WO2020148961A1 - Appareil de production d'eau pure et son procédé de fonctionnement - Google Patents

Appareil de production d'eau pure et son procédé de fonctionnement Download PDF

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Publication number
WO2020148961A1
WO2020148961A1 PCT/JP2019/041361 JP2019041361W WO2020148961A1 WO 2020148961 A1 WO2020148961 A1 WO 2020148961A1 JP 2019041361 W JP2019041361 W JP 2019041361W WO 2020148961 A1 WO2020148961 A1 WO 2020148961A1
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Prior art keywords
water
line
membrane filtration
membrane
concentrated
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PCT/JP2019/041361
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English (en)
Japanese (ja)
Inventor
慶介 佐々木
日高　真生
勇規 中村
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オルガノ株式会社
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Priority to CN201980074544.3A priority Critical patent/CN113015702B/zh
Priority to JP2020511414A priority patent/JP6720428B1/ja
Publication of WO2020148961A1 publication Critical patent/WO2020148961A1/fr

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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
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/06—Energy recovery
    • 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
    • B01D61/42—Electrodialysis; Electro-osmosis ; Electro-ultrafiltration; Membrane capacitive deionization
    • B01D61/44—Ion-selective electrodialysis
    • 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
    • B01D61/42—Electrodialysis; Electro-osmosis ; Electro-ultrafiltration; Membrane capacitive deionization
    • B01D61/44—Ion-selective electrodialysis
    • B01D61/46—Apparatus therefor
    • B01D61/48—Apparatus therefor having one or more compartments filled with ion-exchange material, e.g. electrodeionisation
    • 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
    • B01D61/58—Multistep processes
    • 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
    • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/469—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis

Definitions

  • the present invention relates to a pure water production apparatus and an operating method thereof.
  • a method for producing pure water from raw water such as industrial water, well water and city water
  • a method using a reverse osmosis membrane (RO membrane) or nanofiltration membrane (NF membrane) and an ion exchanger is known.
  • deionized water is produced by separating raw water into permeated water and concentrated water with an RO membrane or an NF membrane and then passing the permeated water through an ion exchanger.
  • a pure water producing device in which a membrane filtration device having an RO membrane or an NF membrane and an electric deionized water producing device are combined (for example, see Patent Document 1). ).
  • raw water is supplied to the RO membrane or NF membrane of the membrane filtration device at a pressure higher than the osmotic pressure, and is separated into permeated water and concentrated water using the principle of reverse osmosis. Therefore, the concentrated water separated by the membrane filtration device has a relatively high pressure.
  • concentrated water pressure energy may be used to recirculate a part of the concentrated water to the upstream side of the membrane filtration device, it cannot be said to be effectively used for other purposes. The current situation is that it is wasted.
  • an object of the present invention is to provide a pure water production apparatus and an operating method thereof that effectively use energy that has been wasted to realize energy saving.
  • the pure water producing apparatus of the present invention comprises a membrane filtration device having a reverse osmosis membrane or a nanofiltration membrane for separating treated water into permeated water and concentrated water, and treated water and permeated water.
  • a water treatment device that treats either water or concentrated water, and a concentrated water line that circulates the concentrated water from the membrane filtration device is provided, and power is generated using the flow of the concentrated water flowing through the concentrated water line.
  • a hydraulic power generation device that supplies generated power to the water treatment device.
  • the operation method of the pure water producing apparatus of the present invention is a membrane filtration device having a reverse osmosis membrane or a nanofiltration membrane for separating treated water into permeated water and concentrated water, treated water, permeated water and concentrated water.
  • the pressure energy of the concentrated water separated by the membrane filtration apparatus is recovered as electric power and used for the water treatment apparatus installed in association with the membrane filtration apparatus. To be done. Thereby, the energy efficiency of the entire system can be improved.
  • FIG. 1 is a schematic configuration diagram of a pure water production apparatus according to the first embodiment of the present invention.
  • FIG. 2 is a schematic configuration diagram of an electric deionized water producing apparatus which constitutes the pure water producing apparatus of FIG. It should be noted that the configurations of the pure water production apparatus and the electric deionized water production apparatus shown in the drawings are merely examples, and do not limit the present invention. Needless to say.
  • the pure water production apparatus 1 produces pure water by sequentially treating raw water (water to be treated), and a membrane filtration apparatus 2 and an electric deionized water production apparatus provided downstream of the membrane filtration apparatus 2.
  • a device hereinafter, also referred to as “EDI device”.
