Accelerating Copper Leaching from Sulfide Ores in Acid-Nitrate-Chloride Media Using Agglomeration and Curing as Pretreatment

Abstract

This work investigates the effect of an agglomeration and curing pretreatment on leaching of a copper sulfide ore, mainly chalcopyrite, using mini-columns in acid-nitrate-chloride media. Ten pretreatment tests were conducted to evaluate different variables, namely the addition of nitrate as NaNO3 (11.7 and 23.3 kg/ton), chloride as NaCl (2.1 and 19.8 kg/ton), curing time (20 and 30 days) and repose temperature (25 and 45 °C). The optimum copper extraction of 58.6% was achieved with the addition of 23.3 kg of NaNO3/ton, 19.8 kg of NaCl/ton, and after 30 days of curing at 45 °C. Under these pretreatment conditions, three samples of ore were leached in mini-columns. The studied parameters were temperature (25 and 45 °C) and chloride concentration (20 and 40 g/L). The optimum copper extraction of 63.9% was obtained in the mini-column leaching test at 25 °C, with the use of 20 g/L of chloride. A higher temperature (45 °C) and a higher chloride concentration (40 g/L) negatively affected the extraction. The pretreatment stage had favorable effects, in terms of accelerating copper dissolution and improving leaching of copper sulfide ore in acid-nitrate-chloride media. Waste salts from caliche industry and waste brine from reverse osmosis can be used for providing the nitrate and chloride media.

1. Introduction

Industrial scale leaching of copper sulfide minerals like chalcopyrite (CuFeS₂) remains a metallurgical challenge. Chalcopyrite is mined worldwide [1], given the depths at which mining operations can now be carried out [2]. Copper sulfide is extracted by flotation, followed by the application of pyrometallurgical methods [3]. Leaching is an alternative metallurgical treatment for chalcopyrite, although chalcopyrite tends to form passive layers around particles during leaching, which results in a slow dissolution rate and low levels of copper extraction [4,5]. Many researchers have reported a higher percentage of copper extraction in acid-chloride media than acid-sulfate media to leach chalcopyrite [6,7,8,9,10,11,12]. A chloride-acid media promotes the formation of copper chloride-complexes [13] and iron chloride-complexes [14] that modify the redox potential (ORP), according Equations (1) and (2):

^Cu2++^Cl−+^e−→CuCl (0.558 V vs SHE)

^Fe3++^Cl−+^e−→^FeCl+ (0.761 V vs SHE)

Cu(I) ions are stabilized in the solution by adding a new redox pair Cu(I)/Cu(II). Porous layer of sulfur is generated around the particle when chloride ions are present. This porous layer facilitates the diffusion of reagents that improves the leaching kinetics [15,16]. A chloride medium can be provided by seawater or processing brines, such as waste solution from reverse osmosis [17,18,19,20,21,22].

Oxidizing agents like oxygen [23], chlorine [24], ferric [25], cupric [26], nitrate [27], and others are required to dissolve chalcopyrite. Some researchers have tested nitric acid [28,29], and nitrite [30] to leach chalcopyrite, with good results in terms of copper extraction. Nitrogen species tend to be very strong oxidizing agents, and there are reports in the literature of obtaining high copper extraction with the use of nitrogen ions [31].

