CN108585385A - A kind of MBBR sewage disposal systems and treatment process - Google Patents
A kind of MBBR sewage disposal systems and treatment process Download PDFInfo
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- CN108585385A CN108585385A CN201810693196.5A CN201810693196A CN108585385A CN 108585385 A CN108585385 A CN 108585385A CN 201810693196 A CN201810693196 A CN 201810693196A CN 108585385 A CN108585385 A CN 108585385A
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- 239000010865 sewage Substances 0.000 title claims abstract description 45
- 238000000034 method Methods 0.000 title claims abstract description 38
- 230000008569 process Effects 0.000 title claims abstract description 28
- 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 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 73
- 239000010802 sludge Substances 0.000 claims abstract description 67
- 239000012528 membrane Substances 0.000 claims abstract description 44
- 238000005189 flocculation Methods 0.000 claims abstract description 26
- 230000016615 flocculation Effects 0.000 claims abstract description 24
- 230000004907 flux Effects 0.000 claims abstract description 14
- 238000011049 filling Methods 0.000 claims abstract description 13
- 238000010992 reflux Methods 0.000 claims abstract description 13
- 238000012545 processing Methods 0.000 claims abstract description 6
- 239000007788 liquid Substances 0.000 claims description 25
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 14
- 238000005276 aerator Methods 0.000 claims description 12
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 10
- 229910052760 oxygen Inorganic materials 0.000 claims description 10
- 239000001301 oxygen Substances 0.000 claims description 10
- 239000000126 substance Substances 0.000 claims description 9
- 238000004891 communication Methods 0.000 claims description 7
- 239000003814 drug Substances 0.000 claims description 6
- 238000005192 partition Methods 0.000 claims description 6
- 239000006228 supernatant Substances 0.000 claims description 5
- 238000000108 ultra-filtration Methods 0.000 claims description 5
- 230000008030 elimination Effects 0.000 claims description 3
- 238000003379 elimination reaction Methods 0.000 claims description 3
- 238000003756 stirring Methods 0.000 claims description 3
- 230000009471 action Effects 0.000 claims description 2
- 238000006213 oxygenation reaction Methods 0.000 claims 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 20
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 abstract description 17
- 229910052698 phosphorus Inorganic materials 0.000 abstract description 17
- 239000011574 phosphorus Substances 0.000 abstract description 17
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 15
- 229910052799 carbon Inorganic materials 0.000 abstract description 15
- 230000000694 effects Effects 0.000 abstract description 15
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 11
- 238000005273 aeration Methods 0.000 abstract description 9
- 238000001914 filtration Methods 0.000 abstract description 4
- 229910019142 PO4 Inorganic materials 0.000 abstract description 3
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 abstract description 3
- 239000010452 phosphate Substances 0.000 abstract description 3
- 230000001360 synchronised effect Effects 0.000 abstract description 3
- 238000000926 separation method Methods 0.000 description 7
- 238000011068 loading method Methods 0.000 description 6
- 244000005700 microbiome Species 0.000 description 6
- 229910002651 NO3 Inorganic materials 0.000 description 4
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 3
- 239000000969 carrier Substances 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-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
- 230000008859 change Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000005243 fluidization Methods 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- BHEPBYXIRTUNPN-UHFFFAOYSA-N hydridophosphorus(.) (triplet) Chemical compound [PH] BHEPBYXIRTUNPN-UHFFFAOYSA-N 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 230000000813 microbial effect Effects 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- 241000894006 Bacteria Species 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 241000605159 Nitrobacter Species 0.000 description 1
- 229920000388 Polyphosphate Polymers 0.000 description 1
- 229920000037 Polyproline Polymers 0.000 description 1
- 241000589516 Pseudomonas Species 0.000 description 1
- GQENKOUTFPKGLE-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3].[OH4+2] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3].[OH4+2] GQENKOUTFPKGLE-UHFFFAOYSA-N 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 238000005842 biochemical reaction Methods 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000000701 coagulant Substances 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910001882 dioxygen Inorganic materials 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 238000004146 energy storage Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 238000007667 floating Methods 0.000 description 1
- -1 flocculant Substances 0.000 description 1
- 230000003311 flocculating effect Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 230000006870 function Effects 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 238000007654 immersion Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000007726 management method Methods 0.000 description 1
- 238000005374 membrane filtration Methods 0.000 description 1
- 239000010841 municipal wastewater Substances 0.000 description 1
- 238000006396 nitration reaction Methods 0.000 description 1
- 230000001546 nitrifying effect Effects 0.000 description 1
- 230000009935 nitrosation Effects 0.000 description 1
- 238000007034 nitrosation reaction Methods 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000001205 polyphosphate Substances 0.000 description 1
- 235000011176 polyphosphates Nutrition 0.000 description 1
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 238000001556 precipitation 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
- 230000009466 transformation Effects 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
- 239000003403 water pollutant Substances 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
Landscapes
- 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 kind of MBBR sewage disposal systems and treatment process, belong to technical field of sewage.The problem which solve sewage treatment plant's processing technological flows traditional in the prior art is long, integrated level is low, load is low, the removal effect of and nitrogen high to carbon source demand, phosphorus, SS are general.It includes anaerobic zone, one area of anoxic, 2nd area of anoxic, flocculation zone, settling zone, biomembrane area, exhalant region and the pipeline for connecting above-mentioned zone, pass through the setting etc. of suspending carrier filling rate, the parameter setting of DO and exhalant region inner membrane member membrane flux, aeration density in the control of adjustment, sludge concentration to reflux and biomembrane area.Settling zone is set to the stage casing of biochemical treatment by the characteristics of using Denitrifying Phosphate Accumulating Organisms, and biomembrane process is coupled with filtering membrane process, with integrated level height, synchronous denitrification dephosphorizing and saving carbon source, water outlet nitrogen, phosphorus, SS concentration are low, and load is high, service life of equipment is long.
