CN108585385B - MBBR sewage treatment system and treatment process - Google Patents
MBBR sewage treatment system and treatment process Download PDFInfo
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- CN108585385B CN108585385B CN201810693196.5A CN201810693196A CN108585385B CN 108585385 B CN108585385 B CN 108585385B CN 201810693196 A CN201810693196 A CN 201810693196A CN 108585385 B CN108585385 B CN 108585385B
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- 239000010865 sewage Substances 0.000 title claims abstract description 54
- 238000000034 method Methods 0.000 title claims abstract description 44
- 230000008569 process Effects 0.000 title claims abstract description 40
- AHEWZZJEDQVLOP-UHFFFAOYSA-N monobromobimane Chemical compound BrCC1=C(C)C(=O)N2N1C(C)=C(C)C2=O AHEWZZJEDQVLOP-UHFFFAOYSA-N 0.000 title claims abstract 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 127
- 239000010802 sludge Substances 0.000 claims abstract description 101
- 239000012528 membrane Substances 0.000 claims abstract description 60
- 238000004062 sedimentation Methods 0.000 claims abstract description 31
- 238000005189 flocculation Methods 0.000 claims abstract description 27
- 230000016615 flocculation Effects 0.000 claims abstract description 25
- 238000005273 aeration Methods 0.000 claims abstract description 19
- 230000000694 effects Effects 0.000 claims abstract description 16
- 230000004907 flux Effects 0.000 claims abstract description 14
- 238000011049 filling Methods 0.000 claims abstract description 13
- 239000007788 liquid Substances 0.000 claims description 24
- 230000001546 nitrifying effect Effects 0.000 claims description 23
- 238000000108 ultra-filtration Methods 0.000 claims description 17
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 16
- 238000005276 aerator Methods 0.000 claims description 14
- 239000000725 suspension Substances 0.000 claims description 13
- 238000004891 communication Methods 0.000 claims description 8
- 238000005192 partition Methods 0.000 claims description 6
- 239000003814 drug Substances 0.000 claims description 5
- 239000012530 fluid Substances 0.000 claims description 5
- 239000006228 supernatant Substances 0.000 claims description 5
- 238000006213 oxygenation reaction Methods 0.000 claims description 3
- 238000003756 stirring Methods 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 2
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 abstract description 25
- 229910052698 phosphorus Inorganic materials 0.000 abstract description 25
- 239000011574 phosphorus Substances 0.000 abstract description 25
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 20
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 16
- 229910052799 carbon Inorganic materials 0.000 abstract description 16
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 11
- 239000000969 carrier Substances 0.000 abstract description 10
- 238000010992 reflux Methods 0.000 abstract description 9
- 241000894006 Bacteria Species 0.000 abstract description 8
- 238000001914 filtration Methods 0.000 abstract description 8
- 230000010354 integration Effects 0.000 abstract description 4
- 230000001360 synchronised effect Effects 0.000 abstract description 3
- 238000001556 precipitation Methods 0.000 description 8
- 238000000926 separation method Methods 0.000 description 7
- 244000005700 microbiome Species 0.000 description 6
- 229910002651 NO3 Inorganic materials 0.000 description 4
- 238000009825 accumulation Methods 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 238000010276 construction Methods 0.000 description 3
- 230000001276 controlling effect Effects 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 239000003344 environmental pollutant Substances 0.000 description 3
- 238000005243 fluidization Methods 0.000 description 3
- 231100000719 pollutant Toxicity 0.000 description 3
- 230000002035 prolonged effect Effects 0.000 description 3
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 2
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 2
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 229910001882 dioxygen Inorganic materials 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 239000000945 filler Substances 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 230000000813 microbial effect Effects 0.000 description 2
- 239000011259 mixed solution Substances 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- 241000108664 Nitrobacteria Species 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- 238000005842 biochemical reaction Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000013043 chemical agent Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000000701 coagulant Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004146 energy storage Methods 0.000 description 1
- 239000008394 flocculating agent Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000005374 membrane filtration Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
-
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
-
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5281—Installations for water purification using chemical agents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2203/00—Apparatus and plants for the biological treatment of water, waste water or sewage
- C02F2203/006—Apparatus and plants for the biological treatment of water, waste water or sewage details of construction, e.g. specially adapted seals, modules, connections
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/10—Solids, e.g. total solids [TS], total suspended solids [TSS] or volatile solids [VS]
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/14—NH3-N
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/16—Total nitrogen (tkN-N)
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/22—O2
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/14—Maintenance of water treatment installations
-
- 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
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
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- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The invention discloses a MBBR sewage treatment system and a MBBR sewage treatment process, and belongs to the technical field of sewage treatment. The method solves the problems of long treatment process flow, low integration level, low load, high carbon source demand and general removal effect of nitrogen, phosphorus and SS of the traditional sewage treatment plant in the prior art. The anaerobic treatment device comprises an anaerobic zone, an anoxic first zone, an anoxic second zone, a flocculation zone, a sedimentation zone, a biological membrane zone, a water outlet zone and pipelines for connecting the zones, wherein the membrane flux and the aeration density of a membrane component in the water outlet zone are set through the adjustment of reflux, the control of sludge concentration, the parameter setting of the filling rate of suspended carriers in the biological membrane zone and DO. By utilizing the characteristics of denitrifying phosphorus accumulating bacteria, the sedimentation area is arranged in the middle section of biochemical treatment, and the biological film process and the filtering film process are coupled, so that the device has the advantages of high integration level, synchronous denitrification and dephosphorization, carbon source saving, low concentration of effluent nitrogen, phosphorus and SS, high load and long service life.