Mining of copper, lithium, nitrates and other minerals represents an important part of the Chilean economy [32]. Nitrate comes from the caliche industry concentrated in northern Chile. Nitrate salts, waste salts and intermediate processing solutions can be used in chalcopyrite leaching. Sokić et al. [27] studied leaching of chalcopyrite concentrate in acid-nitrate media and determined that increasing temperature and acid and nitrate concentrations increases copper extraction to over 75%. Gok and Anderson [30] investigated the effect of addition of sodium nitrite in an acid medium during leaching of chalcopyrite and found that the extraction increased by 5% by using nitrite instead of nitrate, while other conditions remained the same. Shiers et al. [33] studied leaching chalcopyrite using different oxidants: hypochlorous acid, sodium chlorate and sodium nitrate with the addition of ferric ions (ferric sulfate, ferric nitrate and ferric chloride), and obtained a copper extraction of 92% in chloride-nitrate-ferric mixture, which proved favorable for chalcopyrite leaching at 50 °C. Tsogtkhankhai et al. [34] studied the kinetics of leaching copper with nitric acid, and with the estimation of the activation energy determined that temperature has a strong influence on the system. Castellón et al. [35] leached chalcopyrite concentrate in acid-nitrate media using seawater as a dissolvent and obtained a copper extraction of 97% in 24 h under the studied conditions ([H₂SO₄] = [NaNO₃] = 0.5 M) at 45 °C. The nitrogen species catalyzed (NSC) method uses sulfuric and nitric acids to leach sulfide minerals with the use of high pressure and temperature. The main advantage of this process is rapid extraction [31]. Many patents have been filed for leaching sulfide minerals in acid-nitrate media. Queneau and Prater [36] patented a process for leaching copper, iron, cobalt, silver and nickel sulfide in nitric acid. Arias [37] developed a process for leaching copper sulfide ore in heaps with an acid-nitrate media. Hard [38] patented a copper leaching process using sulfuric acid in the presence of nitrate ions. The optimal pH range (0.5 and 1.5), nitrate concentration (1–10%) and ratio between H⁺ and NO₃⁻ ions (ratio of 4 to 1) have been determined. Carnahan and Heinen [39] patented an in situ copper leaching process that uses a diluted acid medium and oxygen with nitrate ions that can come from nitric acid, an alkaline metal or ammonium nitrate. Lueders and Frankiewicz [40] patented a two-step leaching process in which sulfide ores are oxidized with nitrogen dioxide in an acid medium. Anderson et al. [41] patented a process to leach sulfide ores under conditions of temperature and pressure, using an acid medium with sodium nitrite. Hernández et al. [42] studied leaching chalcopyrite by agitation in acid-nitrate media at temperatures between 25 and 70 °C, and compared the use of seawater to that of freshwater. Copper extraction close to 98% were obtained with three days of leaching at 70 °C in a seawater medium, with a high concentration of nitrate and acid (1 M), and an 80% extraction was obtained with seven days of leaching at 45 °C.

Ore agglomeration and curing are carried out prior to leaching in heaps [43,44,45]. From the physical point of view, smaller particles of ore adhere to larger ones, resulting in relatively homogenous and stable material. This in turn results in a significant number of holes in piles, which is essential for adequate liquid and gas permeability of the agglomerated mineral bed [46,47]. The objective of curing is to attack the mineral chemically with concentrated sulfuric acid to dissolve most of the surface copper on particles, which creates a favorable condition for leaching. In this way, solutions with high levels of copper are obtained. Curing also solubilizes iron, contributing the ferric ions necessary to dissolve sulfides and inhibit the formation of colloidal silica to minimize silica passing to the leaching solutions [45]. Cerda et al. [48] studied the effect of a pretreatment stage at the laboratory level on dissolving a copper sulfide ore in a chloride-acid medium, and obtained a copper extraction of 93% leaching ore pretreated with 90 kg Cl⁻/ton of ore and 40 days of repose at 50 °C. A copper extraction of only 55% can be achieved without pretreatment, indicating the significant effect of the pretreatment stage. Bahamonde et al. [49] determined the positive effect of pretreating bornite and chalcopyrite in acid-chloride media to extract copper from these minerals. Taboada et al. [50] evaluated the effect of a pretreatment stage on leaching a mixed copper ore in mini-columns with the addition of ferric and ferrous ions in acid-chloride media and a repose period of 30 days. The process involved a 30-day cycle of pretreatment and 15 additional days of leaching (for a total of 45 days), resulting in 60 and 80% copper extraction, respectively. The addition of ferric ions in the pretreatment enhances copper extraction. Velásquez-Yévenes and Quezada-Reyes [21] studied leaching chalcopyrite in columns with a chloride medium, and a pretreatment with repose periods of 30, 50, 80 and 100 days. For the pretreatment, 5 kg H₂SO₄/ton and 60 kg/ton of seawater or waste brine were used, according to the test, with 0.5 g Cu²⁺/L. Intermittent irrigation began following the repose period. The authors found that the pretreatment improved extraction, which at room temperature and with 100 days of repose were 43 and 37%, respectively with brine and seawater. Velásquez Yévenes et al. [51] studied the effect of adding chloride in agglomeration and a curing process to improve the copper extraction from sulfide ore in leaching by columns. The copper dissolution increased with the curing stage with chloride and acid addition.

