AND COPPER FROM LEACH SOLUTIONS

FIELD

This disclosure relates generally to the recovery of metals by hydrometallurgical process and specifically to the recovery of metals by processes employing ion exchange adsorption and elution steps.

BACKGROUND

Gold is typically recovered from ores using a conventional cyanidation leach process. In the process, gold reacts with cyanide and oxygen by the following reaction:

4Au+0 ₂ +8CN ^" +2H ₂ 0→4Au(CN) ₂ ^40H ^" (1)

Gold is usually then recovered from solution using activated carbon as an adsorbent. Ion exchange resins may also be used to adsorb the gold cyanide complex, followed by elution with an acidic thiourea mixture. Thiosulfate leaching is a potential environmentally acceptable alternative to cyanidation and, in this process, the gold is leached as the gold thiosulfate complex. However, this complex is not readily adsorbed by activated carbon and so anion exchange resins may be preferred. Other metals, such as copper and mercury, also adsorb onto resins concurrently with gold.

The thiosulfate leach process has been demonstrated to be technically viable for a range of different ore types. For instance, Berezowsky et al, U.S. Pat. No. 4,070,182, disclose a process to leach gold from copper-bearing sulfidic material with ammonium thiosulfate. Kerley Jr., U.S. Pat. Nos. 4,269,622 and 4,369,061, disclose using an ammonium thiosulfate leach solution containing copper to leach gold and silver from ores containing manganese. Perez et al, U.S. Pat. No. 4,654,078, disclose leaching gold and silver with a copper-ammonium thiosulfate lixiviant to produce a pregnant leach solution, from which gold and silver are recovered by copper cementation. In these processes, ammonium thiosulfate is the preferred lixiviant, which results in the production of a tailings product which contains ammonia / ammonium ions. This is of concern from an environmental perspective. A leach process incorporating non-ammonium sources of thiosulfate, including sodium thiosulfate and calcium thiosulfate is therefore preferred.

Following leaching, gold may be loaded onto resins from either a slurry or a solution, and the gold is subsequently recovered from the resin by elution or desorption. Gold can be eluted from resins using eluants, such as thiocyanate, polythionate or nitrate based eluants. However, relatively concentrated solutions are required for the elution process. For example, in a nitrate elution process, 2M ammonium nitrate is preferred as disclosed in PCT Application No. WO 01/23626. This is a relatively high concentration of nitrate that creates demonstrable cost implications for the elution step and

environmental impacts in disposing of spent ammonium nitrate solutions.

Thiocyanate solutions are known to rapidly elute gold (either cyanide or thiosulfate complexes) from resins. However, the resin must be regenerated prior to addition back into the resin-in-pulp circuit; otherwise, the thiocyanate will accumulate in process water, eventually leading to environmental problems and reduced gold loading. In addition, the loss of thiocyanate may be economically unacceptable. Regeneration in the thiocyanate system is also complicated as thiocyanate is removed using ferric sulfate followed by regeneration of thiocyanate by addition of sodium hydroxide. The rapid change in pH in the elution and regeneration steps produces osmotic shock in the resin and this leads to resin loss through breakage. A number of chemical reagents are also required at a plant site that may be remote. It is therefore desirable, subject to plant operational efficiency, to reduce the inventory of different chemicals used in plant operation. An aim is to use fewer reagents in lesser quantity.

A polythionate eluant system utilizes a mixture of trithionate and tetrathionate. Since these species are strongly adsorbed on a resin, they can be used to effectively elute gold. The high affinity of polythionates for the resin necessitates a regeneration step. Regeneration is accomplished by treating the resin with sulfide, bisulfide, or polysulfide ions to convert the polythionates to thiosulfate. A problem with polythionate elution is the stability of the tetrathionate solution. In the presence of thiosulfate, tetrathionate undergoes a decomposition reaction to form trithionate and elemental sulfur, and in the presence of silver or copper, decomposes to precipitate copper or silver sulfides.

Trithionate decomposes to form sulfate, especially when present in high concentrations. Such decomposition reactions result in losses that add to the cost of the process.

In United States Patent Application 2011/0011216, it is shown that the addition of sulfite ions to various eluants enables the elution to be conducted with lower

concentrations of reagents. A mixed trithionate/sulfite system is shown to be especially effective at eluting gold from the resin.

There is a need to provide a process for recovery of metals by ion exchange which gives high elution efficiency but does not generate waste solutions or resins, which contain undesirable species that either cause issues with their disposal or recycle back to the process.

