WO2015156242A1 - 膜を用いた水処理方法および水処理装置 - Google Patents
膜を用いた水処理方法および水処理装置 Download PDFInfo
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- WO2015156242A1 WO2015156242A1 PCT/JP2015/060710 JP2015060710W WO2015156242A1 WO 2015156242 A1 WO2015156242 A1 WO 2015156242A1 JP 2015060710 W JP2015060710 W JP 2015060710W WO 2015156242 A1 WO2015156242 A1 WO 2015156242A1
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- ozone
- water
- membrane
- ozone gas
- membrane filtration
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Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
- B01D65/02—Membrane cleaning or sterilisation ; Membrane regeneration
-
- 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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
- B01D2321/04—Backflushing
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
- B01D2321/16—Use of chemical agents
- B01D2321/162—Use of acids
-
- 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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/03—Pressure
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/14—Maintenance of water treatment installations
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/16—Regeneration of sorbents, filters
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/20—Prevention of biofouling
-
- 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
Definitions
- the present invention relates to a water treatment method and a water treatment apparatus using a membrane for membrane treatment of water, industrial water, sewage, sewage secondary treated water, industrial wastewater, seawater, manure, etc. It is related to cleaning.
- the membrane When water is subjected to membrane filtration to remove foreign matters in the water, the membrane is clogged and the filtration pressure increases and the amount of filtered water decreases when the water is continuously treated.
- the foreign substance is a general term for all substances separated from the membrane filtration treated water by the membrane filtration treatment at the time of the membrane filtration treatment, for example, sludge that is a lump of microorganisms (hereinafter the same), SS (Suspended) in the treated water.
- An abbreviation for Solid which is a floating solid substance, and the like below.
- the amount of filtered water per unit time and per unit membrane filtration area is hereinafter referred to as “flux”.
- the cause of clogging of the membrane is foreign matter in the water, microorganisms attached to the membrane surface or in the membrane, or metabolites of the microorganisms. In order to secure 0.2 to 5.0 m 3 / day, it is necessary to periodically remove the films by washing them.
- the membrane is blown out from the direction opposite to the filtration direction of the membrane (the flow direction of the treated water when the treated water is filtered) by ejecting clear water such as membrane filtered water or tap water.
- a back-washing process for washing is performed. That is, during the membrane filtration treatment, water flows from the primary side to the secondary side of the membrane and the filtration treatment is performed. In the backwashing step, clear water is allowed to flow from the secondary side to the primary side to remove dirt on the membrane.
- clear water refers to tap water, membrane filtered water, well water, treated water from a wastewater / sewage treatment plant, and water having turbidity of less than 1 or SS of less than 1 mg / L (the same applies hereinafter).
- the primary side is a region where untreated water exists
- the secondary side is a region where filtered water (in the present invention, filtered water means water after being filtered). That is, the side to be filtered is the primary side and the filtration side is the secondary side across the membrane.
- filtered water filtered water
- clear water such as tap water
- the fouling substance is a metabolic product of microorganisms, and includes, for example, polysaccharides and proteins (the same applies hereinafter).
- membrane is wash
- the ozone gas is entrained, the ozone gas accumulates in the pipe and the inside of the film cannot be cleaned uniformly.
- ozone water that can clean the inside of the membrane is a part of the cleaning water that can pass through the membrane, and most of the ozone water moves to the gas-liquid separation tank.
- the fouling material on the membrane surface is, for example, a high molecular organic substance of a microbial metabolite. Yes, it cannot be removed only by the propulsive force of the bubbles. That is, the macromolecular organic matter of the microbial metabolite cannot be removed by the force of the flow of water caused by the bubbles contacting the macromolecular organic matter or the movement of the bubbles. Furthermore, the microorganisms attached to the membrane surface through this microbial metabolite cannot be removed (see Patent Documents 1 and 2).
- the membrane surface (primary side) is bubble-cleaned with ozone gas, but ozone gas that has not been dissolved is used among ozone gas injected with backwash water. Therefore, the ozone gas concentration is low and the bubble diameter is as large as several millimeters to several centimeters, so that the cleaning effect on the film surface (primary side) is insufficient (see Patent Document 3).
- the membrane means a sheet-like one having fine pores having a pore diameter of 0.001 to 0.5 ⁇ m, or a hollow fiber-like one, and the membrane is combined with a pipe or the like so that water can be filtered.
- a thing is called a membrane module, and a combination of several membrane modules is called a membrane unit.
- the transmembrane pressure difference refers to the difference between the pressure on the secondary side of the membrane during the membrane filtration treatment and the atmospheric pressure. Unless otherwise specified, in the present invention, the transmembrane pressure difference is expressed as an absolute value. Furthermore, when backwashing is repeated, fouling substances that cannot be removed in the membrane and on the membrane surface accumulate, and it becomes impossible to obtain a flux value, for example, 0.2 to 5.0 m 3 / day when designing a membrane filtration facility. It is necessary to replace the membrane if the chemical solution cleaning is carried out or if the transmembrane pressure does not recover.
- the present invention has been made to solve the above-mentioned problems.
- An object of the present invention is to provide a film cleaning method and a film cleaning apparatus that can be removed.
- the water treatment method using the membrane according to the present invention is: Pressurize the clear water that has been filtered through the membrane into wash water, Injecting ozone gas into this cleaning water to generate ozone cleaning water, From the filtration secondary side that is the outlet side of the filtrate during membrane filtration, supplying the ozone cleaning water to the membrane for membrane filtration, washing the inside of the membrane, Bubbles containing ozone are generated on the primary filtration side that is the inlet side of the untreated water during membrane filtration, and the surface of the membrane on the primary filtration side is washed.
- the water treatment apparatus using the membrane according to the present invention is: A membrane filtration separation device for separating foreign matter contained in untreated water that has not been subjected to membrane filtration and filtered water after membrane filtration; A switching valve that switches between normal membrane filtration and backwashing, which is the reverse of normal membrane filtration; Ozone connected to a pipe for supplying the ozone cleaning water to the membrane filtration separator by generating ozone cleaning water in which ozone gas is dissolved in the cleaning water by pressurizing the clear water subjected to the membrane filtration treatment.
- a dissolving part A cleaning water supply pump connected to the ozone dissolving part via a pipe and supplying the cleaning water, An ozone generator for supplying the ozone gas to the ozone dissolving part; With By switching the switching valve from the normal membrane filtration direction, the ozone cleaning water is supplied to the membrane filtration membrane by back washing to wash the membrane.
- the ozone gas is injected into the wash water, which is a clear water under pressure, and ozone is dissolved in the wash water.
- Bubbles containing ozone can be generated from the entire membrane surface in contact with the water to be treated on the primary side, and the membrane surface fouling substance on the primary side of the membrane is in-plane (here, the entire membrane surface in contact with the water to be treated) ) It is possible to enhance the cleaning effect by removing uniformly and suppressing fouling substance adhesion.
- the reaction between the in-film fouling substance and ozone on the secondary side of the film can be promoted by high-concentration ozone water.
- ozone returns to oxygen after being consumed by the reaction with the fouling substance, the dissolved oxygen concentration in the water tank to be treated can be increased.
- the amount of aeration air can be reduced during backwashing and energy saving can be achieved.
- the flux at the time of design is usually set higher because it assumes a decrease in the flux of the membrane, but when the ozone gas is pressurized and injected into the cleaning water, the membrane cleaning effect is higher than when it is not. Therefore, the required film area can be reduced because a high flux can be maintained. That is, the required number of membrane modules or membrane units can be reduced, and the membrane filtration device can be miniaturized.
- FIG. 6 is a block diagram showing a comparative example 1.
- FIG. 10 is a block diagram showing a comparative example 2. It is a figure which shows the daily change of the membrane filtration resistance which concerns on a comparative example and the Example of this invention. It is a figure which shows the relationship between the ozone water density
- FIG. 1 is a block diagram showing Embodiment 1 of the present invention.
- the membrane filtration separation device 2 is immersed in the water tank 1 to be treated and is connected to the switching valve 10 via the membrane connection pipe 11.
- the switching valve 10 is branched into a filtrate water pipe 12 and an ozone water pipe 14, the filtrate water pipe 12 is connected to the switch valve 10, and the filtration pump 7 is on the piping path of the filtrate water pipe 12.
- the ozone water pipe 14 is connected to an ozone mixing tank 5 which is an ozone dissolving part.
- a cleaning water tank 3 is connected to the upstream side via a cleaning water pipe 13, and a cleaning water supply pump 8 is provided on the cleaning water pipe 13 between the ozone mixing tank 5 and the cleaning water tank 3.
- an ozone generator 4 that is an ozone generator is connected to the ozone mixing tank 5 through an ozone gas pipe 16.
- the ozone generator 4 is usually supplied with an oxygen-containing gas indicated by the symbol G unless otherwise specified below.
- an outlet of the water pipe 15 to be treated is installed on the upper surface of the water tank 1 to be treated.
- the membrane filtration separation apparatus 2 the ozone mixing tank 5, the ozone water piping 14, the switching valve 10, the membrane connection piping 11, and the ozone gas piping 16 have ozone resistance.
- the treated water is sent into the treated water tank 1 through the treated water pipe 15 (here, the treated water is water passing through the treated water pipe 15).
- the water to be treated is filtered by the filtration pump 7 via the membrane filtration separation device 2, and the filtered treated water is obtained via the membrane connection pipe 11 via the switching valve 10 and via the filtrate water pipe 12.
- Continued membrane filtration treatment will clog the membrane, so it will be reversed periodically (frequency once every few hours to several weeks or months, depending on design or operating conditions, water quality of the treated water, etc.) Washing is required.
