CN101274809B - Treatment apparatus for organic wastewater - Google Patents
Treatment apparatus for organic wastewater Download PDFInfo
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- CN101274809B CN101274809B CN2008100880415A CN200810088041A CN101274809B CN 101274809 B CN101274809 B CN 101274809B CN 2008100880415 A CN2008100880415 A CN 2008100880415A CN 200810088041 A CN200810088041 A CN 200810088041A CN 101274809 B CN101274809 B CN 101274809B
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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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/20—Controlling water pollution; Waste water treatment
- Y02A20/208—Off-grid powered water treatment
- Y02A20/212—Solar-powered wastewater sewage treatment, e.g. spray evaporation
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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
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- Separation Using Semi-Permeable Membranes (AREA)
- Biological Treatment Of Waste Water (AREA)
- Treatment Of Water By Ion Exchange (AREA)
- Activated Sludge Processes (AREA)
- Physical Water Treatments (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
A processing device of an organic drainage of the invention processes the organic drainage biologically in a first biological processing reaction tank 1 and processes a flotation separation for the biological processing water without agglutination in a first flotation tank 2. After processing biologically the biological processing water in the first flotation tank 2 in a second biological processing reaction tank 3, 8, a solid-liquid separation is processed. Even if processing the solid-liquid separation for micro-organisms in the processing water in the first biological processing reaction tank 1 without agglutination, if the flotation separation is adopted, the micro-organisms can be adequately removed and separated. Because of no use of agglutinant, problems that load of the organism in the biological processing reaction tank is added and the agglutinant is separated out are avoided and a device setting area and an aeration amount are reduced.
Description
Technical field
The present invention relates to a kind for the treatment of unit that contains the organic drainage of dissolved organic matter, the treatment unit that particularly relates to a kind of following organic drainage, namely, when in being made as 2 sections biological treatment reactive tank, the draining that contains dissolved organic matter being carried out a biological disposal upon, not only can keep the water quality of processing water and alleviate the biological treatment load, and can reduce device area is set.
Background technology
In the processing of organic drainage, general enforcement carried out a biological disposal upon, and is to adopt activated sludge process (activated sludge process) and biomembrance process (biofilm process) specifically.In this type of biological treatment, in recent years, in order to alleviate carrying capacity of environment or to economize on water by recycle-water, need the further processing water through highly processing.
In order to improve the water quality of biological treatment of water, the multi-stage type biological treatment device (for example, the clear 55-28759 communique of Japanese Patent Laid-Open, Japanese Patent Laid-Open 2000-42584 communique) that a kind of reactive tank of will carrying out a biological disposal upon is divided into multistage was proposed in the past.Compare with the biological treatment device of 1 segmentation, the biological treatment device of multi-stage type can obtain the higher processing water of water quality.
Yet, be made as in the multi-stage type biological treatment device of routine of multistage at the reactive tank of only will carrying out a biological disposal upon, can obtain the higher processing water of water-quality ratio 1 segmentation biological treatment device, but still exist need larger area and a large amount of these problems of aeration (aeration) of arranging.Below its reason is described.
That is to say, the microbe that generates in the 1st section biological treatment reactive tank flow in the 2nd section biological treatment reactive tank, and become the 2nd section the biological treatment reactive tank organic loading (organicloading), but at BOD (Biochemical Oxygen Demand, biochemical oxygen demand (BOD)) in the 2nd section low biological treatment reactive tank, microbe begins self-digestion, and dissolved goes out the constituent of the microbe that has become extinct, and causes water quality deterioration.Comprise the hard-decomposed organics such as humin (humin) class in the constituent of the microbe that has become extinct, when being carried out the decomposition of microorganism formula, these hard-decomposed organics need to prolong HRT (hydraulic retention time, and area is set broadens Hydraulic retention time).
And, in the 2nd biological treatment reactive tank, because accumulate material in the oxidizing microorganisms body, and consuming dissolved oxygen (dissolved oxygen), institute is so that the increasing of aeration power.
To this, following scheme is proposed: in the multi-stage type biological treatment device, process carrying out aggegation from the biological treatment of water of the 1st section biological treatment reactive tank, in the 2nd section biological treatment reactive tank to the Separation of Water that separates through solid-liquid separation mechanism carry out a biological disposal upon (Japanese Patent Patent 2005-360619).
In this scheme, the processing water of the 1st section biological treatment reactive tank is carried out aggegation process and to make its solid-liquid separation, remove microbe with this, thus, can reduce the organic loading of the 2nd section biological treatment reactive tank, solve the problem of the multi-stage type biological treatment device of above-mentioned routine.
Yet, in the described scheme of Japanese Patent Patent 2005-360619, have following problem.
That is to say, during the aggegation of the processing water of the 1st section biological treatment reactive tank is processed, when using inorganic agglutinant as agglutinant, to processing that water carries out solid-liquid separation and Separation of Water in residual dissolved metal salt arranged, this dissolved metal salt is separated out in the mud of the 2nd section biological treatment reactive tank or diffuser.
Separate out because of the metal-salt in the mud, the proportion of mud is increased, thereby required power increased when aeration etc. was stirred.Particularly, have in the biological treatment reactive tank of fluidized bed-type of carrier (carrier), it is large that the proportion of carrier becomes, so carrier can be deposited in the reactive tank bottom, can't flow fully.
And the separating out of metal-salt in the diffuser so that cause dissolved oxygen not enough because aeration rate reduces, perhaps causes aeration power to increase because differential pressure (differential pressure) rises.