The objective of this study is to determine the effects of copper sulfide pretreatment (agglomeration and curing) on leaching by percolation at a moderate temperature (≤ 45 °C) in acid-nitrate-chloride media in mini-columns. The pretreatment variables studied were the addition of sodium nitrate (11.7 and 23.3 kg/ton), and sodium chloride (2.1 and 19.8 kg/ton), curing time duration (20 and 30 days) and repose temperature (25 and 45 °C). The leaching variables studied were the temperature of the system (25 and 45 °C) and the chloride concentration (20 and 40 g/L).

2. Materials and Methods 2.1. Ore Sample

Copper sulfide from a mine in the Antofagasta Region was used in this work, with particle sizes under 9.53 mm, and a P₈₀ of 7.9 mm. Atomic absorption spectrometry (AAS, Perkin-Elmer 2380, Perkin Elmer, Wellesley, MA, USA) showed that the chemical composition of the ore was 0.70% total Cu, 0.04% soluble Cu and 5.65% total Fe. Ore acid consumption was 33.5 kg/ton ore as determined by a leaching aliquot and titration with NaOH. The mineralogy was determined by quantitative X-ray diffraction (QXRD, Siemens/Bruker, Semi-QXRD, model D5000, Germany) and validated by optical microscopy using point-counting method (Table 1).

2.2. Reagents

Technical grade sulfuric acid (H₂SO₄, 95%), sodium chloride (NaCl, 95%), sodium nitrate (NaNO₃, 95%) and seawater were used as reactive agents. Seawater was obtained from San Jorge Bay, Antofagasta, Chile. It was pumped from the coast and then filtered (pore size 0.001 mm) through a polyethylene membrane. The chemical analyses of seawater shown in Table 2 were obtained by volumetry, gravimetry, inductively coupled plasma atomic emission spectroscopy (ICP-AES, ICPE-9000, Shimadzu, Tokyo, Japan) and AAS.

2.3. Experimental Procedure

2.3.1. Description of Pretreatment Stage

Table 3 shows the variables used to study the effect of pretreatment on copper extraction

Ten copper sulfide ore samples were prepared (500 g), all with the same granulometry. The ore was placed on a plastic sheet where the sodium nitrate and sodium chloride were added, both in solid form. The ore and reactive agents were homogenized by rolling, after which 50% of the sulfuric acid consumption of the ore (16.8 kg/ton) was added and 7% moisture was obtained by adding seawater. The ore was homogenized and the formation of stable agglomerates was observed. The agglomerated ore was stored in sealed plastic bags, the weight of which was registered using an analytical balance (Mettler Toledo C. AX-204, precision of ± 7 × 10⁻⁵ g). To test the effect of a repose temperature of 45 °C, pretreated samples were placed in an oven (Binder model ED115) that remained constant at that temperature throughout the repose period. To test the effect of a repose temperature of 25 °C, the samples were left in the laboratory with temperature control set at that temperature. The moisture level in the samples was checked every two days. Variation in weight indicated moisture loss by evaporation, the samples were sprayed with distilled water until the original weight was obtained. Following the repose period, the pretreated ore was transferred to a beaker, washed with distilled water at a solid/liquid ratio of 1:3 at room temperature, with mechanical agitation (400 rpm) for two hours. The suspension was then filtered using a vacuum pump. The pH and redox potential (ORP) of the resulting solution were then measured (Hanna portable pH/ORP meter, model HI991003, accuracy ±0.02 pH and ±2 mV). The solid residue was dried in an oven at 60 °C until reaching a constant weight. The copper content in the solution and in the solid residue was obtained by AAS. The copper extraction rate was calculated using the copper grades of the head and residual ore, which was corroborated with the results obtained by solutions. A standard deviation of ±2% was obtained by calculating the copper extraction rates from solid and solution for all the tests. These tests were carried out in duplicate.

