CN108503019A - A kind of membrane bioreactor and sewage water treatment method - Google Patents
A kind of membrane bioreactor and sewage water treatment method Download PDFInfo
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- CN108503019A CN108503019A CN201810230661.1A CN201810230661A CN108503019A CN 108503019 A CN108503019 A CN 108503019A CN 201810230661 A CN201810230661 A CN 201810230661A CN 108503019 A CN108503019 A CN 108503019A
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- 239000010865 sewage Substances 0.000 title claims abstract description 92
- 239000012528 membrane Substances 0.000 title claims abstract description 86
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 65
- 238000000034 method Methods 0.000 title claims abstract description 26
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 79
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 79
- 239000001301 oxygen Substances 0.000 claims abstract description 79
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 70
- 239000000919 ceramic Substances 0.000 claims abstract description 62
- 238000005273 aeration Methods 0.000 claims abstract description 57
- 239000007789 gas Substances 0.000 claims abstract description 38
- 238000005276 aerator Methods 0.000 claims abstract description 33
- 239000003963 antioxidant agent Substances 0.000 claims abstract description 26
- 230000003078 antioxidant effect Effects 0.000 claims abstract description 26
- 235000006708 antioxidants Nutrition 0.000 claims abstract description 26
- 239000010802 sludge Substances 0.000 claims abstract description 25
- 238000010992 reflux Methods 0.000 claims abstract description 19
- 230000003647 oxidation Effects 0.000 claims description 34
- 238000007254 oxidation reaction Methods 0.000 claims description 34
- 238000006385 ozonation reaction Methods 0.000 claims description 21
- 238000001514 detection method Methods 0.000 claims description 14
- 239000002351 wastewater Substances 0.000 claims description 14
- 239000007788 liquid Substances 0.000 claims description 10
- 230000001276 controlling effect Effects 0.000 claims description 7
- 210000002700 urine Anatomy 0.000 claims description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 6
- 230000004907 flux Effects 0.000 claims description 6
- 230000002045 lasting effect Effects 0.000 claims description 6
- 230000002906 microbiologic effect Effects 0.000 claims description 6
- 239000000126 substance Substances 0.000 claims description 6
- 230000015556 catabolic process Effects 0.000 claims description 5
- 239000003814 drug Substances 0.000 claims description 5
- 244000005700 microbiome Species 0.000 claims description 5
- 238000005086 pumping Methods 0.000 claims description 5
- 229910052799 carbon Inorganic materials 0.000 claims description 4
- 239000003245 coal Substances 0.000 claims description 4
- 238000004043 dyeing Methods 0.000 claims description 4
- 239000011148 porous material Substances 0.000 claims description 4
- 238000013019 agitation Methods 0.000 claims description 3
- 238000001914 filtration Methods 0.000 claims description 3
- 239000010842 industrial wastewater Substances 0.000 claims description 3
- 238000003756 stirring Methods 0.000 claims description 3
- 238000006243 chemical reaction Methods 0.000 claims description 2
- 230000001105 regulatory effect Effects 0.000 claims description 2
- 238000004891 communication Methods 0.000 claims 1
- 229910052573 porcelain Inorganic materials 0.000 claims 1
- 238000005457 optimization Methods 0.000 abstract description 8
- 238000012545 processing Methods 0.000 description 11
- 230000008569 process Effects 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 5
- 238000011065 in-situ storage Methods 0.000 description 5
- 238000004065 wastewater treatment Methods 0.000 description 5
- 230000008859 change Effects 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 3
- 238000011161 development Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 238000012360 testing method Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 238000010168 coupling process Methods 0.000 description 2
- 238000006731 degradation reaction Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- -1 hydroxyl radical free radical Chemical class 0.000 description 2
- 238000009285 membrane fouling Methods 0.000 description 2
- 238000012544 monitoring process Methods 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 238000000108 ultra-filtration Methods 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000003064 anti-oxidating effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 238000005189 flocculation Methods 0.000 description 1
- 230000016615 flocculation Effects 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 238000010525 oxidative degradation reaction Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 230000002085 persistent effect Effects 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 238000001179 sorption measurement 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
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1268—Membrane bioreactor systems
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
- B01D65/02—Membrane cleaning or sterilisation ; Membrane regeneration
-
- 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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
-
- 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
- C02F3/006—Regulation methods for biological treatment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/14—Activated sludge processes using surface aeration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
- B01D2321/18—Use of gases
-
- 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)
- Chemical & Material Sciences (AREA)
- Water Supply & Treatment (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Organic Chemistry (AREA)
- Microbiology (AREA)
- Biodiversity & Conservation Biology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Health & Medical Sciences (AREA)
- Molecular Biology (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
A kind of membrane bioreactor and sewage water treatment method, the membrane bioreactor include simultaneous oxygen biotic division, aerobe area and the film area being sequentially communicated, and oxygen biotic division sets intake pump and blender；The aerator with air aeration pump connection is set in aerobe area, the first air gas flowmeter is connected between aerator and air aeration pump；Ceramic film component and anti-oxidant aerator are set in film area, and anti-oxidant aerator is below ceramic film component, anti-oxidant aerator is connect with air aeration pump and ozone generator respectively, second air gas flowmeter is connected between anti-oxidant aerator and air aeration pump, and ozone gas flow meter is connected between anti-oxidant aerator and ozone generator；Water outlet pump is set to the water outlet side in film area, is connect with ceramic film component, and mud valve is set to the spoil disposal side in film area, and film area is connected to by reflux pump with simultaneous oxygen biotic division.The application depth optimization effluent quality, and efficiently On-line Control ceramics fouling membranes and excess sludge can be reduced.
