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By H. Kolcz, G. S. Dobby, R. Stratton-Crawley, S. W. Wilson

"The Matte Separation plant at Inco's Copper Cliff Smelter Complex is described. The continuing implementation of flotation column technology in the flowsheet in various applications is reviewed. Comparative studies on 0.038, 0.10, 1.1 and 1.8 m diameter columns have been carried out. It was demonstrated that consistent metallurgical performance was obtained with both pilot- and plant-scale units. Grade-recovery relationships for plant columns can be predicted with confidence from data obtained from test equipment. The work indicates further areas of the flowsheet in which columns present an attractive alternative to conventional cells. INCO’s MATTE SEPARATION PROCESSNickel concentrate from Inco’s Sudbury area mills has been processed in the Copper Cliff smelter for sixty years. Prior to that, Sudbury ores had been smelted directly. Historically, copper-nickel separation from smelter converter matte was achieved by the classical Orford process. In the mid-1940s Inco developed an improved separation scheme based on mineral processing methods, the Matte Separation Process. A generalized Copper Cliff Smelter Complex flowsheet is shown in Figure 1.Iron sulfide and gangue contained in the nickel concentrate are rejected in the smelting-converting process. The molten product, typically containing 50% Ni, 25% CU and 22% s, is cast at about 1000 ºC, into floor moulds and allowed to slowly cool for four days. During this period nickel sulfide (heazlewoodite, Ni,S,), copper sulfide (chalcocite, cu,S) and a copper-nickel metallic alloy precipitate and form a coarse grain structure that is amenable to separation by physical means. The phase chemistry of this system has been described previously by Sproule et al (1). This matte then becomes the feed to the Matte Separation Process.A simplified block flowsheet of the Matte Separation Process is shown in Figure 2. Matte ingots, typically weighing 20 tonnes each, are broken and crushed in a three stage crushing plant to approximately minus 0.01 m and conveyed to the Matte Separation building. Grinding is carried out in two parallel circuits each consisting of a rod and ball mill in series producing a flotation feed which is 65% minus 44 microns. Typical throughput of each grinding circuit is 650 tonnes/day. The metallic fraction of the feed is recovered by magnetic separation. This product, containing about 66% Ni and 15% CU, is a major component of the feed to the Copper Cliff Nickel Refinery."

Jan 1, 1990

By Y. H. Hatzor

"This is an extended abstract for a keynote lecture delivered by the author during the 2015 ISRM congress in Montreal on the application of the numerical discontinuous deformation analysis (DDA) method in rock mechanics practice. Due to the large scope of the topic this lecture will focus on studies performed by the rock mechanics group at Ben-Gurion University, alone or in collaboration which other research groups, and is not intended to provide a comprehensive review of everything that has been done on the subject worldwide during the past two decades. A forthcoming textbook (Hatzor et al., in preparation) will attempt to provide such comprehensive coverage.DDA has been developed by Dr. Gen-hua Shi while he was doing his PhD studies under the supervision of Professor R. E. Goodman at U. C. Berkeley (Shi, 1988). Dr. Shi has invented a new numerical discrete element method which provides a solution for dynamic deformation of block systems, hence its applicability to rock mechanics practice. The method is similar in essence to the finite element method in its implicit formulation of the time integration scheme and where in every time step the minimum potential energy of the entire system is sought, but here every element is a finite block with six degrees of freedom. The blocks are assumed to be stiff (simply deformable) so that most of the energy is consumed by slip along pre-existing discontinuities, the frictional resistance of which is assumed to obey the Coulomb-Mohr failure criterion for rock joints. The greatest advantage of DDA over alternative numerical discrete element methods is its robust area (volume) integration which ensures great accuracy even when the blocks are of irregular shapes, including non-convex blocks which may contain holes. The greatest disadvantage is the necessity to solve in every time step very large matrices of unknowns, imposing great CPU demand when the block system involves a large number of blocks. Another disadvantage is the sensitivity of the solution to the choice of the penalty parameter which is implemented in DDA in the form of stiff springs that are attached to contacts once detected automatically.The inherently dynamic formulation of the DDA method lends itself to solution of dynamic problems in rock mechanics. Dynamic analysis with DDA can be performed in different ways corresponding to different rock mechanics problems and loading conditions. Three main classes of loading conditions which are relevant to rock mechanics applications are discussed here: 1) dynamic loading of a single bock which rests on a stationary foundation, 2) response of a block to dynamic loading of the foundations, 3) wave propagation through a block system.The most common approach is to introduce the dynamic force to a specific block in an otherwise fixed block system and check the resulting deformation, typically the time dependent displacement or rotation of the loaded block. This approach is particularly useful for dynamic rock slope stability studies when a stability of a specific rock block against earthquake vibrations is in question. The first 2D-DDA benchmark test of this approach was performed by Hatzor and Feintuch (2001) who introduced harmonic acceleration functions into a block which rests on an inclined plane. The analytical solution proposed for this problem by Hatzor and Feintuch (2001) was later generalized by Kamai and Hatzor (2008). The first 3D-DDA benchmarking for this approach was presented by Bakun-Mazor et al. (2012) who studied single and double face sliding of blocks which rest on stationary foundations and subjected to harmonic input acceleration functions."

