CN1295164C - Apparatus and method for waste water treatment - Google Patents

Apparatus and method for waste water treatment Download PDF

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Publication number
CN1295164C
CN1295164C CNB038122286A CN03812228A CN1295164C CN 1295164 C CN1295164 C CN 1295164C CN B038122286 A CNB038122286 A CN B038122286A CN 03812228 A CN03812228 A CN 03812228A CN 1295164 C CN1295164 C CN 1295164C
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China
Prior art keywords
mud
aerator tank
mentioned
processing method
tank
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CNB038122286A
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CN1656026A (en
Inventor
若山正宪
碓井次郎
藤井涉
冈田实
田中丸直也
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Japan Sewage Works Agency
Mitsubishi Chemical Corp
Mre Corp
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Japan Sewage Works Agency
Mitsubishi Rayon Engineering Co Ltd
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C02F3/12—Activated sludge processes
    • C02F3/1236—Particular type of activated sludge installations
    • C02F3/1268—Membrane bioreactor systems
    • C02F3/1273—Submerged membrane bioreactors
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C02F3/12—Activated sludge processes
    • C02F3/20—Activated sludge processes using diffusers
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/30—Aerobic and anaerobic processes
    • C02F3/308—Biological phosphorus removal
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2201/00—Apparatus for treatment of water, waste water or sewage
    • C02F2201/002—Construction details of the apparatus
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/04—Oxidation reduction potential [ORP]
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/22—O2
    • 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

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  • Life Sciences & Earth Sciences (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Microbiology (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Molecular Biology (AREA)
  • Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

An apparatus for waste water treatment wherein sludge is circulated between an anaelobic tank and an aeration tank, and thereby waste water is biologically treated, characterized in that in the step of sending a sludge from the aeration tank to the anaelobic tank, the sludge is withdrawn from a position lower than that of an aeration device arranged at the lowest position among such devices provided in the aeration tank. The apparatus allows, for example, the removal of both nitrogen and phosphorus by the use of only two treatment tanks of an anaelobic tank and an aeration tank without the use of a coagulating agent.

Description

Drain treatment apparatus and drainage processing method
Technical field
The present invention relates to a kind of device and method that contains organic draining of handling effectively.
Background technology
As the phosphorus removing method in the drainage processing method, can enumerate, dispose anaerobism groove, aerator tank and settling bath, the mud of settling bath is returned to the so-called AO method of anaerobism groove.This method utilizes polyP bacteria that the form of phosphoric acid with polyphosphoric acid is stored in the cell by active sludge is carried out repeatedly in the anaerobic state circulation continuously of becoming reconciled between the oxygen condition., this method energy dephosphorization but can not denitrogenation.
As the denitrogenation method in the drainage processing method, former widely used be so-called active sludge circulation method, promptly, mud is circulated between anaerobic groove and aerator tank, in aerator tank, ammonia nitrogen is oxidized to nitrate nitrogen, in the anaerobic groove, nitrate nitrogen is reduced into outside the nitrogen discharge system., though this method denitrogenation effectively can not be carried out dephosphorization fully.This be because, the dissolved oxygen that contains in the recirculated water from aerobic slot, nitrate nitrogen and nitrite nitrogen make the anaerobism degree of anaerobic groove not improve fully, causing polyP bacteria to release phosphorus can not take place fully.
Therefore, in the occasion that must carry out denitrogenation dephosphorizing simultaneously, up to now, people have adopted in the anaerobic groove of active sludge circulation method or aerator tank and have added inorganic flocculating agent, make phosphate anion insoluble, with excess sludge discharge outside system method and before the anaerobic groove of active sludge circulation method configuration (fully) anaerobism groove carry out so-called A with biology mode denitrogenation dephosphorizing 2The O method.