- the filtration pump 7 is stopped, and the backwashing process is started by switching the switching valve 10 so that the membrane connection pipe 11 and the ozone water pipe 14 are connected.
- the transmembrane pressure difference may be measured and set to switch to the backwashing process when the transmembrane pressure difference rises to, for example, 20 kPa.
- stationary means that the filtration pump 7 is stopped and is not filtered. At that time, by removing air from the lower direction of the membrane filtration separation device 2 (the direction directly below the membrane filtration separation device 2), an effect of removing the deposit on the membrane surface is expected. At that time, aeration may be performed intermittently.
- an ozone concentration meter can be installed in the membrane connecting pipe 11 or the ozone water pipe 14 in order to measure the ozone water density of the cleaning water containing ozone.
- the ozone gas concentration based on the value of the ozone concentration meter. That is, since the ozone water concentration varies depending on the quality of the treated water (membrane filtered water) used for the cleaning water, if the value of the ozone concentration meter is lower than a predetermined value (for example, 3 mg / L), the ozone gas concentration is increased. It is possible to efficiently generate and use ozone while maintaining a sufficient cleaning ability.
- a predetermined value for example, 3 mg / L
- the backwashing process of the membrane filtration separation apparatus proceeds as follows.
- the cleaning water stored in the cleaning water tank 3 is pressurized by the cleaning water supply pump 8 through the cleaning water pipe 13 and sent to the ozone mixing tank 5.
- the washing water generally means filtered water used when the membrane is backwashed, but may be other clear water such as tap water.
- ozone-containing gas hereinafter referred to as ozone gas
- ozone gas ozone-containing gas generated by the ozone generator 4 is mixed with cleaning water, and ozone is dissolved in water to generate ozone cleaning water.
- the gas-liquid ratio ratio of ozone gas flow rate to cleaning water
- the reason why it can be reduced is, for example, the ozone gas concentration of 30 g / Nm 3 Because the gas concentration required to obtain the same amount of ozone is small
- ozone gas is injected into the pressurized cleaning water more than otherwise. Can dissolve ozone into cleaning water with high efficiency.
- ozone cleaning water in this embodiment can be supplied to the membrane filtration separation device 2 without separating the gas.
- raw materials for ozone gas liquid oxygen, oxygen generated by PSA (Pressure Swing Adsorption) or VPSA (Vacuum Pressure Swing Adsorption) can be used.
- the ozone gas concentration is preferably 30 g / Nm 3 or more and 2100 g / Nm 3 or less. In order to generate an ozone gas concentration of 400 g / Nm 3 or more, it is necessary to temporarily store and concentrate the ozone gas. When the ozone gas concentration is less than 30 g / Nm 3 , the ozone gas flow rate increases (the amount of ozone generated is the product of the ozone gas concentration and the ozone gas flow rate. The ozone gas cannot be efficiently dissolved in the cleaning water.
- the ozone generation efficiency of the ozone generator 4 is lowered, that is, the power consumption per unit ozone generation amount is higher than the ozone gas concentration range of 30 g / Nm 3 or more and 2100 g / Nm 3 or less. Since the amount increases, it is not preferable.
- ozone reacts with organic substances in the treated water, but the ozone water in the washed water can be adjusted to an ozone gas concentration of 30 g / Nm 3 or more.
- the concentration can be increased. This is because the higher the ozone gas concentration, the smaller the gas-liquid ratio, and the smaller the gas-liquid ratio, the higher the ozone gas dissolution efficiency.
- the higher the ozone gas concentration, the higher the partial pressure of the ozone gas, and the higher the ozone water concentration can be increased even if a part of ozone is consumed by the reaction with organic matter.
- FIG. 1 the change of the ozone water concentration with respect to the ozone gas concentration is shown in FIG.
- FIG. 2 when the amount of ozone injected per liter of backwash water, that is, when the ozone injection rate is 10 mg / L, the ozone water concentration of backwash water suddenly increases at an ozone gas concentration of 30 g / Nm 3 or more.
- ozone gas is supplied into the liquid even if ozone is consumed by reaction with organic matter in the treated water (membrane filtered water) by using high-concentration ozone gas. When it is done, it gets bigger. That is, a high film cleaning effect can be obtained at an ozone water concentration of 4 mg / L or more. This is not limited to an ozone injection rate of 20 mg / L.
- the gas / liquid ratios when the ozone gas concentration is 60 g / Nm 3 , 600 g / Nm 3 , and 2100 g / Nm 3 are 0.17, 0.017, and 0.0048, respectively.
- the fouling substance is more easily peeled with a smaller ozone amount as the ozone gas concentration is higher. That is, the fouling substance is oxidized by ozone, the adhesion force to the film is reduced, and it becomes easy to peel off by backwash water. Since this is a secondary reaction depending on the ozone water concentration and the fouling substance concentration, the higher the ozone water concentration, that is, the higher the ozone gas concentration, the more the reaction between ozone and the fouling substance is promoted.
- the reaction with organic matter proceeds more efficiently as the ozone water concentration increases at an ozone gas concentration of 30 g / Nm 3 or more, and the transmembrane pressure difference is recovered. Since the rate becomes high, more efficient backwashing becomes possible by setting the ozone gas concentration to 30 g / Nm 3 or more.
- the ozone cleaning water is supplied to the membrane filtration / separation device 2 via the switching valve 10 via the ozone water pipe 14 and further to the membrane filtration / separation device 2 via the membrane connection pipe 11, and cleaning of the membrane filtration / separation device 2 is started. Washed with washing water. Further, bubbles (hereinafter referred to as ozone bubbles for short) 101 containing ozone having a diameter of 0.1 ⁇ m to 1 mm are generated from the primary side of the membrane surface of the membrane filtration separation device 2, and the membrane surface is washed thereby. . The ozone bubble 101 covers the entire film surface.
- the switching valve 10 When a predetermined time, for example, 20 minutes elapses and the backwashing process is completed, the switching valve 10 is switched so that the filtrate water pipe 12 and the membrane connection pipe 11 are connected, and the membrane filtration process is started again as described above. Is done. In addition, you may provide time to leave still without performing a membrane filtration process before switching. At this time, since ozone cleaning water is used as the cleaning water, the cleaning water remaining in the membrane connection pipe 11 is also used as the treated water, that is, the cleaning water remaining in the pipe, that is, the ozone cleaning water is discarded. Without being treated as treated water filtered through a membrane.
- washing water when using sodium hypochlorite solution as washing water, it is necessary to collect it separately as waste water, but this is not necessary when using ozone washing water. This is because ozone is naturally decomposed over time, and its half-life is 20 to 30 minutes. Further, in the present embodiment, when ozone gas is injected into pressurized cleaning water, ozone cleaning water having a higher ozone concentration is used than in the case where the ozone gas is not so, so the reverse is achieved in a shorter time than in the conventional example. Washing can be completed.
- the washing water may be tap water or may be stored and used as filtered water.
- Fig. 3 shows a block diagram when filtered water is used.
- the configuration is the same as in FIG. 1 except that the filtrate water pipe 12 and the treated water pipe 6 are connected to the washing water tank 3 and the pressure gauge 9 is set in the membrane connection pipe 11.
- the pressure gauge 9 may be located between the switching valve 10 and the filtration pump 7. That is, the filtered water is stored in the washing water tank 3, and the filtered water stored in the washing water tank 3 during the backwashing process is used as the washing water. Further, a pressure gauge 9 is installed in the membrane connection pipe 11, and the pressure is constantly monitored by using the pressure gauge 9. When the pressure rises to a predetermined pressure (a pressure predetermined at the time of design, for example, 5 to 100 kPa), backwashing is performed.
- a predetermined pressure a pressure predetermined at the time of design, for example, 5 to 100 kPa
- the pressure gauge 9 preferably has ozone resistance.
- This negative pressure filtration system is a system that obtains filtered water by sucking the treated water under negative pressure
- the pressure filtration system is a system that pressurizes the filtered water and passes the membrane to obtain filtered water It is.
- a suction pump for obtaining filtrate water is provided on the downstream side of the membrane module
- a pressure pump for pushing filtered water is provided on the upstream side of the membrane module. Yes.
- bubbles containing ozone are not generated from the film surface, and the sludge adhering to the primary side of the film surface cannot be peeled off (see the blowout part of C100).
- oxygen bubbles may be generated, since oxygen does not have oxidizing power, fouling substances or sludge adhering to the primary side of the film surface cannot be removed and peeled off, respectively.
- ozone cleaning water having a higher ozone concentration than that when it is not supplied is supplied as backwashing water.
- the ozone water concentration is high and sufficient fouling material removal is possible (see the C2 blowing part).
- the fouling substance in the membrane can sufficiently react with ozone, and low-concentration ozone water or sodium hypochlorite aqueous solution generated by injecting ozone gas into non-pressurized cleaning water can be washed with cleaning water. The reaction can be completed in a short time compared with the case of using.
- the fouling substance on the primary side of the film surface and ozone can be reacted efficiently, and a large amount of fine bubbles with a diameter of 0.1 ⁇ m to 1 mm are generated from the entire primary side of the film surface.
- the entire film surface can be cleaned uniformly. That is, since bubbles of ozone slide up on the film surface, the removal of the fouling substance on the film surface proceeds (see the blowout portion of C1).
- uniform means that the number of bubbles generated per unit area of the film surface is uniform.
- the amount of bubbles generated is determined by the pressure change, the ozone water concentration, and the pore size of the membrane.