2.3.2. Description of Leaching Tests

The pretreatment conditions that resulted in the highest copper extraction rate were repeated in three experiments using 3 kg of ore with the same size distribution as in the previous tests. The pretreated ore was placed in acrylic mini-columns 40 cm high and 9.5 cm in diameter, similar dimensions used by Taboada et al. [50] and Velasquez-Yévenez et al. [51], and left in repose for a curing time determined by the previous tests. Following the curing time, the ore was leached using a solution of 6.3 g/L NaNO₃ and seawater, with a pH of 1 (using H₂SO₄), and the experimental variables as shown in Table 4. The mini columns at 45 °C were wrapped in plastic hoses through which water circulated at a desired temperature, controlled by a thermostatic bath (Julabo bath F25-ME Refrigerated/Heating Circulator) to keep the temperature constant (Figure 1).

The mini-columns were irrigated with a peristaltic pump in an open cycle at a rate of 8 L/h·m² (Master Flex, Model N° 7557-14/1-100 RPM, Cole-Parmer International, Vernon Hills, IL, USA). At certain intervals, the output solution was removed and mass, pH, ORP and copper content were determined. Following the test (leaching for 8 days), the ore was washed in the mini-columns with an acid solution (pH 1) and tap water for 24 h and then left in repose for another 24 h to completely drain the solution. The leached ore was then removed from the mini-columns and dried in an oven at 60 °C until reaching a constant weight. The solid residue was analyzed for copper content (AAS). A standard deviation of ±1.9% was obtained by calculating copper extraction using solid and solution for all the tests. The tests were carried out in duplicate. In addition, the solid residue was analyzed by optical microscope for the determination of mineralogical species.

3. Results and Discussion 3.1. Effect of Pretreatment on Copper Extraction

Table 5 shows the pretreatment tests, with all the variables used and the average of copper extraction.

The highest copper extraction was obtained in test 8, which involved the highest values of the studied variables. The final pH levels in all the tests were in the range of 2.2 to 3.3, which indicates complete consumption of the aggregate acid in the pretreatment. Redox potential values ranged between 637 and 792 mV (vs SHE), which were higher than the values reported by Cerda et al. [48]. This is attributed to the presence of nitrate, which has a high redox potential. Temperature and the addition of chloride have significant effects on dissolving copper sulfides. The residue obtained from test 8 was analyzed by optical microscope. Figure 2 shows the percentages of the copper species extracted in test 8 by leaching with pretreatment, which was determined by mass balance.

Table 6 shows the copper extraction per mineralogical species and the percentages of the minerals present at the beginning and end of the pretreatment stage.

According to the results shown in Table 6, part of bornite (75%), covellite (95%) and chalcopyrite (53.3%) were only leached with the pretreatment stage. Copper oxide minerals were completely leached.

3.1.1. Effect of Adding Chloride

The addition of chloride increased copper extraction in all the tests, which concurs with what was reported by Senanayake [52] and Watling [6], where chalcopyrite and bornite oxidized more readily in saline water media. The highest extraction of 58.6% was obtained in the test with the addition of 23.3 kg of sodium nitrate and 19.8 kg of sodium chloride per ton at 45 °C, with 30 days of repose. According to Velásquez-Yévenes and Quezada-Reyes [21], the pretreatment with acid and chloride resulted in a more homogenous distribution of reactive agents in the ore, resulting in the dissolution reaction beginning earlier and the formation of soluble species, with better liquid/solid interaction and a higher degree of porosity in the bed, so that moisture is retained in the pores. Velásquez-Yévenes [51] determined that adding sodium chloride in a curing stage improves copper extraction from copper sulfate, based on a test comparing extraction with and without the addition of chloride. They demonstrated that increasing the quantity of chloride from 20 to 70 kg/ton does not significantly increase the copper extraction. This finding concurs with the results of other authors [15,16].

3.1.2. Effect of Adding Nitrate

The addition of sodium nitrate had a positive effect in all the tests, particularly in the test with 30 days of repose at 45 °C and the addition of a high level of chloride. The additional nitrate resulted in more oxidizing ions being available to leach copper sulfides. This concurs with what was reported by Sokić et al. [27], who confirmed that a system with sulfuric acid without the addition of oxidants does not react with chalcopyrite. A mixture with high concentrations of sodium chloride and sodium nitrate in an acid medium was more effective, which concurs with Shiers et al. [33], who reported a 92% extraction for the NO₃⁻/FeCl₃ (50 °C, 168 h) oxidant. The authors suggested that nitrate is the most cost-effective oxidant.

