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WO2000027510A1 - Methode de filtration sur membrane - Google Patents

Methode de filtration sur membrane Download PDF

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Publication number
WO2000027510A1
WO2000027510A1 PCT/JP1999/006227 JP9906227W WO0027510A1 WO 2000027510 A1 WO2000027510 A1 WO 2000027510A1 JP 9906227 W JP9906227 W JP 9906227W WO 0027510 A1 WO0027510 A1 WO 0027510A1
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WO
WIPO (PCT)
Prior art keywords
ozone
filtration
water
membrane
amount
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/JP1999/006227
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English (en)
Japanese (ja)
Inventor
Takehiko Otoyo
Toru Ota
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Asahi Kasei Corp
Asahi Chemical Industry Co Ltd
Original Assignee
Asahi Chemical Industry Co Ltd
Asahi Kasei Kogyo KK
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Asahi Chemical Industry Co Ltd, Asahi Kasei Kogyo KK filed Critical Asahi Chemical Industry Co Ltd
Priority to AU10795/00A priority Critical patent/AU1079500A/en
Publication of WO2000027510A1 publication Critical patent/WO2000027510A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • 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
    • 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
    • B01D61/145—Ultrafiltration
    • 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
    • B01D61/147—Microfiltration
    • 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
    • B01D61/16—Feed pretreatment
    • 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
    • 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
    • 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
    • B01D2311/04—Specific process operations in the feed stream; Feed pretreatment

