WO2010064946A1 - Электрохимическая модульная ячейка для обработки растворов электролитов - Google Patents
Электрохимическая модульная ячейка для обработки растворов электролитов Download PDFInfo
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- WO2010064946A1 WO2010064946A1 PCT/RU2008/000740 RU2008000740W WO2010064946A1 WO 2010064946 A1 WO2010064946 A1 WO 2010064946A1 RU 2008000740 W RU2008000740 W RU 2008000740W WO 2010064946 A1 WO2010064946 A1 WO 2010064946A1
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- Prior art keywords
- anode
- cell
- diaphragm
- cathode
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- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
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- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
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- 229910052810 boron oxide Inorganic materials 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- VTYYLEPIZMXCLO-UHFFFAOYSA-L calcium carbonate Substances [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 1
- 235000010216 calcium carbonate Nutrition 0.000 description 1
- 239000001506 calcium phosphate Substances 0.000 description 1
- 229910000389 calcium phosphate Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-N carbonic acid Chemical class OC(O)=O BVKZGUZCCUSVTD-UHFFFAOYSA-N 0.000 description 1
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- JKWMSGQKBLHBQQ-UHFFFAOYSA-N diboron trioxide Chemical compound O=BOB=O JKWMSGQKBLHBQQ-UHFFFAOYSA-N 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- HTXDPTMKBJXEOW-UHFFFAOYSA-N dioxoiridium Chemical compound O=[Ir]=O HTXDPTMKBJXEOW-UHFFFAOYSA-N 0.000 description 1
- UDYLZILYVRMCJW-UHFFFAOYSA-L disodium;oxido carbonate Chemical class [Na+].[Na+].[O-]OC([O-])=O UDYLZILYVRMCJW-UHFFFAOYSA-L 0.000 description 1
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- WQYVRQLZKVEZGA-UHFFFAOYSA-N hypochlorite Chemical compound Cl[O-] WQYVRQLZKVEZGA-UHFFFAOYSA-N 0.000 description 1
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- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 230000002427 irreversible effect Effects 0.000 description 1
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- ZLNQQNXFFQJAID-UHFFFAOYSA-L magnesium carbonate Chemical class [Mg+2].[O-]C([O-])=O ZLNQQNXFFQJAID-UHFFFAOYSA-L 0.000 description 1
- 239000001095 magnesium carbonate Substances 0.000 description 1
- 235000011160 magnesium carbonates Nutrition 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
- 229910001510 metal chloride Inorganic materials 0.000 description 1
- 150000004692 metal hydroxides Chemical class 0.000 description 1
- 229910001960 metal nitrate Inorganic materials 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 229960000907 methylthioninium chloride Drugs 0.000 description 1
- 229910017464 nitrogen compound Inorganic materials 0.000 description 1
- 150000002830 nitrogen compounds Chemical class 0.000 description 1
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- QVYRGXJJSLMXQH-UHFFFAOYSA-N orphenadrine Chemical compound C=1C=CC=C(C)C=1C(OCCN(C)C)C1=CC=CC=C1 QVYRGXJJSLMXQH-UHFFFAOYSA-N 0.000 description 1
- 239000011224 oxide ceramic Substances 0.000 description 1
- 150000002927 oxygen compounds Chemical class 0.000 description 1
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- 239000011591 potassium Substances 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 235000010333 potassium nitrate Nutrition 0.000 description 1
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Inorganic materials [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
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- MWNQXXOSWHCCOZ-UHFFFAOYSA-L sodium;oxido carbonate Chemical compound [Na+].[O-]OC([O-])=O MWNQXXOSWHCCOZ-UHFFFAOYSA-L 0.000 description 1
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Classifications
-
- 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
- C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
- C25B9/17—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof
- C25B9/19—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof with diaphragms
-
- 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
-
- 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
- C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
- C25B9/17—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof
Definitions
- the invention relates to the field of chemical technology, in particular to devices for the electrochemical processing of electrolyte solutions and can be used in the processes of electrochemical production of various chemical products by electrolysis of electrolyte solutions of io various concentrations, including in processes associated with electrochemical regulation of acid-base, redox properties and catalytic activity of dilute aqueous solutions of electrolytes, the concentration of which is predominant significantly in the range of 0.001 - 0.1 mol / l, as well as other liquids with low
- cylindrical electrolyzers with a diaphragm have relatively low performance characteristics, and are significantly inferior in performance indicators to electrolyzers with bulk or fluidized electrodes [see, for example, Fyoshin M. Ya., Smirnova
- the technical result achieved by using the present invention is to enable the intensification of electrolysis processes in a cylindrical diaphragm cell by improving the design of the cell and choosing the optimal ratio of the sizes of the main elements - electrodes and zo diaphragm.
- This result is enhanced by the use of a diaphragm and electrodes with a different ratio of the areas of geometric (apparent) and true (physical) surfaces, as well as through the use of a diaphragm made of materials in the cell, the combination of which gives the porous-capillary structure of the diaphragm high electroosmotic activity.
- the technical result achieved is the expansion of the functionality of the cell in the processing of electrolyte solutions with different chemical composition and concentration.
- the specified technical result is achieved by the fact that in a cylindrical electrochemical cell for processing solutions containing an inner tubular anode, an outer cylindrical cathode and a permeable tubular ceramic diaphragm located between them, separating the interelectrode space into the anode and cathode chambers, nodes for installing, attaching and sealing the electrodes and diaphragms placed on the end parts of the cell, and devices for supplying and removing processed solutions to and from the electrode chambers, cathode, anode and the diaphragm is installed in nodes and connected to devices for supplying and draining the solution with the formation of the working part of the cell, along the entire length of which the hydrodynamic characteristics of the electrode chambers and the characteristics of the electric field are constant.
- the cathode and anode are made of titanium tubes, while the ratio of the cross-sectional area of the cathode chamber to the sum of the cross-sectional areas of the anode chamber and the diaphragm is 0.9-1, 0, and the length of the working part of the cell is 15-25 of the outer diameters of the anode.
- the anode can be made of a titanium tube with a developed outer surface on which an electrocatalytic coating is applied, and the ratio of the true (physical) surface area of the anode to the true surface area of the cathode is equal to or greater than unity.
