CN1730410A - Improved bioreactor - Google Patents
Improved bioreactor Download PDFInfo
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- CN1730410A CN1730410A CNA2004100416564A CN200410041656A CN1730410A CN 1730410 A CN1730410 A CN 1730410A CN A2004100416564 A CNA2004100416564 A CN A2004100416564A CN 200410041656 A CN200410041656 A CN 200410041656A CN 1730410 A CN1730410 A CN 1730410A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Abstract
The present invention relates to the field of water treatment, especially an aerobic biological treatment bioreactor which contains large particle easy-fluidization filling having a specific density of 0.7-0.95, and a void ratio of >=50%, the loading amount of the filling is 50-90% of the reactor's effective volume, and the aeration apparatus includes separate oxygen supply aeration device and fluidization aeration device.
Description
Technical field
The invention belongs to water treatment field, the aerobe that relates in particular to a kind of water treatment is handled bio-reactor.
Background technology
" submerged fixed biofilm aerating filter " aerobic treatment process of France OTV S.A. exploitation is (typical in BIOSTYR
TMTechnology), it is a kind of Up-flow Biological Aerated Filter that filter tank and biochemical reactor is combined composition, basic structure is seen (Fig. 1): be that the filtrate baffle plate 5 that water filtering cap 8 is housed is set on reaction tank 2 tops, lower bottom part is provided with aerating apparatus 7 and water inlet water-distributing device 1, the centre is filled with lightweight spheroidal particle (3-6mm) filtrate 3 that is referred to as BIOSTYRENETM proportion little 1, for example porous plastics filter pearl.The bigger serface filtrate can adhere to a large amount of microorganisms as microbe carrier to this reactor because employing has very, thereby has higher detergent power and handle load; And microorganism is fixed on the carrier, be not suspended in the water and do not resemble activated sludge process, so the biomass in its unit volume is very big, and processing power is much higher than activated sludge process; Simultaneously also because effluent stream is a compression filtrate direction through the direction of filter bed, rather than expansion filtrate direction, also strengthened crown_interception to suspended matter, has successive physical filtering ability, thereby can omit settling tank, in case and bio-reactor generation problem, the suspended substance of the overwhelming majority still can be removed in the filter tank.But the filtrate voidage of biological filter is lower, and this has just reduced the carrier band biomass, thereby processing efficiency is not really high; Little voidage adds that filler itself is compressed not fluidisation, occurs filtrate easily and hardens, cause filtrate back flushing difficulty, the water yield that not only recoils is big, and recoil is not thorough, shorten the recoil cycle, reduced water production rate and producing water ratio, can cause processing efficiency decline in the use.Secondly, in design for satisfying to the effective back flushing of filtrate, reactor lower part need be provided with the filler expansion space that volume ratio is used for back flushing more greatly, top need be left bigger recoil water storage of volume ratio and balanced reactor fluidised form exhalant region (then needing be provided with recoil water storage pond as not setting out the pool outside reactor) again, make filtrate volume filling rate reduce so again, generally be about about 60%, thereby the reactor volume utilization ratio is not high, can reduces the processing efficiency of reactor yet.Besides, for guaranteeing good back flushing, also need be equipped with high-power recoil pump; The fine particle filtrate adopts the filter cap to cross water, and the filter cap appears in the long-time running meeting to be stopped up, and these also can influence processing efficiency, so the biological filter operation is stable inadequately, thereby the operational management trouble.
