CN101132993A - Organic wastewater treatment method and apparatus - Google Patents
Organic wastewater treatment method and apparatus Download PDFInfo
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Abstract
This invention provides anaerobic biological treatment method and apparatus that can stably treat hardly degradable component-containing organic wastewater in a high-performance manner for a long period of time. The anaerobic biological treatment method for organic wastewater comprises providing an upflow anaerobic reactor (2) packed with activated carbon, withdrawing a part of treatment water (9) from the top of the reactor (2), and circulating the withdrawn water to the reactor (2) in its bottom or raw water inflow part. In this method, the amount of the liquid circulated from the top of the reactor (2) to the bottom or raw water inflow part is regulated according to the treatment status of the reactor (2). For example, the concentration of inhibitory organic matter of the treatment water and/or the amount of methane gas in relationship with inflow COD<SUB>cr</SUB> in the reactor may be mentioned as the treatment status of the reactor (2). Seed sludge may be added to the reactor (2) simultaneously with or after packing of the activated carbon. A multistage gas-liquid-solid separation part (3) for separating the produced methane gas, the treatment water and the packing material provided in a vertical direction may be provided in the reactor (2), and, in addition, means for measuring the amount of the separated methane gas may be provided.
Description
Technical field
This area relates to anaerobism treatment process and the device that makes organic waste water innoxious, more particularly, relates to the biology anaerobism treatment process and the device of the organic waste water that contains hard-decomposed composition.
The activated sludge process under the aerobism is used in the processing of organic waste water more.But, in recent years,, use the microbiological degradation under the anaerobism condition gradually from viewpoint energy-conservation and that cut down the excess sludge growing amount.The present invention relates to fill gac as organism sorbing material-microbe carrier in up-flow reactor, anaerobism ground is handled and is contained waste water that hinders organic matter and the method and apparatus that dilutes organic waste water.
Background technology
In the activated sludge process in the processing of organic waste water under the normally used aerobism, the energy consumption that is used for aeration etc. is many, and surplus sludge volume is many.Therefore, that excess sludge is few, the microbiological degradation practicability under anaerobism condition favourable aspect the energy.The reactor that becomes its main flow is (the Upflow Anaerobic Sludge Blanket of the anaerobism upwelling Sludge Bed from the granulation function that has used microorganism; UASB) formula reactor and modified form thereof.But, in these reactors, must keep from granulation microorganism (particle) in reactor, for the waste water that contains the biological barrier organic matter, contain the dilution organic waste water of the waste water of the SS more than the 100mg/L and the COD below the 1000mg/L etc. etc., because it is more than the proliferative amount of the anerobe in the reactor that particulate is separated the scale of construction, microbial biomass in the reactor reduces, so stabilizing treatment is impossible.
As anaerobic biological barrier organic matter, chloroform, trieline, paratolunitrile etc. are arranged, as the waste water that contains hard-decomposed composition and easy decomposability composition, known purified terephthalic is made waste water, main component is the paratolunitrile of hard-decomposed composition and acetate, phenylformic acid [the Sheng-Shung Cheng etc. of terephthalic acid and easy decomposability, Wat.Sci.Tech., Vol.36,73-82 (1997)].
The organic waste water that contains hard-decomposed composition is carried out have problem shown below in the method for anaerobism processing.
(1) even so-called hard-decomposed composition for anaerobion is to carry out secular processing (general more than 3 months) also not decompose and continue residual composition.This hard-decomposed composition is owing to himself forms obstruction property (not forming matrix) concerning anaerobion, thereby accounts in a high proportion of wastewater treatment at difficulty decomposition composition, and the rate of removing of COD is low.
(2) when handling hard-decomposed composition with the UASB method, because the compactness of granule sludge reduces, granule sludge concentration reduces, and in addition, owing to flow out to the reactor outside easily, therefore handles the difficulty that becomes continuously.
Summary of the invention
The problem that invention will solve
The present invention is in view of above-mentioned prior art, and problem is to provide with the organic waste water that contains hard-decomposed composition as object, can be steadily in the long term, biology anaerobism treatment process and the device handled to high-performance.
