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By D. G. E. Kerfoot

In September 1945, when the Lynn Lake nickel orebody was discovered Sherritt Gordon Mines was a small copper mining company with rapidly depleting ore reserves at its single producing mine at Sherridon in the Cold Lake area of Manitoba, 100 miles north of The Pas. The company has been formed in 1927, largely through the efforts of Eldon L. Brown, a 27-year old mining engineer, with the financial backing of Thayer and Halstead Lindsley and the Gordon family. The Lindsleys were American mine promoters who had been successful in the Sudbury area, and the Gordons had extensive interests in the lumber industry in northern Ontario. Carl Sherritt, who gave his name to the company, was an American trapper and prospector who had staked the copper property and sold his interest to the new company. Carl Sherritt died in a flying accident at The Pas in 1928. The Sherritt Gordon Mine started production in 1931, shipping copper concentrate to the new Hudson Bay copper smelter at Flin Flon, Manitoba. In 1931 the price of copper was 18¢/lb. Within a year the price had fallen to 5¢ /lb and the mine was forced to close. It remained closed through the Depression years.

Jan 1, 1999

By M. M. Papic

"This paper describes the Sasol coal liquefaction process, as used in South Africa. It covers coal supply, coal gasification, gas purification, Fischer-Tropsch synthesis, the major utility systems involved and the economics of the process.IntroductionThe Sasol coal liquefaction process is based on Fischer-Tropsch synthesis of liquid fuels from carbon monoxide and hydrogen, which are in turn obtained by gasification of coal with steam and oxygen. The process is shown schematically in Figure I.The first step in the process is coal preparation, in which the coal is crushed and screened to a 3-50 mm size for gasification on one side and to -3 mm size for steam and power production on the other. Oxygen needed for coal gasificatoin is produced in the air separation plant.Coal is gasified under pressure by steam and oxygen in the Lurgi gasification plant, where raw, impure gas is produced . The raw gas is first washed in a scrubber with a circulating gas liquor, heat is then recovered from it in a waste heat recovery boiler and the gas is further cooled for purification. Water-insoluble materials (tar oils) in the gas liquor are separated from aqueous solution and sent to tar refining for the recovery of tar products. The aqueous portion of the gas liquor goes to a Phenosolvan solvent extraction process, where phenols and ammonia are recovered. Water then proceeds to the effluent treatment plant.The scrubbed and cooled raw gas goes to a Rectisol gas purification plant, where all components other than hydrogen, carbon monoxide and methane are removed as completely as possible by absorption in refrigerated methanol. The acid gases (CO2, H2S) stripped from the methanol in the Rectisol unit are processed in a Stretford plant for recovery of sulphur. Regenerated methanol is returned to the process. The purified synthesis gas is passed to the fluidized-bed Synthol reactors, where Fischer-Tropsch synthesis reactions take place.The synthesis products are recovered in a product recovery unit as separate streams of decant oil containing higher-molecular- weight hydrocarbons, light oil comprised of lower-molecular- weight species, the aqueous stream containing water solubles, a C3/C4 stream, a C2 stream , a methane stream and a hydrogen-rich stream. Most of the hydrogen is recycled to the Synthol reactors; a major portion of the methane is reformed to hydrogen and carbon monoxide for recycle; the C2 fraction goes to an ethylene plant; and liquid streams proceed to the product refinery.The product refinery is used to upgrade and purify the Synthol products to specification fuels and chemicals.Sasol l, the first coal liquefaction plant in South Africa , was built in 1955. It is still operating and has a product output of about half a million tonnes per year. The Sasol II plant is in a commissioning stage and will be in full operation in 1981. It is about five times the size of Sasoll. It uses over 12 million tonnes of coal and produces more than 2 million tonnes of saleable products annually (1,2,3). The Sasol llI plant, which is a mirror image of Sasol II, is under construction and scheduled for completion in 1983."

