US3860509A - Continuous electrowinning cell - Google Patents

Continuous electrowinning cell Download PDF

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Publication number
US3860509A
US3860509A US334157A US33415773A US3860509A US 3860509 A US3860509 A US 3860509A US 334157 A US334157 A US 334157A US 33415773 A US33415773 A US 33415773A US 3860509 A US3860509 A US 3860509A
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United States
Prior art keywords
cathode
conductive
anode
metal
tank
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Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
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US334157A
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English (en)
Inventor
Jr Robert Clarence Emmett
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Envirotech Corp
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Envirotech Corp
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Filing date
Publication date
Application filed by Envirotech Corp filed Critical Envirotech Corp
Priority to US334157A priority Critical patent/US3860509A/en
Priority to CA189,678A priority patent/CA1014890A/en
Priority to ZA740172A priority patent/ZA74172B/xx
Priority to AU64437/74A priority patent/AU487933B2/en
Priority to ZM15/74A priority patent/ZM1574A1/xx
Priority to FR7402802A priority patent/FR2218396B1/fr
Priority to DE19742406473 priority patent/DE2406473C3/de
Priority to GB725374A priority patent/GB1406592A/en
Priority to BR1168/74A priority patent/BR7401168D0/pt
Priority to SU741997533A priority patent/SU704464A3/ru
Priority to JP2037074A priority patent/JPS5610390B2/ja
Priority to IT48589/74A priority patent/IT1008282B/it
Application granted granted Critical
Publication of US3860509A publication Critical patent/US3860509A/en
Anticipated expiration legal-status Critical
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    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
    • C25C7/00—Constructional parts, or assemblies thereof, of cells; Servicing or operating of cells
    • C25C7/02—Electrodes; Connections thereof
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
    • C25C7/00—Constructional parts, or assemblies thereof, of cells; Servicing or operating of cells
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
    • C25C7/00—Constructional parts, or assemblies thereof, of cells; Servicing or operating of cells
    • C25C7/06—Operating or servicing
    • C25C7/08—Separating of deposited metals from the cathode

