CN110759585A - Device and method for removing total nitrogen in sewage - Google Patents
Device and method for removing total nitrogen in sewage Download PDFInfo
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- CN110759585A CN110759585A CN201910958149.3A CN201910958149A CN110759585A CN 110759585 A CN110759585 A CN 110759585A CN 201910958149 A CN201910958149 A CN 201910958149A CN 110759585 A CN110759585 A CN 110759585A
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- 239000010865 sewage Substances 0.000 title claims abstract description 64
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 54
- 238000000034 method Methods 0.000 title claims abstract description 27
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 27
- 238000006243 chemical reaction Methods 0.000 claims abstract description 219
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 60
- 239000010802 sludge Substances 0.000 claims abstract description 37
- 239000012528 membrane Substances 0.000 claims abstract description 18
- 239000000945 filler Substances 0.000 claims abstract description 16
- 239000002131 composite material Substances 0.000 claims abstract description 15
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 33
- 229910052760 oxygen Inorganic materials 0.000 claims description 33
- 239000001301 oxygen Substances 0.000 claims description 33
- 230000001105 regulatory effect Effects 0.000 claims description 13
- 229910002651 NO3 Inorganic materials 0.000 claims description 12
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 claims description 12
- 239000007788 liquid Substances 0.000 claims description 11
- 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 7
- 238000004062 sedimentation Methods 0.000 claims description 7
- 238000000926 separation method Methods 0.000 claims description 6
- 238000000265 homogenisation Methods 0.000 claims description 5
- 238000005273 aeration Methods 0.000 claims description 4
- 238000010992 reflux Methods 0.000 claims description 4
- 239000011259 mixed solution Substances 0.000 claims description 3
- 239000002351 wastewater Substances 0.000 claims 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 9
- 229910052799 carbon Inorganic materials 0.000 abstract description 9
- 239000003344 environmental pollutant Substances 0.000 abstract description 3
- 231100000719 pollutant Toxicity 0.000 abstract description 3
- 230000009286 beneficial effect Effects 0.000 abstract description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 2
- 238000012856 packing Methods 0.000 abstract description 2
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 29
- 229910052698 phosphorus Inorganic materials 0.000 description 29
- 239000011574 phosphorus Substances 0.000 description 29
- 241000894006 Bacteria Species 0.000 description 24
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 11
- 244000005700 microbiome Species 0.000 description 6
- 230000008901 benefit Effects 0.000 description 5
- 230000001546 nitrifying effect Effects 0.000 description 5
- 125000001477 organic nitrogen group Chemical group 0.000 description 5
- 239000002028 Biomass Substances 0.000 description 4
- 238000004140 cleaning Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 241000894007 species Species 0.000 description 4
- JVMRPSJZNHXORP-UHFFFAOYSA-N ON=O.ON=O.ON=O.N Chemical compound ON=O.ON=O.ON=O.N JVMRPSJZNHXORP-UHFFFAOYSA-N 0.000 description 3
- 238000010170 biological method Methods 0.000 description 3
- 235000014113 dietary fatty acids Nutrition 0.000 description 3
- 229930195729 fatty acid Natural products 0.000 description 3
- 239000000194 fatty acid Substances 0.000 description 3
- 150000004665 fatty acids Chemical class 0.000 description 3
- YPJKMVATUPSWOH-UHFFFAOYSA-N nitrooxidanyl Chemical compound [O][N+]([O-])=O YPJKMVATUPSWOH-UHFFFAOYSA-N 0.000 description 3
- 241001148470 aerobic bacillus Species 0.000 description 2
- 230000001651 autotrophic effect Effects 0.000 description 2
- 238000006065 biodegradation reaction Methods 0.000 description 2
- 230000004071 biological effect Effects 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000005514 two-phase flow Effects 0.000 description 2
- 241001148471 unidentified anaerobic bacterium Species 0.000 description 2
- 238000007599 discharging Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000002352 surface water Substances 0.000 description 1
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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
- C02F3/302—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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
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- Life Sciences & Earth Sciences (AREA)
- Biodiversity & Conservation Biology (AREA)
- Microbiology (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The invention discloses a device and a method for removing total nitrogen in sewage. The sewage enters a pre-anoxic reaction tank, an anoxic reaction tank and an anaerobic reaction tank in a multi-point water inlet mode. One part of the sludge mixed liquor in the pre-aerobic reaction tank flows back to the anoxic reaction tank, and the other part of the sludge mixed liquor enters the aerobic tank. And returning a part of the sludge mixed liquor in the aerobic reaction tank to the pre-anoxic reaction tank. The treatment method adopts two schemes, one is a pre-anoxic reaction tank, an anaerobic reaction tank, a pre-aerobic reaction tank and a composite filler with the packing density of 70 percent of an aerobic reaction tank, and the other is that an MBR flat-plate membrane component is placed in the aerobic reaction tank. The invention has the beneficial effects that: the method does not need to add a carbon source, can greatly reduce the concentration of pollutants, and has low sludge production rate and good and stable effluent quality.
