WO2013035576A1 - 含油排水処理システム - Google Patents
含油排水処理システム Download PDFInfo
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- WO2013035576A1 WO2013035576A1 PCT/JP2012/071628 JP2012071628W WO2013035576A1 WO 2013035576 A1 WO2013035576 A1 WO 2013035576A1 JP 2012071628 W JP2012071628 W JP 2012071628W WO 2013035576 A1 WO2013035576 A1 WO 2013035576A1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D21/00—Separation of suspended solid particles from liquids by sedimentation
- B01D21/0084—Enhancing liquid-particle separation using the flotation principle
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D21/00—Separation of suspended solid particles from liquids by sedimentation
- B01D21/02—Settling tanks with single outlets for the separated liquid
- B01D21/04—Settling tanks with single outlets for the separated liquid with moving scrapers
- B01D21/06—Settling tanks with single outlets for the separated liquid with moving scrapers with rotating scrapers
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D21/00—Separation of suspended solid particles from liquids by sedimentation
- B01D21/24—Feed or discharge mechanisms for settling tanks
- B01D21/2427—The feed or discharge opening located at a distant position from the side walls
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/14—Ultrafiltration; Microfiltration
- B01D61/147—Microfiltration
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/14—Ultrafiltration; Microfiltration
- B01D61/16—Feed pretreatment
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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
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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
- B01D63/031—Two or more types of hollow fibres within one bundle or within one potting or tube-sheet
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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
- B01D63/08—Flat membrane modules
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- 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
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D21/00—Separation of suspended solid particles from liquids by sedimentation
- B01D21/01—Separation of suspended solid particles from liquids by sedimentation using flocculating agents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D21/00—Separation of suspended solid particles from liquids by sedimentation
- B01D21/24—Feed or discharge mechanisms for settling tanks
- B01D21/2433—Discharge mechanisms for floating particles
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D21/00—Separation of suspended solid particles from liquids by sedimentation
- B01D21/24—Feed or discharge mechanisms for settling tanks
- B01D21/2488—Feed or discharge mechanisms for settling tanks bringing about a partial recirculation of the liquid, e.g. for introducing chemical aids
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/04—Specific process operations in the feed stream; Feed pretreatment
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2315/00—Details relating to the membrane module operation
- B01D2315/06—Submerged-type; Immersion type
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- 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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D71/00—Semi-permeable membranes for separation processes or apparatus characterised by the material; Manufacturing processes specially adapted therefor
- B01D71/06—Organic material
- B01D71/30—Polyalkenyl halides
- B01D71/32—Polyalkenyl halides containing fluorine atoms
- B01D71/36—Polytetrafluoroethene
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D71/00—Semi-permeable membranes for separation processes or apparatus characterised by the material; Manufacturing processes specially adapted therefor
- B01D71/06—Organic material
- B01D71/66—Polymers having sulfur in the main chain, with or without nitrogen, oxygen or carbon only
- B01D71/68—Polysulfones; Polyethersulfones
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/24—Treatment of water, waste water, or sewage by flotation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/40—Devices for separating or removing fatty or oily substances or similar floating material
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- 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
- C02F2001/007—Processes including a sedimentation step
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/32—Hydrocarbons, e.g. oil
Definitions
- the present invention relates to an oil-containing wastewater treatment system, and more specifically, in an oil-containing wastewater treatment system that combines separation in the previous process by flotation and sedimentation and membrane filtration in the subsequent process, efficient processing by combining the functions of the preceding and following processes. It is intended.
- a pretreatment such as filtration or activated carbon treatment is generally performed after a pretreatment such as coagulation sedimentation or pressurized levitation.
- a pretreatment such as coagulation sedimentation or pressurized levitation.
- the amount of treated water decreases as the post-treatment is performed, and the treatment of oil-containing wastewater discharged in large quantities cannot catch up.
- precise separation means are not suitable in terms of treatment speed.
- a membrane separation apparatus comprising a hollow fiber membrane which removes oil by membrane filtration in a treatment after pretreatment such as coagulation sedimentation and pressurized flotation in Japanese Patent Application Laid-Open No. 2010-36183.
- the membrane separation apparatus uses a hollow fiber membrane having alkali resistance selected from PTFE, PSF, and PES. Since the hollow fiber membrane is a chemically and physically tough membrane, efficient cleaning is possible. This has the advantage that a large amount of waste water can be treated by increasing the processing speed.
