WO2020194820A1 - Module de memebrane à fibres creuses et procédé de nettoyage de celui-ci - Google Patents

Module de memebrane à fibres creuses et procédé de nettoyage de celui-ci Download PDF

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Publication number
WO2020194820A1
WO2020194820A1 PCT/JP2019/041492 JP2019041492W WO2020194820A1 WO 2020194820 A1 WO2020194820 A1 WO 2020194820A1 JP 2019041492 W JP2019041492 W JP 2019041492W WO 2020194820 A1 WO2020194820 A1 WO 2020194820A1
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Prior art keywords
hollow fiber
cleaning
fiber membrane
container
membrane module
Prior art date
Application number
PCT/JP2019/041492
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English (en)
Japanese (ja)
Inventor
貴子 岩見
Original Assignee
栗田工業株式会社
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Application filed by 栗田工業株式会社 filed Critical 栗田工業株式会社
Priority to KR1020217009095A priority Critical patent/KR20210141912A/ko
Priority to JP2020500751A priority patent/JPWO2020194820A1/ja
Publication of WO2020194820A1 publication Critical patent/WO2020194820A1/fr

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
    • B01D63/02—Hollow fibre modules
    • B01D63/021—Manufacturing thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
    • B01D63/02—Hollow fibre modules
    • B01D63/031—Two or more types of hollow fibres within one bundle or within one potting or tube-sheet
    • 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
    • B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
    • B01D65/02—Membrane cleaning or sterilisation ; Membrane regeneration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
    • B01D65/02—Membrane cleaning or sterilisation ; Membrane regeneration
    • B01D65/06—Membrane cleaning or sterilisation ; Membrane regeneration with special washing compositions
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
    • B01D65/08—Prevention of membrane fouling or of concentration polarisation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D69/00—Semi-permeable membranes for separation processes or apparatus characterised by their form, structure or properties; Manufacturing processes specially adapted therefor
    • B01D69/08—Hollow fibre membranes
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2313/00—Details relating to membrane modules or apparatus
    • B01D2313/46—Supply, recovery or discharge mechanisms of washing members
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
    • B01D2321/04—Backflushing
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
    • B01D2321/16—Use of chemical agents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
    • B01D2321/18—Use of gases
    • B01D2321/185—Aeration

