US3454159A - Phosphate flotation - Google Patents
Phosphate flotation Download PDFInfo
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- US3454159A US3454159A US544090A US3454159DA US3454159A US 3454159 A US3454159 A US 3454159A US 544090 A US544090 A US 544090A US 3454159D A US3454159D A US 3454159DA US 3454159 A US3454159 A US 3454159A
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- flotation
- phosphate
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- scrubbing
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D1/00—Flotation
- B03D1/02—Froth-flotation processes
- B03D1/021—Froth-flotation processes for treatment of phosphate ores
-
- 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 beneficiation of phosphate rock and similar phosphatic materials and in particular to an improved method of treating phosphate rock flotation feed to obtain a high grade phosphate concentrate.
- phosphate rock In the usual process for beneficiating such phosphatecontaining material (hereinafter referred to collectively as phosphate rock), the mixture of phosphatic minerals and gangue obtained from the phosphate deposit or mine is first washed to remove trash therefrom and to separate and recover the larger lumps of phosphate minerals (usually referred to as pebble rock).
- the remaining material (washer reject material) consists of a mixture of phosphate rock particles, sand, clay and similar gangue materials, substantially all of which is less than about 10 mesh (Tyler Standard), and preferably is less than 14 mesh in size.
- the phosphate rock consituent of this material is then concentrated and recovered for subsequent use, commonly by froth or table flotation techniques or a combination of both.
- the phosphate rock feed is commonly first deslimed and dewatered, conditioned with an anionic flotation reagent, and subjected to a froth flotation operation, all as described in the Hollingsworth and Sapp patents noted above.
- the phosphate rock feed is sometimes scrubbed, as a slurry with water, prior to desliming and dewatering to aid in removal of adherent materials.
- the anionic flotation operation is not entirely satisfactory in that large quantities of anionic flotation reagents are consumed adding to the cost of beneficiation. Equally important, the flotation is not selective enough, resulting in a significant proportion of insolubles (mostly silica) being separated along with the phosphate.
- the present invention comprises the method of beneficiating phosphate rock by froth flotation comprising scrubbing a phosphate rock feed with an alkaline "ice composition, conditioning the scrubbed rock feed with an anionic flotation reagent consisting essentially of a fatty acid and a fuel oil, and subjecting the conditioned feed to a froth flotation operation to float a final phosphate concentrate which is recovered as thedesired phosphate product.
- the process also comprises dewatering and desliming the scrubbed phosphate rock feed prior to conditioning.
- the alkaline composition is preferably an aqueous solution of caustic soda.
- Other alkaline materials that may be used are soda ash, lime, ammonia, potassium hydroxide, magnesium hydroxide, and the like alkaline materials capable of raising the pH of an aqueous solution to at least about 8 and preferably about 9 and above. It is commercially uneconomical to use a pH above 11 because of the amount of alkaline material required.
- the alkaline material is present in the scrubbing fluid in amount suflicient to adjust the pH of the fluid to about 9 and preferably 10.
- caustic soda NaOH
- the anionic flotation reagent is a combination of a fatty acid and a fuel oil. No alkaline materials are required as part of the reagent as is the case with anionic flotation reagent combination used heretofore in flotation of Florida phosphate rock feeds.
- the fatty acid may be oleic acid, linoleic acid, tall oils, rosin, mixtures thereof, and other like materials commonly used in anionic flotation reagents
- the fuel oil can be any commonly employed in anionic flotation reagents such as diesel oil, kerosene, Bunker C fuel oil, and mixtures thereof.
- the reagent is preferably a combination of 4 parts by weight of a fuel oil to each part by weight of a fatty acid, although proportions ranging from 1:1 to 8:1 can be used.
- the dewaterer, deslimer, conditioner, and flotation apparatus can be those disclosed in the Hollingsworth and Sapp patents discussed above or those commonly used in phosphate beneficiation.
- the scrubber is preferably a standard attrition type scrubber.