Yet the method for adding flocculation agent exists not only that flocculation agent expends cost, and because the generation of excess sludge increases, and the problem that the expense of handling excess sludge is also increased.Again, A 2O method and active sludge circulation method relatively exist and must extra (fully) anaerobism groove be set, and also need the problem of the area of spacious setting device.
The present invention makes for solving described problem, the objective of the invention is to, and provides a kind of with anaerobic groove and 2 treatment troughs of aerator tank, does not use flocculation agent just can remove the drain treatment apparatus and the drainage processing method of denitrification and phosphorus.
Summary of the invention
For achieving the above object, the invention provides a kind of mud that makes circulates between anaerobic groove and aerator tank, handle the drain treatment apparatus of draining in the biology mode, its formation is, when from aerator tank when the anaerobic groove is carried mud as circulation fluid, the mud as circulation fluid is taken out in the below of the aerating apparatus that is positioned at extreme lower position from be configured in aerator tank.Drain treatment apparatus of the present invention only with anaerobic groove and 2 treatment troughs of aerator tank, does not use flocculation agent just can remove denitrification and phosphorus.
In above-mentioned drain treatment apparatus, it is desirable to, from described aerator tank, take out position as the mud of circulation fluid, below the aerating apparatus that is positioned at extreme lower position, and apart from it more than 20cm.
Again, for achieving the above object, the invention provides a kind of mud that makes circulates between anaerobic groove and aerator tank, handle the drainage processing method of draining in the biology mode, it is characterized in that, make from aerator tank transport as the dissolved oxygen concentration (be designated hereinafter simply as DOC) of mud on the position that enters the anaerobic groove of circulation fluid below 0.2mg/L, and/or make DOC on the position of from aerator tank, taking out mud below 0.5mg/L.According to drainage processing method of the present invention,, do not use flocculation agent just can remove denitrification and phosphorus only with anaerobic groove and 2 treatment troughs of aerator tank.
In above-mentioned treatment process, it is desirable to, the oxygen of the mud in the described aerator tank is utilized speed (r r) maintain more than the 15mg/Lh, better is to maintain more than the 25mg/Lh.Thus, can more effectively remove dephosphorization.
In above-mentioned treatment process, it is desirable to, the sludge concentration in the described aerator tank (below be called MLSS concentration) is maintained more than the 5000mg/L.Thus, can remove dephosphorization more reliably.
In above-mentioned treatment process, it is desirable to, the DOC in the aerator tank is maintained 1～3mg/L scope.Thus, can remove dephosphorization more reliably.
In above-mentioned treatment process, it is desirable to, make mud from described aerator tank to anaerobic groove circulation time, the mud delay portion in the aerator tank takes out mud.Wherein, it is desirable to, take out mud from the below of the aerating apparatus that is positioned at extreme lower position that is configured in aerator tank, better is, takes out mud more than the 20cm from the below of the aerating apparatus that is positioned at extreme lower position and apart from it.Can more effectively remove dephosphorization thus.
In above-mentioned treatment process, it is desirable to, the dissolved phosphorus acid ion attitude phosphorus concentration in the anaerobic groove is maintained more than the 10mg/L.
In above-mentioned treatment process, it is desirable to, the redox potential (being designated hereinafter simply as ORP) in the described anaerobic groove is maintained-below the 150mV (silver-silver chloride benchmark).Can remove dephosphorization more reliably thus.
Again, in above-mentioned treatment process, it is desirable to, use the membrane separation unit that is immersed in the aerator tank, treating water is discharged outside the system.Thus, the solid treating water can be obtained not containing fully, the MLSS concentration height in the aerator tank can also be kept.
Description of drawings
Fig. 1 is the mode chart of expression example one example of the present invention.
Fig. 2 is other the mode chart of example one example of expression the present invention.
Fig. 3 is other the mode chart of example one example of expression the present invention.
Embodiment
Explain the present invention below, the present invention is not limited to the explanation of these embodiment.
