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The Kidston Gold Mine i s located in northern Queensland some 2 Ukm northwest of Townsville. I t is the largest gold mine in Australia and produces approximately 25 percent of Australia's gold and one percent of the world's gold.Initially, traditional mining industry management approaches resulted in the rejection of what appeared to be an attractive low-grade deposit as an uneconomic proposition. Critical re-examination revealed that the rejection was based upon managerial inflexibility and traditionally over-conservative methods of mine evaluation, construction, operation, projected commodity prices and contingency factors. "Ihus it tradition was to prevail, the Kidston prospect would never have been realised.

Jan 1, 1985

By Knevitt L. T

PART 1Details of Kiewa Scheme.Introduction.Topography.Preliminary Investigations.Geology.Description of Project.Details of Main Works.Main Transmission of Power.Construction Facilities.PART 2Underground Works.Summary of Projected Works.Administration.Labour.Surveying.Safety and Accident Prevention.Medical Attention and First Aid.PART 3No. 4 Head Race Tunnel.Summary.Geology.

Jan 1, 1950

By C. D. Keen

IN the latter part of the summer of 1913 the Conservation Commission of the State of Louisiana, under presidency of M. L. Alexander, decided to stop the waste of natural gas going on at the "burning gas-well," located about 3/4 mile southeast of Oil City, La. On several occasions, both in newspapers and in reports, comment had been made on the condition of this well, its harmful effect on the Caddo gas field, and the considerable loss, estimated at several thousand dollars each month, caused by the escape of the valuable fuel. But nothing had been done to bring the well under control and prevent further waste of gas until the State Conservation Commission took the matter in hand. The gas fields of Louisiana are among the greatest in the country. So far most of the gas has been found in the Caddo field proper, although considerable development has been done in and around the city of Shreveport and near the town of Mansfield in DeSoto parish. To extend the life of the gas fields and to prevent the quick exhaustion of the supply of the natural fuel are matters of vital importance for this section of the country. Four gas companies have entered the Caddo field and supply the surrounding towns and cities with gas. The Arkansas Natural Gas Co. has pipe lines to Little Rock, Ark., and supplies gas to the following cities and towns in that State: Texarkana, Hope, Garland, Emmet, Prescott, Boughton, Beirne, Gurdon, Arkadelphia, Gum Springs, Malvern, Donaldson, Gifford, Perla,- Beaton, Beauxite, Mabelvale, Bryant, Sheridan, Pine Bluff, Little Rock, Argenta, Pulaski Heights, and Hot Springs. The Southwestern Gas & Electric Co. transports gas to Mooringsport, Blanchard, Caddo, Rodessa, Oil City, Vivian, Bloomburg, Hosston, Ida, Dixie, Belcher, and Shreveport. The Marshall Gas Co. supplies gas to the town of Marshall, Texas. The Louisiana Co. has a line to Shreveport.

Jan 3, 1914

By Wm. T. Bray

SYNOPSIS Canadian Refractories, Limited, produce a wide range of basic refractories. The chief raw material use in their manufacture is the magnesite which is mined, and beneficiated in a heavy media separation plant, at Kilmar, Que. This paper describes the underground operation and the plant and explains how the gravity separation of light, siliceous gangue from the ore has changed the mining practice, increased the ore reserves, and improved the chemical uniformity of the crushed ore. HISTORY REFRACTORIES are essential in the production of steel and base metals and in other high-temperature processes. Basic refractories, chiefly composed of magnesia which is obtained by burning magnesite, are used to line and repair basic furnaces. When World War I cut? off the importation of Austrian magnesite, upon which North American industry had depended, domestic sources bad to be found. In Quebec, work was begun on deposits of magnesite at Kilmar, half way between Ottawa and Montreal and about ten miles north of the Ottawa river. By the end of the war substantial tonnages were being quarried and calcined, but, when Austrian magnesite again became available, the industry declined rapidly. In 1925, the National Research Council, in co-operation with the Federal Department of Mines, began an investigation of the industry's technical problems. The result of this research work, which was taken over fully by the Company in 1943 and is actively continued, is that the single product of the early 1920's has been supplemented by more than forty specialized products serving the metallurgical and chemical industries across Canada and in more than thirty other countries.