Definitions

  • the present invention relates to a hollow fiber membrane module and a cleaning method thereof, and more particularly to a hollow fiber membrane module capable of sufficiently cleaning and removing turbid substances adhering to the membrane and a cleaning method thereof.
  • Hollow fiber membrane modules are widely used in the fields of pure water production and wastewater recovery as a means of removing turbid components and organic substances.
  • Microfiltration membranes (MF membranes) and ultrafiltration membranes (UF membranes) are used as the membranes of the hollow fiber membrane modules according to the separation target.
  • the former is around 0.1 ⁇ m and the latter is 0.005 to 0.
  • a pore of .5 ⁇ m is common.
  • the membrane will be clogged, and not only will the frequency of backwashing and chemical cleaning increase, but the frequency of membrane replacement will also increase. It gets higher.
  • a method of reducing the amount of water flowing per unit area of the membrane is common, but this method has a problem that the number of membranes to be installed increases.
  • Patent Document 1 proposes a backwashing method using air and water in order to improve the turbidity removing property of the membrane.
  • this method may not improve the turbidity removability so much depending on the type and amount of turbidity, and a higher performance backwashing method is required.
  • Patent Document 2 describes a container having a treated water outlet and a concentrated water outlet, a central tube for supplying raw water into the container, and a hollow fiber membrane for separating the raw water into permeated water and concentrated water.
  • a plurality of hollow fiber membranes arranged in the vertical direction in the container and an upper end portion of the hollow fiber membrane are fixed, and an upper end fixing portion arranged in the upper part of the container and an upper end fixing portion thereof.
  • a plurality of permeation water chambers formed in the hollow fiber membranes and communicated with each other, and the central tube extends vertically below the upper end fixing portion and ejects raw water on the side peripheral surface.
  • a method for cleaning a hollow fiber membrane module which is provided with a drainage port for discharging cleaning wastewater when performing bubbling cleaning in which gas is blown from the plurality of ejection holes at the bottom of the container.
  • the method for cleaning the hollow fiber membrane module which performs bubbling cleaning by blowing gas from the plurality of ejection holes and discharges the cleaning wastewater from the drainage port, is described.
  • Patent Document 2 a central tube provided with means for introducing raw water and gas is installed in the center of the module, and air is blown into the module from the central tube to alleviate the difference in the intensity of cleaning air generated above and below the module.
  • a higher raw water pressure acts on the membrane on the central side near the central canal than on the outer peripheral side near the housing, and the membrane on the central side is filtered.
  • the amount is larger than that of the outer membrane. Therefore, the film in the module is unevenly contaminated. In other words, a high load is applied to the hollow fiber membrane on the center side of the module, and the effective membrane area tends to decrease due to membrane contamination or the progress of membrane contamination.
  • the present invention has been made in view of the above-mentioned conventional circumstances, and an object of the present invention is to provide a hollow fiber membrane module capable of sufficiently removing turbidity adhering to the hollow fiber membrane and a cleaning method thereof.
  • the hollow fiber membrane module of the present invention is a container having a treated water outlet at the upper part, a raw water supply means for supplying raw water to the lower part of the container, and a hollow fiber membrane for solid-liquid separation of the raw water.
  • a plurality of hollow fiber membranes arranged in the vertical direction and the upper end portion of the hollow fiber membrane are fixed, and the upper end fixing portion arranged in the upper part of the container and the upper end fixing portion are formed above the upper end fixing portion.
  • a central tube provided with a permeation chamber in which the inside of each hollow fiber membrane is communicated, and a plurality of ejection holes extending in the vertical direction below the upper end fixing portion and ejecting gas on the side peripheral surface.
  • a discharge means for discharging gas and cleaning wastewater from the container.
  • the lower end of the central canal faces the opening on the bottom surface of the container.
  • a means for supplying gas is provided in the lower part of the container.
  • the first bubbling cleaning in which gas is blown from a plurality of ejection holes of the central tube is performed, and the exhaust body and the cleaning drainage are discharged from the discharging means.
  • At least one of a first bubbling cleaning in which gas is blown from a plurality of ejection holes in the central tube and a second bubbling cleaning in which gas is blown from a gas supply means provided at the lower part of the container is performed.
  • Exhaust body and cleaning wastewater are discharged from the discharge means.
  • the second bubbling cleaning is performed before or after the first bubbling cleaning, and the cleaning drainage is discharged from the container.
  • backwashing in which backwashing water is supplied from the treated water outlet is performed.
  • a chemical solution is added to the backwash water.