Description
Technical Field
The invention relates to the technical field of sewage treatment, in particular to a device and a method for removing total nitrogen in sewage.
Background
The nitrogen removal method mainly comprises two main methods, namely a biological method and a chemical method. The biological method can not only remove organic matters, but also convert organic nitrogen and ammonia nitrogen in the sewage into nitrogen through biological nitrification and denitrification, and finally remove the nitrogen from the sewage; the chemical method can only remove ammonia nitrogen, and has the problems of high treatment cost, possible negative influence on the environment, undetermined regeneration method (saturated ion exchanger for ion exchange denitrification) and the like, so the biological method is still practical at present. The denitrification generally comprises nitrification and denitrification, firstly heterotrophic bacteria convert organic nitrogen into ammonia nitrogen, the ammonia nitrogen is oxidized into nitrite nitrogen by autotrophic nitrifying bacteria, the nitrite nitrogen is oxidized into nitrate nitrogen by the autotrophic nitrifying bacteria, and finally the heterotrophic denitrifying bacteria reduce the nitrite nitrogen and the nitrate nitrogen into gaseous nitrogen to be removed from the sewage.
Meanwhile, the pollutant discharge standard of urban sewage treatment plants (survey of comments) proposes special discharge limit values for the first time (the total discharge limit values are equal to the water quality requirements of IV-class water body (except total nitrogen)) of the environmental quality standard of surface water (GB 3838-2002). The COD concentration of the treated effluent is required to be not higher than 30mg/L and BOD in the special discharge limit value5The concentration is not higher than 6mg/L, the total phosphorus concentration is not higher than 0.3mg/L, the ammonia nitrogen concentration is not higher than 1.5mg/L, the total nitrogen concentration is not higher than 10mg/L, and the SS concentration is not higher than 5 mg/L. Although the traditional biological denitrification technology is mature in process, the traditional biological denitrification technology has the defects of long process flow, large occupied area, frequent need of additional carbon sources, high energy consumption, high cost and the like. Therefore, a sewage treatment system or a sewage treatment method process is needed to meet the requirement of removing the total nitrogen.
Disclosure of Invention
The invention aims to provide a device and a method for treating sewage by removing total nitrogen aiming at the defects of the traditional sewage treatment process.
In order to achieve the purpose, the invention adopts the technical scheme that: an apparatus for removing total nitrogen in sewage, comprising: the sewage treatment device comprises an adjusting tank, a pre-anoxic reaction tank, an anaerobic reaction tank, a pre-aerobic reaction tank and an aerobic reaction tank, wherein sewage sequentially passes through the adjusting tank, the pre-aerobic reaction tank and/or the aerobic reaction tank are/is provided with aeration facilities, the adjusting tank is provided with pipelines respectively communicated with the pre-anoxic reaction tank, the anaerobic reaction tank and the pre-aerobic reaction tank, the pre-aerobic reaction tank is provided with a loop communicated with the anoxic reaction tank, and the aerobic reaction tank is provided with a loop and a pre-anoxic reaction tank.
