CN101274809A - Treatment apparatus for organic wastewater - Google Patents
Treatment apparatus for organic wastewater Download PDFInfo
- Publication number
- CN101274809A CN101274809A CNA2008100880415A CN200810088041A CN101274809A CN 101274809 A CN101274809 A CN 101274809A CN A2008100880415 A CNA2008100880415 A CN A2008100880415A CN 200810088041 A CN200810088041 A CN 200810088041A CN 101274809 A CN101274809 A CN 101274809A
- Authority
- CN
- China
- Prior art keywords
- biological treatment
- reactive tank
- liquid separation
- solid
- water
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Classifications
-
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Abstract
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 of treatment unit that contains the organic drainage of dissolved organic matter, the treatment unit that particularly relates to a kind of following organic drainage, promptly, 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 for the treatment of water and alleviate 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,, need further treating water through highly handling in order to alleviate carrying capacity of environment or to economize on water by recycle-water.
In order to improve the water quality of biological treatment of water, the multi-stage type biological treatment device (for example, the Japanese Patent spy opens clear 55-28759 communique, the Japanese Patent spy opens the 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 treating 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 treating water of water-quality ratio 1 segmentation biological treatment device, but still exist need bigger area and a large amount of these problems of aeration (aeration) of being provided with.Below its reason is described.
That is to say, the microbe that is generated 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, causes water quality deterioration.Comprise 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 prolong HRT (hydraulic retention time, and area is set broadens the waterpower residence time).
And, in the 2nd biological treatment reactive tank,, and consuming dissolved oxygen (dissolved oxygen) because accumulate material in the oxidizing microorganisms body, institute is so that the increasing of aeration power.
To this, following scheme is proposed: in the multi-stage type biological treatment device, handle 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 through dried up biological treatment of the isolating branch of solid-liquid separation mechanism (Japanese Patent special be willing to 2005-360619).
In this scheme, the treating water of the 1st section biological treatment reactive tank is carried out aggegation handle 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 Japanese Patent is special is willing to have following problem in the described scheme of 2005-360619.
That is to say, during the aggegation of the treating water of the 1st section biological treatment reactive tank is handled, when using inorganic agglutinant as agglutinant, in that treating water is carried out solid-liquid separation branch residual in dried up 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 increases when aeration etc. is stirred.Particularly, have in the biological treatment reactive tank of thermopnore formula of carrier (carrier), it is big 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 makes to cause the dissolved oxygen deficiency because of aeration rate reduces, and perhaps causes aeration power to increase because of 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, and 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 handling the organic drainage of caused problem because of the aggegation in the described multi-stage type biological treatment device of the special 2005-360619 of hope of as above Japanese Patent.
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 not had aggegation ground carry out solid-liquid separation, and further in the 2nd section biological treatment reactive tank to dried up biological treatment of the isolated branch of this microbe, like this, even being had aggegation ground, microbe do not carry out solid-liquid separation, so long as flotation separation mode, then can fully described microbe be separated and remove, because of 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 of treatment unit of organic drainage is characterized in that comprising:
Have the 1st biological treatment reactive tank of biomembranous thermopnore formula, organic drainage is carried out a biological disposal upon;
The 1st solid-liquid separation mechanism of no aggegation and flotation separation mode is to carrying out solid-liquid separation from the effusive biological treatment of water of described the 1st biological treatment reactive tank; And
The 2nd biological treatment reactive tank of thermopnore formula or film separated activated sludge formula is to through dried up biological treatment of the isolating branch of the 1st solid-liquid separation mechanism.
[2], it is characterized in that also comprising as the treatment unit of [1] described organic drainage:
The 2nd solid-liquid separation mechanism is to carrying out solid-liquid separation from the effusive biological treatment of water of described the 2nd biological treatment reactive tank; And
The height processing mechanism is removed contained solute in the isolating branch of described the 2nd solid-liquid separation mechanism is dried up.
[3] 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] as the treatment unit of each described organic drainage in [1] to [3], it is characterized in that also comprising:
In by the water of described the 1st solid-liquid separation mechanism solid-liquid separation, add the mechanism of flotation aid.
[5] as the treatment unit of each described organic drainage in [2] to [4], it is characterized in that also comprising:
In by the water of described the 2nd solid-liquid separation mechanism solid-liquid separation, add the mechanism of agglutinant.
