CN102285718A - Method for treating ammonia nitrogen wastewater - Google Patents
Method for treating ammonia nitrogen wastewater Download PDFInfo
- Publication number
- CN102285718A CN102285718A CN2011102340273A CN201110234027A CN102285718A CN 102285718 A CN102285718 A CN 102285718A CN 2011102340273 A CN2011102340273 A CN 2011102340273A CN 201110234027 A CN201110234027 A CN 201110234027A CN 102285718 A CN102285718 A CN 102285718A
- Authority
- CN
- China
- Prior art keywords
- reactor
- ammonia nitrogen
- waste water
- swash plate
- nitrogen waste
- 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.)
- Granted
Links
- 238000000034 method Methods 0.000 title claims abstract description 35
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 title claims abstract description 22
- 239000002351 wastewater Substances 0.000 title claims abstract description 17
- 238000006243 chemical reaction Methods 0.000 claims abstract description 32
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 28
- 239000010802 sludge Substances 0.000 claims abstract description 12
- 238000012163 sequencing technique Methods 0.000 claims abstract description 7
- 238000006396 nitration reaction Methods 0.000 claims description 24
- 239000011259 mixed solution Substances 0.000 claims description 16
- 238000001556 precipitation Methods 0.000 claims description 9
- 238000012545 processing Methods 0.000 claims description 9
- 239000007789 gas Substances 0.000 claims description 8
- 125000004122 cyclic group Chemical group 0.000 claims description 5
- 239000002244 precipitate Substances 0.000 claims description 5
- 239000000047 product Substances 0.000 claims description 4
- 239000000758 substrate Substances 0.000 claims description 4
- 238000005273 aeration Methods 0.000 abstract description 14
- 230000000694 effects Effects 0.000 abstract description 8
- 230000001376 precipitating effect Effects 0.000 abstract description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 13
- 238000005516 engineering process Methods 0.000 description 13
- 239000001301 oxygen Substances 0.000 description 13
- 229910052760 oxygen Inorganic materials 0.000 description 13
- 239000007788 liquid Substances 0.000 description 9
- 239000012071 phase Substances 0.000 description 8
- 238000012546 transfer Methods 0.000 description 6
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 238000007599 discharging Methods 0.000 description 4
- 238000004065 wastewater treatment Methods 0.000 description 4
- 230000008021 deposition Effects 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 230000001546 nitrifying effect Effects 0.000 description 3
- 239000010865 sewage Substances 0.000 description 3
- 206010021143 Hypoxia Diseases 0.000 description 2
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 229920001577 copolymer Polymers 0.000 description 2
- 230000007954 hypoxia Effects 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 238000007634 remodeling Methods 0.000 description 2
- 230000000452 restraining effect Effects 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 230000003068 static effect Effects 0.000 description 2
- 208000032843 Hemorrhage Diseases 0.000 description 1
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- 241000220317 Rosa Species 0.000 description 1
- 238000005276 aerator Methods 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 208000034158 bleeding Diseases 0.000 description 1
- 230000000740 bleeding effect Effects 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000012851 eutrophication Methods 0.000 description 1
- 230000002209 hydrophobic effect Effects 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000011954 pollution control method Methods 0.000 description 1
- 239000002861 polymer material Substances 0.000 description 1
- 238000011112 process operation Methods 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000006228 supernatant Substances 0.000 description 1
Images
Landscapes
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Activated Sludge Processes (AREA)
Abstract
The invention relates to a method for treating ammonia nitrogen wastewater. A sequencing batch activated sludge process is performed in a reactor and comprises a water inflow stage, an aeration reaction stage, a precipitating stage, a draining stage and an idle stage. A plurality of layers of inclined plates are arranged in the reactor; air flow in the aeration reaction is blocked and guided by the inclined plates to make mixed liquor in the reactor divided into an aerobic zone and an anoxic zone during the aeration reaction; and the mixed liquor in both zones is circularly moved. The air flow in the aeration reaction is ejected upwards from the bottom of the reactor. The method has the advantages of high treatment efficiency and good treatment effect and is an improved method for treating the ammonia nitrogen wastewater on the basis of the sequencing batch activated sludge process.