SUMMARY

The present disclosure provides a process for recovering metals from ion exchange resins.

In an embodiment, the process is performed exclusively with sulfur- and oxygen- based reagents which ultimately decompose to produce sulfate, which is the same decomposition product of thiosulfate-based leach systems. Therefore, the elution process itself does not produce a waste stream which either needs to be treated separately or will create additional problems when disposed of within the processing plant or tailings dam. If non-sulfur or oxygen-based reagents, such as halide, nitrate, and thiocyanate, are employed, a separate waste treatment and disposal system would be necessary. The reagents required for the process are thiosulfate, a source of sulfite ions (e.g., sulfite, bisulfite, and/or sulfur dioxide), a source of sulfide (e.g., a sulfide and/or polysulfide (which is a compound containing one or a mixture of polymeric ion(s), SX ^2" where X is 2- 6, such as disulfide, bisulfide, trisulfide, tetrasulfide, pentasulfide, and hexasulfide), and hydrogen peroxide (and/or another peroxide). The source of sulfite ions and sulfide ions can be compounded with any cation, with alkali and alkaline earth metals, ammonium, and hydrogen being common.

As will be evident from the discussion below, the process is normally based on generating a trithionate solution in-situ, which is then mixed with a source of sulfite ions (e.g., an alkali and/or alkaline earth metal and/or ammonium sulfite, bisulfite, and/or metabisulfite, and/or sulfur dioxide) to form the effective mixed trithionate/sulfite or trithionate/bisulfite, respectively, eluant. This aspect involves a resin regeneration step which utilizes a concentrated solution of sulfide ions, which produces a concentrated thiosulfate solution. Peroxide is then added to the spent regeneration solution to produce trithionate in-situ. A source of sulfite ions is then added to produce the mixed

trithionate/sulfite eluant, which is very effective at eluting gold from the resin. The addition of sulfite ion can significantly lower trithionate concentrations to be employed. This can reduce the rate of trithionate decomposition. In addition, the use of the spent regeneration solution to produce trithionate in-situ via reaction with peroxide would not generate enough trithionate to effect an efficient gold elution in the absence of sulfite ion, for which a solution concentration of ca. 1M trithionate is required to produce an effective elution. In an embodiment, the present disclosure also discloses a copper pre-elution step, which utilizes a thiosulfate solution containing peroxide. As will be demonstrated, the addition of peroxide to the thiosulfate mixture allows for the conditioning of the resin prior to the gold elution step. The majority of copper is removed by the

thiosulfate/peroxide mixture, which is recycled, with the copper eluant to the leach process to provide the copper and thiosulfate necessary to effect gold dissolution. The trithionate which is formed in-situ from the reaction of peroxide with thiosulfate, adsorbs onto the resin during copper pre-elution. This results in a higher gold elution efficiency when utilizing the trithionate/sulfite mixture. As will be apparent, the reagent feeds to the copper pre-elution and gold elution process are thiosulfate, a source of sulfite ions, a source of sulfide ions, and peroxide. The two streams exiting the process mainly contain thiosulfate and sulfate, which are recycled to the feed of the leaching process. Since the thiosulfate leaching process requires the addition of thiosulfate and produces sulfate as a degradation product, it should be clear that the recycle of the elution streams will not impact on the whole process. In contrast, if the elution were to be conducted with nitrate, chloride, or thiocyanate-based elution systems, these elution systems would produce waste streams which need to be treated or disposed of because a bleed from the elution circuit is needed to remove nitrate, chloride or thiocyanate generated products. In the described process, the bleed from the elution circuit (after electrowinning) can simply be returned to the leach circuit.

The process is particularly applicable to the elution of gold (and other precious metals). It may be applied as an adjunct to any leach or other hydrometallurgical process for the extraction of such metals, including resin-in-pulp processes or other ion exchange unit operations and/or lixiviants other than or in addition to thiosulfate. The process may be particularly advantageously applied to leached metal recovery following a thiosulfate leach process.

In this aspect, there may be provided a process for recovering precious metals comprising the steps of:

(a) leaching a precious metal-containing material with a thiosulfate solution;

(b) recovering leached precious metals by ion exchange with an ion exchange resin; and

(c) eluting the ion exchange resin with the eluant system, whereby trithionate is generated in-situ from the spent regeneration solution, followed by the addition of a source of sulfite. The process may also be applied to ion exchange for metal recovery following other hydrometallurgical processes.

