CN113015702B - Pure water production apparatus and method for operating same - Google Patents
Pure water production apparatus and method for operating same Download PDFInfo
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- CN113015702B CN113015702B CN201980074544.3A CN201980074544A CN113015702B CN 113015702 B CN113015702 B CN 113015702B CN 201980074544 A CN201980074544 A CN 201980074544A CN 113015702 B CN113015702 B CN 113015702B
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 336
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 39
- 238000000034 method Methods 0.000 title claims description 17
- 238000005374 membrane filtration Methods 0.000 claims abstract description 111
- 239000012528 membrane Substances 0.000 claims abstract description 58
- 239000012466 permeate Substances 0.000 claims abstract description 50
- 239000012141 concentrate Substances 0.000 claims abstract description 46
- 238000010248 power generation Methods 0.000 claims abstract description 37
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 9
- 238000001728 nano-filtration Methods 0.000 claims abstract description 7
- 238000010612 desalination reaction Methods 0.000 claims description 30
- 238000009296 electrodeionization Methods 0.000 claims description 30
- 238000011033 desalting Methods 0.000 claims description 29
- 150000001450 anions Chemical class 0.000 claims description 16
- 150000001768 cations Chemical class 0.000 claims description 16
- 239000008367 deionised water Substances 0.000 claims description 16
- 229910021641 deionized water Inorganic materials 0.000 claims description 16
- 150000002500 ions Chemical class 0.000 claims description 15
- 238000005341 cation exchange Methods 0.000 claims description 11
- 238000011144 upstream manufacturing Methods 0.000 claims description 11
- 239000003011 anion exchange membrane Substances 0.000 claims description 10
- 230000005611 electricity Effects 0.000 claims description 7
- 239000000126 substance Substances 0.000 description 27
- 239000007788 liquid Substances 0.000 description 21
- 238000002347 injection Methods 0.000 description 13
- 239000007924 injection Substances 0.000 description 13
- 238000010586 diagram Methods 0.000 description 12
- ZZUFCTLCJUWOSV-UHFFFAOYSA-N furosemide Chemical compound C1=C(Cl)C(S(=O)(=O)N)=CC(C(O)=O)=C1NCC1=CC=CO1 ZZUFCTLCJUWOSV-UHFFFAOYSA-N 0.000 description 10
- 239000003957 anion exchange resin Substances 0.000 description 8
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- -1 hydrogen ions Chemical class 0.000 description 4
- 230000004048 modification Effects 0.000 description 4
- 238000012986 modification Methods 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 3
- 239000003729 cation exchange resin Substances 0.000 description 3
- 239000003814 drug Substances 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 230000002378 acidificating effect Effects 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 229940023913 cation exchange resins Drugs 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000000835 fiber Substances 0.000 description 2
- 239000000945 filler Substances 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 230000003204 osmotic effect Effects 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000002455 scale inhibitor Substances 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 1
- 238000005349 anion exchange Methods 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000004020 conductor Substances 0.000 description 1
- 238000005262 decarbonization Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000007872 degassing Methods 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 239000008235 industrial water Substances 0.000 description 1
- 239000003014 ion exchange membrane Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000003002 pH adjusting agent Substances 0.000 description 1
- 238000005381 potential energy Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000002349 well water Substances 0.000 description 1
- 235000020681 well water Nutrition 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—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
Landscapes
- Engineering & Computer Science (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- Health & Medical Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Urology & Nephrology (AREA)
- Environmental & Geological Engineering (AREA)
- Organic Chemistry (AREA)
- Nanotechnology (AREA)
- Analytical Chemistry (AREA)
- Molecular Biology (AREA)
- Electrochemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Water Treatment By Electricity Or Magnetism (AREA)
Abstract
The invention effectively utilizes the wastefully consumed energy to realize energy saving. The pure water production device (1) comprises: a membrane filtration device (2) having a reverse osmosis membrane or nanofiltration membrane for separating water to be treated into permeate water and concentrate water; a water treatment device (3) for treating any one of treated water, permeate water and concentrated water; and a hydroelectric power generation device (5) which is provided in a concentrated water line (L3) through which the concentrated water from the membrane filtration device (2) flows, generates power by using the flow of the concentrated water flowing through the concentrated water line (L3), and supplies the generated power to the water treatment device (3).
Description
Technical Field
The present invention relates to a pure water production apparatus and a method for operating the same.
Background
As a method for producing pure water from raw water such as industrial water, well water, municipal water, etc., a method using a reverse osmosis membrane (RO membrane) or nanofiltration membrane (NF membrane) and an ion exchanger is known. According to this method, deionized water (pure water) can be produced by separating raw water into permeate water and concentrate water by an RO membrane or NF membrane and then passing the permeate water further through an ion exchanger. That is, as an apparatus for producing pure water from raw water, a pure water producing apparatus is known which combines a membrane filtration apparatus having an RO membrane or NF membrane with an electrodeionization water producing apparatus (for example, refer to patent document 1).
Prior art literature
Patent literature
Patent document 1: japanese patent application laid-open No. 2001-104959
Disclosure of Invention
Problems to be solved by the invention
In such a pure water production apparatus, raw water is supplied to the RO membrane or NF membrane of the membrane filtration apparatus at a pressure equal to or higher than the osmotic pressure, and is separated into permeate water and concentrate water by the principle of reverse osmosis. Thus, the concentrated water separated by the membrane filtration device becomes a higher pressure. However, in the present situation, although the pressure energy of the concentrated water is sometimes used to return a part of the concentrated water to the upstream side of the membrane filtration device, it cannot be said that the concentrated water is effectively used for other purposes, and thus is wastefully consumed.
Accordingly, an object of the present invention is to provide a pure water production apparatus and an operation method thereof, which can effectively utilize wastefully consumed energy to achieve energy saving.
