WO2007097269A1 - 廃水の処理方法 - Google Patents
廃水の処理方法 Download PDFInfo
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- WO2007097269A1 WO2007097269A1 PCT/JP2007/052924 JP2007052924W WO2007097269A1 WO 2007097269 A1 WO2007097269 A1 WO 2007097269A1 JP 2007052924 W JP2007052924 W JP 2007052924W WO 2007097269 A1 WO2007097269 A1 WO 2007097269A1
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- activated sludge
- wastewater
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/14—Ultrafiltration; Microfiltration
- B01D61/22—Controlling or regulating
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1268—Membrane bioreactor systems
- C02F3/1273—Submerged membrane bioreactors
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/24—Quality control
- B01D2311/246—Concentration control
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2315/00—Details relating to the membrane module operation
- B01D2315/06—Submerged-type; Immersion type
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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
-
- 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
- Y02W10/40—Valorisation of by-products of wastewater, sewage or sludge processing
Definitions
- the present invention relates to a method for treating organic wastewater by a membrane separation activated sludge method.
- a membrane separation activated sludge method in which a membrane cartridge is immersed in an activated sludge tank and solid-liquid separation is performed by filtration into activated sludge and a treatment liquid.
- This method can perform solid-liquid separation by increasing the activated sludge concentration (Mixed Liquor Suspended Solid, hereinafter referred to as MLSS) to 20000 mgZl. For this reason, there is an advantage that the volume of the activated sludge tank can be reduced or the reaction time in the activated sludge tank can be shortened.
- SS suspended solids
- the membrane separation activated sludge method has many advantages as described above and has been rapidly spread in recent years.
- a membrane or a hollow fiber membrane is used for the membrane force-tridge.
- the strength of the hollow fiber membrane itself is high, it can withstand long-term use with less damage to the membrane surface due to contact with contaminants mixed in with organic wastewater power.
- backwashing can be performed in which a medium such as filtered water is ejected in the direction opposite to the filtration direction to remove deposits on the membrane surface.
- the activated sludge and the bio-derived polymer produced by metabolism of microorganisms in the activated sludge adhere to the membrane surface, the effective membrane area is reduced and the filtration efficiency is lowered. For this reason, it is necessary to perform backwashing frequently, and there is a problem that stable filtration cannot be performed for a long time.
- Patent Document 1 discloses a method of performing aeration with hollow fiber membrane force—lower force of a bridge using air or the like. In this method, activated sludge aggregates adhering to the membrane surface and between the membranes and contaminants brought in from the raw water are peeled off by the vibration effect of the membrane and the stirring effect due to the upward movement of bubbles. Can prevent them from accumulating.
- a lower ring is installed in the lower part of the hollow fiber membrane cartridge, and a plurality of through holes are provided in the lower ring side adhesive fixing layer, and an air pocket is formed in the lower ring by aeration from the lower part of the force bridge. By doing so, bubbles are generated evenly from the plurality of through holes.
- Patent Document 2 measures the amount of biological polymer in a biological treatment tank (aeration tank) and reduces the amount of biological polymer in the biological treatment tank in a timely manner. And a method for preventing excessive polymer from adhering to the film surface is disclosed.
- the COD (chemical oxygen demand) value is obtained as the amount of biological polymer, and is substituted.
- the COD value includes the value of organic substances that can pass through the pores of the membrane. For this reason, the risk of membrane area reduction due to the attachment of biological polymer is overestimated than it actually is, and it involves the work of reducing biological polymer more than necessary, which may reduce the efficiency of wastewater treatment. there were.
- Patent Document 3 discloses a method for reducing a filterability-inhibiting component composed of a high-molecular organic compound present in a biological treatment tank.
- the filtration-inhibiting component is separated by a filter medium after adding a flocculant, or the filterability-inhibiting component is discarded by performing centrifuge separation. Therefore, it was a very time-consuming method.
- Patent Document 1 Japanese Unexamined Patent Publication No. 2000-157846
- Patent Document 2 JP 2005-40747
- Patent Document 3 Japanese Patent Application Laid-Open No. 2002-1333
- the present invention appropriately evaluates the risk of film area reduction due to adhesion of biological polymers.
- the purpose of the present invention is to provide a method for efficiently treating wastewater while preventing an increase in membrane filtration resistance.
- a substance that adheres to the outer surface of the membrane and inhibits filtration is a bio-derived polymer having a molecular weight of several hundreds of thousands and several millions, mainly composed of saccharides, especially uronic acid. I found out. It was also found that the biological polymer in the aqueous phase of activated sludge can be controlled by increasing or decreasing the amount of organic matter relative to the amount of activated sludge. That is, the wastewater treatment method according to the present invention is as follows.
- a wastewater treatment method characterized by maintaining the sugar concentration in the aqueous phase of the activated sludge within a set value for the separation step.