[6] 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, utilizing the 1st solid-liquid separation mechanism to make the microbe that is generated in the 1st biological treatment reactive tank not have aggegation ground separates, further in the 2nd biological treatment reactive tank to the branch of removing this microbe is dried up carry out a biological disposal upon after, utilize the 2nd solid-liquid separation mechanism that the microbe that the 2nd biological treatment is generated in the 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, handle thereby can stably carry out draining.
And, in the 1st solid-liquid separation mechanism, do not use agglutinant, do not carry out flotation separation but there is aggegation ground, thus, can remove effectively the 1st the biological treatment reactive tank treating water in SS (SuspendedSubstance, suspended substance), and the increase of the organic loading of the 2nd biological treatment in the reactive tank or cause that by agglutinant metal-salt separates out these problems in the time of can avoiding using agglutinant, and, can reduce the reagent cost that is used for the aggegation processing and reduce appliance arrangement, thereby can handle effectively.
The treatment unit of organic drainage of the present invention, more effective in the time must further highly handling by aforesaid 2 sections biological treatments to the water of fully removing organic substance, handle by follow-up height, can obtain the good treating water of water quality.The water quality of the treating water of this height processing mechanism is splendid, therefore can perhaps reclaim the former water (rawwater) as pure water, ultrapure water directly as the water that utilizes again.
And, utilize the height processing mechanism, the water that fully reduces organic substance concentration is handled, so can alleviate the load of highly handling, if the height processing mechanism is a 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 an ion exchange unit,, and can realizes improving water quality treatment, reduce the resin regeneration frequency, reduce the resins exchange frequency then by reducing organic loading, organic contamination.And, if described height processing mechanism is an oxidation unit,, can saves the usage quantity of oxygenant and make device realize miniaturization then by reducing organic loading.
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
Flotation cell 6 in 5: the 2: 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,, get final product, be not particularly limited, for example can enumerate: electronic industry draining, chemical plant's draining, food factories draining etc. so long as carry out comprising of common biological treatment of organic draining as the organic drainage of process object.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 process object of the present invention.
For such organic drainage, for example can enumerate: 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 methyl-sulphoxide organosulfur compounds such as (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), for example be the processing of the draining that contains high-enriched organics of 200～25000mg/L more than or equal to 100mg/L.
[biological treatment reactive tank]
＜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 thermopnore formula 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 a urethane.Also do not have special system limit for the input amount of carrier, 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, especially preferably about 30～50%.
To the oxybiotic organism processing reaction groove that organism decomposes, can use the aerator tank of oxygen (air) feed mechanisms such as being provided with the diffuser that is used in groove, supplying with oxygen (air), aerator as microorganism formula under aerobism state ground.
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, under the situation of 1 slot type, also partition wall can be set in groove.That is to say, among the present invention,, can adopt multi-channel as the 1st biological treatment reactive tank.
＜the 2 biological treatment reactive tank 〉
Among the present invention,, use the biological treatment reactive tank of thermopnore formula or film separated activated sludge formula as the 2nd biological treatment reactive tank.About thermopnore formula biological treatment reactive tank, identical with thermopnore formula biological treatment reactive tank in above-mentioned the 1st biological treatment reactive tank, also can be biological membrane type biological treatment reactive tank with carrier.At this moment, about the 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 in groove, the active sludge height be concentrated, improve biological treatment efficient.
As the 2nd biological treatment reactive tank, adopt the thermopnore formula 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 handle effectively.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 device that miniaturization is set like this.
The 2nd biological treatment reactive tank is identical with the 1st biological treatment reactive tank, can be the oxybiotic organism processing reaction groove that is provided with under the aerobism state microorganism formula ground organism is decomposed (being provided with the aerator tank of oxygen (air) feed mechanisms such as the diffuser that is used to supply with oxygen (air), aerator 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, under the situation of 1 slot type, also partition wall can be set in groove.That is to say, among the present invention,, can adopt multi-channel as the 2nd biological treatment reactive tank.
[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 the no aggegation of not adding agglutinant is handled, employing be the solid-liquid separation mechanism of flotation separation mode.For the flotation separation mode, preferred especially pressure floatation separate mode, stable in order to make flotation separation, also can add interface promoting agent flotation aids such as (interfacial activeagent).