Description
Technical Field
The invention relates to the technical field of MBBR sewage treatment, in particular to an MBBR sewage treatment system and a MBBR sewage treatment process.
Background
In order to strengthen the protection of the water environment, the country puts higher requirements on the water quality of the effluent of the sewage treatment plant, the traditional secondary treatment process flow of the sewage treatment plant has general effect of removing nitrogen and phosphorus, low volume load and large occupied area; the gravity type mud-water separation effluent SS is higher, and cannot meet the requirements of higher and higher effluent SS. These two points are the technical lags of the conventional secondary treatment process flow.
By utilizing the MBBR (Moving Bed Biofilm Reactor, moving bed biomembrane reactor) process, a certain amount of suspension carriers are added into the reactor to serve as carriers for microorganism adhesion growth, and as the biomembrane on the carriers is not limited by the engineering sludge age of sludge discharge, more sludge-age bacteria, especially nitrifying bacteria, can be enriched, so that the high-efficiency ammonia nitrogen nitrifying effect is obtained, the load is high, and the ammonia nitrogen concentration of effluent is low. And the MBBR also has the advantages of land occupation, low capital construction cost, flexible and simple transformation and construction, and the like. At present, the MBBR technology is combined with activated sludge, and coexists in a tank body, and the control conditions are mutually restricted, so that the maximum effect of the MBBR technology cannot be exerted.
In the aspect of sludge-water separation, MBR ultrafiltration membrane filtration is utilized to replace gravity for sludge-water separation, low SS effluent is obtained, and the development trend of sludge-water separation in the future is also realized, but the direct filtration in the activated sludge mixed liquor has the problems of high energy consumption, easy membrane blockage, reduced service life of the membrane, increased energy consumption, depreciation and the like.
At present, a plurality of process modes of combining MBBR suspended carrier processes with MBR filtering membranes exist, and specific researches are as follows:
CN 107311405A discloses a municipal sewage treatment system and process, which is based on the AAO process flow, and after suspended carriers are added in anoxic and aerobic processes, the suspended carriers are simply connected in series with MBR after being precipitated in a precipitation tank, the process flow is long, and the MBR only plays a role in filtering for advanced treatment.
CN 107285467A discloses an MBBR and MBR integrated process and apparatus for a water treatment plant, which simply sets an anoxic zone and places an MBR membrane assembly in an MBBR biological tank, although the process flow is short, and declares that MBBR suspension carriers can clean the surface of the MBR membrane, MBBR suspension carriers scratch the MBR membrane in the fluidization process, and greatly reduces the service life of the MBR membrane. And the nitrogen removal and SS removal effects are only enhanced, the phosphorus removal is not enhanced, and the competition problem of nitrogen and phosphorus on a carbon source is not solved.
Disclosure of Invention
The invention aims to provide an MBBR sewage treatment system which has the advantages of good nitrogen, phosphorus and SS treatment effect, low effluent concentration, high carbon source utilization rate, high system integration level, high statistical load, small occupied area and the like.
In order to achieve the above object, the present invention has the following technical problems to be overcome:
how to solve the problem of poor dephosphorization effect caused by the competition of VFA content in the carbon source of the inflow water and nitrogen denitrification on the carbon source by reasonable functional area setting and reflux setting; and the aerobic phosphorus gathering process can be realized in an anoxic zone containing molecular oxygen nitrate nitrogen, that is, how to utilize the characteristics of the DPB, phosphorus in sewage can be transferred to sludge after passing through the anoxic zone, and a sedimentation tank can be arranged at the rear end of the anoxic zone for sludge-water separation without being arranged behind the aerobic tank.
