WO2018083900A1 - 水処理装置、水処理システム及び水処理方法 - Google Patents
水処理装置、水処理システム及び水処理方法 Download PDFInfo
- Publication number
- WO2018083900A1 WO2018083900A1 PCT/JP2017/033767 JP2017033767W WO2018083900A1 WO 2018083900 A1 WO2018083900 A1 WO 2018083900A1 JP 2017033767 W JP2017033767 W JP 2017033767W WO 2018083900 A1 WO2018083900 A1 WO 2018083900A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- water
- reaction vessel
- ozone
- gas
- hydrogen peroxide
- Prior art date
Links
Images
Classifications
-
- 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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
- B01F23/20—Mixing gases with liquids
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
- B01F25/30—Injector mixers
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
- C01B13/10—Preparation of ozone
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B15/00—Peroxides; Peroxyhydrates; Peroxyacids or salts thereof; Superoxides; Ozonides
- C01B15/01—Hydrogen peroxide
- C01B15/027—Preparation from water
-
- 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
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/46104—Devices therefor; Their operating or servicing
- C02F1/46109—Electrodes
- C02F1/46114—Electrodes in particulate form or with conductive and/or non conductive particles between 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
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/467—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction
- C02F1/4672—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction by electrooxydation
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B1/00—Electrolytic production of inorganic compounds or non-metals
- C25B1/01—Products
- C25B1/28—Per-compounds
- C25B1/30—Peroxides
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B11/00—Electrodes; Manufacture thereof not otherwise provided for
- C25B11/02—Electrodes; Manufacture thereof not otherwise provided for characterised by shape or form
- C25B11/03—Electrodes; Manufacture thereof not otherwise provided for characterised by shape or form perforated or foraminous
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B11/00—Electrodes; Manufacture thereof not otherwise provided for
- C25B11/04—Electrodes; Manufacture thereof not otherwise provided for characterised by the material
- C25B11/042—Electrodes formed of a single material
- C25B11/043—Carbon, e.g. diamond or graphene
-
- 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
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/46104—Devices therefor; Their operating or servicing
- C02F1/46109—Electrodes
- C02F2001/46133—Electrodes characterised by the material
-
- 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
- C02F2201/46—Apparatus for electrochemical processes
- C02F2201/461—Electrolysis apparatus
- C02F2201/46105—Details relating to the electrolytic devices
-
- 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
- C02F2201/46—Apparatus for electrochemical processes
- C02F2201/461—Electrolysis apparatus
- C02F2201/46105—Details relating to the electrolytic devices
- C02F2201/4616—Power supply
- C02F2201/4617—DC only
-
- 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
- C02F2201/78—Details relating to ozone treatment devices
- C02F2201/782—Ozone generators
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/02—Specific form of oxidant
- C02F2305/023—Reactive oxygen species, singlet oxygen, OH radical
Definitions
- Embodiments of the present invention relate to a water treatment apparatus, a water treatment system, and a water treatment method.
- ozone has been used for oxidative decomposition, sterilization, deodorization, and the like of organic substances in water in fields such as clean water, sewage, industrial wastewater, and pools.
- oxidation by ozone cannot be made inorganic even if it can be made hydrophilic and low molecular.
- persistent organic substances such as dioxins and 1,4-dioxane cannot be decomposed.
- OH radicals having a stronger oxidizing power than ozone.
- a method of irradiating ozone-containing water with ultraviolet rays a method of adding ozone to hydrogen peroxide-containing water, a method of irradiating hydrogen peroxide-containing water with ultraviolet rays, hydrogen peroxide, ozone, and ultraviolet rays are all used in combination.
- a method of irradiating ozone-containing water with ultraviolet rays a method of adding ozone to hydrogen peroxide-containing water, a method of irradiating hydrogen peroxide-containing water with ultraviolet rays, hydrogen peroxide, ozone, and ultraviolet rays are all used in combination.
- JP 2004-275969 A JP 2006-82081 A JP-A-10-165971
- the method using ozone and hydrogen peroxide is often used because water with low transmittance such as ultraviolet rays requires a high irradiation amount and requires energy.
- An object of the present invention is to provide a water treatment apparatus, a water treatment system, and a water treatment method.
- the water treatment apparatus can accommodate water to be treated, can be formed from a lower side by introducing the water to be treated from the upper side and being led out from the lower side, and the lower side in the reaction vessel
- the ozonized gas obtained by discharging into the raw material gas is supplied into the reaction vessel, and the aeration unit capable of forming an upward flow of the ozonized gas is disposed on the upper side of the reaction vessel.
- An electrode pair for electrolysis that generates hydrogen peroxide from oxygen gas contained in water to be treated and ozonized gas.
- FIG. 1 is a schematic configuration block diagram of a water treatment system according to the first embodiment.
- FIG. 2 is an explanatory diagram of ozone concentration, hydrogen peroxide concentration, and OH radical concentration distribution in the case of Pattern A.
