US3865703A - Electrowinning with an anode having a multicomponent coating - Google Patents

Electrowinning with an anode having a multicomponent coating Download PDF

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Publication number
US3865703A
US3865703A US352417A US35241773A US3865703A US 3865703 A US3865703 A US 3865703A US 352417 A US352417 A US 352417A US 35241773 A US35241773 A US 35241773A US 3865703 A US3865703 A US 3865703A
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United States
Prior art keywords
percent
anode
metal oxide
group
solution
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US352417A
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Barry A Schenker
James M Kolb
Charles R Franks
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ELECTRODE Corp A CORP OF
Diamond Shamrock Chemicals Co
Diamond Shamrock Corp
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Diamond Shamrock Corp
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Priority to US352417A priority Critical patent/US3865703A/en
Priority to CA195,004A priority patent/CA1037416A/en
Priority to BR3076/74A priority patent/BR7403076D0/pt
Priority to IT50461/74A priority patent/IT1004477B/it
Priority to DE2418741A priority patent/DE2418741B2/de
Priority to SE7405201A priority patent/SE405868B/xx
Priority to GB1710874A priority patent/GB1398378A/en
Priority to JP49043492A priority patent/JPS5011906A/ja
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Publication of US3865703A publication Critical patent/US3865703A/en
Assigned to DIAMOND SHAMROCK CHEMICALS COMPANY reassignment DIAMOND SHAMROCK CHEMICALS COMPANY CHANGE OF NAME (SEE DOCUMENT FOR DETAILS). (SEE DOCUMENT FOR DETAILS), EFFECTIVE 9-1-83 AND 10-26-83 Assignors: DIAMOND SHAMROCK CORPORATION CHANGED TO DIAMOND CHEMICALS COMPANY
Assigned to ELTECH SYSTEMS CORPORATION reassignment ELTECH SYSTEMS CORPORATION ASSIGNMENT OF ASSIGNORS INTEREST. Assignors: DIAMOND SHAMROCK CORPORATION, 717 N. HARWOOD STREET, DALLAS, TX 75201
Assigned to ELECTRODE CORPORATION, A CORP. OF DE reassignment ELECTRODE CORPORATION, A CORP. OF DE ASSIGNMENT OF ASSIGNORS INTEREST. Assignors: ELTECH SYSTEMS CORPORATION
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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
    • C25C1/00—Electrolytic production, recovery or refining of metals by electrolysis of solutions
    • 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