According to the present invention, can utilize no agglutinative flotation separation and efficiently to from the 1st the biological treatment reactive tank biological treatment mud carry 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.Repellency enhanced microbe is because of being subjected to scolding the interaction of water to adsorb bubble easily, even there is not 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 of not forming block (block) so be dispersion state in water, no agglutinative precipitate and separate must reach extremely low LV, the obvious variation of processing efficiency.
As flotation separation, the preferred isolating treatment condition of pressure floatation, 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,, can use unsaturated fatty acid salt more than a kind or 2 kinds or 2 kinds etc. as flotation aid, 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 is produced when iron(ic) chloride inorganic agglutinants such as (III) or organic agglutinant, and implement no agglutinative flotation separation, 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 treating water that aggegation is handled, 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 organism decomposition rate.And, because of 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 can make to cause the dissolved oxygen deficiency because of aeration rate reduces, and perhaps causes aeration power to increase because of differential pressure rises.
On the other hand, when the agglutinant deficiency and aggegation when insufficient, small flocs unit (flock) increases, and flows out to the branch of the solid-liquid separation mechanism flocs unit in dried up and increases.When the 2nd biological treatment reactive tank was the MBR mode, the leakage part of agglutinant caused face to stop up attached to face.
Like this, because of there being dissolved metal salt,, therefore, in the 1st solid-liquid separation mechanism among the present invention, do not use inorganic agglutinant so may cause the serious problems of infringement the 2nd biological treatment reactive tank function.
And, most of organic agglutinants have biological hard-decomposed, when it flow in the biological treatment reactive tank, as mentioned above, understand, thereby may cause stoping oxygen to see through or biological activity is reduced attached to carrier surface, 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 have aggegation ground and do not handle, thus, can play following effect: reduce agglutinant, be used to the equipment adjusting the medicine of pH value and comprise 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 of having added a large amount of agglutinants, so mud (sludge) volume increases, and makes sludge interface increase, it is difficult that solid-liquid separation becomes, but mud volume does not increase in the no agglutinative flotation separation 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 not having aggegation ground handles, also can carry out aggegation handles, but, preferably before solid-liquid separation, carry out aggegation and handle in order to utilize the 2nd solid-liquid separation mechanism to remove microbe and macromolecule organic matter reliably.When back segment is implemented highly to handle, especially preferably add agglutinant and carry out the aggegation processing.
During the aggegation of biological treatment of water is handled, 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 to be made of steel basin rapidly that is used to make agglutinant and processed water fully to contact and steel basin at a slow speed that the aggegation flocs unit is grown up.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 steel basin at a slow speed.
As the inorganic agglutinant that uses in the aggegation processing, can enumerate iron such as iron trichloride, polyiron sulfate is agglutinant, and 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 a kind separately, also can use simultaneously more than 2 kinds or 2 kinds.
When carrying out the aggegation processing, add the pH value as required and adjust agent, to be adjusted into the pH value that employed inorganic agglutinant is fit to.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, is adjusted into more than or equal to effective after the pH value of pH 6.0 smaller or equal to the pH value of pH 5.0, so, preferably as required, add hydrochloric acid (HCl), sulfuric acid (H
2SO
4) wait acid, perhaps sodium hydroxide alkali such as (NaOH) is adjusted the pH value.Carry out aggegation and handle under such pH value condition, can obtain good water quality treatment, its detailed reason is still indeterminate, but deducibility, is neutralized relevant with the electric charge of protein (albuminoid) composition in the biological metabolite.
Handle 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 handles the 2nd solid-liquid separation mechanism that the aggegation treating water of back gained 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, preferred especially pressure floatation groove.And, as the 2nd solid-liquid separation mechanism, especially preferably use 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 handle, with this remove to the biological treatment of water of the 2nd biological treatment reactive tank carry out after the solid-liquid separation branch of gained dried up in contained solute.
About the height processing mechanism, can be further removal utilize the 1st, the 2nd biological treatment mechanism, the 1st, the 2nd solid-liquid separation mechanism remove in the treating water of gained behind the organism in the draining the type of residual dissolved organic matter (dissolved organic matter), and, can be the type of removing solvent salt contained in the treating 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 to remove 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 with anionite-exchange resin and fill the mixed bed tower form, electric desalting apparatus etc.
Oxidation unit: for example, the oxidation unit that is used to remove organic ozone oxidation device, hydrogen peroxide oxidation device, oxychlorination device, ultraviolet oxidation unit etc. or uses these devices simultaneously.In addition, as a rule, in most cases, be provided with the device that is used 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 other treatment unit such as filtration unit or activated carbon treatment device again.