  • the membrane filtration device 2 removes impurities in raw water to generate permeated water, and a reverse osmosis membrane (RO membrane) that separates raw water into concentrated water containing impurities and permeated water from which impurities have been removed. ) Or a nanofiltration membrane (NF membrane).
  • the membrane filtration device 2 supplies a feed line L1 for supplying raw water to the membrane filtration device 2, a permeated water line L2 for circulating permeated water separated by the membrane filtration device 2, and a concentrated water separated by the membrane filtration device 2. It is connected to the concentrated water line L3 to be circulated.
  • the downstream portion of the concentrated water line L3 is branched into two lines, namely, a drainage line L4 for discharging a part of the concentrated water to the outside and a reflux water line L5 for returning the rest to the supply line L1.
  • a drainage line L4 for discharging a part of the concentrated water to the outside
  • a reflux water line L5 for returning the rest to the supply line L1.
  • an upstream portion of the concentrated water line that is not branched is simply referred to as a “concentrated water line” to be distinguished from a downstream portion, but the drainage line and the reflux water line are also referred to as a membrane filtration device. Note that it is part of a concentrate line that distributes concentrate from The reflux water line L5 is connected on the downstream side to the upstream side of the pressurizing pump 4 described later in the supply line L1.
  • the return water line L5 may be connected to a raw water tank (not shown) that stores raw water, instead of being directly connected to the supply line L1. Further, the reflux water line L5 may be omitted, that is, all the concentrated water separated by the membrane filtration device 2 may be discharged to the outside.
  • the supply line L1 is provided with a pressurization pump 4 for supplying the raw water stored in the raw water tank to the membrane filtration device 2.
  • the pressurizing pump 4 has a rotation speed controlled by an inverter (not shown), and may have a function of adjusting the supply pressure of the raw water to the membrane filtration device 2.
  • the drain line L4 is provided with a valve V1 for adjusting the flow rate of the concentrated water flowing through the drain line L4.
  • the reflux water line L5 is provided with a valve V2 for adjusting the pressure balance between the concentrated water flowing through the drainage line L4 and the concentrated water flowing through the reflux water line L5.
  • the EDI device 3 is a device that simultaneously performs the deionization (desalting) process of the water to be treated by the ion exchanger and the regeneration process of the ion exchanger.
  • the EDI device 3 is connected to the membrane filtration device 2 through a permeated water line L2, and receives the permeated water separated by the membrane filtration device 2 as water to be treated.
  • the EDI device 3 includes a treated water line L6 that circulates the treated water (deionized water) from the EDI device 3 and supplies it to a treated water tank or a point of use, and a concentrated water (hereinafter, referred to as “EDI concentrated water”) from the EDI device 3.
  • Electrode water described later is also discharged from the EDI device 3.
  • the EDI device 3 includes an anode chamber E1 having an anode 11, a cathode chamber E2 having a cathode 12, and a desalting chamber D located between the anode chamber E1 and the cathode chamber E2. It has a pair of concentrating chambers C1 and C2 arranged on both sides of the desalting chamber D.
  • the desalting chamber D is partitioned by the anion exchange membrane a1 on the anode 11 side and the cation exchange membrane c1 on the cathode 12 side.
  • the pair of concentrating chambers C1 and C2 are an anode-side concentrating chamber C1 adjacent to the desalting chamber D via the anion exchange membrane a1 and a cathode-side concentrating chamber C2 adjacent to the desalting chamber D via the cation exchange membrane c1. Is included.
  • the anode-side concentration chamber C1 is adjacent to the anode chamber E1 via the cation exchange membrane c2
  • the cathode-side concentration chamber C2 is adjacent to the cathode chamber E2 via the anion exchange membrane a2.
  • the desalting compartment D is filled with at least one of a cation exchanger and an anion exchanger, and preferably with both a cation exchanger and an anion exchanger. That is, it is preferable that the deionization chamber D is filled with a cation exchanger and an anion exchanger in a so-called mixed bed form or a double bed form.
  • the cation exchanger include cation exchange resins, cation exchange fibers, monolithic porous cation exchangers, and the most general-purpose cation exchange resins are preferably used.
  • Examples of the type of cation exchanger include a weakly acidic cation exchanger and a strongly acidic cation exchanger.
  • anion exchanger examples include anion exchange resins, anion exchange fibers, monolithic porous anion exchangers, and the most general-purpose anion exchange resins are preferably used.
  • type of anion exchanger examples include a weakly basic anion exchanger and a strongly basic anion exchanger.
  • the anode-side concentration chamber C1 and the cathode-side concentration chamber C2 are each filled with an ion exchanger in order to suppress the electric resistance of the EDI device 3.
