GB1567765A - Flotation process - Google Patents
Flotation process Download PDFInfo
- Publication number
- GB1567765A GB1567765A GB45100/76A GB4510076A GB1567765A GB 1567765 A GB1567765 A GB 1567765A GB 45100/76 A GB45100/76 A GB 45100/76A GB 4510076 A GB4510076 A GB 4510076A GB 1567765 A GB1567765 A GB 1567765A
- Authority
- GB
- United Kingdom
- Prior art keywords
- values
- solvent
- flotation
- aqueous solution
- solution
- 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
Links
- 238000005188 flotation Methods 0.000 title claims description 151
- 238000000034 method Methods 0.000 title claims description 93
- 230000008569 process Effects 0.000 title claims description 85
- 239000000243 solution Substances 0.000 claims description 107
- 239000007787 solid Substances 0.000 claims description 64
- 229910052500 inorganic mineral Inorganic materials 0.000 claims description 57
- 235000010755 mineral Nutrition 0.000 claims description 57
- 239000011707 mineral Substances 0.000 claims description 57
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 claims description 51
- 239000007864 aqueous solution Substances 0.000 claims description 51
- 229940072033 potash Drugs 0.000 claims description 51
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Substances [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 claims description 51
- 235000015320 potassium carbonate Nutrition 0.000 claims description 51
- 239000002904 solvent Substances 0.000 claims description 47
- 239000012535 impurity Substances 0.000 claims description 39
- 238000005406 washing Methods 0.000 claims description 38
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 28
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 24
- 239000003607 modifier Substances 0.000 claims description 24
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid group Chemical group C(CC(O)(C(=O)O)CC(=O)O)(=O)O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 claims description 22
- 239000002002 slurry Substances 0.000 claims description 22
- 239000003153 chemical reaction reagent Substances 0.000 claims description 19
- 238000012545 processing Methods 0.000 claims description 17
- 230000005484 gravity Effects 0.000 claims description 16
- 239000000203 mixture Substances 0.000 claims description 16
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 10
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 9
- 229910052802 copper Inorganic materials 0.000 claims description 9
- 239000010949 copper Substances 0.000 claims description 9
- KRHYYFGTRYWZRS-UHFFFAOYSA-N Fluorane Chemical compound F KRHYYFGTRYWZRS-UHFFFAOYSA-N 0.000 claims description 8
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 claims description 8
- 238000013019 agitation Methods 0.000 claims description 8
- 150000004985 diamines Chemical class 0.000 claims description 8
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 claims description 8
- 229910052737 gold Inorganic materials 0.000 claims description 8
- 239000010931 gold Substances 0.000 claims description 8
- 239000011591 potassium Substances 0.000 claims description 8
- 229910052700 potassium Inorganic materials 0.000 claims description 8
- 229910052892 hornblende Inorganic materials 0.000 claims description 7
- 239000007788 liquid Substances 0.000 claims description 7
- 150000003512 tertiary amines Chemical class 0.000 claims description 7
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 6
- 125000000217 alkyl group Chemical group 0.000 claims description 6
- 229910052626 biotite Inorganic materials 0.000 claims description 6
- 238000000605 extraction Methods 0.000 claims description 6
- 229910052611 pyroxene Inorganic materials 0.000 claims description 6
- 239000010453 quartz Substances 0.000 claims description 6
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 6
- 229920002401 polyacrylamide Polymers 0.000 claims description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 4
- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 claims description 4
- 239000005708 Sodium hypochlorite Substances 0.000 claims description 4
- 238000007667 floating Methods 0.000 claims description 4
- 229910052655 plagioclase feldspar Inorganic materials 0.000 claims description 4
- 239000011734 sodium Substances 0.000 claims description 4
- 229910052708 sodium Inorganic materials 0.000 claims description 4
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 claims description 4
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 3
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 claims description 3
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 3
- 229910052770 Uranium Inorganic materials 0.000 claims description 3
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 claims description 3
- KXZJHVJKXJLBKO-UHFFFAOYSA-N chembl1408157 Chemical compound N=1C2=CC=CC=C2C(C(=O)O)=CC=1C1=CC=C(O)C=C1 KXZJHVJKXJLBKO-UHFFFAOYSA-N 0.000 claims description 3
- 239000004571 lime Substances 0.000 claims description 3
- 150000003141 primary amines Chemical group 0.000 claims description 3
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 3
- 230000002311 subsequent effect Effects 0.000 claims description 3
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims description 2
- 229910021578 Iron(III) chloride Inorganic materials 0.000 claims description 2
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 claims description 2
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims description 2
- 229910021529 ammonia Inorganic materials 0.000 claims description 2
- 238000006243 chemical reaction Methods 0.000 claims description 2
- 239000000460 chlorine Substances 0.000 claims description 2
- 229910052801 chlorine Inorganic materials 0.000 claims description 2
- 229910000358 iron sulfate Inorganic materials 0.000 claims description 2
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 claims description 2
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 claims description 2
- 229910052744 lithium Inorganic materials 0.000 claims description 2
- 239000011777 magnesium Substances 0.000 claims description 2
- 229910052749 magnesium Inorganic materials 0.000 claims description 2
- 230000001105 regulatory effect Effects 0.000 claims description 2
- 229910052979 sodium sulfide Inorganic materials 0.000 claims description 2
- GRVFOGOEDUUMBP-UHFFFAOYSA-N sodium sulfide (anhydrous) Chemical compound [Na+].[Na+].[S-2] GRVFOGOEDUUMBP-UHFFFAOYSA-N 0.000 claims description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims 4
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 claims 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims 3
- 229910052709 silver Inorganic materials 0.000 claims 3
- 239000004332 silver Substances 0.000 claims 3
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 claims 2
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims 2
- 229910052787 antimony Inorganic materials 0.000 claims 2
- WATWJIUSRGPENY-UHFFFAOYSA-N antimony atom Chemical compound [Sb] WATWJIUSRGPENY-UHFFFAOYSA-N 0.000 claims 2
- 229910052788 barium Inorganic materials 0.000 claims 2
- DSAJWYNOEDNPEQ-UHFFFAOYSA-N barium atom Chemical compound [Ba] DSAJWYNOEDNPEQ-UHFFFAOYSA-N 0.000 claims 2
- 229910052759 nickel Inorganic materials 0.000 claims 2
- 229910052702 rhenium Inorganic materials 0.000 claims 2
- WUAPFZMCVAUBPE-UHFFFAOYSA-N rhenium atom Chemical compound [Re] WUAPFZMCVAUBPE-UHFFFAOYSA-N 0.000 claims 2
- 239000010936 titanium Substances 0.000 claims 2
- 229910052719 titanium Inorganic materials 0.000 claims 2
- JFALSRSLKYAFGM-UHFFFAOYSA-N uranium(0) Chemical compound [U] JFALSRSLKYAFGM-UHFFFAOYSA-N 0.000 claims 2
- ATRRKUHOCOJYRX-UHFFFAOYSA-N Ammonium bicarbonate Chemical compound [NH4+].OC([O-])=O ATRRKUHOCOJYRX-UHFFFAOYSA-N 0.000 claims 1
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims 1
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 claims 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims 1
- 229910052782 aluminium Inorganic materials 0.000 claims 1
- 239000001099 ammonium carbonate Substances 0.000 claims 1
- 235000012501 ammonium carbonate Nutrition 0.000 claims 1
- 239000010941 cobalt Substances 0.000 claims 1
- 229910017052 cobalt Inorganic materials 0.000 claims 1
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims 1
- 230000000694 effects Effects 0.000 claims 1
- 229910017604 nitric acid Inorganic materials 0.000 claims 1
- SATVIFGJTRRDQU-UHFFFAOYSA-N potassium hypochlorite Chemical compound [K+].Cl[O-] SATVIFGJTRRDQU-UHFFFAOYSA-N 0.000 claims 1
- 229910000030 sodium bicarbonate Inorganic materials 0.000 claims 1
- 235000017557 sodium bicarbonate Nutrition 0.000 claims 1
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 claims 1
- 229910052721 tungsten Inorganic materials 0.000 claims 1
- 239000010937 tungsten Substances 0.000 claims 1
- 229910052725 zinc Inorganic materials 0.000 claims 1
- 239000011701 zinc Substances 0.000 claims 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical class O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 28
- 239000002245 particle Substances 0.000 description 26
- 239000000047 product Substances 0.000 description 23
- 238000002386 leaching Methods 0.000 description 18
- 238000000926 separation method Methods 0.000 description 18
- 238000011084 recovery Methods 0.000 description 17
- 239000012267 brine Substances 0.000 description 12
- 239000011435 rock Substances 0.000 description 10
- 238000005201 scrubbing Methods 0.000 description 8
