AU624286B2

AU624286B2 - Extraction and recovery of gold

Info

Publication number: AU624286B2
Application number: AU73031/91A
Authority: AU
Inventors: Craig Clinton Kenna
Original assignee: CRA Services Ltd
Current assignee: Rio Tinto Services Ltd
Priority date: 1990-02-23
Filing date: 1991-02-19
Publication date: 1992-06-04
Anticipated expiration: 2011-02-19
Also published as: AU7303191A

Description

EXTRACTION AND RECOVERY OF GOLD

FIELD OF INVENTION;

This invention relates to the extraction and recovery of gold from gold-bearing material. Such material encompasses gold-bearing ores, concentrates, anodic slimes and residues, as well as gold-bearing metallic scrap, and materials previously treated by roasting, bacterial leaching, pressure leaching or other techniques required to liberate the gold from its matrix.

The invention relates to the extraction and recovery of gold from gold-bearing materials, for example those above mentioned, using leaching methods such as continuous or batch stirred-tank agitation, vat leaching, or the in situ techniques such as dump and heap leaching, or the _in situ technique of solution mining.

SUBSTITUTESHEET Background of the Invention:

At present, the conventional cyanide leach process is used almost universally to extract gold. However, the growing concern over safety and environmental hazards associated with the use of cyanide combined with the limited use of the process for treatment of problematic gold ores (e.g., refractory sulfide ores, carbonaceous ores, ores containing significant amounts of cyanocides) requires development of an economically viable, alternative leach process.

Gold is readily dissolved in acidified solutions containing thiourea, using manganese dioxide, hydrogen peroxide or ferric ions as the oxidant [D.W. Bilston, R.N. Millet and J.T. Woodcock (1987) Proc. Confer. "Research and Development in Extractive Metallurgy" (Aus. I.M.M. Melbourne) pp. 19-28]. However, this gold dissolution process has found little application in the gold industry. The main drawback has been the excessive oxidative degradation of thiourea which occurs in the presence of the above mentioned oxidants. The relevant chemical reactions can be written in two stages involving initial oxidation to formamidine disulfided) , followed by further irreversible decomposition to sulfur, cyanamide and thiourea(2) .

Fe + tu - i(tu)₂ ²⁺ + Fe²⁺ (1)

( u 2 ⁺— sulfinic compound ^ S + CN(NH₂ ) + tu ....(2)

where tu = thiourea and (tu)„²⁺ = formamidine disulfide. Reaction (1) is much faster than reaction (2) and was considered as the dominant reaction in determining the relative consumption of thiourea. Furthermore, the rapid consumption of thiourea during the leach process is often associated with passivation of gold in the feed material, and hence low gold recoveries. Consequently, in the past, the thiourea leaching process has proved very unattractive in comparison with the universally accepted cyanidation process.

In recent work it has been shown that the use of sulphur dioxide in conjunction with thiourea significantly reduces reagent loss through oxidative degradation (R.G. Schulze (1984) J. Metals 3jS (6) pp. 62-653. However, the lowering of thiourea consumption by using sulphur dioxide has not always been achieved in practice [D.W. Bilston, R.N. Millet and J.T. Woodcock (1987) Proc. Conf. "Research and Development in Extractive Metallurgy" (Aus. I.M.M. Melbourne) pp. 19-28]. The same workers have also patented the use of a substituted thiourea, i.e. ethylene thiourea. This particular derivative is more stable to oxidation and exhibits a far greater resistance to oxidative degradation than thiourea [R.G. Schulze (1983) German Patent 3347165]. However, the cost of ethylene thiourea is too high to be considered as an economic alternative.

Summary of the Invention:

The present invention is based on the discovery that

3+ the oxidative degradation of thiourea by Fe is markedly reduced by the use of chemical reagents which have the ability to complex Fe in acidic solutions. The invention accordingly provides a process for the hydrometallurgical recovery of gold from gold-bearing material comprising the step of treating gold-bearing material with an acidic lixiviant solution containing thiourea and ferric ions, characterised in that the said solution also includes a complexing agent for ferric ions.

3+ The oxidising power or strength of Fe is reduced to an extent where gold dissolution still occurs at an appreciable rate and the oxidative degradation of thiourea

3+ by Fe is markedly reduced.