Fig. 1 is the synoptic diagram of expression example one example of the present invention.In Fig. 1, symbol 1 expression anaerobic groove, symbol 2 expression aerator tanks.Draining (former water), (arrow a) to enter anaerobic groove 1, then enter in the aerator tank 2 by spillway (arrow d), 6 places, position below also being positioned at than the aerating apparatus 3 in this groove 2, carry out liquor charging as the attraction stream (arrow b) that causes by pump 4 from managing 9, enter (arrow c) anaerobic groove 1 by discharge portion 5 again, circulate.
In anaerobic groove 1 and aerator tank 2, former water a purifies in biological mode with active sludge with draining.Removing of nitrogen is by mud being circulated between anaerobic groove 1 and aerator tank 2, carrying out so-called nitrated denitrification reaction.Being converted into the organism of BOD, mainly is to utilize the air of discharging from the air discharge portion that is configured in the aerating apparatus 3 in the aerator tank 2, carries out aerobic oxygenolysis.
In the present invention, removing of phosphorus is effect by by the microorganism in the mud (polyP bacteria), takes in as polyphosphoric acid and carries out in the microbe.This microorganism is taken in phosphorus under good oxygen condition, discharge to be stored in intravital phosphorus under anaerobic state.PolyP bacteria is worked between anaerobic state and good oxygen condition repeatedly, then makes its phosphorus that absorbs under good oxygen condition more than the amount that discharges phosphorus under anaerobic state.
The circulation of the mud between anaerobic groove 1 and aerator tank 2 is that use pump 4 is carried to another groove from a groove, flows into by spillway from another groove.At this moment, needn't limit from which groove and use pumped liquid, but it is desirable to,,, thereby reduce energy cost then because only need liquor charging amount seldom to get final product if give anaerobic groove 1 from aerator tank 2 liquor chargings.
In the present invention, enter the DOC at position 5 of anaerobic groove 1 below 0.2mg/L by making from the circulation fluid of aerator tank 2, and/or make from aerator tank 2 and take out the DOC at position 6 of circulation fluids below 0.5mg/L, thus, can suppress dissolved oxygen and flow to anaerobic groove 1, can keep the anaerobism degree in the anaerobic groove 1 fully, thereby, the release of phosphorus impelled.
If in fact do not have dissolved oxygen, nitrate ion, nitrite ion in the anaerobic groove 1, then organism will carry out anaerobic digestion, at this moment, is stored in endobacillary polyphosphoric acid and is discharged into outside the thalline with the form of phosphoric acid.
In the present invention, the DOC at position 5 that is necessary to enter anaerobic groove 1 from the circulation fluid (mud) of aerator tank 2 is below 0.2mg/L, if this value is then more stable and satisfactory because of the removing property that makes phosphorus below 0.1mg/L, if this value is then better below 0.05mg/L.
By prolonging from the taking-up position 6 of aerator tank 2 to the length of the pipeline 9 at the position 5 that enters anaerobic groove 1, in pipeline, consume dissolved oxygen, the DOC that enters the position 5 of anaerobic groove 1 from the circulation fluid (mud) of aerator tank 2 is reduced.Also can it be reduced by the deoxidation means are set in pipeline again.But may not be limited to this,,, then can reduce the DOC at the position that enters anaerobic groove 1 in aerator tank 2 with easy apparatus structure from taking out circulation fluid (mud) here if the very low position of dissolved oxygen is set.
The DOC that will make the position 5 that enters anaerobic groove 1 the experiment proved that, if below 0.2mg/L, then will make the DOC that takes out the position 6 of circulation fluid from aerator tank 2 get final product below 0.5mg/L.If the DOC at position 6 that takes out circulation fluids from aerator tank 2 is then more stable and satisfactory because of the removing property that makes phosphorus below 0.3mg/L, as if at 0.2mg/L with next better.
In addition, the mensuration of DOC can adopt the septum electrode method, uses common DO instrumentation fixed.