Be used to solve the method for problem
In order to solve above-mentioned problem, the invention provides a kind of treatment process of organic waste water, it is characterized in that: when the biological anaerobism of using the upflow type anaerobic reactor of the fixedly filter bed be filled with gac or thermopnore to carry out organic waste water is handled, top extraction unit divisional processing water from this reactor, make its bottom that is circulated to this reactor or inflow place of former water, according to the treatment situation of aforementioned upflow type anaerobic reactor, regulate the circulating fluid volume that is circulated to bottom or former water inflow from the top of this reactor.In the aforementioned processing method, the treatment situation of so-called upflow type anaerobic reactor is meant the concentration of the obstruction organic matter for the treatment of water for example and/or for the biogas generation of the CODcr of inflow reactor.In aforementioned upflow type anaerobic reactor, can or fill interpolation kind of a mud in back when filling gac.In addition, aforementioned upflow type anaerobic reactor is provided with the gas-liquid-solid separated part of separating the biogas, treating water and the weighting agent that generate at the vertical direction multistage, can have the determinator of measuring separated biogas growing amount simultaneously.
In addition, the present invention also provides a kind of device, it has the fixedly filter bed that is filled with gac or the upflow type anaerobic reactor of thermopnore, be circulated to the biological anaerobism treatment unit of organic waste water of the circulation fluid pipeline of the bottom of this reactor or former water inflow with the top that makes partially disposed water from this reactor, it is characterized in that: the COD determinator and/or the biogas growing amount determinator that also have former water and treating water, with the data of using from this COD determinator and/or biogas growing amount determinator, calculate the treatment situation of aforementioned upflow type anaerobic reactor, result in according to this and regulate the device of circulating fluid volume.
In the aforementioned processing device, the upflow type anaerobic reactor multistage have angle with the main wall of this reactor be downwards following and each occupied area of 35 degree for the baffle plate more than 1/2 of the cross-sectional area of this reactor, mensuration can be set by the gas generating amount determinator of the isolating biogas amount of this baffle plate.
Utilize possibility on the industry
The present invention uses the anaerobism up-flow reactor that has circulation line, dropped into gac.Utilize the sorptive power of the gac of filling, the concentration of biological barrier organic matter can be controlled at and hinder below the concentration, on gac, allow to decompose this organic microorganic adhesion propagation simultaneously, make regeneration of activated carbon.In addition, by making partially disposed liquid be circulated to the bottom of reactor from the top of reactor, biological barrier organic matter concentration in can the diluent stream entry, the linear velocity of the upwelling in simultaneously can controlling reactor is so that input absorbent charcoal carrier appropriateness swelling, and can avoid the obstruction that caused by the SS that flows in the water.And, owing to make the microorganism that participates in decomposing on gac, adhere to propagation, therefore also can stably be applicable to the waste water of microbiologically stabilised dilution waste water, high density SS etc. from the granulation difficulty.According to process object waste water, by in reactor, GSS (separating device of gas, treating water, packing material) is set at the vertical direction multistage, the contact reacts of the microorganism that promotes the former water of bottom in the reactor and participate in decomposing, reduce simultaneously as far as possible and decompose microorganism, the outflow of gac in treating water, form the high reactor of cell concentration.
The present invention is an object with the waste water that contains the biological barrier organic matter, the dilution organic waste water that contains the waste water of the SS more than the 100mg/L and the COD below the 1000mg/L etc.The method of handling these waste water as the anaerobism filter bed method of carrier as anaerobism ground with the granulous gac is effective.
When handling beginning, utilize the sorptive power of the gac of filling to control the concentration of biological barrier organic matter for hindering below the concentration.In addition, before the adsorptive capacity that reaches capacity, anaerobism bacterium that utilization kind of mud is supplied with and the anaerobism bacterium that adheres to propagation on gac can carry out the absorption of secular processing and decompose under the anaerobism condition, also can carry out the regeneration biologically of gac.
As an example of former water, have and contain because of the organic waste water of concentration difference to the material of the different obstruction of anaerobism processes and displays.
Description of drawings
The concise and to the point pie graph of [Fig. 1] treatment scheme of the present invention.
The curve of the experimental result of [Fig. 2] expression embodiment 1.
The curve of the experimental result of [Fig. 3] expression embodiment 2.
Among Fig. 1, each symbol has following implication.
1: former water induction pipe, 2: reactor, 3: baffle plate, 4a, 4b: subregion mud district, 5:GSS portion, 5a, 5b: gas phase portion, 6: generate gas recovery pipe arrangement, 7: water sealed tank, 8: gas meter, 9: treating water pipe arrangement, 10: defoamer, 11: gas holder, 12: gac upper surface, 15: circulation fluid pipe arrangement, 16: recycle pump.
