US3730864A - Decreasing the phenolic content of liquids by an electrochemical technique - Google Patents

Decreasing the phenolic content of liquids by an electrochemical technique Download PDF

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Publication number
US3730864A
US3730864A US00133918A US3730864DA US3730864A US 3730864 A US3730864 A US 3730864A US 00133918 A US00133918 A US 00133918A US 3730864D A US3730864D A US 3730864DA US 3730864 A US3730864 A US 3730864A
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particles
electrolyte
cell
phenolic
bed
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US00133918A
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M Tarjanyi
M Strier
H Siegerman
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Occidental Chemical Corp
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Hooker Chemical Corp
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Assigned to OCCIDENTAL CHEMICAL CORPORATION reassignment OCCIDENTAL CHEMICAL CORPORATION CHANGE OF NAME (SEE DOCUMENT FOR DETAILS). EFFECTIVE APRIL 1, 1982. Assignors: HOOKER CHEMICALS & PLASTICS CORP.
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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
    • C02F1/46—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
    • 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

Definitions

  • This invention relates to a process for treating solutions which contain phenolic materials and more particularly it relates to an improved electrochemical process for decreasing the phenolic content of a solution.
  • an object of the present invention to provide an improved process for treating solutions containing phenolic materials so as to reduce the phenolic content of such solutions.
  • a further object of the present invention is to provide an improved process for reducing the phenolic content of a solution by means of an efficient and economical electrochemical treatment.
  • the present invention includes a process for treating a solution containing phenolic materials to decrease the phenolic content thereof which comprises passing an electric current through the solution which contains the phenolic materials, which solution is contained as the electrolyte in a cell, said cell having at least one positive and one negative electrode, between which the current is passed, and wherein the electrolyte also contains a bed of particles, distributed therein such that the porosity of the bed is from about 40 to porosity being defined as Volume of particles
  • the solutions which are electrolyzed to effect the reduction in the phenolic content thereof may be various solutions which contain phenolic materials although, preferably, these are aqueous solutions. These solutions may contain varying amounts of the phenolic materials, solutions containing as much as 10% by Weight and as little as one part per million of the phenolic material being suitable for treatment in accordance with the process of the present invention to etfect a reduction of the phenolic content.
  • the phenolic material in the solutions it is intended to include not only phenol itself, i.e.
  • the solutions containing phenolic materials which are to be treated in accordance with the present method may come from various sources. Thus, for example, they may be effluent streams from industrial plants which have relatively high concentrations of the phenolic materials. Additionally, however, the solutions treated may have a relatively low concentration of phenolic materials, e.g. one part per million or less, which solutions may come from municipal or other water treating plants.
  • the method of the present invention may be used not only to reduce the relatively high content of phenolic materials in industrial and similar waste streams, but, additionally, may also be used to eifect substantially complete removal of relatively small amounts of phenolic materials, as a final purification step in the treatment of water intended for human consumption.
  • this final purification may be effected on either a large scale, e.g. at the municipal water treatiing plants, or on a smaller scale, e.g., in the homes of the ultimate water consumer.
  • these solutions may also contain various other components, in addition to the phenolic materials, such as mixed efiluent streams from several different industrial processes.
  • solutions containing, in addition to the phenolic materials, various chloride materials, such as chlorinated organics, chlorine, HCl, hypochlorites, hypochlorous acid, and the like, may be successfully treated by the process of the present invention.
  • chloride containing solutions are, however, merely exemplary of the mixed waste effiuent solutions which may be treated.
  • the pH of the solution to be treated may vary over a wide range, being either acidic, neutral or basic, pH values of from about 1 to 14 having been found to be suitable.
  • pH values on the basic side e.g. from about 8 to 14 have been found to be advantageous, with a pH range of from about 9 to 13 being particularly preferred.
  • adjustment of the pH may be done by the addition of various support electrolytes to the phenolic solution.
  • Suitable support electrolytes which may be used are aqueous solutions of borates, ammonia, sodium chloride, sulfuric acid, calcium chloride, sodium cyanide, chloroacetates, sodium hydroxide, sodium bicarbonate, hydrochloric acid, and the like.