Description
Technical field
The present invention relates to a kind of sewage water treatment method, specifically, relate to a kind of method that improved ammonia nitrogen waste water is handled of on the basis of sequencing batch active sludge, carrying out.
Background technology
Polluted by nitrogen has become one of the main factor of destruction water body environment (as causing body eutrophication).Bio-denitrification technology is most widely used nitrate pollution control method.Over nearly 20 years, because the low cost and the high-level efficiency of SBR technology (sequencing batch active sludge), be used widely in countries in the world, technologies such as UNITANK, CAST of coming out more newly developed also have hundreds of seat sewage work to go into operation, and fully demonstrate the glamour of SBR technology.
Improve traditional SBR Process for Treating Municipal denitrogenation dephosphorizing rate, towards thinking efficient, energy-conservation, that the higher direction of level of automation develops, though also exist because of the Inlet and outlet water process operations cumbersome, stop up easily during aeration, research and development New type of S BR technology becomes field very active in the water treatment, as: CAST, embrane method SBR, modified form UniFedSBR, TCBS, MSBR, (AO) 2SBR, A2NSBR, two-stage SBR technology etc.
The ammonia nitrogen waste water treatment unit that existing sequencing batch active sludge adopts mainly comprises: reactor, agitator, aerating apparatus, water feed apparatus, discharging device and automatic control system.Water feed apparatus, discharging device link to each other with reactor respectively; Agitator is positioned at reactor; The part of giving vent to anger of aerating apparatus also is positioned at reactor.The working process of automatic controlling system ammonia nitrogen waste water treatment unit.The mixing of mud, water is finished by reducing motor drive stirring arm in the reactor.
The cycle of operation generally is divided into following several stages: water inlet, aerated reaction, hypoxia response, precipitation, draining and idle stage.Each stage mainly carries out in reactor.Behind the reactor water inlet end, the beginning aerated reaction, after the ammonia nitrogen concentration of liquid to be mixed reaches emission standard, stop aeration, under anoxic environment, realize anti-nitration reaction, mixed solution is remained static in reactor carry out solid-liquid separation, after after a while, get rid of supernatant liquor, precipitating sludge enters the idle stage, reactor is in the holding state of preparing the next cycle operation again, and wherein each stage generation excess sludge will regularly discharge.
Existing ammonia nitrogen waste water treatment method mainly contains following shortcoming: 1. aerated reaction and hypoxia response need carry out respectively, just can reach treatment effect preferably, and the time that two reactions steps occupy is longer; 2. the precipitate phase of mud, the precipitation face mainly is the bottom of reactor, the time that needs is longer, inefficiency, sedimentation effect is undesirable.
Summary of the invention
Technical problem at existing in the prior art the objective of the invention is: a kind of effective raising reaction efficiency and sludge settling efficient are provided, improve the method for the ammonia nitrogen waste water processing of treatment effect.
In order to achieve the above object, the present invention adopts following technical scheme:
The method that a kind of ammonia nitrogen waste water is handled adopts the sequencing batch active sludge that carries out in reactor, comprise into water, aerated reaction, precipitation, draining and idle stage; Be provided with the multilayer swash plate in the reactor, during aerated reaction, the air-flow of aerated reaction stops and leads through swash plate makes the mixed solution in the reactor be divided into aerobic zone and oxygen-starved area, and the mixed solution in two districts forms cyclic motion.
After adopting this method, promptly on existing basis, set up the multilayer swash plate, SBR technology and multilayer swash plate are combined, existing SBR technology is improved.
At first, when aerated reaction, the air-flow of aerated reaction stops and leads through swash plate makes the mixed solution in the reactor be divided into aerobic zone and oxygen-starved area, mixed solution in two districts forms cyclic motion, nitration reaction takes place in aerobic zone, anti-nitration reaction takes place, therefore in the oxygen-starved area, nitration reaction and anti-nitration reaction can take place simultaneously, effectively improve reaction efficiency.
Secondly, swash plate the desilting area that has increased mud is set, improved the deposition efficiency of mud.
