CN117019374A - Oxidized ore backwater treatment method - Google Patents
Oxidized ore backwater treatment method Download PDFInfo
- Publication number
- CN117019374A CN117019374A CN202311006086.4A CN202311006086A CN117019374A CN 117019374 A CN117019374 A CN 117019374A CN 202311006086 A CN202311006086 A CN 202311006086A CN 117019374 A CN117019374 A CN 117019374A
- Authority
- CN
- China
- Prior art keywords
- backwater
- ore
- oxidized
- flotation
- regulator
- 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.)
- Pending
Links
- 238000000034 method Methods 0.000 title claims abstract description 72
- 238000000227 grinding Methods 0.000 claims abstract description 80
- 238000005188 flotation Methods 0.000 claims abstract description 59
- 229910052500 inorganic mineral Inorganic materials 0.000 claims abstract description 41
- 239000011707 mineral Substances 0.000 claims abstract description 41
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 32
- 230000008569 process Effects 0.000 claims abstract description 31
- 239000002002 slurry Substances 0.000 claims abstract description 31
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 30
- 239000001301 oxygen Substances 0.000 claims abstract description 30
- 238000000926 separation method Methods 0.000 claims abstract description 28
- 239000012141 concentrate Substances 0.000 claims abstract description 20
- 239000008394 flocculating agent Substances 0.000 claims abstract description 4
- 235000010755 mineral Nutrition 0.000 claims description 40
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 22
- 238000004064 recycling Methods 0.000 claims description 19
- VTIIJXUACCWYHX-UHFFFAOYSA-L disodium;carboxylatooxy carbonate Chemical compound [Na+].[Na+].[O-]C(=O)OOC([O-])=O VTIIJXUACCWYHX-UHFFFAOYSA-L 0.000 claims description 14
- 229940045872 sodium percarbonate Drugs 0.000 claims description 14
- 238000004062 sedimentation Methods 0.000 claims description 13
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 11
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 claims description 10
- 229910052806 inorganic carbonate Inorganic materials 0.000 claims description 8
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 claims description 6
- BHDAXLOEFWJKTL-UHFFFAOYSA-L dipotassium;carboxylatooxy carbonate Chemical compound [K+].[K+].[O-]C(=O)OOC([O-])=O BHDAXLOEFWJKTL-UHFFFAOYSA-L 0.000 claims description 6
- 238000001914 filtration Methods 0.000 claims description 6
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 claims description 6
- 229910000360 iron(III) sulfate Inorganic materials 0.000 claims description 6
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 5
- 239000003795 chemical substances by application Substances 0.000 claims description 5
- GRLPQNLYRHEGIJ-UHFFFAOYSA-J potassium aluminium sulfate Chemical compound [Al+3].[K+].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O GRLPQNLYRHEGIJ-UHFFFAOYSA-J 0.000 claims description 5
- 229910000027 potassium carbonate Inorganic materials 0.000 claims description 5
- 229940103272 aluminum potassium sulfate Drugs 0.000 claims description 4
- 239000011790 ferrous sulphate Substances 0.000 claims description 4
- 235000003891 ferrous sulphate Nutrition 0.000 claims description 4
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 claims description 4
- 229910000359 iron(II) sulfate Inorganic materials 0.000 claims description 4
- ATRRKUHOCOJYRX-UHFFFAOYSA-N Ammonium bicarbonate Chemical compound [NH4+].OC([O-])=O ATRRKUHOCOJYRX-UHFFFAOYSA-N 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
- 229910021578 Iron(III) chloride Inorganic materials 0.000 claims description 3
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 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
- 239000001099 ammonium carbonate Substances 0.000 claims description 3
- 235000012501 ammonium carbonate Nutrition 0.000 claims description 3
- 229960002089 ferrous chloride Drugs 0.000 claims description 3
- NMCUIPGRVMDVDB-UHFFFAOYSA-L iron dichloride Chemical compound Cl[Fe]Cl NMCUIPGRVMDVDB-UHFFFAOYSA-L 0.000 claims description 3
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 claims description 3
- 229920002401 polyacrylamide Polymers 0.000 claims description 3
- 239000011734 sodium Substances 0.000 claims description 3
- 229910052708 sodium Inorganic materials 0.000 claims description 3
- 230000004913 activation Effects 0.000 claims 1
- 238000007667 floating Methods 0.000 abstract description 7
- 238000003672 processing method Methods 0.000 abstract 1
- 230000003647 oxidation Effects 0.000 description 32
- 238000007254 oxidation reaction Methods 0.000 description 32
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 29
- 150000002500 ions Chemical class 0.000 description 22
- 230000000052 comparative effect Effects 0.000 description 20
- 230000000694 effects Effects 0.000 description 20
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 18
- 238000010494 dissociation reaction Methods 0.000 description 15
- 230000005593 dissociations Effects 0.000 description 15
- 229910021645 metal ion Inorganic materials 0.000 description 15
- 238000005868 electrolysis reaction Methods 0.000 description 13
- 238000001179 sorption measurement Methods 0.000 description 12
- 239000003153 chemical reaction reagent Substances 0.000 description 11
- 239000000243 solution Substances 0.000 description 11
- INJRKJPEYSAMPD-UHFFFAOYSA-N aluminum;silicic acid;hydrate Chemical compound O.[Al].[Al].O[Si](O)(O)O INJRKJPEYSAMPD-UHFFFAOYSA-N 0.000 description 10
- 239000011575 calcium Substances 0.000 description 10
- 239000010443 kyanite Substances 0.000 description 10
- 229910052850 kyanite Inorganic materials 0.000 description 10
- 239000011777 magnesium Substances 0.000 description 10
- 230000004048 modification Effects 0.000 description 10
- 238000012986 modification Methods 0.000 description 10
- 229910052761 rare earth metal Inorganic materials 0.000 description 10
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 9
- 230000015556 catabolic process Effects 0.000 description 9
- 238000006731 degradation reaction Methods 0.000 description 9
- 150000002910 rare earth metals Chemical class 0.000 description 9
- 238000005728 strengthening Methods 0.000 description 9
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 description 8
- 229910052744 lithium Inorganic materials 0.000 description 8
- 238000003756 stirring Methods 0.000 description 8
- 230000033558 biomineral tissue development Effects 0.000 description 7
- 230000003197 catalytic effect Effects 0.000 description 7
- 239000003607 modifier Substances 0.000 description 7
- 238000011084 recovery Methods 0.000 description 7
- 230000002829 reductive effect Effects 0.000 description 7
- 230000001105 regulatory effect Effects 0.000 description 7