Furthermore, the aerobic reaction tank is provided with an MBR membrane module.
Furthermore, the pre-anoxic reaction tank, the anaerobic reaction tank, the pre-aerobic reaction tank and the aerobic reaction tank are respectively provided with a composite filler bracket combination, and the aerobic reaction tank is connected with the sedimentation tank.
Furthermore, the pre-anoxic reaction tank, the anoxic reaction tank and the anaerobic reaction tank are respectively provided with a submersible stirrer.
A method for removing total nitrogen in sewage comprises the following steps:
comprises the following steps of (a) carrying out,
the method comprises the following steps: sewage enters the regulating tank through the lifting pump, the regulating tank can also be used as an accident tank, and the homogenization of water quality and water quantity is completed in the regulating tank.
Step two: the sewage is treated in the next step by adopting a multipoint water inlet mode after passing through the regulation reaction tank: wherein the water inflow rate of the pre-anoxic reaction tank is 50 percent of the total water inflow rate, the dissolved oxygen DO is 0.5-1mg/L, the sludge mixed liquor in the aerobic reaction tank enters the pre-anoxic reaction tank through a return pipe, and partial dissolved oxygen and nitrate nitrogen in the returned sludge are dissolved in the pre-anoxic reaction tank.
Step three: the sewage after the pre-anoxic reaction enters an anoxic reaction tank through a lift pump: wherein the water inflow rate of the anoxic reaction tank is 25% of the total water inflow rate, and the dissolved oxygen DO in the anoxic reaction tank is 0.5-0.7 mg/L. The phosphorus accumulating bacteria in the anoxic reaction tank neither absorb phosphorus nor release phosphorus, and the total phosphorus is kept stable; the denitrifying bacteria take undecomposed carbon-containing organic matters in the sewage as a carbon source, and reduce nitrate radical which flows back through internal circulation in the aerobic tank into N2Released into the atmosphere.
Step four: the sewage after the anoxic reaction enters an anaerobic reaction tank through a lifting pump: the water inflow rate in the anaerobic reaction tank is 25 percent of the total water inflow rate, and the dissolved oxygen DO in the anaerobic reaction tank is 0.2-0.4 mg/L. In an anaerobic reaction tank, denitrifying fineThe bacteria are converted into N by biological denitrification2The phosphorus-accumulating bacteria release phosphorus, the total phosphorus concentration gradually rises, and easily degradable organic matters such as lower fatty acid and the like are absorbed.
Step five: the sewage enters a pre-aerobic reaction tank: the blower aerates the pre-aerobic tank, the dissolved oxygen DO in the pre-aerobic reaction stage is 1.0mg/L, in the pre-aerobic section, nitrifying bacteria convert ammonia nitrogen in sewage and ammonia nitrogen formed by ammoniation of organic nitrogen into nitrate through biological nitrification, phosphorus accumulating bacteria absorb a large amount of phosphorus, and therefore total phosphorus TP is rapidly reduced.
Step six: one part of the mixed liquor in the pre-aerobic tank flows back to the anoxic reaction tank at a flow rate of 4 times: nitrate brought by the reflux is subjected to biological denitrification, and the other part of the nitrate enters an aerobic reaction tank;
step seven: the MBR flat membrane is placed in the aerobic reaction tank: the dissolved oxygen DO in the aerobic reaction tank is 2.5mg/L, the sludge age SRT of the aerobic reaction tank is 75-90 days, and the sludge concentration MSSL is 15000-18000 mg/L.