Great majority in organic agglutinant have biological hard-decomposed, when organic agglutinant flows in the 2nd section biological treatment reactive tank, can be attached to carrier surface, so can cause hindering oxygen to see through or reducing biological activity.
Summary of the invention
Therefore, the object of the present invention is to provide and a kind ofly can solve the treatment unit of processing the organic drainage of caused problem because of the aggegation in the described multi-stage type biological treatment device of Japanese Patent Patent 2005-360619 as above.
The people such as present inventor, concentrate on studies in order to solve described problem, found that: after in the 1st section biological treatment reactive tank, having decomposed most of dissolved organic matter, the microbe that generates in this biological treatment reactive tank is carried out solid-liquid separation without aggegation ground, and further the 2nd section the biological treatment reactive tank in to the isolated Separation of Water of this microbe being carried out a biological disposal upon, like this, even microbe is carried out solid-liquid separation without aggegation ground, so long as flotation separation mode, then can fully described microbe be separated and remove, because not using agglutinant, the 2nd section organic loading in the biological treatment reactive tank increases and agglutinant is separated out these problems so can avoid producing, and can reduce device area and aeration rate are set.
The present invention finishes according to as above viewpoint, below explanation main points of the present invention.
[1] a kind for the treatment of unit of organic drainage is characterized in that comprising:
Have the 1st biological treatment reactive tank of biomembranous fluidized bed-type, organic drainage is carried out a biological disposal upon;
Without the 1st solid-liquid separation mechanism of aggegation and flotation separation mode, the biological treatment of water that flows out from described the 1st biological treatment reactive tank is carried out solid-liquid separation; And
The 2nd biological treatment reactive tank of fluidized bed-type or film separated activated sludge formula is carried out a biological disposal upon to the Separation of Water that separates through the 1st solid-liquid separation mechanism.
[2] such as the treatment unit of [1] described organic drainage, characterized by further comprising:
The 2nd solid-liquid separation mechanism carries out solid-liquid separation to the biological treatment of water that flows out from described the 2nd biological treatment reactive tank; And
The height processing mechanism is removed contained solute in the Separation of Water that described the 2nd solid-liquid separation mechanism separates.
[3] such as the treatment unit of [1] or [2] described organic drainage, it is characterized in that:
The solvability BOD clearance of described the 1st biological treatment reactive tank is 30～99%.
[4] such as the treatment unit of each described organic drainage in [1] to [3], characterized by further comprising:
To the mechanism by interpolation flotation aid in the water of described the 1st solid-liquid separation mechanism solid-liquid separation.
[5] such as the treatment unit of each described organic drainage in [2] to [4], characterized by further comprising:
To the mechanism by interpolation agglutinant in the water of described the 2nd solid-liquid separation mechanism solid-liquid separation.
[6] such as the treatment unit of each described organic drainage in [2] to [5], it is characterized in that:
Described height processing mechanism comprises membrane sepn mechanism.
According to the present invention, in the 1st biological treatment reactive tank, make after most of dissolved organic matter matter decomposition, utilize the 1st solid-liquid separation mechanism that the microbe that generates in the 1st biological treatment reactive tank is separated without aggegation ground, after further in the 2nd biological treatment reactive tank, the Separation of Water of removing this microbe being carried out a biological disposal upon, utilize the 2nd solid-liquid separation mechanism that the microbe that generates in the 2nd biological treatment reactive tank is separated.Like this, by carry out a biological disposal upon, these 2 sections processing of solid-liquid separation, can reduce the biological metabolism amount, and can reduce the organic substance concentration that flows in the height processing mechanism, process thereby can stably carry out draining.
And, in the 1st solid-liquid separation mechanism, do not use agglutinant, but carry out flotation separation without aggegation ground, thus, can effectively remove the 1st the biological treatment reactive tank processing water in SS (SuspendedSubstance, suspended substance), and the increase of the organic loading of the 2nd biological treatment in the reactive tank or caused that by agglutinant metal-salt separates out these problems in the time of can avoiding using agglutinant, and, can reduce the reagent cost of processing for aggegation and reduce appliance arrangement, thereby can effectively process.
The treatment unit of organic drainage of the present invention, more effective in the time must further highly processing the water of fully removing organic substance by aforesaid 2 sections biological treatments, process by follow-up height, can obtain the good processing water of water quality.The water quality of the processing water of this height processing mechanism is splendid, therefore can directly as the water of recycling, perhaps reclaim the former water (rawwater) as pure water, ultrapure water.
And, utilize the height processing mechanism, the water that fully reduces organic substance concentration is processed, so can alleviate the load of highly processing, if the height processing mechanism is membrane separation unit, can prevent that then film from polluting, the degree that flux (flux) was reduced along with the time reduces, the processing of stable for extended periods of time.And, if described height processing mechanism is ion exchange unit, then by reducing organic loading, organic contamination, and can realizes improving water quality treatment, reduce the resin regeneration frequency, reduce the resins exchange frequency.And, if described height processing mechanism is oxidation unit, then by reducing organic loading, can saves the usage quantity of oxygenant and make device realize miniaturization.
Description of drawings
Fig. 1 (a) and Fig. 1 (b) are the system diagrams of example of the treatment unit of expression organic drainage of the present invention.
1: the 1 biological treatment reactive tank 1A: diffuser
2: the 1 flotation cells biological treatment in 3: the 2 reactive tank
3A: diffuser 4: coagulating bath
4A: the 1st condensation portion 4B: the 2nd condensation portion
5: the 2 flotation cells 6: filtration unit
7:RO membrane separation unit biological treatment in 8: the 2 reactive tank
8A: diffuser 10: carrier
20: the outer membrane module of groove
Embodiment
Below, be elaborated for the example of the treatment process of the treatment unit of organic drainage of the present invention.
