WO2003070643A1 - Systeme de traitement de l'eau - Google Patents

Systeme de traitement de l'eau Download PDF

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Publication number
WO2003070643A1
WO2003070643A1 PCT/JP2003/001764 JP0301764W WO03070643A1 WO 2003070643 A1 WO2003070643 A1 WO 2003070643A1 JP 0301764 W JP0301764 W JP 0301764W WO 03070643 A1 WO03070643 A1 WO 03070643A1
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Prior art keywords
water
treatment
membrane
gas phase
organic matter
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PCT/JP2003/001764
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English (en)
Japanese (ja)
Inventor
Makio Tamura
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Organo Corporation
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Publication of WO2003070643A1 publication Critical patent/WO2003070643A1/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
    • B01D61/36—Pervaporation; Membrane distillation; Liquid permeation
    • B01D61/362—Pervaporation
    • 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
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • 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
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • 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
    • C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
    • 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
    • C02F1/28—Treatment of water, waste water, or sewage by sorption
    • C02F1/283—Treatment of water, waste water, or sewage by sorption using coal, charred products, or inorganic mixtures containing them
    • 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
    • C02F1/30—Treatment of water, waste water, or sewage by irradiation
    • C02F1/32—Treatment of water, waste water, or sewage by irradiation with ultraviolet light
    • 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
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/448—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by pervaporation
    • 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
    • C02F1/4693—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis
    • C02F1/4695—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis electrodeionisation
    • 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
    • C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
    • C02F2001/422—Treatment of water, waste water, or sewage by ion-exchange using anionic exchangers
    • 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
    • C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
    • C02F2001/425—Treatment of water, waste water, or sewage by ion-exchange using cation exchangers
    • 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
    • C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
    • C02F2001/427—Treatment of water, waste water, or sewage by ion-exchange using mixed beds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • C02F2101/32—Hydrocarbons, e.g. oil
    • C02F2101/322—Volatile compounds, e.g. benzene