1+ Gold in solution as the Au(thiourea) species, in

3+ the presence of Fe and these chemical reagents, can be recovered using known techniques, eg. absorption on activated carbon or resins; cementation with iron or aluminium; electrowon using porous carbon electrodes; reduced using hydrogen; or solvent extracted. Thus the invention extends to methods of extracting and recovering gold from gold-bearing material.

COMPARISON WITH THE PRIOR ART

The present invention differs from the prior art in this field since the essence of the present invention

3+ involves the deliberate complexation of Fe , with the aim

3+ to lower the oxidising power of Fe , which results in a marked reduction in the oxidative loss of thiourea. The essence of other patents in this field is described as follows.

GB 2 152 488 R. Schulze (SKW Trostberg)

Relates to the use of cyclic derivatives of thiourea as complexants for gold. The relevant cyclic thioureas are ethylene thiourea .and propylene thiourea. The cyclic thioureas exhibit greater resistance to oxidative degradation compared to thiourea, whilst still allowing satisfactory gold complexation and gold leaching kinetics. US 4 561 947 R. Schulze (SKW Trostberg)

Relates to the use of SO , sulfur dioxide; (or other compounds that provide a source of S0₂, such as sulfites, hydrogen sulfites, pyrosulfites and the like); as a reductant for regenerating oxidised thiourea, (i.e. formamidine disulfide) . In the leach process, SO₂ is used in conjunction with thiourea and an oxidant, (ie. usually Fe 3+) , to control the leach potential at a desired value where satisfactory precious metal leaching rates are achieved and thiourea degradation is minimised. In this invention, the leach potential is continuously controlled by the use of SO-, which one would expect to first act by

^Δ 3+ reducing a majority of the Fe ion that that is present to Fe ion. The leach potential value will determine the

3+ 2+ extent of the reduction of Fe to Fe . Due to the chemistry of this invention, the predominant oxidant that exists under typical leach conditions is formamidine

3+ disulfide. The complexation of Fe is not an issue in this invention.

GB 2 181 722 R. H. Little

Relates to the use of thiourea in conjunction with urea and potassium lignin sulfonate for the extraction and recovery of precious metals. The role of these compounds in the thiourea leaching reaction is unclear. However, these compounds may effect the recovery of precious metals from thiourea containing solutions by co-adsorbing onto activated carbon and increasing the cation exchange properties of the carbon, and thus increasing the efficiency of the recovery of the precious etal-thiourea complexes using activated carbon. Urea and potassium lignin sulfonate do not form any significant complexes with ferric ions and therefore this invention has no similarities with the present invention. S. Afr. ZA 85/4463 B. K. Loveday et. al. (Anglo American Corp. of Sth. Afr.)

Relates to in situ recovery of gold from the fines on a footwall and in the fissures and cracks therein by passing a solution capable of solubilising the gold across the footwall. An acid solution containing 0.2-1.0 g/1

3+ thiourea and optionally 0.75 g/1 Fe and 1.3 g/1 Na^SO-^ was applied for leaching of gold. The sprayed on solution was collected in a sump for recirculation. Dissolved gold was recovered by passing the loaded solution through a column of activated carbon. This patent is concerned with a leaching technique rather than any specific novel leaching chemistry.

Detailed Description of the Invention:

In simple terms, to leach gold in the presence of thiourea, a leach potential in excess of 380mV vs. N.H.E. is required. However, a leach potential above 420 mV vs.

N.H.E. will also result in the oxidation of thiourea. The oxidation potential of uncomplexed Fe ion is 770mV vs.

N.H.E.. As expected, both gold and thiourea will oxidise

3+ 3+ m the presence of uncomplexed Fe . By complexing Fe ,

3+ the oxidising potential of Fe can be reduced well below

770 mV vs. N.H.E.. The oxidation of gold still occurs at a satisfactory rate, whilst the oxidative loss of thiourea is markedly reduced. As a practical matter, it is preferred to operate at an oxidising potential between 390 and 500 mV vs. N.H.E.

