US3859185A - Calcium containing lead alloy anodes for electrowinning - Google Patents

Calcium containing lead alloy anodes for electrowinning Download PDF

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US3859185A
US3859185A US44621774A US3859185A US 3859185 A US3859185 A US 3859185A US 44621774 A US44621774 A US 44621774A US 3859185 A US3859185 A US 3859185A
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lead
copper
sulfuric acid
anodes
anode
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Iii Andrew G Hood
David L Adamson
Terrell N Andersen
Kenneth J Richards
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Kennecott Utah Copper LLC
Kennecott Corp
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Kennecott Copper Corp
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Priority to US44621774 priority Critical patent/US3859185A/en
Priority to CA215,897A priority patent/CA1068642A/en
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Publication of US3859185A publication Critical patent/US3859185A/en
Priority to GB729575A priority patent/GB1465232A/en
Priority to AU78496/75A priority patent/AU488637B2/en
Priority to DE19752508538 priority patent/DE2508538A1/en
Priority to JP50023514A priority patent/JPS5814514B2/en
Priority to ZM2475A priority patent/ZM2475A1/en
Assigned to KENNECOTT CORPORATION reassignment KENNECOTT CORPORATION CHANGE OF NAME (SEE DOCUMENT FOR DETAILS). EFFECTIVE MAY 7, 1980. (SEE DOCUMENT FOR DETAILS) Assignors: KENNECOTT COPPER CORPORATION
Assigned to KENNECOTT CORPORATION, 200 PUBLIC SQUARE, CLEVELAND OHIO, 44114, A CORP. OF DE. reassignment KENNECOTT CORPORATION, 200 PUBLIC SQUARE, CLEVELAND OHIO, 44114, A CORP. OF DE. ASSIGNMENT OF ASSIGNORS INTEREST. Assignors: KENNECOTT MINING CORPORATION
Assigned to GAZELLE CORPORATION, C/O CT CORPORATION SYSTEMS, CORPORATION TRUST CENTER, 1209 ORANGE STREET, WILMINGTON, DE., 19801, A DE. CORP. reassignment GAZELLE CORPORATION, C/O CT CORPORATION SYSTEMS, CORPORATION TRUST CENTER, 1209 ORANGE STREET, WILMINGTON, DE., 19801, A DE. CORP. ASSIGNMENT OF ASSIGNORS INTEREST. Assignors: RENNECOTT CORPORATION, A DE. CORP.
Assigned to KENNECOTT UTAH COPPER CORPORATION reassignment KENNECOTT UTAH COPPER CORPORATION CHANGE OF NAME (SEE DOCUMENT FOR DETAILS). JULY 5, 1989 - DE Assignors: GAZELLE CORPORATION
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    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22C—ALLOYS
    • C22C11/00—Alloys based on lead
    • C22C11/02—Alloys based on lead with an alkali or an alkaline earth metal as the next major constituent
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22C—ALLOYS
    • C22C11/00—Alloys based on lead
    • C22C11/08—Alloys based on lead with antimony or bismuth as the next major constituent
    • 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
    • C25C1/12—Electrolytic production, recovery or refining of metals by electrolysis of solutions of copper
    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/20—Recycling