Description
Technical field
The present invention relates to MBBR technical field of sewage, and in particular to a kind of MBBR sewage disposal systems and processing work
Skill.
Background technology
In order to strengthen the protection to water environment, to sewage disposal plant effluent water quality, more stringent requirements are proposed for country, tradition
Sewage treatment plant's two stage treatment technological process, it is general to the removal effect of nitrogen, phosphorus, and volumetric loading is low, takes up a large area；
Gravity type mud-water separation is discharged SS higher, cannot meet higher and higher water outlet SS requirements.This 2 points are traditional two stage treatment works
In place of the technological lag of skill flow.
Using MBBR (Moving Bed Biofilm Reactor, moving bed biofilm reactor) technique, to reactor
In add a certain number of suspending carriers, as the carrier of attached growth of microorganisms, due on carrier biomembrane not by spoil disposal
Engineering sludge age limit, can be enriched with more how long sludge age flora, especially nitrifier, obtain efficient Ammonia Nitrification effect, load
Height, water outlet ammonia nitrogen concentration are low.And MBBR also there is occupation of land to save, capital cost is low, and the advantages that flexibly simple is built in transformation.At present
MBBR techniques are mostly combined with activated sludge, are coexisted in a pond body, and control condition mutually restricts, and cannot play MBBR techniques
Maximum effect.
It in terms of mud-water separation, substitutes gravity using MBR ultrafiltration membrance filters and carries out mud-water separation, obtain low SS water outlets, and
The development trend of the following mud-water separation, but directly filtered in active sludge intermixture, there are high energy consumption, film easily blocks, from
And the problems such as reducing the service life of film, increasing energy consumption and depreciation.
At present there are also the technology mode that MBBR suspending carriers technique is combined with MBR filter membranes, specific research has：
107311405 A of CN disclose a kind of urban sewage treatment system and technique, are with AAO technological processes only
Basis, anoxic, it is aerobic in add suspending carrier after, simply connect with MBR after sedimentation basin precipitates, technological process is long, MBR
Only play the filtration of advanced treating.
107285467 A of CN disclose a kind of MBBR for water treatment plant and MBR integrated techniques and equipment, are
It is simple that anoxic zone is set and MBR membrane modules are positioned in MBBR biological tanks, although technological process is short, and declare that MBBR suspends
Carrier can clean MBR film surfaces, but MBBR suspending carriers can scratch MBR films, substantially reduce in fluid mapper process
The service life of MBR films.And all only the removal of nitrogen and the removal effect of SS are strengthened, it is not strong to the removal of phosphorus
Change, also without solution nitrogen, phosphorus to the race problem of carbon source.
Invention content
The purpose of the present invention is to provide a kind of MBBR sewage disposal systems to go out with nitrogen, phosphorus, SS high treating effects
Water concentration is low, and utilization of carbon source rate is high, and level of integrated system is high, and statistics load is high, takes up an area the advantages that few.
To achieve the above object, the technical issues of overcoming needed for the present invention has：
How to be arranged by rational functional area and flowed back and is arranged to solve due to being limited to VFA contents in water-inlet carbon source
And nitrogen denitrification to the competition of carbon source and caused by dephosphorization phosphor-removing effect difference problem；And the process of aerobic phosphorous accumulating is allowed to exist
Anoxic zone containing molecular oxygen nitrate nitrogen can be realized, that is to say, that the characteristics of how utilizing DPB, it can be by lacking
Behind oxygen area, the phosphorus element in sewage is transferred in sludge, is allowed that sedimentation basin can be arranged in anoxic section rear end, is carried out muddy water point
From without being arranged after aerobic tank.