  • the anode chamber E1 and the cathode chamber E2 are also preferably filled with a conductive substance such as an ion exchanger in order to suppress the electric resistance of the EDI device 3.
  • the anode-side concentrating chamber C1, the cathode-side concentrating chamber C2, and the cathode chamber E2 are filled with an anion exchanger, and the anode chamber E1 is filled with a cation exchanger.
  • the permeate line L2 from the membrane filtration device 2 is branched into a plurality (four in the illustrated example), and is connected to the desalting chamber D, the anode-side concentrating chamber C1, the cathode-side concentrating chamber C2, and the cathode chamber E2, respectively. ing.
  • the desalination chamber D is connected to the treated water line L6 on the downstream side.
  • the anode side concentration chamber C1 and the cathode side concentration chamber C2 form a parallel flow path, and are connected to the concentrated water discharge line L7 on the downstream side.
  • the permeated water from the membrane filtration device 2 is supplied to the desalination chamber D as the water to be treated, and is supplied to the anode side concentration chamber C1 and the cathode side concentration chamber C2 as the concentration chamber inflow water.
  • the cathode chamber E2 forms a series flow path with the anode chamber E1, and therefore the permeated water from the membrane filtration device 2 is also supplied from the cathode chamber E2 to the anode chamber E1 as the electrode chamber inflow water, and as the electrode water to the outside. Is discharged to.
  • the permeated water (water to be treated) is supplied to the desalination chamber D from the membrane filtration device 2 through the permeated water line L2, and the ionic components in the permeated water are removed when passing through the desalination chamber D.
  • the permeated water from which the ionic components have been removed is supplied as treated water (deionized water) to the treated water tank or the point of use through the treated water line L6.
  • the ionic components removed in the desalting chamber D move to the concentrating chambers C1 and C2 adjacent to the desalting chamber D due to the potential difference generated by applying the DC voltage between the both electrodes 11 and 12.
  • the cation component is attracted to the cathode 12 side, passes through the cation exchange membrane c1 and moves to the cathode side concentration chamber C2, and the anion component is attracted to the anode 11 side and passes through the anion exchange membrane a1. Then, it moves to the anode-side concentration chamber C1.
  • the ionic components thus moved to the concentration chambers C1 and C2 are taken into the concentration chamber inflow water and discharged to the outside through the concentrated water discharge line L7.
  • a water dissociation reaction (a reaction in which water dissociates into hydrogen ions and hydroxide ions) is continuously progressing.
  • the hydrogen ion is exchanged with the cation component adsorbed on the cation exchanger, and the hydroxide ion is exchanged with the anion component adsorbed on the anion exchanger. In this way, the cation exchanger and the anion exchanger filled in the desalting chamber D are regenerated.
  • an EDI device may include more than one desalination chamber.
  • the desalting chamber and the concentrating chamber are alternately provided via a cation exchange membrane or an anion exchange membrane, the concentrating chamber closest to the anode is adjacent to the anode chamber, and the concentrating chamber closest to the cathode is the cathode chamber. It will be adjacent.
  • the concentrating chamber adjacent to the electrode chamber may be omitted, and the electrode chamber may also serve as the concentrating chamber by adjoining the electrode chamber and the desalting chamber.
  • the electrode chamber also serves as the concentration chamber can be applied regardless of the number of deionization chambers.
  • the desalting chamber may be divided into two small desalting chambers in the direction of direct current flow by an intermediate ion exchange membrane (for example, a single membrane of an anion exchange membrane or a cation exchange membrane or a bipolar membrane). ..
  • the two small desalting chambers form a series flow path, and the small desalting chamber on the anode side is filled with at least an anion exchanger and the small desalting chamber on the cathode side is filled with at least a cation exchanger.
  • the water flow direction to the concentration chamber may be opposite to the water flow direction to the desalting chamber, and the pair of concentration chambers may form a series flow path.
  • the inflow water of the concentrating chamber may be a part of the treated water, and when the desalination chamber is divided into two small desalination chambers, the water to be treated is passed through one small desalination chamber. It may be a part of the intermediate treated water obtained by watering.
  • the inflow water of the electrode chamber may first flow into the anode chamber, and the electrode chambers may form parallel flow paths. Further, the inflow water of the electrode chamber may be a part of the treated water, and when the desalination chamber is divided into two small desalination chambers, the water to be treated is passed through one small desalination chamber. It may be a part of the intermediate treated water obtained by watering.
  • the raw water flowing through the supply line L1 is pressure adjusting means (not shown) such as the pressurizing pump 4 provided in the supply line L1 and the valve provided in the concentrated water line L3.
  • the pressure is increased to a pressure higher than the osmotic pressure and is supplied to the membrane filtration device 2.
