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Journal of the Southern African Institute of Mining and Metallurgy

Print version ISSN 0038-223X

J. S. Afr. Inst. Min. Metall. vol.111 n.6 Johannesburg Jun. 2011

 

JOURNAL PAPERS

 

Potential metallurgical treatment of copper concentrates with high arsenic contents

 

 

I. Mihajlović; N. Štrbac*, D. Nikolic; Z. Živković

Technical Faculty in Bor, University of Belgrade, Vojske Jugoslavije, Serbia

 

 


SYNOPSIS

This paper investigates a potential method for arsenic removal from copper concentrates using hypochlorite leaching. The problems concerning pyrometallurgical processing of copper concentrates with high arsenic contents are discussed. A possible solution to the problem by leaching of natural enargite crystals with sodium hypochlorite under alkaline oxidizing conditions, with enargite converted into crystalline CuO and the soluble arsenic forming AsO43-, was experimentally investigated and results are presented. Kinetic parameters were calculated for enargite leaching, using a model-free approach. Advanced isoconversional methods were used to investigate the dependence of activation energy (Ea) on reaction rate (α).

Keywords: Enargite, copper concentrate, isoconversional method, kinetics, activation energy.


 

 

Introduction

Arsenic is present in the Earth's crust in concentrations of 4.8 ± 0.5 µg/g in the natural form1. The sources of arsenic in industrial areas are natural and anthropogenic2and it can be found in soil, water, and atmospheric dust3 . Among the biggest anthropogenic sources of arsenic are copper smelter plants, which are considered to be major environmental polluters the world over: particularly in Chile, the USA, Sweden, Spain, Russia, Australia, and Serbia4-9.

The technology of copper production at the Bor smelter plant is half a century old. This technology uses the classical process of oxidation roasting, followed by melting in the reverberatory furnace and subsequent converting, with the use of SO2 process gas for sulfuric acid production (Figure 1). Most of the world's copper smelter plants have replaced this kind of technology with modern processes such are the Outokumpu flash furnace, Mitsubishi smelting process, Noranda reactor, Peirce-Smith converting, El Teniente converter and others10.

Unfortunately, the economic situation in Serbia during the last twenty-five years precluded large capital investment in new technology for copper extraction. Thus the Bor copper smelter plant remained among the last ones that use the reverberatory furnace. Closing this smelter plant would lead to major social problems since almost the half of the citizens of Bor are employed by this company. Another reason which prevents closing of this facility is the large reserves of copper ore in this region.

Arsenic is one of the most common toxic impurities found in copper concentrates. The main As-containing mineral species in the copper concentrates obtained from the Bor ore deposits, are enargite (Cu3AsS4) and luzonite (Cu3AsS4), while realgar (As4S4) and arsenopyrite (FeAsS) are present in lesser amounts. Unfortunately, the prevalence of enargite among the copper-bearing minerals and the resulting relatively high arsenic content in the concentrates substantially reduces their economic value, owing to the hazardous emissions generated from pyrometallurgical processing8-11.

Because of this fact, and the difficulties in controlling arsenic in such industrial processes, the amount of arsenic released during the processing of arsenic bearing concentrate by roasting prior to smeltingn, is very high. Arsenic, as well as its oxides, is highly volatile and leaves the reactor in the off-gas constituents. Thus, in unfavorable metal market conditions, direct roasting of such concentrates is not an economical option because the gas cleaning facilities required are too expensive.

Arsenic is a toxic element and as such it is hazardous to human health. It also shows carcinogenic properties2. It has been established that arsenic attacks many human organs and weakens the immune system12. The increased concentration of arsenic in the air in urban areas is always of anthropogenic origin, usually the emissions, from industrial plants.