In order to solve the above technical problems, using following technical solution：
A kind of MBBR sewage disposal systems comprising go to rear sequentially connected anaerobic zone, one area of anoxic, anoxic two certainly
Area, flocculation zone, settling zone, biomembrane area and exhalant region, adjacent region are separated by partition wall, and connection is both provided on the partition wall
Mouthful, adjacent region keeps connection by opening the communication port；
The anaerobic zone is connected with water inlet pipe, and the exhalant region is connected with outlet pipe, treatment sewage through it is described into
Water pipe enters, and is discharged after processing from the outlet pipe；
The flocculation zone is connected with chemical feed pipe, and the settling zone bottom is connected with mud return line one and excess sludge
The other end of delivery pipe, one pipe of sludge reflux is connected to one area of the anoxic, and the excess sludge delivery pipe is used for will
Excess sludge is discharged；
Be connected with nitrification liquid return duct between the exhalant region and one area of anoxic, the anaerobic zone with it is described
2nd area of anoxic between be connected with mud return line two；
It is respectively arranged with blender in the anaerobic zone, one area of anoxic, 2nd area of anoxic and flocculation zone, in the life
It is disposed with suspending carrier, aerator one in the areas Wu Mo and intercepts sieve, hyperfiltration membrane assembly and exposure are provided in the exhalant region
Gas device two.
As a preferred solution of the present invention, the mud return line one, nitrification liquid return duct and mud return line
Water pump is both provided on two.
As the present invention another preferred embodiment, the interception sieve be arranged the exhalant region water outlet it
Before, it is porous plate, is provided with catch basin above the hyperfiltration membrane assembly, the catch basin is located at the water surface or less.
Further, the aerator one is oxygenic aeration device, and the aerator two is backwash aerator.
Further, it is vertical stirrer to be located at the blender in flocculation zone.
The present invention another task be to provide a kind of MBBR sewage treatment process, use above-mentioned MBBR sewage disposals system
System comprising following steps：
Treatment sewage enters through water inlet pipe in anaerobic zone, and flow of inlet water is set as Q, when stopping one section in anaerobic zone
Between, it flows into one area of anoxic, 2nd area of anoxic and flocculation zone successively through communication port, is added thereto centainly by chemical feed pipe in flocculation zone
The medicament of amount, subsequently enters settling zone under the action of stirring, and settling zone sludge is back to anoxic one by mud return line one
The regurgitant volume of area front end, mud return line one is 0.8-1.2Q, and excess sludge passes through excess sludge discharged；
Biomembrane area, exhalant region are sequentially entered through its supernatant of settling zone, exhalant region mixed liquor passes through nitrification liquid return duct
It is back to one area front end of anoxic, nitrification liquid regurgitant volume is 1-3Q；Two area's mixed liquor of anoxic is returned by the sludge of two area end of anoxic
Flow tube two is back to anaerobic zone front end, and two regurgitant volume of mud return line is one regurgitant volume of mud return line and nitrification liquid regurgitant volume
Average value.
Further, the anaerobic zone sludge concentration is 3000-5000mg/L；One area of the anoxic, two area's sludge of anoxic
A concentration of 6000-8000mg/L；The biomembrane area sludge concentration ＜ 500mg/L.
Further, suspending carrier filling rate is 30-67% in the biomembrane area, and the biomembrane area DO is in 1-8mg/
L；Membrane flux 18-25L/m in the exhalant region2/ h, hyperfiltration membrane assembly are aerated density 8-20L/min/m2；
When filling rate is 30%-50%, biomembrane area gas-water ratio is 5:1 to 8:1, exhalant region membrane flux is 20-25L/
m2/ h, it is 8-15L/min/m that hyperfiltration membrane assembly, which is aerated density,2；
When filling rate is 50%-67%, biomembrane area gas-water ratio is 7:1 to 10:1, exhalant region membrane flux 18-22L/
m2/ h, ultrafiltration membrane membrane module are aerated density 12-20L/min/m2。
Further, the water outlet ammonia nitrogen≤2mg/L in biomembrane area, biomembrane area are discharged TN≤8mg/L；When biomembrane area goes out
Water ammonia nitrogen>When 2mg/L, biomembrane area DO 10-20% are improved, until biomembrane area is discharged ammonia nitrogen≤2mg/L, keep DO at this time
It is constant；When biomembrane area is discharged TN>When 8mg/L, biomembrane area DO 10-20% are reduced, until biomembrane area is discharged TN≤8mg/
L, DO is constant at this time for holding.
