WO2014133101A1 - Méthode de production d'eau dessalée - Google Patents

Méthode de production d'eau dessalée Download PDF

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Publication number
WO2014133101A1
WO2014133101A1 PCT/JP2014/054941 JP2014054941W WO2014133101A1 WO 2014133101 A1 WO2014133101 A1 WO 2014133101A1 JP 2014054941 W JP2014054941 W JP 2014054941W WO 2014133101 A1 WO2014133101 A1 WO 2014133101A1
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WO
WIPO (PCT)
Prior art keywords
water
semipermeable membrane
pressure
membrane unit
supply
Prior art date
Application number
PCT/JP2014/054941
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English (en)
Japanese (ja)
Inventor
谷口　雅英
智宏 前田
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東レ株式会社
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Publication date
Application filed by 東レ株式会社 filed Critical 東レ株式会社
Priority to JP2014529360A priority Critical patent/JP6269486B2/ja
Publication of WO2014133101A1 publication Critical patent/WO2014133101A1/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
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/025—Reverse osmosis; Hyperfiltration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/12—Controlling or regulating
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2313/00—Details relating to membrane modules or apparatus
    • B01D2313/36—Energy sources
    • B01D2313/365—Electrical sources
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/008—Control or steering systems not provided for elsewhere in subclass C02F
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/08—Seawater, e.g. for desalination
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2201/00—Apparatus for treatment of water, waste water or sewage
    • C02F2201/009—Apparatus with independent power supply, e.g. solar cells, windpower, fuel cells
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination
    • Y02A20/131—Reverse-osmosis
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/20—Controlling water pollution; Waste water treatment
    • Y02A20/208—Off-grid powered water treatment
    • Y02A20/212—Solar-powered wastewater sewage treatment, e.g. spray evaporation
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/30—Wastewater or sewage treatment systems using renewable energies
    • Y02W10/37—Wastewater or sewage treatment systems using renewable energies using solar energy