- the present invention has been made in view of the above-mentioned problems, and combines a post-process membrane filtration apparatus for performing a microfiltration treatment and a pre-process separation apparatus by flotation / sedimentation in an efficient manner on the operation and on the apparatus.
- An object is to simplify the apparatus.
- the present invention provides a separation tank that floats and separates oil in a raw water supply path made of oil-containing wastewater, and a membrane separation module made of a hollow fiber membrane or a flat membrane downstream of the separation tank. And a membrane filtration tank provided with an air diffuser for generating bubbles below the membrane separation module, and supplying raw water from the separation tank to the membrane filtration tank via a circulation pump.
- An oil-containing wastewater treatment system is provided that includes a supply pipe and a return pipe that returns the unfiltered water containing the oil and bubbles from the membrane filtration tank to the separation tank.
- an air diffuser that generates air bubbles is disposed below the membrane separation module in the membrane filtration tank, and air bubbles are generated by bubbling air for air diffusion.
- the underwater bubbling imparts vibrations to the separation membrane, and at the same time generates an upward flow of bubbles, peeling off foreign matter including oil adhering to the surface of the separation membrane, reducing clogging and reducing the flow rate of membrane filtration. It is preventing.
- the fine oil separated on the surface of the separation membrane accumulates by itself due to the continuous separation, and this becomes a large oil droplet and floats in the membrane filtration tank. Further, the flow rate by the circulation pump has an effect of peeling off oil and solids deposited on the film surface.
- the oil component that has floated is sent to the separation tank through the return pipe, and becomes floating oil in the separation tank and can be separated.
- unfiltered water containing bubbles flows into the separation tank from the return pipe, and the bubbles are supplied at an appropriate position in the separation tank, thereby generating an upward flow of bubbles and attaching oil in the separation tank to the bubbles.
- the oil component can be efficiently separated in the separation tank. At this time, when the unfiltered water is mixed with newly supplied raw water prior to supply into the separation tank, the oil can be separated more efficiently.
- the separation tank and the membrane filtration tank are connected by the return pipe, and the clogging of the membrane is reduced by the coarse bubbles generated by the air diffuser in the membrane filtration tank in the subsequent process, and the fine bubbles are introduced in the front. It can be returned to the separation tank of the process, and the facilities and operations of the preceding and following processes can be functionally combined to simplify the process and reduce the installation area.
- the supply pipe that connects the separation tank and the membrane filtration tank communicates with the upper and lower middle region of the separation tank and communicates with the lower part of the membrane filtration tank, and the return pipe communicates with the upper part of the membrane filtration tank.
- a part of the circulating water supplied from the separation tank to the membrane filtration tank becomes treated water that has been membrane filtered, and the remainder becomes unfiltered water and is returned to the separation tank.
- the greater the flow rate of circulating water the greater the effect of reducing clogging of the membrane in the membrane filtration tank, but in that case, the flow rate of unfiltered water returned to the separation tank increases.
- the liquid level in the separation tank may fluctuate greatly, and the floating oil and the aggregated sediment that settles may be stirred and difficult to separate.
- a configuration in which a guide cylinder is arranged with a gap in the outer periphery of each of the membrane separation modules or the outer periphery of the plurality of membrane separation modules, and air bubbles and raw water are allowed to flow in from the lower end opening of the guide cylinder and flow out from the upper end opening. It is preferable to do. If it is the said structure, a bubble raise can be made efficient in a guide cylinder, and dissipation of a bubble can be prevented. As a result, the vibration effect on the membrane becomes more effective, the circulation flow rate, that is, the return flow rate from the membrane filtration tank to the separation tank can be reduced accordingly, and the circulation rate of the treated water by the circulation pump can be reduced. In addition, it is possible to prevent disturbance of the liquid in the separation tank, and even if the necessary cross-sectional area of the separation tank is reduced, it is possible to easily remove the floating oil and sediment, thereby reducing the initial cost of the separation tank. It becomes possible.
- the separation tank In the separation tank, foreign matter with small oil content and specific gravity floats near the liquid level to be stored, and sludge with large specific gravity accumulates at the bottom of the separation tank. It is preferable to provide a raw water outlet. Moreover, in the membrane filtration tank, it is preferable to take out bubbles rising in the water after acting on the separation membrane, and therefore it is preferable to provide an outlet of the return pipe on the upper side of the membrane filtration tank.
