg/L.
In the invention, when the total nitrogen removal rate of the effluent of the reactor I reaches more than 80 percent and the reactor I stably operates for 7 days, the effluent is discharged into the reactor II, and the reactor II is started to perform subsequent denitrification and dephosphorization.
In the invention, the sludge concentration of the iron autotrophic denitrification sludge inoculated in the reactor II is 3000-4000mg/L. Iron powder is added regularly, for example, a certain amount of iron powder can be added every 2 to 7 days, preferably every day, and the adding amount is 200 to 300mg/L.
In the invention, the operating conditions of the reactor II are as follows: the reaction temperature is 25-35 ℃, the pH value is 6.0-7.0, and the dissolved oxygen concentration is below 0.5mg/L.
In the invention, the treated wastewater is low-carbon-nitrogen-ratio wastewater containing COD, ammonia nitrogen and phosphorus, such as at least one of coal-to-hydrogen wastewater, sludge digestion liquid, municipal sewage and the like, wherein the COD is 50-1000mg/L, the ammonia nitrogen is 50-500mg/L, and the phosphorus is 1-10mg/L.
The invention also provides a device for improving the method for synchronously removing nitrogen and phosphorus from sludge, which mainly comprises a reactor I and a reactor II which are arranged in series, wherein the reactor I is provided with a first external circulation loop, and the loop is provided with a swirler A; the reactor II is provided with a second external circulation loop, and a cyclone B is arranged on the loop; inoculating shortcut nitrification sludge and anaerobic ammonia oxidation sludge in the reactor I for removing ammonia nitrogen, nitrite nitrogen and total nitrogen in the sewage; and (3) discharging water from the reactor I to enter a reactor II, and inoculating iron autotrophic denitrification sludge into the reactor II for removing nitrate nitrogen, total nitrogen and phosphorus in the sewage.
In the apparatus of the present invention, the reactor I and the reactor II may be various stirring type reactors conventionally used in the art, wherein the reactor I is provided with an aeration system and a stirring system, and the reactor II is provided with a stirring system.
In the device, a first external circulation loop is arranged outside a reactor I, namely, a circulation discharge port is arranged at the upper part of the reactor I and is lower than a water discharge port at the upper part, and a circulation return port is arranged at the lower part of the reactor I, so that the external circulation loop from the upper part to the lower part of the reactor I is constructed.
In the invention, a second external circulation loop is arranged outside the reactor II, namely a circulation discharge hole is arranged at the lower part of the reactor II and close to the bottom, a circulation feed back hole is arranged in the middle of the reactor, and the external circulation loop from the lower part to the middle of the reactor II is constructed.
Compared with the prior art, the invention has the following beneficial effects:
(1) According to the invention, the shortcut nitrification-anaerobic ammonia oxidation and iron autotrophic denitrification processes are coupled, and a specific cyclone separation mode is combined, so that the separation of the shortcut nitrification-anaerobic ammonia oxidation sludge and the iron autotrophic denitrification sludge is realized, and the proportion balance of floras is maintained; the problem of mineralization of the iron autotrophic denitrification sludge is also solved, and the long-term stable operation of the system is ensured.
(2) The invention combines the short-cut nitrification-anaerobic ammonia oxidation with a specific cyclone regulation and separation mode to discharge dead sludge, light components and the like, thereby realizing the effective separation of sludge, having high flora activity and improving the nitrogen removal load by more than 10 percent compared with the condition without an external circulation pipeline.
(3) The invention combines the iron autotrophic denitrification with a specific rotational flow regulation and separation mode, realizes the desorption of sludge surface attachments (such as ferric hydroxide, floccules and the like), regularly removes generated ferric salt precipitates and the like, keeps better mass transfer in the reaction process, and effectively solves the sludge mineralization problem while keeping good denitrification and dephosphorization effects.