  • the flow rate of gas passing through the central canal is 50 to 300 NL / min.
  • the central tube extends vertically in the container, and gas is blown from a plurality of ejection holes provided in the central tube to perform bubbling cleaning.
  • the air reaches the whole, and the turbidity adhering to the hollow fiber membrane can be sufficiently removed evenly.
  • the drift in the filtration process can be reduced and the membrane can be used uniformly, which prevents the progress of local membrane contamination and the resulting decrease in membrane area ( (Including suppression).
  • FIG. 1 is a cross-sectional view showing the configuration of the hollow fiber membrane module according to the present embodiment.
  • the hollow fiber membrane module includes a container 1 arranged with the axial center line direction of the cylinder in the vertical direction (vertical direction in this embodiment).
  • a plurality of hollow fiber membranes 2 are arranged in the container 1.
  • the hollow fiber membrane 2 is fixed by the synthetic resin potting portion 3 as a fixing portion on the upper side of the container 1, and is not fixed on the lower side of the container 1.
  • the synthetic resin of the potting portion 3 for example, an epoxy resin can be used.
  • the hollow fiber membrane 2 is incorporated in a U shape, and both ends of the hollow fiber membrane are fixed by the potting portions 3.
  • the intermediate portion of the hollow fiber membrane 2 is located at the lower part of the container 1.
  • one end side of the open hollow fiber membrane 2 is fixed by a potting portion 3, and the sealed other end side is used. It is placed at the bottom of the container 1.
  • the hollow fiber membrane 2 may be either a UF membrane or an MF membrane.
  • the hollow fiber membrane 2 is not particularly limited, but usually one having an inner diameter of 0.2 to 1.0 mm, an outer diameter of 0.5 to 2.0 mm, and an effective length of about 300 to 2500 mm is used.
  • the film material of the hollow fiber membrane 2 is also not particularly limited, but PVDF (polyvinylidene fluoride), polyethylene, polypropylene and the like can be used.
  • a treated water chamber (permeated water chamber) 7 and a raw water chamber 10 are partitioned on the upper side and the lower side of the potting portion 3, respectively.
  • the upper end side of the hollow fiber membrane 2 penetrates the potting portion 3, the opening at the upper end faces the treatment water chamber 7, and the inside of the hollow fiber membrane 2 communicates with the treatment water chamber 7.
  • both ends of the hollow fiber membrane 2 penetrate the potting portion 3.
  • the potting portion 3 has, for example, a disk shape, and its outer peripheral surface or outer peripheral surface is in watertight contact with the inner surface of the container 1.
  • a central canal 4 extends in a substantially vertical direction (axial direction of the container 1).
  • the central canal 4 is arranged along the central axis of the container 1, for example.
  • the central canal 4 is a circular tube having a closed tip (upper end), and a plurality of ejection holes 4a are provided on the side peripheral surface as a whole at intervals in the circumferential direction and vertically.
  • the number of the ejection holes 4a is not particularly limited, but is, for example, about 5 to 50.
  • the size and shape of the ejection hole 4a are not particularly limited, but are, for example, a circular shape having a diameter of 5 to 500 mm.
  • the inner diameter of the central canal 4 is, for example, about 10 to 20 mm.
  • the height (length in the vertical direction) of the central canal 4 is not particularly limited, but it is preferable that the upper end of the central canal 4 is located near the lower surface of the potting portion 3.
  • the upper end of the central canal 4 may be embedded in the potting portion 3.
  • the lower end of the central canal 4 faces the opening 11 on the bottom surface of the container 1.
  • a raw water pipe L1 is connected to the opening 11, and a pump P1 and a valve V1 are provided in the raw water pipe L1.
  • the air introduction pipe L2 is branched from the container 1 side of the raw water pipe L1 from the valve V1, and the air introduction pipe L2 is provided with the valve V2.
  • a pipe L7 for discharging cleaning wastewater is connected to the container 1 side of the pipe L1 valve V1, and the valve V7 is provided in the pipe L7.
  • the supply of raw water / air to the container 1 can be switched.
  • valves V1 and V7 By closing the valves V1 and V7 and opening the valves V2 and supplying air from the air introduction pipe L2, air bubbles can be supplied from the opening 11 and the central filament membrane 2 can be bubbling-cleaned. It is also possible to open the valves V1 and V2 and eject a gas-liquid mixed flow from the opening 11.
  • An air pipe L8 is connected to the lower part of the central pipe 4, and a valve V8 is provided in the pipe L8.
  • a valve V8 is provided in the pipe L8.
  • An outlet 5 for treated water is provided at the top of the container 1.
  • an upper discharge port 8 is provided on the upper part of the side surface of the container 1.
  • the upper discharge port 8 is provided near the lower surface of the potting portion 3.
  • the distance from the potting portion 3 to the upper edge of the upper discharge port 8 is preferably 0 to 30 mm, particularly preferably about 0 to 10 mm.
  • a pipe L5 is connected to the upper discharge port 8, and a valve V5 is provided in the pipe L5.
  • the treated water outlet pipe L3 is connected to the treated water outlet 5, and the treated water (membrane permeated water) is taken out through the treated water take-out pipe L3.