At last, need to consume a large amount of oxygen in nitration reaction, often provide by aerating apparatus, oxygen arrives a large amount of microorganism flcos or the microbial film that exists in the mixed solution through solution-air and liquid-solid transmission.Because the solubleness of oxygen in water is lower, the rate of mass transfer between solution-air is the bottleneck of aerobe reaction often.According to the two-film theory of solution-air mass transfer, the transfer rate of oxygen from the gas phase to the liquid phase can be used
Expression.In the formula, k is the mass transfer coefficient (relevant with water quality) of liquid film, and a is the biography oxygen area of mixed solution unit volume, C* and C
bBe respectively the oxygen concn in gas phase main body and the liquid phase main body.When the occupation rate of air in the reactor rose, the bubbles volume in the unit volume increased, and effectively passed the oxygen area and increased, and oxygen transfer rate is accelerated.Therefore nitration reaction efficient is higher, and treatment effect of the present invention is better.
The air-flow of aerated reaction is in the upwards ejection of the bottom of reactor.The up-flow district forms aerobic zone, falls the stream district and forms the oxygen-starved area.The up-flow district is 1: 1 to 3: 1 with the volume ratio of falling the stream district.Nitration reaction takes place in the aerobic zone, and anti-nitration reaction takes place in the oxygen-starved area; The product of nitration reaction is as the substrate of anti-nitration reaction.
After adopting this structure, air-flow can provide the dissolved oxygen of nitration reaction on the one hand, provides power for the cyclic motion between aerobic zone and the oxygen-starved area on the other hand.During the reactor operation, the position of carrying out aeration in the bottom forms the up-flow district, and this up-flow district is an aerobic zone, and bubble moves upward under buoyancy, and wherein major part is overflowed at top, up-flow district.With respect to the up-flow district, other positions of mixed solution form and fall the stream district, and this falls the stream district and is the oxygen-starved area.Because up-flow district and to fall in the stream district gas content different there are differences the density of mixed solution in two districts, the pressure reduction that is caused by density difference makes mixed solution in the up-flow district with fall to flow and form cyclic motion between distinguishing.Aeration in the denitrification process and liquid return are combined, make aeration not only for nitrifying process provides necessary dissolved oxygen, also the backflow for nitrification liquid provides power.The oxygen that common process only utilizes aerator to provide, and this technology also makes full use of the nitrification liquid backflow that this power carries out necessity, thus reduce operating power consumption.
In the method, the nitrification and denitrification reaction takes place simultaneously, and the product of nitration reaction can be the substrate of anti-nitration reaction, thereby avoids the restraining effect of the nitrite accumulation of nitrifying process generation to nitration reaction, accelerates rate of nitrification.
Volume ratio was limited to 1: 1 to 3: 1, can obtains reaction effect preferably.
The multilayer swash plate is a rectangular plate, be arranged in parallel, and spacing is 10 to 50 centimetres, and the angle of swash plate and horizontal plane is 30 to 60 degree.Choosing along with the increase of reactor volume of swash plate spacing increases.Precipitate phase, mud is at the swash plate surface precipitation.
After adopting this structure, on the one hand, at aeration phase, can realize the nitrification and denitrification reaction in the reactor simultaneously, the removal effect of total nitrogen can reach 65% to 85%.On the other hand, at precipitate phase, the shadow area of every swash plate is exactly the desilting area that increases.For example: 10 swash plates are arranged in the reactor, and the area of every swash plate is s, and the pitch angle is 60 degree, the desilting area A=10 * s * cot60=5s of Zeng Jiaing then, and promptly efficient has improved five times.The number of swash plate is determined according to the size of reactor.The spacing of swash plate is at 10 to 50 centimetres, and when the volume of reactor was big, the spacing of swash plate was chosen 50 centimetres, when the volume of reactor hour, the spacing of swash plate is chosen 10 centimetres.
Two relative edges respectively were connected to pipe connecting about swash plate can be taked, and the two ends of pipe connecting are fixed on the structure of reactor wall.After adopting this structure, the pipe connecting of above and below plays the fixedly effect of swash plate, and caliber is very little, and its intensity is as long as satisfy swash plate fixing.Because caliber is little, have no occluder around the swash plate, no sidewise restraint, so not deposition guarantee that little mud flocs unit also can effectively remove.The swash plate spacing is little, but the mud rapid precipitation, and Reynolds number reduces than conventional equipment, can effectively suppress a settled hydraulic pulse of material.