- the cell diaphragm is made capillary-porous, electroosmotically active and the external true surface of the diaphragm is equal to or less than the true surface of the cathode, and the internal true surface of the diaphragm is equal to or less than the true surface of the anode, but smaller than the true external surface of the diaphragm.
- the product of the interelectrode distance by the quotient of dividing the sum of the true surfaces of the anode and cathode by the total volume of the electrode chambers is 3.9 - 4.1.
- the ceramic diaphragm is made of alumina grains surrounded by particles of zirconia partially stabilized by oxides of rare or rare earth metals and has the following composition - oxide aluminum - 60 - 90% weight, with at least 98% of the phase composition of alumina in alpha form, zirconia - 10 - 40% weight, while at least 98% of the phase composition of zirconia in tetragonal modification.
- additives are used - one or more, of oxides selected from the group consisting of yttrium, scandium, ytterbium, cerium, gadolinium oxides, in a total amount of 1, 0 - 10.0% by weight.
- the attachment points of the electrodes and the diaphragm can be made in the form of one or more parts of dielectric material each, and the devices for supplying and discharging the treated solution to and from the electrode chambers are made in the form of channels and nozzles combined with the parts of the nodes.
- the anode cavity can be equipped with devices for supplying and removing coolant.
- the cell can be made in such a way that the attachment points of the electrodes and the diaphragm are made in the form of one or more parts of dielectric material each, the devices for supplying and / or removing the treated solution to and from the cathode chamber are made in the form of channels and nozzles combined with the parts of the nodes and the devices for supplying and discharging the treated solution to and from the anode chamber are made in the form of nozzles connected to the inner cavity of the anode and installed at its ends, while in the end parts of the anode you holes are filled.
- the attachment points of the electrodes and the diaphragm in the cell can be made in the form of one or more parts of dielectric material each, devices for supplying and discharging the treated solution to and from the cathode chamber are made in the form of holes and nozzles located at the end sections of the cathode, and devices for feeding and drainage of the treated solution to and from the anode chamber is made in the form of nozzles connected to the inner cavity of the anode and installed on its ends, while in the end parts of the anode there are holes and I.
- additional holes can be made evenly spaced along its length along the entire length of the working part of the cell.
- the cathode, anode and diaphragm are installed in the nodes with the formation of the working part of the cell (see Fig. 1), along the entire length of which the constancy of the hydrodynamic, thermophysical and electrophysical characteristics of the electrode chambers is preserved (the given surface roughness, 5 forming the walls of the electrode chambers, are the same radial distances between the cylindrical surfaces of the electrodes and the diaphragm in all cross sections of the working part of the cell, the same thickness of the diaphragm, anode and cathode titanium pipes along the entire length of the working part cell, the same electric field strength in the body of the io diaphragm, the same electrical resistance between the electrodes in any cross section of the working part of the cell), allows to intensify the process of electrochemical exposure due to the uniform, with the same longitudinal speed at all points of the cross section of the electrode chambers, moving processed
- 25 electrolyzers are usually accompanied by the accumulation in them of an increased number of products of electrochemical reactions having a higher electrical conductivity than the initial electrolyte solution. Due to the formation of inhomogeneity of the conducting medium, the redistribution of electric field lines takes place, which is accompanied by local temperature fluctuations, which, in turn, enhance the action of other factors causing the flow heterogeneity. Self-sustaining and self-developing thermophysical, electrochemical and hydrodynamic fluctuations in the working chambers of electrochemical systems lead to unproductive energy consumption and reduce the efficiency of the processes of electrochemical conversion of liquids.
- the implementation of the anode and cathode of the electrochemical cell in the form of titanium tubes with low thermal inertia avoids the occurrence and development of longitudinal (along the cell axis) thermal 5 interference moving in the electrode chambers of the cell displacement fronts of the gas-liquid medium.
- the established hydraulic mode in the chambers of the working part of the cell is ensured when the points of entry and exit of the electrolyte solution into and out of the chamber are located at a distance equal to or greater than the width of the electrode chamber into which it is introduced and from which the electrolyte solution is discharged.
- the ratio of the cross-sectional area of the cell cathode chamber to the sum of the cross-sectional areas of the anode chamber and the diaphragm should be 0.8 - 1, 0, and the length of the working part of the cell should be 15-25 outer diameters of the anode. It is in this range of relationship values
- the effect of the emergence and stable existence of microtoroid flows ensures effective mixing of the starting materials and reaction products in each section of the working part of the cell during the movement of the gas-liquid medium.
- the effect of the emergence and existence of microtoroidal flows caused by the above ratio, allows us to consider the volume of the gas-liquid mixture located between any two arbitrarily close cross sections as a toroidal microreactor of ideal mixing.
- the fulfillment of this ratio contributes to the intensification of the most important processes - hydrodynamic, which include the supply of starting materials to the electrode and the removal of products of electrochemical reactions from the electrode, as well as the processes of removing 5 electrolysis gases from the interelectrode space.
- a decrease or increase in this ratio can be achieved by changing the cross-sectional area of the cathode chamber and the cross-sectional area of the anode chamber.
- a change in the ratio leads to a disruption of the microtoroid structure of the flows in the electrode chambers, io a decrease in the mass transfer rate and, consequently, a decrease in the efficiency of electrochemical processes.
- An increase in the diaphragm cross section with a constant cross section of the electrode chambers leads to an increase in the electric and hydraulic resistance of the diaphragm, which also leads to a decrease in the efficiency of the process. Section reduction
- the 20 of the working part of the cell should not be more than 25D 2 and less than 15D 2 , where D 2 is the outer diameter of the anode.
- D 2 is the outer diameter of the anode.
- the anode can be made of a titanium tube with a developed outer surface on which an electrocatalytic coating is applied
- the cathode can be made of a titanium tube with an inner surface smoother than the surface of the anode, which is achieved by treating the working surfaces of the electrodes using any of the known methods, such like sandblasting, electrochemical etching, chemical etching, polishing, electro polishing, grinding and etc .. This allows you to adjust the ratio of the true (physical, working, active) surfaces of the anode and cathode along the entire length of the working part of the cell.
