Chemical process for the recovery of alkaline and zinc-carbon battery components

Abstract

A process is described for the recovery of the chemical components of the “black paste” resulting from the opening of dead alkaline and zinc-carbon batteries.

Claims

1. A process of chemical treatment of black paste resulting from opening alkaline or zinc-carbon batteries or mixtures thereof, comprising the following steps: a) longitudinally cutting zinc-carbon or alkaline batteries or mixtures thereof dividing each of said batteries in two halves and passing the two halves thus obtained on a vibrating screen, causing leakage and selective dry extraction of the black paste; b) washing the black paste with water to separate potassium hydroxide of the alkaline batteries and ammonium chloride of zinc-carbon batteries in the form of a solution, and recovering a black paste fraction that is insoluble in water; c) treatment of the black paste fraction insoluble in water resulting from step b) with an aqueous solution of sulfuric acid, achieving the solubilisation of metallic zinc and of its compounds and of manganese compounds, and the salification of a residual potassium hydroxide with the formation of potassium sulfate; d) separating an insoluble residue of black paste consisting of manganese dioxide and carbon from the aqueous solution of sulfuric acid; e) treating the aqueous solution of sulfuric acid obtained in step d) with oxalic acid in sub-stoichiometric amounts compared to zinc, obtaining the precipitation of zinc oxalate; f) separation of zinc oxalate from the aqueous solution of sulfuric acid; g) electrolysis of the aqueous solution of sulfuric acid with formation of MnO.sub.2 at an anode.

2. The process according to claim 1, wherein in step b), 500 to 1000 liters of water are used per 100 kg of black paste.

3. The process according to claim 1 wherein, per 100 kg of starting black paste, in step c), 1200 to 2000 liters are used of an aqueous solution of sulfuric acid having a concentration of between 5 and 15% by weight.

4. The process according to claim 1, further comprising a further step b′), consisting in treating the aqueous solution separated after step b) with carbon dioxide, forming potassium carbonate (K.sub.2CO.sub.3).

5. The process according to claim 1, further comprising a further step f′), consisting in recirculating to step c) the aqueous solution of sulfuric acid separated in step f), obtaining the enrichment in manganese sulfates of the solution to be conveyed to electrolysis in step g).

6. The process according to claim 1, further comprising a further step g′), consisting in treating the solution recovered after step g) with further oxalic acid, to complete the precipitation of zinc residues.

7. The process according to claim 4, further comprising a further step h), consisting in adding the potassium carbonate produced in step b′) to the solution resulting from steps g), obtaining the precipitation of manganese (II) carbonate (MnCO.sub.3).

8. The process according to claim 1, further comprising a further step i), wherein the insoluble residue of black paste obtained in step d) is treated with the potassium hydroxide solution obtained in step b).

9. The process according to claim 2, wherein in step b), 700 to 800 liters of water are used per 100 kg of black paste.

10. The process according to claim 3 wherein, per 100 kg of starting black paste, in step c), about 1500 liters of said aqueous solution of sulfuric acid are used.

11. The process according to claim 3 wherein said aqueous solution of sulfuric acid has a concentration of about 8% by weight.

12. The process according to claim 4, further comprising a further step g′), consisting in treating the solution recovered after step g) with further oxalic acid, to complete the precipitation of zinc residues.

13. The process according to claim 12, further comprising a further step h), consisting in adding the potassium carbonate produced in step b′) to the solution resulting from step g′), obtaining the precipitation of manganese (II) carbonate (MnCO.sub.3).

14. The process according to claim 4, further comprising a further step i), wherein the insoluble residue of black paste obtained in step d) is treated with the potassium carbonate obtained in step b′).

Description

DETAILED DESCRIPTION OF THE INVENTION

(1) In the following description, reference is made to various solutions prepared in the course of the process of the invention; in some cases, it is indicated that these solutions contain salts, such as in the case of potassium sulfate which, however, as is known, are completely soluble in water; consequently, when the presence in solution of notoriously soluble salts is indicated hereinafter, it is meant that the solution contains as main constituents the ions constituting said salts, and that the latter may be precipitated from the solution by concentration thereof.

(2) The process of the invention is best applied if the treated cells are of a single type, and in particular only of the alkaline type (the alternative, the treatment of Zn-C batteries alone, is industrially less interesting due to their smaller diffusion compared to alkaline ones); however, the process can also be implemented on a mixture of alkaline and Zn-C batteries deriving from differentiated collection, which statistically comprises about 80 to 90% of alkaline batteries.

