CN101734793B - Sewage treatment system and sewage treatment method - Google Patents
Sewage treatment system and sewage treatment method Download PDFInfo
- Publication number
- CN101734793B CN101734793B CN200810217945A CN200810217945A CN101734793B CN 101734793 B CN101734793 B CN 101734793B CN 200810217945 A CN200810217945 A CN 200810217945A CN 200810217945 A CN200810217945 A CN 200810217945A CN 101734793 B CN101734793 B CN 101734793B
- Authority
- CN
- China
- Prior art keywords
- sewage
- film
- reaction chamber
- chamber
- film reaction
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Abstract
The invention discloses a sewage treatment system. The system comprises a bioreactor provided with a partition wall, wherein the partition wall divides the bioreactor into an anoxic chamber and a film reaction chamber, and is provided with a channel communicated with the anoxic chamber and the film reaction chamber; sewage flows in from the anoxic chamber, and is drained from the film reaction chamber after being treated through the anoxic chamber and the film reaction chamber; the sewage is subjected to denitrification treatment in the anoxic chamber; the film reaction chamber is used for performing nitration reaction on the sewage to remove nitrogen and organic substances, and comprises membrane module and an air diffuser; and the film components comprise a flat film and a nylon net membrane arranged on the flat film. The invention also provides a sewage treatment method using the system. The sewage treatment system and the treatment method can save energy consumption required in the treating process through the filtering effect of the nylon net film; and the film cannot easily cause plugging so as to save cleaning cost.
Description
Technical field
The present invention relates to water technology, relate in particular to a kind of Sewage treatment systems and treatment process thereof that adopts the biological respinse membrane module.
Background technology
Along with country or enterprise to environmental protection and the demand that economizes on resources etc., dirty (give up) water treatment becomes and more and more receives masses' attention.Bioremediation is adopted in comparatively effective and feasible WWT at present usually.For example, traditional biological treatment uses secondary sedimentation basins to come sewage is handled.Yet when carrying out WWT, sewage also need pass through the secondary sedimentation basins post precipitation and just can discharge through behind the biochemical reaction, causes the process of WWT longer.In addition, adopt the treatment process floor space of secondary sedimentation basins big, cost of investment is high.Especially when operation mud age was higher, this can cause bad sludge settling property.Therefore, this treatment system and technology are not suitable for densely populated region.
In recent years, membrane bioreactor (Membrane Bioreactor is called for short MBR) technology becomes the main flow treatment process gradually.The process characteristic of MBR is that the biological degradation processing with active sludge combines with the solid-liquid separation of film, replaces conventional deposition, filtering technique, and makes water quality after the processing directly reach the level of (being superior to) emission standard.Membrane bioreactor has many clear superiorities, for example has system handles efficient height, High Load Rate, an advantage such as floor space is little, displacement mass is high and mud end product amount is low.
Typical membrane bioreactor comprises membrane module and bio-reactor; A large amount of mikrobe (active sludge) fully contacts with matrix (labile organic compound in the waste water etc.) in membrane bioreactor; Carry out metabolism to keep growth, breeding through oxygenolysis; Make organic pollutant degradation simultaneously, membrane module carries out solid-liquid separation to waste water and mud mixed liquid, the combination of biological treatment system and membrane module through mechanical grading, effect such as hold back; The effluent quality of system and the stability of operation have not only been improved; Also prolonged the hydraulic detention time of macromolecular substance in bio-reactor, made it to be degraded to greatest extent, and strengthened the removal effect of system hard-degraded substance.
According to the relative position of membrane module and bio-reactor, MBR mainly contains two kinds of configurations: immersion and AC system (claiming by-pass flow formula or separated type sometimes).The AC system membrane reactor is mainly used in the processing of trade effluent, be easy to the cleaning and the replacing of film, but power consumption is higher.Compare with the AC system membrane reactor, the maximum characteristics of submerged membrane reactor drum are that operation energy consumption is low, and have advantages such as compact construction, volume are little, and can be used for large-scale sewage work, and this also is the reason that the submerged membrane reactor drum is able to widespread use.Great majority adopt immersion MBR in the world at present.