These and other advantages will be apparent from the disclosure of the aspects, embodiments, and configurations contained herein.

The phrases "at least one", "one or more", and "and/or" are open-ended expressions that are both conjunctive and disjunctive in operation. For example, each of the expressions "at least one of A, B and C", "at least one of A, B, or C", "one or more of A, B, and C", "one or more of A, B, or C" and "A, B, and/or C" means A alone, B alone, C alone, A and B together, A and C together, B and C together, or A, B and C together. When each one of A, B, and C in the above expressions refers to an element, such as X, Y, and Z, or class of elements, such as Xi-X _n , Yi-Y _m , and Zi-Z ₀ , the phrase is intended to refer to a single element selected from X, Y, and Z, a combination of elements selected from the same class (e.g., Xi and X ₂ ) as well as a combination of elements selected from two or more classes (e.g., Yi and Z ₀ ).

The terms "a" or "an" entity refers to one or more of that entity. As such, the terms

"a" (or "an"), "one or more" and "at least one" can be used interchangeably herein. It is also to be noted that the terms "comprising", "including", and "having" can be used interchangeably.

"Adsorption" is the adhesion of atoms, ions, biomolecules, or molecules of gas, liquid, or dissolved solids to a surface. The exact nature of the bonding depends on the details of the species involved, but the adsorption process is generally classified as physisorption (characteristic of weak van der Waals forces)) or chemisorption

(characteristic of covalent bonding). It may also occur due to electrostatic attraction.

"Ion exchange resin" refers to a resin that is able, under selected operating conditions, to exchange ions between two electrolytes or between an electrolyte solution and a complex.

A "peroxide" refers to a compound containing an oxygen-oxygen single bond or the peroxide anion [O-O] ^2" . The 0-0 group is called the peroxide group or peroxo group.

"Sorb" means to take up a liquid or a gas either by sorption.

"Desorption" is the reverse of adsorption.

The preceding is a simplified summary of the disclosure to provide an

understanding of some aspects of the disclosure. This summary is neither an extensive nor exhaustive overview of the disclosure and its various aspects, embodiments, and configurations. It is intended neither to identify key or critical elements of the disclosure nor to delineate the scope of the disclosure but to present selected concepts of the disclosure in a simplified form as an introduction to the more detailed description presented below. As will be appreciated, other aspects, embodiments, and configurations of the disclosure are possible utilizing, alone or in combination, one or more of the features set forth above or described in detail below.

BRIEF DESCRIPTION OF THE DRAWINGS

The accompanying drawings are incorporated into and form a part of the specification to illustrate several examples of the present disclosure. These drawings, together with the description, explain the principles of the disclosure. The drawings simply illustrate preferred and alternative examples of how the disclosure can be made and used and are not to be construed as limiting the disclosure to only the illustrated and described examples. Further features and advantages will become apparent from the following, more detailed, description of the various aspects, embodiments, and

configurations of the disclosure, as illustrated by the drawings referenced below.

Figure 1 is a schematic diagram of a thiosulfate resin-in-pulp process;

Figure 2 is a simplified flowsheet showing the copper pre-elution and gold elution steps;

Figure 3 is a simplified flowsheet incorporating copper pre-elution, gold elution, and gold recovery by electrowinning, followed by recycled of the barren electrowinning solution;

Figure 4 is a simplified split elution flowsheet, incorporating copper pre-elution, two stages of gold elution, and gold recovery by electrowinning, followed by recycle of the barren electrowinning solution.

Figure 5 is an elution curve demonstrating elution of gold from an anion exchange resin by 0.2M trithionate in admixture with 0.2 M sodium sulfite. Two different resin samples were utilized, one with 20% polythionate loading, and the other with 40% polythionate loading.

Figure 6 is a copper pre-elution curve demonstrating pre-elution of copper from an anion exchange resin by 0.5 M sodium thiosulfate with and without hydrogen peroxide addition; and

Figure 7 is an elution curve demonstrating elution of gold from an anion exchange resin by 0.2M trithionate in admixture with 0.2 M sodium sulfite following copper pre- elution by 0.5 M sodium thiosulfate with and without hydrogen peroxide addition. DETAILED DESCRIPTION

In a preferred embodiment of the disclosure, gold and other precious and metals in a feed are recovered into solution at a metal recovery plant by a thiosulfate leaching process 100 followed by ion exchange to recover gold thiosulfate complex present in pregnant leach liquor from the leach step via a resin-in-pulp (RIP) or resin-in-leach (RIL) process, as shown schematically in Figure 1. Leaching 100 is normally performed by heap or tank leaching techniques. The tails 112 are sent to a tails tank 116, then to a tails thickener 120, and then to a tailing storage facility 124.