- FIG. 3 is an explanatory diagram of ozone concentration, hydrogen peroxide concentration, and OH radical concentration distribution in the case of Pattern B.
- FIG. 4 is an explanatory diagram of ozone concentration, hydrogen peroxide concentration, and OH radical concentration distribution in the case of Pattern C.
- FIG. 5 is an explanatory diagram of ozone concentration, hydrogen peroxide concentration, and OH radical concentration distribution in the case of Pattern D.
- FIG. 6 is a schematic diagram of hydrogen peroxide generation in the electrode pair for electrolysis.
- FIG. 1 is a schematic configuration block diagram of a water treatment system according to the first embodiment.
- FIG. 2 is an explanatory diagram of ozone concentration, hydrogen peroxide concentration, and OH radical concentration distribution in the case of Pattern A.
- FIG. 7 is an explanatory diagram of the operation of generating OH radicals.
- FIG. 8 is an explanatory diagram of a first modification of the first embodiment.
- FIG. 9 is a schematic configuration block diagram of a water treatment apparatus according to the second embodiment.
- FIG. 10 is an explanatory diagram of the third embodiment.
- FIG. 1 is a schematic configuration block diagram of a water treatment system according to a first embodiment.
- a water supply pump 12 that supplies the water to be treated LQ that is the liquid to be treated, a reaction vessel 13 that contains the water to be treated LQ, and a water to be treated LQ in the reaction vessel 13 that is supplied via the supply pipe 14.
- an aeration unit 15 disposed at the bottom of the reaction vessel 13 and an upper portion in the reaction vessel 13 to generate hydrogen peroxide (H 2 O 2 )
- the water inlet 13A to which the water to be treated is supplied from the water supply pump 12 is disposed on the upper peripheral surface of the reaction vessel 13, and the treated water after the treatment is disposed on the lower peripheral surface of the reaction vessel 13.
- a water outlet 13B to be discharged is disposed.
- the reason why the arrangement relationship of the electrode pair for electrolysis 16, the water inlet 13A and the water outlet 13B is set to the arrangement relationship of the embodiment will be described.
- the water inlet 13 ⁇ / b> A and the electrode pair 16 for electrolysis are arranged in the upper part of the reaction vessel 13, and the water outlet 13 ⁇ / b> B is arranged in the lower part of the reaction vessel 13.
- Patterns A to A the inventors have the following four modes (patterns A to A) regarding the arrangement relationship of the electrode pair 16 for electrolysis, the water inlet 13A, and the water outlet 13B. Pattern D) was examined.
- the electrode pair 16 for electrolysis is arranged on the upper part of the reaction vessel 13 spaced from the aeration unit 15, the water inlet 13 A is arranged on the upper side of the reaction vessel 13, and the water outlet 13 B is arranged on the lower side of the reaction vessel 13. Case (this embodiment).
- the electrode pair 16 for electrolysis is arranged on the upper part of the reaction vessel 13 separated from the air diffusion unit 15, the water inlet 13A is arranged on the lower part of the reaction vessel 13, and the water outlet 13B is arranged on the upper side of the reaction vessel 13. If.
- FIG. 2 is an explanatory diagram of ozone concentration, hydrogen peroxide concentration, and OH radical concentration distribution in the case of Pattern A.
- the electrode pair 16 for electrolysis is arranged on the upper part of the reaction vessel 13 spaced from the aeration unit 15, and the water inlet 13A is arranged on the upper side of the reaction vessel 13.
- the water outlet 13B is disposed at the lower part of the reaction vessel 13.
- the hydrogen peroxide gradually increases in the vicinity of the electrode pair 16 for electrolysis from the upper side to the lower side of the reaction vessel 13, and becomes a substantially constant value at a certain position.
- the concentration of OH radicals becomes maximum near the lower part of the electrode pair 16 for electrolysis as shown in FIG. 2C, and then gradually decreases toward the lower part of the reaction vessel. Concentration distribution.
- FIG. 3 is an explanatory diagram of ozone concentration, hydrogen peroxide concentration, and OH radical concentration distribution in the case of Pattern B.
- the electrode pair 16 for electrolysis is disposed in the vicinity of the air diffusion unit 15 of the reaction vessel 13, and the water inlet 13A is disposed at the lower portion of the reaction vessel 13, The water port 13B is disposed at the top of the reaction vessel 13.
- the respective concentrations when it is assumed that ozone and hydrogen peroxide do not react are gradually increased as the distance from the aeration unit 15 increases, as shown in FIG. To increase. Further, the hydrogen peroxide gradually increases in the vicinity of the electrode pair 16 for electrolysis from the lower side to the upper side of the reaction vessel 13, and becomes a substantially constant value at a certain position.
- FIG. 4 is an explanatory diagram of ozone concentration, hydrogen peroxide concentration, and OH radical concentration distribution in the case of Pattern C.