Definitions

  • ores, ore concentrates, and other materials containing compounds of the desired metals are leached with acids, usually sulfuric acid, and the leach liquor, after upgrading if necessary, is then electrolyzed between an insoluble anode and a cathode, the latter often being of the same metal as that to be deposited.
  • anodes In such processes, large amounts of oxygen are evolved at the anode and contribute to the chemical and mechanical attrition of same. Thus, anodes must be resistant in this respect and must also have a low oxygen overvoltage to ensure economical operation from a standpoint of electrical consumption. Perhaps most typically used for this purpose are lead and lead alloy anodes. Lead anodes nevertheless still have a definite wear-rate, and hence a limited life, and lead to contamination of the cathode deposit with small amounts of lead. Thus, the search had continued for anode materials having a suitable chemical and mechanical resistance coupled with the requisite low oxygen overvoltage.
  • Such a process has the advantagcs ol' anodic oxygen evolution at a low oxygen overvoltage, thereby contributing to electrical efficiency; long operation without anode passivation; and substantially no contamination of the cathode deposit by metals dissolved from the anode.
  • anode passivation it is intended to refer to an increase in operating voltage to a value at which operation no longer may be considered practical (e.g., 8 volts) brought about to a substantial extent by the evolution of oxgen at an anodic surface with consequent formation of nonconductive oxides.
  • the invention encompasses the deposition of metals from aqueous acidic solutions by passing an electrolyzing current through said solution between at least one cathode and a specific, opposed anode within an electrolytic cell.
  • the: cell itself need comprise little more than an open box, usually rectangular. in shape, with the appropriate inlets, outlets, and electrical current conductors and distributors.
  • Such cells may be constructed of any suitably resistant material. for example, PVC-lined concrete.
  • the cathode may be of the same metal as that to be won or may be different and may have any configuration suitable to the process and cell design, e.g., a metallic sheet provided with electrically conductive means (hooks) to depend same from a current collecting bar traversing the cell.
  • a metallic sheet provided with electrically conductive means (hooks) to depend same from a current collecting bar traversing the cell.
  • a variety of metals may be won from solution according to the practice of the present invention, including cobalt, zinc, iron, manganese, chromium, nickel, copper, and cadmium. While the specific details of operation depend upon the metal to be deposited, as is de' scribed more fully hereinbelow, generally operation is at a pH of less than 7, and preferably less than 4. This acidity is contributed by the acid used to leach the metals into solution from ores or other materials containing compounds of same, which acid is usually regenerated in the electrolytic process. Obviously, a large excess of acid is uneconomical and corrosive.
  • the temperature range of the process may be between room temperature and the boiling point of the solution in question. While higher temperatures lower the electrical resistivity of the solution, operation at elevated temperatures contributes to a lower current efficiency, excessive evaporation, and exaggerates the effect of impurities in the solution upon the metal being deposited. Therefore, it is necessary to strike a balance between these considerations and operate somewhat above room temperature but considerably below boil' ing, this often requiring the provision of cooling means.
  • the invention contemplates the use of any of the additive materials conventional to electrowinning appli cations and useful in reducing'the roughness of the deposit with increasing thickness, in reducing the effect ofimpurities on the electrical efficiency, and/or in providing a demisting foam blanket on the surface of the electrolyte.
  • the solutions to be treated are prepared by leaching ores, ore concentrates, metallurgical byproducts, and the like, with an aqueous acid, usually sulfuric, followed in many instances by purification (e.g., cementation), especially if the undesired metals in solution are more noble than the metal to be won.
  • the solution is then ready for electrolysis using the anodes according to the present invention.
  • a critical feature of the present invention is the use of a particular anode which, as mentioned above, is a conductive substrate bearing on at least a portion of the surface thereof a coating of mixed oxides of tin, antimony, at least one platinum group metal, and a valve metal selected from the group titanium and tantalum.
  • the conductive substrate is preferably titanium, although tantalum, niobium, and zirconium may also be employed. ln addition, a covering of one of the aforementioned metals over a more conductive material, such as copper or aluminum, may be used. Further, layers on the substrate intermediate the base metal and the coating, such as those described in U.S. Pat. No. 3,71 1,397, are contemplated.
  • the configuration of the substrate may vary considerablybut is generally in the form of rods or an imperforate or foraminous metal sheet, e.g., of titanium metal.
  • stannic oxide preferably present in the form of crystalline SnO and employed within the range of from 30 to 90, especially 30 to 50, percent by weight of the total coating composition.
  • the antimony oxide component enters into the tin oxide crystal lattice, rendering same more electrically conductive.
  • the antimony is present in an indeterminate oxide form owing to its entrance into the stannic oxide crystal lattice, it is expressed for convenience sake as Sb O
  • the antimony oxide is present within the range from 1.0 to 10, preferably 4.0 to 8.0, percent by weight.
  • tin and antimony oxides are further qualified by the proviso that they be present, respectively, in the range, on a mole ratio basis, of 95:5 to 85:15, especially 90:10. In this fashion, there is obtained the desired doping effect of the antimony on the tin oxide without the presence of an excess separate phase of antimony oxide.
  • the third component of the mixed coating is at least one platinum group metal oxide," by which term it is intended to include the oxides of platinum, palladium, ruthenium, iridium, rhodium, and osmium, especially those of ruthenium and iridium. These platinum group metal oxides are present for the most part in their most highly oxidized state and within the range of from L to 50, especially 20 to 40, percent by weight.
  • An especially preferred anode is one the coating of which contains a combination of Ru0 and [r0 or rhodium oxide.
  • the final component is a valve metal oxide selected from the group consisting oftitanium and tantalum oxides.
  • the titanium is present in the form of TiO and is essentially crystalline (rutile) in nature