(4) The combined process provided by the invention combines cyclone separation to regulate and control the sludge reflux ratio and the sludge composition, improves the synchronism and high efficiency of sludge total nitrogen removal, realizes deep removal of phosphorus, and ensures long-term stable operation of the device. After long-term operation, the total nitrogen removal rate is improved by more than 5 percent, and the concentration of the P in the effluent is stably lower than 0.5mg/L.
Drawings
FIG. 1 is a process flow diagram of the simultaneous phosphorus and nitrogen removal method of the present invention;
wherein, the reactor comprises 1-water inlet pump, 2-air inlet pump, 3-1, 3-2-stirrer, 4-aeration disc, 5-1, 5-2-circular discharge port, 6-1-first circulating pump, 6-2-second circulating pump, 7-1, 7-2-circular feed back port, 8-1-water outlet of reactor I and 8-2-water outlet of reactor II.
Detailed Description
The method and effects of the present invention will be described in detail with reference to examples. The embodiments are implemented on the premise of the technical scheme of the invention, and detailed implementation modes and specific operation processes are given, but the protection scope of the invention is not limited by the following embodiments.
The experimental procedures in the following examples are, unless otherwise specified, conventional in the art. The test materials used in the following examples were purchased from biochemical stores, unless otherwise specified.
In the examples, the COD concentration was measured by the potassium dichromate method, GB11914-1989, determination of chemical oxygen demand for Water; the ammonia nitrogen concentration is measured by GB7478-87 water quality-ammonium measurement-distillation and titration method; the nitrite nitrogen concentration is measured by GB7493-87 water quality-nitrite nitrogen determination-spectrophotometry; the nitrate nitrogen concentration is measured by GB7480-1987 phenol disulfonic acid spectrophotometry for measuring water quality and nitrate nitrogen; the total nitrogen concentration adopts GB 11894-89 'determination of water quality-total nitrogen-alkaline potassium persulfate digestion ultraviolet spectrophotometry'; the concentration of orthophosphate phosphorus is determined by GB11893-1989 ammonium molybdate spectrophotometry. The temperature, pH and dissolved oxygen of the reactor were monitored periodically by portable instruments, with pH being regulated by sodium bicarbonate and dilute hydrochloric acid.
The embodiment of the invention adopts the device shown in the attached figure 1, the reactor I and the reactor II are arranged in series and both adopt stirring type reactors, wherein the reactor I is provided with an aeration system. The inlet water is pumped from the bottom of the reactor by the inlet pump 1 and overflows out of the reactor through the water outlet 8. A circulating discharge port 5-1 is formed in the upper portion of the reactor I and is lower than an upper water discharge port 8-1, a circulating return port 7-1 is formed in the lower portion of the reactor I, and a first external circulation loop which is formed by the circulating discharge port 5-1, a first circulating pump 6-1, a cyclone A and the circulating return port 7-1 is formed from the upper portion to the lower portion of the reactor I. And a circulating discharge hole 5-2 is formed in the lower part of the reactor II and is close to the bottom of the reactor, a circulating feed back hole 7-2 is formed in the middle of the reactor, and a second external circulating loop formed by the circulating discharge hole 5-2, a second circulating pump 6-2, a cyclone B and the circulating feed back hole 7-2 is formed from the lower part to the middle of the reactor.
Example 1
The quality of the sewage to be treated in the embodiment is as follows: the concentration of COD, ammonia nitrogen and P are respectively 500mg/L, 300mg/L and 3.5 mg/L, the pH value is about 7.3, and the alkalinity is NaHCO 3 Provided is a method.
And inoculating the short-cut nitrification flocculent sludge and the anaerobic ammonia oxidation granular sludge in the reactor I at the same time, wherein the concentrations of the inoculated sludge are 2500mg/L and 3000mg/L respectively. The reaction temperature is controlled at 30 ℃, the pH value is 7.4-7.5, and the dissolved oxygen is 0.7-0.8mg/L. At this time, the nitrogen removal load of the sludge in the reactor was measured to be 0.3kgN/kg VSS/d.