Film in traditional membrane module adopts micro-filtration/ultra-filtration membrane, and the aperture of micro-filtration is about 0.1 micron, and the aperture of ultra-filtration membrane is greatly between the 0.001-0.01 micron.Because micro-filtration/ultra-filtration membrane aperture is less, can stop bacterium, virus etc. effectively, promoting effluent quality, thereby can play sterilization, remove morbific action of microorganisms.Yet the cost of investment height and the energy consumption of this kind micro-filtration/hyperfiltration membrane assembly are bigger, and this limits it and obtains using more widely.Therefore; The use of gross porosity film appearred afterwards, non-woven fabrics or the non woven fabric processed of synthon for example, and this film mainly utilizes the secondary filtration layer; The settling that promptly forms on its surface along with membrane filtration time lengthening, this secondary filtration layer are realized the actual effectively filtering function of film.Yet usually, along with increasing biomass are deposited on the film surface, this secondary filtration layer can become more and more thicker, finally causes film to block.
Summary of the invention
In view of this, be necessary to provide the Sewage treatment systems that a kind of cost is low, energy consumption is low.
And a kind of sewage water treatment method that adopts above-mentioned Sewage treatment systems is provided.
A kind of Sewage treatment systems; Be provided with the bio-reactor of partition wall in it comprises, said partition wall is divided into anoxic chamber and film reaction chamber with bio-reactor, and said partition wall offers the passage that is communicated with said film reaction chamber and anoxic chamber; Sewage is got into by said anoxic chamber; Discharged by the film reaction chamber through anoxic chamber and processing back, film reaction chamber, the denitrification processing is carried out to sewage in said anoxic chamber, and it is organic with removal that said film reaction chamber is used for that sewage is carried out the nitration reaction denitrogenation; Said film reaction chamber comprises membrane module and air diffuser, said membrane module comprise flat sheet membrane with above-mentioned Sewage treatment systems and be located at the nylon nethike embrane on the flat sheet membrane.
And, a kind of sewage water treatment method that adopts above-mentioned Sewage treatment systems, it may further comprise the steps:
It is indoor that sewage is imported anoxic, makes sewage under anoxia condition, carry out denitrification and handle;
The sewage of handling through the anoxic chamber gets into the film reaction chamber, to the indoor aeration of film reaction, provides dissolved oxygen to membrane module through air diffuser, makes sewage carry out nitration reaction denitrogenation and organic removal;
After handle the film reaction chamber, discharge water and mud after handling.
Compared with prior art, said Sewage treatment systems and method when carrying out WWT, do not need very big aeration rate recoil through the filteration of nylon membrane, and aeration intensity is low, saves energy consumption than conventional film technology; And film is not easy to form and blocks, and cleans cost thereby save.
Description of drawings
Fig. 1 is the Sewage treatment systems structural representation of the embodiment of the invention.
Fig. 2 is that the sulfur-bearing acid group of the embodiment of the invention is useless, the mixed liquor suspended solid, MLSS (MLSS) in the sewage water treatment method operational process is with change curve working time.
Fig. 3 is that the sulfur-bearing acid group of the embodiment of the invention is useless, the flow rate of water flow in the sewage water treatment method operational process and flow be with change curve working time.
Fig. 4 is that the sulfur-bearing acid group of the embodiment of the invention is useless, the pH value of the water in the sewage water treatment method operational process is with change curve working time.
Fig. 5 is that the sulfur-bearing acid group of the embodiment of the invention is useless, the water temperature in the sewage water treatment method operational process is with change curve working time.
Fig. 6 is that the sulfur-bearing acid group of the embodiment of the invention is useless, the water inlet in the sewage water treatment method operational process and total suspended matter solid (TSS) concentration in the water outlet and TSS removal efficient is with change curve working time.
Fig. 7 is that the sulfur-bearing acid group of the embodiment of the invention is useless, the water inlet in the sewage water treatment method operational process and the COD in the water outlet (COD) and COD removal efficient is with change curve working time.
Fig. 8 is that the sulfur-bearing acid group of the embodiment of the invention is useless, the water inlet in the sewage water treatment method operational process and the biological oxygen demand in the water outlet (BOD) and BOD removal efficient is with change curve working time.
Fig. 9 is that the sulfur-bearing acid group of the embodiment of the invention is useless, the water inlet in the sewage water treatment method operational process and (TKN) concentration of the total organic nitrogen in the water outlet and TKN removal efficient is with change curve working time.
Figure 10 is that the sulfur-bearing acid group of the embodiment of the invention is useless, the water inlet in the sewage water treatment method operational process and the NH in the water outlet
4-N concentration and removal efficient thereof are with change curve working time.