Definitions

  • the present invention relates to a water treatment system in which organic substances are efficiently removed from water containing a small amount of volatile organic substances so that treated water can be reused at low cost.
  • the first method is separation. Separation of concentrated water and permeated water by membrane filtration of organic matter in feed water, adsorption separation with activated carbon and synthetic adsorbents, and separation of ionizable organic substances such as organic acids by ion exchange reaction are included in this category. It is listed as an entry.
  • the second method is decomposition. Oxidative decomposition by ozone or hydrogen peroxide, decomposition by thermochemical reaction under high temperature and high pressure, oxidative decomposition by ultraviolet irradiation, treatment using a catalyst for photooxidative decomposition, decomposition by biological treatment, etc. shall fall into this category. It is mentioned.
  • the water treatment system does not depend on the type of organic matter.
  • reverse osmosis membrane treatment which has a wide range of types of organic substances that can be separated
  • ultraviolet oxidation treatment which can decompose almost all organic substances.
  • the amount of power required for reverse osmosis membrane operation hardly changes with the concentration of TOC (total organic carbon) in the recovered water, but the amount of power required for UV oxidation increases as the concentration of organic matter increases.
  • the TOC concentration is reduced by first passing the water to be treated through the reverse osmosis membrane, and then the remaining T 0 C is completely decomposed into carbonic acid by ultraviolet oxidation, or decomposed into organic acid or carbonic acid and ion-exchange resin. A method of ion exchange removal has been adopted.
  • An object of the present invention is to efficiently and inexpensively remove organic substances contained in treated water containing a small amount of volatile organic substances, which are wastewater and recovered water in various industrial fields.
  • the organic matter is removed from the water containing the volatile organic matter by concentrating it on the gas phase side by an evaporation method.
  • the substance to be removed is left on the liquid phase side and concentrated, and the substance is removed.
  • it is concentrated and removed to the gas phase.
  • Spent wastewater and recovered water in various industrial fields to be treated in the present invention contain a small amount of volatile organic substances to be removed in the treated water. In this case, the system of the present invention is particularly effective.
  • FIG. 1 is a characteristic diagram showing an example of the concept of vapor-liquid equilibrium.
  • FIG. 2 is an equipment system diagram showing a basic configuration of a processing apparatus using an evaporation method according to the present invention.
  • FIG. 3 is an equipment system diagram showing another configuration example of the processing apparatus using the evaporation method in the present invention.
  • FIG. 4 is a system diagram showing still another example of the configuration of the processing apparatus using the evaporation method according to the present invention.
  • FIG. 5 is an equipment system diagram showing an example of the water treatment system according to the present invention.
  • FIG. 6 is an equipment system diagram showing another example of the water treatment system according to the present invention.
  • FIG. 7 is an equipment system diagram showing still another example of the water treatment system according to the present invention.
  • FIG. 8 is an equipment system diagram showing still another example of the water treatment system according to the present invention.
  • the system is based on the combination of reverse osmosis membrane treatment and ultraviolet oxidation treatment because of its high separation performance of reverse osmosis membranes for many types of organic substances and the fact that the ultraviolet oxidizer can reduce the concentration of organic substances to low concentrations. It is considered effective to add some processing to the data.
  • the system according to the present invention incorporates a process of concentrating and removing organic substances on the gas phase side by an evaporation method.
  • Fig. 2 shows the configuration of the basic system (basic system) according to the present invention.
  • the organic substance-containing water to be treated is supplied to the evaporative treatment apparatus 1.
  • volatile organic substances in the water to be treated are vaporized, and organic substances in the water to be treated are removed.
  • the treated water from which organic substances have been removed and reduced is taken out by the pump 2.