- MWNQXXOSWHCCOZ-UHFFFAOYSA-L sodium;oxido carbonate Chemical compound [Na+].[O-]OC([O-])=O MWNQXXOSWHCCOZ-UHFFFAOYSA-L 0.000 description 6
- 230000000593 degrading effect Effects 0.000 description 5
- 239000003814 drug Substances 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 238000002156 mixing Methods 0.000 description 5
- 230000001590 oxidative effect Effects 0.000 description 5
- 230000003213 activating effect Effects 0.000 description 4
- 230000002411 adverse Effects 0.000 description 4
- -1 carbonate anions Chemical class 0.000 description 4
- JYYOBHFYCIDXHH-UHFFFAOYSA-N carbonic acid;hydrate Chemical compound O.OC(O)=O JYYOBHFYCIDXHH-UHFFFAOYSA-N 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 4
- 125000001183 hydrocarbyl group Chemical group 0.000 description 4
- 239000007800 oxidant agent Substances 0.000 description 4
- 239000002957 persistent organic pollutant Substances 0.000 description 4
- 230000002195 synergetic effect Effects 0.000 description 4
- NEAQRZUHTPSBBM-UHFFFAOYSA-N 2-hydroxy-3,3-dimethyl-7-nitro-4h-isoquinolin-1-one Chemical compound C1=C([N+]([O-])=O)C=C2C(=O)N(O)C(C)(C)CC2=C1 NEAQRZUHTPSBBM-UHFFFAOYSA-N 0.000 description 3
- 230000010718 Oxidation Activity Effects 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 239000002253 acid Substances 0.000 description 3
- CNLWCVNCHLKFHK-UHFFFAOYSA-N aluminum;lithium;dioxido(oxo)silane Chemical compound [Li+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O CNLWCVNCHLKFHK-UHFFFAOYSA-N 0.000 description 3
- 238000006555 catalytic reaction Methods 0.000 description 3
- 230000007797 corrosion Effects 0.000 description 3
- 238000005260 corrosion Methods 0.000 description 3
- 238000000354 decomposition reaction Methods 0.000 description 3
- 239000002283 diesel fuel Substances 0.000 description 3
- 235000014113 dietary fatty acids Nutrition 0.000 description 3
- 238000010790 dilution Methods 0.000 description 3
- 239000012895 dilution Substances 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 239000000194 fatty acid Substances 0.000 description 3
- 229930195729 fatty acid Natural products 0.000 description 3
- 150000004665 fatty acids Chemical class 0.000 description 3
- 239000008235 industrial water Substances 0.000 description 3
- 229910052742 iron Inorganic materials 0.000 description 3
- 230000001089 mineralizing effect Effects 0.000 description 3
- 239000003960 organic solvent Substances 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 229910052642 spodumene Inorganic materials 0.000 description 3
- 238000012360 testing method Methods 0.000 description 3
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- 229910019440 Mg(OH) Inorganic materials 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 239000010949 copper Substances 0.000 description 2
- 239000006185 dispersion Substances 0.000 description 2
- 239000002223 garnet Substances 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- YDZQQRWRVYGNER-UHFFFAOYSA-N iron;titanium;trihydrate Chemical compound O.O.O.[Ti].[Fe] YDZQQRWRVYGNER-UHFFFAOYSA-N 0.000 description 2
- 239000005416 organic matter Substances 0.000 description 2
- 239000012188 paraffin wax Substances 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 239000000344 soap Substances 0.000 description 2
- 239000004575 stone Substances 0.000 description 2
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 1
- 229910000851 Alloy steel Inorganic materials 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-M Bisulfite Chemical compound OS([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-M 0.000 description 1
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 1
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 1
- 229910000975 Carbon steel Inorganic materials 0.000 description 1
- 229910001018 Cast iron Inorganic materials 0.000 description 1
- 241000208818 Helianthus Species 0.000 description 1
- 235000003222 Helianthus annuus Nutrition 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- FPOQLQZHRCEVOT-UHFFFAOYSA-N N-hydroxy-2-phenylacetamide Chemical compound ONC(=O)CC1=CC=CC=C1 FPOQLQZHRCEVOT-UHFFFAOYSA-N 0.000 description 1
- 238000003723 Smelting Methods 0.000 description 1
- 229910010413 TiO 2 Inorganic materials 0.000 description 1
- 239000012190 activator Substances 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- WYTGDNHDOZPMIW-RCBQFDQVSA-N alstonine Natural products C1=CC2=C3C=CC=CC3=NC2=C2N1C[C@H]1[C@H](C)OC=C(C(=O)OC)[C@H]1C2 WYTGDNHDOZPMIW-RCBQFDQVSA-N 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 150000001413 amino acids Chemical class 0.000 description 1
- 229910052849 andalusite Inorganic materials 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 239000011805 ball Substances 0.000 description 1
- 229910001570 bauxite Inorganic materials 0.000 description 1
- 239000001110 calcium chloride Substances 0.000 description 1
- 229910001628 calcium chloride Inorganic materials 0.000 description 1
- 229910001424 calcium ion Inorganic materials 0.000 description 1
- 239000010962 carbon steel Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 229910001919 chlorite Inorganic materials 0.000 description 1
- 229910052619 chlorite group Inorganic materials 0.000 description 1
- QBWCMBCROVPCKQ-UHFFFAOYSA-N chlorous acid Chemical compound OCl=O QBWCMBCROVPCKQ-UHFFFAOYSA-N 0.000 description 1
- 230000003750 conditioning effect Effects 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 229910000365 copper sulfate Inorganic materials 0.000 description 1
- ARUVKPQLZAKDPS-UHFFFAOYSA-L copper(II) sulfate Chemical compound [Cu+2].[O-][S+2]([O-])([O-])[O-] ARUVKPQLZAKDPS-UHFFFAOYSA-L 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 239000007857 degradation product Substances 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 230000033444 hydroxylation Effects 0.000 description 1
- 238000005805 hydroxylation reaction Methods 0.000 description 1
- QWPPOHNGKGFGJK-UHFFFAOYSA-N hypochlorous acid Chemical compound ClO QWPPOHNGKGFGJK-UHFFFAOYSA-N 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N iron oxide Inorganic materials [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 1
- RLJMLMKIBZAXJO-UHFFFAOYSA-N lead nitrate Chemical compound [O-][N+](=O)O[Pb]O[N+]([O-])=O RLJMLMKIBZAXJO-UHFFFAOYSA-N 0.000 description 1
- 229910052629 lepidolite Inorganic materials 0.000 description 1
- 150000002632 lipids Chemical class 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- ZLNQQNXFFQJAID-UHFFFAOYSA-L magnesium carbonate Chemical compound [Mg+2].[O-]C([O-])=O ZLNQQNXFFQJAID-UHFFFAOYSA-L 0.000 description 1
- 239000001095 magnesium carbonate Substances 0.000 description 1
- 229910000021 magnesium carbonate Inorganic materials 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000010445 mica Substances 0.000 description 1