In order to make the DOC at position 6 that takes out circulation fluids from aerator tank 2 below 0.5mg/L, be preferably in from aerator tank 2 when anaerobic groove 1 takes out mud, take out from the delay portion of mud.So-called mud delay portion be meant be not subject to that aeration causes to the flow position of influence of mud.For example, if between the bottom surface of aerating apparatus 3 and aerator tank 2, the space is set,, become delay portion because of the mud of the below part that is present in aerating apparatus 3 is not stirred fully.
Thereby, as shown in Figure 1,, can make from aerator tank 2 and take out the DOC at position 6 of circulation fluids (mud) below 0.5mg/L by take out mud from the below of aerating apparatus 3 positions.In addition, the occasion of a plurality of aerating apparatuss 3 is set in aerator tank 2, and the position of taking out circulation fluid (mud) is arranged under the minimum aerating apparatus, again, from aerating apparatus 3 to the distance of discharging position 6 preferably apart from its more than 20cm below, apart from better more than the 30cm.
Again, take out aeration liquid (mud),, also can in aerator tank 2 inside dividing plate 7 be set as illustrated in fig. 3, mud is set not by well-beaten position 6, from taking out mud here as other forms from aerator tank 2.
Flowing of mud in the aerator tank 2 mainly is that the rising that aeration at aerating apparatus 3 partly is accompanied by from the bubble of air blow-off outlet is also risen mud, and descends at the part mud of aeration not, and mud integral body is stirred.At this moment, utilize speed (r if keep the big oxygen of the mud in the aerator tank 2 r), then because be consumed apace, so in aerator tank 2, easily form the position that dissolved oxygen (concentration) reduces in the partial oxygen of aeration not.As concrete r r, preferably maintain more than the 15mg/Lh, if it is maintain more than the 25mg/Lh, then more stable better because of the removing property of phosphorus.
The oxygen of the mud in the aerator tank 2 utilizes speed (r r), can maintain more than the 15mg/Lh by adjusting aeration intensity, MLSS concentration.
In addition, the oxygen of the mud of so-called aerator tank 2 utilizes speed (r r) be meant the r of the mud of partly obtaining from the aeration of aerator tank 2 r, its measuring method can be tried to achieve according to water drain experimental technique (1997, Corporation Japan water drain association).
MLSS concentration in anaerobic groove 1 and the aerator tank 2 can for more stably carrying out dephosphorization, preferably be kept MLSS concentration in high density by SRT (solid retention time) control.If this is because MLSS concentration height, so be consumed apace in the partial oxygen of aeration not, just easily forms the cause at the low position of DOC in aerator tank 2.Also have, the occasion that MLSS concentration is high, because the denitrifying bacteria number in the unit volume is many, so denitrogenation speed is fast, just being easy to generate in anaerobic groove 1 does not have dissolved oxygen and in conjunction with the place of the anaerobic state of oxygen.MLSS concentration in aerator tank 2 specifically, it is desirable to maintain more than the 5000mg/L, and better is to maintain more than the 8000mg/L.In addition, if MLSS concentration is excessive, then the reduction owing to the mud flowability causes the dissolved efficiency of oxygen extremely low, so preferably be controlled at below the 20000mg/L as the upper limit.
In addition, MLSS concentration can be measured according to water drain experimental technique (1997, Corporation Japan water drain association).
The DOC of the aeration portion in the aerator tank 2 is necessary to maintain more than the necessary concentration of organism disaggregating treatment and nitration treatment, preferably maintains more than the 1mg/L.But,, make phosphorus remove performance and reduce, so preferably maintain below the 3mg/L as excessive concentration.The DOC of aeration portion can adjust by the dissolved efficiency of adjusting aeration rate, change aerating apparatus 3.