WO 02/096806 disclosed another kind of fluidisation bio-reactor AGAR
TM(Attached Growth AirliftReactor), basic structure is seen Fig. 2.Be that some dividing plates are set in reactor 2, be divided into a plurality of processing units, different with the biological filter is that reactor adopts macrobead hollow columnar filler 3 to make bio-carrier (fluidized packing material); Adopt lower filling rate (being generally about 35%), so that filler is fluidized state.For reinforcing filler fluid effect and demoulding needs, also have additional central draft tube Fig. 3 in the processing unit.Though this reactor has overcome some shortcomings of BAF, because filler filling rate is lower, biomass is less, causes processing efficiency not high, and reactor volume expands, and floor space is many; Secondly, the fluidizing filler is little to the cutting action of rising bubble fully, thereby aeration aerating efficient is low, must strengthen aeration rate, has increased operation energy consumption again; Besides, the bad adaptability that reactor changes organic loading, for making filler be in good fluidized state, when hanging down organic loading, can not reduce aeration rate (then fluidizing tolerance is just not enough if reduce aeration rate), but if to guarantee fluidisation then oxygenation just have and be imbued with, either way can cause reactor efficiency to reduce.
The disclosed isolated aeration device of Chinese patent 00131548.X, be to adopt at least 1 isolating cylinder that the aeration tank or the biochemical aerating filter of biomembrance process are divided into aeration zone and packing area, the isolating cylinder inner bottom part is equipped with aeration head, make it to become the aeration zone, the bottom side offers the water back window, tube is outer to be the packing area, and the top is submerged in the water.Yet this structured packing still maintains static, thereby reactor stops up easily, and head loss is big; Secondly, aeration does not directly contact with filler, and oxygen-transfer efficiency is lower, and treatment effect can't be better than the biological filter.
Summary of the invention
The objective of the invention is to overcome the deficiency of above-mentioned prior art, a kind of oxygen-transfer efficiency height is provided, head loss is little, and reactor does not stop up, and is stable, and biomass is big, the processing efficiency height, and operational management is bio-reactor easily.
The object of the invention realizes, the main improvement is that to be filled with proportion in reactor be 0.7～0.95 lightweight, voidage big (〉=50%), the easy fluidisation of macrobead (under the situation by other fluidisation power except that gas not, the oxygen supply institute air demand of fluidisation institute air demand≤normally) filler; And make the filler loadings account for the 50-90% of reactor useful volume; Reactor bottom is provided with separately independently oxygen supply aeration and fluidisation aerating apparatus at least.Thereby make reactor reach the oxygen-transfer efficiency height, head loss is little, and is stable, and biomass is big, the processing efficiency height, and operational management is convenient.Specifically, bio-reactor of the present invention, comprise reactor and built-in filler, the following filler baffle plate of the filler top water surface, and bottom aerating apparatus, treating water from bottom to top passes through packing layer, it is characterized in that said filler is proportion 0.7～0.95, voidage 〉=50%, the easy fluidized packing material of macrobead; Said filler loadings accounts for the 50-90% of reactor useful volume; Said aerating apparatus is independently oxygen supply aeration and fluidisation aeration separately.
The said reactor useful volume of the present invention is meant the volume that the reactor water surface is following.
The present invention said independently oxygen supply aeration and fluidisation aeration separately are artificially to set according to its working order, and promptly a cover is used for normally carrying out a biological disposal upon oxygen supply, and a cover is used to make filler to produce fluidisation and demoulding.For guaranteeing that both effectively work, simplify and regulate, the said aerator that is used for oxygen supply, a kind of better is to adopt micro-pore aeration, especially the micro-hole aerator to adopt little tolerance, big density to be equipped with, for example every aerator air demand is for per hour about 0.2～0.6 cubic metre, every square metre of aeration head that is provided with about 25～49; Be used for filler fluidizing aerator, can adopt micro-hole aerator, also can adopt the macropore aerating apparatus, every aeration rate is big, but packing density is little relatively, and for example every aerator air demand is for per hour about 2.0～6.0 cubic metres, every square metre of aeration head that is provided with about 2～6, make aeration concentrated relatively, help the fluidisation of filler like this.The present invention can be according to sewage and running condition, and two class aerators both can independent alternation, also can adjust tolerance and work simultaneously.
