US2105807A - Differential concentration of non - Google Patents
Differential concentration of non Download PDFInfo
- Publication number
- US2105807A US2105807A US2105807DA US2105807A US 2105807 A US2105807 A US 2105807A US 2105807D A US2105807D A US 2105807DA US 2105807 A US2105807 A US 2105807A
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- US
- United States
- Prior art keywords
- silica
- concentrate
- fluorspar
- calcite
- phosphate
- 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.)
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- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 43
- 239000012141 concentrate Substances 0.000 description 35
- 239000000377 silicon dioxide Substances 0.000 description 35
- 239000010436 fluorite Substances 0.000 description 21
- 229910019142 PO4 Inorganic materials 0.000 description 17
- 239000010452 phosphate Substances 0.000 description 17
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 17
- 239000000463 material Substances 0.000 description 14
- 238000000034 method Methods 0.000 description 14
- 239000003795 chemical substances by application Substances 0.000 description 13
- 239000003921 oil Substances 0.000 description 13
- 235000019198 oils Nutrition 0.000 description 12
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 10
- 235000014113 dietary fatty acids Nutrition 0.000 description 10
- 239000000194 fatty acid Substances 0.000 description 10
- 229930195729 fatty acid Natural products 0.000 description 10
- 150000004665 fatty acids Chemical class 0.000 description 10
- 239000000295 fuel oil Substances 0.000 description 10
- 239000007787 solid Substances 0.000 description 10
- WRIDQFICGBMAFQ-UHFFFAOYSA-N (E)-8-Octadecenoic acid Natural products CCCCCCCCCC=CCCCCCCC(O)=O WRIDQFICGBMAFQ-UHFFFAOYSA-N 0.000 description 7
- LQJBNNIYVWPHFW-UHFFFAOYSA-N 20:1omega9c fatty acid Natural products CCCCCCCCCCC=CCCCCCCCC(O)=O LQJBNNIYVWPHFW-UHFFFAOYSA-N 0.000 description 7
- QSBYPNXLFMSGKH-UHFFFAOYSA-N 9-Heptadecensaeure Natural products CCCCCCCC=CCCCCCCCC(O)=O QSBYPNXLFMSGKH-UHFFFAOYSA-N 0.000 description 7
- 229910021532 Calcite Inorganic materials 0.000 description 7
- 239000005642 Oleic acid Substances 0.000 description 7
- ZQPPMHVWECSIRJ-UHFFFAOYSA-N Oleic acid Natural products CCCCCCCCC=CCCCCCCCC(O)=O ZQPPMHVWECSIRJ-UHFFFAOYSA-N 0.000 description 7
- 239000003513 alkali Substances 0.000 description 7
- 238000005188 flotation Methods 0.000 description 7
- QXJSBBXBKPUZAA-UHFFFAOYSA-N isooleic acid Natural products CCCCCCCC=CCCCCCCCCC(O)=O QXJSBBXBKPUZAA-UHFFFAOYSA-N 0.000 description 7
- ZQPPMHVWECSIRJ-KTKRTIGZSA-N oleic acid Chemical compound CCCCCCCC\C=C/CCCCCCCC(O)=O ZQPPMHVWECSIRJ-KTKRTIGZSA-N 0.000 description 7
- 239000002245 particle Substances 0.000 description 7
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- 238000013019 agitation Methods 0.000 description 6
- TZCXTZWJZNENPQ-UHFFFAOYSA-L barium sulfate Chemical compound [Ba+2].[O-]S([O-])(=O)=O TZCXTZWJZNENPQ-UHFFFAOYSA-L 0.000 description 6
- 239000010428 baryte Substances 0.000 description 6
- 229910052601 baryte Inorganic materials 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 229910000019 calcium carbonate Inorganic materials 0.000 description 5
- 235000021588 free fatty acids Nutrition 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- 238000010908 decantation Methods 0.000 description 4
- 229910052500 inorganic mineral Inorganic materials 0.000 description 4
- 239000011707 mineral Substances 0.000 description 4
- 235000010755 mineral Nutrition 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- WUKWITHWXAAZEY-UHFFFAOYSA-L calcium difluoride Chemical compound [F-].[F-].[Ca+2] WUKWITHWXAAZEY-UHFFFAOYSA-L 0.000 description 3
- 239000003153 chemical reaction reagent Substances 0.000 description 3
- 239000000344 soap Substances 0.000 description 3
- RSWGJHLUYNHPMX-UHFFFAOYSA-N Abietic-Saeure Natural products C12CCC(C(C)C)=CC2=CCC2C1(C)CCCC2(C)C(O)=O RSWGJHLUYNHPMX-UHFFFAOYSA-N 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 2
