WO2000027756A1 - Procede de traitement de l'eau - Google Patents
Procede de traitement de l'eau Download PDFInfo
- Publication number
- WO2000027756A1 WO2000027756A1 PCT/JP1998/004980 JP9804980W WO0027756A1 WO 2000027756 A1 WO2000027756 A1 WO 2000027756A1 JP 9804980 W JP9804980 W JP 9804980W WO 0027756 A1 WO0027756 A1 WO 0027756A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- ozone
- membrane
- water
- filtration
- raw water
- Prior art date
Links
Classifications
-
- 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
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/025—Reverse osmosis; Hyperfiltration
-
- 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
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/027—Nanofiltration
-
- 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
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/04—Feed pretreatment
-
- 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
- B01D61/145—Ultrafiltration
- B01D61/146—Ultrafiltration comprising multiple ultrafiltration steps
-
- 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
-
- 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
-
- 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
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/283—Treatment of water, waste water, or sewage by sorption using coal, charred products, or inorganic mixtures containing them
-
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
-
- 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
-
- 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
- B01D2311/06—Specific process operations in the permeate stream
-
- 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
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- 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
- C02F1/008—Control or steering systems not provided for elsewhere in subclass C02F
-
- 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
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by 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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/02—Non-contaminated water, e.g. for industrial water supply
- C02F2103/04—Non-contaminated water, e.g. for industrial water supply for obtaining ultra-pure water
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/78—Details relating to ozone treatment devices
- C02F2201/782—Ozone generators
-
- 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
- C02F2209/003—Downstream control, i.e. outlet monitoring, e.g. to check the treating agents, such as halogens or ozone, leaving the process
Definitions
- the present invention is, advanced treatment of drinking water and sewage secondary treatment water, and a water treatment method for industrial water or waste water. More specifically, in a membrane filtration method for water using ozone, a method for stably and efficiently supplying filtered water having a constant high water quality c Background art Conventional typical water purification method First, chlorine or sodium hypochlorite is added to the raw water that has been withdrawn to oxidize and insolubilize iron and manganese, prevent the growth of microorganisms and other adverse effects in the purification process, and then remove suspended solids.
- a flocculant corresponding to the above is added, the suspended substance is flocculated and separated by sedimentation, the overflowed floc is separated in the next sand filtration step, and the raw water is clarified.
- membrane filtration if membrane filtration is continued, membrane clogging will occur and the membrane filtration flux will gradually decrease, so chemical cleaning must be performed periodically. In order to reduce the frequency of chemical cleaning as much as possible, it is necessary to set a force for performing a heavy pretreatment such as coagulation sedimentation or to set a low membrane filtration flux. limited. Furthermore, membrane filtration removes protozoa such as kryptosporidium contained in the raw water completely, and makes the filtrate safe.However, these parasites are concentrated in the concentrated wastewater generated at the time of membrane filtration. Therefore, strict attention is required for its disposal.
- US Pat. No. 5,271,830 and WO 97/10983 disclose injection of ozone upstream of a filtration membrane. It discloses a method of membrane filtration to prevent membrane clogging while improving water quality.
- it is necessary to inject a large amount of ozone in anticipation of fluctuations in the quality of the raw water, resulting in poor economic efficiency.
- by-products are generated, and ozone remaining in the filtrate reacts with activated carbon in a later step, for example, a step using activated carbon, to increase the load of activated carbon. Such undesired results.
- An object of the present invention is to provide a membrane filtration treatment of water using ozone, which maintains a high filtration flux even when the water quality of the raw water fluctuates, and stably filters water having a constant high water quality. It is to provide a method that can be obtained.
- Another object of the present invention is to provide a method for filtering water remaining in water by membrane filtration using ozone. It is an object of the present invention to provide a treatment method capable of keeping the ozone level low and effectively performing the subsequent water treatment.
- the concentration of ozone present in the filtrate passing through the ozone-resistant membrane is detected, and the ozone concentration is determined to be a predetermined value.
- the feature is that the amount of ozone injected into the raw water is continuously and automatically controlled so that the value becomes as follows.
- the filtrate Prior to treating the filtrate with a reverse osmosis membrane, the filtrate is blown off, the filtrate is treated with activated carbon, or sodium thiosulfate is added to the filtrate.
- FIG. 1 is a diagram showing a processing flow according to an embodiment of the present invention.
- FIG. 2 is a diagram showing a processing flow of another embodiment of the present invention.
- FIG. 3 is a diagram showing a processing port according to another embodiment of the present invention.
- FIG. 4 is a diagram showing a processing flow of another embodiment of the present invention.
- FIG. 5 is a graph showing the relationship between the ozone concentration of the filtrate permeating the ozone-resistant membrane and the membrane filtration flux in Example 1.
- BEST MODE FOR CARRYING OUT THE INVENTION The present invention is basically a water treatment method in which ozone is added to raw water and filtration is performed using an ozone-resistant membrane.
- 1 to 4 are examples of a water treatment flow showing an embodiment of the present invention.
- Fig. 1 shows the basic flow of detecting the ozone concentration of the filtrate passing through the ozone-resistant membrane using an ozone concentration measurement device and automatically controlling the ozone amount of the ozone generator.
- Fig. 2 shows the flow in the case of controlling the amount of ozone added to raw water in the water treatment process where the filtered water that has passed through the ozone-resistant membrane is further treated with an activated carbon treatment device.