- This ratio should be equal to or greater than unity, despite the fact that the apparent (geometric) surface of the anode, as follows from the design, 5 is less than the geometric surface of the cathode - since the outer diameter of the anode is smaller than the inner diameter of the cathode.
- the developed physical surface of the anode allows to reduce the effective density of the anode current and thereby increase the service life of the anode electrocatalytic coating by several times.
- the developed surface io of the anode due to the large number of microgeometric protrusions and depressions, the size of which does not exceed 10 ⁇ m, allows you to create microelectrocatalytic sections that differ in the magnitude of the electrode potential (see Fig. 2). On the protrusions, due to the higher current density of micro scattering, the oxidation potential is higher,
- the developed surface of the anode allows anodic oxidation to be carried out with minimal anodic polarization, which ensures a reduction in heat loss.
- the small geometric surface of the anode in comparison with the large geometric surface of the cathode, forms a radial distribution of electric field lines that are condensed to the center and provide an accelerated supply of the starting materials to the surface of the anode at the distance of the electric field of the diffuse part of the DES, i.e. 10 "5 ... 10 " 4 centimeters, as well as accelerated removal of products of electrochemical reactions from the field of action of the diffuse part of the DES to the volume of the solution.
- the relatively smooth surface of the cathode provides the formation of small hydrogen bubbles and, due to the uniform structure of titanium in the 5 surface and near-surface layers, reduces the rate of dissolution of hydrogen in the metal (hydrogenation process).
- the diaphragm must be capillary porous, have high electroosmotic activity and have a different degree of microroughness on the surfaces facing the cathode and anode.
- the inner and outer surfaces of the diaphragm are made with a given, different, roughness, namely, the outer true or physical surface of the diaphragm must be equal to or smaller than the true surface of the cathode, and the inner true surface of the diaphragm must be equal to or smaller
- the true surface of the diaphragm facing the anode is smaller than its true surface, which facilitates the control of the electromigration transfer of ions from the anode chamber to the cathode due to the increased concentration of cations in the surface layer of the diaphragm.
- the observed decrease in the intensity of electromigration the transfer of hydroxonium ions is very useful and occurs as a result of suppression of the prototropic mechanism of migration of hydroxonium ions in the concentration polarization region on the filter surface of the diaphragm.
- the predominant electromigration transfer of metal cations occurs, which, in contrast to hydroxonium ions, has larger hydrate shells, which is significantly accelerated due to the electroosmotic transfer of water from the anode chamber to the cathode.
- the electroosmotic activity of the diaphragm decreases, but remains higher in comparison with ceramic diaphragms made of aluminum oxide, boron oxide, zirconium oxide, asbestos.
- the product of the value of the inter-electrode distance of the cell by the quotient of dividing the sum of the true surfaces of the anode and cathode by the total volume of electrode chambers should be 3.9 - 4.1 for electrolyte solutions of various concentrations, which can conditionally be
- FIG. Figure 4 shows the dependence of zo (1) of the electrical conductivity of aqueous solutions of various inorganic electrolytes - chlorides, sulfates, carbonates, nitrates of alkali metals, corresponding acids and bases, on their concentration in an aqueous solution.
- Dependence 2 characterizes the theoretically calculated distances between the centers of electrolyte ions in a solution also in depending on the concentration.
- a lower value of the aforementioned ratio (3.9) refers to cells for processing solutions with a concentration of less than 0.1 mol / l
- a larger value (4.1) refers to cells for processing solutions with a concentration of more than 0.1 mol / l
- a decrease or increase in this ratio causes an increase in energy consumption for the electrolysis process and a decrease
- the ceramic diaphragm of the cell is made of alumina grains with a specific surface area of 1-4 m 2 / g, surrounded by particles of alumina oxide with a specific surface area of 10-40 m 2 / g, with the content of aluminum particles with a specific surface area of 1-4 m 2 / g 70 -90% weight, while at least 99% of the phase composition of aluminum oxides are in alpha form.
- the cell diaphragm can also be made of alumina grains with a specific surface of 1-4 m 2 / g surrounded by a mixture of titanium oxide particles and magnesium oxide, with an alumina particle content of at least 99% by weight, with at least 99% of the phase composition of the alumina particles being in alpha form.
- the ceramic diaphragm can be made of grains of aluminum oxide 5 with a specific surface area of 1-4 m 2 / g, surrounded by particles of zirconium dioxide, partially stabilized by oxides of rare or rare earth metals and has the following composition - aluminum oxide - 60 - 90% weight, while not less than 98% of the phase composition of alumina is in alpha form, zirconia is 10 to 40% by weight, while at least 98% of the phase composition of zirconia is in tetragonal modification.
- an additive is used - one or more oxides selected from the group consisting of yttrium, scandium, ytterbium, cerium, gadolinium oxides. The total amount of oxides is 1, 0 - 10.0% by weight.
- the electrochemical cell can be used as an electrochemical reactor with an ion-selective electroosmotically active diaphragm, providing selective ion transfer through the diaphragm
- the magnitude and direction of transfer is determined by the strength (density) of the current, the electric field strength in the diaphragm and the mineralization of aqueous solutions on both sides of it.
- the electrical resistance of the diaphragm with fully formed adsorption layers on its inner and outer surfaces is less than the resistance of the electrolyte filling the pores, and the ion mobility in the pores is higher than the ion mobility in a pure solution.
- the stationary equilibrium between the field strength in the diaphragm, due to the presence of adsorption layers of charged particles, is dynamic.
- diaphragms make it possible to provide a modular electrochemical cell with the ability to work with the same efficiency in both laboratory and industrial conditions, as well as the ability to treat both diluted aqueous 5 electrolyte solutions and concentrated water-salt solutions, moreover, the properties of the diaphragm (its physical - chemical composition and filtration ability) allow you to work in the mode when a concentrated electrolyte solution flows through one of the electrode chambers, and in the other form tsya concentrated solution of the degradation products ⁇ o water and ions of one type from that of the electrolyte (anions or cations), ion-selective migration which is provided by a combination of physical and chemical properties of the diaphragm and the electrophysical parameters of operation of the cell (see FIG. 6).