- the increase or decrease in the amount of organic matter relative to the amount of activated sludge is the amount of organic wastewater that flows into the activated sludge tank, or the amount of organic wastewater that flows into the activated sludge tank and the solid-liquid separation performed by the separation membrane device. 4. The wastewater treatment method according to 3 above, wherein the wastewater treatment method is carried out by increasing or decreasing the amount of liquid discharged outside the activated sludge tank.
- the sugar concentration setting value should be determined according to the filtration flux value of the separation membrane device. 3.
- the sugar concentration in the aqueous phase of the activated sludge is determined by filtering the activated sludge through a filter medium having a larger pore size than the separation membrane of the separation membrane device and measuring the sugar concentration in the obtained filtrate.
- the wastewater treatment method of the present invention by monitoring the sugar concentration and Z or uronic acid concentration in the activated sludge tank, the amount of biological polymer causing membrane clogging If the sugar concentration and Z or uronic acid concentration become high, the clogging of the separation membrane can be prevented by reducing the BOD SS load, and solid-liquid separation can be performed stably for a long time. . On the other hand, if the sugar concentration and Z or uronic acid concentration are much lower than the set value, the B OD-SS load can be increased until the sugar concentration and Z or uronic acid concentration rises close to the set value. This can increase the efficiency of wastewater treatment work.
- FIG. 1 is a block diagram showing an example of a system that performs the wastewater treatment method of the present invention.
- FIG. 2 Relationship between the sugar concentration in the filter paper filtrate of activated sludge and the membrane filtration resistance.
- FIG. 3 Relationship between COD difference in activated sludge and membrane filtration resistance.
- FIG. 4 Relationship between uronic acid concentration and sugar concentration in activated sludge filter paper filtrate.
- FIG.5 GPC sheet of activated sludge filter paper filtrate.
- FIG. 6 GPC chart after membrane filtration of activated sludge filter paper filtrate.
- FIG. 7 Relationship between BOD—SS load and sugar concentration in the aqueous phase of activated sludge.
- FIG. 8 is a graph showing changes over time in transmembrane pressure difference, sugar concentration and influent wastewater volume in Example 1.
- FIG. 9 is a graph showing changes over time in transmembrane pressure difference, sugar concentration, and influent wastewater volume in Example 2.
- the wastewater treatment method of the present invention includes an inflow step of flowing organic wastewater into an activated sludge tank containing activated sludge containing microorganisms, and a treatment liquid biologically treated in the activated sludge tank. It consists of a separation process in which the treatment liquid is separated into solid and liquid by a separation membrane device installed in the tank.
- the inflow process includes a pretreatment facility that removes organic wastewater power contaminants flowing into the activated sludge tank and a flow rate control tank that adjusts the flow rate of organic wastewater that flows into the activated sludge tank.
- the separation process includes an activated sludge tank for biologically treating wastewater, a membrane separation apparatus for solid-liquid separation of the treated liquid, and a suction pump for drawing out the filtrate.
- organic waste water from which large solids and the like are roughly removed is sent to the activated sludge tank while adjusting the flow rate to the activated sludge tank at a constant flow rate.
- organic matter (BOD component) in organic wastewater is decomposed by microorganisms in activated sludge.
- the size of the activated sludge tank and the residence time in the activated sludge tank of organic wastewater are determined according to the amount of organic wastewater discharged and the concentration of organic substances in the wastewater.
- the activated sludge concentration in the activated sludge tank can be set to about 5 to 15 gZL.
- the activated sludge and the organic wastewater in the activated sludge tank are separated into solid and liquid using a separation membrane device.
- the submerged separation membrane device installed in the activated sludge tank is composed of a separation membrane and a water collection section, and is further scoured. Is installed. Clogging is prevented by sending a blower force gas into the skirt to swing the membrane and applying a water flow to the membrane surface to give a shearing force.
- the water collecting part of the separation membrane device is connected to a suction pump, and a pressure gradient is generated on the inner and outer surfaces of the membrane by the suction pump to achieve solid-liquid separation.
- a known separation membrane such as a flat membrane or a hollow fiber membrane can be used for the membrane force-trid used in the separation membrane.
- the hollow fiber membrane is preferable in that it can withstand long-term use with less damage to the membrane surface and contact force with contaminants in organic wastewater, where the strength of the membrane itself is high.
- the filtration membrane can also be backwashed by removing deposits on the membrane surface by ejecting filtered water or the like in the direction opposite to the filtration direction.
- the separation membrane device may be installed by being connected to an activated sludge tank that is simply immersed in the activated sludge tank.
- This method can be applied to the case where the separation membrane device that is connected only by the submerged membrane separation activated sludge method is provided in a separate tank from the activated sludge vessel, or in the case of a pressure type separation membrane device.
- the activated sludge is circulated between the activated sludge tank and the separation membrane device, and the concentrated liquid is returned to the activated sludge tank.