Means for solving the problems
In order to achieve the above object, a pure water production apparatus of the present invention comprises: a membrane filtration device having a reverse osmosis membrane or nanofiltration membrane for separating water to be treated into permeate water and concentrate water; a water treatment device for treating any one of water to be treated, permeate water and concentrated water; and a hydroelectric power generation device which is provided in a concentrated water line through which the concentrated water from the membrane filtration device flows, and which generates power by utilizing the flow of the concentrated water flowing through the concentrated water line, and which supplies power generated by the power generation to the water treatment device.
The method for operating a pure water production apparatus according to the present invention is a method for operating a pure water production apparatus comprising: a membrane filtration device having a reverse osmosis membrane or nanofiltration membrane for separating water to be treated into permeate water and concentrate water; and a water treatment device for treating any one of water to be treated, permeate water and concentrated water, wherein the operation method of the pure water production device comprises the following steps: the power generation is performed by using the flow of the concentrated water from the membrane filtration device, and the power generated by the power generation is supplied to the water treatment device.
According to the pure water production apparatus and the operation method thereof, 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 attached to the membrane filtration apparatus. This can improve the energy efficiency of the entire system.
Effects of the invention
As described above, according to the present invention, energy saving can be achieved by effectively utilizing wastefully consumed energy.
Drawings
FIG. 1 is a schematic configuration diagram of a pure water producing apparatus according to a first embodiment of the present invention.
Fig. 2 is a schematic configuration diagram of an apparatus for producing electrodeionization water according to a first embodiment of the present invention.
Fig. 3 is a schematic diagram showing an example of the structure of the hydroelectric power generator according to the first embodiment of the present invention.
FIG. 4 is a schematic configuration diagram of a pure water producing apparatus according to a second embodiment of the present invention.
FIG. 5 is a schematic configuration diagram of a pure water producing apparatus according to a third embodiment of the present invention.
FIG. 6 is a schematic configuration diagram of a pure water producing apparatus according to a fourth embodiment of the present invention.
Detailed Description
Hereinafter, embodiments of the present invention will be described with reference to the drawings.
(first embodiment)
FIG. 1 is a schematic configuration diagram of a pure water producing apparatus according to a first embodiment of the present invention. FIG. 2 is a schematic configuration diagram of an electrodeionization water producing apparatus constituting the apparatus for producing pure water of FIG. 1. The configurations of the pure water production apparatus and the electrodeionization water production apparatus shown in the drawings are merely examples, and it is needless to say that the present invention is not limited to the examples, and the apparatus can be modified as appropriate depending on the purpose, use, and required performance of the apparatus.
The pure water producing apparatus 1 is an apparatus for producing pure water by sequentially treating raw water (water to be treated), and includes a membrane filter 2 and an electrodeionization water producing apparatus (hereinafter, also referred to as "EDI apparatus") 3 provided downstream of the membrane filter 2.
The membrane filtration device 2 is a device for removing impurities in raw water to produce permeate water, and includes a reverse osmosis membrane (RO membrane) or nanofiltration membrane (NF membrane) for separating raw water into concentrate water containing impurities and permeate water from which impurities have been removed. The membrane filtration device 2 is connected to a feed line L1 for feeding raw water to the membrane filtration device 2, a permeate line L2 for allowing permeate separated by the membrane filtration device 2 to flow therethrough, and a concentrate line L3 for allowing concentrate separated by the membrane filtration device 2 to flow therethrough. The downstream portion of the concentrate line L3 is branched into 2 lines, namely, a drain line L4 for discharging a part of the concentrate to the outside and a return line L5 for returning the remaining part of the concentrate to the supply line L1. Hereinafter, for convenience of explanation, the portion of the concentrate line on the upstream side, which is not branched, will be simply referred to as "concentrate line", and the portion on the downstream side will be distinguished from each other, but it should be noted that the drain line and the return line are also part of the concentrate line through which concentrate from the membrane filtration device flows. The return water line L5 is connected to the supply line L1 on the downstream side thereof on the upstream side of a pressurizing pump 4 described later. The return water line L5 may be connected to a raw water tank (not shown) for storing raw water, instead of being directly connected to the supply line L1. In addition, the return water line L5 may be omitted, that is, all of the concentrated water separated by the membrane filtration device 2 may be discharged to the outside.
The supply line L1 is provided with a pressurizing pump 4 for supplying raw water stored in the raw water tank to the membrane filtration device 2. The pressurizing pump 4 may have a function of controlling the rotation speed by an inverter (not shown) and 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 return water line L5 is provided with a valve V2 for adjusting the pressure balance between the concentrated water flowing through the drain line L4 and the concentrated water flowing through the return water line L5.
The EDI apparatus 3 is an apparatus that performs both the deionized (desalting) treatment of the water to be treated by the ion exchanger and the regenerating treatment of the ion exchanger. The EDI device 3 is connected to the membrane filtration device 2 via a permeate line L2, and receives the permeate separated by the membrane filtration device 2 as the water to be treated. The EDI apparatus 3 is connected to a treatment water line L6 through which the treatment water (deionized water) from the EDI apparatus 3 flows and is supplied to a treatment water tank or a point of use, and a concentrated water discharge line L7 through which the concentrated water (hereinafter, also referred to as "EDI concentrated water") from the EDI apparatus 3 is discharged to the outside. The EDI concentrate may be partially or completely returned to the supply line L1 or the raw water tank according to the water quality. Although not shown in fig. 1, electrode water described later is also discharged from the EDI device 3.