Definitions

  • the present invention relates to a method for producing demineralized water that obtains demineralized water using a water treatment process that removes impurities from the water to be treated using natural energy.
  • Separation membrane utilization technology has been mainly applied to purification of river water, lake water, etc. in order to obtain drinking water, industrial water, agricultural water, and the like.
  • seawater desalination has been promoted mainly by the evaporation method in the Middle East region where water resources are extremely small and heat resources from oil are very abundant.
  • Non-patent Document 1 seawater desalination by reverse osmosis membranes is not universal, and high-concentration seawater, such as in the Middle East, and when the temperature is high, the desalination capacity decreases and the salt concentration of treated water (freshwater) tends to increase (Non-patent Document 1), in order to obtain high-quality treated water, there are many methods called the permeated water two-stage method in which desalted water is treated again with a low-pressure reverse osmosis membrane. There is a need to further reduce energy requirements by improving osmotic membrane performance and improving process systems.
  • Patent Document 1 a method of combining a plurality of types of reverse osmosis membranes (Patent Document 1), a method of treating concentrated water of a reverse osmosis membrane again with a reverse osmosis membrane (Patent Document 2), a pretreatment with a nanofiltration membrane, and a hardness component That improves the recovery rate of reverse osmosis membranes (Patent Document 3), and a method of treating nanofiltration membranes with nanofiltration membranes again (Non-Patent Document 2) has been proposed and has been put to practical use. Not a few.
  • Non-Patent Document 3 and Patent Document 4 attempts have been made to utilize electric power generated by natural energy such as solar energy, wind power, and wave power. Stable supply. That is, almost no solar energy can be obtained at night, and no wind power can be obtained for the kite. Therefore, as described in Non-Patent Document 3, it is necessary to provide a large storage battery and absorb fluctuations in the amount of power generation. However, a high-cost storage battery has a significant impact on desalination costs and is a major obstacle to commercialization and dissemination. It has become.
  • An object of the present invention is to stably produce demineralized water while suppressing membrane deterioration and fouling during operation of a water treatment apparatus using a reverse osmosis membrane mainly using natural energy.
  • the present invention relates to the following embodiments (1) to (7).
  • the water to be treated is pressurized and supplied to the semipermeable membrane unit, separated into permeated water and concentrated water, and the permeated water is used as desalted water.
  • the minimum supply water pressure Pfmin is determined based on the osmotic pressure calculated based on the quality of the water to be treated supplied to the semipermeable membrane unit, and a preset minimum supply water flow rate Qfmin is flowed.
  • the recovery rate R obtained as the value of the ratio of the permeate flow rate Qp to the supply water flow rate Qf is set to 0, or
  • the semipermeable membrane unit is stably operated while suppressing membrane deterioration and fouling of the separation membrane while using unstable electric power obtained from natural energy as a power source.
  • Demineralized water can be produced.
  • FIG. 1 is a flowchart showing an example of an embodiment of a water treatment apparatus applicable to the method for producing desalted water of the present invention.
  • raw water 1 is supplied to a raw water tank 2, supplied to a pretreatment unit 4 by a pretreatment pump 3, processed, and stored in a pretreatment water tank 5.
  • the pretreated water discharged from the pretreated water tank 5 is pressurized by the high-pressure pump 6, supplied and processed to the semipermeable membrane unit 7, and separated into permeated water and concentrated water.
  • the permeated water (demineralized water) is stored in the permeated water tank 8.
  • the concentrated water discharged from the semipermeable membrane unit 7 is taken out from the concentrated water valve 13a through the concentrated water line 12a.
  • a natural energy power generation unit 15 as a power source using natural energy.
  • a small power storage unit 14 can be provided to absorb fluctuations in the amount of power supply for a short time.
  • the power stabilized by the power stable supply control unit 16 is supplied to each unit, for example, the pretreatment pump 3 and the high pressure pump 6 in FIG.
  • examples of the natural energy used by the natural energy power generation unit 15 include sunlight, wind power, wave power, and hydropower.
  • the present invention can be applied to sunlight and wind power, which are greatly affected by climate, and has a great effect.
  • the stable power supply control unit 16 is adjusted so that sudden power fluctuations from the power generation unit 15 can be absorbed to some extent by supplementing the power obtained from the natural energy power generation unit 15 mainly with the power storage unit 14.
  • the power storage unit 14 is not particularly limited, but is preferably a capacitor, a capacitor, a secondary battery, or the like suitable for high output.
  • a capacitor that is most suitable for a large output and less deteriorated due to charge / discharge is most preferable.
  • the usage status of the power storage unit repeats charging and discharging shallower than the repetition of full charge and complete discharge, so a nickel-cadmium battery or nickel metal hydride battery with a memory effect is not very suitable. Lithium ion batteries are preferred.
  • a semipermeable membrane unit flow rate control unit 21 may be installed to determine a threshold value for controlling the operation and to control the operation conditions.
  • the semipermeable membrane unit flow control unit 21 determines the minimum supply water pressure Pfmin based on the osmotic pressure ⁇ calculated based on the quality of the water to be treated measured by the concentration sensor 20, and the measured supply While detecting the water pressure Pf, the operating conditions of the high-pressure pump 6, the concentrated water valve 13a, and the permeated water valve 17 are controlled.