Embodiment
The concise and to the point pie graph of the treatment scheme among the present invention of Fig. 1 illustration explains the present invention based on this figure.
In Fig. 1, be communicated with former water liquid pushing tube 1, up and down the reactor 2 of inaccessible tubular on the wall of the left and right sides of inside, the baffle plate 3 that be provided with respectively that an end is fixed, the other end is extended when the sidewall direction of opposite side descends.Baffle plate 3 at above-below direction by being provided with alternately about 2 places, and sidewall of reactor between form the subregion mud district 4a～4b of acute angle respectively.The downward angle θ that the sidewall of reactor 2 and baffle plate 3 form is the following acute angles of 35 degree, and occupied area is preferably more than 1/2 of cross-sectional area of the reactor of tubular.Angle θ surpasses 35 when spending, and piles up at the top mud or the absorbent charcoal carrier of the baffle plate 3 of mud district 4a, 4b, and it is not enough that flowability becomes, and forms the dead band.In addition, the occupied area of baffle plate 3 is 1/2 when following, and the seizure that generates gas becomes not enough, and it is unfavorable to produce in the solid separation of gas-liquid.That is, gas is left out toward the top from the center of reactor 2, can not accumulation fully in GSS portion described later (gas-liquid-solid separated part) 5.
In addition, relief outlet inner opening the water of the water sealed tank 7 that is filled with water of the generation gas recovery pipe arrangement 6 that connects from the 5a of gas phase portion.Aperture position in water sealed tank 7, is provided with the gas meter 8 of mensuration expellant gas flow from generate gas recovery pipe arrangement 6 in the different suitable depth of water position of hydraulic pressure.Gas holder 11 is installed in position at gas meter 8.In addition, in the upper end of reactor 2, discharge treating water pipe arrangement 9 openings of supernatant liquid.Circulation fluid pipe arrangement 15 is connected with the treating water outflow portion or the treating water pipe arrangement 9 on the top of reactor, is situated between by recycle pump 16, is connected with the bottom of reactor 2.
In the inside of reactor 2, fill the gac of any particle diameter, use as planting mud, drop into the granule sludge or the digested sludge that contain the anaerobism bacterium simultaneously.
Gac can use granulated carbon, pulverizes charcoal, powdery carbon any one because life-time service preferably is being at least 1kg/cm as ultimate compression strength
3Pressure under, still can keep the gac of the granular or disintegrated of shape.The particle diameter of employed gac is decided by flow condition in the reactor and required microbial biomass.That is, (COD is that 3000mg/L is following) can improve the flow velocity in the reactor when organic concentration of former water was lower concentration, can select the bigger gac of particle diameter ratio, selected the gac of small particle size during high density.As the gac that uses among the present invention, can use effective size of grain as 0.05mm～3mm, be preferably 0.2mm～0.7mm scope, impartial coefficient is the gac of 1.2～2 scopes.
If the amount of kind of mud is few, therefore the anaerobism bacterium deficiency of breeding on active embedding surface handles becoming unstable, if too much opposite, the quantity not sufficient of gac, the processing variation during beginning.Therefore, in order to keep the stable treated situation, preferred 5%～30%, preferred 10%～20% the kind mud that adds the gac capacity of being filled, this is from experimental result as can be seen.
It is to be that the mesophilic methane fermentation of optimum temps is handled, is that the anaerobism of all temperature ranges such as high temperature methane fermentation processing of optimum temps is handled as object with 50 ℃～55 ℃ with 30 ℃～37 ℃ that the anaerobism that becomes object of the present invention is handled.
Contain the former water of anaerobism being handled the organic waste water etc. of the material bring obstruction, import to the reactor 2 from liquid pushing tube 1.Water flowing speed in reactor 2 inside also comprises circulation fluid, is preferably 0.1～10m/h.