- a phosphate rock feed is first passed into a scrubber where it is scrubbed with the alkaline composition for time suflicient to render the sur face of the phosphate rock sufliciently alkaline; ordinarily about 20 to about 60 seconds are required for small scale operations and up to about 3 minutes in large commercial installation. Longer treatment times can be used, but, again, this is not commercially desirable.
- the treatment time will vary, dependent upon the type of scrubbing equipment, the type and concentration of alkaline material in the scrubbing liquid. The optimum conditions are readily determinable by making test runs and noting the conditions showing the least amount or reagent used and the greatest recovery of phosphate.
- Phosphate recovery is measured as percent by by weight of bone phosphate of lime (tricalcium phosphate) recovered or percent B.P.L. recovered. Using an amount of caustic soda in the scrubber solution to give a pH of about 10, it is found that treatment of phosphate rock' feed for about 60 seconds will result in greatest percent B.P.L. recovery and lowest reagent consumption. If the feed has not been first subjected to a cationic flotation is should be deslimed prior to scrubbing.
- the amount of alkaline material used in scrubbing and amount of anionic reagent used are measured in pounds per long ton of phosphate rock feed.
- Example 1 The phosphate rock feed 1s then conditloned by being The recess of th resent inventio was m r d admixed with an anionic flotation reagent of the present p e p H CO Pa 6 .nventio
- the exam 168 Set forth below Show that the with conventlonal procedures using a 29.72% B.P.L. i 1 f th H flota phosphate rock feed.
- the feed was scrubbed in a series mven Ion reqmres 68$ 0 a i h of runs, with and without caustic soda, for various periods non reagefts B (fatty an fue P t an of time at 65% solids using a turbo-type mixer.
- the that requlre? li More Pamculajfly w 30 1 several scrubbed feeds were then deslimed and condi- 40% 1655 3111011113 1101311011 reagent 1 an Increase 111 tioned with varying amounts of anionic flotation reagents selectivity (less insolubles) wh1le mamtaimng the same or containing 4 parts by weight of fuel oil to 1 part by weight better B.P.L.
- Example 2 beneficiation runs were made Example 2 with three different phosphate rock feeds in order to take into consideration variations in flotation characteristics which exist from one feed to another. All the scrubbing, desliming, dewatering, conditioning, and flotation of the A 30.89% B.P.L. phosphate rock feed was used and various treatments, with and without scrubbing and including variations in time, were used. The conditioning and flotation procedures used were the same as that used feeds was carried out on the same equipment for all runs in Example 1. The results are summarized in Table 2.
- Example 3 The process of the present invention was compared to conventional anionic floats employing no scrubbing and conventional anionic floats utilizing scrubbing. The other processing conditions used were the same as that used in Example 1. The results are summarized in Table 3.
- the anionic floation procedure of the present invention can bused alone to beneficiate washer reject material or in conjunction with cationic floats carried out prior to or subsequent to the anionic flotation.
- the scrubbing with alkaline material is also beneficial for cationic (silica) flotation as it acts to reduce the amount of reagent necessary while maintaining the same or better B.P.L. recovery.
- the method of beneficiating phosphate rock by froth flotation comprising scrubbing a deslimed phosphate rock feed with an alkaline composition, dewatering and desliming the scrubbed feed to remove slime formed during scrubbing, conditioning the phosphate rock feed with an anionic flotation reagent consisting essentially of a fatty acid and a fuel oil, and subjecting the conditioned feed to a froth flotation operation to float a final phosphate concentrate which is recovered as the desired phosphate product.
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Description
United States Patent Int. Cl. B03d N06 US. Cl. 2093 Claims ABSTRACT OF THE DISCLOSURE A method of beneficiating phosphate rock by anionic froth flotation by scrubbing a deslimed phosphate rock feed with an alkaline composition, dewatering and desliming the scrubbed feed, conditioning the thus treated feed with an anionic flotation reagent and subjecting the conditioned feed to a froth flotation of high grade phosphate concentrate.