- 229910052618 mica group Inorganic materials 0.000 description 1
- 239000011859 microparticle Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- JLXAQYGJCVUJLE-UHFFFAOYSA-N n-hydroxynonanamide Chemical compound CCCCCCCCC(=O)NO JLXAQYGJCVUJLE-UHFFFAOYSA-N 0.000 description 1
- 229910052754 neon Inorganic materials 0.000 description 1
- GKAOGPIIYCISHV-UHFFFAOYSA-N neon atom Chemical compound [Ne] GKAOGPIIYCISHV-UHFFFAOYSA-N 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 230000033116 oxidation-reduction process Effects 0.000 description 1
- NDLPOXTZKUMGOV-UHFFFAOYSA-N oxo(oxoferriooxy)iron hydrate Chemical compound O.O=[Fe]O[Fe]=O NDLPOXTZKUMGOV-UHFFFAOYSA-N 0.000 description 1
- 235000019353 potassium silicate Nutrition 0.000 description 1
- UMPKMCDVBZFQOK-UHFFFAOYSA-N potassium;iron(3+);oxygen(2-) Chemical compound [O-2].[O-2].[K+].[Fe+3] UMPKMCDVBZFQOK-UHFFFAOYSA-N 0.000 description 1
- 239000010453 quartz Substances 0.000 description 1
- 238000007348 radical reaction Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 230000002000 scavenging effect Effects 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- NTHWMYGWWRZVTN-UHFFFAOYSA-N sodium silicate Chemical compound [Na+].[Na+].[O-][Si]([O-])=O NTHWMYGWWRZVTN-UHFFFAOYSA-N 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 238000010408 sweeping Methods 0.000 description 1
- 230000001360 synchronised effect Effects 0.000 description 1
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N titanium dioxide Inorganic materials O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 1
- 229910052613 tourmaline Inorganic materials 0.000 description 1
- 239000011032 tourmaline Substances 0.000 description 1
- 229940070527 tourmaline Drugs 0.000 description 1
- 239000010456 wollastonite Substances 0.000 description 1
- 229910052882 wollastonite Inorganic materials 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
- B03B—SEPARATING SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS
- B03B7/00—Combinations of wet processes or apparatus with other processes or apparatus, e.g. for dressing ores or garbage
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D1/00—Flotation
- B03D1/001—Flotation agents
- B03D1/018—Mixtures of inorganic and organic compounds
-
- 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
- B03D3/00—Differential sedimentation
- B03D3/06—Flocculation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D2201/00—Specified effects produced by the flotation agents
- B03D2201/002—Coagulants and Flocculants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D2201/00—Specified effects produced by the flotation agents
- B03D2201/007—Modifying reagents for adjusting pH or conductivity
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D2203/00—Specified materials treated by the flotation agents; specified applications
- B03D2203/02—Ores
Landscapes
- Chemical & Material Sciences (AREA)
- Inorganic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
The application provides a method for treating backwater of oxidized ore. The processing method comprises the following steps: step S1, adding a flocculating agent into backwater A generated in a flotation process, and settling suspended matters in backwater to obtain backwater B; s2, adding backwater B into ore grinding operation, and adding an regulator with an oxygen release function in the ore grinding operation process to obtain ore pulp C; s3, adding backwater B into the ore pulp C to dilute to the concentration required by the first flotation step, so as to obtain mineralized slurry D to be separated; and S4, carrying out flotation separation on the mineralized slurry D to obtain oxidized ore concentrate E and separated tailings F. The method has simple process, embeds the backwater utilization and treatment into the mineral grinding and floating separation system, does not need to additionally add a backwater treatment system, and has low backwater utilization cost.
Description
Technical Field
The application relates to the technical field of ore dressing backwater recycling, in particular to a backwater treatment method for oxidized ores.
Background
The recovery of the beneficiation backwater is an effective way for saving water, reducing energy consumption and protecting environment; wherein, the utilization of the backwater of the oxidized ore is a common problem in the oxidized ore dressing and smelting industry for a long time. The backwater of the oxidized ore contains more components such as suspended matters of fine particles, refractory organic matters, soluble metal ions and the like, so that the backwater affects the separation process of the mineral of the oxidized ore relatively remarkably, and therefore, the backwater basically needs to be recycled after being treated. At present, the treatment method of the oxidized ore backwater mainly comprises the following steps: neutralization precipitation method, ion exchange method, natural degradation method, biological oxidation method, deep oxidation method, adsorption method, etc. In contrast, in order to satisfy the degradation or decomposition of organic matters with long hydrocarbon chains and complex ring structures used in the floatation operation of oxidized ores, in the aspect of the disposal of the oxidized ore backwater, a relatively efficient organic matter oxidation and degradation method is to degrade organic matter ions in the beneficiation backwater by deep oxidation, such as the utilization of hydroxyl radicals (OH, E) with strong oxidability 0 2.80V) is an oxidant and the oxidant combination is oxidized and decomposed.
In order to achieve the purpose of recycling backwater, the prior art is concentrated on a relatively independent backwater disposal system and a relatively independent backwater disposal method. The research on the degradation of beneficiation backwater by the paper advanced oxidation method is that China color project, volume 10 and fourth period in 2020: 65-71' discuss in H 2 O 2 The US advanced oxidation technology provides relative advantages for the flotation backwater degradation effect of the Bayan obo rare earth ore containing the negative and positive combined ion collector, but does not consider the influence of metal ions, and backwater treatment is required to be carried out in a relatively independent system. The patent application with publication number of CN106977009A provides a rapid treatment and recycling method for spodumene flotation tailing water, which uses a mixture of ferrous sulfate, polymeric ferric sulfate and hypochlorous acid with strong oxidability to carry out multistage treatment on backwater. However, there are few reports on related technologies on the synchronous treatment of organic residues and unavoidable metal ions in the backwater of oxidized ores.