- KRHYYFGTRYWZRS-UHFFFAOYSA-N Fluorane Chemical compound F KRHYYFGTRYWZRS-UHFFFAOYSA-N 0.000 description 2
- 235000019738 Limestone Nutrition 0.000 description 2
- KHPCPRHQVVSZAH-HUOMCSJISA-N Rosin Natural products O(C/C=C/c1ccccc1)[C@H]1[C@H](O)[C@@H](O)[C@@H](O)[C@@H](CO)O1 KHPCPRHQVVSZAH-HUOMCSJISA-N 0.000 description 2
- BCKXLBQYZLBQEK-KVVVOXFISA-M Sodium oleate Chemical compound [Na+].CCCCCCCC\C=C/CCCCCCCC([O-])=O BCKXLBQYZLBQEK-KVVVOXFISA-M 0.000 description 2
- 229910001634 calcium fluoride Inorganic materials 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 235000021323 fish oil Nutrition 0.000 description 2
- 238000009291 froth flotation Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000006028 limestone Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000010665 pine oil Substances 0.000 description 2
- 235000011121 sodium hydroxide Nutrition 0.000 description 2
- KHPCPRHQVVSZAH-UHFFFAOYSA-N trans-cinnamyl beta-D-glucopyranoside Natural products OC1C(O)C(O)C(CO)OC1OCC=CC1=CC=CC=C1 KHPCPRHQVVSZAH-UHFFFAOYSA-N 0.000 description 2
- 241001165050 Ocala Species 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000001143 conditioned effect Effects 0.000 description 1
- 239000008396 flotation agent Substances 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- -1 oleic acid Chemical class 0.000 description 1
- 239000011435 rock Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
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
- B03D1/02—Froth-flotation processes
- B03D1/06—Froth-flotation processes differential
-
- 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
Definitions
- the present invention relates in general to a concentration of non-metallic minerals from their ores, and more particularly to a process of differential concentration applicable to ores of the class consisting of phosphate-calcite-silica ores, fluorspar-calcite-silica ores, and fluorsparbarite-silica ores.
- a pulp of the ore to undergo treatment is agitated in the 9 presence of a fraction of one per cent of a free fatty acid and a fraction of one per cent of a substantially insoluble and unsaponiflable 011, without added agents capable of substantially affecting its pH value, the desired concentrate 5 being subsequently separated by froth flotation or other manner known in the art.
- Either phosphate or fluorspar can thus be separated from both calcite and silica; and fluorspar can be separated from both barite and calcite. It has 35 also been found possible to separate calcite from silica by the process of the present invention.
- the ore for treatment by the 35 process of the present invention In preparing the ore for treatment by the 35 process of the present invention, it is ordinarily first subjected to a preliminary grinding operation and is thereafter screened or classified to remove all particles other than those desired.
- the undersize may then he deslimed and the 40 oversize reground, deslimed, and added to the deslimed undersize; or the oversize may be reground, added to the undeslimed undersize, and the whole then deslimed.
- the deslimed pulp was thickened to contain 72% solids, and then there was added during further agitation- 0.28 pound of a solution of fish-oil fatty acids in an equal weight of fuel oil, enough more fuel oil to make a total of one pound of fuel oil, and 0.14 pound of a frothing agent consisting of three parts of crude rosin residue dissolved in one part of kerosene oil, all per ton of dry material present.
- the pulp showed a pH value of 7.4.
- the thick pulp was then diluted and agitated in the machine for the production of a froth over a period of three minutes, a rougher float concentrate being separated.
- the tailing was discarded and the rougher concentrate cleaned four times by reagitation without added agents.
- the tailing from each cleaning was assayed separately, but constituted a middling which, in commercial operations, could be returned to the flotation cells for additional recovery of values therefrom.