- the air diffuser disposed in the membrane filtration tank supplies pressure air from an air source to an air diffuser pipe arranged below the membrane separation module, and performs membrane separation with bubbles generated from an injection hole of the air diffuser pipe. Apply vibration to the hollow fiber membrane or flat membrane of the module. There are also minute bubbles in the bubbles, and this has the effect of floating the minute oil in the tank.
- a separate fine bubble diffusing device having a hole with a smaller diameter may be provided separately to consciously generate fine bubbles, to float the fine oil in the membrane separation tank and to guide it to the return pipe.
- One diffuser tube may be provided with a hole for coarse bubbles and a hole for fine bubbles.
- the air source for supplying the pressure air to the air diffuser is a blower or a compressor.
- a scum skimmer is connected to the motor drive shaft at the liquid surface position of the separation tank, the floating oil is collected and discharged by the scum skimmer, and a sludge scraper is attached to the lower end of the motor drive shaft. It is preferable that the sludge scraping tool is connected to the bottom surface of the separation tank so that the settling sludge is collected and discharged.
- the filtration membrane of the membrane separation module disposed in the membrane filtration tank may be either a hollow fiber membrane or a flat membrane, but a hollow fiber membrane is particularly preferable in order to exert a peeling effect due to membrane vibration. Even a flat membrane can be suitably used if it is a flexible flat membrane.
- a porous membrane having alkali resistance selected from PTFE (polytetrafluoroethylene), PSF (polysulfone) and PES (polyethersulfone) is preferably used. Therefore, it is desirable to have a strength that can withstand vibration caused by air diffusion or pressure caused by backwashing. Specifically, the tensile strength is desirably 30 N or more.
- a membrane separation module using a hollow fiber membrane or a flat membrane of a porous separation membrane selected from PTFE, PSF, and PES has extremely excellent water-insoluble oil removal performance and chemical resistance, in particular, alkali resistance, and Combines durability (long service life for normal filtration performance).
- the water-insoluble oil adhering to the membrane surface can be dissolved and removed by chemical cleaning with an alkaline aqueous solution and repeatedly regenerated. Filtration can be sustained for a long time.
- the oil-containing wastewater treatment system of the present invention can be used as an oil-containing wastewater treatment system in any field, such as for oil field accompanying water and factory wastewater containing oil. Further, when desalinating seawater, it is particularly effective when seawater contains oil. For example, when a nuclear power plant is destroyed due to tsunami damage caused by the earthquake, radioactive wastewater is generated and treatment is required. In that case, it is necessary to remove the oil in the seawater as a pre-treatment prior to the removal of the radioactive material. Even at that time, the oil can be stably removed with high accuracy, and post-treatment such as adsorption of the radioactive material. Can increase the efficiency.
- a return pipe is installed between the upstream separation tank and the downstream membrane filtration tank, and the circulation flow is supplied to the membrane separation module existing in the membrane filtration tank.
- the stable filtration capacity of the membrane is maintained, and the floating oil content from the membrane filtration tank to the separation tank is maintained. Is removed to remove oil in the membrane separation tank.
- unfiltered water containing bubbles is circulated from the membrane filtration tank to the separation tank, the bubbles exist in the separation tank without providing an air diffuser in the separation tank, and oil is bubbled when the bubbles rise.
- the process can be simplified and the installation area can be reduced.
- by vibrating the separation membrane with coarse bubbles generated in the membrane filtration tank it is possible to exfoliate foreign matter adhering to the surface of the membrane and suppress the reduction in filtration performance, and to circulate the fine bubbles in the separation tank. It can contribute effectively to the floating separation of oil.
- a membrane filtration tank is disposed downstream of the separation tank that performs separation by specific gravity and membrane filtration is performed using the separation membrane, the quality of treated water can be improved and the stability of operation can be enhanced.
- FIG. 1 is an overall view of an oil-containing wastewater treatment system according to an embodiment of the present invention. It is an enlarged view of the membrane filtration tank shown in FIG. It is a principal part enlarged view of the modification of an air diffuser. It is drawing which shows the 1st modification of a membrane separation module. It is drawing which shows arrangement
- reference numeral 1 denotes a separation tank for separating and separating foreign matters
- 2 is a membrane filtration tank for membrane-filtering foreign matters.