- the electrode pair 16 for electrolysis is arranged at the upper part of the reaction vessel 13 spaced from the aeration unit 15, and the water inlet 13A is arranged at the lower part of the reaction vessel 13.
- the water outlet 13B is arranged on the upper part of the reaction vessel 13.
- the hydrogen peroxide gradually increases in the vicinity of the electrode pair 16 for electrolysis from the lower side to the upper side of the reaction vessel 13.
- FIG. 5 is an explanatory diagram of ozone concentration, hydrogen peroxide concentration, and OH radical concentration distribution in the case of Pattern D.
- the electrode pair 16 for electrolysis is arranged in the vicinity of the air diffusion unit 15 of the reaction vessel 13, and the water inlet 13A is arranged on the upper portion of the reaction vessel 13, The water port 13B is disposed at the bottom of the reaction vessel 13.
- the hydrogen peroxide decreases from the lower side to the upper side of the electrolysis electrode pair 16 and becomes almost zero near the upper end of the electrolysis electrode pair 16.
- the concentration of OH radicals becomes maximum near the lower part of the electrode pair 16 for electrolysis as shown in FIG. The concentration distribution gradually decreases.
- the reaction area of ozone gas alone becomes large, and there is a possibility that the risk of generating bromate ions, which are by-products of the ozone reaction, is increased particularly in a water treatment system. Further, there may be a problem that the cost for collecting or processing the residual ozone gas is increased.
- the region where hydrogen peroxide reacts with ozone increases, so that the OH radicals are generated in the vertical direction (vertical direction) of the reaction vessel 13.
- generated will increase and the AOP reaction area
- oxygen gas present as bubbles not oxygen dissolved in water, increases in diameter as it gets closer to the water surface due to water pressure. Therefore, when the electrolysis is performed in a region close to the water surface, the reaction area of the oxygen gas becomes large and more hydrogen peroxide is generated.
- pattern A is more electrolyzed in a region closer to the water surface, so hydrogen peroxide is more likely to be generated, and the AOP reaction region can be further increased. Therefore, in this embodiment, the arrangement relationship of the pattern A is adopted.
- the electrolysis electrode pair 16 includes a cathode (cathode) electrode 16K and an anode (anode) electrode 16A.
- FIG. 6 is a schematic diagram of hydrogen peroxide generation in the electrode pair 16 for electrolysis.
- Hydrogen peroxide (H 2 O 2 ) generation is as shown in equation (1), and oxygen gas contained in the ozonized gas OG supplied from the lower part of the reaction vessel 13 through the aeration unit 15 is used as a raw material.
- the cathode electrode 16K that is suitable for the generation of hydrogen peroxide.
- the amount of hydrogen peroxide generated increases in proportion to the current density (mA / cm 2 ) (current value with respect to the electrode and the apparent area) of the direct current when a direct current voltage is applied.
- the surface of the cathode electrode 16K be hydrophobic so that oxygen gas as a raw material of hydrogen peroxide can be easily taken into the surface.
- the surface is preferably porous (porous) so that the microscopic reaction field is widened and the reaction efficiency can be increased. Therefore, for example, a carbon electrode, which is an electrode core material, is coated with a Teflon (registered trademark) suspension (providing hydrophobicity) and conductive carbon powder (giving porous properties).
- the current efficiency when the carbon electrode is used as the cathode electrode 16K is about 20% to 50%, whereas the Teflon-based suspension and the conductive property are added to the carbon electrode.
- the current efficiency when using an electrode coated with carbon powder was 90% or more.
- the anode electrode 16A has almost no influence on the production of hydrogen peroxide, so there are not many restrictions on the material.
- the anode electrode 16A is not easily restricted by electrolysis, or hardly dissolves even if dissolved.
- a material that can easily conduct electricity is preferable.
- an insoluble metal electrode is mentioned. Specific examples include a platinum electrode and a titanium-coated electrode.
- the hydrogen peroxide generation rate when pure oxygen is supplied will be described more specifically.
- a carbon electrode in which a cathode electrode 16K is coated with a Teflon suspension and conductive carbon powder is used, and platinum is used in the anode electrode 16A.
- the current density is preferably 100 mA / cm 2 or less so as to obtain a necessary generation rate.
- the ozone generator 11 discharges the source gas to generate ozone gas O 3 .
- ozone gas O 3 and the remaining oxygen gas O 2 are collectively referred to as ozonized gas OG.
- FIG. 7 is an explanatory diagram of the operation of generating OH radicals.
- the ozone O 3 constituting the ozonized gas OG is dissolved in the treated water LQ.
- the oxygen O 2 constituting the ozonized gas OG does not dissolve in the treated water LQ so much and continues to rise as bubbles, reaches the position where the electrode pair 16 for electrolysis is disposed, and is a raw material for hydrogen peroxide. It becomes.