- the fouling substance and sludge on the primary side of the film surface can be peeled off by the action of bubbles containing ozone (see the blowing portion of C1).
- MBR Membrane Bioreactor
- oxygen is supplied to the sludge.
- MBR membrane separation activated sludge method
- the sludge activity is increased and the required aeration amount can be reduced.
- some ozone used in the backwashing is supplied to the water tank 1 to be treated and reacts with sludge, it is possible to suppress the sludge growth and reduce the excess sludge, and not to generate surplus sludge. Is possible.
- the flow direction of the filtrate water on the membrane is directed to the primary side of the membrane surface.
- a shearing force can be applied, and a higher cleaning effect can be obtained as compared with a case where bubbles are not supplied by a blower or an air pump.
- a stronger shearing force can be applied compared to the case where the bubbles are not supplied by a blower or an air pump.
- a higher cleaning effect can be obtained as compared with the case where bubbles are not supplied by a blower or an air pump.
- an ejector or an injector type reactor is preferably used as the ozone mixing tank 5, for example.
- a mechanism for promoting gas-liquid mixing such as a static mixer, may be installed on the downstream side of these reactors on the upstream side of the switching valve 10, specifically, in the ozone water pipe 14.
- miniaturization of ozone gas is accelerated
- the ozone gas concentration used in the ozone generator 4 is preferably as high as 30 g / Nm 3 or more.
- ozone cleaning water is generated from cleaning water by setting the ozone gas concentration to 30 g / Nm 3 or more, ozone cleaning water having a higher concentration than ozone water concentration generated at an ozone gas concentration of less than 30 g / Nm 3 may be generated. it can.
- the ratio of the ozone gas flow and cleaning water flow rate (hereinafter referred to as gas-liquid ratio) is made smaller than the gas-liquid ratio of the ozone gas concentration of less than 30 g / Nm 3, the dissolution efficiency of ozone less than 30 g / Nm 3
- the ozone gas concentration should be higher than the gas-liquid ratio so that exhaust ozone gas is not emitted due to the pressure from the cleaning water supply pump 8, or is hardly emitted as compared with the amount of ozone gas having an ozone gas concentration of less than 30 g / Nm 3. Can do. Thereby, ozone gas can be used effectively.
- the pressure for supplying ozone cleaning water as cleaning water is 10 to 500 KPa, more preferably 20 to 400 kPa, and even more preferably 30 to 300 kPa. If the pressure is too high, the pressure resistance of the membrane filtration / separation device may be exceeded. On the other hand, when the pressure is low, the ozone gas is not sufficiently dissolved and the concentration of ozone water becomes low, or the ozone gas that could not be completely dissolved partially accumulates in the pipe. Moreover, these pressures can be set to arbitrary values by adjusting the flow rate of the ozone cleaning water.
- ozone gas is not injected at first, but only treated water (membrane filtered water) is supplied to the membrane filtration separation device 2, and ozone gas is injected when the pressure becomes higher than a certain value (for example, 25 kPa). If the membrane filtration separation device 2 is washed with ozone water and dissolved, washing can be carried out more effectively. That is, since no cleaning water in which ozone gas does not dissolve at a low pressure (for example, 10 kPa) is not generated, a high film cleaning effect can be maintained.
- a pressure regulating valve 22 is preferably ozone resistant.
- the flow rate supplied as washing water should be 1/10 to 10 times the amount of filtered water.
- the amount of filtered water can be calculated from the flux and membrane area. That is, the value obtained by multiplying the flux and the membrane area is the amount of filtered water. If the flow rate supplied as cleaning water is less than 1/10, the transmembrane pressure difference is not lowered, and the cleaning effect is insufficient, which is not preferable. Further, if the flow rate supplied as washing water is larger than 10 times, not only the amount of ozone used is increased, but the amount of filtered water is reduced, which is not preferable.
- the backwash time is preferably 10 seconds or more and 60 minutes or less. If the backwash time is shorter than 10 seconds, backwashing is insufficient, and if it is longer than 60 minutes, the amount of ozone used is increased. On the other hand, if the washing time is increased, the amount of filtered water is reduced because the filtration treatment cannot be performed for that amount of time, which is not preferable. However, it is not limited to this when the value of the flux at a predetermined design, for example, 0.2 to 5.0 m 3 / day can be secured, and it may be within the range of the time at which the flux at the design can be secured. Furthermore, ozone water may be passed for a certain period of time during backwashing and then held as it is. The holding time is preferably 10 seconds or more and 60 minutes or less as described above, and if the flux at the time of the design can be ensured, it may be within the range of the time at which the flux at the time of design can be secured.
- tetrafluoroethylene / perfluoroalkyl vinyl ether copolymer PFA
- PVDF polyvinylidene fluoride
- PTFE polytetrafluoroethylene
- a fluororesin compound such as tetrafluoroethylene / ethylene copolymer (ETFE) is preferably used.
- a microfiltration membrane hereinafter referred to as MF (Micro Filtration) membrane
- MF Micro Filtration
- UF Ultra Filtration membrane
- the average pore diameter of the membrane is 0.001 to 1 ⁇ m, more preferably 0.01 to 0.8 ⁇ m. If the average pore diameter is smaller than this, clogging of the membrane occurs in a short time, and the pressure at the time of membrane filtration further increases, which is not preferable.
- the membrane filtration separation device 2 has a module structure containing these membranes (a combination of piping and the like so that water can be filtered).
- the shape of the membrane of the membrane filtration separation device 2 can be any shape such as hollow fiber (immersion type, casing type), flat membrane (immersion type flat membrane shape, casing type spiral shape), monolith type, etc. It is. Further, the filtration method can be either a full-volume filtration method or a cross flow filtration method. Moreover, although the negative pressure filtration method was shown in the block diagrams of FIGS. 1 and 3, a pressure filtration method may be used.
- the types of water to be subjected to membrane separation in the present embodiment are water, industrial water, sewage, secondary sewage treatment water, industrial wastewater, seawater, manure, etc., and water generated in the course of processing these become.
- the biological treatment can be carried out by combining anaerobic, anoxic, and aerobic treatment.
- the above-mentioned type of water and sludge are introduced into the water tank 1 to be treated, mixed and treated with the membrane filtration / separation device 2 to separate the sludge and the treated water, or the above-mentioned target for membrane separation.
- the present invention can be applied to any case in which membrane filtration is performed directly on each type of water, or membrane filtration is performed without adding sludge to the water tank 1 to be treated. In either case, by using an inorganic or organic flocculant in the water tank 1 to be treated, an effect of improving the flux of the membrane filtration treatment or preventing clogging of the membrane can be obtained.
- FIG. 6 is a block diagram when sewage or factory wastewater is treated by MBR.
- the configuration is added to FIG. 3 as follows.
- An excess sludge extraction pump 201 is connected to the treated water tank 1 via an excess sludge extraction pipe 203.
- a sludge circulation pump 202 is connected to the water tank 1 through a sludge circulation pipe 204.
- the sludge circulation pump 202 is not essential.
- an air diffuser 205 is installed in the lower part of the membrane filtration separation device 2 of the water tank 1 (refers to a place near the bottom surface of the water tank 1 inside the water tank 1).
- the treated water tank 1 is filled with activated sludge having an MLSS (Mixed Liquor Suspended Solid) concentration of 3000 to 20000 mg / L.
- MLSS Mated Liquor Suspended Solid
- organic substances are removed by activated sludge and separated into activated sludge and treated water through the membrane filtration separation device 2.
- the activated sludge is circulated by the sludge circulation pump 202.
- the increased activated sludge is extracted by the excess sludge extraction pump 201, and the MLSS concentration in the water tank 1 to be treated is kept constant.
- Air is supplied to the activated sludge in the water tank 1 to be treated by the air diffuser 205, and the membrane treatment of the membrane filtration separation device 2 is swung with air to stabilize the membrane treatment (here, stable Flux as designed is carried out (meaning that it can be obtained over a long period of time (a period of several tens of days to several hundred days)).
- a blower is connected to the air diffuser 205, but is not shown here.
- the backwashing with the ozone cleaning water described above is periodically performed, so that the ozone water or the low concentration ozone water generated by injecting the ozone gas into the non-pressurized cleaning water or the sodium hypochlorite aqueous solution is washed with the cleaning water.
- High flux can be obtained as compared with the case of using.
- FIG.1, FIG.3, FIG.5 showed the case where the membrane filtration separation apparatus 2 was immersed in the to-be-processed water tank 1, However, it is not necessary to restrict to this and the to-be-processed water tank 1 is divided
- the membrane filtration separation device 2 may be installed in the downstream tank, and the activated sludge on the upstream side and the downstream side may be circulated with a pump.
- the membrane filtration / separation device 2 may be taken out of the water tank 1 to be treated, and the activated sludge in the water tank 1 to be treated may be supplied to the membrane filtration separation device 2 by a pump and circulated.
- the inside of the water tank 1 to be treated may be divided into two, and the membrane filtration separation device 2 may be immersed in the aerobic tank with the upstream side as the anaerobic tank and the downstream side as the aerobic tank. Furthermore, the inside of the water tank 1 may be divided into three, and the membrane filtration separation device 2 may be immersed in an aerobic tank as an anoxic tank, an anaerobic tank, and an aerobic tank in order from the upstream side.
- FIG. 7 is a block diagram in the case where ozone treatment is performed on the filtered water with respect to FIG. That is, in order to further improve the quality of filtered water, the oxidizing power of ozone is used to improve the chromaticity and turbidity of filtered water and to remove organic substances, inorganic substances such as iron and manganese, viruses and the like.