Further, after solid-liquid separation by an MBR membrane, clear water is discharged, and the residual mixed solution flows back to the pre-anoxic reaction tank at a flow rate of 4 times. The purpose is to release dissolved oxygen; the main operation characteristic is that the membrane component is placed in a reaction tank in a submerged manner; the low-pressure water outlet is realized, the working pressure of the system is low, and the power consumption is low; disturbing gas-liquid two-phase flow; the operation is stable for a long time; the membrane is not easy to be polluted, the cleaning frequency is low, and the cleaning operation is convenient.
A method for removing total nitrogen in sewage comprises the following steps:
comprises the following steps of (a) carrying out,
the method comprises the following steps: sewage enters the regulating tank through the lifting pump, the regulating tank can also be used as an accident tank, and the homogenization of water quality and water quantity is completed in the regulating tank.
Step two: the sewage is treated in the next step by adopting a multipoint water inlet mode after passing through the regulation reaction tank: wherein the water inflow rate of the pre-anoxic reaction tank is 50 percent of the total water inflow rate, the dissolved oxygen DO is 0.5-1mg/L, the sludge mixed liquor in the aerobic reaction tank enters the pre-anoxic reaction tank through a return pipe, and partial dissolved oxygen and nitrate nitrogen in the returned sludge are dissolved in the pre-anoxic reaction tank.
Step three: the sewage after the pre-anoxic reaction enters an anoxic reaction tank through a lift pump: wherein the water inflow rate of the anoxic reaction tank is 25% of the total water inflow rate, and the dissolved oxygen DO in the anoxic reaction tank is 0.5-0.7 mg/L. The phosphorus accumulating bacteria in the anoxic reaction tank neither absorb phosphorus nor release phosphorus, and the total phosphorus is kept stable; the denitrifying bacteria take undecomposed carbon-containing organic matters in the sewage as a carbon source, and reduce nitrate radical which flows back through internal circulation in the aerobic tank into N2Released into the atmosphere.
Step four: the sewage after the anoxic reaction enters an anaerobic reaction tank through a lifting pump: the water inflow rate in the anaerobic reaction tank is 25% of the total water inflow rate, the dissolved oxygen DO in the anaerobic reaction tank is 0.2-0.4mg/L, and denitrifying bacteria in the anaerobic reaction tank are converted into N through biological denitrification2The phosphorus-accumulating bacteria release phosphorus, the total phosphorus concentration gradually rises, and easily degradable organic matters such as lower fatty acid and the like are absorbed.
Step five: the sewage enters a pre-aerobic reaction tank: the blower aerates the pre-aerobic tank, the dissolved oxygen DO in the pre-aerobic reaction stage is 1.0mg/L, in the pre-aerobic section, nitrifying bacteria convert ammonia nitrogen in sewage and ammonia nitrogen formed by ammoniation of organic nitrogen into nitrate through biological nitrification, phosphorus accumulating bacteria absorb a large amount of phosphorus, and therefore total phosphorus TP is rapidly reduced.
Step six: one part of the mixed liquor in the pre-aerobic tank flows back to the anoxic reaction tank at a flow rate of 4 times: nitrate brought by the reflux is subjected to biological denitrification, and the other part of the nitrate enters the aerobic reaction tank.
Step seven: the pre-anoxic reaction tank, the anaerobic reaction tank, the pre-aerobic reaction tank and the aerobic reaction tank are respectively provided with a composite filler bracket combination: the dissolved oxygen DO in the aerobic reaction tank is 2.5mg/L, the sludge age SRT of the aerobic reaction tank is 35-45 days, and the sludge concentration MSSL is 3500 mg/L. The composite filler carrier is adopted, so that the biomass and the biological species in the reactor can be improved, and the treatment efficiency of the reaction tank is improved. In addition, each carrier has different biological species inside and outside, anaerobic bacteria or facultative bacteria grow inside, aerobic bacteria grow outside, each carrier is a micro-reactor, and nitrification reaction and denitrification reaction exist at the same time, so that the treatment effect is improved.