- FIG. 3 shows a flow in the case where the amount of ozone added to raw water is controlled in a water treatment step in which filtrate filtered through an ozone-resistant membrane is further treated with a reverse osmosis membrane.
- FIG. 4 shows a flow in the case of adding a flocculant to raw water in the water treatment method of performing the activated carbon treatment of FIG. 2 or the reverse osmosis membrane treatment of FIG.
- the raw water referred to in the present invention is water subject to advanced treatment of water supply, secondary treatment of sewage, and wastewater treatment, such as river water, lake water, groundwater, storage, secondary sewage treatment water, and plant wastewater. .
- the amount of ozone added to raw water to improve water quality depends on the nature of the raw water and the purpose of water quality improvement, but the ozone concentration is in the range of 0.05 mgZ liter to 3 OmgZ liter. If the injection amount of ozone is too large, many by-products of oxidative decomposition due to ozone are generated, increasing the load on the subsequent by-product adsorption step, or manganese in raw water is overoxidized, and the membrane filtration method is used. It is not desirable because it cannot be removed effectively. It is not economical because excess ozone also increases. On the other hand, if the amount of injected ozone is too small, a sufficient water quality improvement effect cannot be obtained.
- the relationship between the amount of ozone injected into the raw water and the membrane filtration flux also differs depending on the raw water quality.
- the present inventors differ in the membrane filtration flux even when the same amount of ozone is injected into the same raw water when ozone remains on the filtration membrane surface and when ozone does not remain. It has been found that the filtration flux is high because the membrane surface is constantly washed.
- the relationship between the ozone concentration of the filtrate and the membrane filtration flux was examined under the condition that ozone remains in the filtrate (the ozone remains on the filtration membrane surface). As a result, it was found that the ozone concentration of the drainage and the membrane filtration flux had a relationship as shown in Fig. 5. That is, the membrane filtration flux is almost constant when the residual ozone of the filtrate is 0.3 mg / liter or more, and the membrane filtration flux greatly depends on the filtrate ozone concentration when the residual ozone is less than 0.05 mgZ liter. The change is steep.
- the ozone concentration of the filtrate is 0.3 mgZ liter or more, no further effect of increasing the membrane filtration flux can be expected, and if the ozone concentration is less than 0.05 mL, the change in the membrane filtration flux is large. It has been found difficult to obtain a stable drainage.
- the amount of ozone to be injected into raw water is continuously and automatically controlled so that the ozone concentration in the filtrate becomes a predetermined value.
- the raw water 1 is treated with ozone in the step of ozone treatment 2, and is subjected to membrane filtration in step 3 by an ozone-resistant membrane.
- the ozone concentration in the filtrate passing through the membrane is constantly measured by the ozone concentration measuring device 4.
- the ozone generation is performed so that the residual ozone concentration becomes a preset value in a range of, for example, 0.05 mg / L or more and less than 0.3 mg / liter.
- the amount of ozone supplied from the machine 5 to the ozone treatment process is automatically adjusted.
- an ultraviolet absorbance method, an electrode method, an iodine titration method, an indigible method, a fluorescence method, a coloring method, or the like can be used, but feedback control with high accuracy and in a short time can be performed.
- the preferred method is to do so.
- the measured value of the ozone concentration meter 4 is C P U
- the ozone generator 5 increases or decreases the generated ozone concentration by means for controlling the current or voltage of the ozone generator, for example.
- ozone added to raw water may be ozone alone or ozonized air.
- the introduction of ozone into the raw water may be carried out via an air diffuser installed in a reaction tower provided in front of the raw water tank or an air diffuser installed at an appropriate position in the raw water tank.
- a U-tube system can be used instead of a reaction tower using a diffuser tube.
- another configuration for adding ozone includes a pipe for guiding raw water to an ozone resistant membrane. On the way, ozone may be added by an ejector method or a line mixing method.
- a raw material for generating ozone in the case of discharge may be air or oxygen.
- ozone generated by electrolysis of water may be used.
- the ozone is supplied continuously into the raw water.
- Addition of ozone can kill microorganisms living in the raw water 1, such as viruses, bacteria, molds, and protozoa.
- suspended substances and organic substances in the raw water 1 can be decomposed, and at the same time, organic substances adhering to or clogged with an ozone-resistant membrane can be filtered while decomposing, so that an extremely high filtration flux can be obtained.
- the organic matter attached to the membrane is repeatedly attacked by the ozone passing through the membrane, so that the filtration is performed while the membrane is constantly self-cleaning. As a result, a high filtration flux is obtained. Obtainable.
- the membrane filtration device used in the present invention includes at least a tank or a tank for storing raw water (hereinafter referred to as a raw water tank), a membrane module, a means for sending raw water to the membrane module (such as a circulation pump), and a membrane filtration water.
- a tank or tank hereinafter referred to as a drainage tank
- a means for backwashing the membrane are provided.
- a line is provided to return raw water (circulating water) that does not pass through the membrane to the raw water tank.
- the ozone-resistant membrane is not particularly limited as long as it is a filtration membrane that is not deteriorated by ozone.