Jan 1, 1981

By G. E. Agar

"The distribution of gold in the grinding-classification circuit of an operating gold plant was determined by assaying the size fractions of samples from each of the streams. This analysis identified the streams with the maximum potential for gravity recovery of gold and revealed that there was up 110 seventy-five times as much gold in the primary cyclone underflow as in the concentrator feed.Laboratory jigging and tabling tests were done on samples from two of the streams to determine what the recovery might be with a gravity circuit and to show that a high grade concentrate could be produced. A numerical simulation procedure was used to calculate a material balance for a circuit that included gravity separation on the primary cyclone underflow. The numerical simulation optimistically indicated that as much as 84% of the gold might be recovered in a reasonable grade of concentrate even though the recovery in batch bench scale tests was only 14%.Incorporation of a gravity separation device would reduce the inventory of gold in the grinding-classification circuit.INTRODUCTIONMany gold concentrating plants include a gravity concentration operation while others do not and the reasons that some do and some do not is not clear. Some of the advantages and disadvantages of gravity circuits are discussed by Penman (Penman 1987) without clear cut resolution. Penman's comments elicited an interesting response from Lloyd (1989) who produced a simple way to determine if the addition of a gravity concentration circuit would enhance the recovery of gold. Lloyd's method does not consider the cost of running the circuit so it only partially answers the question. There are reports in the literature (Wells and Patel 1991, Matwijenko 1988) that as much as 60% of the entire production comes from a gravity circuit when it is used, and that the grade of the concentrate produced often exceeds 65% gold, an assay that far exceeds most Merrill-Crowe precipitates that are sent to refining. In at least one instance (Hood 1984) a range of recovery from 40-50% was indicated from laboratory test work and the plant subsequently realized recoveries in the range of 26-40%. Despite these favorable numbers other plants use gravity separation when as little as 20% of the gold is recovered in the gravity concentrate (Carter 1992)."

Jan 1, 1993

By T. C. Holmes

"Dome mine, in the Porcupine mining camp of northern Ontario, is one of the important gold mines of Canada, its production of gold from the commencement in 1910 to the end of 1946 having a value of $149,000,000.GENERAL GEOLOGYThe oldest rocks in the mine are greenstones of Keewatin age(l). Those to the south are known as the southern greenstones, but little is known of their structure. Those in the northwest part of Fig. 1 and the north part of Fig. 2 are known as the northern greenstones or greenstone 'nose'. They face north, dip steeply north, and end to the east against an unconformity which pitches northeast about 20°. The volcanics are overlain unconformably by Timiskaming .conglomerate and slate. All these rocks are cut by porphyry. Closely associated with the porphyry is a group of rocks that have suffered extreme alteration. Diabase dykes intrude all the other rocks and the ore. The principal massive rocks in the mine are two adjacent flows known asthe andesite (south) and dacite (Fig. 1). They are composed chiefly ofmassive, medium-grained lava. Pillows, flow lines, and other typically volcanicfeatures are found along the tops of both flows and at other places in theandesite. These parts nearly everywhere show a slight schistosity panllelwith the flows except in the orebodies, where they are massive."

Jan 1, 1954

By D. Monder

Fuel cells are promising sources of electrical energy because of their exceptionally high efficiencies and low environmental emissions. Solid oxide fuel cells (SOFC) are high temperature, ceramic electrolyte cells, which unlike most other fuel cells, can work with a variety of fuels besides pure hydrogen, including hydrocarbons and hydrogen sulfide. In this presentation I present the models we have built for a single H2S fuelled SOFC. The goal is to model the electrochemical reaction coupled with mass transfer, fluid flow and current/voltage distribution in an yttria stabilized zirconia electrolyte fuel cell assembly operated between 750 and 850 °C. Two models of the above SOFC are discussed in this work, 1) an algebraic model derived by integrating a one-dimensional model along the thickness of the cell, and 2) a two-dimensional finite element axi-symmetric model. Important physical and kinetic parameters in the 1-D model are fitted using experimental data sets at three different temperatures and reasonable fits are obtained for the data sets at 800 °C and 850 °C. However, the third data set at 750 °C does not give a good fit using this model. We need to apply the curve-fitting to more data sets to investigate it further. The main conclusion that can be drawn from the present study is that the ohmic resistance of the cell is very high. Contact resistances are believed to be the reason behind this although there could be contributions from resistive interphases. The 2-D model also gives reasonable fits to data sets. One of the publications by the laboratory group doing the experimental work in our department presented very interesting data that shows the cell performance being a strong function of fuel flow-rate. We want to model this behaviour and will have to depend on the 2-D model as the 1-D model does not have flow-rates as parameters.