- fatty acids such as oleic acid
- oleic acid have also been found useful as reagents.
- Fluorspar carrying more than 2% of silica yields so much fluosilicic acid as to be useless for. the production of hydrofluoric acid.
- fluorspar containing upwards of 98% of calcium fluoride commands at least double the price of the spar carrying only 96% of calcium fluoride. It has hitherto proved impossible to produce a 98% fluorspar from the relatively impure material generally mined. According'to the present invention, by a suitable choice of reagents it has proved possible to obtain a satisfactory so-called acid spar, as shown by the example given above.
- the wet deslimed material in a pulp containing 72% of solids, was mixed with one pound of fuel oil, one pound of crude oleic acid (red oil) and 0.14 pound of the kerosene-rosin solution above identified. all per ton of. dry material present.
- the thick pulp was diluted and agitated in the flotation machine, and a rougher froth concentrate was separated. Upon removal of the talling, the rougher concentrate was put back into the machine and reagitated without added agents for two minutes, and thereafter a finished or cleaned concentrate was separated.
- the results are shown in the following table. in which the tailing from the cleaning operation is designated as a middling.
- the material thus conditioned was diluted and frothed to separate a small weight concentrate. richer in the carbonate and poorer in the phosphate.
- the remaining pulp was thickened and agitated with 0.2 pound of caustic soda, 4 pounds of fuel 011, 0.84 pound of crude oleic acid, and 0.14 pound of the frothing agent above referred to as Tarol No. 2, all per ton of solids, whereupon it was diluted, and a phosphate float concentrate separated.
- pulp of deslimed material was thickened to 72% solids and agitated with 0.5 pound of fuel 011, 0.19 pound of flsh-oil fatty acids, and 0.14 pound of the kerosene-rosin solution'above identifled, all per ton of flotation feed, whereupon it was diluted and a fluorspar float concentrate separated.
- the fluorspar rougher concentrate thus obtained was refloated four times, in each instance without the addition of further agents, to yield a finished concentrate of over 98% pm'ity, four cleaner tailings constituting middlings being obtained which, in commercial practice, would be retreated to yield further recoveries.
- the fluorspar finished concentrate contained over 86% of the fluorspar in the original material.
- the rougher tailing resulting from the first float was rethickened, agitated with 0.32 pound of caustic soda, 2 pounds of fuel oil, 0.45 pound of fish-oil fatty acid, and 0.14 pound of the kerosene-rosin solution above identified, all per ton of solids present, whereupon it was diluted and agitated to yield a barite rougher concentrate, a final tailing being also obtained.
- the barite rougher concentrate was refloated twice without added agents to yield a finished concentrate, as well as two cleaner tallings constituting middlings. The results are shown in the following table:
- the barite concentrate thus obtained maybe further treated to raise its grade. It will be noted that 86.1% of the original fluorspar was recovered in the form of a concentrate carrying 98.28% of fluorspar and conforming to the most exacting commercial demands.
- a process of differential concentration which comprises agitating a pulp, nearly free from slimes, of suitably divided particles of an ore of the class consisting of phosphate-calcite-silica ores, fluorspar-calcite-silica ores, and fluorsparbarite-silica ores, in the presence of a fraction of one per cent of a free fatty acid and a fraction of one per cent of a substantially insoluble and unsaponiflable oil, without added alkali or other agent capable of substantially aflecting its pH value; and separating in the case of a phosphatecalcite-silica ore a concentrate relatively rich in phosphate'and relatively poor in calcite-sllica, in the case of a fluorspar-calcite-silica ore a concentrate'relatively rich in fluorspar and relatively poor in calcite-silica, and in the case of a fluorspar-barite-silica on a concentrate relatively rich in fluorspar and relatively poor in baritesil
- a process of differential concentration which comprises agitating a pulp, nearly free from slimes, of suitably divided particles of an ore of the class consisting of phosphate-calcite-silica ores, fluorspar-calcite silica ores, and fluorsparbarite-silica ores, in the presence of a fraction of one per cent of a free fatty acid and a fracion of one per cent of a substantially insoluble and unsaponiflable oil, without added alkali or other agent capable of substantially aifecting its pH value; and separating by froth flotation in the case of a phosphate-calcite-silica ore a concentrate relatively rich in phosphate and relatively poor in calcite-silica, in the case of a fluorsparcalcite-silica ore a concentrate relatively rich in fluorspar and relatively poor in calcite-silica, and in the case of a fluorspar-barite-silica ore a concentrate relatively rich in fluorspar and relatively poor in
- a process of diflerential concentration which I comprises agitating a pulp, nearly free from slimes, of suitably divided particles of an ore of the class consisting of phosphate-calcite-sillca ores, fluorspar-calcite-silica ores, and fluorsparbarite-silica ores, in the presence of a fraction of one per cent of a free fatty 0010 and a fraction of one per cent of a substantiallynnsoluble and unsaponlflable oil.