The composite filler has the advantages that: the biological activity is strong: large specific surface area (>1000m2/m3) The amount of the microorganisms is large, and the adsorption capacity to the microorganisms is strong; the biocompatibility is strong: different types of microorganisms can coexist, so that the comprehensive capacity of biodegradation is improved, and the treatment effect of the system is greatly improved; the sludge settling property is good: the biomass of the activated sludge is greatly improved, the yield of excess sludge is reduced, the sludge bulking problem of a system is reduced, and the sludge settling performance is good; the adaptability is strong: strong impact load resistance and low temperature performance, and strong adaptability to water quality, water quantity change and system restart.
Step eight: one part of the mixed liquid in the aerobic tank flows back to the pre-anoxic reaction tank at a flow rate of 4 times, and the other part enters the sedimentation tank for carrying out solid-liquid separation of mud and water. So that the effluent quality is good.
Further, the packing density of the step seven composite filler is 70%.
Compared with the prior art, the invention has the following beneficial effects:
(1) the process adopted by the invention does not need to add a carbon source into the system, and can ensure that the total nitrogen of the effluent is less than or equal to 10 mg/L.
(2) The invention can greatly reduce the concentration of pollutants, has low mud production rate and excellent and stable effluent quality.
(3) The treatment process has low operation and maintenance cost, and can well realize the optimal unification of environmental benefit and economic benefit.
Drawings
FIG. 1 is a schematic diagram of MBR flat membrane module disposed in an aerobic reaction tank in the device for removing total nitrogen in sewage according to the present invention;
FIG. 2 is a schematic diagram of the aerobic reaction tank filled with composite filler in the device for removing total nitrogen in sewage.
In the figure:
1-regulating tank 2-pre-anoxic reaction tank 3-anoxic reaction tank
4-anaerobic reaction tank 5-pre-aerobic reaction tank 6-aerobic reaction tank
7-sedimentation tank 8-composite filler support combination 9-submersible stirrer
10-aeration facility 11-MBR membrane module
Detailed Description
The technical solution is explained and explained in detail below with reference to the accompanying drawings.
As shown in fig. 1 and 2, an apparatus for removing total nitrogen in sewage comprises: the sewage treatment device comprises an adjusting tank, a pre-anoxic reaction tank, an anaerobic reaction tank, a pre-aerobic reaction tank and an aerobic reaction tank, wherein sewage sequentially passes through the adjusting tank, the pre-aerobic reaction tank and/or the aerobic reaction tank are/is provided with aeration facilities, the adjusting tank is provided with pipelines respectively communicated with the pre-anoxic reaction tank, the anaerobic reaction tank and the pre-aerobic reaction tank, the pre-aerobic reaction tank is provided with a loop communicated with the anoxic reaction tank, and the aerobic reaction tank is provided with a loop and a pre-anoxic reaction tank.
The aerobic reaction tank is provided with an MBR membrane component.
The pre-anoxic reaction tank, the anaerobic reaction tank, the pre-aerobic reaction tank and the aerobic reaction tank are respectively provided with a composite filler bracket combination, and the aerobic reaction tank is connected with the sedimentation tank.
The pre-anoxic reaction tank, the anoxic reaction tank and the anaerobic reaction tank are respectively provided with a submersible stirrer.
The sewage treatment is operated according to the following steps:
the first scheme is as follows: and an MBR flat membrane is placed in the aerobic reaction tank.
The method comprises the following steps: sewage enters the regulating tank through the lifting pump, the regulating tank can also be used as an accident tank, and the homogenization of water quality and water quantity is completed in the regulating tank.