- 238000010977 unit operation Methods 0.000 description 8
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 6
- 230000001143 conditioned effect Effects 0.000 description 6
- 238000000227 grinding Methods 0.000 description 6
- 239000002253 acid Substances 0.000 description 5
- 238000007792 addition Methods 0.000 description 5
- 239000000470 constituent Substances 0.000 description 5
- 239000002562 thickening agent Substances 0.000 description 5
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 4
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 description 4
- 239000003795 chemical substances by application Substances 0.000 description 4
- 238000004140 cleaning Methods 0.000 description 4
- 235000014113 dietary fatty acids Nutrition 0.000 description 4
- 239000000428 dust Substances 0.000 description 4
- 239000000194 fatty acid Substances 0.000 description 4
- 229930195729 fatty acid Natural products 0.000 description 4
- 150000004665 fatty acids Chemical class 0.000 description 4
- 238000001556 precipitation Methods 0.000 description 4
- 239000004094 surface-active agent Substances 0.000 description 4
- 230000009471 action Effects 0.000 description 3
- 150000001412 amines Chemical class 0.000 description 3
- 239000012141 concentrate Substances 0.000 description 3
- 238000009826 distribution Methods 0.000 description 3
- -1 ethanol Chemical class 0.000 description 3
- 239000000706 filtrate Substances 0.000 description 3
- 239000011737 fluorine Substances 0.000 description 3
- 229910052731 fluorine Inorganic materials 0.000 description 3
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 description 3
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 description 3
- 230000004044 response Effects 0.000 description 3
- 230000008719 thickening Effects 0.000 description 3
- WRIDQFICGBMAFQ-UHFFFAOYSA-N (E)-8-Octadecenoic acid Natural products CCCCCCCCCC=CCCCCCCC(O)=O WRIDQFICGBMAFQ-UHFFFAOYSA-N 0.000 description 2
- KBPLFHHGFOOTCA-UHFFFAOYSA-N 1-Octanol Chemical compound CCCCCCCCO KBPLFHHGFOOTCA-UHFFFAOYSA-N 0.000 description 2
- LQJBNNIYVWPHFW-UHFFFAOYSA-N 20:1omega9c fatty acid Natural products CCCCCCCCCCC=CCCCCCCCC(O)=O LQJBNNIYVWPHFW-UHFFFAOYSA-N 0.000 description 2
- QSBYPNXLFMSGKH-UHFFFAOYSA-N 9-Heptadecensaeure Natural products CCCCCCCC=CCCCCCCCC(O)=O QSBYPNXLFMSGKH-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- ZQPPMHVWECSIRJ-UHFFFAOYSA-N Oleic acid Natural products CCCCCCCCC=CCCCCCCCC(O)=O ZQPPMHVWECSIRJ-UHFFFAOYSA-N 0.000 description 2
- 239000005642 Oleic acid Substances 0.000 description 2
- JXLHNMVSKXFWAO-UHFFFAOYSA-N azane;7-fluoro-2,1,3-benzoxadiazole-4-sulfonic acid Chemical compound N.OS(=O)(=O)C1=CC=C(F)C2=NON=C12 JXLHNMVSKXFWAO-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 230000003750 conditioning effect Effects 0.000 description 2
- ZSIAUFGUXNUGDI-UHFFFAOYSA-N hexan-1-ol Chemical compound CCCCCCO ZSIAUFGUXNUGDI-UHFFFAOYSA-N 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- QXJSBBXBKPUZAA-UHFFFAOYSA-N isooleic acid Natural products CCCCCCCC=CCCCCCCCCC(O)=O QXJSBBXBKPUZAA-UHFFFAOYSA-N 0.000 description 2
- 238000007885 magnetic separation Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- ZQPPMHVWECSIRJ-KTKRTIGZSA-N oleic acid Chemical compound CCCCCCCC\C=C/CCCCCCCC(O)=O ZQPPMHVWECSIRJ-KTKRTIGZSA-N 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 229960005076 sodium hypochlorite Drugs 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000003784 tall oil Substances 0.000 description 2
- 239000003760 tallow Substances 0.000 description 2
- WUOACPNHFRMFPN-VIFPVBQESA-N (R)-(+)-alpha-terpineol Chemical compound CC1=CC[C@H](C(C)(C)O)CC1 WUOACPNHFRMFPN-VIFPVBQESA-N 0.000 description 1
- QTWJRLJHJPIABL-UHFFFAOYSA-N 2-methylphenol;3-methylphenol;4-methylphenol Chemical compound CC1=CC=C(O)C=C1.CC1=CC=CC(O)=C1.CC1=CC=CC=C1O QTWJRLJHJPIABL-UHFFFAOYSA-N 0.000 description 1
- WVYWICLMDOOCFB-UHFFFAOYSA-N 4-methyl-2-pentanol Chemical compound CC(C)CC(C)O WVYWICLMDOOCFB-UHFFFAOYSA-N 0.000 description 1
- PXRKCOCTEMYUEG-UHFFFAOYSA-N 5-aminoisoindole-1,3-dione Chemical compound NC1=CC=C2C(=O)NC(=O)C2=C1 PXRKCOCTEMYUEG-UHFFFAOYSA-N 0.000 description 1
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonium chloride Substances [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 1
- 108091005950 Azurite Proteins 0.000 description 1
- GAWIXWVDTYZWAW-UHFFFAOYSA-N C[CH]O Chemical group C[CH]O GAWIXWVDTYZWAW-UHFFFAOYSA-N 0.000 description 1
- LZZYPRNAOMGNLH-UHFFFAOYSA-M Cetrimonium bromide Chemical compound [Br-].CCCCCCCCCCCCCCCC[N+](C)(C)C LZZYPRNAOMGNLH-UHFFFAOYSA-M 0.000 description 1
- ZYTUJDHYVZOBJE-UHFFFAOYSA-N Cl.[Ba] Chemical compound Cl.[Ba] ZYTUJDHYVZOBJE-UHFFFAOYSA-N 0.000 description 1
- GALPHPSAKJXOOD-UHFFFAOYSA-N Cl.[Sb] Chemical compound Cl.[Sb] GALPHPSAKJXOOD-UHFFFAOYSA-N 0.000 description 1
- 229920001353 Dextrin Polymers 0.000 description 1
- 239000004375 Dextrin Substances 0.000 description 1
- FCSHMCFRCYZTRQ-UHFFFAOYSA-N N,N'-diphenylthiourea Chemical compound C=1C=CC=CC=1NC(=S)NC1=CC=CC=C1 FCSHMCFRCYZTRQ-UHFFFAOYSA-N 0.000 description 1
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 description 1
- 229910019142 PO4 Inorganic materials 0.000 description 1
- WAKTWVHWRCNIKU-UHFFFAOYSA-N S(=O)(=O)(O)O.[AlH3] Chemical compound S(=O)(=O)(O)O.[AlH3] WAKTWVHWRCNIKU-UHFFFAOYSA-N 0.000 description 1
- 241000907663 Siproeta stelenes Species 0.000 description 1
- DBMJMQXJHONAFJ-UHFFFAOYSA-M Sodium laurylsulphate Chemical compound [Na+].CCCCCCCCCCCCOS([O-])(=O)=O DBMJMQXJHONAFJ-UHFFFAOYSA-M 0.000 description 1
- 239000004141 Sodium laurylsulphate Substances 0.000 description 1
- 229920002472 Starch Polymers 0.000 description 1
- QDRNVVLGMNXAQL-UHFFFAOYSA-I [W+4].[OH-].[Na+].[OH-].[OH-].[OH-].[OH-] Chemical compound [W+4].[OH-].[Na+].[OH-].[OH-].[OH-].[OH-] QDRNVVLGMNXAQL-UHFFFAOYSA-I 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 239000012190 activator Substances 0.000 description 1
- 230000006978 adaptation Effects 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 125000001931 aliphatic group Chemical group 0.000 description 1
- DLHONNLASJQAHX-UHFFFAOYSA-N aluminum;potassium;oxygen(2-);silicon(4+) Chemical compound [O-2].[O-2].[O-2].[O-2].[O-2].[O-2].[O-2].[O-2].[Al+3].[Si+4].[Si+4].[Si+4].[K+] DLHONNLASJQAHX-UHFFFAOYSA-N 0.000 description 1
- 229960001040 ammonium chloride Drugs 0.000 description 1
- 235000019270 ammonium chloride Nutrition 0.000 description 1
- 125000000129 anionic group Chemical group 0.000 description 1
- QRZZGRABHFGTDM-UHFFFAOYSA-L azane;cobalt(2+);carbonate Chemical compound N.[Co+2].[O-]C([O-])=O QRZZGRABHFGTDM-UHFFFAOYSA-L 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 239000004359 castor oil Substances 0.000 description 1
- 235000019438 castor oil Nutrition 0.000 description 1
- 125000002091 cationic group Chemical group 0.000 description 1
- SXPWTBGAZSPLHA-UHFFFAOYSA-M cetalkonium chloride Chemical compound [Cl-].CCCCCCCCCCCCCCCC[N+](C)(C)CC1=CC=CC=C1 SXPWTBGAZSPLHA-UHFFFAOYSA-M 0.000 description 1
- 229960000228 cetalkonium chloride Drugs 0.000 description 1
- 235000015165 citric acid Nutrition 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 229910001779 copper mineral Inorganic materials 0.000 description 1
- 238000010908 decantation Methods 0.000 description 1
- 230000000994 depressogenic effect Effects 0.000 description 1
- 235000019425 dextrin Nutrition 0.000 description 1
- 239000002270 dispersing agent Substances 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- MOTZDAYCYVMXPC-UHFFFAOYSA-N dodecyl hydrogen sulfate Chemical compound CCCCCCCCCCCCOS(O)(=O)=O MOTZDAYCYVMXPC-UHFFFAOYSA-N 0.000 description 1
- JRBPAEWTRLWTQC-UHFFFAOYSA-N dodecylamine Chemical compound CCCCCCCCCCCCN JRBPAEWTRLWTQC-UHFFFAOYSA-N 0.000 description 1
- 239000003925 fat Substances 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 238000009291 froth flotation Methods 0.000 description 1
- ZEMPKEQAKRGZGQ-XOQCFJPHSA-N glycerol triricinoleate Natural products CCCCCC[C@@H](O)CC=CCCCCCCCC(=O)OC[C@@H](COC(=O)CCCCCCCC=CC[C@@H](O)CCCCCC)OC(=O)CCCCCCCC=CC[C@H](O)CCCCCC ZEMPKEQAKRGZGQ-XOQCFJPHSA-N 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 230000002209 hydrophobic effect Effects 0.000 description 1
- MTNDZQHUAFNZQY-UHFFFAOYSA-N imidazoline Chemical compound C1CN=CN1 MTNDZQHUAFNZQY-UHFFFAOYSA-N 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000010423 industrial mineral Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 150000002736 metal compounds Chemical class 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 238000003801 milling Methods 0.000 description 1
- CIXSDMKDSYXUMJ-UHFFFAOYSA-N n,n-diethylcyclohexanamine Chemical compound CCN(CC)C1CCCCC1 CIXSDMKDSYXUMJ-UHFFFAOYSA-N 0.000 description 1
- PSZYNBSKGUBXEH-UHFFFAOYSA-N naphthalene-1-sulfonic acid Chemical compound C1=CC=C2C(S(=O)(=O)O)=CC=CC2=C1 PSZYNBSKGUBXEH-UHFFFAOYSA-N 0.000 description 1
- CBSVJWYOTGMOBT-UHFFFAOYSA-N nitric acid rhenium Chemical compound [Re].[N+](=O)(O)[O-] CBSVJWYOTGMOBT-UHFFFAOYSA-N 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 229910052652 orthoclase Inorganic materials 0.000 description 1
- 239000010452 phosphate Substances 0.000 description 1
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 1
- OMCDTZGWTJOENX-UHFFFAOYSA-N potassium nickel(2+) trihypochlorite Chemical compound [Ni+2].Cl[O-].[K+].Cl[O-].Cl[O-] OMCDTZGWTJOENX-UHFFFAOYSA-N 0.000 description 1