Further, through exhalant region water outlet be discharged water index be：Be discharged TP≤0.2mg/L or TP removal rates >=
90%, it is discharged TN≤8mg/L, is discharged SS≤6mg/L, system TN elimination capacities >=0.1kgN/m3/d。
The present invention is noteworthy characterized by, and using DPB (Denitrifying Phosphate Accumulating Organisms), in anaerobic phosphorus release and absorbs carbon source storage energy
Afterwards, the characteristics of oxygen being replaced to inhale phosphorus as electron acceptor excess using nitrate, the process of aerobic phosphorous accumulating is allowed to contain molecule
The anoxic zone of state oxygen nitrate nitrogen can be realized, that is, the characteristics of utilizing DPB, it can be behind anoxic zone, in sewage
Phosphorus element is transferred in sludge, is allowed that settling zone can be arranged in anoxic section rear end, is carried out mud-water separation, without being arranged good
Behind oxygen area.
Serve mud-water separation settling zone be located at anoxic zone after, the stage casing of entire biochemical reaction, and unconventional biochemistry
Section end (aeration zone).The biomembrane area that supernatant enters behind settling zone, inactive sludge in biomembrane area, using on carrier
The microbial film of enrichment nitrifies ammonia nitrogen, realizes in an Installed System Memory in two kinds of sludge concentrations, anaerobic zone, anoxic zone
Interior sludge concentration is high, carries out the denitrification for releasing phosphorus, poly- phosphorus and nitrate nitrogen, plays in the biomembrane area of nitrification sludge concentration then
It is very low.
After water outlet enters subsequent exhalant region, the SS concentration in mixed liquor is low, it is possible to reduce to exhalant region inner membrane member
Abrasion extends system service life.
Advantageous effects caused by the present invention are：
1) biological phosphor-removing effect is good, and anaerobic zone water inlet includes total mixed liquor intake and flow back from 2nd area of anoxic, anoxic two
The mixed liquor of area end, due to have passed through sufficient denitrification phosphorus-collecting reaction, nitrate concentration is low, after being back to anaerobic zone, no
The anaerobic phosphorus release energy storage for influencing polyP bacteria, to more fully ensure that the effect of biochemical dephosphorization；
2) denitrification volumetric loading is high, and process section end is set to different from the settling zone of traditional two stage treatment technique, this
The settling zone of invention sewage disposal system is set among process section, is discharged non-final water outlet, without having to worry about entrance settling zone
Sludge concentration is excessively high to cause settling zone water outlet SS exceeded, therefore anoxic zone can be allowed to have high sludge concentration, in identical dirt
Under mud load, volumetric loading higher；
3) carbon source, the energy make full use of, and a carbon is multi-purpose, the reflux setting of sewage disposal system of the present invention first, available
The characteristics of DPB Denitrifying Phosphate Accumulating Organisms synchronous denitrifying phosphorus removals, for poly- phosphorus using nitrate nitrogen as electron acceptor, a carbon is dual-purpose.This
Outside, anoxic zone high concentration sludge is precipitated conducive to internal carbon source, can more utilize the endogenous carbon source of system, in water-inlet carbon source deficiency
When, save the non-use of additional carbon.And after settling zone is located at anoxic zone, it is good to avoid carbon source for sludge and without aerobic region
Oxygen is degraded, and can be entered in sludge, improves resource, the energy recovery value of sludge, and what poly- phosphorus utilized is combined oxygen
NO3, reduce the demand to dissolved oxygen, reduce energy consumption；
4) nitrification is abundant, and load is high, and behind settling zone, supernatant enters biomembrane area, since suspending carrier is blocked by sieve
It cuts in fixed area, is conducive to the attachment and growth of the longer microorganism of sludge age, especially nitrosation Pseudomonas and Nitrobacter, nitre
It is good to change effect, can fully nitrify the ammoniacal nitrogen in sewage；
5) a kind of microbial morphology of biomembrane on suspending carrier, operational management and regulation and control letter are only existed in biomembrane area
It is single, and load height is nitrified, meanwhile, using the multilayered structure of biomembrane, can provide favorably for synchronous nitration and denitrification
Condition enhances the removal effect to nitrogen；
6) extend the service life of filter membrane, sewage disposal system of the present invention is provided with settling zone, warp before biomembrane area
The supernatant crossed after precipitation enters biomembrane area, carries out nitrifying process by the microorganism adhered on the suspending carrier in pond, goes out
Water SS concentration is far below active sludge intermixture, it is possible to reduce the filter pressure of film improves membrane flux, reduces the flushing of film and clear
Frequency is washed, the service life of film is extended；
7) load is high, takes up an area and saves, and using sewage disposal system of the present invention, the sludge concentration of anaerobic zone and anoxic zone is high, raw
The areas Wu Mo rely on the nitrification effect of carrier high-efficiency, and volumetric loading is all very high, save pool capacity and take up an area, final mud-water separation goes out hydromining
With membrane filtration, effect takes up an area well province, and level of integrated system is high, although having good removal effect to each index, takes up an area
It saves very much；
8) sewage plant is widely used in create, be transformed, integrated equipment for sewage treatment.