- the choice of diaphragm material is determined by the conditions of the problem being solved and
- the implementation of the ceramic diaphragm from grains of aluminum oxide with a specific surface of 1-4 m 2 / g allows you to provide the necessary flow parameters of the diaphragm. That the alumina particles are surrounded by smaller alumina particles, or particles
- titanium oxide and magnesium, or particles of zirconium dioxide, partially stabilized by oxides of rare or rare earth metals, can increase its chemical resistance.
- the diaphragm made of alumina grains with a specific surface of 1-4 m 2 / g surrounded by particles of alumina with a specific
- the implementation of the diaphragm from grains of alumina with a specific surface area of 1-4 m 2 / g, surrounded by a mixture of particles of titanium oxide and magnesium oxide, with a content of particles of alumina of at least 99% weight makes it possible to increase the stability of the diaphragm and increase its adsorptive properties. At the same time, at least 99% of the phase composition of the alumina particles are in alpha form.
- the diaphragm made from alumina grains surrounded by zirconia particles has the highest chemical resistance.
- the composition of the diaphragm is alumina — 60–90% by weight, with at least 98% of the phase composition of alumina in alpha form, zirconia 5 — 10–40% by weight, with at least 98% of the phase composition of zirconia in tetragonal modifications.
- an additive is used - one or more oxides selected from the group consisting of yttrium, scandium, ytterbium, cerium, gadolinium oxides.
- the total amount of oxides ⁇ réelle is 1, 0 - 10.0% by weight.
- the specified composition provides mechanical resistance and the structure of the diaphragm.
- the organization of input into the cell of the processed electrolyte solution and output of electrolysis products can be different, depending on the chemistry of the processes and the characteristics of the final electrolysis products. In general, this organization of flows is determined by the design of the attachment points, fixation and sealing points of the electrodes and the diaphragm, as well as devices for introducing electrolyte solutions into the electrode chambers and removing electrolysis products from the electrode chambers. These nodes, located on the end parts of the cell, can be made in the form of one or more parts of dielectric materials each. Depending on the requirements for the process occurring in the electrochemical cell, devices for supplying the treated solution to 5 electrode chambers can be connected to one node, and devices for removing electrolysis products to another.
- each of the nodes will be connected to a device for supplying a solution to one io electrode chamber and at the same time with a device for removing electrolysis products from another electrode chamber.
- Devices for supplying the treated solution to the electrode chambers and removal of electrolysis products from the electrode chambers can be made in the form of channels and nozzles combined with these parts, or in the form of holes
- the length of the cathode and / or anode and / or diaphragm is determined by the cell designs and the conditions of its installation.
- Units for mounting, fixing and fixing electrodes and diaphragms can also be made in the form of collectors equipped with channels for
- the anode and cathode must be made with holes that ensure the supply of electrolyte solutions to the electrode chambers and the removal of electrolysis products from the electrode chambers.
- Figure 1 schematically shows the working chamber of the electrochemical cell in the context, where: D 1 and D 2 are the inner and outer diameters of the anode made of a titanium tube with a coating of rare metal oxides deposited on a developed outer surface; D ⁇ and D 4 - respectively, the inner and outer diameters of the ceramic permeable diaphragm; D 5 and D b - respectively, the inner and outer diameters of the cathode made of titanium pipe, the inner apparent (geometric) surface of which is close to the active true (physical) surface; L ec is the length of the working part of the electrochemical cell.
- Figure 2 presents a diagram showing the distribution of the lines of force of the current density and oxidation potential on the microroughnesses of the anode 5 surface in dilute solutions.
- the sizes of microroughnesses in the surface of the anode do not exceed 10 microns with an average difference of the maximum and minimum oxidation potential on their surfaces 0.2 - 0.3 V.
- Fig. 3 shows a schematic representation of microtoroidal flow of solutions in the electrode chambers of an electrochemical cell.
- Each cross-sectional microlayer of the working part of the cell is a cathode and anode chemical reactor
- Figure 4 presents a graph describing the dependence of the electrical conductivity of aqueous solutions of inorganic electrolytes (dependence 1) and the average distance between the ions of these electrolytes depending on the concentration (dependence 2).
- Figure 5 presents a graph showing the change in the gradient of the potential in the interelectrode space of the electrochemical cell, where: a b e f k! - without a diaphragm; and b with h k I - with a ceramic diaphragm from corundum; a b e d q f k l - with a diaphragm of grains of aluminum oxide in the glaze
- Figure 6 presents a diagram of ion-selective electrolysis in a cell with a diaphragm.
- the diaphragm is made of zirconium oxide ceramic.
- the anode product in this process is a moist gaseous mixture of molecular chlorine (about 95%), chlorine dioxide (about 3%) and ozone (about 2%).
- a sodium chloride solution with a concentration of more than 100 g / l is used as the initial one.
- the pressure in the anode chamber (P ⁇ ) exceeds the pressure in the cathode chamber (P k ) by an amount that provides and selective removal of sodium ions from the anode chamber at a given value of the electric field strength in the diaphragm.
- FIG. 1 shows some embodiments of the installation, mounting and fixing of the diaphragm and electrodes and devices for supplying and outputting electrolyte to the electrode chambers.
- Figure 9 shows the scheme for producing electrochemically activated 15 anolyte and catholyte fresh drinking water.
- Figure 10 shows a diagram of experimental studies over time of the parameters of the electrochemically activated anolyte and catholyte of fresh drinking water in comparison with model solutions.
- Fig. 11 shows a comparison of the pH and ORP values of drinking water during chemical and electrochemical regulation and the change in these parameters over time.
- FIG shows a diagram of the electrochemical deoxidation of milk.
- Fig shows a diagram of the production of sulfuric acid, hydrogen and 25 sodium hydroxide solution from the initial solution of sodium sulfate
- FIG shows a diagram of the preparation of electrochemically activated freshwater catholyte.
- the working chamber of the electrochemical cell (Fig. 1) contains a cathode 1, a tubular anode 2 and a ceramic diaphragm 3 dividing the interelectrode space into the anode 4 and the cathode 5 of the chamber.