- an inorganic membrane such as a ceramic having ozone resistance, a polyvinylidene fluoride (PVDF) membrane, a polytetrafluoroethylene (PTF E) )
- PVDF polyvinylidene fluoride
- PPF E polytetrafluoroethylene
- a film an organic film such as a fluorine-based resin film such as an ethylene-tetrafluoroethylene copolymer (ETFE) film, a polyfluoroacrylate (PFA) film, or the like can be used. It is particularly preferable to use a polyvinylidene fluoride (PVDF) film.
- ozone-resistant membranes those whose pore size range is from ultrafiltration (UF) membrane to precision filtration (MF) membrane can be used, but basically a precision membrane with a high ⁇
- a filtration (MF) membrane is used.
- a membrane having an average pore diameter of 0.001 to 1 m is preferable, and a membrane having an average pore diameter of 0.05 to 1 m is more preferable.
- any shape such as a hollow fiber shape, a flat film shape, a pleated shape, a spiral shape, and a tubular shape can be used, and a hollow fiber shape having a large membrane area per unit volume is preferable.
- filtration is performed using a module containing a membrane.
- the filtration method may be either a full filtration method or a cross flow filtration method.
- the air or oxygen in the injected ozone gas is returned to the raw water tank together with the circulating water and separated into gas and liquid.
- the total filtration method it is necessary to remove unreacted gasified air that is present in the raw water side of the membrane module. For example, it is necessary to provide a gas-liquid separator above the membrane module.
- a pressure filtration method or a negative pressure filtration method may be used, but a pressure filtration method is preferable because a higher filtration flux can be obtained.
- Either internal pressure filtration or external pressure filtration may be used.
- the backwashing is performed using the filtrate permeated through the ozone-resistant membrane.
- Air bubbling may be used in combination with backwashing, or in the order of filtration and air bubbling-backwashing, or filtration and backwashing-air and bubbling or filtration (simultaneous backwashing with air and bubbling). You may go in order.
- air bubbling may be performed while flowing raw water at the same time, or may be performed without flowing raw water. Alternatively, these may be alternately combined.
- Air bubbling is preferably 1 second or more and 6 minutes or less. If the time is less than 1 second, the effect cannot be obtained, while if it exceeds 6 minutes, the time during which the filtration is stopped becomes longer, and the amount of the filtered water becomes longer. Less, not preferred.
- the activated carbon treatment device 6 generates trace organic matter contained in the filtered water that has passed through the ozone-resistant membrane, a biodegradable organic substance formed by reaction with ozone, or a reaction with ozone.
- the purpose is to obtain highly treated water, excluding by-products and the like.
- Activated carbon treatment specifically involves draining the permeated water through the ozone-resistant membrane into a tank containing granular activated carbon and performing post-treatment.
- biologically activated carbon biological activated carbon
- BAC biological activated carbon
- it is effective for removing easily decomposable organic substances generated by reacting humic substances with ozone.
- ozone concentration in the filtrate from the ozone-resistant membrane low for the following reasons. If the ozone concentration in the filtered water is high, the activated carbon reacts with ozone, and oxygen gas is generated, causing an airlock phenomenon, which increases the water flow resistance and prevents water flow. This is particularly noticeable at ozone concentrations above 1.0 mg / litre. Also, when the ozone concentration is high, the load of the activated carbon in the activated carbon treatment process increases. Furthermore, ozone can kill microorganisms in biological activated carbon.
- the ozone concentration in the drainage water is from 0.05 mg Z liter to 1.0 mg mg or less, more preferably from 0.05 mg zinc to 0.3 mg Z liter, and still more preferably. Should be in the range of 0.055 to 11.8 liters to 0.25 mg Z liters.
- deozonization of the filtrate is performed to protect the reverse osmosis membrane that does not have ozone resistance. It is desirable to carry out.
- a retention tank is provided, and the residual ozone is decomposed by removing the ozone from the drainage by means of a spike, a reducing agent such as sodium thiosulfate, or activated carbon treatment.
- a coagulation sedimentation-sand filtration method or the like is provided as a pretreatment as a turbidity removal method.
- the content value of the suspended substance contained in the pretreatment water of the reverse osmosis membrane, that is, the FI (filing index) value is set to 3 The following can be done, but it is still insufficient.
- the FI value can be set to 1 or less because the ozone-resistant film blocks suspended substances and microorganisms in the raw water 1. Therefore, in the case of the flow shown in Fig. 3, in which the filtered water that has passed through the ozone-resistant membrane is further treated with a reverse osmosis membrane, the filtered water that has always stable water quality regardless of the water quality fluctuation, water quantity fluctuation, and water temperature fluctuation of the raw water 1 Can be sent to reverse osmosis membrane.
- the membrane filtration method using an ozone-resistant membrane is basically used, the filtration flux is high and the efficiency is high, and as a result, the equipment cost of the entire process can be reduced.
- the membrane filtration treatment 8 using a reverse osmosis membrane can remove even highly hydrophilic organic substances such as polysaccharides which are not digested by microorganisms and are hardly adsorbed on activated carbon by the biological activated carbon treatment.
- the biological activated carbon treatment when the water temperature decreases, the biological activity decreases and the treatment capacity decreases.
- the use of a reverse osmosis membrane has the advantage that the temperature dependence is small.
- the reverse osmosis membrane is not particularly limited.
- a low-pressure reverse osmosis membrane or a nanofilter can be used. It is preferable to use a low-pressure reverse osmosis membrane or a nanofilter suitable for low-pressure treatment because the filtration operation pressure can be increased and the filtration flux can be increased.