Definitions

  • Electrowinning processes are widely used to recover metallic copper from aqueous electrolyte solutions containing dissolved copper valves.
  • Conventional electrowinning processes for copper utilize anodes made of lead or an alloy of lead and antimony.
  • an aqueous electrolyte solution contains a corrosive material, such as sulfuric acid
  • the lead or lead-antimony alloy anodes are subject to corrosion.
  • Antimonial lead anodes have a generally satisfactory service life when the sulfuric acid concentration in the electrolyte solution is small, i.e., below about 80 grams per liter of sulfuric acid.
  • the present invention constitutes an improvement in the known process of electrowinning copper from an aqueous sulfuric acid electrolyte solution containing copper ions.
  • the improvement comprises utilizing anodes consisting of a lead alloy containing from about 0.025 to about 0.10 percent calcium by weight.
  • lead is meant to include pure lead as well as commercial lead and chemical lead, which usually contains small quantities of copper, silver, nickel, zinc and bismuth. This term is also meant to include lead alloys in which the alloying elements do not eliminate the corrosion resistance provided by the calcium addition.
  • the best mode presently contemplated of carrying out the improved process of the invention comprises immersing at least one anode and at least one cathode in an aqueous, sulfuric acid electrolyte containing dissolved copper values, and impressing an electrical potential across the anodes and cathodes to deposit copper on the cathodes.
  • the anodes consist of an alloy of lead containing from about 0.025 to about 0.10 percent calcium by weight.
  • the calcium-lead alloy which is used in the anodes of this invention can be made in any conventional manner, including the procedure described in detail in U.S. Pat. Nos. 1,890,014 and 2,042,840.
  • the invention is applicable to all conventional processes of electrowinning copper from an aqueous, sulfuric acid electrolyte.
  • the electrolyte solution will contain from about 10 to about 300 grams of I-I SO per liter of solution, and from about 0.5 to about 60 grams of dissolved copper per liter of solution.
  • the electrolyte can be passed through conventional electrowinning cells which contain a large number of alternately disposed cathode and anode sheets wherein the anode sheets are made from a lead-calcium alloy according to this invention.
  • the cathodes can be any of those conventionally used in the electrowinning of copper.
  • the cathodes can be made of stainless steel, titanium, or electrolytically deposited copper.
  • the current density can vary over a generally wide range, such as from about 5 to about amps per square foot, with a voltage drop per electrode pair of approximately 2 volts.
  • the improved process of the present invention is advantageously used in electrowinning copper from dilute, sulfuric acid leach solutions which have been used in leaching copper values from copper-bearing material, such as low grade ores and mine waste dumps.
  • the improved process is particularly advantageous in electrowinning copper from somewhat more concentrated sulfuric acid solutions, as those obtained in multi-step,
  • copper scrap and/or cement copper is initially leached with an aqueous ammonical leaching solution under oxidizing conditions to oxidize the copper values to cupric oxide.
  • the cupric oxide then reacts with ammonium hydroxide in the aqueous ammonical leaching solution to form a soluble copper ammonia complex.
  • the copperpregnant ammonical leach solution is passed to an ion exchange zone, wherein it is contacted with an organic, ion exchange liquid which generally contains a liquid organic ion exchange agent dissolved in a suitable, water immiscible, organic solvent, such as kerosene.
  • a suitable liquid organic ion exchange agent is a substituted 2-hydroxy benzophenoxime, such as taught in U.S. Pat. No. 3,428,449, the entire disclosure of which incorporated herein by reference.