Referring to fig. 2, the edi device 3 has: an anode chamber E1 provided with an anode 11; a cathode chamber E2 provided with a cathode 12; a desalting chamber D located between the anode chamber E1 and the cathode chamber E2; a pair of concentrating chambers C1 and C2 disposed on both sides of the desalting chamber D. The desalting chamber D is partitioned by an anion-exchange membrane a1 on the anode 11 side and a cation-exchange membrane c1 on the cathode 12 side. The pair of concentrating chambers C1 and C2 includes an anode-side concentrating chamber C1 adjacent to the desalting chamber D via an anion exchange membrane a1, and a cathode-side concentrating chamber C2 adjacent to the desalting chamber D via a cation exchange membrane C1. The anode-side concentrating chamber C1 is adjacent to the anode chamber E1 through the cation exchange membrane C2, and the cathode-side concentrating chamber C2 is adjacent to the cathode chamber E2 through the anion exchange membrane a 2.
The desalting chamber D is filled with at least one of a cation exchanger and an anion exchanger, preferably with both of the cation exchanger and the anion exchanger. That is, the desalting chamber D is preferably filled with a cation exchanger and an anion exchanger in a so-called mixed bed system or a multiple bed system. Examples of the cation exchanger include cation exchange resins, cation exchange fibers, monolithic porous cation exchangers, and the like, and most preferably general-purpose cation exchange resins are used. Examples of the type of the cation exchanger include a weakly acidic cation exchanger and a strongly acidic cation exchanger. Examples of the anion exchanger include anion exchange resins, anion exchange fibers, monolithic porous anion exchangers, and the like, and most preferably general-purpose anion exchange resins are used. Examples of the type of the anion exchanger include a weakly basic anion exchanger and a strongly basic anion exchanger.
In order to suppress the electric resistance of the EDI device 3, it is preferable that the anode-side concentration chamber C1 and the cathode-side concentration chamber C2 are filled with ion exchangers, respectively. In order to suppress the electrical resistance of the EDI device 3, it is preferable that the anode chamber E1 and the cathode chamber E2 are also filled with a conductive material such as an ion exchanger, respectively. As an example, 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 of (4 in the illustrated example) sections, and is connected to the desalination chamber D, the anode-side concentration chamber C1, the cathode-side concentration chamber C2, and the cathode chamber E2, respectively. The desalination chamber D is connected to a treated water line L6 at its downstream side. The anode-side concentrating chamber C1 and the cathode-side concentrating chamber C2 form parallel channels, and are connected to a concentrated water discharge line L7 on the downstream side thereof. In this way, the permeate 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 concentrate-chamber inflow water. Since the cathode chamber E2 and the anode chamber E1 form a serial flow path, the permeate water from the membrane filtration device 2 is also supplied from the cathode chamber E2 to the anode chamber E1 as electrode chamber inflow water, and is discharged to the outside as electrode water.
In the desalination chamber D, permeate water (water to be treated) is supplied from the membrane filtration device 2 through the permeate water line L2, and ion components in the permeate water are removed when passing through the desalination chamber D. The permeate water from which the ion components have been removed is supplied as treated water (deionized water) to a treatment water tank or a point of use through a treated water line L6. At this time, the ion components removed in the desalting chamber D are moved to the concentrating chambers C1 and C2 adjacent to the desalting chamber D by a potential difference generated by applying a dc voltage between the two electrodes 11 and 12. Specifically, the cation component is attracted to the cathode 12 side, moves to the cathode side concentrating chamber C2 through the cation exchange membrane C1, and the anion component is attracted to the anode 11 side, and moves to the anode side concentrating chamber C1 through the anion exchange membrane a 1. Thus, the ion components moved to the concentrating chambers C1 and C2 are taken into the concentrating chamber inflow water, and discharged to the outside through the concentrating water discharge line L7. On the other hand, in the desalting chamber D, the hydrolysis reaction (reaction of dissociating water into hydrogen ions and hydroxide ions) proceeds continuously. The hydrogen ions are exchanged with the cation component adsorbed to the cation exchanger, and the hydroxide ions are exchanged with the anion component adsorbed to the anion exchanger. In this way, the cation exchanger and the anion exchanger filled in the desalting chamber D are regenerated, respectively.
Further, as mentioned at the outset, the illustrated structure of the EDI device 3 is only one example. The structure (number, arrangement, etc.) of each chamber, the flow path structure, or the addition of valves, gauges, etc. can be appropriately changed according to the purpose, use, and performance required of the apparatus. For example, the EDI apparatus may include 2 or more desalination chambers. In this case, the desalting chamber and the concentrating chamber are alternately arranged with a cation exchange membrane or an anion exchange membrane interposed therebetween, the concentrating chamber closest to the anode being adjacent to the anode chamber, and the concentrating chamber closest to the cathode being adjacent to the cathode chamber. On the other hand, the concentration chamber adjacent to the electrode chamber (anode chamber or cathode chamber) may be omitted, and the electrode chamber may be also used as the concentration chamber by being adjacent to the desalination chamber. The structure in which such an electrode chamber also serves as a concentration chamber can be applied irrespective of the number of desalting chambers. The desalting chamber may be divided into 2 small desalting chambers in the direction of the direct current flow by an intermediate ion exchange membrane (for example, a single membrane of an anion exchange membrane or a cation exchange membrane, a bipolar membrane, or the like). In this case, the 2 small desalination chambers form a serial flow path, and at least the anion exchanger is filled in the small desalination chamber on the anode side, and at least the cation exchanger is filled in the small desalination chamber on the cathode side. The water flow direction to the concentrating chambers may be opposite to the water flow direction to the desalting chambers, and a pair of concentrating chambers may form a series flow path. The concentrate chamber inflow water may be a part of the treated water, or may be a part of the intermediate treated water obtained by passing the treated water through one small desalting chamber when the desalting chamber is divided into 2 small desalting chambers. The electrode chamber inflow water may first flow into the anode chamber, or the electrode chambers may form parallel flow paths. The electrode chamber inflow water may be a part of the treated water, or may be a part of the intermediate treated water obtained by passing the water to be treated through one small desalting chamber when the desalting chamber is divided into 2 small desalting chambers.
