PROCESS FOR REMOVING METAL COMPLEXES FROM WASTE SOLUTIONS

Abstract: The invention relates to a process for treating waste solutions and rinse waters, especially those from electroless plating processes, to remove organometallic complexes and complexing agents, particularly copper and copper-EDTA complexes by eluting the waste solutions through anionic exchange resins.

Description: This invention relates to a process for removing metal ion-chelate complexes and free complexing agents from waste solutions using anionic exchange resins. More particularly, this invention relates to removing metal ions from electroless plating line rinses. Many manufacturing processes produce waste streams which, if expelled from plants without further treatment, pollute the environment and also result in the loss of valuable materials which can be recovered and reused. A process for treating cyanide containing solutions, as from ore treatment, is described in US-A 4,267,159 where an anion exchange resin is used to segregate the cyanide. Subsequently, the free cyanide is recovered by regeneration of the resin with a weak alkaline solution, while stronger alkaline solutions are used for eluting the complexed cyanide. Cyanide is a highly toxic compound and the cyanide complexes react very differently from metal complexes used in plating bath solutions. It has been especially difficult to treat very dilute waste streams economically, such as those which are produced by plating processes and related rinsing operations, in particular, electroless plating processes. Attempts have been made to use sulphide precipitation and starch xanthate processes for this purpose, but they have proven expensive and difficult to control. Further, they produce precipitate end-products which are hard to flocculate and filter. Many plating processes produce, inter alia, waste streams having concentrations of metal ions which are complexed with organic molecules. Regulations in industrialized countries set very strict standards for metal ion concentrations in the effluent from these processes. Moreover, the metal ions and chelating agents in the waste streams are valuable and have the potential tobe recycled through the process. There have been many attempts to recover the chemicals from these waste solutions. For example, it has been suggested that an ion exchange resin which acts as a very powerful complexing agent selectively removes copper from copper complexes in the effluent. One such resin has an iminodiacetic functional group. (R.M. Spearot et al, "Recovery Process for Complexes Copper Bearing Rinse Waters", Environmental Progress, Vol. 3, No. 2, p. 124, 1984). However, this resin was unable to remove copper from effluent in the presence of ethylene-diaminetetraacetic acid (EDTA), a complexing agent which is often used in electroless plating processes. It is generally believed that using an anionic exchange resin to remove transition metal ions complexed with a compound in the plating bath rinse, such as EDTA, would not operate to remove these complexes because the anions of the salts in the bath rinse would be more strongly attracted to the resin than the ions, complexes or complexing agents to be removed. It has been suggested to treat an anionic exchange resin with EDTA, for example, and utilize the treated resin to chromatographically separate metals from a solution. In Plating and Surface Finishing, "A New Treatment for Waste-water Containing Metal Complexes" by Courdevalis et al March 1983, p. 70, and US Patent 4,303,704 it has been suggested trying to remove cooper from its complexes by using a resin prepared by reacting polyethyleneimine with chloracetic acid and cross-linking the polymer. This method was unsuccessful in removing copper from an EDTA complex, although it could be used to remove copper from a solution containing tartrate, or an organic acid ester or N,N,N',N'-tetrakis-(2 hydroxypropyl ethylene diamine, an alkanolamine chelator. In US Patent 4 076 618 is has been suggested to use strong cationic resin with a sulfonic or carboxylic acid functional group to extract cupric ion and alkanolamine chelator complexes. It is, therefore, an object of this invention to provide a process for removing metals from waste solutions such that the waste solutions meet levels prescribed by regulations. It is a further object of this invention to provide a process to remove chelated copper ions which are complexed with a wide variety of complexing agents from waste solutions. It is still a further object of this invention to provide a process to remove copper EDTA complexes from waste solutions. In accordance with the invention, there is provided a process for removing complexed metal ions and complexing agents from aqueous solutions, said aqueous solution is a waste water solution and said complexing agent is an anion, and that said solution is treated with an anion exchange resin loaded with an anion which does not complex with said metal