Description of the drawings
The present invention will be further described below in conjunction with the accompanying drawings：
Fig. 1 is MBBR sewage disposal systems structure diagram of the present invention；
In figure：
C1-anaerobic zone, one area of C2-anoxic, 2nd area of C3-anoxic, C4-flocculation zone, C5-settling zone, C6-biomembrane
Area, C7-exhalant region, S1-anaerobic zone blender, one area's blender of S2-anoxic, two area's blender of S3-anoxic, S4-flocculation
Area's blender, S5-suspending carrier, S6-biomembrane area aeration, S7-interception sieve, S8-exhalant region aeration, S9-ultrafiltration
Film, P1-water inlet pipe, P2-outlet pipe, P3-chemical feed pipe, P4-mud return line one, P5-excess sludge delivery pipe, P6-
Nitrification liquid return duct, P7-mud return line two, B1-sludge reflux pump two (water pump), B2-sludge reflux pump one (water pump),
B3-nitrification liquid reflux pump (water pump).
Specific implementation mode
The present invention proposes a kind of MBBR sewage disposal systems and treatment process, in order to make advantages of the present invention, technical side
Case is clearer, clear, elaborates to the present invention with reference to specific embodiment.
First, it elaborates to MBBR sewage disposal systems of the present invention in conjunction with Fig. 1, goes to rear (from left to right) certainly successively
Including anaerobic zone C1, one area C2 of anoxic, two area C3 of anoxic, flocculation zone C4, settling zone C5, biomembrane area C6, exhalant region C7 and phase
Process pipe is closed, adjacent region is separated by partition wall, communication port is both provided on partition wall, adjacent region is by opening communication port
It includes water inlet pipe P1, outlet pipe P2, chemical feed pipe P3, one P4 of mud return line, excess sludge row to keep connection, related process pipeline
Put pipe P5, nitrification liquid return duct P6, two P7 of mud return line.Wherein, water inlet pipe P1 is communicated with anaerobic zone front end；Outlet pipe P2 with
Exhalant region hyperfiltration membrane assembly communicates；Chemical feed pipe P3 is communicated with flocculation zone water inlet end；One one end P4 of mud return line and settling zone bottom
Portion communicates, and the other end is communicated with one area front end of anoxic；Excess sludge delivery pipe P5 is communicated with settling zone bottom；Nitrification liquid return duct
The one end P6 is communicated with exhalant region drip pan bottom, and the other end is communicated with one area front end of anoxic；Two one end P7 of mud return line with lack
Two area end of oxygen communicates, and the other end is communicated with anaerobic zone front end；One P4 of mud return line, nitrification liquid return duct P6, sludge reflux
It is equipped with water pump on two P7 of pipe, one B2 of sludge reflux pump is set respectively on one P4 of mud return line, in nitrification liquid return duct
Nitrification liquid reflux pump B3 is set on P6, two B1 of sludge reflux pump is set on two P7 of mud return line.
It is mounted on blender, specific installation site ability in above-mentioned anaerobic zone, one area of anoxic, 2nd area of anoxic, flocculation zone
Field technique personnel in combination with learning herein, anaerobic zone, one area of anoxic, 2nd area of anoxic blender be the stirring of fluidization
Device, the activated sludge in assurance function area do not settle, usually low-speed agitator；Blender in flocculation zone has been mixing
The blender of flocculation medicament and mud mixed liquid need to allow flocculation medicament to be sufficiently mixed with mud mixed liquid, and form flco, rotating speed
Comparatively fast, preferably vertical mixing.
It is disposed with suspending carrier, aerator one in biomembrane area and intercepts sieve, ultrafiltration membrane is provided in exhalant region
Component and aerator two.It intercepts sieve to be arranged before the water outlet of exhalant region, is porous plate, is arranged above hyperfiltration membrane assembly
There are catch basin, catch basin to be located at the water surface or less.Suspending carrier is a kind of plastics filler equipment, can be added in reactor,
Without fixation, the biomembrane that microorganism is constituted can be with apposition growth on its surface, by the microorganism on biomembrane in water
Pollutant is degraded, and with water body similar density before and after biofilm, makes it that can suspend in water.Suspending carrier filling rate is biology
Suspending carrier in film area, the total volume under natural packing, the ratio with reactor volume.
Aeration is oxygenic aeration in above-mentioned biomembrane area, and required dissolving during degradation of contaminant is provided for microorganism
Oxygen, not the fluidisation of suspending carrier power is provided, the aeration in exhalant region is that backwash is aerated, the attachment of stripping filter membrane surface
Impurity ensures membrane flux.