3+ The complexation of Fe in acid solution, say

3+ pH<7, can be achieved by a number of compounds. The Fe complexing reagents can be added as commercially available salts or they can be synthesised as a crude product,

3+ (typically a mixture of Fe complexing reagents). For example, the crude product could be made chemically; e.g. by oxidation of cellulosic material to form a complex mixture of polyols, hydroxycarboxylic acids and carboxylic acids which can provide a complexing solution meeting the requirements of this invention, or the crude product can be made biologically; e.g. by using microorganisms such as the fungi Asperqillus niσer to produce carboxylic acids, such as citric acid, that complex Fe 3+

3+ A list of some relevant Fe complexing reagents is given in table 1.

Preferred complexing reagents are compounds which can form ferric complexes having a stability constant of log K greater than 1, and preferably greater than 2.0.

Convenient compilations providing stability constants of many complexing agents for iron are Martell and Calvin, "Chemistry of the Metal Chelate Compounds", U.S. copyright 1952, and "Stability Constants of Metal-Ion Complexes," supplement No. 1, Special Publication No. 25, published by The Chemical Society, U.S. copyright 1971.

The general leach conditions for the "modified" Fe 3+/thiourea gold leaching system (i.e. using complexed Fe 3+) are summarised in Table 2. The range of conditions

₃-₁- listed in Table 2 covers the use of all the Fe complexants given in Table 1.

3+ A comparison of the rate of reaction between Fe and thiourea in the presence and absence of a Fe 3+ complexant (i.e. 0.05M oxalic acid), is illustrated in Figure 1. These data were generated by reaction of 0.05M

3+ thiourea with 0.01M Fe in 0.1M H S0₄ at 25°C. A value of 100% relative thiourea consumption was taken as the

3+ point where all of the Fe ion had been reduced to

Fe ion.

It is clear that the reduction in the oxidative strength of Fe 3+ by complexation with oxalic acid has been effective in lowering the consumption of thiourea. However, the complexation of Fe 3+ by oxalic acid, while lowering the consumption of thiourea, does not have any detrimental effect on the gold leaching reaction. This is

SUBSTITUTESHEET illustrated in Figure 2 where the dissolution of a rotating gold disc electrode was examined. ^• Figure 2 illustrates the effect of 0.05M oxalic acid and solution age on the dissolution of a gold rotating disc electrode.

3+ The initial leach solution contained 0.005M Fe and 0.05M thiourea (0.1M sulfuric acid background, 25°C). In the absence of oxalic acid, the rate of gold dissolution steadily decreased as the solution age increased.

After 20 hours, the rate of gold dissolution was markedly reduced, (i.e. by approximately 73%) and the gold surface had a dark brown appearance which is indicative of some form of passivation. In contrast, the rate of gold dissolution in the presence of oxalic acid exhibited a far more gradual decrease with increasing solution age. For example, after 960 hours (i.e. 40 days), the rate of gold dissolution had decreased by only 40%. The gold surface also maintained a bright lustrous appearance, showing no evidence of passivation.

The "modified" Fe 3+/thiourea gold leaching system was also applied to a column leach experiment which was aimed at simulating a heap leaching operation of a gold ore. The conditions are summarised below:

General Column Leach Conditions

Ore type Refractory, low grade pyritic ore (ca. 7 kg grading 1.2 pp gold)

Ore pre-treatment A biological "heap leaching" simulation was carried out on the ore packed in the column. A target of ca.>80% pyrite oxidation was set prior to any attempts at gold leaching.

SUBSTITUTESHEET Gold Leaching The ore was initially leached with a

(at ambient temp) ssuullpphhuurriicc aacciidd ssoolluuttiioonn ccoomntaining oxalate to stabilize the Fe 3+ concentration. Once the Fe 3+ concentration was stabilized, thiourea was added to the leachant solution.

SUBSTITUTESHEET - 9 -

3+ Gold Leachant Fe ca. 0.005M oxalic acid 0.056M

H₂S0₄ 0.100M thiourea 0.065M

Percolation rate ca. 32 ml/hour (average over 32 days)

The column leaching results are summarised in Table 3. A plot of gold extraction (%) vs . the number of days is given in Figure 3. Extrapolation from day no. 27 (i.e. where thiourea addition was ceased), shows that ca. 80% recovery can be expected after ca. 43 days if thiourea addition was continued throughout.