And starting the reactor to run until the short-cut nitrifying bacteria accounts for 35%, starting a first external circulation loop, conveying the mixture discharged from a circulation discharge port to a cyclone A through a first circulation pump, controlling the volume of the mixture discharged from the reactor to be 25% of the effective volume of the reactor, treating the mixture by the cyclone A, regulating and controlling the discharge of an overflow port to account for 2% of the volume of the mixture entering the cyclone, and returning the rest of the mixture to the reactor I from the bottom of the cyclone A through a circulation return port.
After stable operation, the COD of the effluent of the reactor I is detected to be 35mg/L, the nitrate nitrogen is detected to be 29mg/L, the P is detected to be 3.2mg/L, almost no ammonia nitrogen and nitrite nitrogen exist, and the total nitrogen removal rate reaches over 80 percent. At this time, the nitrogen removal load in the reactor was measured to be 0.34 kgN/kg VSS/d, which is 12% higher than that at the start-up.
Discharging the effluent of the reactor I into a reactor II, and inoculating iron autotrophic denitrification sludge into the reactor II to ensure that the sludge concentration is 3500mg/L. Meanwhile, iron powder is added every day, and the adding amount is 280mg/L. The operating conditions were: the temperature is 30 ℃, the pH is controlled to be about 6.8, and the dissolved oxygen is below 0.5mg/L. When the iron autotrophic denitrifying bacteria account for 30 percent, a second external circulation loop is started, the mixture discharged from a circulation discharge port is conveyed to a cyclone B through a circulating pump, the volume of the mixture discharged from the reactor is controlled to be 25 percent of the effective volume of the reactor, the mixture is treated by the cyclone B, the regulated and controlled underflow accounts for 1 percent of the volume of the mixture entering the cyclone, and the rest is returned to the reactor II through an overflow port and a circulation return port.
After the whole process is operated for 30 days under the conditions, the COD of the effluent is lower than 29mg/L, the total nitrogen is lower than 9mg/L, the ammonia nitrogen is lower than 0.2mg/L, and the P is lower than 0.4mg/L, so that the stable operation of the device is realized, the sludge activity is good, and the mineralization problem does not occur.
Example 2
The same as example 1, except that: (1) When the short-cut nitrifying bacteria account for 30%, starting a first external circulation loop, controlling the volume of a mixture discharged from the reactor to be 30% of the effective volume of the reactor, treating the mixture by using a cyclone A, regulating and controlling the discharge of an overflow port to account for 5% of the volume of the mixture entering the cyclone A, and returning the rest of the mixture to the reactor I from the bottom of the cyclone A through a circulating return port; (2) When the iron autotrophic denitrifying bacteria account for 35 percent, a second external circulation loop is started, the mixture discharged from a circulation discharge port is conveyed to a cyclone B through a circulating pump, the volume of the mixture discharged from the reactor is controlled to be 35 percent of the effective volume of the reactor, the mixture is treated by the cyclone B, the regulated bottom flow accounts for 2 percent of the volume of the mixture entering the cyclone, and the rest of the mixture returns to the reactor II through an overflow port and a circulation return port.
After stable operation, COD of the effluent of the reactor I is detected to be 33mg/L, nitrate nitrogen is detected to be 26mg/L, P is detected to be 3.1mg/L, ammonia nitrogen and nitrite nitrogen are almost not generated, and the total nitrogen removal rate reaches over 80 percent. After the whole process is operated for 30 days under the conditions, the COD of the effluent is lower than 30mg/L, the total nitrogen is lower than 10mg/L, the ammonia nitrogen is lower than 0.4mg/L, and the P is lower than 0.2mg/L, so that the stable operation of the device is realized, the sludge activity is good, and the mineralization problem does not occur.