In one leach circuit configuration, the gold-containing solution in the leach step 100 includes thiosulfate as a leaching agent. The thiosulfate concentration in the solution commonly ranges from about 0.005 to about 5 M and more commonly from about 0.02 to about 2 M. As will be appreciated, in thiosulfate-based gold leaching systems copper is believed to catalytically oxidize gold. In many applications, the gold-containing solution in the leach step 100 is maintained at a leach copper solution concentration in the range of from about 0.1 to about 100 ppm.

In the ion exchange step (which is typically performed in the leach step 100), a strong base anion exchange resin 104 is used to adsorb the gold thiosulfate complex from the gold-containing solution to form a gold- loaded resin 108. There are a number of commercially available strong base ion exchange resins which have an affinity to gold and which are useful for the ion exchange process. The functional group of most strong base resins is quaternary ammonium, R4N+. Such a resin, in sulfate or chloride form, is a Purolite A500™ resin, as supplied by The Purolite Company of Bala Cynwyd,

Pennsylvania, which is employed in a preferred embodiment of the disclosure. Any other anion exchange resin may, however, be used. The typical capacity of the strong base resins is from about 1 to about 1.3 eq/L, and, for the purposes of demonstrating some aspects of the process, the discussion below is based on a resin having a capacity of about 1.2 eq/L. As will be appreciated, such resins also load copper from the pregnant leach liquor.

Following loading or adsorption of the thiosulfate complex onto the resin 104, the gold is recovered from the loaded resin 108 by elution; that is, desorption. A simplified elution flowsheet is shown in Figures 1 and 2. In this flowsheet, any washing or draining stages have been omitted for simplicity, as they do not materially change the nature of the elution system. The first stage is copper pre-elution (step 128 of Fig. 1), which is conducted using a copper eluant solution 133 containing thiosulfate and, optionally, trithionate to precondition the resin 140 (Fig. 1) for precious metal elution. The main purpose of this stage is to strip the copper from the resin before elution, and hence reduce the quantity of copper that reports to the gold product.

The thiosulfate in the copper eluant solution can be any source of thiosulfate, such as an alkali metal thiosulfate (e.g., sodium or potassium thiosulfate), an alkaline earth metal thiosulfate (e.g., calcium thiosulfate), or ammonium thiosulfate. The latter is not preferred, unless the leaching circuit also utilizes ammonium thiosulfate. Alternatively, the thiosulfate stream can be generated internally within the process, for example by treating the leach tailings solution 170 using a membrane concentration (filtration) process 172, such as reverse osmosis or nano filtration. Gypsum is precipitated from the thiosulfate-containing concentrate 174 in step 175. The concentrate is then directed to thiosulfate regeneration 176 or copper eluant preparation 132. A thiosulfate-containing stream 180 from the reclaim tank 182 can also be sent to thiosulfate regeneration 176. The thiosulfate concentration in the pre-elution copper eluant and product 15 typically ranges from about 30 to about 200 g/L, and the desorbed copper concentration in the copper-rich eluant ranges from about 100 to about 1,500 ppm.

When present, the concentration of trithionate in the copper eluant solution 133 typically ranges from about 0.01 to about 0.1 M. The trithionate may be generated by contacting an oxidant, commonly a peroxide, with the copper eluant solution 133, which converts thiosulfate into trithionate per equation (2) below. The copper pre-elution product 136 is used as a thiosulfate feed stream for leaching, and hence is recycled. In one process configuration, the barren electro winning solution 300 is contacted with the resin 140 to elute thiosulfate, which can then be recycled to the leach step 100.

Precious metal elution is then conducted from the resin 144 using a mixture of trithionate and sulfite ion as an eluant 148. Commonly, a concentration of trithionate in the precious metal eluant 148 is at least about 0.01 M, more commonly is at least about 0.05 M, more commonly ranges from about 0.1 to about 5 M, and even more commonly ranges from about 0.2 to about 2 M. The concentration of sulfite ion in the precious metal eluant 148 commonly is at least about 0.01 M, more commonly is at least about 0.1 M, and even more commonly ranges from about 0.1 to about 2 M. The concentration of dissolved gold in the gold-rich eluant 152 typically ranges from about 100 to about 500 ppm. The H of the precious metal eluant 148 is typically maintained within a range of from about pH 4.5 to about pH 14.