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 sand, hard coal filter materials such as (Anthracite), use the membrane filter appts of 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 biological treatment of water from the 1st biological treatment reactive tank 1, no aggegation, 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 branch of the 1st flotation cell 2 dried up, 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 handled from the biological treatment of water of the 2nd biological treatment reactive tank 3; To the aggegation treating water from coagulating bath 4 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 dried up filtration unit of the branch of the 2nd flotation cell 6; 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 handle.
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 handle.In the 1st biological treatment reactive tank 1, remove the most of dissolved organic matter matter (S-TOC) in the former water, can reduce the dissolved organic matter matter concentration of the 2nd biological treatment reactive tank 3 that flow into back segment thus.The 1st biological treatment reactive tank 1 is the biological treating tank that is positioned at leading portion, so, the BOD loading quantitative change height of each microbial biomass in the groove, the oneself who has therefore suppressed the food chain between microorganism decomposes.
The preferable running form of the 1st biological treatment reactive tank 1, 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 and when being filled with spongiform carrier with 30～50% apparent capacity of tankage, 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 biological treatment of water from the 1st biological treatment reactive tank 1, no aggegation ground adds flotation aid and carries out flotation separation in the 1st flotation cell 2, then, the branch of the 1st flotation cell 2 is dried up to be directed in the 2nd biological treatment reactive tank 3, under the aeration of diffuser 3A, carry out oxybiotic organism and handle.The 2nd the biological treatment reactive tank 3 in, to through the 1st the biological treatment reactive tank 1 biological treatment after residual dissolved organic matter matter decompose.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 to reduce as much as possible.The 2nd biological treatment reactive tank 3 especially 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, that good especially 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 (note work " No.2-1 condensation portion " in the table 1 described later) 4A and the dual grooved biological treatment reactive tank that imports the 2nd condensation portion 4B (note is made " No.2-2 condensation portion " in the table 1 described later) formation that has from the water of the 1st condensation portion 4A that biological treatment of water is arranged by importing, biological treatment of water is subjected 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 the pH value and adjust agent and/or polymer coagulant, and make flocs unit thick, then, the aggegation treating water is sent to the 2nd flotation cell 5, adds flotation aid and utilizes flotation process to make aggegation flocs unit solid-liquid separation.
Then, dried up for the branch of the 2nd flotation cell 5, in filtration unit 6, remove residual SS, in RO membrane separation unit 7, carry out the RO membrane sepn afterwards and handle, take out infiltration water as treating 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 it concentrate, circulate, 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),, use same-sign for having the parts of identical function with the parts shown in Fig. 1 (a).
In the treatment unit of the organic drainage shown in Fig. 1 (b), the branch of the 1st flotation cell 2 is dried up to be directed to as the groove external form MBR mode of the 2nd biological treatment reactive tank 8 and to carry 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, carrying out membrane filtration through the biological treatment back by the membrane module outside the groove 20, therefore, shown in Fig. 1 (a), can handle and directly import in the RO membrane separation unit 7 without aggegation processing, flotation separation.
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 the treating water of high water quality thus, 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 treating water steadily in the long term.
In addition, so-called FI value is as following index, and this index is used for judging water fed carries out deionization (deioniztion) when handling 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 handled.Even the amount of 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 of handling that just reduces and can not reduce, 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 method: operate, promptly, feed sample water to the filter membrane with preset aperture (membrane filter), instrumentation filters predetermined amount after the needed time, needs time and the needs time afterwards feeding water scheduled time according to the initial stage are obtained, and this FI value is used to judge that water quality is easily or is difficult for causing that film pollutes, film stops up.In general, even if the FI value smaller 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 smaller or equal to 3 water quality.Therefore, among the present invention, when using the RO membrane separation unit, preferably utilize biological treatment and these 2 sections processing of solid-liquid separation to obtain FI value, and conduct supply to the water of RO membrane separation unit smaller or equal to 3 water as the height processing mechanism.
[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, handle 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 and is handled in former water.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
The 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 handled 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 handled.As flotation aid, identical with embodiment 1, use potassium oleate.
The 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 handle in the mode identical with embodiment 1.