- reverse osmosis membranes can also block micro-polyurethanes and inorganic salts such as soluble organic matter and pesticides, so that highly contaminated raw water or raw water with a high salt concentration can be used for drinking water or industrial water. It is effective when used.
- FIG. 4 illustrates a flow in the case of using a flocculant.
- the coagulant may be added to a storage tank such as a tank for storing the raw water 1, or may be added to an ozone-resistant film in the middle of a pipe for guiding the raw water 1 to a place where ozone is added or after ozone is added. May be added by a line mixing method in the middle of the tube for guiding the mixture.
- the pH of the raw water may be adjusted with a chemical solution or the like as necessary.
- the appropriate pH varies depending on the flocculant used, but the pH before, during or after the flocculant addition is between 2 and 8, preferably between 2 and 7.5.
- the chemical solution for adjusting ⁇ ⁇ may be added prior to or simultaneously with the addition of the flocculant using the same method as that for adding the flocculant (addition to raw water tank, line mixing method, etc.).
- the raw water is alkaline, it can be adjusted to a suitable acid with mineral acid such as hydrochloric acid, sulfuric acid, or nitric acid.
- the raw water is acidic, it can be adjusted to an appropriate ⁇ with sodium hydroxide or hydroxide hydroxide.
- the amount of the flocculant added must be such that the suspended solids contained in the raw water 1 can be flocculated. Generally, it is sufficient to add 1 to 100 mg to one liter of the raw water 1, and more preferably. In other words, 2 to 5 O mg may be added to one liter of raw water 1.
- Example 1 (the present invention)
- raw water 1 river surface water with turbidity of 3 to 4 degrees, chromaticity of 5 to 10 degrees, COD (chemical oxygen demand) of 6 to 8 mg / litre, and water temperature of 12 ° C is used.
- raw water 1-ozone treatment 2 ⁇ membrane filtration treatment 3 using an ozone-resistant membrane was sequentially performed.
- the ozone concentration of the filtrate that has passed through the ozone-resistant membrane is detected by the ozone concentration measuring device 4, and the amount of ozone generated from the ozone generator 5 is automatically increased / decreased via the CPU so that the value becomes a predetermined value. I let it.
- MF hollow fiber microfiltration
- PVDF polyvinylidene fluoride
- PVC polyvinyl chloride
- Filtration is performed by a cross-floor type, and the above-mentioned raw water 1 is supplied to the raw water tank, and constant pressure filtration is performed to supply the PVDF hollow fiber module to the PVDF hollow fiber module at a constant pressure by using a pump.
- the amount of circulating water was adjusted to be one-to-one.
- An ozone addition port of an ejector type was installed between the pump outlet and the module, and ozone was added using air as a raw material.
- the value of the ozone generation amount control signal from the ozone concentration measuring device 4 to the ozone generator 5 is set so that the ozone concentration of the filtrate that has passed through the ozone resistant membrane becomes a predetermined value, and the membrane filtration operation described above is performed. For 50 hours. The membrane filtration flux after 50 hours was measured, and the value obtained by dividing by the value of the clarified water flux at the same membrane filtration pressure was obtained, and the result of FIG. 5 was obtained.
- Example 1 the operation was performed so that the ozone concentration of the filtrate became 0.2 mg / liter, and the filtrate was passed through an activated carbon tank (flow in Fig. 2). Calgon F400 was used as activated carbon, and the design was such that the EB CT (superficial tower contact time) was 20 minutes.
- the filtered water of the ozone-resistant membrane had a turbidity of 0.02 °, a chromaticity of 2 ° or less, and a value of 4 to 5.5 mgZ liter.
- the water quality after the water was 0.02 ° turbidity, chromaticity of 1 ° or less, and a COD of 0.3 to 0.8 mg / litre.
- Example 3 the present invention
- raw water 1 As raw water 1, turbidity is 5 to 11 degrees, chromaticity is 18 to 20 degrees, COD is 20 to 30 mg norr, pH power, '7.2 to 7.6, water temperature is 23 to 25 °
- raw water 1—ozone treatment 2 ⁇ membrane filtration treatment 3 using an ozone-resistant membrane 3 was sequentially performed as in Example 1, using the sewage secondary treatment water C.
- the ozone concentration of the filtrate permeating the ozone-resistant membrane was set to 0.25 mgZ liter.
- the quality of the drainage water was turbidity of less than 0.1 degrees, chromaticity of less than 2 degrees, and COD of 6-8 mgZ liter. Further, a part of the filtrate was collected, and residual microorganisms were detected by a provisional test method for detection of the agar medium and Cribtosporidium. As a result, no survival was confirmed.
- the water treatment method of performing the reverse osmosis membrane treatment shown in Fig. 4 was performed. That is, raw water 1 ⁇ ⁇ ⁇ adjustment 9 ⁇ addition of flocculant 10-ozone treatment 2 membrane filtration treatment 3 with ozone-resistant membrane 3 was sequentially performed, and a part of the obtained filtrate was subjected to deozonization treatment 7. A membrane filtration treatment 8 using a reverse osmosis membrane was performed.