This invention relates to the beneficiation of phosphate rock and similar phosphatic materials and in particular to an improved method of treating phosphate rock flotation feed to obtain a high grade phosphate concentrate.
In the usual process for beneficiating such phosphatecontaining material (hereinafter referred to collectively as phosphate rock), the mixture of phosphatic minerals and gangue obtained from the phosphate deposit or mine is first washed to remove trash therefrom and to separate and recover the larger lumps of phosphate minerals (usually referred to as pebble rock). The remaining material (washer reject material) consists of a mixture of phosphate rock particles, sand, clay and similar gangue materials, substantially all of which is less than about 10 mesh (Tyler Standard), and preferably is less than 14 mesh in size. The phosphate rock consituent of this material is then concentrated and recovered for subsequent use, commonly by froth or table flotation techniques or a combination of both. Patents No. 3,013,664 and 3,086,654 to Hollingsworth and Sapp disclose efficient and economical methods of beneficiation utilizing froth flotation operations comprising cationic (silica) floats and anionic (phosphate) floats. At present, most flotation processes use a anionic float followed by a cationic float.
In such anionic floation operations the phosphate rock feed is commonly first deslimed and dewatered, conditioned with an anionic flotation reagent, and subjected to a froth flotation operation, all as described in the Hollingsworth and Sapp patents noted above. In conventional practice the phosphate rock feed is sometimes scrubbed, as a slurry with water, prior to desliming and dewatering to aid in removal of adherent materials.
While superior to previous methods, the anionic flotation operation is not entirely satisfactory in that large quantities of anionic flotation reagents are consumed adding to the cost of beneficiation. Equally important, the flotation is not selective enough, resulting in a significant proportion of insolubles (mostly silica) being separated along with the phosphate.
A method has now been found whereby the amount of anionic flotation reagents required for effective flotation isgreatly reduced, while at the same time the selectively of the float is increased.
Briefly stated, the present invention comprises the method of beneficiating phosphate rock by froth flotation comprising scrubbing a phosphate rock feed with an alkaline "ice composition, conditioning the scrubbed rock feed with an anionic flotation reagent consisting essentially of a fatty acid and a fuel oil, and subjecting the conditioned feed to a froth flotation operation to float a final phosphate concentrate which is recovered as thedesired phosphate product. In its preferred embodiment, the process also comprises dewatering and desliming the scrubbed phosphate rock feed prior to conditioning.
As to materials, the alkaline composition is preferably an aqueous solution of caustic soda. Other alkaline materials that may be used are soda ash, lime, ammonia, potassium hydroxide, magnesium hydroxide, and the like alkaline materials capable of raising the pH of an aqueous solution to at least about 8 and preferably about 9 and above. It is commercially uneconomical to use a pH above 11 because of the amount of alkaline material required.
As to the proportions, the alkaline material is present in the scrubbing fluid in amount suflicient to adjust the pH of the fluid to about 9 and preferably 10. When caustic soda (NaOH) is the alkaline material to be added to the feed scrubbing step (scrubbing ordinarily is carried out at 65 solids) it is used in the proportion of from about 0.005 part to about 0.05 part by weight for each parts weight of phosphate rock feed.
The anionic flotation reagent is a combination of a fatty acid and a fuel oil. No alkaline materials are required as part of the reagent as is the case with anionic flotation reagent combination used heretofore in flotation of Florida phosphate rock feeds. The fatty acid may be oleic acid, linoleic acid, tall oils, rosin, mixtures thereof, and other like materials commonly used in anionic flotation reagents In like manner, the fuel oil can be any commonly employed in anionic flotation reagents such as diesel oil, kerosene, Bunker C fuel oil, and mixtures thereof. The reagent is preferably a combination of 4 parts by weight of a fuel oil to each part by weight of a fatty acid, although proportions ranging from 1:1 to 8:1 can be used.