Since arsenic is one of the most common toxic impurities found in copper concentrates, the main purpose of the investigations presented in this paper was to determine the behavior of arsenic-bearing mineral species present in copper concentrate during hypochlorite leaching, with the final goal of investigating possibilities of arsenic removal from such concentrates. The reason for such an approach to the arsenic problem in copper extraction metallurgy is the fact that it requires less investment then replacing the complete technology in the Bor copper smelter plant. The research presented in this paper consists of a kinetic study of the process during hydrometallurgical treatment of natural enargite, which is the main arsenic bearing constituent of the copper concentrates with high arsenic content from the Bor ore deposit. A theoretical discussion of the model-free approach for the calculations of kinetic parameters is also presented.

In order to minimize the problems associated with the processing of these very hazardous materials, the arsenic content in copper concentrates must be reduced to low levels (usually less then 0.5% As). Such levels are difficult to obtain by differential flotation of the ore from some sulfide deposits13. According to the World Health Organization14(WHO) values of arsenic in the air above 1.5x10-3 µg/m3 present a high risk to human health. Typical cconcentrations of arsenic in European regions are in the range from 0.2 to 1.5 ng/m3 in rural areas, 0.5 to 3 ng/m3 in urban areas, and up to 50 ng/m3 in industrial zones7 .

The average concentration of arsenic in the air in the urban area of Bor city during 2007 was 24.1 ng/m3. Most of the recent investigations report only the results of measured concentrations of arsenic in air, soil, and water in industrial areas near the Bor copper smelter8,9. The real problem that needs to be solved is how to minimize the concentration of arsenic emitted from the smelter.

In an attempt to solve this problem, we have explored the possibility of hydrometallurgical treatment of the copper concentrates with the purpose of dissolving the arsenic prior to the pyrometallurgical processing, which is depicted in Figure 1.

Two techniques for arsenic removal from enargite are found in the literature15:

Alkaline leaching of energite concentrates using sodium sulfide solutions after mechanical activation by fine grinding16

Leaching of natural enargite crystals with sodium hypochlorite under alkaline oxidizing conditions, with enargite converted into crystalline CuO and the arsenic solubilizing to form (AsO43-)11,13.

We decided to evaluate the possibility of applying the second method, because it is attractive in terms of its potential on a commercial scale, and taking into account the results of previous investigations of this matter.

 

Experimental methods

Large natural crystals of enargite from the Bor copper mine 'H' orebody, were chosen for this study. This material was prepared for the experiments by grinding to a particle size -100 µm.

Mineralogical investigations of the enargite samples and leach products were conducted using X-ray diffraction (XRD) with an atomic powder diffractometer PHILIPS APD SYSTEM PW 1710 (Royal Philips Electronics, Netherlands), under the following conditions: 2θ range 5-90º, velocity 0.05º/s, Cu anti-cathode with 40 A current, and voltage of 35 V.

Inductively coupled plasma (ICP) analyses with an atomic emission spectrometer (AES) (model Plasma Vision 3410+ARL) were used to ascertain the purity of the enargite samples as well as the composition of the products of reaction, with an expected accuracy of ± 0.05%.

The samples were also charactized using scanning electron microscopy (SEM) with EDEX-9100 analysis and a PAX software package, with a resolution of 1 nm (30 kV), excitation voltage of 0.2-30 kV, maximum magnification of 500 000 times, and with a secondary electron detector.

Energy dispersive X-ray fluorescence (EDX) analysis was done on Canberra equipment with the radioisotopes: Cd-109 (22.1 keV) and Am-241 (59.5 keV).

Leaching of enargite samples was conducted in a 1 dm3 three-neck tank with condenser, mechanical stirrer, and ultra-thermometer. The leaching kinetic experiments were performed at nearly constant hypochlorite concentration (0.3M NaClO) by using a large solution volume (800 cm3) and a small amount of solid (0.5 g). The leaching solution was mechanically stirred at 50 r/min and contained 5 g/dm3 NaOH, at pH12 in the starting solution. Leaching temperatures were in the range 25-60ºC, and time intervals up to 120 minutes.

The progress of the reaction was determined by analysing arsenic in the solid residuals using inductively coupled plasma emission spectroscopy. According to the reaction stoichiometry, the fraction of the enargite reacted was determined as a function of arsenic extracted (XAs).