If polyP bacteria discharges a large amount of phosphorus in anaerobic groove 1, then in aerator tank 2, just can take in more phosphorus.Thereby, if under the high state of the phosphorus concentration of the dissolved phosphorus acid ion of anaerobic groove 1, handle, just can improve the performance of removing of phosphorus.The phosphorus concentration of the dissolved phosphorus acid ion in the anaerobic groove 1 it is desirable to remain on more than the 10mg/L, and better is to remain on more than the 15mg/L.
Also have, in order to make a large amount of phosphorus that discharge in anaerobic groove 1, it also is effective keeping the low ORP of anaerobic groove 1.The ORP of anaerobic groove 1 it is desirable to maintain-150mV below (silver-silver chloride benchmark), and better is maintains-below the 200mV.
In addition, ORP is the index of expression one material other materials of easy oxidation or easy other materials of reduction, and just the numeral of (+) is big more, and expression is in the state of easy more other materials of oxidation; The numeral of negative (-) is big more, and expression is in the state of easy more other materials of reduction.The mensuration of this ORP is by using saturated silver chloride electrode to carry out as metal electrode method of reference electrode etc.
In drainage position logos of the present invention, the part of the mud of in aerator tank 2, handling, through solid-liquid separation, sterilization back discharging as required.Do not limit solid-liquid separation means especially, can adopt former precipitate and separate method yet.But, then can access and do not contain solid, the good treating water of water quality in fact and satisfactory if membrane separation unit 8 dipping is filtered.Again,, high MLSS concentration can be easily kept, the efficient of dephosphorization can be improved if carry out solid-liquid separation with membrane separation unit 8.Do not limit membrane separation unit 8 especially, the membrane separation unit that can adopt flat film, hollow fiber membrane, tubular ceramic film, rotating disk film etc. to generally acknowledge.Certainly, membrane separation unit 8 can be set as shown in Figure 2 yet.
In treatment process of the present invention, also can in anaerobic groove 1 or aerator tank 2 or both sides' groove, add microbial fixed carrier.Improve the MLSS concentration of essence thus, and in aerator tank 2, be fixed on the carrier, the digestion rate in the groove is accelerated, thereby carry out denitrogenation processing at short notice by the nitrifier that reproduction speed is slow.Employed carrier does not limit especially, can adopt the hollow foam body of polyolefine system, the carrier of urethane foam system etc.In addition, add the occasion of carrier, flow out, be preferably in the mud conveying end, spillway etc. that take out mud from each groove filtering net, screen cloth are set for not making carrier.Again, arrive delay portion for avoiding sludge settling, preferably the proportion of carrier is below 1.
Again, during rainfall, rainwater is sneaked in the draining in operation, when reducing draining concentration, the phosphorus concentration for the treatment of water is also uprised for the moment.At this moment, add the flocculation agent of poly aluminium chloride etc. in former water, anaerobic groove 1 or the aerator tank 2, the phosphorus concentration for the treatment of water is reduced.
Below, the present invention will be described in more detail by embodiment.
Embodiment 1
Adopt device as shown in Figure 1, during about 450 days, implement city sewage is handled as the draining of former water.The size of each groove is like constitute followingly.
(1) the mud capacity (size) of anaerobic groove 1 and aerator tank 2: 6.75m 3(L150cm * W100cm * H600cm, depth of water 450cm)
(2) aerating apparatus: be arranged on apart from the height of aerator tank bottom surface 60cm
(3) take out the conveying end of circulation fluids from aerator tank 2: be arranged on apart from the height of aerator tank bottom surface 20cm
(4) handle the water yield: 54m 3/ day
(5) the mud taking-up amount from aerator tank 2 to anaerobic groove 1: 6.75m 3/ day
(6) output of excess sludge: 0.48～0.96m 3/ day
(7) aeration rate: 40～70Nm 3/ hr
And in the position of the top of aerating apparatus 50cm, the membrane separation unit 8 that adopts hollow fiber membrane is set, and (die face is amassed 126m 2, mitsubishi rayon (Co., Ltd.) system is used polyethylene hollow fiber membrane, ProductName: X5490V), filtrate is taken out as treating water.