Jan 1, 2005

By J. L. Jambor, E. J. Reardon, E. C. Appleyard, J. A. Cherry

Since the 1957 initiation of deposition of mill tailings at the Heath Steele mine, New Brunswick, periodic detailed studies of the tailings geochemistry and mineralogy have been conducted, thereby providing a unique opportunity to examine the geochemical evolution of a sulfide rich mine>tailings impoundment. When deposited, the tailings contained about 85 wt% sulfide minerals, 1 wt% to 3 wt% carbonate minerals, and 12 wt% to 14 wt% alumino silicate minerals. Mineralogical examination of samples of the tailings from deep in the impoundment indicates that little oxidation occurred prior to tailings deposition. The mill process-water deposited with the tailings was neutral to slightly basic and contained low concentrations of Cu, Pb, Zn and As. Sampling of the tailings five years after deposition indicated that sulfide-oxidation reactions, occurring near the tailings surface, had decreased the tailings-water pH and increased the concentrations of Fe, S042-, Cu, Zn and Pb (up to 10 000 mglL, 25 000 mg/L, 2.5 mg/L, 200 mg/L, and 4.5 mg/L, respectively). In 1975, ten years after decommissioning, the tailings could be divided into three zones: an upper oxidation zone in which sulfide oxidation is actively occurring, a hardpan layer, 15 cm to 20 cm thick, composed of tailings cemented by secondary Fe minerals, and an underlying reduction zone in which the tailings are relatively tin oxidized (Boorman and Watson, 1976). Chemical analyses indicated the presence of low-pH waters containing very high concentrations of SOi-, Fe, and other metals (up to 63 600 mg/L SO42-, 28 600 mg/L Fe, 10 mg/L Pb, 600 mg/L Cu and 4000 mg/L Zn), suggesting that there was a period of intense sulfide oxidation between five and ten years after tailings deposition. More recent sampling, conducted some 20 years after the end of tailings deposition, indicates that relatively little change has occurred in the last ten years, thereby suggesting that the hardpan layer has provided an impediment to the downward movement of dissolved constituents. Analyses of the tailings solids show increased accumulations of many metals at or near the depth of the hardpan layer. Evaluations of the long-term evolution of the tailings can be enhanced by comparison of descriptions of the tailings with descriptions of the gossan that overlay the massivesulfide orebody prior to mining. At Heath Steele, this comparison suggests that many of the mechanisms controlling the distribution of metals in the tailings will probably persist over geologic time.

Jan 1, 1992

By Z. D. Hora

The major fluorite producer in British Columbia was the Rock Candy Mine, inactive since 1942. Other deposits of economic interest include the Rexspar deposit, in which fluorite is associated with uranium and rare earth mineralization, and the Eaglet and Liard River occurrences. THE former Rock Candy fluorite mine, located 26 km north of Grand Forks, is the only major past producer of fluorite in British Columbia. The deposit was in production from 1918 to 1929 and again in 1942; total output was about 36,000 tonnes with average grade between 22 and 32 per cent CaF2. The fluorite body occupies a steeply-dipping vein structure, approximately 175 m long and up to 12 m wide, in porphyritic syenite. The chief vein-filling minerals are quartz and fluorite with local small len ses of barite. Fluorite content decreases with depth and the deposit becomes silicified. The Rexspar (or Birch Island) fluorite deposit is located 130 km north of Kamloops. The deposit is complex with rare earth elements and high uranium values, but !1uorite mineralization forms an independent zone adjacent to the uranium orebodies. Fluorite is present as fine-grained impregnations and as breccia cement in strongly schistose or brecciated alkali feld spar porphyry. Reported reserves are 1,088,000 tonnes of 22 per cent CaF2 or 450,000 tonnes of 29 per cent CaF2. 268 Another potential deposit of fluorite is Eaglet, situated on the north side of Quesnel Lake. Fluorite occurs as a stock work with scattered veins and irregular lenses up to 20 centimetres wide and as impregnations in altered Proterozoic Kaza Group feld spathic gneiss over an area of 1,500 metres by 500 metres. To date (1983) approximately $2 million have been spent on the exploration of this property and reserves of 18.8 mimon tonnes grading 11.59 per cent CaF2 have been outlined . A group of significant occurrences is known from north of Liard River Hot Springs Park , where fluorite occurs in small zones up to 17 m thick along the interface between Middle Devonian Dunedin Formation limestone and Middle Devonian to Mississippian Besa River Formation argillite. Fluorite, associated with witherite, barytocalcite and barite, is present as replacement bodies, breccia fillings and minor veins.