  • the dissolved copper ions are extracted from the aqueous ammonical leach solution by the organic ion exchange agent,'and the organic and aqueous phases are then allowed to separate.
  • the copper-pregnant organic ion exchange agent is thereafter contacted with an aqueous, sulfuric acid solution to strip the majority of the copper therefrom.
  • the aqueous, sulfuric acid solution obtained from the stripping step generally contains from to 300 or more grams per liter of sulfuric acid and from about 20 to about 50 grams per liter of dissolved copper values.
  • Such an ion exchange system can also be utilized to transfer copper ions from a dilute acid leach solution, (such as the dilute sulfuric acid solution mentioned hereinabove) to the more concentrated sulfuric acid solution in a manner similar to that described for transferring copper from an ammonical leach solution to a sulfuric acid solution.
  • a dilute acid leach solution such as the dilute sulfuric acid solution mentioned hereinabove
  • the lead-calcium alloy anodes of this invention have been found to be exceptionally resistant to corrosion even when the electrolyte is one which contains a substantial concentration of sulfuric acid, such as, for example, the electrolyte from the solvent extraction systems discussed above.
  • the copper produced by the process of this invention contains a minimum amount of lead impurities, usually less than 4 parts per million.
  • EXAMPLE A calcium-lead alloy anode was made containing 0.10 weight percent calcium with the balance being essentially lead. Two antimony-lead alloy anodes were also made. One containing 5 weight percent antimony with the balance being lead, and the second containing weight percent antimony and 0.4 weight percent arsenic with the balance being essentially lead. Each of these anodes was approximately 170 cm in area. Each anode was placed into an electrolytic cell so as to be positioned between two cathodes of equal dimensions, with a cathode to anode spacing of one inch. The cathodes were made of copper or titanium metal.
  • An aqueous sulfuric acid electrolyte containing 180 grams per liter of sulfuric acid, 40 grams per liter of dissolved copper, and 2 grams per liter of dissolved iron was introduced into each of the electrolytic cells to submerge the anode and cathodes of each cell in the electrolyte.
  • An electric potential was applied between the anode and cathodes of each cell so that each anode operated under a current density of 16 amps per square foot, with a voltage drop of about 2 volts between the anode and cathodes of each cell.
  • each anode was determined by periodically measuring the weight loss thereof.
  • Each anode exhibited an initial inductance time, that is to say an initial period of time after the anode had been put in service, wherein the weight loss was nil.
  • the induction time a film of PbO formed on the anodes.
  • the corrosion rate, or rate of weight loss was constant.
  • the corrosion rates of the anodes for the period after the initial induction time is shown in the following table.
  • the induction time for each anode and the length of the test of each anode is also shown in the table.
  • the anodes made of the lead-calcium alloys were found to corrode at a rate ofonly 2-3 percent of that of the conventional anodes made of antimony-lead alloys.
  • the life of the lead-calcium anodes would be some 20 to 33 times as long as that of the conventional antimony-lead anodes.
  • a process for electrowinning copper from an aqueous sulfuric acid electrolyte containing dissolved copper values comprising immersing at least one anode and at least one cathode in said electrolyte and impressing an electrical potential across said anode and cathode to deposit copper on said cathode, the anode being a lead alloy containing from about 0.025 to about 0.10 percent calcium by weight.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • Mechanical Engineering (AREA)
  • Electrolytic Production Of Metals (AREA)