  • the treated water is stored in the treated water tank 9.
  • FIG. 1 shows a configuration in which the backwash water pipe L4 is connected to the treated water tank 9 and the treated water is used for the backwash water, but the backwash water may be raw water.
  • the drainage associated with the backwash may be discharged from the opening 11 through the pipe L7, or may be discharged from the upper discharge port 8 through the pipe L5.
  • the discharge from the opening 11 and the discharge from the upper discharge port 8 may be performed at the same time, or may be performed in order (alternately).
  • a chemical solution adding means for adding a chemical solution to the backwash water flowing through the backwash water pipe L4 may be provided.
  • the chemical solution to be added is sodium hypochlorite, a strong alkaline agent, a strong acid agent, or the like, and is selected according to the film deposits.
  • the film deposit is an organic substance or a turbid substance containing an organic substance, it is preferable to add sodium hypochlorite so that 0.05 to 0.3 mgCl 2 / L remains.
  • valves V1 and V3 are opened, valves V2, V4, V5, V7 and V8 are closed, pump P1 is operated, and raw water is supplied to the raw water chamber 10 from the opening 11.
  • This embodiment is a dead end flow, in which the permeated water that has passed through the hollow fiber membrane 2 is taken out from the treated water outlet 5 as treated water and stored in the treated water tank 9 via the treated water take-out pipe L3.
  • the raw water may be filtered by an external pressure method in which raw water is passed through the outside of the hollow fiber membrane 2 by a cross-flow method.
  • the concentrated water that has not passed through the hollow fiber membrane 2 is discharged from the upper discharge port 8 through the pipe L5.
  • the discharged concentrated water may be mixed with raw water and circulated so as to be supplied to the container 1.
  • valves V8 are opened, V1 and V2 are closed, and air is blown from the plurality of ejection holes 4a of the central canal 4 toward the hollow fiber membrane 2. Perform bubbling cleaning.
  • valves V5 and V7 are opened, and the exhaust body and the cleaning drainage are discharged.
  • the valves V5 and V7 may be opened alternately.
  • the first valve V8 is opened, V1 and V2 are closed, and air is blown from the plurality of ejection holes 4a of the central tube 4 toward the hollow fiber membrane 2.
  • Bubbling cleaning and valve V2 are opened, valves V1 and V8 are closed, and at least one of the bubbling cleaning of the second bubbling cleaning in which air is blown from the opening 11 toward the hollow fiber membrane 2 is performed.
  • one or both of the valves V5 and V7 are opened, and the exhaust body and the cleaning drainage are discharged.
  • the valves V5 and V7 may be opened alternately.
  • the second bubbling cleaning is performed before or after the first bubbling cleaning, and the cleaning drainage is discharged from the container.
  • the backwashing that supplies backwashing water from the treated water outlet 5 to the treated water chamber 7 at the same time as the first bubbling washing and / or the second bubbling washing is performed. You may do it.
  • valves V1, V3, and V7 are closed, the valves V2, V4, V5, and V8 are opened, and the openings 11 and the central tube 4 are used.
  • Air is blown into the container 1 to perform bubbling, and the pump P2 is operated to send the treated water as backwash water into the hollow fiber membrane 2 through the treated water chamber 7 to perform backwashing.
  • a chemical solution may be added to the backwash water.
  • the cleaning drainage and exhaust air are discharged from the upper discharge port 8 to the outside of the system via the pipe L5. After bubbling, the cleaning drainage may be discharged from the pipe L7 with the valve V7 opened.
  • the amount of air supplied from the central canal 4 is preferably about 30 to 500 NL / min, particularly preferably 50 to 300 NL / min.
  • the central canal 4 is provided with a large number of ejection holes 4a in the entire vertical direction, air bubbles are injected into the entire hollow fiber membrane 2 including the vicinity of the upper end fixing portion (near the potting portion 3) of the hollow fiber membrane 2. , The turbidity can be thoroughly washed and removed. Further, even if the amount of air during bubbling cleaning is increased, it is possible to prevent the hollow fiber membrane 2 from being twisted or broken as compared with the method in which air is flowed from only the lower part of the module to the upper part.
  • the backwash may be air backwash instead of water backwash.
  • air may be ejected only from the central tube 4.
  • a gas-liquid mixed flow may be supplied from the central canal 4 instead of air.
  • a dispersion plate 12 having a large number of small holes 12a may be provided in the lower part of the container 1 to disperse the raw water from the opening 11 in the container 1.
  • the dispersion plate 12 is provided below the lower end of the hollow fiber membrane 2.
  • the dispersion plate 12 may be made of a potting material, and the lower end of the hollow fiber membrane 2 may be embedded in the dispersion plate 12 as shown in FIG. In FIG. 3, the small holes 12a are shown only partially, but in reality, they are provided over the entire surface of the dispersion plate 12.
  • Example 1 Raw water was passed through the hollow fiber membrane module provided with the hollow fiber membrane module shown in FIG. 3 for 30 minutes via the pipe L1 for filtration treatment.