Definitions

  • the present invention relates to a membrane filtration method using ozone in the field of water treatment such as water supply, sewage, industrial wastewater, domestic wastewater, and human wastewater.
  • Typical treatment methods for conventional water purification treatment include coagulation sedimentation-sand sand filtration-chlorine disinfection, coagulation sedimentation-sand filtration-activated carbon-chlorine disinfection or coagulation sedimentation-sand filtration-ozone-activated carbon-chlorine disinfection.
  • Typical treatment methods for the discharge and reuse of sewage such as human waste and domestic wastewater or industrial wastewater are as follows: first settling tank-aeration-final settling tank-chlorination, first settling tank-aeration. One final sedimentation basin, one coagulation sedimentation, one sand filtration and one chlorine disinfection have been performed.
  • water sources such as water storage dams are being developed as countermeasures against water due to increased demand for domestic water, disorderly deforestation, and abnormal weather.
  • the quality of water sources has deteriorated, and it has become impossible to obtain good drinking water with the conventional methods as described above, which has become a serious problem.
  • sewage such as human waste and domestic wastewater or organic wastewater from factories is discharged after removing various suspended substances and organic components contained by the above-mentioned method.
  • attention has been paid to environmental issues, and such effluents are required to be treated to improve water quality even higher.
  • it has been proposed to reuse sewage and wastewater as water resources for effective use of water For example, various uses are considered, such as park fountains and scenic landscapes, water for water use, miscellaneous water, industrial water, etc. Sewage and drainage have begun to be actually used, especially for landscape views and water for hydrophilic use.
  • the organic matter in the raw water clogs the membrane or is adsorbed by the network inside the membrane, so the filtration flux of the resulting membrane is a fraction of the filtration flux of the clear water. It decreased to several tenths, the membrane filtration cost increased, and the practicality was low from an economic viewpoint.
  • Japanese Patent Application Publication No. Hei 4-110185 proposes performing tangent filtration by adding ozone as an oxidizing gas upstream of the membrane to prevent clogging of the membrane.
  • an oxidizing gas such as ozone as described above, the permeation flux at the time of membrane filtration is several times larger than when ozone is not used, and the installation area of the filtration membrane is reduced and water treatment is performed.
  • the economics for the project are also improved.
  • ozone a great deal of electricity is required to generate ozone, so it is important from an economic point of view how to use the generated ozone effectively.
  • the ozone concentration of the raw water is controlled to a predetermined value.However, in this method, the clarity of the raw water fluctuates, the required amount of ozone decreases, and excessive When ozone was added, the required amount of ozone increased, and the clogging of the membrane gradually progressed, so that a predetermined permeation flux could not be obtained. In addition, excessive addition of ozone was not only economically disadvantageous, but also caused problems such as blocking of activated carbon used in a later step and death of biological activated carbon organisms.
  • An object of the present invention is to perform a high-level treatment of purified water and an advanced sewage by using a membrane. In this case, it is possible to obtain a sufficient quality of treated water, and to effectively use ozone to reduce the amount of added ozone. It is an object of the present invention to provide a practical filtration method for obtaining a high filtration flux.
  • the present invention is a.
  • the amount of ozone to be injected into raw water based on the value of the permeation flux, membrane module inlet pressure or average transmembrane pressure during filtration or backwashing
  • the method comprising controlling It is.
  • FIG. 1 is a flowchart showing an example of the filtration method of the present invention.
  • FIG. 2 is a diagram showing one embodiment of the filtration method of the present invention.
  • FIG. 3 is a diagram showing another embodiment of the filtration method of the present invention.
  • FIG. 4 is a diagram showing another embodiment of the filtration method of the present invention.
  • FIG. 5 is a diagram showing another embodiment of the filtration method of the present invention.
  • the present invention relates to a method of adding ozone to raw water and then performing filtration using a filtration membrane, wherein the ozone is injected into the raw water.
  • the raw water referred to in the present invention is river water, underground water, lake water, lake water, storage water, groundwater and other clean water, human waste water, sewage primary treatment water, sewage secondary treatment water, industrial wastewater, domestic wastewater, pools, baths, Water storage in a water tank for raising aquatic animals, pulp and paper production wastewater, leachate landfill leachate, and the like.
  • the ozone to be added may be ozone alone, ozonized air, or ozone-dissolved water.
  • Ozone is introduced through an ejector, a line mixing method, a diffuser tube, a U-tube, or the like.
  • the source of ozone may be air or oxygen.
  • oxygen it may be oxygen produced by pressure-casing adsorption (PSA) or may be made from liquefied oxygen.
  • PSA pressure-casing adsorption
  • the filtration method using a membrane may be a cross-flow filtration method (circulation filtration method) or a dead-end filtration method (total filtration method).
  • Membrane filtration methods include constant flow filtration and constant pressure filtration. Either method may be used, either the pressurizing method or the depressurizing method may be used, and the external pressure method or the internal pressure method may be used.
  • a method of filtering by allowing ozone to be present up to the membrane surface, or a method of consuming ozone before the filtration treatment by the membrane and then performing filtration may be used.
  • the best method can be selected depending on the condition of the raw water.
  • ozone can be decomposed by adding a reducing agent such as sodium thiosulfate or activated carbon treatment, for example, by installing a retention tank to remove ozone before the filtration process.
  • De-ozone treatment such as, may be performed.