Jan 1, 1984

By A. Koning, P. Lauzon

Pressure hydrometallurgy operations require vessels to be lined with an impermeable membrane for corrosion protection and one or more courses of refractory or ceramic brick. Examples of unit operations that utilize composite lining systems include pressure oxidation autoclaves, sulphide precipitation autoclaves, chloride leach reactors, flash vessels, cyclone separators, and direct contact condensers (heater vessels and quench vessels). The refractory lining must satisfy multiple requirements: it must thermally insulate the membrane from process fluid, be structurally stable, provide erosion resistance, be chemically compatible with process fluid, and provide an economic service life. New hydrometallurgical processes are pushing the pressure, and temperature, with each new generation of plants. A fundamental understanding of all factors affecting the mechanical stability of the lining system is essential as lining designs move further away from the industry's experience base. The impact of irreversible chemical swell, operating factors, design factors, and installation factors are presented based on modifications to the traditional one-dimensional mechanical stress model. A new stability criterion - that the brick lining remain in contact with the steel shell membrane - is presented. This new stability criterion imposes new restrictions on the lining design.The effect of geometry and adding additional degrees of freedom to the analysis is explored using two-dimensional and three-dimensional Finite Element Analysis (FEA). The effect of these additional degrees of freedom on the results of the one-dimensional model are discussed.

Jan 1, 2004

By W. P. Clement, M. C. Bell

"PT International Nickel Indonesia, a subsidiary of Inco Limited, mines and processes nickel laterite ores for the supply of nickel matte, primarily to the Japanese market. It has large ore reserves and a substantial portion of its energy requirement is supplied from its own hydro-electric plant. Since the early 1980s, the company has increased its production level and has dramatically reduced its unit costs. Projects are in progress to further decrease costs and recently a major expansion - 31% increase in nominal capacity - has been undertaken, consistent with marketing opportunity in Japan. The expansion project, which has a low capital cost per unit of production, is outlined in this paper.IntroductionPT Inco is a fully integrated mining and smelting facility located in Indonesia on the island of Sulawesi, and is based on a very large, world class nickel laterite orebody located 60 km inland from the Gulf of Bone. Construction of a single furnace line plant started in 1973. Complete supporting infrastructure of townsite, hospital, schools, shopping centres, road systems, and an airport, all had to be built. Prior to completing the first phase, the decision to expand the plant to a three kiln-furnace line was made. A major factor in the decision was the ability to develop the hydroelectric potential of the nearby Larona River. This involved construction of a 30 m high dam, and a 7 km surface canal to the generating station. The penstocks drop 150m to three 55 Mw turbines. The power generated is sufficient to supply the entire electrical load for the complete smelting complex and town site. The unique capability to supply the high smelting energy requirements for a lateritic nickel ore by fully captive hydro power, has, over the past decade insulated PT Inco from the large upward swings in oil prices suffered by other lateritic nickel producers.Wet ore is first partially dried to 20% moisture in two co-currently fired rotary driers, screened on an internal trommel, and delivered to two dry ore storage buildings. The partially dried ore is calcined at 750°C and partially reduced in three large 100 m by 5.5 m kilns. Reduction is accomplished by lancing bunker C oil onto the ore bed at the discharge end of the kiln. The kilns are equipped with five air pipes with onboard blowers to gradually bum the combustible gases generated by the lance oil. The kilns were also originally equipped with two side burners to supply additional heat close to the feed end of the kiln. Calcined ore is transferred by 20 ton refractory lined containers to the furnace feed bins at the top of the smelter. Smelting is carried out in three 18 m diameter furnaces powered by 45 Mw transformers. Slag is skimmed at 1550°C through water cooled breast plates and removed to the slag dump by Haulmaster Carriers. Matte of 25% Ni, 1O% S, 65% Fe is tapped at 1350°C into the converter aisle. The iron is slagged in converters to produce a nickel sulphide matte at 80% Ni. Three rotary Kaldo converters were initially installed. The product matte is granulated, dried, and shipped in returnable rubber bags to Japan. Most of the matte is fluid-bed roasted to nickel oxide and then directly reduced in a second reducing fluid bed reactor at our facilities in Japan.The smelting complex was designed to smelt two million tonnes of dry ore per year, equivalent to 34 000 tonne nickel production at an ore grade of 2% Ni. The cost of the entire project including working capital was $900 million."