- the amount of hydrogen peroxide produced is proportional to the applied voltage of electrolysis, and hence the magnitude of the direct current flowing between the cathode electrode 16K and the anode electrode 16A.
- the amount of direct current is adjusted according to the component that consumes OH radicals. If the to-be-treated water LQ is supplied from the water inlet 13A by the water supply pump 12 in this state, the to-be-treated water LQ forms a downward flow DS in a state where the generated hydrogen peroxide is dissolved.
- the upward flow US of the ozonized gas OG and the downward flow DS in which hydrogen peroxide is dissolved become counterflows, so that hydrogen peroxide in the water to be treated reacts with dissolved ozone and has strong oxidizing power OH. Radicals are generated.
- a high hydrogen peroxide concentration—low ozone concentration region AR1 ⁇ an oxidation promotion region AR2 ⁇ a low hydrogen peroxide concentration—high ozone concentration region AR3 is formed in the reaction vessel 13 from the top to the bottom.
- the ozonized gas OG is injected into the lower part of the reaction vessel 13 by the aeration unit 15, so that the ozone O 3 is dissolved in the treated water LQ. Ozone treatment is performed.
- hydrogen peroxide as a reagent is not required, and surplus ozone is consumed as short-lived OH radicals by the generated hydrogen peroxide.
- surplus ozone is consumed as short-lived OH radicals by the generated hydrogen peroxide.
- the hydrogen peroxide generation efficiency is high, and the power required for hydrogen peroxide generation can be kept low.
- the hydrogen peroxide generated in the upper part of the reaction vessel 13 can be conveyed to the lower part of the reaction vessel 13 by the downward flow DS. Therefore, OH radicals can be generated in a wide range of the reaction vessel 13 to cause an oxidative decomposition reaction of a hardly decomposable substance in water, thereby improving the treatment capacity. As a result, the utilization efficiency of dissolved ozone is increased, and unreacted ozone can be reduced.
- FIG. 8 is an explanatory diagram of a first modification of the first embodiment.
- the same parts as those in FIG. As shown in FIG. 8, the reaction vessel group 13 ⁇ / b> X formed integrally is in a state where the reaction vessel 13 is connected by the communication path 18.
- the water to be treated LQ that has been subjected to the accelerated oxidation treatment and the ozone treatment is introduced from the water inlet 13A of the subsequent reaction vessel 13 through the communication path 18 and again promoted oxidation treatment. Then, the ozone treatment is performed, and it is supplied to the subsequent treatment through the water outlet 13 ⁇ / b> B and the communication path 18.
- the substance that has not been decomposed by the first treatment is also decomposed by the second treatment, and the effective treatment efficiency can be improved.
- the amount of hydrogen peroxide generated and the amount of ozonized gas OG supplied can be appropriately set as necessary.
- reaction vessels 13 in parallel at the stage closer to the raw water, and to reduce the number of parallel connections sequentially.
- two first-stage reaction vessels 13 are connected in parallel, and the second-stage reaction vessel 13 is one.
- the effective treatment efficiency can be improved by setting the number of stages of water treatment to a plurality of stages.
- FIG. 9 is a schematic configuration block diagram of a water treatment apparatus according to the second embodiment.
- the pressurized water-based gas suction / injection method is a method in which pressurized water is sent to a nozzle and the ozonized gas OG is sucked and injected into water using a pressure difference at the nozzle.
- an apparatus called a so-called injector 19 is used as the pressurized raw water LQP, which is the water to be treated LQ branched, the treated water LQ after treatment, or the clear water such as tap water. To supply.
- the ozonized gas OG is supplied from the ozone generator 11 to the injector 19.
- the injector 19 pressurizes the pressurized raw water LQP while mixing the ozonized gas OG and supplies it to the reaction vessel 13.
- the subsequent operation is substantially the same as the state in which the ozonized gas OG is supplied by the air diffusion unit in the first embodiment.
- dissolved ozone can be generated more reliably, and the processing capacity can be improved.
- FIG. 10 is an explanatory diagram of the third embodiment.
- the rectifying plate 21 has a shape in which the opening area at the lower end is large and the opening area at the upper end is narrow, and is configured to guide the upward flow US of the ozonized gas OG mainly between the cathode electrode 16K and the anode electrode 16A. Yes.
- oxygen O 2 contained in the ozonized gas OG can be efficiently guided between the cathode electrode 16K and the anode electrode 16A that generate hydrogen peroxide H 2 O 2.
- the effective hydrogen peroxide generation efficiency can be improved, and hence the generation efficiency of OH radicals can be improved, and the accelerated oxidation treatment efficiency can be improved.
- the cathode electrode constituting the electrode pair for electrolysis includes a carbon electrode core material, a porous carbon layer laminated on the electrode core material, and a hydrophobic layer formed by coating on the surface of the porous carbon layer. Therefore, the hydrogen peroxide generation efficiency is high and the required power can be kept low.