  • the evaporating apparatus 1 is separated by a membrane into a liquid phase chamber (liquid phase side) la and a gas phase chamber (gas phase side) lb, and water to be treated is supplied to the liquid phase chamber 1a. . Then, the gas phase chamber 1 b is decompressed by the vacuum pump 3 so as to be contained in the water to be treated on the liquid phase side. Organic matter is vaporized through the membrane, obtained in the gas phase chamber lb, and discharged out of the system.
  • an MD membrane hydrophobic porous membrane
  • a PV membrane siloxane or inorganic membrane
  • a PP porous membrane is used as the MD membrane
  • a dimethyl membrane is used as the PV membrane.
  • a siloxane film or the like is used.
  • the material of the film is such that when the film is disposed at the gas-liquid interface, the vapor pressure in the gas phase of the organic substance to be removed becomes high, and the organic substance is easily evaporated.
  • the membrane may have any shape, such as a hollow fiber or a flat plate.
  • the pressure in the gas phase chamber and the temperature in the liquid phase chamber, which are decompressed by the vacuum pump 3, are changed through the membrane according to the vapor pressure of the organic substance to be removed (vapor pressure at the time of vapor-liquid equilibrium). Set to something that can be vaporized.
  • Fig. 3 shows an example of a configuration in which a reverse osmosis treatment unit (RO) 4 is provided in front of the basic system of Fig. 2.
  • Reverse osmosis treatment in which organic matter in the water to be treated is removed by the reverse osmosis treatment unit 4 Evaporation of water It is supplied to the device 1 and processed here. Therefore, low-molecular-weight organic substances such as alcohol which are difficult to remove by the reverse osmosis treatment device 4 are removed in the evaporation treatment device 1.
  • FIG. 4 shows an example of a configuration in which an activated carbon treatment unit (AC) 5 and a reverse osmosis treatment unit (RO) are provided in a stage preceding the basic system in FIG.
  • AC activated carbon treatment unit
  • RO reverse osmosis treatment unit
  • RO reverse osmosis membrane treatment
  • AC activated carbon treatment
  • an evaporation treatment MD using a hydrophobic porous membrane (MD membrane) and an evaporation treatment PV using a siloxane-based membrane (PV membrane) are employed.
  • RO + MD, AC + RO + MD, RO + PV, AC + R 0 + PV combined with reverse osmosis treatment unit (RO) and activated carbon treatment (AC) The test was performed. For reference, water and MD alone were also treated.
  • Table 1 shows the processing results of such tests.
  • water to be treated water having a TOC (total organic carbon) of 800 ppb (zgC / L) and four typical organic waters to be treated in the present invention are referred to. Each was mixed with 500 ju g C / L.
  • IPA isopropyl alcohol
  • ethanol methanol
  • acetone a compound that was difficult to separate with high efficiency by conventional reverse osmosis membrane treatment alone.
  • Reverse osmosis membrane treatment apparatus is Nitto Denko Corp.
  • ES 20- U8 raw water side pressure 8 kg / cm 2 pressurized, permeate flow 1.
  • Activated carbon treatment uses a PCF-2000 manufactured by Organo Co., Ltd.
  • the PV membrane used at the gas-liquid interface has high alcohol selective solubility in water on the surface and diffusion inside.
  • a membrane material having a high surface hydrophobicity and a rough interior was selected so that the water selectivity due to the difference in the properties would not affect the entire permeation.
  • the surface was thinly covered with a perfluoro compound, and a film made of polysiloxane was used inside the film.
  • As the MD membrane a hydrophobic porous PP (polypropylene) hollow fiber membrane was used.
  • RO indicates reverse osmosis membrane treatment
  • AC indicates activated carbon treatment
  • ppb indicates / g C / L.
  • BP [° C] indicates the boiling point of water or added organic matter
  • the RO rejection [%] is 4 O jg C / L because the TOC of the water treated by RO is 5 O jg C / L.
  • Calculated by subtracting 5 OgC / L from the TOC of treated water treated with RO alone for the water to be treated after adding 500 ⁇ gC / L of each type of organic matter, and dividing this by the added organic matter concentration of 500 ⁇ gC / L It was done. In other words, the removal rate of each organic substance by RO alone is shown.
  • VP 30 Torr indicates the degree of vacuum of the gas phase chamber 1 b in the evaporator 1
  • HP indicates the raw water chamber pressure (permeation pressure) in the reverse osmosis apparatus 4.
  • PV film Dimethylsiloxane film V P 30 torr
  • R0 membrane ES20-S8U HP 8 kg / cm 2
  • Table 1 shows that the reverse osmosis membrane has an excellent ability to remove organic matter from water, with a removal rate of 94% for organic matter, but 90% for IPA. % Is relatively good, but not enough. It can be seen that it is 50% for ethanol, 10% for methanol and 50% for acetone. Therefore, even if the reverse osmosis membrane is used multiple times, its removal effect is low.
  • + IPA is 90 j gC / L
  • + ethanol is 290 ⁇ gC / L
  • + methanol is 490 ⁇ gC / L
  • + acetone is 290 ⁇ gC / L. You can see that it is not.