Abstract

An improvement in processes for electrowinning copper from aqueous, sulfuric acid solutions comprises utilizing anodes of an alloy of lead and calcium containing from about 0.025 to about 0.1 percent calcium by weight. Anodes of the lead-calcium alloy have exceptionally superior resistance to corrosion in comparison to conventional lead or lead-antimony alloy anodes when used in electrowinning copper from sulfuric acid solutions.

Description

United States Patent Hood, III. et al.
[4 1 Jan.7,1975
CALCIUM CONTAINING LEAD ALLOY ANODES FOR ELECTROWINNING Inventors: Andrew G. Hood, III.; David L.
Adamson; Terrell N. Andersen; Kenneth J. Richards, all of Salt Lake City, Utah Assignee: Kennecott Copper Corporation,
New York, NY.
Filed: Feb. 27, 1974 App]. No.: 446,217
US. Cl 204/108, 204/293, 75/101 BE,
75/117, 75/167 Int. Cl C22d 1/16, BOlk 3/06 Field of Search 204/293, 108; 75/167 References Cited UNITED STATES PATENTS 11/1941 Shoemaker 75/167 11/1966 Jensen 75/167 2/1974 Manko et a1 204/293 Primary ExaminerR. L. Andrews Attorney, Agent, or FirmMallinckrodt & Mallinckrodt [57] ABSTRACT 4 Claims, No Drawings CALCIUM CONTAINING LEAD ALLOY ANODES FOR ELECTROWINNING BACKGROUND OF THE INVENTION 1. Field The invention relates to processes for electrowinning copper from aqueous sulfuric acid solutions containing dissolved copper values.
2. State of the Art Electrowinning processes are widely used to recover metallic copper from aqueous electrolyte solutions containing dissolved copper valves. Conventional electrowinning processes for copper utilize anodes made of lead or an alloy of lead and antimony. When an aqueous electrolyte solution contains a corrosive material, such as sulfuric acid, the lead or lead-antimony alloy anodes are subject to corrosion. Antimonial lead anodes have a generally satisfactory service life when the sulfuric acid concentration in the electrolyte solution is small, i.e., below about 80 grams per liter of sulfuric acid. However, with electrolytes having higher sulfuric acid concentrations, the corrosion of conventional antimonial lead anodes is greatly accelerated, which creates a serious problem not only from the standpoint of high anode replacement costs but also with respect to lead contaminants which are transmitted to the copper deposited at the cathodes.
The alloying of lead with calcium to obtain a hard lead alloy is disclosed in U.S. Pat. Nos. 1,158,681; 1,890,014; 2,042,840; 2,170,650; 2,198,932; and 3,287,165. The hard lead-calcium alloys are taught as being useful in manufacturing electrical cable sheaths, ammunition, and plates in lead storage batteries. In the latter application, the lead-calcium alloy plates were found to be less susceptible to self-discharge which is inherent with conventional lead-antimony alloy plates due to transfer of antimony between the plates of the battery.
SUMMARY OF THE INVENTION The present invention constitutes an improvement in the known process of electrowinning copper from an aqueous sulfuric acid electrolyte solution containing copper ions. The improvement comprises utilizing anodes consisting of a lead alloy containing from about 0.025 to about 0.10 percent calcium by weight. The term lead is meant to include pure lead as well as commercial lead and chemical lead, which usually contains small quantities of copper, silver, nickel, zinc and bismuth. This term is also meant to include lead alloys in which the alloying elements do not eliminate the corrosion resistance provided by the calcium addition.
It has been found that incorporation of small amount of calcium in the lead forms an alloy, which, when used as an anode in electrowinning copper from aqueous sulfuric acid solutions, is remarkably stable and exhibits exceptionally superior resistance to corrosion in comparison to conventional lead or lead-antimony alloy anodes. Further, the use of the lead-calcium alloy anodes results in significant reduction of lead contaminants in the cathode-deposited copper.
DETAILED DESCRIPTION OF THE PREFERRED PROCEDURE The best mode presently contemplated of carrying out the improved process of the invention comprises immersing at least one anode and at least one cathode in an aqueous, sulfuric acid electrolyte containing dissolved copper values, and impressing an electrical potential across the anodes and cathodes to deposit copper on the cathodes. The anodes consist of an alloy of lead containing from about 0.025 to about 0.10 percent calcium by weight. The calcium-lead alloy which is used in the anodes of this invention can be made in any conventional manner, including the procedure described in detail in U.S. Pat. Nos. 1,890,014 and 2,042,840.
The invention is applicable to all conventional processes of electrowinning copper from an aqueous, sulfuric acid electrolyte. Generally, the electrolyte solution will contain from about 10 to about 300 grams of I-I SO per liter of solution, and from about 0.5 to about 60 grams of dissolved copper per liter of solution. The electrolyte can be passed through conventional electrowinning cells which contain a large number of alternately disposed cathode and anode sheets wherein the anode sheets are made from a lead-calcium alloy according to this invention. The cathodes can be any of those conventionally used in the electrowinning of copper. For example, the cathodes can be made of stainless steel, titanium, or electrolytically deposited copper. The current density can vary over a generally wide range, such as from about 5 to about amps per square foot, with a voltage drop per electrode pair of approximately 2 volts.
The improved process of the present invention is advantageously used in electrowinning copper from dilute, sulfuric acid leach solutions which have been used in leaching copper values from copper-bearing material, such as low grade ores and mine waste dumps. The improved process is particularly advantageous in electrowinning copper from somewhat more concentrated sulfuric acid solutions, as those obtained in multi-step,