- the working chamber of the cell is characterized by the following dimensions: Di and D 2 — respectively, the inner and outer diameters of the anode made of a titanium pipe coated with rare metal oxides deposited on a developed outer surface; Dz and D 4 - respectively, the inner and outer diameters of the ceramic permeable diaphragm; D 5 and D 6 - respectively, the inner and outer diameters of the cathode made of a titanium tube, the inner apparent (geometric) surface of which is close to the active 5 true (physical) surface; L ec is the length of the working part of the electrochemical cell.
- FIG. 8a shows the options for the installation of mounting and fixing the diaphragm and electrodes, as well as devices for supplying and discharging solutions of electrolytes.
- the attachment points of the electrodes and the diaphragm are made in the form of one or more parts of dielectric material each, and the devices for supplying and discharging the treated solution to and from the electrode chambers are made in the form of channels and nozzles combined with the parts of the units.
- FIG. 8a Such an embodiment is shown in FIG. 8a, where on
- nodes are placed, which consist of two parts each, in which pipes and channels are made, communicating with one of the electrode chambers.
- the nodes also contain gaskets made of elastic material, providing sealing of the electrode chambers.
- the nodes are made in the form of dielectric bushings located at the ends of the electrochemical cell, and grooves are made at the ends of the bushings, and the cell contains dielectric collector heads made with an axial channel, moreover, the heads are mounted in the grooves of the bushings with the possibility of rotation, while the diaphragm is fixed in
- the anode is fixed in the heads by means of elastic seals located in the axial channels of the heads, and channels are made in the heads and in the bushings, respectively, for supplying and discharging the treated water and / or solution, respectively, of the anode and cathode chambers.
- the channels are displayed on the lateral surface of the bushings and heads, and are equipped with fittings.
- the internal hollow electrode can be made with input and output nozzles in communication with it cavity and placed respectively at the ends of the hollow anode (Fig. ⁇ b).
- This embodiment provides the possibility of flow of the coolant through the hollow anode, and, accordingly, reducing the cost of conducting the electrochemical process due to the removal of thermal disturbances.
- Such a 5 cell can be used for processing low-concentrated solutions, upon receipt of disinfectant solutions of various chemical compositions with a low total salt content.
- a cell using the cavity of the anode to pass the coolant can be used in the processes of water purification from nitrates.
- the attachment points of the electrodes and the diaphragm can be made in the form of one or more parts of dielectric material each, devices for supplying and discharging the processed solution of the cathode chamber are made in the form of channels and nozzles combined with the parts of the units.
- Input and output devices are made in the form of input and output devices
- FIG. 15 of the treated solution of the anode chamber are made in the form of pipes located at the end sections of the anode, while the anode is made with holes.
- FIG. 8c Such an embodiment is shown in FIG. 8c, where the nodes are made in the form of three to four parts, including dielectric bushings, and gasket systems.
- the input and output nozzles of the cathode chamber are shown in FIG. 8c, where the nodes are made in the form of three to four parts, including dielectric bushings, and gasket systems.
- the input and output nozzles of the cathode chamber are made in the form of pipes located at the end sections of the anode, while the anode is made with holes.
- a cell with such flow organization can be used in the processes of obtaining oxygen and hydrogen, as well as in the processes of obtaining
- the electrochemical cell for processing solutions can be made in such a way that the attachment points of the electrodes and the diaphragm are made in the form of one or more parts of dielectric material each, and the devices for input and output of the cathode chamber being processed by the solution are made in the form of holes and nozzles located at the end sections of the cathode.
- Devices for supplying and outputting the treated solution of the anode chamber are made in the form of nozzles connected to the internal cavity of the anode, and holes are made in the end parts of the anode.
- additional holes should be made evenly spaced along its length along the entire length of the working part of the cell. Such an embodiment is shown in FIG. 8d.
- the attachment points of the electrodes and the diaphragm also consist of three to four parts each and a gasket system.
- the inlet and outlet pipes of the anode chamber are made of electrically conductive material, mounted on the ends of the hollow anode, and communicate with its cavity.
- the hollow anode is made with perforations.
- holes are provided, equipped with nozzles that are input and output, and communicating with the cathode chamber.
- Such cells can be used in the processing of concentrated solutions of sodium chloride, for example, to obtain products of anodic oxidation from solutions of alkali metal chlorides.
- the cell works as follows. Through devices for supplying an electrolyte solution (not shown in FIG. 1), the treated solution is supplied to the anode 4 and cathode 5 of the cell chamber. Depending on the chemistry of the process, the movement of the electrolyte to the chambers is carried out in a parallel flow - from bottom to top or top to bottom, or countercurrent. A variant is possible in which the filling of one of the electrode chambers occurs due to electrostatic filtration through the diaphragm from another chamber or due to filtration under the influence of the differential pressure across the diaphragm. After the passage of the electrode chambers, the electrolyte, through the output devices (not shown in FIG. 1), is removed from the cell. Processing the solution is carried out either with a single flow through the chambers 4 and 5, or, in the case of anode 2 with openings, when the solution circulates in the anode chamber.
- the invention is illustrated by the following examples, which, however, do not exhaust all the possibilities of implementing the invention.
- AT examples depending on the conditions of the problem being solved, electrochemical cells were used, the length of the working part of which was 180 - 300 mm, the interelectrode distance was 3-11 mm, and the thickness of the diaphragm was 0.7 - 2.8 mm.
- Table 2 shows the cell parameters that were used in the implementation of examples of the use of the present invention. In the examples, the number of the cell that was used in each case is indicated.
- Example 1 Obtaining electrochemically activated anolyte and catholyte from fresh water.
- an Ns 5 electrochemical cell with an uncooled anode was used (see table 2 and Fig. 8a).
- HSE + 280 mV
- the volume flow rate of the anolyte was within. 5 - 6 l / h, catholyte - 10 - 12 l / h.
- the pressure in the cathode chamber was 0.8 - 0.9 kgf / cm 2 and exceeded the pressure in the anode chamber by 0.4 - 0.5 kgf / cm 2 .