However, in the pure water production apparatus 1, the raw water flowing through the supply line L1 is supplied to the membrane filtration apparatus 2 by being pressurized to a pressure equal to or higher than the osmotic pressure by a pressure pump 4 provided in the supply line L1 and a pressure adjusting means (not shown) such as a valve provided in the concentrate line L3. Then, the raw water supplied to the membrane filtration device 2 is separated into permeate water and concentrate water by the principle of reverse osmosis. Thus, the concentrated water separated by the membrane filtration device 2 and flowing through the concentrated water line L3 becomes a relatively high pressure. However, although the pressure energy of the concentrated water is utilized when the concentrated water is returned to the upstream side of the membrane filtration device 2 through the return water line L5, the pressure energy cannot be effectively utilized for other applications, and is thus wastefully consumed.
Therefore, the pure water production apparatus 1 of the present embodiment includes the 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 hydro-power generator 5 is provided in a concentrated water line L3 through which the concentrated water from the membrane filter device 2 flows, generates power by the concentrated water flowing through the concentrated water line L3, and supplies the power generated by the power generation to the EDI device 3. With such a hydroelectric power generation device 5, 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 can be improved as a whole system.
The hydro-power generator 5 may be used instead of the dc power supply device of the EDI device 3, or may be additionally used as a power supply of such a dc power supply device. In the hydroelectric power generator 5, power generation and energization to the EDI device 3 are performed in conjunction with the operation of the membrane filtration device 2. Therefore, the use of the hydraulic power generation device 5 instead of or in addition to the direct-current power supply device of the EDI device 3 is also advantageous in terms of power supply control in which it is not necessary to perform power supply in accordance with the supply of water from the membrane filtration device 2 to the EDI device 3. In addition, when the fluctuation of the power generation amount of the hydro-power generating device 5 is large, the power supply from the hydro-power generating device 5 to the EDI device 3 may be performed via a charging device or a stabilized power supply device.
The position of the hydroelectric power generator 5 is not limited to the concentrate line L3 as long as it can generate electricity by the flow of concentrate, and may be, for example, a drain line L4 or a return line L5. However, in order to recover more energy, the hydroelectric power generator 5 is preferably installed at a position where the pressure of the concentrated water is highest and the flow rate is greatest. That is, as in the present embodiment, when the drain line L4 and the return line L5 are connected to the downstream side of the concentrate line L3, the hydroelectric power generator 5 is preferably provided in the concentrate line L3.
The configuration of the hydroelectric power generator 5 is not particularly limited as long as it can convert the pressure energy (potential energy or kinetic energy) of the concentrated water into electric energy, and any suitable known hydroelectric power generator can be used depending on the flow rate range of the concentrated water or the required amount of electric power generation. Among them, a hydroelectric generator having an impeller that rotates by receiving the flow of the concentrated water flowing through the concentrated water line L3 is preferable, and in particular, it is preferable to detect the flow rate of the concentrated water based on the rotation speed of the impeller. By using such a hydroelectric generator, it is not necessary to provide a flowmeter in the concentrate line L3. In this case, the rotation speed of the impeller may be inversely calculated based on the measured value of the operation current (the direct current flowing between the two electrodes 11, 12) or the operation voltage (the direct voltage applied between the two electrodes 11, 12) of the EDI device 3. The type of the hydroelectric generator is not particularly limited, and an alternator may be used in addition to the dc generator. However, it should be noted that, in the case of using as the power source of the dc power source device of the EDI device 3, the alternator may be directly connected to the dc power source device, but in the case of using as an alternative to the dc power source device, it is necessary to connect to the EDI device 3 via an ac/dc conversion device.
The number of the hydro-generators constituting the hydro-generator device 5 is not limited to 1, and a plurality of the hydro-generators may be arranged in series in the concentrate line L3. In this case, their electrical connections may be in series, parallel, or a combination of series and parallel. In the case of using a plurality of hydro generators, it is preferable that the pressure loss of each hydro generator is small in order to recover as much energy as possible, and thus, as many hydro generators as possible can be arranged. On the other hand, the use of a plurality of hydro generators is also advantageous in that the amount of generated electricity (the amount of electric power supplied to the EDI device 3) can be adjusted as needed. An example of the structure of the hydroelectric power generator 5 will be described below with reference to fig. 3. Fig. 3 is a schematic diagram showing an example of the structure of the hydroelectric power generator according to the present embodiment.
The hydro-power generation device 5 shown in fig. 3 includes: 2 hydro-generators 51, 52 arranged in series in the concentrate line L3; the bypass line L31 is connected to the concentrated water line L3 so as to bypass the second hydro generator 52 of the 2 hydro generators 51, 52. The 2 hydro-generators 51, 52 are electrically connected in parallel, and are connected to the EDI device 3 as a direct-current power supply 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-side connection portion between the concentrate line L3 and the bypass line L31, and the valve V5 is provided on the upstream side of the downstream-side connection portion between the concentrate line L3 and the bypass line L31. By opening the valve V3 of the bypass line L31 and closing the valves V4 and V5 of the concentrate line L3, the concentrate flowing through the concentrate line L3 can be circulated only to the first hydro generator 51. Accordingly, since the electric power generation is performed only by the first hydro-generator 51, the supply current to the EDI device 3 can be reduced. Further, by closing the valve V3 of the bypass line L31 and opening the valves V4 and V5 of the concentrated water line L3, the concentrated water flowing through the concentrated water line L3 can be circulated to both the first and second hydro generators 51 and 52. In this way, since both the first and second hydro generators 51 and 52 are used to generate electric power, the supply current to the EDI device 3 can be increased.