Definitions

  • An electrolytic cell is formed with a housing enclosing a flat-faced cathode and anode in closely spaced faceto-face relationship.
  • the cathode comprises a plurality of small diameter cathode elements held in spacedapart relationship by an insulating matrix. Each of the elements terminates in a small diameter tip. Metal deposits on the tips in dendritric form and is scraped therefrom.
  • the anode face is porous and connections are provided for withdrawing gaseous products from the face as they are formed. Operation is continuous, recovered metal being flushed from the cell in spent electrolyte asthe latter is displaced by fresh electrolyte.
  • Electrowinning a well-known process, utilizes an electric current to reduce an ionized metal for deposit as elemental metal on a cathode.
  • the ionized metal is carried in an electrolyte usually yielded from an acid leach of a metal bearing ore or concentrate.
  • a conventional electrowinning cell comprises a tank in which one or more sets of insoluble anodes and cathodes are immersed in an electrolyte. When a current passes through the electrolyte between the electrodes, metal is deposited on the cathode.
  • electrowinning is a batch operation conducted in large tanks in which a plurality of cathodes and anodes are suspended.
  • the anodes are usually chemically inert, typically, a lead alloy such as lead-antimony.
  • the cathodes are usually thin starting sheets of the same metal as that which is to be recovered and are retained in the electrolyte for one to three weeks until a commercially usable quantity of metal builds on them.
  • This invention provides improved ways and means for continuous electrowinning of metal in commercial acceptable form.
  • the mechanism includes a cathode of novel construction on which metal is deposited as small dense particles. Means are provided for continuously removing deposited metal while electrolysis continues.
  • the cathode is formed so that its exposed face comprises a plurality of smallarea tips held in-spaced-apart relationship by an insulating matrix. With this construction, each small-area tip functions as a separate cathode.
  • the invention is predicated on the discovery that if the individual cathode tips have a small exposed area, metal will deposit thereon in a particular configuration and with such a fragile bond that it is subjected to easy harvesting without harming the tips.
  • a harvesting means is provided to continuously remove deposited metal from the cathode tips, and means are also provided to remove the metal particles from the cell as they are harvested.
  • a porous anode of special design is also provided to continuously withdraw gaseous products from the cell.
  • FIG. 1 is a side view of an electrolytic cell embodying the invention. For purposes of illustrating internal components, a portion of the cell wall is shown as partially cut away;
  • FIG. 2 is a plan view of the cell illustrated in FIG. I with portions of the wall cut away for purposes of revealing internal components. Additionally, electrolyte supply piping is also illustrated;
  • FIG. 3 is a pictorial view, partially cut away, of the cathode employed in the cell illustrated in FIGS. 1 and FIG. 4 is a sectional view taken in a plane passing through the line 44 of FIG. 3 and viewed in the direction of the arrows 4;
  • FIG. 5 is an enlarged detailed view of that part of the cathode encompassed within the line 55 of FIG. 4;
  • FIG. 6 is a pictorial view of an anode suitable for use in the cell illustrated in FIG. 1;
  • FIG. 7 is a sectional view taken in a plane passing through the line 7-7 of FIG. 6 and viewed in the direction of the arrows 7 and
  • FIG. 8 is a detailed view of a metal harvesting means adapted for use with the cell.
  • the electrowinning cell illustrated in FIGS. I and 2 generally comprises a housing 12 in which are mounted a cathode l3 and an anode 14 in face-to-face relationship.
  • The-housing 12 may be sealed to facilitate capture of gaseous products of electrolysis and prevent escape of corrosive vapors.
  • the inner wall of the housing is electrically insulated, preferably with a corrosionresistant material.
  • the cathode 13 is designed so that metal of proper characteristics will be efficiently deposited thereon at a high rate and in a form susceptible to continuous removal without damage to the cathode or interruption of the process.
  • the cathode 13 comprises a plurality of exposed electrically conductive tips 30, each of which functions as a separate cathodic element.
  • the tips are the terminal ends of thin conductors 31, such as small-diameter wires, which are s'upported'in spaced-apart relationship by a matrix of insulating material 32 held in an insulated holder 43 with only the tips 30 exposed.
  • the other ends of the conductors 31 are all connected inside the holder to a common electrically conductive base 34.
  • the exposed surface or face of the cathode 13 should be smooth so thatdeposits on the individual cathode tips do not physically stick to the insulating matrix 32 and none of the sidewalls of the individual cathodic elements 31 are exposed.
  • the conductive cathode surface may be described as being a smooth surface formed from the free ends of a plurality of electrical-conductors held in spaced-apart relationship by a matrix of non-conducting materials
  • the cathode tips 30 are sufficiently small that the metal deposits thereon in a configuration which exhibits a weak bond and extends outwardly from the oathode face, thereby enhancing removal by a light scraping action. As illustrated, the cathode tips are flat, round surfaces about 0025-0.
  • One technique for fabricating a suitable cathode is to first fix segments of relatively large diameter stainless steel wire to a base strip to provide a comb-like component. A number of such strips are fixed together to form a brush-like cluster. The diameters of the wires are then decreased by known etching techniques and the cluster is encapsulated in a suitable insulating material such as a ceramic, glass or appropriate plastic.
