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By 0. H. ESCHHOZ

HARMON F. FISHER,* New York, N. Y. Mr. Eschholz discusses the particular case of large precipitators installed in connection with large metallurgical operations, and receiving their high-potential energy through the conversion of alternating current to direct current by means of the mechanical rectifier. He classifies these mechanical rectifier installations, according to source of power, as follows: System A.-Applications utilizing individual alternating-current generators, either single-phase or polyphase, installed exclusively for furnishing energy to one or more transformer-rectifier-precipitator units. System. B.-Applications having no special alternating-current generators, but utilizing the existing alternating-current industrial or lighting mains to supply the energy to one or more transformer-rectifier-precipitator units. System C.-Applications receiving their energy from high-tension power circuits supplied directly to potential regulator-rectifier-precipitator units. I do not intend here to enter upon a detailed technical discussion of the foregoing classes, which would really interest only the manufacturers of electrical apparatus and the electrical engineers. A brief general discussion follows:

Jan 11, 1918

By William P. Dyrenforth

The principle of electrostatic separation is discussed and elaborated on by dividing into the three main mechanisms of electrification as applied to separation of solid substances, i.e., (1) contact electrification, (2) electrification by conductive induction, (3) electrification by ion bombardment. Types of equipment used for electrostatic processing are described and the effects of humidity mentioned. Processing of iron ore, titanium minerals, rare earths and cassiterite is discussed and some existing plants are described.

Jan 1, 1978

By H. A. Wentworth

THE Huff electrostatic plant of the United States Smelting Company operated in conjunction with its wet concentrator at Midvale, Utah, was the second plant of substantial size installed using the Huff process, and the first plant to be put in operation on the so-called Western complex ores. In spite of the machinery being of early design and consequently embracing many of the mechanical weaknesses incident to a pioneer plant the mill has operated steadily and uniformly since the summer of 1909, about five years now, without any material change other than some re-arrangement of the machinery for better handling of the sizes. The ore, at present coming almost entirely. from the company's mines in Bingham, is of practically the same composition as that upon which the plant was first put in operation. The crude ore, consisting of the sulphides of copper, lead, zinc, and iron, and containing small amounts of gold and silver, is brought by train and delivered to the hoppers of the wet concentrator, where by jig and table treatment, there are produced a shipping lead concentrate, a tailing and a middling product, the latter being conveyed in push cars to the adjoining electrostatic mill. The crude ore delivered to the wet concentrator contains from 6 to 9.5 per cent. zinc. At times the plant is used also for the treatment of custom ores from the Bingham district and elsewhere, and at such times the results of the plant vary according to the material in use, but as by far the larger portion of the product is that from the company's own mines, the results given below are fairly indicative of the general work obtained. The accompanying diagram illustrates graphically the flow of the ore through the electrostatic mill. The middling coming from the wet mill containing from 15 to 18 per cent. moisture is hoisted while on the cars by an elevator, and delivered from the top of the elevator to a hopper over the drier. The drier first installed was of too low capacity to take care of the moisture present in the tonnage to which the mill was later

Jan 8, 1914

By Diego L. Romero, Joy P. Romero

"IntroductionThe purpose of this paper is to explain the theory and demonstrate the industrial applications of electrostatic separation. Wabush Mines' use of this type of processing for the concentration of iron ore is unique in the industry. Other minerals are concentrated electrostatically but the process is not widely used.Typical minerals separated by electrostatic separation techniques are:Non-ConductorsAnhydriteApatiteBariteBastnasiteBerylCalciteChrysotileCorundumDiamondEpidoteFeldsparsFluoriteGarnetGypsumHornblendeKyaniteAcmiteAugiteBrookiteCassiteriteChalcopyriteChromiteColumbiteCopperDaviditeEuxeniteFerberiteFrankliniteGalenaGoldGraphiteHematiteMica (Biotite)Mica (Muscovite)MonaziteOlivinePerovskiteQuartzScheeliteSideriteSillimaniteSpheneStauroliteSulphurTopazTourmalineXenotimeZirconConductorsIlmeniteIlmenite-( High Iron)IlvaiteKoppiteMagnetiteMarmatiteMolybdenitePyriteRutileSamarskiteSphaleriteTantaliteWolframiteWulfeniteThe limitations of this process are:1. There must be a difference in conductivity between the minerals being separated.2. The size range must not be very wide.3. The specific gravity of minerals being separated should be similar or the minerals to be pinned should be lighter. 4. The feed must be dry.5. The particle shape should be more or less uniform. 6. The feed must not be high in true middling particles."

Jan 1, 1989

By Grant S. Diamond

THE BIBLIOGRAPHY on the use of static electricity in mineral beneficiation consists largely of patents. Some references are found in mineral textbooks, but very little data on flow-sheets of commercial installations are known to the writer. As a matter of fact there have been relatively few successful commercial applications of importance. Johnson prepared and published a Table showing the polarity and static field intensity requirements of many minerals. There have been reports of successful beneficiation of rutile, zir-con, coal, potassium chloride, and phosphate rock. Otherwise, the field of success has been very limited. This may be due to three reasons: first, the mining industry has been averse to dry processes, be-cause of dust nuisances in dry crushing; second, the electrostatic processes used in the past apparently developed no substantial economic advantages; and third, because flotation or other . methods have proven successful on many minerals, the industry has not felt the need for a radically different process. In the feldspar industry there was ?an attempt at electrostatic beneficiation about twenty years ago which was based on the use of fluoride fuming of the pegmatite head feed, in order to make the mineral reactive in a static field. This process was originally said to be successful, but was discontinued because of corrosion damage to machinery. Another effort by use of a chemical additive such as an or-ganic hydroxyl compound has also been attempted. Neither of these processes is known to be in use today.

Jan 1, 1957

By F. Fraas

ELECTROSTATIC methods are used to separate and concentrate or purify granular particles derived from ores or various synthetic and agricultural products. Compared with other separation methods that require many technological refinements, the electrostatic attraction of fibers, grass, and seeds to charged surfaces clan be accomplished under the most primitive circumstances, and the early development of this method of beneficiation seemed very promising. Precise application of the method to provide high selectivity, however, is a complex procedure, and interest in this method declined. During this period Mr. O. C. Ralston initiated a Bureau of Mines research program oil electrostatic separation. It is the purpose of thins publication to describe the development of the electrostatic method of particle separation from the early beginning to the present resurgence of interest. Most of the information for this description bas been derived from references, a few of which were not available for thorough review. Much information has been drawn from the investitions of the Bureau. Acknowledgments Mr. O. C. Ralston, former Chief metallurgist of the Bureau of Mines, began the research program on the subject and did research on the mils literature. Both Mr. Ralston and Mr. H. B. Johnson, former president of the Huff Electrostatic Separator Co., furnished patent references. A critical review by Mr. F. D. Lamb, Research director, and Mr. M. J. Spendlove, Supervisory metallurgist, Bureau of Mines, College Park Metallurgy Research Center, lifts been of much value in preparing this report.

Jan 1, 1962

By K. W. Warren, F. R. Prestridge, B. A. Sinclair

Separating oil from water may seem simple enough, but in fact, tremendous efforts have gone into this common process problem. The petroleum industry is constantly looking for better ways to separate the emulsion of oil and connate water that is pumped from the ground and its latest development, the electrostatic emulsion separator, may find an important offshoot application in hydrometallurgy. The patent-pending OSX coalescer, developed by C-E Natco, recovers entrained solvent from both raffinate and the pregnant strip liquor. It has already undergone successful testing at the Bluebird copper circuit in Arizona and is currently being prepared for testing at a uranium SX plant.

Jan 4, 1978

By Ghiani M, Satta F, Zucca A, Peretti R

After a brief introduction on the principles of contact electrification and a synthetic illustration of the Turbocharger separator, the successful results obtained with different raw materials are given and discussed, with particular reference to a North African run-of-mine with carbonate gangue, a crude ore from India containing pyrite and a mineral sample from Angola having quartzeous gangue. The pre-eminent effect of target surface temperature in the charging device of the separator is emphasised. On the basis of the results of both batch experiments and long-run tests the prospects of industrial application appear very interesting both from the technical and economic points of view, even when compared with froth flotation.

Jan 1, 1993

By A. F. Usov

The paper is concerned with an analysis of the experience gained in development of special electro-technical installations applied in electric-pulse destruction of materials. A principle scheme of an electric electric-pulse installation is given, and electric circuit variants of its blocks made on various element bases are discussed. Also assessed are some ideas to further improve the technical and economic characteristics of the equipment.

Jan 1, 2014

The General Electric Co., in cooperation with the Montana School of Mines and under a research grant from the Anaconda Co., is presently experimenting on a new non-explosive method of breaking rock with radio-frequency electrical power. The method is known as electrothermal forcing. It must be understood that present equipment has not been designed to perform primary blasting functions. Its conceived use will be restricted to small pieces of rock too large to pass through a chute or grizzly. However, even this use is still far in the future. Experiments to date have been limited mostly to rock smaller than 18 in.

Jan 11, 1961

By T. R. Raponi, D. Barnes

The Williams Mine mines and mills 6000 t/d (6600 stp’d) of gold ore using SAG/ball milling, leaching and CIP, electrowinning and refining. Electrowinning, high-pressure cathode washing, filtering, retorting and refining are based around the use of knitted stainless steel mesh cathodes. Their primary advantage over conventional steel wool cathodes is that electrowon gold can be washed off and the cathode can then be reused. Typically, the knitted cathodes have a useful life of up to 15 months. Gold production of up to15 t/month (50,000 oz/month) is easily processed with this system. Presented is a description of this operation, including a review of the equipment and performance data.

Jan 1, 1992

By J. E. Murphy

Neodymium was electrowon into a Mg-Cd molten cathode at 650 °C from NdC1,-KC1 electrolyte. With the chloride system, neodymium was deposited into the molten alloy cathode until the neodymium concentration reached 20 wt pct. The alloy was then vacuum melted to remove the Mg and Cd. The current efficiency exceeded 80 pct under optimum conditions and the purity of the metal was 99.9 pct after vacuum melting. As an alternative approach, neodymium was electrowon at 1,030 °C from Nd,O, dissolved in a molten fluoride eleotrolyte. With the oxide-fluoride electrolyte, the metal was electrowon in a molten state with current efficiencies up to 60 pct. The purity of the metal was 99.8 pct with oxygen and carbon as major impurities. A number of problems were encountered including anode effect, low oxide solubility in the electrolyte, high neodymium metal solubility in the electrolyte, and reactivity of the metal with the cell materials. Approaches to improved cell, operation and prospects for commercial adoption of the electrolytic production of neodymium metal are discussed.

Jan 1, 1995

By T. ?kre, O. M. Dotterud, S. Haarberg, J. Thonstad, G. M. Haarberg

An electrowinning pilot plant has been constructed at Falconbridge Nikkelverk A/S, Kristiansand, Norway. The equipment consists of a mixing tank where the electrolyte composition and temperature are controlled, an electrowinning tank equipped with five cathodes and six anodes of commercial size and design and a dechlorination facility. Electrowinning experiments were carried out in this pilot plant using acid cobalt chloride solution from the cobalt tankhouse. Key parameters were varied to obtain an improved understanding of the cobalt electrowinning process, focusing on the detrimental deposition of cobalt oxide on dimensionally stable anodes. The extent of anode scaling was found to be dependent on the electrowinning conditions. Low pH, temperature and cobalt concentration resulted in less scale being formed, however at the expense of cobalt current efficiency and cell voltage, adversely affecting electrowinning production capacity and energy consumption. When operating at high acidity, pH in the anolyte was higher than in the catholyte, which is believed to be due to H+ ions taking part in the current transport across the diaphragm, migrating out of the bags surrounding each anode.

Jan 1, 2005

The maximum current density at which conventional copper electrowinning plants will result in satisfactory, adherent, and dendrite·free cathodes is determined by the thickness of the diffusion boundary layer. A decrease in the value of that thickness will permit an increase in the current density. This fact is utilized to develop a high current density cell in which the reduction of the boundary layer thickness is accomplished by means of a specially designed electrolyte circulation system. The high current density cell is used to determine the effect of current density on such process parameters as current efficiency, cell voltage, power consumption, and cathode purity. A number of empirical equations are developed for the purpose of estimating the magnitude of these effects.

Jan 1, 1972

By Andersen AK

As part of a research program sponsored by Continental Copper and Steel Industries, Inc. (cos), investigations have been conducted by the Colorado School of Mines Research Foundation, Inc. to study the effect of high current densities on electrolytic processes. The importance of high current densities has long been recognized, particularly in the deposition of copper, and the results of considerable research on the subject have been reported in recent years (19 29 39). This is not surprising because, besides plant capacity, current density is the other major factor which will determine the process economics. In the production of electrolytic copper, current efficiency, steam consumption, number of cells, building area, metal inventory, cathode purity, and power consumption are all affected by current density. The ability to maintain a high current efficiency and satisfactory cathode purity while increasing the current density to twice or three times that commonly practiced could result in considerable saving of capital investment and reduce the operating cost per ton of metal produced. The optimum current density i.e., that current density of which production cost would be at a minimum, can be established from an analysis of the various inter- relating factors (49 59). A review of.all operating electrolytic plants (electrowinning and electrorefining) will indicate that most of these plants are operating at 50% or less of the optimum current density (6). One of the reasons for not using the optimum current density may be attributed to the fact that conventional electrolytic tank- house equipment does not perform satisfactorily at high current density operations. Various investigators (19 79 8) have attempted to overcome this limitation by modifying the design of the electrolytic cell, virtually unchanged since it was first introduced in the late 1800's. Previously, these attempts have not resulted in,a cell design suitable for commercial application. However, recently, a cell has been designed which performs efficiently under such conditions. This is a CCS development (patents applied for).

Jan 1, 1969

By Andersen AK

A previous paper (1) indicated that electrowinning of copper at current densities considerably higher than those currently employed in electrowinning operations is technically feasible. It is of interest, therefore, to establish the extent of economic benefits which may be obtained from high current density operation and to determine the value of the optimum current density. Optimization of electrorefining processes has been discussed in considerable detail by Ibl (2) and Schmidt (3) whop from theoretical considerations, derived expressions for the optimum current density. In this work, general equations relating both the capital investment and the production cost for copper electrowinning plants to current density and plant capacity are established. From these equations, the optimum current density can be calculated for any desired plant capacity.

Jan 1, 1969

By D. J. Fray, F. Tailoka

Microporous ceramic tubes (15 micrometre pore diameter) and PVC membranes (10 micrometre diameter) have been used as spargers in the electrowinning of copper from concentrated and dilute chloride electrolytes. At a current density of 600 A/m2 and a nitrogen gas sparging flow rate (at NTP) of 1.53 cm3/s per unit electrode length, it was possible to electrowin planar rather than powdery deposits with copper concentrations as low as 0.157 M. To obtain a planar deposit at higher concentrations of cupric chloride the most realistic optimum current density appears to be between 1 000 and 1 500 A/m2.

Jan 4, 1993

By J. B. Scuffham, G. Eggett, W. R. Hopkins

With solvent extraction now being accepted as a major method for recovering copper from leach liquors, the authors' company decided that in tankhouse design full advantage was not being taken of the benefits available from sol- vent extraction produced electrolytes. Consequently, a major development program was undertaken to examine means of operating such tankhouses with current densities in excess of current electrowinning practice. Techniques investigated included high circulation of liquors, current reversal and the application of ultrasonics. At the same time there was a necessity for improving the quality of cathodes produced from electrolytes of high free acid content. The application of anodes which are capable of reducing or eliminating the lead content of cathodes is described in the paper. The other problem area in eletrowinning from solvent extraction produced electrolytes is the production of a higher degree of acid mist. Techniques for alleviating this problem are described bearing in mind their possible effects on the solvent extraction section of the plant.

Jan 1, 1973

By J. E. Murphy, L. A. Walters, F. H. Nehl, G. B. Atkinson

The US Bureau of Mines investigated the selective electrowinning of Ag and Au from cyanide solutions contaminated with Cu with the goal of decreasing the amount of Cu codeposited. Decreasing Cu codeposited will reduce refinery costs. Direct current was applied to the cell in pulsed and square wave voltages at 0.7 A h/150 mL of solution. Times tested for each cycle ranged from 1 to 10,000 msecs. Graphite, lead and stainless steel were evaluated as electrode materials. Square wave electrowinning at 70°C (158° F) gave the best separation of Ag and Au from Cu. Applying 2.5 V during the duty cycle, 0.0 V the rest of the period, a duty cycle of 10% to 30%, and a period of 100 msecs to 1000 msecs gave the following results: Ag concentrations decreased from 34 µg/mL to 0.1 µg/mL. Au concentrations decreased from 54 µg/mL to 0.2 µg/mL and Cu concentrations remained almost constant at 560 µg/mL.

Jan 1, 1995

By F. H. Nehl

The U.S. Bureau of Mines investigated the selective electrowinning of Ag and Au from cyanide solutions contaminated with Cu with the goal of decreasing the amount of Cu co-deposited. Decreasing Cu co-deposited will reduce refinery costs. Direct current was applied to the cell in pulsed and square wave voltages at 0.7 A?h per 150 mL of solution. Times tested for each cycle ranged from 1 to 10,000 ms. Graphite, lead, and stainless steel were evaluated as electrode materials. Square wave e1ectrowinning at 70? C gave the best separation of Ag and Au from Cu. Applying 2.5 V during the duty cycle, 0.0 V the rest of the period, a duty cycle of 10 to 30 pct, and a period of 100 ms to 1,000 ms gave the following results: Ag concentrations decreased from 34 µ g/mL to 0.1 µ g/mL, Au concentrations decreased from 54 µ g/mL to 0.2 µ g/mL, and Cu concentrations remained almost constant at 560 µ g/mL.

Jan 1, 1993