Although many advantageous techniques for the treatment and utilization of beneficiation backwater have been reported, in particular in advanced oxidation treatment of backwater. However, in relative terms, the existing advanced oxidation techniques suffer from more or less from the following drawbacks: 1) The method is mainly dependent on the effective concentration and the oxidation performance of the advanced oxidant, and has the advantages of large medicament demand and low oxidation efficiency; 2) Independent water treatment systems are needed, and large-scale industrial systems have large investment and high treatment cost; 3) When the strong active oxidant is used for catalytic oxidation, organic pollutants are mostly used as target degradation products, and unavoidable ions (Ca) in backwater are usually ignored 2+ \Mg 2+ \Al 3+ \Fe 3+ \Cu 2+ \Pb 2+ Etc.) on mineral sorting.
Oxidized ore backwater is often limited by the influences of micro-particle suspended matters, organic medicament residues, unavoidable metal ions and the like in backwater, and the existing oxidized ore backwater is basically used after being treated, and the backwater utilization technology has the following defects: 1) The organic pollutants in the backwater are mostly refractory organic matters, the treatment efficiency is generally low, the flotation separation system is easy to be disturbed, and the consumption of the medicament required by treatment is large and the cost is high. 2) The different components in the backwater have obvious influence on the sorting index of the oxidized minerals, the deterioration trend of different expression of residual organic matters and soluble unavoidable ions is difficult to synchronously treat or avoid the influence of metal ions and organic matters residues. 3) The output of backwater from a large-scale factory is large, the treatment time is usually limited, and particularly in the area of water shortage, the fast treatment and recycling of backwater are difficult.
Therefore, the development of new oxidized ore backwater treatment and the utilization of new technology are of great significance.
Disclosure of Invention
The application mainly aims to provide a method for treating oxidized ore backwater, which aims to solve the problem of low oxidized ore backwater treatment efficiency in the prior art.
In order to achieve the above object, according to one aspect of the present application, there is provided an oxidized ore backwater treatment method comprising: step S1, adding a flocculating agent into backwater A generated in a flotation process, and settling suspended matters in backwater to obtain backwater B; s2, adding backwater B into ore grinding operation, and adding an regulator with an oxygen release function in the ore grinding operation process to obtain ore pulp C; s3, adding backwater B into the ore pulp C to dilute to the concentration required by the first flotation step, so as to obtain mineralized slurry D to be separated; and S4, carrying out flotation separation on the mineralized slurry D to obtain oxidized ore concentrate E and separated tailings F.
Further, the flocculant includes: any one or more of polyaluminium chloride, polyaluminium sulfate, aluminum sulfate, ferric sulfate, ferrous sulfate, aluminum chloride, ferric chloride, ferrous chloride, aluminum potassium sulfate and polyacrylamide.
Further, the addition amount of the flocculant is 0.02-1.0 g/L.
Further, the regulator with oxygen release function is a carbonation modifying regulator, and the preferred carbonation modifying regulator is any one or more of sodium percarbonate, sodium biperfarbonate and potassium percarbonate.
Further, the addition amount of the regulator with the oxygen release function is 0.1-5.0 g/L relative to the clarified backwater B.
Further, inorganic carbonate is added in the ore grinding operation process, preferably, the inorganic carbonate is selected from any one or more of sodium carbonate, ammonium carbonate and potassium carbonate; preferably, the addition amount of the inorganic carbonate is 0.1-5.0 g/L relative to the clarified backwater B.
Further, in the step S2, the mass concentration of the ore pulp in the ore grinding operation process is 40% -70%.
Further, in the step S3, the mass concentration of the mineralized slurry D to be sorted is 10% -45%.
Further, in step S3, an activated sorting regulator and/or a mineral collector is added to the pulp C.
And further, returning the beneficiation backwater produced after the sedimentation and filtration of the concentrate E and the tailings F as backwater A to the step S1 for recycling.
By applying the technical scheme of the application, backwater treatment and ore grinding flotation are coupled, i.e. a modified regulator with oxygen release function is added in the ore grinding process, and O is formed by the property of slowly releasing oxygen and the reductive Fe generated by corrosion of ore grinding medium 2 /H 2 O 2 oxidation-Fe reduction catalytic micro-electrolysis, degrading organic matters in backwater, and simultaneously cooperating with OH - The influence of unavoidable metal ions in the adsorption modified backwater can be achieved, and the following purposes are achieved: the degradation or decomposition degree of organic matters in backwater is improved by the strong oxidation micro-electrolysis effect of Fe catalysis, and the adverse effect of the organic matters is avoided; on one hand, a carbonate-hydroxide synergistic conversion reaction system is used for strengthening sedimentation and hydrophilic modification of unavoidable ions of a solution, avoiding adsorption pollution of the unavoidable ions on the surface of a mineral, strengthening differential expression of the surface characteristics of the mineral and reducing influence of the unavoidable ions of backwater; on the other hand, in the stirring dilution mineralization flotation operation section, the oxidation state of the solution is stabilized by utilizing the action of slow-release oxygen, so that the influence of unavoidable ions in the synergistic adsorption of backwater organic pollutants and carbonate-hydroxide is reduced by oxidation, and backwater treatment and high-efficiency recycling are synchronously realized in the grinding flotation separation process. The method has simple process, embeds the backwater utilization and treatment into the mineral grinding and floating separation system, does not need to additionally add a backwater treatment system, and has low backwater utilization cost.
Detailed Description
It should be noted that, without conflict, the embodiments of the present application and features of the embodiments may be combined with each other. The present application will be described in detail with reference to examples.
As analyzed by the background technology of the application, the problem of low treatment efficiency of the backwater of the oxidized ore exists in the prior art, and in order to solve the technical problem, the application provides a backwater treatment method of the oxidized ore. The oxidized ore backwater treatment method comprises the following steps: step S1, adding a flocculating agent into backwater A generated in a flotation process, and settling suspended matters in backwater to obtain backwater B; s2, adding backwater B into ore grinding operation, and adding an regulator with an oxygen release function in the ore grinding operation process to obtain ore pulp C; s3, adding backwater B into the ore pulp C to dilute to the concentration required by the first flotation step, so as to obtain mineralized slurry D to be separated; and S4, carrying out flotation separation on the mineralized slurry D to obtain oxidized ore concentrate E and separated tailings F.
