TH41100B - Equipment and methods for non-electroless regeneration of metal plating solutions. - Google Patents

Abstract

DC60 (20/09/54) In the non-electrodialysis metal bath regenerative by electrodialysis, it was found that the metal of the metal bath was deposited in the electrodialysis arrangement system. This small electrolysis in order to fix this problem Improvements have been introduced to enhance the regeneration of the existing arts. Such improvements consist in the provision of a primary cation exchanger to lead This metal ion exits the concentrated fluid. This main cation exchanger is coupled with The separation chamber for the concentrates of this electrolysis arrangement system in such a way as to allow The concentrated fluid which flows through the separation chamber for this concentrate passes to the main cation exchanger. and recirculated into the separation chamber for this new concentrate. In the non-electrodialysis metal impregnation bath regenerative, it was found that the metal of the impregnation bath was found to be deposited in this electrolysis arrangement. in order to fix this problem Improvements have been introduced to enhance the regeneration of the existing arts. Such improvements consist in the provision of a primary cation exchanger to lead This metal ion exits the concentrated fluid. This main cation exchanger is coupled with The separation chamber for the concentrates of this electrolysis arrangement system in such a way as to allow The concentrated fluid which flows through the separation chamber for this concentrate passes to the main cation exchanger. and recirculated into the separation chamber for this new concentrate.

Claims (12)