Figure 11 is that the sulfur-bearing acid group of the embodiment of the invention is useless, the water inlet in the sewage water treatment method operational process and the nitride concentration in the water outlet and removal efficient thereof is with change curve working time.
Figure 12 is that the sulfur-bearing acid group of the embodiment of the invention is useless, the water inlet in the sewage water treatment method operational process and the nitrate concentration in the water outlet be with change curve working time.
Figure 13 is that the sulfur-bearing acid group of the embodiment of the invention is useless, adopt in the sewage water treatment method operational process film before and after the back flushing to pass through pressure (TMP) with change curve working time.
Embodiment
In order to make the object of the invention, technical scheme and advantage clearer,, the present invention is further elaborated below in conjunction with accompanying drawing and embodiment.Should be appreciated that specific embodiment described herein only in order to explanation the present invention, and be not used in qualification the present invention.
See also Fig. 1; The Sewage treatment systems 10 of the embodiment of the invention comprise successively the homogeneous pond 12 that is communicated with, in be provided with the bio-reactor 14 and the outlet sump 16 of partition wall 13; Partition wall 13 is divided into anoxic chamber 15 and film reaction chamber 17 with bio-reactor 14; Partition wall 14 offers the passage that is communicated with film reaction chamber 17 and anoxic chamber 15, and promptly opening 18.
In the present embodiment,, original sewage carries out filter just through a grid 11 earlier before getting into homogeneous pond 12, to remove the big foreign material of particle.The aperture of grid 11 is about the 2-5 millimeter, is preferably 3 millimeters.Sewage through after grid 11 filter just gets into homogeneous pond 12, gets into anoxic chamber 15 then, and the water after handling through anoxic chamber 15 and film reaction chamber 17 enters outlet sump 16, and mud is then discharged by the bottom of film reaction chamber 17.In addition; Can after through grid 11 filter just, water inlet trier 112 be set respectively; So that the various indexs of the sewage before handling are measured; And set out water sampler 162 in the outlet of outlet sump 16, so that the various indexs of the sewage after handling are measured, assess thereby can the sewage each item index before and after handling be carried out treatment effect.
Particularly, contain microorganism active mud in the anoxic chamber 15, be used for that sewage is carried out denitrification and handle.Further, anoxic chamber 15 also can be provided with stirring mixer, mixes the increase processing efficiency with what promote sewage and mud.Film reaction chamber 17, Aerobic Pond just, it is used for the nitration reaction denitrogenation and removes organicly, comprises membrane module 172 and air diffuser 174, and membrane module 172 comprises flat sheet membrane and is located at the nylon nethike embrane on the flat sheet membrane that flat sheet membrane can adopt the multilayer lamina membranacea.Air diffuser 174 links to each other with an aerator 176, and air diffuser 174 is positioned at the bottom position of membrane module 172, is used for aeration in film reaction chamber 17 continuously, and sufficient mixing and dissolved oxygen are provided, and keeps the required dissolved oxygen in film reaction chamber 17.The aerator 176 of present embodiment adopts the continuous aeration mode that aeration is carried out in film reaction chamber 17.In sewage treatment process; Mikrobe in the film reaction chamber 17 forms the structure of a similar biological filter cake on the film surface of flat sheet membrane together with the extracellular polymeric of microorganism secretion etc.; Effluent stream in the film reaction chamber 17 is crossed biological filter cake of this layer and the film itself that the film surface forms, and the water outlet after the filtration is transported in the outlet sump 16 with peristaltic pump.
At the reflux pump 19 that also comprises between anoxic chamber 15 and the film reaction chamber 17 sewage backflow to the anoxic chamber 15 after handling through film reaction chamber 17, realize the internal recycle between anoxic chamber 15 and the film reaction chamber 17, make sewage obtain treatment effect more fully.
Wherein, flat sheet membrane comprises two-layer porous lamina membranacea, and the tiling of every layer of template surface is one deck nylon nethike embrane fixedly.The aperture of every layer of template is the 1-10 millimeter, and effective filtration area is greater than 50% of the template total area, and this effective filtration area depends on the filter pore area of template.
