WO2012144384A1 - Méthode de purification d'eau contenant un halogène radioactif, procédé de production d'eau filtrée, et dispositif de purification d'eau contenant un halogène radioactif - Google Patents

Méthode de purification d'eau contenant un halogène radioactif, procédé de production d'eau filtrée, et dispositif de purification d'eau contenant un halogène radioactif Download PDF

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Publication number
WO2012144384A1
WO2012144384A1 PCT/JP2012/059849 JP2012059849W WO2012144384A1 WO 2012144384 A1 WO2012144384 A1 WO 2012144384A1 JP 2012059849 W JP2012059849 W JP 2012059849W WO 2012144384 A1 WO2012144384 A1 WO 2012144384A1
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Prior art keywords
water
semipermeable membrane
radioactive halogen
unit
membrane unit
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English (en)
Japanese (ja)
Inventor
谷口雅英
前田智宏
佐々木崇夫
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Toray Industries Inc
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Toray Industries Inc
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Priority to JP2012522851A priority Critical patent/JPWO2012144384A1/ja
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • G—PHYSICS
    • G21—NUCLEAR PHYSICS; NUCLEAR ENGINEERING
    • G21F—PROTECTION AGAINST X-RADIATION, GAMMA RADIATION, CORPUSCULAR RADIATION OR PARTICLE BOMBARDMENT; TREATING RADIOACTIVELY CONTAMINATED MATERIAL; DECONTAMINATION ARRANGEMENTS THEREFOR
    • G21F9/00—Treating radioactively contaminated material; Decontamination arrangements therefor
    • G21F9/04—Treating liquids
    • G21F9/06—Processing
    • G—PHYSICS
    • G21—NUCLEAR PHYSICS; NUCLEAR ENGINEERING
    • G21F—PROTECTION AGAINST X-RADIATION, GAMMA RADIATION, CORPUSCULAR RADIATION OR PARTICLE BOMBARDMENT; TREATING RADIOACTIVELY CONTAMINATED MATERIAL; DECONTAMINATION ARRANGEMENTS THEREFOR
    • G21F9/00—Treating radioactively contaminated material; Decontamination arrangements therefor
    • G21F9/04—Treating liquids
    • G21F9/06—Processing
    • G21F9/08—Processing by evaporation; by distillation
    • G—PHYSICS
    • G21—NUCLEAR PHYSICS; NUCLEAR ENGINEERING
    • G21F—PROTECTION AGAINST X-RADIATION, GAMMA RADIATION, CORPUSCULAR RADIATION OR PARTICLE BOMBARDMENT; TREATING RADIOACTIVELY CONTAMINATED MATERIAL; DECONTAMINATION ARRANGEMENTS THEREFOR
    • G21F9/00—Treating radioactively contaminated material; Decontamination arrangements therefor
    • G21F9/04—Treating liquids
    • G21F9/06—Processing
    • G21F9/12—Processing by absorption; by adsorption; by ion-exchange
    • 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
    • C02F1/70—Treatment of water, waste water, or sewage by reduction
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/006—Radioactive compounds

Definitions

  • the present invention relates to a method for purifying seawater, river water, groundwater, wastewater treated water containing radioactive halogen, particularly radioactive iodine, and a device for purifying radioactive halogen-containing water.
  • Patent Document 1 As a method of separating and removing radioactive substances in water, a method of adsorbing on activated carbon, ion exchange resin, zeolite, etc. is the most popular, and is exemplified in Non-Patent Document 1 and Patent Documents 1 and 2, for example. Furthermore, recently, as shown in Non-Patent Document 2, various membrane separation applications have been attempted. Further, Patent Document 3 gives an example in which a reducing agent is added to wastewater and then removed with a reverse osmosis membrane capable of removing low molecules.
  • adsorbents are not preferred, especially when the salinity of the raw wastewater is high because the ability to adsorb halogens such as iodine is inhibited by the salinity.