As to equipment the dewaterer, deslimer, conditioner, and flotation apparatus can be those disclosed in the Hollingsworth and Sapp patents discussed above or those commonly used in phosphate beneficiation. The scrubber is preferably a standard attrition type scrubber.
As to processing conditions, a phosphate rock feed is first passed into a scrubber where it is scrubbed with the alkaline composition for time suflicient to render the sur face of the phosphate rock sufliciently alkaline; ordinarily about 20 to about 60 seconds are required for small scale operations and up to about 3 minutes in large commercial installation. Longer treatment times can be used, but, again, this is not commercially desirable. The treatment time will vary, dependent upon the type of scrubbing equipment, the type and concentration of alkaline material in the scrubbing liquid. The optimum conditions are readily determinable by making test runs and noting the conditions showing the least amount or reagent used and the greatest recovery of phosphate. Phosphate recovery is measured as percent by by weight of bone phosphate of lime (tricalcium phosphate) recovered or percent B.P.L. recovered. Using an amount of caustic soda in the scrubber solution to give a pH of about 10, it is found that treatment of phosphate rock' feed for about 60 seconds will result in greatest percent B.P.L. recovery and lowest reagent consumption. If the feed has not been first subjected to a cationic flotation is should be deslimed prior to scrubbing.
3 After scrubbing, it is preferred to deslime and dewater the phosphate rock feed to remove slime produced in the scrubbing operation. Slime, either phosphatic or clay, if present in any appreciable amount, act to lower the effectiveness of the anionic flotation.
to eliminate variatons due to equipment differences. The amount of alkaline material used in scrubbing and amount of anionic reagent used are measured in pounds per long ton of phosphate rock feed.
Example 1 The phosphate rock feed 1s then conditloned by being The recess of th resent inventio was m r d admixed with an anionic flotation reagent of the present p e p H CO Pa 6 .nventio The exam 168 Set forth below Show that the with conventlonal procedures using a 29.72% B.P.L. i 1 f th H flota phosphate rock feed. The feed was scrubbed in a series mven Ion reqmres 68$ 0 a i h of runs, with and without caustic soda, for various periods non reagefts B (fatty an fue P t an of time at 65% solids using a turbo-type mixer. The that requlre? li More Pamculajfly w 30 1 several scrubbed feeds were then deslimed and condi- 40% 1655 3111011113 1101311011 reagent 1 an Increase 111 tioned with varying amounts of anionic flotation reagents selectivity (less insolubles) wh1le mamtaimng the same or containing 4 parts by weight of fuel oil to 1 part by weight better B.P.L. recovery. of fatty acid and floated in a standard flotation cell. The The invention will be further described in connection fuel oil used was Bunker C fuel oil API gravity 19-20 with the following examples of the practice of it WhlCh and the fatty acld was Unitol OT (a tall oil fraction). are set forth for purposes of illustration only. The results are summarized in Table 1.