- a plurality of separation membranes may be used as necessary. By using multiple systems, it is possible to perform separation work for each line of separation membranes or to stop the separation work, so that the wastewater treatment speed can be adjusted.
- the organic waste water 1 flowing into the activated sludge tank 1 is temporarily stored in the flow rate adjusting tank 3 after the impurities are removed by the pretreatment facility 2, and is discharged from the flow rate adjusting tank 3 at a constant flow rate. Supplied to activated sludge tank (aeration tank) 4.
- the organic matter (BOD component) in the organic wastewater 1 is decomposed and removed by microorganisms in the activated sludge put in the tank.
- Solid-liquid separation of the activated sludge mixture in the activated sludge tank 4 is performed by the separation membrane device 5 submerged in the tank.
- a scut 6 and a blower 7 are installed in the lower part of the separation membrane device 5, and a blower gas is sent into this scat.
- the filtrate 9 treated by the separation membrane device 5 is sucked by the suction pump 8, disinfected in the sterilization tank 10 as necessary, and discharged as treated water 11.
- microorganisms decompose BOD components and release metabolites outside the body.
- the metabolite of this microorganism Biological polymers based on a certain sugar or protein can be used in the presence of excessive amounts of organic substances, especially in the case of an activated sludge tank, or when the concentration of organic substances in the inflowing water varies greatly.
- organic liquid flows into the activated sludge tank the biological polymer is remarkably discharged from the body and promotes clogging of the separation membrane.
- the risk of clogging the separation membrane by the biological polymer is appropriately evaluated by measuring the sugar concentration, preferably the uronic acid concentration in the aqueous phase of the activated sludge contained in the activated sludge tank 4. This is possible.
- Waste water that can be effectively treated by the method of the present invention includes food factory waste water, sugar factory waste water, detergent factory waste water, starch factory waste water, tofu factory waste water, etc., and BO D is lOOmgZL or more. It is more effective when it is some wastewater.
- the upper limit of the set value of the sugar concentration must be 100 mg / L or less. If this value is exceeded, clogging of the bio-derived polymer and activated sludge into the separation membrane will become significant, and the filtration pressure will increase.
- it is 80 mgZL or less, more preferably 50 mgZL or less, and most preferably about 30 mgZL.
- the lower the sugar concentration is, the more preferable it is because clogging of the membrane is less likely to occur, but the wastewater treatment capacity decreases accordingly.
- the lower limit of the sugar concentration should be 5 mgZL, preferably about 20 mgZL, more preferably lOmgZL.
- the uronic acid concentration within the set value instead of the sugar concentration in that the clogging risk of the membrane can be grasped more accurately.
- the sugar concentration when used as an indicator of clogging substances, it can be derived from organic wastewater in addition to sugar, which is a biological polymer. Since sugar is also measured, the amount of clogged substances may be overestimated. In such cases, clogging can be more accurately evaluated by measuring the uronic acid concentration.
- a more preferable upper limit of the uronic acid concentration is 50 mgZL or less, more preferably 30 mgZL or less, still more preferably 20 mgZL or less, and most preferably lOmgZL.
- the preferable lower limit of the uronic acid concentration is 3 mg ZL or more, more preferably 5 mg ZL or more.
- each concentration is preferably determined according to the filtration flux.
- the filtration flux is generally 0.1 to 1. OmZD, and 0.4 to 0.8 mZD is preferable from the viewpoint of efficient wastewater treatment. In this case, the following range is most preferable as a standard of sugar concentration.
- Separation membrane device filtration Flux is 0.4mZD, 50mgZL or less
- the filtration flux of 0.6 mZD means an operation in which a filtrate of 0.6 m 3 is passed in 24 hours per filtration area of lm 2 .
- the method for measuring the sugar concentration is not particularly limited, and examples thereof include a method in which the sugar concentration is measured by a phenol sulfuric acid method and is determined by a calibration curve prepared in dalcose.
- the activated sludge is filtered through a filter medium having a pore size larger than that of the separation membrane of the separation membrane device to obtain a sludge filtrate. It is preferable to do. By this operation, only the suspended matter in the activated sludge is captured by the filter medium, and the sugar component passes through the filter paper. Therefore, by measuring the sugar concentration and Z or uronic acid concentration in the filtrate, the concentration of the bio-derived polymer that becomes the clogging substance of the membrane can be measured more accurately.
- the pore diameter of the filter medium is preferably 5 times or more, more preferably 10 times or more the separation membrane pore diameter provided in the separation membrane device.
- the upper limit of the pore size of the filter medium is preferably 10 m, and the upper limit of the pore size of the filter medium is more preferably about 100 times or less.
- a hydrophilic material is preferred because it has less sugar component adsorption.
- a filter medium for example, a filter paper made of a cell mouthpiece can be used.