  • adsorbents are not preferred, especially when the salinity of the raw wastewater is high because the ability to adsorb halogens such as iodine is inhibited by the salinity.
  • radioactive materials are concentrated in the adsorbent itself, and the risk of the treatment facility increases.
  • the method of removing with a reverse osmosis membrane after adding a reducing agent is easy to achieve a stable state in which iodine is easily removed, but the wastewater is mixed with natural water such as river water or rainwater, or the wastewater itself is natural.
  • the effect of the reducing agent such as the need to add a large amount of reducing agent in order to form a complex equilibrium state, such as halogen is taken into various impurities to form a complex May not be fully demonstrated.
  • An object of the present invention is to efficiently remove halogens, in particular iodine, from seawater, river water, groundwater, wastewater treated water, etc. containing radioactive halogens.
  • the present invention has the following configuration.
  • a solid-liquid separation unit that obtains pretreatment water by solid-liquid separation of radioactive halogen-containing water, a first oxidation-reduction potentiometer that measures the oxidation-reduction potential before treatment of the solid-liquid separation unit, and pretreatment water
  • a reducing agent addition unit for adding a reducing agent; a semipermeable membrane unit for separating pretreated water to which the reducing agent is added into concentrated wastewater and permeated water; and a second for measuring a redox potential before the semipermeable membrane unit treatment.
  • Purification equipment for radioactive halogen-containing water equipped with a redox potentiometer.
  • halogen particularly iodine
  • seawater river water, groundwater, wastewater treated water, etc. containing radioactive halogen
  • FIG. 1 An example of the purification apparatus for radioactive halogen-containing water of the present invention is shown in FIG.
  • the purification apparatus for radioactive halogen-containing water shown in FIG. 1 raw wastewater 1 is temporarily stored in a wastewater tank 2, then processed by a pretreatment unit 4 by a supply pump 3, and sent to a pretreatment water tank 5.
  • the pretreatment unit 4 is intended to remove suspended substances, and includes sedimentation separation, flotation separation, sand filtration, and membrane filtration.
  • the flocculant is used. Therefore, it is preferable not to add a flocculant and to apply membrane filtration that can reliably remove suspended components.
  • the oxidation-reduction potential is 800 mV or less, preferably 500 mV or less, and 200 mV or more.
  • wastewater that stays in an anaerobic state in the basement or in the tank may have a redox potential lower than 200 mV in advance. In such a case, there is a problem with supplying it to the pretreatment as it is. Absent. However, since suspended organic matter contained in wastewater is incorporated to some extent by complexing or adsorbing halogen, the oxidation-reduction potential of the wastewater is oxidized by the supply water to the semipermeable membrane unit.
  • the halogen incorporated in the suspension is ionized and solid-liquid separation cannot be performed, and then the redox potential rises and tends to be difficult to remove with a semipermeable membrane unit. It is preferable to lower the oxidation-reduction potential of the pretreatment water supplied to the first semipermeable membrane unit 8 as compared with the oxidation-reduction potential of the wastewater supplied to the unit 4. In addition, it is not deny that the oxidizing agent is added intermittently (for example, several minutes to several tens of minutes / day) for the purpose of cleaning the piping, but it is necessary to pay attention to fluctuations in treated water during that time. Moreover, it is also possible to add a flocculant and an adsorbent only during that time.
  • the reducing agent is added in the reducing agent injection unit 6 so that the pretreatment water has an oxidation-reduction potential below the halogen reduction potential, specifically 500 mV or less, preferably 200 mV or less, more preferably 100 mV or less. Then, it is sent to the first semipermeable membrane unit 8 by the first booster pump 7 and separated (first embodiment of the present invention). As described above, even when the oxidation-reduction potential of the waste water is less than 200 mV, the oxidation-reduction potential may rise before being supplied to the first semi-permeable membrane unit 8, so the first semi-permeable membrane unit.