Continue to consult Fig. 1, below introduce the treatment process of the treatment system in the present embodiment, may further comprise the steps: it is indoor that (1) imports anoxic with sewage, makes sewage under anoxia condition, carry out denitrification and handle; (2) sewage of handling through the anoxic chamber gets into the film reaction chamber; To the indoor aeration of film reaction, provide dissolved oxygen through air diffuser, make sewage carry out nitration reaction denitrogenation and organic removal to membrane module; (3) after handle the film reaction chamber, discharge water and mud after handling.
Particularly, sewage is mentioned on the ground from the direct pump of blowdown outfall sewer net, through entering system after 3 millimeters grids 11 filter just with pump.The sewage of just filtering through grid 11 at first gets into a homogeneous pond 12; Mode with even flow gets into biological reaction tank 14 again, and in biological reaction tank 14, sewage is introduced into anoxic pond 15; Through the internal recycle between anoxic pond 15 and the film reaction chamber 17; Reach the purpose of removing organic and denitrogenation, last clear water flows into outlet sump 16, and mud is discharged by the bottom.The effective film flux is that every square metre of film is handled 3-10 cubic meter sewage every day, and present embodiment adopts the processing power of 4 cubic metres of sewage.
In treating processes; Air diffuser 174 carries out aeration continuously in film reaction chamber 17, this is different from traditional intermittent aeration mode, and traditional intermittent aeration mode need be used very big aeration rate recoil at set intervals; To reduce the settling on reaction film, avoid blocking fenestra.And the sewage water treatment method of present embodiment; Since adopt the nylon nethike embrane overanxious, aeration rate recoil that need not be very big, and aeration rate is less than 20 times of the processing water yield; This kind aeration intensity is low; Only need in film reaction chamber 17, to carry out aeration continuously, save at least 50% energy consumption than conventional film technology with lower aeration intensity.
In addition; Because the good overanxious performance of nylon nethike embrane, the treatment process of present embodiment operation continuously can be cleaned film without chemical reagent more than 6 months; Only certain interval of time can prevent promptly that with the water outlet recoil film from polluting; Keep lower film and pass through pressure (Transmembrane Pressures abbreviates TMP as), can reduce cost thus.Particularly, in treating processes, be preferably 48 hours with the water outlet recoil in every interval 12-72 hour, make flat sheet membrane keep unimpeded.Decide according to the lamina membranacea quantity of flat sheet membrane and area etc. concrete pitch time, and the lamina membranacea of flat sheet membrane is more and areas are big more, and then pitch time is short more.In addition, in treating processes, remain water level in the anoxic pond 15 a little more than the water level of film reaction chamber 17.
Below with a pilot scale biological reaction tank example; The useful volume of this biological reaction tank is 1.5 cubic metres; Operational condition is: hydraulic detention time is 6 hours; Solid retention time is 15-50 days, and mixed liquor suspended solid, MLSS (Mixed Liquor Suspended Solids abbreviates MLSS as) concentration is 2000-4000mg/L.
In the pilot scale process, carry out the test of following various operating parameterss.
1. the membrane flux of sewage: membrane flux is big more, and the processing power of technology is big more, and cost is low more.Present embodiment is respectively with 1m
3/ m
2D (cubic meter/square metre. day), 2m
3/ m
2D, 3m
3/ m
2.d and 4m
3/ m
2.d four kinds of membrane fluxs are as subjects, and to keep mixed liquor suspended solid, MLSS concentration in the steady stage be 4500mg/L, and membrane area is constant, obtains a result like following table:
Processing property parameter under the different membrane fluxs of table 1
Usually F/M is big more, and HRT is more for a short time to show that the processing efficiency of system is high more, and the membrane flux of common MBR is merely 0.2-0.5.Thereby this shows to show that native system is under the condition of higher membrane flux, and when membrane flux increased, HRT still can descend with certain proportion, explains that this system can works better under higher membrane flux, guarantees aquifer yield, and the situation of film obstruction can not occur.