- the pH was adjusted by installing a static mixer in the middle of a line that supplies raw water to a raw water tank (not shown) in an ozone-resistant membrane filtration device, adding sulfuric acid using a pump, and adjusting the pH. 6. Adjusted to 2-6.5. Thereafter stage, the further the static mixer between the raw water tank is provided after the addition at a rate of 3 5 mg to raw water 1 liter ferric chloride (F e C 1 3) as a flocculant, O Dzon treatment was performed. The ozone concentration of the filtrate that has passed through the ozone-resistant membrane is detected by the ozone concentration measuring device 4, and the amount of ozone generated from the ozone generator 5 is determined via the CPU so that the value becomes 0.05 mg norr. Automatically increased or decreased.
- the quality of the filtered water that passed through the ozone-resistant membrane had a turbidity of 0.1 ° or less, a chromaticity of 1 ° or less, and a C0D of 4 to 6 mg Z liter.
- sodium thiosulfate was added to the filtrate of the ozone-resistant membrane at a ratio of 0.15 mg to 1 liter of raw water to decompose residual ozone.
- This aromatic polyamide composite membrane spiral type nanofilter had a NaC1 rejection of 65%, a MgC rejection of 50%, and a sucrose rejection of 99%.
- the aromatic polyimide composite membrane spiral type nanofilters were arranged in a two-stage cascade type, with a 70% drainage recovery rate, and operated for 2 months at a filtration pressure of 40 kPa. Stable operation was performed over the entire period, and a filtration flow rate of 5 m 3 Z days was obtained. The TOC (total organic carbon) removal rate was stable at 90-97% over the entire period, and the quality of the treated water obtained was sufficient for reuse.
- Example 5 (invention)
- Filtration was carried out using the raw water of Example 1 by a constant-pressure filtration method. That is, the same amount of water as that of the filtrate was supplied to the raw water tank, and a gas-liquid separator was provided above the membrane module. The method of adding ozone, the ozone resistant film used, and the operating conditions are the same as in Example 1.
- the amount of residual ozone in the filtered water can be kept low, and the subsequent water treatment can be performed effectively.
- a water treatment method that can obtain a high-quality treatment liquid with a compact system and does not generate harmful waste can be realized.
- treated water having good water quality is economically and stably supplied in advanced treatment of waterworks and sewage secondary treatment water, and industrial water or wastewater treatment. I can do it.
Landscapes
- 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)
- Nanotechnology (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Description
Claims
Priority Applications (7)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
KR10-2000-7007421A KR100384668B1 (ko) | 1998-11-05 | 1998-11-05 | 수처리 방법 |
AU97616/98A AU737042B2 (en) | 1998-11-05 | 1998-11-05 | Water treatment process |
US09/582,033 US6464877B1 (en) | 1997-05-08 | 1998-11-05 | Water treating method |
DE69828821T DE69828821T2 (de) | 1998-11-05 | 1998-11-05 | Wasserbehandlungsverfahren |
PCT/JP1998/004980 WO2000027756A1 (fr) | 1998-11-05 | 1998-11-05 | Procede de traitement de l'eau |
EP98951694A EP1044928B1 (en) | 1998-11-05 | 1998-11-05 | Water treating method |
CNB98812937XA CN1135206C (zh) | 1998-11-05 | 1998-11-05 | 水处理方法 |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
PCT/JP1998/004980 WO2000027756A1 (fr) | 1998-11-05 | 1998-11-05 | Procede de traitement de l'eau |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2000027756A1 true WO2000027756A1 (fr) | 2000-05-18 |
Family
ID=14209331
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP1998/004980 WO2000027756A1 (fr) | 1997-05-08 | 1998-11-05 | Procede de traitement de l'eau |
Country Status (7)
Country | Link |
---|---|
US (1) | US6464877B1 (ja) |
EP (1) | EP1044928B1 (ja) |
KR (1) | KR100384668B1 (ja) |
CN (1) | CN1135206C (ja) |
AU (1) | AU737042B2 (ja) |
DE (1) | DE69828821T2 (ja) |
WO (1) | WO2000027756A1 (ja) |