Example 3
The same as example 1, except that: (1) When the short-cut nitrifying bacteria account for 30%, starting a first external circulation loop, controlling the volume of a mixture discharged from the reactor to be 40% of the effective volume of the reactor, treating the mixture by using a cyclone A, regulating and controlling the discharge of an overflow port to account for 10% of the volume of the mixture entering the cyclone A, and returning the rest of the mixture to the reactor I from the bottom of the cyclone A through a circulating return port; (2) When the iron autotrophic denitrifying bacteria account for 35 percent, a second external circulation loop is started, the mixture discharged from a circulation discharge port is conveyed to a cyclone B through a circulating pump, the volume of the mixture discharged from the reactor is controlled to be 30 percent of the effective volume of the reactor, the mixture is treated by the cyclone B, the regulated bottom flow accounts for 5 percent of the volume of the mixture entering the cyclone, and the rest of the mixture returns to the reactor II through an overflow port and a circulation return port.
After stable operation, the COD of the effluent of the reactor I is detected to be 31mg/L, the nitrate nitrogen is detected to be 29mg/L, the P is detected to be 3.4mg/L, almost no ammonia nitrogen and nitrite nitrogen exist, and the total nitrogen removal rate reaches over 80 percent. After the whole process is operated for 30 days under the conditions, the COD of the effluent is lower than 27mg/L, the total nitrogen is lower than 8mg/L, the ammonia nitrogen is lower than 0.5mg/L, and the P is lower than 0.3mg/L, so that the stable operation of the device is realized, the sludge activity is good, and the mineralization problem does not occur.
Example 4
The same as example 1, except that: (1) When the short-cut nitrifying bacteria account for 30%, starting a first external circulation loop, controlling the volume of a mixture discharged from the reactor to be 35% of the effective volume of the reactor, treating the mixture by using a cyclone A, regulating and controlling the discharge of an overflow port to account for 15% of the volume of the mixture entering the cyclone A, and returning the rest of the mixture to the reactor I from the bottom of the cyclone A through a circulating return port; (2) When the iron autotrophic denitrifying bacteria account for 35 percent, a second external circulation loop is started, the mixture discharged from a circulation discharge port is conveyed to a cyclone B through a circulating pump, the volume of the mixture discharged from the reactor is controlled to be 30 percent of the effective volume of the reactor, the mixture is treated by the cyclone B, the regulated bottom flow accounts for 10 percent of the volume of the mixture entering the cyclone, and the rest of the mixture returns to the reactor II through an overflow port and a circulation return port.
After stable operation, COD of the effluent of the reactor I is detected to be 36mg/L, nitrate nitrogen is detected to be 26mg/L, P is detected to be 3.4mg/L, ammonia nitrogen and nitrite nitrogen are hardly generated, and the total nitrogen removal rate reaches over 80 percent. After the whole process is operated for 30 days under the conditions, the COD of the effluent is lower than 33mg/L, the total nitrogen is lower than 13mg/L, the ammonia nitrogen is lower than 1.2mg/L, and the P is lower than 0.7mg/L, so that the stable operation of the device is realized, the sludge activity is good, and the mineralization problem does not occur.
Comparative example 1
The difference from example 1 is that: and an external circulation loop is not arranged outside the two reactors, and sludge is discharged through a sludge discharge port according to the amount equal to that of the sludge discharged by the cyclone.
After 30 days of operation, the concentration of nitrogen and phosphorus in the effluent of the whole process fluctuates, sludge flocs in the shortcut nitrification-anaerobic ammonia oxidation reactor increase, the total nitrogen removal capacity is reduced, the COD (chemical oxygen demand) of the effluent is 33mg/L, the nitrate nitrogen is 35mg/L, the ammonia nitrogen is 5.7mg/L, the nitrite nitrogen is 2.5mg/L, the P is 3.6mg/L, and the removal load of nitrogen is reduced by 12% compared with that of the effluent when the process is started; mineralization of sludge in the iron autotrophic denitrification reactor appears, COD of effluent is 34mg/L, total nitrogen is 29mg/L, ammonia nitrogen is 5.3mg/L, and P is 1.9mg/L.