  • the oxidation-reduction potential before being supplied to 8 is measured, and preferably the reducing agent is sufficiently added so that the oxidation-reduction potential of the pretreated water supplied to the first semipermeable membrane unit 8 is 200 mV or less, more preferably Is preferably maintained at 100 mV or less.
  • the measurement position of the oxidation / reduction potential of the wastewater is preferably in front of the pretreatment unit 4, particularly in the vicinity of the water intake, but even if it is behind the pretreatment unit 4, the object of the present invention is substantially achieved. It is possible to achieve. That is, when a high oxidation-reduction potential is shown at the outlet of the pretreatment unit 4, it is possible to take measures such as adding a reducing agent in front of the pretreatment unit 4. Of course, there is no problem in monitoring the oxidation-reduction potential both before and after the pretreatment unit 4.
  • the redox potential in front of the first semipermeable membrane unit 8 In order to suppress the redox potential in front of the first semipermeable membrane unit 8, it is common to monitor the redox potential in front of the semipermeable membrane unit. Monitoring the redox potential, or both. In particular, it is also preferable to prepare for both in consideration of a case where an increase in the redox potential in the semipermeable membrane unit occurs by monitoring both. Furthermore, monitoring the oxidation-reduction potential before and after the reducing agent injection unit 6 makes it easy to control the amount of reducing agent injection, and to easily detect more than injection, which is one of the preferred embodiments.
  • the redox potential can be measured online or offline using a commercially available ORP meter (redox potential meter). However, when measuring offline, the effects of dissolution of the outside air and temperature changes can be observed. In order to receive, it is preferable to measure online, but it is not particularly limited.
  • ORP meter suitable for this application include PH202 (or OR100) / OR8EFG and PH72 / OR72SN manufactured by Yokogawa Electric Corporation.
  • the separation treatment by the semipermeable membrane has a first purpose of removing iodine.
  • the first semipermeable membrane is obtained by reducing the supply water of the first semipermeable membrane unit 8.
  • the removal rate of iodine in the unit 8 can be improved, further, as a second object, other halogens and the like that become inhibitors when being adsorbed in the adsorption unit 12 at the subsequent stage can be removed.
  • the permeated water of the first semipermeable membrane unit 8 can be discharged or reused as purified water 13 as it is, but subsequently treated by the adsorption unit 12 to reduce the iodine concentration. It is preferable to reduce (the third embodiment of the present invention).
  • the applicable adsorption unit 12 is not particularly limited as long as it can adsorb iodine such as activated carbon or ion exchange resin, but it has high adsorption efficiency and can be desorbed / regenerated.
  • An anion exchange resin is optimal (fourth embodiment of the present invention).
  • FIG. 1 illustrates the case where the semipermeable membrane unit has one stage, but as shown in FIG. 2, the semipermeable membrane may have a plurality of stages.
  • the intermediate water tank 9 and the second booster pump 10 it is possible to provide the intermediate water tank 9 and the second booster pump 10, or directly connect the transmission side of the first semipermeable membrane unit 8 and the supply side of the second semipermeable membrane unit 11, It is possible to omit the intermediate water tank 9 or omit the second booster pump 10.
  • a reducing agent for the purpose of enhancing the removal performance of the second semipermeable membrane unit 11, it is possible to add a reducing agent again, but the reducing agent is added in front of the first semipermeable membrane unit 8.
  • the pH be 8 or more, preferably 9 or more, and then supplied to the second semipermeable membrane unit 11 (fifth embodiment of the present invention). That is, depending on the charge characteristics of the semipermeable membrane, when the reducing agent is acidic or neutral, the permeated water of the first semipermeable membrane unit 8 is often shifted to acidic. To increase the pH. In FIG. 2, the concentrated water of the second semipermeable membrane unit 11 is preferably returned to the upstream side of the first semipermeable membrane unit 8 because the iodine concentration is increased.