- a hollow fiber membrane module (membrane separation module) 3 is accommodated in the membrane filtration tank 2, and an air diffuser 4 for generating bubbles is accommodated in the lower part of the hollow fiber membrane module 3.
- the upper and lower intermediate region of the separation tank 1 and the lower region of the membrane filtration tank 2 are connected by a supply pipe 6 having a pump 5 interposed therebetween, and the upper region of the membrane filtration tank 2 and the upper region of the separation tank 1 are communicated.
- a return pipe 7 is provided, and unfiltered water containing bubbles is returned from the return pipe 7 to the separation tank 1 for circulation.
- the raw water W1 composed of oil-containing wastewater supplied to the separation tank 1 is temporarily stored in a chemical mixing tank 8, and a pH adjuster, an adsorbent, a flocculant, etc., if necessary, from the chemical injection apparatus 9 in the chemical mixing tank 8. Injecting.
- the liquid is fed from the chemical mixing tank 8 to the liquid level adjusting tank 10, and the raw water W 1 is supplied from the liquid level adjusting tank 10 to the separation tank 1 through the raw water supply pipe 11.
- the separation tank 1 is a tank that floats oil and foreign substances to the liquid surface side according to the specific gravity and separates the oil and foreign substances by sedimentation to the bottom side.
- a scum skimmer 12 that collects foreign matter that has floated to the top of the separation tank 1 is disposed on the liquid surface.
- the scum skimmer 12 fixes the scum skimmer 12 to a drive shaft 13a suspended from a motor 13 mounted on the upper side, and collects foreign matter including oil components that are horizontally rotated by the motor 13 and floated.
- the lower end of the drive shaft 13a is positioned on the bottom wall 1a protruding in the conical shape of the separation tank 1, and is connected to the sludge scraping tool 14 arranged along the bottom wall 1a. The sludge that is driven to rotate and settles on the upper surface side of the bottom wall 1a is scraped to the lowermost end of the center.
- a scum discharge pipe 15 is opened on the lower surface side of the scum skimmer 12 and piped, and a sludge discharge pipe 16 is opened at the lowermost end of the separation tank 1 to connect the scum discharge pipe 15 and the sludge discharge pipe 16. The other end is connected to a scum / sludge tank 17.
- the raw water supply pipe 11 for supplying the raw water W1 from the liquid level adjusting tank 10 is opened at a position on the lower surface side of the scum skimmer 12 of the separation tank 1.
- the return pipe 7 is communicated with the raw water supply pipe 11, and unfiltered water containing bubbles circulating through the return pipe 7 and the raw water W 1 are merged and supplied to the upper region of the separation tank 1.
- the oil component is attached to the air bubbles so that the oil component can be easily floated, and the oil component is easily attached to the scum skimmer 12.
- the separation tank 1 has a side wall opposite to the side wall to which the raw water supply pipe 11 is connected, and an intermediate region excluding the vertical position where the scum skimmer 12 and the sludge scraper 14 are disposed.
- the outlet is open. Since the pump 5 is provided in the supply pipe 6, the separation liquid in the separation tank 1 is sucked into the supply pipe 6 and supplied into the membrane filtration tank 2 from the opening provided in the lower part of the side wall of the membrane filtration tank 2. Yes.
- the discharge pressure of the pump 5 is 50 to 300 kPa.
- the membrane filtration tank 2 is an immersion tank provided with an air valve and the like.
- the hollow fiber membrane module 3 is accommodated therein, and a diffuser 4 for generating bubbles is accommodated in the lower part of the hollow fiber membrane module 3.
- the hollow fiber membrane module 3 and the air diffuser 4 are immersed in the raw water W1 supplied from the pipe 6.
- the hollow fiber membrane module 3 is an immersion type module that permeates the raw water W1 from the outside to the inside of the hollow fiber membrane 20 by sucking the raw water W1 from the inside of the hollow fiber membrane 20.
- the hollow fiber membrane module 3 includes a converging body 21 in which a plurality of hollow fiber membranes 20 (3500 in this embodiment) are bundled, and the lower end opening of each hollow fiber membrane 20 is closed with a fixing material 40.
- the upper end of the hollow fiber membrane 20 is opened and fixed with a fixing material 23, and an upper cap 24 is attached to the fixing material 23.
- the fixing member 23 and the fixing member 40 are connected by a support rod 41, and a skirt member 42 protruding downward is fixed to the fixing member 40.