The 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 (note is made " No.1-1 condensation portion " in the table 1 described later) and the 2nd condensation portion (note is made " 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 handled, carry out solid-liquid separation at settling bath afterwards, in addition, all handle in the mode identical with embodiment 1.
The 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 medium filtration device
※ 5: flotation aid: potassium oleate 4mg/L
[table 2]
※ testing method: ASTM D4189-95
[table 3]
| Embodiment 1 | |
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 had aggegation ground and does not carry out solid-liquid separation and remove.And, among the embodiment 1, further the no agglutinative to the 1st biological treatment reactive tank 1 divides dried up the processing in the 2nd biological treatment reactive tank 3, like this, the carrier proportion that can avoid being produced because of separating out of dissolved metal salt increases and carrier precipitation, further highly decomposes institute's residual organic, and, by remove SS in the 2nd flotation cell 5, the result can obtain the lower treating water of S-TOC than comparative example 1 and 2.
Relative therewith, in the comparative example 1, because of 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 removal, compendency, filterableness are worsened.In the comparative example 2, replace flotation cell because of 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 (6)
1, a kind of treatment unit of organic drainage is characterized in that comprising:
Have the 1st biological treatment reactive tank of biomembranous thermopnore formula, organic drainage is carried out a biological disposal upon;
The 1st solid-liquid separation mechanism of no aggegation and flotation separation mode is to carrying out solid-liquid separation from the effusive biological treatment of water of described the 1st biological treatment reactive tank; And
The 2nd biological treatment reactive tank of thermopnore formula or film separated activated sludge formula is to through dried up biological treatment of the described isolating branch of the 1st solid-liquid separation mechanism.
2, the treatment unit of organic drainage according to claim 1 is characterized in that also comprising:
The 2nd solid-liquid separation mechanism is to carrying out solid-liquid separation from the effusive biological treatment of water of described the 2nd biological treatment reactive tank; And
The height processing mechanism is removed contained solute in the isolating branch of described the 2nd solid-liquid separation mechanism is dried up.
3, the treatment unit of organic drainage according to claim 1 and 2 is characterized in that the solvability BOD clearance of wherein said the 1st biological treatment reactive tank is 30～99%.
4,, it is characterized in that also comprising according to the treatment unit of each described organic drainage of claim 1-2:
In by the water of described the 1st solid-liquid separation mechanism solid-liquid separation, add the mechanism of flotation aid.
5, the treatment unit of organic drainage according to claim 2 is characterized in that also comprising:
In by the water of described the 2nd solid-liquid separation mechanism solid-liquid separation, add the mechanism of agglutinant.
6, the treatment unit of organic drainage according to claim 2 is characterized in that wherein said height processing mechanism comprises membrane sepn mechanism.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2007091666A JP5223219B2 (en) | 2007-03-30 | 2007-03-30 | Organic wastewater treatment equipment |
| JP2007-091666 | 2007-03-30 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101274809A true CN101274809A (en) | 2008-10-01 |
| CN101274809B CN101274809B (en) | 2013-01-09 |
Family
ID=39971971
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2008100880415A Active CN101274809B (en) | 2007-03-30 | 2008-03-27 | Treatment apparatus for organic wastewater |
Country Status (3)
| Country | Link |
|---|---|
| JP (1) | JP5223219B2 (en) |
| CN (1) | CN101274809B (en) |
| TW (1) | TWI494281B (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102272052A (en) * | 2009-03-10 | 2011-12-07 | 株式会社日立制作所 | Water-treating method and water-treating member |