  • the temperature of the electrolyte i.e., the solution being treated, may also vary over a wide range, the only criteria being that at the temperature used, the electrolyte remain a liquid. Thus, temperatures within the range of about to 100 degrees centrigrade have been found, generally, to be suitable. For economy in operation, however, it has frequently been found to be preferred to utilize these solutions at ambient temperatures. Similarly, the present process is desirably carried out at atmospheric pressure although either subor super atmospheric pressures may be employed, if desired.
  • the electrolyte i.e., the solution being treated
  • a suitable electrolytic cell contains a bed of particles which are distributed in the electrolyte in the cell, such that the porosity of the bed ranges from about 40 to 80%
  • volume of cell wherein the) X 100 particles are distributed By determining the density of the particles used and weighing them, the term volume of the particles in the above porosity formula may be replaced by the value for the weight of the particles divided by the true density of the particles.
  • the particle density can be measured by filling a one liter container with particles, the weight of which is known. Then, an electrolyte is added to the container to fill the voids between the particles, the amount of electrolyte needed being measured as it is added.
  • the true density of the particles, in grams per cm. is the weight of the particles in grams divided by the true volume of the particles in cm.
  • the true volume of the particles is the bulk volume minus the volume of the voids in the particle bed, the latter being the volume of the electrolyte which is added to the one liter container.
  • the true volume of the particles in this instance would be 1000 cubic centimeters minus the volume of the voids, i.e., the volume of electrolyte added to the container.
  • the porosity of the bed of particles maintained in the electrolyte which is being treated in the cell may be varied and that with different types of particles, under the same operating conditions or with similar particles under different operating conditions, changes in the bed porosity will take place.
  • the true density of the particle will vary depending upon the porosity of the particles themselves, e.g., graphite as compared to glass beads, with similar variations in den- Volume of particles sity being effected by the electrolyte itself because of the differences in the surface tension of various electrolyte solutions.
  • the particles of the bed are generally dispersed or distributed by the flow of the electrolyte through the cell, variations in the fiow characteristics will also result in changes in the bed porosity.
  • the porosity of the bed is now Volume of particles in cc.
  • the porosity of the bed has increased.
  • the porosity of the bed of particles dispersed in the electrolyte may range from about 40 to In many instances, a preferred range for the bed porosity is from about 55 to 75% with a specifically preferred range being from about 60% to 70%.
  • the particles employed to form the porous bed in the present process typically are solid, particulate materials that may be conductive, non-conductive or semi-conductive.
  • conductive it is meant that the material of which the particles are made will normally be considered an electron-conducting material.
  • the particles may have a metallic surface, either by virtue of the particles themselves being metallic or by being made of non-conductive material on which a metallic surface has been deposited.
  • Typical of the metals which may be employed are the metals of Group VIII of the Periodic Table, such as ruthenium and platinum, as well as other conductive elements, such as graphite, copper, silver, zinc, and the like.
  • the conductive particles may be electrically conductive metal compounds, such as ferrophosphorus, the carbides, borides or nitrides of various metals such as tantalum, titanium, and zirconium, or they may be various electrically conductive metal oxides, such as lead dioxide, ruthenium dioxide, and the like.
  • the particles may be made of various materials, such as glass, Teflon coated glass, polystyrene spheres, sand, various plastic spheres and chips, and the like.
  • Exemplary of various semi-conductive materials of which the particles may be made are fly ash, oxidized ferrophos, zirconia, alumina, conductive glasses, and the like.
  • the particles used desirably range in size from about 5 to 5000 microns, with particle sizes of from about 50 to 2000 microns being preferred. In many instances, a particularly preferred range of particle sizes has been found to be from about to 800 microns. Although it is not essential to the successful operation of the process of the present invention that all of the particles in the porous bed distributed in the electrolyte have the same size, for the most preferred operation of the process, it has been found to be desirable if the range of particle sizes is maintained as small as is practical.