Description
Technical field
The invention belongs to sewage treatment fields, and in particular to a kind of membrane bioreactor and sewage water treatment method.
Background technology
With the continuous development of world economy level and being continuously increased for the size of population, water environment pollution problem has caused
The extensive concern of the public.Municipal sewage treatment is that China inevitably needs the water process faced during Development of China's Urbanization
Problem.Traditional dirty water living creature processing technique, including A2O techniques, oxidation ditch process and anaerobic ammonia oxidation process etc..However, close
As sewage disposal discharge standard is gradually increased in country over year, traditional biologic treating technique can not achieve increasingly strict
Sewage drainage standard, for this purpose, various recycled water further treatment techniques continue to bring out, including ozone oxidation and activated carbon adsorption
Deng.
In recent years, membrane separation technique, floor space high by feat of mud-water separation rate be small and the advantages such as effluent quality is good,
Through being widely used in sewage treatment field, especially organic ultrafiltration membrane.In order to effectively control fouling membrane and depth optimization water outlet
Water quality, ultrafiltration membrane technique combine the pretreatment units such as various flocculation/oxidations or are followed by oxidation/absorption even depth processing unit
Coupling technique has been widely used in the upgrading of municipal sewage plant.However, coupling multiple pretreatments or depth
Processing unit directly extends the processing unit of sewage, increases floor space and sewage plant capital construction and upgrading cost, together
When, membrane pollution problem can lead to flux depression, effluent quality deterioration, the membrane module lost of life, therefore restrict always
Further genralrlization application of the membrane separation technique in sewage treatment field.Obviously, how effective while improving effluent quality
Ground reduces sewage treatment unit and controls the bottleneck problem that fouling membrane has been urgently to be resolved hurrily in sewage disposal.
Studies have shown that in sewage treatment field, the mainly macromolecular organic pollution of fouling membrane is caused.Ozone is as one
Kind strong oxidizer efficiently oxidation of organic compounds, especially degradation can remove the organic pollution of bio-refractory in sewage, because
This ozone oxidation can also improve effluent quality while efficiently controlling fouling membrane.However, the strong oxidizing property of ozone can be
Organic membrane module is damaged to a certain extent, and therefore, ozone Oxidation Treatment is either handled with the connected applications of organic membrane technology
Unit is integrated or ozone dosage is all greatly limited.
Invention content
For solve traditional biological treatment technology treated sewage water quality difficulty it is up to standard, processing unit is cumbersome, sewage treating efficiency is low,
The technical bottlenecks such as control membrane fouling efficiency is low in membrane bioreactor and excess sludge is difficult, the present invention propose a kind of film biology
Reactor and sewage water treatment method, have simplified processing unit, depth optimization effluent quality, and can efficiently On-line Control ceramics
Fouling membrane is simultaneously reduced excess sludge.
The technical problem of the present invention is resolved by technical solution below：
A kind of membrane bioreactor, including the simultaneous oxygen biotic division, aerobe area and the film area that are sequentially communicated, further include into water
Pump, blender, air aeration pump, the first air gas flowmeter are aerator, ceramic film component, anti-oxidant aerator, smelly
Oxygen Generator, ozone gas flow meter and the second air gas flowmeter, water outlet pump, mud valve and reflux pump；The intake pump
It is located at described and oxygen biotic division influent side, the blender is located in described and oxygen biotic division；The aerator is located at institute
It states in aerobe area, and pumps and connect with the air aeration, the first air gas flowmeter is connected to the aeration dress
It sets between air aeration pump；The ceramic film component and the anti-oxidant aerator are set in the film area, and institute
It states anti-oxidant aerator to be located at below the ceramic film component, the anti-oxidant aerator is pumped with the air aeration respectively
It is connected with the ozone generator, the second air gas flowmeter is connected to the anti-oxidant aerator and the air
Between aeration pump, the ozone gas flow meter is connected between the anti-oxidant aerator and the ozone generator；Institute
The water outlet side that water outlet pump is set to the film area is stated, is connect with the ceramic film component, the mud valve (20) is set to the film area
Spoil disposal side, the film area be connected to by the reflux pump with described and oxygen biotic division, by the dirt partly Jing Guo ozone oxidation
Mud is back to described and oxygen biotic division.