- a lead-out port that communicates the inside of the upper cap 24 with the hollow portion of each hollow fiber membrane 20 is provided, and the lead-out port is connected to the filtered liquid outlet pipe 25.
- the filtered liquid W2 is led out to the post-treatment tank 27 by providing a suction pump 26 in the filtered liquid extraction pipe 25.
- a suction pump 26 in the filtered liquid extraction pipe 25.
- activated carbon adsorption, biological treatment / precipitation treatment, reverse osmosis membrane treatment, or the like may be added.
- An air vent pipe 28 is attached to the upper wall of the membrane filtration tank 2.
- a discharge port of untreated water that has not been filtered is provided in the upper part of the side wall of the membrane filtration tank 2, and the discharge port communicates with the return pipe 7.
- the air diffuser 4 disposed at the lower part of the hollow fiber membrane module 3 includes an air diffuser air introduction pipe 30 connected to a blower 31.
- An injection hole 32 provided in the air introduction pipe 30 for aeration is arranged below the hollow fiber membrane module 3 so that air is injected into the skirt material 42 from the injection hole 32.
- a plurality of injection holes 32 having the same diameter are provided. Coarse bubbles K1 and some fine bubbles K2 are generated by the air injected from one injection hole 32.
- the injection hole 32 may be provided with a large diameter hole 32a for generating coarse bubbles and a small diameter hole 32b for generating fine bubbles.
- a hydrophobic porous membrane pipe, membrane material or the like is preferably used.
- the air diffuser 4 always diffuses from below during filtration operation, diffuses toward each hollow fiber membrane 20 of the focusing body 21, and generates coarse bubbles K1 and fine bubbles K2 upward in the raw water W1. .
- the coarse bubble K1 mainly vibrates the hollow fiber membrane 20 and peels off foreign matter adhering to the membrane surface of the hollow fiber membrane 20 so that the hollow fiber membrane 20 is not clogged.
- the coarse bubbles K1 are discharged to the atmosphere through the air vent pipe 28.
- the fine bubbles K2 are led out from the return pipe 7 disposed above and circulated in the separation tank 1.
- the hollow fiber membrane 20 used in the present embodiment is a porous multilayer hollow provided with a support layer made of a porous expanded PTFE tube, and a filtration layer made of a porous membrane expanded PTFE sheet on the outer surface of the support layer. It consists of a yarn membrane. Furthermore, what was hydrophilized with hydrophilic polymer etc. can be used.
- the average maximum length of each of the pores present in large numbers on the outer peripheral surface of the filtration layer is set to be smaller than the average maximum length of each of the pores surrounded by the fibrous skeleton present in the support layer.
- the average length of the pores in the filtration layer is preferably 1% to 30% of the average length of the pores in the support layer, and is preferably as small as possible.
- transmittance from the outer peripheral surface side to an inner peripheral surface side can be improved.
- the area occupation ratio of the pores with respect to the total surface area of the outer surface is 30% to 90% as measured by image processing. Even if the maximum length of the holes is small, if the area occupation ratio of the holes is large to some extent, the flow rate is not reduced and the filtration performance can be improved efficiently.
- the porosity of the filtration layer is 30% to 80%, and the porosity of the support layer is 50% to 85%.
- transmittance from the outer peripheral surface side of a hollow fiber membrane to an inner peripheral surface side can further be improved, maintaining a balance with intensity
- the thickness of the filtration layer is 5 ⁇ m to 100 ⁇ m. If it is smaller than the above range, it is difficult to form a filtration layer.
- the thickness of the support layer is 0.1 mm to 5 mm. As a result, good strength can be obtained in any of the axial direction, radial direction, and circumferential direction, and durability against internal / external pressure, bending, and the like can be improved.
- the inner diameter of the support layer is 0.3 mm to 12 mm.
- the filter layer has an average pore diameter of 0.01 to 1 ⁇ m.
- the hollow fiber membrane 20 has an inner diameter of 0.3 to 12 mm, an outer diameter of 0.8 to 14 mm, a bubble point of 50 to 400 kPa, a film thickness of 0.2 to 1 mm, a porosity of 30 to 90%, and a maximum. It is preferable that the allowable transmembrane pressure has a pressure resistance of 0.1 to 1.0 MPa.
- the hollow fiber membrane 20 has a tensile strength of 30 N or more.
