PROCESSES FOR TREATING WASTE STREAMS

Abstract: Processes for treating aqueous streams, such as waste streams and metal ion containing streams by utilizing reverse osmosis and electrodialytic water splitting. The processes use a minimum of treatment water, recovers chemical reagents and can recover metals, and reduce pollution in a wide range of waste waters. Specific examples illustrate treatment of battery wastes.

Description: TITLE PROCESSES FOR TREATING WASTE STREAMS BACKGROUND OF THE INVENTION The present invention relates to a novel pro¬ cess for the treatment of aqueous streams such as waste streams and metal ion-containing or other precipitatable material aqueous streams with a minimum of treatment water by utilizing reverse osmosis and electrodialytic water splitting, in sequence.. At the present time, given the ever-increasing cost of energy and the increased demands for the control of environmental pollution on the one hand, and the need to conserve important metal resources on the other, there arises a serious need for new and cost-effective process¬ es to treat industrial process streams some of which are dilute in metals. Sometimes this is done for the purpose of recovering metal values; other times it is for the purpose of avoiding environmental pollution. Typical metals which are sources of environ¬ mental pollution and which are valuable as minerals are copper, lead and cadmium, which are found in a wide range of waste waters resulting from plating and finishing processes such as metal finishing, from various rinses from pickling operations, from acid mine drainage and OMPI also from the extraction of metals as from depleted ore tailings by dump leaching. In certain processes, the rinse solutions are so dilute that a simple process of neutralization, precipitation and collection of an insol- uble precipitate suffices. However, in the case of cadmium and lead as examples, the allowable toxic metal levels in effluents are so low that removal by precipita¬ tion often does not suffice. In the case of the copper recovery from the acid leach dumps, the residual coπcen- tration of acid is so high as to require a substantial amount of base for its neutralization. In many industrial processes which formerly were able to employ lime for the precipitation of heavy metals and for the neutralization of acid such as sulfuric acid, with the formation of insoluble calcium sulfate, these are no longer environmentally acceptable because even the low level of contamination of heavy metals causes the solid waste to be classified as a toxic waste, requiring transportation to special dumps at considerable expense. Electrodialysis, including especially electro¬ dialytic water-splitting, processes are well known and of considerable value in industry. In electrodialysis, electrolytes are removed by the electric current from a feed compartment and selectively transported across ion- permeable membranes into a concentrate stream, with the feed stream being thus converted into a deionate stream. In water splitting, a feed stream contains anions and cations, wherein the anions of the feed stream plus hydrogen ions from the water pass by the current from a bipolar membrane into an acid compartment, while cations from the feed stream plus hydroxide ions from the water pass from the bipolar membrane into a base compartment. OMPI The electrodialysis process is highly developed and is described in several texts including the chapter by Shaffer and Mintz in "Principles of Desalination, Part A" edited by Spigler and Laird, Academic Press, New York 1980. Bipolar membranes and the process of water splitting are also well known. Bipolar membranes have been articles of commerce for several years, with those described by Dege, Chlanda et al ^ . , US Patents 4,116,8S9 and " 4,253,900 as recent examples. Water-splitting processes are also described in several recent patents including 3,787,304, 4,219,396, 4,238,305 and 4,017,015. Likewise, the technique of reverse osmosis (hereinafter "RO" ) is well known and has been utilized for various applications. For example, RO has been employed in the automobile industry to treat the rinse water emanating from various painting operations. Yet, these, technologies have not been hereto¬ fore utilized cojointly in a fashion to deal with the several and diverse problems associated with the problem streams described herein. It is accordingly an object of the invention to provide a process which will handle all these manifold problem streams, one which does not require elaborate chemical processing and one which can be operated on the very large scale of acid leach operations on the one hand as for copper recovery and also on a small scale for battery manufacture, smelters, electroplating, metal finishing and pickling operations on the other. Another general object of this invention provides a process which can eliminate the disposal problems associated with toxic wastes. A related and more specific object is to provide a process in which the toxic wastes that would-otherwise have to be disposed of are rendered useful so as to be capable of being returned in some fashion to either the manufacturing process involved or as an aid in the treatment of the stream resulting from such manufacturing process. BRIEF DESCRIPTION OF THE INVENTION This and other objects are realized in accor¬ dance with the present invention