Step two: and (4) carrying out next treatment on the sewage in a multi-point water inlet mode after the sewage passes through the regulation reaction tank. Wherein the water inflow rate of the pre-anoxic reaction tank is 50 percent of the total water inflow rate, the dissolved oxygen DO is 0.5-1mg/L, the sludge mixed liquor in the aerobic reaction tank enters the pre-anoxic reaction tank through a return pipe, and partial dissolved oxygen and nitrate nitrogen in the returned sludge are dissolved in the pre-anoxic reaction tank.
Step three: and (3) the sewage after the pre-anoxic reaction enters an anoxic reaction tank through a lift pump, wherein the water inlet flow of the anoxic reaction tank is 25% of the total water inlet flow, and the dissolved oxygen DO in the anoxic reaction tank is 0.5-0.7 mg/L. The phosphorus accumulating bacteria in the anoxic reaction tank neither absorb phosphorus nor release phosphorus, and the total phosphorus is kept stable; the denitrifying bacteria take undecomposed carbon-containing organic matters in the sewage as a carbon source, and reduce nitrate radical which flows back through internal circulation in the aerobic tank into N2Released into the atmosphere.
Step four: sewage after the anoxic reaction enters an anaerobic reaction tank through a lift pump, the water inflow rate in the anaerobic reaction tank is 25 percent of the total water inflow rate, the dissolved oxygen DO in the anaerobic reaction tank is 0.2-0.4mg/L, and denitrifying bacteria are converted into N through biological denitrification in the anaerobic reaction tank2Discharging into the atmosphere, wherein phosphorus is released by the phosphorus accumulating bacteria, the total phosphorus concentration is gradually increased, and easily degradable organic matters such as lower fatty acid and the like are absorbed;
step five: sewage enters a pre-aerobic reaction tank, an air blower aerates the pre-aerobic reaction tank, dissolved oxygen DO in a pre-aerobic reaction stage is 1.0mg/L, nitrifying bacteria convert ammonia nitrogen in the sewage and ammonia nitrogen formed by ammoniation of organic nitrogen into nitrate through biological nitrification in a pre-aerobic section, phosphorus accumulating bacteria absorb phosphorus in large quantities, and therefore total phosphorus TP is reduced rapidly.
Step six: part of the mixed liquor in the pre-aerobic tank flows back to the anoxic reaction tank at a flow rate of 4 times, and nitrate brought in by the backflow performs biological denitrification; the other part enters an aerobic reaction tank.
Step seven: an MBR flat membrane is placed in the aerobic reaction tank, the dissolved oxygen DO in the aerobic reaction tank is 2.5mg/L, the sludge age SRT of the aerobic reaction tank is 75-90 days, and the sludge concentration MSSL is 15000-18000 mg/L. After solid-liquid separation by an MBR membrane, clear water is discharged, and the residual mixed solution flows back to the pre-anoxic reaction tank at a flow rate of 4 times, so as to release dissolved oxygen; the main operation characteristic is that the membrane component is placed in a reaction tank in a submerged manner; the low-pressure water outlet is realized, the working pressure of the system is low, and the power consumption is low; disturbing gas-liquid two-phase flow; the operation is stable for a long time; the membrane is not easy to pollute, the cleaning frequency is low, and the cleaning operation is convenient;
the advantage of the flat membrane of MBR: the effluent quality is excellent and stable; the output of the excess sludge is low; the occupied area is small and is not limited by the arrangement occasion; the operation and management are convenient, and the automatic control is easy to realize.
Scheme II: the pre-anoxic reaction tank, the anaerobic reaction tank, the pre-aerobic reaction tank and the aerobic reaction tank are filled with composite fillers, and the filling density of the fillers is 70%.
Step one to step six are the same as the step one to step six in the first scheme;
step seven: the dissolved oxygen DO in the aerobic reaction tank is 2.5 mg/L. The sludge age SRT of the aerobic reaction tank is 35-45 days, and the sludge concentration MSSL is 3500 mg/L. The composite filler carrier is adopted, so that the biomass and the biological species in the reactor can be improved, and the treatment efficiency of the reaction tank is improved. In addition, each carrier has different biological species inside and outside, anaerobic bacteria or facultative bacteria grow inside, aerobic bacteria grow outside, each carrier is a micro-reactor, and nitrification reaction and denitrification reaction exist at the same time, so that the treatment effect is improved.