- 159000000001 potassium salts Chemical class 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- AOJFQRQNPXYVLM-UHFFFAOYSA-N pyridin-1-ium;chloride Chemical compound [Cl-].C1=CC=[NH+]C=C1 AOJFQRQNPXYVLM-UHFFFAOYSA-N 0.000 description 1
- 230000029219 regulation of pH Effects 0.000 description 1
- 230000003252 repetitive effect Effects 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- 229910052604 silicate mineral Inorganic materials 0.000 description 1
- IYAGECKNKFUYAJ-UHFFFAOYSA-N silver;sodium;dicyanide Chemical compound [Na+].[Ag+].N#[C-].N#[C-] IYAGECKNKFUYAJ-UHFFFAOYSA-N 0.000 description 1
- OWMYFPZSWSYFNQ-UHFFFAOYSA-J sodium gold(3+) hydrogen carbonate Chemical compound C([O-])(O)=O.[Na+].[Au+3].C([O-])(O)=O.C([O-])(O)=O.C([O-])(O)=O OWMYFPZSWSYFNQ-UHFFFAOYSA-J 0.000 description 1
- 235000019333 sodium laurylsulphate Nutrition 0.000 description 1
- IZWPGJFSBABFGL-GMFCBQQYSA-M sodium;2-[methyl-[(z)-octadec-9-enoyl]amino]ethanesulfonate Chemical compound [Na+].CCCCCCCC\C=C/CCCCCCCC(=O)N(C)CCS([O-])(=O)=O IZWPGJFSBABFGL-GMFCBQQYSA-M 0.000 description 1
- WFRKJMRGXGWHBM-UHFFFAOYSA-M sodium;octyl sulfate Chemical compound [Na+].CCCCCCCCOS([O-])(=O)=O WFRKJMRGXGWHBM-UHFFFAOYSA-M 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 239000008107 starch Substances 0.000 description 1
- 235000019698 starch Nutrition 0.000 description 1
- 229910052569 sulfide mineral Inorganic materials 0.000 description 1
- BDHFUVZGWQCTTF-UHFFFAOYSA-N sulfonic acid Chemical compound OS(=O)=O BDHFUVZGWQCTTF-UHFFFAOYSA-N 0.000 description 1
- WQSRXNAKUYIVET-UHFFFAOYSA-N sulfuric acid;zinc Chemical compound [Zn].OS(O)(=O)=O WQSRXNAKUYIVET-UHFFFAOYSA-N 0.000 description 1
- 229940104261 taurate Drugs 0.000 description 1
- XOAAWQZATWQOTB-UHFFFAOYSA-N taurine Chemical compound NCCS(O)(=O)=O XOAAWQZATWQOTB-UHFFFAOYSA-N 0.000 description 1
- 150000003558 thiocarbamic acid derivatives Chemical class 0.000 description 1
- BAKALPNAEUOCDL-UHFFFAOYSA-N titanium hydrochloride Chemical compound Cl.[Ti] BAKALPNAEUOCDL-UHFFFAOYSA-N 0.000 description 1
- GWBUNZLLLLDXMD-UHFFFAOYSA-H tricopper;dicarbonate;dihydroxide Chemical compound [OH-].[OH-].[Cu+2].[Cu+2].[Cu+2].[O-]C([O-])=O.[O-]C([O-])=O GWBUNZLLLLDXMD-UHFFFAOYSA-H 0.000 description 1
- 239000012991 xanthate 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03B—SEPARATING SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS
- B03B9/00—General arrangement of separating plant, e.g. flow sheets
-
- 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
Landscapes
- Manufacture And Refinement Of Metals (AREA)
- Extraction Or Liquid Replacement (AREA)
- Separation Of Solids By Using Liquids Or Pneumatic Power (AREA)
- Physical Water Treatments (AREA)
Description
(54) FLOTATION PROCESS
(71) We, FLUOR UTAH, INCORPORATED, a corporation of the State of California, 177
Bovet Road, San Mateo, California, United
States of America, do hereby declare the invention, for which we pray that a patent may be granted to us, and the method by which it is to be performed, to be particularly described in and by the following statement: This invention relates to the hydrometallurgical processing of ores. More particularly, it relates to an improvement in processing ores hydrometallurgically whereby the recovery of desired metallic values from the ores is substantially increased.Still more particularly, it relates to a novel procedure for separating mineral matter from ores containing metallic values whereby the loss of metallic values, normally encountered in solid.liquid separations, is substantially reduced.
For effective recovery of dissolved metallic values from solid mineral matter, it is conventional to make a series of liquid-solid
separations following repetitive stages of washing of the the solid phase with counterflow of solution removed from each subsequent stage of liquid-solid separation, washing being done with water and/or barren slution prior to the last stage. Barren solu
tion is the commonly used terminology for the solution or solvent remaining after the metallic values have been recovered by processes such as precipitation or electrolytic separation. The most efficient methods to date have involved the application of one of the following equipment systems: countercurrent thickening circuits, selfcleaning filters or solid-bowl centrifuges.By these methods, however, a substantial amount, usually from about 8% to 15two, of metallic values is removed with the solid mineral matter. Frequently, with ores containing a high percentage of clays, fine silicate particles and the like, the percentage of metallic values removed with the mineral matter well exceeds 15%. This is because such constituents either absorb a relatively large amount of the metallic values solution and/or cannot be effectively washed and dewatered. When the foregoing methods are utilized, such constituents are generally separated with the solid mineral matter, carrying metallic values with them. The metallic values lost in the liquid-solid separation steps have nct previously been economically available for recovery through subsequent processing.
In fact, separation of the disolved metallic values from the undissolved mineral matter has meant extremely high capital costs and operating costs per ton of daily plant capacity. Further, a method of separating the dissolved metallic values may be incompatible with other processing steps. For example, in potash metallurgy, a continuous countercurrent decantation (CCD) thickening circuit is not economically combinable with amine flotation of mineral matter particles from particles of potash.
It is an object of the present invention to reduce the significant loss of metallic values associated with liquid-solid separations.
It is also an object of the present invention to provide a method of separating the dissolved metallic values from undissolved mineral matter which offers the possibility of lower capital costs per ton of daily plant capacity or, similarly, a higher recovery of metallic values for comparable capital costs per daily ton.
Another object of the present invention is to provide a process for recovering metallic values from mineral matter which affords better washing action through continuous agitation during separation, which cannot be achieved by conventional practices involving thickeners, centrifuges and/or filters.
Another object of the present invention is to provide a method of obtaining a better contact between particles bearing metallic values and solution through continuous agitation during separation, which affords a better opportunity for leaching the metallic values.
A further object of the present invention is to provide a proces of obtaining metallic values from mineral matter which has a fewer number of washing and separation steps than utilized with conventional practices for equivalent yields.
The present invention provides a process for recovering metallic values from a mixture thereof with mineral impurities, comprising:
(A) washing the mixture with a sol
vent for the metallic values, in which
solvent the impurities are substantially
insoluble, forming a solution of the
metallic values in the solvent and float
ing the insoluble impurities in the solu
tion, removing the floated impurities
from the solution,
(B) subjecting the floated impurities
to at least one subsequent flotation and
washing step, and where there are two
or more such flotation/washing steps, the
flow of solution being counter to that of
the impurities, the subsequent or the last
subsequent flotation/washing being with
water or barren solution, the solution
from the first subsequent or the subse
quent flotation/washing being used as
the solvent in step (A), and
(C) treating the solution from step
(A) to yield the metallic values.
It has been found that by employing the process of this invention, in a preferred embodiment, liquid-solid separation can be effected by a process in which metallic values are leached from host rock and the resultant pulped ore is conditioned with appropriate reagents, followed by froth flotation of the solid mineral matter, accompanied by simultaneous washing with counterflow of solution removed from an immediately subsequent flotation stage. The solution resulting from this first flotationwashing step, referred to herein as 1st countercurrent tails, is further processed as required to recover the desired metallic values in the solution.To abstract the metallic values contained in the resultant mineral matter froth, the froth is subjected to a series of liquid-solid separations by flotation, accompanied by simultaneous washing with counterflow of solution removed from each subsequent stage of flotation, water and/or barren solution being used for washing in the last stage. Processing of pulped ore in this manner is referred to as countercurrent flotation.
Often, it is the practice in the art to subject original ore pulp to preliminary classification steps, such as screening, cycloning and/or hydroseparating, whereby a
major proportion of fine particles, or slimes, is separated from the coarse mineral size fraction and either processed separately from the coarse mineral size fraction or discarded.
However, if these slimes are treated by the process of this invention a solution will be obtained containing practically all the soluble metallic values associated therewith, which may be substantially recovered by routing the solution to subsequent well known processing steps, such as precipitation of electrolytic separation.