In reactor 2, because the anaerobism bacterium exists wherein, the biological barrier organic matter decomposes, and generates decomposition gas.The gas that generates separates in the GSS portion 5 of each subregion mud district 4a～4b upper end and collects, and each self-forming gas phase 5a of portion arrives water sealed tank 7 by generating gas recovery pipe arrangement 6.This generates gas and write down its output in gas meter 8, is sent in the gas holder 11.Part generate gas in subregion mud district 4a～4b attached to bio-carrier on, its apparent specific gravity is alleviated, simultaneous mud or absorbent charcoal carrier arrive the water surface of GSS portion 5.This generation gas forms bubble, temporarily is trapped in the water surface gas phase 5b of portion.Bubble in the water surface gas phase 5b of portion set breaks very soon, generation gas is separated with mud or absorbent charcoal carrier, mud or absorbent charcoal carrier are returned to original proportion and precipitate in water, generate gas from generating gas recovery pipe arrangement 6 by water sealed tank 7, are discharged to outside the system.Organism decomposes and becomes clarifying water from the reactor upper end, is discharged to outside the system by treating water pipe arrangement 9, and circulation fluid is situated between by recycle pump 16 by circulation fluid pipe arrangement 15 simultaneously, is supplied to reactor bottom.
Because the air pressure difference of the 5a of gas phase portion of each GSS portion 5, thereby its pressure reduction can be regulated by water sealed tank 7.With the order near former water liquor charging side, the water seal that needs to keep high is pressed.The pressure of gas recovery is regulated except that the method for using water sealed tank 7, and a lot of methods are arranged.For example, can the applying pressure valve etc.
During the former water of foaminess, the 5a of gas phase portion in the GSS5 and generate gas recovery pipe arrangement 6 obturations generates the gas recovery difficulty that becomes.At this moment, by in the inflow water of reactor 2, adding defoamer 10 in advance, can suppress the foaming in the GSS5.Compare with the method that in GSS5 defoamer is splashed into, sprays, present method is effective to the froth breaking in enclosed space.As defoamer 10, have and the corresponding defoaming effect of former water-based shape, in being suitable for middle temperature of fermented liquid froth breaking (30～35 ℃) or high temperature (55～55 ℃), can use the defoamer of not losing defoaming effect.As the kind of defoamer, can use any of silicone antifoam agent, alcohol defoaming agent.
Because the influence of former water-based shape etc., when forming foam easily, the surface of the 5b of gas phase portion in GSS5 and the inner foam that forms, the recovery that the generates gas difficulty that becomes.At this moment, will generate gas and be blown into pipe arrangement (not diagram) and generate gas recovery pipe arrangement 6 and is connected, and, can carry out foamy destruction or prevent foam formation by the generation gases in the gas holder 11 are supplied with in the GSS5.
As the circulating fluid volume of material particular of the present invention, can use following method to regulate individually or simultaneously.
(1) method of employing concentration determination
(a) adopt batch experiment etc. to measure biological barrier concentration (C in advance as the organic substance of object
0).
(b) obstruction organic matter concentration, the Yuan Shui (C of mensuration inflow reactor
In) and treating water (C
Out), according to following (1) formula, set quantity of circulating water Q
rSo that the obstruction organic matter concentration (C) in the reactor inflow portion is C
0Following scope.Hinder organic matter concentration (C) need less than with C
0Identical concentration, preferred in fact C=1/2C
0
C＜C
0=(C
In* Q+C
Out* Q
r)/(Q+Q
r) ... (1) formula
Q: flow into the water yield (m
3/ d), Q
r: quantity of circulating water (m
3/ d)
C, C
0, C
In, C
Out: hamper concentration or total organic concentration, unit (mg/ liter)
(2) adopt the method that generates gas volume
(a), calculate the methane-generated quantity (C of autoreactor by the gas generating amount of gas meter and the methane concentration of gas concentration meter
Out), try to achieve the COD amount (Δ COD) of removing, calculate the COD concentration for the treatment of water or the residual organic matter concentration (C for the treatment of water then
Out).
The COD amount of (b) removing is tried to achieve according to following (2) formula.
Δ COD (kg/d)=G
Out(m
3/ d) ÷ 0.3～0.4 (kg/m
3) ... (2) formula
(c) C
OutCalculate by (3) formula.
C
Out=C
In-(Δ COD ÷ Q * 1000) ... (3) formula
In (1) formula, import the C that calculates by (3) formula
OutTry to achieve required circulating fluid volume.
Embodiment
Below, be described more specifically the present invention by embodiment.
2 series (A series, B series) of upflow type anaerobic reactor of gac of in experiment, having used as shown in Figure 1 filling.
