US3078996A - Method of improving recovery of mineral values from ores - Google Patents

Method of improving recovery of mineral values from ores Download PDF

Info

Publication number
US3078996A
US3078996A US668820A US66882057A US3078996A US 3078996 A US3078996 A US 3078996A US 668820 A US668820 A US 668820A US 66882057 A US66882057 A US 66882057A US 3078996 A US3078996 A US 3078996A
Authority
US
United States
Prior art keywords
flotation
solids
slurry
chlorine
amine
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
US668820A
Inventor
Robert E Snow
Fred N Oberg
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
International Minerals and Chemical Corp
Original Assignee
International Minerals and Chemical Corp
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by International Minerals and Chemical Corp filed Critical International Minerals and Chemical Corp
Priority to US668820A priority Critical patent/US3078996A/en
Application granted granted Critical
Publication of US3078996A publication Critical patent/US3078996A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

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
    • B03D1/01—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
    • B03D2201/06—Depressants
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S209/00—Classifying, separating, and assorting solids
    • Y10S209/902—Froth flotation; phosphate

Definitions

  • This invention relates to the bencficiation of phosphate ores. More particularly, it relates to the treatment of the products of flotation with nitrogenous positive ion agents to render them susceptible to further processing. Still more particularly, it relates to a method of removing aliphatic amine reagents from flotation products.
  • Florida phosphate ore is generally beneficiated by flotation of the 35 +150 mesh standard screen size particles produced by the classification and screening, washing, and desliming treatments of phosphate matrix.
  • a slurry of the particles is admixed with negative ion agents such as tall oil, oleic acid and the like, and subjected to agitation and aeration in one or more flotation operations; the first operation generally being designated as a rougher separation and the concentrates therefrom being refloated in so-called cleaner and recleaner flotation operations.
  • preciable phosphate is floated off with the silica in a product which, while a relatively'small portion of the total ore being processed, i.e., 10 to nevertheless carries a high percentage, 10 to 30% BPL, to waste if the silica tail is not further processed.
  • this silica product In order to be able to recycle this silica product to recover its phosphate con-' tent, it is necessary to remove the nitrogenous positive ion agent. Sulfuric acid, while effective to remove fatty acid reagent, is relatively ineffective to remove the nitrogenous positive ion agents.
  • Slimes and clays of -150 mesh particle size have been shown to be moderately elfective in removing the nitrogen-bearing reagents permitting further processing to recover the heavy minerals and additional phosphate, but require large desliming and washing facilities.
  • nitrogenous positive ion reagents are removed from reagentized solid particles or degradated to the point of ineffectiveness by agitation of an aqueous slurry of reagentized particles in the pres ence of a halogen or halogens.
  • the flotation product bearing nitroge truly positive ion reagent thereon, is contacted by mixing into the slurry, water having chlorine in solution or by bubbling gaseous chlorine directly into the flotation operation products.
  • the froth product of the amine flotation product comprising silica, phosphate material, and heavy minerals, passes by launder to an accumulator, usually a sump. If water containing chlorine in solution is mixed with this accumulated slurry, the diluted slurry is thickened in a hydroseparator or equivalent apparatus, the reagent being removed in the discard or wash water.
  • the solids after water washing may be recycled to a fatty acid flotation stepwhere the feed corresponds in B PL content to the recycle material, as for example, to the rougher flotation operation.
  • halogen which effectively destroy the' hydrophobic amine coating range from about 0.15 pound to about 0.45 pound per ton of solids in the slurry mass although amounts outside this range may housed under special operating conditions. It will be recognized that various halogens have different solu-bilities in water, i.e., chlorine water is saturated at 28 C. with about 0.57% chlorine while bromine can be raised to about 3%, and that plant solutions should be kept at lower halogen concentrations.
  • the solids content of the slurry may vary from about 30% to 60% solids with 45 to 55% being considered as a good operative range. Agitation of the pulp is generally carried out for 3 to 5 minutes although the time is not too critical if subsequent processing, such as a reflotation, is to be employed. During the agitating a gaseous halogen may also be bubbled through the aqueous slurry mixture containing previously introduced halogen.
  • Example 1 Florida phosphate matrix was subjected to classification, desliming, washing, and screening operations in accordance with standard phosphate operating procedures to produce a 35 mesh flotation feed.
  • the flotation feed was subjected to amine flotation in a Denver cell at approximately 25% solids content using 1.4 pounds of Alamac 26 and 2 pounds of kerosene per ton of ore.
  • the silica float product, or so-called amine tail was divided into three fractions, A, B, and C.