  • ozone passing through the membrane repeatedly attacks the organic substances attached to the membrane, so that the membrane is always self-cleaned and filtered. As a result, a higher permeation flux can be obtained.
  • the concentration of ozone added to raw water to kill microorganisms and remove odorous substances is generally 0.5 ppm or more, depending on the quality of raw water. If the ozone concentration is too high, the economic efficiency is reduced. Therefore, ozone having a concentration of preferably about 0.05 to 50 ppm, more preferably 0.1 to 30 ppm is added.
  • addition of hydrogen peroxide, ultraviolet irradiation, or a promoted oxidation catalyst such as titanium oxide may be used in combination for the purpose of enhancing the oxidizing power of ozone and promoting accelerated oxidation.
  • control of the amount of ozone added to the raw water to an appropriate value is performed based on the permeation flux, the pressure at the membrane module inlet, or the average transmembrane pressure during filtration or backwashing described below.
  • ozone when controlling the amount of ozone to be injected based on the value of the permeation flux at the time of filtration or backwashing at constant pressure filtration, if the permeation flux value falls below a preset value, ozone Increase the amount of ozone added, and in the opposite case reduce or stop adding ozone.
  • the pressure at the membrane module inlet during filtration or backwashing When controlling the amount of ozone to be injected based on the value or the average transmembrane pressure, the value should be larger than the preset value of the membrane module inlet pressure or the value of the average transmembrane pressure. In such cases, increase the amount of ozone added, and in the opposite case, reduce or stop the addition of ozone.
  • Methods for controlling the amount of ozone to be added include, for example, detecting the absolute value or the rate of change of time with respect to the above-mentioned value, which is the basis for control, and adjusting the current or voltage of the ozone generator, or the amount of ozone at the inlet. Is adjusted. Although manual control is possible, it is practical and preferable to calculate the above value and feed it back as an ozone control signal to automatically control the injected ozone amount or concentration.
  • an ozone-resistant membrane is used in a process in which ozone is present up to the membrane surface, but in a process in which ozone is removed before the filtration treatment by the membrane, the membrane is used. You don't have to worry about ozone resistance.
  • the ozone-resistant membrane is not particularly limited as long as it is a filtration membrane that is not deteriorated by ozone.
  • examples thereof include an inorganic membrane such as an ozone-resistant ceramic, a polyvinylidene fluoride (PVDF) membrane, and a polytetrafluoroethylene (PTFE) membrane.
  • Organic membranes such as a membrane, an ethylene-tetrafluoroethylene copolymer (ETFE) membrane, and a fluorine-based resin membrane such as a tetrafluoroethylene-perfluoroalkylvinylester copolymer (PFA) membrane can be applied.
  • PFA tetrafluoroethylene-perfluoroalkylvinylester copolymer
  • a polyolefin film such as a polyethylene film or a polypropylene film, a polysulfone film, a polyacrylonitrile film, a cellulose acetate film, a polycarbonate film, a polyamide film, etc., in addition to the film of the above materials, Can be applied.
  • Examples of the shape of the membrane include a flat membrane, a spiral membrane, a pleated membrane, a hollow fiber membrane, and a tubular membrane, but a hollow fiber membrane is preferred.
  • the pore size of the membrane As the pore size of the membrane, the pore size range of the ultrafiltration (UF) membrane to the microfiltration (MF) membrane can be used, but the microfiltration (MF) membrane is used because the permeation flux of the membrane is basically high.
  • the pore size of the membrane is preferably from 0.001 to 1 ⁇ , and from 0.05 to 1 ⁇ m.
  • the pore size of the membrane When performing membrane filtration, when the pore size of the membrane is in the microfiltration (MF) region, the pore size increases, and suspended substances (SS) and bacteria in the raw water enter the membrane. Therefore, in the case of raw water with a high concentration of suspended solids and bacteria, a high permeation flux will require many ozone injections.
  • a coagulant such as polyaluminum chloride (PACL), bansulfate, ferrous chloride and ferric chloride, and an adsorbent such as activated carbon can be used prior to ozone addition.
  • PCL polyaluminum chloride
  • adsorbent such as activated carbon
  • the flocculant and the adsorbent may be added to an ozonated water tank that stores raw water, or may be added by a line mixing method in a pipe that guides raw water to a place where ozone is added.
  • the amount of the flocculant added must be such that the suspended solids contained in the raw water can be flocculated, and generally 1 to 100 mg per liter of the raw water, and more preferably. Is 2 to 5 O mg per liter of raw water.
  • the membrane module used is selected from known internal pressure type modules and external pressure type modules.
  • the external pressure type module for example, a module having a module structure as described in WO97108993 can be used.
  • Backwashing backwashing
  • air publishing are effective physical cleaning methods.
  • Backwashing is a method in which filtration is stopped for a certain time, filtration is stopped, and washing is performed by flowing a washing solution from the permeate side of the membrane. It is preferable to use filtered water that has passed through the membrane as the washing liquid.
  • Air bubbling After filtration for a certain period of time, filtration is stopped, gas is sent to the membrane surface, and the membrane is washed by vibrating the membrane surface.
  • ozone present on the membrane surface, the organic substances adsorbed on the membrane surface are decomposed by ozone and become non-adsorbent, and thus block the pores of the membrane.
  • Non-adsorbent substances organic and inorganic substances
  • Air bubbling is very effective as a method of cleaning the membrane.
  • Air publishing may be used in combination with backwashing, followed by filtration and air bubbling-backwashing, or filtration and backwashing and air bubbling, or filtration (backwashing at the same time as vacuuming). You may.
  • the air bubbling time is preferably from 1 second to 6 minutes. If it is shorter than 1 second, the effect of air-bubbling is reduced, and if it is longer than 6 minutes, filtration is not performed during air bubbling, and the amount of filtered water is undesirably reduced.
  • FIG. 1 is a flowchart showing an example of the filtration method of the present invention.