  • tantalum is employed, as in the preferred embodiment, a generally amorphous tantalum oxide results. Therefore, although it is expressed as Ta O it is understood that mixtures of tantalum oxides may in fact be present.
  • the amounts of valve metal oxide employed are generally within the range of from 0.5 to 30 percent by weight, especially to 25.
  • a preferred electrode comprises a titanium substrate bearing a coating containing about 47 percent SnO 5 percent Sb O 23.5 percent RuO 4.5 percent ho and percent Ta O
  • the preferred method of preparing the multicomponent coating composition on the titanium substrate is by deposition from a solution of the appropriate thermochemically decomposable salts. For example, it is desirable to paint or brush an acidified alcoholic solution of said salts onto the substrate followed by drying at l00-l40C for from 3 to 10, especially 5, minutes and finally by baking in an oxidizing atmosphere, e.g., air, at 450 to 520C, especially 500C, for from 5 to 10, especially about 7, minutes.
  • an oxidizing atmosphere e.g., air
  • the preferred solvents for the thermally decomposable salts are the lower alkanols such as ethanol, propanol, amyl alcohol, and especially n-butyl alcohol, although other solvents including water may be employed.
  • an acid such as hydrochloric acid.
  • concentration of the metals in the solution from which the coating composition is to be derived ranges between about 50 to 200 grams per liter.
  • the salts employed are generally any thermally decomposable inorganic or organic salt or organic ester of the metals in question such as the chlorides, nitrates, alkoxides, alkoxy halides, resinates, amines, and the like.
  • Specific and illustrative examples include potassium hexachloroplatinate, hexachloroiridic acid, ruthenium trichloride or tribromide, orthobutyl titanate, antimony trichloride or pentachloride, and stannic chloride or dibutyl tin dichloride.
  • preformed oxides of the various component metal and salts of the remaining materials although it is generally believed that preformed valve metal oxides should not be employed nor should separately preformed'tin and antimony oxides be used.
  • thermal decomposition is incomplete, small amounts of salts may remain without detrimental effect in the coating, for example.
  • small amounts of chloride in the primarily oxide coat Perhaps most exemplary of the process of the present invention is the electrowinning of copper from an aqueous solution comprising copper sulfate and sulfuric acid employing a copper sheet cathode and anode according to the present invention.
  • electrolysis During electrolysis, generally occuring at a current density within the range of 15 to amperes per square foot, sulfuric acid is regenerated and copper is deposited at the cathode.
  • the pH of the electrolyte will range from less than 1 up to about 2.0 and a temperature of 30 to 65C is most commonly employed.
  • concentration of the electrolyte In order to obtain a chemically pure, physically dense, and adherent cathode deposit, the concentration of the electrolyte must be controlled, as severe depletion cannot be allowed.
  • a typically advantageous amount of copper in the solution is within the range of 25 to 50 grams per liter. Of course, the presence or absence of other metals will depend upon the nature of the material leached.
  • electrolysis is generally of a zinc sulfate solution that has usually been purified to some extent by a cementation reaction.
  • electrolysis is of a solution containing from 40 to 50 gpl zinc at a pH of from less than 1.0 to about 2.0 and a temperature within the range of 30 to 40C.
  • aluminum cathodes may again be employed in the electrolysis of a solution containing from 100 to 200 gpl cadmium at a pH of from less than 1 to about 1.5, a temperature within the range of 20 to 35C and at a current density of 4 to 10 asf.
  • An anode coating solution is prepared from 45 ml ethanol, 4.5 g TaCl 1.1 g SbCl 15.1 g SnCl .5H O, and 7.6 g RuCl .xH- O (38Ru).
  • An etched titanium l f i chrome; 3: fgb g 5 mesh substrate is coated by brushing, drying at 1 10, C zzg z hggf xg i 5 e Ca for 3 minutes, and baking at 500 C for 7 minutes.
  • the y p n um epo coating procedure is repeated until a coating having a ally on a stainless steel cathode at a current denslty ruthemum content of 1 gram per square foot is obwithin the range of 45 to 70 asf and a temperature on l o O tamed. This is labeled Anode 4. theorderof50 to60C.
  • Electrowinning of manganese likewise takes lace in .110 e prepare m an entlca] ashlon but Submtutmg 0.92 g of lrCl and 6.54 g RuCl .xl-l O for the rua diaphragm type cell employing a feed contalnmg bethemum content of Anode 4.
  • Anode 6 is likewise simitween and gpl manganese as manganese sulfate lar with th ex th I l 28 f Rhcl 3H 0 d together with ammonium sulfate.
  • Sulfuric acid is again regenen eye as e .ectiowmnmg es i evd ermed in the anolyte compartment.
  • Exam- Further processes include the electrowinning of cok 1 above Anodes and 6 have f l f respeci bah (15 50 gpl CO PH l.5 7.0 5 o o and 3O 4O t1vely,of 185, 250, and 350 hours. Th1s indlcates the asf) and nickel (50:10 gpl, pH 304.5 0 0 and 1mproved operation possible employing a mixture of 1540 as precious metal oxides in the coating.
  • a coating consisting essentially of from resultant solution is brushed onto an expanded titanium I 10 Percent n im ny oxide, as z al On Weight mesh substrate previously cleaned by etching for 30 basis, from 30 t0 90 Percent 2 from to 50 P minutes in boiling (l8%) aqueous hydrochloric acid.
  • c of at least 0118 Platinum g p metal OXide, 21nd The solution is applied to the mesh by brushing, folfrom 15 to 25 percent of a valve metal oxide selected lowed by drying the anode for 3 minutes at l 10C and from the group consisting of titanium and tantalum oxfiring in air at 500C for 7 minutes.
  • the test is continued until consists essentially of from 4.0 to 8.0 percent Sbg03, the anodes have passivated, i.e., a voltage of 8.0 volts from 30 to 50 percent SnO from 20 to 40 percent of or greater is obtained.
  • the lifetime of the anode, that at least one platinum metal oxide, and from 15 to 25 the umbe Of hours of Successful operation until percent ofa valve metal oxide selected from the group passivation occurs, is reported in the following table. consisting of titanium and tantalum oxides.
  • a process for winning copper from an acidic aque processes wherein an acidic aqueous electrolyte is to be ous copper sulfate solution, which process comprises treated can be operated for extended periods of time employing anodes within the definition of the present invention.
  • anode comprises an electrically conductive supporting substrate bearing on at least a portion of the surface thereof a coating consisting essentially of from 1.0 to 10 percent antimony oxide, as Sb O on a weight basis, from 30 to 90 percent SnO from 1.0 to 50 percent of at least one platinum group metal oxide, and from to 25 percent ofa valve metal oxide selected from the group consisting of titanium and tantalum oxides, with the proviso that the mole ratio of tin to antimony oxides is between 95:5 and 85:15.