3.1.3. Effect of Curing Time

Increasing the curing time from 20 to 30 days increased copper extraction in all the tests by providing more time for the dissolution reaction to occur. This is because the mineral is exposed to a high ionic charge provided by sodium nitrate, sodium chloride and sulfuric acid, which, along with a low amount of water, allow dissolution reactions to occur rapidly. This concurs with Cerda et al. [48], Velásquez-Yévenes and Quezada-Reyes [21], and Velásquez-Yévenes et al. [51] who found that a higher extraction was obtained with a longer repose period.

3.1.4. Effect of Repose Temperature

Dissolution reactions are more rapid with higher temperatures because less energy is necessary to activate dissolution and to break molecular bonds and thus dissolve mineralogical species in contact with the leaching agents [48].

3.1.5. Chemical Reactions in Pretreatment

Table 7 shows the main proposed reactions that can occur during agglomeration and curing.

Table 8 shows the standard Gibbs energy of proposed reactions 3 to 6 at temperatures of 25 and 45 °C, which were calculated with HSC software [53].

As can be observed, all the reactions are thermodynamically feasible at atmospheric pressure and in a temperature range of 25 to 45 °C.

3.2. Effect on Mini-Column Leaching

Test C1 obtained a copper extraction of 63.9%, while test C2 obtained one of 55.0%, and test C3 one of 55.4%. Figure 3 shows the copper extraction curves versus the repose period and subsequent leaching for columns 1 to 3. Table 4 shows the leaching conditions.

It can be seen from Figure 3 that the highest copper extraction of 63.9% was obtained with C1 at 38 d (30 d of pretreatment and 8 d of leaching) at 25 °C. The pretreatment resulted in high dissolution rates in all the experiments. Velásquez-Yévenes and Quezada-Reyes [21] conducted chalcopyrite leaching tests in columns at room temperature, with 30 days of repose and 55–60 days of irrigation with sulfuric acid, cupric ions and seawater or brine. The highest copper extraction obtained was less than 25%. Comparing this to the results with C1, it is evident that nitrate is the most favorable oxidizing agent for extracting copper. Figure 3 shows that the C2 and C3 curves have similar kinetics. The two columns show differences in temperature and chloride concentrations. According to the results, temperature can be replaced by chloride concentration. This concurs with what was found in the pretreatment stage, where the two variables are the most significant in the dissolution system.

C1 reached a copper extraction of 63.9% with 8 days of leaching. Comparing this result to the extraction obtained in the pretreatment stage alone (58.6%), it can be observed that the leaching stage is only improved by 9%. C2 and C3 obtained copper extraction close to that obtained in the pretreatment, from which it can be inferred that the leaching only washed the solubilized species during the pretreatment. No contribution from the leaching process was observed.

Based on our results, pretreatment is recommended, followed by washing with an acid solution (pH 1) in the leaching process, without other additives like nitrate or chloride. Other options include using higher concentrations of nitrate (greater oxidation potential), other oxidants, or higher concentrations of acid, among others. The process could also be carried out in two stages, first an acid wash of the pretreated ore, followed by oxidative leaching.

The pH levels of the output solutions of the three columns were ≥ 1.5, indicating acid consumption. The patterns of redox potential values (Figure 4) were similar for C1 and C3, and higher than those obtained for C2. The redox potential values of C2 indicate that there are fewer oxidants in the system at 45 °C than at 25 °C.

3.2.1. Effect of Temperature on the Leaching Stage

The copper extraction was lower at 45 °C than at 25 °C, which could be because the mini-columns are open to the air, so that NOx gas formed by the reaction between H₂SO₄ and NaNO₃ escape from the leaching system, which results at 45 °C in fewer nitrate ions being available for the copper dissolution reaction, as shown in Equation (7):

2_NaNO3+_{H2 SO4}→2_HNO3(g)+_{Na2 SO4}

With ΔG_{25 °C} = 1.3 kcal/mol and ΔG_{45 °C} = −0.1 kcal/mol.

Oxidant loss could not occur at 25 °C, therefore the availability of oxidants would be higher than at 45 °C which would affect the copper dissolution.