pursuant to which there is provided a process for the treatment of an aqueous stream containing a precipitatable material and an acid and/or base, comprising (a) separating the precipitatable material from the aqueous stream, (b) subjecting the aqueous stream to (i) a treatment to produce a relatively pure stream of water and a concentrated aqueous stream, and (ii) water split¬ ting to produce a stream of base, a stream of acid and a dilute aqueous stream of a concentration lower than the concentrated aqueous stream, the treatments (i) and (ii) being effected in either order, and (c) recycling at least part of the pure water stream produced in (b) (i) to an earlier stream either in the production leading to said aqueous stream or to step (a), (b)(i) or (b)((ii) or to another step in the process, (d) recycling at least part of the acid and/or base streams produced in (b)(ii) to an earlier stream either in the production leading to said aqueous stream or to another step in the process, and (e) recycling at least part of the lower con¬ centration stream produced in (b)(ii) to either (b)(i) or to another step in the process. In short, the logical order of operation is selected in order to maximize efficiency. More specifi¬ cally, the particular sequence employed will be dependent upon factors such as the parameters of the aqueous stream to be treated and the conditions desired for the manufac¬ turing process involved. However the operation is carried out, the present invention may be preferably and advantageously employed to wholly obviate the need for disposing of any stream. In short, the present invention can provide total reuseability of the aqueous stream. DETAILED DESCRIPTION OF THE INVENTION For illustrative purposes, one can consider a waste wash stream from the production of lead storage batteries, the stream comprising a dilute stream of _ sulfuric acid containing small amounts of heavy metals such as lead. Mere neutralization of the sulfuric acid with lime to produce insoluble calcium sulfate will not suffice since the precipitate is contaminated with lead so that it cannot simply be dumped. Either the lead must be removed or the precipitate must be disposed of in an expensive fashion. The present invention in effect separates and concentrates the lead to an extent that it may be treated in a smelter rather than being discarded while effective- ly recycling the sulfuric acid waste after purification and concentration. The invention is applicable to removal of other transition and/or heavy metals as well, e.g. nickel. cadmium, chromium, zinc, and the like as well as to streams not having metal ions or other precipitatable materials. Where the aqueous stream includes a precipita- table material, the first step in the process involves separation, typically separation of such material in ■ solid form as, for example, by adding magnesium hydroxide to a dilute sulfuric acid waste stream to form a dilute solution of magnesium sulfate, plus solid lead sulfate. This may be suitably followed by filtration in conven¬ tional presses or other filtration to remove the lead sulfate which can be treated, if desired, in a lead smelter to recover its lead content. In one embodiment, the residual stream of magnesium sulfate solution is subjected to RO, yielding a substantially pure stream of water and a more concen¬ trated solution of magnesium sulfate. The pure water may then be recycled to the battery manufacturing process, e.g. the initial washing operation or to any other step where needed. It is most economical to recycle all the water; although if desired, the pure water could be disposed of in whole or in part, so that none or only part of the water is used for a recycle. The concentrated magnesium sulfate solution is then subjected to electrodialytic splitting in a water splitting cell producing a partly demineralized feed for recycle, sulfuric acid and magnesium hydroxide, all of which are recycled. Again, as was the case with the pure water, it will be most economical to utilize the entire outputs from the water splitting for recycle, although there is no necessity to do so. Similarly, while the stream being treated is described as being aqueous, it will be appreciated by those skilled in the art that the stream can be any liquid which is capable of being treated in a water-splitting cell with the efficiency needed for the particular operation. Typically, this will mean that the stream will comprise principally water, with the quantity of other organic liquids that may be present being dictated by relative operability and efficiency considerations. Thus, in effect, the only material that need be withdrawn from the system is the heavy metal impurity, minimizing any waste disposal problems and need for large water supplies, except for small make-up quantities. In a variant, the sequence is changed but the various steps are substantially the same. The invention will be further described with reference to the accompanying drawings wherein: Figs. 1 and IA are schematic flow sheets of processes in accordance with the invention for treating a dilute sulfuric acid lead-containing solution, such as is obtained in a conventional washing operation in the production of lead-acid storage batteries; Fig. 2 is a schematic flow sheet of a process for treating waste water from pickling of iron; Figs. 3 and 3A are schematic flow sheets of