The application aims to couple backwater treatment with ore grinding flotation, namely, a modified regulator with oxygen release function is added in the ore grinding process, and O is formed by the property of slowly releasing oxygen and reducing Fe generated by corrosion of ore grinding medium 2 /H 2 O 2 oxidation-Fe reduction catalytic micro-electrolysis, degrading organic matters in backwater, and simultaneously cooperating with OH - The influence of unavoidable metal ions in the adsorption modified backwater can be achieved, and the following purposes are achieved: the degradation or decomposition degree of organic matters in backwater is improved by the strong oxidation micro-electrolysis effect of Fe catalysis, and the adverse effect of the organic matters is avoided; on one hand, a carbonate-hydroxide synergistic conversion reaction system is used for strengthening sedimentation and hydrophilic modification of unavoidable ions of a solution, avoiding adsorption pollution of the unavoidable ions on the surface of a mineral, strengthening differential expression of the surface characteristics of the mineral and reducing influence of the unavoidable ions of backwater; on the other hand, in the stirring dilution mineralization flotation operation section, the oxidation state of the solution is stabilized by utilizing the action of slow-release oxygen, so that the influence of unavoidable ions in the synergistic adsorption of backwater organic pollutants and carbonate-hydroxide is reduced by oxidation, and backwater treatment and high-efficiency recycling are synchronously realized in the grinding flotation separation process. The method has simple process, embeds the backwater utilization and treatment into the mineral grinding and floating separation system, does not need to additionally add a backwater treatment system, and has low backwater utilization cost.
The backwater treatment method is suitable for the beneficiation backwater utilization in a neutral or alkaline oxidized ore flotation system, and is suitable for treating oxidized ore collector floating systems such as fatty acid, amino acid, sulfonic acid, amine, hydroxamic acid and the like, and the backwater treatment method comprises flotation systems such as bastnaesite, bauxite, lithium ore (spodumene and lepidolite), kyanite, garnet, wollastonite, andalusite, neon stone, serpentine and the like.
In the step S1, in order to reduce the influence of the fine suspended matters in the backwater, a regulator with electrostatic sedimentation effect or accelerating sedimentation of particles, that is, the flocculant is added into the backwater a newly produced in the flotation process, so as to regulate the fine suspended matters in the sedimentation backwater, thereby obtaining the clarified backwater B for preliminary treatment.
The above-described flocculant may be selected in the art, and the present application is not particularly limited, and in some embodiments of the present application, the flocculant comprises: any one or more of polyaluminium chloride, polyaluminium sulfate, aluminum sulfate, ferric sulfate, ferrous sulfate, aluminum chloride, ferric chloride, ferrous chloride, aluminum potassium sulfate and polyacrylamide has a good sedimentation effect on fine suspended matters in backwater generated in a flotation process. Preferably, the flocculant is added in an amount of 0.02 to 1.0g/L.
In the step S2, in order to reduce the influence of the residual organic agent and inorganic unavoidable ions in the backwater on the mineral flotation process, the clarified backwater B obtained in the step S1 is introduced into the ore grinding operation of the oxide ore separation for use to obtain backwater ore pulp C after ore grinding, wherein the ore grinding medium of the ore grinding operation is iron materials such as cast iron balls, carbon steel, alloy steel and the like, and the reducing Fe with oxygen release function and the reducing Fe eroded by the ore grinding medium are added in the ore grinding process to form high-activity O 2 /H 2 O 2 -Fe 2+ /Fe 3+ And a micro-electrolysis loop for rapidly decomposing the residual organic medicament molecules. The regulator with the function of slowly releasing oxygen has the function of releasing O 2 、H 2 O 2 And the active components and the reducing surface of the ore grinding iron ball medium form an oxidation micro-battery, so that the high-activity micro-electrolysis is used for strengthening and degrading the residual organic solvent in the backwater, and the influence of the backwater residual organic medicament is reduced.
In some exemplary embodiments of the present application, the oxygen-releasing modifier is a carbonation modifying modifier, and the CO is utilized by carbonation of the added modifying modifier 3 2- /HCO 3 - The characteristic adsorption of metal ions in the system effectively reduces Ca 2+ /Mg 2+ /Fe 3+ /Cu 2+ /Pb 2+ And the surface is polluted by improper adsorption of ions on the surface of the oxidized ore mineral, so that the differential expression of the mineral surface characteristics of backwater ore grinding is enhanced. The effect of the carbonation modifying regulator is, on the one hand, that the CO produced is isolated with the modifying regulator 3 2- 、HCO 3 - Selectively reacts with active species of the system to compete for precipitation or adsorb easily soluble unavoidable ions (Ca 2+ \Mg 2+ \Fe 3+ Etc.) to avoid indiscriminate adsorption of unavoidable ions on the dissociated surface of the mineral and its adverse effects, on the other hand, O 2 /H 2 O 2 Strengthening OH in aqueous solution - To supplement modification of hydroxylation hydrophilic behavior of mineral interface, to accelerate low concentration Mg in backwater 2+ 、Ca 2+ The process of converting to the basic carbonate effectively reduces the adverse effect of unavoidable ions; in the process of the step S2, the organic reagent pollution in the backwater is degraded by catalytic oxidation, the influence of unavoidable ions in the backwater is reduced by sedimentation conversion, and meanwhile, the selective regulation and control of the mineral surface are enhanced by utilizing the high activity of the new dissociation surface of the mineral.
In some embodiments of the present application, the carbonate modification modifier with the oxygen release function is one or more of sodium percarbonate, sodium biperfarbonate and potassium percarbonate, and the additive amount of the modifier is 0.1-5.0 g/L relative to the clarified backwater B, i.e. 0.1-5.0 g of the carbonate modification modifier with the oxygen release function is added to each L backwater B. Has better effect.
In the step S2, the electrolysis reaction of the micro-electrolysis cell formed by oxidation-reduction of peroxide-iron released by the regulator with oxygen release function is taken as an example, the regulator is sodium percarbonate,
2Na 2 CO 3 ·3H 2 O 2 →4Na + +2CO 3 2- +3H 2 O 2 (6OH - )
by reducing Fe to Fe 2+ →Fe 3+ The conversion process of (2) is the strengthening catalysis of adding the slow release oxygen function, and the strong oxidation electrolysis reaction can be expressed as:
the step S2 is to strengthen the main chemical reaction of the system mineral surface and the backwater solution, which is unavoidably influenced by ions Ca/Mg/Fe, and can be expressed as follows:
Ca 2+ /Mg 2+ +CO 3 2- →CaCO 3 /MgCO 3
Fe 3+ /Ca 2+ /Mg 2+ +2OH - →Fe(OH) 3 /Ca(OH) 2 /Mg(OH) 2
2Mg 2+ +CO 3 2- +2OH - →MgCO 3 ·Mg(OH) 2
wherein Mg is 2+ The mineral surface or solution ions can be preferentially and selectively reacted and settled into basic magnesium carbonate with lower solubility product, so as to improve the Mg content 2+ The modification and adjustment efficiency of the components reduces the adsorption pollution of magnesium element, thereby strengthening the difference of the surface characteristics of minerals.