Comparative example 2
The difference from example 1 is that: a first external circulation loop is not arranged outside the shortcut nitrification-anaerobic ammonia oxidation reactor, namely, the sludge does not pass through the cyclone A for sludge discharge, and the sludge with the same amount is discharged through a sludge discharge port.
After 30 days of operation, the COD of the effluent of the shortcut nitrification-anaerobic ammonia oxidation reactor is 33mg/L, the nitrate nitrogen is 28mg/L, the ammonia nitrogen is 5.3mg/L, the nitrite nitrogen is 1.5mg/L, the P is 3.4mg/L, and the removal load of the nitrogen is reduced by 10 percent compared with that of the reactor when in starting. After running for 30 days, the COD of the effluent of the whole process is 31mg/L, the total nitrogen is 23mg/L, the ammonia nitrogen is 4.3mg/L, and the P is 1.3mg/L.
Comparative example 3
The same as example 1, except that: and a second external circulation loop is not arranged outside the iron autotrophic denitrification reactor, namely, the equivalent sludge is discharged through a sludge discharge port without passing through the sludge discharge of the cyclone B.
After 30 days of operation, the COD of the effluent of the shortcut nitrification-anaerobic ammonia oxidation reactor is 34mg/L, the nitrate nitrogen is 29mg/L, the P is 3.2mg/L, almost no ammonia nitrogen and nitrite nitrogen exist, and the total nitrogen removal rate reaches over 80 percent. In the iron autotrophic denitrification reactor, the sludge is mineralized, the concentrations of nitrogen and phosphorus in the effluent are increased, the COD of the effluent is 30mg/L, the total nitrogen is 24mg/L, no ammonia nitrogen exists, and the P is 1.0mg/L.
Comparative example 4
The same as example 1, except that: the amount of the flocculent sludge discharged from the short-cut nitrification-anaerobic ammonia oxidation reactor through the cyclone A accounts for 19 percent of the volume of the mixture entering the cyclone.
After stable operation, the COD of the effluent of the shortcut nitrification-anaerobic ammonia oxidation reactor is 34mg/L, the nitrate nitrogen is 35mg/L, the ammonia nitrogen is 1.9mg/L, the nitrite nitrogen is 1.4mg/L, the P is 3.4mg/L, and the removal load of the nitrogen is reduced by 7 percent compared with that of the effluent when the shortcut nitrification-anaerobic ammonia oxidation reactor is started. After the whole process is operated for 30 days, the COD of the effluent is 31mg/L, the total nitrogen is 20mg/L, the ammonia nitrogen is 1.2mg/L, and the P is 0.8mg/L.
Comparative example 5
The difference from example 1 is that: the sludge discharged from the iron autotrophic denitrification reactor through the cyclone is 14% of the volume of the mixture entering the cyclone.
After stable operation, the COD of the effluent of the shortcut nitrification-anaerobic ammonia oxidation reactor is 29mg/L, the nitrate nitrogen is 25mg/L, the P is 3.4mg/L, almost no ammonia nitrogen or nitrite nitrogen exists, and the nitrogen removal efficiency reaches over 80 percent. After running for 30 days, the concentration of nitrogen and phosphorus in the effluent of the whole process is increased, the COD of the effluent is 29mg/L, the total nitrogen is 19mg/L, ammonia nitrogen is not available, and P is 0.7mg/L.
Comparative example 6
The same as example 1, except that: the external circulation loops of both reactors are arranged in the same way as the first.
After stable operation, the COD of the effluent of the shortcut nitrification-anaerobic ammonia oxidation reactor is 33mg/L, the nitrate nitrogen is 24mg/L, the P is 3.3mg/L, ammonia nitrogen and nitrite nitrogen are almost not generated, and the nitrogen removal efficiency reaches more than 80 percent. After 30 days of operation, COD of the effluent of the iron autotrophic denitrification reactor is 39mg/L, nitrate nitrogen is 29mg/L, P is 1.4mg/L, and the sludge activity is reduced, wherein the inorganic matter accounts for 53 percent, and mineralization is serious.