In order to solve the technical problems, the following technical scheme is adopted:
an MBBR sewage treatment system comprises an anaerobic zone, an anoxic first zone, an anoxic second zone, a flocculation zone, a sedimentation zone, a biological film zone and a water outlet zone which are sequentially connected from front to back, wherein adjacent zones are separated by partition walls, the partition walls are provided with communication ports, and the adjacent zones are communicated by opening the communication ports;
the anaerobic zone is connected with a water inlet pipe, the water outlet zone is connected with a water outlet pipe, sewage to be treated enters through the water inlet pipe, and is discharged from the water outlet pipe after being treated;
the flocculation zone is connected with a dosing pipe, the bottom of the sedimentation zone is connected with a first sludge return pipe and a residual sludge discharge pipe, the other end of the first sludge return pipe is connected to the anoxic zone, and the residual sludge discharge pipe is used for discharging residual sludge;
a nitrifying liquid return pipe is connected between the water outlet area and the anoxic first area, and a sludge return pipe II is connected between the anaerobic area and the anoxic second area;
the anaerobic zone, the anoxic zone and the flocculation zone are respectively provided with a stirrer, the biological membrane zone is internally provided with a suspension carrier, an aerator I and an interception screen, and the water outlet zone is internally provided with an ultrafiltration membrane component and an aerator II.
As a preferable scheme of the invention, the first sludge return pipe, the nitrifying liquid return pipe and the second sludge return pipe are respectively provided with a water pump.
As another preferable scheme of the invention, the interception screen is arranged in front of the water outlet area and is a porous plate, and a water collecting tank is arranged above the ultrafiltration membrane component and is positioned below the water surface.
Further, the first aerator is an oxygenation aerator, and the second aerator is a back flush aerator.
Further, the stirrer in the flocculation zone is a vertical stirrer.
Another task of the present invention is to provide an MBBR sewage treatment process, which adopts the above MBBR sewage treatment system, comprising the following steps:
the sewage to be treated enters an anaerobic zone through a water inlet pipe, the water inlet flow is set to be Q, the sewage stays in the anaerobic zone for a period of time, the sewage flows into an anoxic zone I, an anoxic zone II and a flocculation zone in sequence through a communication port, a certain amount of medicament is added into the sewage through a medicament adding pipe in the flocculation zone, the sewage enters a sedimentation zone under the stirring effect, sludge in the sedimentation zone flows back to the front end of the anoxic zone I through a sludge return pipe I, the return flow of the sludge return pipe I is 0.8-1.2Q, and residual sludge is discharged through a residual sludge discharge pipe;
supernatant fluid of the sedimentation zone sequentially enters a biological membrane zone and a water outlet zone, mixed liquid in the water outlet zone flows back to the front end of the anoxic zone through a nitrifying liquid return pipe, and the nitrifying liquid return amount is 1-3Q; and the mixed liquor in the anoxic zone II flows back to the front end of the anaerobic zone through a sludge return pipe II at the tail end of the anoxic zone II, wherein the return quantity of the sludge return pipe II is the average value of the return quantity of the sludge return pipe I and the return quantity of the nitrifying liquor.
Further, the sludge concentration in the anaerobic zone is 3000-5000mg/L; the sludge concentration in the anoxic first area and the anoxic second area is 6000-8000mg/L; the sludge concentration of the biological film area is less than 500mg/L.
Further, the filling rate of the suspended carrier in the biological film area is 30-67%, and the DO in the biological film area is 1-8mg/L; the membrane flux in the water outlet area is 18-25L/m 2 And/h, the aeration density of the ultrafiltration membrane component is 8-20L/min/m 2 ；
When the filling rate is 30% -50%, the gas-water ratio of the biological film area is 5:1 to 8:1, and the film flux of the water outlet area is 20-25L/m 2 And/h, the aeration density of the ultrafiltration membrane component is 8-15L/min/m 2 ；
When the filling rate is 50% -67%, the gas-water ratio of the biological film area is 7:1 to 10:1, and the film flux of the water outlet area is 18-22L/m 2 And/h, the aeration density of the ultrafiltration membrane component is 12-20L/min/m 2 。
Further, ammonia nitrogen in the effluent of the biological film area is less than or equal to 2mg/L, and TN in the effluent of the biological film area is less than or equal to 8mg/L; when ammonia nitrogen in the effluent of the biological film area is more than 2mg/L, the DO of the biological film area is improved by 10-20 percent until the ammonia nitrogen in the effluent of the biological film area is less than or equal to 2mg/L, and the DO is kept unchanged at the moment; when the water TN of the biological film area is more than 8mg/L, the DO of the biological film area is reduced by 10-20 percent until the water TN of the biological film area is less than or equal to 8mg/L, and the DO is kept unchanged at the moment.
Further, the water discharged from the water outlet of the water outlet area has the following indexes: the TP of the effluent is less than or equal to 0.2mg/L or the TP removal rate is more than or equal to 90 percent, the TN of the effluent is less than or equal to 8mg/L, the SS of the effluent is less than or equal to 6mg/L, and the TN removal load of the system is more than or equal to 0.1kgN/m 3 /d。
The invention is characterized in that after the DPB (denitrifying phosphorus accumulating bacteria) is used for anaerobically releasing phosphorus and absorbing carbon source to store energy, nitrate can be used for replacing oxygen to be used as an electron acceptor for excessively absorbing phosphorus, so that the aerobic phosphorus accumulating process can be realized in an anoxic zone containing molecular oxygen nitrate nitrogen, that is, after the DPB passes through the anoxic zone, phosphorus in sewage can be transferred into sludge, a sedimentation zone can be arranged at the rear end of the anoxic zone for sludge-water separation without being arranged behind the aerobic zone.
