CN117548236B - Method for reducing tin content in desulfurization flotation foam and application thereof - Google Patents
Method for reducing tin content in desulfurization flotation foam and application thereof Download PDFInfo
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- CN117548236B CN117548236B CN202410038798.2A CN202410038798A CN117548236B CN 117548236 B CN117548236 B CN 117548236B CN 202410038798 A CN202410038798 A CN 202410038798A CN 117548236 B CN117548236 B CN 117548236B
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- flotation
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- tailings
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- 238000005188 flotation Methods 0.000 title claims abstract description 147
- ATJFFYVFTNAWJD-UHFFFAOYSA-N Tin Chemical compound [Sn] ATJFFYVFTNAWJD-UHFFFAOYSA-N 0.000 title claims abstract description 131
- 238000000034 method Methods 0.000 title claims abstract description 72
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 40
- 230000023556 desulfurization Effects 0.000 title claims abstract description 40
- 239000006260 foam Substances 0.000 title claims abstract description 27
- 239000012141 concentrate Substances 0.000 claims abstract description 88
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 71
- 239000011593 sulfur Substances 0.000 claims abstract description 71
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 71
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims abstract description 51
- 230000002000 scavenging effect Effects 0.000 claims abstract description 50
- 239000000463 material Substances 0.000 claims abstract description 48
- 238000000227 grinding Methods 0.000 claims abstract description 29
- 239000002245 particle Substances 0.000 claims abstract description 29
- 230000005484 gravity Effects 0.000 claims abstract description 25
- 229910052500 inorganic mineral Inorganic materials 0.000 claims abstract description 24
- 239000011707 mineral Substances 0.000 claims abstract description 24
- 239000004088 foaming agent Substances 0.000 claims abstract description 17
- 238000002156 mixing Methods 0.000 claims abstract description 14
- 238000000926 separation method Methods 0.000 claims abstract description 14
- 230000001105 regulatory effect Effects 0.000 claims abstract description 7
- XOLBLPGZBRYERU-UHFFFAOYSA-N tin dioxide Chemical compound O=[Sn]=O XOLBLPGZBRYERU-UHFFFAOYSA-N 0.000 claims description 60
- 238000011084 recovery Methods 0.000 claims description 30
- 230000008569 process Effects 0.000 claims description 25
- QWENMOXLTHDKDL-UHFFFAOYSA-N pentoxymethanedithioic acid Chemical compound CCCCCOC(S)=S QWENMOXLTHDKDL-UHFFFAOYSA-N 0.000 claims description 15
- TUZCOAQWCRRVIP-UHFFFAOYSA-N butoxymethanedithioic acid Chemical compound CCCCOC(S)=S TUZCOAQWCRRVIP-UHFFFAOYSA-N 0.000 claims description 13
- DBMJMQXJHONAFJ-UHFFFAOYSA-M Sodium laurylsulphate Chemical compound [Na+].CCCCCCCCCCCCOS([O-])(=O)=O DBMJMQXJHONAFJ-UHFFFAOYSA-M 0.000 claims description 7
- FQENQNTWSFEDLI-UHFFFAOYSA-J sodium diphosphate Chemical compound [Na+].[Na+].[Na+].[Na+].[O-]P([O-])(=O)OP([O-])([O-])=O FQENQNTWSFEDLI-UHFFFAOYSA-J 0.000 claims description 7
- 229940048086 sodium pyrophosphate Drugs 0.000 claims description 7
- 235000019818 tetrasodium diphosphate Nutrition 0.000 claims description 7
- 239000001577 tetrasodium phosphonato phosphate Substances 0.000 claims description 7
- DPXJVFZANSGRMM-UHFFFAOYSA-N acetic acid;2,3,4,5,6-pentahydroxyhexanal;sodium Chemical compound [Na].CC(O)=O.OCC(O)C(O)C(O)C(O)C=O DPXJVFZANSGRMM-UHFFFAOYSA-N 0.000 claims description 6
- 239000001768 carboxy methyl cellulose Substances 0.000 claims description 6
- 235000019353 potassium silicate Nutrition 0.000 claims description 6
- 235000019812 sodium carboxymethyl cellulose Nutrition 0.000 claims description 6
- 229920001027 sodium carboxymethylcellulose Polymers 0.000 claims description 6
- NTHWMYGWWRZVTN-UHFFFAOYSA-N sodium silicate Chemical compound [Na+].[Na+].[O-][Si]([O-])=O NTHWMYGWWRZVTN-UHFFFAOYSA-N 0.000 claims description 6
