CN115382660B - Separation method of fluorite-containing lepidolite concentrate - Google Patents
Separation method of fluorite-containing lepidolite concentrate Download PDFInfo
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- CN115382660B CN115382660B CN202211054383.1A CN202211054383A CN115382660B CN 115382660 B CN115382660 B CN 115382660B CN 202211054383 A CN202211054383 A CN 202211054383A CN 115382660 B CN115382660 B CN 115382660B
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- fluorite
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- lepidolite
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- 239000012141 concentrate Substances 0.000 title claims abstract description 153
- WUKWITHWXAAZEY-UHFFFAOYSA-L calcium difluoride Chemical compound [F-].[F-].[Ca+2] WUKWITHWXAAZEY-UHFFFAOYSA-L 0.000 title claims abstract description 136
- 239000010436 fluorite Substances 0.000 title claims abstract description 136
- 229910052629 lepidolite Inorganic materials 0.000 title claims abstract description 125
- 238000000926 separation method Methods 0.000 title claims abstract description 40
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 69
- 238000000034 method Methods 0.000 claims abstract description 63
- 239000003112 inhibitor Substances 0.000 claims abstract description 58
- 230000008569 process Effects 0.000 claims abstract description 34
- 229940006295 sulfonated oleic acid Drugs 0.000 claims abstract description 29
- GVGUFUZHNYFZLC-UHFFFAOYSA-N dodecyl benzenesulfonate;sodium Chemical compound [Na].CCCCCCCCCCCCOS(=O)(=O)C1=CC=CC=C1 GVGUFUZHNYFZLC-UHFFFAOYSA-N 0.000 claims abstract description 28
- 229940080264 sodium dodecylbenzenesulfonate Drugs 0.000 claims abstract description 28
- 239000002283 diesel fuel Substances 0.000 claims abstract description 27
- 229920002472 Starch Polymers 0.000 claims abstract description 24
- 239000008107 starch Substances 0.000 claims abstract description 24
- 235000019698 starch Nutrition 0.000 claims abstract description 24
- 239000003518 caustics Substances 0.000 claims abstract description 23
- REYJJPSVUYRZGE-UHFFFAOYSA-N Octadecylamine Chemical group CCCCCCCCCCCCCCCCCCN REYJJPSVUYRZGE-UHFFFAOYSA-N 0.000 claims abstract description 18
- JRBPAEWTRLWTQC-UHFFFAOYSA-N dodecylamine Chemical group CCCCCCCCCCCCN JRBPAEWTRLWTQC-UHFFFAOYSA-N 0.000 claims abstract description 18
- 150000002888 oleic acid derivatives Chemical class 0.000 claims abstract 5
- 230000002000 scavenging effect Effects 0.000 claims description 44
- 239000003795 chemical substances by application Substances 0.000 claims description 10
- 239000002516 radical scavenger Substances 0.000 claims description 4
- 239000007790 solid phase Substances 0.000 claims description 4
- 239000002002 slurry Substances 0.000 claims description 3
- 238000011084 recovery Methods 0.000 abstract description 54
- 238000005188 flotation Methods 0.000 abstract description 37
- 239000003814 drug Substances 0.000 abstract description 6
- 230000002401 inhibitory effect Effects 0.000 abstract description 6
- 230000007547 defect Effects 0.000 abstract description 4
- 239000010445 mica Substances 0.000 abstract description 4
- 229910052618 mica group Inorganic materials 0.000 abstract description 4
- 229910004261 CaF 2 Inorganic materials 0.000 description 24
- 150000002889 oleic acids Chemical class 0.000 description 21
- 238000012360 testing method Methods 0.000 description 21
- 230000000052 comparative effect Effects 0.000 description 18
- 230000000694 effects Effects 0.000 description 10
- ZQPPMHVWECSIRJ-KTKRTIGZSA-N oleic acid Chemical compound CCCCCCCC\C=C/CCCCCCCC(O)=O ZQPPMHVWECSIRJ-KTKRTIGZSA-N 0.000 description 8
- NTHWMYGWWRZVTN-UHFFFAOYSA-N sodium silicate Chemical compound [Na+].[Na+].[O-][Si]([O-])=O NTHWMYGWWRZVTN-UHFFFAOYSA-N 0.000 description 8
- 239000006260 foam Substances 0.000 description 5
- 235000019353 potassium silicate Nutrition 0.000 description 5
- WRIDQFICGBMAFQ-UHFFFAOYSA-N (E)-8-Octadecenoic acid Natural products CCCCCCCCCC=CCCCCCCC(O)=O WRIDQFICGBMAFQ-UHFFFAOYSA-N 0.000 description 4
- LQJBNNIYVWPHFW-UHFFFAOYSA-N 20:1omega9c fatty acid Natural products CCCCCCCCCCC=CCCCCCCCC(O)=O LQJBNNIYVWPHFW-UHFFFAOYSA-N 0.000 description 4
- QSBYPNXLFMSGKH-UHFFFAOYSA-N 9-Heptadecensaeure Natural products CCCCCCCC=CCCCCCCCC(O)=O QSBYPNXLFMSGKH-UHFFFAOYSA-N 0.000 description 4
- ZQPPMHVWECSIRJ-UHFFFAOYSA-N Oleic acid Natural products CCCCCCCCC=CCCCCCCCC(O)=O ZQPPMHVWECSIRJ-UHFFFAOYSA-N 0.000 description 4
- 239000005642 Oleic acid Substances 0.000 description 4
- 239000002253 acid Substances 0.000 description 4
- 229910052500 inorganic mineral Inorganic materials 0.000 description 4
- QXJSBBXBKPUZAA-UHFFFAOYSA-N isooleic acid Natural products CCCCCCCC=CCCCCCCCCC(O)=O QXJSBBXBKPUZAA-UHFFFAOYSA-N 0.000 description 4
- 239000011707 mineral Substances 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 229910011763 Li2 O Inorganic materials 0.000 description 3
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 description 3
- 239000004115 Sodium Silicate Substances 0.000 description 3
- DBMJMQXJHONAFJ-UHFFFAOYSA-M Sodium laurylsulphate Chemical compound [Na+].CCCCCCCCCCCCOS([O-])(=O)=O DBMJMQXJHONAFJ-UHFFFAOYSA-M 0.000 description 3
- 239000003153 chemical reaction reagent Substances 0.000 description 3
- 229910052744 lithium Inorganic materials 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 229940083575 sodium dodecyl sulfate Drugs 0.000 description 3
- 235000019333 sodium laurylsulphate Nutrition 0.000 description 3
- 229910052911 sodium silicate Inorganic materials 0.000 description 3
- KRHYYFGTRYWZRS-UHFFFAOYSA-N Fluorane Chemical compound F KRHYYFGTRYWZRS-UHFFFAOYSA-N 0.000 description 2
- 229910018068 Li 2 O Inorganic materials 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 125000002091 cationic group Chemical group 0.000 description 2
- 230000005764 inhibitory process Effects 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000000178 monomer Substances 0.000 description 2
- QNILTEGFHQSKFF-UHFFFAOYSA-N n-propan-2-ylprop-2-enamide Chemical compound CC(C)NC(=O)C=C QNILTEGFHQSKFF-UHFFFAOYSA-N 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000010408 sweeping Methods 0.000 description 2
- OYHQOLUKZRVURQ-NTGFUMLPSA-N (9Z,12Z)-9,10,12,13-tetratritiooctadeca-9,12-dienoic acid Chemical compound C(CCCCCCC\C(=C(/C\C(=C(/CCCCC)\[3H])\[3H])\[3H])\[3H])(=O)O OYHQOLUKZRVURQ-NTGFUMLPSA-N 0.000 description 1
- GDFCSMCGLZFNFY-UHFFFAOYSA-N Dimethylaminopropyl Methacrylamide Chemical compound CN(C)CCCNC(=O)C(C)=C GDFCSMCGLZFNFY-UHFFFAOYSA-N 0.000 description 1
- 235000019483 Peanut oil Nutrition 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- -1 aerospace Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 150000001768 cations Chemical class 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000007123 defense Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000002608 ionic liquid Substances 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 235000019198 oils Nutrition 0.000 description 1
- 239000000312 peanut oil Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000010526 radical polymerization reaction Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- GCLGEJMYGQKIIW-UHFFFAOYSA-H sodium hexametaphosphate Chemical compound [Na]OP1(=O)OP(=O)(O[Na])OP(=O)(O[Na])OP(=O)(O[Na])OP(=O)(O[Na])OP(=O)(O[Na])O1 GCLGEJMYGQKIIW-UHFFFAOYSA-H 0.000 description 1
- 235000019982 sodium hexametaphosphate Nutrition 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 235000018553 tannin Nutrition 0.000 description 1
- 229920001864 tannin Polymers 0.000 description 1
- 239000001648 tannin Substances 0.000 description 1
- 239000001577 tetrasodium phosphonato phosphate 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
- 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
- B03D1/004—Organic compounds
- B03D1/012—Organic compounds containing sulfur
-
- 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
- B03D2201/00—Specified effects produced by the flotation agents
- B03D2201/02—Collectors
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D2201/00—Specified effects produced by the flotation agents
- B03D2201/06—Depressants
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- 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
- Chemical & Material Sciences (AREA)
- Inorganic Chemistry (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention relates to a separation method of fluorite-containing lepidolite concentrate, which comprises the following steps: adding an inhibitor and a collector A into fluorite lepidolite concentrate ore pulp to perform roughing operation to obtain fluorite rough concentrate and roughing tailings; adding an inhibitor into the fluorite rough concentrate to carry out concentration operation, so as to obtain a fluorite concentrate product; and (3) pulp mixing is carried out on the roughing tailings, then a collector B is added for recleaning, lepidolite rough concentrate and recleaning tailings are obtained, and the obtained lepidolite rough concentrate is subjected to blank concentration to obtain a lepidolite concentrate product. The inhibitor is caustic starch and sodium hydroxide; the collector A is sulfonated oleic acid, diesel oil and sodium dodecyl benzene sulfonate; the collector B is dodecylamine and octadecylamine. According to the invention, the method of carrying out mixed flotation on the fluorite lepidolite and then separating the fluorite lepidolite is adopted, so that the defects of long process flow, multiple medicament types, low recovery rate and the like caused by adopting a method for inhibiting the mica to float the fluorite in the prior art are overcome, and the efficient separation of fluorite lepidolite mixed concentrate resources is realized.
Description
Technical Field
The invention relates to the field of mineral processing, in particular to a separation method of fluorite-containing lepidolite concentrate.
Background
With the gradual exhaustion of high-grade fluorite ore resources, the utilization of concomitant (co) raw fluorite ore resources improves the schedule, and a flotation process is the most main beneficiation method of fluorite ore.
Lithium is widely applied to the fields of new energy, ceramics, aerospace, medicine, national defense and military industry and the like, and lepidolite is one of the most important resources for extracting lithium elements, so that the utilization rate of lepidolite resources is improved, and the high-quality development of the lithium industry is promoted.
Many existing methods for recovery of fluorite using flotation, such as CN104399592a, disclose a fluorite flotation process comprising the steps of: the method comprises the steps of taking fluorite ore low-grade products as raw materials, taking linoleic acid, peanut oil and sodium dodecyl sulfate as collecting agents, sequentially adding sulfuric acid, sodium silicate, hydrofluoric acid and the collecting agents in the carefully selecting process, and carrying out flotation three times to obtain the flotation fluorite. CN107790290a discloses a beneficiation method for recovering fluorite from scheelite rough concentrate, comprising the following steps: pre-concentrating the scheelite rough concentrate by using inhibitor water glass, adding a collector NAK for rough concentration, and adding inhibitor acidified water glass for ten times of concentration. CN103316773a discloses a fluorite ore floatation method, which comprises the steps of one roughing, one scavenging, nine concentrating and sequentially returning middlings; in the flotation process, saponified oleic acid is used as a collector; salinized water glass (15 parts of water glass, 10 parts of sodium hexametaphosphate, 2 parts of tannin extract and 245 parts of water) is used as an inhibitor. CN105289848a discloses a fluorite flotation method, which uses fluorite ore as raw material, modified oleic acid ionic liquid as collector, sodium silicate as inhibitor, sodium carbonate as pH value regulator, and adopts XFD series flotation machine with volume of 1.5L to make rougher flotation.
The mineral separation of lepidolite mainly adopts a floatation method, for example, CN111151381A discloses a cationic temperature-sensitive collector which is used for floatation of ores with the Li 2 O content of 1.2-1.8% and unobvious lepidolite characteristics, and mainly comes from floatation of hole-picked lepidolite ores. The cationic temperature-sensitive collector is prepared by copolymerizing two monomers, namely N-isopropyl acrylamide (NIPAM) and N- [ 3-dimethylaminopropyl ] methacrylamide (DMAPMA) by a free radical polymerization method, wherein the molar ratio of the two monomers is 1:5-8:1. The prepared cation temperature-sensitive collector has a good floatation effect on floatation of ores with the Li 2 O content of 1.2-1.8% and unobvious lepidolite characteristics, and is mainly derived from floatation of hole-picked lepidolite ores.
At present, the fluorite and lepidolite are generally recycled respectively in industry, and the method for inhibiting the lepidolite by adopting the floatation fluorite has the advantages of long process, various medicament types and low recycling rate.
Disclosure of Invention
In view of the problems existing in the prior art, the invention aims to provide a separation method of fluorite-containing lepidolite concentrate, aiming at the mixed concentrate obtained by fluorite lepidolite mixed flotation, the technical scheme of inhibiting lepidolite by using the floatation fluorite is adopted, so that the efficient separation of fluorite lepidolite mixed concentrate resources is realized, the flow is short, the recovery rate is high, and the resource utilization rate of fluorite concentrate and lepidolite concentrate is improved.
To achieve the purpose, the invention adopts the following technical scheme:
the invention provides a separation method of fluorite-containing lepidolite concentrate, which comprises the following steps:
Adding an inhibitor and a collector A into fluorite lepidolite concentrate ore pulp to perform roughing operation to obtain fluorite rough concentrate and roughing tailings;
Adding an inhibitor into the fluorite rough concentrate to carry out concentration operation, so as to obtain a fluorite concentrate product;
And (3) pulp mixing is carried out on the roughing tailings, then a collector B is added for recleaning, lepidolite rough concentrate and recleaning tailings are obtained, and the obtained lepidolite rough concentrate is subjected to blank concentration to obtain a lepidolite concentrate product.
The inhibitor consists of caustic starch and sodium hydroxide; the collector A consists of sulfonated oleic acid, diesel oil and sodium dodecyl benzene sulfonate; the collector B consists of dodecyl amine and octadecylamine.
According to the invention, a flotation mode is improved, fluorite and lepidolite mixed flotation is selected, and the obtained mixed concentrate is separated, so that the defects of long process flow, multiple medicament types, low recovery rate and the like of a method for respectively recovering fluorite and lepidolite and adopting a method for inhibiting mica by floatation of fluorite and adopting the method for inhibiting mica in the prior art are overcome, and the high-efficiency separation of fluorite and lepidolite mixed concentrate resources is realized.
According to the invention, the reagent system of fluorite flotation is improved, and fluorite concentrate is separated from mixed concentrate of fluorite lepidolite by utilizing the combination collector of sulfonated oleic acid, diesel oil and sodium dodecyl benzene sulfonate to be matched with a compound inhibitor. Wherein, the cooperation of sulfonated oleic acid, diesel oil and sodium dodecyl benzene sulfonate can promote the collapse of excessive foam to form a secondary enrichment effect, improve the grade of rough concentrate and adjust the thickness of a foam layer, and the foam has a stable state, is favorable for the stability of flotation operation and can be more stably adsorbed on the surface of fluorite. The combined collector has the characteristics of good selectivity, strong collecting capacity, good foam state and the like, and the better flotation effect can be achieved by using a small amount in the roughing process.
According to the invention, the inhibitor formed by combining caustic starch and sodium hydroxide is added in the fluorite fine-selection operation process, and the chemical bonding effect is carried out on Al 3+ and Li + on the surface of the lepidolite, so that the starch is adsorbed on the surface of the lepidolite, thereby hydrophilizing the surface of minerals, realizing the inhibition effect, improving the floatation separation effect of fluorite, lepidolite and gangue, and obtaining fluorite concentrate with higher grade and recovery rate.
In the invention, the grade of fluorite in the fluorite lepidolite concentrate is obviously higher than that of lepidolite, wherein the grade of the fluorite is more than or equal to 50:1, and the fluorite lepidolite concentrate can be concentrate obtained by flotation of corresponding raw ore or concentrate obtained by flotation of corresponding tailings.
In the invention, the pH value of the fluorite-containing lepidolite ore concentrate pulp can be 7-9.
In a preferred embodiment of the present invention, the mass concentration of the solid phase in the fluorite-containing lepidolite ore concentrate slurry is 20-40%, for example, 20%, 22%, 24%, 26%, 28%, 30%, 32%, 34%, 36%, 38% or 40%, etc., but the present invention is not limited to the recited values, and other values not recited in the range are equally applicable.
As a preferred embodiment of the present invention, the weight ratio of caustic starch to sodium hydroxide in the inhibitor is (4-5): 1, for example, it may be 4:1, 4.1:1, 4.2:1, 4.3:1, 4.4:1, 4.5:1, 4.6:1, 4.7:1, 4.8:1, 4.9:1 or 5:1, etc., but not limited to the recited values, and other non-recited values within this range are equally applicable.
Preferably, the mass ratio of sulfonated oleic acid, diesel oil and sodium dodecyl benzene sulfonate in collector A is (4-5): 1:1, for example, it may be 4:1:1, 4.1:1:1, 4.2:1:1, 4.3:1:1, 4.4:1:1, 4.5:1:1, 4.6:1:1, 4.7:1:1, 4.8:1:1, 4.9:1:1 or 5:1:1, etc., but not limited to the recited values, and other non-recited values within this range are equally applicable.
Preferably, the mass ratio of dodecylamine to octadecylamine in collector B is (1-1.5): 1, and may be, for example, 1:1, 1.1:1, 1.2:1, 1.3:1, 1.4:1, or 1.5:1, etc., but is not limited to the recited values, and other non-recited values within this range are equally applicable.
As a preferable embodiment of the present invention, the inhibitor may be added in an amount of 10 to 100g/t, for example, 10g/t, 20g/t, 30g/t, 40g/t, 50g/t, 60g/t, 70g/t, 80g/t, 90g/t, 100g/t, etc., but not limited to the values recited, and other values not recited in the range are equally applicable.
The addition amount of the collector A in the roughing operation is preferably 10 to 50g/t, and may be, for example, 10g/t, 20g/t, 30g/t, 40g/t, 50g/t, or the like, but is not limited to the recited values, and other values not recited in the range are equally applicable.
In a preferred embodiment of the present invention, the roughing operation is performed at least 1 time, for example, 1 time, 2 times, or 3 times, but the roughing operation is not limited to the values listed, and other values not listed in the above range are equally applicable and specifically selected according to the actual situation.
Preferably, the roughing tailings are subjected to at least 1 scavenging operation, for example, 1,2 or 3 scavenging operations, but the roughing tailings are not limited to the listed values, and other non-listed values in the range are applicable as well, and the roughing tailings are specifically selected according to practical situations.
Preferably, the collecting agent A added in the scavenging operation is 5-10g/t, for example, 5g/t, 6g/t, 7g/t, 8g/t, 9g/t or 10g/t, etc., but is not limited to the recited values, and other non-recited values in the range are equally applicable.
Preferably, middlings obtained in the scavenging operation sequentially return to the previous operation.
In a preferred embodiment of the present invention, the selection operation is performed at least 3 times, for example, 3 times, 4 times, or 5 times, but the present invention is not limited to the above-mentioned values, and other values not shown in the above-mentioned range are equally applicable, and the selection operation is specifically selected according to the actual situation.
Preferably, the inhibitor is added in an amount of 10-60g/t, for example, 10g/t, 20g/t, 30g/t, 40g/t, 50g/t, 60g/t, etc., but not limited to the recited values, and other non-recited values within this range are equally applicable.
Preferably, the middlings from the beneficiation operation are sequentially returned to the previous operation.
In a preferred embodiment of the present invention, the slurry is prepared by adjusting the pH of the roughing tailings to 2 to 5, for example, 2, 2.5, 3, 3.5, 4, 4.5 or 5, but not limited to the values listed, and other values not listed in the range are equally applicable.
Preferably, the addition amount of the reselection collector B is 5-10g/t, for example, 5g/t, 6g/t, 7g/t, 8g/t, 9g/t or 10g/t, etc., but not limited to the recited values, and other non-recited values within the range are equally applicable.
In the invention, the reselection can be performed for a plurality of times, such as 1 time, 2 times, 3 times, and the like, and the reselection is specifically selected according to actual conditions.
As a preferred technical scheme of the invention, the scavenger tailings are subjected to scavenging for at least 1 time, for example, 1 time, 2 times or 3 times, etc., but the scavenger tailings are not limited to the listed values, and other non-listed values in the range are applicable as well, and the scavenger tailings are specifically selected according to practical situations.
Preferably, the collector B is added with 1-5g/t in the sweeping, for example, 1g/t, 2g/t, 3g/t, 4g/t or 5g/t, etc., but the collector B is not limited to the listed values, and other non-listed values in the range are equally applicable.
Preferably, the middlings obtained in the sweeping are sequentially returned to the previous operation.
In a preferred embodiment of the present invention, the blank selection is performed at least 3 times, for example, 3 times, 4 times, or 5 times, but the blank selection is not limited to the values listed, and other values not listed in the range are equally applicable, and specific selection is performed according to actual conditions.
Preferably, the middlings obtained by blank concentration are sequentially returned to the previous operation.
As a preferred technical scheme of the present invention, the separation method comprises: adding an inhibitor and a collector A into fluorite lepidolite concentrate ore pulp to perform roughing operation to obtain fluorite rough concentrate and roughing tailings; the addition amount of the inhibitor in the roughing operation is 10-100g/t, the addition amount of the collector A in the roughing operation is 10-50g/t, the roughing operation is performed at least 1 time, and the roughing tailings are subjected to at least 1 scavenging operation; the collecting agent A with the concentration of 5-10g/t is added in the scavenging operation, and middlings obtained in the scavenging operation sequentially return to the previous operation;
Adding an inhibitor into the fluorite rough concentrate to carry out concentration operation, so as to obtain a fluorite concentrate product; the carefully chosen operation is carried out for at least 3 times, the addition amount of the inhibitor used in the carefully chosen operation is 10-60g/t, and middlings obtained in the carefully chosen operation sequentially return to the previous operation;
Pulp mixing is carried out on rough tailings, then a collector B is added for recleaning, lepidolite rough concentrate and recleaning tailings are obtained, and the obtained lepidolite rough concentrate is subjected to blank recleaning to obtain a lepidolite concentrate product; the size mixing is to adjust the pH value of the rougher tailings to 2-5; the addition amount of the re-selected collector B is 5-10g/t; at least 1 scavenging is carried out on the recleaning tailings, 1-5g/t of collecting agent B is added in the scavenging, and the middlings obtained in the scavenging sequentially return to the previous operation; the blank concentration is carried out for at least 3 times, and middlings obtained by the blank concentration sequentially return to the previous operation;
the mass concentration of the solid phase in the fluorite-containing lepidolite ore concentrate pulp is 20-40%;
The inhibitor consists of caustic starch and sodium hydroxide, wherein the weight ratio of the caustic starch to the sodium hydroxide in the inhibitor is (4-5) 1;
The collector A consists of sulfonated oleic acid, diesel oil and sodium dodecyl benzene sulfonate, wherein the mass ratio of the sulfonated oleic acid to the diesel oil to the sodium dodecyl benzene sulfonate in the collector A is (4-5) 1:1;
the collector B consists of dodecyl amine and octadecylamine, and the mass ratio of the dodecyl amine to the octadecylamine in the collector B is (1-1.5): 1.
In the invention, the addition amount g/t of the reagent refers to adding a certain amount of reagent based on the mass t of solids in the fluorite-containing lepidolite concentrate for flotation.
Compared with the prior art, the invention has the following beneficial effects:
(1) The method aims at separating the mixed concentrate recovered by the simultaneous floatation of fluorite and lepidolite, has short flow and high recovery rate, overcomes the defects of long flow, multiple medicament types, low recovery rate and the like when the fluorite and lepidolite are usually recovered respectively in the industry at present, and can improve the resource utilization rate of the fluorite lepidolite.
(2) The invention adopts the sulfonated oleic acid, diesel oil and sodium dodecyl benzene sulfonate as the combined collector, and the three components generate a coordination effect, so that the sulfonated oleic acid, diesel oil and sodium dodecyl benzene sulfonate can be more stably adsorbed on the surface of fluorite. The combined collector has the characteristics of good selectivity, strong collecting capacity, good foam state and the like, and the better flotation effect can be achieved by using a small amount in the roughing process.
(3) According to the invention, the inhibitor formed by combining caustic starch and sodium hydroxide is added in the fluorite concentration operation process, so that the caustic starch and the sodium hydroxide are matched, the inhibition effect on lepidolite and gangue minerals is enhanced, the floatation separation effect of fluorite, lepidolite and gangue is improved, fluorite concentrate with higher grade and recovery rate can be obtained, the grade of the fluorite concentrate is more than or equal to 95.01%, and the recovery rate is more than or equal to 70.09%.
(4) According to the invention, after fluorite flotation, the lepidolite is recovered by adopting acid activation and a combined collector of dodecylamine and octadecylamine, so that the recovery of lepidolite in fluorite lepidolite bulk concentrate is realized to the greatest extent, the grade of lepidolite is more than or equal to 1.33%, and the recovery rate is more than or equal to 50.67%.
Drawings
Fig. 1 is a schematic diagram of the flotation circuit in example 1 of the present invention.
The present invention will be described in further detail below. The following examples are merely illustrative of the present invention and are not intended to represent or limit the scope of the invention as defined in the claims.
Detailed Description
For a better illustration of the present invention, which is convenient for understanding the technical solution of the present invention, exemplary but non-limiting examples of the present invention are as follows:
Example 1
Some fluorite lepidolite mixed concentrate contains 1.02% of CaF 2 95.20％、Li2 O. The fluorite flotation operation of the flotation process provided by the embodiment adopts a coarse and one-sweep three-fine process, as shown in fig. 1, wherein middlings of the first concentration and the first scavenging return to the coarse concentration, and middlings obtained from the second and third concentration return to the previous concentration operation in sequence; the lepidolite flotation operation adopts a coarse-fine process, wherein middlings obtained by the first concentration and the first scavenging return to coarse concentration, and middlings obtained by the second concentration and the third concentration return to the previous concentration operation in sequence.
The flotation is carried out according to the following steps:
(1) Adding water into fluorite lepidolite mixed concentrate to adjust the mixture into ore pulp (pH value is 8) with the mass concentration of 31%, adding an inhibitor into the ore pulp, then adding a collector A for one-time roughing operation, and obtaining fluorite rough concentrate and rough tailings after roughing is finished; the inhibitor is a combination of caustic starch and sodium hydroxide, the mass ratio of the caustic starch to the sodium hydroxide is 4:1, and the adding amount of the inhibitor is 80g/t according to the mass of the fluorite lepidolite mixed concentrate; the collector A is a combination of sulfonated oleic acid, diesel oil and sodium dodecyl benzene sulfonate, the mass ratio of the sulfonated oleic acid to the diesel oil to the sodium dodecyl benzene sulfonate is 4:1:1, and the adding amount of the collector A is 22g/t;
(2) Performing primary scavenging operation on the roughing tailings obtained in the step (1); the total adding amount of the collector A in the scavenging process is 7g/t according to the mass of the fluorite lepidolite mixed concentrate, and the middlings obtained by scavenging are sequentially returned to the previous operation;
(3) Adding an inhibitor into the fluorite rough concentrate obtained in the step (1) to perform three concentration operations, and obtaining a fluorite concentrate product after the concentration is completed; wherein, the adding amount of the inhibitor is 40g/t according to the mass of the fluorite lepidolite mixed concentrate, the mass ratio of caustic starch to sodium hydroxide is 4:1, and the middlings obtained by carefully selecting are sequentially returned to the previous operation.
(4) Adding acid into tailings subjected to scavenging in the step (2) to adjust the pH value of the ore pulp to be 4, then adding a collector B for recleaning, wherein the collector B is a combination of dodecyl amine and octadecylamine, the mass ratio of the dodecyl amine to the octadecylamine is 1:1, and lepidolite rough concentrate and recleaning tailings are obtained after recleaning is finished; the total adding amount of the collector B in the reselection process is 10g/t according to the mass of the fluorite lepidolite mixed concentrate;
(5) And (3) carrying out one-time scavenging operation on the re-tailings obtained after the re-scavenging in the step (4), wherein the total adding amount of the collecting agent B in the scavenging process is 3g/t according to the mass of the fluorite lepidolite mixed concentrate, and sequentially returning the middlings obtained by scavenging to the previous operation.
(6) And (3) performing three blank concentration operations on the lepidolite rough concentrate obtained in the step (4), obtaining lepidolite concentrate products after the concentration is completed, and sequentially returning the middlings obtained by the concentration to the previous operation.
The final obtained closed-circuit test indexes are as follows: the fluorite concentrate contains CaF 2 97.41 percent, and the recovery rate is 82.06 percent; the lepidolite concentrate contains Li 2 O2.88 percent, and the recovery rate is 50.67 percent.
Example 2
Some fluorite lepidolite bulk concentrate contains 0.70% CaF 2 83.36％、Li2 O. The fluorite flotation operation of the flotation process provided by the embodiment adopts a coarse-fine process, wherein middlings obtained by first fine selection and fine-fine separation return to coarse separation, and middlings obtained by second fine selection and third fine selection return to the previous fine selection operation in sequence; the lepidolite flotation operation adopts a coarse-fine process, wherein middlings obtained by the first concentration and the first scavenging return to coarse concentration, and middlings obtained by the second concentration and the third concentration return to the previous concentration operation in sequence.
The flotation is carried out according to the following steps:
(1) Adding water into the fluorite lepidolite mixed concentrate to adjust the fluorite lepidolite mixed concentrate into ore pulp (pH value is 9) with the mass concentration of 28%, adding an inhibitor into the ore pulp, then adding a collector A for one-time roughing operation, and obtaining fluorite rough concentrate and roughing tailings after roughing is finished; the inhibitor is a combination of caustic starch and sodium hydroxide, the mass ratio of the caustic starch to the sodium hydroxide is 4:1, and the adding amount of the inhibitor is 60g/t according to the mass of the fluorite lepidolite mixed concentrate; the collector A is a combination of sulfonated oleic acid, diesel oil and sodium dodecyl benzene sulfonate, the mass ratio of the sulfonated oleic acid to the diesel oil to the sodium dodecyl benzene sulfonate is 4:1:1, and the adding amount of the collector A is 18g/t;
(2) Performing primary scavenging operation on the roughing tailings obtained in the step (1); the total adding amount of the collector A in the scavenging process is 5g/t according to the mass of the fluorite lepidolite mixed concentrate, and the middlings obtained by scavenging are sequentially returned to the previous operation;
(3) Adding an inhibitor into the fluorite rough concentrate obtained in the step (1) for at least three times of concentration operation, and obtaining a fluorite concentrate product after the concentration is completed; wherein, according to the mass of the fluorite lepidolite mixed concentrate, the adding amount of the inhibitor is 35g/t, the mass ratio of caustic starch to sodium hydroxide is 4:1, and the middlings obtained by carefully selecting are sequentially returned to the previous operation.
(4) Adding acid into the cleaned tailings obtained in the step (2) to adjust the pH value of the ore pulp to be 2, then adding a collector B for recleaning, wherein the collector B is a combination of dodecyl amine and octadecylamine, the mass ratio of the dodecyl amine to the octadecylamine is 1:1, the rough lepidolite concentrate and the recleaning tailings are obtained after recleaning, and the total adding amount of the collector B in the recleaning process is 7g/t according to the mass of the fluorite lepidolite bulk concentrate;
(5) And (3) carrying out one-time scavenging operation on the re-tailings obtained after the re-scavenging in the step (4), wherein the total adding amount of the collecting agent B in the scavenging process is 2g/t according to the mass of the fluorite lepidolite mixed concentrate, and sequentially returning the middlings obtained by scavenging to the previous operation.
(6) Performing three blank concentration operations on the lepidolite rough concentrate obtained in the step (4), and obtaining a lepidolite concentrate product after concentration is completed; and sequentially returning the middlings obtained by carefully selecting to the previous operation.
The final obtained closed-circuit test indexes are as follows: the fluorite concentrate contains CaF 2 95.01 percent and the recovery rate is 70.09 percent; the lepidolite concentrate contains Li 2 O1.33% and the recovery rate is 51.19%.
Example 3
Some fluorite lepidolite bulk concentrate contains 0.74% CaF 2 85.80％、Li2 O. The fluorite flotation operation of the flotation process provided by the embodiment adopts a coarse-fine process, wherein middlings obtained by first fine selection and fine-fine separation return to coarse separation, and middlings obtained by second fine selection and third fine selection return to the previous fine selection operation in sequence; the lepidolite flotation operation adopts a coarse-fine process, wherein middlings obtained by the first concentration and the first scavenging return to coarse concentration, and middlings obtained by the second concentration and the third concentration return to the previous concentration operation in sequence.
The flotation is carried out according to the following steps:
(1) Adding water into fluorite lepidolite mixed concentrate to adjust the mixture into ore pulp (pH value is 7) with the mass concentration of 30%, adding an inhibitor into the ore pulp, then adding a collector A for one-time roughing operation, and obtaining fluorite rough concentrate and rough tailings after roughing is finished; the inhibitor is a combination of caustic starch and sodium hydroxide, the mass ratio of the caustic starch to the sodium hydroxide is 4:1, and the adding amount of the inhibitor is 50g/t according to the mass of the fluorite lepidolite mixed concentrate; the collector A is a combination of sulfonated oleic acid, diesel oil and sodium dodecyl benzene sulfonate, the mass ratio of the sulfonated oleic acid to the diesel oil to the sodium dodecyl benzene sulfonate is 4:1:1, and the adding amount of the collector A is 20g/t;
(2) Performing secondary scavenging operation on the roughing tailings obtained in the step (1); the total adding amount of the collector A in the scavenging process is 6g/t according to the mass of the fluorite lepidolite mixed concentrate, and the middlings obtained by scavenging are sequentially returned to the previous operation;
(3) Adding an inhibitor into the fluorite rough concentrate obtained in the step (1) to perform three concentration operations, and obtaining a fluorite concentrate product after the concentration is completed; wherein, according to the mass of the fluorite lepidolite mixed concentrate, the adding amount of the inhibitor is 30g/t, the mass ratio of caustic starch to sodium hydroxide is 4:1, and the middlings obtained by carefully selecting are sequentially returned to the previous operation.
(4) The pH value of ore pulp is adjusted to be 5 by adding acid into tailings after scavenging in the step (2), then a collector B is added for recleaning, the collector B is a combination of dodecyl amine and octadecylamine, the mass ratio of the dodecyl amine to the octadecylamine is 1:1, lepidolite rough concentrate and recleaning tailings are obtained after recleaning, and the total adding amount of the collector B in the rough dressing process is 8g/t according to the mass of the lepidolite bulk concentrate;
(5) And (3) carrying out one-time scavenging operation on the re-tailings obtained after the re-scavenging in the step (4), wherein the total adding amount of the collecting agent B in the scavenging process is 2g/t according to the mass of the fluorite lepidolite mixed concentrate, and sequentially returning the middlings obtained by scavenging to the previous operation.
(6) Performing three blank concentration operations on the lepidolite rough concentrate obtained in the step (4), and obtaining a lepidolite concentrate product after concentration is completed; and sequentially returning the middlings obtained by carefully selecting to the previous operation.
The final obtained closed-circuit test indexes are as follows: the fluorite concentrate contains CaF 2 95.14.14 percent and the recovery rate is 72.63 percent; the lepidolite concentrate contains Li 2 O1.37% and the recovery rate is 55.25%.
Comparative example 1
In comparison to example 1, the procedure and conditions were exactly the same as in example 1, except that collector a was replaced with oleic acid. That is, only oleic acid was used as collector a, and the total addition amount of collector a was unchanged.
The final obtained closed-circuit test indexes are as follows: the fluorite concentrate contains CaF 2 96.01 percent, and the recovery rate is 82.93 percent; the lepidolite concentrate contains Li 2 O2.58% and the recovery rate is 43.11%.
Comparative example 2
In comparison to example 1, the procedure and conditions were exactly the same as in example 1, except that collector A was replaced with sulfonated oleic acid. That is, only sulfonated oleic acid was used as collector A, and the total addition amount of collector A was unchanged.
The final obtained closed-circuit test indexes are as follows: the fluorite concentrate contains CaF 2, 96.42% and the recovery rate is 82.25%; the lepidolite concentrate contains Li 2 O2.55% and the recovery rate is 45.61%.
Comparative example 3
In comparison with example 1, the procedure and conditions were exactly the same as in example 1, except that collector a was replaced with sodium dodecylbenzenesulfonate. Namely, only sodium dodecyl benzene sulfonate is used as the collector A, and the total addition amount of the collector A is unchanged.
The final obtained closed-circuit test indexes are as follows: the fluorite concentrate contains CaF 2 96.01 percent and the recovery rate is 81.91 percent; the lepidolite concentrate contains Li 2 O2.56% and the recovery rate is 44.83%.
Comparative example 4
In comparison with example 1, the procedure and conditions were exactly the same as in example 1, except that collector A was replaced with sulfonated oleic acid and sodium dodecylbenzenesulfonate (4:1 mass ratio). Only sulfonated oleic acid and sodium dodecyl benzene sulfonate are selected as the collector A, and the total addition amount of the collector A is unchanged.
The final obtained closed-circuit test indexes are as follows: the fluorite concentrate contains CaF 2, 96.37% and the recovery rate is 82.62%; the lepidolite concentrate contains Li 2 O2.57 percent and the recovery rate is 41.93 percent.
Comparative example 5
In comparison to example 1, the procedure and conditions were exactly the same as in example 1, except that collector A was replaced with sulfonated oleic acid and diesel oil (mass ratio 4:1). Only sulfonated oleic acid and diesel oil are selected as the collector A, and the total addition amount of the collector A is unchanged.
The final obtained closed-circuit test indexes are as follows: the fluorite concentrate contains CaF 2 97.17 percent, and the recovery rate is 79.93 percent; the lepidolite concentrate contains Li 2 O2.55% and the recovery rate is 49.42%.
Comparative example 6
In comparison with example 1, the procedure and conditions were exactly the same as in example 1, except that collector A was replaced with sodium dodecylbenzenesulfonate and diesel oil (mass ratio 1:1). Namely, only sodium dodecyl sulfate and diesel oil are selected as the collector A, and the total addition amount of the collector A is unchanged.
The final obtained closed-circuit test indexes are as follows: the fluorite concentrate contains CaF 2 96.85.85%, and the recovery rate is 75.85%; the lepidolite concentrate contains Li 2 O2.15 percent and the recovery rate is 47.54 percent.
Comparative example 7
In comparison to example 1, the procedure and conditions were exactly the same as in example 1, except that the inhibitor was replaced with caustic starch. Namely, only caustic starch is selected as the inhibitor, and the total addition amount of the inhibitor is unchanged.
The final obtained closed-circuit test indexes are as follows: the fluorite concentrate contains CaF 2, 96.92% and the recovery rate is 84.70%; the lepidolite concentrate contains Li 2 O2.82% and the recovery rate is 41.63%.
Comparative example 8
In comparison to example 1, the procedure and conditions were exactly the same as in example 1, except that the inhibitor was replaced with sodium hydroxide. Namely, only sodium hydroxide is selected as the inhibitor, and the total addition amount of the inhibitor is unchanged.
The final obtained closed-circuit test indexes are as follows: the fluorite concentrate contains CaF 2 96.06.06 percent and the recovery rate is 86.97 percent; the lepidolite concentrate contains Li 2 O1.38% and the recovery rate is 16.27%.
Comparative example 9
In comparison with example 1, the procedure and conditions were exactly the same as in example 1, except that the inhibitor was replaced with conventional water glass. Namely, only conventional sodium silicate is selected as the inhibitor, and the total addition amount of the inhibitor is unchanged.
The final obtained closed-circuit test indexes are as follows: the fluorite concentrate contains CaF 2 96.33 percent, and the recovery rate is 86.16 percent; the lepidolite concentrate contains Li 2 O1.25% and the recovery rate is 16.04%.
Comparative example 10
In comparison with example 1, the procedure and conditions were exactly the same as in example 1, except that the collector B was replaced with octadecylamine. Namely, only octadecylamine is selected as the collector B, and the total addition amount of the collector B is unchanged in the selection process.
The final obtained closed-circuit test indexes are as follows: the fluorite concentrate contains CaF 2 97.43 percent, and the recovery rate is 81.98 percent; the lepidolite concentrate contains Li 2 O2.76% and the recovery rate is 48.02%.
Comparative example 11
In comparison with example 1, the procedure and conditions were exactly the same as in example 1, except that collector B was replaced with dodecylamine. Namely, only laurylamine is selected as the collector B, and the total addition amount of the collector B is unchanged in the selection process.
The final obtained closed-circuit test indexes are as follows: the fluorite concentrate contains CaF 2 97.56 percent, and the recovery rate is 81.10 percent; the lepidolite concentrate contains Li 2 O2.73% and the recovery rate is 48.30%.
Comparative example 12
The only thing compared to example 1 is to replace the diesel oil in collector a with an equal amount of kerosene.
The final obtained closed-circuit test indexes are as follows: the fluorite concentrate contains CaF 2 97.33 percent, and the recovery rate is 79.81 percent; the lepidolite concentrate contains Li 2 O2.65% and the recovery rate is 48.19%.
Comparative example 13
The only difference compared to example 1 is that the diesel in collector a is replaced with an equal amount of No. two oil.
The final obtained closed-circuit test indexes are as follows: the fluorite concentrate contains CaF 2 96.27.27%, and the recovery rate is 81.27%; the lepidolite concentrate contains Li 2 O2.63% and the recovery rate is 45.61%.
Comparative example 14
The only thing compared to example 1 is to replace the sulfonated oleic acid in collector a with an equivalent amount of oleic acid.
The final obtained closed-circuit test indexes are as follows: the fluorite concentrate contains CaF 2 and is 96.61 percent, and the recovery rate is 80.35 percent; the lepidolite concentrate contains Li 2 O2.61% and the recovery rate is 47.93%.
Comparative example 15
The only thing compared to example 1 is that the sodium dodecylbenzene sulfonate in collector a is replaced by an equivalent amount of sodium dodecylsulfate.
The final obtained closed-circuit test indexes are as follows: the fluorite concentrate contains CaF 2 96.71.71%, and the recovery rate is 80.65%; the lepidolite concentrate contains Li 2 O2.63% and the recovery rate is 47.06%.
Comparative example 16
The only difference compared with example 1 is that the mass ratio of sulfonated oleic acid, diesel oil and sodium dodecyl benzene sulfonate in collector A is 2:1:1.
The final obtained closed-circuit test indexes are as follows: the fluorite concentrate contains CaF 2 96.14.14%, and the recovery rate is 79.70%; the lepidolite concentrate contains Li 2 O2.60 percent and the recovery rate is 47.95 percent.
Comparative example 17
The only difference compared to example 1 is that the mass ratio of sulfonated oleic acid, diesel oil and sodium dodecylbenzene sulfonate in collector A is 4:1:4.
The final obtained closed-circuit test indexes are as follows: the fluorite concentrate contains CaF 2 95.64 percent, and the recovery rate is 81.65 percent; the lepidolite concentrate contains Li 2 O2.60 percent and the recovery rate is 46.20 percent.
Comparative example 18
The only difference compared to example 1 is that the mass ratio of sulfonated oleic acid, diesel oil and sodium dodecylbenzene sulfonate in collector A is 4:4:1.
The final obtained closed-circuit test indexes are as follows: fluorite concentrate contains CaF 2 95.86.86% and has a recovery rate of 79.32%; the lepidolite concentrate contains Li 2 O2.50% and the recovery rate is 48.20%.
According to the invention, the flotation mode is improved, the fluorite lepidolite mixed flotation is selected, and the obtained mixed concentrate is separated, so that the defects of long process flow, multiple medicament types, low recovery rate and the like caused by adopting a method for inhibiting mica flotation of fluorite in the prior art are overcome, and the efficient separation of fluorite lepidolite mixed concentrate resources is realized.
It is stated that the detailed structural features of the present invention are described by the above embodiments, but the present invention is not limited to the above detailed structural features, i.e., it does not mean that the present invention must be implemented depending on the above detailed structural features. It should be apparent to those skilled in the art that any modifications of the present invention, equivalent substitutions of selected components of the present invention, addition of auxiliary components, selection of specific modes, etc., are within the scope of the present invention and the scope of the disclosure.
The preferred embodiments of the present invention have been described in detail above, but the present invention is not limited to the specific details of the above embodiments, and various simple modifications can be made to the technical solution of the present invention within the scope of the technical concept of the present invention, and all the simple modifications belong to the protection scope of the present invention.
In addition, the specific features described in the above embodiments may be combined in any suitable manner, and in order to avoid unnecessary repetition, various possible combinations are not described further.
Moreover, any combination of the various embodiments of the invention can be made without departing from the spirit of the invention, which should also be considered as disclosed herein.
Claims (22)
1. A method for separating fluorite-containing lepidolite concentrate, the method comprising:
Adding an inhibitor and a collector A into fluorite lepidolite concentrate ore pulp to perform roughing operation to obtain fluorite rough concentrate and roughing tailings;
Adding an inhibitor into the fluorite rough concentrate to carry out concentration operation, so as to obtain a fluorite concentrate product;
Pulp mixing is carried out on rough tailings, then a collector B is added for recleaning, lepidolite rough concentrate and recleaning tailings are obtained, and the obtained lepidolite rough concentrate is subjected to blank recleaning to obtain a lepidolite concentrate product;
the inhibitor consists of caustic starch and sodium hydroxide; the collector A consists of sulfonated oleic acid, diesel oil and sodium dodecyl benzene sulfonate; the collector B consists of dodecyl amine and octadecylamine.
2. The separation method according to claim 1, wherein the mass concentration of the solid phase in the fluorite-containing lepidolite concentrate slurry is 20-40%.
3. The separation process of claim 1 wherein the weight ratio of caustic starch to sodium hydroxide in the inhibitor is (4-5): 1.
4. The separation method according to claim 1, wherein the mass ratio of sulfonated oleic acid, diesel oil and sodium dodecyl benzene sulfonate in the collector A is (4-5): 1:1.
5. The separation method according to claim 1, wherein the mass ratio of dodecylamine to octadecylamine in the collector B is 1 to 1.5:1.
6. The separation method according to claim 1, wherein the inhibitor is added in an amount of 10 to 100g/t in the roughing operation.
7. The separation method according to claim 1, wherein the addition amount of the collector A in the roughing operation is 10-50g/t.
8. The separation method of claim 1, wherein the roughing operation is performed at least 1 time.
9. The separation process of claim 1, wherein the rougher tailings are subjected to at least 1 scavenger operation.
10. The separation method according to claim 9, wherein 5-10g/t of collector A is added in the scavenging operation.
11. The separation method as claimed in claim 9, wherein the middlings from the scavenging operation are sequentially returned to the previous operation.
12. The separation method of claim 1, wherein the beneficiation operation is performed at least 3 times.
13. The separation process of claim 1, wherein the inhibitor is added in an amount of 10 to 60g/t.
14. The separation method according to claim 1, wherein the middlings from the beneficiation process are sequentially returned to the previous process.
15. The separation method according to claim 1, wherein the size mixing is to adjust the pH of the rougher tailings to 2-5.
16. The separation method according to claim 1, wherein the addition amount of the re-selected collector B is 5-10g/t.
17. The separation process of claim 1, wherein the recleaning tailings are subjected to at least 1 sweep.
18. The separation method according to claim 17, wherein 1-5g/t of collector B is added during the scanning.
19. The separation method as claimed in claim 17, wherein the middlings obtained in the sweep are sequentially returned to the previous operation.
20. The separation method of claim 1, wherein the blank beneficiation is performed at least 3 times.
21. The separation method according to claim 1, wherein the middlings obtained from the blank beneficiation are sequentially returned to the previous operation.
22. The separation method of claim 1, wherein the separation method comprises:
adding an inhibitor and a collector A into fluorite lepidolite concentrate ore pulp to perform roughing operation to obtain fluorite rough concentrate and roughing tailings; the addition amount of the inhibitor in the roughing operation is 10-100g/t, the addition amount of the collector A in the roughing operation is 10-50g/t, the roughing operation is performed at least 1 time, and the roughing tailings are subjected to at least 1 scavenging operation; the collecting agent A with the concentration of 5-10g/t is added in the scavenging operation, and middlings obtained in the scavenging operation sequentially return to the previous operation;
Adding an inhibitor into the fluorite rough concentrate to carry out concentration operation, so as to obtain a fluorite concentrate product; the carefully chosen operation is carried out for at least 3 times, the addition amount of the inhibitor used in the carefully chosen operation is 10-60g/t, and middlings obtained in the carefully chosen operation sequentially return to the previous operation;
Pulp mixing is carried out on rough tailings, then a collector B is added for recleaning, lepidolite rough concentrate and recleaning tailings are obtained, and the obtained lepidolite rough concentrate is subjected to blank recleaning to obtain a lepidolite concentrate product; the size mixing is to adjust the pH value of the rougher tailings to 2-5; the addition amount of the re-selected collector B is 5-10g/t; at least 1 scavenging is carried out on the recleaning tailings, 1-5g/t of collecting agent B is added in the scavenging, and the middlings obtained in the scavenging sequentially return to the previous operation; the blank concentration is carried out for at least 3 times, and middlings obtained by the blank concentration sequentially return to the previous operation;
The mass concentration of the solid phase in the fluorite-containing lepidolite ore concentrate pulp is 20-40%;
The inhibitor consists of caustic starch and sodium hydroxide, wherein the weight ratio of the caustic starch to the sodium hydroxide in the inhibitor is (4-5) 1;
The collector A consists of sulfonated oleic acid, diesel oil and sodium dodecyl benzene sulfonate, wherein the mass ratio of the sulfonated oleic acid to the diesel oil to the sodium dodecyl benzene sulfonate in the collector A is (4-5) 1:1;
the collector B consists of dodecyl amine and octadecylamine, and the mass ratio of the dodecyl amine to the octadecylamine in the collector B is (1-1.5): 1.
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| CN110560257A (en) * | 2019-09-17 | 2019-12-13 | 长沙三博矿业科技有限公司 | Beneficiation method for recovering associated fluorite from multi-metal tailings |
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| CN110560257A (en) * | 2019-09-17 | 2019-12-13 | 长沙三博矿业科技有限公司 | Beneficiation method for recovering associated fluorite from multi-metal tailings |
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