Jan 1, 1951

By Julien Deby

THE sinking of a deep shaft is always a serious undertaking, especially when the strata to be traversed are of great hardness, or when they are feebly coherent or highly saturated with water. In the, first case, that of solid rock, modern appliances, such as the rock-drill, put into motion by air-compressors, along with suitable explosives, will generally answer the purposes of the mining engineer until he has reached the main water-levels. When these have

Jan 1, 1877

By L. A. André Santos

Atmospheric processing of nickel lateritic ores with low costs has been encouraged. In this work the kinetic of atmospheric acid leaching of a northern- Brazilian ore with 1.63% Ni and large amount of fine particles (d50 ≈ 0.075 mm and 40% below 0.038 mm) is presented. Chemical analysis showed a trend of Ni and Fe concentration in finer fraction (−0.075 mm) and Si and Mg in the coarsest one (−0.500 + 0.150 mm) associated to distinct mineral phases. Nickel is widespread in the mineral matrix. Distinct behaviors were observed as a function of particle size associated to the distribution of silicates and iron oxides in the ore. The kinetic modeling indicated that leaching is controlled by porous layer diffusion at 65 °C, but at 95 °C exhibits a mixed control by porous layer diffusion in initial minutes (60 min) and by chemical reaction or diffusion through the pore layer in final minutes (60–240 min) depends on metal evaluated.

By M. J. Nicol, P. D. Scott

The kinetics of the non-oxidative dissolution in acids ofthe iron sulphides FeS, Fe-FeS, and Fe9S10 were studied by the use of rotating-disc electrodes of the various compounds. It was found that the rates of dissolution vary by orders of magnitude with changes in surface potential. The dissolution rates depend on non-integral orders of hydrogen-ion concentration, which in turn vary with potential. A mechanism based on the following premises is proposed to explain the kinetics of dissolution of the iron sulphides. (I) Only an FeS compound that is exactly stoichiometric dissolves in accordance with the accepted theory of ionic charge transfer. (2) Any non-stoichiometric iron-deficient iron sulphides must be reduced to exactly stoichiometric FeS before spontaneous non-oxidative dissolution can occur. The dissolution of Fe.S1o and slightly iron-deficient FeS compounds under open-circuit conditions occurs only when an oxidation reaction (usually the oxidation of hydrogen sulphide to elemental sulphur) can provide the electrons necessary for the production of exactly stoichiometric FeS. The establishment of such a mixed-potential system is the reason for the induction period that occurs during the dissolution of pyrrhotites in acids.

Jan 1, 1979

By R. Hogg, T. F. Dumm, L. G. Austin, M. Yekeler

"Dedicated to Professor Kurt Leschonski on the occasion of his 60th birthdayAbstractThe kinetics of batch grinding quartz from a feed of 600 by 425 Jim to a product of 80% less than 10 µm have been determined using screening and laser diffractometer sizing for size analysis. The specific rates of breakage decreased by a factor of about three when the material became less than about 100 µm in size, but the primary breakage distribution function also changed to give proponionately more fine material, so that the grinding efficiency expressed as the development of surface area (B.E:T.) per unit of energy input did not decrease. Analysis of the shape of the particles in the 2S x 38 µm size range showed that particles of this size produced by roll crushing or by 8 minutes of grinding of a 42S x 600 µm feed were not different but at long grinding times the particles were rounded. This suggests that the breakage mechanism changes to give more chipping and abrasion and less disintegrative fracture. As the material approached the ultrafine size range it adhered to the mill case and there was no further size reduction. However, a technique for striking the mill case to dislodge the particles was successful in allowing further grinding to 400Jo by weight less than 2 µm.1 IntroductionIt has long been known that it is difficult to accomplish ultrafme grinding in a tumbling ball mill. It has been reported [12, 13] that there is no further size reduction after some hours of grinding cement clinker in laboratory ball mills. Austin and Bagga (1] and Shah and Austin [16] have given an analysis of the kinetics of dry grinding in a laboratory ball mill, introducing the concept of a slowing-down factor K, which is the ratio of the specific rates of breakage at some long time of grinding to the normal specific rates of breakage. They showed that this factor decreased as fine material accumulated in the mill charge. Cottaar and co-workers [8-10] showed that the movement of solid in a dry laboratory ball mill was influenced by the fineness of the solid and by the presence of air, and that evacuation of air from the mill caused particle sedimentation and low rates of breakage.The concept of the slowing-down factor has also been used in wet grinding [17, 18]. At very .high slurry concentrations it appears to be correlated with a steady decrease of mill power caused by the build up of a layer of deposit sticking to the mill case. This reduces the effective mill diameter and, eventually, the balls start to adhere in the layer and centrifuge. A decrease of mill power always indicates less lifting and tumbling of the media and, hence, less breakage. However, slowing-down of breakage rates was also observed at lower slurry concentrations where there was no change in mill power."