The easy fluidized packing material of the said macrobead of the present invention is meant that filler satisfies under the situation by other fluidisation power except that gas not, fluidisation institute air demand≤normal oxygen supply institute air demand, and it can be for example various hollow tubular fillers, or other non-structured packings.Wherein better be to adopt hollow tubular, for example filler axially with radially than being 0.9～1.1, hollow tubular filler about every cubic metre 300,000～450,000, its inner hollow, not only improved the voidage of filler, and behind filler fluidisation demoulding, its inside still can keep a certain amount of microbial film, helps answering processing power rapidly behind the demoulding; The voidage of said filler is preferably 70～90%, and said filler loadings is preferably and accounts for 65～80% of reactor useful volume.
Bio-reactor of the present invention, its treating processes are divided into oxygen supply stage and filler fluidisation demoulding stage.In the oxygen supply stage, pressurized air or oxygen enter reactor by oxygen supply aerator homodisperse, and microorganism carries out oxygen supply in reactor, and this moment, the fluidisation aerator also can be worked, and just air demand is turned down.Because the reactor filler loading level is big, this moment, the upper strata filler had the biological filter function, and filler has cutting action to bubble, thereby has improved aeration aerating efficient; The underclad portion filler is fluidized state under the aeration effect, be equivalent to the fluidized-bed function again, and can impel into that water mixes rapidly, has not only omitted the water inlet water distributor, but also has helped improving processing efficiency.Along with the microbial film thickness of treatment progress on the filler increases, make the excessive or processing efficiency of head loss reduce when excessive, change the fluidisation demoulding stage over to.Close the oxygen supply aerator or reduce aeration rate, open the fluidisation aerator or strengthen aeration rate, pressurized air or oxygen enter reactor by the fluidisation aerator, because aeration rate is concentrated relatively, aeration intensity is big, making light filler be fluidisation reaches and runs foul of each other and demoulding, filler recovers high processing power through demoulding regeneration, as adopting the hollow tubular filler, because of filler inside is hollow state, thereby still keep certain biomass, thereby can change normal biochemical behind the demoulding soon over to and handle in filler inside.Because in the fluidisation demoulding stage, still can keep in the reactor than high biological activity, so still have processing power, and do not need as other reactors, close into water, continuous operation that can the realization response device.
If aeration rate is controlled in the low scope, the present invention also uses as anoxic reacter.
Therefore, the present invention has than prior art
(1) oxygen-transfer efficiency height.Because of most of filler of oxygen supply stage is in stationary state, bubble there is cutting action, not only prolonged the path that bubble rises to the water surface, and make bubble be the irregularity shape, increase the gas-to-liquid contact area, also strengthened the relative operation of gas-liquid-solid three-phase, effectively improved the transport velocity of oxygen, oxygen-transfer efficiency is improved, and more aerobic fluidized bed oxygen-transfer efficiency can improve more than 20%.Adopting the micro-pore aeration oxygen supply in addition, also is that reactor obtains one of reason of high oxygen-transfer efficiency.
(2) loss of reactor operating head polishing is little.Because of filler has very big voidage, packing layer can keep less resistance for a long time, in case the blocked up resistance of biofilm development can not increase much yet, and makes packing layer recover less resistance again very soon by filler fluidisation demoulding.In the oxygen supply stage, the total cross section aeration, the reactor operation is equivalent to an airlift, and this is a little important factor of head loss also.
(3) biomass is big.Because of reactor unit volume filler amount of fill big, packing layer has bigger voidage again, oxygen supply stage air scouring intensity is little and even, this just makes packing layer that the space that holds mud is more greatly arranged, and the microbial film difficult drop-off, existing aerobic fluidized bed sludge concentration improves nearly 5 times, improves nearly 2 times than BAF, thereby improved biomass greatly, improved processing power.
(4) reactor for treatment efficient height, good economy performance.When reaching the same treatment effect, because above advantage makes reactor volume, than existing aerobic fluidized bed reducing more than 50%, energy consumption reduces more than 20%, and investment cost is basic identical.