The sedimentation zone with mud-water separation function is positioned behind the anoxic zone, and is the middle section of the whole biochemical reaction, but not the tail end (aeration zone) of the traditional biochemical section. The supernatant fluid enters the biological film area after the precipitation area, no activated sludge exists in the biological film area, the ammonia nitrogen is nitrified by utilizing the enriched microbial film on the carrier, two kinds of sludge concentrations exist in one system, the sludge concentration in the anaerobic area and the anoxic area is high, the denitrification of phosphorus release, phosphorus accumulation and nitrate nitrogen is carried out, and the sludge concentration in the biological film area playing a role of nitrification is very low.
After the effluent enters the subsequent effluent area, the SS concentration in the mixed solution is low, so that the abrasion to the membrane component in the effluent area can be reduced, and the service life of the system is prolonged.
The beneficial technical effects brought by the invention are as follows:
1) The biological phosphorus removal effect is good, the water inlet of the anaerobic zone comprises total water inlet and mixed liquid flowing back from the anoxic zone II, and the mixed liquid at the tail end of the anoxic zone II has low nitrate concentration after full denitrification phosphorus accumulation reaction, and after flowing back to the anaerobic zone, the anaerobic phosphorus release energy storage of phosphorus accumulation bacteria is not influenced, so that the biochemical phosphorus removal effect is more fully ensured;
2) The denitrification volume load is high, unlike the traditional two-stage treatment process, the sedimentation zone of the sewage treatment system is arranged at the tail end of the process section, the sedimentation zone of the sewage treatment system is arranged in the middle of the process section, the effluent is not finally discharged, and the problem that the SS of the effluent of the sedimentation zone exceeds the standard due to the fact that the concentration of the sludge entering the sedimentation zone is too high is avoided, so that the anoxic zone can be allowed to have high sludge concentration, and the volume load is higher under the same sludge load;
3) The invention has the advantages that the carbon source and the energy source are fully utilized, the carbon is multipurpose, firstly, the reflux arrangement of the sewage treatment system can utilize the characteristic of synchronous denitrification and dephosphorization of DPB denitrification phosphorus accumulating bacteria, and the phosphorus accumulating bacteria can utilize nitrate nitrogen as an electron acceptor, and the carbon is dual-purpose. In addition, the high-concentration sludge in the anoxic zone is beneficial to the precipitation of internal carbon sources, so that the endogenous carbon sources of the system can be utilized more, and when the carbon sources of the inflow water are insufficient, the additional carbon sources are saved and are not used. And the sedimentation area is positioned in the hypoxiaAfter the area, the sludge does not pass through an aerobic area, so that the carbon source is prevented from being degraded aerobically, the carbon source can enter the sludge, the resource and energy recovery value of the sludge is improved, and the phosphorus is polymerized by using the compound oxygen NO 3 The requirement for dissolved oxygen is reduced, and the energy consumption is reduced;
4) The suspended carrier is intercepted in the fixed area by the screen mesh, which is favorable for the attachment and growth of microorganisms with longer mud age, especially nitrobacteria and nitrifying bacteria, and has good nitrification effect, and can fully nitrify ammoniacal nitrogen in sewage;
5) The biological membrane area only has one microbial form of the biological membrane on the suspension carrier, the operation management and the regulation are simple, the nitrification load is high, and meanwhile, the multi-layer structure of the biological membrane is utilized, so that favorable conditions can be provided for the synchronous nitrification and denitrification, and the nitrogen removal effect is enhanced;
6) The sewage treatment system is provided with a precipitation zone in front of a biological membrane zone, supernatant fluid after precipitation enters the biological membrane zone, and the supernatant fluid enters the biological membrane zone to carry out a nitrification process by virtue of microorganisms attached to a suspension carrier in a pool, so that the concentration of effluent SS is far lower than that of an activated sludge mixed solution, the filtration pressure of a membrane can be reduced, the flux of the membrane can be improved, the washing and cleaning frequency of the membrane can be reduced, and the service life of the membrane can be prolonged;
7) The sewage treatment system has the advantages that the load is high, the occupied area is saved, the sludge concentration in the anaerobic area and the anoxic area is high, the biological membrane area depends on the high-efficiency nitrification effect of the carrier, the volume load is very high, the occupied area of the pond is saved, the final mud-water separated water is filtered by the membrane, the effect is good, the occupied area is saved, the system integration level is high, and the occupied area is quite saved although the system has good removal effect on each index;
8) The method is widely applicable to new construction and transformation of sewage plants and integrated sewage treatment equipment.