- the concentration of uronic acid was determined according to the method described in NELLY BLUMENKRANTZ, GUSTAV ASBOE—HAN SJSISI “New Method for Quantitative Determination It can be measured with a calibration curve prepared using one polygalataturonic acid, specifically according to the following procedure. 1) Take 0.5 mL of sludge filtrate and polygalataturonic acid aqueous solution of known concentration into a test tube, and add 3. OmL of 0.0125 M Na BO concentrated sulfuric acid solution to each.
- Changes in sugar concentration and Z or uronic acid concentration over time can be determined by periodically measuring sugar concentration and Z or uronic acid concentration, for example, once every few hours to several days. Monkey.
- Periodic sugar concentration and Z or uronic acid concentration measurements show that the sugar concentration and Z or uronic acid concentration, that is, the concentration of the biological polymer, has increased, and prevent the membrane from becoming clogged. Can hit. It is most preferable to monitor sugar concentration and Z or uronic acid concentration at all times and adjust within the specified range.
- the inventors have found that the BOD-SS load is deeply related to the sugar concentration and Z or uronic acid concentration in the aqueous phase of activated sludge.
- the high BOD—SS load is a situation where there are more organic materials that are good relative to the amount of microorganisms. In such a situation, microorganisms will actively metabolize and will excrete biological polymers, ie sugars, that become clogging substances. Conversely, if the microbe is placed in a starvation state, the metabolic activity is reduced and the biological polymer is not discharged. In addition, the sugar concentration is lower because microorganisms are thought to consume sugar.
- the amount of organic matter in the activated sludge tank may be increased or decreased.
- Specific methods include the following methods. For example, (1) a method of increasing or decreasing the amount of organic wastewater flowing into the activated sludge tank, (2) the amount of organic wastewater flowing into the activated sludge tank, and the amount of the filtrate separated into solid and liquid by the separation membrane device (3) Filtration Flux increase / decrease method, etc.
- the method for increasing or decreasing the amount of organic substances is not limited to the above-described method, and the following method is also conceivable.
- a method of removing organic matter from organic wastewater by separating solid organic matter using a filter medium a method of increasing activated sludge concentration by reducing the amount of excess sludge extraction, that is, controlling the amount of excess sludge extraction To increase or decrease the activated sludge concentration; to reduce the activated sludge tank liquid level and reduce the amount of activated sludge present there, i.e. to control the activated sludge tank liquid level
- Possible methods include controlling volume and increasing / decreasing the amount of activated sludge; adding water to the activated sludge tank.
- the method of increasing or decreasing the amount of organic wastewater flowing into the activated sludge tank is the simplest and preferable. Specifically, sugar concentration and Z or uronic acid concentration can be lowered by reducing the amount of organic wastewater flowing into the activated sludge tank. On the other hand, when the sugar concentration and Z or uronic acid concentration are lower than the set values, the sugar concentration and Z or uronic acid concentration can be increased by increasing the amount of organic wastewater flowing into the activated sludge tank. . By doing this, it is possible to increase the efficiency of wastewater treatment while preventing clogging of the separation membrane.
- Increase / decrease amount of organic wastewater flowing into the activated sludge tank and increase / decrease amount of BOD-SS load must be determined for each organic wastewater to be treated. For example, when the amount of organic wastewater flowing into the activated sludge tank is reduced by half, that is, when the BOD-SS load is reduced by half, how much the sugar concentration and Z or uronic acid concentration change. To understand trends. Based on the trends obtained, decide how much to increase or decrease the amount of organic wastewater
- the specific increase / decrease amount of organic wastewater depends on the size of the activated sludge tank and the type of activated sludge. Therefore, when the strength of case-by-case, for example, sugar concentration and z or uronic acid concentration increases, as a guideline, if the BOD—SS load is reduced to 0.02 kg—BODZ (kg'day), the sugar concentration and Z or uronic acid The concentration can be lowered to about half of the original concentration in about one week.
- the polymers of biological origin such as saccharides, proteins and nucleic acids as described above
- it is a polymer mainly composed of saccharides, particularly uronic acid, which causes clogging by adhering to the surface of the separation membrane. . Therefore, by maintaining the sugar concentration and Z or uronic acid concentration within the set values as in the present invention, it is possible to prevent the biological filtration polymer from adhering to the membrane surface and increasing the membrane filtration resistance. The separation membrane will eventually become clogged and need to be washed, but if the method of the present invention is used, the frequency can be minimized.
- the activated sludge containing organic wastewater is filtered with a filter paper (Advantech, manufactured by Cell Kose, 5C (trade name)) having a pore size of 1 ⁇ m, and the resulting filtrate (hereinafter referred to as sludge filter). Called liquid).
- the effective membrane length was 15 cm, the inner diameter was Z, and the outer diameter was 0.6 / 1.2 mm).
- the filtration resistance Rc has a relationship represented by the following formula (I).
- n is the number of filtration cycles
- Pn is the mean value of the transmembrane pressure difference at the nth cycle [Pa]
- ⁇ is the viscosity of water [Pa's]
- J is Flux [mZD].