(5) reactor is reliable, and operational management is convenient.Because but the filler in the reactor is a fluidizing, satisfy in water inlet under the prerequisite of pre-treatment requirement, latch up phenomenon can not occur, thereby guarantee the work of reactor reliability service.Secondly, can be according to the variation of influent load, aeration rate can be adjusted in a big way, and does not influence reactor for treatment efficient, thereby it is strong to adapt to the load variations ability.
(6) simple in structure.Because of reactor underclad portion filler is fluidized state, be equivalent to the fluidized-bed function again, can also omit water distribution system.
Reactor of the present invention not only can be used for sewage disposal, can also be used for feedwater, water treatment.
The present invention and BIOSTYR
TMBiological filter, AGAR
TMThe fluidized reactor contrast table
Below in conjunction with an embodiment, further specify the present invention, but the embodiment concrete structure not to concrete qualification of the present invention.
Description of drawings
Fig. 1 is prior art BIOSTYR
TMThe bacteria filter structure synoptic diagram.
Fig. 2 is prior art AGAR
TMThe fluidized reactor structural representation.
Fig. 3 is prior art AGAR
TMThe another kind of structural representation of fluidized reactor.
Fig. 4 is an embodiment of the invention structural representation.
Fig. 5 is a filler perspective view in the embodiment of the invention.
Fig. 6-Fig. 9 is other hollow tubular filling-material structure synoptic diagram.
Embodiment
Embodiment: referring to Fig. 4,5, in reaction vessel 2, be filled with proportion 0.9, voidage and be 85%, axially and ratio radially be 0.9～1.1 hollow tubular filler 3 (size is every cubic metre 300,000～450,000), the filler amount of fill accounts for 65～80% of reactor useful volume, reactor top top underwater 100～200mm has protruded packing baffle plate 5, its aperture is 5～10mm, the top has water outlet 4, bottom that oxygen supply aerating system 7 and fluidisation aerating system 6 are arranged, and water inlet pipe 1.The oxygen supply aeration adopts micro-hole aerator, and every aerator air demand is per hour 0.2～0.6 cubic metre, and packing density is 25～49 every square metre; The fluidisation aeration adopts the single hole aerator, and every aerator air demand is per hour 2.0～6.0 cubic metres, and packing density is 2～6 every square metre.Two class aerators both can independent alternation when operation was handled, and also can adjust tolerance and work simultaneously.
The present invention can also adopt other as Fig. 6-hollow tubular filler shown in Figure 9, or other have the filler of the easy fluidization characteristics of macrobead.
According to the sewage situation, apparatus of the present invention can singlely be moved, also can a plurality of serial or parallel connection operations.
Claims (12)
1, a kind of bio-reactor, comprise reactor and built-in filler, the following filler baffle plate of the filler top water surface, and bottom aerating apparatus, treating water from bottom to top passes through packing layer, it is characterized in that said filler is proportion 0.7～0.95, voidage 〉=50%, the easy fluidized packing material of macrobead; Said filler loadings accounts for the 50-90% of reactor useful volume; Said aerating apparatus is independently oxygen supply aeration and fluidisation aeration separately.
2,, it is characterized in that said filler loadings accounts for the 65-80% of reactor useful volume according to the described bio-reactor of claim 1.
3, according to the described bio-reactor of claim 1, it is characterized in that filler voidage 70～90%.
4,, it is characterized in that said filler is a hollow tubular according to claim 1,2 or 3 described bio-reactors.
5,, it is characterized in that every cubic metre 300,000 of said filler～450,000 according to the described bio-reactor of claim 4.
6, according to the described bio-reactor of claim 4, it is characterized in that said filler axially with radially than being 0.9～1.1.
7,, it is characterized in that said oxygen supply aerator is a micro-hole aerator according to claim 1,2 or 3 described bio-reactors.