  • a suitable insulating material such as a ceramic, glass or appropriate plastic.
  • the insulating material should be corrosion-resistant and of sufficient strength that it does not flex or permit working loose of the conductors to the extent that greater cathode areas are exposed lest the character of the metal deposits change and they become difficult to remove.
  • Suitable cathodes have been formed where the individual tips have a rectangular configuration, say 0.0250.l mm by 0.5-2.5 mm (area 0.0l25mm to 025mm), and with spacing between adjacent tips ranging from 0.250.6 mm at the closest points. Again, the spacing is important to avoid bridging between adjacent tips.
  • an insulated shaft 46 is rigidly fixed to and extends from the rear face of the cathode holder 43 to extend through the adjacent endwall of the housing 12 where it connects to a suitable drive 48 adapted to effect slow rotation of shaft 46 and the cathode holder 43.
  • a conventional stuffing box 49 encircles the shaft where it exits the housing.
  • An electrical conductor 51 (FIGS. 3 and 4) extends from the common base 34 through the insulated shaft 46 to terminate outside the housing at a contactor 51a adapted to be connected to a direct current source, not shown, but which typically supplies a potential of about 2-8 volts across the electrodes. If the cell contains more than one pair of electrodes, the DC source should be capable of supplying 2-8 volts across each pair.
  • the anode 14 (FIGS. 6-7) is designed to serve as the inlet for fresh electrolyte simultaneously with removal of gaseous electrolysis products.
  • the anode includes a flat face plate 53 made from a perforated or otherwise porous material.
  • the plate 53 may comprise two super-imposed layers of perforated titanium sheet which are coated with a metal or oxide capable of functioning as an inert anode whereby to promote oxygen release.
  • anode face plate 53 forms the conductive anode surface and is in closely spaced parallel relationship to the conductive cathode surface 13.
  • the face plate 53 fits over a hollow cylindrical holder 54 in which is fitted a solid divider 55 which divides the anode transversely into a front chamber or plenum 56, just back of the anode face plate, and a back chamber or plenum 57 adjacent the rear of the holder.
  • the holder and the divider should be made from nonconductive, anodic-corrosion-proof material.
  • An insulated shaft 58 is connected and extends rearward from the holder.
  • a suitable conductor 67 extends through the shaft to connect the face plates 53 to the D.C. source.
  • a plurality of short, electrically non-conductive conduits 59 extend through the divider 55, thence across the front chamber 56 and through the anode face plate 53 to thus provide communication between the rear chamber 57 through the face plate 53 into the interior of the housing 12.
  • a bore 61 in the shaft forms a conduit which connects the back chamber 57 to a source of electrolyte, all as more fully described hereinafter.
  • a second bore 63 extends longitudinally through the shaft 58 thence through the back chamber 57 and the divider 55 to provide communication between the front chamber 56 and the exterior of the anode whereby enabling withdrawal of gas through the porous anode face 53.
  • the withdrawal of gas may be facilitated by application of vacuum to the front chamber via conduit 63 in addition to the pressure differential created by introduction of electrolyte.
  • the electrolyte supply conduits 59 are sized and spaced on the anode face 53 to permit an adequate supply of fresh electrolyte into the housing 12 without un necessary jetting that might result in premature removal of metal deposits from the face of the cathode 13. Usually about 2 mm separates the two electrode faces but the distance can range from about 1 mm to 10 mm.
  • the shaft 58 connects to the rear of the anode assembly and extends through the wall of the housing 12. Fluid leakage from the housing is contained by a flexible sleeve 64 (FIGS. 1 and 2).
  • the shaft 58 serves to support and adjust the anode 14 to selected positions within the housing. Adjustment of anode position is effected by mounting the shaft in a mechanism 65 outside the housing which enables adjustment in an axial direction. For fine adjustments of the anode position, use is made of simple draw bolts 66.
  • an electrical conductor 67 extends from the anode face 53 through the shaft 58 to the electrical power source. It is insulated except where it contacts the plates 53.
  • Metal-bearing electrolyte is introduced to the cell via a, main feed line 90 and one or more of the valved branch lines 91, 92 and 93.
  • conduit 91 connects to passage 61 in shaft 58 to supply electrolyte through the anode face into the housing.
  • Conduit 92 connects through the wall directly into the interior of the housing.
  • Conduit 93 connects to special conduit on the scraper blade assembly for purposes to be more fully explained hereinafter.
  • electrolyte will normally be supplied through both branches 91 and 92 to keep the housing, including the inter-electrode space, full without excessive liquid movement transverse to the electrode faces.
  • fresh electrolyte enters through the anode surface and through the housing wall.
  • Some electrolyte is withdrawn through the anode face with the gas and the balance is withdrawn through the flush conduit with the harvested metal.
  • a further inlet conduit 75 is provided to supply low-acid content feedv electrolyte to the harvesting blade area to assist in flushing out the loosened metal while diluting the acid content of the spent electrolyte in which the metal is flushed from the cell.
  • a harvester is provided for continuously removing deposited metal from the cathode points.