Above-mentioned interception sieve makes for stainless steel perforated plate, and eye diameter is less than the ruler diameter of floating stuffing, can intercept outstanding
Float carrier is used for this system, can also play the role of film grid, big impurity is avoided to enter exhalant region in fixed region,
Influence the service life of membrane module；
Above-mentioned catch basin, the local Pool body design that drip pan is exhalant region, mixed liquor can be allowed to collect and stored one
In region, and ensure certain capacity, convenient for being discharged or linking pipeline；
Above-mentioned flocculation zone chemical feed pipe, is connected with medicine storing pot, can be that flocculation zone adds the chemical drugs such as flocculant, coagulant
Agent assists the removal of the flocculating setting and phosphorus of sludge.
Using above-mentioned MBBR sewage disposal systems, MBBR sewage treatment process is proposed, the specific steps are：
Water inlet passes sequentially through anaerobic zone C1, one area C2 of anoxic, two area C3 of anoxic, flocculation zone C4, settling zone C5, biomembrane area
C6, exhalant region C7, realize the removal of pollutant；Flow of inlet water is Q, and settling zone sludge is back to scarce by one P4 of mud return line
One area front end of oxygen, one regurgitant volume of mud return line are 0.8-1.2Q, and excess sludge is discharged by excess sludge delivery pipe 5；Water outlet
Area's mixed liquor is back to one area front end of anoxic by nitrification liquid return duct P6, and nitrification liquid regurgitant volume is 1-3Q；2nd area of anoxic mixes
Liquid is back to anaerobic zone front end by two P7 of mud return line of two area end of anoxic, and two regurgitant volume of mud return line is returned for sludge
The average value of flow tube one regurgitant volume and nitrification liquid regurgitant volume.
Above-mentioned anaerobic zone sludge concentration is 3000-5000mg/L, and one area of anoxic, two area's sludge concentration of anoxic are 6000-
8000mg/L；Biomembrane area sludge concentration ＜ 500mg/L.
Suspending carrier filling rate is 30-67% in above-mentioned biomembrane area, and biomembrane area DO is in 1-8mg/L；It is put in exhalant region
Set hyperfiltration membrane assembly, membrane flux 18-25L/m2/ h, membrane module are aerated density 8-20L/min/m2；As filling rate 30%-50%,
Biomembrane area gas-water ratio 5:1 to 8:1, exhalant region membrane flux is 20-25L/m2/ h, membrane module are aerated density 8-15L/min/m2；When
Filling rate 50%-67%, biomembrane area gas-water ratio 7:1 to 10:1, exhalant region membrane flux 18-22L/m2/ h, membrane module aeration are close
Spend 12-20L/min/m2。
Present invention process step, is sequentially controlled according to the following steps：
1) control biomembrane area DO is in 3-5mg/L；
2) when biomembrane area is discharged ammonia nitrogen>When 2mg/L, biomembrane area DO10-20% is improved, until biomembrane area is discharged ammonia
Nitrogen≤2mg/L, DO is constant at this time for holding；
3) when biomembrane area is discharged TN>When 8mg/L, biomembrane area DO10-20% is reduced, until biomembrane area water outlet TN≤
8mg/L, DO is constant at this time for holding；
4) step 2) and step 3) are repeated, ensures that biomembrane area is discharged ammonia nitrogen≤2mg/L, biomembrane area is discharged TN≤8mg/
L。
After present invention process is handled, the water index being discharged from water outlet is：Be discharged TP≤0.2mg/L or TP removal rates >=
90%, it is discharged TN≤8mg/L, is discharged SS≤6mg/L, system TN elimination capacities >=0.1kgN/m3/d。
It elaborates with reference to specific embodiment.
Embodiment 1：
It intakes using the water outlet of certain Primary Settling Tanks of Municipal Wastewater Treatment Plant as system, water 8.3m3/ h, pH mean value 6.90, water inlet
COD concentration 120~300mg/L, BOD concentration 60~125mg/L, TN 32~45mg/L of concentration, ammonia nitrogen concentration 25~40mg/L, TP
120~200mg/L of concentration 2~6mg/L, SS concentration.High-efficiency sewage treatment process anaerobic zone residence time 1.5h；One area of anoxic
1.5h；Two area 1.5h of anoxic；Settling zone surface loading 8m3/m2/h；Biomembrane area residence time 2.5h, suspending carrier used compare table
Area 800m2/m3, filling rate 45%；Exhalant region uses immersion hyperfiltration membrane assembly, negative pressure suction type filtering.