8,, it is characterized in that per hour 0.2～0.6 cubic metre of every air demand of said oxygen supply aerator according to the described bio-reactor of claim 7.
9,, it is characterized in that 25～49 every square metre of said oxygen supply aerator packing densities according to the described bio-reactor of claim 7.
10,, it is characterized in that said fluidisation aerator is the single hole aerator according to claim 1,2 or 3 described bio-reactors.
11,, it is characterized in that per hour 2.0～6.0 cubic metres of every aerator air demands of said fluidisation aerator according to claim 1,2 or 3 described bio-reactors.
12,, it is characterized in that 2～6 every square metre of said fluidisation aerator packing densities according to claim 1,2 or 3 described bio-reactors.
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| CNB2004100416564A CN100337936C (en) | 2004-08-08 | 2004-08-08 | Improved bioreactor |
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| CNB2004100416564A CN100337936C (en) | 2004-08-08 | 2004-08-08 | Improved bioreactor |
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| CN1730410A true CN1730410A (en) | 2006-02-08 |
| CN100337936C CN100337936C (en) | 2007-09-19 |
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2010140898A1 (en) * | 2009-06-03 | 2010-12-09 | Biowater Technology AS | Method and reactor for biological purification of waste water. |
| CN102351304A (en) * | 2011-09-09 | 2012-02-15 | 北京林业大学 | Novel biological aerated filter capable of solving backwashing problem |
| CN103466787A (en) * | 2013-09-17 | 2013-12-25 | 西安绿标水环境科技有限公司 | Combined aeration moving bed bio-membrane reactor |
| CN105347466A (en) * | 2015-11-20 | 2016-02-24 | 清勤水处理科技（上海）有限公司 | Three-dimensional filling material used for wastewater treatment |
| CN106830297A (en) * | 2017-03-29 | 2017-06-13 | 天津西敦津洋环保科技有限公司 | A kind of light particle system and method for sewage disposal |
| CN106904794A (en) * | 2017-03-29 | 2017-06-30 | 天津西敦津洋环保科技有限公司 | A kind of box-type sewage disposal device containing suspended particulate system |
| CN109851049A (en) * | 2019-04-11 | 2019-06-07 | 信开水环境投资有限公司 | Sewage treatment unit and its application method and purposes |
| CN109851181A (en) * | 2019-04-11 | 2019-06-07 | 信开水环境投资有限公司 | Sewage-treatment plant, system and application method comprising it |
| CN110407410A (en) * | 2019-07-31 | 2019-11-05 | 华南理工大学 | A kind of wastewater treatment equipment and its method based on biofilm particles sewage sludge reactor |
| CN110436624A (en) * | 2019-07-31 | 2019-11-12 | 华南理工大学 | Granule sludge composite biological film expanded bed reactor and its wastewater treatment method |
| CN116514269A (en) * | 2023-04-15 | 2023-08-01 | 广州清源凯旋环保科技有限公司 | Fluidized bed reactor by biomembrane method and process for treating formaldehyde wastewater with wide-area concentration |
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| JPS60212292A (en) * | 1984-04-06 | 1985-10-24 | Shinko Fuaudoraa Kk | Apparatus for high degree treatment of sewage |
| JPH0389997A (en) * | 1989-09-01 | 1991-04-15 | Ngk Insulators Ltd | Fluidized bed type waste water treatment method and apparatus |
| JP2000279982A (en) * | 1999-03-29 | 2000-10-10 | Mitsubishi Kakoki Kaisha Ltd | Fludized bed type waste water treating device |
| CN1331776C (en) * | 2002-09-09 | 2007-08-15 | 同济大学 | Original water biologic pretreatment method using suspended padding and apparatus therefor |
| CN2719834Y (en) * | 2004-08-08 | 2005-08-24 | 江苏鹏鹞环境工程技术研究中心有限公司 | Improved bioreactor |