- the to-be-processed water LQ flows in from the inlet 13A (inflow part) installed in the upper part of the reaction container 13, the main flow becomes a downward direction.
- the ozone dissolution efficiency can be increased by counter-current contact with the rise of the ozonized gas OG injected into the lower portion of the reaction vessel 13.
- hydrogen peroxide generated by electrolysis near the water inlet 13A (inflow portion) comes into contact with dissolved ozone together with the downward flow of water to generate OH radicals. It is possible to oxidatively decompose the hardly-degradable substance.
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Electrochemistry (AREA)
- Water Supply & Treatment (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Life Sciences & Earth Sciences (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Inorganic Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Water Treatment By Electricity Or Magnetism (AREA)
- Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
- Oxygen, Ozone, And Oxides In General (AREA)
- Electrodes For Compound Or Non-Metal Manufacture (AREA)
Abstract
Description
OHラジカルの生成には、オゾン含有水に紫外線を照射する方法、過酸化水素含有水にオゾンを添加する方法、過酸化水素含有水に紫外線を照射する方法、過酸化水素、オゾン、紫外線全て併用する方法、が水処理において一般的に用いられている。
[1]第1実施形態
図1は、第1実施形態の水処理システムの概要構成ブロック図である。
水処理システム10は、原料ガスとしての酸素又は乾燥空気に放電し、オゾンガスを発生させ、オゾンガスを含むオゾン化ガス(=O3+O2あるいは、O3+O2+N2)を供給するオゾン発生装置11と、処理対象の液体である被処理水LQを供給する給水ポンプ12と、被処理水LQを収納する反応容器13と、反応容器13内の被処理水LQに供給配管14を介して供給されたオゾン化ガスOGをバブル状として供給するために反応容器13の底部に配置された散気ユニット15と、反応容器13内の上部に配置され、過酸化水素(H2O2)を生成するための電気分解用電極対16と、電気分解用電極対16に直流電力を供給する直流電源17と、を備えている。
図1に示したように、本実施形態においては、反応容器13の上部に入水口13A及び電気分解用電極対16を配置し、出水口13Bを反応容器13の下部に配置している。
以下、それぞれのパターンについて検討する。
パターンAの場合には、図2(a)に示すように、電気分解用電極対16を散気ユニット15から離間した反応容器13の上部に配置し、入水口13Aを反応容器13上部に配置し、出水口13Bを反応容器13下部に配置している。
この状態でオゾンと過酸化水素が反応すると、図2(c)に示すように電気分解用電極対16の下部付近でOHラジカルの濃度は最大となり、その後徐々に反応容器の下部に向かって減少するという濃度分布となる。
パターンBの場合には、図3(a)に示すように、電気分解用電極対16を反応容器13の散気ユニット15近傍に配置し、入水口13Aを反応容器13下部に配置し、出水口13Bを反応容器13上部に配置している。
また、過酸化水素は、反応容器13の下部側から上部側に向かって、電気分解用電極対16付近で徐々に増加し、ある位置でほぼ一定の値となる。
パターンCの場合には、図4(a)に示すように、電気分解用電極対16を散気ユニット15から離間した反応容器13の上部に配置し、入水口13Aを反応容器13下部に配置し、出水口13Bを反応容器13上部に配置している。
パターンDの場合には、図5(a)に示すように、電気分解用電極対16を反応容器13の散気ユニット15近傍に配置し、入水口13Aを反応容器13上部に配置し、出水口13Bを反応容器13下部に配置している。
この状態でオゾンと過酸化水素が反応すると、図5(c)に示すように電気分解用電極対16の下部付近でOHラジカルの濃度は最大となり、電気分解用電極対16の上端に向かって徐々に減少するという濃度分布となる。
さらに残存オゾンガスを回収または処理するコストが大きくなると言う問題も生じ得る。
したがって、本実施形態では、パターンAの配置関係を採用した。
上記構成において、電気分解用電極対16は、カソード(陰極)電極16Kと、アノード(陽極)電極16Aと、を備えている。
過酸化水素(H2O2)生成は、(1)式の通りとなっており、反応容器13下部から散気ユニット15を介して供給されたオゾン化ガスOGに含まれる酸素ガスが原料となる。
このときの過酸化水素の生成効率に特に影響を与えるのはカソード電極16Kの材質である。
O2+2H++2e-→H2O2 …(1)
例えば、カソード電極16Kは、直流電圧が印加されることによる直流電流の電流密度(mA/cm2)(電極と見かけ面積に対する電流値)に比例して過酸化水素生成量が大きくなる。