TABLE 1 Serubbin Lbs., Reag Concentrate Middling Tailing ent 11F. Lbs., Feed Percent NaOH/ Wt. Wt. Wt. B.P.L. 4:1 Run No. Time 'I.F. B.P.L. Insol. percent B.P.L. Insol. percent B.P.L. percent B.P.L. Reey. Mix NaOH Standard Phosphate Floats {Caustic added to conditioner) 1 seconds None 29. 72 61. 71 3. 7 03 None 29. 72 01. 71 20.5 70.75 2.17 7.0 00.58 72.5 13.07 07.0 3.7 .00 None 29.72 01. 71 20.0 77.19 2.70 7.2 00.92 72.8 13.18 07.1 3.7 .10 None 29. 72 01. 71 19.0 70.41 2. 39 0. 5 04. 12 74. 5 15. 19 01.1 3. 7 11 None 29. 72 01. 71 3. 7 .43 None 29. 72 01. 71 34. 4 74. 74 4. 50 3. 4 30. 94 02. 2 4. 80 89. 5 5. 0 10 None 29.72 01. 71 19.9 75.73 2.86 10.9 04.04 09.2 11.58 72.0 5.0 .43 None 29. 72 01. 71 30. 5 72. 73 0. 17 5. 5 19. 07 58. 0 3. 45 92. 7 8. 1
Efieets of Scrubbing With Caustic (No caustic used in conditioner) 9 15 seconds--- .40 29.72 01. 71 12.4 70.52 2.00 9.5 70.73 78.1 17.20 54.1 3.7 None 10 30 seconds .22 29.72 61.71 6.1 65. 49 15.89 93.9 26.17 19.9 3.8 None 11.. 0 .43 29.75 01. 71 33.0 74.90 3.10 3.0 38.20 02.8 5.23 88.5 3.7 None 12 do- .43 29.72 01. 71 29.7 70.00 2.01 4.9 53.40 05.4 7.24 83.6 3.7 None 13-- do .43 29.72 01. 71 20.9 70.18 2.08 8.0 00.10 71.1 11.92 71.0 3.7 None 14-. do .05 29.72 01.71 33.0 75.40 2.87 3.4 48. 93 03.0 4.58 90.0 3.7 None 15 .-do .05 29.72 01. 71 37.0 73.84 5.71 3.2 20.73 59.8 3.08 92.4 5.0 None NH4OH 10 do .43 29.72 01. 71 20.0 70.18 2. 0.0 60.81 68.0 8.40 80.4 3.7 None 1 These conditions produced no float. 1 N o float. a Feed was not deslimed after scrubbing.
In the following examples, beneficiation runs were made Example 2 with three different phosphate rock feeds in order to take into consideration variations in flotation characteristics which exist from one feed to another. All the scrubbing, desliming, dewatering, conditioning, and flotation of the A 30.89% B.P.L. phosphate rock feed was used and various treatments, with and without scrubbing and including variations in time, were used. The conditioning and flotation procedures used were the same as that used feeds was carried out on the same equipment for all runs in Example 1. The results are summarized in Table 2.
TABLE 2 Concentrate Middling Tailing Lbs. Reagent] Scrubber T.F.
Per- Per- Per- Percent N aOH/ Feed, cent cent cent B. 4:1 Run No. Time T.F. pH B.P.L. Wt. B.P.L. Insol. Wt. B.P.L. Wt B.P.L. Ratio Reey. Mix NaOH pH Standard Phosphate Floats (control) Effects of Scrubbing 19 30 seconds- None 1 7. 5 30.89 21. 5 72.48 8. 83 78. 5 20.00 4. 82 48. 7 5. 4 4 9. 2
20 do 7 30.89 34. 4 76. 57 3. 69 .23 62. 7 5. 2. 83 87. 6 5. 8 None 21 d0 6 1O 2 30.89 32. 5 77.61 2. 37 4. 2 45.08 63. 3 6. 34 2. 90 86. 6 5. 4 None 9. 0
30 vs. 60 sec. Scrubbing 22 30 seconds. 7 10. 4 30. 89 37. 0 75.48 5. 06 2. 6 22.06 60.4 3. 2. 66 91. 9 5. 4 None 9.0
23 60 seconds 7 10. 3 30. 89 36. 0 75.87 4. 56 2.8 26. 66 61. 2 4. 45 2. 70 91.0 6. 4 None 9.0
1 pH of ores in the mixer prior to adding flotation reagents.
5 Example 3 The process of the present invention was compared to conventional anionic floats employing no scrubbing and conventional anionic floats utilizing scrubbing. The other processing conditions used were the same as that used in Example 1. The results are summarized in Table 3.
6 3. The method according to claim 2 in which the alkaline material is used in an amount sufficient to adjust the pH of the solution to at least about 8.
4. The method according to claim 1 in which the phosphate rock feed is scrubbed with the alkaline composition for about 20 second to about 3 minutes.