  • the raw water supplied to the membrane filtration device 2 is separated into permeated water and concentrated water using the principle of reverse osmosis. Therefore, the concentrated water separated by the membrane filtration device 2 and flowing through the concentrated water line L3 has a relatively high pressure.
  • such pressure energy of the concentrated water is used when refluxing the concentrated water to the upstream side of the membrane filtration device 2 through the reflux water line L5, but cannot be said to be effectively used for other purposes. The current situation is that it is wasted.
  • the pure water production apparatus 1 of the present embodiment has a hydroelectric power generation device 5 for recovering the pressure energy of the concentrated water separated by the membrane filtration device 2 as electric power.
  • the hydroelectric power generation device 5 is provided in a concentrated water line L3 that circulates the concentrated water from the membrane filtration device 2, generates electric power by using the concentrated water flowing in the concentrated water line L3, and supplies the generated electric power to the EDI device 3. To supply.
  • the pressure energy of the concentrated water separated by the membrane filtration device 2 can be used for the EDI device 3, and the energy efficiency of the entire system can be improved.
  • the hydraulic power generation device 5 may be used as a substitute for the DC power supply device of the EDI device 3, or may be additionally used as a power source of such a DC power supply device.
  • power generation and energization of the EDI device 3 are performed in conjunction with the operation of the membrane filtration device 2. Therefore, using the hydroelectric power generation device 5 instead of or in addition to the DC power supply device of the EDI device 3 controls the power supply such that power is supplied in accordance with the water flow from the membrane filtration device 2 to the EDI device 3. It is also advantageous in that it need not be performed.
  • the power supply from the hydroelectric power generation device 5 to the EDI device 3 may be performed via a charging device or a stabilized power supply device.
  • the installation position of the hydroelectric power generation device 5 is not limited to the concentrated water line L3 as long as it can generate electric power by using the flow of the concentrated water, and for example, on the drain line L4 or the return water line L5. May be However, in order to recover more energy, the installation position of the hydroelectric power generation device 5 is preferably the position where the pressure of the concentrated water is the highest and the flow rate is the highest. That is, when the drainage line L4 and the return water line L5 are connected to the downstream side of the concentrated water line L3 as in the present embodiment, the hydraulic power generation device 5 is preferably provided in the concentrated water line L3.
  • the hydroelectric power generation device 5 there is no particular limitation on the configuration of the hydroelectric power generation device 5 as long as it can convert the pressure energy (potential energy or kinetic energy) of the concentrated water into electric energy, and it is appropriate according to the flow range of the concentrated water and the required power generation amount
  • Any known hydropower generator can be used. Among them, those having an impeller that rotates by receiving the flow of the concentrated water flowing through the concentrated water line L3 are preferable, and in particular, those configured to detect the flow rate of the concentrated water from the number of revolutions of the impeller are preferable. By using such a hydroelectric generator, it becomes unnecessary to install a flow meter in the concentrated water line L3.
  • the rotational speed of the impeller is calculated back from the measured value of the operating current (DC current flowing between the two electrodes 11 and 12) or operating voltage (DC voltage applied between the two electrodes 11 and 12) of the EDI device 3.
  • the type of hydroelectric generator and an alternating current generator can be used in addition to a direct current generator.
  • the AC generator may be directly connected to the DC power supply when used as a power supply for the DC power supply of the EDI device 3, but when used as an alternative to the DC power supply, the AC generator may be connected to the EDI via the AC/DC converter. Note that it is necessary to connect to the device 3.
  • the number of hydroelectric generators that configure the hydroelectric generator 5 is not limited to one, and a plurality of hydroelectric generators may be arranged in series in the concentrated water line L3. In that case, those electrical connections may be in series or in parallel, or may be a combination of series and parallel.
  • each hydroelectric generator has a small pressure loss in order to recover as much energy as possible, which allows as many hydroelectric generators as possible to be arranged. Become.
  • using a plurality of hydroelectric generators is also advantageous in that the amount of power generation (the amount of power supplied to the EDI device 3) can be adjusted as necessary.
  • FIG. 3 is a schematic diagram showing a configuration example of the hydraulic power generation device of the present embodiment.
  • the hydroelectric generator 5 shown in FIG. 3 bypasses the two hydroelectric generators 51 and 52 arranged in series in the concentrated water line L3 and the second hydroelectric generator 52 of the two hydroelectric generators 51 and 52.
  • it has a bypass line L31 connected to the concentrated water line L3.
  • the two hydraulic power generators 51 and 52 are electrically connected in parallel and are connected to the EDI device 3 as a DC power source of the EDI device 3.