  • ozone is added to raw water 1 to perform ozone treatment 2, and suspended substances and organic substances in the raw water 1 are decomposed by ozone.
  • the permeation flux, the membrane module inlet pressure or the average transmembrane pressure difference is detected, and the amount of ozone injected into the raw water is controlled based on the detected values.
  • the permeation flux can be measured by measuring the amount of filtrate permeated through the membrane or the backwash water with a flow meter 16.
  • the pressure at the inlet of the membrane module can be measured by a pressure gauge 13 provided at the inlet of the membrane module at the time of filtration, and can be measured by the pressure gauge 15 at the time of backwashing.
  • the average transmembrane pressure is measured using a pressure gauge 13 provided at the membrane module inlet, a pressure gauge 14 provided at the membrane module circulating water outlet, and a pressure gauge provided at the membrane module filtration water outlet. It is a value calculated from the pressure measured in 15 by the following formula.
  • the average transmembrane pressure is a value calculated by the following formula.
  • Fig. 1 shows only the basic process.
  • a treatment such as an activated carbon treatment or a reverse osmosis membrane treatment may be performed at a subsequent stage.
  • the ozonized air generated by the ozone generator 4 is added to the raw water 1 by the ozone injection means (ejector 1) 5 and supplied to the ozonated water tank 6, and then the ozonized water is Is supplied to the membrane module 9 by the supply means (pump) 8 and filtered.
  • the ozonized water is Is supplied to the membrane module 9 by the supply means (pump) 8 and filtered.
  • filtration is performed by cross-flow filtration, raw water that does not pass through the filtration membrane is returned to the ozonated water tank 6 as circulating water as shown by a broken line in FIG.
  • all of the ozone-treated water supplied to the membrane module 9 permeates through the membrane, and the filtrate is stored in the filtrate tank 10.
  • the amount of ozone injected into the raw water is controlled based on one of the permeation flux, the inlet pressure of the membrane module, or the average transmembrane pressure.
  • a pressure gauge 13 at the raw water inlet a pressure gauge 15 at the filtered water outlet, a pressure gauge 14 at the circulating water outlet, and a flow meter 16 at the filtered water outlet of the membrane module 9 It can be provided.
  • 12 denotes a raw water supply means (pump)
  • 20 denotes a backwash pump
  • 21 denotes an activated carbon treatment tank.
  • the current or voltage of the ozone generator 4 is adjusted to change the ozone generation amount, thereby controlling the ozone addition amount or ozone concentration in the ejector 15.
  • the amount of ozone injected into the ejector 5 is increased, and when the permeation flux increases, ozone injection is stopped.
  • the injected ozone amount can be controlled by reducing the injected ozone amount in the ejector 5.
  • the amount of ozone injected into the ejector 15 increases, and conversely, if the pressure at the inlet of the filtration membrane decreases,
  • the amount of injected ozone can be controlled by stopping the injection of ozone or decreasing the amount of injected ozone in the ejector 15.
  • the amount of injection ⁇ zone in the ejector 15 increases, and conversely, if the inlet pressure of the filtration membrane decreases,
  • the amount of injected ozone can be controlled by reducing the ozone injection force and the injected ozone amount in the ejector 15.
  • raw water 1 is first supplied to an ozonated water tank 6, and Except for injecting ozonized air into a part (circulating water) of raw water extracted from the treated water tank 6 by the circulation means (pump) 7 and returning it to the ozone water treatment tank 6 again, There is no difference from the filtration method of 2.
  • ozone can be continuously injected into the circulating water from the ozonated water tank 6. The amount of injected ozone is controlled in the same manner as in the filtration method of FIG.
  • the circulating water amount of the pump 7 is preferably 0.2 to 10 times the supply amount of the raw water 1.
  • ozonized air is injected into the raw water 1 by the ejector 5, supplied to the ozonated water tank 6, and a part of the ozonized raw water is extracted by the pump 7 and mixed with the raw water 1.
  • ozonized air is injected again by the ejector 15 there.
  • Figure 5 shows an example of a process for removing ozone prior to filtration by a membrane.
  • the chemical Prior to supplying the ozonated water from the ozonated water tank 6 to the hollow fiber membrane module 9 via the pump 8, the chemical is added from the chemical tank 18 via the pump 17 while mixing with the static mixer 19. Removes ozone. Except for this point, it is the same as the filtration method of FIG.
  • an external pressure type module was prepared in which 1,800 hollow fiber membranes were accommodated in a PVC (polyvinyl chloride) casing having a diameter of 3 inches. This module has a membrane area of 7.0 m 2 and a clear water permeation flux of 1.8 m per hour. At this time, the module filtration pressure was 0.5 kgf / cm 2 .
  • the filtration was carried out by a constant permeation flux filtration of a cross flow system (circulation filtration system).
  • a cross flow system circulation filtration system
  • the ozone treated water tank 6 1.5 m 3 / h.
  • the ozonated water from the tank 6 via the pump 8 is supplied in an amount per hour 2.
  • the concentration of ozone remaining in the filtered water in the filtered water tank 10 was from 0.2 ppm to 0.3 ppm.
  • the activated carbon treatment tank used was designed so that LV was 25 OmZ days and SV was 1 O / Hr.
  • the injection of ozone is performed by calculating the difference between the initial setting value of the membrane module inlet pressure and the actual membrane module inlet pressure, feeding back the signal to the ozone generator 4, and automatically controlling the injected ozone amount. went.
  • Membrane module inlet 0. 80 kg / cm 2 an initial setting value of the pressure, to set the injection amount of ozone at that time 2. O g, each time the membrane module inlet pressure 0. 05 k gZc m 2 rises, The injected ozone volume was increased by 0.3 g, and when the membrane module inlet pressure was less than the initial set value, the operation was continued with the ozone injection reduced.
  • the filtration flux level was maintained at the initial value of 1.5 m / h for 2 months, during which time there was no increase in the pressure at the inlet of the membrane module.