Also, it is often the practice in the art to subject the mineral matter froth from a flotation process to cleaning by subsequent stages of flotation and grinding, if required, whereby the concentration of desired values is increased by rejection of unwanted mineral matter. If the resultant, rejected mineral matter from such cleaning is treated by the process of the invention, a solution will be obtained which contains practically all the soluble metallic values associated therewith, which may be substantially recovered by routing the solution to subsequent processing steps.
In addition, the mineral matter froth from a flotation process, mentioned above, could be directly treated with the process of this invention with substantially the same results being obtained in regard to the metallic values. This is also true for other mineral concentrates, such as those which are the products of other separation processes, including jigging, tabling, heavy media separation, and magnetic separation.
Figure 1 is a flowsheet depicting a preferred embodiment of this invention, which is basically applicable to all soluble substances, although soluble metals and metal compounds are of primary concern herein.
Figure 2 is a flowsheet for the recovery of gold according to the instant invention, with numerals designating streams described in detail in Example III.
Figure 3 is a flowsheet depicting a preferred embodiment of this invention as used in conjunction with a potash flotation circuit.
Figure 4 is a flowsheet for the recovery of potash utilizing a conventional potash flotation recovery system accompanied by a countercurrent flotation system, with numerals designating streams described in detail in Example IV.
The process of the invention may be advantageously applied to either originally mined ore, a slimes fraction and/or particular size fraction obtained by classification, rejected mineral matter from the cleaning of flotation mineral matter froth, or a mineral concentrate generated from a separation process, such as jigging, tabling, heavy media or magnetic separation, and flotation
Furthermore, the process of this invention can be adapted for use under varying circumstances. For example, countercurrent flotation can be applied to substantially any flow of slurry within a mineral processing facility, such as the slurry discharged from a leaching circuit.The leaching circuit may handle either crude ore or mineral concentrates, subject only to limitations of particle size or particle size distribution of the mineral impurities and/or reaction products of the leaching, known as leach residue. In general, although flotation is most effective when the top size of the mineral particles does not exceed 48 mesh, there are, however, exceptions. For example, in the potash and phosphate industry, successful flotation has been achieved on particles as coarse as 8 mesh. This is also true for the flotation of coal and silicate minerals at various operating plants in the U.S. and Europe. Throughout this specification, reference to "Mesh" are to Tyler Standard mesh sizes.
If the size of mineral particles in the slurry to countercurrent flotation must be regulated to meet specific process requirements, such regulations may be achieved by utilizing apparatus such as screens, classifiers, cyclones, centrifuges, thickeners, etc.
For example, if circumstances require, cyclones may be used to separate plus 65 mesh material from minus 65 mesh particles, with the fine fraction being processed through a countercurrent flotation circuit.
Likewise, overflow from a thickener (minus 400 mesh), effluent from a centrifuge (minus 200 mesh), filtrate from a filter (minus 150 mesh), underflow from a thickener (minus 65 mesh), etc. may be routed to a countercurrent flotation circuit in appropriate situations.
This invention may be applied to any desired values, elements or compounds, which can be dissolved in the presence of insoluble impurities. Illustrative examples of specific metallic values recoverable by the process of the instant invention, along with repre- sentative leaching media, are as follows::
METALLIC
VALUE LEACHING MEDIUM
Potassium Water
Sodium Water
Magnesium Water
Lithium Water
Copper Aqueous Solution of Sulfuric Acid, Hydrochloric Acid or
Ferric Chloride
Uranium Aqueous Solution of Sulfuric Acid or Sodium Carbonate
and Sodium Bicarbonate
Gold Aqueous Solution of Sodium Cyanide
Silver Aqueous Solution of Sodium Cyanide, Sodium Hypochlor
ite or Potassium Hypochlorite
Nickel Aqueous Solution of Ammonia or Ammonia Carbonate
Cobalt Aqueous Solution of Sulfuric Acid
Zinc Aqueous Solution of Sulfuric Acid
Aluminum Aqueous Solution of Sodium Hydroxide
Tungsten Aqueous Solution of Hydrochloric Acid
Titanium Aqueous Solution of Sulfuric Acid or Hydrochloric Acid
Antimony Aqueous Solution of Sodium Sulfide or Hydrochloric Acid
Barium Aqueous Solution of Hydrofluoric Acid or Nitric Acid
Rhenium Aqueous Solution of Chlorine or Sodium Hypochlorite
The impurities typically separated from the metallic values by application of the instant invention are the insoluble constituents of the host rock with which the metallic values are associated and/or the insoluble reaction products of the leaching operation.
The selection of flotation reagents to be used in the process of the instant invention depends on the constituents of the host rock associated with the desired metallic values.
A report by R. A. Wyman, Head, Industrial
Minerals Milling Section, Mineral Processing
Division, Mines Branch, Department of
Energy, Mines and Resources, Ottawa,
Canada, entitled "The Floatability of
Twenty-One Non-Metallic Minerals", incorporated herein by reference, gives illustractive reagent selection for 21 minerals.
The reagents, mentioned above, with which the pulped ore is conditioned normally include collectors and modifiers.
Collectors are agents which render the surfaces of minerals to be floated hydrophobic, i.e. lacking affinity for water, thus allowing attachment to an air bubble and elevation to the surface. The chemicals involved are the so-called surface active agents, or surfactants.
In general, the collectors used for flotation of insoluble impurities in the process of this invention would be oils, organic hydrocarbons, having cationic or anionic groups, or mixtures of such collectors. Normally, neither alcohols, such as ethanol, nor inorganic salts would be suitable as collectors.
Exemplary collectors or types of collectors
are:
1. "Green acid"--type petroleum sul
phonate
2. Sodium alkyl-aryl petroleum sul
phonic acid
3. Naphthalene sulphonic acid deriva
tive
4. Fatty acid aliphatic sulphonate
5. Sulphonated castor oil (60to fats)
6. Sulphonated fatty acids
7. Sodium octyl sulphate
8. Sodium lauryl sulphate
9. Diethyl cyclohexylamine lauryl sul
phate
10. Sodium - N - methyl - N - tal'ow acid taurate
11. Sodium - N - methyl - N - oleoyl taurate
12. Technical tallow amine acetate
13. Coco amine acetate
14. Primary beta amine
15. Tallow diamine di-acetate
16. Coco diamine di-acetate
17. Beta diamine
18. Hydroxyethyl alkyl imidazoline (gly
oxalidine)
19. Lauryl amine 20.Beta tertiary amine
21. N0auroyl-colamino-formyl-methyl) pyridinium chloride
22. n-alkyl trimethyl ammonium chlor
ide
23. Cetyl trimethyl ammonium bromide
24. Cetyl dimethyl benzyl ammonium
chloride
25. Tall oil base fatty acid
26. Tall oil fatty acid
27. Oleic acid blend
28. Oleic acid
Those familiar with flotation processes are well aware of considerations given to selection of a suitable collector. Thus, none of the 21 minerals evaluated in the Mine's
Branch report would respond favourably to flotation using the following collectors:
Xanthates
Thiocarbamates
Dithiosphosphates
Thiocarbanilide
Xanthogen.
However, if sulfide minerals were present in the host rock, those skilled in the art would recognize that the above collectors would be used in combination with others.
Modifiers are agents which are capable of performing many functions. Such agents may be utilized to aid in getting the collector onto the surface of the mineral to be floated, an action called activation. On the other hand, modifying agents may be employed to prevent a collector from getting onto the surface of unwanted minerals, an action called depression. The former use is that to which modifiers are normally put in accordance with the process of the present invention.
In addition, modifiers may be used for pH regulation, the cleaning of mineral particle surfaces, dispersion of ultra-fine solids or precipitation of dissolved salts. Some modifiers may even serve more than one purpose, e.g., sodium carbonate may act as an activator, depressant, pH regulator or dispersant.
The modifiers used for flotation in accordance with the process of the present invention generally include all flotation reagents whose principal function is neither collecting nor frothing.
Exemplary modifiers are H2SO, NaCO3, FeSOs, AL(SOA)3, HF, starch, dextrin and citric acid.
In commercial flotation practices, the addition of frothers is normally required to promote the formation of froth capable of supporting mineral-laden bubbles on the surface of the slurry or solution within the flotation cells. Frothers accomplish this objective by imparting temporary toughness to the covering film of the bubble and lowering the surface---tension -of the - water.
Customarily added into the feedboxes of the flotation cells, frothers conventionally used are organic heteropolar compounds, for example, glycol, hexanol, methyl isobutyl carbinol, terpenol, mixed capryl alcohol, and cresylic acid.
Operating parameters for the process of the present inventior, including flow rates, recycle rations and degree of agitation, are discussed below.
In practising the process of the present invention, flow rates are readily determinable by those skilled in the art by a consideration of the following well known factors:
(a) design capacity of a particular faci
lity;
(b) time required for separation of solids
by flotation from the solution in
volved;
(c) percent solids of the feed slurry re
quired for flotation;
(d) specific gravity of solution and
solids; and
(e) size of the flotation cells used.
Hydrometallurgical plants have ranged in daily production capacity from several tons to over 15,000 tons.
Flotation time and percent solids in the feed are interdependent and are established by the flotation characteristics of the solids.
Both variables may range widely from one type of ore to another. Flotation time may vary from about 1 to over about 30 minutes.
Solids concentration may vary from about 10 to about 50 percent.
An excellent reference for recycle ratios and the number of washing stages required is a paper by R. J. Woody entitled "Geographical Representation of Theoretical
Soluble Losses by CCD", incorporated herein by reference.
Although this paper is related to thickeners, the same principles apply to countercurrent flotation. It is expected, however, that either the number of wash stages or volume of wash solution would be less than required using a CCD thickening circuit.
Generally, the number of washing stages may vary between one and about eight and the recycle ratio, expressed as
liquid volume of solution (W) r=
liquid volume in froth product (D) may range between one and about six.
The degree of agitation would be that utilized in currently practised flotation processes, well known to those skilled in the art, for comparable particle size and tank volume.