  • the bypass line L31 is provided with a valve V3, and the concentrated water line L3 is also provided with valves V4 and V5.
  • the valve V4 is provided on the downstream side of the upstream connecting portion between the concentrated water line L3 and the bypass line L31, and the valve V5 is provided on the upstream side of the downstream connecting portion between the concentrated water line L3 and the bypass line L31. There is.
  • the valve V3 of the bypass line L31 By opening the valve V3 of the bypass line L31 and closing the valves V4 and V5 of the concentrated water line L3, the concentrated water flowing in the concentrated water line L3 can be circulated only to the first hydraulic power generator 51. As a result, power is generated only by the first hydroelectric generator 51, so that the current supplied to the EDI device 3 can be reduced.
  • the concentrated water flowing in the concentrated water line L3 is supplied to the first hydraulic power generator 51 and the second hydraulic power generator. 52 can be distributed. As a result, power is generated by both the first hydraulic power generator 51 and the second hydraulic power generator 52, so that the current supplied to the EDI device 3 can be increased.
  • the hydraulic power generation device 5 shown in FIG. 3 has a control unit (not shown) that switches the above-described two power generation modes based on the operating current of the EDI device 3.
  • ions are removed according to the amount of electricity supplied to the EDI device 3.
  • the electrical resistance of the EDI device 3 may fluctuate due to changes in the water temperature of the water to be treated and the ion composition. .. Then, as the electric resistance of the EDI device 3 increases, more electric power is required to supply the EDI device 3 with the current necessary to move the ions to be removed to the concentration chamber. Therefore, in the hydraulic power generation device 5 shown in FIG.
  • the above-described power generation mode is switched according to the fluctuation of the electric resistance of the EDI device 3, and the supply current from the hydraulic power generation device 5 to the EDI device 3 is adjusted. As a result, it becomes possible to maintain operation at the current required by the EDI device 3. For example, in a state where the electric resistance of the EDI device 3 is low, the concentrated water is passed through the bypass line L31 so that power is generated only by the first hydroelectric generator 51, but the electric resistance of the EDI device 3 increases. When the operating current becomes low, the water flow to the bypass line L31 is stopped. As a result, both the first hydroelectric generator 51 and the second hydroelectric generator 52 generate electric power, so that the supply current to the EDI device 3 increases and the constant current operation of the EDI device 3 is maintained. Will be possible.
  • the switching of the power generation mode described above may be performed based on the water quality of the raw water supplied to the membrane filtration device 2 or the deionized water produced by the EDI device 3. That is, when the water quality of the raw water deteriorates or the treated water quality of the EDI device 3 deteriorates, in order to increase the operating current of the EDI device 3 and improve the treatment performance, the water flow to the bypass line L31 is increased. May be stopped, and power generation may be performed by both the first hydraulic power generator 51 and the second hydraulic power generator 52.
  • FIG. 3 exemplifies a case where the number of hydraulic power generators constituting the hydraulic power generation device 5 is two, the number of hydraulic power generators may be three or more.
  • the bypass line may be connected to the concentrated water line L3 so as to bypass two or more hydroelectric generators.
  • two or more bypass lines may be connected to the concentrated water line L3, in which case each bypass line may bypass a different number of hydroelectric generators.
  • the hydroelectric generator 5 is composed of a plurality of hydroelectric generators, they may have the same configuration or different configurations, and depending on the flow rate range of the concentrated water and the required power generation amount, Hydropower generators of various configurations can be used in any suitable combination.
  • FIG. 4 is a schematic configuration diagram of a pure water producing apparatus according to the second embodiment of the present invention.
  • the same reference numerals are given to the drawings, the description thereof will be omitted, and only the configuration different from that of the first embodiment will be described.
  • This embodiment is a modification of the first embodiment, and in addition to the EDI device (first EDI device) 3 of the first embodiment, another EDI device (second EDI device) is provided on the downstream side thereof.
  • Device 6 is provided, which is the difference from the first embodiment.
  • the second EDI device 6 has basically the same configuration as the first EDI device 3. That is, although not shown, the second EDI device 6 is similar to the deionization chamber D of the first EDI device 3 and the pair of concentration chambers C1 and C2 of the first EDI device 3. And a pair of concentrating chambers.
  • the second EDI device 6 processes the water flowing out from the pair of concentrating chambers C1 and C2 of the first EDI device 3, that is, the EDI concentrated water from the first EDI device 3, and supplies the treated water to the supply line L1. It will be sent back to. Therefore, the desalination chamber of the second EDI device 6 is connected to the concentrated water discharge line L7 of the first EDI device 3 on the upstream side, and the treated water is returned to the supply line L1 on the downstream side. It is connected to the treated water return line L8.