  • the COD chemical oxygen demand
  • the turbidity was 0.02 °
  • Escherichia coli and general bacteria were not detected, and other items were drinking water. As well as meeting the criteria.
  • Example 2 Except for injecting a fixed amount of 2.0 g of ozonized air per hour into raw water 1 with ozone amount and not controlling the amount of added ozone, the same conditions as in Example 1 except for the cross-floor opening method (circulating filtration method) ) was performed. At this time, the residual ozone concentration in the filtered water was 0.3 to 0.3 ppm.
  • Example 1 filtration and backwashing and washing operations were repeated to perform air publishing.
  • the pressure at the inlet of the membrane module increased by 0.5 kg / cm 2 in two months.
  • the filtration was carried out by a constant permeation flux filtration of a cross flow system (circulation filtration system).
  • the raw water 1, to together is supplied in an amount per hour 1.
  • 5 m 3 from the ozone-treated water tank 6 withdrawn by a pump 7, the O Zon generator 4, Ozonated air was injected as an ozone amount of 2.0 g to 2.4 g / h through the ejector 15.
  • the ozonated water from the tank 6 via the pump 8 is supplied in an amount per hour 2.
  • 5 m 3 is taken out by the flux, back film ozonated water tank 6 by not ozonated water per hour 1 m 3, such to transmit.
  • the residual ozone concentration in the filtered water was 0.2 ppm to 0.3 ppm.
  • the activated carbon treatment tank used was designed so that LV was 25 OmZ days and SV was 1 O / Hr.
  • the permeation flux level was maintained at the initial value of 1.5 m / h for 2 months, and there was no increase in the membrane module inlet pressure during that time.
  • the COD (chemical oxygen demand) value was 0.4 mg / L
  • the turbidity was 0.02 degrees
  • Escherichia coli and general bacteria were not detected.
  • the standard for drinking water was sufficiently satisfied.
  • Raw water 1 has a turbidity of 10 degrees, a COD (chemical oxygen demand) value of 13 to 20 mg Z liter, a BOD (biological oxygen demand) value of 20 to 30 mg Z liter, and a secondary sewage water temperature of 25 ° C.
  • COD chemical oxygen demand
  • BOD biological oxygen demand
  • the filtration was carried out by a constant permeation flux filtration of a cross flow system (circulation filtration system).
  • the residual ozone concentration in the filtered water at this time is 0.1 to 0 Injecting ozone, the difference between the initial set value of the average transmembrane pressure and the actual average transmembrane pressure was calculated, and the signal was fed back to the ozone generator 4.
  • the initial setting of the membrane module differential pressure was set to 0.5 kg / cm 2 , and the amount of injected ozone was set to 10.0 g at that time. each time the differential pressure is increased 0. 05 k gZc m 2, the injection amount of ozone is increased by 0.
  • the filtration flux level was maintained at the initial value of 1. Om / hour for 2 months, and there was no increase in the average transmembrane pressure during this period.
  • Raw water 1 has a turbidity of 10 degrees, a COD (chemical oxygen demand) value of 13 to 20 mg liter, a BOD (biological oxygen demand) value of 20 to 3 OmgZ liter, and a water temperature of 25 ° C.
  • the raw water ⁇ ozone treatment ⁇ filtration treatment with an ozone resistant membrane was sequentially performed using the apparatus shown in Fig. 4.
  • the ozone generator 4 Into the water 1, the ozone generator 4, after the ozonized air per hour 10 g to 1 1. 5 g injected as amount of ozone through the Ezekuta one 5, the ozonated water tank 6 of the hourly 1. Om 3 It supplies an amount, extracting raw water from the ozone treated water tank 6 hour 4. 0 m 3 by the pump 7 and, after mixing with raw water in the raw water 1 supply line was injected ozone through the E Zekuta 5. Further, the ozonized water was supplied from the ozonated water tank 6 via the pump 8 to the same PVDF hollow fiber membrane module used in Example 1 at an initial module inlet pressure of 0.9 kg / cm 2. was supplied so as to, the module is taken out of the drainage in filtered water outlet pressure 0.
  • Injecting ozone is a method of calculating the difference between the initial value of the membrane permeation flux and the actual membrane permeation flux and feeding back the signal to the ozone generator 4 to automatically control the amount of ozone to be injected.
  • I went in. Set the initial value of the membrane permeation flux to 1.0 m 3 / hr and the amount of injected ozone at that time to 10.0 g, and inject ozone every time the membrane permeation flux decreases by 0.1 m 3 hr. The amount was increased by 0.3 g, and if the permeation flux exceeded the initial setting, the operation was continued with the ozone injection reduced.
  • the operating conditions were 2 Nm / hour after 10 minutes of filtration. This operation was repeated by supplying air from the lower part of the module, performing air bubbling for 60 seconds, and performing backwashing using backwater by the backwashing pump 20 for 20 seconds. During backwashing and air bubbling, the pump 8 was stopped and the automatic valve 11 was closed to stop the supply of raw water.However, the pump 7 and the ozone generator 4 were constantly operated, and the injection of ozone was continued. . In this case, 5. Om 3 of water per hour was withdrawn from the ozonated water tank 6 by the pump 7 and ozone was injected through the ejector 15.
  • the membrane module inlet pressure 0. 9Kg / cm 2
  • the average filter medium differential pressure is 0. 55 Kg / cm 2
  • the initial level of Wataruconnection can be maintained to 2 months, transparently flux drainage amount therebetween There was no decline.
  • the quality of the obtained drainage water was 0.05 ° C, the ⁇ 00 value was 12 mgZ liter, the BOD value was lmg, and the water quality was sufficient for landscape water and hydrophilic water.
  • Turbidity is 10 degrees as raw water 1
  • COD chemical oxygen demand
  • BOD biological oxygen demand
  • water temperature is 25
  • Raw water-> ozone treatment-de-ozone treatment-> filtration treatment using a membrane was sequentially performed using the secondary treatment water at ° C and the apparatus shown in Fig. 5.
  • Hollow fiber microfiltration (MF) made of HDPE (high-density polyethylene) with a pore diameter of 0.1 ⁇ m, an inner diameter of 0.7 stroke ⁇ , and an outer diameter of 1.25 mm0, prepared based on JP-A-3-42025 as a membrane A membrane was used.
  • An external pressure type module was prepared in which 1800 hollow fiber membranes were housed in a 3 inch diameter PVC (polyvinyl chloride) casing. This module has a membrane area of 7.0 m 2 and a clear water permeation flux of 1.8 m 3 per hour. Yule filtration pressure was 0. 5Kg f / cm 2.