processes for treating waste water from copper plating; Fig. 4 is a schematic flow sheet of a process for treating waste water from the extraction of copper; and Figs. 5 and 5A are schematic flow sheets of processes for treating waste water from the production of nickel-cadmium batteries. OJ to t H p- o Ui o I o where needed; and a base stream which is permitted to settle, the liquid being recycled to the water-splitting cell and the slurry being .recycled to the neutralization step. The water-splitting cell also produces a third stream containing some salts, less concentrated than the stream entering the water-splitting cell. This stream may be desirably recycled to either the water-splitting cell or to the RO step. In the preferred embodiment, sodium sulfate or other soluble salt is added to the water-splitting cell to prevent insoluble compounds such as magnesium and calcium hydroxide forming therein from fouling the membrane in the water-splitting cell, as described more fully in Gregor application Serial No. 542,916 , filed concurrently herewith, the disclosure of which is herein incorporated by reference. Alternatively, and while considered less desirable, other known techniques could be employed to prevent the potential fouling of the membrane as are described in the Gregor application. The details of construction of suitable water- splitting cells are likewise described in the Gregor application, the disclosure of which is herein incorpo¬ rated by reference. It has been found particularly desirable for this embodiment to utilize a three- compartment water-splitting cell, as is described in the Gregor application. By this process, the lead is removed from the wash water in a concentrated form which can be sent to a lead smelter; substantially everything else may be re¬ cycled with no water pollution or solid waste problems. OMPI - "' Any other metal ions in the starting waste stream, e.g. cadmium, will come down with the lead. If desired, the neutralization and filtration steps can be carried out in reverse order, i.e. filtra- tion being carried out prior to neutralization. In one variant, in place of magnesium hydrox¬ ide, only sodium hydroxide is employed. It will still yield lead sulfate, but the problem of solid magnesium hydroxide in the water-splitting cell will be reduced but not entirely eliminated because traces of metals and/or salts which cause precipitates are almost impossible to avoid, and other means of controlling them must be employed. These salts and/or others that could form precipitates within the water splitting cell can be re- moved by treating the feed stream of the water-splitting cell with selective ion exchange to remove the trouble¬ some salt forms. This process does require the addition¬ al treatment of the chemicals used to wash and regenerate the ion exchange system. The magnesium hydroxide option is accordingly preferred, however, since it means the volume of alkali used for neutralization will be less, a more insoluble heavy metal (lead) salt will result, the volume of base needed for neutralization is reduced so storage is -simplified, and the rejection of salts by the RO process is improved. Further advantages are that, when magnesium salts are involved, the water-splitting process produces magnesium hydroxide which, due to its insoluble nature, is quite concentrated and can be stored conveniently. Further, magnesium hydroxide is more effective than soluble bases in the precipitation of lead compounds. An additional benefit is that magnesium sulfate is easier to concentrate by RO than is sodium hydroxide. Magnesium sulfate produces about half the back osmotic pressure per neutralization equivalent as compared to sodium sulfate, which means that a lower RO pressure is required. Fur¬ ther, the RO permeate is more free of dissolved salts than when sodium salts are used. The use of magnesium salts in the water-splitting process is substantially problem-free, especially when certain dissolved electro- lytes are present in the water-splitting cell, as described in the above-identified Gregor application. Yet another variant involves utilizing a suit¬ able RO membrane which does not require a substantially neutral starting stream. There is thus no need for carrying out an initial neutralization, and the magnesium hydroxide produced from the water-splitting cell is merely recycled to such cell, rather than, in part, being recycled to the neutralization tank. Suitable membranes of this type are known, one such material being a synthetic polymer known as polybenzi idazale (PBI) (C7H6 2)n, made by Celanese Corporation. In the preferred illustrated embodiment of Fig. 1, the starting stream has a pH of about 0.8 to 2.5, preferably about 1 to 1.5 and a lead content of about 10 to 1000 ppm, preferably about 100 to 500 ppm. Neutrali¬ zation is carried out to bring the pH of about 7.8 to about 8.2, preferably about 8 which gives good results for precipitating lead as lead sulfate. After filtra¬ tion, the neutral effluent is then concentrated by RO to about 0.2 to 0.4 N MgSO-j. Depending upon the membrane employed, it may be necessary to adjust the pH, as in the case of a cellulose acetate membrane where a pH of about 6 is desirable. The acid necessary may be obtained from the acid side of the water-splitting cell. The purpose of this concentration is two-fold, to produce a pure water permeate for recycle