  • the suspended substance can be reliably treated without the addition of a flocculant in order to reduce the load on the subsequent semipermeable membrane unit.
  • fine particles of 0.45 ⁇ m or more can be removed by 95% or more, more preferably 99% or more, and furthermore, 0.01 ⁇ m or more of fine particles can be removed by 80% or more, and further 90% or more.
  • it can be done (second embodiment of the invention).
  • the removal performance of the fine particles of the membrane is 0.45 ⁇ m
  • polystyrene latex fine particles K045, manufactured by Iwai Chemicals Co., Ltd.
  • concentration of the filtrate after membrane filtration is measured. Can be obtained.
  • liquids containing 1000 ppm of dextran having different molecular weights for example, molecular weights of 70 kDa, 100 kDa, 200 kDa, and 500 kDa
  • an approximated curve can be created by the Gompertz function, 150 kDa is regarded as 0.01 ⁇ m, and the blocking performance at 150 kDa is estimated.
  • a stirring type ultra folder (UHP-43K, capacity 70 mL) having a membrane area of 11.64 cm 2 is used, and the dispersion is stirred while being stirred at a pressure of 10 kPa.
  • a mini-module having an effective length of about 20 cm ⁇ 2 pieces is produced, and the apparent membrane surface linear velocity is 1 to 1.5 m.
  • the filtered water obtained by the solid-liquid separation unit 17 can be returned to the waste water tank 2 as illustrated in FIG. 4 or can be returned to the front of the pretreatment unit 4.
  • some raw wastewater may contain volatile iodine, it can be volatile by degassing it by aeration with a gas that does not contain radioactive materials or contain low concentrations in advance. It is also possible to remove iodine (eighth embodiment of the present invention). Volatile iodine may be difficult to remove with a semipermeable membrane unit depending on the pH or temperature of the wastewater, and this is a preferred embodiment because the amount of added chemicals can be reduced in view of the case of pH adjustment at a later stage.
  • FIG. 3 illustrates a case where the concentrated wastewater of the first semipermeable membrane unit 8 is processed by the third semipermeable membrane unit 25.
  • the permeated water 26 of the third semipermeable membrane unit which has a lower quality than the permeated water of the first semipermeable membrane unit 8, may be generated. There is no problem if it can be properly used depending on the situation, and it is also possible to return to the upstream side of the first semipermeable membrane unit 8.
  • the reducing agent may react with the reducing agent to generate an oxidizing agent, and the reducing power of the concentrated water that has passed through the first semipermeable membrane unit 8. It is also a preferable aspect that a reducing agent is added again to the concentrated waste water of the first semipermeable membrane unit 8 since the oxidation-reduction potential may increase.
  • a reducing agent is added again to the concentrated waste water of the first semipermeable membrane unit 8 since the oxidation-reduction potential may increase.
  • the pH of the water supplied to the third semipermeable membrane unit 25 is preferably 7 or less.
  • the concentrated water line of the first semipermeable membrane unit 8 and the supply water line to the third semipermeable membrane unit 25 are directly connected to increase the pressure by the intermediate booster pump 28.
  • the concentrated water of one semipermeable membrane unit 8 is temporarily stored in an intermediate tank or the like and then supplied again to the third semipermeable membrane unit 25 by a booster pump.
  • the pressure energy of the concentrated water in the first semipermeable membrane unit 8 is recovered, energy loss is inevitable, but the chemical addition can be performed at an open or low pressure.
  • FIG. 4 shows an example of the case where the second semipermeable membrane unit 11 and the third semipermeable membrane unit 25 are used together.
  • the first semipermeable membrane unit 8 and It is possible to control the recovery rate ( permeate / feed water) of the second semipermeable membrane unit 11 so that the water quality of the purified water 13 is satisfied at a certain level.
  • the fluctuation that is, the amount of water sent to the concentrated water storage tank 24
  • the third semipermeable membrane unit 25 can be controlled by the third semipermeable membrane unit 25.