  • each slurry was dewatered by decanta tion and the solids fed to a Denver flotation cell without adding reagents so as to determine the amount of solids refloata-ble upon agitation and aeration.
  • the flotation feed cited in Example I was subjected as flotation using tall oil, kerosene, fuel oil and caustic soda and the phosphate concentrate obtained thereby was scrubbed with sulfuric acid to remove the reagents.
  • the washed concentrate was reagentized With a mixture of about 73% m-onooctadecyl amine and about 24% monohexadecyl amine in the form of the acetic acid addition salt.
  • This reagentized concentrate in slurry form was subjected to a flotation operation in a Fagergren machine at approximately 30% solids content to recover a phosphate concentrate of approximately 77% BPL and a silica float product.
  • the amine flotation tail was divided into four fractions, A, B, C, and D. To these fractions were added 0.14 pound, 0.27 pound, 0.48 pound, and 1.20 pounds of chlorine per ton of tail solids and each fraction was agitated at 50% solids by vigorous stirring for three minutes.
  • each slurry was dewatered by decantation and the solids fed to a Denver flotation cell without adding reagents so as to determine the amount of solids refloatable upon agitation and aeration.
  • Example 111 A silica froth product overflowing from the amine flotation cells of the phosphate flotation circuit described in Example II assayed as follows: 22.1% BPL, 69.5% insoluble.
  • This silica froth product which was a slurry of about 50% solids content, was dewatered to a solids content of about 70% and to the resultant slurry was added water and an amount of chlorine corresponding to approximately 1.2 pounds of chlorine per ton of solids.
  • the slurry mixture was agitated for three minutes at 50% solids with a Lightning mixer, and then the solids were dewatered by 'decantation.
  • the dereagentized solids were converted to an aque ous pulp of about 60% solids content and reagentized with about 3.6 pounds of a reagent mixture comprising 25% tall oil, 25 kerosene, and 50% fuel oil per ton .of solids treated. Suflicient caustic soda was added to give the mixture a pH of between about 8.2 and 8.6.
  • the reagentized pulp was diluted to about 30% solids content and subjected to a single flotation operation in a Denver flotation machine.
  • slurry at least one halogen selected from the group consisting of chlorine and bromine, agitating the mixture and washing the solids.
  • the method of dereagentizing products obtained by flotation of finely divided ore with amine flotation agents which comprises preparing an aqueous slurry of said product of about 30 to 60% solids content, adding to said slurry at least one halogen selected from the group consisting of chlorine and bromine, agitating the mixture three to five minutes and washing the solids.
  • the method of dereagentizing products obtained by flotation of finely divided ore with amine flotation agents which comprises preparing an aqueous slurry of said product of about 30 to 60% solids content, adding to said slurry between about 0.15 pound and 0.45 pound of at least one halogen selected from the group consisting of chlorine and bromine per ton of solids being treated, agitating the mixture and washing the solids.
  • the method of dereagentizing products obtained by flotation of finely divided ore with amine flotation agents which comprises preparing an aqueous slurry of said product of about 30 to 60% solids content, adding to said slurry at least one halogen selected from the group consisting of chlorine and bromine, agitating an aqueous slurry of reagentized solids and bubbling at least one gaseous halogen selected from the group consisting of chlorine and bromine thercthrough, and washing the solids.
  • the method of dereagentizing products obtained by flotation of finely divided ore with amine flotation agents which comprises preparing an aqueous slurry of said product of about 30 to 60% solids content, introducing into said aqueous slurry gaseous chlorine, in quantities less than that required for saturation, agitating the mixture and washing the solids.
  • the method of dcreagentizing products obtained by flotation of finely divided ore with an amine flotation agent which comprises preparing an aqueous slurry of said product of from about 30 to about 60% solids content, agitating said aqueous slurry and bubbling at least one halogen selected from the group consisting of chlorine and bromine therethrough, and washing the solids.
  • the method which comprises dereagentizing reagentized solids obtained by flotation of materials with a nitrogenous positive ion flotation reagent selected from the group consisting of amines, amine-acid salts and mixtures thereof by agitating an aqueous slurry of said reagentized solids in the presence of at least one halogen selected from the group consisting of chlorine and bromine.
  • a nitrogenous positive ion flotation reagent selected from the group consisting of amines, amine-acid salts and mixtures thereof by agitating an aqueous slurry of said reagentized solids in the presence of at least one halogen selected from the group consisting of chlorine and bromine.
  • a method which comprises dereagentizing a reagentized silica float product obtained in a flotation beneflciation of phosphatic ore with a nitrogenous positive ion flotation reagent selected from the group consisting of amines, amine-acid salts and mixtures thereof by agitating an aqueous slurry of said reagentized silica float product in the presence of at least one halogen selected from the group consisting of chlorine and bromine.