Claims (19)
1. A method for improving synchronous nitrogen and phosphorus removal of sludge is characterized by comprising the following steps: the reactor I and the reactor II are arranged in series, the reactor I is provided with a first external circulation loop, and the loop is provided with a cyclone A; the reactor II is provided with a second external circulation loop, and a cyclone B is arranged on the loop; inoculating shortcut nitrification sludge and anaerobic ammonium oxidation sludge in the reactor I, starting and running until the proportion of shortcut nitrification bacteria reaches 30-40%, starting a first external circulation loop, regulating and controlling the proportion of overflow substances of the cyclone A to be lower than 15%, discharging the overflow substances out of the reactor I, and circulating underflow substances to the reactor I; and (3) draining water from the reactor I into a reactor II, inoculating iron autotrophic denitrification sludge into the reactor II, running until the ratio of iron autotrophic denitrifying bacteria reaches 30-40%, starting a second external circulation loop, regulating and controlling the ratio of bottom flow of the cyclone B to be lower than 10%, discharging the bottom flow out of the reactor II, and circulating overflow back to the reactor II.
2. The method of claim 1, wherein: a first external circulation loop is arranged outside the reactor I, namely, a circulation discharge port is arranged on the upper portion of the reactor I and is lower than a water discharge port on the upper portion of the reactor I, a circulation return port is arranged on the lower portion of the reactor I, an external circulation loop from the upper portion to the lower portion of the reactor I is constructed, and a mixture discharged from the circulation discharge port is conveyed to the cyclone A through a circulation pump.
3. The method according to claim 1 or 2, characterized in that: the volume of the mixture discharged from the reactor I is controlled to be not more than 40%, preferably 20% to 30%, of the effective volume of the reactor I.
4. The method according to claim 1 or 2, characterized in that: after the treatment of the cyclone A, the regulated overflow accounts for less than 15 percent of the volume of the mixture entering the cyclone A, preferably 1 to 10 percent, and the rest mixture returns to the reactor I from the bottom of the cyclone A through a circulating feed back hole.
5. The method of claim 1, wherein: and a second external circulation loop is arranged outside the reactor II, namely a circulation discharge hole is arranged at the lower part of the reactor II and close to the bottom of the reactor II, a circulation feed back hole is arranged in the middle of the reactor, an external circulation loop from the lower part to the middle part of the reactor II is constructed, and a mixture discharged from the circulation discharge hole is conveyed to the swirler B through a circulation pump.
6. The method according to claim 1 or 5, characterized in that: the volume of the mixture discharged from the reactor II is controlled not to exceed 40%, preferably 20% to 30%, of the effective volume of the reactor II.
7. The method according to claim 1 or 5, characterized in that: and (3) treating by using the cyclone B, regulating and controlling the underflow to account for less than 10 percent, preferably 1 to 5 percent of the volume of the mixture entering the cyclone B, and returning the rest mixture to the reactor II through an overflow port and a circulating feed back port.
8. The method of claim 1, wherein: the sludge concentration of the inoculated shortcut nitrification sludge in the reactor I is 2000-3000 mg/L, and the sludge concentration of the inoculated anaerobic ammonia oxidation sludge is 3000-4000mg/L.
9. The method according to claim 1 or 8, characterized in that: the short-cut nitrified sludge is flocculent sludge, and the anaerobic ammonium oxidation sludge is granular sludge.
10. The method of claim 1, wherein: the operating conditions of the reactor I are as follows: the reaction temperature is 25-35 ℃, the pH value is 7.0-8.0, and the dissolved oxygen concentration is below 1.0mg/L.
11. The method of claim 1, wherein: and when the total nitrogen removal rate of the effluent of the reactor I reaches more than 80 percent and the reactor I stably operates for 7 days, discharging the effluent into a reactor II, and starting the reactor II to perform subsequent denitrification and dephosphorization.
12. The method of claim 1, wherein: the sludge concentration of the iron autotrophic denitrification sludge inoculated in the reactor II is 3000-4000mg/L.