Preferably, the bottom of described and oxygen biotic division side is connected to the bottom of the side in the aerobe area, dirty
Water flow to the aerobe area by the bottom of described and oxygen biotic division the side.
Preferably, the top of the other side in the aerobe area is connected to by overflow manner with the film area, and sewage is logical
The top overflow of the other side in the aerobe area is crossed to the film area.
Preferably, the average membrane pore size of the ceramic membrane of the ceramic film component is 50-200nm.
Preferably, further include the relay being connected between the water outlet pump and the ceramic film component, the water outlet pump
Row of stopping transport is taken out with Heng Tong amount with ceramic film component described in the relay co- controlling.
Preferably, it is additionally provided with the first dissolving oxygen detection in described and oxygen biotic division, in the aerobe area also
Equipped with the second dissolving oxygen detection.
Preferably, further include the liquid level gauge being set in the film area, be connected to the water outlet pump and the ceramic film component
Between pressure gauge, further include automatic control cabinet, the intake pump, blender, air aeration pump, ozone generator, reflux pump,
Mud valve, the first dissolving oxygen detection, the second dissolving oxygen detection, the first air gas flowmeter, ozone gas flow meter, the
Two air gas flowmeters, pressure gauge, water outlet pump, liquid level gauge are respectively communicated to connect with automatic control cabinet.
A kind of sewage water treatment method is carried out using the membrane bioreactor, is included the following steps：
S1, by thickness grid treated sewage by intake pump promoted from and the top of oxygen biotic division enter and oxygen is given birth to
Object area, and oxygen biotic division in, the lower sewage used in the stirring of blender and the facultative microbe foster microorganism that becomes reconciled come into full contact with
It reacts, organic pollution is removed by microorganism initial breakdown in sewage；
After S2, sewage are adequately processed in simultaneous oxygen biotic division, into aerobe area, under air aeration agitation, sewage
It is come into full contact with aerobic activated sludge, the organic pollution in sewage is further degraded removal by aerobic microbiological；
After S3, sewage are adequately processed in aerobe area, into film area, in film area, the residual organic matter in sewage
The further oxygenolysis of aerobic microbiological in envelope area, by air aeration and the lasting aeration of ozonation aerated switching, ozone exposes
Gas oxidation removal bio-refractory organic pollution, and the organic pollution inside oxidation removal ceramic membrane surface and fenestra；
It after S4, sewage are handled in film area, is discharged through water outlet pump after ceramic film component filters, ozone is passed through in film area
The partial sludge of oxidation is back to through reflux pump and oxygen biotic division is reused as carbon source, and excess sludge is discharged through mud valve.
Preferably, hydraulic detention time of the sewage in simultaneous oxygen biotic division is 3h~10h, waterpower of the sewage in aerobe area
Residence time is 6h~10h, and hydraulic detention time of the sewage in film area is 1h~10h, and sewage is in aerobe area and film area
The sum of hydraulic detention time be sewage and 2~5 times of hydraulic detention time of oxygen biotic division.
Preferably, in step S3, air aeration and the lasting aeration of ozonation aerated switching refer to：Ozonation aerated frequency is 1
~3 times/2 days, when ozonation aerated every time, the dosage of ozone was more than 0 and≤0.66mg-O3/ g-SS, remaining when for air expose
Gas.
Preferably, in step S3, air aeration and it is ozonation aerated when, the gas-water ratio of aeration is controlled 6:1-8:Between 1.
Preferably, the Dissolved Oxygen concentration Control of described and oxygen biotic division is more than 0 and≤0.5mg/L, aerobe area
Dissolved Oxygen concentration Control is in 1.5-2.5mg/L.
Preferably, it is taken out and is stopped transport with Heng Tong amount by ceramic film component described in the water outlet pump and the relay co- controlling
Row, operating flux is sub-critical pressure, in 15L/m2H~60L/m2Between h, pumping is stopped than for 8~10min:1~2min.
Preferably, the reflux ratio of the partial sludge in step S4 Jing Guo ozone oxidation is 1:2~1:4.