Description

United States Patent Office 3,078,996 Patented Feb. 26, 1963 3,078,996 MEN-D OF fltdPROViNG RECOVERY OF MINERAL VALUES FROM ORES Robert E. Snow and Fred N. Oberg, Lalreland, Fla, as-
signors to international Minerals & Chemical Corporation, a corporation of New York No Drawing. Filed lune 28, 1957, Ser. No. 668,820
8 Claims. (Cl. 209166) This invention relates to the bencficiation of phosphate ores. More particularly, it relates to the treatment of the products of flotation with nitrogenous positive ion agents to render them susceptible to further processing. Still more particularly, it relates to a method of removing aliphatic amine reagents from flotation products.
Florida phosphate ore is generally beneficiated by flotation of the 35 +150 mesh standard screen size particles produced by the classification and screening, washing, and desliming treatments of phosphate matrix. In these well-known flotation operations, a slurry of the particles is admixed with negative ion agents such as tall oil, oleic acid and the like, and subjected to agitation and aeration in one or more flotation operations; the first operation generally being designated as a rougher separation and the concentrates therefrom being refloated in so-called cleaner and recleaner flotation operations.
Current practice in some phosphate, feldspar, and other beneficiation plants is to further upgrade the concentrates obtained by flotation with negative ion agents, through flotation with positive ion agents having an affinity for silica, such as the high molecular weight aliphatic amines containing an alkyl group or groups of twenty carbon atoms and their water soluble addition salts With acids. In the positive ion agent flotation, the silica and other gangue materials such as heavy minerals are overflowed in a froth and the phosphate is obtained as an underflow product.
While this method floats off the minor component (silica),
the separation is not highly selective and. ap-
preciable phosphate is floated off with the silica in a product which, while a relatively'small portion of the total ore being processed, i.e., 10 to nevertheless carries a high percentage, 10 to 30% BPL, to waste if the silica tail is not further processed. In order to be able to recycle this silica product to recover its phosphate con-' tent, it is necessary to remove the nitrogenous positive ion agent. Sulfuric acid, while effective to remove fatty acid reagent, is relatively ineffective to remove the nitrogenous positive ion agents. Slimes and clays of -150 mesh particle size have been shown to be moderately elfective in removing the nitrogen-bearing reagents permitting further processing to recover the heavy minerals and additional phosphate, but require large desliming and washing facilities.
It is a primary object of this invention to provide a method wherein nitrogenous positive ion reagents are removed from flotation products in a highly effective manner.
It is another object to provide a method of removing nitrogeneous positive ion reagent without addition of special equipment for handling the operation.
Now it has been discovered that nitrogenous positive ion reagents are removed from reagentized solid particles or degradated to the point of ineffectiveness by agitation of an aqueous slurry of reagentized particles in the pres ence of a halogen or halogens.
More in detail, the flotation product, bearing nitroge nous positive ion reagent thereon, is contacted by mixing into the slurry, water having chlorine in solution or by bubbling gaseous chlorine directly into the flotation operation products.
Generally, the froth product of the amine flotation product comprising silica, phosphate material, and heavy minerals, passes by launder to an accumulator, usually a sump. If water containing chlorine in solution is mixed with this accumulated slurry, the diluted slurry is thickened in a hydroseparator or equivalent apparatus, the reagent being removed in the discard or wash water.