- the tensile strength was based on JIS K 7161, and the hollow fiber membrane itself was used as a test body.
- the tensile speed during the test was 100 mm / min, and the distance between the marked lines was 50 mm.
- the thermal deformation temperature of the hollow fiber membrane 20 is 100 ° C. or higher, thermal deterioration is unlikely to occur even when used over time.
- the dimensional average value between the hollow fiber membranes 20 in the converging body 21 is relatively wide as 0.5 mm to 5 mm, and the cross-sectional area of the converging body 21 is increased.
- the filling rate of the hollow fiber membrane 20 to 20% to 60%.
- the fine bubbles K2 are mixed with the unfiltered raw water W1 that has not been filtered and led to the return pipe 7. Since the return pipe 7 is merged with the raw water supply pipe 11, the raw air W1 of unfiltered water that has not been filtered and the fine bubbles K2 are mixed with the raw water W1 and introduced into the separation tank 1. In this way, by introducing the fine bubbles K2 into the separation tank 1, oil adheres to the fine bubbles K2 in the separation tank 1, and the oil easily floats together with the fine bubbles K2, so that the scum skimmer 12 is efficient. Can be collected.
- the raw water W1 is supplied to the membrane filtration tank 2 and thus membrane filtration.
- Foreign matter consisting of oil and sludge adhering to the surface of the hollow fiber membrane 20 of the hollow fiber membrane module 3 disposed in the tank 2 can be reduced.
- the membrane filtration performance of the hollow fiber membrane 20 does not deteriorate, and the reduction of the amount of treated water can be prevented.
- the bubble generated with the diffuser 4 used for the membrane filtration tank 2 is circulated to the separation tank 1 and used functionally, the separation function in the separation tank 1 can be enhanced.
- the facilities can be simplified and the installation area can be reduced.
- FIGS. 4A and 4B show a first modification of the membrane filtration tank 2.
- Each of the plurality of hollow fiber membrane modules 3 immersed in the membrane filtration tank 2 is covered with a guide tube 45 with a gap around the outer periphery of the converging body 21 of the hollow fiber membrane 20.
- the guide tube 45 has openings 45a and 45b at both upper and lower ends, and the raw water W1 flows into the guide tube 45 through the opening 45b at the lower end and is filtered by the hollow fiber membrane 20, and the unfiltered raw water W1 that has not been filtered is the upper end. It flows out through the opening 45a of the guide tube 45, flows downward on the outer peripheral side of the guide tube 45, and circulates. Further, the air injected from the air diffuser 4 is also injected into the guide tube 45 from the lower end opening 45b.
- the guide tube 45 that is, the vicinity of the membrane surface of the converging body 21 of the hollow fiber membrane 20 is formed.
- the linear velocity of the flowing raw water W1 increases, and the solid content and oil content deposited on the membrane surface of the hollow fiber membrane 20 can be more efficiently separated.
- the generated bubbles can be efficiently loaded on the surface of the hollow fiber membrane 20 to shake the hollow fiber membrane, and the amount of air supply can be reduced to reduce the running cost.
- the cross-sectional area of the separation tank necessary for realizing rapid sedimentation can be reduced, and the initial cost can be reduced. It becomes possible.
- FIG. 5 shows a second modification.
- a plurality of hollow fiber membrane modules 3 immersed in the membrane filtration tank 2 are divided into a plurality of groups (in the embodiment, 24 hollow fiber membrane modules 3 arranged in parallel in the vertical and horizontal directions are divided into four groups), Each is covered with one guide tube 48.
- the hollow fiber membrane modules 3 when the hollow fiber membrane modules 3 are arranged relatively densely and covered with one guide tube 48, the hollow fiber membrane modules can be arranged in the membrane filtration tank 2 with high density.
- the hollow fiber membrane converging body is used as the hollow fiber membrane module 3 installed in the membrane filtration tank 2, but a flat membrane may be used instead of the hollow fiber membrane. Even when the flat membrane is used, an air diffuser for generating bubbles is disposed below the flat membrane as in the above embodiment.