Preferably, step S1~S4 is monitored in real time by automatic control cabinet and is regulated and controled online.
Preferably, the sewage be sanitary sewage, lavatory human excrement and urine's urine waste water, dyeing waste water, petrochemical wastewater,
At least one of coal chemical industrial waste water and biological medicine waste water.
The beneficial effect of the present invention compared with the prior art includes：
1, the present invention is highly integrated by biological processing unit and membrane technology and deep oxidation treatment technology, according to ceramics
The strong anti-oxidation of membrane module is directly integrated in membrane module bottom by ozonation aerated, directly pre- instead of ozone in traditional handicraft
Ozone deep oxidation processing in oxidation processes or Sewage advanced treatment, greatly reduces treatment unit for waste water, has and subtract
The advantages that few floor space, raising operational efficiency.
2, the biological stability of ceramic membrane is strong, operating flux is high, service life is long, while anti-oxidant aerator is directly pacified
Mounted in the lower section of ceramic film component, can directly carry out ozonation aerated so that ozone bubbles farthest contact ceramic membrane table
Face, or even under strong suction force effect, ozone bubbles can enter inside ceramic fenestra, to be urged using ozone and ceramic membrane
It is efficiently organic inside oxidation removal ceramic membrane surface and fenestra to change the hydroxyl radical free radical of the strong oxdiative power that ozone degradation generates
Pollutant, can efficient On-line Control ceramics fouling membrane.
3, the low concentration ozone in film area is aerated the ozone molecule being dispersed in sewage while efficiently control fouling membrane
Biologic treating technique that can be further in oxidative degradation and oxygen biotic division and aerobic biotic division is difficult to the organic pollution removed,
Such as emerging pollutant (such as drug and personal care articles, incretion interferent), while depth optimization biological phosphate-eliminating, further carry
High effluent quality directly saves the advanced treatment of wastewater unit subtracted in sewage plant upgrading in recent years.
4, ozone oxidation can also be reduced excess sludge, alleviate that a large amount of spoil disposals of membrane bioreactor, sludge are difficult etc. to ask
Topic, i.e. sludge of the part Jing Guo ozone oxidation can be periodically back to and oxygen biotic division, can be used as microbe carbon source by sharp again
With, reach decrement excess sludge target of sustainable development.
5, further, the present invention is provided with automatic control system, can be with overall monitor and regulation and control membrane bioreactor
Normal operation, unattended, the automatic operating of sewage disposal may be implemented, at the water for reaching " wisdom water utilities " new era
Manage target.
Description of the drawings
Fig. 1 is the example schematic of the membrane bioreactor in the specific embodiment of the invention；
Fig. 2 is the net transmembrane pressure of ceramic membrane when carrying out contrast experiment in the specific embodiment of the invention with run time
Change curve.
Specific implementation mode
Below against attached drawing and in conjunction with preferred embodiment, the invention will be further described.
In a specific embodiment, as shown in Figure 1, a kind of membrane bioreactor, including the simultaneous oxygen biotic division that is sequentially communicated
1, aerobe area 2 and film area 3, further include intake pump 4), blender 5, air aeration pump the 8, first air gas flowmeter 9,
Aerator 10, ceramic film component 15, anti-oxidant aerator 12, ozone generator 14, ozone gas flow meter 13 and second
Air gas flowmeter 11, water outlet pump 19, mud valve 20 and reflux pump 21；Wherein, intake pump 4 is located at described and oxygen biotic division 1
Influent side, blender 5 is located in described and oxygen biotic division 1；Aerator 10 is located in the aerobe area 2, and with sky
Gas aeration pump 8 connects, and the first air gas flowmeter 9 is connected between aerator 10 and air aeration pump 8；Ceramic membrane
Component 15 and anti-oxidant aerator 12 are set in film area 3, and anti-oxidant aerator 12 is located under the ceramic film component 15
Side, anti-oxidant aerator 12 are connect with air aeration pump 8 and ozone generator 14 respectively, and the second air gas flowmeter 11 connects
It is connected between anti-oxidant aerator 12 and air aeration pump 8, ozone gas flow meter 13 is connected to anti-oxidant aerator 12
Between ozone generator 14；Water outlet pump 19 is set to the water outlet side in film area 3, is connect with ceramic film component 15, mud valve 20 is set to
The spoil disposal side in film area 3, film area 3 are connected to by reflux pump 21 with simultaneous oxygen biotic division 1, and the sludge by part Jing Guo ozone oxidation returns
It flow to simultaneous oxygen biotic division 1.
