DAHAL MADHAV P (CA)
GEISLER ROBERT A (CA)
DAHAL MADHAV P (CA)
| US4043599A | 1977-08-23 | |||
| US3868439A | 1975-02-25 | |||
| US3347662A | 1967-10-17 | |||
| US20060002834A1 | 2006-01-05 | |||
| US4376098A | 1983-03-08 |
| CLAIMS 1. A process of leaching mineral values from a permeable ore body or from particulates derived from an ore, the ore having metal carbonate and metal sulfide components, comprising: a) leaching first the carbonates with an aqueous leachant comprising an acid selected to dissolve the carbonates but not the sulfides, while for in situ ores controlling the leach rate to avoid release of CO2 gas in the ore body; b) leaching the sulfides with an aqueous leachant comprising a multivalent metal salt able to oxidize the sulfides into soluble oxidation products; and c) recovering the desired metal values from the separate leachates. 2. The process of claim 1 , wherein the leaching steps are carried out in situ in a permeable ore body. 3. The process of claim 2, wherein the rate of leaching in step a) is controlled by adjusting leachant pressure, temperature and concentration to avoid CO2 gas release in situ. 4. The process of claim 3, wherein between steps a) and b) the leached in situ strata are rinsed to remove acid leachant remaining from step a). 5. The process of claim 1 , wherein the leaching steps are carried out on ore-derived particulates of the types: crushed ore, ore concentrates and mine discharge tailings. 6. The process of any one of claims 1 to 5, wherein the acid component of step a) leachant is selected from acetic, formic, nitric, sulphuric, hydrochloric, fluoboric acid and fluosilicic acid. 7. The process of claim 6, wherein the acid of step a) is acetic and the metals recovered from step a) leachate comprise manganese calcium and magnesium. 8. The process of any one of claims 1 to 7, wherein the salt-containing leachant of step b) is an aqueous solution of a salt of a metal having multiple valence states, and in the highest valence state. 9. The process of claim 8, wherein the metal is selected primarily from Fe containing compounds. 10. The process of claim 8, wherein leachant of step b) comprises a ferric salt selected to oxidize the sulfides present. 11. The process of claim 10, wherein the ferric salt is at least one of the fluosilicate, the fluoborate, the sulphate and the nitrate, and the metals recovered mainly comprise lead and zinc. 12. In the process of leaching metal carbonate-containing permeable ore bodies with acid leachant, the improvement comprising: adjusting the leachant pressure, temperature and acid concentration to control the leach rate to rates that avoid the release of CO2 gas in the ore body, and maintain the ore body permeability. 13. The process of claim 12, wherein the threshold of CO2 gas release is determined by maximum solubility of the gas in the leachate under the temperature and pressure employed underground and the leach rate is controlled so that the dissolved CO2 is below this threshold. |
This invention relates to a mineral recovery process employing target selective in situ or ex situ leaching to recover minerals, some of which occur as carbonates and the others as sulphides and in the former case from a permeable host. Mineral recovery is performed from the host in two consecutive steps: (1) extraction of calcium, manganese, magnesium and associated carbonate minerals leaching with e.g. dilute acetic acid followed by (2) extraction of lead, zinc and associated sulphide minerals by again leaching the host now with e.g. a ferric salt. During (1), the strength of the acetic acid is adjusted according to the subsurface conditions to prevent creating excess CO 2 gas and thereby blocking bedrock permeability avenues to prevent acid delivery for subsequent mineral digestion. The leachant concentration is a function of target temperature plus atmospheric pressure (depth). Ex situ targets do not require pressure and temperature adjustments. Re-circulation of leachant may be necessary to completely extract the total amount of target minerals in the host. The carbonate mineral depleted host is then re-leached in step (2) with e.g. a ferric salt to recover its remaining Pb, Zn and associated sulphide minerals. The leachate from steps (1) and (2) are separately treated chemically to selectively recover their dissolved constituents to yield high value industrial products ready for sale. The technology has a particular advantage in the recovery of manganese for use in lithium ion batteries because it prevents formation of fine metallic particles in the manganese product which happens during conventional mining recovery and consequently could potentially short circuit batteries for which it is used.