- the configuration is added to FIG. 6 as follows.
- the ozone treated water pipe 302 is connected to the treated water pipe 6 through the ozone reaction tank 301.
- the ozone reaction tank 301 is connected to the ozone generator 4 via a treated water ozone gas pipe 303 mixed with treated water.
- the treated water exhaust ozone gas treatment facility 305 for exhausting the ozone gas emitted from the treated water is connected to the ozone reaction tank 301 via the treated water exhaust ozone gas pipe 304 for exhausting the ozone gas.
- the filtered water stored in the washing water tank 3 is sent to the ozone reaction tank 301 through the treated water pipe 6.
- the ozone gas generated by the ozone generator 4 is supplied to the ozone reaction tank 301 through the treated water ozone gas pipe 303 mixed with the treated water, whereby the filtered water is subjected to ozone treatment.
- Undissolved ozone gas is decomposed into oxygen by the treated water exhaust ozone gas treatment facility 305 that exhausts ozone gas emitted from the treated water through the treated water exhaust ozone gas pipe 304 for exhausting the ozone gas, detoxified, and released to the atmosphere. Is done.
- the ozone-treated water is used as reused water or the like through the ozone-treated water pipe 302.
- the ozone generator 4 for generating ozone cleaning water for backwashing for ozone treatment of filtered water, the ozone generator can be used more efficiently and the quality of filtered water can be further improved. it can.
- backwashing of the membrane filtration separation device 2 is performed intermittently (turned on once a day to several weeks for several months), and when the above ozone cleaning water is used as backwashing water, Since the reaction with the fouling substance is completed in a short time of 10 seconds or more and within 60 minutes, there is no need to collect backwash water as waste water, so the ozone generator 4 is effectively used when the filtered water is treated with ozone. Can be used.
- the treated water which flows in via the treated water piping 6 is stored in the ozone reaction tank 301, and ozone treatment is started in the ozone reaction tank 301 as soon as the backwashing is completed. Then, the ozone-treated water flows out through the ozone-treated water pipe 302.
- the ozone treatment is carried out for the required amount of high-quality treated water. It is also possible not to treat the rest with ozone.
- the present embodiment is not limited to MBR, and can be implemented as long as it is a combination of membrane filtration treatment and ozone treatment.
- FIG. FIG. 8 is a block diagram showing an example of the second embodiment of the present invention.
- the configuration is added to FIG. 3 as follows.
- An ozone gas storage tank 17 capable of storing ozone gas is installed between the ozone generator 4 and the ozone mixing tank 5 via an ozone gas pipe 16. Further, the ozone gas storage tank 17 and the ozone generator 4 are connected via an oxygen gas pipe 18.
- the ozone gas generated by the ozone generator 4 using oxygen gas as a raw material is sent to the ozone gas storage tank 17 through the ozone gas pipe 16, and is adsorbed by an adsorbent such as silica gel at a low temperature in the ozone gas storage tank 17.
- an adsorbent such as silica gel at a low temperature in the ozone gas storage tank 17.
- the ozone generator 4 is supplied with an oxygen-containing gas as indicated by the symbol G. In this case, it is more preferable to supply an oxygen gas generated from liquid oxygen rather than an oxygen-containing gas.
- the oxygen gas that has not been adsorbed by the silica gel in the ozone gas returns to the ozone generator 4 through the oxygen gas pipe 18 and is used again as a raw material for ozone gas.
- the supply of ozone gas from the ozone generator 4 to the ozone gas storage tank 17 is stopped, and the path from the ozone gas storage tank 17 to the ozone generator 4 is also blocked.
- an injector-type reactor in the ozone mixing tank 5 the ozone gas stored in the ozone gas storage tank 17 is sucked by the negative pressure generated thereby, and the sucked ozone gas is dissolved in the washing water to obtain the ozone washing water. It produces
- the ozone gas in the ozone gas storage tank 17 may be sucked with a pump and sent to the ozone mixing tank 5.
- ozone gas is again supplied from the ozone generator 4 to the ozone gas storage tank 17, and the ozone gas is adsorbed onto an adsorbent such as silica gel at a low temperature of ⁇ 30 ° C. to ⁇ 90 ° C.
- ozone gas with a high concentration can be used, so the gas flow rate required to generate ozone cleaning water can be reduced.
- the ozone gas can be increased as compared with the case where the ozone gas is not stored or concentrated.
- oxygen used in this embodiment is preferably high-purity oxygen that contains as little nitrogen as possible.
- oxygen gas obtained by vaporizing liquid oxygen may be used.
- the oxygen gas discharged from the ozone gas storage tank 17 is recovered at the initial stage of desorption (stage where oxygen is first released), so that a higher concentration can be obtained. It becomes possible to take out ozone gas. 15 wt% as ozone gas concentration (226g / m 3) ⁇ 100wt % (2,143g / m 3) is preferable. More preferably 25wt% (390g / m 3) ⁇ 99wt% (2,111g / m 3). At this time, it is possible to install a pump in the ozone gas pipe 16 and draw out the ozone gas stored in the ozone gas storage tank 17 with the pump.
- an ozone concentration meter can be installed in the membrane connecting pipe 11 or the ozone water pipe 14 in order to measure the ozone water density of the cleaning water containing ozone.
- the ozone gas concentration based on the value of the ozone concentration meter. That is, since the ozone water concentration varies depending on the quality of the treated water (membrane filtered water) used for the washing water, it is sufficient to increase the ozone gas concentration if the value of the ozone concentration meter is lower than a predetermined value, for example, 3 mg / L. It is possible to efficiently generate and use ozone while maintaining a good cleaning ability.
- the ozone gas storage tanks 17 are made into two series, the ozone gas stored in the ozone gas storage tank 17 can be taken out mutually, so that the fluctuation of the ozone gas concentration is small more stably than in the case of one series. Below, it becomes possible to extract high-concentration ozone gas.
- FIG. 9 an example in which an ejector 52 is provided in the ozone mixing tank 5 and an ozone water circulation pump 51 that sends ozone water to the ejector is provided and connected to each other by an ozone water circulation pipe 53 will be described.
- the cleaning water supply pump 8 is installed on the ozone water pipe 14.
- the member in the liquid contact portion needs to have ozone resistance.
- an exhaust ozone gas pipe 23 for discharging ozone gas that has not been dissolved in water is connected to the upper portion of the ozone mixing tank 5.
- the cleaning water is supplied from the cleaning water tank 3 to the ozone mixing tank 5 by, for example, gravity dropping.
- the cleaning water in the ozone mixing tank 5 is supplied to the ejector 52 by the ozone water circulation pump 51, and at this time, the high pressure concentrated in the ejector 52 from the ozone gas storage tank 17 by using the negative pressure generated in the ejector 52.
- the ozone gas is sucked and the cleaning water and the ozone gas are mixed by the ejector 52.
- a pump (not shown) may be provided in the ozone gas pipe 16 between the ejector 52 and the ozone gas storage tank 17, and ozone gas may be supplied using this pump.
- ozone concentration in the wash water in the ozone mixing tank is increased.
- an ozone concentration meter installed in the ozone water circulation pipe 53 is used to prepare ozone water having a predetermined concentration, for example, a concentration of 10 mg / L, as cleaning water, and cleaning is performed at the timing of backwashing. Backwashing is performed by supplying high-concentration ozone water to the membrane filtration separation device 2 via the ozone water pipe 14 using the water supply pump 8.
- the ozone gas that does not dissolve in the ozone mixing tank 5 and passes through the exhaust ozone gas pipe is decomposed into harmless oxygen by the catalyst and released to the atmosphere. Or it is also possible to inject
- concentrated ozone gas is used, sufficiently high concentration ozone water, that is, high concentration ozone water having a concentration of, for example, 3 mg / L or more can be generated.
- the membrane can be cleaned efficiently.
- the ozone gas stored in the ozone gas storage tank 17 may be taken out by a pump without going through the ejector 52 and supplied by bubbling from the lower part of the ozone mixing tank 5 through an air diffuser or the like. The same effect as above can be obtained.
- FIG. 10 is a block diagram in the case of generating ozone cleaning water for backwashing using exhausted ozone gas discharged from the ozone reaction tank 301 with respect to FIG.
- the configuration is added to FIG. 8 as follows.
- An exhaust ozone gas switching valve 307 is installed in the treated water exhaust ozone gas pipe 304 and is connected to the ozone mixing tank 5 via the exhaust ozone gas reuse pipe 306. Further, the ozone gas storage tank 17 is installed on the exhaust ozone gas reuse pipe 306.
- the waste ozone gas treatment of the treated water waste ozone gas treatment facility 305 is also continuously carried out correspondingly.
- the ozone gas is stored by switching the exhaust ozone gas switching valve 307 so that the exhaust ozone gas is introduced into the ozone gas storage tank 17 during a period of storing the necessary ozone amount.
- the ozone gas can be stored efficiently.
- the exhaust ozone gas switching valve 307 is switched so that the exhaust ozone gas discharged from the ozone reaction tank 301 can be processed by the treated water exhaust ozone gas processing facility 305. Thereby, ozone can be efficiently used by reusing exhaust ozone gas.
- the ozone cleaning water can be generated by drawing the exhaust ozone gas and efficiently dissolving the ozone gas in the cleaning water.
- this form is not restricted to MBR, If it is the combination of a membrane filtration process and ozone treatment, it can be implemented.
- FIG. 11 is a block diagram in the case where the water to be treated entering the water tank 1 is pre-ozone treated and the ozone cleaning water for backwashing is generated using the exhausted ozone gas discharged from the ozone reaction tank 501. .