The redox potential values in the output solutions of C1 and C3 were higher than that of C2 (see Figure 4), which could be due to a smaller quantity of oxidant in the C2 medium than in those of C1 or C3. It could also be due to ferric sulfate being generated in C2 by the pretreatment, which would have reacted with chalcopyrite in the leaching stage, forming ferrous sulfate and resulting in a lower redox potential.

_CuFeS2+4^Fe3+→^Cu2++5^Fe2++2S

_CuFeS2+4^Fe3++^Cl−→^CuCl++5^Fe2++2S

With ΔG_{25 °C} = −31.9 kcal/mol equation 8 and ΔG_{25 °C} = −32.4 kcal/mol Equation (9).

The results obtained indicate that under the conditions used in this study, copper dissolution is not favored by increasing the temperature from 25 to 45 °C.

3.2.2. Effect of Chloride Concentration on Leaching Stage

Copper extraction rates was higher in the column with 20 g/L of chloride (C1) than in the column with 40 g/L (C3), which could be due to greater saturation of the leaching medium (more ionic strength) in a higher chloride concentration, which is unfavorable for copper dissolution under the studied conditions. Several authors have determined that the presence of chloride ions in leaching systems improves copper extraction [6,8,9]. However, the increase in chloride concentration is not necessarily proportional to the copper extraction rate [15,51].

3.2.3. Analyses of Solid Residues

Table 9 shows the residual mineral species in C1 obtained by leaching test (observed with an optical microscope) in comparison to the original mineralogical state (head ore).

Table 9 shows the presence of copper sulfide in the residue, with reduced levels of chalcopyrite, bornite and covellite, while copper oxide was totally leached. It is possible to dissolve 62% of the chalcopyrite in the ore using a pretreatment/leaching process in acid-nitrate-chloride media.

4. Conclusions

We studied the effects of a pretreatment stage, adding nitrate and chloride and varying repose time and temperature on chalcopyrite dissolution in acid-nitrate-chloride media. The main findings are:

1. The copper sulfide pretreatment provided satisfactory results, with 58.6% Cu extraction with the addition of 23.3 kg sodium nitrate and 19.8 kg sodium chloride per ton, and 30 days of curing time at 45 °C.

2. The acid-nitrate-chloride media at high concentrations was effective in the pretreatment, providing oxidizing ions in the repose period.

3. A copper extraction of 63% was obtained by leaching pretreated ore in mini-columns using a leaching solution of 6.3 g/L of sodium nitrate and 20 g/L of chloride at pH 1 and a temperature of 25 °C. Raising the temperature and increasing the chloride concentration did not improve copper extraction rates under the studied conditions.

4. Chalcopyrite, bornite and covellite were only partially leached in the mini-columns, while copper oxides were completely leached.

5. A favorable copper dissolution from sulfide ore was obtained in acid-nitrate-chloride media with the inclusion of a pretreatment stage in the leaching system. Waste salts from the caliche industry can be used for the nitrate medium, while waste brine from reverse osmosis can provide the chloride medium.

6. An emphasis on the pretreatment stage is proposed given that this results in copper extraction rates in the range of 60%, so in the next phase only an acid wash will be required.

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Mineral	Chemical Formula	Amount (wt. %)	Cu (wt. %)
Chalcopyrite	CuFeS2	1.69	0.59
Bornite	Cu5FeS4	0.10	0.06
Covellite	CuS	0.02	0.01
Atacamite	CuCl2⋅3Cu(OH)2	0.07	0.04
Chrysocolla	Cu1.75Al0.25H1.75(Si2O5)(OH)4⋅0.25(H2O)	0.01	<0.01
Pyrite	FeS2	3.81
Magnetite	Fe3O4	0.40	-
Hematite	Fe2O3	0.08	-
Limonite	FeOOH	0.07
Quartz	SiO2	38.39
Gangues	-	55.36	-
Total Cu			0.70

Method of Analysis	ICP-AES				AAS		Volumetric Analysis	Gravimetric Analysis
Ionic Species	Na+	Mg2+	Ca2+	K+	Cu2+	NO3−	Cl−	SO42−
Amount (g/L)	10.73	1.29	0.40	0.39	7.2 × 10−5	3 × 10−3	20.06	2.81

Sodium Nitrate Addition (kg/ton)	Sodium Chloride Addition (kg/ton)	Curing Time (Days)	Repose Temperature (°C)
11.7	2.1 *	20	25
23.3	19.8	30	45

* chloride contributed by seawater (humidity) without any additives.

