US3528896A

US3528896A - Process for electrochemically cleaning and brightening copper alloy and brass strip

Info

Publication number: US3528896A
Application number: US721936A
Authority: US
Inventors: Charles Davidoff; Albert E Howe; Sheldon W Dean
Original assignee: Olin Corp
Current assignee: Olin Corp
Priority date: 1968-04-17
Filing date: 1968-04-17
Publication date: 1970-09-15
Anticipated expiration: 1987-09-15
Also published as: JPS4939737B1; CA922265A; SE340929B; DE1919365A1; FR2006374A1; GB1196395A

Description

United States Patent 3,528,896 PROCESS FOR ELECTROCHEMICALLY CLEAN- ING AND BRIGHTENING COPPER ALLOY AND BRASS STRIP Charles Davidoff, Manhasset, N.Y., Albert E. Howe, Columbus, Ohio, and Sheldon W. Dean, Hamden, Conn., assignors to Olin Corporation, a corporation of Virginia No Drawing. Filed Apr. 17, 1968, Ser. No. 721,936 Int. Cl. C23b 1/00 US. Cl. 204-141 15 Claims ABSTRACT OF THE DISCLOSURE A process for cleaning cooper alloy strip is provided comprising soaking the strip in an electrolyte solution of polyphosphate and organic hydroxycarboxylic acid, and making the strip the anode in an electrochemical cell, the electrolyte in said cell being a solution of polyphosphate and organic hydroxycarboxylic acid.

The usual process for cleaning and brightening copper alloy strip either in process or at finish gauge involves immersing the strip in solutions of sulfuric acid, sulfuric acid plus chromic acid (or sodium dichromate) or, in some cases, sodium cyanide. These solutions are very corrosive, toxic and present problems in disposal when they are spent. Furtherfore, strip treated with these solutions is frequently not cleaned uniformly and -will often develop stains rapidly after cleaning.

It is an object of the present invention to provide a process for cleaning copper alloys and brass strip rapidly and completely to produce an attractive uniform surface while dissolving only a miniscule quantity of metal.

It is another object of the present invention to produce a passive surface on these alloys which has some resistance to tarnishing.

Another object of the present invention is to avoid the use of toxic, corrosive, or expensive chemicals and alleviate the problems of corrosion and the danger of handling toxic chemicals.

It is another object of the present invention to provide a solution which can be regenerated continuously and, therefore, never need to be dumped, and, thus, ease the problems of waste disposal and stream pollution.

The foregoing objects are achieved in a two-step process.

The first step is a soaking operation in which the stained strip is exposed to the electrolyte solution. The electrolyte soaks through the stains and appears to soften the stain.

The second step is an electrochemical stepin which the strip is made the anode in a cell with controlled flow. A small quantity of metal under the stain dissolves so that the stain or oxide is no longer attached to the metal. Then a reaction occurs between the electrolyte and the anodic strip which forms an extremely thin, transparent, passive layer on the metal.

The strip then leaves the bath and is rinsed, dried and coiled.

The electrolyte which is used in both the soaking and electrochemical steps is a solution of polyphosphate and organic hydroxycarboxylic acid. The pH of this solution should be adjusted to be between 6.0 and 9.0 with 8.0 as a preferred operating value. The electrochemical cleaning process does not proceed when the pH exceeds 9.0 and the polyphosphates are not sufiiciently stable below pH 6 0.

Any polyphosphate including pyrophosphate, tripolyphosphate, tetrapolyphosphate, etc., can be used for this solution, but the sodium pyrophosphate is preferred.

The concentration of polyphosphate shoud be between 50 and grams per liter of anhydrous phosphate radical. For anhydrous tetrasodium pyrophosphate, this is approximately equivalent to a range of 75 to 140 grams per liter. The preferred concentration of sodium pyrophosphate is approximately grams per liter.