Jan 1, 1990

By A. C. Stevenson

"The most common theory is that, since thyristors, diodes, and insulated gate bipolar transistors (IGBTs) are “solid state” they will live forever. This is not so. They have wear-out mechanisms (e.g. insulation) and other mechanical parts such as motor bearings. These wear-out phenomena can be easily calculated. In this paper we will look at some of the failures and the failure rate of thyristors in power converters to see what affects them and to see what improvements can be made. If converter failures do occur, some simple forensic engineering steps will show if this is the root cause of the problem.IntroductionLook at the general failure rate curve for thyristors, diodes, gate turn off devices (GTOs) and IGBTs shown in Figure 1. We see that there is an initial high failure rate due to manufacturing defects, application problems, and drive start-up stresses that lasts for a few weeks. This is followed by a long period of (hopefully) several years with a relatively low but very slowly rising failure rate. At the end of this period, the devices start to wear out and the failure rate suddenly starts to increase rapidly over a few months. This signals the end of life for the devices in the system. We will start by looking at this end of life area."

Jan 1, 2000

By Jo Render

Expectations of your management approach ??Life of mine applicability ??Tailor scale of activity to scale of project ??Assess impacts, risks, and opportunities ??Use global good practice, backed up by rigorous analysis ??Support with trained monitoring and evaluation team ??Information infrastructure to allow ongoing trend analysis and tracking of progress ??Public reporting using standardized indicators Yes, we are talking about a ?management system?

May 1, 2011

By E. O. Magnusson

THE orebodies of the Preston East Dome mine show a considerable variation in size,? shape, dip, and ground condition. They vary from small and large irregular masses being mined by shrinkage, cut-and-fill, and square set-and-fill mining methods to narrow veins being mined by open stoping. Standardization of mining operations has necessarily been difficult. This considerable variation in mining condition prompted the development of a bonus system which would give more equitable bonus payments through-out the mine than those obtained by the usually accepted methods of calculating mine bonus. PRINCIPLES ON WHICH THE SYSTEM IS BASED Under an incentive bonus system, performance (efficiency) and a price per unit of work done are inter-related. It is in the application of this? principle to working conditions .in the Preston East Dome mine that the system to be described differs from the standard methods of calculating mine bonus. It was found that the method of paying a fixed price per unit of work done, under the 'contract' system, gave satisfactory results in development, less satisfactory results in timbering, and results which were not satisfactory in stoping. Under the fixed price system, bonus payments, in timbering and stoping particularly, were very erratic and did not necessarily represent fair payment for the work done. A fixed price in development is satisfactory because the work done, and the conditions under which the work is done, are uniform. The drilling and blasting cycle is completed in one shift, the size of heading is con-trolled, and a minimum number of holes are required in order to obtain a satisfactory break. The performance possible under these conditions has been found to be confined to a fairly narrow range. By performance in development is meant the efficiency of the working crew as expressed in terms of the two variables of feet of advance per round and pounds of ex-plosives consumed per foot of advance. A change in rock formation, how-ever, may alter to a marked degree the performance possible, quite independent of the skill and energy of the working crew. The changes in working conditions that affect development performance from the standpoint of bonus calculation are usually easily apparent and are satisfactorily met by establishing several fixed prices.

Jan 1, 1944

By Chuck Crowell

ISO Standards ?Provide Information to Address Commercial and Safety Needs for Standardization: ?Definitions and Terminology ?Test Methods ?Performance Criteria ?Conformity Assessment Process ?Developed by Global Experts ?Promote Global Harmonization

May 1, 2013

By Mark Holdsworth

In 2002, Kennecott Utah Copper Copperton Concentrator installed an Expert Control system for optimization of their SAG and Ball milling circuits. The advanced process control has been well received and is utilized well over 95% of the time. In the years since, many lessons have been learned and many advances have been made. Improvements have produced millions of dollars of benefits and have included directly controlling feedrate with complex logic as opposed to using a bearing pressure controller, modifications to how sound is used for control, modifying logic for maximizing asset utilization and using advanced control for automating equipment restart.