- Other configurations and operations are the same as those in FIG.
- FIG. FIG. 12 is a block diagram showing an example of the third embodiment of the present invention. The configuration is added to FIG. 3 as follows.
- An acid storage tank 19 is connected to the ozone water pipe 14 via an acid supply pipe 21.
- an acid supply pump 20 is installed on an acid supply pipe 21 between the acid storage tank 19 and the ozone water pipe 14.
- the operation will be described.
- the acid in the acid storage tank 19 is supplied to the ozone cleaning water in the ozone water piping 14 by the acid supply pump 20 through the acid supply piping 21.
- the membrane filtration separation device 2 is backwashed by generating acidic ozone cleaning water. It is also possible to install a static mixer or the like downstream from the point where the acid is injected into the ozone water pipe 14 to improve the mixability of the acid and the ozone cleaning water, that is, to increase the solubility of ozone and increase the dissolved ozone concentration. It is.
- an inorganic acid such as hydrochloric acid, sulfuric acid or nitric acid, or an organic acid such as oxalic acid or citric acid
- an inorganic acid such as hydrochloric acid, sulfuric acid or nitric acid, or an organic acid such as oxalic acid or citric acid
- the so-called scale (“scale”) such as iron, calcium, magnesium, silica, aluminum, etc. attached to the inside and the surface of the film means a deposit mainly composed of an inorganic substance. ) Can be enhanced.
- the acid injection timing may be before, after, or at the same time as supplying ozone cleaning water as backwashing water to the membrane filtration separation device 2. That is, after cleaning by injecting acid, cleaning with ozone cleaning water is performed, or acid is added to ozone cleaning water in advance and cleaning is performed, or after cleaning with ozone cleaning water, acid is injected. It is possible to carry out any mode of cleaning. In addition, before washing with acid, washing water (membrane filtered water) into which ozone gas has not been injected may be used first.
- an acid when switching from backwashing to filtration treatment, it is necessary to once collect the wash water remaining in the membrane filtration separation device 2 or the membrane connection pipe 11. This is because the acid does not satisfy the pH range which is the standard for drainage or discharge.
- an inorganic acid when used as the acid, it can be used as treated water after only pH adjustment.
- an organic acid when used as the acid, it is preferably returned to the water tank 1 to be treated. However, if the amount of the organic acid used is diluted to a level that can satisfy the drainage or discharge standard, it can be recovered as treated water without being returned to the treated water tank 1 due to the dilution effect.
- FIG. 13 is a block diagram showing an example of the fourth embodiment of the present invention. The configuration is added to FIG. 3 as follows.
- An exhaust ozone gas pipe 23 is connected to the membrane connection pipe 11, and a pressure relief valve 28 and an exhaust ozone gas treatment facility 24 are sequentially installed via the exhaust ozone gas pipe 23.
- the pressure relief valve 28 opens when the pressure measured by the pressure gauge 9 exceeds a predetermined value, for example, 50 kPa, during backwashing.
- a predetermined value for example, 50 kPa
- the pressure relief valve 28 is closed. That is, it operates as a vent intermittently.
- the exhaust ozone treatment apparatus described in Patent Document 1 is always released, and the pressure control in the backwash water tank 30 that generates ozone wash water is not carried out. Therefore, the exhaust ozone gas treatment facility of the present embodiment 24 is different from the exhaust ozone treatment apparatus described in Patent Document 1.
- the pressure relief valve 28 sets opening and closing times and automatically adjusts the opening and closing of the valve. Alternatively, it can be controlled by the value of the pressure gauge 9.
- the upper and lower pressure limits are set. When the pressure reaches the upper limit, the pressure relief valve 28 is opened, and when the pressure reaches the lower limit, the pressure relief valve 28 is closed.
- the pressure relief valve 28 may be a valve that opens when a pressure rises to a predetermined pressure, such as a safety valve.
- the shearing force by the ozone water in the membrane that is, the force to shift or rub the membrane surface with the ozone water increases, and the cleaning effect is further improved. It becomes possible to raise.
- the pressure according to the gas-liquid ratio of the high-concentration ozone gas and the cleaning water it is possible to further increase the ozone gas dissolution efficiency.
- the pressure of the backwash water can be controlled within a predetermined value, for example, 50 kPa, and the membrane filtration separation device 2 can be prevented from being damaged.
- FIG. FIG. 14 is a block diagram showing a part of the apparatus configuration of an example of the fifth embodiment of the present invention. The following configuration is added to FIG. 1, FIG. 3, or FIG.
- the membrane connection pipe 11 is connected to the header 25, and the first membrane connection pipe 26 and the second membrane connection pipe 31 are connected to the header 25.
- the first membrane connection pipe 26 and the second membrane connection pipe 31 are connected in the membrane filtration separation device 2. It is preferable to install the membrane connection pipe 26 and the second membrane connection pipe 31 at a position where a pair of the membrane filtration separation device 2 which is a membrane module is paired.
- the ozone water concentration in the membrane filtration / separation device is made uniform by supplying ozone cleaning water from the paired position of the membrane filtration / separation device 2 it can. Further, the header 25 has a function of uniformly distributing the ozone cleaning water flowing into the membrane filtration / separation apparatus 2 from the membrane connection pipe 26 and the second membrane connection pipe 31.
- filtered water is sent to the washing water tank 3 through each of the first membrane connection pipe 26 and the second membrane connection pipe 31.
- the pressure buffering action works in the header 25, and ozone washing water as washing water is uniformly in the membrane filtration separation device 2 through the first membrane connection pipe 26 and the second membrane connection pipe 31. Since it is supplied (becomes uniform because the header 25 is connected), the inside of the film and the film surface can be cleaned uniformly. If ozone cleaning water that is cleaning water cannot be supplied uniformly, a portion that cannot be cleaned in the film is generated.
- FIG. 15 is a block diagram showing a part of the apparatus configuration of another example of the fifth embodiment of the present invention.
- the following configuration is added to FIG. 1, FIG. 3, or FIG. That is, the washing water branches from the membrane connection pipe 11 and enters the washing water adjustment valve 32, and the washing water is supplied to the membrane filtration separation device 2 via the membrane connection pipe 11 and the washing water adjustment valve 32.
- a second membrane connection pipe 31 is branched from the pipe 11 and connected to the membrane filtration separation device 2.
- the membrane connection pipe 11 and the second membrane connection pipe 31 are connected in the membrane filtration separation device 2.
- a membrane connection pipe pressure gauge 33 and a second membrane connection pipe pressure gauge 34 are connected to the membrane connection pipe 11 and the second membrane connection pipe 31, respectively. These pressure gauges are pressure gauge signal lines for the membrane connection pipe, respectively.
- the second membrane connection pipe 31 is provided with a washing water adjustment valve 32 that is a washing water flow rate adjustment valve, and the washing water adjustment valve 32 is connected to a control device 35 via a valve control line 36.
- the pressure values of the membrane connection pipe pressure gauge 33 and the second membrane connection pipe pressure gauge 34 are used as signals, and the pressure gauge signal line 37 for the membrane connection pipe and the pressure for the second membrane connection pipe, respectively.
- the signal is sent to the control device 35 through the meter signal line 38, and a signal is sent to the cleaning water adjusting valve 32 through the valve control line 36 so that these values become equal, thereby adjusting the opening of the valve.
- ozone cleaning water which is cleaning water, is always supplied uniformly into the membrane filtration / separation device 2 through the membrane connection pipe 11 and the second membrane connection pipe 31 so that the inside of the membrane and the membrane surface can be cleaned uniformly. It becomes possible.
- FIG. 16 is a block diagram showing a part of the apparatus configuration of an example of the sixth embodiment of the present invention.
- the membrane filtration separation device is divided into upper and lower two stages. And the structure is added as follows with respect to FIG.1 or FIG.3 or FIG.8.
- An upper membrane connection pipe 11p and a lower membrane connection pipe 11q are connected to the upper membrane filtration separation apparatus 2p and the lower membrane filtration separation apparatus 2q, respectively.
- the second membrane connection pipe 31 branches off from the upper membrane connection pipe 11p as described above, and a washing water adjustment valve 32 is attached to the second membrane connection pipe 31.
- the tip of the second membrane connection pipe 31 is at the lower part of the upper membrane filtration separation device 2p, and a plurality of ozone water supply devices 44 are attached.
- the ozone water supply device 44 has a role of supplying ozone cleaning water from the lower part of the membrane filtration / separation device 2p to the membrane filtration / separation device 2p. appear.
- an air diffuser 41 is installed in the lower part of the lower membrane filtration separation device 2q of the water tank 1 to be treated, and is connected to the blower 43 through the air supply pipe 42.
- ozone washing water as washing water is supplied to the membrane filtration separation device 2 from the upper membrane connecting pipe 11p and the lower membrane connecting pipe 11q.
- Supplying ozone water by supplying a part of the ozone cleaning water supplied to the upper membrane connection pipe 11p from the ozone water supply device 44 to the upper membrane filtration separation device 2p via the second membrane connection pipe 31.
- a pressure drop occurs in the vessel 44 and ozone bubbles 101 having a diameter of 0.1 ⁇ m to 1 mm are generated, and the surface of the upper membrane filtration separation device 2p is slid up to further enhance the cleaning effect of the upper membrane filtration separation device 2p. it can.
- FIG. 17 is a block diagram showing a part of the apparatus configuration of an example of the seventh embodiment of the present invention.
- FIG. 17 is a processing flow of MBR.
- Eight membrane filtration separation devices 2a to 2h are installed in the series A in the water tank 1 to be treated, and membrane connection pipes 11a to 11h are connected to each.