[organic drainage]
Among the present invention, the organic drainage as processing object gets final product so long as carry out comprising of common biological treatment of organic draining, is not particularly limited, and can enumerate such as electronic industry draining, chemical plant's draining, food factories draining etc.For example, in the electronic component manufacturing processed, from developing procedure, stripping process, etching work procedure, matting etc., the various organic drainages of a large amount of generations, and people wish to reclaim draining, reuse after its purifying treatment being become the degree of pure water, so these drainings are suitable as the draining of processing object of the present invention.
For such organic drainage, can enumerate such as the organic drainage that comprises Virahol, ethanol etc., comprise Monoethanolamine MEA BASF (MEA, Mono Ethanol Amine), Tetramethylammonium hydroxide (TMAH, Tetramethyl ammonium hydroxide) organic drainage of organic nitrogen, ammonia-state nitrogen such as, the organic drainage that comprises the organosulfur compounds such as methyl-sulphoxide (DMSO, Dimethyl Sulfoxide).
The organic concentration of organic drainage of the present invention is not particularly limited, but the present invention is specially adapted to solvability TOC (Total Organic Carbon, total organic carbon) more than or equal to 100mg/L, for example be the processing of the draining that contains high-enriched organics of 200～25000mg/L.
[biological treatment reactive tank]
The＜the 1 biological treatment reactive tank 〉
As the biological treatment reactive tank that is used for draining is carried out a biological disposal upon, as long as organic decomposition efficiency is excellent, can adopt existing aerobism or anaerobic biological treatment reactive tank, but among the present invention, as the 1st biological treatment reactive tank, use the fluidized bed-type biological treatment reactive tank of microbial film mode.As the 1st biological treatment reactive tank, preferably thalline is carried out UASB (upflow anaerobicsludge bed, the upflow anaerobic sludge blanket process) mode of granulation or the biological treatment reactive tank of use carrier.
As carrier, can use gac, various plastic carrier, sponge carrier etc. any, but preferably use sponge carrier.If the use sponge carrier then can make microorganism keep high density.Also be not particularly limited for sponge material, but preferred ester is urethane.Input amount for carrier is also limit without special system, and still, usually, the carrier in the reactive tank of preferably carrying out a biological disposal upon is about 10～50% with respect to the apparent capacity (apparent capacity) of tankage, particularly preferably is about 30～50%.
To the oxybiotic organism processing reaction groove that organism decomposes, can use the aerator tank that is provided with for oxygen (air) feed mechanisms such as the diffuser that in groove, supplies oxygen supply (air), aerators as the ground of microorganism formula under the aerobism state.
On the other hand, to the anaerob processing reaction groove that organism decomposes, can use the anaerobism groove of UASB mode or maintenance carrier as the ground of microorganism formula under the anaerobism state.
The 1st biological treatment reactive tank, can be 1 slot type of oxybiotic organism processing reaction groove or anaerob processing reaction groove, also can be the multi-channel of oxybiotic organism processing reaction groove and/or anaerob processing reaction groove, and, in the situation of 1 slot type, also partition wall can be set in groove.That is to say, among the present invention, as the 1st biological treatment reactive tank, can adopt multi-channel.
The＜the 2 biological treatment reactive tank 〉
Among the present invention, as the 2nd biological treatment reactive tank, use the biological treatment reactive tank of fluidized bed-type or film separated activated sludge formula.About fluidized bed-type biological treatment reactive tank, identical with fluidized bed-type biological treatment reactive tank in above-mentioned the 1st biological treatment reactive tank, also can be the biological membrane type biological treatment reactive tank with carrier.At this moment, about kind and the input amount thereof of the carrier that uses, also with above-mentioned the 1st biological treatment reactive tank in identical.
And, biological treatment reactive tank as the film separated activated sludge formula, can adopt groove external form MBR (the Membrane Bioreactor that outside the groove of biological treatment reactive tank, is provided with membrane module, membrane bioreactor) mode also can adopt and flood the immersion type MBR that disposes membrane module in the groove of biological treatment reactive tank.If use film separated activated sludge formula biological treatment reactive tank, can be in groove that the active sludge height is concentrated, improve biological treatment efficiency.
As the 2nd biological treatment reactive tank, adopt the fluidized bed-type or the film separated activated sludge formula biological treatment reactive tank that utilize carrier, like this, difficulty can be decomposed composition decomposer body and remain in the groove, and can effectively process.Particularly when using the biological treatment reactive tank of film separated activated sludge formula, be that the impregnated membranes as the 2nd solid-liquid separation mechanism of back segment is configured in this biological treatment reactive tank, can make like this device that miniaturization is set.
The 2nd biological treatment reactive tank is identical with the 1st biological treatment reactive tank, can be and be provided with the oxybiotic organism processing reaction groove that microorganism formula ground decomposes organism under the aerobism state (being provided with the aerator tank for oxygen (air) feed mechanisms such as the diffuser that supplies oxygen supply (air), aerators in the groove), also can be the anaerob processing reaction groove that microorganism formula ground decomposes organism under the anaerobism state.