- the sugar concentration in the filtrate was measured by the phenol sulfuric acid method. To create a calibration curve, the concentration was determined using dalcose. As a result, as shown in FIG. 2, it was found that the calculated filtration resistance value and the sugar concentration in the filtrate were in a proportional relationship.
- the uronic acid concentration was determined by the following procedure according to the method of “New Method for Quantitative Determination of Uronic Acid J ANALYTICAL BIOCHEMISTRY 54, 484-489 Mitsugu (published in 1973)”. Specifically, the procedure was as follows.
- Fig. 5 and Fig. 6 respectively.
- the horizontal axes in Fig. 5 and Fig. 6 are obtained by subjecting various PVAs with known molecular weights to high-speed chromatography to determine the relationship between the output retention time and the molecular weight, and using this relationship, the retention time represented on the horizontal axis. Is described in terms of molecular weight. As shown in the figure, the height of the peak in the part where the molecular weight is in the hundreds of thousands to millions in FIG. 5 has become smaller in FIG. 6, and the substance having this molecular weight is reduced by membrane filtration. That was a powerful thing.
- the membrane clogging substance in the membrane separation activated sludge method is mainly composed of sugar. It can be estimated that the polymer has a molecular weight of hundreds of thousands of power and several million of uronic acid.
- the filtration resistance was measured using a solution obtained by dissolving polygalacturonic acid in sludge filtrate at four concentrations of 40 mgZL, 60 mg / L, 80 mg / L, and lOOmg ZL.
- the solution obtained by dissolving polygalataturonic acid was larger than the inclination of the activated sludge filter paper filtrate. That is, it was found that the liquid containing a large amount of uronic acid among sugars has a higher filtration resistance.
- Patent Document 2 the activated sludge is filtered with the same filter paper as above, and the obtained COD of the filtrate and the filtrate are further mixed with the above hollow fiber membrane.
- the difference from the COD of the filtrate filtered using was obtained as the COD difference value and plotted in FIG. Since COD difference values include values based on components that can pass through the membrane, it was found that using the COD difference value in the filtration resistance value had a larger error than the sugar concentration.
- Fig. 7 shows the obtained results.
- the sugar concentration and uronic acid concentration were also high.
- the sugar concentration and uronic acid concentration were low.
- wastewater from a sugar factory with a BOD of 750 mgZL was treated by the membrane separation activated sludge method in continuous operation.
- the sugar and uronic acid concentrations in the wastewater were 60 mgZL and OmgZL, respectively.
- the separation membrane device 5 a separation membrane device in which a microfiltration hollow fiber membrane having a pore diameter of 0.1 ⁇ m is modularized (manufactured by Asahi Kasei Chemicals Co., Ltd., PVDF, membrane area 0.015 m 2 , effective membrane length) 15 cm, inner diameter Z outer diameter: 0.6 / 1.2 mm) was immersed in an activated sludge tank 4 having an effective volume of 10 L.
- the MLSS concentration in the activated sludge tank was constant at lOgZL, and the residence time of wastewater in the activated sludge tank 4 was 18 hours.
- the filtration pressure at the start of the treatment was 4 kPa.
- the liquid volume of activated sludge is always constant, the separation membrane device 5 is divided into two lines with the same membrane area, and the filtration flux is set to 0.6m ZD, and the entire amount of filtrate is discharged out of the activated sludge tank 4. .
- the sugar concentration in the aqueous phase of activated sludge tank 4 was set so that the upper limit was 50 mgZL and the lower limit was 20 mgZL.
- the upper limit of uronic acid concentration was 18 mgZL and the lower limit was 5 mgZL.
- air was sent from the bottom of the membrane module at a flow rate of 200LZh.
- the sugar concentration was determined by measuring the sludge obtained by filtering activated sludge with a filter paper (pore size 1 ⁇ m; manufactured by Advantech Co., Ltd., Cell mouth-seed 5 C) by the phenol sulfuric acid method, and was prepared with darcos. Obtained from a calibration curve.
- the uronic acid concentration was determined by a calibration curve of polygalataturonic acid in the same procedure as described above.
- Figure 8 shows the results of measuring the sugar concentration and uronic acid concentration in the aqueous phase of activated sludge once a day.
- the sugar concentration and uronic acid concentration in the aqueous phase of activated sludge rapidly increased, and on day 11 the sugar concentration and uronic acid concentration were 50 mgZL and 20 mgZL, respectively. It was. Therefore, the amount of filtrate discharged to the outside of the activated sludge tank and the amount of wastewater flowing into the activated sludge tank were reduced by half by stopping one line of the separation membrane device 5, and the sugar concentration and uronic acid were reduced. Concentrations could be reduced to 20 mgZL and 5 mgZL, respectively.