One other important variable is process temperature. In certain leaching operations, the temperature may be elevated to accelerate reaction rates. For flotation of various minerals, results are improved by heating the feed slurry. Temperatures for the process of invention could range from about OOC to about 105"C.
Another variable is pressure. Pressure may be used in some flotation processes to induce air agitation rather than mechanical agitation. For example, in one pressure flotation cell, the Eimco's Flotator vessel, the feed slurry is introduced at a pressure between 15 and 60 psi. By sudden pressure release, a mild aeration results which promotes the formation of a mineral froth at the surface of the vessel. "Eimco", besides being the name by which a certain company is known, is also its trade mark for some products.
Referring to Figure 1, which depicts a preferred embodiment of the present invention, host rock 10 containing the desired metallic values and mineral matter impurities is introduced, usually after appropriate grinding and classification, into a leaching unit 11 concurrently with a leaching medium 9. (The leaching medium or a portion thereof may be introduced during grinding and classification.) Ore pulp 12, containing a metallic values solution and solid mineral matter impurities, is drawn from the leaching vat 11 and introduced into a conditioner 13, along with selected reagents 14 comprising conditioners and/or modifiers.
The conditioned ore pulp 15 is then introduced into 1st countercurrent flotation cells 16, along with a frother 17 and a stream from a subsequent flotation step for washing the conditioned ore pulp 15, as will be discussed below. This mixture is agitated in the 1st countercurrent flotation cells 16 to facilitate simultaneous washing and flotation.
Mineral froth, called 1st countercurrent froth 18 herein, then floats to the top of the
Ist couontercurrent flotation cells 16 leaving a solution of the desired metallic values.
This solution, the 1st countercurrent tails 19 herein, is taken from the approximate bottom of the 1st countercurrent flotation cells 16 and directed to subsequent processing for extraction of the desired metallic values.
The 1st countercurrent froth 1S, on the other hand, is taken from the top of the 1st countercurrent flotation cells 16 and introduced into 2nd countercurrent flotation cells 20 along with countercurrent tails from a subsequent countercurrent flotation step (as will be discussed below) for washing - and flotation. Here they are agitated by means of impellers and/or air injection', as will the 1 sot countercurrent flotation cells 16, and 2nd countercurrent froth 21 raises to the top of the cells, leaving a solution containing the desired metallic values, i.e. 2nd countercurrent tails 22.This solution, which is taken from the approximate bottom of the 2nd countercurrent flotation cells 20, is the stream referred to above that is introduced into the 1st countercurrent flotation cells 16, along with the conditioned ore pulp, for washing and flotation.
The 2nd countercurrent froth 21 is taken from the top of the 2nd countercurrent flotation cells 20 and introduced into 3rd countercurrent flotation cells 23 concurrently with countercurrent tails from a subsequent countercurrent flotation step (as will be discussed below) for washing and flotation. Here they are agitated as described above for the 1st and 2nd countercurrent flotation cells with 3rd countercurrent froth 24 rising to the top, leaving a metallic values solution, i.e. 3rd countercurrent tails 25. It is this solution that is used to wash the mineral froth 18 in the 2nd countercurrent flotation cells 20.
The 3rd countercurrent froth 24 taken from this step is introduced into 4th countercurrent flotation cells 26 along with water and/or barren solution 29 for washing and flotation. Again, they are subjected to agitation with 4th countercurrent froth 27 rising to the top, leaving the 4th countercurrent tails 28, which are used for washing the 2nd countercurrent froth 21.
The 4th countercurrent froth 27 which is taken from this step has had substantially all of the desired metallic values removed therefrom by the process just described and can be discarded or utilized for purposes apparent to those skilled in the art.
It should be noted in regard to the process just described that the number of flotation steps utilized is optional. One or more flotation steps subsequent to the first, may be utilized depending upon the total yield of metallic values desired. In general, the more steps that are utilized, the greater the total yield will be. However, a point will be reached where the utilization of additional flotation steps will cause such a small increase in the total yield that it will normally be impractical to make such an addition.
When more than one subsequent flotation step is utilized, water and/or barren solution may be utilized in conjunction with countercurrent tails for washing in flotation steps prior to the last, and a portion of the 1st countercurrent tails stream, described above as going to subsequent processing, may be used for washing in the last flotation stage.
It should be further noted that the water and/or barren solution which is used for washing may be controlled to maintain desired concentrations of advancing solutions in order to optimize recovery of the desired metallic values.
The invention is further illustrated by the examples which follow.
EXAMPLE I
The ore to be treated is found in a deposit which contains malachite, azurite and chrysocolla as copper values with the host rock comprising diorite. A diorite usually contains plagioclase, quartz, hornblende, biotite and pyroxene. The diorite constituents constitute the mineral matter impurities, while the copper values are the desired metallic values.
Material from the deposit is mined, then crushed and ground to a particle size to accommodate successful leaching of the copper minerals with an aqueous solution of sulfuric acid.
After leaching, countercurrent flotation is applied either to the entire flow of slurry (solids, dissolved copper acid solution) or a portion of the flow (a fine solids size fraction) obtained by use of mechanical classifiers, cyclones and/or dewatering.
The pH for flotation is established by use of sulfuric acid for leaching. Consequently, reagent selection must be based on response to an acid circuit.
A tabulation based on the aforementioned
Mine's Branch report shows the following for acid circuit flotation of the minerals present in diorite:
Mineral Collector Section Modifiers
Plagioclase (response similar to Tertiary Amine Citric Acid
orthoclase)
Quartz Tertiary Amine Citric Acid
Hornblende Diamine Fluorine
Biotite Tertiary Amine Citric Acid
Pyroxene (response similar to Diamine Fluorine
hornblende)
Based on the above tabulation, the selected reagent schedule would include use of two amines, a tertiary amine and a diamine, as collectors, with either a combination of two modifiers, citric and hydrofluoric acid (or elemental fluorine, applied by bubbling into the solution), or just one, citric acid. The frother is selected from well known frothers for such systems including an alcohol, a glycol, a surfactant or a combination thereof.
In addition, the reagent combination which includes a polyacrylamide flocculant as modifier and an ethanolated alkyl guanidineamine complex as collector may be employed for diorite, since this combination appears to behave as a universal reagent combination.
EXAMPLE II
As in Example I, the host rock is diorite, but the metallic value is gold. After crushing and grinding, the gold may be leached with an aqueous solution of cyanide, using lime to maintain a basic pH. Under these circumstances, the pH for flotation is basic.
Consequently, reagent selection must be made accordingly. Based on the Mine's Branch Report, the reagent schedule would include use of a primary amine as the collector with additions of iron and aluminum sulfates as modifiers. The frother should be either an alcohol, a glycol, a surfactant or a combination thereof.
As in Example I, the reagent combination including a polyacrylamide flocculant and an ethanolated alkyl guanidineamine complex may also be employed here.
EXAMPLE III
Figure 2 is a flowsheet for the recovery of gold according to the instant invention. The following are illustrative flow rates for such a process: GALLONS PER SPECIFIC
UNIT OPERATION TONS PER HOUR PERCENT MINUTE GRAVITY
Pulp or
Solids Solution Solids Solids Solution Pulp Solution
Grinding & Classification
Feed Streams (1) Host Rock 475 25 95 717 100 817 2.45 (2) Cyanide solution - 2 - - 8 8 1.08 (20) Barren Solution - 176.6 - - 706 706 1.00
Discharge (3) 475 203.6 70 717 814 1531 1.77
Leaching & Conditioner (4) & (5) 475 203.6 70 717 814 1531 1.77 1st Countercurrent Flotation Cells
Feed Streams (5) Conditioner Discharge 475 203.6 70 717 814 1531 1.77 (11) 2nd Countercurrent Tails - 1696.4 - - 6786 6786 1.00 (6) Total Feed 475 1900.0 20 717 7600 8317 1.14
Products (7) 1st Countercurrent Froth 475 882.1 35 717 3528 4245 1.28 (8) 1st Countercurrent Tails - 1017.9 - - 4072 4072 1.00 GALLONS PER SPECIFIC
UNIT OPERATION TONS PER HOUR PERCENT MINUTE GRAVITY
Pulp of
Solids Solution Solids Solids Solution Pulp Solution 2nd Courtercurrent Flotation Cells
Feed Streams (7) 1st Countercurrent Froth 475 882.1 35 717 3528 4245 1.28 (14) 3rd Countercurrent Tails - 1696.4 - - 6786 6786 1.00 (9) Total Feed 475 2578.5 13.5 717 10314 11031 1.11
Products (10) 2nd Countercurrent Froth 475 882.1 35 717 3528 4245 1.28 (11) 2nd Countercurrent Tails - 1696.4 - - 6786 6786 1.00 3rd Counterurrent Flotation Cells
Feed Streams (10) 2nd Countercurrent Froth 475 882.1 35 717 3528 4245 1.28 (18) 4th Countercurrent Tails - 1696.4 - - 6786 6786 1.00 (12) Total Feed 475 2578.5 13.5 717 10314 11031 1.11
Products (13) 3rd Countercurrent Froth 475 882.1 35 717 3528 4245 1.28 (14) 3rd Countercurrent Tails - 1696.4 - - 6736 6736 1.00 GALLONS PER SPECIFIC
UNIT OPERATION TONS PER HOUR PERCENT MINUTE GRAVITY
Pulp or
Solids Solution Solids Solids Solution Pulp Solution 4th Countercurrent Flotation Cells
Feed Streams (13) 3rd Countercurrent Froth 475 882.1 35 717 3528 4245 1.28 (21) Barren Solution - 841.3 - - 3366 3366 1.00 (15) Water - 855.1 - - 3420 3420 1.00 (16) Total Feed 475 2578.5 13.5 717 10314 11031 1.11
Products (17) 4th Countercurrent Froth 475 882.1 35 717 3528 4245 1.28 (18) 4th Countercurrent Tails - 1696.4 35 - 6786 6786 1.00
Solution Purification & Gold Precipitation
Feed Stream (8) 1st Countercurrent Tails - 1017.9 - - 4072 4072 1.00 - 4072 4072 1.00
Discharge - 1017.9 (19) Barren Solution
Barren Solution Distribution (20) Grinding & Classification - 176.6 - - 706 706 1.00 (21) 4th Countercurrent Flotation - 841.3 - - 3366 3366 1.00 The process of the present invention is particularly adaptable for use with a conventiop potash flotation recovery system. In such a system, flotation is utilized to separate solid potash particles, e.g. particles of K2Co, and miscellaneous other potassium salts, from solid mineral matter particles.