The 2nd biological treatment reactive tank, can adopt 1 slot type of oxybiotic organism processing reaction groove or anaerob processing reaction groove, also can adopt the multi-channel of oxybiotic organism processing reaction groove and/or anaerob processing reaction groove, and, in the situation of 1 slot type, also partition wall can be set in groove.That is to say, among the present invention, as the 2nd biological treatment reactive tank, can adopt multi-channel.
[the 1st solid-liquid separation mechanism]
Among the present invention, as to carrying out the 1st solid-liquid separation mechanism of solid-liquid separation from the biological treatment of water of the 1st biological treatment reactive tank, in not adding the processing without aggegation of agglutinant, employing be the solid-liquid separation mechanism of flotation separation mode.For the flotation separation mode, particularly preferably the pressure floatation separate mode is stable in order to make flotation separation, also can add the flotation aids such as interface promoting agent (interfacial activeagent).
According to the present invention, can utilize without the flotation separation of aggegation efficiently the biological treatment mud from the 1st biological treatment reactive tank is carried out solid-liquid separation, it the reasons are as follows described.
The 1st biological treatment reactive tank of multi-stage type biological treatment device is cut apart the high condition of organic loading that reaches by reactive tank, and the microbe that generates in the 1st biological treatment reactive tank is in the logarithmic proliferation phase (logarithmic growth phase).The state of the microbe of logarithmic proliferation phase is to have few, the repellency enhancing of secretory volume of the extracellular polysaccharide class of hydrophilic radical.The microbe that repellency strengthens is because being subject to scolding the interaction of water to adsorb easily bubble, even without aggegation, so long as flotation separation so just can be carried out solid-liquid separation with the water flowing speed (LV) faster than precipitate and separate.
In addition, the microbe of logarithmic proliferation phase because not forming block (block) so be dispersion state in water, must reach extremely low LV, the obvious variation of processing efficiency without the precipitate and separate of aggegation.
As the treatment condition that flotation separation, preferred pressure floatation separate, there is no special system limit, but preference such as water flowing LV are 5～25m/hr.When LV exceeds this scope, have SS and flow out, and not good in economy when being lower than this scope.
And, when using flotation aid, as flotation aid, can use unsaturated fatty acid salt more than a kind or 2 kinds or 2 kinds etc., for former water, the addition of described flotation aid is preferably about 0.1～10mg/L.In addition, usually, flotation aid is to add before pressure floatation separates.
In general, what the solid-liquid separation of mud adopted is the aggegation processing of adding agglutinant according to ordinary method, among the present invention, for fear of adding polymerize aluminum chloride (PAC, Poly AluminumChloride) or the problem that produces when the inorganic agglutinant such as iron(ic) chloride (III) or organic agglutinant, and implement flotation separation without aggegation, it the reasons are as follows described.
That is to say, if add inorganic agglutinant, then as mentioned above, and the residual dissolved metal salt that has by inorganic agglutinant in the processing water that aggegation is processed, in the 2nd biological treatment reactive tank, described dissolved metal salt can produce in carrier or diffuser and separate out.
Dissolved metal salt separating out on carrier can be reduced the facies posterior hepatis of microbe, thereby reduces the microbial biomass that adheres to, and therefore can cause the reduction of organic substance decomposing speed.And, because the proportion of carrier strengthens, so carrier is deposited in the 2nd biological treatment reactive tank bottom, can't be fully mobile, and required power increases when aeration etc. is stirred.
And, metal-salt separating out on diffuser, meeting is so that because the aeration rate reduction causes dissolved oxygen not enough, perhaps cause aeration power to increase because differential pressure rises.
On the other hand, when the agglutinant deficiency and aggegation when insufficient, small flocs unit (flock) increases, and the flocs unit that flows out in the Separation of Water of solid-liquid separation mechanism increases.When the 2nd biological treatment reactive tank was the MBR mode, the leakage of agglutinant partly was attached to face, caused face to stop up.
Like this, because there being dissolved metal salt, so may cause the serious problems of infringement the 2nd biological treatment reactive tank function, therefore, in the 1st solid-liquid separation mechanism among the present invention, do not use inorganic agglutinant.
And, most of organic agglutinants have biological hard-decomposed, when it flow in the biological treatment reactive tank, as mentioned above, can be attached to carrier surface, thereby may cause stoping oxygen to see through or biological activity is reduced, therefore, in the 1st solid-liquid separation mechanism among the present invention, same with inorganic agglutinant, do not add organic agglutinant yet.
Utilize the 1st solid-liquid separation mechanism to process without aggegation ground, thus, can play following effect: reduce agglutinant, be used for adjusting the medicine of pH value and the equipment that comprises the needed reactive tank of agglutination reaction and gauge.
And, when former water TOC concentration is carried out a biological disposal upon more than or equal to the draining that contains high-enriched organics of 100mg/L, outstanding absurd creature matter concentration increases, when coagulation sedimentation separates because having added a large amount of agglutinants, so mud (sludge) volume increases, so that sludge interface increases the solid-liquid separation difficult, but not increasing without mud volume in the flotation separation of aggegation among the present invention can easily carry out solid-liquid separation.
[the 2nd solid-liquid separation mechanism]
When for from the biological treatment of water of the 2nd biological treatment reactive tank when carrying out solid-liquid separation, can process without aggegation ground, also can carry out aggegation processes, but in order to utilize the 2nd solid-liquid separation mechanism to remove reliably microbe and macromolecule organic matter, preferably before solid-liquid separation, carry out aggegation and process.When back segment is implemented highly to process, particularly preferably add agglutinant and carry out the aggegation processing.