- the volumetric flow rate of catholyte was in the range of 6 - 7 l / h, anolyte - 10 - 12 l / h. Regulation of the above hydraulic characteristics was carried out using variable hydraulic resistances at the inlet to the cell’s electrode chambers and pressure regulators “up to” at the outlet of the electrode chambers (not shown in the diagram).
- the specific cost of the amount of electricity in the treatment of water was about 1000 pounds per liter (KnIn).
- Number 1 indicates the source of drinking water, the parameters of which were subjected to chemical and electrochemical regulation.
- a quantitative characteristic of the acidity or alkalinity of water is a hydrogen pH, which is determined by the activity of hydrogen ions ( ⁇ i + ) or, otherwise, the ratio of ion concentration
- the redox potential (ORP or, in other words, ⁇ ) is another important parameter, since it characterizes the activity of electrons in an aqueous solution (water). It is measured using a high-resistance millivoltmeter and a pair of electrodes, one of which
- auxiliary 20 is a reference electrode (auxiliary) and the other is a measurement electrode.
- HSE silver chloride electrode
- 25 packs i.e. Ideally, it can be considered as a reservoir with electrons.
- a contact arises between two phases that have a common particle - an electron; therefore, the equilibrium condition for the "electrode-solution" interface is characterized by the equality of the electrochemical potentials of the electrons in the electrode and the solution.
- ORP there is a relationship between ORP and pH, which is practically expressed in the fact that when changing the pH of drinking water by 1 unit by adding sodium hydroxide or hydrochloric acid, ORP, respectively changes by approximately 59 mV - increases with decreasing pH and decreases with increasing pH.
- the potential of the inert electrode the oxidation potential of the solution
- the activity of solvated electrons in the solution which is established on the basis of 5 fundamental laws discovered by Nernst, it follows that the increase in the oxidation potential ⁇ is due to a decrease in the activity of electrons in the solution and, conversely, a decrease in ⁇ is determined by an increase in activity electrons.
- ORP The nature of the ORP is primarily due to the quantum-mechanical characteristics of atoms of an elementary electrochemical system (“electrode-solution”), the peculiarities of its electronic structure, which determine the ionization potentials of elements.
- electrode-solution an elementary electrochemical system
- the electronic structures of atoms and ions also largely determine the nature and energy of ion hydration processes.
- the relaxation rate is determined by the time during which the measured characteristic of the system changes e times compared with the initial value. zo.
- the rate and magnitude of relaxation changes of a parameter is usually the higher, the more effective is the process of electrochemical activation itself, i.e.
- DEL double electric layer
- Example 2 Inversion of sugar syrup into glucose-fructose syrup.
- Sugar syrup with a concentration of 67% was supplied from a container with a volume of 5 5 liters using a peristaltic pump into the anode chamber of the cell at a rate of 1.0 l / h.
- a peristaltic pump into the anode chamber of the cell at a rate of 1.0 l / h.
- sugar syrup was pumped in the forward flow mode at a rate of 1.0 liter per hour.
- the cell anode io was cooled by running tap water flowing at a rate of 1.0 liter per hour.
- a current of 0.4 ampere at a voltage of 100 volts was passed through the cell.
- an excess pressure of 0.5 kgf / cm 2 was created in comparison with the pressure in the cathode
- the pH of the syrup after exiting the anode chamber was 3.5.
- the degree of sugar inversion in this case, depending on the exposure time at elevated temperature (20, 30 and 40 minutes) was 15, 30 and 50%, respectively.
- Example 3 The deoxidation of milk.
- an electrochemical modular cell Ns 4 was used (see table. 2)
- the acidity of milk is due to hydrogen ions formed as a result of electrolytic dissociation of acids and acid salts contained in milk. Hydrogen ions are very active, destroying the casein-calcium phosphate complex, secrete casein, curdle milk and affect its salt component. With increasing acidity, the properties of milk, both a food product and raw materials for processing, gradually change. In quantitative accounting, the acidity of milk is usually expressed in degrees Turner ( 0 T). The acidity of freshly milked milk is on average 16–18 0 T. The pH value of such milk is in the range of 6.3–6.8.
- FIG. 12 A schematic diagram explaining the studies performed is shown in FIG. 12.
- the object of the study was fresh and pasteurized cow's milk with a fat mass fraction of 3.2%, having a different acidity: 28 and 32 ° T.
- Example 4 The regeneration of oxidized fats.
- an Ns 3 electrochemical modular cell was used (see Table 2).
- the technology for the regeneration of oxidized fats is based on the cathodic
- the pressure drop across the diaphragm should be at least 0.3 - 0.5 kgf / cm 2 .
- hot tap water with a temperature of about 70 ° C at a speed of 4 l / h was also fed into the lower part of the cell in the forward flow mode.
- Example 5 The synthesis of peroxocarbonate disinfectant solution. An electrochemical cell of Na 5 (see table. 2) was used 15 to obtain a peroxocarbonate solution.
- Cylindrical tubular electrodes with a 0.7 mm thick ceramic diaphragm separating them are coaxially mounted in the cell.
- Ceramic composition aluminum oxide - 80%, modified zirconia - 15%. Modified zirconia contains 5.0% 20 yttrium oxide.
- the electrodes used were titanium coated with iridium oxide (anode) and titanium with a pyrocarbon coating (cathode).
- the length of the cell’s working chamber is 185 mm, the volume of the cathode electrode chamber is 10 ml, and the anode electrode chamber is 7 ml.
- the resulting solution Perox anolyte, has the following characteristics: the content of mono-angular and diacitric acids is from 25 20 to 50 mg / l, the redox potential is in the range from + 500 to + 800 mV relative to the silver chloride reference electrode.
- Example 6 The synthesis of a low saline disinfectant solution (neutral anolyte AN) with a high specific content of chlorine-oxygen and hydroperoxide oxidants.
- the electrochemical cell Ns 5 (see Table 2) according to the invention was used to synthesize a low saline solution with a high specific content of oxidants.
- Drinking water was supplied from the cell to the anode chamber at a rate of 3 l / h.
- the total salinity of the water was 0.15 g / l.
- the pressure stabilizer installed at the outlet of the anode chamber provided a constant pressure in the anode chamber equal to 1.2 kgf / cm 2 .