- Example 1 The same wastewater as in Example 1 was treated using the same system as in Example 1. After 20 days from the start of treatment, the sugar concentration reached 80 mgZL and the uronic acid concentration reached 35 mgZL, but the treatment continued. As a result, the filtration pressure exceeded 25 kPa, and it was necessary to clean the separation membrane.
- Separation membrane device 5 is a separation membrane device with a 0.1 ⁇ m pore diameter filtered hollow fiber membrane (Asahi Kasei Chemicals, PVDF, membrane area 0.015 m 2 , effective membrane length 15 cm, inner diameter Z outer diameter: 0.6 / 1.2mm) was immersed in an activated sludge tank with an effective volume of 10L.
- the MLSS concentration was constant at lOgZL, and the residence time of wastewater in the activated sludge tank 4 was 18 hours.
- the filtration pressure at the start of the treatment was 4 kPa.
- the liquid volume of activated sludge was always constant, a series of separation membrane equipment was installed, the filtration flux was set at 0.6 m / D, and the entire amount of filtrate was discharged out of the activated sludge tank 4.
- the sugar concentration in the aqueous phase of activated sludge tank 4 was set so that the upper limit was 70 mgZL and the lower limit was lOmgZL.
- the upper limit of uronic acid concentration was 20 mgZL and the lower limit was 5 mgZL.
- air was sent from the bottom of the membrane module at a flow rate of 200 LZh.
- the sugar concentration was measured by the phenol-sulfuric acid method after the activated sludge was filtered with filter paper (pore size 1 ⁇ m; Advantech, Cellulose, 5C). It was obtained from a calibration curve made with a glass. The uronic acid concentration was also determined by a calibration curve for polygalataturonic acid using the same procedure as above.
- Fig. 9 shows the results of measuring sugar concentration and uronic acid concentration in the aqueous phase of activated sludge once a day. Even after about one week from the start of operation, the sugar concentration and uronic acid concentration in the aqueous phase of the activated sludge were about 5 mgZL and 2 mgZL, respectively, far below the set values. Therefore, on the eighth day from the start of operation, the membrane area of the separation membrane unit was doubled and the amount of wastewater flowing into the activated sludge tank was doubled. Subsequently, the sugar concentration and uronic acid concentration did not increase beyond 20 mgZL and 7 mgZL, respectively. In this way, even if the inflow wastewater volume was doubled, the transmembrane pressure difference could be stably operated without increasing rapidly. (Example 3)
- the wastewater from the starch plant with a BOD of 750 mgZL was treated by the membrane separation activated sludge method in continuous operation.
- the sugar and uronic acid concentrations in the wastewater were 800 mgZL and OmgZL, respectively.
- the sugar concentration in this wastewater was about 800 mgZL.
- the same separation membrane apparatus as in Example 2 was immersed as a separation membrane.
- the MLSS concentration was constant at 10 gZ L, and the residence time of sugar factory wastewater in the activated sludge tank was 18 hours.
- the amount of activated sludge was always constant, a series of separation membrane equipment was installed, the filtration flux was set to 0.6 mZD, and the entire amount of filtrate was discharged out of the activated sludge tank 4.
- air was fed from the bottom of the membrane module at a flow rate of 200 LZh.
- the sugar concentration was obtained by measuring a solution obtained by filtering activated sludge with a filter paper (pore size: 1 ⁇ m; manufactured by Advantech 5C) by the phenol sulfuric acid method, and using a calibration curve prepared by DARCOSE.
- the uronic acid concentration was determined by a calibration curve of polygalataturonic acid in the same procedure as described above.
- the initial filtration pressure was 5 kPa.
- the sugar concentration was 80 mgZL in terms of dalcose, and the concentration of potent uronic acid was measured to be 17 mg ZL in terms of polygalataturonic acid.
- the transmembrane pressure did not increase, and it was 13 kPa on the 25th day of operation compared to lOkPa in the initial stage. It was found that clogging can be predicted more accurately by measuring the uronic acid concentration in this way.
- Example 2 The same wastewater treated in Example 1 was treated in the same manner as in Example 1.
- a separation membrane device 5 a separation membrane device with a pore size of 0 .: L m microfiltration hollow fiber membrane (Made by Asahi Kasei Chemicals, PVDF, membrane area 0.022 m 2 , effective membrane length) 15 cm, inner diameter Z outer diameter: 0.6 / 1.2 mm) was used.
- Separation membrane device filtration Flux is 0.6mZD, 20mgZL or less
- the present invention appropriately evaluates the risk that the effective membrane area decreases due to the adhesion of biological polymers to the membrane surface, and provides a method for efficiently treating wastewater while preventing an increase in membrane filtration resistance. To do. Therefore, it can be used effectively for the regeneration treatment of various factory wastewater.