- the same filtration equipment and backwash equipment as those shown in FIG. 1, FIG. 3 or FIG. 8 are connected to the tip of each of the membrane connection pipes 11a to 11h.
- ozone cleaning water in which ozone gas is dissolved in cleaning water may be used as backwashing water.
- the series B is provided with the same configuration.
- This series B is installed in parallel with the series A, and both or only one of them can be used. Although only two lines are shown in the figure, it is possible to implement at least two lines, for example, three lines. A method of changing the number of series according to the amount of water can also be implemented.
- MBR is adopted by separating the activated sludge in the final sedimentation basin such as the standard activated sludge method and returning it to the aeration tank (corresponding to the water tank 1 to be treated in this embodiment) instead of MBR.
- Parallel operation is also possible. This makes it possible to cope with troubles in MBR (series A).
- the treated water quality of MBR (series A) and the standard activated sludge method (series B) is mixed, the treated water quality of MBR is better than the treated water quality of the standard activated sludge method when a very high quality of treated water is not required. Therefore, it is possible to easily achieve the required treated water quality.
- FIG. 18 shows a case where the processing sequence is at least two or more.
- the membrane filtration water of each of the membrane filtration separation devices 2a to 2d is collected in the membrane connection pipe 11i, and the filtration equipment and backwash equipment similar to the configuration shown in FIG. 1, FIG. 3, or FIG. ing.
- the membrane filtrate of each of the membrane filtration / separation devices 2e to 2h is collected in the membrane connection pipe 11j, and similarly, filtration equipment and backwash equipment are connected.
- the basic operation method is the same as that shown in FIG. 16, it is possible to operate by switching between series A and series B, for example, in response to fluctuations in the amount of treated water or water load.
- the backwashing method was carried out on-line backwashing as four conditions of Examples 1 and 2 and Comparative Examples 1 and 2 shown below, and the daily change of membrane filtration resistance in MBR was evaluated.
- the MBR operating conditions are shown in Table 1.
- Example 1 As the backwash water, ozone wash water (concentration 13 to 15 mg / L) in which ozone gas was dissolved in the wash water was used, and 380 mL was used as the backwash water amount.
- the present Example 1 was implemented with the block diagram shown in FIG. In Example 1, bubbles containing a large amount of ozone were generated from the membrane filtration separation device 2 during backwashing.
- Example 2 As the backwash water, ozone wash water (concentration 13 to 15 mg / L) in which ozone gas was dissolved in the wash water and an oxalic acid aqueous solution (concentration 1000 mg / L) were used, and 190 mL each was used as the backwash water amount.
- the present Example 2 was implemented with the block diagram shown in FIG. In Example 2, bubbles containing a large amount of ozone were generated from the membrane filtration separation device 2 during backwashing.
- FIG. 19 shows a block diagram of backwashing using a sodium hypochlorite aqueous solution.
- a sodium hypochlorite raw water tank 404 storing a 12% sodium hypochlorite aqueous solution is connected to a sodium hypochlorite aqueous solution adjusting tank 402 via a sodium hypochlorite supply pipe 403.
- a washing water tank is connected to a sodium hypochlorite aqueous solution adjustment tank 402 via a washing water pipe 13.
- the cleaning water supply pump 8 and the sodium hypochlorite aqueous solution adjustment tank 402 are connected via a sodium hypochlorite water pipe 405, and the cleaning water supply pump 8 and the switching valve 10 are connected.
- the cleaning water pipe 13 is provided with a cleaning water valve 401.
- Other configurations are the same as those in FIG.
- the 12% sodium hypochlorite aqueous solution stored in the sodium hypochlorite raw water tank 404 is sent to the sodium hypochlorite aqueous solution adjustment tank 402 via the sodium hypochlorite supply pipe 403 and mixed with filtered water.
- a sodium hypochlorite aqueous solution having a concentration of 6000 mg / L is produced.
- This is supplied to the membrane filtration / separation apparatus 2 through the sodium hypochlorite water pipe 405, the switching valve 10, and the membrane connection pipe 11 by the washing water supply pump 8, and backwashing is performed.
- bubbles containing ozone were not generated from the membrane filtration separator 2 during backwashing.
- FIG. 20 shows a block diagram of backwashing using the ozone water of this comparative example.
- the ozone mixing tank 5 is connected to a waste ozone gas treatment facility 24 via a waste ozone gas pipe 23.
- the washing water supply pump 8 is disposed between the switching valve 10 and the ozone mixing tank 5 and is connected by an ozone water pipe 14. Further, since the cleaning water supply pump 8 is in contact with ozone water, a pump having ozone resistance is used.
- the ozone water pipe 14, the switching valve 10, the membrane connection pipe 11, the pressure gauge 9, and the membrane filtration / separation apparatus 2 are also ozone resistant. Other configurations are the same as those in FIG.
- the ozone gas generated by the ozone generator 4 is injected into the ozone mixing tank 5 through the ozone gas pipe 16 to generate ozone water.
- the undissolved ozone gas is decomposed into oxygen by the exhaust ozone gas treatment facility 24 through the exhaust ozone gas pipe 23 as an exhaust ozone gas, detoxified and released to the atmosphere.
- Backwashing is performed by supplying ozone water having a concentration of 2 mg / L in the ozone mixing tank 5 to the membrane filtration / separation device 2 through the ozone water pipe 14, the switching valve 10, and the membrane connection pipe 11 by the washing water supply pump 8. Is done.
- FIG. 21 shows changes with time in membrane filtration resistance.
- the membrane filtration resistance R was calculated from the following formula (1).
- R membrane filtration resistance (m ⁇ 1 )
- ⁇ P transmembrane pressure difference (Pa)
- J membrane permeate flux (m / day)
- ⁇ membrane permeate viscosity coefficient (Pa ⁇ s) is there.
- Comparative Example 1 the membrane filtration resistance increased most rapidly compared to other examples even when backwashing was performed regularly, and two off-line washings (5000 mg / L sodium hypochlorite) were performed during this evaluation period. 2 hours immersion in a solution + 10000 mg / L oxalic acid aqueous solution for 2 hours). Furthermore, even when offline cleaning was performed, the membrane filtration resistance did not return to the initial state, and each time offline cleaning was repeated, the membrane filtration resistance after offline cleaning tended to increase.
- Comparative Example 2 Although not as much as Comparative Example 1, membrane filtration resistance gradually increased.
- an increase in membrane filtration resistance was significantly suppressed as compared with Comparative Examples 1 and 2. This is because the cleaning effect by high-concentration ozone cleaning water was obtained.
- the increase in membrane filtration resistance was further suppressed than in Example 1. This is because the removal of not only organic substances but also inorganic substances is promoted by using an oxalic acid aqueous solution in combination with ozone cleaning water.
- the treated water quality is BOD (Biochemical oxygen demand): 4 to 7 mg / L, COD (Chemical oxygen demand): 7 to 12 mg in all Examples and Comparative Examples.
- / L, SS Stable generally less than 0.5 mg / L, that is, the fluctuation of the water quality was small, and it was within the range of the above BOD, COD, and SS values.
- this wash water was created using this treated water.
- the transmembrane differential pressure when the ozone water concentration in the vicinity of the membrane on the secondary side of the membrane, that is, the point in contact with the membrane is changed to 0.5 to 15 mg / L
- the recovery rate of the membrane filtration resistance obtained from the above was evaluated. The obtained result is shown in FIG.
- the recovery rate (%) of the membrane filtration resistance obtained from the transmembrane pressure difference was calculated from the following formula (2).
- the concentration of ozone water immediately after ozone gas injection was 1 to 17 mg / L.
- the membrane filtration resistance when not used was calculated
- the recovery rate of the membrane filtration resistance obtained from the transmembrane pressure difference increased rapidly by increasing the ozone water concentration to more than 3 mg / L, and reached nearly 100% at the ozone water concentration of 10 mg / L. . That is, the higher the ozone water concentration, the higher the recovery rate of the membrane filtration resistance obtained from the transmembrane pressure difference, which is stable, that is, the flux as designed is long-term (a period of several tens to several hundred days). It was found that the membrane filtration treatment can be carried out with a high flux.
- FIG. 23 to FIG. 25 show the results of evaluating the ozone gas concentration dependency when the ozone gas shown in FIG. 8 is concentrated under the conditions shown in Table 1.
- the ozone gas was concentrated when the ozone gas concentration was 220 g / m 3 or more.
- treated water was used as backwash water, and the ozone injection rate of treated water (the amount of ozone injected per unit treated water amount) was 85 mg / L.
- FIG. 23 shows the change in ozone concentration in the backwash water relative to the ozone gas concentration.
- the result was obtained that the ozone concentration in the backwash water increased as the ozone gas concentration increased.
- the ozone gas concentration was 50 g / Nm 3 or less
- the ozone concentration in the backwash water was as small as about 1 mg / L, and a sufficient cleaning effect was not obtained.
- the organic matter remaining in the treated water reacted with ozone, and ozone was consumed ineffectively. That is, the higher the ozone gas concentration, the smaller the ineffective consumption of ozone.
- FIG. 24 shows the ratio of the ozone concentration in the backwash water to the ozone gas concentration and the ozone gas concentration. As shown in this figure, when the ozone gas concentration is 50 g / Nm 3 or less, the ratio is small and the ozone gas concentration is 220 g / Nm 3 or more, so that the ozone in the gas can be efficiently converted to ozone in the backwash water. I understand.