| CN102781850A (en) * | 2010-03-05 | 2012-11-14 | 栗田工业株式会社 | Water treatment method and process for producing ultrapure water |
| CN104981435A (en) * | 2013-02-13 | 2015-10-14 | 栗田工业株式会社 | Method for treating development wastewater from color filter production step |
| CN107530592A (en) * | 2015-05-19 | 2018-01-02 | 栗田工业株式会社 | Agglutinant and method for treating water |
| CN111268863A (en) * | 2020-03-06 | 2020-06-12 | 上海东振环保工程技术有限公司 | Developing solution wastewater treatment method and system |
| CN111285547A (en) * | 2020-03-06 | 2020-06-16 | 上海东振环保工程技术有限公司 | Method for treating waste liquid of developing solution |
| TWI721256B (en) * | 2017-03-15 | 2021-03-11 | 日商栗田工業股份有限公司 | Membrane water treatment medicine and membrane treatment method |
Families Citing this family (20)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP5444684B2 (en) * | 2008-10-21 | 2014-03-19 | 栗田工業株式会社 | Organic wastewater treatment method and treatment equipment |
| TWI385128B (en) * | 2008-12-19 | 2013-02-11 | Ind Tech Res Inst | Anaerobic non-woven membrane bioreactor and method for treating wastewater |
| JP5205316B2 (en) * | 2009-03-23 | 2013-06-05 | 株式会社神鋼環境ソリューション | Wastewater treatment method |
| TWI568687B (en) * | 2009-06-15 | 2017-02-01 | 沙烏地阿拉伯油品公司 | Suspended media membrane biological reactor system and process including suspension system and multiple biological reactor zones |
| 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 |
| CN104039713B (en) | 2012-01-11 | 2016-08-24 | 栗田工业株式会社 | reverse osmosis processing method |
| JP5986819B2 (en) * | 2012-06-18 | 2016-09-06 | 前澤工業株式会社 | Water treatment method and equipment |
| CN103693730B (en) * | 2013-11-28 | 2015-08-05 | 内蒙古工业大学 | A kind of device and method of supercritical water oxidation method process high concentration hard-degraded organic waste water |
| 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 |
| JP2016117018A (en) * | 2014-12-19 | 2016-06-30 | 三浦工業株式会社 | Recovery filtration unit |
| JP2016117017A (en) * | 2014-12-19 | 2016-06-30 | 三浦工業株式会社 | Recovery filtration unit |
| JP2016117016A (en) * | 2014-12-19 | 2016-06-30 | 三浦工業株式会社 | Recovery filtration unit |
| JP6318193B2 (en) * | 2016-05-18 | 2018-04-25 | 前澤工業株式会社 | Water treatment method and equipment |
| JP6934358B2 (en) * | 2017-08-18 | 2021-09-15 | 水ｉｎｇ株式会社 | Organic wastewater treatment equipment and treatment method |
| JP2019202260A (en) * | 2018-05-22 | 2019-11-28 | 積水化学工業株式会社 | Water treatment system and water treatment method |
| JP7119568B2 (en) * | 2018-05-23 | 2022-08-17 | 王子ホールディングス株式会社 | Water treatment device and water treatment method |
| CN109160674B (en) * | 2018-08-28 | 2022-01-11 | 苏州爱源环境工程技术服务有限公司 | Purification method of emulsion-containing wastewater |
| CN110015821A (en) * | 2019-05-24 | 2019-07-16 | 北京中水清源环境技术有限公司 | A kind of ectoenzyme flotation advanced treatment device |
Family Cites Families (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS54108461A (en) * | 1978-02-15 | 1979-08-25 | Mitsui Miike Mach Co Ltd | Method of denitrifying high concentration nitrogen contained waste water |
| JPH0729115B2 (en) * | 1990-03-23 | 1995-04-05 | 荏原インフイルコ株式会社 | Treatment method for human waste |
| JP3335500B2 (en) * | 1994-08-03 | 2002-10-15 | シャープ株式会社 | Wastewater treatment device and wastewater treatment method |
| TW387864B (en) * | 1996-10-09 | 2000-04-21 | Hoechst Ag | Biological waste water treatment at high sludge concentrations |
| JPH10202281A (en) * | 1997-01-28 | 1998-08-04 | Maezawa Ind Inc | Waste water treating device |
| JP3947588B2 (en) * | 1997-01-30 | 2007-07-25 | 前澤工業株式会社 | Wastewater treatment equipment |
| JPH10296287A (en) * | 1997-04-30 | 1998-11-10 | Shinko Pantec Co Ltd | Method and device for treating water containing organic matter |
| JP3258600B2 (en) * | 1997-06-30 | 2002-02-18 | 神鋼パンテツク株式会社 | Method and apparatus for treating organic-containing water |
| JP2002307088A (en) * | 2001-04-11 | 2002-10-22 | Hitachi Plant Eng & Constr Co Ltd | Wastewater treatment apparatus |
| JP4552482B2 (en) * | 2004-03-31 | 2010-09-29 | 栗田工業株式会社 | Organic wastewater treatment method |
| JP2006000828A (en) * | 2004-06-21 | 2006-01-05 | Japan Organo Co Ltd | Organic wastewater treatment method |