  • the supply water flow rate Qf Qp / Qf obtained as the value of the ratio of the permeated water flow rate Qp to is operated with 0, or the operation of the semipermeable membrane unit is stopped.
  • the permeate water is controlled while controlling the recovery rate R so that the concentrated water flow rate Qb is larger than the minimum supply water flow rate Qfmin. Operate to obtain stable (demineralized water).
  • the recovery rate R is controlled so that the concentrated water flow rate Qb does not fall below the supply water minimum flow rate Qfmin.
  • the minimum supply water flow rate Qfmin it is most common and safe to follow the instructions for the minimum concentrated water flow rate Qbmin based on the guidelines and technical data of the semipermeable membrane manufacturer. That is, when the permeate flow rate Qp is 0, the supply water minimum flow rate Qfmin is equal to the minimum concentrated water flow rate Qbmin, which is the smallest value.
  • the premise is that the permeated water maximum flow rate Qpmax or the permeated water maximum flux (maximum permeate flow rate per membrane area) Fpmax is included in the guideline. . That is, when the actual design permeate flow rate is smaller than the permeate maximum flux Qpmax of the instruction, the concentrated water minimum flow rate Qbmin can be set to a value smaller than the instruction.
  • Non-patent literature M.
  • Taniguchi et al. “Behavior of a reverse osmosis plant adopting a brine conversion two-stage process and its computer simulation,” Journal of Membrane Science 183, p249-257, 2001) It can also be obtained by performing a simulation calculation based on the concentration polarization model shown in FIG. Experimentally, a component having relatively low solubility under the conditions of the permeate maximum flow rate Qpmax and the permeate minimum flow rate Qpmin, that is, a component that easily precipitates (for example, soluble silica) is supplied water (treated water).
  • the concentration of the solute is increased and the solute begins to precipitate in the semipermeable membrane unit, that is, the solute concentration when the pressure loss starts to increase due to the precipitation is obtained.
  • the concentrated water flow rate Qb is lowered, and the pressure loss in the semipermeable membrane unit is a pressure loss corresponding to the concentrated water flow rate.
  • the concentrated water flow rate Qb when starting to become larger than this can be obtained, and this can be used as the concentrated water minimum flow rate Qbmin. That is, in the present invention, the concentrated water minimum flow rate Qbmin at this time is preset as the supply water minimum flow rate Qfmin.
  • the supply water flow rate Qf to the semipermeable membrane unit 7 can be adjusted according to the operating conditions of the high-pressure pump 6.
  • the minimum supply water pressure Pfmin in the semipermeable membrane unit 7 is determined based on the osmotic pressure ⁇ calculated based on the quality of the water to be treated supplied to the semipermeable membrane unit 7 measured by the concentration sensor 20.
  • Pfmin ⁇ + Pp + ⁇ .
  • ⁇ is the osmotic pressure [atm] of the water to be treated
  • Pp is the permeated water pressure [atm]
  • ⁇ is a pressure [atm] greater than zero.
  • the permeated water pressure Pp is a pressure when a slight pressure loss or the like on the permeated water side occurs, and is otherwise almost zero.
  • ⁇ may be any number exceeding 0, but when ⁇ is close to 0, the quality of the permeate decreases when the supply water pressure Pf of the semipermeable membrane unit 7 is close to the minimum supply water pressure Pfmin, If ⁇ is too large, the operable pressure range in which the permeated water can be obtained becomes narrow, so care must be taken.
  • ⁇ is preferably 2 to 5 atm.
  • the concentration CM [mg / l] of the water to be treated supplied to the semipermeable membrane unit 7 measured by the concentration sensor 20 is calculated.
  • the osmotic pressure ⁇ [atm] of the water to be treated is calculated.
  • ⁇ CM ⁇ R ⁇ (T + 273.15)
  • ⁇ osmotic pressure [atm]
  • CM Molar concentration [mol / l]
  • T Temperature [°C]
  • the osmotic pressure ⁇ can be obtained based on the approximate expression by measuring the component of the water to be treated and if the approximate expression based on the actual measurement value can be obtained. I can do it.
  • the permeate pressure is basically the same as the supply water pressure Pf. It is necessary to set the supply water pressure Pf so as not to exceed.
  • the pressure resistance on the supply water side is often about 70 to 80 atm and the pressure resistance on the permeate side is often about 10 atm, so the pressure on the permeate side of the device exceeds the pressure limit. It is preferable to provide safety measures such as providing a limiter for the supply water pressure Pf or installing a relief valve or pressure release plate on the permeate side.
  • the recovery rate R 0
  • the water to be treated supplied to the semipermeable membrane unit is directly discharged from the concentrated water discharge line. Therefore, in order to suppress the loss that the water to be treated flows out of the apparatus, it is also preferable to recirculate the water to be treated discharged from the concentrated water discharge line 12a to the pretreatment water tank 5 as it is.
  • the power consumption of the semipermeable membrane unit 7 is reduced. It is also a preferred embodiment to use the electric power obtained from the power source) by turning it to other units such as pretreatment, for example, increasing the pretreatment flow rate. As another example, as shown in FIG. 2, it is possible to equip the downstream side of the semipermeable membrane unit 7 with a post-processing unit 10, and in this case, the power saved by stopping the semipermeable membrane unit 7. Can be distributed to post-processing in addition to pre-processing. In FIG.
  • the desalinated water stored in the permeate tank 8 is processed by the low pressure semipermeable membrane unit which is the post-treatment unit 10 by the booster pump 9, and the permeate is used as product water (demineralized water). Sent to. Moreover, the concentrated water discharged