- FIG. 25 shows the amount of sodium hypochlorite solution backwash water having a concentration of 6000 mg / L with respect to the ozone gas concentration required for 100% recovery of the transmembrane pressure difference, and the ozone required for 100% recovery of the transmembrane pressure difference.
- the change in the ratio of the amount of backwash water is shown.
- the ozone gas concentration is 50 g / Nm 3 or less
- the washing water amount ratio is approximately 0.6.
- the ozone gas concentration is drastically reduced. That is, the amount of water required for backwashing can be reduced as the ozone gas concentration is higher.
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Abstract
Description
水深方向に多段に組み込まれている膜ユニットを同時に逆洗する場合も同様に、水深の異なる各膜ユニット間で均一に洗浄することができない。ここでは、膜とは、孔径0.001~0.5μmの微細な孔を持つシート状のもの、もしくは中空糸状のものを言い、その膜について水をろ過できるように配管等を取り付けて組み合わせたものを膜モジュール、その膜モジュールをいくつか組み合わせたものを膜ユニットと呼ぶ。
膜ろ過した処理した清澄な水を加圧して洗浄水とし、
この洗浄水にオゾンガスを注入してオゾン洗浄水を生成し、
膜ろ過の際のろ過水の出口側であるろ過二次側から、前記オゾン洗浄水を膜ろ過用の膜に供給して、前記膜の内部を洗浄するとともに、
膜ろ過の際の未処理水の入り口側であるろ過一次側でオゾンを含有する気泡を発生させ、前記ろ過一次側の前記膜の表面を洗浄するものである。
膜ろ過処理されていない未処理水に含まれる異物と膜ろ過したろ過水とを分離する膜ろ過分離装置と、
通常の膜ろ過とこの通常の膜ろ過とは逆方向の洗浄である逆洗とを切替える切替弁と、
膜ろ過処理した清澄な水を加圧して洗浄水とし、この洗浄水にオゾンガスを溶解させたオゾン洗浄水を生成し、前記膜ろ過分離装置に前記オゾン洗浄水を供給する配管に接続されたオゾン溶解部と、
このオゾン溶解部に配管を介して接続され、前記洗浄水を供給する洗浄水供給ポンプと、
前記オゾンガスを前記オゾン溶解部に供給するオゾン発生器と、
を備え、
前記切替弁を通常の膜ろ過の方向と切り替えることにより、前記オゾン洗浄水を膜ろ過用の膜に、逆洗により供給して、前記膜を洗浄するものである。
また、過飽和のオゾン水を使用するため、高濃度のオゾン水によって膜の二次側での膜内ファウリング物質とオゾンとの反応を促進できる。また、オゾンがファウリング物質との反応で消費された後は酸素に戻るため、被処理水槽の溶存酸素濃度を高めることができる。
また、逆洗時に曝気風量を削減でき、省エネ化を図れる。
さらに、通常、設計時のフラックスは膜のフラックス低下を想定しているため高めに設定しているが、オゾンガスを加圧して洗浄水に注入した場合には、そうでない場合よりも膜の洗浄効果が高く、高いフラックスを維持できることから必要な膜面積を低減できる。すなわち、必要な膜モジュール数もしくは膜ユニット数を低減させることができ、膜ろ過装置を小型化できる。
実施の形態1.
図1は本発明の実施の形態1を示すブロック図である。本実施の形態の構成においては、膜ろ過分離装置2が被処理水槽1内に浸漬され、膜接続配管11を介して切替弁10に接続されている。切替弁10において、ろ過水配管12とオゾン水配管14とに分岐されており、ろ過水配管12は切替弁10に接続されており、ろ過水配管12の配管経路上にろ過ポンプ7がある。また、オゾン水配管14にはオゾン溶解部であるオゾン混合槽5が接続されている。また、その上流側に洗浄水配管13を介して洗浄水槽3が接続されており、オゾン混合槽5と洗浄水槽3の間の洗浄水配管13上には洗浄水供給ポンプ8がある。また、オゾン混合槽5にはオゾンガス配管16を介してオゾン発生部であるオゾン発生器4が接続されている。このオゾン発生器4には、以下で特にコメントする場合を除き、記号Gで示した酸素含有ガスが通常、供給される。さらに、被処理水槽1の上面には被処理水配管15の出口が設置されている。なお、膜ろ過分離装置2、オゾン混合槽5、オゾン水配管14、切替弁10、膜接続配管11、オゾンガス配管16は、オゾン耐性を持つことが好ましい。
オゾン混合槽5では、オゾン発生器4で発生させたオゾン含有ガス(以降、オゾンガスと呼ぶ)が洗浄水と混合されてオゾンが水中に溶解してオゾン洗浄水が生成される。その際、オゾンガス濃度が30g/Nm3以上の高濃度のオゾンガスを使用するため、ガス液比(オゾンガス流量と洗浄水の比率)を小さくでき(小さくできる理由は、例えばオゾンガス濃度を30g/Nm3以上の高濃度としており、同じオゾン量を得るために必要なガス量が小さくなるため)、さらに加圧していることにより、オゾンガスを加圧した洗浄水に注入した場合には、そうでない場合よりも高効率にオゾンを洗浄水中へ溶解できる。
図8は本発明の実施の形態2の一実施例を示すブロック図である。図3に対して、以下のとおり構成が追加されている。オゾンガスを貯蔵できるオゾンガス貯蔵槽17がオゾンガス配管16を介してオゾン発生器4とオゾン混合槽5の間に設置されている。さらに、オゾンガス貯蔵槽17とオゾン発生器4が酸素ガス配管18を介して接続されている。
図示していないが、例えばオゾン水循環配管53に設置したオゾン濃度計で、所定の濃度、例えば10mg/Lの濃度が計測されたオゾン水を洗浄水として作成しておき、逆洗のタイミングで洗浄水供給ポンプ8を使用して、オゾン水配管14を介して、高濃度のオゾン水を膜ろ過分離装置2に供給して逆洗を実施する。オゾン混合槽5で溶解せず、排オゾンガス配管を通ったオゾンガスは触媒により、無害な酸素に分解されて大気に放出される。あるいは、排オゾンガスを分解せずに、被処理水槽1もしくは洗浄水槽3に注入することも可能である。
以上に説明したように、濃縮したオゾンガスを使用しているため、十分に高濃度のオゾン水、すなわち、濃度としては例えば3mg/L以上の高濃度オゾン水を生成でき、これを使用することで膜を効率的に洗浄することが可能となる。なお、エジェクタ52を介さずにポンプでオゾンガス貯蔵槽17に貯蔵されたオゾンガスを取り出して、オゾン混合槽5の下部から散気装置等を介してバブリングして供給してもよく、この場合にも上記と同様の効果が得られる。
図12は本発明の実施の形態3の一実施例を示すブロック図である。図3に対して、以下のとおり構成が追加されている。酸貯留槽19が酸供給配管21を介してオゾン水配管14に接続されている。さらに、酸貯留槽19とオゾン水配管14の間の酸供給配管21上に酸供給ポンプ20が設置されている。
図13は本発明の実施の形態4の一実施例を示すブロック図である。図3に対して、以下のとおり構成が追加されている。膜接続配管11に排オゾンガス配管23が接続され、排オゾンガス配管23を介して圧力逃がし弁28、および排オゾンガス処理設備24が順に設置されている。
圧力逃がし弁28は開と閉の時間を設定して、自動で弁の開閉を調整する。もしくは、圧力計9の値で制御することも可能である。圧力の上限および下限を設定し、圧力が上限に達したら圧力逃がし弁28を開放し、下限に達したら圧力逃がし弁28を閉じる。もしくは、圧力逃がし弁28に、安全弁等予め定められた圧力まで上昇したときに弁が開く構造の弁を使用してもよい。
図14は本発明の実施の形態5の一実施例の装置構成の一部を示すブロック図である。
図1もしくは図3、あるいは図8に対して、以下のとおり構成が追加されている。膜接続配管11はヘッダー25に接続され、ヘッダー25には、第一の膜接続配管26および第二の膜接続配管31それぞれが接続されている。第一の膜接続配管26および第二の膜接続配管31は膜ろ過分離装置2内で繋がっている。膜接続配管26と第二の膜接続配管31は、膜モジュールである膜ろ過分離装置2の対をなす位置に設置することが好ましい。オゾンは膜モジュール内のファウリング物質と反応して消費されるため、膜ろ過分離装置2の対をなす位置からオゾン洗浄水を供給することで、膜ろ過分離装置内のオゾン水濃度を均一化できる。また、ヘッダー25は膜接続配管26と第二の膜接続配管31から膜ろ過分離装置2へ流入するオゾン洗浄水を均一に分配する働きを持つ。
図16は本発明の実施の形態6の一実施例の装置構成の一部を示すブロック図である。