- the fatty acid being carried in at least a part of the oil; and separating in the case of a phosphate-calcitesiiica ore a concentrate relatively rich in phosphate and relatively poor in calcite-silica, in the case of a fluorspar-calcitesilica ore a concentrate relatively rich in fluorspar and relatively poor in calcite-silica, and in the case of a fluorspar-barite-silica ore a concentrate relatively rich in fluorspar and relatively poor in barite-silica.
- a process of diflerential concentration comprising agitating a pulp, nearly free from slimes, of suitably divided particles of a phosphate-calcite-silica ore in the presence of a fraction of one per cent of a fatty acid soap and a fraction of one per cent of a substantially insoluble and unsaponiflable oil separating a float concentrate relatively rich in calcite and relatively poor in phosphate-silica: dewatering the remaining pulp;
- a process of differential concentration comprising agitating a pulp, nearly free from slimes, of suitably divided particles of a phosphate-calcite-silicaore in the presence of a fraction of one per cent of a free fatty acid and a fraction of one per cent of a substantially insoluble and unsaponiflable oil, without added alkali or other agent capable of substantially affecting its pH value: separating a small-weight float concentrate richer in calcite and poorer in phosphate; dewatering the remaining pulp; agitating the dewatered pulp in the presence of a fraction of one per cent of a fatty acid soap and a fraction of one per cent of a substantially insoluble and unsaponiflable oil: and separating a float concentrate relatively rich in phosphate and relatively poor in calcite- 7o
Description
Patented Jan. 18, 1938 DIITERENTIAL CONCENTRATION OI." NON- METALLIC MINERALS Arthur Crago, Mulberry, Fla., aalignor to Phosphate Recovery Corporatiom-New York, N. Y., a corporation of Delaware I No Drawing. Application February 15, 1933,
Serial No. 656,887
5 Claims.
The present invention relates in general to a concentration of non-metallic minerals from their ores, and more particularly to a process of differential concentration applicable to ores of the class consisting of phosphate-calcite-silica ores, fluorspar-calcite-silica ores, and fluorsparbarite-silica ores.
In accordance with the invention, a pulp of the ore to undergo treatment is agitated in the 9 presence of a fraction of one per cent of a free fatty acid and a fraction of one per cent of a substantially insoluble and unsaponiflable 011, without added agents capable of substantially affecting its pH value, the desired concentrate 5 being subsequently separated by froth flotation or other manner known in the art. By this procedure omitting the use of alkali or other pH-affecting substance, it has been found possible to differentially concentrate one non-metallic mineral withrespect to both another non-metallic mineral and siliceous gangue. Either phosphate or fluorspar can thus be separated from both calcite and silica; and fluorspar can be separated from both barite and calcite. It has 35 also been found possible to separate calcite from silica by the process of the present invention.
In order that the best results may be obtained by the process of the present invention, it has been found advisable to limit rather narrowly 30 the size of the ore particles subjected to the concentrating operation, as well as to largely deslime the ore pulp prior to its admixture with the reagents.
In preparing the ore for treatment by the 35 process of the present invention, it is ordinarily first subjected to a preliminary grinding operation and is thereafter screened or classified to remove all particles other than those desired. The undersize may then he deslimed and the 40 oversize reground, deslimed, and added to the deslimed undersize; or the oversize may be reground, added to the undeslimed undersize, and the whole then deslimed.