2. mixed liquor suspended solid, MLSS concentration: present embodiment respectively with 0-150mg/L (low scope), 0-1500mg/L (high scope) and three kinds of concentration of 0-15000mg/L (higher scope) as subjects; And maintenance flow unchanged; The F/M proportional range is 0.1-0.2g COD/g MLSSd, and solid retention time (So1id Retention Time abbreviates SRT as) is in 25-60 days scopes; The aeration constant rate is 3L/min, and membrane flux suitably is adjusted into 1.7m
3/ m
2D, obtain a result like following table:
Processing property parameter under the different mixed solution suspended sediment concentrations of table 2
Relation research according to common MBR membrane flux and living weight (MLSS) can be known, after MLSS increases to a certain degree, then because the film blockage problem can't continue to increase membrane flux.And in native system,, MLSS still can guarantee higher membrane flux (1.7) when being 6000.Generally speaking, activated sludge concentration high more (being that MLSS is high more) in the MBR technology, the processing power of sewage is strong more.Therefore, the data declaration native system of table 2 can move under higher load, and can reach desired process well effect.
In addition, it is following when pilot scale, to have measured other parameters:
Flooding parameter: pH, TSS (total suspended matter solid), BOD
5(biochemical oxygen demand on the 5th)., Total COD (COD) (COD), NH
4 +-N (ammonia nitrogen), TKN (total organic nitrogen), NO
2-N (nitrite nitrogen), NO
3-N (nitric nitrogen), (TN) (total nitrogen), DO (dissolved oxygen) and temperature
In the mixing solutions: pH, MLSS, DO (film reaction is indoor) and temperature
Water outlet parameter: TSS, BOD
5, COD, NH
4 +-N, TKN, NO
2-N, NO
3-N, TN and temperature.
Concrete mensuration result is shown in Fig. 2-13.Can know that by figure the various range of operating parameters of present embodiment are following:
Flow: 2-3m
3/ d
Flow velocity: 3-5m/d
pH：5.5-7.0
Water temperature: be stable at 22-26 ℃ in the processing later stage
Can know that from Fig. 6 the total suspended matter solids concn is stabilized in 100-300mg/L in the water inlet, handle back water outlet total suspended matter solids concn and maintain lower level that below 20mg/L, suspended substance solid clearance on average reaches 92% greatly.
Can know that from Fig. 7 the COD concentration stabilize is at 200-400mg/L in the water inlet, the COD concentration of handling the back water outlet maintains lower level, and below 100mg/L, the COD clearance on average reaches 90% greatly.
Can know that from Fig. 8 the BOD concentration stabilize is at 100-200mg/L in the water inlet, the BOD concentration of handling the back water outlet maintains lower level, and below 50mg/L, the BOD clearance on average reaches 90% greatly.
Can know that from Fig. 9 the total organic nitrogen concentration stabilize is at 20-40mg/L in the water inlet, the total organic nitrogen concentration of handling the back water outlet maintains lower level, and below 10mg/L, the organonitrogen clearance on average reaches 93% greatly.
Can know that from Figure 10 ammonia nitrogen concentration is stabilized in 30mg/L in the water inlet, the ammonia nitrogen concentration of handling the back water outlet maintains lower level, and below 2mg/L, ammonia nitrogen removal frank on average reaches 93% greatly.
Can know that from Figure 11 and 12 concentration of nitric acid of handling the back water outlet is lower, greatly below 1mg/L.
Can know that from Figure 13 after the each back flushing of process, film passes through pressure and gets back to new membrane stage basically, therefore not need matting.
Last process result is as shown in the table:
The removal effect table of this treatment process of table 3
| Parameter | Remove |
| COD | |
| 92 | |
| TSS | 94 |
| TN | 81 |
| |
93 |
Can be known that by last table the removal efficient of the COD of the sewage water treatment method of present embodiment, TSS, ammonia nitrogen is all up to more than 90%, the removal efficient of TN also can reach 81%, shows excellent treatment effect.Because present embodiment has adopted the nylon nethike embrane to filter, in sewage treatment process, do not need very big aeration rate recoil, aeration intensity is low, saves at least 50% energy consumption than conventional film technology; And film is not easy to form and blocks, and cleans cost thereby save.In addition, also fenestra and effective filtration area are designed, to reach good wastewater treatment efficiency.
The above is merely preferred embodiment of the present invention, not in order to restriction the present invention, all any modifications of within spirit of the present invention and principle, being done, is equal to and replaces and improvement etc., all should be included within protection scope of the present invention.