ions or forms a weaker complex with said metal than said complexing agent or with a non-complexing anion which is present in the waste water solution, and subsequently eluting a solution of free complexing agent through the resin and then eluting an inorganic saline solution through the resin to separate organic metal complexes from the free complexing agent in the waste water solution. The Figure is a flow-chart for a system for treating waste solutions from plating baths employing the method of this invention. Certain technology that will be used throughout the description of the process of this invention is defined as follows: "Bed volume" is the volume of resin that is present in an ion exchange column. "Breakthrough" is the point at which the concentration of the ions being adsorbed to the ion exchange resin rises to an appreciable value in the column effluent. In accordance with this invention, aqueous solutions containing metal ion complexes and complexing agents for said metal ions may be treated to remove certain metal ion complexes, particularly transition metal complexes, and more particularly, EDTA-copper complexes, using anion exchange resins. The novel process of this invention removes anionic organic metal complexes from waste solutions, particularly those of electroless plating baths, with high efficiency. Surprisingly, the process of this invention removes EDTA-copper complexes as well as other organic metal complexes. It had been generally believed that a cation exchange resin should remove the copper from complexes. Surprisingly, however, it has been found that anion exchange resins remove such complexes, due to the negative charge on the complexes. The ion exchange resin used in the process of this invention is preferably a strong base anion exchange resin. Preferably, it contains quaternary ammonium groups or similar strongly basic groups incorporated into the framwork. Preferably, the resin framework should be a polystyrene. A macroreticular-type or a gellular type resin may be used. Macroreticular resins are large-pore resins having a rigid shape. Gellular resins shrink and swell on contact with liquid. The use of gellular resins is preferred because the potential flow rate through the resin and the treatment capacity are higher. The process of this invention is preferably performed by using a vertical column to contain the ion exchange resin. Preferably, the flow rate of solution through the column is 1 to 100 l/h/l resin. However, any type of ion exchange bed can be used. The height of the column and the aspect ratio (height:diameter) are not critical to the efficient operation of the treatment process of this invention. Other methods of contacting the waste solution with ion exchange resins may be used. Included among these processes are moving bed ion exchange and liquid systems using liquid ion exchange resins.The process of this invention can be performed efficiently at a wide range of atmospheric temperatures and pressures. Because the organic metal complex is a weaker anion than the free complexing agent, it has a slightly lower affinity for the anionic resin than does the free complexing agent (or "coordinating liquid") molecule. This difference in affinities provides a means for separating the free liquid molecules and the metal-liquid coordination compound. Two zones are created in the resin: a leading zone, in which the resin contains organic metal coordination compounds, and a trailing zone, in which the organic metal complexes have been replaced by free coordinating liquid molecules. The resin may be placed in a column and the waste solution eluted down through the resin bed, and the treated waste effluent collected at the bottom of the bed. As the resin becomes exhausted, the two zones also move downward toward the bottom of the bed. When the leading zone reaches the exit portion of the resin bed, a "breakthrough" of organic metal-containing solution takes place, at which point the process is terminated and the resin should be regenerated. The pH of the waste solution during the treatment process of this invention is dependent on the composition of the plating bath. It is preferably kept between about 3 and 12.4. For example, an EDTA solution containing copper chloride is optionally treated at a pH of between 9 and 10.5. However, an EDTA solution with copper sulfate can be treated at any pH. Using the appropriate pH may increase the capacity of the resin from 250 to 800 bed volumes prior to exhaustion. Various complexing agents and metal ions may be present in the waste solution, particularly anionic complexing agents. Among the complexing agents which may be present with anionic complexing agents are non-anionic complexing agents such as alkanolamine and non-alkanolamine complexing agents, such as N,N,N',N'-tetrakis-(2-hydroxypropyl) ethylene diamine (Quadrol ® ) and triethanolamine. Anionic complexing agents include organic acids, organic acid esters , and salts