Jan 1, 2012

By Henry Smith, Stu Brown

"The Williams Mine is Canada's largest gold producer, with annual production of some 500 000 ounces of gold from two million tonnes of ore. Highly mechanized and automated underground mining practices are utilized at the property in order to help achieve high levels of productivity and the most cost-effective mining possible.Planning and design parameters for the underground ore handling system at the Williams Mine are described in this paper. Particular reference is made to the considerations that were built into the system to provide maximum operating flexibility through the use of multiple orepass systems, portable low profile jaw crushers, underground conveyors and automated hoisting equipment.IntroductionThe Williams Mine is situated in the Hernlo area of northwestern Ontario, approximately 40 Ian east of the town of Marathon (Fig. I). It is operated by the Williams Operating Corporation, which is owned equally by Teck Corporation and Corona Corporation, and is one of three adjacent properties forming the HernIo gold camp.The mine commenced operation in October 1985 at a nominal production rate of 3000 tpcd. Through an ongoing capital development program, winch was completed in late 1989, the production rate at the property was increased to its current level of 6000 tpcd. This paper describes the mine planning process and the evolution of current mining strategies with particular reference to the underground ore handling system .HistoryGold mineralization was discovered in 1944 in the Hemlo area of Northern Ontario, near the north shore of Lake Superior. A year later, 11 claims were staked over the showing and subsequently patented by the late Dr. Jack Kerr Williams.Over the next 35 years, other claims were subsequently staked, explored and abandoned in the immediate area of the 11 patented claims . In 1980 a predecessor of the Corona Corporation acquired claims adjoining the Williams property to the east. Drilling on this claim group started early in 1981 and intersected the Hemlo orebody in May of that year. In December 1981, Corona Corporation entered into an option agreement with Teck Corporation to explore and develop the property.A drilling program by LAC Minerals on the II patented claims discovered the Williams orebody in March 1982. The mine started production in 1985, pouring its first official bar of gold on December 6 of that year. Corona Corporation was awarded ownership of the Williams Mine conclusively by a decision of the Supreme Court of Canada on August 11, 1989. The court's ruling ended a legal dispute with LAC Minerals over the property initiated eight years earlier."

Jan 1, 1991

By Rodney Allen

Background: Development of the Project ?European GEODE collaboration 1999: considers possible projects, including a VMS project, to continue after GEODE ?GEODE-CODES-Canada collaboration 1999: Questionaire, database ?Workshop at CODES 2000: project theme and strategy selected ?GEORANGE (Sweden-EU) 2001 supports development of Global VMS Project: interest from 12 nations ?Skellefte VMS Project set up as Sweden?s component of Global VMS, 2002; other projects in Spain, Canada collaborate ?Low metal prices ---> little funding from mining industry 2001-2003, change in strategy ?IGCP/UNESCO support 2004: enlargement to over 20 nations

Apr 1, 2005

By L. E. Reed, I. G. L. Sinclair

An exploration program seeking kimberlite pipes, the common primary hosts for diamonds, Was' conducted during the years 1979 through 1982 in the James Bay Lowlands of Ontario by Selco Mining Corporation (now the Mining Division of BP Resources Canada) and Esso Minerals Canada. The area to be explored was selected on the basis of its regional geological setting, and because of the known presence of kimberlite indicator minerals in the region. The primary exploration technique was low level airborne magnetic surveying, followed by detailed ground geophysics. This work located many pipe-like bodies, with diameters of a few hundred metres, as well as several dykes. Targets located by these geophysical methods were drilled, intersecting a total of45 intrusions, consisting of34 alkaline diatremes containing tuffisitic breccias, 7 carbonatites, and 4 massive alnoites. K-Ar determinations indicated ages of 152 Ma and 180 Ma for two of the massive alnoites. The texture and general mineralogy of the tuffisitic breccias are similar to those of diatreme facies kimberlites, but detailed examination of their mineralogy and chemistry demonstrated that they lie within the alnoitic rather than the kimberlitic compositional field. Although the exploration program did not lead to the discovery of true kimberlites, it did demonstrate the presence of a large, previously unknown province of alkaline volcanic activity, which has no surface expression.