The hydroxycarboxylic organic acid for the solution includes citric, tartaric, glycolic, gluconic, and sugar acids. Citric acid is preferred. Because pH adjustment is necessary, it is desirable to add equal weights of citric acid and sodium citrate. If this is done, then the pH will need little or no adjustment. The concentration range of citric acid and sodium citrate is from 10 grams to 60 grams per liter each. The exact concentration chosen is based on other process requirements as discussed below.

The electrolyte temperature should be in the range of 4080 C. Low temperatures are undesirable because the voltage requirements are higher and pyrophosphate tends to crystallize out at lower temperatures. On the other hand, high temperatures produce excessive evaporation and require excessive heat inputs to maintain temperature. The preferred operating temperature range is 60- 70 C.

The soaking time requirement is dependent largely upon the type of stain present. Heavy or dense stains require soak times up to 60 seconds, while light stains need only 2-10 seconds. Most industrial strip can be cleaned adequately with less than 30-second soaks. The electrochemical step in the process is critical to produce a satisfactory surface. The electrolyte must flow past the strip during treatment at a uniform velocity determined by the equations given below. The current density J of the anodic treatment must be set between the limits shown by these equations:

where I max. is the maximum current density in amps per square inch; J min. is the minimum current density in amps per square inch; V is the fluid velocity in feet per second and may vary from 2 to 15; Vs is the strip velocity in feet per second and may vary from 0 to 10; and Cl is the concentration of sodium citrate and citric acid in the electrolyte expressed in grams per liter.

In these equations, the velocity terms represent vectorial quantities and so the velocity difference shown must be the magnitude of the vectorial velocity difference. Furthermore, these equations apply only to well-developed turbulent flow and so appropriate corrections must be made when considering any other flow regime situation. Wall shear is the important criteria in these relations.

If the current density exceeds the maximum set by these equations, then a brown or red stain or deposit will appear on the metal surface and the metal will not be clean. On the other hand, if the current density is too low, then the metal surface will be etched and cleaning will again be unsatisfactory. In the range specified, the cleaning rate is optimum and the metal acquires a bright, passive surface.

For some alloys, the minimum current density is lower than that shown. This group of alloys includes the alloys of copper and tin, and also of copper and aluminum. For these alloys, the minimum current density is about one third the value calculated from Equation 2.

The citrate is consumed by an electrochemical oxidation reaction in this process. This reaction is necessary to produce the desirable cleaning and passivation which results from this process. However, it is necessary to add citrate to the bath to make up that consumed in the reaction.

The voltage requirement of this process is dependent upon a number of factors including: the cathode material, cathode-anode ray ratio, alloy being cleaned, current density, electrolyte temperature, and composition and resistances in the external circuitry.

More specifically, this voltage is given by an expression of the form:

where V is the applied voltage in volts; V is a constant voltage determined by the alloy in volts; a, b and c are constants and may vary respectively from 0.01 to 2.0, 0.01 to 1.00, and 0.1 to 3.0; p is the electrical resistivity of the allow and is from 10 to 100 ohms mil ft. for copper and copper alloys; g is the gauge of the strip; w is the width of the strip; and J is the current density in amps per square inch.

The constants a and b are determined by the external circuit and C is determined by the electrochemical cell para-meters.

The treatment time in the electrochemical portion of the process is dependent upon the nature of the stain present and upon the current density used. This treatment time is therefore given by Equation 4:

where t is the treatment time in seconds; ml is the extent of treatment in coulombs per square inch; and J is the current density in amps per square inch.

For most industrial strip, in is approximately coulombs per square inch, although in cases of heavy stains, annealing oxides, etc., In should be increased to values between and 20 for adequate cleaning.

This process will dissolve copper and other alloying elements into the electrolyte. As time goes on, the electrolyte will become less effective because of these heavy metals in solution. Therefore, it is desirable to keep the copper concentration of the electrolyte below 3 grams per liter and other alloying element concentrations below 5 grams per liter total.

This can be accomplished by plating these elements out in a regeneration cell composed of cathode starter sheets and stainless steel anodes. The electrode sheets should be hung vertically in this regeneration and should be at least two feet long in the vertical direction. The current density in this regenerator should be maintained between about 1 and 20 ams per square foot and will vary according to the concentration of heavy metals in the electrolyte.

The zinc content of the metal deposited on the cathodes will be given by Equation 5:

where Zn is the present zinc in the deposit; and J is the regenerator cathode current density in a-mperes per square foot.

Equation 5 holds when the zinc content of the electrolyte is about 3 grams per liter and the copper content is 1.5 grams per liter and the temperature is 50-60" C., and the current density is between 4 and 10 amps per square foot. If the copper concentration of the electrolyte exceeds 1.5 grams per liter, the copper content of the deposit would be greater than predicted, and if it falls below 1.5 grams per liter, current efliciency of the cell would fall off. If the zinc content falls below the 3 grams per liter, the zinc content of the deposit would be lower than predicted. This behavior can be used to control the elecelectrolyte composition accurately while recovering the heavy metal values from the electrolyte.

If zinc is not present in the electrolyte, heavy metals, for example, including Fe, Pb, Sn, Ni, Co and Mn can be removed from the solution by operating the regenerator at current densities of 1 to 20 amperes per square foot. However, most heavy metals can be removed with current densities of 2 to 6 amps per square foot with heavy metal concentrations up to about 5 grams per liter.

The following examples illustrate the invention without limiting its scope:

Example I.Cleaning an alloy 260 brass strip An apparatus was constructed to treat coils of brass strip.

The strip was first immersed in a tank with an immersive length of about 7 feet. Then the strip passed over a 3-foot diameter roller on which the electrochemical treatment was carried out. A curved stainless steel cathode, 30 inches long, was placed over the roller so that the distance between the cathode and the strip was inch uniformly over its length and width. The electrolyte was pumped from a nozzle in this cathode-anode space, such that its velocity was opposed to that of the strip.

A volume of 200 liters of electrolyte consisting of grams per liter anhydrous sodium pyrophosphate, 10 grams per liter each of sodium citrate and citric acid was made up and heated to 60 C. A l-inch wide strip of alloy 260 brass with a dull grey stain on its surface was threaded through the apparatus. The strip speed was adjusted to 100 feet per minute and the solution flow adjusted to 50 gallons per minute. This corresponded to a flow velocity of 7.3 feet per second. The current was adjusted to 132 amperes at 8.9 volts corresponding to current density of about 4.4 a.s.i. and a treatment of 6.7 coulombs per square inch. The voltage relationship values for Equation 3 were p=37 ohms mil ft., g=8.5rnilS, w=l.00 inch, V0=0.3 volt, a=0.1l, b=0.24 and c: 103.

The strip acquired a bright, lustrous surface.

However, when the current was increased above amperes (5.0 a.s.i.), the surface became covered with brown stains.

When the current was decreased below 91 amperes (2.8 a.s.i.), the surface became etched and matte in appearance. The strip was rinsed, dried and coiled after treatment.

Example II.-Cleaning an alloy 230 strip An alloy 230 strip, 2.1 inches wide, with a severe water stain on its surface, was placed in the apparatus described in Example I.

The electrolyte was identical to Example I.

The voltage relationship values for Equation 3 were p=37 ohms mil ft., 5 :10.8 mil, w=2.10 inches, V0=0.6 volt, and a, b, and c as given in Example I.

The strip speed was adjusted to 40 feet per minute and the electrolyte flow rate was adjusted to 35 gallons per mlnute (or 6.5 ft. per sec.). The current was set at 215 amperes (3.4 a.s.i.) and the extent of treatment was 13 coulombs per square inch. A voltage of 6.2 volts was required for this current.

The strip was cleaned completely and acquired a lustrous, attractive surface after treatment.

Example III.-Cleaning an alloy 260' strip in a high citrate electrolyte An apparatus was constructed with a pre-immersion soak length of three feet and a system of five nozzles, each with a 1-inch long cathode.

A black, heat-stained strip of alloy 260 brass, 2.5-inches wide, was treated in this apparatus at 50 feet per minute, with 500 amperes (22.7 a.s.i.), and a treatment of 20 coulombs per square inch, 17 volts were required for this treatment and 37 gallons per minute total flow was passed, i.e., 7.4 gallons per minute, through each nozzle (or 8.0 ft./sec.).

This treatment produced a bright, lustrous finish and complete removal of stain.

Example IV.Regeneration of electrolyte Current density (amps per sq. foot) Zn content of cathode deposit, percent Example V.Stain resistance of treated metal An alloy 230 strip cleaned by the process of the present invention in a 100 grams per liter sodium pyrophosphate, 10 grams per liter each of sodium citrate and citric acid, electrolyte at 70 C. with 3 a.s.i. current density and 10 coulombs per square inch treatment, rinsed and dried, was prepared.

A stain test was performed in which panels were cooled to 40 F. and then exposed to an environment at 100 F. with a relative humidity of 95% for 3 days.

Panels cleaned in sulfuric acid developed a dark, matted appearance and were given an appearance rating of 33 The panels treated with the process of the present invention showed a brighter, more uniform appearance and were given an appearance rating of 63 It is to be understood that the invention is not limited to the illustrations described and shown herein which are deemed to be merely illustrative of the best modes of carrying out the invention, and which are susceptible of modifications of form, size, arrangement of parts and detail of operation, but rather is intended to encompass all such modifications which are within the spirit and scope of the invention as set forth in the appended claims.

What is claimed is:

1. A process for cleaning copper alloy strip comprising:

(a) soaking the strip in an electrolyte solution consisting essentially of a polyphosphate and an organic hydroxycarboxylic acid, and

(b) making the strip the anode in an electrochemical cell, the electrolyte in said cell being a solution consistening essentially of a polyphosphate and an organic hydroxycarboxylic acid having a pH of from 6-9 and being maintained at a temperature in the range of from about 40 C. to about 80 C., and wherein said strip is subjected, as the anode to an electric current for a suflicient time so that 1-30 coulombs per square inch flow through said strip.

2. A process according to claim 1 in which the pH of the solution to be used in step (a) is between 6.0 and 9.0.

3. A process according to claim 1 in which the polyphosphate in steps (a) and (b) is selected from the group consisting of pyrophosphate, tripolyphosphate, and tetrapolyphosphate.

4. A process according to claim 3 in which the polyphosphate is sodium pyrophosphate.

5. A process according to claim 1 in which the concentration of polyphosphate is between 50-90 grams per liter.

6. A process according to claim 1 in which the hydroxycarboxylic acid is selected from the group consisting of citric, tartaric, glycolic, gluconic, and sugar acids.

7. A process according to claim 6 in which the acid is citric acid.

8. A process according to claim 1 in which the temperature of the electrolyte is maintained in step (a) in the range of approximately 40-80 C.

9. A process according to claim 8 in which the temperature is approximately -70 C.

10. A process according to claim 1 in which the soaking time in step (a) is 2-60 seconds.

11. A process according to claim 1 in which the current density J is maintained within the range I max. and J min., in which J max.=.53(Vf-Vs) (Ct/10) and J min.=.36 (Vf-Vs).

12. A process according to claim 1 in which the electrolyte is electrochemically regenerated.

13. A process according to claim 12 in which the current density is maintained in the range of 1 to 20 amps per square foot.

14. A process according 0t claim 13 in which the regeneration solution contains zinc and the zinc content of the metal deposited on the cathodes is given by the equation Zn=7.5 (J -4), where Zn is the percent zinc in the deposit; and I, is the regenerator cathode current density in amperes per square foot and is in the range of approximately 4 to 10.

15. A process according to claim 14 where the copper content of the regeneration is at least 0.5 gram per liter.

References Cited H. B. Linford: Plating, December 1950, pp. 1265-9.

ROBERT K. MIHALEK, Primary Examiner US. Cl. X.R. 13426