It is not necessary, however, to eliminate the products of the reaction of amine reagent and halogen from contact with the solids before the solids can be further processed. If gaseous chlorine is bubbled through the slurry in the accumulator, the solids after water washing may be recycled to a fatty acid flotation stepwhere the feed corresponds in B PL content to the recycle material, as for example, to the rougher flotation operation.
The amount of halogen required varies. somewhat depending upon the amount of nitrogenous positive ion agent being used. v
In general, utilizing chlorine or bromine, amounts of halogen which effectively destroy the' hydrophobic amine coating range from about 0.15 pound to about 0.45 pound per ton of solids in the slurry mass although amounts outside this range may housed under special operating conditions. It will be recognized that various halogens have different solu-bilities in water, i.e., chlorine water is saturated at 28 C. with about 0.57% chlorine while bromine can be raised to about 3%, and that plant solutions should be kept at lower halogen concentrations.
When agitating the slurry mixture containing introduced halogen, the solids content of the slurry may vary from about 30% to 60% solids with 45 to 55% being considered as a good operative range. Agitation of the pulp is generally carried out for 3 to 5 minutes although the time is not too critical if subsequent processing, such as a reflotation, is to be employed. During the agitating a gaseous halogen may also be bubbled through the aqueous slurry mixture containing previously introduced halogen.
The invention will be further understood from a study of the following examples which are given by way of illustration and without any intention that the invention be limited thereto.
1 Example 1 Florida phosphate matrix was subjected to classification, desliming, washing, and screening operations in accordance with standard phosphate operating procedures to produce a 35 mesh flotation feed.
The flotation feed was subjected to amine flotation in a Denver cell at approximately 25% solids content using 1.4 pounds of Alamac 26 and 2 pounds of kerosene per ton of ore. The silica float product, or so-called amine tail, was divided into three fractions, A, B, and C.
To these fractions were added 0.08 pound, 0.14 pound, and 0.17 pound of chlorine per ton of tail solids and each fraction was agitated at 50% solids by vigorous stirring for three minutes.
After agitation, each slurry was dewatered by decanta tion and the solids fed to a Denver flotation cell without adding reagents so as to determine the amount of solids refloata-ble upon agitation and aeration.
Results were as follows:
The flotation feed cited in Example I was subjected as flotation using tall oil, kerosene, fuel oil and caustic soda and the phosphate concentrate obtained thereby was scrubbed with sulfuric acid to remove the reagents.
The washed concentrate was reagentized With a mixture of about 73% m-onooctadecyl amine and about 24% monohexadecyl amine in the form of the acetic acid addition salt. This reagentized concentrate in slurry form was subjected to a flotation operation in a Fagergren machine at approximately 30% solids content to recover a phosphate concentrate of approximately 77% BPL and a silica float product.
The amine flotation tail was divided into four fractions, A, B, C, and D. To these fractions were added 0.14 pound, 0.27 pound, 0.48 pound, and 1.20 pounds of chlorine per ton of tail solids and each fraction was agitated at 50% solids by vigorous stirring for three minutes.
After agitation, each slurry was dewatered by decantation and the solids fed to a Denver flotation cell without adding reagents so as to determine the amount of solids refloatable upon agitation and aeration.
Results were as follows: i
Example 111 A silica froth product overflowing from the amine flotation cells of the phosphate flotation circuit described in Example II assayed as follows: 22.1% BPL, 69.5% insoluble.