(3) In the first embodiment thereof, the process of the invention comprises a series of operations which enables the effective and quantitative recovery of the black paste components of Zn-C and alkaline batteries in view of their recycling in subsequent productions.

(4) The first step of the process, a), consists in the longitudinal cutting of the batteries and passage of the two halves thus obtained on a vibrating screen, which causes the leakage of the black paste from the open battery enclosure; the particular mode of opening of the batteries and extraction of the black paste by vibrating screen is described in the patent application “Station for cutting AA, D and/or C type batteries, process for the separation and recovery of components of said batteries and plant for carrying out such a process” filed concurrently with the present application. By operating in this way, it is possible to recover the black paste alone, without carrying in the subsequent operations residues of the other parts of the batteries, such as electrodes, parts of the metal enclosure or parts of organic fraction (paper and plastic) generally present on the outside of the batteries; this allows carrying out the subsequent chemical treatments with high efficacy.

(5) The next step, b), consists in the neutral washing of the black paste thus extracted with water between room temperature and 50° C., under constant stiffing. In this way, potassium hydroxide (KOH) deriving from the alkaline batteries (and possibly ammonium chloride, NH.sub.4Cl, of Zn-C batteries, but in much smaller amounts than KOH), is solubilized. The amount of water required for this operation is generally between about 500 and 1000 liters, preferably between 700 and 800 liters, per 100 kg of black paste.

(6) The resulting solution is separated from the water-insoluble fraction by physical methods, such as by centrifugation or preferably by filtration on filter press.

(7) The fraction of black paste not solubilized in the previous step, washed and still wet, is then processed, in step c) with a solution of sulfuric acid having a concentration of between 5 and 15% by weight, preferably of about 8% by weight; the sulfuric acid solution is used in amounts of between 1200 and 2000 liters, preferably about 1500 liters, for initial 100 kg of black paste, at a temperature between room temperature and 40° C., under constant stirring. In this operation, the dissolution of manganese oxides MnO and Mn.sub.2O.sub.3 formed from the dioxide, MnO.sub.2 during operation of the battery is accomplished; the metallic zinc (present in powder form in alkaline batteries and as fragments of shell enclosure of Zn-C batteries) and compounds of the element, such as oxide or hydroxide (ZnO and Zn(OH).sub.2) are also solubilized; and any residues of potassium hydroxide left in traces from step b) is also solubilized, forming potassium sulfate (K.sub.2SO.sub.4).

(8) The solid residue of this treatment is an insoluble part, consisting of MnO.sub.2, graphite electrodes (or the coal powder of Zn-C batteries), in addition to residues of the elements that in the initial battery separate the cathodic component from the anodic one. This solid is the main by-product of the process.

(9) Step d) consists in separating the sulfuric solution from this insoluble residue, preferably by filtration (filter press).

(10) In step e), the sulfuric solution obtained in the previous step is treated with oxalic acid; oxalic acid (C.sub.2H.sub.2O.sub.4, used preferably in the form of the dihydrate thereof, C.sub.2H.sub.2O.sub.4.Math.2H.sub.2O) is used in a slightly understoichiometric amount with respect to the amount of zinc ion present in the solution; the purpose of employing at this stage a slightly lower amount of oxalic acid than what would be required by the stoichiometry of the reaction with zinc is to ensure that an even slight excess of oxalic acid is avoided, which in the acidic solution would react with manganese, leading to a loss of yield in the recovery of the element and to a pollution of the zinc oxalate with manganese oxalate. The concentration of zinc ions in this solution, the knowledge of which is essential to determine the amount of oxalic acid to be used, is derived by atomic emission spectroscopy analysis with ICP source. Zinc oxalate dihydrate, ZnC.sub.2O.sub.4.Math.2H.sub.2O, is an insoluble salt which precipitates from the solution and can then be recovered by filtration in the subsequent step, f), of separation of the solid obtained from the solution; this separation is preferably carried out by filtration (filter press). A very pure salt (>99%) is thus obtained, which is the third product of the process.

(11) The remaining sulfuric solution mainly contains manganese (II) and (III) sulfates, the non-precipitated residue of zinc sulfate, potassium sulfate and sulfuric acid.

(12) In the next step, g), the sulfuric solution separated in step f) is subjected to electrolysis, obtaining the formation at the anode of the manganese (IV) oxide, MnO.sub.2. The cell, thermostated at 50° C., and with platinum electrodes, has a consumption of about 4 kWh per kg of MnO.sub.2 produced.

(13) The MnO.sub.2 thus recovered, known in the industry as “Electrolytic Manganese Dioxide” or its abbreviation EMD, is a high-purity material that can be recycled to produce new batteries.