Jan 1, 2015

By Nitin Bhavsar, Kaushik Vakil, Lakshmikanth Reddy, Sanjay Sarkar, Tathavadkar. Vilas, Bhavin Desai, Raghavendra Adiga

Gold and platinum group metals (PGM) do not dissolve in sulfate electrolyte from anode during electro-refining of primary copper. The PGM form solid ‘slimes’ which accumulates at bottom of the electrolytic cell. Typically, 8 to 10 ppm silver is present in copper cathodes, which is equivalent to almost 2% of silver loss during electro-refining. The silver can be cemented with cathode copper as soon as it is dissolved into the electrolyte from anode or during entrapment of slime particles in cathode. Over a period of time, the concentrates grade has deteriorated and change in type & amount of impurities in concentrate has resulted in higher silver loss during refining process. Therefore, an in-depth investigation was carried out in both fire- and electro-refining processes to understand the root causes of higher silver loss in copper cathodes. The detailed characterization and the plant data analysis were carried out. The results of study revealed that higher silver loss in 3rd crop cathodes as compared to 1st and 2nd crop cathodes from same anode. In anode silver was present in two forms, dissolved in copper (solid solution) and in slime phases such as Cu2-xAgxSeTe. SEM-EDX study of anode cross section confirmed higher silver and oxygen content in central region (core) of anode as compared that in both air and mold sides. This is due to non-uniform cooling of anode which was confirmed by the solidification modeling. Higher concentration of oxygen & silver at core of anode rised Ag+ concentration in electrolyte and slime particles during 3rd crop. The results of study were used to optimize the anode cooling process and also electrolyte chemistry to reduce the silver loss. The details of study carried out are discussed in this paper using the results of modeling, characterization and experimental studies. INTRODUCTION In the electrolytic refining of copper, fire refined copper anodes are used as raw material. Anodes contains copper of the range 99.5 to 99.6%, rest being the impurities. Hence, the purpose of the refining is (1) to remove the impurities so that final cathode conforms to the LME specifications and also (2) to recover the precious metal from the anode copper. When anode is dissolved, most of the impurities reports to the anode slime settled at the bottom of the cell, and rest dissolves in the electrolyte. Dissolved impurities remains in electrolyte and are removed during electrolyte recycling. However, sometime dissolved impurities and slime particles get entrapped in cathode due to disturbances in operational conditions. Metals dissolving in the electrolyte are the elements such as Ni, Co, Fe, Zn. The electrode potential of As, Sb and Bi being close to that of copper, these elements partly dissolve in the electrolyte. Noble metals like Ag, Au, Pt and Pd are generally insoluble and are thus expected to report to the anode slime. A small amount of the sliver content from the anode is dissolved in the electrolyte. Because the dissolved silver electroplates on the cathode at a smaller applied potential than copper, the cathode typically contains up to 8 ppm of silver. This is referred to as ‘silver loss’ in cathode (Cooper, 1987). Fortunately, silver is a rather benign impurity in copper due to its electrical conductivity being higher than copper. However, higher silver loss in cathode is loss of revenue for Copper smelter due to significant difference in their LME price.

Jan 1, 2019

By Denni Nikols

"Planning for coal beneficiation in the electric utility industry is relatively complex, involving the coordination of experts and specialists in a broad range of fields, as well as compliance with a wide variety of government regulations.This paper examines the role of the planner, reviews possible benefits of coal beneficiation, identifies potential problems and illustrates a typical planning schedule.The steps involved in the planning process are:Step I-Bench- and pilot- washability studyStep 2- Wash plant designStep 3- Power plant and boiler designStep 4-Mine designStep 5-Major environmental and technical problems to address.IntroductionElectrical utilities and coal have a long and intimate relationship . Cleaned coal is becoming an increasingly popular fuel with the utilities for a variety of reasons. Generally, the greatest impetus to burn a cleaned or prepared coal fuel comes from the need to control airborne pollutants.Long-range planning is a standard practice for electric utilities, forecasts of demand must be made well into the future. Since the lead time required to provide new facilities is often as long as 10 years and the cost very high , planning becomes an important task.For a utility that owns and directs the operation of its coal mines, the mine planning or fuel acquisition planning takes on the magnitude of other corporate planning functions. It is from this perspective that a utility would view coal preparation. Except for the interaction of a coal-fi red plant on the actual mine design the planning considerations o f a beneficiating facility for a captive mine or a contract raw coal supply are about the same. Because TransAlta Utilities is currently supplied from captive mines, this discussion will tend to focus in that direction.It is the role of a planner to plan. This is easy to say but it is not always easy to do. Often we are working within a context that resembles the geological time scale. Frequently the objectives are not clearly defined when we begin and ultimately our plans are tested in the waters of government regulations and cost benefit analyses .Planning for beneficiation of Plains coal, or any coal, provides just such a test. The planner's role in this endeavour requires a wide vision. While parts of the process may be amenable to classical methods of project scheduling, the broad range of subjects and interaction of seemingly unrelated tasks is sure to obscure some of the considerations that must be made. Therefore, the planner's chief role is coordinating the work of many experts and specialists toward the final objective.Among the specialists are combustion , geo technical, mining, civil , and mineral processing engineers , geologists, hydrogeologists, soil, and reclamation experts to list a few.When one considers coal beneficiation, the planning part o f that consideration is probably more complex than any other single engineering function. Due to the company's location in the Alberta Plains and the proximity o f the mine to the thermal generating station, this paper will tend to emphasize that situation.Beneficiation may offer some advantages over run-of-mine coal to the power plant opeator. Some of these advantages are: removal of a contaminant, power plant efficiency gains , lower plant capital costs (for new plants), possible lower mining costs."

Jan 1, 1984

By Chuan-Jian Zhong

Gold-based nanoparticles in the size range of a few nm have attracted increasing interests in catalysis, sensors and biomedical applications. The study of the unique catalytic properties of nanosized gold was inspired by the pioneering work of Haruta on the nanogold-catalyzed CO oxidation (1-4). There have been a number of excellent reports discussing both fundamental and application aspects of gold nanoparticles in catalysis (3-8). Our work reported herein is aimed at investigating the preparation and application of gold and its alloy nanoparticles for potential applications in fuel cell catalysis. Fuel cells operating by electrochemical oxidation of hydrogen or methanol fuels at the anode and reduction of oxygen at the cathode are attractive power sources due to their high conversion efficiencies, low pollution, lightweight and high power density. While methanol offers the advantage of easy storage and transportation in comparison with hydrogen fuel cell, its energy density (~2000 Wh/kg) and operating cell voltage (0.4 V) are much lower than the theoretical energy density (~6000 Wh/kg) and the thermodynamic potential (~1.2 V). The poor activity of the anode catalysts and inefficient activity or issue related to "methanol cross-over" at the cathode electrode are associated with the loss of about one-third of the available energy at the cathode and the other one-third at the anode. Extensive studies have been focused on Pt-group metals (Pt+Pd+Rh+Ru+Ir (PGM)) for both anode and cathode catalysts. A major problem is the poisoning of Pt by COlike intermediate species (9,10). Recently, oxide-supported gold nanoparticles in the <10 nm size range have emerged as one of the best catalysts for CO oxidation (1-3,11), and for water gas shift reaction in reforming stage using 5 nm Au on Fe2O3 (6). Gold and its alloy with other metals in the nanosize range present new alternatives (2,12). Whether the unique properties of gold nanoparticles can be exploited for addressing these problems is a focus area of our work. The ability to harness the large surface area-to-volume ratios and the unique surface sites of nanoparticles in <10 nm size range, especially in heterogeneous catalysis, constitutes a major driving force in fundamental research and practical applications of nanoparticle catalysts. It is this size range over which the metal particles undergo a transition from atomic to metallic properties. The understanding of factors controlling the morphological and surface reconstitution associated with such a size range is of fundamental importance to the ultimate exploration of nanostructured catalysts. We have been investigating the interfacial structures and properties of core-shell types of nanoparticles consisting of gold or alloy nanocrystal cores and organic monolayer shells that were prepared by twophase synthesis (13) and processing (14) protocols. Important attributes of such nanoparticles include controllable size monodispersity, processibility, and stability towards size- and composition-tunable catalysis (15-21). Some of these attributes were studied for understanding their electrocatalytic properties in the oxidation of methanol and reduction of oxygen, which are of fundamental interest to fuel cell technology.

Oct 1, 2003

By C. A. Young, H-H. Huang, L. G. Twidwell

Solid particles, especially oxides/hydroxides, develop an electrical charge on their surface when submerged in aqueous solution. Parks was able to relate PZC (point of zero charge) of an oxide to its minimum solubility and isoelectric point. Dzombak has compiled an extensive database for adsorption reactions on ferrihydrite surfaces using the double layer theory. The equilibrium calculational program, STABCAL has been used to extend the considerations of Parks and Stumm. The PZC for many hydroxides, complex oxides, and non-oxides have been investigated and the results are reported in the literature. Removal of arsenic and metals by adsorption on ferrihydrite as the substrate has been computed using ST ABCAL and the computational results are compared to experimental data. Absorbents other than ferrihydrite such as aluminum hydroxide are also discussed.

Jan 1, 2005

The rate of liquid copper deoxidation during top blowing of reducing flames has been investigated using a high capacity thermogravimetric unit at 1200 °C. For 1 kg copper samples, it was observed that the rate of deoxidation was proportional to the flow rate of the reducing reagent (H2 or CO). Under similar experimental conditions, it was found that H2 is more effective than CO even though both have similar thermodynamic potential to deoxidize liquid copper. The rate of deoxidation of liquid copper with reducing 0 2/CH4 flames was measured for 0 2/CH4 molar ratios of 1.5 to 2. The deoxidation rate depends on the 0 2/CH4 ratio and decreases as it approaches the stoichiometric ratio (02/CH4 = 2). Estimation of the rate of deoxidation of liquid copper with top blowing flames based on the thermodynamic composition ofH2 and CO in the product gases, agrees well with measured values.

Jan 1, 2007

By S. M. C. Santos

Preliminary bench-scale studies were carried out on the leaching of a zinc sulphide concentrate from Somincor, Portugal, and the purification of the resulting pregnant solution using solvent extraction techniques. The sulphide concentrate contained 36% Zn, 36% S, 2% Fe and 4% Cu. The leaching was carried out with sulphuric acid in the presence of ferric sulphate as the oxidant. Important leaching parameters, such as the effect of reaction time, the solid-liquid ratio, temperature and concentrations of acid and oxidant, were investigated. After leaching, the recovered solution was contacted with an organic phase containing Acorga 5640 to remove the copper. Subsequently, the removal of iron from the leaching solution was achieved with a mixture of Cyanex 272 and TBP. This solvent mixture was relatively selective for iron over zinc. The stripping of the loaded solvent was performed with 200 g/L H2SO4. Six countercurrent extraction stages achieved a separation of about 99% of the iron from the leaching solution. The iron-free leachate can be further treated to recover minor metals by cementation, and finally, zinc by liquid-liquid extraction. The advantages of the suggested process relative to the traditional jarosite process are discussed.

Jan 1, 2006

By G. Song

Magnesium has excellent bio-compatibility in terms of its density, strength, elastic modulus and toxicity. However, due to its poor corrosion performance, so far magnesium has not been successfully used in the human body as a permanent implant material. Nevertheless, there is a possibility to utilize the low corrosion resistance of magnesium to make magnesium into a temporary implant component that can gradually dissolve in the human body after surgical region heals. This will avoid the secondary operation to remove the temporarily implanted component and the chronic inflammatory discomfort caused by the implant. This paper is aimed at exploring the possibility of using magnesium as a degradable bio-material through investigating the corrosion behaviors of pure magnesium and surface treated magnesium in a simulated body fluid (SBF) solution. It was found that magnesium corroded rapidly in the SBF solution, resulting in vigorous hydrogen evolution and a strong alkalization effect. Hence, it is impractical to use magnesium as a permanent implanted material or even a degradable implant. However, a proper anodizing treatment can significantly improve the corrosion resistance of magnesium, and hence slower down the hydrogen evolution and alkalization processes, which will allow to control the corrosion or degradation of magnesium at a desired rate in the human body. With a controllable corrosion rate, it is believed that magnesium as a degradable implanted material will be eventually achievable.

Jan 1, 2006

By S. G. Shabestari

In the metal casting industry an improvement of component quality mainly depends on better control over the production parameters. Thus, thermal analysis cooling curve of the alloy is used for process control in aluminum casting industry. Cooling rates of the alloy during solidification process affect microstructure, grain size, eutectic silicon morphology, and dendrite arm spacing (DAS). In this research, effect of cooling rate on the microstructure and solidification parameters of 319 aluminum alloy that is a widely used alloy in automotive industry, has been investigated by means of thermal analysis. Seven different cooling rates have been obtained by using CO2-bonded silica sand molds with two different wall thicknesses, hot-work tool steel molds (H13) with and without coating, thin-wall steel molds with different coatings. In each case, cooling curve and first derivative cooling curve have been plotted by use of very accurate thermal analysis equipment. Effect of different cooling rates on solidification parameters e.g. Nucleation temperature (TN,a), nucleation undercooling (ATN,a), recalescence temperature (TR,a), solidification range (AT,s), and total solidification time (t 0 have been studied in the liquidus region. Microstructural evaluation has been carried out and DAS were measured in all solidification conditions. A numerical equation was proposed to predict cooling rates via measuring DAS in 319 aluminum alloy. Nucleation process and the effect of cooling rate have been interpreted by using thermal analysis cooling curves and microstructural study.

Jan 1, 2004

By J. Dilbeck, J. K. Ratliff, T. Petrov, Z. Brown

"In efforts to improve dust control during deep cut continuous mining a supplemental atomizing spray system, mounted on 14CM15 continuous miner, has been designed and successfully implemented in a U.S. coal mine. The mine is 2.1 m (7-ft) high and uses a blowing curtain face ventilation system with 1.1 m (3.5-ft) curtain offset from the rib. The face ventilation design parameters were set to 9.4 m3/s (20,000-cfm); 4.2 m3/s (9,000-cfm) line curtain flow rate, and 3.8 m3/s (8,000-cfm) scrubber capacity. The performed in-mine measurements, before and after the implementation of the atomizing spray system, showed a significant decrease in the respirable dust levels at the operator place as well as at the return. The paper describes the supplemental water spray system design and performance supported by three-dimensional computational fluid dynamics (CFD) simulations and in-mine test data.INTRODUCTIONThe work on this project have started in 2015 with a study of the conventionally applied face ventilation layouts. The specific behaviour of the face ventilation system have been analyzed trough in-mine measurements and computer modeling of typical cut scenarios. An computer modeling methodology have been developed for estimation the respirable dust concentration (RDC) using tracer gas to RDC contour mapping, calibrated by a single point value, provided by in-mine measurement. Utilizing the results of this study the engineering staff of the mine designed and implemented a supplemental atomizing spray system to improve the dust control during the deep cut continuous mining. Today the atomized spray system is successfully applied demonstrating steady performance and a significant decrease in respirable dust concentration on the working places of the continuous miner (CM) and coal transporters (CT) operators as well as at the return air stream. Information about the applied type of spray nozzles provided by other researchers (Cheng, 1973; Dick et al., 1996; Organiscak & Page, 1998; Pollock & Organiscak, 2007) and spray system manufacturers (Spraying System Co, 2011–2018; Steinen Mfg., 2016) have been used in this project. CFD code and simulation approach validated in a study conducted in 2000-2014 have been applied (Turner et al., 2002; Wala et al., 2004, 2007; Petrov, 2014)."

Jan 1, 2019

Flotation works very well for particles that are typically in the range 20 to 150 µmin diameter, for base metal ores. In this range, it is possible to get quite high recoveries in conventional flotation machines. Outside this range, the recoveries decline progressively, whether it be with the very fine or the coarse end of the size spectrum. In this paper, the reasons for the drop-off in recovery are briefly reviewed, together with strategies for future work. Recent progress in the author&apos;s laboratory will be described. These include the Concorde Cell, which takes advantage of the high dissipation rates in the shock wave created when a gas-liquid mixture reaches supersonic velocities. The environment thus created is very beneficial for the flotation of ultrafines. For coarse particles, the reasons for the drop-off in recovery can be related to the highly turbulent nature of the pulp in a conventional flotation cell. To improve recovery, it is necessary to find a way of bringing particles and bubbles into contact in a quiescent environment. A new process for coarse particle flotation will be described, in which a fluidized bed is created in the flotation cell. The flow conditions are very gentle, and the high solids concentration leads to rapid rates of capture of the particles. Experimental results are presented. It is apparent that the maximum floatable size for coal and minerals can be increased by a factor often over the limits found in current practice. Advances

Jan 1, 2009

By P. A. Bahri, D. G. Dixon, T. M. Woodward

A comprehensive mathematical model of the Sherritt-Gordon ammoniacal pressure leaching process at K winana Nickel Refinery has been constructed. The process is comprised of six autoclaves functioning as a three-stage leach circuit, operating over the temperature and pressure ranges of 85-95°C and 750-1000 kPa, respectively. The process chemistry forms a complex series-parallel reaction network, characterised by: (1) the gas-liquid mass transfer and reduction of oxygen, (2) the oxidation of eight distinct minerals, (3) the oxidation of sulphur, and successive reactions involving various intermediately oxidised sulphur species, and (4) the oxidation of Fe(II) to Fe(III), and subsequent precipitation as a hydrated ferric oxide. Material balances were developed for species in all three phases, and an energy balance to account for all reactions and phase conversions. The multiple convolution integral (MCI) statistical reactor model was employed for the scale-up of particle kinetics. The model has been validated against plant data, and simulation results are in agreement with plant performance.

Jan 1, 2005

By P. Cleyle, J. H. Masliyah, R. S. Chow, Z. H. Xu, Z. A. Zhou

Bubble nucleation in water under dynamic conditions was investigated using an autoclave at an air saturation pressure of 7 atm. Agitation during air saturation of water was found to be crucial in enhancing tiny bubble formation. More bubbles nucleated on hydrophobic surfaces at a higher agitation rate, due to cavity formation by the more intense hydrodynamic conditions. Flotation recovery of bitumen from oil sands demonstrated a significant role of bubbles nucleated in water: more than 50-170% increase in bitumen recovery from different oil sands was obtained by using air supersaturated than the regular water.

Jan 1, 2009

By S. Kelebek, E. Yalcin

"Diethylenetriamine (DETA) and/or triethylenetetramine (TETA) are reagents that can generally be categorized under ""flotation modifiers"". These polyamines are known to be effective for the deactivation/depression of pyrrhotite that is present in Canadian nickel-copper sulphide ores in large quantities. Recent bench scale testing on some of these complex ores indicated that chalcopyrite flotation can also be adversely affected under certain conditions involving polyamines, which may be taken to be an evidence of their specific affinity towards chalcopyrite. In general, DETA shows no significant depressant action on chalcopyrite while TETA&apos;s promotion of hydrophilicity for this mineral has been observed even in the presence of xanthate. This prompted an investigation on thermodynamic equilibria involving these polyamines and copper ions. Results serve a useful purpose to identify conditions for deactivation phenomena. CuDETA2+ and CuTETA2+ chelates as products of sequestration have large predominance areas covering a wide range of redox and pH conditions, where copper xanthate species are not stable, especially in the presence of TETA."

Jan 1, 2009

By Du Xinfeng

The resource quantity of the low rank coalbed methane (CBM) accounts for 47% of the total resource quantity of CBM in China. Compared with the exploration and development of the high rank CBM in Qinshui Basin, China and the low rank CBM in Powder River Basin, USA and Albert Basin, Canada, the exploration and development of the low rank CBM are still in the initial test stage. In this paper, on the basis of analyzing the mining geological conditions such as that the Huanglong Jurassic Coalfield is largely situated in the hills and gullies zones, and the coal reservoir has the features such as the low metamorphic degree, large coal seam thickness, simple coal matrix texture, high permeability and small CBM content and so on, it discusses the key technologies such as the development pattern of CBM, well location arrangement, drilling and well completion technology and fracturing technology and so on. It indicates that the underbalanced drilling and the cavity well completion based on the reservoir protection will be the development directions of the CBM development technology in this area.

Aug 1, 2013

By A. J. McLaren

Introduction Gold holds an important place among the mineral products of Manitoba. In value, it ranks second only to copper, which in 1931 attained first place. The gold production increased from 23,189 fine ounces in 1930 to 102,969fine ounces in 1931. The production for 1930, worth $479,359, came almost entirely from the Central Manitoba mine. The production for 1931 was worth $2,128,558, of which $1,509,018 came from the Flin Flon mine, $528,951 from the Central Manitoba, and $83,497 from the Sherritt Gordon. The Gem Lake mine and some prospects produced $7,785. The total output of gold in Manitoba, from the first recorded production in 1917 to the end of 1931, is estimated at 178,669 fine ounces, valued at $3,693,332. The production for 1932 promises to reach a new high record, due chiefly to the stepping-up of tonnage at the Flin Flon plants and the coming into production of the San Antonio mill in May. History The Manitoba Act, constituting Manitoba a Province of the Dominion, was passed in 1870 and provided for the vesting in the Crown of all un-granted or waste lands of Manitoba, as well as for the administration of these lands by the Dominion of Canada for the purposes of the Dominion "subject to, and except and so far as the same may be affected by, the conditions and stipulations contained in the agreement for the surrender of Rupert&apos;s Land by the Hudson&apos;s Bay Company to the Crown". Included in these waste lands were large areas later prospected and staked out as mineral lands. Up to the year 1912, that vast territory extending from the 12th base line to the 60th parallel of latitude, and from the Saskatchewan boundary to Hudson bay, was part of the District of Keewatin. Although added to Manitoba in 1912, the administration of its mineral lands also remained vested in the Dominion, so that all mineral lands within the Province upon which deposits of gold ore have been found were disposed of and administered by the Mineral Lands Division, Department of the Interior, until the transfer of the natural resources to the Province of Manitoba, on July 15th, 1930.

Jan 1, 1932

By Christopher Andreae

Years before iron and steel works were established at Sydney, several thriving although short-lived iron works operated in Nova Scotia. These furnaces reflected the general nineteenth-century North American experience with iron works. At the beginning of the century, small furnaces struggled to supply local needs. Charcoal was the principal fuel and water powered most furnace equipment. By the end of the century, a few huge primary iron and steel works dominated production for Nova Scotia and the rest of Canada. Two sites achieved prominence in the nineteenthcentury Nova Scotia iron industry: Londonderry and Ferrona (Fig. 1). Londonderry, the larger and longerlasting of the two sites, is today a small village on the south flank of the Cobequid Mountains, about 30 km west of Truro. Prior to the establishment of an iron works in 1849, no community existed. At the peak of operation in the 1880s, however, over 2600 people were located there. The second site, Ferrona, today is a mere crossroads on the map, about 10 km south of New Glasgow. Following the construction of a blast furnace there in 1892, a small village grew up around the furnace. But once the furnace was blown out in 1904, the population gradually drifted away.

Jan 1, 1999

By A. L. Valdivieso

"The correlation obtained by plotting pH of maximum adsorption of dextrin versus the isoelectric point of involved metal hydroxides can be used to predict the depressing effect of dextrin on flotation in ""pure"" sulfide mineral systems. Sulfides are strongly depressed by dextrin whenever their surfaces are coated by the corresponding metal hydroxide. The efficiency of dextrin as a depressant is affected by the adsorption of the sulfhydryl collector. Hydrolyzable cations modify this relationship in flotation of sulfide ores. This type of deviation of the real-life systems from the predictions based on the behavior of the pure systems shows the possible ways that could be followed to further improve the obtained correlations. Advances in Mineral Processing Science and Technology Proceedings of the 48th Annual Conference of Metallurgists ofCIM Sudbury, Ontario, Canada Edited by"

Jan 1, 2009

By A. R. Naji Meidani, A. Cameron, A. Richardson, M. Isac, R. I. L. Guthrie

The supersonic core of shrouded jets remain coherent over longer distances vs conventional supersonic jets. This phenomenon should allow for greater penetration of oxygen into slag/steel reactor systems. As such, they hold the promise for faster slag/metal mixing in BOF type metallurgical reactor systems, possibly creating greater surface area/volume ratios of reacting phases, and thereby faster kinetics, as compared to conventional supersonic jet systems. In order to assess the potential of shrouded supersonic jets versus their conventional counterparts, an experimental investigation of impinging shrouded supersonic jets into a water model of a simplified BOF system was carried out in the MMPC&apos;s water modelling laboratory. The experimental results for three different designs of a shrouded supersonic jet nozzle have been compared in terms of greater penetration depths and reduced mixing times. Based on a novel dimensional analysis, the depth of penetration of a gas jet into a liquid bath is shown to depend on the nozzle-bath distance, the liquid&apos;s Froude, Reynolds and Weber numbers, reflecting the ratios of gravity, viscous and surface tension forces to the jet&apos;s inertial, or momentum, forces. Good agreement between the mathematical model and experiment was obtained in terms of predicted and observed depths of penetration. Further efforts have been made to study jet penetration into liquid metals. The effects of mean liquid density of slag/metal mixtures and a wide range of gas flow rates on the penetration depth were investigated theoretically. The results show that the penetration depth can be increased with increasing gas flow rate and decreased bath density.

Jan 1, 2004