of organic acids , for example, citrates, tartrates, succinates, lactates, glycolates, and Rochelle salts and the like. Other coordinating liquids or complexing agents include amino acids such as ehylenediamine tetraacetic acid (EDTA). Metals which are generally present in waste solutions of plating operations and which can exist in chelated form are subject to the treatment process of this invention. This invention is especially suited for treatment of complexes of metals which form organic metal complexes with complexing agents which are more stable than the complexes the metals can form with other ions in the waste solution, e. g. , more stable than the metal-chloride complexes, metal-amiac complexes or metal-alkanolamine complexes. Transition metals such as copper and nickel are among those generally present in such plating processes and which form such complexes. It is believed that other transition metals and alkaline earth metals which complex with EDTA or other organic complexing agents are subject to treatment using the method of this invention, for example, lead, cadmium, iron, calcium, magnesium, barium, cobalt, chromium, zinc, manganese and the like. For example, in nickel plating baths, nickel may be present with complexing agents such as citrates, acetates, EDTA, ethylenediamine and triethanolamine. In boiler cleaning and anti-fouling operations, iron may be present with a complexing agent such as EDTA, citrate and the like. The wash streams from these operations may be treated using the method of this invention. Anions which do not combine with metal ions to form organo-metallic complexes are also generally present in the waste solution, e.g. , sulfates, chlorides, and the like. The ion exchange resin is preferably loaded with a monovalent anion present in a neutral salt solution prior to eluting the waste solution through the column, i .e. , the resin should be loaded with an anion having a lower charge density and a lower selectivity coefficient than the complexed anion. Preferably, the anion exchange resin is regenerated when breakthrough occurs. Regeneration is preferably performed with a salt solution. Prior art processes would have suggested that regeneration be undertaken with an hydroxide solution. However, the bond of the organic metal complex may be unstable under extremely alkaline conditions and cause the precipitation of metallic oxide or metallic hydroxide in the pores of the resin when hydroxide is used to regenerate the resin bed. In the process of this invention, the regeneration of the resin is accompl_ished with an inorganic salt solution such as sodium chloride and the like so as to preserve the integrity of the organic metal complex.This allows the recovery of the complexing agent as well as the complex itself for re-use in the plating process from which it came. The steps of the regeneration process depend upon both the composition of the original solution, e.g. , plating waste solution, and the desired form of the effluent from the regeneration process. If it is desired that the regeneration effluent be composed of both free complexing agent and organic metal complex, a simple salt regeneration solution should be eluted through the resin bed, displacing both free complexing agent and organic metal complex from the resin. If, however, it is desired that the organic metal complex solution be separated from the free complexing agent, the column is first eluted with a solution of complexing agent. Because the free complexing agent has a higher affinity for the resin than does the organic metal complex, it displaces the complex. The column is then eluted with a salt solution to displace the complexing agent. The process of this invention may also be used to produce an organic metal plating solution from a metal salt solution. The resulting plating solution will have a low concentration of inorganic anions. A solution of the complexing agent is eluted through the column, thus placing the resin in a form having free complexing agent bonded to the functional groups. An uncomplexed metal solution is passed through the column and the metal ions complex with the free complexing agent. When the remaining complexing agent has reacted with metal ions, deionized water is passed through the column to rinse away excess metal. A complexing agent solution is then eluted through the system, displacing organic metal complexes and rinsing them from the column. The process of the invention may be implemented in a two-resin bed ion exchange system, thus optimizing capacity. Referring to the Figure, the waste solution from plating bath 1 is sent to a rinse bath 5 in which the waste solution is mixed with water. The resulting solution is routed to sump 7 from which the solution is pumped by pump 9 into particulate filter 11. From filter 11 , the solution is sent to equalization tank 13, which prevents spikes in concentration of the different elements of the waste solution composition. The