TABLE 3 Concentrate Middling Tailing Lbs. Reagent/T.F. Percent NaOH/ Feed, Percent Percent 6 Percent B.P.L. 4: 1 Run No T.F. pH B.P.L. Wt. B.P.L. Insol. Wt. B. P'L. Wt. B.P.L. Ratio Reey. Mix NaOH pH Standard Phosphate Floats 36. 66 9. 7 80. 55 1. 46 15. 7 74. 18 74. 6 22. 17 4. 03 54. 5 5. 4 3 9. 5 36. 66 37. 6 79. 05 3. 68 3. 8 37542 58. 6 9. 52 2. 56 84. 2 7. 6 3 9. 36. 66 37. 6 78. 38 4. 33 4. 4 35. 42 '58. 0 9. 85 2. 55 83. 8 8. 8 3 9. 0 36. 66 39. 78. 28 4. 55 4. 5 29. 67 56. 0 8. 64 2. 49 85. 8 8. 8 3 9. 2
30 Sec. Scrubbing Without daustic 36. 66 25. 3 79. 67 2. 02 8. 9 64. 55 65. 8 15. 14 2. 99 72. 6 5. 4 3 36. 66 39. 2 76. 71 5. 58 3. 2 19. 86 57. 6 10. 75 2. 55 82. 1 6. 6 3 9. 2 36. 66 41. 5 77. 70 4. 63 4. 1 26. 23 54. 4 8. 78 2. 47 85. 8 8. 8 3 9. 2
Sec. Scrubbing With Caustic; v
31 3 10 36. 66 41. 5 77. 43 4. 66 3. 5 95 55. 0 6. 58 2. 36 89. 6 6. 2 None 9. 2 32 3 10 36. 66 40. 7 78. 46 3. 56 3. 5 32. 04 55. 8 6. 26 2. 37 90. 3 5. 8 None 9. 2
While the exact theory is not precisely understood, it is believed that scrubbing of the phosphate ore in the presence of an alkaline material prior to conditioning acts to clean the surface of the ore and to make the surface more alkaline or positive. This more positive charge on the clean surface, in turn, renders the separation in the anionic float more definite, greatly reducing the amount of insolubles separated with the phosphate and requiring much less anionic flotation reagent for etfective flotation.
The anionic floation procedure of the present invention can bused alone to beneficiate washer reject material or in conjunction with cationic floats carried out prior to or subsequent to the anionic flotation.
The scrubbing with alkaline material is also beneficial for cationic (silica) flotation as it acts to reduce the amount of reagent necessary while maintaining the same or better B.P.L. recovery.
What is claimed is:
1. The method of beneficiating phosphate rock by froth flotation comprising scrubbing a deslimed phosphate rock feed with an alkaline composition, dewatering and desliming the scrubbed feed to remove slime formed during scrubbing, conditioning the phosphate rock feed with an anionic flotation reagent consisting essentially of a fatty acid and a fuel oil, and subjecting the conditioned feed to a froth flotation operation to float a final phosphate concentrate which is recovered as the desired phosphate product.
2. The method according to claim 1 in which the alkaline composition is caustic soda.
References Cited UNITED STATES PATENTS 2,313,360 3/1943 Ralston 209-166 2,336,437 12/ 1943 Erickson 209-166 2,424,552 7/ 1947 Clemmer 209-166 2,660,303 11/1953 Maseman 2O95 3,302,785 2/1967 Greene 2095 3,349,903 10/1967 Olsen 209-166 X OTHER REFERENCES Taggart, handbook of Mineral Dressing, Wiley and Sons, Inc., New York, 1945, 3-15, 3-17, 10-01, 10-07, TN 500 T3, 1945.
HARRY B. THORNTON, Primary Examiner.