A series is same configuration with the device of B series, and the baffle plate of 2 inclinations is installed, and the angle that makes device sidewall and baffle plate 3 is 30 degree, adds defoamer in former water.The capacity of liquid layer portion is 100 liters.Water temperature in the reactor is controlled at 35 ℃ temperature.In these 2 reactors, having filled 60 liters of effective size of grain is that 0.3mm, impartial coefficient are granular carbon and 10 liters of UASB particles (MLSS concentration 5%) as the processing beverage class waste water of planting mud of 1.5.
In former water, use sodium-acetate (based on COD
CrConvert, be the 750mg/ liter) and terephthalic acid (based on COD
CrConvert, be the 350mg/ liter) mix, added the former water of inorganic nutrients salts (nitrogen, phosphorus etc.).In this composite waste, show as the terephthalic acid of hard-decomposed organic matter hinder property concentration range by batch test as can be known, based on COD
CrBe scaled more than the 200mg/ liter.
Two series all make the COD load (below, abbreviate the COD load as) of former water be 3kg/m
3/ day, begin to handle.Fig. 2 represents experimentation.
In A series, from handling the beginning back, do not make recirculated water 15 inflow reactors by the 90th day, only feed former water (Q).At this moment treatment situation is that acetate almost completely decomposed up to the 60th day, and terephthalic acid is slowly removed variation, and at the 90th day, terephthalic acid was based on COD
CrBe scaled the 80mg/ liter, residual concentration raises.After the 91st day, be less than the concentration range of demonstration obstruction property (based on COD for making terephthalic acid
CrBe scaled the 170mg/ liter), make the treating water of 2 times (2Q) amount of the former water water yield be circulated to the bottom of reactor.Its as a result removing of terephthalic acid improve, in the time of the 150th day, based on COD
CrBe scaled the 10mg/ liter.
In B series, be recycled to the bottom of reactor from handling the treating water that just makes 2 times of amounts of former water after the beginning.In the time of the 30th day, though terephthalic acid is the 35mg/ liter, because below the obstruction concentration of terephthalic acid, thereby the activity degree of anaerobism bacterium is also high, the terephthalic acid for the treatment of water can maintain below the 10mg/ liter.
By above result as can be known, make when flowing into upflow type anaerobic reactor as the terephthalic acid of hardly-degradable substance, as B series,, then between short-term, begin anaerobic digestion if carry out the circular treatment for the treatment of water so that reach below the concentration range of terephthalic acid demonstration obstruction property.
On the other hand, do not carry out the A series during the circular treatment, terephthalic acid does not almost decompose, begin circulation, make terephthalic acid in recirculated water when the concentration range that shows obstruction property is following, the decomposition of terephthalic acid is slowly carried out, and effect of the present invention obtains confirming.
The B series that use is used in the foregoing description 1 uses the former water of embodiment 1 to begin experiment once more.Experimental result as shown in Figure 3.During by the 90th day, the COD load is 3kg/m
3/ day, the former water yield is 150 liters/day, circulating fluid volume is 300 liters/day.The biogas growing amount is 55 liters/day, and the COD concentration for the treatment of water is the 35mg/ liter.After the 91st day, make the COD load be 6kg/m
3/ day, circulating fluid volume still is 300 liters/day, only makes the former water water yield increase to 300 liters/day.Up to the 100th day, be accompanied by the rising of load, the COD concentration for the treatment of water is 35mg/L, almost do not change, though the increase of the gas generating amount for the treatment of water, after this, the concentration of finding terephthalic acid hinders, and in the time of the 150th day, the biogas growing amount is reduced to 90 liters/day.Biogas growing amount in the time of thus calculates, and the concentration of terephthalic acid is the 200mg/ liter, can judge that terephthalic acid has surpassed the concentration range that shows obstruction property.In fact, the COD for the treatment of water is the 205mg/ liter.Therefore, circulating fluid volume was adjusted to 600 liters/day in the 151st day, the increase of results verification gas generating amount and the concentration of the terephthalic acid in the treating water reduce, and in the time of the 210th day, the biogas growing amount is 115 liters/day, and the COD concentration for the treatment of water is the 35mg/ liter.