  • the activated carbon treatment AC is effective from the viewpoint of removing the oxidizing agent and utilizing the function of protecting the reverse osmosis membrane.
  • the evaporation treatment of the present invention is very effective for the water to be treated containing the above-mentioned organic substances IPA, ethanol, methanol, acetone and the like.
  • an extremely effective organic matter removal system is constructed by using it in combination with a reverse osmosis membrane.
  • the use of a PV membrane has higher organic matter removal performance under the same conditions than the use of a hydrophobic porous membrane.
  • the vapor pressure of each organic substance does not change due to the gas-liquid equilibrium at the normal gas-liquid interface.
  • the PV film selectively guides the organic matter to the gas phase, so that the vapor pressure of the various organic materials in the gas phase becomes higher than in the normal gas-liquid equilibrium. Therefore, by disposing the PV film, the removal of organic substances from water into the gas phase is promoted.
  • an ultraviolet oxidizing device in order to further reduce the concentration of organic matter in the treated water in the treatment using these evaporating devices, as shown in a more specific system construction example described below, an ultraviolet oxidizing device and It is preferable that the treatment is further performed by an ion exchange device, an electric regeneration type desalination device, or the like.
  • FIG. 1 shows the concept of vapor-liquid equilibrium in the case where ethanol is considered as an example of a volatile organic substance to be used in the present invention.
  • the horizontal axis is the molar fraction of ethanol in the liquid phase (X [mol / mo1]), and the vertical axis is the molar fraction of ethanol in the gas phase (Y [mo1 / mo1]).
  • Curve A shows the vapor-liquid equilibrium relationship at a simple gas-liquid interface
  • curve B shows the apparent vapor-liquid equilibrium relationship when an ethanol-selective pervaporation membrane (PV membrane) is used.
  • PV membrane ethanol-selective pervaporation membrane
  • the PV film examples include a blend film of p (perfluoroalkyloxydimethylsilyl) styrene and polydimethylsiloxane (the former is lwt%).
  • a membrane containing silicon or fluorine tends to be an organic-selective membrane, probably because of high hydrophobicity.
  • the organic matter (vapor) concentration in the gas phase is Y1 as shown in Curve A in a normal gas-liquid equilibrium relationship.
  • a PV membrane having the characteristics of the curve B is used, a vapor is generated which is concentrated to the organic matter concentration Y 2 in the gas phase with respect to the organic matter concentration X 1 in the liquid phase.
  • the T ⁇ C concentration in the treated water also increases.
  • the concentration of IPA in the water to be treated increases, but the ratio is much lower than that of the conventional method.
  • the treated water concentration is the same as the IPA addition concentration of 500 ⁇ gC / L, and even when the IPA concentration is 100 000 ⁇ //, the treatment in the treatment of 110 +? Water TOC has a very low concentration of 290 ⁇ gC / L.
  • the concentration region of about 100000 ppb (jug C / h) in Table 2 is also a region where the present invention can be applied more effectively than the conventional method.
  • Tables 3 and 4 show test results on the effects of operating conditions (temperature, degree of vacuum) on the system of the present invention. These are the test results using the system shown in Fig. 3.
  • the vapor pressure of pure IPA is reported to be 17 mmHg (Torr) at 10 ° C and 32 mmHg (Torr) at 20 ° C. Even in the dilute aqueous solution used in this test, it is considered that the partial pressure of IPA became 3 OmmHg or more between 15 and 20 ° C, and the movement from the liquid phase to the gas phase increased rapidly. That is, there is a temperature range in which the movement from the liquid phase to the gas phase rapidly increases, and by operating at a liquid temperature higher than that temperature range, the concentration and removal performance to the gas phase can be enhanced.
  • the liquid phase side in the evaporation method is operated at a liquid temperature within an optimum temperature range in consideration of the boiling point of the organic substance to be removed at the pressure during operation. That is, it is preferable to operate at a temperature higher than the temperature range in which the vapor pressure of the pure substance greatly changes from the vapor pressure at the vapor-liquid equilibrium, and the substance is easily vaporized.
  • the gas phase side in the evaporation method is operated at an optimum pressure in consideration of the vapor pressure of the organic matter to be removed at the operating temperature.
  • the operation is performed at a vacuum degree (low pressure) higher than the vacuum degree range where the vapor pressure greatly changes from the vapor pressure at the vapor-liquid equilibrium of the pure substance and the substance is easily vaporized. Is preferred.