When operation, biomembrane area to one area's mixed liquid recycle ratio 240% of anoxic, 2nd area of anoxic to anaerobic zone reflux ratio
160%, settling zone to one area's return sludge ratio 80% of anoxic.Anaerobic zone sludge concentration 4000mg/L, one area of anoxic, two area's sludge
Concentration keeps 7000mg/L, sludge concentration about 400mg/L in biomembrane area.Flocculant is added in flocculation zone, assists sludge settling
And dephosphorization.
Control biomembrane area gas-water ratio 7.5:1, DO in 3.5~4.5mg/L.Exhalant region membrane flux is 18-20L/m2/ h, film
Component is aerated density about 12L/min/m2。
By processing, the COD concentration≤30mg/L being always discharged, TN concentration≤7mg/L, ammonia nitrogen concentration≤1.5mg/L, TP is dense
Degree≤0.15mg/L, SS concentration≤5mg/L.
Embodiment 2：
It intakes using certain small towns Sewage Disposal regulating reservoir water outlet as system, water 4.2m3/ h, pH mean value 6.90, water inlet
COD concentration 100~400mg/L, BOD concentration 50~225mg/L, TN 25~45mg/L of concentration, ammonia nitrogen concentration 20~40mg/L, TP
150~250mg/L of concentration 3~8mg/L, SS concentration.Anaerobic zone residence time 1.5h；One area 1.0h of anoxic；Two area 1.5h of anoxic；
Settling zone surface loading 8m3/m2/h；Biomembrane area residence time 3h, suspending carrier specific surface area 800m used2/m3, filling rate
50%；Immersed membranes component, negative pressure suction type filtering are set in exhalant region.
When operation, biomembrane area to one area's mixed liquid recycle ratio 200% of anoxic, 2nd area of anoxic to anaerobic zone reflux ratio
150%, settling zone to one area's return sludge ratio 100% of anoxic.Anaerobic zone sludge concentration 4500mg/L, one area of anoxic, 2nd area are dirty
Mud concentration keeps 7500mg/L, sludge concentration about 300mg/L in biomembrane area.Flocculant is added in flocculation zone, auxiliary sludge is heavy
Drop and dephosphorization.
Control biomembrane area gas-water ratio 7:1, DO in 4~4.5mg/L.Exhalant region membrane flux is 20-22L/m2/ h, membrane module
It is aerated density about 10L/min/m2。
By processing, COD concentration≤25mg/L that process system is always discharged, TN concentration≤6mg/L, ammonia nitrogen concentration≤
1.0mg/L, TP concentration≤0.15mg/L, SS concentration≤5mg/L.
It takes or uses for reference prior art and can be realized in the part that do not addressed in aforesaid way.
It should be noted that any equivalent way that those skilled in the art are made under the introduction of this specification, or
Obvious variant should all be within the scope of the present invention.
Claims (10)
1. a kind of MBBR sewage disposal systems, it is characterised in that：It includes going to rear sequentially connected anaerobic zone, anoxic one certainly
Area, 2nd area of anoxic, flocculation zone, settling zone, biomembrane area and exhalant region, adjacent region are separated by partition wall, on the partition wall
It is provided with communication port, adjacent region keeps connection by opening the communication port；
The anaerobic zone is connected with water inlet pipe, and the exhalant region is connected with outlet pipe, and treatment sewage is through the water inlet pipe
Into after processing from outlet pipe discharge；
The flocculation zone is connected with chemical feed pipe, and the settling zone bottom is connected with mud return line one and excess sludge discharge
The other end of pipe, one pipe of sludge reflux is connected to one area of the anoxic, and the excess sludge delivery pipe is used for will be remaining
Sludge is discharged；
Nitrification liquid return duct is connected between the exhalant region and one area of anoxic, the anaerobic zone is lacked with described
Oxygen is connected with mud return line two between 2nd areas；
It is respectively arranged with blender in the anaerobic zone, one area of anoxic, 2nd area of anoxic and flocculation zone, in the biomembrane
It is disposed with suspending carrier, aerator one in area and intercepts sieve, hyperfiltration membrane assembly and aerator are provided in the exhalant region
Two.
2. a kind of MBBR sewage disposal systems according to claim 1, it is characterised in that：The mud return line one,
It is both provided with water pump on nitrification liquid return duct and mud return line two.
3. a kind of MBBR sewage disposal systems according to claim 1, it is characterised in that：The interception sieve setting exists
It is porous plate before the water outlet of the exhalant region, catch basin, the catch basin position is provided with above the hyperfiltration membrane assembly
Below the water surface.
4. a kind of MBBR sewage disposal systems according to claim 1, it is characterised in that：The aerator one is oxygenation
Aerator, the aerator two are backwash aerator.
5. a kind of MBBR sewage disposal systems according to claim 1, it is characterised in that：Blender in flocculation zone
For vertical stirrer.