The material of swash plate adopts the fine polymer materials, for example is the second third co-polymer plate.It has good shear stability, has good anti-pressure ability and thermostability simultaneously, and this material has hydrophobic property, is unfavorable for that mud adheres to, and helps spoil disposal.
The aspect ratio of reactor is 3: 1 to 5: 1.When the reactor aspect ratio is low, suitably increase the performance that aspect ratio helps improving reactor.But it is approximate irrelevant that the aspect ratio result shows the height of gas containing ratio in the reactor and riser tube, and liquid circulation rate then increases with the riser tube height.The reactor aspect ratio is not the bigger the better, and its reason is: along with the increase of riser tube height, the also corresponding increase of mixing time in the reactor, and the decline of the solution-air contact area in the unit volume are unfavorable for mixing and mass transfer.
The aerating apparatus and the under meter that carry out aerated reaction join, and under meter connects compressed gas source; Under meter is adjusted the size of the airshed of aerated reaction.Can adjust the size of airshed according to actual needs, making airshed both can satisfy provides necessary dissolved oxygen, and also can satisfy for mixed solution circulates provides necessary driving force.
Description of drawings
Fig. 1 is a schematic diagram of the present invention.
Among the figure, 1 is water tank, and 2 is intake pump, and 3 is escape pipe, and 4 is under meter, and 5 is compressed gas source, and 6 is wet-pit, and 7 is swash plate, and 8 is rising pipe, and 9 is reactor, and 10 is water inlet pipe.
Embodiment
The present invention will be further described in detail below in conjunction with the drawings and specific embodiments.
Figure 1 shows that the ammonia nitrogen waste water treatment unit, comprise reactor 9, agitator, aerating apparatus, water feed apparatus, discharging device and automatic control system.
Wherein, the water inlet of this method, aerated reaction, precipitation, draining and idle stage mainly carry out in reactor.The vertical section of the bottom of reactor is inverted isosceles trapezoid, and the angle that is positioned at the below is 120 degree.Be provided with temperature monitor, well heater and agitator in the reactor.The time series of reactor is controlled automatically by time control switch.Employed all electrical appliances of reactor are controlled automatically by time control switch.Be provided with the orthogonal swash plate that multilayer is parallel to each other in the reactor, the swash plate spacing is 40 centimetres, and the angle of swash plate and horizontal plane is 60 degree.Swash plate is the second third co-polymer plate.Two relative edges up and down of swash plate 7 respectively are provided with pipe connecting, and the two ends of pipe connecting are fixed on reactor wall.The aspect ratio of reactor is 3: 1.
Aerating apparatus is made up of the escape pipe 3 that joins successively, under meter 4 and compressed gas source 5.Wherein escape pipe 3 is arranged on the bottom of reactor 9.
Water feed apparatus comprises water tank 1, intake pump 2 and the water inlet pipe 10 that water route successively joins, and water inlet pipe 10 stretches in the reactor 9.
Discharging device comprises the rising pipe 8 that stretches in the reactor 9, and the some wet-pits of arranging according to height 6 that join with reactor 9.
The operating process of present method is described below:
Under meter 4 aeration rate is as required adjusted flow, and the aerated reaction stage is finished in blast aeration 3 to 10 hours.Escape pipe 3 exhaust that makes progress from the bottom of reactor 9, air-flow stopping and lead through swash plate 7, formation up-flow district above escape pipe 3, this up-flow district is an aerobic zone, and nitration reaction takes place herein.With respect to other zones in the mixed solution in up-flow district, the stream district falls in formation, this falls the stream district and is the oxygen-starved area, anti-nitration reaction takes place herein, the product of nitration reaction can be the substrate of anti-nitration reaction, thereby avoid the restraining effect of the nitrite accumulation of nitrifying process generation, accelerate rate of nitrification nitration reaction.The up-flow district is not fairly obvious with the boundary of falling the stream district, and volume ratio is 1: 1 generally.Mainly the adjusting with escape pipe 3 positions realizes by swash plate 7 in the adjusting of volume ratio.The air-flow of spray also provides motivating force for the mixed solution circulation interval with falling stream of up-flow district on the escape pipe 3 except the necessary dissolved oxygen of reaction is provided.