leach-solvent extraction processes.
In one such multi-step process, copper scrap and/or cement copper is initially leached with an aqueous ammonical leaching solution under oxidizing conditions to oxidize the copper values to cupric oxide. The cupric oxide then reacts with ammonium hydroxide in the aqueous ammonical leaching solution to form a soluble copper ammonia complex. Thereafter, the copperpregnant ammonical leach solution is passed to an ion exchange zone, wherein it is contacted with an organic, ion exchange liquid which generally contains a liquid organic ion exchange agent dissolved in a suitable, water immiscible, organic solvent, such as kerosene. A suitable liquid organic ion exchange agent is a substituted 2-hydroxy benzophenoxime, such as taught in U.S. Pat. No. 3,428,449, the entire disclosure of which incorporated herein by reference. The dissolved copper ions are extracted from the aqueous ammonical leach solution by the organic ion exchange agent,'and the organic and aqueous phases are then allowed to separate. The copper-pregnant organic ion exchange agent is thereafter contacted with an aqueous, sulfuric acid solution to strip the majority of the copper therefrom. The aqueous, sulfuric acid solution obtained from the stripping step generally contains from to 300 or more grams per liter of sulfuric acid and from about 20 to about 50 grams per liter of dissolved copper values. Such an ion exchange system can also be utilized to transfer copper ions from a dilute acid leach solution, (such as the dilute sulfuric acid solution mentioned hereinabove) to the more concentrated sulfuric acid solution in a manner similar to that described for transferring copper from an ammonical leach solution to a sulfuric acid solution.
The lead-calcium alloy anodes of this invention have been found to be exceptionally resistant to corrosion even when the electrolyte is one which contains a substantial concentration of sulfuric acid, such as, for example, the electrolyte from the solvent extraction systems discussed above. In addition, the copper produced by the process of this invention contains a minimum amount of lead impurities, usually less than 4 parts per million.
The invention is further described in connection with the following example which is intended to illustrate the invention but not to limit the scope thereof.
EXAMPLE A calcium-lead alloy anode was made containing 0.10 weight percent calcium with the balance being essentially lead. Two antimony-lead alloy anodes were also made. One containing 5 weight percent antimony with the balance being lead, and the second containing weight percent antimony and 0.4 weight percent arsenic with the balance being essentially lead. Each of these anodes was approximately 170 cm in area. Each anode was placed into an electrolytic cell so as to be positioned between two cathodes of equal dimensions, with a cathode to anode spacing of one inch. The cathodes were made of copper or titanium metal.
An aqueous sulfuric acid electrolyte containing 180 grams per liter of sulfuric acid, 40 grams per liter of dissolved copper, and 2 grams per liter of dissolved iron was introduced into each of the electrolytic cells to submerge the anode and cathodes of each cell in the electrolyte. An electric potential was applied between the anode and cathodes of each cell so that each anode operated under a current density of 16 amps per square foot, with a voltage drop of about 2 volts between the anode and cathodes of each cell.
The corrosion rate of each anode was determined by periodically measuring the weight loss thereof. Each anode exhibited an initial inductance time, that is to say an initial period of time after the anode had been put in service, wherein the weight loss was nil. During the induction time, a film of PbO formed on the anodes. After the induction period, the corrosion rate, or rate of weight loss was constant. The corrosion rates of the anodes for the period after the initial induction time is shown in the following table. The induction time for each anode and the length of the test of each anode is also shown in the table.
As can be seen from the above data, the anodes made of the lead-calcium alloys were found to corrode at a rate ofonly 2-3 percent of that of the conventional anodes made of antimony-lead alloys. Thus, the life of the lead-calcium anodes would be some 20 to 33 times as long as that of the conventional antimony-lead anodes.
The process taking place in the three cells that utilized the three lead-calcium anodes produced copper in which the lead impurity did not exceed 4 parts per million.
Whereas this invention is described herein with respect to certain preferred procedures thereof, it is to be understood that many variations are possible without departing from the inventive concepts particularly pointed out in the following claims.
What we claim is:
1. A process for electrowinning copper from an aqueous sulfuric acid electrolyte containing dissolved copper values comprising immersing at least one anode and at least one cathode in said electrolyte and impressing an electrical potential across said anode and cathode to deposit copper on said cathode, the anode being a lead alloy containing from about 0.025 to about 0.10 percent calcium by weight.
2. A process in accordance with claim 1, wherein the anode consists of from about 0.025 to 0.1 percent calcium by weight, with the remainder being lead.
3. A process in accordance with claim 1, wherein the aqueous sulfuric acid electrolyte contains from about 10 to about 300 grams per liter of sulfuric acid.
4. A process in accordance with claim 3, wherein the electrolyte contains at least 10 grams per liter of sulfuric acid.