Specifically, in the application, air aeration and it is ozonation aerated switch over and recycle with optimal conditions, air aeration
When, anti-oxidant aerator 12 connects air aeration pump 8, and controls aeration quantity, air by the second air gas flowmeter 11
Bubble directly washes away ceramic membrane surface.When ozonation aerated, anti-oxidant aerator 12 connects ozone generator 14, and passes through ozone
The control of gas flowmeter 13 carries out low concentration ozone and is aerated in situ, and ozone bubbles wash away ceramic membrane surface and direct oxidation organic film
Polluter, while depth optimization water quality, entire membrane bioreactor ozone free pretreating zone or ozone advanced treating area.
Include following step using the method that the membrane bioreactor in above-mentioned specific implementation mode carries out sanitary sewage disposal
Suddenly：
S1, by thickness grid treated sewage by intake pump 4 promoted from and the top of oxygen biotic division 1 enter and oxygen
Biotic division 1, and oxygen biotic division 1 in, the lower sewage used in the stirring of blender 5 and the facultative microbe foster microorganism that becomes reconciled are abundant
Haptoreaction, organic pollution is removed by microorganism initial breakdown in sewage；
It is dirty under air aeration agitation into aerobe area 2 after S2, sewage are adequately processed in simultaneous oxygen biotic division 1
Water comes into full contact with aerobic activated sludge, and the organic pollution in sewage is further degraded removal by aerobic microbiological；
After S3, sewage are adequately processed in aerobe area 2, into film area 3, in film area, the residual in sewage is organic
The further oxygenolysis of aerobic microbiological in object envelope area passes through air aeration and the lasting aeration of ozonation aerated switching, ozone
Aerating oxidation removes bio-refractory organic pollution, and the organic pollution inside oxidation removal ceramic membrane surface and fenestra；
It after S4, sewage are handled in film area 3, is discharged through water outlet pump 19 after the filtering of ceramic film component 15, warp in film area 3
The partial sludge for crossing ozone oxidation is back to through reflux pump and oxygen biotic division 1 is reused as carbon source, and excess sludge is through spoil disposal
Valve 20 is discharged.
In other embodiments, at least one of following optimize can be selected：
And the bottom of the side of oxygen biotic division 1 is connected to the bottom of the side in aerobe area 2, and in step sl, sewage
It flow to aerobe area 2 by the bottom of the side of simultaneous oxygen biotic division 1.
The top of the other side in aerobe area 2 is connected to by overflow manner with film area 3, and in step s3, sewage passes through
The top overflow of the other side in aerobe area 2 is to film area 3.
Membrane bioreactor further includes the relay 18 being connected between water outlet pump 19 and ceramic film component 15, water outlet pump 19
Row of stopping transport is taken out with Heng Tong amount with 18 co- controlling ceramic film component 15 of relay.Air aeration and ozonation aerated friendship are carried out in film area
During persistent loop, ceramic film component continues the operation of Heng Tong amount to take out stop mode, each other not by any interference.Preferably
It is that the operating flux of ceramic film component is sub-critical pressure, in 15L/m2H~60L/m2Between h, pumping stop than for 8~
10min:1~2min.
It is additionally provided with the first dissolving oxygen detection 6 in simultaneous oxygen biotic division 1, the second dissolving is additionally provided in aerobe area 2
Oxygen detection 7.Preferably, and the Dissolved Oxygen concentration Control of oxygen biotic division is more than 0 and≤0.5mg/L, aerobe area
Dissolved Oxygen concentration Control is in 1.5-2.5mg/L.
The average membrane pore size of the ceramic membrane of the ceramic film component 15 is 50-200nm.
Membrane bioreactor further includes the liquid level gauge 16 being set in film area 3, is connected to water outlet pump 19 and ceramic film component 15
Between pressure gauge 17, further include automatic control cabinet 22, wherein intake pump 4, blender 5, air aeration pump 8, ozone generator
14, reflux pump 21, mud valve 20, first dissolve oxygen detection 6, second dissolve oxygen detection 7, the first air gas flowmeter 9,
Ozone gas flow meter 13, the second air gas flowmeter 11, pressure gauge 17, water outlet pump 19, liquid level gauge 16 respectively with automatically
Switch board 22 communicates to connect, to realize unattended, the automatic operating of sewage disposal.