上記(1)式の反応が起こっている場合に、過酸化水素の理論生成量をm[g]とし、過酸化水素の分子量をM(=34)とし、カソード電極16Kとアノード電極16Aとの間を流れる直流電流をI[A]とし、反応時間をt[sec]とし、価数をz(=2)とし、ファラデー定数をF[C/mol](=9.6485×104)とすると、ファラデーの電気分解の法則より、過酸化水素の理論生成量mは、次式で現される。
m=(I・t・M)/(z・F)
そして過酸化水素の実生成量をm1とした場合、電流効率X[%]は、(2)式で表される。
X=m1/m×100 …(2)
例えば、カソード電極16Kにテフロン系懸濁液と導電性の炭素粉末をコーティングした炭素系電極を用い、アノード電極16Aには白金を用いたものとする。
なお、実際の運用にあたっては、必要な生成速度となるよう、電流密度は100mA/cm2以下とするのが好ましい。
まず、オゾン発生装置11は、原料ガスとしての酸素又は乾燥空気が供給されると、原料ガスに放電を行い、オゾンガスO3を発生させる。
オゾン発生装置11により発生されたオゾン化ガスOG(=O3+O2)は、供給配管14を介して散気ユニット15に供給され、バブル状となって被処理水LQ中に放出され、オゾン化ガスOG(=O3+O2)の上昇流USを形成する。
この状態で給水ポンプ12により被処理水LQが入水口13Aから供給されると、被処理水LQは、生成された過酸化水素が溶け込んだ状態で下降流DSを形成する。
被処理水LQの下降流DSが反応容器13下方に進むにつれて、被処理水中に溶け込んでいた過酸化水素は消費され、溶存オゾンも消費されていくこととなる。
したがって、被処理水LQ中の難分解性の水中化合成分を効率良く分解することができる。
これらの結果、残存したオゾンを処理あるいは回収する必要もなく、特に上水処理においては、臭素酸、ブロモホルム等の臭化物の生成を抑制することができる。
以上の説明においては、反応容器が一つの場合について説明したが、本第1変形例においては、反応容器が実効的に複数設けられている。
図8において、図1と同一の部分には同一の符号を付すものとする。
図8に示すように、一体に形成された反応容器群13Xは、反応容器13を連通路18でつないだ状態となっている。
この場合において、各反応容器13において、過酸化水素の発生量及びオゾン化ガスOGの供給量は、必要に応じて適宜設定することが可能である。
以上の説明においては、電気分解用電極対16は、各反応容器13に一対のみ設けていたが、反応容器13の大きさに応じて複数対を設置してもよい。これにより必要とされる過酸化水素を十分にまかなえるようになる。
以上の第1実施形態では、オゾンガスO3を被処理水LQに溶解するに際して、散気ユニット15を用いていたが、本第2実施形態は、これに代えて、インジェクタを用い、加圧水利用ガス吸引注入方式でオゾンガスを被処理水LQに溶解する場合のものである。
加圧水利用ガス吸引注入方式とは、加圧水をノズルへ送り、ノズルでの圧力差を利用してオゾン化ガスOGを吸引し水中へ注入する方式である。
そしてインジェクタ19は、加圧原水LQPにオゾン化ガスOGを混合しつつ加圧して反応容器13内に供給する。
本第2実施形態によれば、第1実施形態の効果に加えて、より確実に溶存オゾンを発生させることができ、処理能力の向上が図れる。
以上の第1実施形態及び第2実施形態においては、オゾン化ガスOGの上昇流USの流れについては何ら制御を行わないでいたが、本第3実施形態においては、オゾン化ガスOGに含まれる酸素O2を、過酸化水素を発生させるカソード電極16Kとアノード電極16Aとの間に導くために整流板を電気分解用電極対16の下方に設けた点である。
図1において、図1と同一の部分には同一の符号を付すものとする。
整流板21は、下端部の開口面積が広く、上端部の開口面積が狭い形状とされ、オゾン化ガスOGの上昇流USを主としてカソード電極16Kとアノード電極16Aとの間に導く形状とされている。
各実施形態によれば、試薬としての過酸化水素を用いることなく、簡易な構成で低コストの水処理装置、ひいては、水処理システムを構築できる。
Claims (7)
- 被処理水を収容可能で、前記被処理水が上部側から導入され、下部側から導出されることにより下降流を形成可能な反応容器と、
前記反応容器内の下部側からオゾンガス及び酸素ガスを含むオゾン化ガスを前記反応容器内に供給し、前記オゾン化ガスの上昇流を形成可能なオゾン供給部と、
前記反応容器の上部側に配置され、電気分解により前記被処理水及び前記オゾン化ガスに含まれる前記酸素ガスから過酸化水素を生成する電気分解用電極対と、
を備えた水処理装置。 - 前記電気分解用電極対を構成するカソード電極は、炭素製の電極芯材と、
前記電極芯材に積層された多孔質炭素層と、
前記多孔質炭素層の表面にコーティングにより形成された疎水層と、
を備えた請求項1記載の水処理装置。 - 前記多孔質炭素層は、導電性の炭素粉末をコーティングして積層され、
前記疎水層は、テフロン系懸濁液をコーティングして形成された、
請求項2記載の水処理装置。 - 前記オゾン供給部及び前記電気分解用電極対が配置された前記反応容器を、前段の前記反応容器から導出された前記被処理水が導入されるように複数段縦続接続された、
請求項1乃至請求項3のいずれか一項記載の水処理装置。 - 前記オゾン供給部として、散気ユニットあるいはインジェクタを用いる、
請求項1乃至請求項4のいずれか一項記載の水処理装置。 - 請求項1乃至請求項4のいずれか一項記載の水処理装置と、
酸素を含む原料ガスに放電し前記オゾン化ガスとして前記反応容器に配置された散気ユニットに供給するオゾン生成装置と、
前記電気分解用電極対に直流電力を供給する直流電源と、
を備えた水処理システム。 - 上部に入水口及び電気分解用電極対が設けられ、下部に出水口及び散気ユニットが設けられた反応容器を備えた水処理装置において実行される方法であって、
前記入水口を介して被処理水を導入して下降流を形成する過程と、
前記散気ユニットを介してオゾンガス及び酸素ガスを含むオゾン化ガスを供給してオゾン化ガスの上昇流を形成する過程と、
溶存オゾンにより前記被処理水のオゾン処理を行う過程と、
前記電気分解用電極対に直流電力を供給して前記酸素ガス及び前記被処理水から過酸化水素を生成し、前記下降流に供給する過程と、
前記下降流及び前記上昇流を向流として混合させることにより前記溶存オゾンと前記過酸化水素を反応させてOHラジカルを生成し、促進酸化処理を行う過程と、
を備えた水処理方法。