In summary, the results are extremely encouraging with respect to gold recovery, leaching kinetics, and thiourea consumption. This technology also creates new possibilities for treating low grade gold ores which are either inherently acidic or require an acidic pretreatment step such as biological oxidation. The application of alkaline cyanidation under these circumstances is limited due to the need for expensive and most likely ineffective neutralisation, and more than likely high cyanide consumption.

Recovery of gold from the modified acid-thiourea leaching systems was achieved by cementation of gold into iron powder. However other techniques as described by Deschnes (G. Deschnes (1986) C.I.M. Bulletin, 7 pp. 76-83.], such as absorption on carbon, electrowinning, solvent extraction, hydrogen reduction or cementation on lead powder are equally applicable. In a typical experiment, iron powder was added to a solution containing 100 ppm Au(tu) , 0.066M thiourea, 0.1M sulphuric acid and 0.05M oxalic acid. Approximately 90% of the gold in solution was cemented out after 30 minutes. - 10 -

TABLE 1: RELEVANT ACID-STABLE COMPLEXING AGENTS FOR 3+

Fe WHICH ARE APPLICABLE TO THE "MODIFIED' Fe ³⁺/THIOUREA GOLD LEACHING SYSTEM

General Type Examples

carboxylic acids oxalic acid and oxalate (di-and tri-) salts, citric acid and citrate salts, tartaric acid and tartrate salts, gluconic acid and gluconate salts.

phosphate based phosphoric acid and phosphate reagents salts, ortho-phosphate salts, pyro-phosphate salts, poly-phosphate salts.

thiocyanate ammonium thiocyanate sodium thiocyanate

fluorides hydrofluoric acid sodium fluoride

fluorosilicate fluorosilicic acid fluorosilicate salts

EDTA ethylene diamine tetra acetic acid, EDTA salts. - 11

TABLE 2: GENERAL CONDITIONS FOR THE "MODIFIED" FERRIC/THIOUREA GOLD LEACHING SYSTEM

VARIABLE CONDITIONS

Fe 0.0025 to 0.1M

Thiourea 0.005 to 0.4M preferably 0.02 to 0.4M

pH 0.5 to 4.5

Potential 350 to 700 mV vs NHE (Normal Hydrogen Electrode)

3+

Fe complexants 0.01 to 1.0M preferably 0.01 to 0.2M

Temperature 10 to 90° C

- 12 -

TABLE 3: COLUMN LEACH TEST RESULTS USING THE

"MODIFIED" FERRIC-THIOUREA LEACH SYSTEM.

NUMBER OF DAYS %GOLD EXTRACTION

18.0

10 36.1

15 45.7

22 57.9

32 68.7

NB: 1. After 27 days, thiourea addition was stopped 2. % thiourea recovered after 32 days = 98%

It will be clearly understood that the invention in its general aspects is not limited to the specific details referred to hereinabove.

Claims

- -CLAIMS

1. A process for the hydrometallurgical recovery of gold from gold-bearing material comprising the step of treating gold-bearing material with an acidic lixiviant solution containing thiourea and ferric ions, characterised in that the said solution also includes a complexing agent for ferric ions.

2. A process according to claim 1, which the complexing agent is selected from the group consisting of di- and tri-carboxylic acids, phosphoric acid and phosphate salts, thiocyanates, fluorides, fluosilicic acid and fluosilicate salts, EDTA and EDTA salts, and mixtures thereof.

3. A process according to claim 1 or claim 2, in which the treatment is carried out a temperature within the range 10 to 90°C, the lixiviant solution has a pH in the range 0.5 to 4.5, contains 0.0025 to 0.1M Fe , 0.005 to

3+ 0.4M thiourea, and 0.01 to 1.0M Fe complexant, and has a leach potential in the range 350 to 700 V vs Normal

Hydrogen Electrode.

4. A process according to claim 3 in which the leach potential is in the range 390 to 500 mV vs NHE.

5. A process according to any one of the preceding claims in which the complexant forms ferric complexes having a stability constant of log K greater than 1.

6. A process according to claim 5, in which the complexant comprises oxalic acid.

SUBSTITUTESHEET