13. The method according to claim 1 or 12, characterized in that: and adding iron powder regularly, and preferably adding a certain amount of iron powder every 2-7 days, wherein the adding amount is 200-300mg/L.
14. The method of claim 1, wherein: the operating conditions of the reactor II are as follows: the reaction temperature is 25-35 ℃, the pH value is 6.0-7.0, and the dissolved oxygen concentration is below 0.5mg/L.
15. The method of claim 1, wherein: the treated wastewater is low-carbon-nitrogen-ratio wastewater containing COD (chemical oxygen demand) 50-1000mg/L, ammonia nitrogen 50-500mg/L and phosphorus 1-10mg/L.
16. The device for improving the synchronous nitrogen and phosphorus removal method of the sludge according to any one of claims 1 to 15 is characterized by mainly comprising a reactor I and a reactor II which are arranged in series, wherein the reactor I is provided with a first external circulation loop, and the loop is provided with a cyclone A; the reactor II is provided with a second external circulation loop, and a cyclone B is arranged on the loop; inoculating shortcut nitrification sludge and anaerobic ammonia oxidation sludge in the reactor I for removing ammonia nitrogen, nitrite nitrogen and total nitrogen in the sewage; and (3) discharging water from the reactor I to enter a reactor II, and inoculating iron autotrophic denitrification sludge into the reactor II for removing nitrate nitrogen, total nitrogen and phosphorus in the sewage.
17. The apparatus of claim 16, wherein: the reactor I and the reactor II adopt stirring type reactors, wherein the reactor I is provided with an aeration system and a stirring system, and the reactor II is provided with a stirring system.
18. The apparatus of claim 16, wherein: a first external circulation loop is arranged outside the reactor I, namely, a circulation discharge port is arranged at the upper part of the reactor I and is lower than a water discharge port at the upper part, and a circulation feed back port is arranged at the lower part of the reactor I, so that an external circulation loop from the upper part to the lower part of the reactor I is constructed.
19. The apparatus of claim 16, wherein: and a second external circulation loop is arranged outside the reactor II, namely a circulation discharge hole is arranged at the lower part of the reactor II and close to the bottom of the reactor II, a circulation return hole is arranged in the middle of the reactor II, and the external circulation loop from the lower part of the reactor II to the middle of the reactor II is constructed.
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Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104944582A (en) * | 2015-07-07 | 2015-09-30 | 北京工业大学 | Test device and method of coupled SBR denitrification dephosphorization and integrated anaerobic ammonia oxidation |
| CN106630414A (en) * | 2016-12-18 | 2017-05-10 | 北京工业大学 | Multistage A/O autotrophic denitrification device and method employing half shortcut nitrification-anaerobic ammonia oxidation |
| WO2018107740A1 (en) * | 2016-12-14 | 2018-06-21 | 江南大学 | Wastewater nitrogen and phosphorus removal device and application thereof |
| CN108264201A (en) * | 2018-03-28 | 2018-07-10 | 北京交通大学 | A kind of low C/N sewage treatment process method of synchronous denitrification dephosphorizing |
| CN109721156A (en) * | 2019-01-21 | 2019-05-07 | 北京工业大学 | Intermittent aerating integration/short-cut denitrification-Anammox processing treatment of advanced stage landfill leachate apparatus and method |
| CN110054291A (en) * | 2019-04-24 | 2019-07-26 | 北京工业大学 | Low C/N is followed by short-cut denitrification/anaerobic ammonia oxidation process device and method than sanitary sewage short distance nitration/Anammox |