 

Results and discussion

Table I shows the composition of the natural enargite samples used in the experiments.

X-Ray diffractometric analysis (Figure 2) shows that the sample contains a significant concentration of enargite.

 

 

Figure 3 shows the results of SEM/EDX analysis of an enargite sample.

Figure 3 (a) shows the SEM image of the enargite sample. For the spot indicated as Spectrum 1, EDX analysis was performed, and the results are presented in Figure 3(b) and 3(c). It is obvious that besides enargite, quartz was detected in the starting sample, which confirmed the results of the X-ray analysis (Figure 2). The EDX analysis also indicated a small amount of iron in the sample, which was not detected using X-ray analysis because of its low concentration (below 3%). Nevertheless, iron was detected in the sample by chemical analysis (presented in Table I).

Leaching experiments

Leach tests were conducted in the 1-litre thermostated reactor containing NaClO solution mechanically stirred at 500 r/min. Leaching temperatures were in the range 25-60ºC, and time intervals up to 120 minutes. The leaching kinetic experiments were performed at nearly constant hypochlorite concentration (0.3M NaClO) by using a large solution volume (800 cm3) and a small amount of solid (0.5 g). The leaching solution contained 5 g/dm3 NaOH, with the starting solution at pH 12.

A sample leached in hot NaClO solution (60ºC) for 120 minutes was analysed by SEM-EDX (Figure 4).

EDX investigations of the spot indicated as Spectrum 2 in Figure 4 (a) indicated that there is no arsenic present in the sample. The chemical composition of the copper-bearing species corresponds to the mineral tenorite, as indicated in Figure 4 (b). It can be seen that surface of the sample, formed during leaching under constant agitation, is composed of a large number of fine grains (Figure 4(a)). The reason for such a surface structure is in the high stirring rate during leaching.

The leach residues were also analysed using XRD to determine the mineralogical changes undergone during hypochlorite leaching. The data obtained (Figure 5) were found to agree with previous SEM/EDX analysis, as well as with results reported in the literature for tenorite (CuO) detected as the oxidation product of enargite. All of these investigations13,15,17, concerning leaching of enargite in sodium hypochlorite solution, reported tenorite as the main oxidation product. Thus, under these experimental conditions the leaching reaction can be written as11:

 

 

Results of the kinetic analysis

The influence of temperature on arsenic removal during enargite leaching is shown in Figure 6, where arsenic removal efficiency is plotted versus time for varying solution temperatures. These results were obtained under the experimental conditions described earlier.

 

 

Since enargite is usually present in orebodies that contain gold as a trace constituent, sodium hypochlorite leaching of the concentrates obtained from such locations is being extensively investigated. Curreli et al.15, reported the results of hypochlorite leaching of the concentrate from the Serrenti-Furtei gold-bearing deposit, located in southern Sardinia. After leaching the concentrate in 0.3M hypochlorite solution, at 45ºC for 120 minutes, they achieved 96% arsenic removal without significant Au and Cu losses.

During our investigations, the results of which are presented in Figure 6, we achieved almost 99% arsenic removal with the same sodium hypochlorite concentration and same time interval. The higher arsenic removal, that we obtained results from the higher leaching temperature (60ºC) in our experiments. Similar high values of arsenic removal were also reported by Vinals et al.13, who also investigated the effects of sodium hypochlorite leaching of large natural enargite samples from Huencavelica (Peru). They used similar conditions to those in the present investigation, and obtained almost the same arsenic removal.

An analysis of the kinetic parameters for the process described in this paper, under isothermal conditions, was done using the model-free isoconversional method18. With the use of classical-deterministic kinetic models, problems arise from the calculation procedures, where different methods give different results due to the compensation effect among Arrhenius parameters if the temperature dependence of the rate constant k(T) is described by the Arrhenius equation19,20.