R. HALPER, Assistant Examiner.
US. Cl. X.R. 209-12, 166
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US54409066A | 1966-04-21 | 1966-04-21 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| US3454159A true US3454159A (en) | 1969-07-08 |
Family
ID=24170705
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US544090A Expired - Lifetime US3454159A (en) | 1966-04-21 | 1966-04-21 | Phosphate flotation |
Country Status (1)
| Country | Link |
|---|---|
| US (1) | US3454159A (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4040519A (en) * | 1974-03-28 | 1977-08-09 | Nittetsu Mining Company, Ltd. | Froth flotation process for recovering sheelite |
| US4059509A (en) * | 1976-01-09 | 1977-11-22 | Mobil Oil Corporation | Phosphate ore flotation |
| US4189103A (en) * | 1978-03-10 | 1980-02-19 | International Minerals & Chemical Corporation | Method of beneficiating phosphate ores |
| US4436616A (en) | 1980-11-06 | 1984-03-13 | Philippe Dufour | Process for the beneficiation of phosphate ores |
| US5221466A (en) * | 1989-04-20 | 1993-06-22 | Freeport-Mcmoran Resource Partners, Limited Partnership | Phosphate rock benefication |
| US5295297A (en) * | 1986-11-25 | 1994-03-22 | Hitachi, Ltd. | Method of producing semiconductor memory |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2313360A (en) * | 1940-05-24 | 1943-03-09 | Armour & Co | Process of concentrating nonmetalliferous ores |
| US2336437A (en) * | 1940-09-13 | 1943-12-07 | American Cyanamid Co | Froth flotation of acidic minerals |
| US2424552A (en) * | 1945-05-01 | 1947-07-29 | Clemmer Julius Bruce | Froth flotation of nonmetallic minerals |
| US2660303A (en) * | 1951-09-10 | 1953-11-24 | Tennessee Valley Authority | Selective flocculation of colloidal phosphate ore in the presence of clay |
| US3302785A (en) * | 1963-10-14 | 1967-02-07 | Minerals & Chem Philipp Corp | Phosphate matrix beneficiation process |
| US3349903A (en) * | 1966-12-28 | 1967-10-31 | Grace W R & Co | Process for beneficiating unground pebble phosphate ore |
-
1966
- 1966-04-21 US US544090A patent/US3454159A/en not_active Expired - Lifetime
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2313360A (en) * | 1940-05-24 | 1943-03-09 | Armour & Co | Process of concentrating nonmetalliferous ores |
| US2336437A (en) * | 1940-09-13 | 1943-12-07 | American Cyanamid Co | Froth flotation of acidic minerals |
| US2424552A (en) * | 1945-05-01 | 1947-07-29 | Clemmer Julius Bruce | Froth flotation of nonmetallic minerals |
| US2660303A (en) * | 1951-09-10 | 1953-11-24 | Tennessee Valley Authority | Selective flocculation of colloidal phosphate ore in the presence of clay |
| US3302785A (en) * | 1963-10-14 | 1967-02-07 | Minerals & Chem Philipp Corp | Phosphate matrix beneficiation process |
| US3349903A (en) * | 1966-12-28 | 1967-10-31 | Grace W R & Co | Process for beneficiating unground pebble phosphate ore |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4040519A (en) * | 1974-03-28 | 1977-08-09 | Nittetsu Mining Company, Ltd. | Froth flotation process for recovering sheelite |
| US4059509A (en) * | 1976-01-09 | 1977-11-22 | Mobil Oil Corporation | Phosphate ore flotation |
| US4189103A (en) * | 1978-03-10 | 1980-02-19 | International Minerals & Chemical Corporation | Method of beneficiating phosphate ores |
| US4436616A (en) | 1980-11-06 | 1984-03-13 | Philippe Dufour | Process for the beneficiation of phosphate ores |
| US5295297A (en) * | 1986-11-25 | 1994-03-22 | Hitachi, Ltd. | Method of producing semiconductor memory |
| US5221466A (en) * | 1989-04-20 | 1993-06-22 | Freeport-Mcmoran Resource Partners, Limited Partnership | Phosphate rock benefication |
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