  • the harvester 72 (FIGS. 6-8) includes a blade 73 which is hooded, as hereinafter explained, and is fixed to a reciprocatable arm 74 which moves the blade and associated hood radially to-and-fro within a solid walled slot 76 formed in the anode face 53 (see FIG. 6).
  • the blade enlarged in FIG. 8, is much shorter than the slot 76.
  • the blade extends toward the cathode face and terminates close to the cathode face so that as the cathode 13 rotates, the edge of the blade 73 scrapes the metal deposits from the cathode tips.
  • Electrolyte such as an acid leach solution
  • main conduit 90 and branches 91 and 92 are introduced via main conduit 90 and branches 91 and 92 into the housing thus feeding both through the anode face and the housing wall to maintain the cell substantially filled with electrolyte.
  • the electrolyte flow rate, the applied voltage and the distance between the electrode faces are all adjusted to obtain the desired rate and quality of deposit.
  • Typical current densities will range from about 0.5 to about 2.0 amperes per square cm (about 460 amperes/ft. to about 1859 amperes/ft?) As used herein, current densities are computed on total surface area of the cathode face not just the cathode tips.
  • the configuration of metal deposits on the cathode, except for some very soft deposits obtained at high current densities, is that shown in FIG. 5.
  • a test model constructed substantially as shown in the drawing was used for test work.
  • the cathode and anode were each 6 inches in diameter.
  • the anode was constructed as described in connection with FIGS. 6 and 7.
  • the anode face was formed from two layers of perforated titanium plate with 1.5 mm perforations.
  • the plates were slightly spaced apart (1 mm) and the perforations were offset tocreate a tortuous path through the face. Twelve feed conduits 59 were provided in the anode face.
  • a single cell may employ a plurality of pairs of anodes and cathodes.
  • the anodecathode pairs may, in the same cell, be connected either in series or in parallel. The series connection is more attractive economically.
  • the cell may beformed in an open tank, the use of a completely closed cell enables operation at elevated temperatures without the release of free steam. This is advantageous because high temperature operation is desirable since it reduces electrolyte resistance and thus power consumption. Also, at a constant current density and electrolyte composition, a higher temperature will yield a metal product of higher bulk density and improved flow-ability.
  • the inlet and outlet will be arranged to accommodate continuous feed and discharge while maintaining a constant volume of solution to keep the electrodes submerged to the desired degree.
  • the electrodes may vary in overall size; however, the dimensions and cross-sectional areas of the individual cathode conductors as well as the tip spacing should remain within the specified limits in order to achieve the desired results.
  • the conductive cathode and anode surfaces are shown as being flat, it will be appreciated that embodiments utilizing other forms may be constructed.
  • the conductive cathode surface may be cylindrical so long as it is smooth and presents a plurality of small conductors held in spaced-apart relationship by a matrix of non-conductive material. Similar comments apply to the anode.
  • Apparatus for electrowinning of metal from a metal bearing electrolyte solution comprising a tank having an inlet and outlet and adapted to contain a substantially constant volume of electrolyte in continuous flow therethrough, an anode and a cathode mounted in said tank with conductive surfaces in functional relationship to each other, and said conductive surface of said cathode comprising a smooth surface formed from the free ends of a plurality of relatively small electrical conductors each of cross-sectional area in the range from 0.0005mm to 0.018mm and a matrix of nonconductive material holding said small conductors spaced-apart a distance of at least 0.25mm.
  • Apparatus for electrolytic recovery of metal from a metal bearing electrolyte solution comprising a tank having an inlet and an outlet for receiving and discharging electrolyte solution and arranged to maintain in said tank a quantity of solution having a predetermined upper level, at least one flat-faced anode and one flatfaced cathode in said tank said flat faces being respcc' tively the conductive anode and the conductive cathode surfaces', said anode and cathode being arranged with their conductive surfaces in closely spaced faceto-face relationship and at an elevation such that at least a portion of both said conductive surfaces are below said predetermined upper level of solution, said conductive cathode surface comprising an exposed smooth surface formed from the free ends of a plurality of electrical conductors each of a cross-sectional area not exceeding 025mm encapsulated in a matrix of non-conductive material to be held spaced apart at said surface a distance of at least 0.25mm, means connecting said conductive anode and catho
  • Apparatus according to claim 4 in which said means for dislodging metal from said conductive cathode surface comprises a scraper and means to effect relative movement between said cathode surface and said scraper.
  • Apparatus according to claim 6 with the addition of means for introducing a supplemental supply of electrolyte into the tank adjacent the inlet to said product discharge conduit means to provide at least part of the solution making up the mixture discharged from adjacent said scraper.
  • Apparatus according to claim 5 in which said means effecting relative movement between said cathode and said scraper comprises rotatably journalled shaft means connected to said cathode, and means outside said tank for rotatably driving said shaft and cathode.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Electrolytic Production Of Metals (AREA)
US334157A 1973-02-20 1973-02-20 Continuous electrowinning cell Expired - Lifetime US3860509A (en)