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- Engineering & Computer Science (AREA)
- Water Supply & Treatment (AREA)
- Life Sciences & Earth Sciences (AREA)
- Chemical & Material Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Organic Chemistry (AREA)
- Biodiversity & Conservation Biology (AREA)
- Microbiology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Activated Sludge Processes (AREA)
Abstract
Description
Claims
Priority Applications (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AU2007218762A AU2007218762C1 (en) | 2006-02-23 | 2007-02-19 | Method of treating wastewater |
CA 2643269 CA2643269C (en) | 2006-02-23 | 2007-02-19 | Method of treating wastewater |
EP07714450A EP1988060A4 (en) | 2006-02-23 | 2007-02-19 | METHOD FOR TREATING WASTEWATER |
CN2007800065038A CN101389572B (zh) | 2006-02-23 | 2007-02-19 | 废水的处理方法 |
US12/280,193 US20100282671A1 (en) | 2006-02-23 | 2007-02-19 | Method of treating wastewater |
JP2008501696A JP5399065B2 (ja) | 2006-02-23 | 2007-02-19 | 廃水の処理方法 |
Applications Claiming Priority (2)
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JP2006-047293 | 2006-02-23 | ||
JP2006047293 | 2006-02-23 |
Publications (1)
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WO2007097269A1 true WO2007097269A1 (ja) | 2007-08-30 |
Family
ID=38437309
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
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PCT/JP2007/052924 WO2007097269A1 (ja) | 2006-02-23 | 2007-02-19 | 廃水の処理方法 |
Country Status (11)
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US (1) | US20100282671A1 (ja) |
EP (1) | EP1988060A4 (ja) |
JP (1) | JP5399065B2 (ja) |
KR (1) | KR101030480B1 (ja) |
CN (1) | CN101389572B (ja) |
AU (1) | AU2007218762C1 (ja) |
CA (1) | CA2643269C (ja) |
MY (1) | MY147057A (ja) |
RU (1) | RU2394778C2 (ja) |
TW (1) | TW200800812A (ja) |
WO (1) | WO2007097269A1 (ja) |
Cited By (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2011043232A1 (ja) * | 2009-10-05 | 2011-04-14 | 旭化成ケミカルズ株式会社 | 膜分離活性汚泥法に用いる添加剤 |
JP2012200631A (ja) * | 2011-03-24 | 2012-10-22 | Kubota Corp | 分離膜のファウリングの評価方法及び膜分離設備の運転方法 |
JP2012250180A (ja) * | 2011-06-03 | 2012-12-20 | Sumitomo Electric Ind Ltd | 濾過膜の目詰まり速度の予測方法、及び濾過システム |
JP2013022548A (ja) * | 2011-07-25 | 2013-02-04 | Kubota Corp | 膜分離活性汚泥処理装置の立上げ方法 |
JP2013022549A (ja) * | 2011-07-25 | 2013-02-04 | Kubota Corp | 膜分離活性汚泥処理装置の運転方法 |
JP2017056430A (ja) * | 2015-09-18 | 2017-03-23 | 国立研究開発法人産業技術総合研究所 | 膜分離型活性汚泥装置に使用される分離膜の目詰まりを予測する方法 |
Families Citing this family (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN110117125A (zh) * | 2018-12-18 | 2019-08-13 | 贵州省材料产业技术研究院 | 机油废水高效处理装置及方法 |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH10286567A (ja) * | 1997-04-16 | 1998-10-27 | Nkk Corp | 膜分離方法 |
JP2001276823A (ja) * | 2000-03-30 | 2001-10-09 | Sumitomo Heavy Ind Ltd | 膜分離方法及び装置 |
JP2006055766A (ja) * | 2004-08-20 | 2006-03-02 | Mitsubishi Rayon Co Ltd | 有機性排水の処理方法 |
JP2006212470A (ja) * | 2005-02-01 | 2006-08-17 | Toray Ind Inc | 溶解性有機物含有液の処理方法および処理装置 |
Family Cites Families (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4867883A (en) * | 1987-04-21 | 1989-09-19 | Hampton Roads Sanitation District Of The Commonwealth Of Virginia | High-rate biological waste water treatment process using activated sludge recycle |
US5338452A (en) * | 1993-01-14 | 1994-08-16 | The Lemna Corporation | High rate anaerobic reactor for primary treatment of high strength wastewater |
JPH0929280A (ja) * | 1995-07-20 | 1997-02-04 | Toyo Bio Reactor Kk | 廃水の処理方法 |