The procedures herein described in detail are 4 flotation procedures, but in many cases parallel results may be obtained by effecting the concentrating operation on a shaking table, the concentrate coming off at the side of the table as if it were the lighter material and the tailing at the 50 end as if it were the heavier material.
Other features and advantages will appear in connection with the examples described below.
Ground crude fluorspar ore from Hillside Fiuorspar Mines, Rosiclare, Illinois, with a 55 gangue principally of calcium carbonate, but
containing some silica, was screened through 35- mesh, the oversize being ground to pass 35-mesh and added to the undersize; The resulting mixture was agitated in a relatively large amount of 9 water to facilitate removal of the slimes, the
agitation being conducted in a subaeration-flotation laboratory testing machine, and the slimes removed by decantation. The deslimed pulp was thickened to contain 72% solids, and then there was added during further agitation- 0.28 pound of a solution of fish-oil fatty acids in an equal weight of fuel oil, enough more fuel oil to make a total of one pound of fuel oil, and 0.14 pound of a frothing agent consisting of three parts of crude rosin residue dissolved in one part of kerosene oil, all per ton of dry material present. The pulp showed a pH value of 7.4.
After three minutes agitation the thick pulp was then diluted and agitated in the machine for the production of a froth over a period of three minutes, a rougher float concentrate being separated. The tailing was discarded and the rougher concentrate cleaned four times by reagitation without added agents. The tailing from each cleaning was assayed separately, but constituted a middling which, in commercial operations, could be returned to the flotation cells for additional recovery of values therefrom.
The results are shown in the foliowingtable:
Percent Percent Percent Percent :g CaF: sic, 02.0 0. e
red
Feed 100. 0 52. 76 9. 11 37. 37 Finished cone. 32. 3 98. 38 0. l8 0. 88 60. 4 4th midd 2. 4 94. 48 0. 16 5.05 4. 3 3rd m1dd 3. 5 87. 54 0. 00 12.24 '5; 7
1st and 2d mlddl6. 4 51. 60 0. 51 47. 48 16. Tails 35. 10.02 23. 42 65. 57 6. 8 Slimes 10. 4 34. 64 7. 45 55. 29 6. 8
Other fatty acids, such as oleic acid, have also been found useful as reagents.
Fluorspar carrying more than 2% of silica yields so much fluosilicic acid as to be useless for. the production of hydrofluoric acid. As a result of this and other reasons, fluorspar containing upwards of 98% of calcium fluoride commands at least double the price of the spar carrying only 96% of calcium fluoride. It has hitherto proved impossible to produce a 98% fluorspar from the relatively impure material generally mined. According'to the present invention, by a suitable choice of reagents it has proved possible to obtain a satisfactory so-called acid spar, as shown by the example given above.
A phosphate ore from North Africa, known as Constantine rock, with a gangue largely of calcium carbonate, was raised from uncommercial grade to commercial grade by flotation with fuel oil and a soap-forming fatty acid. The ore was ground to pass a 35-mesh sieve, and deslimed by agitation with water and decanting the slimes.
The wet deslimed material, in a pulp containing 72% of solids, was mixed with one pound of fuel oil, one pound of crude oleic acid (red oil) and 0.14 pound of the kerosene-rosin solution above identified. all per ton of. dry material present. The thick pulp was diluted and agitated in the flotation machine, and a rougher froth concentrate was separated. Upon removal of the talling, the rougher concentrate was put back into the machine and reagitated without added agents for two minutes, and thereafter a finished or cleaned concentrate was separated. The results are shown in the following table. in which the tailing from the cleaning operation is designated as a middling.
cent B. P. L. 0000 Ins. recov- Wt. mm cry 56. I8 26. 8 s. 26 O. 70 14. 8 0. 99 72. 82. 9 68. 56 I. 7 l. 42 18.8 18. 0 17.66 66. 2 15.6! 1.0 15.4 E. 92 40. 6 19. 3 12. 2 8S. 1
It was found that better results were some times obtained when solid fatty acids of flsh oil. dissolved in part of the fuel oil, were substituted for the oleic acid.