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Abstract
Description
このように、分離槽と膜濾過槽とを返送管で連結して、後工程の膜濾過槽内の散気装置で発生させる粗大な気泡で膜の目詰まりを低減するとともに微小な気泡を前工程の分離槽へ返送し、前後工程の設備および操作を機能的に組み合わせて、プロセスの単純化、設置面積の減少を図ることができる。
前記構成とすると、ガイド筒内において気泡上昇を効率化でき、気泡の散逸を防ぐことができる。その結果、膜への振動効果等がより効果的になり、その分循環流量すなわち膜濾過槽から分離槽への返送流量も低減でき、循環ポンプによる処理水の循環量を低減することが可能となり、かつ、分離槽の液の乱れを防止でき、必要な分離槽の断面積を小さくしても、浮上油、沈殿物の除去を容易にすることができるため、分離槽のイニシャルコストを低減させることも可能になる。
特に、膜濾過槽内で発生させる粗大気泡で分離膜を振動させることにより、膜表面に付着する異物を剥離させて濾過性能の低下を抑制でき、かつ、微細気泡を分離槽に循環させることで油分の浮上分離に有効に寄与させることができる。 また、比重により分離を行う前記分離槽の下流に膜濾過槽を配置し、分離膜を用いて膜濾過を行うため、処理水質を向上できると共に、運転の安定性を高めることができる。
図1および図2に本発明の実施形態を示す。
図1に示す全体構成図において、1は異物を浮上および沈降させて分離する分離槽、2は異物を膜濾過する膜濾過槽である。
膜濾過槽2内に中空糸膜モジュール(膜分離モジュール)3を収容すると共に、該中空糸膜モジュール3の下部に気泡を発生させる散気装置4を収容している。
前記分離槽1の上下中間領域と膜濾過槽2の下部領域とをポンプ5を介設した供給管6で連続すると共に、膜濾過槽2の上部領域と分離槽1の上部領域とを連通する返送管7を設け、該返送管7から気泡を含む未濾過水を分離槽1へ返送し循環させている。
分離槽1の上部へ浮上した異物を集めるスカムスキマー12を液面に配置している。該スカムスキマー12は、上方に搭載するモータ13から垂下した駆動軸13aにスカムスキマー12を固定して、モータ13により水平回転させて浮上した油分を含む異物を集めるようにしている。また、駆動軸13aの下端を分離槽1の円錐形状に突出させた底壁1aに位置させ、該底壁1aに沿って配置する汚泥掻き寄せ具14に連結し、該汚泥掻き寄せ具14を回転駆動させて底壁1aの上面側に沈降する汚泥を中央最下端部に掻き寄せるようにしている。
中空糸膜モジュール3は、中空糸膜20の内側から原水W1を吸引することにより中空糸膜20の外側から内側に向けて原水W1を透過させる浸漬型のモジュールとしている。
前記上部キャップ24の内部を各中空糸膜20の中空部と連通させた導出口を設け、該導出口を濾過済み液取出配管25と接続している。該濾過済み液取出配管25に吸引ポンプ26を介設して、濾過済み液W2を後処理槽27へ導出している。該後処理槽27として活性炭吸着、生物処理・沈殿処理、逆浸透膜処理等を付加する場合もある。
また、前記膜濾過槽2の上壁にエアベント管28を取り付けている。かつ、膜濾過槽2の側壁上部に、濾過されなかった未処理水の排出口を設け、該排出口を前記返送管7と連通している。
なお、図3の変形例に示すように、噴射穴32は粗大気泡を発生させる大径穴32aと微細気泡を発生させる小径穴32bを設けてもよい。該小径穴32bを形成するために、例えば、疎水性多孔質膜のパイプ、膜材などが好適に用いられる。
濾過層の外表面において、該外表面の全表面積に対する前記空孔の面積占有率が、画像処理で測定して、30%~90%としている。空孔の最大長さが小さくても、空孔の面積占有率がある程度大きいと、流量を減らすこともなく、効率良く、濾過性能を向上することができる。
具体的には、濾過層の空孔率は30%~80%、支持層の空孔率は50%~85%としている。これにより、強度とのバランスを保ちながら、中空糸膜の外周面側から内周面側への透過性をさらに高めることができる。
また、中空糸膜20は、中空糸膜全体で内径0.3~12mm、外径0.8~14mm、バブルポイント50~400kPa、膜厚0.2~1mm、気孔率30~90%、最大許容膜間差圧は0.1~1.0MPaの耐圧性を備えたものとすることが好ましい。
なお、抗張力はJIS K 7161に準拠し、試験体としては中空糸膜そのものを用いた。試験時の引張速度は100mm/分、標線間距離は50mmとして測定した。また、該中空糸膜20の熱変形温度は100℃以上であるため、経年使用しても熱劣化が発生しにくいものとしている。