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CA3046265A CA3046265A1 (en) | 2016-11-04 | 2017-09-19 | Water treatment apparatus, water treatment system and water treatment method |
US16/344,687 US20200055754A1 (en) | 2016-11-04 | 2017-09-19 | Water treatment apparatus, water treatment system and water treatment method |
CN201780067798.3A CN109982978A (zh) | 2016-11-04 | 2017-09-19 | 水处理装置、水处理系统及水处理方法 |
AU2017354437A AU2017354437A1 (en) | 2016-11-04 | 2017-09-19 | Water treatment apparatus, water treatment system and water treatment method |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2016-216637 | 2016-11-04 | ||
JP2016216637A JP6921503B2 (ja) | 2016-11-04 | 2016-11-04 | 水処理装置、水処理システム及び水処理方法 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2018083900A1 true WO2018083900A1 (ja) | 2018-05-11 |
Family
ID=62076866
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2017/033767 WO2018083900A1 (ja) | 2016-11-04 | 2017-09-19 | 水処理装置、水処理システム及び水処理方法 |
Country Status (6)
Country | Link |
---|---|
US (1) | US20200055754A1 (ja) |
JP (1) | JP6921503B2 (ja) |
CN (1) | CN109982978A (ja) |
AU (1) | AU2017354437A1 (ja) |
CA (1) | CA3046265A1 (ja) |
WO (1) | WO2018083900A1 (ja) |
Families Citing this family (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2020136982A1 (ja) * | 2018-12-28 | 2020-07-02 | 日本碍子株式会社 | 殺菌水、殺菌水の製造方法及び殺菌済物体の製造方法 |
CN110339666A (zh) * | 2019-08-12 | 2019-10-18 | 中国科学院城市环境研究所 | 一种提升气体中臭氧生成浓度的方法 |
CN110642340B (zh) * | 2019-09-30 | 2021-06-11 | 河海大学 | 一种循环过流式电助臭氧水处理设备及利用其处理水的方法 |
KR102536400B1 (ko) * | 2022-10-13 | 2023-05-26 | 주식회사 엑세스워터 | 전기분해와 오존반응을 접목하여 toc 제거효율이 향상한 복합 페록손 기반의 고도산화처리시스템 |
SE2251224A1 (en) | 2022-10-19 | 2024-04-20 | Chemox I Umeaa Ab | Water purification involving an electro-peroxone process |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS51136355A (en) * | 1975-04-04 | 1976-11-25 | Kobe Steel Ltd | Method and apparatus for treating waste water with electrolyzed ozone |
JPS6028884A (ja) * | 1983-07-28 | 1985-02-14 | Agency Of Ind Science & Technol | 電解を含む排水の処理方法 |
JP2000084522A (ja) * | 1998-07-17 | 2000-03-28 | Mitsubishi Heavy Ind Ltd | 有害物質処理方法およびその装置 |
WO2014094399A1 (zh) * | 2012-12-17 | 2014-06-26 | Wang Yujue | 一种原位电产生 h 2 o 2 协同 o 3 氧化的废水处理装置及方法 |
Family Cites Families (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH05317870A (ja) * | 1992-05-14 | 1993-12-03 | Penta Ocean Constr Co Ltd | 水質浄化装置 |
JP2000079395A (ja) * | 1998-07-08 | 2000-03-21 | Mitsubishi Heavy Ind Ltd | 廃水処理方法 |
JP2003126861A (ja) * | 2001-10-29 | 2003-05-07 | Toshiba Corp | 水処理方法及び装置 |
-
2016
- 2016-11-04 JP JP2016216637A patent/JP6921503B2/ja active Active
-
2017
- 2017-09-19 WO PCT/JP2017/033767 patent/WO2018083900A1/ja active Application Filing
- 2017-09-19 US US16/344,687 patent/US20200055754A1/en not_active Abandoned
- 2017-09-19 CA CA3046265A patent/CA3046265A1/en not_active Abandoned
