US3883421A - Measurement of oxidation reduction potential in ore beneficiation - Google Patents

Measurement of oxidation reduction potential in ore beneficiation Download PDF

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US3883421A
US3883421A US288306A US28830672A US3883421A US 3883421 A US3883421 A US 3883421A US 288306 A US288306 A US 288306A US 28830672 A US28830672 A US 28830672A US 3883421 A US3883421 A US 3883421A
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slurry
flotation
cell
ore
oxidation
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Dale Emerson Cutting
Richard Arthur Womack
Joseph Vernon Macguffie
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Priority to CS736277A priority patent/CS199549B2/cs
Priority to AU60147/73A priority patent/AU477450B2/en
Priority to IE1612/73A priority patent/IE38236B1/xx
Priority to GB4295573A priority patent/GB1434545A/en
Priority to FR7332717A priority patent/FR2199000B1/fr
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03B—SEPARATING SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS
    • B03B13/00—Control arrangements specially adapted for wet-separating apparatus or for dressing plant, using physical effects
    • B03B13/04—Control arrangements specially adapted for wet-separating apparatus or for dressing plant, using physical effects using electrical or electromagnetic effects
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation

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  • This invention relates to ore beneficiation to separate mineral values by flotation in maximum yield and economy by precise measurement of the need and control of supply of beneficiating chemicals to a fine ore slurry in water, in response to optimum oxidation-reduction potentials of the ore flotation suspension for effecting the separation.
  • the invention is directed, in preferred aspect, to treatment of an ore containing sulfidable values to be separated by flotation from gangue materials economically in optimum yield by supplying sulfiding chemicals to the ore slurry in quantity controlled to develop an optimum range of pre-determined oxidation-reduction potentials as the mixture passes a selected control point such as through a flotation cell.
  • Mineral values to be separated from gangue materials in an ore by flotation such as sulfide minerals, usually contain other mineral values desirably separated with the natural mineral sulfides, such as oxides, hydroxides, carbonates, sulfates, native metals and complexes thereof. These constitute common sulfidable ore components with which the sulfides may occur in the ore and are desirably recovered with the naturally occurring sulfides.
  • the common practice in the art has been to add to such ores a sulfiding agent such as sodium sulfide, sodium bisulfide or hydrogen sulfide together with flotation chemicals, flocculants, etc.
  • sulfiding agents react at least superficially with such sulfidable mineral components of the finely ground ore particles to form a thin or superficial sulfide coating on some of the particle surfaces sufficient to improve their wettability by the flotation agent and thus tend to become more separable in the flotation as a froth, together with the normal sulfide values of the ore.
  • the difficulty has been that the sulfidable components for which a sulfiding agent is added to the ground ore slurry before flotation may vary in quantity in the ore being processed and will vary in size range and in particulate surface exposure in the batch under process, so that there may be too little or too much sulfiding agent supplied as the processing continues. There is some tendency to add an excess merely to effect the superficial sulfide coating needed for flotation; but this would involve substantial losses in economy.
  • the quantity of benificiating chemical, typically sulfiding agent added to the ore to improve flotation, and sometimes including the quantity of flotation agent used is precisely controlled in supply of these chemicals to a continuous flotation mix by varying the quantity responsively to maintain an optimum oxidation-reduction potential in the flotation cell. More practically, the quantity of sulfiding agent and usually flotation agent is variably supplied to the ore slurry to be processed as needed to maintain a selected range of the developed oxidationreduction potential in the flotation cell, the selected range being optimum for the specific ore being treated.
  • the recoverable value is, for example, substantially in the form of copper sulfide to be separated by flotation, and in which the ore also contains oxidized copper values such as cuprite, malachite or azurite, or mixtures thereof, whereby the copper sulfide is a natural mixture with copper oxide, copper carbonate or copper hydroxide, or mixtures thereof, and also sometimes to a minor extent, copper sulfate and native copper, and which is usually further admixed with gangue materials, typically sandstone and harder rock matrices, the ore must first be ground to substantially release the mineral values in small particle form.
  • oxidized copper values such as cuprite, malachite or azurite, or mixtures thereof
  • the ore may, for example, be ground by milling to a range of about to 200 microns, a sieve size of about 30 to l40 mesh U.S. standard sieve.