Priority Applications (12)

Application Number Priority Date Filing Date Title
US334157A US3860509A (en) 1973-02-20 1973-02-20 Continuous electrowinning cell
CA189,678A CA1014890A (en) 1973-02-20 1974-01-08 Continuous electrowinning cell
ZA740172A ZA74172B (en) 1973-02-20 1974-01-09 Continuous electrowinning cell
AU64437/74A AU487933B2 (en) 1973-02-20 1974-01-11 Continuous electrowinning cell
ZM15/74A ZM1574A1 (en) 1973-02-20 1974-01-22 Continuous electrowinning cell
FR7402802A FR2218396B1 (enExample) 1973-02-20 1974-01-29
DE19742406473 DE2406473C3 (de) 1973-02-20 1974-02-11 Vorrichtung zur elektrolytischen Gewinnung von Metall aus einer Metall enthaltenden Elektrolytlösung
GB725374A GB1406592A (en) 1973-02-20 1974-02-18 Cathode and apparatus for and a process of electrolytically extracting metal from an electrolyte solution
BR1168/74A BR7401168D0 (pt) 1973-02-20 1974-02-18 Aparelho para a extracao de metal por via eletrolitica de uma solucao de eletrolito contendo metal
SU741997533A SU704464A3 (ru) 1973-02-20 1974-02-19 Электролизер дл извлечени металлов из водных растворов
JP2037074A JPS5610390B2 (enExample) 1973-02-20 1974-02-20
IT48589/74A IT1008282B (it) 1973-02-20 1974-02-20 Cella per estrazione elettrolitica con processo continuo

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Application Number Priority Date Filing Date Title
US334157A US3860509A (en) 1973-02-20 1973-02-20 Continuous electrowinning cell

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US3860509A true US3860509A (en) 1975-01-14

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US (1) US3860509A (enExample)
JP (1) JPS5610390B2 (enExample)
BR (1) BR7401168D0 (enExample)
CA (1) CA1014890A (enExample)
FR (1) FR2218396B1 (enExample)
GB (1) GB1406592A (enExample)
IT (1) IT1008282B (enExample)
SU (1) SU704464A3 (enExample)
ZA (1) ZA74172B (enExample)
ZM (1) ZM1574A1 (enExample)