Unfortunately, substantial amounts of potash are entrained with the mineral matter particles which are thereby separated. The potash associated with this mineral matter portion has heretofore been considered economically uncoverable. However, such is not the case when the process of the present invention is utilized.
Referring to Figure 3, which depicts a preferred embodiment of such utilization, host rock 10 containing the potash, i.e., the desired potassium values, as well as mineral matter impurities is, normally after crushing and classification, introduced into a scrubbing unit 11 concurrent with a scrubbing medium 9, such as saturated brine.
Saturated brine, as used herein, refers to an aqueous solution containing the maximum possible amount of potash dissolved therein. The scrubbing unit 11 is used to attrite the potash particles thereby liberating mineral matter particles which are contained in the host rock 10. Unlike the process of the present invention in which a leaching medium is utilized to bring the desired values into solution, the conventional potash flotation recovery proces utilizes scrubbing media, such as saturated brine, to keep potash values from going into solution so that a solid-solid separation can be made of the potash particles and the mineral matter particles in the initial flotation step of the process.
Scrubbing unit discharge 12, containing solid potash values and solid mineral matter particles is discharged from the scrubbing unit 11 and introduced into a container 13, along with selected reagents 14 comprising modifiers and/or collectors, e.g. a poly acrylamide flocculant as a modifier and an ethanolated alkyl guanidineamine complex as a collector. Additional saturated brine may sometimes be added into conditioner 13 to reduce the percentage of solids therein and thereby facilitate the conditioning of scrubber discharge 12. The desirability of such addition depends upon the nature of
the host rock 10 being processed and will be readily apparent to those skilled in the art.
The conditioned scrubber discharge 15 is then introduced into rougher flotation cells
16, normally along with a frother 17, and agitated by impellers and/or air injection.
Rougher froth 18, including mineral matter particles and entrained potash particles, then floats to the top of the rougher flotation cells 16, leaving rougher tails 19, including saturated brine and solid potash particles.
The rougher tails 19 are directed to subsequent processing for extraction of the desired values, while the rougher froth 18 is introduced into 1st countercurrent flotation cells 20, along with 2nd countercurrent tails 25 from 2nd countercurrent flotation cells 23. It should be noted that for the purposes of the process of the present invention, these 2nd countercurrent tails 25 become the initial leaching medium for the potash in rougher froth 18 and that usually no more reagents need be added to the rougher froth 18, since the particles therein have already been subjected to conditioning in conditioner 13. To achieve desired flotation results with some ores, however, introduction of additional amounts of reagents into selected countercurrent flotation cells may be required.
From this point on, countercurrent flotation is conducted just as described earlier.
The 1st countercurrent tails 22 are directed to subsequent processing, while the 1st countercurrent froth 21 is introduced into 2nd countercurrent flotation cells 23, along with 3rd countercurrent tails 28 from 3rd countercurrent flotation cells 26, etc.
Although Figure 3 depicts three countercurrent flotation stages, as was discussed earlier, more or less might be used, depending upon the yield of potash desired from the countercurrent flotation operation.
It should be noted that although the entire stream of 1st countercurrent tails 22 could be directed to a unit, such as a crystallizer, for the extraction of substantially all the potash therein, it is more advantageous to regulate the addition of water and/or barren solution to the last countercurrent flotation cells such that the 1st countercurrent tails 22 will be a saturated brine solution and then to combine this stream with other saturated brine streams which are normally generated in a conventional potash flotation recovery system. By doing this, sufficient saturated brine is made available for operation of the conventional potash recovery system without additional saturated brine having to be generated, and the saturated brine from these combined streams which is not needed for operation of the conventional potash recovery system may be routed to an appropriate extraction unit, such as a crystallizer, for the recovery of potash values therein. An illustration of such an arrangement is given in the following example.
EXAMPLE IV
Figure 4 is a flowsheet for the recovery of potash according to the adaptation of the instant invention just discussed. The following are illustrative flow rates for such a process: GALLONS PER SPECIFIC
UNIT OPERATION TONS PER HOUR PERCENT MINUTE GRAVITY
Pulp or
Solids Solution Solids Solids Solution Pulp Solution
Scrubbing Unit
Feed Streams (1) Potash Ore 400 20 95 800 65 865 1.94 (2) Brine - 151 - - 487 487 1.24
Discharge (3) 400 171 70 800 552 1352 1.69
Conditioner
Feed Streams (3) Scrubbing Unit Discharge 400 171 70 800 552 1352 1.69 (4) Brine - 762 - - 2458 2458 1.24
Discharge (5) 400 933 30 800 3010 3810 1.40
Rougher Flotation Cells
Feed Streams (5) Conditioner Discharge 499 933 30 800 3010 3810 1.40
Products (6) Rough Tails 366 627 36.8 732 2023 2755 1.44 (7) Rougher Froth 34 306 10 68 987 1055 1.29 GALLONS SPECIFIC
UNIT OPERATION TONS PER HOUR PERCENT MINUTE GRAVITY
Pulp or
Solids Solution Solids Solids Solution Pulp olution 1st Countercurrent Flotation Cells
Feed Streams (7) Rougher Froth 34 306 10 68 987 1055 1.29 (8) 2nd Countercurrent Tails - 340 - - 1104 1104 1.23 (9) Total Feed 34 646 - 68 2091 2159 1.26
Products (10) 1st Countercurrent Tails - 375 - - 1210 1210 1.24 (11) 1st Countercurrent Froth 32 273 10.5 64 881 945 1.29 2nd Countereurrent Flotation Cells
Feed Streams (11) 1st Countercurrent Froth 32 273 10.5 64 881 945 1.29 (12) 3rd Countercurrent Tails - 251 - - 838 838 1.20 (13) Total Feed 32 524 - 64 1719 1783 1.25
Products (8) 2nd Countercurrent Tails - 340 - - 1104 1104 1.23 (14) 2nd Countercurrent Froth 27 189 12.5 54 615 669 1.29 GALLONS PER SPECIFIC
UNIT OPERATION TONS PER HOUR PERCENT MINUTE GRAVITY
Pulp or
Solids Solution Solids Solids Solution Pulp Solution 3RD Countercurrent Flotation Cells
Feed Streams (14) 2nd Countercurrent Froth 27 189 12.5 54 615 669 1.29 (15) Water . . ... - 40 - - 160 160 1.00 (16) Crystallizer Muds (Barren
Solution) ... ... ... - 126 - - 430 430 1.17 (17) Total Feed ... 27 355 - 54 1205 1259 1.21
Products (12) 3rd Countercurrent Tails - 251 - - 838 838 1.20 (18) 3rd Countercurrent Froth 21 110 16 42 267 409 1.28
Potash Flotation Circuit
Feed Stream (6) Rougher Flotation Tails 366 627 36.8 732 2023 2755 1.44
Products (19) Potash Froth Product 80 149 35 160 481 641 1.43 (20) Potash Flotation Tails .... 286 478 37.4 572 1542 2114 1.45 GALLONS PER SPECIFIC
UNIT OPERATION TONS PER HOUR PERCENT MINUTE GRAVITY
Pulp or
Solids Solution Solids Solids Solution Pulp Solution
Potash Froth Dewatering
Feed Stream (19) Potash Froth Product 80 149 35 160 481 641 1.43
Products (21) Filtrate (Saturated Brine) - 142 - - 458 458 1.24 (25) Potash Cake ... ... 80 7 92 160 23 183 1.90
Potash Dryer
Feed Stream (25) Potash Cake 80 7 92 160 23 183 1.90
Products (26) Standard Red Product 66 0.3 99.5 132 - 132 2.00 (27) Dryer Dust ... 15 0.3 93 30 - 30 2.00 (M) Water Vapor . - 5.4 - - 21 21 1.00
Potash Flotation Tails Dewatering
Feed Stream (20) Potash Flotation Tails 386 478 37.4 572 1542 2114 1.45
Products (22) Filtrate (Saturated Brine) - 453 - - 1461 1461 1.24 (34) Tails Cake ...... 286 25 92 572 81 653 1.91 GALLONS PER SPECIFIC
UNIT OPERATION TONS PER HOUR PERCENT MINUTE GRAVITY
Pulp or
Solids Solution Solids Solids Solution Pulp Solution
Dryer Dust Agitator
Feed Stream (27) Dryer Dust 15 0.3 98 30 1 31 2.00 (28) Water - 62 - - 248 248 1.00
Product (29) Brine - 77.4 - - 249 249 1.24
Brine Balance
Recovered Brine (23) Dewatering Circuits (21) & (22) - 595 - - 1919 1919 1.24 (10) 1st Countercurrent Tails ... - 375 - - 1210 1210 1.24
Total Brine Recovered (24) - 970 - - 3129 3129 1.24
Prepared Brine (29) Dryer Dust Agitator .. - 77 - - 249 249 1.24
Total Available Brine (24) & (29) - 1047 - - 3378 3378 1.24
Brine Distribution (31) Returned to Process (2) & (4) . - 913 - - 2945 2945 1.24 (32) Routed to Crystallizer ... - 134 - - 433 433 1.24
Crystallizer Operation
Feed Stream (32) Brine - 134 - - 433 433 1.24
Products (33) White Product - 8 - 16 - 16 2.00 (16) Muds ... - 126 - - 430 430 1.17 The size of commercial flotation cells presently available range from 1 cubic foot to 2,000 cubic feet. Under these circumstances, it is necessary to calculate cell volume based on laboratory and/or pilot data for each particular installation. Calculations for a recovery system employing the process of the invention for a commercial size plant are given below, by way of example.