JP3608690B2 (ja) * | 1996-07-23 | 2005-01-12 | 株式会社荏原製作所 | 有機性排水の処理法及び装置 |
JPH10151494A (ja) * | 1996-11-25 | 1998-06-09 | Maezawa Ind Inc | 排水処理装置の運転方法 |
CN1103324C (zh) * | 1999-07-02 | 2003-03-19 | 中国科学院沈阳应用生态研究所 | 一种污水处理方法 |
JP2004268023A (ja) * | 2003-02-21 | 2004-09-30 | Toray Ind Inc | 溶解性有機物含有液の処理方法および処理装置 |
JP4046661B2 (ja) * | 2003-07-25 | 2008-02-13 | 株式会社クボタ | 汚水の処理方法 |
JP2005329397A (ja) * | 2004-04-23 | 2005-12-02 | Mitsubishi Rayon Co Ltd | 分離方法および分離装置 |
JP5172082B2 (ja) * | 2005-09-15 | 2013-03-27 | 三菱レイヨン株式会社 | 被処理水の処理方法 |
-
2007
- 2007-02-16 TW TW96106333A patent/TW200800812A/zh not_active IP Right Cessation
- 2007-02-19 JP JP2008501696A patent/JP5399065B2/ja not_active Expired - Fee Related
- 2007-02-19 US US12/280,193 patent/US20100282671A1/en not_active Abandoned
- 2007-02-19 CN CN2007800065038A patent/CN101389572B/zh not_active Expired - Fee Related
- 2007-02-19 KR KR20087019374A patent/KR101030480B1/ko not_active IP Right Cessation
- 2007-02-19 EP EP07714450A patent/EP1988060A4/en not_active Withdrawn
- 2007-02-19 MY MYPI20083210 patent/MY147057A/en unknown
- 2007-02-19 RU RU2008137783A patent/RU2394778C2/ru not_active IP Right Cessation
- 2007-02-19 AU AU2007218762A patent/AU2007218762C1/en not_active Ceased
- 2007-02-19 CA CA 2643269 patent/CA2643269C/en not_active Expired - Fee Related
- 2007-02-19 WO PCT/JP2007/052924 patent/WO2007097269A1/ja active Application Filing
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH10286567A (ja) * | 1997-04-16 | 1998-10-27 | Nkk Corp | 膜分離方法 |
JP2001276823A (ja) * | 2000-03-30 | 2001-10-09 | Sumitomo Heavy Ind Ltd | 膜分離方法及び装置 |
JP2006055766A (ja) * | 2004-08-20 | 2006-03-02 | Mitsubishi Rayon Co Ltd | 有機性排水の処理方法 |
JP2006212470A (ja) * | 2005-02-01 | 2006-08-17 | Toray Ind Inc | 溶解性有機物含有液の処理方法および処理装置 |
Non-Patent Citations (1)
Title |
---|
See also references of EP1988060A4 * |
Cited By (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2011043232A1 (ja) * | 2009-10-05 | 2011-04-14 | 旭化成ケミカルズ株式会社 | 膜分離活性汚泥法に用いる添加剤 |
AU2010304445B2 (en) * | 2009-10-05 | 2013-11-07 | Asahi Kasei Chemicals Corporation | Additive used in a membrane-separation activated sludge process |
JP5788327B2 (ja) * | 2009-10-05 | 2015-09-30 | 旭化成ケミカルズ株式会社 | 膜分離活性汚泥法に用いる添加剤 |
JP2012200631A (ja) * | 2011-03-24 | 2012-10-22 | Kubota Corp | 分離膜のファウリングの評価方法及び膜分離設備の運転方法 |
JP2012250180A (ja) * | 2011-06-03 | 2012-12-20 | Sumitomo Electric Ind Ltd | 濾過膜の目詰まり速度の予測方法、及び濾過システム |
JP2013022548A (ja) * | 2011-07-25 | 2013-02-04 | Kubota Corp | 膜分離活性汚泥処理装置の立上げ方法 |
JP2013022549A (ja) * | 2011-07-25 | 2013-02-04 | Kubota Corp | 膜分離活性汚泥処理装置の運転方法 |
JP2017056430A (ja) * | 2015-09-18 | 2017-03-23 | 国立研究開発法人産業技術総合研究所 | 膜分離型活性汚泥装置に使用される分離膜の目詰まりを予測する方法 |
Also Published As
Publication number | Publication date |
---|---|
EP1988060A4 (en) | 2011-01-19 |
AU2007218762A1 (en) | 2007-08-30 |
KR101030480B1 (ko) | 2011-04-25 |
CN101389572B (zh) | 2011-04-13 |
US20100282671A1 (en) | 2010-11-11 |
AU2007218762B2 (en) | 2010-04-08 |
EP1988060A1 (en) | 2008-11-05 |
RU2394778C2 (ru) | 2010-07-20 |
JP5399065B2 (ja) | 2014-01-29 |
JPWO2007097269A1 (ja) | 2009-07-16 |
TW200800812A (en) | 2008-01-01 |
CA2643269A1 (en) | 2007-08-30 |
CN101389572A (zh) | 2009-03-18 |
TWI349652B (ja) | 2011-10-01 |
CA2643269C (en) | 2013-06-04 |
MY147057A (en) | 2012-10-15 |
AU2007218762C1 (en) | 2010-09-23 |
KR20080089472A (ko) | 2008-10-06 |
RU2008137783A (ru) | 2010-03-27 |
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