During the aggegation of biological treatment of water is processed, use be common coacervation treating device.The coagulating bath of this coacervation treating device can only be 1 groove, but also is made as 2 grooves or more than 2 grooves multistage.
In general, coacervation treating device is by the rapidly steel basin that is used for making agglutinant and processed water fully to contact and the low rate mixing groove of aggegation flocs unit growth is consisted of.Therefore, when 2 grooves or the coagulating bath more than 2 grooves are made as multistage, preferably with the leading portion coagulating bath as steel basin rapidly, and with the back segment coagulating bath as the low rate mixing groove.
As the inorganic agglutinant that uses in the aggegation processing, can enumerate the iron such as iron trichloride, polyiron sulfate is agglutinant, and the aluminium such as Tai-Ace S 150, aluminum chloride, polymerize aluminum chloride are agglutinant, but considers from aggegation effect aspect, and preferred iron is agglutinant.These inorganic agglutinants can use separately a kind, also can use simultaneously more than 2 kinds or 2 kinds.
When carrying out the aggegation processing, add as required pH value adjusting agent, the pH value that is fit to be adjusted into employed inorganic agglutinant.That is to say that as pH value condition, for example, iron is in the agglutinant, it is effective reacting with the pH value of pH 4～8; Aluminium is in the agglutinant, after reacting less than or equal to the pH value of pH 5.0, is adjusted into more than or equal to effective after the pH value of pH 6.0, so, preferably as required, add hydrochloric acid (HCl), sulfuric acid (H
2SO
4) etc. acid, perhaps the alkali such as sodium hydroxide (NaOH) is adjusted the pH value.Carry out aggegation and process under such pH value condition, can obtain good water quality treatment, its detailed reason is still not clear, but deducibility, is neutralized relevant with the electric charge of protein (albuminoid) composition in the biological metabolite.
Process by aggegation, make dissolved organic matter and outstanding absurd creature in the biological treatment of water become flocs unit.For described aggegation flocs unit is grown up, can in the 1st coagulating bath, add inorganic agglutinant, in the 2nd coagulating bath, add polymer coagulant.
As to the biological treatment of water of the 2nd biological treatment reactive tank, preferably this biological treatment of water is carried out aggegation and is processed after the aggegation of gained process the 2nd solid-liquid separation mechanism that water carries out solid-liquid separation, be not defined as settling bath, flotation cell, separating centrifuge etc., so long as the easy flotation separation of aggegation flocs unit of biological treatment of water and area get final product less than the device of settling bath, so, pressure floatation groove particularly preferably.And, as the 2nd solid-liquid separation mechanism, particularly preferably use the membrane sepn mechanisms such as impregnated membranes.At this moment, as mentioned above, use immersion type MBR to be used as the 2nd biological treatment reactive tank, like this, will be configured in as the impregnated membranes of the 2nd solid-liquid separation mechanism in the 2nd biological treatment reactive tank, thereby can make equipment miniaturization.
[height processing mechanism]
In addition, among the present invention, also can carry out height and process, remove with this biological treatment of water of the 2nd biological treatment reactive tank is carried out contained solute in the Separation of Water of gained after the solid-liquid separation.
About the height processing mechanism, can be further removal utilizes the 1st, the 2nd biological treatment mechanism, the 1st, the 2nd solid-liquid separation mechanism to remove the type of dissolved organic matter (dissolved organic matter) residual in the processing water of gained behind the organism in the draining, and, can be the type of solvent salt contained in the Transformatin water, also can be and remove the two type.
As the height processing mechanism, can be listed below type.
Membrane separation unit: for example, be used for removing RO film (the Reverse Osmosismembrane of organism or desalination, the anti-film that soaks into), NF film (nano-filter membrane, nano-filtration membrane), UF film (ultrafiltration membrane, ultrafilter membrane) tripping device etc.
Ion exchange unit: for example, be used for desalination or remove organic anionite-exchange resin tower, Zeo-karb tower, Zeo-karb and mix mixed bed tower that filling forms, electric desalting apparatus etc. with anionite-exchange resin
Oxidation unit: for example, be used for the oxidation unit of removing organic ozone-oxidizing device, hydrogen peroxide oxidation device, oxychlorination device, ultraviolet oxidation unit etc. or using simultaneously these devices.In addition, as a rule, in most cases, be provided with device for ion-exchange, membrane sepn etc. at the back segment of this oxidation unit.
These height processing mechanisms also can suitably be used in combination more than 2 kinds or 2 kinds.And, as the part of height processing mechanism, also can add again other treatment unit such as filtration unit or activated carbon treatment device.
When using the RO membrane separation unit as the height processing mechanism, particularly preferably in the leading portion of RO membrane separation unit filtration unit is set, SS in dewatering makes a return journey.As filtration unit, can use the filling stratotype filtration unit of having filled the filter materials such as sand, hard coal (Anthracite), use the membrane filter appts of the films such as MF film (Microfiltration membrane, secondary filter film), UF film etc.
[treatment unit of organic drainage]
Below, with reference to an example of the treatment unit of description of drawings organic drainage of the present invention.
Fig. 1 (a) and Fig. 1 (b) are the system diagrams of example of the treatment unit of expression organic drainage of the present invention.In addition, Fig. 1 is an example of the treatment unit of organic drainage of the present invention, and the treatment unit of organic drainage of the present invention is not limited to device shown in Figure 1.For example, the height processing mechanism is not limited to the RO membrane separation unit, also can be ion exchange unit or oxidation unit, and the biological treatment reactive tank is not limited to aerator tank, also can be anaerob processing reaction groove.