Wherein, pressure gauge 17 monitors the operating pressure of ceramic membrane operation on-line, and controls net transmembrane pressure △ TMP (△ TMP
=practical transmembrane pressure-film self resistance pressure difference) it is advisable in 30kPa or less, when △ TMP are more than given threshold (such as from about 30kPa),
Ceramic Membrane cleaning need to be carried out in time.The liquid level in film area can be controlled by liquid level gauge 16 and designed within liquid level ± 2cm.First dissolving
The data that oxygen detection 6, second dissolves the on-line monitoring of oxygen detection 7, liquid level gauge 16 and pressure gauge 17 can be by data line
For real-time Transmission to automatic control cabinet 22, automatic control cabinet 22 can analyze the operation data of membrane bioreactor, and reference in real time
The design parameter of membrane bioreactor is to intake pump 4, blender 5, air aeration pump 8, ozone generator 14, reflux pump 21, row
Slurry valve 20, the first air gas flowmeter 9, ozone gas flow meter 13, the second air gas flowmeter 11 and water outlet pump 19 etc.
The online real-time monitoring of instrument (as shown in the dotted arrow direction in Fig. 1), may be implemented membrane bioreactor automation nobody
Operation on duty.
In domestic sewage processing method, one of preferably following technological parameter or arbitrary combination：Sewage is in simultaneous oxygen biotic division
Hydraulic detention time be 3h~10h, sewage aerobe area hydraulic detention time be 6h~10h, sewage is in film area
Hydraulic detention time is 1h~10h, and hydraulic detention time the sum of of the sewage in aerobe area and film area be sewage and oxygen
2~5 times of the hydraulic detention time of biotic division.In step S3, air aeration and it is ozonation aerated when, the gas-water ratio of aeration controls
6:1-8:Between 1, the gas-water ratio of the two can be identical, can not also the identical (experimental group when lower section carries out contrast test
In, gas-water ratio when the two is aerated is selected as identical).In step S3, air aeration and the lasting aeration of ozonation aerated switching refer to：
Ozonation aerated frequency is 1~3 time/2 days, and when ozonation aerated every time, the dosage of ozone is more than 0 and≤0.66mg-O3/g-
SS, remaining when be air aeration.The reflux ratio of partial sludge in step S4 Jing Guo ozone oxidation is 1:2~1:4.
Inventive film bioreactor and sewage water treatment method can be used for sanitary sewage disposal, lavatory human excrement and urine's urine
Wastewater treatment, treatment of dyeing wastewater, petrochemical wastewater processing, coal chemical industrial waste water processing and biological medicine wastewater treatment etc..
Hereinafter, by contrast experiment, the application is further elaborated.
Membrane bioreactor is applied in sanitary sewage disposal, the membrane biological reaction for the two groups of same volumes that run parallel for a long time
Device, one of which are set as compareing, the areas control group operational process Zhong Mo ozone free aeration；Another group is experimental group, more than
Membrane bioreactor in embodiment.Experimental group and the service condition of control group are：The average membrane pore size of ceramic membrane is
100nm；Hydraulic detention time of the sewage in simultaneous oxygen biotic division is 3h, and hydraulic detention time of the sewage in aerobe area is 6h,
Hydraulic detention time of the sewage in film area is 1h；When film area air aeration, the gas-water ratio of aeration is controlled 7:Between 1；And oxygen
The Dissolved Oxygen concentration Control of biotic division is in 0.3mg/L, and the Dissolved Oxygen concentration Control in aerobe area is in 2.0mg/L；In film area
The reflux ratio of the partial sludge of ozone oxidation is 1:3；Ceramic membrane operating flux is sub-critical pressure 15L/m2H, ceramic membrane are adopted
The Heng Tong amount pumping stop mode for stopping 1min with pumping 9min carries out dead-end filtration.In addition to this, experimental group is in the process of running in film area
It also carries out intermittent ozone to be aerated in situ, it is 1 time/2 days that ozone, which adds frequency, ozone dosage 0.66mg-O3/ g-SS is smelly
When oxygen is aerated, the gas-water ratio of aeration is also controlled 7:1.Test of many times the result shows that, the membrane bioreactor of experimental group can be same
Step realizes the targets such as effluent quality depth optimization, the efficient On-line Control of fouling membrane and mud decrement discharge.Specific test effect is such as
Shown in the following table 1：
1 two groups of membrane bioreactor effluent quality results of table
It is deep by the effluent quality result in table 1 it is found that the membrane bioreactor of the application can further improve effluent quality
Degree optimization biological phosphor-removing effect is the most notable.