Drawings
The invention is further described below with reference to the accompanying drawings:
FIG. 1 is a schematic diagram of an MBBR sewage treatment system;
in the figure:
the device comprises a C1-anaerobic zone, a C2-anoxic zone, a C3-anoxic zone, a C4-flocculation zone, a C5-sedimentation zone, a C6-biomembrane zone, a C7-water outlet zone, a S1-anaerobic zone stirrer, a S2-anoxic zone stirrer, a S3-anoxic zone stirrer, a S4-flocculation zone stirrer, a S5-suspension carrier, a S6-biomembrane zone aeration, a S7-interception screen, a S8-water outlet zone aeration, a S9-ultrafiltration membrane, a P1-water inlet pipe, a P2-water outlet pipe, a P3-dosing pipe, a P4-sludge return pipe, a P5-excess sludge discharge pipe, a P6-nitrifying liquid return pipe, a P7-sludge return pipe, a B1-sludge return pump (water pump), a B2-sludge return pump (water pump), and a B3-nitrifying liquid return pump (water pump).
Detailed Description
The invention provides an MBBR sewage treatment system and a MBBR sewage treatment process, and the invention is described in detail below with reference to specific embodiments in order to make the advantages and the technical scheme of the invention clearer and more definite.
Firstly, referring to fig. 1, the MBBR sewage treatment system of the invention is described in detail, which sequentially comprises an anaerobic zone C1, an anoxic zone C2, an anoxic zone C3, a flocculation zone C4, a sedimentation zone C5, a biological film zone C6, a water outlet zone C7 and related process pipelines from front to back (from left to right), wherein adjacent zones are separated by partition walls, the partition walls are provided with communication ports, the adjacent zones are communicated by opening the communication ports, and the related process pipelines comprise a water inlet pipe P1, a water outlet pipe P2, a dosing pipe P3, a sludge return pipe P4, a residual sludge discharge pipe P5, a nitrifying liquid return pipe P6 and a sludge return pipe P7. Wherein the water inlet pipe P1 is communicated with the front end of the anaerobic zone; the water outlet pipe P2 is communicated with the ultrafiltration membrane component in the water outlet area; the dosing pipe P3 is communicated with the water inlet end of the flocculation area; one end of a first P4 sludge return pipe is communicated with the bottom of the sedimentation zone, and the other end of the first P4 sludge return pipe is communicated with the front end of the anoxic zone; the residual sludge discharge pipe P5 is communicated with the bottom of the sedimentation zone; one end of the nitrifying liquid return pipe P6 is communicated with the bottom of the water collecting bucket of the water outlet area, and the other end of the nitrifying liquid return pipe P6 is communicated with the front end of the anoxic first area; one end of the second sludge return pipe P7 is communicated with the tail end of the anoxic second area, and the other end of the second sludge return pipe P7 is communicated with the front end of the anaerobic area; the first and second sludge return pipes P4, P6 and P7 are respectively provided with a water pump, the first and second sludge return pipes P4, P4 and P6 are respectively provided with a first sludge return pump B2, the second nitrifying liquid return pipe P6 is provided with a second nitrifying liquid return pump B3, and the second sludge return pipe P7 is provided with a second sludge return pump B1.
The stirrers are arranged in the anaerobic zone, the anoxic zone and the flocculation zone, and the specific installation positions can be known by those skilled in the art in combination with the description, the stirrers in the anaerobic zone, the anoxic zone and the anoxic zone are the stirrers with fluidization function, so that the activated sludge in the functional zone is ensured not to be settled, and the stirrer is usually a low-speed stirrer; the stirrer in the flocculation area is a stirrer for mixing the flocculation reagent and the sludge mixed liquid, the flocculation reagent and the sludge mixed liquid are required to be fully mixed, flocs are formed, the rotating speed is high, and vertical stirring is preferred.
A suspension carrier, a first aerator and an interception screen are arranged in the biological membrane area, and an ultrafiltration membrane component and a second aerator are arranged in the water outlet area. The interception screen is arranged in front of the water outlet area, is a porous plate, and a water collecting tank is arranged above the ultrafiltration membrane component and is positioned below the water surface. The suspended carrier is a plastic filler device, can be added into a reactor without fixation, and a biomembrane formed by microorganisms can be attached to and grow on the surface of the reactor, so that pollutants in water are degraded by the microorganisms on the biomembrane, and the density of the biomembrane is similar to that of a water body before and after film formation, so that the biomembrane can be suspended in the water. The filling rate of the suspension carrier is the ratio of the total volume of the suspension carrier in the biological film area under natural accumulation to the volume of the reactor.