Behind the aerated reaction, close aerating apparatus, mixed solution remained static in reactor 1 to 2 hour, and carried out solid-liquid separation, finished precipitate phase.The spacing of swash plate 7 is little, its setting can make the mud rapid precipitation, and Reynolds number reduces than conventional equipment, can effectively suppress the hydraulic pulse of particles settling, again because structural optimization does not have not deposition of sidewise restraint, thereby guarantee that little mud flocs unit also can effectively remove.Simultaneously, the setting of multilayer swash plate has significantly improved space utilization efficient, and this technology equates under the situation that at heavy mud area its efficient is many times of SBR technology with SBR technology.
Subsequently, open the wet-pit 6 of corresponding position, discharge the clear liquid of top, finish bleeding stage according to the need water displacement.
Precipitating sludge enters the idle stage, and be 0.5 to 1 hour idle mixing time, and reactor is in the holding state of preparing the next cycle operation again, and wherein each stage generation excess sludge will regularly discharge.The exchange ratio of reactor is 0.5 (promptly going up half water yield that one-period reacted stays in the reactor), and water inlet and water outlet time are fixed value 0.5h, adopts the aeration mode of limiting the quantity of (promptly intake finish then begin aeration again).Finish the entire sewage treating processes thus.
In a word, the present invention has enumerated above-mentioned preferred implementation, but should illustrate that those skilled in the art can carry out various variations and remodeling.Therefore, unless such variation and remodeling have departed from scope of the present invention, otherwise all should be included in protection scope of the present invention.
Claims (10)
1. the method handled of an ammonia nitrogen waste water, the sequencing batch active sludge that employing is carried out in reactor, comprise into water, aerated reaction, precipitation, draining and idle stage, it is characterized in that: be provided with the multilayer swash plate in the described reactor, during aerated reaction, the air-flow of aerated reaction stops and leads through swash plate makes the mixed solution in the reactor be divided into aerobic zone and oxygen-starved area, and the mixed solution in two districts forms cyclic motion.
2. according to the method for the described a kind of ammonia nitrogen waste water processing of claim 1, it is characterized in that: the air-flow of described aerated reaction is in the upwards ejection of the bottom of reactor.
3. according to the method for the described a kind of ammonia nitrogen waste water processing of claim 2, it is characterized in that: described up-flow district forms aerobic zone, falls the stream district and forms the oxygen-starved area.
4. according to the method for the described a kind of ammonia nitrogen waste water processing of claim 3, it is characterized in that: described up-flow district is 1: 1 to 3: 1 with the volume ratio of falling the stream district.
5. the method for handling according to each described a kind of ammonia nitrogen waste water in the claim 1 to 4 is characterized in that: in the described aerobic zone nitration reaction takes place, anti-nitration reaction takes place in the oxygen-starved area; The product of nitration reaction is as the substrate of anti-nitration reaction.
6. according to the method for each described a kind of ammonia nitrogen waste water processing in the claim 1 to 4, it is characterized in that: described multilayer swash plate is a rectangular plate, be arranged in parallel, and spacing is 10 to 50 centimetres, and the angle of swash plate and horizontal plane is 30 to 60 degree.
7. according to the method for the described a kind of ammonia nitrogen waste water processing of claim 6, it is characterized in that: choosing along with the increase of reactor volume of described swash plate spacing increases.
8. according to the method for each described a kind of ammonia nitrogen waste water processing in the claim 1 to 4, it is characterized in that: described precipitate phase, mud is at the swash plate surface precipitation.
9. according to the method for each described a kind of ammonia nitrogen waste water processing in the claim 1 to 4, it is characterized in that: the aspect ratio of described reactor is 3: 1 to 5: 1.