The above-described regulator having an oxygen releasing function may also be used in combination with inorganic carbonates, including, for example, any one or more of sodium carbonate, ammonium carbonate and potassium carbonate. The adding amount of the inorganic carbonate is 0.1-5.0 g/L relative to the clarified backwater B.
In the step S2, the concrete implementation method of the ore grinding operation may refer to the prior art, and in some embodiments of the present application, the mass concentration of the ore pulp in the ore grinding operation is 40% -70%.
The grinding fineness of the ore can be selected to be 40% -95% of-0.074 mm according to the sorting granularity requirement.
And S3, adding the clarified backwater B treated in the step S1 into the backwater ore grinding ore pulp C obtained in the step S2 to dilute the backwater ore grinding ore pulp C to the mass concentration required by the first step of flotation, and carrying out mineralization adjustment on the ore pulp to be separated to obtain mineralized slurry D, wherein the mass concentration of the ore pulp required by the first cloth flotation, namely the mass concentration of the mineralized slurry D to be separated is 10-45%.
In some exemplary embodiments of the present application, the step S3 further includes adding other agents to the pulp C required for activating the separation of the oxidized minerals such as the separation modifiers and/or the mineral collectors. The conditioning agent and/or mineral collector may be selected in the art according to the particular pulp type of flotation and the application is not particularly limited and will not be described in detail herein.
Wherein, after the treatment of the step S2 and the step S3, the influence of backwater is basically controlled effectively; and S3, controlling the influence of clarified backwater B, namely, utilizing the oxygen slow-release function regulator added in the step S2, enabling the solution to be in a high oxidation state through slowly released oxygen, strengthening the influence of oxidation regulation backwater B organic residues, and regulating the influence of unavoidable metal ions, wherein the regulation is mainly realized by the cooperation of carbonate anions and hydroxide ions.
And S4, carrying out flotation separation and recovery of the mineralized slurry D generated in the step S3 in a proper technological process to obtain oxidized ore concentrate E and separated tailings F. The specific process flow of flotation separation can refer to the prior art, and the application has no special requirement and is not repeated.
In some typical embodiments of the application, the ore concentrate E and the tailings F obtained in the step S4 are subjected to sedimentation filtration, and the produced ore concentrate backwater is returned to the step S1 as backwater A for recycling, so that the efficient recycling of the oxidized ore backwater is realized. In addition, when the flotation operation of fine scavenging flotation requires additional backwater, the clarified backwater B treated in the step 1) can be recycled.
The advantageous effects of the present application will be further described below with reference to examples and comparative examples.
Example 1
The backwater treated in this embodiment is the final backwater A produced by the bastnaesite flotation system, wherein the backwater is the beneficiated backwater of rare earth ore with ROE content of 4.57% in the raw bastnaesite, and the raw backwater contains Ca 2+ The concentration is 310mg/L, mg 2+ The concentration reaches 150mg/L, the TOC of the organic solvent is 200mg/L, and the organic is mainly hydroxamic acids with long hydrocarbon chains, and belongs to complex backwater which is difficult to degrade and adsorb and settle;
1) Regulating the returned water suspended matters, adding 0.6g/L polymeric ferric sulfate into the final returned water A produced by the bastnaesite flotation system, settling and standing to obtain clarified returned water B from which the returned water suspended matters are removed;
2) Adding the clarified backwater B obtained in the step 1) into rare earth ore grinding and dissociation operation according to the recycling proportion of 70%, grinding with the mass concentration of ore pulp being 50%, adding 0.8g/L potassium percarbonate, and separating out CO produced by percarbonate 3 2- -H 2 O 2 The micro-electrolysis effect with high oxidation activity is formed with Fe on the surface of the grinding medium, and the oxidation backwater degradation avoids the influence of backwater residual organic matters and simultaneously directionally modifies backwater metal ions and the mineral surface. Grinding and dissociating until the fineness of-0.074 mm accounts for 85%, and grinding and discharging to obtain ground slurry C;
3) And (3) mineralizing and adjusting backwater grinding slurry, namely adding the clarified backwater B treated in the step (1) into the grinding modified and regulated grinding slurry C obtained in the step (2), mixing slurry according to the flotation mass concentration of 26%, adding 20mg/L lead nitrate, activating and stirring for 3min, and stirring for 3min by taking 1200+300mg/L alkyl hydroxamic acid and octyl hydroxamic acid as collectors to obtain mineralized ore slurry D to be separated after mineralization.
4) And (3) carrying out floatation separation on mineralized ore pulp, namely carrying out floatation separation on mineralized slurry D generated in the step (3) by adopting a coarse-five-fine two-sweep process to recover rare earth elements, so as to obtain oxidized ore concentrate E and separated tailings F, wherein the REO content and REO recovery rate in the concentrate E are shown in the following table 1.
And (3) separating the obtained concentrate and the ore dressing backwater produced after tailing sedimentation and filtration, and returning the backwater to the step (1) for recycling so as to realize the efficient recycling of the backwater of oxidized ore.
Comparative example 1
The difference from example 1 is that in steps 2) and 3), no backwater is used, the clarified backwater B is replaced with industrial water, and no percarbonate or carbonate is added in the rare earth ore grinding and dissociation operation of step 2).
Example 2
The difference with the embodiment 1 is that 0.2+0.6g/L potassium percarbonate+potassium carbonate is added to replace 0.8g/L potassium percarbonate for catalytic oxidation in the grinding and dissociation operation of the rare earth ore in the step 2); other flotation reagents and classification were then added under the same conditions as in example 1.
Comparative example 1
The difference with the embodiment 1 is that in the step 2) rare earth ore grinding and dissociation operation, a regulator with oxygen release function is not added, and 0.8g/L of potassium carbonate is added for selective dispersion regulation; other flotation reagents and classification were then added under the same conditions as in example 1.
Comparative example 2
The difference with the embodiment 1 is that in the step 1), 0.6g/L of polymeric ferric sulfate is used for treating suspended matters, 1.5g/L of potassium ferrate is used for carrying out strong oxidation treatment on backwater to obtain backwater B, and in the step 2), a regulator with an oxygen release function is not added in the rare earth ore grinding dissociation operation, 0.8g/L of sodium carbonate is added to modify the mineral surface and avoid the influence of solution metal ions; other flotation reagents and classification were then added under the same conditions as in example 1.
The test results of the above examples, comparative examples and comparative examples are shown in Table 1.