Jan 1, 1990

By A. S. Ibrado, D. W. Fuerstenau

"Gold, silver and copper form various complexes with cyanide, of which only the singly charged dicyano form adsorbs appreciably on activated carbon. The adsorption of the dicyano complexes appears to be controlled predominantly by chemical reaction at the surface of a shrinking unreacted core. Metal uptake over time is non-linear, which eliminates control by boundary layer diffusion. The rate of adsorption is not enhanced by a reaction interruption, which suggests the absence of concentration gradients in the pores. Finally, the rate of adsorption increases with decreasing activated carbon size in a manner consistent with the shrinking core model. The results of this investigation accentuate the importance of efficient acid washing of carbon and removing carbon fines from the barren carbon stream. INTRODUCTION With the dwindling reserves of high-grade ores, most of the world’s gold is produced from low-grade ores by cyanide leaching. In the past, leaching was followed by the Merrill-Crowe process, in which gold is precipitated from clarified pregnant solutions by zinc cementation. This process is still being used for high-silver ores, where the cost of carbon stripping becomes prohibitive. For deposits with silver-to-gold ratios of about 4 or less, adsorption on activated carbon would be the usual solution purification step taken. The process simplifies solid-liquid separation and offers a viable solution to preg-robbing organic carbon in some ores. The modern industrial application of carbon adsorption started with the carbon-in-pulp (CIP) process, where carbon adsorption was used mainly as a solution purification step. In 1973, Homestake Mining Company commissioned the first large-scale CIP plant in the U.S.A.1 Later, carbon was added earlier in the circuit to control preg-robbing by adsorbing gold cyanide onto activated carbon as soon as it is dissolved. The scheme is successful because activated carbon is a stronger adsorber than the organic carbon found in preg-robbing ores. This process came to be known as the carbon-in-leach (CIL) process. Numerous research investigations have been performed on the chemistry involved in the CIP process, which at the time of its introduction was not clearly understood. Of these, research on the kinetics of adsorption probably bears the most immediate impact on industrial practice,2,3 where adsorption systems rarely reach equilibrium, if at all, and slight slowdowns in the adsorption rate can translate into significant decreases in revenue. To illustrate this, organic compounds, like flotation reagents, have been known to impair CIP circuits. However, laboratory tests showed that the organic compounds do not significantly affect the adsorption capacity of activated carbon. Rather, the harmful effect may be attributed to a lowered adsorption rate.4,5 Also well known is the faster rate at which fine activated carbon powders reach equilibrium compared to coarse activated carbon, even though the final (equilibrium) amount of material adsorbed per unit weight is the same."

Jan 1, 2015

By E. Krystad, G. Tranell

"The kinetics of boron removal from liquid silicon during slag refining, as a process step in the production of solar grade silicon, has been investigated by means of small scale mass transfer experimental series at 1600°C, using a graphite crucible. The slags were SiO2-CaO based, with or without addition of approx. 19 wt% MgO. Experiments were carried out at slag-metal ratios of 1 or 2, where the silicon initially contained approx. 250 ppm boron. The metal-slag mass transfer coefficients for boron were found to be in the order of 1-3 · 10-6 m/s and were largely influenced by slag composition. The mass transfer rate was higher for the MgO-containing slag than the slags without MgO. The final equilibrium distribution of boron between metal and slag, LB, was determined to be in the order of 2.3-3.3.I. INTRODUCTIONRecent years have seen a race in industry and research aimed at obtaining a reliable metallurgical route for production of silicon for solar cells (SoG-Si) from metallurgical grade (MG) silicon. Metallurgical routes can successfully challenge the traditional chemical routes for production of SoG-Si if they generate metal of sufficient purity while being less expensive in terms of production cost and energy consumption. Efficient removal of boron is one of the greatest obstacles in the refining of silicon by a metallurgical route, because the segregation coefficient of boron in silicon makes directional solidification unfeasible; in addition, the vapour pressure of boron is not high enough for removal by vacuum refining. However, the thermodynamic properties of boron makes removal from silicon by oxidation possible, and thus the process of slag refining of silicon has been receiving increasing attention as a method for boron removal."