| CN110228911A (en) * | 2019-07-04 | 2019-09-13 | 沈阳建筑大学 | Multistage tandem type autotrophic-heterotrophic denitrification coupling nitrogen and phosphorus removal method and device |
| CN111661924A (en) * | 2020-07-14 | 2020-09-15 | 北京城市排水集团有限责任公司 | System and method for sulfur autotrophic short-cut denitrification coupling anaerobic ammonia oxidation denitrification |
| WO2020200262A1 (en) * | 2019-04-02 | 2020-10-08 | 北京工业大学 | Method and device for realizing heterotrophic and autotrophic coupling deep denitrification and simultaneous sludge reduction in aoa-sbr |
| CN112250180A (en) * | 2020-09-24 | 2021-01-22 | 北京工业大学 | Device and method for realizing deep denitrification of domestic sewage by coupling half-shortcut nitrification-anaerobic ammonia oxidation with sulfur autotrophic denitrification |
| WO2021035806A1 (en) * | 2019-08-29 | 2021-03-04 | 南京大学 | Method for stating integrated denitrification system combining short-term denitrification and anammox |
-
2021
- 2021-06-29 CN CN202110727817.9A patent/CN115536151A/en active Pending
Patent Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104944582A (en) * | 2015-07-07 | 2015-09-30 | 北京工业大学 | Test device and method of coupled SBR denitrification dephosphorization and integrated anaerobic ammonia oxidation |
| WO2018107740A1 (en) * | 2016-12-14 | 2018-06-21 | 江南大学 | Wastewater nitrogen and phosphorus removal device and application thereof |
| CN106630414A (en) * | 2016-12-18 | 2017-05-10 | 北京工业大学 | Multistage A/O autotrophic denitrification device and method employing half shortcut nitrification-anaerobic ammonia oxidation |
| CN108264201A (en) * | 2018-03-28 | 2018-07-10 | 北京交通大学 | A kind of low C/N sewage treatment process method of synchronous denitrification dephosphorizing |
| CN109721156A (en) * | 2019-01-21 | 2019-05-07 | 北京工业大学 | Intermittent aerating integration/short-cut denitrification-Anammox processing treatment of advanced stage landfill leachate apparatus and method |
| WO2020200262A1 (en) * | 2019-04-02 | 2020-10-08 | 北京工业大学 | Method and device for realizing heterotrophic and autotrophic coupling deep denitrification and simultaneous sludge reduction in aoa-sbr |
| CN110054291A (en) * | 2019-04-24 | 2019-07-26 | 北京工业大学 | Low C/N is followed by short-cut denitrification/anaerobic ammonia oxidation process device and method than sanitary sewage short distance nitration/Anammox |
| CN110228911A (en) * | 2019-07-04 | 2019-09-13 | 沈阳建筑大学 | Multistage tandem type autotrophic-heterotrophic denitrification coupling nitrogen and phosphorus removal method and device |
| WO2021035806A1 (en) * | 2019-08-29 | 2021-03-04 | 南京大学 | Method for stating integrated denitrification system combining short-term denitrification and anammox |
| CN111661924A (en) * | 2020-07-14 | 2020-09-15 | 北京城市排水集团有限责任公司 | System and method for sulfur autotrophic short-cut denitrification coupling anaerobic ammonia oxidation denitrification |
| CN112250180A (en) * | 2020-09-24 | 2021-01-22 | 北京工业大学 | Device and method for realizing deep denitrification of domestic sewage by coupling half-shortcut nitrification-anaerobic ammonia oxidation with sulfur autotrophic denitrification |
Non-Patent Citations (1)
| Title |
|---|
| 吕;孟凡能;张树军;周军;甘一萍;王毅;张春苹;: "半短程硝化-厌氧氨氧化处理污泥消化液的脱氮研究", 北京工业大学学报, no. 11, 15 November 2011 (2011-11-15) * |
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Effective date of registration: 20240115 Address after: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Applicant after: CHINA PETROLEUM & CHEMICAL Corp. Applicant after: Sinopec (Dalian) Petrochemical Research Institute Co.,Ltd. Address before: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Applicant before: CHINA PETROLEUM & CHEMICAL Corp. Applicant before: DALIAN RESEARCH INSTITUTE OF PETROLEUM AND PETROCHEMICALS, SINOPEC Corp. |
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