This elution mixture is generated by mixing peroxide with the spent regeneration solution 156 from resin regeneration 160 which contains sodium thiosulfate, as per reaction 2.

2Na ₂ S203+4H ₂ 02→ Na ₂ S ₃ 0 ₆ + Na ₂ S0 ₄ +4H ₂ 0 (2)

The sodium thiosulfate is itself generated in-situ through the reaction of a sulfide, such as an alkali and/or alkaline earth metal and/or ammonium sulfide, bisulfide, and/or polysulfide, hydrogen sulfide (H ₂ S), with the resin (step 160) containing trithionate, as shown in reaction 3, where R represents a resin functional site. Preferably, the sulfide ion addition for regeneration is between about 0.3 and about 0.65 moles of S ^2" ion per L of resin.

R ₂ S ₃ 0 ₆ +Na ₂ S→ R ₂ S ₂ 0 ₃ + Na ₂ S ₂ 0 ₃ (3)

The reaction between the thiosulfate in the spent regeneration solution 156 and the added peroxide in the trithionate reactor 164 is shown above in reaction 2. This reaction also generates heat, and therefore the preferred embodiment of the flowsheet utilizes either a cooled or chilled reactor to remove heat. The reaction temperature is preferably in the range of about 10°C to about 60°C. At higher reaction temperatures, some loss of trithionate becomes evident. The addition of peroxide should be between about 75 % and about 110 % of the stoichiometric amount to react with the thiosulfate contained in the spent regeneration solution 156 (reaction 2).

After elution, the resin 104 is almost completely loaded with trithionate, and as shown in reaction 3, the regeneration reaction converts commonly most, if not all, of this trithionate back to thiosulfate. Therefore, the resin 104 is recycled back to the adsorption or leach stage 100 with mainly thiosulfate loaded, and hence the resin is very active in adsorbing gold in the following cycle. On the other hand, trithionate is known to reduce the equilibrium gold loading in the adsorption circuit, and therefore recycle of a resin without the regeneration (and hence fully loaded with trithionate) would be problematic.

An advantage of in-situ generation of the sodium thiosulfate for trithionate synthesis is that sodium thiosulfate itself is an expensive reagent, especially since about 50% of the thiosulfate is oxidised to sulfate by peroxide. Utilizing other sources of thiosulfate for trithionate synthesis are less desirable. For instance, the use of ammonium thiosulfate results in the accumulation of ammonium sulfate, which may need to be disposed of separately due to the environmental impact of ammonia. The use of calcium thiosulfate can also be problematic, as the trithionate synthesis generates 1 mole of sulfate per mole of trithionate (reaction 2), which leads to the generation of gypsum in the trithionate reactor 164, and hence significant issues with equipment scaling.

The gold can be recovered from the trithionate product solution 152 by a number of technologies, including but not limited to, electrowinning 168, cementation by metals such as copper and zinc, and precipitation by sulfide-containing solutions. Each one of these technologies has been demonstrated to successfully recover the gold to very low concentrations (>99% removal of gold). In the preferred embodiment, standard gold electrowinning cells 168 are adopted, and the integrated elution/electro winning flowsheet is shown in Figure 3. The barren electrowinning solution 300 is recycled back to the trithionate synthesis step 164 and/or after copper preelution. By adding the barren electrowinning solution 300 to the trithionate synthesis, some additional thiosulfate that is stripped off the resin during gold elution is recycled. Alternatively, when adding the barren electrowinning solution 300 as a step after pre-elution, the sulfite present in this stream reacts with any adsorbed tetrathionate on the resin, which is an effective conditioning step to ensure optimum gold elution performance. The same benefit is achieved when recycling the barren electrowinning solution either before the copper preelution, or by mixing the barren electrowinning with the copper pre-eluant. For all these options, trithionate is recycled back to the elution system, and to maintain the water balance, there is an additional volume of copper pre-eluate, which mainly contains copper, sulfate and thiosulfate, since this product is taken before trithionate and gold break through, as discussed below.

A similar principle applies for the recovery of gold using cementation of precipitation, whereby the barren solution is recycled back to the elution system to recover trithionate.