The treatment unit of the organic drainage among Fig. 1 (a) comprises: as the aerator tank of the 1st biological treatment reactive tank (below be called " the 1st biological treatment reactive tank ") 1; For the biological treatment of water from the 1st biological treatment reactive tank 1, without aggegation ground, that is to say the 1st flotation cell that do not add any agglutinant ground and carry out solid-liquid separation (below be called " the 1st flotation cell ") 2; Importing have from the Separation of Water of the 1st flotation cell 2, as the aerator tank of the 2nd biological treatment reactive tank (below be called " the 2nd biological treatment reactive tank ") 3; To carrying out the coagulating bath 4 that aggegation is processed from the biological treatment of water of the 2nd biological treatment reactive tank 3; To process from the aggegation of coagulating bath 4 water carry out solid-liquid separation, as the flotation cell of the 2nd solid-liquid separation mechanism (below be called " the 2nd flotation cell ") 5; Importing has the filtration unit 6 of the Separation of Water of the 2nd flotation cell; And the RO membrane separation unit 7 that imports the conduct height processing mechanism of the filtered water that filtration unit 6 is arranged.
In addition, among Fig. 1 (a) and Fig. 1 (b), the 1st biological treatment reactive tank 1 and the 2nd flotation cell 2 can be configured to respectively more than 2 sections or 2 sections, carry out multistage according to the order of biological treatment reactive tank → flotation cell → biological treatment reactive tank → flotation cell and process.
Former water (organic drainage) is imported in the 1st biological treatment reactive tank 1, under the aeration of diffuser 1A, carry out oxybiotic organism and process.In the 1st biological treatment reactive tank 1, remove the most of dissolved organic matter matter (S-TOC) in the former water, can reduce thus the dissolved organic matter matter concentration of the 2nd biological treatment reactive tank 3 that flow into back segment.The 1st biological treatment reactive tank 1 is the biological treating tank that is positioned at leading portion, so, in the groove BOD loading quantitative change of each microbial biomass high, the oneself who has therefore suppressed the food chain between microorganism decomposes.
The 1st biological treatment reactive tank 1 turn form than good speed, according to the decomposability of organic substance contained in the former water and some difference, but preferably with BOD groove load 1.5～60Kg-BOD/m
3/ day, TOC groove load 0.6～24Kg-C/m
3/ day removes the lifting capacity of the solvability BOD (S-BOD) of 30～99% in the former water.
And, if in the 1st biological treatment reactive tank 1, carry out above-mentioned high loaded process, will be difficult to form the good microorganism flocs unit of precipitation threshold, therefore, as shown in the figure, preferably in groove, drop into carrier 10, stably to keep microbial biomass.Maintenance sludge quantity when having added carrier can be according to carrier and filling ratio and is different, but in general, when with 30～50% apparent capacity of tankage and when being filled with spongiform carrier, the mud maintenance dose of each groove reaches about 2500～6000mg-VSS/L, therefore, loading when groove is 1.5～60Kg-BOD/m
3During/day, sludge loading reaches 0.5～10Kg-BOD/Kg-VSS/day, becomes the generation area of disperseing bacterium.
Then, for the biological treatment of water from the 1st biological treatment reactive tank 1, in the 1st flotation cell 2, add flotation aid without aggegation ground and carry out flotation separation, then, the Separation of Water of the 1st flotation cell 2 is directed in the 2nd biological treatment reactive tank 3, under the aeration of diffuser 3A, carry out oxybiotic organism and process.In the 2nd biological treatment reactive tank 3, to decomposing through residual dissolved organic matter matter after the biological treatment of the 1st biological treatment reactive tank 1.In the 2nd biological treatment reactive tank 3, comparatively ideal is to decompose reliably, flow into as the organic concentration in the RO membrane separation unit 7 of back segment height processing mechanism with reduce.The 2nd biological treatment reactive tank 3 particularly preferably remains on carrier 10 type in the groove or keeps the type of thalline in the MBR mode, like this, also can stably keep microbial biomass under underload.The groove load of the 2nd biological treatment reactive tank 3 is 0.03～2Kg-BOD/m
3/ day, particularly preferred is 0.1～1.2Kg-BOD/m
3/ day.And, when adopt using the biological treatment reactive tank of carrier, preferably fill carrier with 30～50% apparent capacity of tankage; When adopting the MBR mode to be, preferred MLSS concentration is 2000～12000mg/L.
Then, the biological treatment of water from the 2nd biological treatment reactive tank 3 is directed in the coagulating bath 4.This coagulating bath 4 is the 1st condensation portion (being denoted as " No.2-1 condensation portion " in the table 1 described later) 4A of biological treatment of water to be arranged and imported the dual grooved biological treatment reactive tank that has from the 2nd condensation portion 4B (being denoted as " No.2-2 condensation portion " in the table 1 described later) formation of the water of the 1st condensation portion 4A by importing, biological treatment of water is subject to the aggegation processing at first add inorganic agglutinant in the 1st condensation portion 4A after, afterwards, further in the 2nd condensation portion 4B, add pH value adjusting agent and/or polymer coagulant, and make flocs unit thick, then, aggegation is processed water and is sent to the 2nd flotation cell 5, adds flotation aid and utilizes flotation process to make aggegation flocs unit solid-liquid separation.
Then, for the Separation of Water of the 2nd flotation cell 5, in filtration unit 6, remove residual SS, in RO membrane separation unit 7, carry out afterwards the RO membrane separation, take out infiltration water as processing water.