Jan 1, 2012

By Ahmad Ghahreman, James McNeice

"Cerium is the most abundant rare earth metal and is often found in deposits along with small amounts of more valuable metals such as neodymium and gadolinium1. As a result, the production of cerium oxide often exceeds market demands, thus in some cases it would make more sense to remove the cerium from the process solutions before further purification. A common method of cerium removal is to precipitate CeO2 from the acidic leach liquors by raising the pH to oxidize cerium(III) to cerium(IV). This study investigates the oxidation kinetics using three oxidants; hydrogen peroxide, sodium hypochlorite, and potassium permanganate. The effect of oxidant, pH, cerium concentration and temperature on the oxidation kinetics will be discussed. Cerium oxidation in solutions with pH ranging from 1.0 to 4.0 was investigated at cerium concentrations ranging from 2.0 g/L to 16.0 g/L. A cerium recovery of 40% can be achieved at different conditions with each oxidant at room temperature, with higher recovery at 60°C.INTRODUCTION Over the last 70 years, the rare earth elements (REE) have become crucial components of modern technology. These metals are categorized as light rare earths (LREE) or heavy rare earths (HREE) by governments and miners based on weight, abundance, and therefore value. The minerals bastnaesite, monazite, and xenotime compose the majority of the world?s exploitable sources of these metals (Binnemans, 2013; Parker and Baroch, 1971). Geologists classify the LREE ores as „cerium group? minerals, approximately 50% cerium oxide by weight. The cerium group minerals monazite and bastnaesite compose the majority of world production, leading to an overproduction of cerium relative to world demand. This ratio of light to heavy REE in deposits has led to a phenomenon referred to as the balance problem (Binnemans et al., 2013). As an example, to produce 1 tonne of europium oxide from a bastnaesite deposit 450 tonnes of cerium oxide must be processed. This means that any push to increase production and access the value of the HREE metals will drive down the value of the LREE metals leading to diminishing returns (Zepf, 2016). These ores also contain measurable levels of thorium, subjecting them to complex radioactive waste regulations. During the 20th century, the USA was the largest producer of rare earth metals (REMs), primarily sourced from the Mountain Pass mine in California. However, due to a combination of market dynamics and regulations, China has dominated the market for the last two decades. The largest Chinese REE mine, Bayan Obo, produces rare earth (RE) concentrate as a byproduct of iron mining, decreasing their relative production costs (Gupta and Krishnamurthy, 2005). This mine alone represents about half of world bastnaesite production (Zhi and Yang, 2014). Rising demand for high-tech products has forced Chinese producers to commission other large mines, climbing to 90% of world production in the early years of the new millennium (Mancheri, 2016). This presents the west with a looming supply risk of these critical metals in the future."

Jan 1, 2017

By M. J. Virnig, C. P. J. Van Vuuren, A. J. Botha

The Zadra, AARL and organic elution processes and variations of them are presently widely used to recover gold from activated carbon. Despite this the study of the kinetics of elution have received relatively little attention. It is the aim of this study to investigate the rate processes taking place during elution in both inorganic and organic solutions. Batch adsorption and elution rate and equilibrium experiments were performed. The spatial concentration of gold inside carbon particles at various stages of the adsorption and elution processes were measured with a scanning electron microscope using an image analyzer to control and manage the micro-analysis data. The activated carbon particles exhibited film and intra-particle mass transfer rate- controlled behaviour during adsorption in a caustic aqueous solution at 95°C. Elutions in the aqueous caustic acetone solution at 30°C and the caustic aqueous solution at 95°C were unaffected by change in stirring rate. Elution was modelled by desorption reaction rate-control at the outer surface of the carbon particle. Adsorption and elution isotherms under duplicated solution conditions showed reasonable agreement for the inorganic solution and a large disparity for the organic solution.

Jan 1, 1993

By P. R. Taylor

Batch leaching experiments have been performed to study the kinetics of galena leaching in fluosilicic acid solutions with oxidants. Variables studied included: fluosilicic acid concentration, oxidant type, oxidant concentration, particle size and leaching temperature. It was found that hydrogen peroxide was the most effective oxidant, compared to the others studied, and the effect of the oxidant concentration on the leaching behavior of galena was very significant. Also, decreasing the particle size and increasing the leaching temperature increased the extraction rate. The initial, apparent activation energy was calculated to be 11.72 kJ/mole (2.8 kcal/mole) and suggested that galena leaching in fluosilicic acid solution, with hydrogen peroxide as an oxidant, may be controlled by fluid film mass transfer initially. The reaction appears to be retarded by the formation of elemental sulfur and the sulfur oxidation becomes a major resistance to the overall leaching reaction.

Jan 1, 1992

By Moo Eob Choi

The reduction of iron oxide particles by hydrogen is one of the most widely investigated gas-solid reactions. The search for new methods for producing iron by the direct reduction of iron oxide has resulted in a large number of exhaustive studies of the various aspects of this reaction. However, previous studies have largely been done with either pellets or lump ores. Little has been published on the hydrogen reduction of very fine concentrate particles smaller than 37 µm (-400 mesh). The kinetics of hydrogen reduction of fine iron oxide concentrates were investigated in the temperature range of 900 - 1300°C.