  • the treated water return line L8 may be connected to the permeated water line L2 instead of the supply line L1 depending on the treated water quality of the second EDI device 6.
  • the second EDI device 6 is also connected to a concentrated water discharge line L9 that discharges the EDI concentrated water from the second EDI device 6 to the outside.
  • the second EDI device 6 does not require so much processing performance, so power control does not require so much accuracy. Therefore, in the pure water producing apparatus 1 including the two EDI devices 3 and 6 as in the present embodiment, a normal DC power supply device is used for the first EDI device 3 that requires more stable power supply control. Is preferable, and the hydroelectric power generation device 5 is preferably used as a DC power supply device of the second EDI device 6. However, depending on the power generation amount of the hydraulic power generation device 5, power may be supplied from the hydraulic power generation device 5 to the first EDI device 3 via a charging device or a stabilized power supply device. In particular, when the hydroelectric generator 5 is composed of a plurality of hydroelectric generators (see FIG. 3 ), the two EDI devices 3 and 6 may be supplied with electric power from different hydroelectric generators.
  • connection form of the two EDI devices 3 and 6 is not limited to the form shown in FIG. 4, and for example, although not shown, the two EDI devices 3 and 6 are connected in series and supplied from the membrane filtration device 2.
  • the permeated water may be treated sequentially. That is, the second EDI device 6 processes the water flowing out from the deionization chamber D of the first EDI device 3 (the deionized water produced by the first EDI device 3), and the treated water is treated water. It may be supplied to a tank or a point of use. In this case, the power supply from the hydroelectric generator 5 may be supplied to either of the two EDI devices 3 and 6, or may be supplied to both of them.
  • FIG. 5 is a schematic block diagram of the pure water manufacturing apparatus which concerns on the 3rd Embodiment of this invention.
  • the same reference numerals are given to the drawings, the description thereof will be omitted, and only the configuration different from the above-described embodiment will be described.
  • the present embodiment is a modification of the first embodiment, and in addition to the membrane filtration device (first membrane filtration device) 2 of the first embodiment, another membrane filtration device (first membrane filtration device) is provided on the downstream side thereof.
  • the second embodiment is different from the first embodiment in that the second membrane filtration device 7 is provided.
  • the second membrane filtration device 7 has an RO membrane or an NF membrane similarly to the first membrane filtration device 2, and the first membrane filtration device 2 via the permeated water line (first permeated water line) L2. It is connected to the. That is, the second membrane filtration device 7 is connected in series to the first membrane filtration device 2 on the downstream side of the first membrane filtration device 2 and separated by the first membrane filtration device 2 as water to be treated.
  • the second membrane filtration device 7 is connected to a second permeate line L10 for circulating the permeated water separated by the second membrane filtration device 7, and the second permeate line L10 is connected to the EDI device 3 It is connected to the.
  • the second membrane filtration device 7 is connected to a second concentrated water line L11 for circulating the concentrated water separated by the second membrane filtration device 7. Since the second membrane filtration device 7 further separates the permeated water from the first membrane filtration device 2 into permeated water and concentrated water, from the viewpoint of water quality, the concentrated water from the second membrane filtration device 7 is It is not always necessary to discharge it to the outside. Therefore, from the viewpoint of saving water, the second concentrated water line L11 is supplied on the upstream side of the pressurizing pump 4 in order to return all the concentrated water separated by the second membrane filtration device 7 to the supply line L1. It is connected to the line L1.
  • the second concentrated water line L11 may be connected to a raw water tank (not shown) provided in the supply line L1 instead of being directly connected to the supply line L1.
  • a drain line for discharging may be connected.
  • the hydroelectric power generation device 5 is provided in the first concentrated water line L3 connected to the first membrane filtration device 2, but the installation position of the hydroelectric power generation device 5 is not limited to this, and for example, the second It may be on the concentrated water line L11.
  • the feed pressure of the water to be treated (raw water) to the first membrane filtration device 2 is increased. Is greater than the supply pressure of the water to be treated (permeated water from the first membrane filtration device 2) to the second membrane filtration device 7. Accordingly, the pressure of the concentrated water from the first membrane filtration device 2 becomes larger than the pressure of the concentrated water from the second membrane filtration device 7. Therefore, the hydroelectric power generation device 5 is preferably provided in the first concentrated water line L3 connected to the first membrane filtration device 2 from the viewpoint that a high power generation amount can be expected.
  • the two membrane filtration devices 2 and 7 are connected in series, and the permeated water from the first membrane filtration device 2 is supplied to the second membrane filtration device 7.