  • the ground ore fineness is sufficient to allow reaction and superficial coating of the sulfidable components with a sulfide film formed in reaction with the sulfiding agent upon these known sulfidable forms of copper, thereby modifying the particle surfaces with sulfide film.
  • Such surfaces so modified allow wetting with the sulfide selective flotation agent for separation of the sulfide coated copper values along with the native copper sulfide by flotation.
  • this superficial film in combination with other variable components of the flotation mixture such as the air introduced into the cell to effect the flotation, the degree of reaction of the sulfidable component upon the recoverable values and the conductive character of the flotation agent per se, all present in the liquid and air suspension in the flotation cell, will develop a measureable oxidation-reduction potential which, according to this invention, applicants use as a guide to determine whether this mixture as supplied to the flotation cell will allow optimum separation of the mineral values by flotation.
  • applicants use the oxidation-reduction potential as a basis upon which to adjust the chemical supply to the ore slurry to effect optimum separation.
  • an ore body is crushed and then ground and classified to a flotable slurry in water. It is then treated with beneficiating chemicals such as flotation agents; and, where the ore is of a mixed type, with a sulfiding agent to improve flotation of non-sulfide values occurring in the mixed ore body.
  • beneficiating chemicals such as flotation agents; and, where the ore is of a mixed type, with a sulfiding agent to improve flotation of non-sulfide values occurring in the mixed ore body.
  • These chemicals are supplied in quantity found by analysis to be usually optimum for floating the total mineral substance desirably recovered in the ore.
  • the slurry is also treated with the optimum quantity of flotation agents and other usual beneficiating substances i.e. aerofloat, flocculant, superfloc, etc., commonly added to the ore in preparation for flotation, the mixture being then passed to a flotation cell such as a commerical Maxwell cell. Air in controlled quantity is also admitted to the cell, mixing with
  • An electrolytic voltaic cell of any commercial type such as a standard cell of calomel-platinum electrodes, is mounted in contact with the aerated slurry with the electrode dipping into or in conductive contact with the slurry at a selected reference point, preferably near the top of the flotation cell in a manner such that the slurry is made the electrolyte of the cell whose EMF is measured usually in millivolts by leads connected to the electrodes and to a voltmeter.
  • the measured EMF of the cell is that produced by the flotation slurry per se as it continuously flows by and the EMF output of the cell thus formed is the oxidation-reduction potential and it will vary with the condition of the flowing slurry.
  • the efficiency of the flotation over a series of tests is noted, particularly the variation in oxidationreduction potential of the cell is measured with these several variants, such as by slightly varying the quantity of ore beneficiating and flotation chemicals as needed, and determining the approximate optimum recovery of metal values from the ore with respect to quantities of beneficiating chemical, and recording the oxidationreduction potentials of the cell developed over such range of operating conditions.
  • the optimum yield of a flotation cell with variable quantities of beneficiating chemical is determined in terms of the oxidation-reduction potential developed in the flotation slurry being treated.
  • An optimum specific oxidation-reduction potential for treating a particular ore will be found but, more practically, a narrow range of oxidation-reduction potential values will be found for most efficient operation of the flotation cell making minor allowances for some variables.
  • beneficiating treat ment of an ore body containing between A and l percent of copper values including sulfidable components that it requires a feed of between l and 2 pounds per ton of sulfiding agent such as sodium sulfide and be tween 0.1 and 0.3 pounds per ton of a xanthate flotation agent for optimum removal of copper values from such ore in which from 0.5 to 0.1 per cent of the copper is an oxide to be sulfided.
  • sulfiding agent such as sodium sulfide and be tween 0.1 and 0.3 pounds per ton of a xanthate flotation agent
  • such variation of beneficiating chemicals is made in quantity needed to maintain the cell potential within the above stated range; that is, to maintain an oxidation-reduction potential within the Maxwell cell in the determined optimum range.
  • the feed of the beneficiatng chemicals supplied to the ore slurry is varied, modifying such quantity so as to maintain the oxidation-reduction potential of the cell in the preferred acceptable range.
  • FIG. 1 shows an ore beneficiating flow sheet
  • FIG. 2 shows a system in which the feed of ore beneficiating chemical may be automatically controlled in selected quantityv
  • crushed ore fines comprising about 40 percent solids crushed initially to coarse fragments of which about percent of three-eighths inch or less enters the system conveyor line 10 and is passed to a ball mill I2 by way of a hopper l4, and is milled in water to a slurry with particles ranging in size from about to 200 microns.