The upflow type anaerobic reactor of gac that in experiment, used filling shown in Figure 1.The internal structure of reactor, the gac of filling and kind mud are identical with embodiment 1.In former water, used the ethylene glycol waste water of chemical plant.The COD of this former water
CrConcentration is about 10, the 000mg/ liter.
Two kinds of RUN1 and RUN2 have been carried out in experiment.RUN1 only feeds former water and does not carry out the circulation for the treatment of water, and in RUN2, the treating water of 4 times of amounts of the former water yield is circulated to the bottom of reactor.In the batch experiment of obstruction property, can obtain ethylene glycol waste water and show that the concentration range of obstruction property is based on COD
CrBe scaled 4000mg/ and rise above result.
Having studied RUN1, RUN2 is 10kg/m with the COD load setting all
3The rate of removing during/sky and the critical loading of rate more than 80% that be removed.
In the experiment of RUN1, the COD load is 10kg/m
3The rate of removing in/sky is 65～70%.In order to keep the rate of removing 80%, the result is that the COD load is 7kg/m
3/ sky is appropriate.
And in the experiment of RUN2, the COD load is 10kg/m
3The rate of removing in/sky is 85～90%.In order to keep the rate of removing 80%, the result fully obtains maximum COD load 20kg/m
3/ day.
Claims (6)
1. method, the biological anaerobism that is to use the upflow type anaerobic reactor of the fixedly filter bed that is filled with gac or thermopnore to carry out organic waste water is given birth to the method for handling, it is characterized in that: from the top extraction unit divisional processing water of this reactor, make its bottom that is circulated to this reactor or inflow place of former water, according to the treatment situation of above-mentioned upflow type anaerobic reactor, adjust the circulating fluid volume that is circulated to bottom or former water inflow from the top of this reactor.
2. the treatment process of the described organic waste water of claim 1 is characterized in that: the treatment situation of aforementioned upflow type anaerobic reactor be treating water the obstruction organic matter concentration and/or with respect to the COD of inflow reactor
CrThe biogas growing amount.
3. the treatment process of claim 1 or 2 described organic waste waters is characterized in that: in aforementioned upflow type anaerobic reactor, add kind of a mud when filling gac or after filling.
4. the treatment process of claim 1,2 or 3 described organic waste waters, it is characterized in that: in above-mentioned upflow type anaerobic reactor, the gas-liquid-solid separated part of separating the biogas, treating water and the weighting agent that generate is set, the determinator of measuring separated biogas growing amount is set simultaneously at the vertical direction multistage.
5. device, it is the biological anaerobism treatment unit of organic waste water that has the upflow type anaerobic reactor of the fixedly filter bed of having filled gac or thermopnore and partially disposed water is circulated to the circulation fluid pipeline of the bottom of this reactor or former water inflow from the top of this reactor, it is characterized in that: the COD determinator and/or the biogas growing amount determinator that also have former water and treating water, with the treatment situation that is used to calculate aforementioned upflow type anaerobic reactor, result in based on this and to regulate the device of circulating fluid volume from the data of this COD determinator and/or biogas growing amount determinator.
6. the treatment unit of the described organic waste water of claim 5, it is characterized in that: aforementioned upflow type anaerobic reactor multistage have angle with the main wall of this reactor be downwards following and each occupied area of 35 degree for the baffle plate more than 1/2 of the cross-sectional area of this reactor, be provided with mensuration by the gas generating amount determinator of the amount of the isolating biogas of this baffle plate.
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| JP2004298543A JP4428188B2 (en) | 2004-10-13 | 2004-10-13 | Organic wastewater treatment method and treatment apparatus |
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| CN103936147A (en) * | 2010-11-24 | 2014-07-23 | 栗田工业株式会社 | Anaerobic Treatment Method And Apparatus |
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| CN103936147A (en) * | 2010-11-24 | 2014-07-23 | 栗田工业株式会社 | Anaerobic Treatment Method And Apparatus |
| CN103936147B (en) * | 2010-11-24 | 2016-06-29 | 栗田工业株式会社 | The processing method of organic drainage |
| CN102344197A (en) * | 2011-10-18 | 2012-02-08 | 浙江大学 | Method for rapidly starting anaerobic ammonium oxidation reactor |
| CN102344197B (en) * | 2011-10-18 | 2012-09-05 | 浙江大学 | Method for rapidly starting anaerobic ammonium oxidation reactor |
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| WO2006041128A1 (en) | 2006-04-20 |
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