In the treatment unit of the organic drainage among Fig. 1 (b), the aerator tank that replaces the 2nd biological treatment reactive tank 3 among Fig. 1 (a), and groove external form MBR mode that diffuser 8A and groove the have membrane module 20 outward reactive tank of carrying out a biological disposal upon is set, as the 2nd biological treatment reactive tank 8, and utilize pump (bump) P, send the mixed solution in the 2nd biological treatment reactive tank 8 to membrane module 20, make its concentrated, circulation, omitted coagulating bath 4 and the 2nd flotation cell, and other structures are all identical with the device shown in Fig. 1 (a).Among Fig. 1 (b), for having the parts of identical function with the parts shown in Fig. 1 (a), use same-sign.
In the treatment unit of the organic drainage shown in Fig. 1 (b), the Separation of Water of the 1st flotation cell 2 is directed to as the groove external form MBR mode of the 2nd biological treatment reactive tank 8 and carries out a biological disposal upon in the reactive tank, implements identical processing.About the carry out a biological disposal upon treatment condition of reactive tank of this groove external form MBR mode, preferred MLSS concentration is that 5000mg/L, groove load are 1.0Kg-BOD/m
3/ day, flux are 0.4m
3/ m
2Day.
From the carry out a biological disposal upon biological treatment of water of reactive tank 8 of this groove external form MBR mode, after through biological treatment, carry out membrane filtration by the membrane module 20 outside the groove, therefore, shown in Fig. 1 (a), can without aggegation processing, flotation separation, process and directly import in the RO membrane separation unit 7.
In the device shown in Fig. 1 (a) and Fig. 1 (b), carry out a biological disposal upon and these 2 sections processing of solid-liquid separation at the leading portion of RO membrane separation unit 7, can obtain thus the processing water of high water quality, and, water supply that can the FI value is low is in RO membrane separation unit 7, so, can suppress the reduction of the membrane flux of RO membrane separation unit 7, and can obtain steadily in the long term to process water.
In addition, so-called FI value is as following index, and this index is used for judging water passed into carries out deionization (deioniztion) when processing in the RO membrane separation unit, and whether the water quality that supplies to the water of RO membrane separation unit is suitable for the RO film is processed.Even the amount of the dissolved organic matter in the water or SS about equally, when described water being carried out the processing of RO film, membrane flux also may occur can be in the early stage situation that just reduces and can not reduce of processing, and at this moment, the FI value that supplies to the water of RO can produce difference.
The FI value can be obtained according to following methods: operate, namely, (membrane filter) passes into sample water to the filter membrane with preset aperture, instrumentation filters predetermined amount after the needed time, obtain according to needs time at initial stage and needs time of passing into after the water scheduled time, this FI value is used for judging that water quality is easily or is difficult for causing that film pollutes, the film obstruction.In general, even if the FI value less than or equal to 5 water quality, also is allowed to sometimes as supplying to the water (being the water supply of RO) of RO, but as a rule, hope is the FI value less than or equal to 3 water quality.Therefore, among the present invention, when using the RO membrane separation unit as the height processing mechanism, preferably utilize biological treatment and these 2 sections processing of solid-liquid separation to obtain FI value less than or equal to 3 water, and conduct supply to the water of RO membrane separation unit.
[embodiment]
Below, enumerate embodiment and comparative example, the present invention is carried out more specific description.
[embodiment 1]
In the device shown in Fig. 1 (a), with principal constituent be Tetramethylammonium hydroxide (TMAH) for the plant drainage of following water quality as former water, process with the processing water yield of 2000L/day.In addition, deducibility, the quantity not sufficient of phosphorus in the biological treatment of this former water, therefore, so that TOC: P=100: 3 mode is added phosphoric acid in the former water and is processed.In addition, as flotation aid, use potassium oleate.
＜raw water quality 〉
S-TOC：328mg/L
Kj-N：76mg/L
PO
4-P：0.8mg/L
Specification and the treatment condition of the employed device of expression in the table 1.
And, the water quality of expression each several part in the table 2, the proportion of the carrier in the 1st, the 2nd biological treatment reactive tank is added in expression in the table 3.
[embodiment 2]
In the device shown in Fig. 1 (b), identical with disposition among the embodiment 1, plant drainage as former water, is processed with the processing water yield of 2000L/day.In addition, deducibility, the quantity not sufficient of phosphorus in the biological treatment of this former water is so so that TOC: P=100: 3 mode is added phosphoric acid in the former water to and processed.As flotation aid, identical with embodiment 1, use potassium oleate.
Specification and the treatment condition of the employed device of expression in the table 1.
And, the water quality of expression each several part in the table 2, the proportion of the carrier in the 1st biological treatment reactive tank is added in expression in the table 3.
[comparative example 1]
Settling bath (below be called " the 1st settling bath ") is set replaces the 1st flotation cell among the embodiment 1, in settling bath, the biological treatment of water of the 1st biological treatment reactive tank is carried out solid-liquid separation, in addition, all process in the mode identical with embodiment 1.
Specification and the treatment condition of the employed device of expression in the table 1.
And, the water quality of expression each several part in the table 2, the proportion of the carrier in the 1st, the 2nd biological treatment reactive tank is added in expression in the table 3.
[comparative example 2]
Coagulating bath and settling bath (the 1st settling bath) are set replace the 1st flotation cell among the embodiment 1, in coagulating bath (coagulating bath that comprises the dual grooved of the 1st condensation portion (being denoted as " No.1-1 condensation portion " in the table 1 described later) and the 2nd condensation portion (being denoted as " No.1-2 condensation portion " in the table 1 described later)), the biological treatment of water of the 1st biological treatment reactive tank 1 is carried out aggegation to be processed, carry out solid-liquid separation at settling bath afterwards, in addition, all process in the mode identical with embodiment 1.