  • the raw water 1, to the ozonated water tank 6, is supplied with monitor, the raw water from the ozonated water tank 6 hour 4. 0 in 3 withdrawn by the pump 7 in an amount per hour 0. 7 m 3, an ozone generator From 4, 10 g to 11 l / h of ozonized air were injected as an ozone amount via ejector 15. Further, the pump ozone treated water from the ozonated water tank 6 via the pump 8, prior to supply an amount per hour 0. 7m 3 to the hollow fiber membrane module manufactured by the HDPE, the Chio sulfate Natoriumu solution, from the tank 1 8 7 g was added per hour in terms of sodium thiosulfate while stirring and mixing with a static mixer 19 through 17. The drainage was drawn off at 0.7 m / h. At this time, the residual ozone concentration at the inlet of the membrane module was 0 ppm.
  • the injection of ozone is performed by calculating the difference between the initial setting value of the membrane module inlet pressure and the actual membrane module inlet pressure, feeding back the signal to the ozone generator 4, and automatically controlling the injection ozone amount.
  • I went.
  • the initial setting of the membrane module inlet pressure was set at 0.80 kgZc and the amount of injected ozone at that time was set at 10 Og, and the membrane module inlet pressure was 0.05 kg / cm. Each time it increased, the amount of injected ozone was increased by 0.3 g, and when the inlet pressure of the membrane module became less than the initial setting, the operation was continued with the injection of ozone decreased.
  • the operating conditions were 2 Nm / hour after 10 minutes of filtration.
  • the operation of supplying air from the lower part of the module, performing air publishing for 60 seconds, and performing backwashing with the backwash pump 20 using drainage for 20 seconds was repeated.
  • the pump 8 was stopped and the automatic valve 11 was closed to stop the supply of raw water.
  • the pump 7 and the ozone generator 4 were constantly operated, and the injection of ozone was continued.
  • the pump 17 for adding the sodium thiosulfate aqueous solution was also stopped at the same time.
  • the permeation flux level was 1.0 m / h, the initial value. For two months, during which time there was no increase in the membrane module inlet pressure.
  • the quality of the obtained drainage water is 0.05 degree, turbidity is 0.05 mg, COD (chemical oxygen demand) value is SmgZ litre, and 8 ⁇ 0 value is 1 111 8 / l, which is enough for landscape water and hydrophilic water The water quality was excellent.
  • Example 7 (invention)
  • the ozone injection is calculated by calculating the difference between the initial set value of the membrane module inlet pressure during backwashing and the actual membrane module inlet pressure during backwash, and the signal is fed back to the ozone generator 4 for injection.
  • the procedure was performed under the same conditions as in Example 1 except that the method was used to automatically control the amount of ozone.
  • the initial setting of the membrane module inlet pressure during backwashing is set to 1.60 kcm 2 , and the amount of injected ozone at that time is set to 2.
  • the COD (chemical oxygen demand) value was 0.4 mg / L
  • the turbidity was 0.02 degrees
  • E. coli and general bacteria were not detected.
  • the items also fully satisfied the criteria for drinking water.
  • the injection of ozone is calculated by calculating the difference between the initial setting of the average transmembrane pressure difference during backwashing and the actual average transmembrane pressure difference during backwashing, and the signal is fed back to the ozone generator 4 for injection.
  • the procedure was performed under the same conditions as in Example 4, except that the method was used to automatically control the amount of ozone.
  • the initial setting value of the average transmembrane pressure during backwashing 0. 5 5 k gZc m 2, to set the injection O zone down amount at that time to 1 0. 0 g, the film between the average pressure difference at the time of backwashing 0. every time 05 kg Roh cm 2 rises, if the injection amount of ozone is increased by 0. 3 g, an average transmembrane pressure during backwashing is less than the initial set value, reduce the injection of ozone And continued driving.
  • the filtration flux level was maintained at the initial value of 1.0 m 3 / h for 2 months, and there was no increase in the average transmembrane pressure during this period.
  • the water quality of the obtained drainage water was 0.05 ° C, the COD value was 12 mgZ liter, the BOD value was 1 mgZ liter, and the water quality was sufficient for landscape water and hydrophilic water.
  • Example 9 (invention)
  • the ozone injection is calculated by calculating the difference between the initial set value of the membrane permeation flux during backwashing and the actual membrane permeation flux during backwashing, and the signal is fed back to the ozone generator 4 for injection.
  • the procedure was carried out under the same conditions as in Example 5, except that the method was used to automatically control the amount of ozone.
  • the initial setting of the membrane permeation flux during backwashing 1. 5 m 3 hr, to set the injection amount of ozone when its 1 0. 0 g, membrane permeation flux during backwashing 0. lm 3 / hr reduced
  • the amount of injected ozone was increased by 0.3 g, and when the membrane permeation flux during backwash exceeded the initial set value, the operation was continued with the injection of ozone decreased.
  • the inlet pressure of the membrane module was 0.9 kg / cm 2
  • the average transmembrane pressure was 0.55 kg / cm 2
  • the initial level could be maintained for 2 months. None.
  • the water quality of the obtained drainage water was 0.05 degree, the COD value was 12 rag / liter, and the BOD value was 1 mgZ liter, which was sufficient for landscape water and hydrophilic water.
  • the present invention relates to a filtration method capable of obtaining a sufficient treated water quality and a filtration flux without depending on the properties of raw water, the type and content of organic matter, in performing advanced treatment of purified water and advanced treatment of sewage using ozone. Can be provided.
  • the amount of ozone injected can be controlled while monitoring the filtration status.Therefore, it is necessary to maintain a high filtration flux with a small amount of ozone added. Can be. It is possible to provide long-term stable filtration by feeding back the monitored value and automatically controlling the process of adjusting the amount of ozone to be added.
  • the present invention can provide a practical and economical filtration method that does not require a special measuring device for control.