本実施の形態は、膜ろ過分離装置が上下2段に分かれている。そして、図1もしくは図3、または図8に対して、以下のとおり構成が追加されている。上段の膜ろ過分離装置2p、下段の膜ろ過分離装置2qにはそれぞれ上段の膜接続配管11pおよび下段の膜接続配管11qが接続されている。上段の膜接続配管11pからは第二の膜接続配管31が上述のように分岐しており、第二の膜接続配管31には洗浄水調整弁32が取付けられている。第二の膜接続配管31の先端は上段の膜ろ過分離装置2pの下部にあり、オゾン水供給器44が複数個取付けられている。このオゾン水供給器44はオゾン洗浄水を膜ろ過分離装置2pの下部から膜ろ過分離装置2pに供給する役割を持ち、被処理水槽1に注入されると圧力が低下してオゾンを含む気泡が発生する。さらに、被処理水槽1の下段の膜ろ過分離装置2qの下部に散気装置41が設置され、空気供給配管42を介してブロワー43に接続されている。
図17は本発明の実施の形態7の一実施例の装置構成の一部を示すブロック図である。
図17はMBRの処理フローであり、被処理水槽1内の系列Aに8つの膜ろ過分離装置2a~2hが設置され、それぞれに膜接続配管11a~11hが接続されている。本図には記載していないが、それぞれの膜接続配管11a~11hの先には図1もしくは図3、または図8で示した構成と同様のろ過設備および逆洗設備が接続されている。また、逆洗用の水として洗浄水にオゾンガスを溶解させたオゾン洗浄水を使用してもよい。さらに本実施の形態では、下水量が変動して増加した場合、あるいは有機物等の濃度が高くなって水質負荷が高くなった場合には、被処理水槽1に投入できる膜ろ過分離装置2の数はスペースの関係上、限りがあり、その結果、膜面積が不足して、必要なフラックスが得られないため、同様の構成で系列Bを設ける。この系列Bは、系列Aと並列に設置されており、両方もしくは片方のみを使用することができる。なお本図には2系列しか示していないが、少なくとも二つ以上の系列で実施することが可能であり、例えば3系列でもよい。なお、水量に応じて系列数を変動させる方法も実施可能である。
逆洗水として洗浄水にオゾンガスを溶解させたオゾン洗浄水(濃度13~15mg/L)を使用し、逆洗水量として380mLを使用した。本実施例1は図3に示したブロック図で実施した。本実施例1では逆洗時に膜ろ過分離装置2から大量のオゾンを含有する気泡が発生した。
逆洗水として洗浄水にオゾンガスを溶解させたオゾン洗浄水(濃度13~15mg/L)およびシュウ酸水溶液(濃度1000mg/L)を使用し、逆洗水量としてそれぞれ190mLを使用した。本実施例2は図12に示したブロック図で実施した。本実施例2では逆洗時に膜ろ過分離装置2から大量のオゾンを含有する気泡が発生した。
逆洗水として洗浄水に次亜塩素酸ナトリウムを溶解させた次亜塩素酸ナトリウム水溶液(濃度6000mg/L)を使用し、逆洗水量として380mLを使用した。図19に次亜塩素酸ナトリウム水溶液を用いて逆洗するブロック図を示す。12%次亜塩素酸ナトリウム水溶液を貯留した次亜塩素酸ナトリウム原水槽404が次亜塩素酸ナトリウム供給配管403を介して次亜塩素酸ナトリウム水溶液調整槽402に接続されている。また洗浄水槽が洗浄水配管13を介して次亜塩素酸ナトリウム水溶液調整槽402に接続されている。さらに洗浄水供給ポンプ8と次亜塩素酸ナトリウム水溶液調整槽402が次亜塩素酸ナトリウム水配管405を介して接続され、洗浄水供給ポンプ8と切替弁10とが接続されている。なお、洗浄水配管13には、洗浄水用弁401が設置されている。その他の構成は図3と同様である。
逆洗水として洗浄水にオゾンガスを溶解させたオゾン水(濃度2mg/L)を使用し、逆洗水量として380mLを使用した。図20に本比較例のオゾン水を用いて逆洗するブロック図を示す。オゾン混合槽5には排オゾンガス配管23を介して排オゾンガス処理設備24に接続されている。洗浄水供給ポンプ8は切替弁10とオゾン混合槽5の間に配置され、オゾン水配管14で接続されている。また洗浄水供給ポンプ8はオゾン水と接触するため、オゾン耐性のあるポンプを使用している。また、オゾン水配管14、切替弁10、膜接続配管11、圧力計9、膜ろ過分離装置2もオゾン耐性がある。その他の構成は図3と同様である。
ここで、R:膜ろ過抵抗(m-1)、ΔP:膜間差圧(Pa)、J:膜透過水フラックス(m/日)、μ:膜透過水の粘性係数(Pa・s)である。
さらに、表1に示した条件において、図8で示したオゾンガスを濃縮した場合について、オゾンガス濃度依存性を評価した結果を図23~図25に示す。なお、オゾンガス濃度220g/m3以上の場合にオゾンガスを濃縮した。さらに逆洗水として処理水を使用し、処理水のオゾン注入率(単位処理水量当たりのオゾン注入量)を85mg/Lとした。
2a 系列Aの第一の膜ろ過分離装置、2b 系列Aの第二の膜ろ過分離装置、2c 系列Aの第三の膜ろ過分離装置、2d 系列Aの第四の膜ろ過分離装置、2e 系列Aの第五の膜ろ過分離装置、2f 系列Aの第六の膜ろ過分離装置、2g 系列Aの第七の膜ろ過分離装置、2h 系列Aの第八の膜ろ過分離装置、2p 上段の膜ろ過分離装置、2q 下段の膜ろ過分離装置、11a 系列Aの第一の膜接続配管、11b 系列Aの第二の膜接続配管、11c 系列Aの第三の膜接続配管、11d 系列Aの第四の膜接続配管、11e 系列Aの第五の膜接続配管、11f 系列Aの第六の膜接続配管、11g 系列Aの第七の膜接続配管、11h 系列Aの第八の膜接続配管、11i、11j1 膜接続配管、11p 上段の膜接続配管、11q 下段の膜接続配管。
Claims (10)
- 膜ろ過処理した清澄な水を加圧して洗浄水とし、
この洗浄水にオゾンガスを注入してオゾン洗浄水を生成し、
膜ろ過の際のろ過水の出口側であるろ過二次側から、前記オゾン洗浄水を膜ろ過用の膜に供給して、前記膜の内部を洗浄するとともに、
膜ろ過の際の未処理水の入り口側であるろ過一次側でオゾンを含有する気泡を発生させ前記ろ過一次側の前記膜の表面を洗浄することを特徴とする膜を用いた水処理方法。 - 前記膜と前記オゾン洗浄水中に残留する未溶解のオゾンガスあるいは酸素を排気するための排オゾンガス設備との間に設置した、前記オゾン洗浄水の圧力を下げる圧力逃がし弁を用いて、前記オゾン洗浄水の圧力を下げることを特徴とする請求項1に記載の膜を用いた水処理方法。
- 前記膜を洗浄する際に、前記オゾン洗浄水の供給圧力を変動させることを特徴とする請求項1または請求2に記載の膜を用いた水処理方法。
- 洗浄水槽に前記洗浄水を貯蔵するとともに、
膜ろ過処理されていない未処理水に含まれる異物と前記ろ過水とを分離する膜ろ過分離装置に接続された膜接続配管を通じて前記膜まで、貯蔵した前記洗浄水を送る場合に、前記膜接続配管に設置された圧力計により前記洗浄水の圧力を測定し、
この圧力が予め定めた圧力に達した後に、前記オゾン洗浄水の生成を行って逆洗処理を開始することを特徴とする請求項1に記載の膜を用いた水処理方法。 - 貯蔵したオゾンガスを前記洗浄水に注入することを特徴とする請求項1または請求項4に記載の膜を用いた水処理方法。
- 前記オゾン洗浄水で膜の内部を洗浄する前もしくは後に前記洗浄水に酸を添加して、前記ろ過二次側から前記膜に前記酸が添加された洗浄水を供給し、前記膜を洗浄することを特徴とする請求項1から5のいずれか1項に記載の膜を用いた水処理方法。
- 膜ろ過処理されていない未処理水に含まれる異物と膜ろ過したろ過水とを分離する膜ろ過分離装置と、
通常の膜ろ過とこの通常の膜ろ過とは逆方向の洗浄である逆洗とを切替える切替弁と、
膜ろ過処理した清澄な水を加圧して洗浄水とし、この洗浄水にオゾンガスを溶解させたオゾン洗浄水を生成し、前記膜ろ過分離装置に前記オゾン洗浄水を供給する配管に接続されたオゾン溶解部と、
このオゾン溶解部に配管を介して接続され、前記洗浄水を供給する洗浄水供給ポンプと、
前記オゾンガスを前記オゾン溶解部に供給するオゾン発生器と、
を備え、
前記切替弁を通常の膜ろ過の方向と切り替えることにより、前記オゾン洗浄水を膜ろ過用の膜に、逆洗により供給して、前記膜を洗浄することを特徴とする膜を用いた水処理装置。 - 前記オゾン発生器と前記オゾン溶解部との間に前記オゾンガスを貯蔵するオゾンガス貯蔵部を備えたことを特徴とする請求項7に記載の膜を用いた水処理装置。
- 前記洗浄水に酸を添加する構成要素を備え、通常の膜ろ過とは逆方向の洗浄である逆洗の際、膜ろ過用の膜に前記酸を添加した洗浄水を供給して前記膜を洗浄することを特徴とする請求項7または請求項8に記載の膜を用いた水処理装置。
- 前記膜ろ過分離装置に接続され、この膜ろ過分離装置と前記切替弁の間に設置されて、前記逆洗の際、前記膜ろ過分離装置に加圧したオゾン洗浄水を送るための膜接続配管と、
この膜接続配管に接続され、前記オゾンガスの圧力を調整する圧力逃がし弁と、
前記加圧したオゾン洗浄水に未溶解のオゾンガスを排気して酸素に分解する排オゾンガス処理設備と、
を備えたことを特徴とする請求項7から9のいずれか1項に記載の膜を用いた水処理装置。
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JP7120496B1 (ja) * | 2022-01-31 | 2022-08-17 | 三菱電機株式会社 | 濾過膜洗浄装置、水処理装置及び濾過膜洗浄方法 |
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