- -1 alkyl sulfonic acid Chemical compound 0.000 claims description 5
- 238000007670 refining Methods 0.000 claims description 4
- WUOACPNHFRMFPN-UHFFFAOYSA-N alpha-terpineol Chemical compound CC1=CCC(C(C)(C)O)CC1 WUOACPNHFRMFPN-UHFFFAOYSA-N 0.000 claims description 2
- SQIFACVGCPWBQZ-UHFFFAOYSA-N delta-terpineol Natural products CC(C)(O)C1CCC(=C)CC1 SQIFACVGCPWBQZ-UHFFFAOYSA-N 0.000 claims description 2
- 229940116411 terpineol Drugs 0.000 claims description 2
- 230000000052 comparative effect Effects 0.000 description 29
- 238000005406 washing Methods 0.000 description 16
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 14
- 238000003756 stirring Methods 0.000 description 10
- 235000019333 sodium laurylsulphate Nutrition 0.000 description 6
- AFNRRBXCCXDRPS-UHFFFAOYSA-N tin(ii) sulfide Chemical compound [Sn]=S AFNRRBXCCXDRPS-UHFFFAOYSA-N 0.000 description 6
- DSCFFEYYQKSRSV-UHFFFAOYSA-N 1L-O1-methyl-muco-inositol Natural products COC1C(O)C(O)C(O)C(O)C1O DSCFFEYYQKSRSV-UHFFFAOYSA-N 0.000 description 5
- VJXUJFAZXQOXMJ-UHFFFAOYSA-N D-1-O-Methyl-muco-inositol Natural products CC12C(OC)(C)OC(C)(C)C2CC(=O)C(C23OC2C(=O)O2)(C)C1CCC3(C)C2C=1C=COC=1 VJXUJFAZXQOXMJ-UHFFFAOYSA-N 0.000 description 5
- DSCFFEYYQKSRSV-KLJZZCKASA-N D-pinitol Chemical compound CO[C@@H]1[C@@H](O)[C@@H](O)[C@H](O)[C@H](O)[C@H]1O DSCFFEYYQKSRSV-KLJZZCKASA-N 0.000 description 5
- 238000005273 aeration Methods 0.000 description 5
- 239000003153 chemical reaction reagent Substances 0.000 description 5
- 230000000694 effects Effects 0.000 description 4
- 239000010419 fine particle Substances 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 229910052569 sulfide mineral Inorganic materials 0.000 description 4
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 229910052683 pyrite Inorganic materials 0.000 description 3
- 239000011028 pyrite Substances 0.000 description 3
- NIFIFKQPDTWWGU-UHFFFAOYSA-N pyrite Chemical compound [Fe+2].[S-][S-] NIFIFKQPDTWWGU-UHFFFAOYSA-N 0.000 description 3
- 239000010453 quartz Substances 0.000 description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 3
- 238000001179 sorption measurement Methods 0.000 description 3
- 239000002562 thickening agent Substances 0.000 description 3
- 239000002253 acid Substances 0.000 description 2
- 230000033558 biomineral tissue development Effects 0.000 description 2
- 239000008396 flotation agent Substances 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- NLYAJNPCOHFWQQ-UHFFFAOYSA-N kaolin Chemical compound O.O.O=[Al]O[Si](=O)O[Si](=O)O[Al]=O NLYAJNPCOHFWQQ-UHFFFAOYSA-N 0.000 description 2
- 229910052622 kaolinite Inorganic materials 0.000 description 2
- 239000012991 xanthate Substances 0.000 description 2
- 229910021532 Calcite Inorganic materials 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 238000005054 agglomeration Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000003750 conditioning effect Effects 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- YGANSGVIUGARFR-UHFFFAOYSA-N dipotassium dioxosilane oxo(oxoalumanyloxy)alumane oxygen(2-) Chemical compound [O--].[K+].[K+].O=[Si]=O.O=[Al]O[Al]=O YGANSGVIUGARFR-UHFFFAOYSA-N 0.000 description 1
- 238000010494 dissociation reaction Methods 0.000 description 1
- 230000005593 dissociations Effects 0.000 description 1
- 229910000514 dolomite Inorganic materials 0.000 description 1
- 239000010459 dolomite Substances 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 229910052976 metal sulfide Inorganic materials 0.000 description 1
- 239000011859 microparticle Substances 0.000 description 1
- 238000005065 mining Methods 0.000 description 1
- 229910052627 muscovite Inorganic materials 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 229910052950 sphalerite Inorganic materials 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000004448 titration Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D1/00—Flotation
- B03D1/02—Froth-flotation processes
-
- 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