By slightly varying conditions, it was found possible to float limestone away from silica. A mixture consisting of one part Ocala limestone, largely calcite, and about three parts of the tailings from a mill of the Phosphate Recovery Corporation treating Florida pebble phosphate, was screened through 24-rnesh, and the oversize ground to the same mesh and added to the undersize. The rmulting material was deslimed by agitation with water and decantation, and thickened to contain 70% solids. The thick pulp was agitated for three minutes with 2 pounds of fuel oil and 0.53 pound of crude oleic acid, both per ton of dry material present, the pH value of the pulp being 7.8. No bubble-forming agent or other added flotation agent was found necessary.
The oiled pulp was diluted and frothed in the flotation machine for one minute, during which a calcium carbonate float was separated. The results are shown in the following table:
Percent Area C 001 wt. 0008' reohvery The tailings were evidentlymostly silica, which was the principal ingredient of the phosphate tailings put into the original mixture.
Another lot of the same Constantine ore was around to pass 65-mesh, and deslimed by agita-' tion with water and decantatlon. The deslimed coarse material in a dilute pulp was. agitated with 1.20 pounds of sodium oleate and 0.1 pound of pine oil, both per ton of solids, and a carbonate float concentrate was flrst removed. The sodium oleate was of course a soap, produced from fatty acid and alkali. The tailing remaining was thickened and in this state agitatedwith 1 pound of fuel oil, 0.5 pound of crude oleic acid, and 0.14 pound of the kerosene-rosin solution above identlfled, all per ton of original solids in the deslimed pulp, whereupon it was diluted and a phosphate float concentrate removed.
Thedetailedresultsandasaaya arelhcwnln, the following table:
Per- 00.
B.P.L. Ins. 00 m use 141 11.51
10.67 1.21 sass 1.s 1a:
00.40 1.00 an 70.1 an
as 11114 11.10 a4 a1 sass 1am 11.00 1111 40.4
oassan 0.11: 042 40.0
can an; 7.0a 112.4 41.4
A lot of phosphate ore from Consolidated Inning and melting Co., of Trail, 3. 0., had to be ground to pass ZOO-mesh to free the silica gangue. The ore was then treated to remove part of a calcium carbonate gangue, whereupon a phosphate concentrate was separated. To eifeet these results the ground ore was deslimed by agitation with water and decantation. The deslimed material in the state of a thick pulp was agitated with 2.5 pounds of fuel oil, 0.84 pound of crude oleic acid, and 0.28 pound of Tarol No. 2 (a mixture of 75% steam distilled pine oil and rosin oil by volume), all per ton of deslimed solids. The material thus conditioned was diluted and frothed to separate a small weight concentrate. richer in the carbonate and poorer in the phosphate. The remaining pulp was thickened and agitated with 0.2 pound of caustic soda, 4 pounds of fuel 011, 0.84 pound of crude oleic acid, and 0.14 pound of the frothing agent above referred to as Tarol No. 2, all per ton of solids, whereupon it was diluted, and a phosphate float concentrate separated.
the following table:
B. P. L.
s ay-9w 88 382325 The foregoing procedure raised the B. P. L. content to a grade of commercial utility.