The aeration in the biological film zone is oxygenation aeration, which provides dissolved oxygen required in the pollutant degradation process for microorganisms, and does not provide power for fluidization of suspended carriers, the aeration in the water outlet zone is backwash aeration, and impurities attached to the surface of the filtering film are blown off, so that the film flux is ensured.
The interception screen is made of a stainless steel perforated plate, the diameter of the holes is smaller than the diameter of the suspended filler, and the interception screen can intercept suspended carriers in a fixed area and can play a role of a membrane grid, so that large impurities are prevented from entering a water outlet area, and the service life of a membrane assembly is prolonged;
the water collecting tank and the water collecting bucket are designed as local tank bodies of the water outlet area, so that mixed liquid can be collected and stored in one area, a certain capacity is ensured, and water outlet or pipeline connection is facilitated;
the flocculation area dosing pipe is connected with the medicine storage tank, and can be used for dosing chemical agents such as flocculating agent, coagulant and the like to the flocculation area so as to assist flocculation sedimentation of sludge and removal of phosphorus.
By utilizing the MBBR sewage treatment system, an MBBR sewage treatment process is provided, and the concrete steps are as follows:
the inlet water sequentially passes through an anaerobic zone C1, an anoxic zone C2, an anoxic zone C3, a flocculation zone C4, a precipitation zone C5, a biological membrane zone C6 and a water outlet zone C7, so that pollutants are removed; the inflow water flow is Q, the sludge in the sedimentation zone flows back to the front end of the anoxic zone through a first sludge return pipe P4, the return flow of the first sludge return pipe is 0.8-1.2Q, and the residual sludge is discharged through a residual sludge discharge pipe 5; the mixed liquor in the water outlet area flows back to the front end of the anoxic first area through a nitrifying liquor backflow pipe P6, and the nitrifying liquor backflow amount is 1-3Q; and the mixed liquor in the anoxic zone II flows back to the front end of the anaerobic zone through a sludge return pipe II P7 at the tail end of the anoxic zone II, wherein the return quantity of the sludge return pipe II is the average value of the return quantity of the sludge return pipe I and the return quantity of the nitrifying liquor.
The sludge concentration of the anaerobic zone is 3000-5000mg/L, and the sludge concentration of the anoxic first zone and the anoxic second zone is 6000-8000mg/L; the sludge concentration in the biomembrane zone is less than 500mg/L.
The filling rate of the suspended carrier in the biological film area is 30-67%, and the DO of the biological film area is 1-8mg/L; an ultrafiltration membrane component is placed in the water outlet area, and the membrane flux is 18-25L/m 2 And/h, the aeration density of the membrane component is 8-20L/min/m 2 The method comprises the steps of carrying out a first treatment on the surface of the When the filling rate is 30% -50%, the gas-water ratio of the biological film area is 5:1 to 8:1, and the film flux of the water outlet area is 20-25L/m 2 And/h, the aeration density of the membrane component is 8-15L/min/m 2 The method comprises the steps of carrying out a first treatment on the surface of the When the filling rate is 50% -67%, the gas-water ratio of the biological film area is 7:1 to 10:1, and the film flux of the water outlet area is 18-22L/m 2 And/h, the aeration density of the membrane component is 12-20L/min/m 2 。
The invention comprises the following steps:
1) Controlling the DO of the biological membrane area to be 3-5mg/L;
2) When ammonia nitrogen in the effluent of the biological film area is more than 2mg/L, the DO of the biological film area is improved by 10-20 percent until the ammonia nitrogen in the effluent of the biological film area is less than or equal to 2mg/L, and the DO is kept unchanged at the moment;
3) When the water TN of the biological film area is more than 8mg/L, the DO of the biological film area is reduced by 10-20 percent until the water TN of the biological film area is less than or equal to 8mg/L, and the DO is kept unchanged at the moment;
4) And (3) repeating the step 2) and the step 3), and ensuring that ammonia nitrogen in the effluent of the biological film area is less than or equal to 2mg/L and TN in the effluent of the biological film area is less than or equal to 8mg/L.
After being treated by the process of the invention, the indexes of the water discharged from the water outlet are as follows: the TP of the effluent is less than or equal to 0.2mg/L or the TP removal rate is more than or equal to 90 percent, the TN of the effluent is less than or equal to 8mg/L, the SS of the effluent is less than or equal to 6mg/L, and the TN removal load of the system is more than or equal to 0.1kgN/m 3 /d。
The following describes in detail the specific embodiments.