Claims (9)
1. Sewage treatment systems; Be provided with the bio-reactor of partition wall in it comprises, said partition wall is divided into anoxic chamber and film reaction chamber with bio-reactor, and said partition wall offers the passage that is communicated with said film reaction chamber and anoxic chamber; Sewage is got into by said anoxic chamber; Discharged by the film reaction chamber through anoxic chamber and processing back, film reaction chamber, the denitrification processing is carried out to sewage in said anoxic chamber, and it is organic with removal that said film reaction chamber is used for that sewage is carried out the nitration reaction denitrogenation; Said film reaction chamber comprises membrane module and air diffuser, and said membrane module comprises flat sheet membrane and is located at the nylon nethike embrane on the flat sheet membrane.
2. Sewage treatment systems as claimed in claim 1 is characterized in that said air diffuser is located at the bottom position of membrane module, is used for continuously to the indoor aeration of film reaction, to keep the required dissolved oxygen in film reaction chamber.
3. Sewage treatment systems as claimed in claim 1 is characterized in that, said flat sheet membrane comprises two-layer porous lamina membranacea, and fixedly one deck nylon nethike embrane tiles on every layer of foraminous die plate surface.
4. Sewage treatment systems as claimed in claim 3 is characterized in that, the aperture of every layer of foraminous die plate is the 1-10 millimeter, and effective filtration area is greater than 50% of the template total area.
5. sewage water treatment method; The bio-reactor that is provided with partition wall in using carries out WWT; Said partition wall is divided into anoxic chamber and film reaction chamber with bio-reactor, and said partition wall offers the passage that is communicated with said film reaction chamber and anoxic chamber, and said film reaction chamber comprises membrane module and air diffuser; Said membrane module comprises flat sheet membrane and is located at the nylon nethike embrane on the flat sheet membrane that this method may further comprise the steps:
It is indoor that sewage is imported anoxic, makes sewage under anoxia condition, carry out denitrification and handle;
The sewage of handling through the anoxic chamber gets into the film reaction chamber, to the indoor aeration of film reaction, provides dissolved oxygen to membrane module through air diffuser, makes sewage carry out nitration reaction denitrogenation and organic removal;
After handle the film reaction chamber, discharge water and mud after handling.
6. sewage water treatment method as claimed in claim 5 is characterized in that, in treating processes, makes flat sheet membrane keep unimpeded with the water outlet recoil in every interval 12-72 hour.
7. sewage water treatment method as claimed in claim 5 is characterized in that, the effective film flux of said membrane module is that every square metre of film is handled 3-10 cubic meter sewage every day.
8. sewage water treatment method as claimed in claim 5 is characterized in that, said air diffuser is continuously and quantitatively to the indoor aeration that carries out of film reaction, and the aeration rate of said aeration is less than 20 times of the processing water yield.
9. sewage water treatment method as claimed in claim 5 is characterized in that, through after the WWT; COD concentration is below 100mg/L, and BOD concentration is at 50mg/L, and total organic nitrogen concentration is below 10mg/L; Ammonia nitrogen concentration is below 2mg/L, below the total solids concentration 20mg/L.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200810217945A CN101734793B (en) | 2008-11-27 | 2008-11-27 | Sewage treatment system and sewage treatment method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200810217945A CN101734793B (en) | 2008-11-27 | 2008-11-27 | Sewage treatment system and sewage treatment method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101734793A CN101734793A (en) | 2010-06-16 |
| CN101734793B true CN101734793B (en) | 2012-10-10 |
Family
ID=42458905
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200810217945A Active CN101734793B (en) | 2008-11-27 | 2008-11-27 | Sewage treatment system and sewage treatment method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101734793B (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101863590B (en) * | 2010-06-17 | 2011-11-16 | 同济大学 | Combined anoxic/aerobic enhanced biological activated carbon dynamic membrane nitrogen and phosphorus removal process |
| CN103922535B (en) * | 2013-01-16 | 2015-09-30 | 成都康洁水务有限公司 | A kind of MBMBR sewerage disposing device |
| CN104611246B (en) * | 2013-11-05 | 2017-12-15 | 中国石油化工股份有限公司 | A kind of synchronous culture nitrifier and the method for aerobic denitrifying bacteria |