- the inlet and outlet of the cathode chamber 5 were connected by flexible hoses with a circulation capacity of 0.2 liters, also filled with drinking water and placed at a level 10 centimeters above the vertically mounted cell.
- a voltage of 40 volts was applied to the cell from a constant current source of direct current, the current strength, gradually increasing from the initial value of 0.8 A, reached a value of 3 A.
- catholyte was circulated in the cathode chamber of the cell due to the gas lift operating due to hydrogen evolved.
- Example 7 Water purification from anionic surface active substances (AAS).
- An Ns 3 electrochemical cell (see Table 2) with a cooled anode was used to remove anionic surfactants from water (AAS).
- AAS anionic surface active substances
- An auxiliary electrolyte solution the volume of which in the tank was 1 liter, was also pumped through the cathode chamber of the cell using a peristaltic pump also in circulation mode at a speed of 15 l / h.
- a flow of cooling water was carried out through the anode cavity at a rate of 5 liters per hour.
- the results presented in the table show that in 11 hours it is possible to almost completely remove the surfactant from 9 liters of the model solution.
- Example 8 Purification of water from nitrates.
- the electrochemical cell Ns 2 ju (see table. 2) according to the invention was used to purify water from nitrates.
- the tests were carried out in a laboratory setup consisting of a single cell, a direct current source that allows you to adjust and maintain voltage and current in the range of 0 - 30 volts and 0-3 amperes, respectively, peristaltic pump and containers for circulation
- test procedure was as follows: the treated water containing dissolved nitrates was pumped using a pump in the circulation mode, first through the cathode chamber of the cell, and then through the anode chamber in countercurrent mode. Recirculating water periodically
- the model solution prepared by adding ammonium sulfate solution to tap water until the concentration of ammonium ions reaches 145 - 185 mg / l, pH 7.6 - 7.8 was used as purified water. In some cases, in
- the experiment was carried out with simultaneous circulation of the purified solution through the cathode, and then through the anode chamber.
- the volume of the solution is 3.8 liters.
- the circulation speed of the solution is 30 l / h.
- a constant current strength of 2.5 A was maintained, while the voltage on the cell was 20–22 V.
- the pH of the solution was maintained in the range of 6–8. The results are shown in table 4.
- the next experiment was carried out similarly to the previous one, with the difference that 1 g / L of sodium chloride was added to the initial solution.
- the volume of the solution is 3.8 liters.
- the circulation speed of the solution is 30 l / h.
- a constant current strength of 3.0 A was maintained, while the voltage on the cell was about 10 V.
- the pH of the solution was maintained in the range of 6 - 8. The results obtained are shown in the following table 5.
- Example 9 Obtaining sulfuric acid, hydrogen and sodium hydroxide from a solution of sodium sulfate.
- the indicated method was implemented using cell Ns 1 (see Table 2 and Fig. 8d).
- a schematic diagram of the implementation of the method is shown in FIG. 13.
- a solution of sodium sulfate with a concentration of 100 g / l was dosed into the anode chamber of the cell at a rate of 0.25 l / h.
- Fresh water was introduced into the cathode chamber at a rate of 0.6 l / h.
- the pressure in the anode chamber exceeded the pressure in the cathode chamber by 0.4 kgf / cm 2 .
- sodium ions from the anode chamber migrate to the cathode chamber, forming sodium hydroxide.
- the total electrochemical reaction is described by the following equation.
- the diaphragm was made of ceramic composition: zirconium oxide - 70%, alumina - 27% and yttrium oxide - 3%.
- the surface of the titanium anode was coated with ORTA, the inlet and outlet nozzles of the anode chamber were made of BT1-00 grade titanium, the diaphragm seals were made of F4 grade fluoroplastic.
- the operation diagram of the electrochemical modular cell in this technology is shown in FIG.
- the main reaction is the evolution of molecular chlorine in the anode chamber and the formation of sodium hydroxide in the cathode chamber:
- ozone is formed due to direct decomposition of water and due to the oxidation of the released oxygen: 5 3H 2 O - be -> O 3 + 6H + ;
- the process of ion selective electrolysis was carried out as follows. A solution of sodium chloride with a concentration of 200 g / l at a rate of 0.3 l / h was dosed into the anode chamber. The pressure in the anode chamber was maintained equal to 1, 1 kgf / cm 2 due to the pressure stabilizer at the 15th output of the anode chamber (not shown in Fig. 6). After filling the cathode chamber with an atmospheric pressure from the anode chamber, the voltage from the DC source equal to 3.2 V was applied to the cell electrodes. At the same time, a current of 30 A flowed through the cell. The performance of the studied electrochemical 20 system was approximately 40 g oxidants per hour in chlorine equivalent, which in terms of specific indicators exceeds industrial chlorine electrolyzers.
- Example 11 Obtaining electrochemically activated catholyte fresh water in the preparation technology of enriched 25 nitrogen fertilizer irrigation water for plants.
- a Ne 5 cell was used (see Table 2 and Fig. 8 b).
- the ideological basis of the technological process under consideration was laid by the work of Justus Liebig, the creator of the theory of mineral nutrition of plants, who almost two centuries ago showed that rainwater contains nitrogen fertilizers of natural origin, absorbed by water from the atmosphere. In atmospheric water, the concentration of these fertilizers is only a fraction of a milligram per liter. But with such a low content, their rainwater It has an effect on plant growth that cannot be obtained when watering from earth sources, even when it is more than enough.
- Nitrogen fertilizers are vital for the normal growth and development of plants.
- devices of a specific purpose are used: inverters, absorbers, strippers, heat exchangers, refrigerators, filters, sumps, superheaters, condensers, evaporators, crystallizers, drying drums and other equipment.
- the following chemical reagents are used: caustic soda, soda ash, table salt, hydroxides of calcium, magnesium, sulfuric and nitric acid, etc. Electricity, steam, and hot water are used.
- nitrate fertilizers As a result, the production process of nitrate fertilizers is accompanied by the release of pollutants into the environment. Regardless of the technical level of such production, it inevitably pollutes the environment and worsens the environmental situation.