EXAMPLE V
Rougher Flotation Cells:
Hourly Design Tonnage 420 short tons of mine-run ore (400 short
tons dry)
Flotation Time 12 minutes
Percent Solids of Flotation Feed 30 (undissolved)
Specific Gravity of Solids 2.0 gms/cu. cm.
Specific Gravity of Brine 1.24 gms/cu. cm.
Tons/Hr of Slurry 400/.30=1333
Tons/Hr of Brine 1333-400=933 (933) (2000) GPM of Brine = = 3010 (1.24 (8.33) (60)
(400) (4)
GPM of Solids = 800
2.0
GPM of Slurry 3010+800=3810
Cell Volume Required 2010x12 minutes=45.720 gals.
Flotation Cell Specified 500 cu. ft.
Active Cell Volume 3200 gallons/cell
Number of Flotation Cells Required 45,720/3200=14.3
To maintain circuit synunetry 16 cells would generally be utilized.
Possible Ar@angements: 4 rows having 4 cells each
2 rows having 8 cells each (preferred to prevent short circuiting of
feed slurry)
Flow Rates:
4 rows- 952 GPM of slurry each
2 rows-1905 GPM of slurry each Products yew Flotation: Rougher Froth (advanced to 1st
countercurrent flotation cells) 34 tons/hr of slurry at 10% solids; 1055
GPM flotation Tails (feed to potash
flotation circuit) 993 tons/hr. of slurry at 36.8% solids:
2755 GPM -1st Countercurrent Flotation Cells:
Rougher Froth 340 tons/hr of slurry at 10% solids; 1055
GPM
Counterflow of 2nd Countercurrent
Tails 340 tons/hr of solution at 1.23 gms/cu.
cm. specific gravity; 1104 GPM
Total Flotation Feed 680 tons/hr of slurry at 5% solids; 2159
GPM
Flotation Time 15minutes
Total GPM of Feed Slurry 2159
Total Volume Required 2159 GPM X 15 minutes--32,385 gals.
Flotation Cell Specified 500 cu. ft.
Active Cell Volume 3200 gals.
Number of Flotation Cells Re
quired 32,385/3200----10.1 Arrangement One row of 10 cells
Flow rate 2159 GPM of slurry
Products from Flotation:
1st Countercurrent Froth
(advanced to 2nd countercurrent
flotation cells) 305 tons/hr at 10.5% solids; 945 GPM
1st Countercurrent Tails
(advanced to subsequent pro
cessing for extraction of desired
potash values) 375 tons/hr at 1.24 specific gravity; 1210
GPM
The recycle ratio r (see above) is calculated as follows:
340 tons/hr froth at 10% solids represents a liquid filow of 987 GPM.
340 tons/hr tails at 1.23 specific gravity represents a liquid flow of 1104 GPM.
1104
Consequently, r= =1.12 987
WHAT WE CLAIM IS:- 1. A process for recovering metallic values from a mixture thereof with mineral impurities, comprising:
(A) washing the mixture with a sol
vent for the metallic values, in which
solvent the impurities are substantially
insoluble, forming a solution of the
metallic values in the solvent and float
ing the insoluble impurities in the solu
tion, removing the floated impurities
from the solution,
(B) subjecting the floated impurities
to at least one subsequent flotation and
washing step, and where there are two
or more such flotation/washing steps, the
flow of solution being counter to that of
the impurities, the subsequent or the last
subsequent flotation/washing being with
water or barren solution, the solution
from the first subsequent or the subse
quent flotation / washing being used as
the solvent in step (A), and
(C) treating the solution from step
(A) to yield metallic values.
2. The process of claim 1, wherein step
B comprises three subsequent stages of flotation/washing, the first subsequent stage being carried out with counterflow of solution removed from the second stage, the second subsequent stage being carried out with counterflow of solution from the third stage, the third subsequent stage being carried out with water or barren solution and the solution portion of the first subsequent stage being used as the solvent in step (A).
3. The process of claim 1 or claim 2 wherein at least one flotation reagent selected from the group consisting of collectors and modifiers is added to the solution to achieve flotation of the insoluble mineral impurities.
4. The process of claim 3 wherein the values are copper values, the floated impurities are plagioclash quartz, hornblende, biotite and pyroxene, the collectors are a tertiary amine and a diamine, the modifier is citric acid and the solvent is an aqueous solution of sulfuric acid.
5. The process of claim 3 wherein the values are gold values, the floated impurities are plagioclase, quartz, hornblende, biotite and pyroxene, the collector is a primary amine, the modifiers are iron sulfate and aluminum sulfate, the solvent is an aqueous solution of cyanide, and lime is used to maintain a basic pH.
6. The process of any one of claims 1
**WARNING** end of DESC field may overlap start of CLMS **.
Claims (42)
- **WARNING** start of CLMS field may overlap end of DESC **.Total Flotation Feed 680 tons/hr of slurry at 5% solids; 2159 GPM Flotation Time 15minutes Total GPM of Feed Slurry 2159 Total Volume Required 2159 GPM X 15 minutes--32,385 gals.Flotation Cell Specified 500 cu. ft.Active Cell Volume 3200 gals.Number of Flotation Cells Re quired 32,385/3200----10.1 Arrangement One row of 10 cells Flow rate 2159 GPM of slurry Products from Flotation: 1st Countercurrent Froth (advanced to 2nd countercurrent flotation cells) 305 tons/hr at 10.5% solids; 945 GPM 1st Countercurrent Tails (advanced to subsequent pro cessing for extraction of desired potash values) 375 tons/hr at 1.24 specific gravity; 1210 GPM The recycle ratio r (see above) is calculated as follows:340 tons/hr froth at 10% solids represents a liquid filow of 987 GPM.340 tons/hr tails at 1.23 specific gravity represents a liquid flow of 1104 GPM.1104 Consequently, r= =1.12 987 WHAT WE CLAIM IS:- 1. A process for recovering metallic values from a mixture thereof with mineral impurities, comprising: (A) washing the mixture with a sol vent for the metallic values, in which solvent the impurities are substantially insoluble, forming a solution of the metallic values in the solvent and float ing the insoluble impurities in the solu tion, removing the floated impurities from the solution, (B) subjecting the floated impurities to at least one subsequent flotation and washing step, and where there are two or more such flotation/washing steps, the flow of solution being counter to that of the impurities, the subsequent or the last subsequent flotation/washing being with water or barren solution, the solution from the first subsequent or the subse quent flotation / washing being used as the solvent in step (A), and (C) treating the solution from step (A) to yield metallic values.
- 2. The process of claim 1, wherein step B comprises three subsequent stages of flotation/washing, the first subsequent stage being carried out with counterflow of solution removed from the second stage, the second subsequent stage being carried out with counterflow of solution from the third stage, the third subsequent stage being carried out with water or barren solution and the solution portion of the first subsequent stage being used as the solvent in step (A).
- 3. The process of claim 1 or claim 2 wherein at least one flotation reagent selected from the group consisting of collectors and modifiers is added to the solution to achieve flotation of the insoluble mineral impurities.
- 4. The process of claim 3 wherein the values are copper values, the floated impurities are plagioclash quartz, hornblende, biotite and pyroxene, the collectors are a tertiary amine and a diamine, the modifier is citric acid and the solvent is an aqueous solution of sulfuric acid.
- 5. The process of claim 3 wherein the values are gold values, the floated impurities are plagioclase, quartz, hornblende, biotite and pyroxene, the collector is a primary amine, the modifiers are iron sulfate and aluminum sulfate, the solvent is an aqueous solution of cyanide, and lime is used to maintain a basic pH.
- 6. The process of any one of claims 1to 3 wherein the values are potassium values and the solvent is water.
- 7. The process of any one of claims 1 to 3 wherein the values are sodium values and the solvent is water.
- 8. The proces of any one of claims 1 to 3 wherein the values are magnesium values and the solvent is water.
- 9. The process of any one of claims 1 to 3 wherein the values are lithium values and the solvent is water.
- 10. The process of any one of claims 1 to 3 wherein the values are copper values and the solvent is an aqueous solution of sulfuric acid.
- 11. The process of any one of claims 1 to 3 wherein the values are copper values and the solvent is an aqueous solution of hydrochloric acid.
- 12. The process of any one of claims 1 to 3 wherein the values are copper values and the solvent is an aqueous solution of ferric chloride.
- 13. The process of any one of claims 1 to 3 wherein the values are uranium values and the solvent is an aqueous solution of sulfuric acid.
- 14. The process of any one of claims 1 to 3 wherein the values are uranium values and the solvent is an aqueous solution of sodium carbonate and sodium bicarbonate.
- 15. The process of any one of claims 1 to 3 wherein the values are gold values and the solvent is an aqueous solution of sodium cyanide.
- 16. The process of any one of claims 1 to 3 wherein the values are silver values and the solvent is an aqueous solution of sodium cyanide.
- 17. The process of any one of claims 1 to 3 wherein the values are silver values and the solvent is an aqueous solution of sodium hypochlorite.
- 18. The process of any one of claims 1 to 3 wherein the values are silver values and the solvent is an aqueous solution of potassium hypochlorite.
- 19. The process of any one of claims 1 to 3 wherein the values are nickel values and the solvent is an aqueous solution of ammonia.
- 20. The process of any one of claims 1 to 3 wherein the values are nickel values and the solvent is an aqueous solution of ammonium carbonate.
- 21. The process of any one of claims 1 to 3 wherein the values are cobalt values and the solvent is an aqueous solution of sulfuric acid.
- 22. The process of any one of claims 1 to 3 wherein the values are zinc values and the solvent is an aqueous solution of sulfuric acid.