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  • Engineering & Computer Science (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Organic Chemistry (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Treatment Of Water By Oxidation Or Reduction (AREA)

Abstract

L'invention concerne une méthode de filtration sur membrane dans laquelle de l'ozone est ajoutée à une eau originale (1) pour traiter cette dernière à l'ozone (2) en vue de décomposer des substances suspendues et des substances organiques contenues dans l'eau originale. Un traitement par filtration (3) est ensuite effectué, qui consiste à réguler la quantité d'ozone devant être injectée dans l'eau originale sur la base d'un flux d'eau de perméation, d'une pression de l'orifice d'entrée d'un module à membranes ou d'une différence de pression moyenne entre membranes, pendant l'opération de filtration ou de rinçage. Cette régulation de la quantité d'ozone produit une qualité d'eau traitée satisfaisante et une utilisation efficace d'ozone. On obtient ainsi un débit élevé d'eau filtrée pour une faible quantité d'ozone ajoutée. Un flux d'eau de perméation et une pression de l'orifice d'entrée d'un module à membranes sont mesurés au moyen d'un débitmètre (16) et d'un manomètre (13 ou 15), respectivement, et une différence de pression moyenne entre membranes est calculée à partir des valeurs mesurées par les manomètres (13, 14 et 15).
PCT/JP1999/006227 1998-11-10 1999-11-09 Methode de filtration sur membrane Ceased WO2000027510A1 (fr)