Specification and the treatment condition of the employed device of expression in the table 1.
And, the water quality of expression each several part in the table 2, the proportion of the carrier in the 1st, the 2nd biological treatment reactive tank is added in expression in the table 3.
[table 1]
The polyurethane sponge apparent capacity that ※ 1:3mm is square
The ferric chloride aqueous solutions of ※ 2:38wt% (weight percent)
※ 3: adjust by adding NaOH
※ 4: be filled with sand, anthracitic Double-filtering device
※ 5: flotation aid: potassium oleate 4mg/L
[table 2]
※ testing method: ASTM D4189-95
[table 3]
| Embodiment 1 | Embodiment 2 | Comparative example 1 | Comparative example 2 | ||
| The 1st biological treatment reactive tank | Carrier proportion [Kg/L] | 1.03 | 1.03 | 1.03 | 1.03 |
| The 2nd biological treatment reactive tank | Carrier proportion [Kg/L] | 1.01 | - | 1.02 | 1.09 |
According to above result, be known as below content.
Among the embodiment 1,2, in the 1st biological treatment reactive tank 1, can remove the most of organism in the former water, and can be before carrying out self-digestion with microbe as SS, in the 1st flotation cell 2, described microbe is carried out solid-liquid separation without aggegation ground and removes.And, among the embodiment 1, further in the 2nd biological treatment reactive tank 3, the Separation of Water without aggegation of the 1st biological treatment reactive tank 1 is processed, like this, the carrier proportion that can avoid producing because of separating out of dissolved metal salt increases and carrier precipitation, further highly decomposes residual organism, and, by remove SS in the 2nd flotation cell 5, the result can obtain the lower processing water of S-TOC than comparative example 1 and 2.
Relative therewith, in the comparative example 1, because having used settling bath but not flotation cell, so the separation property of SS is relatively poor, biological treatment causes load to back segment, and organic matter removal, compendency, filterableness are worsened.In the comparative example 2, replace flotation cell because having used coagulating bath and settling bath, so the removal of SS is good, but the back segment flowability of carrier obviously worsens, so S-TOC worsens.
In addition, using the groove external form MBR mode reactive tank of carrying out a biological disposal upon to be used as among the embodiment 2 of the 2nd biological treatment reactive tank, the removal of S-TOC and RO film water quality treatment are good, and flux (permeation flux (permeation flux)) is also stable.
Claims (3)
1. the treatment unit of an organic drainage is characterized in that comprising:
Have the 1st biological treatment reactive tank of biomembranous fluidized bed-type, organic drainage is carried out a biological disposal upon, the concentration of the solvability total organic carbon of described organic drainage is 200～25000mg/L;
Without the 1st solid-liquid separation mechanism of aggegation and pressure floatation separate mode, the biological treatment of water that flows out from described the 1st biological treatment reactive tank is carried out solid-liquid separation;
The 2nd biological treatment reactive tank of film separated activated sludge formula is carried out a biological disposal upon to the Separation of Water that separates through described the 1st solid-liquid separation mechanism; And
The height processing mechanism comprises membrane sepn mechanism, and to processing from the biological treatment of water of described the 2nd biological treatment reactive tank.
2. the treatment unit of organic drainage according to claim 1 is characterized in that the solvability BOD clearance of wherein said the 1st biological treatment reactive tank is 30～99%.
3. the treatment unit of organic drainage according to claim 1 characterized by further comprising:
To the mechanism by interpolation flotation aid in the water of described the 1st solid-liquid separation mechanism solid-liquid separation.
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| JP5444684B2 (en) * | 2008-10-21 | 2014-03-19 | 栗田工業株式会社 | Organic wastewater treatment method and treatment equipment |
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| JP5581669B2 (en) * | 2009-03-10 | 2014-09-03 | 株式会社日立製作所 | Water treatment method, water treatment member and water treatment facility |
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| WO2011108478A1 (en) * | 2010-03-05 | 2011-09-09 | 栗田工業株式会社 | Water treatment method and process for producing ultrapure water |
| JP5753668B2 (en) * | 2010-06-22 | 2015-07-22 | 株式会社神鋼環境ソリューション | Waste water treatment method and waste water treatment equipment |
| JP5914964B2 (en) * | 2010-10-18 | 2016-05-11 | 栗田工業株式会社 | Ultrapure water production method |
| JP2012205990A (en) * | 2011-03-29 | 2012-10-25 | Kurita Water Ind Ltd | Treatment apparatus of organic wastewater |
| WO2013105421A1 (en) | 2012-01-11 | 2013-07-18 | 栗田工業株式会社 | Reverse osmosis treatment process |
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| JP5828327B2 (en) * | 2013-02-13 | 2015-12-02 | 栗田工業株式会社 | Method for processing development wastewater in color filter manufacturing process |
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| JP6554781B2 (en) * | 2013-12-26 | 2019-08-07 | 栗田工業株式会社 | Operation method of reverse osmosis membrane device and reverse osmosis membrane device |
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| JP6015811B1 (en) * | 2015-05-19 | 2016-10-26 | 栗田工業株式会社 | Water treatment method and water treatment apparatus |
| JP6318193B2 (en) * | 2016-05-18 | 2018-04-25 | 前澤工業株式会社 | Water treatment method and equipment |
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