The hydro-power generation device 5 shown in fig. 3 includes a control unit (not shown) that performs the switching of the 2 power generation modes based on the operation current of the EDI device 3. In general, in the EDI device 3, ion removal is performed according to the amount of electricity supplied to the EDI device 3, but there are cases where the resistance of the EDI device 3 varies due to a change in the water temperature of the water to be treated or the ion composition. When the electrical resistance of the EDI device 3 increases, more power is required to supply the EDI device 3 with a current required to move the ions to be removed to the concentration chamber. Therefore, in the hydro-power generator 5 shown in fig. 3, the above-described power generation mode is switched according to the fluctuation of the resistance of the EDI device 3, and the supply current from the hydro-power generator 5 to the EDI device 3 is adjusted. As a result, the EDI device 3 can be maintained in operation at a current required for the EDI device. For example, while the concentrated water is passed through the bypass line L31 in a state where the electrical resistance of the EDI device 3 is low, the first hydroelectric generator 51 is used only to generate electricity, but when the electrical resistance of the EDI device 3 increases and the operating current decreases, the water supply to the bypass line L31 is stopped. As a result, by generating electric power by both the first and second hydro-generators 51 and 52, the supply current to the EDI device 3 increases, and thus the constant current operation of the EDI device 3 can be maintained.
The switching of the power generation mode may be performed based on the quality of raw water supplied to the membrane filtration device 2 or deionized water produced by the EDI device 3. That is, when the quality of raw water is deteriorated or the quality of treated water of the EDI device 3 is lowered, in order to increase the operation current of the EDI device 3 and to improve the treatment performance, the water supply to the bypass line L31 may be stopped and the electric power may be generated by both the first and second hydro generators 51 and 52.
In fig. 3, the case where the number of hydro-generators constituting the hydro-generator device 5 is 2 is illustrated, but the number of hydro-generators may be 3 or more. In the case where the number of hydro-generators is 3 or more, the bypass line may be connected to the concentrated water line L3 so as to bypass 2 or more hydro-generators. Alternatively, more than 2 bypass lines may be connected to the concentrate line L3, in which case each bypass line may bypass a different number of hydro-generators. In the case where the hydroelectric power generator 5 is constituted by a plurality of hydroelectric power generators, they may have the same structure or may have different structures, and hydroelectric power generators having various structures may be appropriately combined and used according to the flow rate range of the concentrated water or the required power generation amount.
(second embodiment)
FIG. 4 is a schematic configuration diagram of a pure water producing apparatus according to a second embodiment of the present invention. Hereinafter, the same components as those of the first embodiment are denoted by the same reference numerals in the drawings, and the description thereof is omitted, and only the components different from those of the first embodiment will be described.
The present embodiment is a modification of the first embodiment, and differs from the first embodiment in that another EDI device (second EDI device) 6 is provided on the downstream side thereof in addition to the EDI device (first EDI device) 3 of the first embodiment. The second EDI device 6 has substantially the same structure as the first EDI device 3. That is, although not shown, the second EDI device 6 has a desalination chamber identical to the desalination chamber D of the first EDI device 3 and a pair of concentration chambers identical to the pair of concentration chambers C1 and C2 of the first EDI device 3. The second EDI device 6 processes the water flowing out of the pair of concentrating chambers C1, C2 of the first EDI device 3, that is, the EDI concentrated water from the first EDI device 3, and returns the processed water to the supply line L1. 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 thereof, and to the treated water return line L8 for returning the treated water to the supply line L1 on the downstream side thereof. The treated water quality of the second EDI device 6 may be connected to the permeate line L2 instead of the supply line L1. The second EDI device 6 is also connected to a concentrated water discharge line L9 for discharging the EDI concentrated water from the second EDI device 6 to the outside.
The second EDI apparatus 6 does not require as high a processing performance as the first EDI apparatus 3 for manufacturing pure water, and therefore does not require as high a precision in power supply control. Therefore, in the pure water production apparatus 1 including 2 EDI devices 3 and 6 as in the present embodiment, it is preferable to use a normal dc power supply device for the first EDI device 3 requiring more stable power supply control, and it is preferable to use the hydro-power generation device 5 as a dc power supply device for the second EDI device 6. However, the first EDI device 3 may be supplied with electric power from the hydro-power generating device 5 via a charging device or a stabilized power supply device according to the amount of electric power generated by the hydro-power generating device 5. In particular, in the case where the hydro-power generator 5 is configured by a plurality of hydro-power generators (see fig. 3), power may be supplied to the 2 EDI devices 3 and 6 from different hydro-power generators.
The connection method of the 2 EDI devices 3 and 6 is not limited to that shown in fig. 4, and for example, although not shown, the 2 EDI devices 3 and 6 may be connected in series to sequentially treat the permeate supplied from the membrane filtration device 2. That is, the second EDI device 6 may process water (deionized water produced by the first EDI device 3) flowing out of the desalination chamber D of the first EDI device 3, and supply the processed water to the processing water tank or the point of use. In this case, the power supply from the hydro-power generator 5 may be performed by either one of the 2 EDI devices 3 and 6, or may be performed by both of them.
(third embodiment)
FIG. 5 is a schematic configuration diagram of a pure water producing apparatus according to a third embodiment of the present invention. In the following, the same components as those of the above-described embodiments are denoted by the same reference numerals in the drawings, and the description thereof is omitted, and only the components different from those of the above-described embodiments will be described.