  • the density of the particles used should be such, that in conjunction with the size and shape of the particles, it will provide the proper balance between the drag force created by the electrolyte motion and the buoyancy and gravitational forces required to achieve particle dispersion or distribution at the desired bed porosity.
  • the particle densities typically may range from about 0.1 (less than the density of the electrolyte) to about 1.0 gram per cc.
  • the particle densities typically may range from about 1.1 to grams per cc. and preferably from about 1.5 to 3.5 grams per cc.
  • the most preferred operating conditions have been found to be when the particles are dispersed throughout the electrolyte, Within the cell, during the movement of the electrolyte and when the particles are more dense than the electrolyte.
  • the electrolytic cell may be of any suitable material and configuratioln which will permit electrolysis of the phenolic containing solution to effect a reduction in its phenolic content and which will permit retention of the porous bed of particles in the electrolyte, within the cell.
  • suitable materials of construction which may be used for the cell are various plastics, such as the polyacrylates, polymethacrylates, polytetrahaloethylenes, polypropylenes, and the like, rubber, as well as materials conventionally used in the construction of chlor-alkali cells such as concretes.
  • the cells may be made of metal, such as iron or steel. In such instances, electrically insulating coatings should be provided on the metal surfaces in the cell interior or electrical insulation provided between the metal of the cell and the electrodes.
  • the size of the electrolytic cell may also vary widely, depending upon the nature and quantity of the phenolic containing solution which is to be treated.
  • the cell may be relatively large and include a multiplicity of treating zones, whereas for the treatment of water for individual home use, appreciably smaller units may be utilized, similar in size to conventional soft-water treating units.
  • the cell may be of a suitable size so as to be portable, for use at camp sites, and the like.
  • the cell will have a suitable inlet and outlet means for introducing and removing the solutio n to be treated, means for retaining the porous bed of particles dispersed in the electrolyte within the cell and means for supporting at least one positive and one negative electrode in contact with the electrolyte in which the porous bed of particles is distributed.
  • the electrolytic cell has within it at least one positive and one negative electrode. These are disposed within the cell so as to be in contact with the electrolyte in which is distributed the porous bed of particulate material. These electrodes may be formed of various materials, as are known to those in the art.
  • Suitable electrode materials which may be used are graphite; noble metals and their alloys, such as platinum, iridium, ruthenium dioxide, and the like, both as such and as deposits on a base metal such as titanium, tantalum, and the like; conductive compounds such as lead dioxide, manganese di oxide, and the like; metals, such as cobalt, nickel, copper, tu ngsten bronzes, and the like; and refractory metal compounds, such as the nitrides and borides of tantalum, titanium, zirconium, and the like.
  • the positive and negative electrodes will be positioned within the electrolytic cell so as to be separated sufliciently to permit the flow of the electrolyte through the cell and the movement of the particle within the electrolyte. It will be appreciated, of course, that as the separation between the electrodes is increased, the voltage necessary to effect the desired reduction in the phenolic content of the electrolyte will also increase. Accordingly, in many instances it has been found to be desirable if the separation between the positive and negative electrode in the cell is from about 0.1 to 5.0 centimeters, with a separation of from about 0.3 to about 3.0 centimeters being preferred and a separation of from about 0.5 to 2.0 centimeters being particularly preferred. Although particular reference has been made to an electrolytic cell having one positive and one negative electrode, it will be appreciated that the cell may be provided with a plurality of electrode pairs,
  • the flow of the electrolyte through the electrode area will also be dependent upon the size and density of the particles which are distributed in the electrolyte to form the porous bed.
  • this flow which is described in terms of the linear flow velocity of the electrolyte, will be within the range of from about 0.1 to 1000 centimeters per second.
  • a preferred electrolyte flow velocity has been found to be from about 0.5 to centimeters per second with a flow velocity of from about 1 to 10 centimeters per second being specifically preferred. Under these operating conditions, current densities within the range of about 1.0 to 500 milliamps per square inch have been found to be typical of those which are utilized.