or reuse, and a sufficiently concentrated feed which lowers the cost of the subsequent water-splitting process as compared to when a dilute feed is used. The RO permeate can be very pure, with less than 100 ppm of dissolved salts as a rule and very low levels of dissolved lead. However, since this effluent returns to the lead-acid plant, the presence of lead offers no problems. The backwash or blowdown from the ultrafiltration or microfiltration devices gives fairly concentrated lead materials which can be returned directly to a smelter. The RO concentrate is then passed into a three- compartment water-splitting device, employing bipolar membranes such as r^e_ sold by Allied Corporation to convert the anions contained therein into approximately 5% sulfuric acid. Acid of this concentration is readily returned to the lead-acid battery manufacturing process. Base produced by the water-splitting device is recycled to the neutralization process. In Fig. IA, the water-splitting step precedes the RO step, the acid stream from the water splitting again being recycled to battery manufacture and the base stream from the water splitting is again recycled to the neutralization process. In Fig. 2, there is shown an embodiment for the recycle and reuse of spent liquor and wash water from the pickling of iron or other metals. The spent pickle liquor is treated by water splitting to produce a suspen¬ sion of ferrous hydroxide along with sodium hydroxide and sodium chloride in solution. The .acid product stream is concentrated by electrodialysis to reconstitute the pickle acid for reuse. The acid rinse water is neutra¬ lized by base generated by the water-splitting cell and then concentrated by RO to produce pure water for reuse as rinse water and a concentrate which is recycled to the water-splitting cell. Suitable parameters are described in Fig. 2. The treatment of the rinse water of an acid- copper plating bath is shown in Fig. 3 where the rinse water originally is 0.006 N in sulfuric acid and 0.02 N in copper sulfate. This is then neutralized with either a suspension of magnesium hydroxide containing some sodium hydroxide or a solution of sodium hydroxide, both resulting from the water-splitting cell. After neutrali¬ zation, the pH is 9; and the solution has been effective¬ ly converted into magnesium and/or sodium sulfate. A precipitate of copper with traces of lead, zinc, cadmium and other metals is obtained and the precipitated material is then removed by ultrafiltration or micro- filtration in conjunction with ordinary filtration where necessary, to provide an appropriate pretreatment for RO. The pH of this water can then be reduced to approxi¬ mately the neutral point by acid generated by water splitting. This then provides the feed for RO which raises the concentration in the concentrate to 0.2 - 0.3 N in sodium sulfate or magnesium sulfate. This is the feed to the water-splitting device which produces a base product stream which is either sodium hydroxide or a mixture of magnesium hydroxide and sodium hydroxide, with at least 0.1 N sodium sulfate present. The acid product stream is approximately 1 N sulfuric acid which is returned to the copper-plating operation. The RO device produces pure rinse water for recycle, and the deionate from water splitting is returned to the feed to the RO process for recycle. In Fig. 3A, there is shown a variant of Fig. 3, the water splitting in Fig. 3A preceding the RO, but the steps being essentially the same. Fig. 4 shows a process for the treatment of acid leach liquors resulting from the dump-leach extraction of copper or a similar metal, wherein the leach liquor which contains usually 5 grams per liter of copper or more and where the pH of the leach liquor is approximately 1-2. To reduce water consumption, substan¬ tially all water is recycled. The process is similar to that of Fig. 1, with the leach liquor being neutralized by base, the metals separating out in solid form and being removed by a filter press or similar device. The neutralized stream can either be recycled for further extraction upon the addition of acid from water splitting or, if it has a high salt content, purified by RO, pro¬ ducing a concentrate which is the feed to the water splitting and pure water which returns to the process. Since water treatment costs are an important part of overall costs for this process, an optimal combination of water recycle and water treatment is employed. The process is in other respects as in Fig. 1 where the water-splitting cell provides base for neutralization and acid for continuing extraction. The concentrated acid can be used to dissolve the solid copper hydroxide pre- cipitate, and then metal is recovered electrolytically. Fig. 5 shows an embodiment for the treatment of the waste stream from the manufacture of nickel-cadmium OMPI batteries, one which is highly alkaline and contains nickel and cadmium along with traces of other toxic metals as insoluble hydroxides, carbonates or other insoluble basic salts. The process involves filtration (combined with microfiltration and/or ultrafiltration to remove suspended solids where desirable), followed by neutralization with acid produced by water splitting to provide a neutral feed for concentration by RO, with the RO permeate recycled as rinse water. The RO concentrate goes to the water-splitting cell which produces acid concentrated for