その際、前記のように、粗大気泡K1で中空糸膜20を振動しつつ、中空糸膜20の膜面に付着している非水溶性油分および固形分をふるい剥ぎ取っている。
膜濾過槽2に浸漬する複数の中空糸膜モジュール3にはそれぞれ、中空糸膜20の集束体21の外周に隙間をあけてガイド筒45を被せている。このガイド筒45は上下両端を開口45a、45bとし、下端の開口45bより原水W1がガイド筒45内部に流入して中空糸膜20で濾過され、濾過されなかった未濾過水の原水W1が上端の開口45aから流出し、ガイド筒45の外周側を下向きに流れて循環するようにしている。また、散気装置4から噴射するエアも下端の開口45bからガイド筒45内に噴射されるようにしている。
第2変形例では、膜濾過槽2内に浸漬する複数の中空糸膜モジュール3を複数組に分けて(実施形態では縦横並列した24個の中空糸膜モジュール3を4組に分ける)、組ごとに1つのガイド筒48で覆っている。このように、中空糸膜モジュール3を比較的密に配置して、1つのガイド筒48で覆うと、膜濾過槽2内に高密度に中空糸膜モジュールを配置することができる。
2 膜濾過槽
3 中空糸膜モジュール
4 散気装置
6 供給管
7 返送管
K1 粗大気泡
K2 微細気泡
W1 原水
W2 濾過済み液
Claims (6)
- 含油排水からなる原水の供給経路に、油分を浮上分離させる分離槽と、
前記分離槽の下流に、中空糸膜または平膜からなる膜分離モジュールを槽内に配置すると共に前記膜分離モジュールの下方に気泡を発生させる散気装置を設置した膜濾過槽とを配置し、
前記分離槽から前記膜濾過槽へ循環ポンプを介設して原水を供給する供給管と、
前記膜濾過槽から前記分離槽へ前記油分および気泡を含む未濾過水を返送する返送管を設けていることを特徴とする含油排水処理システム。 - 前記各膜分離モジュールの外周または複数の膜分離モジュールの外周に隙間をあけてガイド筒を配置し、前記ガイド筒の下端開口から気泡および原水を流入させると共に、上端開口から流出させる構成としている請求項1に記載の含油排水処理システム。
- 前記膜濾過槽内に配置する前記膜分離モジュールの分離膜は、PTFE(ポリテトラフルオロエチレン)、PSF(ポリスルホン)およびPES(ポリエーテルスルホン)から選択される多孔質膜からなる請求項1または請求項2に記載の含油排水処理システム。
- 前記分離槽と前記膜濾過槽とを連結する前記供給管は、前記分離槽の上下中間領域に連通させると共に前記膜濾過槽の下部に連通させ、前記返送管は膜濾過槽の上部に連通している請求項1乃至請求項3のいずれか1項に記載の含油排水処理システム。
- 前記膜濾過槽内に配置する前記散気装置は、前記膜分離モジュールの下方に配管される散気管に空気源から圧力空気を送給し、該散気管に大径穴と小径穴を設け、大径穴から発生させる粗大気泡で膜分離モジュールの中空糸膜または平膜に振動を付与する一方、前記小径穴から微細気泡を前記返送管へ導出させている請求項1乃至請求項4のいずれか1項に記載の含油排水処理システム。
- 前記分離槽の液面位置にスカムスキマーをモータの駆動軸に連結して配置し、浮上する油分をスカムスキマーで集めて排出すると共に、前記モータの駆動軸の下端に汚泥掻き寄せ具を連結し、前記汚泥掻き寄せ具を前記分離槽の底面上に配置し、沈降する汚泥を掻き集めて排出する構成としている請求項1乃至請求項5のいずれか1項に記載の含油排水処理システム。
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Publication number | Publication date |
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CN103298750A (zh) | 2013-09-11 |
JP5564021B2 (ja) | 2014-07-30 |
US20130264254A1 (en) | 2013-10-10 |
CA2823920A1 (en) | 2013-03-14 |
JP2013052364A (ja) | 2013-03-21 |
MY170503A (en) | 2019-08-08 |
AU2012305529A1 (en) | 2013-07-11 |
CN103298750B (zh) | 2015-01-07 |
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