Jan 1, 2006

The production of synthetic rutile from ilmenite using hydrochloric acid leaching is investigated. Previously published data is used to comment on the optimum process conditions. It is shown that the most important aspect to consider is the maximisation of impurity dissolution and the minimisation of titanium losses.

Jan 1, 2001

By Tsuchiya N, Takada Y, Okabe K

Alkalis in the blast furnace are removed mainly by the slag, Alkali removal by the slag was studied as a rate process of alkali vapor- ization from the slag flowing through the dropping zone in the blast furnace. The vapor-, ization rate of I:20 from CaO-Si02-A1203 IZ20 slag was- measured under various experimental conditions. An empirical formula for the vaporization rate was obtained as a function of slag basicity, temperature and surface area per unit mass of slag. A simulation model of IC20 vaporization in the dropping zone was evaluated using the rate equation when the true velocity and surface area of the slag was de- termined from a flow dynamic model of counter- current gas-liquid flow through packed beds. The influence of the dynamic conditions of flow, as well as the slag basicity and temperature, on alkali removal by the slag was estimated.

Jan 1, 1980

By I. González, G. Lapidus, M. Teutli

The cementation kinetics of silver with aluminum particles were studied with model solutions under nitrogen atmosphere, varying the temperature, aluminum/silver ratio, pH and concentrations of thiourea and surface activator Recoveries were evaluated both by solution concentrations and by REDOX measurements. Tafel curves were determined for this system. The results showed the cementation process to be essentially independent of the pH and thiourea concentration. However, a strong influence was observed with respect to temperature, aluminum/silver ratio and the quantity of activator. There is evidence that the controlling step is the dissolution of aluminum oxide from the particle surface.

Jan 1, 1990

By M. J. Nicol, C. van Wensveen

The kinetics of the oxidation of thiosulfate by copper(I I) in ammoniacal solutions have been studied in the presence and absence of dissolved oxygen. The formation of an intermediate mixed ammine/thiosulfate copper(II) complex ion has been confirmed and the rate of the reaction monitored by simultaneous on-line spectrophotometric, dissolved oxygen and potentiometric measurements. The rate of the anaerobic oxidation of thiosulfate by copper(II) was found to be orders of magnitude slower than that in the presence of dissolved oxygen and is inhibited in the presence of ammonia and anions such as sulfate and chloride as a result of competition with thiosulfate for the axial coordination sites on the copper(II) tetrammine complex. In the presence of dissolved oxygen, it was found that the copper(I) thiosulfate complexes are only very slowly oxidized while the copper(I) diammine complex is rapidly reoxidised to the copper(II) state. Thus, the initial rapid reaction with copper(II) leads to a pseudo steady-state condition in which the concentration of copper(I) is relatively constant and the rate of oxidation of thiosulfate can be predicted from the measured rate of oxidation of copper(I) by oxygen in ammoniacal solutions. The effects of the concentrations of ammonia and thiosulfate on the oxidation rate can be rationalized on the basis of the above coupled to the species distribution of copper(I) in the ammonia/thiosulfate system. It is shown that, with relatively simple measurements of dissolved oxygen and copper concentrations, the rate of oxidation of thiosulfate can be predicted under typical leaching conditions.

Jan 1, 2005

By M. J. Nicol

The kinetics of the dissolution of colloidal silver in aerated cyanide solutions has been investigated with the aim of developing a relatively rapid and convenient method for monitoring the ?leaching power? of solutions typically used in the cyanidation process. Experimental results obtained are consistent with an electro-chemical model, in which the mixed potential is set up in the active region of the polarization curve for the anodic dissolution of silver, giving rise to a rate of dissolution which is controlled by the rate of mass transport of either cyanide or oxygen to the surface of the silver. The rate of dissolution of colloidal silver was found to respond to variations in the reactant concentrations in a similar manner to gold (and silver) in a typical free-milling ore. The use of this technique for the monitoring and control of the cyanide leach process is discussed.

Jan 1, 1998

By G. Cifuentes

The kinetics of the electrolytic oxidation of cyanide to cyanate on PbO2-coated stainless steel anodes have been studied by both experimental and theoretical means. The anodes were based on 316 steel and performed in a satisfactory fashion. The pH of the studied KCN solutions exhibited a constant value about 11. Values for all the kinetic parameters have been determined and a mechanism for the studied reaction is proposed.

Jan 1, 1999