  • this system includes an electrolytic cell 1 having a fluid inlet 6 and a fluid outlet 9. Within the cell 1 are disposed a positive electrode 2 and a negative, electrode 3. Although these electrodes are shown as being separated by a diaphragm 4, in many instances, the use of such a diaphragm has not been found to be necessary. Where such a diaphragm is used, e.g., to control the particles in the anolyte or catholyte compartments, the diaphragm may be formed of various materials, such as a Teflon coated screen.
  • An electrolyte 8 is provided within the cell, which electrolyte is a solution containing phenolic material.
  • a source 5 of this electrolyte is provided, from which the electrolytes may be introduced into the cell through the inlet 6.
  • Distributed within the electrolyte 8 are particles 7, which particles are distributed randomly through the electrolyte, the nature of the distribution depending upon the electrolyte flow, size and density of the particles, density of the electrolyte, and the like.
  • the electrolyte 8 is pumped into the cell 1 through the inlet 6 from the electrolyte source 5 and exits from the cell through the outlet 9 for recirculation through line 12 or for subsequent processing through line 13, as is desired.
  • the cell is further provided with screens 10 and 11, screen 11 serving to support the particles in the cell and screen 10 serving to maintain the particles within the cell and prevent their discharge through the outlet 9.
  • screens 10 and 11 serving to support the particles in the cell
  • screen 10 serving to maintain the particles within the cell and prevent their discharge through the outlet 9.
  • the distance between the screens 10 and 11 is changed, the volume of that portion of the cell in which the particles are distributed will likewise vary, thus, varying the porosity of the bed of particles which is maintained within the cell.
  • the use of particles in an electrolytic cell in the manner which has been described has been found to have the following advantages.
  • a conventional electrolytic cell such as a chlor-allkali cell
  • the amount of electrode surface at which the electrolytic reaction is conducted is dependent upon the surface area of the electrodes. Typically, this surface area will be about 1.3 time 10 cm. With a typical cell volume of about 3.5 times 10 cm. the resulting ratio of the electrode area per cell volume is about 0.037 cm. /cm.
  • Example 7 The procedure of Example 7 was repeated with the exception that the phenol-containing solution was an organic efiluent containing 2,4,5-trichlorophenol and having an initial phenol content of 3.0 parts/million.
  • the trolyte flow a the Pamela t denshty and type and particles were graphite, having a size of about 177 mithe concentration of the phenolic material.
  • the phenol solution mllhon was circulated through apparatus similar to that shown EXAMPLE in the drawing for 15 minutes to allow for equilibration.
  • the procgdu -e f Example .5 was repeated with the A 5o'mllhhtel" Sample was then Withdrawn and h y exception that the particles used were glass beads having for Ph content-
  • the analyses Showed substahtlally a particle size of 500 microns.
  • the support electrolyte h h Q l Phenol content of 1000 Parts was a 0.3 M NaCl solution, added in an amount to make PF mllhoh, lhdlcatlhg httle it y absorptloh 011 the p the solution pH 4.65.
  • the solution was electrolyzed for trcles or electrodes in the cell.
  • the phenol solution was 11 hours at a current f 1,0 amp d an average l then electrolyzed under the conditions indicated in the age of 336 volts, using a fl t which provided a bed following table.
  • the electrolyte was then drained from porosity f 5% At h end f this time, the phenol the apparatus and agam analyzed for phenol Content All content of the solution was found to be reduced from Phenol analyses were done y gas Chromatographic techthe initial 1000 parts/million to 0.52 part/million. nique.
  • the olf gases from the cell were collected by the l downward displacement of water and carbon dioxide was EXAMPLE 11 measured by infrared analysis.
  • EXAMPLE 11 measured by infrared analysis.
  • the procedure of Example 10 was repeated with the was no diaphragm used in the cell, the particles were exception that the phenol content of the solution treated graph1te, having a particle size of from 596840 microns, was 1145 parts/ million.
  • the electrolysis was effected for the anode was graph1te, the cathode was nickel and the a period of 19.5 hours at a. current of 1 amp, a voltage separation between the anode and cathode was 0.5 centiof 4.855.4 volts and an anode separation of 0.65 centimeter.