Conditions	C1	C2	C3
Irrigation temperature (°C)	25	45	25
Chloride (g/L)	20	20	40

Test	Sodium Nitrate Addition (kg/ton)	Sodium Chloride Addition (kg/ton)	Curing Time (Days)	Temperature (°C)	Cu Extraction (wt. %)
1	11.7	2.1	20	45	19.8
2	23.3	2.1	20	45	22.9
3	11.7	19.8	20	45	34.9
4	23.3	19.8	20	45	36.6
5	11.7	2.1	30	45	28.7
6	23.3	2.1	30	45	30.7
7	11.7	19.8	30	45	44.9
8	23.3	19.8	30	45	58.6
9	11.7	2.1	30	25	11.8
10	23.3	2.1	30	25	22.8

Mineral	Extraction (%)	Feed Ore (%)	Pretreatment Ore (%)
Chalcopyrite	53.3	1.69	0.79
Bornite	75.0	0.10	0.03
Covellite	95.0	0.02	<0.01
Atacamite	100.0	0.07	0
Chrysocolla	100.0	0.01	0

Mineral	Proposed Chemical Reaction	N°
CuFeS2	2CuFeS2+10H2 SO4+10NaNO3+4NaCl→2CuCl2+Fe2 (SO4)3+10NO2+4S+10H2O+7Na2 SO4	(3)
CuS	3CuS+4H2 SO4+2NaNO3+6NaCl→3CuCl2+2NO+3S+4H2O+4Na2 SO4	(4)
Cu5FeS4	Cu5 FeS4+12H2 SO4+12NaNO3+10NaCl→5CuCl2+FeSO4+12NO2+4S+12H2O+11Na2 SO4	(5)
FeS2	3FeS2+4H2 SO4+2NaNO3+6NaCl→3FeCl2+2NO+6S+4H2O+4Na2 SO4	(6)

Equation N°	∆G°25 °C (kcal/mol)	∆G°45 °C (kcal/mol)
3	−209.5	−216.8
4	−97.8	−98.8
5	−234.4	−243.0
6	−115.5	−117.4

Mineral	Chemical Formula	Ore		C1 Residue
		Amount (wt. %)	Cu (wt. %)	Amount (wt. %)	Cu (wt. %)
Chalcopyrite	CuFeS2	1.69	0.59	0.64	0.22
Bornite	Cu5FeS4	0.10	0.06	<0.02	<0.01
Covellite	CuS	0.02	0.01	<0.02	<0.01
Atacamite	CuCl2⋅3Cu(OH)2	0.07	0.04	0.00	0.00
Chrysocolla	Cu1.75Al0.25H1.75(Si2O5)(OH)4⋅0.25(H2O)	0.01	<0.01	0.00	0.00
Pyrite	FeS2	3.81	-	3.29	-
Magnetite	Fe3O4	0.40	-	0.60	-
Hematite	Fe2O3	0.08	-	0.04	-
Limonite	FeOOH	0.07	-	0.05	-
Quartz	SiO2	38.39	-	33.12	-
Gangues	-	55.36	-	62.23	-
Total Cu			0.70		0.24

Author Contributions

Conceptualization, P.C.H. and Y.P.J.; Formal analysis, O.O.H. and C.M.T.; Investigation, J.D.; Supervision, P.C.H. and Y.P.J.; Validation, O.O.H. and C.M.T.; Writing—original draft, P.C.H.

Funding

The authors are grateful for the financial support provided by CONICYT through Fondecyt Iniciación Project N° 11170179 and PAI/Concurso Nacional Inserción en la Academia, Convocatoria 2015 folio N° 79150003.

Acknowledgments

Special thanks to Departamento de Ingeniería en Minas and Laboratorio de Investigación de procesos of Departamento de Ingeniería Química y Procesos de Minerales, of Universidad de Antofagasta for the assistance in ore preparation and technical support with equipment and materials.

Conflicts of Interest

The authors declare no conflict of interest.

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