  • FIG. 5 shows an example in which the concentration separation unit 18 is applied instead of the third semipermeable membrane unit 25 and FIG. 6 shows the separation of the permeated water 26 of the third semipermeable membrane unit 25 by the concentration separation unit 18. Then, an example in which the concentrated water 19 is refluxed upstream of the first semipermeable membrane unit 8 is shown.
  • the semipermeable membrane unit applicable to the present invention is not particularly limited, but for easy handling, a hollow fiber membrane-like or flat membrane-like semipermeable membrane is housed in a casing to form a fluid separation element (element). It is preferable to use what was loaded in a pressure vessel.
  • the fluid separation element is formed of a flat membrane, for example, generally a semipermeable membrane is wound in a cylindrical shape together with a flow path material (net) around a cylindrical central pipe having a large number of holes.
  • TM700 series and TM800 series manufactured by Toray Industries, Inc. can be mentioned. It is also preferable to configure the semipermeable membrane unit by connecting one or more fluid separation elements in series or in parallel.
  • the membrane structure has a dense layer on at least one side of the membrane, and on the asymmetric membrane having fine pores gradually increasing from the dense layer to the inside of the membrane or the other side, or on the dense layer of the asymmetric membrane.
  • a composite film having a very thin functional layer formed of another material may be used.
  • the feed water is concentrated. Therefore, scale inhibitors, acids and alkalis are added to the feed water of each semipermeable membrane unit to prevent scale precipitation due to concentration and to adjust pH. It is possible to In addition, it is preferable to implement scale inhibitor addition upstream from pH adjustment so that the addition cost can be exhibited. It is also preferable to prevent an abrupt concentration or pH change in the vicinity of the addition port by providing an in-line mixer immediately after the addition of the chemical, or by directly contacting the addition port with the flow of the supply water. .
  • the scale inhibitor is a substance that forms a complex with a metal, a metal ion, or the like in a solution and solubilizes the metal or metal salt, and an organic or inorganic ionic polymer or monomer can be used.
  • organic polymers synthetic polymers such as polyacrylic acid, sulfonated polystyrene, polyacrylamide, and polyallylamine, and natural polymers such as carboxymethylcellulose, chitosan, and alginic acid can be used, and ethylenediaminetetraacetic acid can be used as a monomer.
  • polyphosphate etc. can be used as an inorganic type scale inhibitor.
  • polyphosphate and ethylenediaminetetraacetic acid are particularly preferably used from the viewpoints of availability, ease of operation such as solubility, and cost.
  • the polyphosphate refers to a polymerized inorganic phosphate material having two or more phosphorus atoms in a molecule typified by sodium hexametaphosphate and bonded with an alkali metal, an alkaline earth metal and a phosphate atom.
  • Typical polyphosphates include tetrasodium pyrophosphate, disodium pyrophosphate, sodium tripolyphosphate, sodium tetrapolyphosphate, sodium heptapolyphosphate, sodium decapolyphosphate, sodium metaphosphate, sodium hexametaphosphate, and potassium salts thereof. Etc.
  • sulfuric acid, sodium hydroxide, and calcium hydroxide are generally used as the acid and alkali, but hydrochloric acid, oxalic acid, potassium hydroxide, sodium bicarbonate, ammonium hydroxide, and the like can also be used. However, it is better not to use calcium or magnesium in order to prevent an increase in scale components in seawater.
  • sand filtration when sand filtration is used for pretreatment, it is possible to apply gravity-type filtration that naturally flows down, or it is possible to apply pressurized filtration in which a pressure tank is filled with sand. .
  • sand to be filled single-component sand can be applied.
  • anthracite, silica sand, garnet, pumice, and the like can be combined to increase filtration efficiency.
  • the microfiltration membrane and the ultrafiltration membrane are not particularly limited, and a flat membrane, a hollow fiber membrane, a tubular membrane, a pleat type, or any other shape can be used as appropriate.