10. according to the method for each described a kind of ammonia nitrogen waste water processing in the claim 1 to 4, it is characterized in that: described aerating apparatus and the under meter that carries out aerated reaction joins, and under meter connects compressed gas source; Under meter is adjusted the size of the airshed of aerated reaction.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110234027 CN102285718B (en) | 2011-08-16 | 2011-08-16 | Method for treating ammonia nitrogen wastewater |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110234027 CN102285718B (en) | 2011-08-16 | 2011-08-16 | Method for treating ammonia nitrogen wastewater |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102285718A true CN102285718A (en) | 2011-12-21 |
| CN102285718B CN102285718B (en) | 2013-04-17 |
Family
ID=45332506
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201110234027 Active CN102285718B (en) | 2011-08-16 | 2011-08-16 | Method for treating ammonia nitrogen wastewater |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102285718B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102765858A (en) * | 2012-08-08 | 2012-11-07 | 鲍洪泉 | System and method for constant water level sequential batch type sewage treatment system with continuous variable volume |
| CN114506922A (en) * | 2022-03-02 | 2022-05-17 | 山东问清环境科技有限公司 | Unpowered constant water level automatic drainer and drainage method thereof |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH08141587A (en) * | 1994-11-18 | 1996-06-04 | Hitachi Chem Co Ltd | Method and apparatus for treating waste water |
| CN1301673A (en) * | 1999-12-29 | 2001-07-04 | 孙复华 | Vertical sectional integrated waste water biochemical treatment method and device |
| CN1408649A (en) * | 2002-04-24 | 2003-04-09 | 陈启松 | Integrated A2/O biochemical system |
| CN1648069A (en) * | 2004-11-30 | 2005-08-03 | 东南大学 | Horizontal integrated three phase inner circulation fluidized reactor and its biological reaction process |
| CN101698555A (en) * | 2009-11-13 | 2010-04-28 | 南京大学 | Integrated up-flow reactor and advanced treatment method of fermentation industrial effluent |
-
2011
- 2011-08-16 CN CN 201110234027 patent/CN102285718B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH08141587A (en) * | 1994-11-18 | 1996-06-04 | Hitachi Chem Co Ltd | Method and apparatus for treating waste water |
| CN1301673A (en) * | 1999-12-29 | 2001-07-04 | 孙复华 | Vertical sectional integrated waste water biochemical treatment method and device |
| CN1408649A (en) * | 2002-04-24 | 2003-04-09 | 陈启松 | Integrated A2/O biochemical system |
| CN1648069A (en) * | 2004-11-30 | 2005-08-03 | 东南大学 | Horizontal integrated three phase inner circulation fluidized reactor and its biological reaction process |
| CN101698555A (en) * | 2009-11-13 | 2010-04-28 | 南京大学 | Integrated up-flow reactor and advanced treatment method of fermentation industrial effluent |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102765858A (en) * | 2012-08-08 | 2012-11-07 | 鲍洪泉 | System and method for constant water level sequential batch type sewage treatment system with continuous variable volume |
| CN102765858B (en) * | 2012-08-08 | 2013-08-07 | 鲍洪泉 | System and method for constant water level sequential batch type sewage treatment system with continuous variable volume |
| CN114506922A (en) * | 2022-03-02 | 2022-05-17 | 山东问清环境科技有限公司 | Unpowered constant water level automatic drainer and drainage method thereof |
| CN114506922B (en) * | 2022-03-02 | 2023-04-25 | 山东问清环境科技有限公司 | Unpowered constant-water-level automatic drainer and drainage method thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102285718B (en) | 2013-04-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN201313860Y (en) | Integrated aeration-sedimentation aerobic reactor | |
| CN106946355B (en) | Jet aeration type A/O integrated sewage treatment device and sewage treatment process thereof | |
| CN102180543A (en) | Highly-efficient stable bio-doubling sewage treatment device | |
| CN101792230A (en) | Non-reflux continuous aeration type sewage treatment system and treatment method | |
| CN102139972A (en) | Sewage treatment method and device | |
| CN102417279A (en) | Sewage treatment and recycling system method for coal powder/coal slurry gasification device | |