Example 1:
taking the effluent of a primary sedimentation tank of a sewage treatment plant in a certain city as the water inlet of a system, wherein the water quantity is 8.3m 3 The pH value is 6.90, the COD concentration of the inlet water is 120-300 mg/L, the BOD concentration is 60-125 mg/L, the TN concentration is 32-45 mg/L, the ammonia nitrogen concentration is 25-40 mg/L, the TP concentration is 2-6 mg/L, and the SS concentration is 120-200 mg/L. The residence time of the anaerobic zone of the high-efficiency sewage treatment process is 1.5h; anoxic first zone 1.5 hours; the anoxic second zone is 1.5 hours; surface load of precipitation zone 8m 3 /m 2 /h; the residence time of the biological film zone is 2.5h, and the specific surface area of the used suspension carrier is 800m 2 /m 3 The filling rate is 45%; the water outlet area adopts an immersed ultrafiltration membrane component and negative pressure suction type filtration.
During operation, the reflux ratio of nitrifying liquid from the biological film zone to the anoxic zone I is 240%, the reflux ratio from the anoxic zone II to the anaerobic zone is 160%, and the reflux ratio of sludge from the sedimentation zone to the anoxic zone I is 80%. The sludge concentration in the anaerobic zone is 4000mg/L, the sludge concentration in the anoxic zone I and II is kept 7000mg/L, and the sludge concentration in the biological film zone is about 400mg/L. Adding flocculant in the flocculation area to assist in sludge sedimentation and dephosphorization.
Controlling the air-water ratio of the biological film area to be 7.5:1, and DO to be 3.5-4.5 mg/L. The membrane flux of the water outlet area is 18-20L/m 2 And/h, the aeration density of the membrane component is about 12L/min/m 2 。
After treatment, the COD concentration of the total effluent is less than or equal to 30mg/L, the TN concentration is less than or equal to 7mg/L, the ammonia nitrogen concentration is less than or equal to 1.5mg/L, the TP concentration is less than or equal to 0.15mg/L, and the SS concentration is less than or equal to 5mg/L.
Example 2:
the effluent of the regulating tank of a sewage treatment station in a certain village and town is taken as the water inlet of the system, and the water quantity is 4.2m 3 The pH value is 6.90, the COD concentration of the inflow water is 100-400 mg/L, the BOD concentration is 50-225 mg/L, the TN concentration is 25-45 mg/L, the ammonia nitrogen concentration is 20-40 mg/L, the TP concentration is 3-8 mg/L, and the SS concentration is 150-250 mg/L. The residence time of the anaerobic zone is 1.5 hours; anoxic first zone 1.0h; the anoxic second zone is 1.5 hours; surface load of precipitation zone 8m 3 /m 2 /h; the residence time of the biological film area is 3h, and the specific surface area of the used suspension carrier is 800m 2 /m 3 The filling rate is 50%; an immersed membrane component and negative pressure suction type filtration are arranged in the water outlet area.
When the device is operated, the reflux ratio of nitrifying liquid from the biological film zone to the anoxic zone I is 200%, the reflux ratio from the anoxic zone II to the anaerobic zone is 150%, and the reflux ratio of sludge from the sedimentation zone to the anoxic zone I is 100%. The sludge concentration in the anaerobic zone is 4500mg/L, the sludge concentration in the anoxic zone and the anoxic zone is 7500mg/L, and the sludge concentration in the biological film zone is about 300mg/L. Adding flocculant in the flocculation area to assist in sludge sedimentation and dephosphorization.
Controlling the air-water ratio of the biological film area to be 7:1 and DO to be 4-4.5 mg/L. The membrane flux of the water outlet area is 20-22L/m 2 And/h, the aeration density of the membrane component is about 10L/min/m 2 。
After treatment, the COD concentration of the total effluent of the process system is less than or equal to 25mg/L, the TN concentration is less than or equal to 6mg/L, the ammonia nitrogen concentration is less than or equal to 1.0mg/L, the TP concentration is less than or equal to 0.15mg/L, and the SS concentration is less than or equal to 5mg/L.
The parts not described in the above modes can be realized by adopting or referring to the prior art.
It is noted that any equivalent or obvious modification made by those skilled in the art under the teachings of this specification shall fall within the scope of this invention.