waste solution is then sent to one of ion exchange columns 15. Ion exchange column 15 is approximately 50 to 75% filled with anionic exchange resin. The waste solution is eluted through ion exchange column 15 in which it undergoes treatment for removal of organo-metallic complexes. The eluted solution is sent to a sewer 17. To regenerate the ion exchange column 15, a salt solution, from tank 19 is sent through the resin bed in column 15. The salt solution may be made up fresh or it may be obtained from plating bath 1. The plating solution from plating bath 1 is treated in treatment tank 21 such that the copper is plated out of solution and in tank 23 such that the EDTA is precipitated out of solution. The remaining salt solution is sent to salt tank 19. The eluted solution from the treatment process taking place in ion exchange column 15 may be discarded or it may be recycled and reused as recovered bath to plating bath 1. The following examples further illustrate the treatment of metal complex containing solutions with anion exchanger resins and the regeneration of the loaded resins. EXAMPLE 1 500 ml of a strong basic macroreticular anion exchange resin having quaternary amine functional groups in a polystyrene framework (IRA-900 ® ) was loaded into a 1.0 1 ion exchange column. The resin's anion was the chloride ion. A waste stream of rinse water from an electroless copper plating solution having the following composition was eluted through the column at a rate of 70 ml/min. After every forty bed volumes, i .e., every 20 l, of rinse water put through the copper concentration of the effluent sample was measured in milligrams copper per liter of effluent. Table I shows the results of these measurements. EXAMPLE 2 300 ml of the same strong basic anion exchange resin as used in Example 1 were loaded into a 0.6 l column. Electroless plating process rinse water having the following composition was contacted with the resin at a rate of 47 ml/min. Samples of the effluent were collected after every 40 bed volumes, or 12 l, of rinse water put through the column and measured for copper concentrate. Table II shows the results of these measurements: EXAMPLE 3 300 ml of a strong basic gellular anion exchange resin having quaternary amine functional groups on a polystyrene framework (IRA-400 ® ) was loaded into a 0.6 l ion exchange column. The resin's anion was the chloride ion. Rinse water having the following composition was eluted through the ion exchange column at a rate of 80 ml/min Samples of the column's effluent were taken every forty bed volumes, or 12 liters, and measured for copper content. Table III shows the results of these measurements: EXAMPLE 4 300 ml of a strong basic gellular anion exchange resin having quaternary amine functional groups on a polystyrene framework, ASB-1®, was loaded into a 0.6-1 ion exchange column. The resin's anion was the chloride ion. Rinse water having the composition given in Example 3 was eluted through the column at a rate of 80 ml/min. Samples were taken every 40 bed volumes, or 12 liters, of rinse water put through and measured for copper content. Table IV shows the results of these measurements: EXAMPLE 5 An ion exchange column as described in Example 4 was constructed. Rinse water having the following composition was eluted through the column at a rate of 80 ml/min: Every 20 bed volumes (6.0 l) of rinse water throughput samples of the effluent were taken and measured for copper content. Table V shows the results of these measurements: EXAMPLE 6 50 ml of the resin used in Examples 4 and 5 were loaded into a 100 ml column. Simulated rinse water having the following composition was eluted through the column at a rate of 11 ml/min: Samples of effluent were collected after every 40 bed volumes, or 2.0 l , of elute and measured for copper content. Table VI shows the results of these measurements: EXAMPLE 7 An ion exchange column was constructed as in Example 6. Simulated rinse water having the following composition was eluted through the column at a rate of 12 ml/min: Samples were collected after every 40 bed volumes, or 2.0 l of rinse water throughput. Table VII shows the results of these measurements: EXAMPLE 8 The resin used in Example 1 was regenerated by contact with a 15 weight % of sodium chloride at a flow rate of 10 ml/min. Samples of the effluent were collected after every 0.2 bed volumes, or 100 ml of regenerate throughput and measured for copper content. Table VIII shows the results of these measurements: EXAMPLE 9 The resin used in Example 6 was regenerated by contact with a regenerating solution of 15 weight % of sodium chloride. The flow rate was 1.0 to 2.5 ml/min. Samples of the effluent were collected after every bed volume, or 50 ml , and measured for copper content. Table IX shows the results of these measurements. EXAMPLE 10 The resin used in Example 7 was regenerated by contact with a 15 weight % solutiom of sodium chloride. The flow rate was 1.0 to 2.5 