CN101734793A - Sewage treatment system and sewage treatment method - Google Patents
Sewage treatment system and sewage treatment method Download PDFInfo
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- CN101734793A CN101734793A CN200810217945A CN200810217945A CN101734793A CN 101734793 A CN101734793 A CN 101734793A CN 200810217945 A CN200810217945 A CN 200810217945A CN 200810217945 A CN200810217945 A CN 200810217945A CN 101734793 A CN101734793 A CN 101734793A
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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 is subjected to masses' attention.Bioremediation is adopted in comparatively effective and feasible sewage disposal at present usually.For example, traditional biological treatment uses secondary sedimentation basins to come sewage is handled.Yet when carrying out sewage disposal, sewage also needs just can discharge through the secondary sedimentation basins post precipitation through behind the biochemical reaction, causes the process of sewage disposal longer.In addition, adopt the treatment process floor space of secondary sedimentation basins big, the cost of investment height.Especially when operation mud age was higher, this can cause bad sludge settling.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 precipitation, filtering technique, and makes water quality after the processing directly reach the level of (being better than) emission standard.Membrane bioreactor has many clear superiorities, for example has that system handles efficient height, High Load Rate, floor space are little, an advantage such as ` displacement mass height and mud end product amount are low.
Typical membrane bioreactor comprises membrane module and bio-reactor, a large amount of microorganism (active sludge) fully contacts with matrix (labile organic compound in the waste water etc.) in membrane bioreactor, carry out metabolism to keep growth by oxygenolysis, breeding, make organic pollutant degradation simultaneously, membrane module passes through mechanical grading, effect such as hold back is carried out solid-liquid separation to waste water and mud mixed liquid, the combination of biological treatment system and membrane module, 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, make 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 characteristics of submerged membrane reactor maximum are that operation energy consumption is low, and have advantages such as compact construction, volume be little, and can be used for large-scale sewage work, and this also is the reason that the submerged membrane reactor 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 made of synthon for example, and this film mainly utilizes the secondary filtration layer, promptly along with the settling of membrane filtration time lengthening in its surface formation, this secondary filtration layer is 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 provide a kind of sewage water treatment method that adopts above-mentioned Sewage treatment systems.
A kind of Sewage treatment systems, in comprising, it is provided with the bio-reactor of partition wall, described partition wall is divided into anoxic chamber and film reaction chamber with bio-reactor, described partition wall offers the passage that is communicated with described film reaction chamber and anoxic chamber, sewage is entered by described anoxic chamber, discharge by the film reaction chamber through anoxic chamber and processing back, film reaction chamber, described anoxic chamber is carried out denitrification to sewage and is handled, described film reaction chamber is used for sewage is carried out the nitration reaction denitrogenation and removes organic, described film reaction chamber comprises membrane module and air diffuser, described membrane module comprise flat sheet membrane with above-mentioned Sewage treatment systems and be located at 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 carry out denitrification under anoxia condition and handle;
The sewage of handling through the anoxic chamber enters the film reaction chamber, to the indoor aeration of film reaction, provides dissolved oxygen to membrane module by 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, described Sewage treatment systems and method when carrying out sewage disposal, do not need very big aeration rate recoil by 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 chemical oxygen demand (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 NH4-N concentration in the water outlet and removal efficient thereof is 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 the saturating pressure of film (TMP) before and after the back flushing with change curve working time.
Embodiment
In order to make purpose of the present invention, technical scheme and advantage clearer,, the present invention is further elaborated below in conjunction with drawings and Examples.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, before entering homogeneous pond 12, original sewage carries out filter just through a grid 11 earlier, to remove the big foreign material of particle.The aperture of grid 11 is about the 2-5 millimeter, is preferably 3 millimeters.Enter homogeneous pond 12 through the sewage after grid 11 filter just, enter anoxic chamber 15 then, enter outlet sump 16 through the water after anoxic chamber 15 and 17 processing of film reaction chamber, mud is then discharged by the bottom of film reaction chamber 17.In addition, can after through grid 11 filter just, water inlet sampler 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 the every index of sewage before and after handling can 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 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, microorganism 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 floor 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.
Also comprising between anoxic chamber 15 and the film reaction chamber 17 with the reflux pump 19 of the sewage backflow after handling through film reaction chamber 17 to anoxic chamber 15, 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 carry out denitrification under anoxia condition and handle; (2) sewage of handling through the anoxic chamber enters the film reaction chamber, to the indoor aeration of film reaction, provide dissolved oxygen by 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, just entered system after the filter through 3 millimeters grids 11 with pump.The sewage of just filtering through grid 11 at first enters a homogeneous pond 12, mode with Continuous Flow enters biological reaction tank 14 again, in biological reaction tank 14, sewage is introduced into anoxic pond 15, by 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 needs at set intervals with very big aeration rate recoil, to reduce the settling on reaction film, avoid blocking fenestra.And the sewage water treatment method of present embodiment, owing to adopt the nylon nethike embrane overanxious, aeration rate recoil that need not be very big, 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 moves more than 6 months continuously, can clean film without chemical reagent, only certain interval of time can prevent promptly that with the water outlet recoil film from polluting, keep the saturating pressure of lower film (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 many more and area is 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, 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 sky), 2m
3/ m
2D, 3m
3/ m
2D and 4m
3/ m
2Four kinds of membrane fluxs of d 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 as 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 only is 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, illustrates that this system can works better under higher membrane flux, guarantees aquifer yield, and the situation that film stops up 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 keep flow constant, the F/M proportional range is 0.1-0.2g COD/g MLSSd, and solid retention time (Solid RetentionTime, abbreviate SRT as) 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 as following table:
Processing property parameter under the different mixed solution suspended sediment concentrations of table 2
According to the relation research of common MBR membrane flux and biomass (MLSS) as 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, when being 6000, MLSS still can guarantee higher membrane flux (1.7).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 good treatment effect.