This silica froth product, which was a slurry of about 50% solids content, was dewatered to a solids content of about 70% and to the resultant slurry was added water and an amount of chlorine corresponding to approximately 1.2 pounds of chlorine per ton of solids. The slurry mixture was agitated for three minutes at 50% solids with a Lightning mixer, and then the solids were dewatered by 'decantation.
The dereagentized solids were converted to an aque ous pulp of about 60% solids content and reagentized with about 3.6 pounds of a reagent mixture comprising 25% tall oil, 25 kerosene, and 50% fuel oil per ton .of solids treated. Suflicient caustic soda was added to give the mixture a pH of between about 8.2 and 8.6.
The reagentized pulp was diluted to about 30% solids content and subjected to a single flotation operation in a Denver flotation machine.
Results were as follows:
Percent Percent Percent BIL Iusol. Heavy Minerals Feed 2-2. 06 69. 53 5. 46 T 11 8. 16 87. 58 0. 23 33. 39 54. 83 9. 73
slurry at least one halogen selected from the group consisting of chlorine and bromine, agitating the mixture and washing the solids.
2. The method of dereagentizing products obtained by flotation of finely divided ore with amine flotation agents which comprises preparing an aqueous slurry of said product of about 30 to 60% solids content, adding to said slurry at least one halogen selected from the group consisting of chlorine and bromine, agitating the mixture three to five minutes and washing the solids.
3. The method of dereagentizing products obtained by flotation of finely divided ore with amine flotation agents which comprises preparing an aqueous slurry of said product of about 30 to 60% solids content, adding to said slurry between about 0.15 pound and 0.45 pound of at least one halogen selected from the group consisting of chlorine and bromine per ton of solids being treated, agitating the mixture and washing the solids.
4. The method of dereagentizing products obtained by flotation of finely divided ore with amine flotation agents which comprises preparing an aqueous slurry of said product of about 30 to 60% solids content, adding to said slurry at least one halogen selected from the group consisting of chlorine and bromine, agitating an aqueous slurry of reagentized solids and bubbling at least one gaseous halogen selected from the group consisting of chlorine and bromine thercthrough, and washing the solids.
5. The method of dereagentizing products obtained by flotation of finely divided ore with amine flotation agents which comprises preparing an aqueous slurry of said product of about 30 to 60% solids content, introducing into said aqueous slurry gaseous chlorine, in quantities less than that required for saturation, agitating the mixture and washing the solids.
6. The method of dcreagentizing products obtained by flotation of finely divided ore with an amine flotation agent which comprises preparing an aqueous slurry of said product of from about 30 to about 60% solids content, agitating said aqueous slurry and bubbling at least one halogen selected from the group consisting of chlorine and bromine therethrough, and washing the solids.
7. The method which comprises dereagentizing reagentized solids obtained by flotation of materials with a nitrogenous positive ion flotation reagent selected from the group consisting of amines, amine-acid salts and mixtures thereof by agitating an aqueous slurry of said reagentized solids in the presence of at least one halogen selected from the group consisting of chlorine and bromine.
8. A method which comprises dereagentizing a reagentized silica float product obtained in a flotation beneflciation of phosphatic ore with a nitrogenous positive ion flotation reagent selected from the group consisting of amines, amine-acid salts and mixtures thereof by agitating an aqueous slurry of said reagentized silica float product in the presence of at least one halogen selected from the group consisting of chlorine and bromine.
References Cited in the file of this patent UNITED STATES PATENTS pages 1216-1218.