TABLE 1
| REO content, percent | REO recovery% | |
| Comparative example 1 | 55.7 | 70.4 |
| Example 1 | 55.8 | 73.5 |
| Example 2 | 54.3 | 71.4 |
| Comparative example 1 | 43.3 | 68.2 |
| Comparative example 2 | 50.8 | 71.7 |
Example 3
The backwater treated in this example is the final backwater A produced by the lithium ore floatation system, which is Li 2 Spodumene ore flotation backwater with O content of 1.25 percent, wherein the backwater contains Ca 2+ The concentration is 20mg/L, mg 2+ The concentration reaches 40mg/L, and most of organic matters in backwater are fatty acid collecting agents with long hydrocarbon chains;
1) Regulating the returned water suspended matters, adding 0.2g/L aluminum potassium sulfate into the final returned water A produced by the lithium ore flotation system, settling and standing to obtain clarified returned water B from which the returned water suspended matters are removed;
2) Adding clarified backwater B obtained in the step 1) into lithium ore grinding and dissociation operation according to the recycling proportion of 80%, grinding with the ore pulp concentration of 66%, adding sodium percarbonate of 1.2g/L and separating out CO produced by percarbonate 3 2- -H 2 O 2 Forming a micro-electrolysis area with high oxidation activity with Fe on the surface of a grinding medium, degrading organic matters in backwater, simultaneously directionally modifying backwater metal ions and the surface of minerals, grinding and dissociating until the fineness of-0.074 mm accounts for 70%, and grinding and discharging to obtain ground slurry C;
3) Mineralizing and adjusting backwater grinding slurry, namely adding clarified backwater B treated in the step 1) into the grinding modified and regulated grinding slurry C obtained in the step 2), mixing slurry according to the flotation mass concentration of 33%, then adding 0.2g/L sodium hydroxide as an alkali corrosion change regulator, mechanically stirring for 10min, adding 20mg/L calcium chloride as a calcium ion activator, stirring and activating for 3min, adding 800mg/L oxidized paraffin soap 731 as a collector, and stirring for 3min to obtain mineralized ore slurry D to be separated after mineralization;
4) The mineralized ore pulp is subjected to floatation separation, and the mineralized slurry D generated in the step 3) is subjected to floatation separation by adopting a coarse, fine and sweeping process to recover lithium, so that oxidized ore concentrate E and separated tailings F are obtained, wherein Li in the concentrate E 2 The grade of O and the recovery rate are shown in Table 2; and (3) separating the obtained concentrate and the ore dressing backwater produced after tailing sedimentation and filtration, and returning the backwater to the step (1) for recycling so as to realize the efficient recycling of the backwater of oxidized ore.
Comparative example 2
The difference from example 3 is that in steps 2) and 3) no backwater is used, the clarified backwater B is replaced with industrial water, and no percarbonate or carbonate is added in the step 2) epidesmine ore grinding dissociation operation.
Example 4
The difference with the embodiment 3 is that in the step 2) of the lithium ore grinding and dissociation operation, 0.2+1.0g/L sodium percarbonate+sodium carbonate is added to replace 1.2g/L sodium percarbonate, and the grinding is degraded and oxidized to return water; other flotation reagents and sorting were then added under the same conditions as in example 3.
Example 5
The difference with the embodiment 3 is that 1.2+0.2g/L sodium percarbonate+sodium carbonate is added to replace 1.2g/L sodium percarbonate in the grinding and dissociating operation of the lithium ore in the step 2), and the grinding is degraded and oxidized to return water; other flotation reagents and sorting were then added under the same conditions as in example 3.
Comparative example 3
The difference with the embodiment 3 is that in the step 2) the lithium ore grinding and dissociating operation, a regulator with an oxygen release function is not added, and 1.2g/L sodium carbonate is added for grinding, degrading and oxidizing backwater; other flotation reagents and sorting were then added under the same conditions as in example 3.
Comparative example 4
The difference from example 3 is that in step 1), the suspension is treated with 0.2g/L of potassium aluminum sulfate and then with 0.8g/L of H 2 O 2 In the strong oxidation treatment backwater, backwater B is obtained by treatment, and in the step 2), a regulator with an oxygen release function is not added in the rare earth ore grinding and dissociation operation, 1.2g/L sodium carbonate is added to modify the surface of the mineral and avoid the influence of solution metal ions; other flotation reagents and sorting were then added under the same conditions as in example 3.
The test results of the above examples, comparative examples and comparative examples are shown in Table 2.
TABLE 2
Example 6
The backwater treated by the embodiment is a certain blueThe final backwater A produced by the spar ore flotation system, wherein the amount of the kyanite ore in the original kyanite ore is 35%, quartz is 50%, mica is 10%, and the other ore is a small amount of minerals such as tourmaline, ferric oxide, rutile, chlorite, garnet and the like, and the raw ore contains Al 2 O 3 The content is 25.5%, the TOC of an organic solvent in the original backwater is 120mg/L, and the organic matters are mainly complex organic impurity systems of fatty acids, hydroxamic acids, sunflower lipids and diesel oil with long hydrocarbon chains, and belong to the difficultly treated backwater for mineral separation;
1) Regulating the returned water suspended matters, adding 0.2g/L polyaluminium chloride into the final returned water A produced by the kyanite ore flotation system, settling and standing to obtain clarified returned water B from which the returned water suspended matters are removed;
2) Adding the clarified backwater B obtained in the step 1) into ore grinding and dissociation operation of kyanite minerals according to the recycling proportion of 75%, grinding the ores with the mass concentration of 60%, adding 1.2g/L sodium percarbonate, and separating out CO produced by percarbonate 3 2- -H 2 O 2 The micro-electrolysis effect with high oxidation activity is formed with Fe on the surface of the grinding medium, and the oxidation backwater degradation avoids the influence of backwater residual organic matters and simultaneously directionally modifies backwater metal ions and the mineral surface. Grinding and dissociating until the fineness of-0.074 mm accounts for 80%, and grinding and discharging to obtain ground slurry C;
3) Mineralizing and adjusting backwater grinding slurry, adding clarified backwater B treated in the step 1) into the grinding modified and regulated grinding slurry C obtained in the step 2), mixing slurry according to the mass concentration of flotation of 30%, and then adding 400+30mg/L of oxidized paraffin soap and diesel oil to carry out flotation to remove the phosphocalpain, thereby obtaining the phosphocalpain Dan Zazhi; mixing the flotation tail slurry with 100mg/L of acid water glass, and floating an ilmenite foam product with 300mg/L of benzyl hydroxamic acid to obtain an ilmenite product; and then adding 0.5g/L sodium percarbonate into the flotation tailings to adjust the pH value, adding 10mg/L copper sulfate, activating and stirring for 3min, and obtaining the kyanite mineralized ore pulp D to be separated after mineralization when the concentration of the hexyl ester and the diesel oil is 200mg/L and the concentration of the kyanite is 200 mg/L.