(14) Finally, the sulfuric solution recovered after the electrolysis of step g) is returned to step c).

(15) In a preferred embodiment, the process of the invention comprises one or more of the following additional and optional steps which further increase the effectiveness of recovery of the chemical components of black paste.

(16) A first possible step is step b′), which can be carried out in parallel to the process and without any temporal relation (or execution order) with respect to the other operations of the process itself. In this step b′), the aqueous solution separated after step b), containing potassium hydroxide, is treated with carbon dioxide, which may result for example from the flue gas of the carbon residues of black paste; from the so treated solution, after concentration thereof, potassium carbonate (K.sub.2CO.sub.3) is obtained which can be used in further process steps, as described hereinafter.

(17) A second possible additional step, f′), consists in recirculating the sulfuric solution separated in step f) to step c), i.e. to the sulfuric acid addition step. In this way, the sulfuric solution is conveyed to electrolysis only after the build-up of chemical components resulting from two or more charges of black paste in the process. The object is to obtain the enrichment of the solution in manganese sulfates which is then separated in step f) and sent to electrolysis in step g), to obtain a higher yield in MnO.sub.2 in the latter.

(18) Another optional step, g′), consists in the treatment with further oxalic acid of the solution recovered after step g) in which EMD has formed, to complete the precipitation of zinc residues, recovering by physical separation a further amount of zinc oxalate which is added to that recovered in step f). Zinc oxalate can be sold as raw material in the chemical industry.

(19) The potassium carbonate produced in step b′) can be added, in a further optional step h), to the solution resulting from steps g) or g′), resulting in the precipitation of manganese (II) carbonate (MnCO.sub.3), which precipitates as a solid, and of further potassium sulfate. The manganese (II) ion forming the carbonate is that residual from the electrolysis step: it is known that the electrolysis operations are never lengthened until completion, because in the latter stages thereof, when the reagent species reaches low concentrations, the efficiency of the electrolytic discharge reaction of the desired species decreases drastically, electricity consumption increases considerably and parasitic reactions are established. After precipitation, MnCO.sub.3 is physically separated (e.g. by filtration) and the resulting solution is concentrated to recover potassium sulfate, which can be sold for the production of fertilizers for agriculture.

(20) Finally, in one last possible optional step i), the solid residue of black paste separated from the sulfuric solution in step d) can be treated with the KOH solution obtained in step b), or with the solution of potassium carbonate produced in step b′), to neutralize this residue before drying it for sale.

(21) The invention will be further described in the following experimental section.

EXAMPLE 1

(22) This example relates to a complete treatment process of black paste resulting from alkaline batteries.

(23) 140 kg of alkaline batteries from the recovery of dead batteries are treated. After sorting, separation by type, treatment of the integrated system with cutting, deferrization (i.e. separation of the iron part using magnets) and screening (specially to remove fragments of plastics), the crude black paste is subjected to washing with 750 L water (step b)). A suspension is formed, which is separated by filtration in an aqueous solution of KOH, yielding 114 kg of wet black paste; on this material, with a measurement using a Sartorius thermobalance, a moisture content equal to about 31.6% (equivalent to 78 kg of dry black paste) is determined.

(24) A chemical analysis is carried out on a small part of this black paste by atomic emission spectroscopy with ICP source. The following results are obtained for the concentrations of the main elements:

(25) Zn: 25.6%;

(26) Mn: 30.5% (total manganese, all oxidation states);

(27) K: 0.77%;

(28) C: 7%.

(29) The wet black paste obtained in the previous step is treated with 1500 L of an aqueous solution of H.sub.2SO.sub.4 at a concentration of 8% by weight (step c)).

(30) The suspension thus obtained is filtered (step d)).

(31) A new (sulfuric) solution and a new solid residue are obtained.

(32) The sulfuric solution obtained in the previous step is treated with 20 kg of oxalic acid dihydrate (step e)); the formation of 54 kg of a precipitate is observed, which is separated by filtration from the supernatant solution (step f)).

(33) The resulting solid consists of wet zinc oxalate and, upon an analysis with a thermobalance of a sample of the same, it results constituted by about 44.7% moisture, equal to 24.1 kg of water; by difference, it is noted that the solid contains an amount of anhydrous zinc oxalate equal to 29.9 kg.

(34) The liquid phase separated in step f) is subjected to electrolysis (step g)), obtaining the formation of the 1a anode of 4.37 kg manganese (IV) oxide, MnO.sub.2. The cell, thermostated at 50° C. and using platinum electrodes, has a consumption of about 4 kWh per kg of MnO.sub.2 produced.