  • the water to be treated is a mixed solution of various substances, and therefore, the preferable operation range is the boiling point of the organic matter to be removed at the pressure during operation, and the steam at the temperature during operation.
  • the optimum operating conditions can be determined by trial calculations and experiments with reference to the pressure.
  • the evaporation method used in the present invention is to heat organic water to evaporate organic matter and reduce organic matter.
  • a method of evaporating and removing organic substances by supplying water to the decompressor, a hydrophobic porous membrane such as PP, PE, polymethylpentene, PFA, PTFE, etc.
  • a vaporizer that evaporates organic substances through this porous membrane, an organic PV membrane such as dimethylsiloxane, and an inorganic PV membrane such as zeolite and silicalite.
  • An evaporator or the like devised so that the organic matter concentration becomes higher on the gas phase side than the equilibrium relationship can be used. In that case, timely heating of the feedwater, heat recovery from the treated water to the feedwater, decompression to promote the transfer of organic matter to the gas phase, and injection of a sweep gas can be used.
  • the organic matter separated into the gas phase by the evaporation method is treated by cooling liquefaction and adsorbent adsorption alone or in combination, whereby the organic matter to be removed is removed. Collection or disposal can be performed efficiently.
  • various types of systems can be constructed by incorporating the evaporative treatment apparatus (EV) for evaporating and removing the organic substances as described above.
  • EV evaporative treatment apparatus
  • vaporization and removal of organic matter by the above-mentioned evaporation method activated carbon treatment equipment (AC), cartridge polisher (CP), reverse osmosis membrane treatment equipment (RO), electric desalination treatment equipment (EDI) and ultraviolet oxidation treatment equipment
  • the system can be constructed as a combination of at least one processing unit, UVox) and ultrafiltration unit (UF).
  • FIG. 5 shows examples of various system constructions.
  • an evaporator (EV) 11 for performing the evaporating method of the present invention as a pretreatment of RO is provided, and the organic matter concentrated on the gas phase side is removed by a vacuum pump (VP) 12.
  • the liquid phase in the state (the water treated by the evaporator 11) is sent to the reverse osmosis membrane processor (RO) 14 via the pump 13.
  • the permeated water of the reverse osmosis membrane treatment device (RO) 14 is subjected to organic matter decomposition treatment by the ultraviolet oxidation treatment device (UVox) 15, passed through the electric desalination treatment device (EDI) 16, and is taken out as treated water It is like that.
  • UVox ultraviolet oxidation treatment device
  • EDI electric desalination treatment device
  • Organic matter remaining in the permeated water of the reverse osmosis membrane treatment device 14 is irradiated with ultraviolet rays by the ultraviolet oxidation treatment device 15, whereby the remaining organic matter is decomposed into organic acids and carbonic acids. Then, by treating the treated water of the ultraviolet oxidation treatment device 15 with the electric desalination treatment device 16, organic acids and the like are removed, and treated water having a very low TOC can be obtained. In the electric desalination treatment device 16, various inorganic salts are also removed.
  • an evaporator (EV) 23 for performing the evaporating method of the present invention is provided as a post-treatment by the activated carbon processor (AC) 21 and the reverse osmosis membrane processor (RO) 22.
  • AC activated carbon processor
  • RO reverse osmosis membrane processor
  • the vacuum pump (VP) 24 is for reducing the gas phase of the evaporator 23.
  • the treated water of the evaporator 23 passes through the subsequent electric desalination unit (EDI) 25 and is then taken out as treated water.
  • EDI electric desalination unit
  • C In the system shown in Fig. 7, for example, the process recovered water is supplied to the reverse osmosis membrane treatment unit (RO) 32 via the pressure pump 31 and the permeated water is removed from the system.
  • the gaseous phase (gas) in the evaporator 33 is sucked by a vacuum pump (VP) 34 through a condenser 35.
  • VP vacuum pump
  • the supplied gas is cooled and liquefied.
  • the organic matter in the exhaust gas from the evaporator 33 is liquefied together with the water and discharged through the pump 36.
  • the gas phase components that have not been liquefied in the condenser 35 are subjected to an adsorption treatment in an adsorption treatment device (AD) 37, so that they are rendered harmless and exhausted.
  • AD adsorption treatment device
  • UVox ultraviolet oxidation unit
  • CP cartridge police
  • UF ultrafiltration unit