The present embodiment is a modification of the first embodiment, and differs from the first embodiment in that a membrane filtration device (second membrane filtration device) 7 is provided on the downstream side thereof in addition to the membrane filtration device (first membrane filtration device) 2 of the first embodiment. The second membrane filtration device 7 has an RO membrane or an NF membrane, and is connected to the first membrane filtration device 2 via a permeate line (first permeate line) L2, similarly to the first membrane filtration device 2. That is, the second membrane filtration device 7 is connected in series with the first membrane filtration device 2 on the downstream side of the first membrane filtration device 2, and receives the supply of the permeate separated by the first membrane filtration device 2 as the water to be treated. The second membrane filtration device 7 is connected to a second permeate line L10 through which permeate separated by the second membrane filtration device 7 flows, and the second permeate line L10 is connected to the EDI device 3. As a result, in the present embodiment, compared with the first embodiment, permeate water having better water quality can be produced and supplied to the EDI device 3.
The second membrane filtration device 7 is connected to a second concentrate line L11 through which concentrate separated by the second membrane filtration device 7 flows. The second membrane filtration device 7 further separates the permeate from the first membrane filtration device 2 into permeate and concentrate, and thus, from the standpoint of water quality, it is not necessarily necessary to discharge the concentrate from the second membrane filtration device 7 to the outside. Therefore, from the viewpoint of water saving, the second concentrate line L11 is connected to the supply line L1 upstream of the pressure pump 4 so that all of the concentrate separated by the second membrane filtration device 7 flows back to the supply line L1. Alternatively, 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. In addition, in the case of cleaning the RO membrane or NF membrane of the second membrane filtration apparatus 7, a drain line that discharges a part or all of the concentrated water from the second membrane filtration apparatus 7 to the outside may be connected to the second concentrate line L11.
The hydro-power generation device 5 is provided in the first concentrate line L3 connected to the first membrane filtration device 2, but the position where the hydro-power generation device 5 is provided is not limited to this, and may be, for example, the second concentrate line L11. However, in the present embodiment, since it is necessary to supply raw water to the 2 membrane filtration devices 2 and 7 by the 1 pressurizing pump 4, the supply pressure of the water to be treated (raw water) to the first membrane filtration device 2 is higher than the supply pressure of the water to be treated (permeate 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 is greater than the pressure of the concentrated water from the second membrane filtration device 7. Therefore, in order to be able to expect a high amount of power generation, the hydro-power generation device 5 is preferably provided in the first concentrate line L3 connected to the first membrane filtration device 2.
In the present embodiment, the 2 membrane filtration devices 2 and 7 are connected in series, and the permeate from the first membrane filtration device 2 is supplied to the second membrane filtration device 7, but the connection method of the 2 membrane filtration devices 2 and 7 is not limited to this method. For example, the primary sides (the sides through which raw water and concentrated water flow) of the 2 membrane filtration devices (RO membranes or NF membranes) 2 and 7 may be connected in series, and the secondary sides (the sides through which permeate water flows) may be connected in parallel. That is, the concentrated water from the first membrane filtration device 2 may be supplied to the second membrane filtration device 7, and the permeate water from the first membrane filtration device 2 and the permeate water from the second membrane filtration device 7 may be supplied to the EDI device 3. In such a case, the hydro-power generation device 5 is preferably provided in the first concentrate line L3 through which the concentrated water having a higher pressure flows.
(fourth embodiment)
FIG. 6 is a schematic configuration diagram of a pure water producing apparatus according to a fourth embodiment of the present invention. In the following, the same components as those of the above-described embodiments are denoted by the same reference numerals in the drawings, and the description thereof is omitted, and only the components different from those of the above-described embodiments will be described.
The present embodiment is a modification of the first embodiment, and is different from the first embodiment in that a chemical liquid injection device 8 and a deaerator 9 are additionally provided, and the hydro-power generator 5 functions as a power source of each of the chemical liquid injection device 8 and the deaerator 9. In other words, the present embodiment differs from the first embodiment in that electric power generated by the hydro-power generation device 5 is supplied to the chemical liquid injection device 8 and the deaeration device 9, respectively. However, depending on the amount of power generated by the hydro-power generator 5, the generated power may be supplied to only one of the chemical liquid injection device 8 and the deaerator 9, or may be supplied to the EDI device 3 in addition to the chemical liquid injection device 8 and the deaerator 9.
The chemical liquid injection device 8 is provided upstream of the membrane filtration device 2, and is a device for adding a chemical liquid such as a scale inhibitor or a slurry control agent to raw water. The chemical liquid injection device 8 includes: a chemical tank 21 for storing chemical; the chemical pump 22 is connected to the supply line L1 via the chemical supply line L12, and injects the chemical stored in the chemical tank 21 into the supply line L1. Since the electric power generated by the hydro-power generator 5 is supplied to the chemical pump 22, the chemical solution is added to the raw water in the chemical solution injector 8 in conjunction with the operation of the membrane filter device 2. The position of adding the chemical liquid is not limited to the position shown in the drawing 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 connection portion between the supply line L1 and the return line L5. In addition to the scale inhibitor and the slurry control agent, the type of chemical solution to be added may be a pH adjuster or a reducing agent.
The deaerator 9 is provided on the permeate line L2 downstream of the membrane filter device 2, and removes the gas such as carbon dioxide or oxygen dissolved in the permeate from the membrane filter device 2. The configuration of the deaerator 9 is not particularly limited, and any known deaerator may be used as appropriate depending on the type of gas to be removed. Examples of such a deaerator include a membrane deaerator and a decarbonation tower. The membrane deaerator is a device that reduces the pressure of the secondary side of the deaeration membrane by a vacuum pump while passing the water to be treated through the primary side of the deaeration membrane, and removes the dissolved oxygen in the water to be treated by passing the water to be treated through the primary side of the deaeration membrane to the secondary side of the deaeration membrane. The decarbonization tower is a device that sprays water to be treated from above to a filler filled therein, introduces air from below by a blower, and causes the water to be treated to contact air in a gas-liquid manner on the surface of the filler, thereby diffusing dissolved carbon dioxide in the water to be treated into the air and removing the carbon dioxide. When the deaerator 9 is a membrane deaerator, electric power generated by the hydroelectric power generator 5 is supplied to a vacuum pump, and when the deaerator 9 is a decarbonizer, electric power is supplied to a blower. Therefore, in the deaerator 9, deaeration is performed in conjunction with the operation of the membrane filter device 2. The installation position of the deaeration device 9 is not limited to the position shown in the drawing, and may be, for example, the upstream side of the membrane filtration device 2.