One limitation with the in-situ generation of thiosulfate is the quantity of thiosulfate which can be produced. For a resin capacity of 1.2 eq/L, the maximum loading of trithionate, which is a 2- charge, is 0.6 mole / L of resin. Based on reaction 3, the maximum generation of sodium thiosulfate is 0.6 moles of thiosulfate per L of resin. After undergoing trithionate synthesis, this will produce 0.3 moles of trithionate per L of resin. In order for the resin to be close to saturated with trithionate after elution, a condition which is required to ensure optimal gold elution, a loading of 0.6 moles of trithionate per L of resin is required. Therefore prior to elution, the resin should contain at least about 0.3 moles of polythionates per L of resin (50% loaded with polythionates on a mole basis), since the trithionate synthesis only generates an extra 0.3 moles per L of resin. As is pointed out in United States Patent Application 2011/0011216, all the polythionates adsorbed on the resin prior to elution are converted to trithionate due to the presence of sulfite.

As will be demonstrated in the Examples below, the process can be adapted to operate for loaded resin samples with less than 50% polythionate loadings.

An effective means of utilizing a small volume of concentrated trithionate, for example 1.5 BV of 0.2 M trithionate, is in a split elution system. In such a system, the gold elution is conducted in two stages, with the 2nd stage elution product becoming the feed for the 1st stage gold elution for the next cycle. Figure 4 shows a split elution system, which also incorporates the recycle of barren electro winning solution to recover additional trithionate. Split elution cycles elution 2 feed from trithionate reactor 164 through the resin to form eluate 2. Eluate 2 is cycled to the resin, as elution 1 feed, to form eluate 1 (152). Eluate 2 and eluate 1 each comprise desorbed gold, with eluate 1 being richer in gold than eluate 2.

For testing copper pre-elution and gold elution efficiency, after loading gold from a thiosulfate leach solution, the Purolite A500™ resin was lightly packed into a column. Each eluant or eluant system was pumped through the glass column at a speed of 2 bed volumes per hour. Samples were then diluted 10-fold with 0.01M NaCN before being analysed by atomic absorption spectroscopy.

Example 1

When the loaded resin sample is >50%> loaded with polythionates (mole 30 basis), as discussed above, the in-situ generation of thiosulfate from regeneration, followed by trithionate synthesis generates enough trithionate to ensure that the resin is close to saturated after gold elution (and before regeneration). To demonstrate that the process can be self-sustaining, without additional thiosulfate being required to produce additional trithionate, 12 cycles of the flowsheet shown in Figure 4 were conducted whereby 20%> of the barren electrowinning solution was recycled to the trithionate synthesis, and 80% recycled after copper pre-elution. For these tests, the loaded resin was 60 mole%> loaded with polythionates, along with 1750 g/t gold and 4440 g/t copper. At steady state after 12 elution cycles, the trithionate synthesis stage generated 1.83 BV of 0.21 M trithionate, demonstrating that the process is effective at generating a small volume of concentrated trithionate solution. The steady state concentration of trithionate in gold elution feed 1 was 0.161 M, and that for the 1.6 BV of barren electrowinning recycled after copper pre-elution was 0.095 M. The electrowinning feed contained 279 mg/L gold, the elution 2 product only had 3 mg/L gold, and there were very low levels of gold left on the barren resin following elution.

Similar to above, cyclic experiments were also conducted utilizing the flowsheet shown in Figure 4, except that 100% of the barren electrowinning solution was recycled to the column after copper pre-elution. After 5 such cycles, the steady state concentration of trithionate in the 1.6 BV feed to the elution system was 0.19 M, demonstrating that the in- situ generation of sodium thiosulfate for trithionate synthesis was successful without recycle of barren electrowinning solution to the trithionate synthesis stage. After the gold elution 2 stage, the resin bed was washed with 0.4 BV of water prior to regeneration, generating 2 BV of solution for elution 1 feed. The steady state concentration of trithionate in the elution 1 feed was 0.14 M trithionate, and the electrowinning barren solution was 0.092 M trithionate. The electrowinning feed contained 269 mg/L gold, the elution 2 product only had 2.3 mg/L gold, and there were very low levels of gold left on the barren resin following elution. The gold assays demonstrate the effectiveness of the split elution system with recycle of barren electrowinning solution, as it produces 3 feed streams which sequentially pass through the column: 2 BV of 0.092 M trithionate;

followed by 2 BV of 0.14 M trithionate; and followed by 1.6 BV of 0.19 M trithionate. Example 2