  • the electrolyte fiow rate was adjusted during the meter.
  • the solution flow rate was such as to establish electrolysis so as to have a porosity of the bed of graphite a bed porosity of At the end of this time, the phe- 45 particles of from 63-74%. Additionally, various supnol concentration was found to be 0.002 part/million. port electrolyte solutions were added to the phenol solu- While there have been described various embodiments tion to adjust the pH to the values shown.
  • the g $1 3 anode in the cell was graphite, the cathode was nickel 1 Z Is i a th h u f and the space between them was 2.1 cm.
  • the flow rate 1 me for ecfeasmg P c cofltent o a of the solution was adjusted so as to provide a porosity so which. compnsfasl Passlng l f in the bed of particles of 65%.
  • electrolyte algg contains a bed of particles, dlstrlubbed therein such that the porosity of the bed is from about 40 to 80%, porosity being defined as Volume of particles 2.
  • the method as claimed in claim 12 wherein the porosity of the bed of particles is from about to 14.
  • the method as claimed in claim 1 wherein the separation between the positive and negative electrode within the cell is from about 0.1 to 5.0 centimeters.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Chemistry (AREA)
  • Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
  • Water Treatment By Electricity Or Magnetism (AREA)
US00133918A 1971-04-14 1971-04-14 Decreasing the phenolic content of liquids by an electrochemical technique Expired - Lifetime US3730864A (en)

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BE (1) BE782071A (OSRAM)
DE (1) DE2218121A1 (OSRAM)
FR (1) FR2133734A1 (OSRAM)
GB (1) GB1335941A (OSRAM)
IT (1) IT953305B (OSRAM)
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Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2437273A1 (de) * 1973-08-03 1975-02-20 Parel Sa Elektrochemisches verfahren
DE2618864A1 (de) * 1975-04-30 1976-11-11 Westinghouse Electric Corp Verfahren zur beseitigung von verunreinigungen aus wasser und geraet zur ausfuehrung des verfahrens
JPS52103850A (OSRAM) * 1976-02-06 1977-08-31 Ontario Ltd 308489
US4072596A (en) * 1975-04-30 1978-02-07 Westinghouse Electric Corporation Apparatus for removal of contaminants from water
US4118295A (en) * 1976-04-20 1978-10-03 Dart Industries Inc. Regeneration of plastic etchants
US4119506A (en) * 1973-04-12 1978-10-10 George Charles Bashforth Fuels
US4125445A (en) * 1977-05-20 1978-11-14 Hercules Incorporated Electroreduction of nitrate esters
US4260484A (en) * 1979-03-29 1981-04-07 Standard Oil Company (Indiana) Process for renewing the adsorptive capacity of a bed of active carbon
EP0052907A1 (en) * 1980-11-25 1982-06-02 Nederlandse Organisatie voor toegepast-natuurwetenschappelijk onderzoek TNO Process for the detoxification of chemical waste materials
US4337125A (en) * 1980-12-08 1982-06-29 Stauffer Chemical Company Electrochemical synthesis of organophosphorus compounds from the element
US4338166A (en) * 1980-12-08 1982-07-06 Stauffer Chemical Company Electrochemical synthesis of organophosphorus compounds
US4351734A (en) * 1977-05-02 1982-09-28 Ametek, Inc. Spark cell ozone generator
US5662789A (en) * 1995-03-03 1997-09-02 National Research Council Of Canada Removal of organics from aqueous solutions
CN106064962A (zh) * 2016-06-03 2016-11-02 浙江科技学院 利用污泥和粉煤灰制备催化粒子电极的方法及应用
EP3257818A1 (en) * 2016-06-15 2017-12-20 Aquatec, Proyectos Para El Sector Del Agua, S.A.U. A method and system for electrochemically purifying water