  • the water to be treated (process recovery water in this embodiment) is blended with pure water produced from industrial water.
  • This pure water is used for industrial water On-exchange resin tower (K) 41, decarbonation tower (D) 42, anion-exchange resin tower (A) 43, ion-exchange processor 45 equipped with a mixed-bed tower of cation-exchange resin and anion-exchange resin (MB) 44 It is manufactured by processing using Then, this pure water is blended with the process recovery water to be treated water of the present water treatment system.
  • the water to be treated is first treated by a reverse osmosis membrane treatment device (RO) 46, and the permeated water is deaerated by a vacuum deaeration device (VD) 47.
  • the degassed water undergoes an organic matter decomposition treatment by an ultraviolet oxidation treatment device (UVox) 48 and an organic matter separation treatment by a cartridge polisher (CP) 49, and then is subjected to an evaporation treatment device according to the present invention.
  • UVox ultraviolet oxidation treatment device
  • CP cartridge polisher
  • EV evaporation treatment device
  • the water subjected to the evaporating treatment is supplied to the point of use and the like as reusable treated water after being subjected to an organic matter filtration treatment by an ultrafiltration unit (UF) 51.
  • UF ultrafiltration unit
  • partly unused treated water is returned to, for example, a stage preceding an ultraviolet oxidation treatment device (UVox) 48 and is circulated. Further, the water on the concentration side in the ultrafiltration unit (UF) 51 is returned to, for example, a stage preceding the reverse osmosis membrane treatment unit (RO) 46.
  • the water used at each use point is recovered as post-process recovered water after passing through an ultraviolet oxidation treatment device (UVox) 52, an activated carbon treatment device (AC) 53, and a mixed bed tower (MB) 54. As described above, it is blended with pure water produced from industrial water to be treated water of the water treatment system using the evaporation method according to the present invention.
  • the water to be treated is once degassed by a vacuum deaerator (VD) 47, blended with pure water produced from industrial water, and collected and reused.
  • VD vacuum deaerator
  • the organic matter removal performance in the evaporation method can be improved.
  • the ultraviolet oxidizer 48 acetone and the like are generated when the organic load is high.
  • the evaporator 50 according to the present invention is disposed at the subsequent stage of the ultraviolet oxidizer and in front of the ultrafiltration device in order to remove acetone and the like generated by the ultraviolet oxidizer 48. You.
  • the water treatment system provided with the evaporative treatment device according to the present invention can adopt various aspects.
  • the content of the organic matter contained in the water to be treated such as wastewater or recovered water in various industrial fields is extremely efficiently reduced. Can be removed, and treated water with low organic matter concentration can be reused.
  • the evaporating apparatus in the present invention is arranged at an optimum position with respect to the reverse osmosis membrane processing apparatus and the ultraviolet oxidation processing apparatus, it is possible to utilize the advantages of the performance of separating various organic substances by the reverse osmosis membrane processing and to perform the ultraviolet oxidation.
  • the power consumption in processing can be reduced, and the system as a whole can be operated at low cost while exhibiting high organic matter removal performance.
  • the organic matter separated into the gas phase by the evaporation method can be treated, for example, by cooling or liquefaction or adsorption of an adsorbent alone or in combination. This makes it possible to efficiently extract the organic matter separated into the gas phase.
  • the water to be treated contains deaerated water, the performance of separating and concentrating organic substances into a gas phase by the evaporation method is improved. For this reason, it is particularly preferable to include such degassed water in all or part of the water to be treated.
  • the organic substance is separated into gaseous phase and concentrated by the above-mentioned evaporation method, there is a range of optimum operating conditions according to the characteristics of the organic substance to be removed, so the conditions are determined within this range. It is preferable that the removal efficiency can be further improved. For example, it is preferable that the liquid phase side in the evaporation method is operated at a liquid temperature within an optimum temperature range in consideration of the boiling point of the organic substance to be removed at the pressure during operation. Further, it is preferable that the gas phase side in the evaporation method is operated at an optimum pressure (optimum vacuum degree) in consideration of a vapor pressure of an organic substance to be removed at an operating temperature.