When the loaded resin contains less than 50 mole% polythionate loading, additional trithionate may be required to ensure that the resin is close to saturated with trithionate prior to regeneration. This can be demonstrated by plotting an elution curve to determine the breakthrough before gold elution, as shown in Figure 5. It should be clear that, for the resin with the lower polythionate loading, gold is not readily eluted until at least 2 BV of 0.2 M trithionate had passed through the column. During the first 2 BV (prior to significant gold break through), the trithionate in the eluant is adsorbed onto the resin, replacing thiosulfate. Hence, this stream mainly contains thiosulfate and sulfate (since sulfate is only weakly adsorbed on the resin). Prior to break through of gold, the sulfate/thiosulfate solution is bled back to the leach circuit to control the concentration of both of these species in the elution circuit. For the resin containing the higher loading of polythionates, the breakthrough bed volume is reduced by ca. 0.5 BV of 0.2 M trithionate, i.e., 0.1 moles of trithionate per L of resin.

In Example 1, the trithionate synthesis was shown to generate 1.83 BV of 0.21 M trithionate (which is equivalent to 0.38 moles of trithionate per litre of resin), which would not be adequate to elute this resin sample. From the analysis of the resin (20 %

polythionate loading), it can be estimated that 0.48 moles of trithionate are required to fully saturate a litre of the resin. This analysis also confirms that additional trithionate is required.

One method of generating additional trithionate is to add extra thiosulfate to the trithionate synthesis stage. When running an ammonium thiosulfate-based leach system, the addition of ammonium thiosulfate to trithionate synthesis is ideal. However, if the generation of ammonium sulfate in the process is not desired, another approach is required. Sodium thiosulfate can be used, but it is an expensive reagent. Alternatively, sodium thiosulfate can be generated from the cheaper calcium thiosulfate feed material by precipitation of calcium. The precipitation of calcium can be conducted using a source of either sodium sulfate and/or sodium carbonate.

In this example, the thiosulfate was obtained from two sources. Firstly, the solution tails from leaching was concentrated using reverse osmosis to produce a concentrate containing 0.3 to 0.4 M thiosulfate. The thiosulfate concentration was increased by the addition of calcium thiosulfate, producing a solution containing 0.5 to 0.7 M thiosulfate. The calcium was firstly precipitated using sodium sulfate in a gypsum removal circuit. The product containing ca. 1 g/L calcium was utilized to supplement the thiosulfate in the trithionate synthesis, producing 2 BV of 0.5 M thiosulfate. After trithionate synthesis, the 2BV product contained 0.24 M trithionate, which was adequate to effect gold elution for a resin containing polythionate loadings as low as 25 mole%. It was however observed that some scaling due to calcium precipitate formation occurred, and therefore a second stage calcium precipitation was adopted after the gypsum removal stage, whereby a source of carbonate was added, for example soda ash, or trona. After the second stage, the calcium concentration was reduced to 12 mg/L, and no precipitation issues were observed in trithionate synthesis. On average over 8 cycles, the elution product contained 160 mg/L gold and the barren resin on contained 57 g/t gold, giving an average elution efficiency of 95%. This indicates that resins with less than 50%

polythionate loading can be effectively treated in this manner. Example 3

An alternative method for generating additional trithionate is to make use of some of the thiosulfate in the copper pre-elution feed. By adding peroxide to this stream, a larger volume (for instance 5BV) of lower concentration trithionate can be generated. This is advantageous, since the heat of reaction is taken up by the large solution volume, and, hence, an additional cooling system or cooling capacity is not necessary.

Figure 6 shows the profile for copper pre-elution for a 0.5 M sodium thiosulfate solution, compared to a solution for which sodium thiosulfate and peroxide were mixed to give a composition of 0.5 M sodium thiosulfate + 0.05 M sodium trithionate, as per reaction 2. The presence of trithionate in the thiosulfate pre-eluant results in a higher quantity of copper being stripped from the resin during 30 copper pre-elution. This is beneficial to the gold elution process, as increasing the stripping of copper during pre- elution results in less copper in the final gold product. Another significant advantage of adding peroxide to the copper pre-elution stream is an improvement in the gold elution performance in terms of required breakthrough volume. Figure 7 shows the gold elution profiles obtained for a mixture of 0.2 M trithionate + 0.2 M sulfite. The resin which had been pre-eluted in the presence of the trithionate undergoes elution earlier than the other sample resin, with the gold elution peak being after 1.3 bed volumes of solution, compared to 2.6 bed volumes, respectively. In addition, the peak gold concentration is higher for the resin which had been pre-eluted in the presence of trithionate. This is also advantageous, as more concentrated gold electrowinning product may be generated. For the data in Figures 6 and 7, the resin had the same loading of all species, including copper and gold.