neutralization and reuse, sodium hydroxide concentrated for reuse in the battery-forming operation, with the deionate recycled to the feed to the RO process. In Fig. 5A, the water splitting precedes the RO but the process is otherwise essentially the same as in Fig. 5. The invention will be further described in the following illustrative example wherein all parts are by weight unless otherwise expressed. Example By the process illustrated in Fig. 1, there is treated an effluent from the rinsing step in a lead-acid battery manufacturing operation. The effluent is supplied at the rate of 50 gallons per minute and is 0.04 N in sulfuric acid, containing 400 mg/1 of Pb. This passes into a neutralizing tank where a slurry of magne¬ sium hydroxide sufficient to raise the ph to 8 is added. The heavy suspended solids are removed by a press filter; and the residual, finely divided suspended solids are removed by microfiltration and/or ultrafiltration to provide the necessary pretreatment for RO, with the solids being recirculated to the filter press and an effluent of approximately 0.035 N magnesium sulfate with small amounts of sodium sulfate being the product. RO produces 0.3 N magnesium sulfate solution plus small amounts of water with the (permeate) water of high purity of less than 100 mg/1 of dissolved solids being returned for rinse water reuse. The RO concentrate then passes into the feed compartment of the water-splitting cell where it emerges as a deionate which is then recycled back to the feed of the RO plant for reconcentration. The acid product is approximately 3-5% sulfuric acid which is returned to battery manufacture. The base stream originally is approximately 0.1 N in sodium sulfate and is kept at that level through recycle. The base product stream consisting of magnesium hydroxide precipitate, sodium hydroxide and sodium sulfate is then treated to settle out the magnesium hydroxide concentrate as a high- solids slurry which is then sent to the neutralizing tank. The remainder is recycled to the base compartment. It is understood that the specification and examples are illustrative but not limitative of the present invention and that other embodiments within the spirit and scope of the invention will suggest themselves to those skilled in the art. OMPI

Claims: CLAIMS 1. A process for the treatment of an aqueous stream containing a precipitatable material and an acid and/or base, comprising (a) separating the precipitatable material from the aqueous stream, (b) subjecting the aqueous stream to (i) a treatment to produce a relatively pure stream of water and a concentrated aqueous stream, and (ii) water splitting to produce a stream of base, a stream of acid and a dilute aqueous stream of a concentration lower than the concentrated aqueous stream, the treatments (i) and (ii) being effected in either order, (c) recycling at least part of the pure water stream produced in (b)(i) to an earlier stream either in the production leading to said aqueous stream or to step (a), (b)(i) or (b)(ii) or to another step in the process, (d) recycling at least part of the acid and/or base streams produced in (b)(ii) to an earlier stream either in the production leading to said aqueous stream or to another step in the process, and (e) recycling at least part of the lower concentration stream produced in (b)(ii) to either (b)(i) or to another step in the process. 2. A process according to claim 1, comprising (a) separating the precipitatable material in solid form from the aqueous stream, (b) treating the aqueous stream from (a) to O5 produce a relatively pure stream of water and a concentrated aqueous stream, (c) recycling at least part of the pure water stream produced in (b) to an earlier stream either in the production leading to said aqueous stream or to step (a), 10 (b), (c) or to another step in the process, (d) subjecting the concentrated aqueous stream produced in (b) to water splitting thereby to produce a stream of base, a stream of acid and a dilute aqueous stream of a concentration lower than the concentrated 15 aqueous stream, (e) recycling at least part of the acid and/or base streams produced in (d) to the water splitting in (d) or to an earlier stream either in the production leading to said aqueous stream or to another step, in the 20 process, and (f) recycling at least part of the lower concentration stream produced in (d) to either the water splitting in (d) or to another step in the process. 3. A process according to claim 1, comprising (a) separating the precipitatable material in solid form from the aqueous stream, (b) subjecting the aqueous stream produced in (a) to water splitting thereby to produce a stream of base, a stream of acid and a dilute aqueous stream of a concentration lower than the original aqueous stream produced in (a), (c) recycling at least part of the acid and/or base streams produced in (b) to an earlier stream either in the production leading to said aqueous stream or to another step in the process, (d) recycling at least part of the dilute aqueous stream produced in (b) to either the water splitting in (b) or to another step in the process, (e) at least in part treating the dilute liquid stream from (b) to produce a relatively pure stream of water and a concentrated aqueous stream, (f) recycling at least in part the pure water stream produced in (e) to an earlier stream either in the production leading to said aqueous stream or to another step in the process, and (g) subjecting the concentrated liquid stream produced in (e) to water splitting in (b). 