The chemical liquid injection device and the deaeration device according to the present embodiment can be provided not only in the first embodiment but also in the second and third embodiments. In this case, the installation position of the chemical liquid injection device and the deaeration device is not particularly limited, and the chemical liquid injection device and the deaeration device may be installed at appropriate positions according to the type of chemical liquid to be added and the type of gas to be removed. For example, in the third embodiment, as shown in fig. 5, in the configuration in which 2 membrane filtration devices 2 and 7 are connected in series, the chemical liquid injection device may be provided at a position where the chemical liquid is added to the permeate water from the first membrane filtration device 2. On the other hand, as a modification of the third embodiment, as described above, in the configuration in which the primary sides of the 2 membrane filtration devices 2, 7 are connected in series and the secondary sides are connected in parallel, the chemical liquid injection device may be provided at a position where the chemical liquid is added to the concentrated water from the first membrane filtration device 2.
Example (example)
Next, effects of the present invention will be described with reference to specific examples.
As an example, using the pure water production apparatus having the structure shown in fig. 1, an operation was performed for 500 hours, and the water quality of the water to be treated (conductivity of the water to be treated) were measured in the membrane filtration apparatus and the electrodeionization water production apparatus, respectively. Then, the desalination rate of the membrane filtration apparatus, the desalination rate of the electrodeionization water producing apparatus, and the desalination rate of the entire system were calculated by the following formula (1).
Desalination rate (%) =
(1- (treated water conductivity/treated water conductivity)). Times.100 (1)
Here, the desalination rate of the membrane filtration device is calculated from the conductivity of raw water (treated water conductivity) and the conductivity of permeate water (treated water conductivity) from the membrane filtration device. The desalination rate of the electrodeionization water producing apparatus was calculated from the conductivity of the permeate water (treated water conductivity) from the membrane filtration apparatus and the conductivity of the deionized water (treated water conductivity) from the electrodeionization water producing apparatus. The desalination rate of the whole system is calculated based on the conductivity of raw water (conductivity of treated water) and the conductivity of deionized water (conductivity of treated water) from the electrodeionization water producing device.
As the membrane filtration apparatus, RO membranes were used, and as the electrodeionization water production apparatus, an apparatus having the structure shown in fig. 2, specifically, an apparatus having a 4-chamber desalting chamber and 10cm×10cm×1cm in size of each of the desalting chamber, the concentrating chamber, and the electrode chamber was used. In each desalting chamber of the electrodeionization apparatus, cation exchange resin and anion exchange resin are filled in a mixed bed manner, and in each concentrating chamber, anion exchange resin is filled. As the water to be treated (raw water), water having a conductivity of about 200 μs/cm was used, and the flow rate of raw water supplied to the membrane filtration device was set to 330L/h. The treatment flow rate of the electrodeionization water producing apparatus (flow rate of the water to be treated flowing into the treatment chamber), the flow rate of the water flowing into the concentration chamber and the flow rate of the water flowing into the electrode chamber were set to 40L/h, 25L/h and 15L/h, respectively. At this time, the flow rate and pressure of the concentrated water flowing from the membrane filtration apparatus to the concentrated water line were 250L/h and 0.53MPa, respectively.
As the hydroelectric power generating apparatus, an apparatus in which 7 hydroelectric power generators (product No. DB-2689, manufactured by Foshan Shunde Zhongjiang Energy Saving Electronics company) are spatially connected in series and electrically connected in parallel is used. Then, instead of the direct-current power supply device, the electric power generated by the hydro-power generation device is supplied to the electrodeionization water production device. The operation current of the electrodeionization water producing apparatus at this time was 0.1A, and the operation voltage (supply voltage) was 6V. The pressure loss of the entire hydroelectric power generator was 0.13MPa.
The conductivity of raw water, the conductivity of permeate water from the membrane filtration device, and the conductivity of deionized water from the electrodeionization water production device were measured, and the results were 198. Mu.S/cm, 4.72. Mu.S/cm, and 0.15. Mu.S/cm, respectively. Then, from these conductivities, the desalination rate of the membrane filtration apparatus, the desalination rate of the electrodeionization water producing apparatus, and the desalination rate of the entire system were calculated by the above formula (1), and the results were 97.6%, 96.8%, and 99.9%, respectively. Therefore, it was confirmed that a desired water quality can be obtained without using a normally used dc power supply device.
In addition, as another example, the same electrodeionization device as in the above example was used except that the number of desalting chambers was 1, and how the operating voltage of the electrodeionization device was changed was examined depending on whether or not each concentrating chamber was filled with anion exchange resin. Specifically, in both cases where the anion exchange resin was filled and in the case where the anion exchange resin was not filled in each of the concentration chambers, the operation was performed under the same conditions (the condition in which water having an electric conductivity of 3.6 μs/cm (water passing through the membrane filtration apparatus) was used as the water to be treated, and the operation current was set to 0.1A), and the respective operation voltages were compared. As a result, it was confirmed that the operating voltage of the former was about 1/7 of the operating voltage of the latter. Therefore, the filling of the anion exchange resin (ion exchanger) in each concentrating chamber of the electrodeionization water producing apparatus causes a drop in the operating voltage, and is therefore considered to be particularly effective in the case where the amount of electricity generated by the hydroelectric power generating apparatus is not so large.