  • the material of the membrane is also particularly limited, and inorganic materials such as polyacrylonitrile, polyphenylene sulfone, polyphenylene sulfide sulfone, polyvinylidene fluoride, polypropylene, polyethylene, polysulfone, polyvinyl alcohol, cellulose acetate, and ceramics can be used.
  • inorganic materials such as polyacrylonitrile, polyphenylene sulfone, polyphenylene sulfide sulfone, polyvinylidene fluoride, polypropylene, polyethylene, polysulfone, polyvinyl alcohol, cellulose acetate, and ceramics can be used.
  • inorganic materials such as polyacrylonitrile, polyphenylene sulfone, polyphenylene sulfide sulfone, polyvinylidene fluoride, polypropylene, polyethylene, polysulfone, polyvinyl alcohol, cellulose acetate, and ceramics can be used
  • the feed water contains a large amount of soluble organic matter
  • a chelating agent such as an organic polymer electrolyte or sodium hexametaphosphate may be added, or exchanged with soluble ions using an ion exchange resin or the like.
  • iron or manganese is present in a soluble state, it is also preferable to use an aeration oxidation filtration method, a contact oxidation filtration method, or the like.
  • nanofiltration membrane for pretreatment in order to remove specific ions and polymers in advance and operate the purification apparatus for radioactive halogen-containing water of the present invention with high efficiency.
  • the present invention relates to a method and apparatus for purifying radioactive halogen-containing water that removes radioactive halogen, particularly radioactive iodine, from seawater, river water, groundwater, wastewater-treated water, etc. containing radioactive halogen, and is contained in trace amounts in water. Radioactive iodine can be removed efficiently.

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  • General Engineering & Computer Science (AREA)
  • High Energy & Nuclear Physics (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
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Abstract

La présente invention concerne une méthode et un dispositif de purification d'eau qui contient un halogène radioactif : l'eau contenant un halogène radioactif est régulée de façon à avoir un potentiel d'oxydoréduction inférieur ou égal à 800 mV et est soumise à une séparation solide-liquide, et l'eau prétraitée obtenue est ensuite régulée de façon à avoir un potentiel d'oxydoréduction inférieur ou égal à 500 mV et traitée avec une unité à membrane semi-perméable afin de séparer l'eau prétraitée en eau usée concentrée et eau filtrée. L'halogène radioactif, en particulier l'iode radioactif, est alors éliminé de l'eau (eau de mer, eau de rivière, eau souterraine ou eaux usées traitées par exemple) qui contient l'halogène radioactif. De ce fait, l'iode radioactif présent en petites quantités dans l'eau est éliminé efficacement.
PCT/JP2012/059849 2011-04-21 2012-04-11 Méthode de purification d'eau contenant un halogène radioactif, procédé de production d'eau filtrée, et dispositif de purification d'eau contenant un halogène radioactif Ceased WO2012144384A1 (fr)