Without wishing to be bound by theory, it appears that the role of peroxide addition to the copper pre-elution is to generate a low concentration of trithionate, which does not strip the gold during the copper pre-elution stage, but conditions the resin by adsorbing trithionate prior to the gold elution stage. This results in a significantly better performance during the elution step. Preferably, the addition of peroxide to the copper pre-elution should be between about 0.1 and 2.0 moles of hydrogen peroxide per L of resin to be eluted to produce a concentration of trithionate in pre-elution ranging from about 0.025 to about 0.5 moles / L resin. For 20 the data in Figure 6, 5 BV of solution containing 0.05 M trithionate was utilized, for which the peroxide addition was 1 mole per L of resin, and the quantity of trithionate was 0.25 moles per L of resin. Tests were also conducted with 5 BV of copper pre-eluant containing 0.025 M trithionate (i.e. 0.5 moles of peroxide per L of resin), and good results were also obtained. It should be apparent that, when the loaded resin contains a higher concentration of polythionates, less conditioning, i.e., 0.1 moles of peroxide per L of resin, may be preferred. However if the loaded resin contains a very low loading of polythionates, more conditioning may be required.

Therefore this is a robust process that can treat a wide range of resin feeds.

Various sources of thiosulfate can be adopted for pre-elution, and since the product is recycled to leach, the thiosulfate salt needs to be compatible with the leach system. When adopting an ammonium thiosulfate leach, the preferred reagent for elution would be ammonium thiosulfate. However, for non-ammonium based leach systems, alternative reagents such as calcium thiosulfate can be adopted. However, as discussed above, a calcium removal step may be required. For instance, the system described in Example 2 can also be adopted here, whereby the reverse osmosis concentrate is combined with calcium thiosulfate, followed by gypsum removal. Ideally, the peroxide is added prior to gypsum removal, since reaction 2 generates sulfate.

A number of variations and modifications of the disclosure can be used. It would be possible to provide for some features of the disclosure without providing others.

The present disclosure, in various aspects, embodiments, and configurations, includes components, methods, processes, systems and/or apparatus substantially as depicted and described herein, including various aspects, embodiments, configurations, subcombinations, and subsets thereof. Those of skill in the art will understand how to make and use the various aspects, aspects, embodiments, and configurations, after understanding the present disclosure. The present disclosure, in various aspects, embodiments, and configurations, includes providing devices and processes in the absence of items not depicted and/or described herein or in various aspects, embodiments, and configurations hereof, including in the absence of such items as may have been used in previous devices or processes, e.g., for improving performance, achieving ease and\or reducing cost of implementation.

The foregoing discussion of the disclosure has been presented for purposes of illustration and description. The foregoing is not intended to limit the disclosure to the form or forms disclosed herein. In the foregoing Detailed Description for example, various features of the disclosure are grouped together in one or more, aspects, embodiments, and configurations for the purpose of streamlining the disclosure. The features of the aspects, embodiments, and configurations of the disclosure may be combined in alternate aspects, embodiments, and configurations other than those discussed above. This method of disclosure is not to be interpreted as reflecting an intention that the claimed disclosure requires more features than are expressly recited in each claim. Rather, as the following claims reflect, inventive aspects lie in less than all features of a single foregoing disclosed aspects, embodiments, and configurations. Thus, the following claims are hereby incorporated into this Detailed Description, with each claim standing on its own as a separate preferred embodiment of the disclosure.

Moreover, though the description of the disclosure has included description of one or more aspects, embodiments, or configurations and certain variations and modifications, other variations, combinations, and modifications are within the scope of the disclosure, e.g., as may be within the skill and knowledge of those in the art, after understanding the present disclosure. It is intended to obtain rights which include alternative aspects, embodiments, and configurations to the extent permitted, including alternate,

interchangeable and/or equivalent structures, functions, ranges or steps to those claimed, whether or not such alternate, interchangeable and/or equivalent structures, functions, ranges or steps are disclosed herein, and without intending to publicly dedicate any patentable subject matter.