The composite filler has the advantages that: the biological activity is strong: large specific surface area (>1000m2/m3) The amount of the microorganisms is large, and the adsorption capacity to the microorganisms is strong; the biocompatibility is strong: different types of microorganisms can coexist, so that the comprehensive capacity of biodegradation is improved, and the treatment effect of the system is greatly improved; the sludge settling property is good: the biomass of the activated sludge is greatly improved, the yield of excess sludge is reduced, the sludge bulking problem of a system is reduced, and the sludge settling performance is good; the adaptability is strong: strong impact load resistance and low temperature performance, and strong adaptability to water quality, water quantity change and system restart.
Step eight: one part of the mixed liquid in the aerobic tank flows back to the pre-anoxic reaction tank at a flow rate of 4 times, and the other part enters the sedimentation tank for solid-liquid separation of mud and water, so that the effluent quality is good.
The above-described basis is merely an exemplary embodiment of the present invention, the scope of which is defined by the claims. The technical scope of the present invention is not limited to the content of the specification, and must be determined according to the scope of the claims. Various modifications and equivalents may be made by those skilled in the art within the spirit and scope of the present invention, and such modifications and equivalents should also be considered as falling within the scope of the present invention.
Claims (8)
1. An apparatus for removing total nitrogen in sewage, comprising: the sewage passes through an adjusting tank, a pre-anoxic reaction tank, an anaerobic reaction tank, a pre-aerobic reaction tank and an aerobic reaction tank in sequence, wherein the pre-aerobic reaction tank and/or the aerobic reaction tank are/is provided with aeration facilities, and the sewage treatment device is characterized in that: the adjusting tank is provided with pipelines which are respectively communicated with the pre-anoxic reaction tank, the anaerobic reaction tank and the pre-aerobic reaction tank, the pre-aerobic reaction tank is provided with a loop which is communicated with the anoxic reaction tank, and the aerobic reaction tank is provided with a loop and the pre-anoxic reaction tank.
2. The apparatus for removing total nitrogen in sewage as claimed in claim 1, wherein: the aerobic reaction tank is provided with an MBR membrane module.
3. The apparatus for removing total nitrogen in sewage as claimed in claim 1, wherein: the pre-anoxic reaction tank, the anaerobic reaction tank, the pre-aerobic reaction tank and the aerobic reaction tank are respectively provided with a composite filler bracket combination, and the aerobic reaction tank is connected with the sedimentation tank.
4. The apparatus for removing total nitrogen in wastewater according to claim 1, 2 or 3, wherein: the pre-anoxic reaction tank, the anoxic reaction tank and the anaerobic reaction tank are respectively provided with a submersible stirrer.