Cited By (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2000288587A (ja) * | 1999-03-31 | 2000-10-17 | Nkk Corp | し尿系汚水の処理方法および処理装置 |
KR100384668B1 (ko) * | 1998-11-05 | 2003-05-22 | 아사히 가세이 가부시키가이샤 | 수처리 방법 |
JP2007289940A (ja) * | 2006-03-29 | 2007-11-08 | Toray Ind Inc | 中空糸膜モジュールの洗浄方法 |
JP2009509737A (ja) * | 2005-09-30 | 2009-03-12 | オテヴェ・ソシエテ・アノニム | 高速沈降ステップと、続く精密濾過膜または限外濾過膜による直接の濾過ステップを含む水処理方法、および対応する装置 |
AU2002354050B2 (en) * | 2002-05-06 | 2009-10-29 | Debasish Mukhopadhyay | Method and apparatus for fluid treatment by reverse osmosis under acidic conditions |
WO2013055659A1 (en) * | 2011-10-11 | 2013-04-18 | Carter International, Llc | Produced water treatment process |
CN111807557A (zh) * | 2020-07-23 | 2020-10-23 | 上海城市水资源开发利用国家工程中心有限公司 | 一种同步去除污染物并控制三卤甲烷生成的深度处理***及工艺 |
Families Citing this family (36)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CA2422608A1 (en) * | 2002-05-10 | 2003-11-10 | Maurice Lacasse | Transportable water treatment apparatus |
US8080163B2 (en) * | 2002-12-04 | 2011-12-20 | Blue Water Technologies, Inc. | Water treatment method |
US7445721B2 (en) * | 2003-12-03 | 2008-11-04 | Idaho Research Foundation, Inc. | Reactive filtration |
AU2003299642A1 (en) | 2002-12-04 | 2004-06-23 | Idaho Research Foundation, Inc. | Reactive filtration |
US8071055B2 (en) | 2002-12-04 | 2011-12-06 | Blue Water Technologies, Inc. | Water treatment techniques |
US20040222165A1 (en) * | 2003-05-08 | 2004-11-11 | Kraft Foods Holdings, Inc. | Flexible film packaging for use with ozone sterilization applications |
DE10324136A1 (de) * | 2003-05-26 | 2004-12-16 | Bergische Universität Wuppertal | Vorrichtung zur Behandlung von Abwässern, insbesondere enthaltend Küpenfarbstoffe, hierbei eingesetzte Filtrationsmembran sowie Verfahren zur Behandlung von Abwässern unter Verwendung dieser Vorrichtung |
US20050279686A1 (en) * | 2004-06-21 | 2005-12-22 | Maxwell Hsu | Multifunctional oxygenaged water generation system |
AT501991B1 (de) * | 2005-06-10 | 2007-04-15 | Adler Herwig Dipl Ing | Verfahren zur behandlung von abwasser aus der olivenölproduktion |
FR2904572B1 (fr) * | 2006-08-01 | 2008-10-24 | Otv Sa | Reacteur membranaire pour le traitement d'effluents liquides comprenant une membrane de diffusion d'un gaz oxydant et une membrane selective definissant entre elles un espace de reaction |
CN101495414B (zh) | 2006-08-01 | 2011-09-28 | 美得华水务株式会社 | 废水再利用方法 |
DE102006060592B3 (de) * | 2006-12-21 | 2008-04-30 | Chmiel, Horst, Prof. Dr.-Ing. | Hybridprozess zur Meerwasserentsalzung |
KR100737352B1 (ko) | 2006-12-27 | 2007-07-09 | 케미코아 주식회사 | 목욕탕 배출수를 재활용하기 위한 장치 및 방법 |
GR20070100189A (el) * | 2007-03-28 | 2008-10-13 | Νικολαος Πηττας | Αυτοματη διαταξη επεξεργασιας εκροων βιολογικων σταθμων λυματων με εκπληρωση των προδιαγραφων του ποσιμου νερου |
US8999154B2 (en) | 2007-08-02 | 2015-04-07 | Ecosphere Technologies, Inc. | Apparatus for treating Lake Okeechobee water |
US8721898B2 (en) * | 2007-08-02 | 2014-05-13 | Ecosphere Technologies, Inc. | Reactor tank |
CA2607713C (en) | 2007-11-14 | 2009-05-26 | Dagua Inc. | Water treatment apparatus |
US7713426B2 (en) * | 2008-01-11 | 2010-05-11 | Blue Water Technologies, Inc. | Water treatment |
KR20100127234A (ko) * | 2008-03-21 | 2010-12-03 | 메타워터 가부시키가이샤 | 재생수의 제조 방법 |
US8741154B2 (en) | 2008-10-17 | 2014-06-03 | Remembrance Newcombe | Water denitrification |
WO2010115233A1 (en) * | 2009-04-07 | 2010-10-14 | Dewatering Filtration Technology Services Pty Ltd | Process and system for producing potable water |
CN102471101A (zh) * | 2009-08-21 | 2012-05-23 | 东丽株式会社 | 造水方法 |
SG185671A1 (en) | 2010-05-21 | 2012-12-28 | Adrian Brozell | Self-assembled surfactant structures |
DE102010041827A1 (de) * | 2010-09-30 | 2012-04-05 | Krones Aktiengesellschaft | Verfahren und Produktionsanlage zum Herstellen von Sterilwasser |
CN102001798B (zh) * | 2010-12-24 | 2012-08-29 | 清华大学深圳研究生院 | 采用耐氧化膜对饮用水深度净化的方法及*** |
WO2013078464A1 (en) | 2011-11-22 | 2013-05-30 | Znano Llc | Self-assembled surfactant structures |