  • Tap water was stored in the raw water tank, bentonite was added at 10 mg / L, and sodium hydrogencarbonate manufactured by Kishida Chemical Co., Ltd., and then the pH was adjusted to 8.0 with sulfuric acid manufactured by Kishida Chemical Co., Ltd.
  • Water was pumped from the raw water tank to the coagulation tank, and the residence time was set to 10 minutes.
  • a product obtained by adding 100 mg / L of industrial ferric chloride (concentration 38%) before the coagulation tank was used as raw water.
  • the configuration of the hollow fiber membrane module is as follows.
  • Container 1 Inner diameter 200 mm, height 1500 mm
  • Hollow fiber UF membrane made of polyvinyl fluoride den with an outer diameter of 1.4 mm, membrane area 32 m 2
  • Central canal 4 Length 1300 mm, inner diameter 13 mm, outer diameter 18 mm extending in the container 1
  • Ejection hole 4a Diameter 10 mm, 48 pieces
  • Small hole 12a of dispersion plate 12 Diameter 8 mm, 44 pieces
  • Example 2 The same treatment as in Example 1 was performed except that the backwash water was discharged from the pipe L7 through the opening 11. The measurement results are shown in Table 1.
  • Example 3 Before supplying air from the central pipe 4, backwashing was performed for 30 seconds, and the same treatment as in Example 2 was performed except that a step of draining the backwashing water from the upper discharge port 8 was added. The measurement results are shown in Table 1.
  • Example 4 The same treatment as in Example 3 was performed except that the supply amount of bubbling air was set to 150 NL / min. The measurement results are shown in Table 1.
  • Example 5 The same treatment as in Example 4 was carried out except that sodium hypochlorite was added to the backwash water so as to have a concentration of 300 mgCl 2 / L. The measurement results are shown in Table 1.
  • Example 6 Before supplying air from the central pipe 4, bubbling cleaning was performed in which air was supplied from the lower opening 11 of the container 1 at 150 NL / min for 30 seconds, and a step of discharging the drainage and the exhaust air from the upper discharge port 8 was added. Except for this, the same treatment as in Example 4 was performed. The measurement results are shown in Table 1.
  • Example 1 A hollow fiber membrane module not provided with the central tube 4 was used, and the same treatment as in Example 1 was performed except that the bug ring cleaning using the central tube 4 was omitted. The measurement results are shown in Table 1.
  • Comparative Example 2 A hollow fiber membrane module without a central tube 4 is used, air cleaning using the central tube 4 is omitted, and instead, air for bag ring is blown from the container lower opening 11 of the hollow fiber membrane module during back cleaning.
  • the same treatment as in Comparative Example 1 was carried out except that 80 NL / min was supplied and backwash water and exhaust air were discharged from the upper discharge port 8. The measurement results are shown in Table 1.
  • Example 1 had a higher turbidity removal rate by cleaning than cleaning with only back cleaning (Comparative Example 1) and cleaning with bubbling air blown from the lower part of the container (Comparative Example 2).
  • Example 2 by draining the washing drainage from the drainage port at the bottom of the container, a higher turbidity exclusion rate was obtained as compared with the washing (Example 1) in which the washing drainage was discharged from the upper drainage port.
  • Example 3 a higher turbidity exclusion rate than in Example 2 was obtained by adding backwash before the cleaning in Example 2.
  • Example 4 the amount of bubbling air was increased from 80 NL / min to 150 NL / min to obtain a higher turbidity exclusion rate than in Example 3.
  • Example 5 by adding an oxidizing agent to the backwash water, a higher turbidity exclusion rate than in the non-addition condition (Example 4) was obtained.
  • Example 6 a higher turbidity exclusion rate than in Example 4 was obtained by introducing air cleaning in which bubbling air is supplied from the lower part of the container before the cleaning in Example 4.
  • Example 7 Well water was passed through the hollow fiber membrane module used in Example 1, and the change over time of the intermembrane differential pressure was measured. The results are shown in FIG.
  • the opening 11 and the drainage pipe L7 are omitted, and instead, a drainage port 6 is provided at the lower part of the side surface of the container 1.
  • the drain port 6 is provided near the bottom surface of the container 1.
  • a pipe L6 is connected to the drain port 6, and a valve V6 is provided in the pipe L6.
  • the air pipe L8 is omitted, and instead, the pipe L1 is connected to the lower part of the central pipe 4.
  • the configuration of the hollow fiber membrane module of FIG. 4 is as follows.
  • Container 1 Inner diameter 200 mm, height 1300 mm
  • Hollow fiber UF membrane made of polyvinyl fluoride den with an outer diameter of 1.25 mm, membrane area 30 m 2
  • Central canal 4 Length 1000 mm, inner diameter 20 mm, outer diameter 25 mm extending in the container 1
  • Ejection hole 4a 10 mm in diameter
  • Example 7 the increase in the intermembrane differential pressure was suppressed and stabilized in Example 7 in which the raw water was supplied from the lower part of the raw water chamber, as compared with Comparative Example 3 in which the raw water was supplied from the central pipe.
  • the structure of the present invention is less likely to cause the drift of raw water in the module, and the entire membrane can be used for filtration evenly, so that the membrane contamination is not locally accelerated, and the effective membrane generated thereby. This is because the area did not decrease.