Priority Applications (1)

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AU10795/00A AU1079500A (en) 1998-11-10 1999-11-09 Method for filtration with membrane

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JP10/319201 1998-11-10
JP31920198 1998-11-10

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Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2002028651A (ja) * 2000-07-17 2002-01-29 Mitsubishi Rayon Co Ltd 浄水処理システムおよび浄水処理方法
JP2005230730A (ja) * 2004-02-20 2005-09-02 Kurita Water Ind Ltd 水処理方法及び水処理装置
JP2007021408A (ja) * 2005-07-19 2007-02-01 Mitsubishi Rayon Eng Co Ltd 水処理装置及び方法
WO2010110065A1 (fr) * 2009-03-27 2010-09-30 メタウォーター株式会社 Procédé de production d'eau régénérée et système de production d'eau régénérée
US8158405B2 (en) 2008-06-30 2012-04-17 General Electric Company Process for concentrating and processing fluid samples
US8546127B2 (en) 2008-06-30 2013-10-01 General Electric Company Bacteria/RNA extraction device
AT516359A1 (de) * 2014-10-01 2016-04-15 Deltacore Gmbh Vorrichtung zur Filtration von Wasser mit einer Filteranordnung

Citations (4)

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Publication number Priority date Publication date Assignee Title
JPS5432179A (en) * 1977-08-15 1979-03-09 Ebara Infilco Co Ltd Controlling method for operation of fresh water making apparatus
JPS57194005A (en) * 1981-05-25 1982-11-29 Hitachi Plant Eng & Constr Co Ltd Method and device for cleaning of membrane separator
JPH0929070A (ja) * 1995-07-24 1997-02-04 Tohoku Electric Power Co Inc 水処理用膜分離装置
JPH09192459A (ja) * 1996-01-17 1997-07-29 Kubota Corp 浸漬型膜分離装置の洗浄方法

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5432179A (en) * 1977-08-15 1979-03-09 Ebara Infilco Co Ltd Controlling method for operation of fresh water making apparatus
JPS57194005A (en) * 1981-05-25 1982-11-29 Hitachi Plant Eng & Constr Co Ltd Method and device for cleaning of membrane separator
JPH0929070A (ja) * 1995-07-24 1997-02-04 Tohoku Electric Power Co Inc 水処理用膜分離装置
JPH09192459A (ja) * 1996-01-17 1997-07-29 Kubota Corp 浸漬型膜分離装置の洗浄方法

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2002028651A (ja) * 2000-07-17 2002-01-29 Mitsubishi Rayon Co Ltd 浄水処理システムおよび浄水処理方法
JP2005230730A (ja) * 2004-02-20 2005-09-02 Kurita Water Ind Ltd 水処理方法及び水処理装置
JP2007021408A (ja) * 2005-07-19 2007-02-01 Mitsubishi Rayon Eng Co Ltd 水処理装置及び方法
US8158405B2 (en) 2008-06-30 2012-04-17 General Electric Company Process for concentrating and processing fluid samples
US8546127B2 (en) 2008-06-30 2013-10-01 General Electric Company Bacteria/RNA extraction device
WO2010110065A1 (fr) * 2009-03-27 2010-09-30 メタウォーター株式会社 Procédé de production d'eau régénérée et système de production d'eau régénérée
JP2015024409A (ja) * 2009-03-27 2015-02-05 メタウォーター株式会社 再生水製造方法、及び再生水製造システム
US9028695B2 (en) 2009-03-27 2015-05-12 Metawater Co., Ltd. Process for producing reclaimed water and system for producing reclaimed water
AT516359A1 (de) * 2014-10-01 2016-04-15 Deltacore Gmbh Vorrichtung zur Filtration von Wasser mit einer Filteranordnung
AT516359B1 (de) * 2014-10-01 2021-06-15 Deltacore Gmbh Vorrichtung zur Filtration von Wasser mit einer Filteranordnung
EP3201139B1 (fr) * 2014-10-01 2023-04-12 Deltacore GmbH Dispositif et procede de filtration de l'eau

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