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JP2012522851A JPWO2012144384A1 (ja) 2011-04-21 2012-04-11 放射性ハロゲン含有水の浄化方法、透過水の製造方法および放射性ハロゲン含有水の浄化装置

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Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2014128748A (ja) * 2012-12-28 2014-07-10 Hitachi Ltd 淡水化システム
JP2017186770A (ja) * 2016-04-04 2017-10-12 清水建設株式会社 地下水の処理方法
JP2017186772A (ja) * 2016-04-04 2017-10-12 清水建設株式会社 地下水リチャージシステム
JP2017186771A (ja) * 2016-04-04 2017-10-12 清水建設株式会社 地下水リチャージシステム
EP3225595A4 (fr) * 2014-11-27 2018-06-27 Toray Industries, Inc. Procédé de production d'eau
CN109741850A (zh) * 2018-12-27 2019-05-10 中核四0四有限公司 一种铀纯化转化生产线设备清洗液的处理装置及方法
JP2020060098A (ja) * 2016-04-04 2020-04-16 清水建設株式会社 地下水リチャージシステム
EP3778496A4 (fr) * 2018-03-27 2021-07-14 Toray Industries, Inc. Procédé de traitement de l'eau et dispositif de traitement de l'eau

Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS59162285A (ja) * 1983-03-04 1984-09-13 Asahi Chem Ind Co Ltd イオン交換膜法による食塩の電解方法
JPS61116695A (ja) * 1984-11-12 1986-06-04 科学技術庁原子力局長 放射性ヨウ素含有水溶液の処理法
JPH07191190A (ja) * 1993-12-27 1995-07-28 Power Reactor & Nuclear Fuel Dev Corp 放射性物質取扱施設の廃水処理装置
JP2005037147A (ja) * 2003-07-15 2005-02-10 Showa Engineering Co Ltd 復水器および低圧タービンからの放射性ヨウ素の除去方法
JP2005305265A (ja) * 2004-04-20 2005-11-04 Jfe Engineering Kk 塩水からのヨウ素除去方法
JP2008064703A (ja) * 2006-09-11 2008-03-21 Japan Organo Co Ltd 放射性物質含有排水の処理方法および装置
JP2008296188A (ja) * 2007-06-04 2008-12-11 Toray Ind Inc 膜分離装置および膜分離方法
JP2010201313A (ja) * 2009-03-02 2010-09-16 Kurita Water Ind Ltd 逆浸透膜分離方法
JP2011161435A (ja) * 2010-01-14 2011-08-25 Toray Ind Inc 半透膜の性能回復処理方法

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS59162285A (ja) * 1983-03-04 1984-09-13 Asahi Chem Ind Co Ltd イオン交換膜法による食塩の電解方法
JPS61116695A (ja) * 1984-11-12 1986-06-04 科学技術庁原子力局長 放射性ヨウ素含有水溶液の処理法
JPH07191190A (ja) * 1993-12-27 1995-07-28 Power Reactor & Nuclear Fuel Dev Corp 放射性物質取扱施設の廃水処理装置
JP2005037147A (ja) * 2003-07-15 2005-02-10 Showa Engineering Co Ltd 復水器および低圧タービンからの放射性ヨウ素の除去方法
JP2005305265A (ja) * 2004-04-20 2005-11-04 Jfe Engineering Kk 塩水からのヨウ素除去方法
JP2008064703A (ja) * 2006-09-11 2008-03-21 Japan Organo Co Ltd 放射性物質含有排水の処理方法および装置
JP2008296188A (ja) * 2007-06-04 2008-12-11 Toray Ind Inc 膜分離装置および膜分離方法
JP2010201313A (ja) * 2009-03-02 2010-09-16 Kurita Water Ind Ltd 逆浸透膜分離方法
JP2011161435A (ja) * 2010-01-14 2011-08-25 Toray Ind Inc 半透膜の性能回復処理方法

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2014128748A (ja) * 2012-12-28 2014-07-10 Hitachi Ltd 淡水化システム
EP3225595A4 (fr) * 2014-11-27 2018-06-27 Toray Industries, Inc. Procédé de production d'eau
JP2017186770A (ja) * 2016-04-04 2017-10-12 清水建設株式会社 地下水の処理方法
JP2017186772A (ja) * 2016-04-04 2017-10-12 清水建設株式会社 地下水リチャージシステム
JP2017186771A (ja) * 2016-04-04 2017-10-12 清水建設株式会社 地下水リチャージシステム
JP2020060098A (ja) * 2016-04-04 2020-04-16 清水建設株式会社 地下水リチャージシステム
EP3778496A4 (fr) * 2018-03-27 2021-07-14 Toray Industries, Inc. Procédé de traitement de l'eau et dispositif de traitement de l'eau
CN109741850A (zh) * 2018-12-27 2019-05-10 中核四0四有限公司 一种铀纯化转化生产线设备清洗液的处理装置及方法

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