Claims (1)

1. THE METHOD OF DEREAGENTIZING PRODUCTS OBTAINED BY FLOTATION OF FINELY DIVIDED ORE WITH AMINE FLOTATION AGENTS WHICH COMPRISES PREPARING AN AQUEOUS SLURRY OF SAID PRODUCT OF ABOUT 30 TO 60% SOLIDS CONTENT, ADDING TO SAID SLURRY AT LEAST ONE HALOGEN SELECTED FROM THE GROUP CONSISTING OF CHLORINE AND BROMINE, AGITATING THE MIXTURE AND WASHING THE SOLDDS.
US668820A 1957-06-28 1957-06-28 Method of improving recovery of mineral values from ores Expired - Lifetime US3078996A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US668820A US3078996A (en) 1957-06-28 1957-06-28 Method of improving recovery of mineral values from ores

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US668820A US3078996A (en) 1957-06-28 1957-06-28 Method of improving recovery of mineral values from ores

Publications (1)

Publication Number Publication Date
US3078996A true US3078996A (en) 1963-02-26

Family

ID=24683868

Family Applications (1)

Application Number Title Priority Date Filing Date
US668820A Expired - Lifetime US3078996A (en) 1957-06-28 1957-06-28 Method of improving recovery of mineral values from ores

Country Status (1)

Country Link
US (1) US3078996A (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20150174588A1 (en) * 2013-12-20 2015-06-25 Chemtreat, Inc. Methods for facilitating mineral extraction

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2195724A (en) * 1938-08-24 1940-04-02 Antoine M Gaudin Process of ore concentration
US2559104A (en) * 1948-03-23 1951-07-03 Phelps Dodge Corp Flotation recovery of molybdenite
US2614692A (en) * 1948-06-08 1952-10-21 Int Minerals & Chem Corp Recovery of metallic minerals from phosphate-silica ores containing minor amounts of the metallic minerals
US2922522A (en) * 1957-06-28 1960-01-26 Int Minerals & Chem Corp Method of recovering mineral values from ore

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2195724A (en) * 1938-08-24 1940-04-02 Antoine M Gaudin Process of ore concentration
US2559104A (en) * 1948-03-23 1951-07-03 Phelps Dodge Corp Flotation recovery of molybdenite
US2614692A (en) * 1948-06-08 1952-10-21 Int Minerals & Chem Corp Recovery of metallic minerals from phosphate-silica ores containing minor amounts of the metallic minerals
US2922522A (en) * 1957-06-28 1960-01-26 Int Minerals & Chem Corp Method of recovering mineral values from ore

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20150174588A1 (en) * 2013-12-20 2015-06-25 Chemtreat, Inc. Methods for facilitating mineral extraction
US9889452B2 (en) * 2013-12-20 2018-02-13 Chemtreat, Inc. Methods for facilitating mineral extraction

Similar Documents

Publication Publication Date Title
US2293640A (en) Process of concentrating phosphate minerals
US4098687A (en) Beneficiation of lithium ores by froth flotation
US4256227A (en) Froth flotation method for recovering metal values from their ores by thiourea or substituted thiourea
US3259242A (en) Beneficiation of apatite-calcite ores
US3314537A (en) Treatment of phosphate rock slimes
US2195724A (en) Process of ore concentration
US4192737A (en) Froth flotation of insoluble slimes from sylvinite ores
US2231265A (en) Process of ore concentration
US4737273A (en) Flotation process for recovery of phosphate values from ore
US2753997A (en) Concentration of phosphate minerals
US3902602A (en) Froth flotation method for recovery of minerals
US2312387A (en) Froth flotation of acidic minerals
US3331505A (en) Flotation process for reagent removal
US3078996A (en) Method of improving recovery of mineral values from ores
US3037627A (en) Method of beneficiating sulfide and oxide ores of copper, manganese, lead and zinc
US6685027B2 (en) Method of concentrating phosphates from their ores
US3469693A (en) Beneficiation of ores by froth flotation using sulfosuccinamates
US2970688A (en) Method for recovery of minerals
US4253614A (en) Flotation of non-sulfide zinc materials
US3259326A (en) Method of slime beneficiation
US2922522A (en) Method of recovering mineral values from ore
US2811254A (en) Method for the beneficiation of phosphate ores
US3454159A (en) Phosphate flotation
US2682337A (en) Froth flotation of phosphate values involving ph control
US3454161A (en) Froth flotation of complex zinc-tin ore