  • the slurry is continuously withdrawn from a collection box 16 by way of a pump 18 controlled by a density meter 20, passing to a classifier 22 in which the selected oversize of particles are returned to the hopper 14 by way ofline 24 and the slurry of fines, controlled in size for flotation, pass by way ofline 26 to a distributor box 28.
  • the slurry is then divided, passing by way of lines 30 and 32 to Maxwell cells 34 and 36, respectively.
  • Beneficiating chemical solution which for a copper ore identified above would comprise sulfiding agent, flotation agent, flocculating agent, etc.
  • sulfiding agent for a copper ore identified above
  • flotation agent for a copper ore identified above
  • Flotation air is also supplied at any usual point of the system indicated only diagrammatically at 38 and 40.
  • Oxidation-reduction primary cells 42 and 44 which may be standard calomel-platinum electrode cells are mounted with their electrodes dipping in the flotation slurry near the tops of each Maxwell cell 34 and 36.
  • the voltage output of standard cell 42, by way of electrical lines 43, is indicated on a millivolt meter 47 and the output of cell 44 by way of line 45 is measured by voltmeter 49.
  • the quantity of beneficiating chemical added through lines 35 and 37 may be respectively controlled manually by adjustment of valves 39 and 41, passing a solution of necessary chemicals in adjusted quantity into the flotation slurry as it passes through lines 30 and 32, respectively, the quantity of chemical fluid being adjusted to flow therein at a rate to maintain the volt meter readings 47 and 49 at the pre-selected relatively constant millivolt values within a pre-selected narrow range.
  • the oxidationreduction potential of cells 34 and 36 are maintained at the selected narrow range values of the meter readings 47 and 49 by adjustment of the supply beneflciating chemicals, each controlled by valves 39 and 41.
  • the floated mineral values of the Maxwell cells 34 and 36 are withdrawn from line 51 and, as mentioned Examples 1 and I] below, may be handled as separated mineral concentrate without further treatment.
  • the concentrate in line 51 can be passed to the second Fagergren cell 54.
  • the residual slurry withdrawn by way of lines 46 and 48 may pass by way of line 50 to the first cell 52 of of the series of Fagergren roughers; at least the first two of which 52 and 54 have mounted similar primary cells 56 and 58, each connected by lines 60 and 62 to millivolt meters 64 and 66, respectively.
  • Tailings are withdrawn by line 72 from an after portion of the last Fagergren.
  • the floated concentrate separated as the froth in the Maxwell cells may also be passed by line 51 in a series through Fagergren rougher cells 54 and 68 and finally out of the system by way of cell 68 and outlet 72.
  • the flotation slurry in line 50 enter the first Fagergren cell 52 and leaves the system from cell 68.
  • the mineral values as concentrate overflow the cells into a launder 71 and leaves by way of line 70 for further thickening, filtration and then storage as concentrated ore values ready for further refining.
  • the tailings leave the Fagergren rougher cell 68 by way of line 72 for further disposal.
  • the further treatment in the Fagergren cells is controlled by primary cells 56 and 58, each mounted near the top of a Fagergren 52 and 54 to measure the oxidation-reduction potential in the slurry in each of these cells.
  • the entering slurry in line 50 is floated in Fagergren 52 and has its oxidation-reduction potential measured in millivolts at this point by the primary cell 56 which is indicated as EMF upon meter 64.
  • Additional beneficiating chemical and flotation agent is supplied to line 50 by way of a supply pipe 74 controlled by a valve 76 and the quantity of chemical added is a small adjustment of the system responsive only to maintain the optimum voltage indicated in meter 64.
  • last traces comprising comparatively smaller quantities of beneficiating chemical is supplied by way of line 78 controlled by a valve 80 which adds the chemical to the floated slurry just before it enters the second Fagergren 54.
  • This supply of chemical is also made controllable to the EMF reading on meter 66 responsive to the current developed in the electrolytic cell 58 mounted similarly near the top of the Fagergren 54.
  • the necessary supply of air to the rougher flotation cells 52 and 54 enters through any conventional point 40.
  • beneficiating chemical is supplied in exact quantity by control of valves 39, 41, 76, and 80, each manually or automatically set to supply sufficient beneficiating chemical response to the oxidation-reduction potential developed in each flotation cell, according to a predetermined EMF range.
  • FIG. 2 shows in plan the Maxwell cells 34 and 36, each having primary cells 42 and 44 mounted near its top, their respective outputs being connected by lines 43 and 45 to meters 47 and 49.
  • Meter 47 in turn is electrically connected by control line 82 to a solenoid 84 having an armature 86 which controls the flow of beneficiating chemical fluid through valve 39 to the Maxwell 34 by way of line 20.
  • the meter 49 output current is connected by control line 88 to a solenoid 90 having an armature 91 mounted connected to control the flow of beneficiating chemical through valve 41 to Maxwell 36 by way of line 32.
  • An original make-up tank 92 contains a mixture of beneficiating chemical 94 in controlled concentration for supply to the system.
  • a pump 96 is mounted to pump liquid chemical from the tank 92 and pass the same to a supply pipe 98 for supply of the system with the beneficiating and usually also flotation. chemical 94 under a controlled flow pressure.
  • the supply pipe 98 joins valve 39 as its supply of fluid and the solenoid 84 controlled quantity of fluid passing to valve 39, passing the requisite quantity of chemical to line 30 responsive to solenoid 84 movement and the EMF of the cell 42.
  • line 98 also passes liquid chemical supply to valve 41, which supplies slurry carrying line 32 with a controlled quantity of beneficiating chemical as it passes to Maxwell cell 36 responsive to the current developed in the cell 44 mounted therein.
  • valve 76 controls valve 76 to pass chemical through lines 74 and 106 in response to the EMF developed in meter 64, as the oxidation-reduction potential of the Fagergren 52.
  • Valve 76 so controlled, draws a supply of beneficiating chemical from the supply line 98, passing the same into the entering slurry of the Fagergren 52.
  • the valve is controlled by primary cell 58 and meter 66 to control the supply of chemical to Fagergren 54, drawing the same from supply line 78 connected to the source 98 in response to the setting of solenoid 108 controlled by the meter output 66.
  • the quantity of chemical to each cell is automatically controlled to pass the chemical from the main supply line 98 into flotation slurry lines passing respectively to cells 34, 36, 52 and 54 in response to the respective oxidation-reduction potentials developed and measured in each of these cells.
  • the quantity of the chemical is that needed by each cell and automatically supplied according to its oxidation-reduction potential of the particular flotation cell.
  • the characteristics of the copper are such that the ratio of the oxidized copper to the copper sulfides will vary continuously in a very minor range from batch to batch as the product is mined and milled.
  • the sodium sulfide solution is passed into the Maxwell cell at a rate of l3,000 milliliters per minute together with xanthate solution at 13,500 milliliters per minute for a period of 24 hours without variation of this constant feed. At the end of this period it was found that 59 percent of the total copper content was recovered using a total feed of sodium sulfide of 1.3 pounds per ton of ore fed and for the xanthate a feed of 0.22 pounds per ton.
  • Example Ill The method as disclosed in Example ll was repeated, but controlling the oxidation-reduction potential in both Maxwell cells and subsequent Fagergren cells to approximately 155 millivolts by addition of sufficient and variable quantities of sodium sulfide and xanthate solution in each cell as the flotation proceeded, to maintain a substantially constant millivolt potential. It was found that the total recovery of copper was 65.5 percent and the total consumption of sodium sulfide was found to be 1.22 pounds per ton and the xanthate was 0.20 pounds per ton.
  • EXAMPLE IV The method as disclosed in Example I] was repeated, controlling the millivolt potential to 135.0 in each cell while adding H 8 in the amount of 0.32 pounds per ton of ore and xanthate in the amount of 0.20 pounds per ton. Recovery of the copper was 64.5 percent.
  • EXAMPLE V The method as disclosed in Example IV was repeated, controlling the millivolt potential to l40 millivolts in each cell, while adding N HS in the amount of 0.90 pounds per ton of ore. Recovery of the copper was 65.5 percent.
  • non-ferrous metal such as copper
  • other metals particularly those usually purifiable by flotation and particularly those minerals whose ores are usually available as sulfides, sometimes admixed with oxides, hydroxides, carbonates or the like.
  • Such other metals include silver, lead, zinc, molybdenum and other typical metals usually concentratible by flotation.
  • the method is also applicable to certain ferrous metal ores such as manganese, cobalt, cadmium, oftimes further in admixture with copper and sometimes with small quantities of native metals.
  • beneficiating chemicals for recovery of other metal values as would be better suited to such other ores would be used where the metal being recovered is not primarily copper.
  • any other primary voltaic cell capable of developing an easily measured EMF between electrodes, using the flotation slurry as electrolyte may serve as an EMF indicator. as control for operation of the flotation process, using the developed oxidation-reduction potential of such cell as control.
  • Such other cells will be equally useful when standarized to an EMF output indicative of optimum operation of the flotation process under its control whereby the beneficiating chemicals may be varied by such EMF output as a control to effect opti mum operation.
  • the improvement comprising pre-determining a range of oxidation-reduction potentials developed in a slurry of the ore beneficiated to a condition of high flotation yield of mineral values therein, and then modifying the quantity of beneficiating chemical substance supplied to said slurry to continuously maintain an oxidation-reduction potential of said slurry in the same pre-determined range as the flotation proceeds.
  • the sulfiding agent is a member of the group consisting of hydrogen sulfide, alkali metal hydrosulfide and alkali metal sulfide.
  • the sulfiding agent is selected from the group consisting of hydrogen sulfide, alkali metal hydrosulfide and alkali metal sulfide.

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  • Physics & Mathematics (AREA)
  • Electromagnetism (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Separation Of Solids By Using Liquids Or Pneumatic Power (AREA)
US288306A 1972-09-12 1972-09-12 Measurement of oxidation reduction potential in ore beneficiation Expired - Lifetime US3883421A (en)

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Application Number Priority Date Filing Date Title
US288306A US3883421A (en) 1972-09-12 1972-09-12 Measurement of oxidation reduction potential in ore beneficiation
CS736277A CS199549B2 (en) 1972-09-12 1973-09-10 Method of metallic ore flotation
AU60147/73A AU477450B2 (en) 1972-09-12 1973-09-10 Ore beneficiation by oxidation reduction control
IE1612/73A IE38236B1 (en) 1972-09-12 1973-09-11 Ore beneficiation
GB4295573A GB1434545A (en) 1972-09-12 1973-09-12 Ore beneficiation
FR7332717A FR2199000B1 (en:Method) 1972-09-12 1973-09-12

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CS (1) CS199549B2 (en:Method)
FR (1) FR2199000B1 (en:Method)
GB (1) GB1434545A (en:Method)
IE (1) IE38236B1 (en:Method)

Cited By (23)

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Publication number Priority date Publication date Assignee Title
US4006014A (en) * 1975-07-28 1977-02-01 Canadian Industries Limited Use of tetraalkylammonium halides as flotation collectors
US4011072A (en) * 1975-05-27 1977-03-08 Inspiration Consolidated Copper Company Flotation of oxidized copper ores
US4090867A (en) * 1975-04-30 1978-05-23 Canadian Patents & Development Limited Flotation of non-sulphide copper ores
US4561970A (en) * 1982-11-02 1985-12-31 Outokumpu Oy Process for the froth flotation of complex metal compounds
US4585549A (en) * 1984-01-30 1986-04-29 Exxon Research & Enginerring Company Flotation of upper zone copper sulfide ores
US4917775A (en) * 1984-10-30 1990-04-17 Outokumpu Oy Method for measuring and adjusting electrochemical potential and/or component content in the process of treating valuable materials
US5108495A (en) * 1988-05-13 1992-04-28 Outokumpu Oy Method controlling a process by impedance analysis
WO1993022060A1 (en) * 1992-05-04 1993-11-11 Cyprus Minerals Company Method for achieving enhanced copper-containing mineral concentrate grade by oxidation and flotation
US5307937A (en) * 1993-02-17 1994-05-03 North Carolina State University High throughput flotation column process
US5439115A (en) * 1992-11-12 1995-08-08 Metallgesellschaft Aktiengesellschaft Process for selective flotation of copper-lead-zinc sulfide
US5753104A (en) * 1994-07-06 1998-05-19 Boc Gases Australia Limited Physical separation processes for mineral slurries
US5783057A (en) * 1996-09-19 1998-07-21 Nippon Mining & Metals Co., Ltd. Method of purifying copper electrolytic solution
US5795466A (en) * 1995-06-08 1998-08-18 Falconbridge Limited Process for improved separation of sulphide minerals or middlings associated with pyrrhotite
US5855770A (en) * 1994-11-25 1999-01-05 Boc Gases Australia Limited Base metal mineral flotation processes
US6390303B1 (en) 1998-07-24 2002-05-21 Boc Gases Austrailia Ltd. Method for optimizing flotation recovery
US20030221972A1 (en) * 2002-05-30 2003-12-04 Clariant International Ltd. Electrochemical process for preparing zinc metal and process for preparing zinc dithionite using electrochemically produced zinc metal
WO2004081552A1 (en) * 2003-03-14 2004-09-23 Outokumpu Technology Oy Method for controlling a process
CN100435966C (zh) * 2006-12-08 2008-11-26 凌源市盛唐矿冶有限责任公司 一种利用比重性质选别非磁性铁矿的方法
US20090317313A1 (en) * 2006-11-15 2009-12-24 University Of Capetown Sulfidisation process and apparatus for enhanced recovery of oxidised and surface oxidised base and precious metal minerals
CN102869449A (zh) * 2010-04-30 2013-01-09 奥图泰有限公司 回收有价值的金属的方法
WO2013169140A1 (en) 2012-05-10 2013-11-14 Outotec Oyj Method and apparatus for controlling the flotation process of pyrite - containing sulphide ores
WO2014104915A1 (en) 2012-12-28 2014-07-03 Outotec Oyj Method and apparatus for monitoring the quality of ore
US10717090B2 (en) * 2014-04-11 2020-07-21 Tessenderlo Kerley, Inc. Depression of copper and iron sulfides in molybdenite flotation circuits

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RU2141384C1 (ru) * 1998-11-02 1999-11-20 ЗАО "Механобр Инжиниринг Автоматик" Способ флотации руд цветных металлов
RU2234548C2 (ru) * 2002-08-13 2004-08-20 Читинский государственный технический университет Способ извлечения окисленного молибдена при переработке смешанных молибденовых руд
CN102896037B (zh) * 2012-10-08 2014-04-02 湖南有色金属研究院 一种矿石中含离子态铜钴镍矿的选矿方法

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US1236504A (en) * 1916-02-07 1917-08-14 George D Van Arsdale Art of concentration of ores by flotation.
US1334734A (en) * 1916-11-25 1920-03-23 Metals Recovery Co Method of and apparatus for concentrating oxidized ores by flotation
US1335000A (en) * 1913-08-15 1920-03-30 Frankforter Process of treating metalliferous materials
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US3486847A (en) * 1967-01-24 1969-12-30 Titan Gmbh Process for automatically regulating the reduction of the iron and titanium values in a digestion liquor
US3501392A (en) * 1967-06-28 1970-03-17 Dow Chemical Co Electromotive sensing device
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US1335000A (en) * 1913-08-15 1920-03-30 Frankforter Process of treating metalliferous materials
US1236504A (en) * 1916-02-07 1917-08-14 George D Van Arsdale Art of concentration of ores by flotation.
US1334734A (en) * 1916-11-25 1920-03-23 Metals Recovery Co Method of and apparatus for concentrating oxidized ores by flotation
US2184115A (en) * 1938-09-27 1939-12-19 Hugh W Coke Apparatus for flotation concentration of ores
US2607718A (en) * 1946-06-17 1952-08-19 Petrolite Corp Process and apparatus for control of reagents
US2651413A (en) * 1948-06-14 1953-09-08 Mining Process & Patent Co Dual aerating flotation machine
US3094484A (en) * 1958-08-22 1963-06-18 R Alfonso Rizo-Patron Process of froth flotation of ores
US3051631A (en) * 1959-04-07 1962-08-28 Diamond Alkali Co Method and apparatus for the control of oxidation-reduction reactions
US3421850A (en) * 1965-07-02 1969-01-14 Anaconda Co Separate recovery of copper sulfide and zinc sulfide from aqueous solutions containing water-soluble salts of copper and zinc
US3486847A (en) * 1967-01-24 1969-12-30 Titan Gmbh Process for automatically regulating the reduction of the iron and titanium values in a digestion liquor
US3501392A (en) * 1967-06-28 1970-03-17 Dow Chemical Co Electromotive sensing device
US3735931A (en) * 1972-07-19 1973-05-29 D Weston Flotation of copper ores

Cited By (30)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4090867A (en) * 1975-04-30 1978-05-23 Canadian Patents & Development Limited Flotation of non-sulphide copper ores
US4011072A (en) * 1975-05-27 1977-03-08 Inspiration Consolidated Copper Company Flotation of oxidized copper ores
US4006014A (en) * 1975-07-28 1977-02-01 Canadian Industries Limited Use of tetraalkylammonium halides as flotation collectors
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US4585549A (en) * 1984-01-30 1986-04-29 Exxon Research & Enginerring Company Flotation of upper zone copper sulfide ores
US4917775A (en) * 1984-10-30 1990-04-17 Outokumpu Oy Method for measuring and adjusting electrochemical potential and/or component content in the process of treating valuable materials
US5108495A (en) * 1988-05-13 1992-04-28 Outokumpu Oy Method controlling a process by impedance analysis
US5295585A (en) * 1990-12-13 1994-03-22 Cyprus Mineral Company Method for achieving enhanced copper-containing mineral concentrate grade by oxidation and flotation
WO1993022060A1 (en) * 1992-05-04 1993-11-11 Cyprus Minerals Company Method for achieving enhanced copper-containing mineral concentrate grade by oxidation and flotation
US5439115A (en) * 1992-11-12 1995-08-08 Metallgesellschaft Aktiengesellschaft Process for selective flotation of copper-lead-zinc sulfide
US5307937A (en) * 1993-02-17 1994-05-03 North Carolina State University High throughput flotation column process
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US5855770A (en) * 1994-11-25 1999-01-05 Boc Gases Australia Limited Base metal mineral flotation processes
US5795466A (en) * 1995-06-08 1998-08-18 Falconbridge Limited Process for improved separation of sulphide minerals or middlings associated with pyrrhotite
US5783057A (en) * 1996-09-19 1998-07-21 Nippon Mining & Metals Co., Ltd. Method of purifying copper electrolytic solution
US6390303B1 (en) 1998-07-24 2002-05-21 Boc Gases Austrailia Ltd. Method for optimizing flotation recovery
US20030221972A1 (en) * 2002-05-30 2003-12-04 Clariant International Ltd. Electrochemical process for preparing zinc metal and process for preparing zinc dithionite using electrochemically produced zinc metal
WO2004081552A1 (en) * 2003-03-14 2004-09-23 Outokumpu Technology Oy Method for controlling a process
US20060216827A1 (en) * 2003-03-14 2006-09-28 Kari Pulkkinen Method for controlling a process
AU2004219922B9 (en) * 2003-03-14 2010-02-04 Outokumpu Technology Oy Method for controlling a process
AU2004219922B2 (en) * 2003-03-14 2009-06-18 Outokumpu Technology Oy Method for controlling a process
US20090317313A1 (en) * 2006-11-15 2009-12-24 University Of Capetown Sulfidisation process and apparatus for enhanced recovery of oxidised and surface oxidised base and precious metal minerals
CN101583728B (zh) * 2006-11-15 2012-11-14 开普敦大学 提高氧化和表面氧化的贱金属和贵金属矿物回收率的硫化方法和设备
US8883097B2 (en) * 2006-11-15 2014-11-11 University Of Cape Town Sulfidisation process and apparatus for enhanced recovery of oxidised and surface oxidised base and precious metal minerals
CN100435966C (zh) * 2006-12-08 2008-11-26 凌源市盛唐矿冶有限责任公司 一种利用比重性质选别非磁性铁矿的方法
CN102869449A (zh) * 2010-04-30 2013-01-09 奥图泰有限公司 回收有价值的金属的方法
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WO2014104915A1 (en) 2012-12-28 2014-07-03 Outotec Oyj Method and apparatus for monitoring the quality of ore
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Also Published As

Publication number Publication date
GB1434545A (en) 1976-05-05
FR2199000A1 (en:Method) 1974-04-05
AU6014773A (en) 1975-03-13
IE38236B1 (en) 1978-02-01
IE38236L (en) 1974-03-12
CS199549B2 (en) 1980-07-31
FR2199000B1 (en:Method) 1977-09-30

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