  • the connection form of the two membrane filtration devices 2 and 7 is not limited to such a form.
  • the primary sides (the side through which raw water and concentrated water flow) of two membrane filtration devices (RO membrane or NF membrane) 2, 7 are connected in series, and the secondary sides (the side through which permeated water flows) are connected in parallel. It may be connected. That is, the concentrated water from the first membrane filtration device 2 is supplied to the second membrane filtration device 7, and the permeated water from the first membrane filtration device 2 and the permeated water from the second membrane filtration device 7 are EDI. It may be adapted to be supplied to the device 3. Also in such a case, it is preferable that the hydroelectric power generation device 5 be provided in the first concentrated water line L3 through which the higher-pressure concentrated water flows.
  • FIG. 6 is a schematic configuration diagram of a pure water producing apparatus according to the fourth embodiment of the present invention.
  • the same reference numerals are given to the drawings, the description thereof will be omitted, and only the configuration different from the above-described embodiment will be described.
  • the present embodiment is a modified example of the first embodiment, in which a chemical liquid injector 8 and a deaerator 9 are additionally provided, and a hydroelectric power generator 5 is a power source for the chemical liquid injector 8 and the deaerator 9, respectively. Is different from that of the first embodiment. In other words, the present embodiment is different from the first embodiment in that the electric power generated by the hydraulic power generation device 5 is supplied to the chemical liquid injection device 8 and the degassing device 9, respectively. However, depending on the power generation amount of the hydroelectric power generation device 5, the generated power may be supplied to only one of the chemical liquid injection device 8 and the degassing device 9, or in addition to the chemical liquid injection device 8 and the degassing device 9. It may also be supplied to the EDI device 3.
  • the chemical liquid injection device 8 is provided on the upstream side of the membrane filtration device 2 and adds a chemical liquid such as a scale inhibitor or slime control agent to raw water.
  • the chemical liquid injector 8 includes a chemical liquid tank 21 that stores the chemical liquid, and a chemical injection pump 22 that is connected to the supply line L1 via the chemical liquid supply line L12 and injects the chemical liquid stored in the chemical liquid tank 21 into the supply line L1.
  • a chemical injection pump 22 that is connected to the supply line L1 via the chemical liquid supply line L12 and injects the chemical liquid stored in the chemical liquid tank 21 into the supply line L1.
  • Have The electric power generated by the hydroelectric power generation device 5 is supplied to the chemical injection pump 22. Therefore, in the chemical liquid injection device 8, the chemical liquid is added to the raw water in conjunction with the operation of the membrane filtration device 2.
  • the addition position of the chemical liquid is not limited to the illustrated position as long as it is on the upstream side of the membrane filtration device 2, and may be, for example, on the downstream side of the connecting portion between the supply line L1 and the reflux water line L5.
  • the type of the added chemical solution may be a pH adjusting agent or a reducing agent, in addition to the above-mentioned scale inhibitor or slime controlling agent.
  • the deaerator 9 is provided in the permeate line L2 on the downstream side of the membrane filtration device 2 and removes gases such as carbon dioxide and oxygen dissolved in the permeate from the membrane filtration device 2.
  • the configuration of the deaerator 9 is not particularly limited, and a known deaerator suitable for the type of gas to be removed can be used. Examples of such a deaerator include a membrane deaerator and a decarbonation tower.
  • the membrane deaerator removes the dissolved oxygen in the treated water from the primary side of the degassed membrane by depressurizing the secondary side of the degassed membrane with a vacuum pump while passing the treated water through the primary side of the degassed membrane.
  • the electric power generated by the hydroelectric power generation device 5 is supplied to a vacuum pump when the degassing device 9 is a membrane degassing device, and is supplied to a blower when the degassing device 9 is a decarbonation tower.
  • the degassing process is performed in conjunction with the operation of the membrane filtration device 2.
  • the installation position of the deaerator 9 is not limited to the illustrated position, and may be, for example, on the upstream side of the membrane filtration device 2.
  • the installation of the chemical liquid injector and the deaerator as in the present embodiment is possible not only in the first embodiment but also in the second and third embodiments.
  • the installation position of the chemical injection device or the degassing device is not particularly limited, and the chemical injection device or the degassing device is installed at an appropriate position according to the type of the added chemical liquid or the type of gas to be removed. be able to.
  • the chemical liquid injector is the permeated water from the first membrane filtration device 2. It may be installed at a position where a chemical solution is added to.
  • the chemical liquid injection device is It may be installed at a position where the chemical solution is added to the concentrated water from the membrane filtration device 2 of No. 1.