- nitric acid 0.455 tons of nitric acid, 0.03 tons of soda, 2.5 tons of steam (8 atm.), 65 m 3 5 pure water, 120 kWh of electricity are currently consumed. 0.38 tons of nitrogen oxides are obtained as waste (per 1 ton of sodium nitrate).
- Electrochemical technologies implemented in modular electrochemical cells allow you to create an environmentally friendly process for the production of nitrogen fertilizers.
- Sodium, calcium, magnesium and potassium saltpeter are synthesized directly from salts (chlorides, sulfates, carbonates) naturally dissolved in irrigation water.
- Water is preliminarily subjected to an electrochemical cathodic treatment in an electrochemical reactor, and then nitric acid is introduced into it in a concentration providing an indicator of alkalinity of water in
- Fresh irrigation water with a total salinity of 0.24 g / L was pumped through the cathode chamber of the cell, the pressure in which was higher than the pressure in the anode chamber by 0.8 kgf / cm 2 .
- the water flow before feeding into the cathode chamber of the cell passed through the internal cavity of the anode, cooling it.
- the flow rate of water ranged from 10 to 20 l / h.
- Water enriched with nitrogen compounds can be used to irrigate crops of agricultural plants.
- the environmental cleanliness of the technology is due to the fact that the process of producing nitrate fertilizers is not accompanied by emissions of polluting substances, and the use of fertilizers obtained by the proposed method does not increase the mineral pollution of the soil, since nitrates of alkaline and alkaline earth metals are synthesized from salts naturally dissolved in irrigation water.
- concentration that ensures the biological need of plants is the nitrate content of 5 to 15 milligrams in 1 liter of irrigation water. It was also established that watering plants during the entire period of cultivation with water with a low nitrate content allows you to get 5 the maximum possible crop yields with high biological value of the product.
- Periodic introduction of fertilizers into the soil by known methods is associated with environmental pollution and crop production, because commonly used liquid nitrate fertilizers have a concentration of about 25,000 to 50,000 times greater than the biologically optimal one.
- EFFECT invention makes it possible to intensify electrolysis processes in a diaphragm type cell and due to
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DE112008004180T DE112008004180T5 (de) | 2008-12-03 | 2008-12-03 | Elektrochemische modulare Zelle zur Verarbeitung von Eektrolytlösungen |
PCT/RU2008/000740 WO2010064946A1 (ru) | 2008-12-03 | 2008-12-03 | Электрохимическая модульная ячейка для обработки растворов электролитов |
GB1110956.8A GB2479286B (en) | 2008-12-03 | 2008-12-03 | Electrochemical modular cell for processing electrolyte solutions |
US13/131,266 US8961750B2 (en) | 2008-12-03 | 2008-12-03 | Electrochemical modular cell for processing electrolyte solutions |
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US9222182B2 (en) | 2013-06-14 | 2015-12-29 | Simple Science Limited | Electrochemical activation device |
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US9777383B2 (en) * | 2010-01-08 | 2017-10-03 | Clarentis Holding, Inc. | Cell and system for preparation of antimicrobial solutions |
US9085474B2 (en) | 2012-12-28 | 2015-07-21 | Lean Environment Inc. | Modular system for storm water and/or waste water treatment |
WO2014204332A1 (ru) * | 2013-06-17 | 2014-12-24 | Bakhir Vitold Mikhaylovich | Электрохимическая модульная ячейка для обработки растворов электролитов |
WO2015048537A1 (en) | 2013-09-27 | 2015-04-02 | R-Hangel, LLC | Activated solutions for water treatment |
US10071921B2 (en) | 2013-12-02 | 2018-09-11 | Lean Environment Inc. | Electrochemical reactor system for treatment of water |
DE102017119566B4 (de) | 2017-08-25 | 2021-08-12 | Blue Safety Gmbh | Vorrichtung zur Gewinnung von Produkten der Elektrolyse von Alkalimetallchloridlösung |
RU2751891C1 (ru) * | 2020-06-29 | 2021-07-19 | Федеральное государственное бюджетное образовательное учреждение высшего образования "Сибирский государственный университет путей сообщения" (СГУПС) | Способ очистки природных и сточных вод от нитратов |
EP4091992A1 (en) | 2021-05-19 | 2022-11-23 | Blue Safety GmbH | Method for purification of water and water purification system |
WO2023142839A1 (zh) * | 2022-01-29 | 2023-08-03 | 青岛海尔电冰箱有限公司 | 气体处理装置以及具有其的冰箱 |
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2008
- 2008-12-03 DE DE112008004180T patent/DE112008004180T5/de not_active Withdrawn
- 2008-12-03 US US13/131,266 patent/US8961750B2/en active Active
- 2008-12-03 WO PCT/RU2008/000740 patent/WO2010064946A1/ru active Application Filing
- 2008-12-03 GB GB1110956.8A patent/GB2479286B/en not_active Expired - Fee Related
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
RU2088693C1 (ru) * | 1996-02-09 | 1997-08-27 | Витольд Михайлович Бахир | Установка для получения продуктов анодного оксиления раствора хлоридов щелочных или щелочно-земельных металлов |
US5635040A (en) * | 1996-03-11 | 1997-06-03 | Rscecat, Usa, Inc. | Electrochemical cell |
WO1998058880A1 (en) * | 1997-06-25 | 1998-12-30 | Sterilox Technologies International Limited | Method and apparatus for the electrochemical treatment of water and aqueous salt solutions |
RU2130786C1 (ru) * | 1998-08-11 | 1999-05-27 | Мееркоп Геннадий Евсеевич | Электрохимическое устройство для обработки жидкой среды |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US9222182B2 (en) | 2013-06-14 | 2015-12-29 | Simple Science Limited | Electrochemical activation device |
Also Published As
Publication number | Publication date |
---|---|
US8961750B2 (en) | 2015-02-24 |
GB2479286A (en) | 2011-10-05 |
WO2010064946A8 (ru) | 2010-07-29 |
GB201110956D0 (en) | 2011-08-10 |
GB2479286B (en) | 2013-09-18 |
DE112008004180T5 (de) | 2012-08-30 |
US20110226615A1 (en) | 2011-09-22 |
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