Vyazovkin19,21 developed an integral kinetic method where no model has to be selected (model free-kinetics), which allows both simple and complex reaction to be evaluated. When applying the isoconversional method to the experimental results presented in Figure 6, it is important to differentiate the dependence of the degree of reaction (α) on time (τ.) This way, the dependence of rate of reaction (dα/dτ) on time can be obtained for different isotherms.

The isoconversional kinetic analysis described in this paper was performed using differential equations proposed by Friedman22, which allow 'model-free' calculation of apparent activation energy from the slopes of the lines when the logarithm of reaction rate (dα/dτ) is plotted against the inverse temperature of reaction (1000/T), for different time periods of the process.

The differential isoconversional method suggested by Friedman22is based on the equation:

where: α is the degree of reaction, T the temperature, τ is the time, A the pre-exponential factor, E the activation energy, R the gas constant, and f(α) the differential reaction function (reaction model).

From Equation [2] it turns out that the kinetic triplet (A, E, f (α)) gives the kinetic description of a certain reaction. In order to determine this, various procedures were developed, which can be classified as differential and integral23, depending on whether they are based on only one heating rate or more than one heating rate. In this paper we present and discuss a method for evaluating isothermal kinetic parameters obtained at several temperatures during oxidative roasting of the investigated samples. These methods are known to allow for model-independent estimates of the activation energy. Their use allows the dependence of activation energy on the degree of reaction to be investigated.

The activation energy is determined by Friedman's method from the logarithmic form of the rate equation:

This way of consideration enables model-free calculations of activation energy, using Equation [3]. For each time period

from the beginning of the process, ln was plotted versus (1000/T), giving a straight line with the slope (-Eα/R). The activation energy is thus obtained as a function of time and consequently the degree of reaction.

To calculate the other important kinetic parameters (Arrhenius pre-exponential factor (A) and order of reaction (n)), the reaction model f(α) should be determined. The proposed single step reaction model was used, which is usually used in model-free calculations24,25,26:

This means that order of reaction can be defined using the Coats-Red-Fern or Piloyan-Novikova method, which defines rate of reaction as27:

For the isotherms presented in Figure 6, the diagram of dependences: ln=f(ln(l-α)) was constructed, which enabled calculation of the order of reaction n as well as the rate constant k for the process. The calculated kinetic parameters are presented in Table II.

 

 

After introducing the kinetic parameters presented in Table II in the model defined with Equation [7], values of α can be calculated for different time intervals and for all four leaching temperatures. Calculated values for the coefficient α, together with experimentally obtained values, are presented in Figure 7. The correlation between calculated and measured α values is presented in Figure 8.

 

 

 

 

According to the results presented in Figures 7 and 8, correlation between experimentally determined values for enargite removal and values calculated using the defined kinetic model is very high (R2=0.966). This demonstrates that the kinetic model developed using the isoconversional method described in this paper can be used for the prediction of natural enargite leaching results with an accuracy of 96.6%.

Selectivity of the leaching reagent

For the hypochlorite leaching procedure to be applied on a commercial scale, it was important to investigate the behaviour of the other potential constitutions of the copper concentrate during leaching. To determine the selectivity of the leaching reagent, we performed leaching experiments on different natural mineral constituents that can be present in copper concentrates obtained from the ore mined at different locations in the Bor deposit. Each mineral constituent was leached in a separate experiment. According to the results, presented in Table III, it is obvious that this leaching reagent is highly selective, considering the components usually present in the Bor copper concentrate. This concentrate usually contains 50-55 % chalcopyrite, 20-25% pyrite, 1-2% chalcocite, and 1-3% covellite with the remainder consisting of minor constituents and quartz. The usual arsenic content in this concentrate is 0.10%-0.40%, in the form of enargite. Nevertheless, when considering that the amount of concentrate treated in Bor smelter is up to 90 000 tons per month, the quantity of arsenic that enters the pyrometallurgical treatment step can reach up to 350 tons per month. The arsenic content in the copper concentrate can occasionally reach more than 0.5% and can approach up to 1.5 % in the form of enargite, if produced from the ore mined at the locations where this mineral is usually present. Two of the 27 orebodies in the Bor ore deposit contain elevated arsenic levels in the form of enargite. Those two orebodies - the 'H' and 'Lipa' orebodies- usually contain significant amounts of gold and silver in addition to copper. This is the main reason for the occasional exploitation of those orebodies.