| CN105502843B (en) * | 2016-01-19 | 2018-02-09 | 清华大学 | Sewage disposal system and application thereof |
| CN105884128A (en) * | 2016-04-09 | 2016-08-24 | 深圳市赛威赢环境技术工程有限公司 | Nickel-containing wastewater treating system and method |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6616843B1 (en) * | 1998-12-18 | 2003-09-09 | Omnium De Traitement Et De Valorisation | Submerged membrane bioreactor for treatment of nitrogen containing water |
| CN1524810A (en) * | 2003-02-28 | 2004-09-01 | 杭玉君 | Method for cyclically utilizing middle water of public toilet sewage and specialized equipment therefor |
| EP1484287A1 (en) * | 2002-02-01 | 2004-12-08 | Universidade De Santiago De Compostela | Hybrid biological membrane reactor for the treatment of urban and industrial waste water |
| CN1785829A (en) * | 2005-11-15 | 2006-06-14 | 中国科学院生态环境研究中心 | Composite membrane bioreactor |
| CN1800052A (en) * | 2006-01-12 | 2006-07-12 | 上海大学 | Integral membrane biological reaction device for water treatment |
-
2008
- 2008-11-27 CN CN200810217945A patent/CN101734793B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6616843B1 (en) * | 1998-12-18 | 2003-09-09 | Omnium De Traitement Et De Valorisation | Submerged membrane bioreactor for treatment of nitrogen containing water |
| EP1484287A1 (en) * | 2002-02-01 | 2004-12-08 | Universidade De Santiago De Compostela | Hybrid biological membrane reactor for the treatment of urban and industrial waste water |
| CN1524810A (en) * | 2003-02-28 | 2004-09-01 | 杭玉君 | Method for cyclically utilizing middle water of public toilet sewage and specialized equipment therefor |
| CN1785829A (en) * | 2005-11-15 | 2006-06-14 | 中国科学院生态环境研究中心 | Composite membrane bioreactor |
| CN1800052A (en) * | 2006-01-12 | 2006-07-12 | 上海大学 | Integral membrane biological reaction device for water treatment |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101734793A (en) | 2010-06-16 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Davies et al. | Intensified activated sludge process with submerged membrane microfiltration | |
| CN101928096B (en) | Sewage treatment method and system in ecological sensitive areas | |
| US9975796B2 (en) | Process, apparatus and membrane bioreactor for wastewater treatment | |
| US9512021B2 (en) | Membrane system and method for treating sewage and wastewater capable of automated removal/destruction of scum/foam with high energy efficiency, high flux and low operation costs and haying process conversion method from constant level continuous batch reactor process | |
| DE60304456T2 (en) | MEMBRANE HYBRID BIOREACTOR FOR THE TREATMENT OF URBAN AND INDUSTRIAL WASTE WATER | |
| CN107021597A (en) | Improve the system and method for biochemical and deeply treating wastewater using Powdered Activated Carbon | |
| CN101734793B (en) | Sewage treatment system and sewage treatment method | |
| US20120012524A1 (en) | Membrane bioreactor process | |
| CN105884128A (en) | Nickel-containing wastewater treating system and method | |
| CN109264859A (en) | A2O2Sewage disposal system and its processing method | |
| CN111170458A (en) | Two-stage AO efficient nitrogen and phosphorus removal sewage treatment process | |
| CN115818862A (en) | Cold water area mariculture tail water treatment system | |
| CN215480419U (en) | Combined sewage treatment system combining oxidation ditch and deep bed denitrification filter | |
| CN105110556A (en) | Integrated denitrification decarbonization biological aerated filter and processing system thereof | |
| KR101186606B1 (en) | Advanced treatment apparatus to removing nitrogen and phosphorus from wastewater | |
| KR101044826B1 (en) | An operation method to increase advanced treatment efficiency in membrane bio reacter and an advanced treatment appartus there of | |
| Blšt’áková et al. | Domestic wastewater treatment with membrane filtration—two years experience | |
| Guglielmi et al. | Membrane bioreactors for winery wastewater treatment: case-studies at full scale | |
| Ng et al. | Effects of solid retention time on the performance of submerged anoxic/oxic membrane bioreactor | |
| AU2020101380A4 (en) | Milking parlour wastewater treatment system and method | |
| CN210825845U (en) | MBR application effluent treatment plant | |
| RU2644904C1 (en) | Method of biological purification of wastewater from nitrogen phosphoric and organic compounds | |
| CN208700837U (en) | A kind of recovery processing structure for sewage | |
| KR19990083645A (en) | Organic material and nitrogen, phosphate removal method using intermitted aeration process and plate type microfiltration membrane | |
| Rachmani | Cost and Performance Comparison of a Membrane Bioreactor (MBR) Plant and a Bardenpho Plant for Wastewater Treatment |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |