EP0453677A1 - Drücken von Kieselsäure oder siliziumgehaltiger Gangart bei Erzflotation - Google Patents

Drücken von Kieselsäure oder siliziumgehaltiger Gangart bei Erzflotation Download PDF

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Publication number
EP0453677A1
EP0453677A1 EP90304633A EP90304633A EP0453677A1 EP 0453677 A1 EP0453677 A1 EP 0453677A1 EP 90304633 A EP90304633 A EP 90304633A EP 90304633 A EP90304633 A EP 90304633A EP 0453677 A1 EP0453677 A1 EP 0453677A1
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European Patent Office
Prior art keywords
acid
flotation
minerals
hydroxy
mixture
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EP90304633A
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English (en)
French (fr)
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EP0453677B1 (de
Inventor
Richard Robert Klimpel
Robert Douglas Hansen
Donald Eugene Leonard
Basil Stewart Fee
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Dow Chemical Co
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Dow Chemical Co
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Priority to CA002014882A priority Critical patent/CA2014882C/en
Application filed by Dow Chemical Co filed Critical Dow Chemical Co
Priority to DE69021553T priority patent/DE69021553D1/de
Priority to EP90304633A priority patent/EP0453677B1/de
Priority to AU54774/90A priority patent/AU619979B2/en
Priority to ZA903531A priority patent/ZA903531B/xx
Priority to FR9005770A priority patent/FR2661844B1/fr
Priority to CN90102733A priority patent/CN1056445A/zh
Publication of EP0453677A1 publication Critical patent/EP0453677A1/de
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Classifications

    • 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
    • B03D1/001—Flotation agents
    • B03D1/004—Organic compounds
    • B03D1/012—Organic compounds containing sulfur
    • 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
    • B03D1/001—Flotation agents
    • B03D1/004—Organic compounds
    • B03D1/008—Organic compounds containing oxygen
    • 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
    • B03D1/001—Flotation agents
    • B03D1/004—Organic compounds
    • B03D1/01—Organic compounds containing nitrogen
    • 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
    • B03D2201/00—Specified effects produced by the flotation agents
    • B03D2201/02—Collectors
    • 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
    • B03D2203/00—Specified materials treated by the flotation agents; Specified applications
    • B03D2203/02—Ores
    • 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
    • B03D2203/00—Specified materials treated by the flotation agents; Specified applications
    • B03D2203/02—Ores
    • B03D2203/025—Precious metal ores

Definitions

  • This invention is related to the recovery of minerals by froth flotation.
  • Flotation is a process of treating a mixture of finely divided mineral solids, e.g., a pulverulent ore, suspended in a liquid whereby a portion of the solids is separated from other finely divided mineral solids, e.g., silica, siliceous gangue, clays and other like materials present in the ore, by introducing a gas (or providing a gas in situ ) in the liquid to produce a frothy mass containing certain of the solids on the top of the liquid, and leaving suspended (unfrothed) other solid components of the ore.
  • a gas or providing a gas in situ
  • Flotation is based on the principle that introducing a gas into a liquid containing solid particles of different materials suspended therein causes adherence of some gas to certain suspended solids and not to others and makes the particles having the gas thus adhered thereto lighter than the liquid. Accordingly, these particles rise to the top of the liquid to form a froth.
  • the minerals and their associated gangue which are treated by froth flotation generally do not possess sufficient hydrophobicity or hydrophilicity to allow adequate separation. Therefore, various chemical reagents are often employed in froth flotation to create or enhance the properties necessary to allow separation.
  • Collectors are used to enhance the hydrophobicity and thus the floatability of different mineral values. Collectors must have the ability to (1) attach to the desired mineral species to the relative exclusion of other species present; (2) maintain the attachment in the turbulence or shear associated with froth flotation; and (3) render the desired mineral species sufficiently hydrophobic to permit the required degree of separation.
  • a number of other chemical reagents are used in addition to collectors.
  • additional reagents include frothers, depressants, pH regulators, such as lime and soda, dispersants and various promoters and activators.
  • Depressants are used to increase or enhance the hydrophilicity of various mineral species and thus depress their flotation.
  • Frothers are reagents added to flotation systems to promote the creation of a semi-stable froth. Unlike both depressants and collectors, frothers need not attach or adsorb on mineral particles.
  • Froth flotation has been extensively practiced in the mining industry since at least the early twentieth century.
  • a wide variety of compounds are taught to be useful as collectors, frothers and other reagents in froth flotation.
  • xanthates, simple alkylamines, alkyl sulfates, alkyl sulfonates, carboxylic acids and fatty acids are generally accepted as useful collectors.
  • Reagents useful as frothers include lower molecular weight alcohols such as methyl isobutyl carbinol and glycol ethers.
  • the specific additives used in a particular flotation operation are selected according to the nature of the ore, the conditions under which the flotation will take place, the mineral sought to be recovered and the other additives which are to be used in combination therewith.
  • Minerals and their associated ores are generally categorized as sulfides or oxides, with the latter group including carbonates, hydroxides, sulfates and silicates. While a large proportion of the minerals existing today are contained in oxide ores, the bulk of successful froth flotation systems is directed to sulfide ores. The flotation of oxide minerals is recognized as being substantially more difficult than the flotation of sulfide minerals and the effectiveness of most flotation processes in the recovery of oxide ores is limited.
  • Some of the recognized collectors such as the carboxylic acids, alkyl sulfates and alkyl sulfonates discussed above are taught to be effective collectors for oxide mineral ores.
  • existing collectors are known to be useful in sulfide flotation.
  • the selectivity to the desired mineral value may not be as high as desired and, in the case of oxide flotation, is typically quite poor. That is, the grade or the percentage of the desired mineral contained in the recovered mineral is unacceptably low.
  • the present invention is a process for the recovery of mineral values by froth flotation comprising subjecting a particulate ore, which contains silica or siliceous gangue and is in an aqueous slurry, to froth flotation under conditions such that the minerals to be recovered are floated wherein the flotation of the silica or siliceous gangue is depressed by the use of an effective amount of a hydroxy-containing compound selected from the group comprising ethanol amine, propanol amine, butanol amine, lactic acid, glycolic acid, ß-hydroxy-1-propane sulfonic acid, ethylene glycol, diethylene glycol, propylene glycol, dipropylene glycol, glycerol, trihydroxy benzoic acid, hydroxy benzoic acid, butylene glycol, dibutylene glycol, diethanol amine, dipropanol amine, tripropanol amine, triethanol amine and simple sugar alcohols such as sucrose, glucose and dex
  • improved selectivity it is meant that the total amount of mineral recovered and/or the grade of the mineral recovered is increased while the amount of silica or siliceous gangue not recovered, i.e. remaining in the aqueous phase, is also increased.
  • the ability to separate silica and/or siliceous gangue from desirable mineral values is enhanced. That is, the tendency of the silica or siliceous gangue to float is depressed.
  • the flotation process of this invention is useful in the recovery of various minerals, including oxide minerals, by froth flotation.
  • the flotation process of this invention is useful in the recovery of mineral values from a variety of ores.
  • An ore herein refers to the mineral as it is taken out of the ground and includes the mineral-containing species intermixed with gangue.
  • Gangue are those materials which are of little or no value and need to be separated from the mineral values.
  • gangue specifically includes silica and siliceous materials.
  • collectors are effective with different types of ores.
  • Certain anionic collectors described below and useful in the present invention, have been found to be surprisingly effective in the flotation of oxide ores.
  • the oxide minerals which can be treated by the practice of this invention include carbonates, sulfates and silicates as well as oxides.
  • the anionic collectors in the flotation process of this invention are also effective in the flotation of sulfide ores and mixed oxide/sulfide ores.
  • Non-limiting examples of oxide ores which can be floated using the practice of this invention preferably include iron oxides, nickel oxides, phosphorus oxides, copper oxides and titanium oxides.
  • Other types of oxygen-containing minerals which can be floated using the practice of this invention include carbonates such as calcite or dolomite and hydroxides such as bauxite.
  • sulfide ores which can be floated by the process of this invention include those containing chalcopyrite, chalcocite, galena, pyrite, sphalerite and pentlandite.
  • Noble metals such as gold and silver and the platinum group metals wherein platinum group metals comprise platinum, ruthenium, rhodium, palladium, osmium, and iridium, can also be recovered by the practice of this invention.
  • such metals are sometimes found associated with oxide and/or sulfide ores.
  • platinum is sometimes found associated with troilite.
  • such metals can be recovered in good yield.
  • Non-limiting examples of oxide ores which can be subjected to froth flotation using the process of this invention are those including cassiterite, hematite, cuprite, vallerite, calcite, talc, kaolin, apatite, dolomite, bauxite, spinel, corundum, laterite, azurite, rutile, magnetite, columbite, ilmenite, smithsonite, anglesite, scheelite, chromite, cerussite, pyrolusite, malachite, chrysocolla, zincite, massicot, bixbyite, anatase, brookite, tungstite, uraninite, gummite, brucite, manganite, psilomelane, goethite, limonite, chrysoberyl, microlite, tantalite and samarskite.
  • oxide ores wherein oxide is defined to include carbonates, hydroxides, sulfates and silicates as well as oxides and sulfide ores.
  • Ores for which the process of this invention using anionic thiol collectors are useful include sulfide mineral ores containing copper, zinc, molybdenum, cobalt, nickel, lead, arsenic, silver, chromium, gold, platinum, uranium and mixtures thereof.
  • metal-containing sulfide minerals which can be concentrated by froth flotation using the composition and process of this invention include copper-bearing minerals such as covellite (CuS), chalcocite (Cu2S), chalcopyrite (CuFeS2), bornite (Cu5FeS4), vallerite (Cu2Fe4S7 or Cu3Fe4S7), tetrahedrite (Cu3SbS2), enargite (Cu3(As2Sb)S4), tennantite (Cu12As4S13), cubanite (Cu2SFe4S5), brochantite (Cu4(OH)6SO4), antlerite (Cu3SO4(OH)4), famatinite (Cu3(SbAs)S4), and bournonite (PbCuSbS3); lead-bearing minerals such as galena (PbS); antimony-bearing minerals such as stibnite (Sb2S3); zinc
  • Preferred metal-containing sulfide minerals include molybdenite (MoS2), chalcopyrite (CuFeS2), chalcocite (Cu2S), galena (Pbs), sphalerite (ZnS), bornite (Cu5FeS4), and pentlandite [(FeNi)9S8].
  • Sulfidized metal-containing oxide minerals are minerals which are treated with a sulfidization chemical, so as to give such minerals sulfide mineral characteristics. The minerals so treated can then be recovered in froth flotation using collectors which recover sulfide minerals. Sulfidization results in oxide minerals having sulfide mineral characteristics. Oxide minerals are sulfidized by contact with compounds which react with the minerals to form a sulfur bond or affinity. Such methods are well known in the art. Such compounds include sodium hydrosulfide, sulfuric acid and related sulfur-containing salts such as sodium sulfide.
  • Sulfidized metal-containing oxide minerals and oxide minerals for which this process utilizing the thiol collectors described below is useful include oxide minerals containing copper, aluminum, iron, titanium, magnesium, chromium, tungsten, molybdenum, manganese, tin, uranium, and mixtures thereof.
  • metal-containing minerals which may be sulfidized by froth flotation using the thiol collectors described below include copper-bearing minerals such as malachite (Cu2(OH)2CO3), azurite (Cu3(OH)2(CO3)2), cuprite (Cu2O), atacamite (Cu2Cl(OH)3), tenorite (CuO), chrysocolla (CuSiO3); aluminum-bearing minerals such as corundum; zinc-containing minerals such as zincite (ZnO) and smithsonite (ZnCO3); tungsten-bearing minerals such as wolframite [(Fe2Mn)WO4]; nickel-bearing minerals such as bunsenite (NiO); molybdenum-bearing minerals such as wulfenite (PbMoO4) and powellite (CaMoO4); iron-containing minerals such as hematite and magnetite; chromium-
  • metal-containing minerals for which the use of thiol collectors in this process is useful include gold-bearing minerals such as sylvanite (AuAgTe2) and calaverite (AuTe); platinum- and palladium-bearing minerals such as sperrylite (PtAs2); and silver-bearing minerals such as hessite (AgTe2). Also included are metals which occur in a metallic state, e.g., gold, silver and copper.
  • copper-containing sulfide minerals, nickel-containing sulfide minerals, lead-containing sulfide minerals, zinc-containing sulfide minerals or molybdenum ⁇ containing sulfide minerals are recovered.
  • a copper-containing sulfide mineral is recovered.
  • Ores do not always exist purely as oxide ores or as sulfide ores. Ores occurring in nature may comprise both sulfur-containing and oxygen-containing minerals as well as, in some cases, noble metals. Metals may be recovered from the oxides found in such ores by the practice of this invention. This may be done in a two-stage flotation where one stage comprises conventional sulfide flotation to recover primarily sulfide minerals and the other stage of the flotation utilizes the process of the present invention using the anionic collectors described below to recover primarily the oxide minerals. Alternatively, the various types of minerals may be recovered simultaneously by the practice of this invention.
  • the flotation process of this invention is useful in the flotation of oxides and sulfides from other sources.
  • the waste materials from various processes such as heavy media separation, magnetic separation, metal working and petroleum processing often contain oxides and/or sulfides that may be recovered using the flotation process of the present invention.
  • anionic collectors are useful in the practice of the present invention.
  • the anionic portion of the anionic collector is preferably derived from carboxylic, sulfonic, sulfuric, phosphoric or phosphonic acids.
  • the anionic collector is also hydrophobic. Its hydrophobicity is derived from a saturated or unsaturated hydrocarbyl or saturated or unsaturated substituted hydrocarbyl moiety. Examples of suitable hydrocarbyl moieties include straight or branched alkyl, arylalkyl and alkylaryl groups. Non-limiting examples of substituents for the hydrocarbyl group include alkoxy, ether, amino, hydroxy and carboxy. When the hydrocarbyl moiety is unsaturated, it is preferably ethylenically unsaturated. It should also be recognized that the anionic surfactant may be a mixture of compounds.
  • the anionic collector may be used in acid form or in salt form, depending on which is soluble under conditions of use.
  • the appropriate form of the anionic collector will vary depending on the particular collector used and other conditions present in the flotation process.
  • the anionic collectors useful in the present invention will be soluble in the acid form under conditions of use while others will be soluble in the salt form.
  • oleic acid is preferably used in the acid form and saturated carboxylic acids are preferably used in salt form.
  • the counter ion may be a calcium ion, a magnesium ion, a sodium ion, a potassium ion or an ammonium ion.
  • the choice of an appropriate counter ion depends on the particular anionic collector used and its solubility. It is generally preferred that the counter ion be a sodium ion, a potassium ion or an ammonium ion.
  • Non-limiting examples of suitable anionic collectors include linolenic acid, oleic acid, lauric acid, linoleic acid, octanoic acid, capric acid, myristic acid, palmitic acid, stearic acid, arachidic acid, behenic acid, 2-naphthalene sulfonic acid, sodium lauryl sulfate, sodium stearate, dodecane sodium sulfonic acid, hexadecyl sulfonic acid, dodecyl sodium sulfate, dodecyl phosphate, chloride derivative of dodecyl phosphonic acid, 2-naphthoic acid, pimelic acid, and dodecyl benzene sulfonate and mixtures thereof.
  • Preferred anionic collectors include those derived from carboxylic acids and sulfonic acids.
  • the anionic surfactants derived from carboxylic acids the unsaturated acids such as oleic acid, linoleic acid and linolenic acids or mixtures thereof are preferred. Examples of mixtures of these carboxylic acids include tall oil and coconut oil.
  • the anionic collector is derived from sulfonic acids
  • alkyl or alkylaryl sulfonic acids examples include dodecyl benzene sulfonic acid, dodecyl sulfonic acid, alkylated diphenyl oxide monosulfonic acid and salts thereof.
  • the thiol collectors of this invention are compounds selected from the group consisting of thiocarbonates, thionocarbamates, thiocarbanilides, thiophosphates, thiophosphinates, mercaptans, xanthogen formates, xanthic esters and mixtures thereof.
  • Preferred thiocarbonates are the alkyl thiocarbonates represented by the structural formula: wherein R1 is independently a C1 ⁇ 20, preferably C2 ⁇ 16, more preferably C3 ⁇ 12 alkyl group; Z1 and Z2 are independently a sulfur or oxygen atom; and M+ is an alkali metal cation.
  • the compounds represented by this formula include the alkyl thiocarbonates (both Z1 and Z2 are oxygen), alkyl dithiocarbonates (Z1 is O, Z2 is S) and the alkyl trithiocarbonates (both Z1 and Z2 are sulfur).
  • alkyl monothiocarbonates examples include sodium ethyl monothiocarbonate, sodium isopropyl monothiocarbonate, sodium isobutyl monothiocarbonate, sodium amyl monothiocarbonate, potassium ethyl monothiocarbonate, potassium isopropyl monothiocarbonate, potassium isobutyl monothiocarbonate and potassium amyl monothiocarbonate.
  • Preferred alkyl dithiocarbonates include potassium ethyl dithiocarbonate, sodium ethyl dithiocarbonate, potassium amyl dithiocarbonate, sodium amyl dithiocarbonate, potassium isopropyl dithiocarbonate, sodium isopropyl dithiocarbonate, sodium sec-butyl dithiocarbonate, potassium sec-butyl dithiocarbonate, sodium isobutyl dithiocarbonate, potassium isobutyl dithiocarbonate, and the like.
  • alkyl trithiocarbonates include sodium isobutyl trithiocarbonate and potassium isobutyl trithiocarbonate. It is often preferred to employ a mixture of an alkyl monothiocarbonate, alkyl dithiocarbonate and alkyl trithiocarbonate.
  • Preferred thionocarbamates correspond to the formula: wherein each R2 is independently a C1 ⁇ 10, preferably a C1 ⁇ 4, more preferably a C1 ⁇ 3, alkyl group; Y is -S ⁇ M+ or -OR3, wherein R3 is a C1 ⁇ 10, preferably a C2 ⁇ 6, more preferably a C3 ⁇ 4, alkyl group; a is the integer 1 or 2; and b is the integer 0 or 1, wherein a+b must equal 2.
  • Examples of preferred dialkyl dithiocarbamates include methyl butyl dithiocarbamate, methyl isobutyl dithiocarbamate, methyl sec-butyl dithiocarbamate, methyl propyl dithiocarbamate, methyl isopropyl dithiocarbamate, ethyl butyl dithiocarbamate, ethyl isobutyl dithiocarbamate, ethyl sec-butyl dithiocarbamate, ethyl propyl dithiocarbamate, and ethyl isopropyl dithiocarbamate.
  • alkyl thionocarbamates examples include N-methyl butyl thionocarbamate, N-methyl isobutyl thionocarbamate, N-methyl sec-butyl thionocarbamate, N-methyl propyl thionocarbamate, N-methyl isopropyl thionocarbamate, N-ethyl butyl thionocarbamate, N-ethyl isobutyl thionocarbamate, N-ethyl sec-butyl thionocarbamate, N-ethyl propyl thionocarbamate, and N-ethyl isopropyl thionocarbamate.
  • N-ethyl isopropyl thionocarbamate and N-ethyl isobutyl thionocarbamate are most preferred.
  • Thiophosphates useful herein generally correspond to the formula: wherein each R4 is independently hydrogen or a C1 ⁇ 10 alkyl, preferably a C2 ⁇ 8 alkyl, or an aryl, preferably an aryl group having from 6-10 carbon atoms, more preferably cresyl; Z is oxygen or sulfur; and M is an alkali metal cation.
  • thiophosphates those preferably employed include the monoalkyl dithiophosphates (one R4 is hydrogen and the other R4 is a C1 ⁇ 10 alkyl and Z is S), dialkyl dithiophosphates (both R4 are C1 ⁇ 10 alkyl and Z is S) and dialkyl monothiophosphate (both R4 are a C1 ⁇ 10 alkyl and Z is O).
  • Examples of preferred monoalkyl dithiophosphates include ethyl dithiophosphate, propyl dithiophosphate, isopropyl dithiophosphate, butyl dithiophosphate, sec-butyl dithiophosphate, and isobutyl dithiophosphate.
  • Examples of dialkyl or aryl dithiophosphates include sodium diethyl dithiophosphate, sodium di-sec-butyl dithiophosphate, sodium diisobutyl dithiophosphate, and sodium diisoamyl dithiophosphate.
  • Preferred monothiophosphates include sodium diethyl monothiophosphate, sodium di-sec-butyl monothiophosphate, sodium diisobutyl monothiophosphate, and sodium diisoamyl monothiophosphate.
  • Thiocarbanilides (dialkyl thioureas) are represented by the general structural formula: wherein each R5 is individually H or a C1 ⁇ 6, preferably a C1 ⁇ 3, hydrocarbyl.
  • Thiophosphinates are represented by the general structural formula: wherein M+ is as hereinbefore described and each R6 is independently an alkyl or aryl group, preferably an alkyl group having from 1 to 12, more preferably an alkyl group having from 1 to 8 carbon atoms. Most preferably, each R6 is isobutyl.
  • Mercaptan collectors are preferably alkyl mercaptans represented by the general structural formula: R7-S-H wherein R7 is an alkyl group, preferably an alkyl group having at least 10, more preferably from 10 to 16, carbon atoms.
  • Xanthogen formates are represented by the general structural formula: wherein R8 is an alkyl group having from 1 to 7, preferably from 2 to 6 carbon atoms and R9 is an alkyl group having 1 to 6, preferably 2 to 4, more preferably 2 or 3, carbon atoms.
  • Xanthic esters are preferably compounds of the general structural formula: wherein R10 is an allyl group and R11 is an alkyl group having from 1 to 7 carbon atoms.
  • Preferred thiol compounds for use as a collector are the thiocarbonates, thionocarbamates and the thiophosphates due to the surprisingly high recoveries and selectivities towards mineral values which can be achieved.
  • the thiol collectors described above are particularly useful in the flotation of sulfide minerals or sulfidized oxide minerals.
  • the other anionic collectors described above are useful in the flotation of certain sulfide minerals, but are also surprisingly useful in the flotation of oxide minerals.
  • the hydroxy-containing compounds useful in the practice of this invention comprises compounds containing at least one -OH moiety.
  • This hydroxy compound is selected to be essentially non-frothing under the conditions of use.
  • non-frothing compounds are those which have minimal frothing action under the conditions of use.
  • their frother power generally increases with the number of carbon atoms in the alcohol up to about six or seven. When the number of carbon atoms reaches this point, the effectiveness of the alcohol as a frother drops.
  • monohydric alcohols such as octanol, nonanol, decanol, undecanol and dodecanol may be useful as non-frothing hydroxy-containing compounds.
  • Laboratory scale flotation work using relatively pure water has shown that these alcohols may be non-frothing and useful in the practice of this invention.
  • these alcohols demonstrate sufficient frothing so that their use is not preferred.
  • the hydroxy-containing compound used in the practice of this invention is ethanolamine, propanolamine, butanolamine, lactic acid, glycolic acid, beta-hydroxy-l-propane sulfonic acid, ethylene glycol, diethylene glycol, glycerol, trihydroxybenzoic acid, hydroxybenzoic acid, butylene glycol, ditbutylene glycol, diethanolamine, dipropanolamine, tripropanolamine, triethanolamine or a simple sugar alcohol such as sucrose, glucose or dextrose, or a mixture of two or more thereof.
  • the hydroxy-containing compounds is ethanol amine, propanol amine, butanol amine, diethanol amine, dipropanol amine, tripropanol amine, triethanol amine or a mixture of two or more thereof.
  • the alkanol amines useful in the practice of this invention are available commercially. As will be recognized by one skilled in the art, commercially available alkanol amines will have varying degress of purity. For example, diethanol amine may contain varying amounts of ethanol amine and/or triethanol amine. Such alkanol amines are suitable in the practice of the present invention.
  • the hydroxy-containing compounds may be added directly to the float cell or may be added to the grinding stage. The preferred time of addition will vary depending on the particular ore bing floated, the other reagents present and the processing system being used.
  • the hydroxy-containing compounds are not pre-mixed with the collector prior to addition to the flotation process. They are preferably added to the flotation system separately from the collector. They are also preferably added prior to the addition of the collector. For example, the hydroxy-containing compounds may be added to the grinding stage.
  • the collector can be used in any concentration which gives the desired recovery of the desired metal values.
  • concentration used is dependent upon the particular mineral to be recovered, the grade of the ore to be subjected to the froth flotation process and the desired quality of the mineral to be recovered. Additional factors to be considered in determining dosage levels include the amount of surface area of the ore to be treated. As will be recognized by one skilled in the art, the smaller the particle size, the greater the amount of collector reagents needed to obtain adequate recoveries and grades.
  • the concentration of the collector is at least about 0.001 kg/metric ton, more preferably at least about 0.005 kg/metric ton. It is also preferred that the total concentration of the collector is no greater than about 5.0 kg/metric ton and more preferred that it is no greater than about 2.5 kg/metric ton. It is more preferred that the concentration of the collector is at least about 0.005 kg/metric ton and no greater than about 0.100 kg/metric ton. It is generally preferred to start at the lower concentration range and gradually increase the concentration to obtain optimum performance.
  • the concentration of the hydroxy-containing compounds useful in this invention is preferably at least about 0.001 kg/metric ton and no greater than about 5.0 kg/metric ton. A more preferred concentration is at least about 0.005 kg/metric ton and no more than about 0.500 kg/metric ton. As discussed above, it is generally preferred to start at the lower concentration range and gradually increase the concentration to obtain optimum performance. This is particularly important when thiol collectors are used in the flotation of sulfide minerals since the general trend is that selectivity is increased at the expense of overall recovery.
  • stage addition it is meant that a part of the total collector dose is added; froth concentrate is collected; an additional portion of the collector is added; and froth concentrate is again collected. This staged addition can be repeated several times to obtain optimum recovery and grade.
  • the number of stages in which the collector is added is limited only by practical and economic constraints. Preferably, no more than about six stages are used.
  • frothers may be and preferably are also used. Frothers are well-known in the art and reference thereto is made for the purposes of this invention. Non-limiting examples of useful frothers include C5 ⁇ 8 alcohols, pine oils, cresols, C1 ⁇ 6 alkyl ethers of polypropylene glycols, dihyroxylates of polypropylene glycols, glycol fatty acids, soaps, alkylaryl sulfonates and mixtures thereof.
  • anionic collectors When anionic collectors are used, pH is believed to play a role in the flotation process.
  • the nature of the anionic collectors of the present invention is related to the charge characteristics of the particular oxide mineral to be recovered. Thus, pH plays an important role in the froth flotation process of the present invention. While not wishing to be bound by any particular theory, it is assumed that the anionic collector attaches to the oxide at least in part through charge interaction with the mineral surface. Thus, pH conditions under which the charge of the oxide mineral is suitable for attachment are required in the practice of this invention.
  • the pH in flotation systems may be controlled by various methods known to one skilled in the art.
  • a common reagent used to control pH is lime.
  • reagents such as potassium hydroxide, sodium hydroxide and sodium carbonate and other reagents having monovalent cations to regulate pH.
  • Reagents having divalent cations such as magnesium hydroxide and calcium hydroxide may be used, but are not preferred since their use results in the need to use larger dosages of the collector.
  • the anionic collector is derived from sulfonic and sulfuric acids, the presence of divalent and/or metal cations is not as detrimental.
  • Hallimond tube flotation is a simple way to screen collectors, but does not necessarily predict the success of collectors in actual flotation. Hallimond tube flotation does not involve the shear or agitation present in actual flotation and does not measure the effect of frothers. Thus, while a collector must be effective in a Hallimond tube flotation if it is to be effective in actual flotation, a collector effective in Hallimond tube flotation will not necessarily be effective in actual flotation. It should also be noted that experience has shown that collector dosages required to obtain satisfactory recoveries in a Hallimond tube are often substantially higher than those required in a flotation cell test. Thus, the Hallimond tube work cannot precisely predict dosages that would be required in an actual flotation cell.
  • the effect of various collectors on the flotation of copper was determined using a Hallimond tube.
  • About 1.1 g of (1) malachite, a copper oxide mineral having the approximate formula Cu2CO3(OH)2, or (2) silica was sized to about -60 to +120 U.S. mesh and placed in a small bottle with about 20 ml of deionized water. The mixture was shaken 30 seconds and then the water phase containing some suspended fine solids or slimes was decanted. This desliming step was repeated several times.
  • a 150-ml portion of deionized water was placed in a 250-ml glass beaker. Next, 2.0 ml of a 0.10 molar solution of potassium nitrate was added as a buffer electrolyte. The pH was adjusted to about 10.0 with the addition of 0.10 N HCl and/or 0.10 N NaOH. Next, a 1.0-g portion of the deslimed mineral was added along with deionized water to bring the total volume to about 180 ml. The collector and hydroxy-containing compound, as identified in the various runs reported in Table I below, were added and allowed to condition with stirring for 15 minutes. The pH was monitored and adjusted as necessary.
  • the slurry was transferred into a Hallimond tube designed to allow a hollow needle to be fitted at the base of the 180-ml tube. After the addition of the slurry to the Hallimond tube, a vacuum of 5 in (12.7 cm) of mercury was applied to the opening of the tube for a period of 10 minutes. This vacuum allowed air bubbles to enter the tube through the hollow needle inserted at the base of the tube. During flotation, the slurry was agitated with a magnetic stirrer set at 200 revolutions per minute (RPM).
  • RPM revolutions per minute
  • the floated and unfloated material was filtered out of the slurry and oven dried at 100°C. Each portion was weighed. After each test, all equipment was washed with concentrated HCl and rinsed with 0.10 N NaOH and deionized water before the next run.
  • Example 2 The procedure outlined for Example 1 is followed with the exception that chrysocolla (Cu2H2Si2O5(OH)4) is used in place of malachite. In addition, in some cases different collectors and hydroxy-containing compounds are used. The results obtained are set out in Table II following.
  • the resulting pulp was next deslimed.
  • the pulp was placed in a flotation cell.
  • the cell was filled with water, the slurry pH adjusted to 9.2 with sodium carbonate and then stirred for 5 minutes.
  • the solids in the cell were allowed to settle for 120 seconds and then the water phase containing finely divided solids was decanted. This process was repeated four times.
  • This deslimed pulp was used in Run 8. In Runs 1-7, the desliming steps were omitted.
  • the pulp was transferred to a 1500-ml Agitair Flotation cell outfitted with an automatic paddle removal system.
  • the pH of the slurry was adjusted to 9.2 by the addition of sodium carbonate, if necessary.
  • the collectors and hydroxy-containing compounds specified in Table III were added separately to the slurry in the amounts specified in Table III and the slurry was allowed to condition for one minute after the addition of each.
  • a polyglycol ether frother in the amount of 40 g per ton of dry ore, was then added and the slurry allowed to condition for one additional minute.
  • the flotation cell was agitated at 1150 RPM and air introduced at a rate of 4.5 liters per minute. Samples of the froth concentrate were collected at 1.0 and 6.0-minute intervals after the air was first introduced into the cell. Samples of the tailings and concentrate were dried, weighed, and pulverized for analysis. After being pulverized, they were dissolved with the use of acid and the copper content determined using a DC Plasma spectrometer. The assay data was used to determine fractional recoveries and grades using standard mass balance formulas.
  • a series of samples containing 500 g of ore from Central Africa were prepared. The ore contained greater than 90 percent chrysocolla and the remainder comprised additional copper oxide minerals and gangue.
  • a 500-g sample was ground with 257 g of deionized water in a rod mill at about 60 RPM for six minutes. The resulting pulp was transferred to an Agitair 1500 ml flotation cell outfitted with an automated paddle removal system. The pH of the slurry was adjusted by the addition of either sodium carbonate or HCl. The natural ore pH in slurry form was 7.8. After addition of the hydroxy-containing compounds as shown in Table IV, the slurry was allowed to condition for one minute. The collector was then added followed by an additional minute of conditioning. A polyglycol ether frother was added in an amount of 20 g per ton of dry ore followed by an additional minute of conditioning.
  • the float cell was agitated at 1150 RPM and air is introduced at a rate of 4.5 liters per minute.
  • Samples of the froth concentrate were collected at 1.0 and 6.0 minute intervals after the air was first introduced.
  • the samples of the concentrates and the tailings were dried, weighed, pulverized for analysis and dissolved with the use of acid.
  • the copper content was determined by the use of DC Plasma Spectrometer. Using the assay data, fractional recoveries and grades were calculated using standard mass balance formulas. The results obtained are shown in Table IV following.
  • Table IV generally demonstrates the effectiveness of the collector composition of the present invention. Run 2 approximates current industry standards.
  • a series of 600-g samples of iron oxide ore from Michigan were prepared.
  • the ore contained a mixture of hematite, martite, goethite and magnetite mineral species.
  • Each 600-g sample was ground along with 400 g of deionized water in a rod mill at about 60 RPM for 10 minutes.
  • the resulting pulp was transferred to an Agitair 3000 ml flotation cell outfitted with an automated paddle removal system.
  • the pH of the slurry was adjusted from a natural pH of 7.3 to a pH of 8.5 using sodium carbonate.
  • the hydroxy-containing compound, if used, was added and the slurry allowed to condition for one minute. This was followed by the addition of the collector, followed by an additional minute of conditioning.
  • an amount of a polyglycol ether frother equivalent to 40 g per ton of dry ore was added followed by another minute of conditioning.
  • the float cell was agitated at 900 RPM and air introduced at a rate of 9.0 liters per minute.
  • Samples of the froth concentrate were collected at 1.0 and 6.0 minutes after the start of the air flow.
  • Samples of the froth concentrate and the tailings were dried, weighed and pulverized for analysis. They were then dissolved in acid, and the iron content determined by the use of a D.C. Plasma Spectrometer. Using the assay data, the fractional recoveries and grades were calculated using standard mass balance formulas. The results are shown in Table V following.
  • a series of 30-g samples of -60 mesh copper ore from Arizona were prepared. It should be noted that this ore is very fine and, thus, very difficult to float.
  • the make-up of the valuable components of the ore was about 60 percent azurite [Cu3(CO3)(OH)2], 35 percent malachite [Cu2CO3(OH)2], and 5 percent chalcocite [Cu2S].
  • Each sample of ore was ground with 15 g of deionized water in a rod mill (2.5 inch diameter with 0.5 inch rods)(6.35 cm dia. with 1.27 cm rods) for 240 revolutions. The resulting pulp was transferred to a 300 ml flotation cell.
  • the pH of the slurry was left at natural ore pH of 8.0 unless otherwise noted. After addition of the hydroxy-containing compound as shown in Table VI, the slurry was allowed to condition for one minute. Next, the collector was added with an additional minute of conditioning. Next, the frother, a polyglycol ether, was added in an amount equivalent to 0.050 g per ton of dry ore and the slurry allowed to condition an additional minute.
  • the float cell was agitated at 1800 RPM and air introduced at a rate of 2.7 liters per minute.
  • Samples of the froth concentrate were collected by standard hand paddling at 1.0 and 6.0 minutes after the start of the introduction of air into the cell.
  • Samples of the concentrate and the tailings were dried and analyzed as described in the previous examples. The results obtained are presented in Table VI following.
  • Table VI demonstrates the effectiveness of the collector composition of the present invention in the flotation of difficult to float Arizona copper oxide ore.
  • a series of 30-g samples of -10 mesh copper ore from Canada were prepared.
  • the make-up of the valuable portion of the ore was approximately 50 percent malachite [Cu2CO3(OH)2] and 50 percent chalcopyrite [CuFeS2].
  • Each sample was ground along with 15 grams of deionized water in a rod mill (2.5 inch diameter with 0.5 inch rods) for 1000 revolutions.
  • the resulting pulp was transferred to a 300 ml flotation cell.
  • the pH of the slurry was adjusted to 9.0 by the addition of sodium carbonate.
  • the hydroxy-containing compound, collector and frother were added as described in the previous examples.
  • a series of 30-g samples of a -10 mesh mixture of corundum (Al2O3) and silica (SiO2) were prepared. Each sample was ground and transferred to a 300 ml flotation cell as described in Example 7 with the exception that the sample was ground 2000 revolutions. The pH of the slurry was left at the natural pH of 7.4. Collector, hydroxy compound and frother were added and the float cell operated as described in Example 7. Samples were obtained as described in Example 7 and were dried, weighed, pulverized and the aluminum content determined by X-ray fluorescence. The results obtained are shown in Table VIII following.
  • Example 1 The general procedure described in Example 1 were followed with the exception that various oxide ores were used in place of the copper ore of Example 1. The results obtained are shown in Table IX following.
  • This example demonstrates the efficacy of the present invention in floating a broad range of oxide and sulfide minerals. Also demonstrated is the ability to distinguish these various minerals from silica, the major gangue constituent found with these minerals in natural ores.
  • This example used the general Hallimond tube procedure outlined in Example 1 except that instead of using only pure mineral specimens in each run, a specific test consisted of running a pre-mixed sample of 10 percent malachite (or 10 percent chrysocolla) along with 90 percent silica. Copper assays were performed on flotation concentrate and flotation tailings using the acid dissolution procedure and D.C. plasma spectrometry as discussed in Example 3. The results are shown in Table Xa for malachite and Table Xb for chrysocolla. All runs were determined at a pH of 10.0 with the collector dosages as indicated.
  • the pulp was transferred to a 1500-ml Agitair Flotation cell outfitted with an automatic paddle removal system.
  • the cell was agitated at 1150 RPM.
  • The, pH of the slurry adjusted to 8.5 by the addition of additional lime, if necessary.
  • the collector potassium amyl xanthate, unless specified otherwise in Table XIII, was added to the slurry at a dosage of 8 g per ton and the slurry allowed to condition for one minute.
  • a polyglycol ether frother in the amount of 18 g per ton of dry ore, was then added and the slurry allowed to condition for one additional minute.
  • the flotation cell was agitated at 1150 RPM and air introduced at a rate of 4.5 liters per minute. Samples of the froth concentrate were collected for a period of eight minutes after the air was first introduced into the cell. These samples of the tailings and concentrate were dried overnight in an oven, weighed, and pulverized for analysis. After being pulverized, they were dissolved with the use of acid and the copper content determined using a DC Plasma spectrometer. The assay data was used to determine fractional recoveries and grades using standard mass balance formulas. The recoveries represent the fractional amount of the specified mineral present that was recovered. Selectivity was determined by dividing the copper recovery by the silica gangue recovery.
  • a series of 30-g samples of mixed copper sulfide ore from Nevada were prepared.
  • the make-up of the valuable components of the ore was about 0.25 weight percent copper, about 0.004 weight percent molybdenum and about 4 g/metric ton gold.
  • Each sample of ore was ground dry for about 20 seconds in a swing mill to about 12 percent greater than 100 mesh. The resulting ore was transferred to a 300 ml flotation cell and diluted with water.
  • the pH of the slurry was adjusted to 8.5 with lime.
  • the alkanol amine as specified in Table XIV was added and the slurry allowed to condition for one minute.
  • a first portion of the collector, sodium isopropyl xanthate, (0.050 kg/metric ton of ore) was added with an additional minute of conditioning.
  • the frother, a polyglycol ether was added in an amount equivalent to 0.020 g per ton of dry ore and the slurry allowed to condition an additional minute.
  • the float cell was agitated at 1800 RPM and air introduced at a rate of 2.7 liters per minute. Samples of the froth concentrate were collected by standard hand paddling at 2.0 minutes after the start of the introduction of air into the cell. Next, a second dose of collector (0.025 kg/metric ton of ore) was added with one minute of conditioning and a six minute concentrate collected. Samples of the concentrate and the tailings were combined and then dried and analyzed as described in the previous examples. The results obtained are presented in Table XIV following. In each case, the copper, gold, molybdenum and silica recoveries represent the total amount recovered at the 2 and 6 minute intervals.
  • Example 13 The general procedure outlined in Example 13 was followed using a southern Africa mixed sulfide/oxide copper ore.
  • the sulfide copper ore was floated by the practice of this invention and the remaining oxide ore recovered in a subsequent step such as leaching or oxide flotation.
  • the sulfide minerals contained in this ore was quite small, less than about 0.22 weight percent of the total ore.
  • Example 13 One modification to the procedure outlined in Example 13 was that the ore was ground for 700 revolutions to produce a size distribution of 13 percent greater than 100 mesh.
  • the collector used was potassium amyl xanthate at a concentration of 0.025 kg/metric ton of ore.
  • the alkanol amine used was diethanol amine in the amounts specified. The results obtained are shown in Table XV following.
  • Example 6 The procedure outlined in Example 6 was followed with the exception that the apatite used was from a different source and contained about 30 percent apatite and about 70 percent silica.
  • the hydroxy-containing compound used in each case was diethanol amine and the anionic collector oleic acid.
  • the manner in which the diethanol amine and oleic acid were added to the flotation system varied.
  • diethanol amine was added to the cell and allowed to condition for one minute. This was followed by the addition of the oleic acid followed by an additional minute of conditioning.
  • Run 2 the order of addition is reversed.
  • diethanol amine and oleic acid were each added to the cell at the same time and in approximately the same physical location and allowed to condition for one minute.
  • Runs 1-3 embodiments of this invention clearly demonstrate its effectiveness.
  • Run 4 shows that when the components of the invention are pre-mixed, the recovery of phosphorus obtained is substantially less than when oleic acid is used alone.
  • Run 5 shows that a fatty acid/diethanol amine condensate is ineffective in this process.

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EP90304633A 1990-04-19 1990-04-27 Drücken von Kieselsäure oder siliziumgehaltiger Gangart bei Erzflotation Expired - Lifetime EP0453677B1 (de)

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CA002014882A CA2014882C (en) 1990-04-19 1990-04-19 Depression of the flotation of silica or siliceous gangue in mineral flotation
DE69021553T DE69021553D1 (de) 1990-04-19 1990-04-27 Drücken von Kieselsäure oder siliziumgehaltiger Gangart bei Erzflotation.
EP90304633A EP0453677B1 (de) 1990-04-19 1990-04-27 Drücken von Kieselsäure oder siliziumgehaltiger Gangart bei Erzflotation
AU54774/90A AU619979B2 (en) 1990-04-19 1990-05-07 Depression of the flotation of silica or siliceous gangue in mineral flotation
ZA903531A ZA903531B (en) 1990-04-19 1990-05-09 Depression of the flotation of silica or siliceous gangue in mineral flotation
FR9005770A FR2661844B1 (fr) 1990-04-19 1990-05-09 Abaissement de la flottation de la silice ou d'une gangue siliceuse dans la flottation de minerais.
CN90102733A CN1056445A (zh) 1990-04-19 1990-05-11 矿物浮选过程中抑制硅石或含硅脉石浮选的方法

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CA002014882A CA2014882C (en) 1990-04-19 1990-04-19 Depression of the flotation of silica or siliceous gangue in mineral flotation
EP90304633A EP0453677B1 (de) 1990-04-19 1990-04-27 Drücken von Kieselsäure oder siliziumgehaltiger Gangart bei Erzflotation
ZA903531A ZA903531B (en) 1990-04-19 1990-05-09 Depression of the flotation of silica or siliceous gangue in mineral flotation
CN90102733A CN1056445A (zh) 1990-04-19 1990-05-11 矿物浮选过程中抑制硅石或含硅脉石浮选的方法

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SOVIET INVENTIONS ILLUSTRATED, week 8533, 26th September 1985, no. 85=201864/33, Derwent Publications Ltd, london, GB; & SU-A-1135 497 (BELORUSS KIROV TECHN. INS.) 23-01-1985 *
SOVIET INVENTIONS ILLUSTRATED, week 8806, 11th February 1988, no. 88-041129/06, Derwent Publications Ltd, London, GB; & SU-A-1318 302 (LENINGRAD PLEKHANOV MINE) 23-06-1987 *
SOVIET INVENTIONS ILLUSTRATED, week B46, 2nd January 1980, no. 83749B/46, Derwent Publications Ltd, London, GB; & SU-A-649 469 (NON-FERRORE ENRICH) 08-02-1979 *

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0520739A3 (de) * 1991-06-24 1994-03-30 Dow Chemical Co
WO2016162344A1 (en) * 2015-04-09 2016-10-13 Akzo Nobel Chemicals International B.V. Collector composition for reverse flotation

Also Published As

Publication number Publication date
DE69021553D1 (de) 1995-09-14
CA2014882C (en) 1996-02-20
CA2014882A1 (en) 1991-10-19
FR2661844B1 (fr) 1993-10-29
AU5477490A (en) 1991-11-07
CN1056445A (zh) 1991-11-27
FR2661844A1 (fr) 1991-11-15
AU619979B2 (en) 1992-02-06
ZA903531B (en) 1992-01-29
EP0453677B1 (de) 1995-08-09

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