| JP4591678B2 (en) * | 2004-12-14 | 2010-12-01 | 栗田工業株式会社 | Biological treatment equipment |
| TWI300059B (en) * | 2004-12-20 | 2008-08-21 | Ind Tech Res Inst | Anaerobic biological wastewater treatment system and process |
| JP4997724B2 (en) * | 2005-08-02 | 2012-08-08 | 栗田工業株式会社 | Organic wastewater treatment method |
-
2007
- 2007-03-30 JP JP2007091666A patent/JP5223219B2/en active Active
-
2008
- 2008-03-27 CN CN2008100880415A patent/CN101274809B/en active Active
- 2008-03-27 TW TW097111014A patent/TWI494281B/en active
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102272052A (en) * | 2009-03-10 | 2011-12-07 | 株式会社日立制作所 | Water-treating method and water-treating member |
| CN102781850A (en) * | 2010-03-05 | 2012-11-14 | 栗田工业株式会社 | Water treatment method and process for producing ultrapure water |
| CN104981435A (en) * | 2013-02-13 | 2015-10-14 | 栗田工业株式会社 | Method for treating development wastewater from color filter production step |
| CN107530592A (en) * | 2015-05-19 | 2018-01-02 | 栗田工业株式会社 | Agglutinant and method for treating water |
| TWI721256B (en) * | 2017-03-15 | 2021-03-11 | 日商栗田工業股份有限公司 | Membrane water treatment medicine and membrane treatment method |
| CN111268863A (en) * | 2020-03-06 | 2020-06-12 | 上海东振环保工程技术有限公司 | Developing solution wastewater treatment method and system |
| CN111285547A (en) * | 2020-03-06 | 2020-06-16 | 上海东振环保工程技术有限公司 | Method for treating waste liquid of developing solution |
Also Published As
| Publication number | Publication date |
|---|---|
| JP5223219B2 (en) | 2013-06-26 |
| JP2008246386A (en) | 2008-10-16 |
| TWI494281B (en) | 2015-08-01 |
| TW200848375A (en) | 2008-12-16 |
| CN101274809B (en) | 2013-01-09 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101274809B (en) | Treatment apparatus for organic wastewater | |
| JP5315587B2 (en) | Apparatus and method for treating wastewater containing organic matter | |
| Mutamim et al. | Application of membrane bioreactor technology in treating high strength industrial wastewater: a performance review | |
| CN101830595B (en) | Method for treating leather-making industrial wastewater | |
| JP4862361B2 (en) | Waste water treatment apparatus and waste water treatment method | |
| US20070003370A1 (en) | A method for treating landfill leachate | |
| JP5017854B2 (en) | Apparatus and method for treating wastewater containing organic matter | |
| KR101967179B1 (en) | Membrane separation water treatment system with reverse osmosis membrane concentrated water treatment facility | |
| KR100784933B1 (en) | Apparatus for treating organic matter and nitrogen of high density organic wastewater | |
| CN101337752B (en) | Advanced treatment process for paper-making waste water | |
| Sanguanpak et al. | Membrane fouling and micro-pollutant removal of membrane bioreactor treating landfill leachate | |
| CN101723526A (en) | Film treatment method for wastewater produced by synthetic rubber | |
| KR20080078550A (en) | Method for biological processing of water containing organic material | |
| JP2007029826A (en) | Apparatus for treating waste water and method for treating waste water using the apparatus | |
| KR100957851B1 (en) | Method of water treatment | |
| KR20090008518A (en) | High efficient piggery wastewater treatment apparatus for treating piggery wastewater and method thereof | |
| JP4997724B2 (en) | Organic wastewater treatment method | |
| CN102510839A (en) | Biotreatment method for water containing organic substance | |
| KR102078434B1 (en) | Method and device for treating organic wastewater | |
| KR100825518B1 (en) | Device and method for Biological Treatment of Wastewater using MBR and Zeolite Powder | |
| KR101931346B1 (en) | Membrane separation water treatment system with reverse osmosis membrane concentrated water treatment facility | |
| KR0129831B1 (en) | A process for sewage treatment wsing denitrification and dephosphorization | |
| CN101979346A (en) | Comprehensive treatment method for high-concentration pesticide wastewater | |
| JPH0649197B2 (en) | Organic wastewater treatment method | |
| KR101877208B1 (en) | Membrane separation water treatment system with reverse osmosis membrane concentrated water treatment facility |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |