US3661734A - Carbonate removal - Google Patents

Abstract

Removal of carbonate ions from cyanide-containing electroplating baths, or bath rinse solutions by contacting with an acid ion exchange resin, and liberating the carbon dioxide formed as off gas.

Description

United States Patent Sloan 51 May 9, 1972 154] CARBONATE REMOVAL [72] lnventor: Walter John Sloan, Newark, Del.

[73] Assignee: Remington Arms Company, lnc.,

Bridgeport, Conn.

[22] Filed: July 2, 1970 [21] Appl. No.: 52,142

[52] U.S. Cl ..204/52 Y, 204/45 R, 204/46,

UNlTED STATES PATENTS 1,442,348 1/1923 McDermet ..210/26 2,117,631 5/1938 Seyb ..2l0/26 2,164,927 7/1939 Hull ..204/55 Y X 2,434,191 l/1948 Benner et a1... .....204/52 Y OTHER PUBLICATIONS Knodler et al., Metalloberflache, Vol. 13, No. 10 pp. 327- 330 (1959).

Primary Examiner-F. C. Edmundson Attorney-Harry J. McCauley 57 ABSTRACT Removal of carbonate ions from cyanide-containing electroplating baths, or bath rinse solutions by contacting with an acid ion exchange resin, and liberating the carbon dioxide formed as ofi gas.

4 Claims, No Drawings CARBQNATE REMOVAL BRIEF SUMMARY OF THE INVENTION Generally, this invention comprises the removal of carbonate ions from cyanide-containing electroplating bath, or bath rinse solutions comprising, in sequence, (1) contacting said solutions with the hydrogen form of a cation exchanger selected from the group consisting of carboxylic, phosphonic and sulfonic ion exchange resins to convert said carbonate ions to carbonic acid; (2) reducing the pressure on said solutions to promote decomposition of said carbonic acid to water and carbon dioxide; and (3) recycling said solutions, reduced in carbonate ion content, to said electroplating bath.

Electroplating of nickel, copper, and other metals frequently utilizes a cyanide ion-containing bath which is usually operated at temperatures in the range of 120 to 160 F., maintained by steam coils or other indirect heating means. Under these conditions, substantial cyanide is oxidized to the carbonate, which is associated with sodium or potassium ions, which are also normal ingredients of the baths.

The presence of a limited amount of carbonate salts in plating baths is not objectionable and, in fact, is desirable, in that the electrical conductivity of the baths is thereby improved. However, excessive amounts adversely affect the quality of the electroplating obtained and, therefore, carbonate concentration is normally controlled by crystallization of carbonates from the plating bath, as by refrigeration or evaporation, or by discarding the plating bath. Discarding can be effected by running the entire bath to the sewer, or by replacing with fresh water the normal drag-out" of plating solution occurring as a result of plating solution being carried off as surface wetness by articles which have been plated.

Both loss by either blow-down or by drag-out is objectionable, since cyanides constitute a toxicity hazard, as do metal ions which are also a bath ingredient. Moreover, the lost chemicals constitute an appreciable economic loss. The chemical treatments for cyanide wastes, such as electrooxidation, or oxidation with hypochlorite, or chlorine plus caustic, are relatively expensive. Also, the sludges which result from the complex metal cyanides must be disposed of in a suitable manner.

The principal object of this invention is to remove excess carbonates from plating bath solutions followed by return of valuable constituents of the bath, such as cyanide and complex metal cyanides, back to the plating bath system.

This I accomplish by contacting the bath solution with a weak acid ion exchange resin, such as CC-3, a polymer of cross-linked acrylic acid, for example. The hydrogen form of such a resin converts carbonate to carbonic acid, which readily decomposes to water and carbon dioxide, which can then be vented to the atmosphere as off gas. The resin also converts sodium cyanide to hydrogen cyanide, which may remain substantially in solution because of the presence of complex metal cyanides, and the pH of the processed solution. Only a minor conversion of the complex metal cyanides to their corresponding acids occurs, because the hydrogen form of a weak acid ion exchange resin cannot generate an acid greater than its own strength.

The hydrogen cyanide will be neutralized by the normally present and excess basicity in the plating bath, supplemented, if necessary, by the addition of more caustic. Also, the very small amounts of acids corresponding to complex metal cyanides will be neutralized by the basicity of the bath. Since the hydrogen cyanide produced by the resin is poorly ionized, it may be held, to some extent, by the water which is occluded in the ion exchange resin particles. A rinse with an alkali, e.g., sodium or potassium hydroxide, will remove any hydrogen or alkali cyanide in the bed, and preclude hydrogen cyanide release when the exchanger is eventually regenerated with acid.

Weak and intermediate acid ion exchange resins are particularly preferred over strong acid resins in the practice of my invention. If a strong acid resin is utilized, there could be a loss in useful capacity of the system, because of the complete conversion of complex cyanides to their corresponding acids. Also, the strong acid resins generate more waste, because they require at least two times theoretical acid for proper regeneration, and this excess acid must be neutralized later in a subsequent waste stream. ln contrast, the weak acid and intermediate acid resins do not require a large excess of regenerant acid, and what excess there is can be utilized. Thus, if one accumulates the second half of the effluent from a given regeneration, it, of course, contains, substantially, the excess acid. Then, if the recovered acid solution is used as the first solution through a later exchanger requiring regeneration, substantially all of the excess acid is converted to salt. The usual acid addition can then be made, and it displaces the recovered solution from the bed. The second half of this second acid addition is again collected, and the sequence is repeated during the next-occurring regeneration of an exhausted exchanger.

If a strong acid resin is utilized to reduce carbonates, all of the salts in the plating bath or bath rinse will be converted to their corresponding acids. By proper control, the acid solution can be mixed under pressure with untreated bath or rinse in such a manner that the alkali carbonate is neutralized. On exposure to the atmosphere, the carbonic acid will be decomposed to form water and carbon dioxide, which escapes. If the acid stream is not neutralized, or neutralization is incomplete, a low pH results, and considerable HCN will escape, because its solubility decreases markedly with decrease in pH.

The lower the pl(,, of the hydrogen form of a resin, the lower the pH of ion exchange-treated plating bath or bath rinse solution. lf HCN release is to be retarded, the carbonate removal should be accomplished with the resin having the highest pl(,,. Table II, infra, shows that lRC -50, a copolymer of methacrylic acid and divinylbenzene, and having a pK 5.9, reduced the pH of a solution from about 12 to the range of 5.7-6.0, and that IRC -84, a polymer of cross-linked acrylic acid, and having a pK,, of 5.3, reduced the pH of the same solution to the range of 4.5-4.9. A phosphonic resin has a pK in the 3.0-3.5 range. Strong acids such as sulfonics are not defined in terms of a pK, value.

When the pH of a cyanide-containing electroplating bath, or bath rinse solution is reduced, by carbonate and alkali removal by ion exchange or direct acid addition, the solubility of the metal cyanide is decreased. For example, if all the alkalinity due to carbonate and hydroxide is removed from a copper plating bath by ion exchange, cuprous cyanide (CuCN) will become visible as a very fine white precipitate. As noted in Table I1, infra, the lower pH caused the heaviest CuCN precipitate. The amount of precipitate can be minimized by maintaining a relatively high pH, e.g.,using a resin with a high pK, and operating upflow such that some bypassing occurs in the exchanger bed. This type of operation has the disadvantage of limiting carbonate removal. The CuCN precipitate is not necessarily objectionable. It forms slowly, and does not plug the exchanger bed or pipelines. lt dissolves in the plating bath to which the treated solution is returned, and absence of the turbidity, in normal operation, is an index of exhaustion of the exchanger bed.

The lowering of the pH of a cyanide-containing electroplating bath processed with a carboxylic resin can be minimized, and to some degree controlled, by partially neutralizing the hydrogen form of the resin. This can be done batchwise with hydroxides, carbonates or bicarbonates. Another method is to add a neutral salt, e.g., NaCl or KCl, too a bed of the hydrogen form of the resin. The degree of neutralization effected is determined by such variables as amount of chemical added, concentration, time of contact and the type of chemical employed. The partial neutralization limits the conversion of complex metal cyanides to their corresponding acids, and the resulting relatively higher pH minimizes the precipitation of cuprous cyanides. The loss of hydrogen cyanide is, at the same time, decreased because of its greater solubilities at the relatively higher pH levels.

Usually, bath rinse solution can be turned directly to the plating bath after the ion exchange resin contacting, thereby making up for normal evaporation from the bath. However, if the drag-out or rinse is excessive in volume, evaporation can be resorted to before ion exchanger treatment of the waste.

It is preferred to effect carbonate removal by contacting the ion exchange resin by upflowing the solution. The carbon dioxide will rise with the solution, as do the metal cyanide precipitates. The carbon dioxide can generally be held in solution by, operation at moderate pressures, and downflow operation can then be used. However, bubbles of carbon dioxide would then be released in localized regions, and their presence interferes with the normal and even flow through the bed. Also, with downflow, the metal cyanide precipitate can cause plugging of the exchanger bed unless precautions are taken to minimize its formation, e.g., with a fast flow rate, the treated solution discharges before the precipitate formed. Such a fast rate is sometimes feasible, as previously discussed, where the effluent is mixed with untreated solution. The slow reaction rates of the weak acid resins can be improved if they are mixed with strong, sulfonic type, cation resins.

In tests conducted with my invention, I was able to reduce readily the carbonate content of a copper plating bath from about 68 gm/liter to 7.4 gm/liter by using a fluidized bed. In a static bed test it was practicable to reduce carbonate to zero value for the first hundred milliliters of solution passed through a 30 cm bed in a 25 mm inside diameter column. A cross-linked acrylic polymer, lRC-84, was used for the tests.

A larger scale test was made with CO3, a weak acid ion exchange resin consisting of a cross-linked acrylic polymer in the hydrogen form. Drag-out from a commercial copper plating bath was run upflow at 0.35 gpm through a column 173/8 inch inside diameter, containing about 6 cu ft. of resin. Substantial CuCN precipitate was formed and most of it rose through the equipment with upflowing effluent. As shown by Table 1, all of the alkalinity of the solution was removed, and a trace of acidity was formed. Samples of 100 ml were titrated, and methyl orange indicator was used.

The weak acid resins (carboxylic type) vary in acidity. The following data show how the acidity, indicated by the pK, value, affects the removal of alkalinity NaOH, Na,CO;,, and basicity due to NaCN) from a diluted copper plating bath.,The flow was upward through a 30 embed in a 25 mm ID tube at 10 ml/min.

What is claimed is:

l. A process for removal of carbonate ions from cyanidecontaining electroplating bath, or bath rinse solutions, comprising, in sequence, (1) contacting said solutions with the hydrogen form of a cation exchanger selected from the group consisting of carboxylic, phosphonic, and sulfonic ion exchange resins to convert said carbonate ions to carbonic acid; (2) reducing the pressure on said solutions to promote decomposition of said carbonic acid to water and carbon dioxide; and (3) recycling said solutions, reduced in carbonate ion content, to said electroplating bath.

2. A process for removal of carbonate ions from cyanidecontaining electroplating bath or bath rinse solutions according to claim 1 in which said solutions are flowed upwardly through said cation exchanger.

3. A process for removal of carbonate ions from cyanidecontaining electroplating bath or bath rinse solutions according to claim 1 in which the said solution which has been contacted with said hydrogen form of a cation resin is mixed with said solution which has not been ion-exchange pI-I treated, to obtain a recycle solution of preselected pH. 7

4. A process for removal of carbonate ions from cyanidecontaining electroplating bath or bath rinse solutions according to claim 1 wherein said hydrogen form of said cation exchanger is partially neutralized prior to said contacting with said solutions as provided in step l 3 3 3 UNITED STATES PATENT OFFICE CERTIFICATE OF CORRECTION Patent NO. j 6 6 l 73 Dated M81 2, 1972 In'ventor(s) WALTER JOHN SLOAN It is certified that error appears in the above-identified patent and that said Letters Patent are hereby corrected as shown below:

Page 1, right-hand column, second line Cancel "2,161,927" and substitute Signed and sealed this 5th day of September 1972.

(SEAL) Attest:

EDWARD I I.FLETCI-IER,JR. ROBERT GOI'TSCHALK Attesting Officer Commissioner of Patents

Claims (3)

1. 2. A process for removal of carbonate ions from cyanide-containing electroplating bath or bath rinse solutions according to claim 1 in which said solutions are flowed upwardly through said cation exchanger.
2. 3. A process for removal of carbonate ions from cyanide-containing electroplating bath or bath rinse solutions according to claim 1 in which the said solution which has been contacted with said hydrogen form of a cation resin is mixed with said solution which has not been ion-exchange pH treated, to obtain a recycle solution of preselected pH.
3. 4. A process for removal of carbonate ions from cyanide-containing electroplating bath or bath rinse solutions according to claim 1 wherein said hydrogen form of said cation exchanger is partially neutralized prior to said contacting with said solutions as provided in step (1).