In addition, it is as follows to have measured other parameters when pilot scale:
Flooding parameter: pH, TSS (total suspended matter solid), BOD
5(biochemical oxygen demand (BOD) on the 5th), Total COD (COD) (chemical oxygen demand (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 measurement result is shown in Fig. 2-13.As seen from the figure, the various range of operating parameters of present embodiment are as follows:
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
As can be seen from Figure 6, the total suspended matter solids concn is stabilized in 100-300mg/L in the water inlet, handles back water outlet total suspended matter solids concn and maintains lower level, and below 20mg/L, suspended substance solid clearance on average reaches 92% greatly.
As can be seen from Figure 7, the COD concentration stabilize is at 200-400mg/L in the water inlet, and the COD concentration of handling the back water outlet maintains lower level, and below 100mg/L, the COD clearance on average reaches 90% greatly.
As can be seen from Figure 8, the BOD concentration stabilize is at 100-200mg/L in the water inlet, and the BOD concentration of handling the back water outlet maintains lower level, and below 50mg/L, the BOD clearance on average reaches 90% greatly.
As can be seen from Figure 9, the total organic nitrogen concentration stabilize is at 20-40mg/L in the water inlet, and 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.
As can be seen from Figure 10, ammonia nitrogen concentration is stabilized in 30mg/L in the water inlet, and 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.
From Figure 11 and 12 as can be known, the concentration of nitric acid of handling the back water outlet is lower, greatly below 1mg/L.
As can be seen from Figure 13, after the each back flushing of process, the saturating pressure of film is got back to new membrane stage substantially, does not therefore need matting.
The result of Chu Liing is as shown in the table at last:
The removal effect table of this treatment process of table 3
| Parameter | Remove efficient |
| ??COD | ??92 |
| ??TSS | ??94 |
| ??TN | ??81 |
| Ammonia nitrogen | ??93 |
As seen from the above 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%, and 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 only is preferred embodiment of the present invention, not in order to restriction the present invention, all any modifications of being done within the spirit and principles in the present invention, 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, in comprising, it is provided with the bio-reactor of partition wall, described partition wall is divided into anoxic chamber and film reaction chamber with bio-reactor, described partition wall offers the passage that is communicated with described film reaction chamber and anoxic chamber, sewage is entered by described anoxic chamber, discharge by the film reaction chamber through anoxic chamber and processing back, film reaction chamber, described anoxic chamber is carried out denitrification to sewage and is handled, described film reaction chamber is used for sewage is carried out the nitration reaction denitrogenation and removes organic, described film reaction chamber comprises membrane module and air diffuser, and described membrane module comprises flat sheet membrane and is located at nylon nethike embrane on the flat sheet membrane.
2. Sewage treatment systems as claimed in claim 1 is characterized in that described 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, described 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 1 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, carry out sewage disposal with the interior bio-reactor that is provided with partition wall, described partition wall is divided into anoxic chamber and film reaction chamber with bio-reactor, described partition wall offers the passage that is communicated with described film reaction chamber and anoxic chamber, described film reaction chamber comprises membrane module and air diffuser, described membrane module comprises flat sheet membrane and is located at 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 carry out denitrification under anoxia condition and handle;
The sewage of handling through the anoxic chamber enters the film reaction chamber, to the indoor aeration of film reaction, provides dissolved oxygen to membrane module by 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, described effective film flux 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, described air diffuser is continuously and quantitatively to the indoor aeration that carries out of film reaction, and described aeration rate 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 sewage disposal, 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.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101863590A (en) * | 2010-06-17 | 2010-10-20 | 同济大学 | Combined anoxic/aerobic enhanced biological activated carbon dynamic membrane nitrogen and phosphorus removal process |
| CN103922535A (en) * | 2013-01-16 | 2014-07-16 | 成都康洁水务有限公司 | Apparatus for processing reclaimed water in MBMBR |
| CN104611246A (en) * | 2013-11-05 | 2015-05-13 | 中国石油化工股份有限公司 | Synchronous cultivation method of nitrobacteria and aerobic denitrobacteria |
| CN105502843A (en) * | 2016-01-19 | 2016-04-20 | 清华大学 | Sewage treatment system and use 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 |
Family Cites Families (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 |
| ES2190895B2 (en) * | 2002-02-01 | 2004-05-16 | Universida De Santiago De Compostela | HYBRID BIOLOGICAL REACTOR OF MEMBRANES FOR TREATMENT OF INDUSTRIAL AND URBAN RESIDUAL WATERS. |
| CN100344559C (en) * | 2003-02-28 | 2007-10-24 | 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 |
| CN100357197C (en) * | 2006-01-12 | 2007-12-26 | 上海大学 | Integral membrane biological reaction device for water treatment |
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2008
- 2008-11-27 CN CN200810217945A patent/CN101734793B/en active Active
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101863590A (en) * | 2010-06-17 | 2010-10-20 | 同济大学 | Combined anoxic/aerobic enhanced biological activated carbon dynamic membrane nitrogen and phosphorus removal process |
| 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 |
| CN103922535A (en) * | 2013-01-16 | 2014-07-16 | 成都康洁水务有限公司 | Apparatus for processing reclaimed water in MBMBR |
| 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 |
| CN104611246A (en) * | 2013-11-05 | 2015-05-13 | 中国石油化工股份有限公司 | Synchronous cultivation method of nitrobacteria and aerobic denitrobacteria |
| 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 |
| CN105502843A (en) * | 2016-01-19 | 2016-04-20 | 清华大学 | Sewage treatment system and use 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 |
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| Publication number | Publication date |
|---|---|
| CN101734793B (en) | 2012-10-10 |
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