Description of the reference numerals
1 pure water producing apparatus
2 Membrane filtration device (first membrane filtration device)
3EDI device (first EDI device)
4 booster pump
5 hydroelectric power generation device
51 first hydroelectric generator
52 second hydroelectric generator
6 second EDI device
7 second membrane filter
8 medicine liquid injection device
21 medicine liquid tank
22 dosing pump
9 degassing device
L1 supply line
L2 permeate line (first permeate line)
L3 concentrated water line (first concentrated water line)
L31 bypass line
L4 drainage pipeline
L5 backflow water pipeline
L6 treatment water pipeline
L7, L9 concentrate discharge line
L8 treated water return pipeline
L10 second water-permeable pipeline
L11 second concentrated water pipeline
L12 liquid medicine supply pipeline
V1-V5 valve.
Claims (10)
1. A pure water production apparatus includes:
a membrane filtration device having a reverse osmosis membrane or nanofiltration membrane for separating water to be treated into permeate water and concentrate water;
an electrodeionization water producing device; and
a hydroelectric power generation device having at least one hydroelectric power generator provided in a concentrated water line through which the concentrated water from the membrane filtration device flows, and a bypass line connected to the concentrated water line so as to bypass the at least one hydroelectric power generator, wherein the hydroelectric power generation device generates power by using the flow of the concentrated water flowing through the concentrated water line, and supplies power generated by the power generation to the electrodeionization water production device,
the hydroelectric power generating apparatus includes a plurality of hydroelectric power generators including the at least one hydroelectric power generator disposed in series in the concentrated water line, valves provided in the bypass line and the concentrated water line, and a control unit,
the control section switches between a power generation mode in which the concentrated water is caused to flow through the bypass line to generate power by a generator other than the at least 1 hydro-generator and a power generation mode in which the concentrated water is not caused to flow through the bypass line to generate power by the plurality of hydro-generators, based on any one of the quality of deionized water produced by the electro-deionized water production apparatus and an operation current of the electro-deionized water production apparatus,
the control unit switches the power generation mode according to the fluctuation of the resistance of the electrodeionization device, and adjusts the supply current from the hydroelectric power generation device to the electrodeionization device.
2. The apparatus for producing pure water according to claim 1, wherein,
the hydro-power generation device functions as a power supply device of the electric deionized water manufacturing device or functions as a power supply of the power supply device.
3. The apparatus for producing pure water according to claim 2, wherein,
the apparatus for producing electric deionized water comprises: a desalination chamber located between an anode and a cathode, partitioned by an anion exchange membrane on the anode side and a cation exchange membrane on the cathode side, and filled with at least one of a cation exchanger and an anion exchanger; and a pair of concentrating chambers disposed on both sides of the desalting chamber with the anion exchange membrane and the cation exchange membrane interposed therebetween.
4. The apparatus for producing pure water according to claim 3, wherein,
the pair of concentrating chambers are filled with ion exchangers, respectively.
5. The pure water manufacturing apparatus according to claim 3 or 4, wherein,
the desalination chamber of the electrodeionization water producing apparatus is connected to the membrane filtration apparatus to treat the permeate from the membrane filtration apparatus.
6. The pure water manufacturing apparatus according to claim 3 or 4, wherein,
the pure water manufacturing apparatus has a further electric deionized water manufacturing apparatus different from the electric deionized water manufacturing apparatus, the further electric deionized water manufacturing apparatus having: a desalination chamber located between an anode and a cathode, partitioned by an anion exchange membrane on the anode side and a cation exchange membrane on the cathode side, and filled with at least one of a cation exchanger and an anion exchanger; and a pair of concentrating chambers disposed on both sides of the desalting chamber with the anion exchange membrane and the cation exchange membrane interposed therebetween,
the desalination chamber of the additional electrodeionization water producing means is connected to the membrane filtration means to treat the permeate from the membrane filtration means,
the desalination chamber of the electrodeionization device is connected to the other electrodeionization device to treat either one of water flowing out of the pair of concentrating chambers of the other electrodeionization device and water flowing out of the desalination chamber.
7. The pure water production apparatus according to any one of claims 1 to 4, wherein,
the portion on the downstream side of the concentrated water line is branched into a drain line that discharges a part of the concentrated water to the outside and a return water line that returns the remaining part of the concentrated water to a supply line for supplying the treated water to the membrane filtration device,
the hydroelectric power generation device is disposed in a portion of the concentrate line that is not branched into the drain line and the upstream side of the return line.
8. The pure water production apparatus according to any one of claims 1 to 4, wherein,
the hydroelectric power generator of the hydroelectric power generating apparatus has an impeller that rotates in response to the flow of the concentrated water, and is configured to detect the flow rate of the concentrated water based on the rotation speed of the impeller.
9. The pure water production apparatus according to any one of claims 1 to 4, wherein,
the pure water production apparatus has another membrane filtration apparatus connected to the membrane filtration apparatus on the downstream side of the membrane filtration apparatus, the other membrane filtration apparatus having a reverse osmosis membrane or a nanofiltration membrane.
10. A method of operating a pure water producing apparatus according to any one of claims 1 to 9,
the operation method of the pure water manufacturing device comprises the following steps:
a step of providing at least one hydroelectric generator in a concentrated water line through which the concentrated water from the membrane filtration device flows, and connecting a bypass line to the concentrated water line so as to bypass the at least one hydroelectric generator; and
and a step of generating electricity by using the flow of the concentrated water flowing through the concentrated water line and supplying the electricity generated by the generation to the electrodeionization water producing device.
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| TW202035013A (en) | 2020-10-01 |
| TWI748318B (en) | 2021-12-01 |
| WO2020148961A1 (en) | 2020-07-23 |
| CN113015702A (en) | 2021-06-22 |
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