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US4014756A (en) * 1976-01-21 1977-03-29 Fromson H A Process for making metal powders
DE2711610A1 (de) * 1976-04-01 1977-10-13 Falconbridge Nickel Mines Ltd Wiedergebrauchsfaehige kathodeneinheit, verfahren zum galvanisieren einer kathodeneinheit mit mehreren metallgalvanoschichten sowie kathodisch abgelagertes metallprodukt
US4086082A (en) * 1976-04-16 1978-04-25 Shalom Mahalla Copper crystal and process
US4132623A (en) * 1976-12-03 1979-01-02 Compagnie Generale D'electricite Device for regenerating zinc
US4139430A (en) * 1976-04-01 1979-02-13 Ronald Parkinson Process of electrodeposition and product utilizing a reusable integrated cathode unit
US4235696A (en) * 1979-07-23 1980-11-25 The International Nickel Co., Inc. Mandrel for nickel rounds with a monolithic surface
WO1987000210A1 (en) * 1985-06-27 1987-01-15 Cheminor A/S A method for the production of metals by electrolysis
US5792328A (en) * 1990-12-31 1998-08-11 Electric Fuel (E.F.L.) Ltd. Apparatus for removing zinc particle deposits from an electrode
US6376063B1 (en) 1998-06-15 2002-04-23 The Boeing Company Making particulates of controlled dimensions by electroplating
US6569310B2 (en) * 2001-02-02 2003-05-27 Clariant Finance (Bvi) Limited Electrochemical process for preparation of zinc powder
US6569311B2 (en) * 2001-02-02 2003-05-27 Clariant Finance (Bvi) Limited Continuous electrochemical process for preparation of zinc powder
US20040007477A1 (en) * 2002-07-09 2004-01-15 Hatch Ltd Recovery and re-use of anode oxygen from electrolytic cells
WO2004024996A1 (en) * 2002-09-12 2004-03-25 Metallic Power, Inc. Method for operating a metal particle electrolyzer
US20040074627A1 (en) * 2002-10-17 2004-04-22 Ravi Verma Method for processing of continuously cast aluminum sheet
US20040108200A1 (en) * 2002-09-12 2004-06-10 Des Jardins Stephen R. Controlled concentration electrolysis system
US20040168922A1 (en) * 2002-09-12 2004-09-02 Smedley Stuart I. Discrete particle electrolyzer cathode and method of making same
US20050098442A1 (en) * 2002-09-12 2005-05-12 Smedley Stuart I. Method of production of metal particles through electrolysis
US20070062030A1 (en) * 1999-11-04 2007-03-22 Richard Sigrist Machine for localised cleaning with an electrolytic cell, for pickling and/or polishing metal surfaces
US20080142374A1 (en) * 2004-08-17 2008-06-19 The Furukawa Electric Co., Ltd. Apparatus For Recovery Metal
US20090045070A1 (en) * 2006-02-06 2009-02-19 Becker Aaron J Cathode for electrolytic production of titanium and other metal powders
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US20100243433A1 (en) * 2009-03-25 2010-09-30 Honda Motor Co., Ltd. Electrical isolation of vehicle body carriers
US20120093680A1 (en) * 2009-03-20 2012-04-19 Przemyslaw Los Method for obtaining copper powders and nanopowders from industrial electrolytes including waste industrial electrolytes
WO2012096728A1 (en) * 2010-12-09 2012-07-19 Flsmidth A/S Continuous electrowinning process and system thereof
WO2012135826A1 (en) * 2011-04-01 2012-10-04 Flsmidth A/S System and process for the continuous recovery of metals
CN109183069A (zh) * 2013-11-19 2019-01-11 艾库伊金属有限公司 连续处理来自铅酸蓄电池的铅材料的方法、以及电解槽
US10316420B2 (en) 2015-12-02 2019-06-11 Aqua Metals Inc. Systems and methods for continuous alkaline lead acid battery recycling
US10689769B2 (en) 2015-05-13 2020-06-23 Aqua Metals Inc. Electrodeposited lead composition, methods of production, and uses
US10793957B2 (en) 2015-05-13 2020-10-06 Aqua Metals Inc. Closed loop systems and methods for recycling lead acid batteries
US11028460B2 (en) 2015-05-13 2021-06-08 Aqua Metals Inc. Systems and methods for recovery of lead from lead acid batteries
WO2023209544A1 (en) * 2022-04-26 2023-11-02 Technische Universiteit Eindhoven Systems and methods for continuous electrolytic production of metals
WO2024020642A1 (en) * 2022-07-28 2024-02-01 Loop Hydrometallurgy Pty Ltd An electrowinning cell and a cathode
RU230894U1 (ru) * 2023-12-05 2024-12-24 Акционерное общество "Кольская горно-металлургическая компания" Катод для получения полутороидальных ронделей