Claims (4)

1. A PROCESS FOR ELECTROWINNING COPPER FROM AN AQUEOUS SULFURIC ACID ELECTROLYTE CONTAINING DISSOLVED COPPER VALUES COMPRISING IMMERSING AT LEAST ON ANODE AND AT LEAST ONE CATHODE IN SAID ELECTROLYTE AND IMPRESSING AN ELECTRICAL POTENTIAL ACROSS SAID ANODE AND CATHODE TO DEPOSIT COPPER ON SAID CATHODE, THE ANODE BEING A LEAD ALLOY CONTAINING FROM ABOUT 0.025 TO ABOUT 0.10 PERCENT CALCIUM BY WEIGHT.
2. A process in accordance with claim 1, wherein the anode consists of from about 0.025 to 0.1 percent calcium by weight, with the remainder being lead.
3. A process in accordance with claim 1, wherein the aqueous sulfuric acid electrolyte contains from about 10 to about 300 grams per liter of sulfuric acid.
4. A process in accordance with claim 3, wherein the electrolyte contains at least 10 grams per liter of sulfuric acid.
US44621774 1974-02-27 1974-02-27 Calcium containing lead alloy anodes for electrowinning Expired - Lifetime US3859185A (en)

Priority Applications (7)

Application Number Priority Date Filing Date Title
US44621774 US3859185A (en) 1974-02-27 1974-02-27 Calcium containing lead alloy anodes for electrowinning
CA215,897A CA1068642A (en) 1974-02-27 1974-12-12 Calcium containing lead alloy anodes for electrowinning copper
GB729575A GB1465232A (en) 1974-02-27 1975-02-21 Process for electrowinning copper
AU78496/75A AU488637B2 (en) 1974-02-27 1975-02-24 Process for electrowinning copper
ZM2475A ZM2475A1 (en) 1974-02-27 1975-02-27 Calcium containing lead alloy anodes for electrowinning
JP50023514A JPS5814514B2 (en) 1974-02-27 1975-02-27 How do you do your job?
DE19752508538 DE2508538A1 (en) 1974-02-27 1975-02-27 PROCESS FOR ELECTROLYTIC EXTRACTION OF COPPER

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4124482A (en) * 1974-11-22 1978-11-07 Knight Bill J Method and apparatus for casting anodes
US4272339A (en) * 1980-03-10 1981-06-09 Knight Bill J Process for electrowinning of metals
FR2492415A1 (en) * 1980-10-20 1982-04-23 Samim Spa

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2264251A (en) * 1940-07-24 1941-11-25 Robert J Shoemaker Lead alloy bearing metal
US3287165A (en) * 1964-12-03 1966-11-22 Eltra Corp High capacity lead acid battery with lead calcium negative grids
US3794570A (en) * 1972-08-11 1974-02-26 Alpha Metals Electroplating chromium with a nonconsumable chrome plating anode

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2264251A (en) * 1940-07-24 1941-11-25 Robert J Shoemaker Lead alloy bearing metal
US3287165A (en) * 1964-12-03 1966-11-22 Eltra Corp High capacity lead acid battery with lead calcium negative grids
US3794570A (en) * 1972-08-11 1974-02-26 Alpha Metals Electroplating chromium with a nonconsumable chrome plating anode

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4124482A (en) * 1974-11-22 1978-11-07 Knight Bill J Method and apparatus for casting anodes
US4272339A (en) * 1980-03-10 1981-06-09 Knight Bill J Process for electrowinning of metals
WO1981002589A1 (en) * 1980-03-10 1981-09-17 B Knight Process for electrowinning of metals
FR2492415A1 (en) * 1980-10-20 1982-04-23 Samim Spa

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ZM2475A1 (en) 1975-12-22
CA1068642A (en) 1979-12-25
JPS50157220A (en) 1975-12-19
GB1465232A (en) 1977-02-23
DE2508538A1 (en) 1975-08-28
JPS5814514B2 (en) 1983-03-19
AU7849675A (en) 1976-08-26

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