BACKGROUND OF THE INVENTION AND PRIOR ART The main traditional industrial use for calcium has been in its carbonate form (CaCO 3 ) as a filler for paper and rubber. Recently its use has risen as a filler for plastics and paints in the form of increasingly smaller particles in the sub nanometer range in order to provide improved characteristics to its hosts resulting from the diminished size of the calcium material. In some instances the improvements to the host have been sufficiently pronounced to warrant dramatic increase in the price of the calcium material. For use as a filler the calcium material attributes of main concern to the buyer are particle size, uniformity and packing density which are the chief controls of performance. Calcium is also widely utilized as a soil supplement or fertilizer and to a lesser extent in pharmaceuticals.
Calcium occurs mainly as calcium carbonate referred to as limestone, or in the form of calcium magnesium carbonate referred to as dolomite. Both are marine deposits usually of substantial size. They are generally mined on a large scale by open pit and the individual components selectively recovered by mechanical or chemical means. The chief form of manganese ore is as manganese dioxide (pyrolusite), MnO 2 . Deposits are usually as veins recovered by underground mining. The main use of manganese is as a steel alloy. It is recovered in large pieces, crushed to useable size and fed with iron ore into blast furnaces to make steel. In this way it does not command a very high price. It also has some chemical uses. Recently manganese has become increasingly important however as the principal component in rechargeable batteries utilized for a growing variety of industrial, electronic and power equipment extending to automobile batteries with concomitant increase in price. The desired form for batteries is as lithiated manganese dioxide (Li Mn 2 O 4 ) referred to as LMD.
Pyrolusite can and is being used for this purpose. It is mined, crushed, dissolved into a solution and electrochemically recovered as electrolytic manganese dioxide (EMD). This must then be re-crushed and treated with a lithium compound at high temperature to form LMD. This process is a complicated and costly procedure. In addition it has been found that the resulting LMD frequently contains minute metal particles that apparently could cause the batteries made from it to short circuit. The particles might not be removed electromagnetically nor can their presence be completely identified by scanning electron micrograph (SEM). The solution to the problem so far has been to test all new batteries employing LMD and discard those that are found to be faulty. Alternatively multiple treatment steps may be utilized to purify MnO 2 as a precursor material. We have found to our surprise that manganese as carbonate veins that cannot be economically mined normally but which exist in geology with sufficient permeability can be advantageously recovered by in situ leach mining (ISLM) as leachate producing high purity LMD. Such solution is free of metal particles because it does not entail conventional mining or crushing and thus have the possibility of causing electrical short circuit problems in batteries for which it is employed. Moreover the presence of calcium carbonate with the manganese that normally occurs in such settings offers the opportunity for its recovery as well with the manganese thereby further increasing the economics of the process. A patent search disclosed two methods, one proposed by Geisler in United States Patent 5,523,066 and the other by Turner in United States Patent 6,726,828, that describe use of ISLM utilizing a mixture of acetic acid and hydrogen peroxide (for sulphide oxidation) to recover Ca, Mn, Pb and Zn as a combined leachate from a permeable geological host. Both methods rely on a separate oxidant (i.e. peroxide) and take no precautions against progressive subsurface blockage of flow-channels preventing further leaching. Neither of these methods suggest what is proposed herein.
Another patent noted (United States Patent No. 4,500,398) treated sulfide ore with fluosilicic acid plus an oxidizing agent, to release the metal values.
SUMMARY OF THE INVENTION The invention includes a process of leaching mineral values from ores having metal carbonate and metal sulfide components, comprising: leaching the carbonates with an acid leachant selected to dissolve the carbonates but not the sulfides at a rate chosen to avoid in situ release of CO 2 gas and subsequently leaching the sulfides with an oxidative leachant to dissolve the sulfides followed by selective recovery of desired metal values from the separate leachates.