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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)
  • Electrodes For Compound Or Non-Metal Manufacture (AREA)
US352417A 1973-04-19 1973-04-19 Electrowinning with an anode having a multicomponent coating Expired - Lifetime US3865703A (en)

Priority Applications (8)

Application Number Priority Date Filing Date Title
US352417A US3865703A (en) 1973-04-19 1973-04-19 Electrowinning with an anode having a multicomponent coating
CA195,004A CA1037416A (en) 1973-04-19 1974-03-14 Electrowinning with an anode having a multicomponent coating
BR3076/74A BR7403076D0 (pt) 1973-04-19 1974-04-17 Aperfeicoamento em processo de eletroproducao de metais
DE2418741A DE2418741B2 (de) 1973-04-19 1974-04-18 Anode für die elektrolytische Gewinnung von Metallen aus deren wäßrigen Lösungen
SE7405201A SE405868B (sv) 1973-04-19 1974-04-18 Anod for anvendning vid elektrolytisk utvinning av metaller fran suravattenhaltiga losningar
GB1710874A GB1398378A (en) 1973-04-19 1974-04-18 Electrowinning of metal
IT50461/74A IT1004477B (it) 1973-04-19 1974-04-18 Procedimento elettrolitico per il recupero di metalli da soluzioni acquose acide
JP49043492A JPS5011906A (enrdf_load_stackoverflow) 1973-04-19 1974-04-19

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US352417A US3865703A (en) 1973-04-19 1973-04-19 Electrowinning with an anode having a multicomponent coating

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US3865703A true US3865703A (en) 1975-02-11

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US352417A Expired - Lifetime US3865703A (en) 1973-04-19 1973-04-19 Electrowinning with an anode having a multicomponent coating

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US (1) US3865703A (enrdf_load_stackoverflow)
JP (1) JPS5011906A (enrdf_load_stackoverflow)
BR (1) BR7403076D0 (enrdf_load_stackoverflow)
CA (1) CA1037416A (enrdf_load_stackoverflow)
DE (1) DE2418741B2 (enrdf_load_stackoverflow)
GB (1) GB1398378A (enrdf_load_stackoverflow)
IT (1) IT1004477B (enrdf_load_stackoverflow)
SE (1) SE405868B (enrdf_load_stackoverflow)

Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3940323A (en) * 1974-08-02 1976-02-24 Hooker Chemicals & Plastics Corporation Anode for electrolytic processes
US3943042A (en) * 1974-08-02 1976-03-09 Hooker Chemicals & Plastics Corporation Anode for electrolytic processes
US3951766A (en) * 1974-08-02 1976-04-20 Hooker Chemicals & Plastics Corporation Electrolytic cell and method of using same
US3956083A (en) * 1974-08-02 1976-05-11 Hooker Chemicals & Plastics Corporation Electrochemical anode and process using the anode
US4061558A (en) * 1975-06-09 1977-12-06 Tdk Electronics Co., Ltd. Electrode
US4067783A (en) * 1977-03-21 1978-01-10 Bell Telephone Laboratories, Incorporated Gold electroplating process
US4213843A (en) * 1978-03-24 1980-07-22 Permelec Electrode Ltd. Electrolysis electrodes and method of making same
US4422917A (en) * 1980-09-10 1983-12-27 Imi Marston Limited Electrode material, electrode and electrochemical cell
DE3731285A1 (de) * 1987-09-17 1989-04-06 Conradty Metallelek Dimensionsstabile anode, verfahren zu deren herstellung und verwendung derselben
US5227032A (en) * 1991-09-24 1993-07-13 The United State Of America As Represented By The Administrator Of The National Aeronautics And Space Administration Method for producing oxygen from lunar materials
US7781679B1 (en) * 2005-09-09 2010-08-24 Magnecomp Corporation Disk drive suspension via formation using a tie layer and product
CN116102124A (zh) * 2022-12-14 2023-05-12 上海电力大学 一种铜/锌/锑共掺杂的钛基-二氧化锡阳极材料及其制备和应用

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5263176A (en) * 1975-11-20 1977-05-25 Hodogaya Chem Co Ltd Anode for electrolysis
US4040939A (en) * 1975-12-29 1977-08-09 Diamond Shamrock Corporation Lead dioxide electrode
CA2203410C (en) * 1995-08-28 2001-12-18 Yosuke Hoshijima Process for vacuum refining molten steel and apparatus therefor

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3701724A (en) * 1968-10-18 1972-10-31 Ici Ltd Electrodes for electrochemical processes
US3775284A (en) * 1970-03-23 1973-11-27 J Bennett Non-passivating barrier layer electrodes

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3853479A (en) * 1972-06-23 1974-12-10 Sherwood Medical Ind Inc Blood oxygenating device with heat exchanger
JPS4938411A (enrdf_load_stackoverflow) * 1972-08-15 1974-04-10

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3701724A (en) * 1968-10-18 1972-10-31 Ici Ltd Electrodes for electrochemical processes
US3775284A (en) * 1970-03-23 1973-11-27 J Bennett Non-passivating barrier layer electrodes

Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3940323A (en) * 1974-08-02 1976-02-24 Hooker Chemicals & Plastics Corporation Anode for electrolytic processes
US3943042A (en) * 1974-08-02 1976-03-09 Hooker Chemicals & Plastics Corporation Anode for electrolytic processes
US3951766A (en) * 1974-08-02 1976-04-20 Hooker Chemicals & Plastics Corporation Electrolytic cell and method of using same
US3956083A (en) * 1974-08-02 1976-05-11 Hooker Chemicals & Plastics Corporation Electrochemical anode and process using the anode
US4061558A (en) * 1975-06-09 1977-12-06 Tdk Electronics Co., Ltd. Electrode
US4067783A (en) * 1977-03-21 1978-01-10 Bell Telephone Laboratories, Incorporated Gold electroplating process
US4213843A (en) * 1978-03-24 1980-07-22 Permelec Electrode Ltd. Electrolysis electrodes and method of making same
US4422917A (en) * 1980-09-10 1983-12-27 Imi Marston Limited Electrode material, electrode and electrochemical cell
DE3731285A1 (de) * 1987-09-17 1989-04-06 Conradty Metallelek Dimensionsstabile anode, verfahren zu deren herstellung und verwendung derselben
US5227032A (en) * 1991-09-24 1993-07-13 The United State Of America As Represented By The Administrator Of The National Aeronautics And Space Administration Method for producing oxygen from lunar materials
US7781679B1 (en) * 2005-09-09 2010-08-24 Magnecomp Corporation Disk drive suspension via formation using a tie layer and product
US20100230144A1 (en) * 2005-09-09 2010-09-16 Magnecomp Corporation Disk drive suspension via formation using a tie layer and product
CN116102124A (zh) * 2022-12-14 2023-05-12 上海电力大学 一种铜/锌/锑共掺杂的钛基-二氧化锡阳极材料及其制备和应用

Also Published As

Publication number Publication date
DE2418741A1 (de) 1974-11-07
SE405868B (sv) 1979-01-08
IT1004477B (it) 1976-07-10
BR7403076D0 (pt) 1974-11-19
DE2418741B2 (de) 1979-09-27
CA1037416A (en) 1978-08-29
GB1398378A (en) 1975-06-18
JPS5011906A (enrdf_load_stackoverflow) 1975-02-06

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