5. A method of an apparatus for removing total nitrogen in wastewater according to claim 2, comprising the steps of:
the method comprises the following steps: the sewage enters a regulating tank through a lifting pump, and the homogenization of the water quality and the water quantity is completed in the regulating tank;
step two: the sewage is treated in the next step by adopting a multipoint water inlet mode after passing through the regulation reaction tank: wherein the water inflow rate of the pre-anoxic reaction tank is 50 percent of the total water inflow rate, the dissolved oxygen DO is 0.5-1mg/L, the sludge mixed liquor in the aerobic reaction tank enters the pre-anoxic reaction tank through a return pipe, and partial dissolved oxygen and nitrate nitrogen in the returned sludge are dissolved in the pre-anoxic reaction tank;
step three: the sewage after the pre-anoxic reaction enters an anoxic reaction tank through a lift pump: wherein the water inflow rate of the anoxic reaction tank is 25% of the total water inflow rate, and the dissolved oxygen DO in the anoxic reaction tank is 0.5-0.7 mg/L;
step four: the sewage after the anoxic reaction enters an anaerobic reaction tank through a lifting pump: the water inflow rate in the anaerobic reaction tank is 25 percent of the total water inflow rate, and the dissolved oxygen DO in the anaerobic reaction tank is 0.2-0.4 mg/L;
step five: the sewage enters a pre-aerobic reaction tank: aerating the pre-aerobic tank by an air blower, wherein dissolved oxygen DO at the pre-aerobic reaction stage is 1.0 mg/L;
step six: one part of the mixed liquor in the pre-aerobic tank flows back to the anoxic reaction tank at a flow rate of 4 times: nitrate brought by the reflux is subjected to biological denitrification, and the other part of the nitrate enters an aerobic reaction tank;
step seven: the MBR flat membrane is placed in the aerobic reaction tank: the dissolved oxygen DO in the aerobic reaction tank is 2.5mg/L, the sludge age SRT of the aerobic reaction tank is 75-90 days, and the sludge concentration MSSL is 15000-18000 mg/L.
6. The apparatus for removing total nitrogen in sewage according to claim 2, wherein: after solid-liquid separation by an MBR membrane, clear water is discharged, and the residual mixed solution flows back to the pre-anoxic reaction tank at a flow rate of 4 times.
7. A method of an apparatus for removing total nitrogen in wastewater according to claim 3, comprising the steps of:
the method comprises the following steps: the sewage enters a regulating tank through a lifting pump, and the homogenization of the water quality and the water quantity is completed in the regulating tank;
step two: the sewage is treated in the next step by adopting a multipoint water inlet mode after passing through the regulation reaction tank: wherein the water inflow rate of the pre-anoxic reaction tank is 50 percent of the total water inflow rate, the dissolved oxygen DO is 0.5-1mg/L, the sludge mixed liquor in the aerobic reaction tank enters the pre-anoxic reaction tank through a return pipe, and partial dissolved oxygen and nitrate nitrogen in the returned sludge are dissolved in the pre-anoxic reaction tank;
step three: the sewage after the pre-anoxic reaction enters an anoxic reaction tank through a lift pump: wherein the water inflow rate of the anoxic reaction tank is 25% of the total water inflow rate, and the dissolved oxygen DO in the anoxic reaction tank is 0.5-0.7 mg/L;
step four: the sewage after the anoxic reaction enters an anaerobic reaction tank through a lifting pump: the water inflow rate in the anaerobic reaction tank is 25 percent of the total water inflow rate, and the dissolved oxygen DO in the anaerobic reaction tank is 0.2-0.4 mg/L;
step five: the sewage enters a pre-aerobic reaction tank: aerating the pre-aerobic tank by an air blower, wherein dissolved oxygen DO at the pre-aerobic reaction stage is 1.0 mg/L;
step six: one part of the mixed liquor in the pre-aerobic tank flows back to the anoxic reaction tank at a flow rate of 4 times: nitrate brought by the reflux is subjected to biological denitrification, and the other part of the nitrate enters an aerobic reaction tank;
step seven: the pre-anoxic reaction tank, the anaerobic reaction tank, the pre-aerobic reaction tank and the aerobic reaction tank are respectively provided with a composite filler bracket combination: dissolved oxygen DO in the aerobic reaction tank is 2.5mg/L, sludge age SRT of the aerobic reaction tank is 35-45 days, and sludge concentration MSSL is 3500 mg/L;
step eight: one part of the mixed liquid in the aerobic tank flows back to the pre-anoxic reaction tank at a flow rate of 4 times, and the other part enters the sedimentation tank for carrying out solid-liquid separation of mud and water.
8. The apparatus for removing total nitrogen in sewage as set forth in claim 3, wherein: the filling density of the composite filler obtained in the step seven is 70%.
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