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

Abstract

Ce module de membrane à fibres creuses comprend : un récipient 1 ayant une sortie d'eau traitée 5 et une sortie de décharge supérieure 8; une pluralité de membranes à fibres creuses 2 pour effectuer une séparation solide-liquide d'eau brute, les membranes à fibres creuses 2 étant disposées dans la direction verticale à l'intérieur du récipient 1; une partie de fixation d'extrémité supérieure 3 qui fixe les extrémités supérieures des membranes à fibres creuses 2 et est disposée dans une partie supérieure à l'intérieur du récipient 1; une chambre d'eau perméable 7 formée au-dessus de la partie de fixation d'extrémité supérieure 3, la chambre d'eau perméable 7 étant en communication avec les intérieurs des membranes à fibres creuses 2; une tuyauterie L1 qui fournit de l'eau brute dans le récipient 1; et un tuyau central 4 pour effectuer un nettoyage par bullage. Le tuyau central 4 s'étend verticalement au-dessous de la partie de fixation d'extrémité supérieure 3 et est pourvu d'une pluralité de trous d'éjection 4a qui éjectent de l'air vers une surface latérale périphérique.
PCT/JP2019/041492 2019-03-27 2019-10-23 Module de memebrane à fibres creuses et procédé de nettoyage de celui-ci WO2020194820A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
KR1020217009095A KR20210141912A (ko) 2019-03-27 2019-10-23 중공사막 모듈 및 그 세정 방법
JP2020500751A JPWO2020194820A1 (ja) 2019-03-27 2019-10-23 中空糸膜モジュール及びその洗浄方法

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JP2019060929 2019-03-27
JP2019-060929 2019-03-27

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KR (1) KR20210141912A (fr)
TW (1) TW202110528A (fr)
WO (1) WO2020194820A1 (fr)

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH0596136A (ja) * 1991-10-04 1993-04-20 Toray Ind Inc 中空糸膜モジユールおよびその使用方法
JP2015226883A (ja) * 2014-06-02 2015-12-17 栗田工業株式会社 中空糸膜モジュール
JP2017176966A (ja) * 2016-03-29 2017-10-05 栗田工業株式会社 中空糸膜モジュールの洗浄方法

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH05154356A (ja) * 1991-12-10 1993-06-22 Sanki Eng Co Ltd 膜濾過モジュール
JP3094407B2 (ja) * 1994-06-29 2000-10-03 株式会社石垣 中空糸膜を用いた濃縮装置
JP4269171B2 (ja) 2004-11-26 2009-05-27 旭化成ケミカルズ株式会社 エアレーションフラッシング用外圧式中空糸膜モジュールのろ過方法

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH0596136A (ja) * 1991-10-04 1993-04-20 Toray Ind Inc 中空糸膜モジユールおよびその使用方法
JP2015226883A (ja) * 2014-06-02 2015-12-17 栗田工業株式会社 中空糸膜モジュール
JP2017176966A (ja) * 2016-03-29 2017-10-05 栗田工業株式会社 中空糸膜モジュールの洗浄方法

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