- 23. The process of any one of claims 1 to 3 wherein the values are aluminum values and the solvent is an aqueous solution of sodium hydroxide.
- 24. The process of any one of claims 1 to 3 wherein the values are tungsten values and the solvent is an aqueous solution of hydrochloric acid.
- 25. The process of any one of claims 1 to 3 wherein the values are titanium values and the solvent is an aqueous solution of sulfuric acid.
- 26. The process of any one of claims 1 to 3 wherein the values are titanium values and the solvent is an aqueous solution of hydrochloric acid.
- 27. The process of any one of claims 1 to 3 wherein the values are antimony values and the solvent is an aqueous solution of sodium sulfide.
- 28. The process of any one of claims 1 to 3 wherein the values are antimony values and the solvent is an aqueous solution of hydrochloric acid.
- 29. The process of any one of claims 1 to 3 wherein the values are barium values and the solvent is an aqueous solution of hydrofluoric acid.
- 30. The process of any one of claims 1 to 3 wherein the values are barium values and the solvent is an aqueous solution of nitric acid.
- 31. The process of any one of claims 1 to 3 wherein the values are rhenium values and the solvent is an aqueous solution of chlorine.
- 32. The process of any one of claims 1 to 3 wherein the values are rhenium values and the solvent is an aqueous solution of sodium hypochlorite.
- 33. The process of any one of claims 1 to 3 wherein the values are potassium values, recovered from potash, and the solvent is water.
- 34. The process of claim 4 wherein hydrofluoric acid is also employed as a modifier.
- 35. The process of any one of claims 1 to 3 and 6 to 33 wherein the modifier is polyacrylamide and the collector is an ethanolated alkyl guanidineamine.
- 36. A process for recovering potassium values from a mixture of impurities and potassium as potash, comprising: a. adding to the mixture an aqueous solution containing the maximum amount of potash dissolved therein: b. adding to the mixture and aqueous solution at least one flotation reagent selected from the group consisting of collectors and modifiers to effect flotation of the impurities; c. floating the impurities in the aqueous solution; d. removing the floated impurities from said aqueous solution; e. processing the aqueous solution and the undissolved potash associated therewith to separate the undissolved potash, f. subjecting the floated impurities to subsequent stages of flotation! washing with counterflow of solution removed from each subsequent stage of flotation, water being used in the last stage; solution from the first subsequent stage being used as the solution for step (a) and g. processing either (1) solution portion of the first subsequent stage or (2) the aqueous solution from step (e), or both (1) and (2), to yield the potassium values dissolved therein.
- 37. The process of claim 36 wherein the modifier is polyacrylamide and the collector is ethanolated alkyl guanidineamine.
- 38. The process of claim 36 or claim 37 wherein: a. the water added to the last stage is regulated such that the solution portion of the first subsequent stage is a solution with the maximum amount of potash dissolved therein; b. the solution portion from the first subsequent stage is mived with the aqueous solution formerly associated with the undissolved potash after the undissolved potash has been separated therefrom; c. a portion of the resulting solution mixture is used as the aqueous solution containing the maximum amount of potash dissolved therein initially added to the mixture of potash and impurities; and d. the portion of the resulting solution mixture not needed for addition to the mixture of potash and impurities is processed to yield the potassium dissolved therein.
- 29. The process of any one of claims 1 to 38, wherein washing and flotation are facilitated in at least one step by agitation.
- 40. The process of claim 1 conducted substantially as described in any one of the Examples herein.
- 41. The process of claim 1 conducted substantially as described with reference to the reaction schemes set out in any one of Figures 1 to 4 herein.
- 42. A purified value obtained by the process of any one of claims 1 to 41.
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US62794975A | 1975-11-03 | 1975-11-03 |
Publications (1)
Publication Number | Publication Date |
---|---|
GB1567765A true GB1567765A (en) | 1980-05-21 |
Family
ID=24516779
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
GB45100/76A Expired GB1567765A (en) | 1975-11-03 | 1976-10-29 | Flotation process |
Country Status (8)
Country | Link |
---|---|
JP (1) | JPS5286977A (en) |
AU (1) | AU509567B2 (en) |
BR (1) | BR7607300A (en) |
CA (1) | CA1085172A (en) |
DE (3) | DE2649708C3 (en) |
FR (1) | FR2329352A1 (en) |
GB (1) | GB1567765A (en) |
ZA (1) | ZA766304B (en) |
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB2129714A (en) * | 1982-11-13 | 1984-05-23 | Kloeckner Humboldt Deutz Ag | Method of and apparatus for preparing very fine coal |
GB2150049A (en) * | 1983-11-22 | 1985-06-26 | Cominco Ltd | Flotation of insolubles from potashores |
WO2006069760A1 (en) * | 2004-12-24 | 2006-07-06 | Basf Aktiengesellschaft | Use of surfactants in the production of metal |
WO2016164600A1 (en) * | 2015-04-08 | 2016-10-13 | Ecolab Usa Inc. | Leach aid for metal recovery |
CN115090410A (en) * | 2022-06-22 | 2022-09-23 | 江西博瑞新材料科技有限公司 | Technological method for purifying ceramic raw material from lithium ore pressing tail mud |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2912759A1 (en) * | 2007-02-16 | 2008-08-22 | Suez Environnement Sa | Utilizing blast furnace dust and sludge, by granulometrically sorting light component to give recyclable heavy fraction and zinc and/or lead enriched light fraction |
CN112301226B (en) * | 2020-10-01 | 2022-04-29 | 承德石油高等专科学校 | Soil rubidium salt circulating leaching and content calculating method |
Family Cites Families (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2923408A (en) * | 1954-12-27 | 1960-02-02 | Dow Chemical Co | Flotation process |
US3738692A (en) * | 1971-07-16 | 1973-06-12 | Scient Anglers Inc | Pre-tied nail knot |
CA998840A (en) * | 1972-03-07 | 1976-10-26 | Nathaniel Arbiter | Recovery of metals |
CA971368A (en) * | 1972-11-20 | 1975-07-22 | Paul Kawulka | Recovery of zinc from zinc sulphides by direct pressure leaching |
JPS5067716A (en) * | 1973-10-22 | 1975-06-06 | ||
JPS50131617A (en) * | 1974-04-06 | 1975-10-17 |
-
1976
- 1976-10-22 ZA ZA766304A patent/ZA766304B/en unknown
- 1976-10-29 BR BR7607300A patent/BR7607300A/en unknown
- 1976-10-29 DE DE2649708A patent/DE2649708C3/en not_active Expired
- 1976-10-29 GB GB45100/76A patent/GB1567765A/en not_active Expired
- 1976-10-29 DE DE2660422A patent/DE2660422C2/en not_active Expired
- 1976-10-29 DE DE2660423A patent/DE2660423C2/en not_active Expired
- 1976-11-01 AU AU19204/76A patent/AU509567B2/en not_active Expired
- 1976-11-02 CA CA264,658A patent/CA1085172A/en not_active Expired
- 1976-11-02 FR FR7633002A patent/FR2329352A1/en active Granted
- 1976-11-02 JP JP13225476A patent/JPS5286977A/en active Granted
Cited By (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB2129714A (en) * | 1982-11-13 | 1984-05-23 | Kloeckner Humboldt Deutz Ag | Method of and apparatus for preparing very fine coal |
GB2150049A (en) * | 1983-11-22 | 1985-06-26 | Cominco Ltd | Flotation of insolubles from potashores |
WO2006069760A1 (en) * | 2004-12-24 | 2006-07-06 | Basf Aktiengesellschaft | Use of surfactants in the production of metal |
US7862785B2 (en) | 2004-12-24 | 2011-01-04 | Basf Aktiengesellschaft | Use of surfactants in the production of metal |
WO2016164600A1 (en) * | 2015-04-08 | 2016-10-13 | Ecolab Usa Inc. | Leach aid for metal recovery |
CN107406909A (en) * | 2015-04-08 | 2017-11-28 | 艺康美国股份有限公司 | Leaching agent for metal recovery |
US10344353B2 (en) | 2015-04-08 | 2019-07-09 | Ecolab Usa Inc. | Leach aid for metal recovery |
CN107406909B (en) * | 2015-04-08 | 2020-06-26 | 艺康美国股份有限公司 | Leaching aid for metal recovery |
EA037655B1 (en) * | 2015-04-08 | 2021-04-27 | ЭКОЛАБ ЮЭсЭй ИНК. | Leach aid for metal recovery |
CN115090410A (en) * | 2022-06-22 | 2022-09-23 | 江西博瑞新材料科技有限公司 | Technological method for purifying ceramic raw material from lithium ore pressing tail mud |
CN115090410B (en) * | 2022-06-22 | 2023-11-14 | 江西博瑞新材料科技有限公司 | Technological method for purifying ceramic raw material by using lithium ore pressed tail mud |
Also Published As
Publication number | Publication date |
---|---|
ZA766304B (en) | 1977-09-28 |
AU1920476A (en) | 1978-05-11 |
FR2329352A1 (en) | 1977-05-27 |
JPS5618657B2 (en) | 1981-04-30 |
JPS5286977A (en) | 1977-07-20 |
CA1085172A (en) | 1980-09-09 |
DE2649708B2 (en) | 1979-08-02 |
BR7607300A (en) | 1977-09-13 |
FR2329352B3 (en) | 1979-07-13 |
DE2649708A1 (en) | 1977-05-05 |
DE2649708C3 (en) | 1980-04-10 |
AU509567B2 (en) | 1980-05-15 |
DE2660423C2 (en) | 1981-10-01 |
DE2660422C2 (en) | 1981-10-01 |
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Legal Events
Date | Code | Title | Description |
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PS | Patent sealed [section 19, patents act 1949] | ||
732 | Registration of transactions, instruments or events in the register (sect. 32/1977) | ||
PCNP | Patent ceased through non-payment of renewal fee |