4. A process according to claim 1, wherein the precipitatable material are metal ions dissolved in the initial aqueous stream, the separation (a) being effected by neutralization to insolubilize the ions followed by filtration. 5. A process according to claim 1, wherein the aqueous stream treated in (b) is substantially neutralized prior to such treatment. 6. A process according to claim 5, wherein the neutralization is effected by the acid or base stream produced by water splitting. 7. A process according to claim 1, wherein the treatment in (b)(i) is reverse osmosis. 8. A process according to claim 1, wherein the treatment in (b)(ii) is an electrodialytic water splitting employing bipolar membranes. 9. A process according to claim 1, wherein the initial aqueous stream is acidic, the base stream produced in (b)(ii) being employed in (a) to insolubilize the precipitatable material. 10. A process according to claim 1, wherein the initial aqueous stream is alkaline, the acid stream produced in (b) (ii) being employed in (a) to insolubilize the precipitatable material. 11. A process according to claim 1, wherein the initial aqueous stream is a dilute sulfuric acid solution containing lead. OMPI 12. A process according to claim 1, wherein the initial aqueous stream is a dilute sulfuric acid solution containing lead and obtained in the production of a lead-acid battery, the acid stream produced in -05 (b)(ii) being recycled to an earlier stage in the battery production, and the base stream produced in (b)(ii) being employed in (a) to insolubilize the lead. 13. A process according to claim 1, wherein the initial aqueous stream is a dilute hydrochloric acid solution containing iron. 14. A process according to claim 1, wherein the initial aqueous stream is a dilute hydrochloric acid solution containing iron and obtained in the pickling of iron or steel, the acid stream produced in (b)(ii) being 05 .recycled to an early stage in the pickling-,-_and the base stream produced in (b)(ii) being employed in (a) to insolubilize the iron. 15. A process according to claim 1, wherein the initial aqueous stream is a dilute acid solution containing copper. 16. A process according to claim 1, wherein the initial aqueous stream is a dilute acid solution containing copper and obtained in the plating of copper, the acid stream produced in (b)(ii) being recycled to an 5 earlier stage in the plating, and the base stream produced in (b)(ii) being employed in (a) to insolubilize the copper. OMPI. 17. A process according to claim 1, wherein the initial aqueous stream is a dilute acid solution containing copper and obtained in the acid extraction of copper-containing material, the acid stream produced in (b)(ii) being recycled to an earlier stage in the extraction, and the base stream produced in (b)(ii) being employed in (a) to insolubilize the copper. 18. A process according to claim 1, wherein the initial aqueous stream is a dilute alkaline solution containing nickel and/or cadmium. 19. A process according to claim 1, wherein the initial aqueous stream is a dilute alkaline solution containing nickel and/or cadmium and obtained in the production of a nrckel-cadmium battery, the base stream produced in (b) (ii) being recycled to an earlier stage in the battery production, and the acid stream being employed in (a) to insolubilize the nickel and/or cadmium. 20. A process according to claim 1, wherein a solution of a salt of an anion and a cation which do not form a precipitate with any of the ions of the concentrated aqueous stream from step (b)(i) is introduced to the water-splitting cell having a bipolar membrane therein, whereby a non-adherent precipitate is formed. 21. A process according to claim 20, wherein said salt is an alkali metal salt. 22. A process according to claim 21, wherein said alkali metal salt is selected from the group com¬ prising sodium sulfate, chloride, nitrate, carbonate and mixtures thereof. 23. A process for the treatment of an aqueous stream containing an acid and/or base, comprising (a) subjecting the aqueous stream to (i) a treatment to produce a relatively pure stream of water and a concentrated aqueous stream, and (ii) water splitting to produce a stream of base, a stream of acid and a dilute aqueous stream of a concentration lower than the concentrated aqueous stream, the treatments (i) and (ii) being effected in either order, (b) recycling at least part of the pure water stream produced in (a)(i) to an earlier stream either in the production leading to said aqueous stream or to step (i) or (ii), (c) recycling at least part of the acid and/or base streams produced in (a)(ii) to an earlier stream either in the production leading to said aqueous stream or to an earlier step in the process, and (d) recycling at least part of the lower concentration stream produced in (a)(ii) to either (a)(i) or to another step in the process. 24. The invention as herein described and shown.

Inventors: GREGOR HARRY PAUL, MILTON EVERETT CHARLES, GREGOR, HARRY, PAUL, MILTON, EVERETT, CHARLES
Applicants: GNB BATTERIES INC, GNB BATTERIES INC.
Application year: 1984
Main classification: B01D13
IPC codes: B01D61, C02F1, C02F9, C22B7, C22B13, C22B15, C22B17, C22B23, C22B26, C23F1, H01M10