ml/min. Samples of effluent were collected after every bed volume of regenerate throughput and measured for copper content. The results of these measurements are shown in Table X. EXAMPLE 11 A solution containing iron/EDTA chelate, EDTA ion and no other ion was diluted through the anionic resin described in Example 4. A solution had an initial iron concentration of about 30 to 40 ppm. A solution was eluted at a rate of approximately 80 ml/min. Samples were taken of the effluent from the column after 10 bed volumes were eluted. The iron concentration of the effluent after 10 bed volumes were eluted was less than 2 ppm. EXAMPLE 12 Example 11 was repeated using a solution containing iron-citrate chelates and citrate. The initial concentration of iron-citrate chelate was approximately 30 to 40 ppm. The solution was eluted through the column at a rate of 80 ml/ min. After 10 bed volumes of the solution were eluted through the column, the concentration of iron in the effluent was measured. It was found to be less than 2 ppm. EXAMPLE 13 Example 11 was repeated starting with a solution containing nickel-EDTA chelates and EDTA. The solution was eluted through the column at a rate of approximately 80 ml/min. After approximately 10 bed volumes were eluted through the column, the nickel concentration in the effluent was negligible. EXAMPLE 14 Example 11 was repeated starting with a solution containing EDTA and chelates of EDTA and group 11A alkaline earth metals, barium, calcium, magnesium. The solution was eluted through the ion exchange column as described in Example 4. After 10 to 20 bed volumes of solution were eluted through the column, measurements were taken of the barium, calcium and magnesium concentration in the effluent. These concentrations were negligible. EXAMPLE 15 A solution containing lead/EDTA chelate and EDTA was eluted through a column containing the anionic resin described in Example 4. The solution had an initial concentration of lead/EDTA chelate of approximately 30 to 40 ppm. After about 10 bed volumes were eluted through the column, the lead concentration of the effluent was measured and found to be less than 2 ppm. EXAMPLE 16 Example 11 was repeated starting with a zinc-EDTA chelate and EDTA solution. It was found after 10 to 20 bed volumes were eluted through the column, that the effluent concentration of zinc was negligible. EXAMPLE 17 Example 11 was repated. However, the starting solution contained chromium/EDTA chelates and EDTA. A starting solution containing chromium/formate and formates may also be used. A solution was eluted through the column and after 10 to 20 bed volumes, the chrome concentration in the effluent was measured and found to be negligible. EXAMPLE 18 Example 11 was repeated. However, chelates of EDTA and transition metals such as manganese, cobalt and cadmium were present in the starting solutions. The solutions were eluted through a column containing an anionic exchange resin such as used in Example 4. The concentrations of manganese, cobalt and/or cadmium were measured after 10 to 20 bed volumes of solution were eluted through the column.These concentrations were found to be negligible.

Claims: A process for removing complexed metal ions and complexing agents from aqueous solutions, wherein said aqueous solution is a waste water solution and said complexing agent is an anion, and the solution is treated with an anion exchange resin loaded with an anion which does not complex with said metal ions or forms a weaker complex with said metal than said complexing agent or with a non-complexing anion which is present in the waste water solution, and subsequently eluting a solution of free complexing agent through the resin and then eluting an inorganic saline solution through the resin to separate organic metal complexes from the free complexing agent in the waste water solution. The process of claim 1 wherein said exchange resin is loaded with a non-complexing anion which is present in the waste water solution. The process of claim 1 wherein said metal is selected from barium, calcium, magnesium, lead, zinc, iron, chromium, copper, maganese, nickel, colbalt and cadmium. The process of claim 1 wherein said complexing agent is an ethylene diamine derivative compound. The process of claim 1 wherein said complexing agent is selected from organic acids, organic acid esters and organic acid salts. The process of claim 4 wherein said compound is ethylene diamine tetraacetic acid. The process of claim 5 wherein said compound is selected from the group consisting of citric acid, citrate, tartaric acid and tartrate. The process of claim 1 wherein said anionic exchange resin is a strong base anionic exchange resin. The process of claim 1 wherein said resin is selected from the group consisting of macroreticular resin and gellular resin.

Inventors: VIGNOLA, MICHAEL A.
Applicants: KOLLMORGEN CORPORATION
Application year: 1986
Main classification: B01J41
IPC codes: B01J41, C23C18, C02F1