4) And (3) carrying out flotation separation on the mineralized ore pulp D, and obtaining kyanite concentrate E and separation tailings F (separation middlings and separation tailings) through a coarse and fine open-circuit flotation process.
Al in concentrate E 2 O 3 Content and recovery rate of (2) and impurity component Fe in concentrate E 2 O 3 、TiO 2 The content and recovery rate of (2) are shown in Table 3.
And (3) separating the obtained concentrate and the ore dressing backwater produced after tailing sedimentation and filtration, and returning the backwater to the step (1) for recycling so as to realize the efficient recycling of the backwater of oxidized ore.
Comparative example 3
The difference from example 6 is that in steps 2) and 3), no backwater is used, the clarified backwater B is replaced with industrial water, and no percarbonate or carbonate is added in the rare earth ore grinding and dissociation operation of step 2).
Example 7
The difference with the embodiment 6 is that 0.2+0.6g/L sodium percarbonate+sodium carbonate is added to replace 1.2g/L sodium percarbonate for catalytic oxidation in the ore grinding and dissociation operation of the blue crystal stone ore in the step 2); other flotation reagents and sorting were then added under the same conditions as in example 6.
Comparative example 5
The difference with the embodiment 6 is that in the step 2) sodium percarbonate ore grinding and dissociation operation, a regulator with oxygen release function is not added, and 0.8g/L sodium carbonate is added for selective dispersion regulation; other flotation reagents and sorting were then added under the same conditions as in example 6.
Comparative example 6
The difference with the embodiment 6 is that in the step 1), 0.8g/L of polyaluminium chloride is used for treating suspended matters, then 5.0g/L of hydrogen peroxide is used for carrying out strong oxidation treatment on backwater to obtain backwater B, in the step 2), a regulator with an oxygen release function is not added in the ore grinding dissociation operation of the kyanite, and 0.8g/L of sodium carbonate is added to modify the surface of minerals and avoid the influence of metal ions in solution; other flotation reagents and sorting were then added under the same conditions as in example 6.
The test comparative results of the above examples, comparative examples and comparative examples kyanite concentrates are shown in table 3.
TABLE 3 Table 3
From the above description, it can be seen that the above embodiments of the present application achieve the following technical effects:
1) The method of the application utilizes the addition of the regulator with the function of slowly releasing oxygen in the ore grinding process, and utilizes the regulator to isolate the released O 2 /H 2 O 2 Micro-electrolysis cell based on conversion of strong oxidation-Fe reduction, reducing influence of backwater residual organic matters and utilizing CO 3 2- \HCO 3 - The carbonate modification effect of different minerals in the ore grinding process is enhanced, the mineral surface modification efficiency, the solution ion influence avoiding efficiency, the particle dispersing efficiency and the like are improved, and the influence of backwater components on the mineral flotation process is reduced by the cooperation of strong catalytic oxidation and carbonate selective adsorption.
2) According to the method, the regulator with the slow-release oxygen function is added, so that on one hand, the grinding floating body is in a relatively high oxidation state, the high oxidation potential can effectively avoid the influence of organic matters in backwater in a mineralization slurry mixing stage of backwater dilution flotation operation concentration, on the other hand, the carbonate radical-hydroxyl radical reaction activity is synergistically enhanced, the unavoidable ion concentration and the pollution to the surface of minerals are effectively reduced, the difference of the characteristic expression of the dissociated surfaces of the minerals is enhanced, and the mineral separation efficiency is improved.
3) The method has simple process, embeds the backwater utilization and treatment into the mineral grinding and floating separation system, does not need to additionally add a backwater treatment system, and has low backwater utilization cost.
The above description is only of the preferred embodiments of the present application and is not intended to limit the present application, but various modifications and variations can be made to the present application by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present application should be included in the protection scope of the present application.
Claims (10)
1. A method for treating backwater of oxidized ore, which is characterized by comprising the following steps:
step S1, adding a flocculating agent into backwater A generated in a flotation process, and settling suspended matters in the backwater to obtain backwater B;
s2, adding the backwater B into ore grinding operation, and adding an adjusting agent with an oxygen release function in the ore grinding operation process to obtain ore pulp C;
s3, adding the backwater B into the ore pulp C to dilute to the concentration required by the first flotation step, so as to obtain mineralized slurry D to be separated;
and S4, carrying out flotation separation on the mineralized slurry D to obtain oxidized ore concentrate E and separated tailings F.
2. The oxidized ore backwater treatment method according to claim 1, wherein said flocculant comprises: any one or more of polyaluminium chloride, polyaluminium sulfate, aluminum sulfate, ferric sulfate, ferrous sulfate, aluminum chloride, ferric chloride, ferrous chloride, aluminum potassium sulfate and polyacrylamide.
3. The oxidized ore backwater treatment method according to claim 2, wherein the addition amount of the flocculant is 0.02 to 1.0g/L.
4. The method for treating backwater of oxidized ore according to claim 1, wherein the regulator having an oxygen release function is a carbonation modifying regulator, and preferably the carbonation modifying regulator is any one or more of sodium percarbonate, sodium biperfarbonate and potassium percarbonate.
5. The method for treating backwater of oxidized ore according to claim 4, wherein the amount of the regulator having an oxygen release function is 0.1 to 5.0g/L based on the clarified backwater B.
6. The oxidized ore backwater treatment method according to claim 1, wherein an inorganic carbonate is further added during the ore grinding operation, preferably, the inorganic carbonate is selected from any one or more of sodium carbonate, ammonium carbonate and potassium carbonate; preferably, the addition amount of the inorganic carbonate is 0.1-5.0 g/L relative to the clarified backwater B.
7. The oxidized ore backwater treatment method according to claim 1, wherein in the step S2, the mass concentration of the ore pulp during the ore grinding operation is 40% to 70%.
8. The oxidized ore backwater treatment method according to claim 1, wherein in the step S3, the mass concentration of the mineralized slurry D to be sorted is 10% -45%.
9. The method according to claim 1, wherein in the step S3, an activation and separation regulator and/or a mineral collector is further added to the pulp C.
10. The oxidized ore backwater treatment method according to claim 1, wherein the beneficiation backwater produced after the concentrate E and the tailings F are subjected to sedimentation filtration is returned to the step S1 as backwater a for recycling.
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