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FR2526446B1 (fr) * 1982-05-06 1986-02-21 Penarroya Miniere Metall Procede et appareil de preparation de metal par electrolyse, notamment de plomb, et demi-produit obtenu par leur mise en oeuvre
DE4400056C1 (de) * 1994-01-04 1995-07-06 Rittel Andreas Elektrolyseapparat
US7709070B2 (en) * 2001-12-20 2010-05-04 The Procter & Gamble Company Articles and methods for applying color on surfaces
RU208678U1 (ru) * 2021-06-24 2021-12-29 Публичное акционерное общество "ГМК "Норильский никель" Катод для получения сферических ронделей
WO2022271052A1 (ru) * 2021-06-24 2022-12-29 Публичное акционерное общество "Горно-металлургическая компания "Норильский никель" Катод с вынесенными контактными площадками для получения сферических ронделей

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US1959376A (en) * 1930-09-26 1934-05-22 Nichols Copper Co Process for producing metal powders
US2805986A (en) * 1952-01-11 1957-09-10 Harold B Law Method of making fine mesh screens
US3414486A (en) * 1966-02-18 1968-12-03 Esb Inc Method for producing flakes of nickel

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US1251302A (en) * 1915-07-06 1917-12-25 Urlyn Clifton Tainton Electrolytic recovery of metals from their solutions.
US1959376A (en) * 1930-09-26 1934-05-22 Nichols Copper Co Process for producing metal powders
US2805986A (en) * 1952-01-11 1957-09-10 Harold B Law Method of making fine mesh screens
US3414486A (en) * 1966-02-18 1968-12-03 Esb Inc Method for producing flakes of nickel
US3419901A (en) * 1966-02-18 1968-12-31 Esb Inc Method for producing flakes of nickel

Cited By (52)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4014756A (en) * 1976-01-21 1977-03-29 Fromson H A Process for making metal powders
DE2711610A1 (de) * 1976-04-01 1977-10-13 Falconbridge Nickel Mines Ltd Wiedergebrauchsfaehige kathodeneinheit, verfahren zum galvanisieren einer kathodeneinheit mit mehreren metallgalvanoschichten sowie kathodisch abgelagertes metallprodukt
US4082641A (en) * 1976-04-01 1978-04-04 Falconbridge Nickel Mines Limited Reusable integrated cathode unit
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FR2218396B1 (enExample) 1978-06-02
JPS49115003A (enExample) 1974-11-02
BR7401168D0 (pt) 1974-11-05
ZA74172B (en) 1974-11-27
FR2218396A1 (enExample) 1974-09-13
GB1406592A (en) 1975-09-17
IT1008282B (it) 1976-11-10
DE2406473B2 (de) 1976-05-06
ZM1574A1 (en) 1974-09-23
AU6443774A (en) 1975-07-17
JPS5610390B2 (enExample) 1981-03-07
SU704464A3 (ru) 1979-12-15
DE2406473A1 (de) 1974-09-05
CA1014890A (en) 1977-08-02

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