Claims (6)
1. An MBBR sewage treatment process, uses an MBBR sewage treatment system, its characterized in that: the anaerobic treatment device comprises an anaerobic zone, an anoxic zone, a flocculation zone, a sedimentation zone, a biological film zone and a water outlet zone which are sequentially connected from front to back, wherein adjacent zones are separated by partition walls, the partition walls are provided with communication ports, and the adjacent zones are communicated by opening the communication ports;
the anaerobic zone is connected with a water inlet pipe, the water outlet zone is connected with a water outlet pipe, sewage to be treated enters through the water inlet pipe, and is discharged from the water outlet pipe after being treated;
the flocculation zone is connected with a dosing pipe, the bottom of the sedimentation zone is connected with a first sludge return pipe and a residual sludge discharge pipe, the other end of the first sludge return pipe is connected to the anoxic zone, and the residual sludge discharge pipe is used for discharging residual sludge;
a nitrifying liquid return pipe is connected between the water outlet area and the anoxic first area, and a sludge return pipe II is connected between the anaerobic area and the anoxic second area;
the anaerobic zone, the anoxic zone and the flocculation zone are respectively provided with a stirrer, the biological membrane zone is internally provided with a suspension carrier, an aerator I and an interception screen, and the water outlet zone is internally provided with an ultrafiltration membrane component and an aerator II;
the interception screen is arranged in front of a water outlet of the water outlet area and is a porous plate, a water collecting tank is arranged above the ultrafiltration membrane component, and the water collecting tank is positioned below the water surface;
the process comprises the following steps:
the sewage to be treated enters an anaerobic zone through a water inlet pipe, the water inlet flow is set to be Q, the sewage stays in the anaerobic zone for a period of time, the sewage flows into an anoxic zone I, an anoxic zone II and a flocculation zone in sequence through a communication port, a certain amount of medicament is added into the sewage through a medicament adding pipe in the flocculation zone, the sewage enters a sedimentation zone under the stirring effect, sludge in the sedimentation zone flows back to the front end of the anoxic zone I through a sludge return pipe I, the return flow of the sludge return pipe I is 0.8-1.2Q, and residual sludge is discharged through a residual sludge discharge pipe;
supernatant fluid of the sedimentation zone sequentially enters a biological membrane zone and a water outlet zone, mixed liquid in the water outlet zone flows back to the front end of the anoxic zone through a nitrifying liquid return pipe, and the nitrifying liquid return amount is 1-3Q; the mixed liquor in the anoxic zone II flows back to the front end of the anaerobic zone through a sludge return pipe II at the tail end of the anoxic zone II, and the return quantity of the sludge return pipe II is the average value of the return quantity of the sludge return pipe I and the return quantity of nitrifying liquor;
ammonia nitrogen in effluent of the biological film area is less than or equal to 2mg/L, and TN in effluent of the biological film area is less than or equal to 8mg/L; when ammonia nitrogen in the effluent of the biological film area is more than 2mg/L, the DO of the biological film area is improved by 10-20 percent until the ammonia nitrogen in the effluent of the biological film area is less than or equal to 2mg/L, and the DO is kept unchanged at the moment; when the water TN of the biological film area is more than 8mg/L, the DO of the biological film area is reduced by 10-20 percent until the water TN of the biological film area is less than or equal to 8mg/L, and the DO is kept unchanged at the moment;
the water indexes discharged from the water outlet of the water outlet area are as follows: the TP of the effluent is less than or equal to 0.2mg/L or the TP removal rate is more than or equal to 90 percent, the TN of the effluent is less than or equal to 8mg/L, the SS of the effluent is less than or equal to 6mg/L, and the TN removal load of the system is more than or equal to 0.1kgN/m 3 /d。
2. The MBBR sewage treatment process according to claim 1, wherein: and the first sludge return pipe, the nitrifying liquid return pipe and the second sludge return pipe are respectively provided with a water pump.
3. The MBBR sewage treatment process according to claim 1, wherein: the first aerator is an oxygenation aerator, and the second aerator is a back flush aerator.
4. The MBBR sewage treatment process according to claim 1, wherein: the stirrer in the flocculation zone is a vertical stirrer.
5. The MBBR sewage treatment process according to claim 1, wherein: the sludge concentration in the anaerobic zone is 3000-5000mg/L; the sludge concentration in the anoxic first area and the anoxic second area is 6000-8000mg/L; the sludge concentration of the biological film area is less than 500mg/L.
6. The MBBR sewage treatment process according to claim 1, wherein: the filling rate of the suspended carrier in the biological film area is 30-67%, and the DO in the biological film area is 1-8mg/L; membrane flux in the water outlet area18-25L/m 2 And/h, the aeration density of the ultrafiltration membrane component is 8-20L/min/m 2 ；
When the filling rate is 30% -50%, the gas-water ratio of the biological film area is 5:1 to 8:1, and the film flux of the water outlet area is 20-25L/m 2 And/h, the aeration density of the ultrafiltration membrane component is 8-15L/min/m 2 ；
When the filling rate is 50% -67%, the gas-water ratio of the biological film area is 7:1 to 10:1, and the film flux of the water outlet area is 18-22L/m 2 And/h, the aeration density of the ultrafiltration membrane component is 12-20L/min/m 2 。
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| CN109289258B (en) * | 2018-10-30 | 2024-03-01 | 青岛思普润水处理股份有限公司 | Water treatment sedimentation tank |
| CN110104910A (en) * | 2019-06-21 | 2019-08-09 | 安吉国千环境科技有限公司 | A kind of sewage disposal technology method based on MBBR technique |
| CN112551822B (en) * | 2020-12-22 | 2023-11-24 | 青岛思普润水处理股份有限公司 | MBBR (moving bed biofilm reactor) system for enhanced ammonia nitrogen treatment of flocculation sedimentation tank and operation method |
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