1. The electroless regeneration equipment for metal plating consists of: a) an electrodialysis system (E1, E2), each containing separate chambers for the diluent (Dila, Di2a, Di2b) to hold the metal plating; and separate chambers for the concentrate (Kola, Ko1b, Ko2a), which are separated from the diluent chambers (Di1a, Di2a, Di2b) by an ion exchange membrane and are intended to hold the concentrate fluid, which acts as an adsorbent to remove interfering substances from the metal plating, including the anode (An) and cathode (Ka); and b) a primary cation exchanger (Ix) for removing metal ions from the concentrate fluid. This cation exchanger is coupled to the diluent chambers (Ko1a, Ko1b, Ko2a) in a way that allows the concentrate fluid to pass through the primary cation exchanger (Ix) and recirculate back into the diluent chambers (Ko1a, Ko2a), leaving the concentrate fluid to be removed. The flow will be recirculated in the first circuit between the separation chambers for concentrates (Ko1a, Ko1b, Ko2a) and the collection tank (Vk), and in the second circuit between the collection tank (Vk) and the main cation exchanger (Ix). 2. The device according to claim 1, which comprises: a) a system for the first electrodialysis (E1) containing separate chambers for concentrates (Ko1a, Ko1b) and dilutes (Di1a), with alternating cathodes (Ka) and anodes (An), and separate dilute chambers (Dila) each separated on the cathode side of this separation chamber from the adjacent concentrate chambers (Ko1a, Ko1b) by an exchange membrane. a) The arrangement for the second electrodialysis system (E2), which has separate chambers for diluents (Di2a, Di2b) and a separate chamber for concentrates (Ko2a), as well as alternating cathodes (Ka) and anodes (An), each separate chamber for concentrates (Ko2a) is separated on the cathode side by anion exchange membrane (A) and on the anode side of this separation chamber from the adjacent separate chambers for diluents (Di2a, Di2b) by a monoselective anion exchange membrane (AS), so that this plating solution can be passed through all the separate chambers for diluents (Di1a, Di2a, Di2b) in the two interconnected electrodialysis arrangements (E1, E2). They are connected in parallel and simultaneously convey concentrated fluids through separate chambers for the concentrates (Ko1a, Ko1b, Ko2a) in total in two electrodialysis arrangement systems (E1, E2), which are connected in parallel, and c) the current sources (S) for the cathode (Ka) and anode (An) of the arrangement system for the first electrodialysis (E1) and the arrangement system for the second electrodialysis (E2). 3. Any device under any of the preceding claims which is provided with an additional regenerating fluid vessel (VRS1) to hold the regenerating fluid intended for the regeneration of the primary cation exchanger (IX), such vessel shall be coupled to the primary cation exchanger (IX). 4. Any of the equipment provided under the prior claims, which is provided with an additional accumulator (VZK) for the support of concentrated fluids, such accumulator is coupled with a collection tank (VK) and the main cation exchanger (IX). 5. Equipment pursuant to one of the prior claims, which is provided in addition to a safety cation exchanger (IS), such exchanger is coupled to the primary cation exchanger (IX) for subsequent treatment of concentrated fluids previously treated in the primary cation exchanger (IX). 6. An apparatus under one of the prior claims which is provided with a second regenerating fluid vessel (VRS2) for the purpose of regenerating the regenerating fluid intended for the regeneration of the safety cation exchanger (IS). 7. The method for electroless regeneration of the plating solution consists of: a) passing the plating solution through individual diluent separation chambers (Dila, Di2a, Di2b) of the electrodialysis system (E1, E2); and b) passing the concentrated fluid, which acts as an adsorbent for interfering substances to be removed from the plating solution, through the concentrate separation chambers (Ko1a, Ko1b, Ko2a) of the electrodialysis system (E1, E2). These concentrate separation chambers are separated from the diluent separation chambers (Di1a, Di2a, Di2b) by an ion exchange membrane; and c) further passage of the concentrated fluid through the main cation exchanger (Ix) and recirculation of the fluid back into the concentrate separation chambers (Ko1a, Ko1b, Ko2a) by recirculation. The concentrated fluid flows in the first circuit between the separation chambers for the concentrates (Ko1a, Ko1b, Ko2a) and the collection tank (VK), and in the second circuit between the collection tank and the main cation exchanger (IX). 8. The procedure pursuant to claim 7, in which the plating solution a) is introduced through the diluent separation chamber (Di1a) in the first electrodialysis arrangement system (E1) which comprises the concentrate separation chambers (Ko1a, Ko1b) and the diluent separation chamber (Di1a) with alternating cathodes (Ka) and anodes (An), the diluent separation chamber (Di1a) is separated on the cathode side of this separation chamber from the adjacent concentrate separation chambers (Ko1a, Ko1b) by a monoselective cation exchange membrane (KS) and on the anode side of this separation chamber from the adjacent concentrate separation chambers (Ko1a, Ko1b) by an anion exchange membrane (A), and b) passes through the diluent separation chambers (Di2a, Di2b) in the first electrodialysis arrangement system. The second dialysis (E2) consists of alternating separate chambers for diluents (Di2a, Di2b) and concentrates (Ko2a), as well as the cathode (Ka) and anode (An). The concentrate chamber (Ko2a) is separated on the cathode side from the adjacent diluent chambers (Di2a, Di2b) by an anion exchange membrane (A), and on the anode side from the adjacent diluent chambers (Di2a, Di2b) by a monoselective anion exchange membrane (AS). The plating solution is then simultaneously passed through all the diluent chambers (Di1a, Di2a, Di2b) in a two-system electrodialysis arrangement (E1, E2). They are connected in parallel, and the concentrated fluids flow through separate chambers for the concentrates (Ko1a, Ko1b, Ko2a) in a total arrangement for two electrodialysis systems (E1, E2). 9. Under either claim 7 or 8, for the regeneration of the primary cation exchanger (Ix), the concentrated fluid present in the primary cation exchanger (IX) is replaced by the regenerating fluid and this concentrated fluid is recirculated back into the storage tank (VK), and the primary cation exchanger (IX) is regenerated in this process. 10. The method pursuant to claim 9 in which the regenerating fluid is removed from the first regenerating fluid vessel (VRS1) and transferred into the primary cation exchanger (IX). 11. Under either claim 9 or 10, where this regenerating fluid is replaced by a concentrated fluid after complete regeneration of the primary cation exchanger (IX), this regenerating fluid is recirculated back into the first regenerating fluid vessel (VRS1). 12. Any of the methods under claims 7 through 11 in which the concentrated fluid flows through multiple principal cation exchangers (IX) at different times, with regenerating fluid being circulated through those principal cation exchangers (IX), where the concentrated fluid is not circulated for regeneration of these principal cation exchangers.