Jan 1, 1991

By B. G. Cousins, B. O’Rourke, C. Spence

"Some non-flotation chemicals are added to flotation circuits directly and indirectly to control issues such as scaling and dust in other areas of the operations. Since dosage levels are generally not high, a standard laboratory float test may not be able to determine the effect of a specific chemical on the productivity of the flotation circuit. This paper presents a laboratory testing protocol that uses kinetic float studies to test the effect of normal to extreme doses of antiscalant and dust chemistries (5–100 g/t). Results indicate that this protocol helps to predict potential interference by a particular chemistry on the flotation circuit.RÉSUMÉ Certains produits chimiques ne servant pas à la flottation sont ajoutés directement et indirectement aux circuits de flottation afin de contrôler des problèmes tels que l’entartage et la poussière dans d’autres secteurs des opérations. Étant donné que les niveaux de dosage sont généralement faibles, un essai standard de flottation en laboratoire pourrait ne pas être en mesure de déterminer l’effet d’un produit chimique spécifique sur la productivité du circuit de flottation. Le présent article définit une procédure d’essai en laboratoire qui utilise des études cinétiques de flottation pour vérifier l’effet de doses normales à extrêmes de produits chimiques antitartre et anti-poussière (5 à 100 g/t). Les résultats indiquent que ce protocole aide à prédire l’interférence potentielle d’un produit chimique particulier sur le circuit de flottation."

Jan 1, 2016

By J. A. Finch

"This paper describes major technical developments in rod mill design and operating practice since its introduction into the North American minerals industry over fifty years ago. The basic operating characteristics of the wet, overflow rod mill are described, and significant operating variables are reviewed in terms of their effects on mill power draw, power efficiency, and practical aspects of circuit operation. Key factors for improving the economic performance of rod milling circuits are identified. IntroductionThis paper summarizes the findings of a detailed review of available technical information on the operation of rod mills. One of the basic problems in historical comminution testwork has been the lack of a standard measure of circuit performance. The Bond Operating Work Index, not introduced until after 1950, has proven of immeasurable value in this regard, but first has to be carefully considered in terms of its utility and limitations. Its prescribed use is described in a later section of this paper.During this review, it became apparent that rod mill performance is generally not well understood. Because of combined interactions, the effects of different operating variables may be difficult to assess, and even at times appear erratic. It is obviously difficult to rationalize plant testwork or circuit adjustments when the results are highly unpredictable. The purposes of this review, therefore, were:a) to establish what basic facts have been learned about rod mill performance;b) to define some genera l guidelines for efficient rod mill design and operation; and,c) to establish a basis for specific recommendations for plant tests or adjustments with minimum risk, and maximum potential for circuit performance improvement."

Jan 1, 1986

By P. Hanniala, S. Harkki, B. Andersson

"The Outokumpu Flash Smelting Process was put into commercial operation in 1949. The original process was based on the use of preheated air. The adoption of oxygen enrichment of the flash smelting process air in 1971 was a crucial improvement, especially for smelter capacity. Oxygen use according to the Outokumpu method means selection of the most suitable oxygen content for the process air on the basis of the concentrate composition, capacity and matte grade. The furnace is not bound to only one fixed degree of process air oxygen enrichment; the oxygen content may vary from 21% to 100%.The degree of oxygen enrichment and the matte grade are the most important process parameters in reducing the operating costs of the whole system, including smelting, converting and acid production. Raising the matte grade allows more efficient use of the reaction heat in the smelting stage. Sulphur is recovered in a high-strength, constant-flow gas stream. The blowing time in the converters is reduced considerably.Oxygen enrichment and high matte grade improve the energy efficiency of the plant complex as long as the surplus heat from the system is not wasted. When the operating costs and investment expenditure of the total plant complex are taken into account, a reasonably high degree of oxygen enrichment (35-80°/0) is the best alternative in practice. Existing operating smelters have achieved single-stream thoughputs of over one million t/yr of concentrates.HistoryLocal capital and operating costs as well as lower energy consumption per unit of metal produced are now the crucial factors in determining the choice of process. In the late I940s, the same reasons prompted Outokumpu to develop the original flash smelting process in Finland. Between 1900 and 1940, very few technical changes in pyrometallurgical copper production took place. However, the commercial use of the flash smelting technique began a new era in metal extraction from sulphide concentrates. The characteristic feature of the method is that the concentrate is smelted in suspension: this offers the most favourable conditions for heat and mass transfer, and thus high reaction velocities. Outokumpu was the first to exploit the known advantages of flash smelting in a commercial installation at Harjavalta in 1949."

Jan 1, 1982