EP2882691A4 (en) * | 2012-08-10 | 2016-02-10 | Xylem Water Solutions Zelienople Llc | METHOD AND DEVICE FOR MONITORING AND CONTROLLING OZONATION AND VENTED FILTRATION BY UV AND MEASURING A VISIBLE SPECTRUM AND AN OXIDATION REDUCTION POTENTIAL |
US10005686B2 (en) * | 2013-11-01 | 2018-06-26 | 1934612 Ontario Inc. | Fluid treatment system |
AT519319B1 (de) * | 2016-11-14 | 2020-09-15 | Va Tech Wabag Gmbh | Aufbereitung von Abwasser zu Trinkwasser mittels Ozon |
CN106698638A (zh) * | 2017-01-09 | 2017-05-24 | 北京林业大学 | 一种用于臭氧催化氧化工艺的催化剂优化投加控制方法 |
KR102027900B1 (ko) * | 2017-09-20 | 2019-11-04 | 한국지역난방공사 | 전오존 처리를 적용한 수처리 장치 및 공법 |
DE202017106774U1 (de) | 2017-09-27 | 2018-10-01 | BLüCHER GMBH | Anlage für die Behandlung und/oder Aufreinigung von Wasser |
KR101935863B1 (ko) * | 2018-07-03 | 2019-01-07 | 한창기전 주식회사 | 오존수 농도 제어기를 구비한 오존수 발생 시스템 |
WO2020023993A1 (en) * | 2018-08-01 | 2020-02-06 | Membrane Systems Australia Pty Ltd | System and process for removing polyfluorinated pollutants from water |
DE102018119771B4 (de) * | 2018-08-14 | 2021-11-11 | Jürgen Matzat | Filtervorrichtung zur Behandlung von Trinkwasser |
CZ2020544A3 (cs) * | 2020-10-06 | 2022-04-13 | Envi-Pur, S.R.O. | Způsob úpravy vody a zařízení k provádění tohoto způsobu |
Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS6230599A (ja) * | 1985-07-31 | 1987-02-09 | Mitsubishi Heavy Ind Ltd | 純水製造装置の前処理方法 |
JPH07256253A (ja) * | 1993-11-30 | 1995-10-09 | Otv Omnium De Traitement & De Valorisation Sa | 沈めた濾過膜で水を飲用可能にする装置 |
Family Cites Families (19)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS62230599A (ja) | 1986-03-31 | 1987-10-09 | 富士重工業株式会社 | 荷物移送装置 |
FR2655642B1 (fr) * | 1989-12-11 | 1992-02-28 | Anjou Rech | Installation de traitement des eaux par une boucle de filtration tangentielle. |
JPH0790219B2 (ja) * | 1990-08-01 | 1995-10-04 | 日本錬水株式会社 | 純水製造装置及び製造方法 |
JP2621699B2 (ja) | 1991-07-19 | 1997-06-18 | 日立プラント建設株式会社 | 汚水の処理方法及び装置 |
JP3220216B2 (ja) * | 1992-03-31 | 2001-10-22 | 旭化成株式会社 | 水処理方法 |
JPH06230599A (ja) * | 1993-02-05 | 1994-08-19 | Kao Corp | 画像形成方法 |
US5547584A (en) * | 1994-03-17 | 1996-08-20 | Electronic Drilling Control, Inc. | Transportable, self-contained water purification system and method |
US5466367A (en) * | 1994-04-06 | 1995-11-14 | Environmental Restoration Services, Inc. | Industrial waste water treatment |
US5645727A (en) * | 1994-05-06 | 1997-07-08 | Illinois Water Treatment, Inc. | On-line ozonation in ultra pure water membrane filtration |
US5514284A (en) * | 1994-05-12 | 1996-05-07 | Wheelabrator Engineered Systems Inc. | Method and apparatus for water treatment |
JP3251145B2 (ja) | 1995-03-23 | 2002-01-28 | 東北電力株式会社 | 膜分離装置及び酸化剤添加量の制御方法 |
US5711887A (en) * | 1995-07-31 | 1998-01-27 | Global Water Industries, Inc. | Water purification system |
WO1997010893A1 (fr) * | 1995-09-21 | 1997-03-27 | Asahi Kasei Kogyo Kabushiki Kaisha | Module a membranes a fibres creuses |
US5741416A (en) * | 1996-10-15 | 1998-04-21 | Tempest Environmental Systems, Inc. | Water purification system having plural pairs of filters and an ozone contact chamber |
KR100254136B1 (ko) * | 1997-05-29 | 2000-04-15 | 허목 | 생물막여과 및 오존탈질법에 의한 육상수조직 해산어류 양식시설의 순환여과시스템 |
JPH11277081A (ja) | 1998-03-31 | 1999-10-12 | Kurita Water Ind Ltd | 浄水処理装置 |
JP3449248B2 (ja) | 1998-10-05 | 2003-09-22 | Jfeエンジニアリング株式会社 | 水処理方法およびその装置 |
KR100296887B1 (ko) * | 1998-10-09 | 2001-10-26 | 조현서 | 해산어육상축양장의수질개선방법및그장치 |
CN1135206C (zh) * | 1998-11-05 | 2004-01-21 | 旭化成株式会社 | 水处理方法 |
-
1998
- 1998-11-05 CN CNB98812937XA patent/CN1135206C/zh not_active Expired - Fee Related
- 1998-11-05 US US09/582,033 patent/US6464877B1/en not_active Expired - Fee Related
- 1998-11-05 EP EP98951694A patent/EP1044928B1/en not_active Expired - Lifetime
- 1998-11-05 DE DE69828821T patent/DE69828821T2/de not_active Expired - Lifetime
- 1998-11-05 AU AU97616/98A patent/AU737042B2/en not_active Ceased
- 1998-11-05 KR KR10-2000-7007421A patent/KR100384668B1/ko not_active IP Right Cessation
- 1998-11-05 WO PCT/JP1998/004980 patent/WO2000027756A1/ja active IP Right Grant
Patent Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS6230599A (ja) * | 1985-07-31 | 1987-02-09 | Mitsubishi Heavy Ind Ltd | 純水製造装置の前処理方法 |