Meanwhile in experimentation, the net transmembrane pressure of control group and the ceramic membrane of experimental group is compared with run time
Change curve, as shown in Figure 2, wherein curve C1 is control group, and curve C2 is experimental group, as can be seen from Figure 2, identical
Under experimental condition, compared to the membrane bioreactor of control group, the ceramic membrane fouling rate in the membrane bioreactor of the application
Extremely slowly.In control group, referring to the solid arrow pointed location of curve C1, water flushing need to be carried out the 16th day, the 20th day,
Under the conditions of no ozonation aerated, it is clear need to carry out chemistry for the first time in operation fouling membrane aggravation in the 22nd day for the ceramic membrane of control group
It washes, at the 41st day, the secondary aggravation of fouling membrane need to carry out second of chemical cleaning.And under the control of ozone in-situ oxidation, referring to
The solid arrow pointed location of curve C2, the ceramic membrane stable operation in the membrane bioreactor of experimental group (i.e. the application) 48 days
It just needs to carry out first time chemical cleaning afterwards.Specifically, when running the 17th day, the △ TMP of control group increase to 28.4kPa, and originally
The △ TMP of the membrane bioreactor of application increase to 2.8kPa, and fouling membrane rate of rise reduces by 10 under the control of ozone in-situ oxidation
Times or more.
After two groups of membrane bioreactor stable operation 45d, a concentration of 7.8g/L of control group mean sludge, and the film of the application
The sludge concentration of bioreactor is 7.3g/L, it will be apparent that, ozone in-situ oxidation has effectively been reduced excess sludge.
To sum up, the present invention truly has depth optimization effluent quality, efficient On-line Control ceramics fouling membrane, minimizing remaining dirty
Mud simplifies the advantages that sewage treatment unit, reduction floor space, is worthy of promotion and application in sewage treatment industry, especially suitable
In sanitary sewage disposal, lavatory human excrement and urine's urine wastewater treatment, treatment of dyeing wastewater, petrochemical wastewater processing, coal chemical industry
Wastewater treatment and biological medicine wastewater treatment etc..
The above content is a further detailed description of the present invention in conjunction with specific preferred embodiments, and it cannot be said that
The specific implementation of the present invention is confined to these explanations.For those skilled in the art to which the present invention belongs, it is not taking off
Under the premise of from present inventive concept, several equivalent substitute or obvious modifications can also be made, and performance or use is identical, all answered
When being considered as belonging to protection scope of the present invention.
Claims (10)
1. a kind of membrane bioreactor, which is characterized in that including be sequentially communicated simultaneous oxygen biotic division (1), aerobe area (2) and
Film area (3) further includes intake pump (4), blender (5), air aeration pump (8), the first air gas flowmeter (9), aeration dress
Set (10), ceramic film component (15), anti-oxidant aerator (12), ozone generator (14), ozone gas flow meter (13) and
Second air gas flowmeter (11), water outlet pump (19), mud valve (20) and reflux pump (21)；
The intake pump (4) is located at described and oxygen biotic division (1) influent side, and the blender (5) is located at described and oxygen biology
In area (1)；
The aerator (10) is located in the aerobe area (2), and is connect with air aeration pump (8), and described the
One air gas flowmeter (9) is connected between the aerator (10) and air aeration pump (8)；
The ceramic film component (15) and the anti-oxidant aerator (12) are set in the film area (3), and described anti-oxidant
Aerator (12) is located at below the ceramic film component (15), and the anti-oxidant aerator (12) exposes with the air respectively
Air pump (8) and the ozone generator (14) connection, the second air gas flowmeter (11) are connected to the anti-oxidant exposure
Between device of air (12) and air aeration pump (8), the ozone gas flow meter (13) is connected to the anti-oxidant aeration
Between device (12) and the ozone generator (14)；
The water outlet pump (19) is set to the water outlet side of the film area (3), is connect with the ceramic film component (15), the mud valve
(20) it is set to the spoil disposal side of the film area (3), the film area (3) passes through the reflux pump (21) and described and oxygen biotic division (1)
Connection, by sludge reflux of the part Jing Guo ozone oxidation to described and oxygen biotic division (1).
2. membrane bioreactor as described in claim 1, which is characterized in that the bottom of described and oxygen biotic division (1) side
It is connected to the bottom of the side of the aerobe area (2), sewage is flow to by the bottom of described and oxygen biotic division (1) the side
The aerobe area (2)；The top of the other side of the aerobe area (2) is connected by overflow manner and the film area (3)
Logical, sewage passes through the top overflow of the other side of the aerobe area (2) to the film area (3)；The ceramic film component
(15) average membrane pore size of ceramic membrane is 50-200nm.
3. membrane bioreactor as described in claim 1, which is characterized in that further include being connected to the water outlet pump (19) and institute
The relay (18) between ceramic film component (15) is stated, is made pottery described in the water outlet pump (19) and the relay (18) co- controlling
Porcelain membrane module (15) takes out row of stopping transport with Heng Tong amount；It is additionally provided with the first dissolving oxygen detection (6) in described and oxygen biotic division (1),
It is additionally provided with the second dissolving oxygen detection (7) in the aerobe area (2).