  • the desalination rate in the membrane filtration device was calculated from the conductivity of raw water (conductivity of treated water) and the conductivity of permeated water from the membrane filter (conductivity of treated water).
  • the desalination rate in the electric deionized water production device is the conductivity of the permeated water from the membrane filtration device (conductivity of treated water) and the conductivity of the deionized water from the electric deionized water production device (treated water Conductivity).
  • the desalination rate of the entire system was calculated from the electrical conductivity of the raw water (conductivity of the treated water) and the electrical conductivity of the deionized water from the electric deionized water production apparatus (conductivity of the treated water).
  • the size of each chamber was 10 cm ⁇ 10 cm ⁇ 1 cm.
  • Each of the deionization chambers of the electric deionized water production apparatus was filled with a cation exchange resin and an anion exchange resin in a mixed bed form, and each concentration chamber was filled with an anion exchange resin.
  • Water having a conductivity of about 200 ⁇ S/cm was used as the water to be treated (raw water), and the flow rate of the raw water supplied to the membrane filtration device was 330 L/h.
  • the processing flow rate of the electric deionized water production apparatus (the flow rate of the water to be treated flowing into the processing chamber), the flow rate of the concentration chamber inflow water, and the flow rate of the electrode chamber inflow water were 40 L/h, 25 L/h and 15 L, respectively. /H.
  • the flow rate and pressure of the concentrated water flowing from the membrane filtration device to the concentrated water line were 250 L/h and 0.53 MPa, respectively.
  • hydroelectric generator As the hydroelectric generator, seven hydroelectric generators (product number “DB-2689”, Foshan Shunde Zhongjiang Energy Saving Electronics made by Spatial Electronics) were spatially connected in series and electrically connected in parallel. Then, the electric power generated by the hydraulic power generation device was supplied to the electric deionized water manufacturing device as a substitute for the DC power supply device. At this time, the operating current of the electric deionized water producing apparatus was 0.1 A, and the operating voltage (supply voltage) was 6V. The pressure loss of the entire hydroelectric power generation device was 0.13 MPa.
  • the conductivity of the raw water, the conductivity of the permeated water from the membrane filtration device, and the conductivity of the deionized water from the electric deionized water production device were measured to be 198 ⁇ S/cm, 4.72 ⁇ S/cm, and 0, respectively. It was 0.15 ⁇ S/cm.
  • the desalination rate in the membrane filtration apparatus, the desalination rate in the electric deionized water production apparatus, and the desalination rate in the entire system were calculated from these electrical conductivities by the above formula (1), 97.6%, 96.8%, and 99.9%, respectively. Therefore, it was confirmed that the desired water quality can be obtained without using the normally used DC power supply device.
  • an electric deionized water producing apparatus similar to the above-mentioned embodiment is used, except that the number of the deionization chamber is one, and each concentration chamber is filled with anion exchange resin. It was investigated how the operating voltage of the electric deionized water production device changes depending on whether or not the electric deionized water is produced. Specifically, the same conditions (water having a conductivity of 3.6 ⁇ S/cm as the water to be treated (membrane filtration device) were used in both cases where each concentration chamber was filled with anion exchange resin and not filled with anion exchange resin. The permeated water from the above) was used and the operation was performed under the condition that the operating current was set to 0.1 A), and the respective operating voltages were compared.

Abstract

Le but de la présente invention est de réaliser des économies d'énergie en utilisant efficacement une énergie perdue. L'invention concerne un appareil de production d'eau pure 1 équipé : d'un dispositif de filtration à membrane 2 muni d'une membrane d'osmose inverse ou d'une membrane de nanofiltration chacune apte à séparer l'eau présentant un intérêt en eau osmosée et en eau condensée ; d'un dispositif de traitement de l'eau qui peut traiter l'eau présentant un intérêt et l'une ou l'autre de l'eau osmosée et de l'eau condensée ; et d'une unité de puissance hydraulique qui est disposée sur une ligne d'eau condensée L3 à travers laquelle l'eau condensée provenant du dispositif de filtration à membrane 2 doit être mise en circulation, pouvant générer de l'énergie électrique à l'aide de l'écoulement de l'eau condensée s'écoulant dans la ligne d'eau condensée L3 et pouvant fournir l'énergie électrique générée au dispositif de traitement d'eau 3.
PCT/JP2019/041361 2019-01-16 2019-10-21 Appareil de production d'eau pure et son procédé de fonctionnement WO2020148961A1 (fr)

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TWI779847B (zh) * 2021-09-27 2022-10-01 國立臺灣大學 含溶解性鹽類或酸類排水的處理方法

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