The performance of raw water quality and mud is illustrated in the table 1, treating water water quality is illustrated in the table 2.
Table 1
Project Scope
Former water BOD 100～400mg/L
Former water COD 50～200mg/L
The full nitrogen of former water 20～60mg/L
The full phosphorus of former water 2～10mg/L
Former water solid content 50～500mg/L
The ORP of anaerobic groove mud -250～-400mV
Anaerobic groove dissolved phosphorus acid ion attitude phosphorus concentration 15～40mg/L
The DOC of aerator tank aeration portion 2～3mg/L
The DOC of the circulation fluid conveying end of aerator tank 0～0.1mg/L
The MLSS concentration of aerator tank 8000～13000mg/L
The rr of aerator tank aeration portion 40～90mg/L·h
Table 2
Project Scope
Treating water BOD 0.3～2mg/L
Treating water COD 5～10mg/L
The full nitrogen for the treatment of water 2～10mg/L
The full phosphorus for the treatment of water 0.04～1mg/L
The treating water solids content Below the 1mg/L
In addition, each measuring method carries out as following according to water drain experimental technique (1997, Corporation Japan water drain association).
(1) BOD:BOD does not add inhibiting nitrification reagent to measure.
(2) COD:COD tries to achieve from the consumption of potassium permanganate, measures with so-called mangaic acid method.
(3) full nitrogen: full nitrogen is to measure with synthetic method.
(4) full phosphorus: full phosphorus is to measure with decomposing quantitative method fully.
(5) DOC:DOC is with dissolved oxygen meter (Yokogawa electromechanics (strain) system dissolved oxygen sensor (model: DO30G) measure with dissolved oxygen umformer (model: DO402G)).
(6) ORP (silver-silver chloride benchmark); ORP is that ((model: OR8EFG) measure with ORP umformer (model: OR400G)), the saturated silver chloride electrode of electrode is used the numerical value that directly reads to Yokogawa electromechanics (strain) system ORP transmitter with the ORP meter.
(7) dissolved phosphorus acid ion attitude phosphorus concentration: dissolved phosphorus acid ion attitude phosphorus concentration, with anaerobic groove mud sample with dry paper 5B drying after, with molybdenum blue (xitix reduction) Their Determination by Spectrophotometry filtrate.
(8) solids content and MLSS concentration: measure with centrifugal separation.Just, get an amount of mud sample and be put in the sediment tube,, outwell supernatant liquor with the rotating speed centrifugation of 3000～4000rpm 2～3 minutes, in sediment tube, add water, stir, similarly carry out centrifugally again, outwell supernatant liquor, this throw out is washed furnace pot, drying is 2 hours under 105～110 ℃, and quality measurement is calculated by following calculating formula.
The dry mass of MLSS concentration=mud (mg)/sample size (L)
(9) r of aerator tank aeration portion r: get 1L mud from the aeration portion of aerator tank and be put into narrow-mouthed bottle, leave standstill 10～20 minutes after, its supernatant liquor is drawn in the thin mouthful bottle with siphon pipe.In the high occasion of MLSS concentration,, utilize centrifuging that mud is separated with supernatant liquor because of almost not leaving standstill the sedimentation of generation.Then, for the DOC of the supernatant liquor that makes narrow-mouthed bottle reaches about 5mg/L and uses aerating apparatus, aeration is after 5～10 minutes tempestuously, itself and above-mentioned sedimentary mud are stirred fully, in order not make air admission, insert the detecting means of DO meter (center chemistry (strain) system UC101), note the reduction of oxygen concn.In the minimizing curve of record, use the straight line portion at initial stage, by following formula, try to achieve oxygen and utilize speed.