- 2017-09-19 AU AU2017354437A patent/AU2017354437A1/en not_active Abandoned
- 2017-09-19 CN CN201780067798.3A patent/CN109982978A/zh not_active Withdrawn
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS51136355A (en) * | 1975-04-04 | 1976-11-25 | Kobe Steel Ltd | Method and apparatus for treating waste water with electrolyzed ozone |
JPS6028884A (ja) * | 1983-07-28 | 1985-02-14 | Agency Of Ind Science & Technol | 電解を含む排水の処理方法 |
JP2000084522A (ja) * | 1998-07-17 | 2000-03-28 | Mitsubishi Heavy Ind Ltd | 有害物質処理方法およびその装置 |
WO2014094399A1 (zh) * | 2012-12-17 | 2014-06-26 | Wang Yujue | 一种原位电产生 h 2 o 2 协同 o 3 氧化的废水处理装置及方法 |
Also Published As
Publication number | Publication date |
---|---|
CA3046265A1 (en) | 2018-05-11 |
CN109982978A (zh) | 2019-07-05 |
JP6921503B2 (ja) | 2021-08-18 |
US20200055754A1 (en) | 2020-02-20 |
AU2017354437A1 (en) | 2019-06-20 |
JP2018069212A (ja) | 2018-05-10 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
WO2018083900A1 (ja) | 水処理装置、水処理システム及び水処理方法 | |
KR100754526B1 (ko) | 복합 산화 방식의 수처리 장치 및 그를 이용한 수처리 방법 | |
JP2009056364A (ja) | 配管型の水処理装置 | |
US20150307371A1 (en) | Electric arc for aqueous fluid treatment | |
CN104355389B (zh) | 一种去除水中难降解有机物的方法和装置 | |
KR100805378B1 (ko) | 난분해성 폐액처리를 위한 오존-전기분해/반도체촉매복합장치 및 그 사용방법 | |
JPH0290995A (ja) | 電解オゾンを使用する水処理方法及び装置 | |
KR20070057671A (ko) | 계면활성제 함유수의 처리방법 및 처리장치 | |
KR102052039B1 (ko) | 전기-페록손 반응 기반 수처리 장치 | |
JP6911002B2 (ja) | 水処理制御装置および水処理システム | |
KR20120097974A (ko) | 복합전해방식을 이용한 유기물 처리방법 및 장치 | |
JP2010188306A (ja) | ジオキサン分解方法 | |
US20210179455A1 (en) | Hydrogen peroxide water manufacturing device | |
WO2019093036A1 (ja) | 水処理システム | |
JP2006281129A (ja) | 水処理方法及び装置 | |
KR20110137223A (ko) | 미세 오존 접촉 장치와 광촉매·전극, 유체 순환 시스템에 의한 고효율 수산화 라디칼 발생기 | |
JP2001029966A (ja) | 内分泌攪乱物質又は発癌性物質を含有する有機性廃水の処理方法及び処理装置 | |
JP2019126758A (ja) | 液体処理装置 | |
KR101814871B1 (ko) | 희토류 추출 폐수 중 유기물 처리 시스템 및 이를 이용한 희토류 폐수 중 유기물 처리 방법 | |
KR20230009294A (ko) | 저온 마이크로 플라즈마 기반 오존을 이용한 스마트 loT 제어 고도 산화 공정 시스템 | |
WO2023282470A1 (ko) | 저온 마이크로 플라즈마 기반 오존을 이용한 스마트 iot 제어 고도 산화 공정 시스템 | |
WO2021192154A1 (ja) | 液体処理装置 | |
JP2011200844A (ja) | 廃水処理装置及び処理方法 | |
JP2004057887A (ja) | 電気分解と電子ビーム照射による水処理方法と装置 | |
KR20230108180A (ko) | 제어형 난분해성 공정수 고도분해 장치 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 17867419 Country of ref document: EP Kind code of ref document: A1 |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
ENP | Entry into the national phase |
Ref document number: 3046265 Country of ref document: CA |
|
ENP | Entry into the national phase |
Ref document number: 2017354437 Country of ref document: AU Date of ref document: 20170919 Kind code of ref document: A |
|
122 | Ep: pct application non-entry in european phase |
Ref document number: 17867419 Country of ref document: EP Kind code of ref document: A1 |