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| US9758402B2 (en) | 2009-06-03 | 2017-09-12 | Biowater Technology AS | Method and reactor for biological purification of waste water |
| WO2010140898A1 (en) * | 2009-06-03 | 2010-12-09 | Biowater Technology AS | Method and reactor for biological purification of waste water. |
| CN102448894A (en) * | 2009-06-03 | 2012-05-09 | 生物水技术公司 | Method and reactor for biological purification of waste water |
| EA022513B1 (en) * | 2009-06-03 | 2016-01-29 | Биоуотер Текнолоджи Ас | Method and reactor for biological purification of waste water |
| CN102448894B (en) * | 2009-06-03 | 2014-04-09 | 生物水技术公司 | Method and reactor for biological purification of waste water |
| AU2010254693B2 (en) * | 2009-06-03 | 2014-06-19 | Biowater Technology AS | Method and reactor for biological purification of waste water. |
| CN102351304A (en) * | 2011-09-09 | 2012-02-15 | 北京林业大学 | Novel biological aerated filter capable of solving backwashing problem |
| CN103466787A (en) * | 2013-09-17 | 2013-12-25 | 西安绿标水环境科技有限公司 | Combined aeration moving bed bio-membrane reactor |
| CN105347466A (en) * | 2015-11-20 | 2016-02-24 | 清勤水处理科技（上海）有限公司 | Three-dimensional filling material used for wastewater treatment |
| CN106904794A (en) * | 2017-03-29 | 2017-06-30 | 天津西敦津洋环保科技有限公司 | A kind of box-type sewage disposal device containing suspended particulate system |
| CN106830297A (en) * | 2017-03-29 | 2017-06-13 | 天津西敦津洋环保科技有限公司 | A kind of light particle system and method for sewage disposal |
| CN109851181B (en) * | 2019-04-11 | 2024-05-03 | 信开环境投资有限公司 | Sewage treatment device, system comprising same and use method |
| CN109851049A (en) * | 2019-04-11 | 2019-06-07 | 信开水环境投资有限公司 | Sewage treatment unit and its application method and purposes |
| CN109851181A (en) * | 2019-04-11 | 2019-06-07 | 信开水环境投资有限公司 | Sewage-treatment plant, system and application method comprising it |
| CN110436624B (en) * | 2019-07-31 | 2024-04-19 | 华南理工大学 | Granular sludge composite biological membrane expanded bed reactor and wastewater treatment method thereof |
| CN110436624A (en) * | 2019-07-31 | 2019-11-12 | 华南理工大学 | Granule sludge composite biological film expanded bed reactor and its wastewater treatment method |
| CN110407410B (en) * | 2019-07-31 | 2024-04-26 | 华南理工大学 | Wastewater treatment device and method based on biomembrane particle sludge reactor |
| CN110407410A (en) * | 2019-07-31 | 2019-11-05 | 华南理工大学 | A kind of wastewater treatment equipment and its method based on biofilm particles sewage sludge reactor |
| CN116514269A (en) * | 2023-04-15 | 2023-08-01 | 广州清源凯旋环保科技有限公司 | Fluidized bed reactor by biomembrane method and process for treating formaldehyde wastewater with wide-area concentration |
| CN116514269B (en) * | 2023-04-15 | 2023-10-31 | 广州清源凯旋环保科技有限公司 | Fluidized bed reactor by biomembrane method and process for treating formaldehyde wastewater with wide-area concentration |
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Effective date of registration: 20191230 Address after: 214214 Jiangsu city of Wuxi province Gaocheng Town, Yixing City Industrial Zone (Xu Jing Cun) Patentee after: JIANGSU PENGYAO ENVIRONMENTAL ENGINEERING CONTRACTING CO., LTD. Address before: 214205 Jiangsu city of Yixing province huankeyuan dragon Chi Lu No. 35 Co-patentee before: Yixing Pengyao Yangguang Environmental Protection Co., Ltd. Patentee before: Jiangsu Pengyao Environment Engineering & Technology Research Center |
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