Oxygen utilize speed (rr) (mg/Lh)=oxygen reduction (mg/L)/elapsed time (time)
As shown in table 2, during handling, each water quality project can both reach the good performance of removing, especially relevant phosphorus, although do not add flocculation agent, during the on average rate of removing be approximately 96%, can reach the high rate of removing.
As above detailed explanation, according to the present invention, only, can carry out removing of nitrogen, BOD with anaerobic groove and two grooves of aerator tank, also can carry out removing of phosphorus.And,, can suppress the generation of excess sludge because do not add flocculation agent.

Claims (11)

1. drain treatment apparatus, mud is circulated in described drain treatment apparatus system between anaerobic groove and aerator tank, handle the drain treatment apparatus of draining in the biology mode, it is characterized in that the structure of described device is:
In above-mentioned aerator tank, have,
Aerating apparatus partly makes mud rise at aeration, in the part of aeration not mud is descended;
Membrane separation unit in the impregnated configuration in the top of above-mentioned aerating apparatus, is expelled to the system outside with treating water,
When from above-mentioned aerator tank when above-mentioned anaerobic groove is carried mud as circulation fluid, from taking out mud as circulation fluid than being configured in place that above-mentioned aerating apparatus in the above-mentioned aerator tank is in the below.
2. drain treatment apparatus as claimed in claim 1 is characterized in that, takes out the position as the mud of circulation fluid from described aerator tank, below the above-mentioned aerating apparatus that is positioned at extreme lower position, and apart from it more than 20cm.
3. drainage processing method that uses drain treatment apparatus as claimed in claim 1, it is characterized in that, make the dissolved oxygen concentration DOC of mud on the position that enters the anaerobic groove that transports from above-mentioned aerator tank as circulation fluid, below 0.2mg/L, and/or make from above-mentioned aerator tank DOC on the position of taking out mud below 0.5mg/L.
4. drainage processing method as claimed in claim 3 is characterized in that, the oxygen of the mud in the described aerator tank utilizes speed r rMaintain more than the 15mg/Lh.
5. drainage processing method as claimed in claim 3 is characterized in that, the oxygen of the mud in the described aerator tank utilizes speed rr to maintain more than the 25mg/Lh.
6. drainage processing method as claimed in claim 3 is characterized in that, the MLSS concentration as sludge concentration in the described aerator tank maintains more than the 5000mg/L.
7. drainage processing method as claimed in claim 3 is characterized in that, maintains 1～3mg/L scope as the DOC of the dissolved oxygen concentration in the described aerator tank.
8. drainage processing method as claimed in claim 3 is characterized in that, the dissolved phosphorus acid ion attitude phosphorus concentration in the anaerobic groove maintains more than the 10mg/L.
9. drainage processing method as claimed in claim 3 is characterized in that, the redox potential ORP in the described anaerobic groove maintain the silver-silver chloride benchmark-below the 150mV.
10. drain treatment apparatus as claimed in claim 1 is characterized in that, from taking out the mud as circulation fluid between above-mentioned aerating apparatus and the aerator tank bottom.
11. drain treatment apparatus as claimed in claim 1 is characterized in that, is provided with a plurality of above-mentioned aerating apparatuss in above-mentioned aerator tank, takes out the mud as circulation fluid from minimum aerating apparatus below.
CNB038122286A 2002-05-31 2003-05-28 Apparatus and method for waste water treatment Expired - Fee Related CN1295164C (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
JP159466/2002 2002-05-31
JP2002159466A JP3962284B2 (en) 2002-05-31 2002-05-31 Waste water treatment apparatus and waste water treatment method
PCT/JP2003/006686 WO2003101896A1 (en) 2002-05-31 2003-05-28 Apparatus and method for waste water treatment

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CN1656026A CN1656026A (en) 2005-08-17
CN1295164C true CN1295164C (en) 2007-01-17

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JP2010253428A (en) * 2009-04-28 2010-11-11 Asahi Kasei Chemicals Corp Wastewater treatment apparatus and wastewater treatment method
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