By a somewhat modified procedure fluorspar has been separated from barite. A table feed fluorspar ore carrying calcium carbonate, from Hillside Fluorspar Mines, Rosiclare, 111., was mixed with an equal weight of deslimed barite ore from Paga Mining Co., Cartersville, 6a., and the mixture ground to pass -mesl1. The ground material was deslimed by agitation for a threeminute period with water and decantation until all the slimes seemed to have been removed. The results of the desliming operation are shown in the following table:
pulp of deslimed material was thickened to 72% solids and agitated with 0.5 pound of fuel 011, 0.19 pound of flsh-oil fatty acids, and 0.14 pound of the kerosene-rosin solution'above identifled, all per ton of flotation feed, whereupon it was diluted and a fluorspar float concentrate separated. The fluorspar rougher concentrate thus obtained was refloated four times, in each instance without the addition of further agents, to yield a finished concentrate of over 98% pm'ity, four cleaner tailings constituting middlings being obtained which, in commercial practice, would be retreated to yield further recoveries. The fluorspar finished concentrate contained over 86% of the fluorspar in the original material. The rougher tailing resulting from the first float was rethickened, agitated with 0.32 pound of caustic soda, 2 pounds of fuel oil, 0.45 pound of fish-oil fatty acid, and 0.14 pound of the kerosene-rosin solution above identified, all per ton of solids present, whereupon it was diluted and agitated to yield a barite rougher concentrate, a final tailing being also obtained. The barite rougher concentrate was refloated twice without added agents to yield a finished concentrate, as well as two cleaner tallings constituting middlings. The results are shown in the following table:
am Percent of Pay. ya NOOVGI'Y Product :tnt
' Cal, 010, 0000 1311804 car, B01804 r000 100.0 20.10 20.10 10.10 21.40 1000 100.0 001 100110--.. 20.0 0020 0.00 1.00 0.10 2.0 0.1 Midd 0.4 00.01 0.42 21.01 4.04 1.0 01 Midd 1.0 0010 0.00 00.00 10.40 1.0 01 MidcLfl- 2.0 21.10 1.00 41.01 04.42 22 01 MiddJl- 0.0 4.00 4.10 41.00 40.00 1.0 10.0 30001 0 1 0 04.0 000 14.00 01.04 40.00 00 14.2 #2 0.4 000 01.00 0.02 0.10 01 0.0 M100.
#1--.- 00 020 00.04 000 004 00 00 Tall 10.0 0.40 0012 002 0.00 0.0 0.0
The barite concentrate thus obtained maybe further treated to raise its grade. It will be noted that 86.1% of the original fluorspar was recovered in the form of a concentrate carrying 98.28% of fluorspar and conforming to the most exacting commercial demands.
Having thus described certain embodiments of the invention, what is claimed is:
1. A process of differential concentration which comprises agitating a pulp, nearly free from slimes, of suitably divided particles of an ore of the class consisting of phosphate-calcite-silica ores, fluorspar-calcite-silica ores, and fluorsparbarite-silica ores, in the presence of a fraction of one per cent of a free fatty acid and a fraction of one per cent of a substantially insoluble and unsaponiflable oil, without added alkali or other agent capable of substantially aflecting its pH value; and separating in the case of a phosphatecalcite-silica ore a concentrate relatively rich in phosphate'and relatively poor in calcite-sllica, in the case of a fluorspar-calcite-silica ore a concentrate'relatively rich in fluorspar and relatively poor in calcite-silica, and in the case of a fluorspar-barite-silica on a concentrate relatively rich in fluorspar and relatively poor in baritesilica.
2. A process of differential concentration which comprises agitating a pulp, nearly free from slimes, of suitably divided particles of an ore of the class consisting of phosphate-calcite-silica ores, fluorspar-calcite silica ores, and fluorsparbarite-silica ores, in the presence of a fraction of one per cent of a free fatty acid and a fracion of one per cent of a substantially insoluble and unsaponiflable oil, without added alkali or other agent capable of substantially aifecting its pH value; and separating by froth flotation in the case of a phosphate-calcite-silica ore a concentrate relatively rich in phosphate and relatively poor in calcite-silica, in the case of a fluorsparcalcite-silica ore a concentrate relatively rich in fluorspar and relatively poor in calcite-silica, and in the case of a fluorspar-barite-silica ore a concentrate relatively rich in fluorspar and relatively poor in barite-silica.
3. A process of diflerential concentration which I comprises agitating a pulp, nearly free from slimes, of suitably divided particles of an ore of the class consisting of phosphate-calcite-sillca ores, fluorspar-calcite-silica ores, and fluorsparbarite-silica ores, in the presence of a fraction of one per cent of a free fatty 0010 and a fraction of one per cent of a substantiallynnsoluble and unsaponlflable oil. without added 'alkali or other agent capable of substantially affecting its pH value, the fatty acid being carried in at least a part of the oil; and separating in the case of a phosphate-calcitesiiica ore a concentrate relatively rich in phosphate and relatively poor in calcite-silica, in the case of a fluorspar-calcitesilica ore a concentrate relatively rich in fluorspar and relatively poor in calcite-silica, and in the case of a fluorspar-barite-silica ore a concentrate relatively rich in fluorspar and relatively poor in barite-silica.