The ore-derived particulates may include crushed ores, ore concentrates and mine discharge tailings. Various acids may be selected for step a) leachant e.g. acetic, formic, nitric, sulphuric, hydrochloric, fluosilicic acid and fluoboric acid.
For step b), the oxidative leachant comprises a selected salt of a metal having multiple valence states, and in the highest valence state. Preferred salts for the step b) oxidative leachant include ferric fluosilicate, ferric fluoborate, ferric sulphate and ferric nitrate.
Leach step b) has been found to be more efficient if a rinse step is inserted between steps a) and b).
In a broad aspect, the invention comprises the ore body carbonate acid leach (independent of the sulfide leach) controlled to a leach rate that avoids the release of
CO 2 gas in the ore body and maintains the ore permeability. The leach rate is controlled by adjusting leachant pressure, temperature and acid concentration to provide a leach rate below that where CO 2 gas begins to be released. This has been found to maintain the ore body permeability. The threshold of CO 2 gas release can be found by comparing the gas dissolved in the leachate with the maximum solubility under temperature and pressure employed underground.
DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS
In one embodiment Ca, Mn and Pb (in sulfide form) are recovered from a carbonate host containing same by means of two-stage ISL mining techniques well known to those skilled in the art. The Ca and Mn are initially recovered by employing a dilute acetic acid leach. Following completion of this step, the wellfield being leached is rinsed with water to remove all traces of acetic acid and the deposit is re-leached with ferric fluorosilicate solution to recover remaining Pb. The chemical reactions of two sequential leaching steps are depicted below as (A) and (B). INITIAL LEACH (A)
(A) Carbonate Leaching Reactions Calcium and manganese carbonates react with acetic acid leachant to form soluble calcium and manganese acetates.
CaCO 3 + 2CH 3 COOH = (CH 3 COO) 2 Ca + CO 2 + H 2 O MnCO 3 + 2CH 3 COOH = (CH 3 COO) 2 Mn + CO 2 + H 2 O (A) Calcium Recovery Reactions
Calcium is selectively precipitated from the leachate consisting of a mixture of calcium and manganese acetate employing sulfuric acid. This is possible because calcium sulfate is insoluble whereas manganese sulfate is a soluble compound. This step also regenerates the leachant (acetic acid). Calcium sulfate is subsequently converted to precipitated calcium carbonate by reacting it with ammonium carbonate. Ammonium sulfate is produced as a high purity saleable byproduct during this process.
(CH 3 COO) 2 Ca + H 2 SO 4 = CaSO 4 + 2CH 3 COOH CaSO 4 + (NH 4 ) 2 CO 3 = CaCO 3 + (NH 4 ) 2 SO 4
(A) Manganese Recovery Reactions Calcium stripped leachate consisting mainly of manganese acetate is treated with potassium permanganate to selectively oxidize manganese to manganese dioxide. Manganese dioxide thus obtained may be used as a precursor material to make lithiated manganese dioxide by heating it with lithium carbonate at higher temperature. Manganese could also be selectively recovered by solvent extraction. 3Mn 2+ + 2KMnO 4 + 2H 2 O→ 5MnO 2 + 4H + + 2K +
The regenerated leachant is injected underground forming a closed loop operation. Subsequent Leach (B)
(B) Lead Leaching Reaction Using Ferric Fluosilicate Leachant
Fe 2 (SiFe) 3 + PbS -> 2FeSiF 6 + PbSiF 6 + S In a preferred aspect lead is recovered as high purity lead metal by electrowinning from the resulting leachate. The electrowinning process regenerates the original leachant by oxidizing ferrous fluosilicate to ferric fluosilicate at the anode and the ferric fluosilicate is recovered for recycle.
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