6. a kind of MBBR sewage treatment process, which is characterized in that it is used at claim 1-5 any one of them MBBR sewage
Reason system, the technique include the following steps：
Treatment sewage enters through water inlet pipe in anaerobic zone, and flow of inlet water is set as Q, stays for some time in anaerobic zone, warp
Communication port flows into one area of anoxic, 2nd area of anoxic and flocculation zone successively, is added thereto by chemical feed pipe in flocculation zone a certain amount of
Medicament subsequently enters settling zone, before settling zone sludge is back to one area of anoxic by mud return line one under the action of stirring
The regurgitant volume at end, mud return line one is 0.8-1.2Q, and excess sludge passes through excess sludge discharged；
Biomembrane area, exhalant region are sequentially entered through its supernatant of settling zone, exhalant region mixed liquor is flowed back by nitrification liquid return duct
To one area front end of anoxic, nitrification liquid regurgitant volume is 1-3Q；The mud return line that two area's mixed liquor of anoxic passes through two area end of anoxic
Two are back to anaerobic zone front end, and two regurgitant volume of mud return line is one regurgitant volume of mud return line and nitrification liquid regurgitant volume is averaged
Value.
7. a kind of MBBR sewage treatment process according to claim 6, it is characterised in that：The anaerobic zone sludge concentration is
3000-5000mg/L；One area of the anoxic, two area's sludge concentration of anoxic are 6000-8000mg/L；Biomembrane area sludge is dense
Spend ＜ 500mg/L.
8. a kind of MBBR sewage treatment process according to claim 6, it is characterised in that：It suspends and carries in the biomembrane area
Body filling rate is 30-67%, and the biomembrane area DO is in 1-8mg/L；Membrane flux 18-25L/m in the exhalant region2/ h, ultrafiltration
Membrane module is aerated density 8-20L/min/m2；
When filling rate is 30%-50%, biomembrane area gas-water ratio is 5:1 to 8:1, exhalant region membrane flux is 20-25L/m2/ h,
It is 8-15L/min/m that hyperfiltration membrane assembly, which is aerated density,2；
When filling rate is 50%-67%, biomembrane area gas-water ratio is 7:1 to 10:1, exhalant region membrane flux 18-22L/m2/ h surpasses
Filter membrane membrane module is aerated density 12-20L/min/m2。
9. a kind of MBBR sewage treatment process according to claim 6, it is characterised in that：The water outlet ammonia nitrogen in biomembrane area≤
2mg/L, biomembrane area are discharged TN≤8mg/L；When biomembrane area is discharged ammonia nitrogen>When 2mg/L, biomembrane area DO 10- are improved
20%, until biomembrane area is discharged ammonia nitrogen≤2mg/L, DO is constant at this time for holding；When biomembrane area is discharged TN>When 8mg/L, reduce
Biomembrane area DO 10-20%, until biomembrane area is discharged TN≤8mg/L, DO is constant at this time for holding.
10. a kind of MBBR sewage treatment process according to claim 6, which is characterized in that be discharged through exhalant region water outlet
Water index be：It is discharged TP≤0.2mg/L or TP removal rate >=90%, is discharged TN≤8mg/L, is discharged SS≤6mg/L, system TN
Elimination capacity >=0.1kgN/m3/d。
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| CN108975490A (en) * | 2018-10-08 | 2018-12-11 | 天津城建大学 | Separated type MBBR-MBR based on Internet of Things couples sewage disposal system |
| CN109289258A (en) * | 2018-10-30 | 2019-02-01 | 青岛思普润水处理股份有限公司 | A kind of sedimentation pond for water treatment |
| 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 |
| CN110255700A (en) * | 2019-07-26 | 2019-09-20 | 广东紫方环保技术有限公司 | MBBR-MBR treatment facility for sewage treatment |
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Inventor after: Zheng Zhijia Inventor after: Sun Qinghua Inventor after: Wu Di Inventor after: Li Chuangxiu Inventor before: Zheng Zhijia Inventor before: Sun Qinghua Inventor before: Li Chuangxiu Inventor before: Wu Di |
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Effective date of registration: 20230925 Address after: The entire building of the factory building at No. 155 Yanhe Road, Huangdao District, Qingdao City, Shandong Province, 266000 Applicant after: QINGDAO SPRING WATER TREATMENT Co.,Ltd. Applicant after: Qingdao Sipurun Intelligent System Co.,Ltd. Applicant after: Qingdao Sipurun Water Environmental Technology Co.,Ltd. Address before: No. 155 Yanhe Road, West Coast New Area (Huangdao District), Huangdao District, Qingdao, Shandong 266500 Applicant before: QINGDAO SPRING WATER TREATMENT Co.,Ltd. |
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