4. membrane bioreactor as claimed in claim 3, which is characterized in that further include the liquid level being set in the film area (3)
It counts (16), the pressure gauge (17) being connected between the water outlet pump (19) and the ceramic film component (15), further includes controlling automatically
Cabinet (22) processed, the intake pump (4), blender (5), air aeration pump (8), ozone generator (14), reflux pump (21), spoil disposal
Valve (20), the first dissolving oxygen detection (6), the second dissolving oxygen detection (7), the first air gas flowmeter (9), ozone gas
Flowmeter (13), the second air gas flowmeter (11), pressure gauge (17), water outlet pump (19), liquid level gauge (16) respectively with from
Dynamic switch board (22) communication connection.
5. a kind of sewage water treatment method is carried out using membrane bioreactor described in claim 1, which is characterized in that including such as
Lower step：
S1, by thickness grid treated sewage by intake pump (4) promoted from and the top of oxygen biotic division (1) enter and oxygen
Biotic division (1), and oxygen biotic division (1) in, the lower sewage used in the stirring of blender (5) and facultative microbe are become reconciled foster micro- life
Object comes into full contact with reaction, and organic pollution is removed by microorganism initial breakdown in sewage；
It is dirty under air aeration agitation into aerobe area (2) after S2, sewage are adequately processed in simultaneous oxygen biotic division (1)
Water comes into full contact with aerobic activated sludge, and the organic pollution in sewage is further degraded removal by aerobic microbiological；
After S3, sewage are adequately processed in aerobe area (2), into film area (3), in film area, the residual in sewage is organic
The further oxygenolysis of aerobic microbiological in object envelope area passes through air aeration and the lasting aeration of ozonation aerated switching, ozone
Aerating oxidation removes bio-refractory organic pollution, and the organic pollution inside oxidation removal ceramic membrane surface and fenestra；
After S4, sewage are handled in film area (3), it is discharged through water outlet pump (19) after ceramic film component (15) filtering, film area (3)
The interior partial sludge by ozone oxidation is back to through reflux pump and oxygen biotic division (1) is reused as carbon source, excess sludge
It is discharged through mud valve (20).
6. sewage water treatment method as claimed in claim 5, which is characterized in that hydraulic detention time of the sewage in simultaneous oxygen biotic division
For 3h~10h, hydraulic detention time of the sewage in aerobe area is 6h~10h, and hydraulic detention time of the sewage in film area is
1h~10h, and hydraulic detention time the sum of of the sewage in aerobe area and film area is that waterpower of the sewage in simultaneous oxygen biotic division is stopped
Stay 2~5 times of time.
7. sewage water treatment method as claimed in claim 5, which is characterized in that in step S3, air aeration and ozonation aerated cut
Changing lasting aeration refers to：Ozonation aerated frequency is 1~3 time/2 days, when ozonation aerated every time, the dosage of ozone be more than 0 and
≤0.66mg-O3/ g-SS, remaining when be air aeration；In preferred steps S3, air aeration and it is ozonation aerated when, aeration
Gas-water ratio is controlled 6:1~8:Between 1.
8. sewage water treatment method as claimed in claim 5, which is characterized in that described and oxygen biotic division Dissolved Oxygen concentration Control
More than 0 and≤0.5mg/L, the Dissolved Oxygen concentration Control in aerobe area is in 1.5-2.5mg/L；Pass through the water outlet pump (19)
Row of stopping transport is taken out with Heng Tong amount with ceramic film component (15) described in the relay (18) co- controlling, operating flux is subcritical logical
Amount, in 15L/m2H~60L/m2Between h, pumping is stopped than for 8~10min:1~2min.
9. sewage water treatment method as claimed in claim 5, which is characterized in that the partial sludge in step S4 Jing Guo ozone oxidation
Reflux ratio be 1:2~1:4；Preferred steps S1~S4 is monitored in real time by automatic control cabinet (22) and is regulated and controled online.
10. sewage water treatment method as claimed in claim 5, which is characterized in that the sewage is sanitary sewage, lavatory human body excrement
Just at least one of urine waste water, dyeing waste water, petrochemical wastewater, coal chemical industrial waste water and biological medicine waste water.
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| CN115231770A (en) * | 2022-07-06 | 2022-10-25 | 中国矿业大学(北京) | System and method for treating coal chemical industry wastewater by coupling anaerobic ammonia oxidation of ceramic membrane bioreactor |
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| CN115231770A (en) * | 2022-07-06 | 2022-10-25 | 中国矿业大学(北京) | System and method for treating coal chemical industry wastewater by coupling anaerobic ammonia oxidation of ceramic membrane bioreactor |
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