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  • Engineering & Computer Science (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
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  • Separation Using Semi-Permeable Membranes (AREA)
  • Physical Water Treatments (AREA)
  • Water Treatment By Electricity Or Magnetism (AREA)
  • Water Treatment By Sorption (AREA)
  • Treatment Of Water By Ion Exchange (AREA)
  • Heat Treatment Of Water, Waste Water Or Sewage (AREA)

Abstract

L'invention concerne un système de traitement de l'eau pour une eau contenant un matériau organique volatile, ce matériau organique volatile étant concentré dans côté de phase gazeuse à l'aide d'un procédé d'évaporation, puis éliminé. De préférence, une membrane séparant la phase gazeuse d'une phase liquide est utilisée pour concentrer le matériau organique au-dessus de l'équilibre gaz-liquide. Ce système peut être utilisé pour éliminer un matériau organique volatile d'une eau devant être traitée contenant une petite quantité d'un matériau organique volatile, cette eau étant typiquement une eau résiduaire ou une eau de récupération dans diverses industries.
PCT/JP2003/001764 2002-02-20 2003-02-19 Systeme de traitement de l'eau WO2003070643A1 (fr)

Applications Claiming Priority (2)

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JP2002043436A JP3922935B2 (ja) 2002-02-20 2002-02-20 水処理システム
JP2002-43436 2002-02-20

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WO2003070643A1 true WO2003070643A1 (fr) 2003-08-28

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JP (1) JP3922935B2 (fr)
TW (1) TW200303850A (fr)
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CN102531140A (zh) * 2012-01-19 2012-07-04 中国科学院地球化学研究所 利用胶质芽孢杆菌处理含汞废水的方法
CN107427038A (zh) * 2014-12-22 2017-12-01 红牛有限责任公司 用于借助于过程液体处理食物和/或容器的方法和设备
CN112537873A (zh) * 2020-10-12 2021-03-23 太原理工大学 一种含细微粉尘煤化工废水的处理工艺和装置

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KR101007418B1 (ko) * 2008-05-28 2011-01-12 순천향대학교 산학협력단 아민 포함 폐수로부터의 아민 회수 방법
US9738575B2 (en) 2012-05-16 2017-08-22 China Petroleum & Chemical Corporation Apparatus for producing ethylene and a producing method thereof
CN103539214B (zh) * 2012-07-12 2015-04-08 中国石油化工股份有限公司 乙醇脱水制乙烯的有机废水处理方法
RU2666424C2 (ru) * 2013-06-04 2018-09-07 Басф Се Способ снижения содержания общего органического углерода в сточных водах
WO2016100997A1 (fr) * 2014-12-22 2016-06-30 Red Bull Gmbh Procédé et dispositif de traitement de produits alimentaires et/ou de récipients au moyen d'un fluide de traitement
CN115417550B (zh) * 2022-09-02 2024-06-18 安徽国星生物化学有限公司 一种吡啶废水资源化利用的方法

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102531140A (zh) * 2012-01-19 2012-07-04 中国科学院地球化学研究所 利用胶质芽孢杆菌处理含汞废水的方法
CN102531140B (zh) * 2012-01-19 2014-04-02 中国科学院地球化学研究所 利用胶质芽孢杆菌处理含汞废水的方法
CN107427038A (zh) * 2014-12-22 2017-12-01 红牛有限责任公司 用于借助于过程液体处理食物和/或容器的方法和设备
CN112537873A (zh) * 2020-10-12 2021-03-23 太原理工大学 一种含细微粉尘煤化工废水的处理工艺和装置

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JP3922935B2 (ja) 2007-05-30
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