 

 

According to the results presented in the Table III, apart from enargite, only covellite is extensively leached in the hypochlorite solution. This could present a problem if the ore is rich in this mineral. However, the presence of covellite in concentrations above 3% in the Bor concentrate is highly uncommon, particularly in the orebodies that contain large amounts of enargite. We therefore conclude that the treatment of the copper concentrates with higher arsenic contents, using the methodology described in this paper would not result in large copper losses due to covellite leaching.

To prove this assumption, and for the purpose of further investigation of the selectivity of the leaching agent, we performed leaching experiments using copper concentrate from one of the locations with a high arsenic content. The experiments were conducted under same conditions as used in the earlier part of this investigation. The chemical composition of the initial concentrate and the residue after hypochlorite leaching are presented in Table IV.

 

 

According to the results, arsenic concentration decreased from 1.47% to 0.006%, and the copper concentration decreased from 19.75% to 15.92%. This remaining copper content is high enough for subsequent pyrometallurgical treatment, bearing in mind that this concentrate will be mixed with concentrates obtained from other orebodies with a lower arsenic content, which do not require leaching.

 

Conclusion

The main arsenic-bearing mineral in the Bor copper concentrate is enargite. Since arsenic is highly toxic and cancinogenic we explored the possibility of its removal from the concentrate prior to pyrometallurgical treatment. We conclude that selective alkaline-oxidizing leaching of enargite in hypochlorite media can be used for arsenic removal from copper concentrates. Reaction rates are fast, with a starting activation energy of 27 kJ/mol. Most of the arsenic is removed during the first 30 minutes of the process, with almost 89% removal at 60ºC (Figure 6). The reaction becomes slower after a layer of copper oxides is formed on the enargite surface (moving dipper in the diffusion area) and activation energy decrease to17 kJ/mol. After 120 minutes at a temperature of 60ºC, almost all of the enargite is reacted (99%).

Diffusion control of enargite leaching in sodium hypochlorite was also reported by Herreros et al.28. They conducted experiments on the dissolution kinetics of enargite with chlorine generated in solution by the reaction between sodium hypochlorite and hydrochloric acid. The kinetics of the dissolution were characterized by two sequential stages: a relatively fast reaction initially, which later became very slow. In the first stage, the fraction of copper extracted varied linearly with time, whereas in the second stage, the dissolution was well represented by the shrinking core model controlled by diffusion through a porous product layer. The calculated activation energies were 15.0 kJ/mol for the first stage and 21.0 kJ/mol for the second.

Values of activation energy obtained in the experiments described in the current investigation are in the same range, which is characteristic for difussion control of the process. The leaching procedure presented in this paper could be the basis of a process for removing arsenic from copper concentrates. Copper converted to CuO can be easily utilized by leaching with H2SO4 solution, which is a standard procedure that needs no explanation. Copper concentrate, after arsenic removal, can also be treated pyrometallurgically by the standard procedure described in Figure 1. After calculation of the correlation between experimentally determined values for arsenic removal during the leaching process and the values calculated using the kinetic model developed it was determined that the correlation coefficient is extremely high (R2=0.996). The isoconversional method of modeling presented in this paper can therefore be regarded as suitable for describing the process with very high accuracy29,30.

 

Acknowledgements

This research was funded by the Serbian Ministry of Science, as the part of Project No: TR-19030.

 

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Paper received Jul. 2009; revised paper received Mar. 2011.

 

 

© The Southern African Institute of Mining and Metallurgy, 2011. SA ISSN 0038-223X/3.00 + 0.00.