JPH07256253A (ja) * | 1993-11-30 | 1995-10-09 | Otv Omnium De Traitement & De Valorisation Sa | 沈めた濾過膜で水を飲用可能にする装置 |
Cited By (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
KR100384668B1 (ko) * | 1998-11-05 | 2003-05-22 | 아사히 가세이 가부시키가이샤 | 수처리 방법 |
JP2000288587A (ja) * | 1999-03-31 | 2000-10-17 | Nkk Corp | し尿系汚水の処理方法および処理装置 |
AU2002354050B2 (en) * | 2002-05-06 | 2009-10-29 | Debasish Mukhopadhyay | Method and apparatus for fluid treatment by reverse osmosis under acidic conditions |
JP2009509737A (ja) * | 2005-09-30 | 2009-03-12 | オテヴェ・ソシエテ・アノニム | 高速沈降ステップと、続く精密濾過膜または限外濾過膜による直接の濾過ステップを含む水処理方法、および対応する装置 |
JP2007289940A (ja) * | 2006-03-29 | 2007-11-08 | Toray Ind Inc | 中空糸膜モジュールの洗浄方法 |
WO2013055659A1 (en) * | 2011-10-11 | 2013-04-18 | Carter International, Llc | Produced water treatment process |
CN111807557A (zh) * | 2020-07-23 | 2020-10-23 | 上海城市水资源开发利用国家工程中心有限公司 | 一种同步去除污染物并控制三卤甲烷生成的深度处理***及工艺 |
Also Published As
Publication number | Publication date |
---|---|
CN1284933A (zh) | 2001-02-21 |
EP1044928A4 (en) | 2001-01-24 |
KR20010033860A (ko) | 2001-04-25 |
KR100384668B1 (ko) | 2003-05-22 |
DE69828821D1 (de) | 2005-03-03 |
DE69828821T2 (de) | 2005-11-17 |
AU9761698A (en) | 2000-05-29 |
EP1044928B1 (en) | 2005-01-26 |
US6464877B1 (en) | 2002-10-15 |
AU737042B2 (en) | 2001-08-09 |
EP1044928A1 (en) | 2000-10-18 |
CN1135206C (zh) | 2004-01-21 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
WO2000027756A1 (fr) | Procede de traitement de l'eau | |
EP1900417B1 (en) | Method of bacteriostasis or disinfection for permselective membrane | |
CN105384316B (zh) | 一种电子工业含氟含氨氮废水的处理方法 | |
CN106132518B (zh) | 使用膜的水处理方法以及水处理装置 | |
JP2007245078A (ja) | 水処理装置及び水処理方法 | |
JP6194887B2 (ja) | 淡水製造方法 | |
JP2007244979A (ja) | 水処理方法および水処理装置 | |
Guo et al. | Effect of ozone on the performance of a hybrid ceramic membrane-biological activated carbon process | |
WO2014007301A1 (ja) | 造水方法および造水装置 | |
JP2001191086A (ja) | 水処理装置 | |
JP5103747B2 (ja) | 水処理装置及び水処理方法 | |
JPH07275671A (ja) | 外圧型中空糸限外濾過膜モジュールの運転方法 | |
JP5055746B2 (ja) | 膜利用による水循環使用システム | |
JPH11239789A (ja) | 高度水処理方法 | |
WO2000027510A1 (en) | Method for filtration with membrane | |
JP3552580B2 (ja) | し尿系汚水の処理方法および処理装置 | |
JP2005177744A (ja) | 再生水の製造装置および再生水の製造方法 | |
JP3697938B2 (ja) | 用排水処理装置 | |
JP3565083B2 (ja) | し尿系汚水の処理方法および処理装置 | |
JPH11165192A (ja) | 下水、排水の高度処理方法 | |
JPH11277060A (ja) | マンガン含有水処理装置 | |
Cromphout et al. | Design and operation of an ultrafiltration plant for the production of drinking water out of the river Scheldt | |
JP3449247B2 (ja) | 水処理方法およびその装置 | |
JP2005040661A (ja) | 淡水またはかん水の処理方法および処理装置 | |
JP2000000566A (ja) | 高度な水処理方法 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
WWE | Wipo information: entry into national phase |
Ref document number: 98812937.X Country of ref document: CN |
|
AK | Designated states |
Kind code of ref document: A1 Designated state(s): AU CN JP KR US |
|
AL | Designated countries for regional patents |
Kind code of ref document: A1 Designated state(s): AT BE CH CY DE DK ES FI FR GB GR IE IT LU MC NL PT SE |
|
WWE | Wipo information: entry into national phase |
Ref document number: 97616/98 Country of ref document: AU |
|
WWE | Wipo information: entry into national phase |
Ref document number: 1998951694 Country of ref document: EP |
|
WWE | Wipo information: entry into national phase |
Ref document number: 09582033 Country of ref document: US |
|
WWE | Wipo information: entry into national phase |
Ref document number: 1020007007421 Country of ref document: KR |
|
121 | Ep: the epo has been informed by wipo that ep was designated in this application | ||
WWP | Wipo information: published in national office |
Ref document number: 1998951694 Country of ref document: EP |
|
WWP | Wipo information: published in national office |
Ref document number: 1020007007421 Country of ref document: KR |
|
WWG | Wipo information: grant in national office |
Ref document number: 97616/98 Country of ref document: AU |
|
WWG | Wipo information: grant in national office |
Ref document number: 1020007007421 Country of ref document: KR |
|
WWG | Wipo information: grant in national office |
Ref document number: 1998951694 Country of ref document: EP |