4. A process of diflerential concentration comprising agitating a pulp, nearly free from slimes, of suitably divided particles of a phosphate-calcite-silica ore in the presence of a fraction of one per cent of a fatty acid soap and a fraction of one per cent of a substantially insoluble and unsaponiflable oil separating a float concentrate relatively rich in calcite and relatively poor in phosphate-silica: dewatering the remaining pulp;
agitating the dewatered pulp in the presence of a fraction of one per cent of a free fatty acid and a fraction of one per centof a substantially insoluble and unsaponiflable oil, without added alkali or other agent capable of substantially affecting its pH value; and separating a float concentrate relatively rich in phosphate and relatively poor in calcite-silica.
5. A process of differential concentration comprising agitating a pulp, nearly free from slimes, of suitably divided particles of a phosphate-calcite-silicaore in the presence of a fraction of one per cent of a free fatty acid and a fraction of one per cent of a substantially insoluble and unsaponiflable oil, without added alkali or other agent capable of substantially affecting its pH value: separating a small-weight float concentrate richer in calcite and poorer in phosphate; dewatering the remaining pulp; agitating the dewatered pulp in the presence of a fraction of one per cent of a fatty acid soap and a fraction of one per cent of a substantially insoluble and unsaponiflable oil: and separating a float concentrate relatively rich in phosphate and relatively poor in calcite- 7o
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US2105807A true US2105807A (en) | 1938-01-18 |
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US2105807D Expired - Lifetime US2105807A (en) | Differential concentration of non |
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Cited By (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
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 |
US3063561A (en) * | 1960-01-25 | 1962-11-13 | Int Minerals & Chem Corp | Beneficiation of ores |
US3259242A (en) * | 1962-11-29 | 1966-07-05 | Int Minerals & Chem Corp | Beneficiation of apatite-calcite ores |
US3534854A (en) * | 1967-11-20 | 1970-10-20 | Int Minerals & Chem Corp | Beneficiation of calcite-apatite-quartz ores |
US4008151A (en) * | 1973-10-29 | 1977-02-15 | Office Cherifien Des Phosphates | Process for enrichment, by flotation, of phosphate ores with gangues containing carbonates |
US4317715A (en) * | 1977-11-22 | 1982-03-02 | Outokumpu Oy | Process for the selective froth-flotation of phosphate and carbonate minerals from finely-divided phosphate-carbonate-silicate ores or concentrates |
US4472270A (en) * | 1983-05-18 | 1984-09-18 | Mobil Oil Corporation | Beneficiation of ores |
US4636303A (en) * | 1985-10-07 | 1987-01-13 | Tennessee Valley Authority | Beneficiation of dolomitic phosphate ores |
US6685027B2 (en) | 2001-08-09 | 2004-02-03 | Arr-Maz Products, Lp | Method of concentrating phosphates from their ores |
-
0
- US US2105807D patent/US2105807A/en not_active Expired - Lifetime
Cited By (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
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 |
US3063561A (en) * | 1960-01-25 | 1962-11-13 | Int Minerals & Chem Corp | Beneficiation of ores |
US3259242A (en) * | 1962-11-29 | 1966-07-05 | Int Minerals & Chem Corp | Beneficiation of apatite-calcite ores |
US3534854A (en) * | 1967-11-20 | 1970-10-20 | Int Minerals & Chem Corp | Beneficiation of calcite-apatite-quartz ores |
US4008151A (en) * | 1973-10-29 | 1977-02-15 | Office Cherifien Des Phosphates | Process for enrichment, by flotation, of phosphate ores with gangues containing carbonates |
US4317715A (en) * | 1977-11-22 | 1982-03-02 | Outokumpu Oy | Process for the selective froth-flotation of phosphate and carbonate minerals from finely-divided phosphate-carbonate-silicate ores or concentrates |
US4472270A (en) * | 1983-05-18 | 1984-09-18 | Mobil Oil Corporation | Beneficiation of ores |
US4636303A (en) * | 1985-10-07 | 1987-01-13 | Tennessee Valley Authority | Beneficiation of dolomitic phosphate ores |
US6685027B2 (en) | 2001-08-09 | 2004-02-03 | Arr-Maz Products, Lp | Method of concentrating phosphates from their ores |
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