  • the amount of reflux can be increased.
  • the concentration sensor 20a it is also a preferred embodiment to include a concentration sensor 20b for the supply water to the semipermeable membrane unit 7 after the reflux water is mixed.
  • the concentration sensor 20b it is also a preferred embodiment to include a concentration sensor 20b for the supply water to the semipermeable membrane unit 7 after the reflux water is mixed.
  • the concentration sensor 20b it is preferable to control the reflux amount to reduce the concentration of water supplied to the semipermeable membrane unit 7 (the quality of the water to be treated), that is, the fluctuation of the osmotic pressure.
  • the maximum recovery rate Rmax is an upper limit value of the recovery rate R in the semipermeable membrane unit 7.
  • the maximum recovery rate Rmax can be determined based on the measured value of the quality of the supplied treated water or the concentration limit based on the component ratio of the supplied treated water that has been actually measured. Specifically, the concentration limit concentration based on the solubility product can be obtained by calculation, or the concentration at which the feed water is concentrated and precipitation starts is measured, so that the concentration does not exceed the maximum concentration at which precipitation does not occur. It is advisable to determine the maximum recovery rate Rmax.
  • the recovery rate R may exceed the concentration limit of the water to be treated simply by controlling the concentrated water flow rate Qb to be larger than the minimum supply water flow rate Qfmin. In this case, it becomes a problem that a component that cannot be completely dissolved becomes a scale. For this reason, it is necessary to determine the maximum recovery rate Rmax so as not to exceed this value.
  • the supply water flow rate Qf is increased, the concentrated water flow rate Qb is increased, that is, the permeate flow rate Qp is decreased, and the like.
  • the supply water pressure Pf can be controlled.
  • Rmax is a function of the scale inhibitor addition concentration.
  • the supply of the water to be treated to the semipermeable membrane unit is temporarily stopped and the water to be treated supplied in the semipermeable membrane unit is temporarily stopped.
  • the flow direction is set to the opposite direction and the supply of the water to be processed to the semipermeable membrane unit is resumed, the fouling substance adhered and deposited in the semipermeable membrane element or on the membrane surface can be removed. Therefore, it is preferable. That is, before and after stopping the supply of treated water to the semipermeable membrane unit, the inlet of treated water to the semipermeable membrane unit and the outlet for concentrated water from the semipermeable membrane unit are switched. Thus, it is preferable to operate the semipermeable membrane unit.
  • the concentrated water taken out from the semipermeable membrane unit 7 is drained, but this concentrated water causes a pressure loss at the concentrated water valve 13a in FIGS. Yes.
  • an energy recovery unit instead of the concentrated water valve 13a.
  • the energy recovery unit include a reverse pump, a Pelton turbine, a turbocharger, and a pressure exchange.
  • the supply water pressure Pf is varied in order to control the concentrated water flow rate Qb. It is preferable to use a pressure exchange type energy recovery unit suitable for such conditions.
  • the energy recovery efficiency of the pressure exchange type energy recovery unit is greatly influenced by the flow rate, but is not greatly affected by the pressure, so in the present invention where the flow rate range is narrow, by using the pressure exchange type energy recovery unit, High energy recovery efficiency can be achieved under any operating conditions.
  • Other energy recovery is not very suitable for the present invention because the efficiency is affected by pressure fluctuation and flow rate fluctuation and it is difficult to maintain high energy recovery efficiency.
  • An example of the apparatus provided with the pressure exchange type energy recovery unit 18 is shown in FIG.
  • examples of the pretreatment unit 4 include sand filtration and a separation membrane.
  • a separation membrane various separation membrane units can be used.
  • a wound filter, non-woven filter, microfiltration membrane, ultrafiltration membrane, etc. capable of high-precision solid-liquid separation of micrometer or less can be used. Can be used.
  • these pretreatment units, semipermeable membrane units and the like are contaminated by dirt components contained in the raw water, it is common to perform on-line or off-line cleaning as appropriate in order to restore performance.
  • the cleaning chemical is injected into the water to be treated.
  • examples include hypochlorous acid, chloramine, chlorine dioxide, potassium permanganate, sodium hyposulfite, 2,2-dibromo-3-nitrilopropionamide (which is continuously or intermittently injected into water intake and supply water to the unit, etc.
  • bactericides such as DBNPA
  • general acids such as sulfuric acid, hydrochloric acid and citric acid
  • alkalis such as sodium hydroxide.
  • the treated water or treated water is used as it is, or it is generally heated or added with the above-mentioned cleaning chemicals to increase the cleaning effect, supply to the contaminated part, flush, or dip Is.
  • the contaminated part here may be on either the treated water side or the treated water side, but it is preferably applied to the treated water side where contamination easily occurs.
  • the treated water (raw water) to which the present invention is applicable is not particularly limited, and various treated water such as river water, seawater, sewage treated water, rain water, industrial water, industrial waste water, or mixed water thereof. Although water can be mentioned, application to seawater or brackish water having osmotic pressure is particularly suitable.
  • the present invention prevents the contamination of the separation membrane unit and reduces the environmental load by operating the semipermeable membrane unit and other units efficiently while using electric power obtained from unstable natural energy as a power source. It is possible to provide a method for stably operating the semipermeable membrane unit.