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JPS6450998A (en) * 1987-08-21 1989-02-27 Power Reactor & Nuclear Fuel Electrolysis treating method of radioactive waste liquid
SE466196B (sv) * 1989-06-13 1992-01-13 Pavel Voracek Foerfarande och anordning foer elektrisk behandling av en elektrolytisk loesning samt loesningsfraktioner framstaellda enligt foerfarandet
GB2253860B (en) * 1991-03-12 1995-10-11 Kirk And Charashvili Internati The electrochemical treatment of water and a device for electrochemically treating water
US5705050A (en) * 1996-04-29 1998-01-06 Sampson; Richard L. Electrolytic process and apparatus for the controlled oxidation and reduction of inorganic and organic species in aqueous solutions
US5419816A (en) * 1993-10-27 1995-05-30 Halox Technologies Corporation Electrolytic process and apparatus for the controlled oxidation of inorganic and organic species in aqueous solutions
DE202009013771U1 (de) 2009-10-02 2010-07-22 Hidde, Axel R., Dr. System- oder Rohrtrenner in Modulbauweise als Patrone
CN110004403B (zh) * 2019-04-23 2020-10-09 永济市汇越新材料工程技术有限公司 一种稀土改性多元复合盐浴离子渗处理工件的改性工业化方法

Cited By (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4119506A (en) * 1973-04-12 1978-10-10 George Charles Bashforth Fuels
DE2437273A1 (de) * 1973-08-03 1975-02-20 Parel Sa Elektrochemisches verfahren
US3981787A (en) * 1973-08-03 1976-09-21 Parel Societe Anonyme Electrochemical circulating bed cell
DE2618864A1 (de) * 1975-04-30 1976-11-11 Westinghouse Electric Corp Verfahren zur beseitigung von verunreinigungen aus wasser und geraet zur ausfuehrung des verfahrens
US4072596A (en) * 1975-04-30 1978-02-07 Westinghouse Electric Corporation Apparatus for removal of contaminants from water
JPS52103850A (OSRAM) * 1976-02-06 1977-08-31 Ontario Ltd 308489
US4118295A (en) * 1976-04-20 1978-10-03 Dart Industries Inc. Regeneration of plastic etchants
US4351734A (en) * 1977-05-02 1982-09-28 Ametek, Inc. Spark cell ozone generator
US4125445A (en) * 1977-05-20 1978-11-14 Hercules Incorporated Electroreduction of nitrate esters
US4260484A (en) * 1979-03-29 1981-04-07 Standard Oil Company (Indiana) Process for renewing the adsorptive capacity of a bed of active carbon
EP0052907A1 (en) * 1980-11-25 1982-06-02 Nederlandse Organisatie voor toegepast-natuurwetenschappelijk onderzoek TNO Process for the detoxification of chemical waste materials
US4337125A (en) * 1980-12-08 1982-06-29 Stauffer Chemical Company Electrochemical synthesis of organophosphorus compounds from the element
US4338166A (en) * 1980-12-08 1982-07-06 Stauffer Chemical Company Electrochemical synthesis of organophosphorus compounds
US5662789A (en) * 1995-03-03 1997-09-02 National Research Council Of Canada Removal of organics from aqueous solutions
CN106064962A (zh) * 2016-06-03 2016-11-02 浙江科技学院 利用污泥和粉煤灰制备催化粒子电极的方法及应用
CN106064962B (zh) * 2016-06-03 2018-07-20 浙江科技学院 利用污泥和粉煤灰制备催化粒子电极的方法及应用
EP3257818A1 (en) * 2016-06-15 2017-12-20 Aquatec, Proyectos Para El Sector Del Agua, S.A.U. A method and system for electrochemically purifying water
WO2017216116A1 (en) * 2016-06-15 2017-12-21 Aquatec, Proyectos Para El Sector Del Agua, S.A.U. A method, a system and a reactor for electrochemically purifying water

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IT953305B (it) 1973-08-10
NL7205016A (OSRAM) 1972-10-17
BE782071A (fr) 1972-10-13
FR2133734A1 (OSRAM) 1972-12-01
GB1335941A (en) 1973-10-31
DE2218121A1 (de) 1972-10-26

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