| CN101857334A (en) | Sewage treatment device and sewage treatment process thereof | |
| CN102765858A (en) | System and method for constant water level sequential batch type sewage treatment system with continuous variable volume | |
| CN102285718B (en) | Method for treating ammonia nitrogen wastewater | |
| CN202186923U (en) | Ammonia nitrogen wastewater treatment device | |
| CN100564281C (en) | Inversed baffled aerobic particle sewage sludge reactor | |
| CN210261290U (en) | Integrated wastewater treatment device | |
| CN206033378U (en) | Nitrogen and phosphorus removal sewage treatment device | |
| CN208218501U (en) | A kind of perseverance water level SBR sewage disposal device | |
| AU2015298397B2 (en) | Sequencing batch facility and method for reducing the nitrogen content in waste water | |
| CN201999827U (en) | High-efficiency stable sewage treatment device with bio-doubling process | |
| CN215049470U (en) | Biochemical neutralization treatment device for high-acidity HMX production wastewater | |
| CN109485151A (en) | The device and its treatment process of synthesis gas preparing ethylene glycol production wastewater treatment | |
| CN108726660A (en) | A kind of MBBR reactors for electroplating wastewater processing | |
| CN104310587A (en) | Denitrification and dephosphorization wastewater treatment system and process | |
| CN204490586U (en) | From interception type aerobic reactor | |
| CN103936140A (en) | MBBR pretreatment method and system for high-ammonia nitrogen micro-polluted raw water | |
| CN204058056U (en) | A kind of Continuous Flow permanent water level SBR waste disposal plant | |
| CN209338199U (en) | A kind of MBBR reactor for electroplating wastewater processing | |
| CN103058457B (en) | Device for controlling MBR (Membrane Bio-Reactor) membrane pollution and supplementing aeration and control method of same |
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 | ||
| C56 | Change in the name or address of the patentee |
Owner name: GUANGDONG BRUNP RECYCLING CO., LTD. Free format text: FORMER NAME: FOSHAN BRUNP RECYCLING TECHNOLOGY CO., LTD. |
|
| CP01 | Change in the name or title of a patent holder |
Address after: Water sand village Nanhai District 528000 in Guangdong province Foshan City Industrial Zone Chung Patentee after: Guangdong Brunp Recycling Technology Co., Ltd. Address before: Water sand village Nanhai District 528000 in Guangdong province Foshan City Industrial Zone Chung Patentee before: Foshan Brunp Recycling Technology Co., Ltd. |
|
| C56 | Change in the name or address of the patentee |
Owner name: GUANGDONG BANGPU CIRCULATION TECHNOLOGY CO., LTD. Free format text: FORMER NAME: GUANGDONG BRUNP RECYCLING CO., LTD. |
|
| CP03 | Change of name, title or address |
Address after: Water sand village Nanhai District 528244 in Guangdong province Foshan City Industrial Zone Chung Patentee after: GUANGDONG BRUNP RECYCLING TECHNOLOGY CO., LTD. Address before: Water sand village Nanhai District 528000 in Guangdong province Foshan City Industrial Zone Chung Patentee before: Guangdong Brunp Recycling Technology Co., Ltd. |
|
| TR01 | Transfer of patent right |
Effective date of registration: 20171214 Address after: Water sand village Nanhai District 528244 in Guangdong province Foshan City Industrial Zone Chung Co-patentee after: Hunan Brunp Circulation Technology Co., Ltd. Patentee after: GUANGDONG BRUNP RECYCLING TECHNOLOGY CO., LTD. Address before: Water sand village Nanhai District 528244 in Guangdong province Foshan City Industrial Zone Chung Patentee before: GUANGDONG BRUNP RECYCLING TECHNOLOGY CO., LTD. |
|
| TR01 | Transfer of patent right | ||
| CP02 | Change in the address of a patent holder |
Address after: No.6 Zhixin Avenue, Leping Town, Sanshui District, Foshan City, Guangdong Province Patentee after: GUANGDONG BRUNP RECYCLING TECHNOLOGY Co.,Ltd. Patentee after: HUNAN BRUNP RECYCLING TECHNOLOGY Co.,Ltd. Address before: 528244 shangshayong Industrial Zone, Lishui Shangsha village, Nanhai District, Foshan City, Guangdong Province Patentee before: GUANGDONG BRUNP RECYCLING TECHNOLOGY Co.,Ltd. Patentee before: HUNAN BRUNP RECYCLING TECHNOLOGY Co.,Ltd. |
|
| CP02 | Change in the address of a patent holder |