Abstract

　Selon l'invention, de l'eau dessalée est produite de façon stable avec une dégradation et un encrassement de membrane minimaux pendant le fonctionnement d'un appareil de traitement d'eau basé sur une membrane d'osmose inverse utilisant de l'énergie naturelle comme énergie principale. L'invention concerne une méthode consistant à mettre sous pression de l'eau à traiter, fournir l'eau à une unité à membrane semi-perméable (7), traiter l'eau, et obtenir de l'eau dessalée en utilisant comme source d'énergie principale de l'énergie électrique obtenue à partir d'une unité générateur à énergie naturelle (15), une pression d'eau d'alimentation minimale (Pfmin) étant déterminée en fonction d'une pression osmotique calculée à partir de la qualité de l'eau à traiter qui est fournie à l'unité à membrane semi-perméable (7), et si la pression ne peut pas être augmentée jusqu'à Pfmin lorsqu'un débit volumique d'eau minimum prédéfini (Qfmin) d'eau d'alimentation a été fourni, soit une opération est effectuée dans laquelle le taux de récupération (R), qui est la valeur du rapport entre le débit volumique d'eau traversant (Qp) et le débit volumique d'eau fournie (Qf), est réglé à zéro, soit le fonctionnement de l'unité à membrane semi-perméable (7) est arrêté et le taux de récupération (R) est régulé pour que le débit volumique d'eau concentrée ne dépasse pas Qfmin lorsque la pression peut être augmentée jusqu'à Pfmin.
PCT/JP2014/054941 2013-02-28 2014-02-27 Méthode de production d'eau dessalée WO2014133101A1 (fr)

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JP2014529360A JP6269486B2 (ja) 2013-02-28 2014-02-27 脱塩水の製造方法

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JP2013-038199 2013-02-28
JP2013038199 2013-02-28

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN107879421A (zh) * 2016-09-29 2018-04-06 东丽先端材料研究开发（中国）有限公司 一种净水装置及净水装置的运行方法
JP2018519158A (ja) * 2015-07-02 2018-07-19 マスカラ ヌーベル テクノロジー 再生可能エネルギー源を動力源とする脱塩プラントを制御する方法及び関連プラント
WO2023153325A1 (fr) * 2022-02-10 2023-08-17 ウォーターポイント株式会社 Système de purification d'eau

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Publication number Priority date Publication date Assignee Title
JPS614510A (ja) * 1984-06-18 1986-01-10 Yamaha Motor Co Ltd 造水装置
JP2000288368A (ja) * 1999-04-06 2000-10-17 Nitto Denko Corp 複合逆浸透膜
JP2001252662A (ja) * 2000-03-10 2001-09-18 Toray Ind Inc 造水方法
JP2011020010A (ja) * 2009-07-13 2011-02-03 Mitsubishi Heavy Ind Ltd 生成水製造装置
JP2012170841A (ja) * 2011-02-17 2012-09-10 Hitachi Plant Technologies Ltd 複合淡水化システム

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS614510A (ja) * 1984-06-18 1986-01-10 Yamaha Motor Co Ltd 造水装置
JP2000288368A (ja) * 1999-04-06 2000-10-17 Nitto Denko Corp 複合逆浸透膜
JP2001252662A (ja) * 2000-03-10 2001-09-18 Toray Ind Inc 造水方法
JP2011020010A (ja) * 2009-07-13 2011-02-03 Mitsubishi Heavy Ind Ltd 生成水製造装置
JP2012170841A (ja) * 2011-02-17 2012-09-10 Hitachi Plant Technologies Ltd 複合淡水化システム

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2018519158A (ja) * 2015-07-02 2018-07-19 マスカラ ヌーベル テクノロジー 再生可能エネルギー源を動力源とする脱塩プラントを制御する方法及び関連プラント
EP3317229B1 (fr) 2015-07-02 2020-01-29 Mascara Nouvelles Technologies Procede de pilotage d'une installation de dessalement alimentee par une source d' energie renouvelable et installation associee
CN107879421A (zh) * 2016-09-29 2018-04-06 东丽先端材料研究开发（中国）有限公司 一种净水装置及净水装置的运行方法
WO2023153325A1 (fr) * 2022-02-10 2023-08-17 ウォーターポイント株式会社 Système de purification d'eau

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