- B03B1/00—Conditioning for facilitating separation by altering physical properties of the matter to be treated
-
- 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
- B03B1/00—Conditioning for facilitating separation by altering physical properties of the matter to be treated
- B03B1/04—Conditioning for facilitating separation by altering physical properties of the matter to be treated by additives
-
- 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
- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention relates to the technical field of mineral separation, in particular to a method for reducing tin content in desulfurization flotation foam and application thereof. The method comprises the following steps: grinding the gravity tailings to obtain a ground mineral material, removing particles with the granularity lower than 0.01-0.02 mm, adding a first regulator and a second regulator, regulating the pH value to 6-8 to obtain a material to be floated, mixing the material with a sulphide ore flotation collector and a foaming agent, and carrying out primary flotation roughing through a flotation machine to obtain roughing concentrate and roughing tailings; the roughing tailings are subjected to three scavenging by a flotation machine, and scavenging concentrate obtained by the three scavenging is sequentially returned to the upper working procedure to form circulation; and (3) carrying out three blank concentration on the rougher concentrate through a cyclone-static flotation column to obtain sulfur concentrate and sulfur-containing tin middlings, and mixing the sulfur-containing tin middlings with tin tailings obtained through three scavenging for later use. The method can effectively reduce the tin content in the desulfurization flotation foam and solve the problem of serious tin inclusion in the desulfurization flotation foam.
Description
Technical Field
The invention relates to the technical field of mineral separation, in particular to a method for reducing tin content in desulfurization flotation foam and application thereof.
Background
Cassiterite is a major tin-containing mineral that is often co-present with metal sulphide ores. With rapid mining of high-grade rich ores, development of lean, fine and miscellaneous tin polymetallic ore resources is increasingly important. Currently, cassiterite is recovered mainly through combined processes such as gravity separation, flotation and the like according to the difference of the granularity and the composition of the cassiterite. Flotation is an effective recovery means for fine-grained cassiterite. However, since the micro-fine cassiterite also contains a large amount of sulfide ores, the cassiterite has poor collecting effect due to the existence of the sulfide ores, and the consumption of flotation agents is large, so that the quality of cassiterite concentrate products is reduced, desulfurization flotation operation is usually carried out before micro-fine cassiterite flotation, so that adverse effects caused by the sulfide ores are eliminated.
However, because the cassiterite has finer granularity, the cassiterite is extremely easy to mud, entrainment is extremely easy to occur in the desulfurization flotation process, and the cassiterite is lost in sulphide ore foam.
In view of this, the present invention has been made.
Disclosure of Invention
The first object of the invention is to provide a method for reducing the tin content in desulfurization flotation froth, which can effectively reduce the tin content in the desulfurization flotation froth and solve the problem that cassiterite is lost in sulphide ore froth due to entrainment in the desulfurization flotation process.
A second object of the invention is to provide the use of a method for reducing the tin content of a desulphurised flotation froth in the recovery of cassiterite.
In order to achieve the above object of the present invention, the following technical solutions are specifically adopted:
The invention firstly provides a method for reducing tin content in desulfurization flotation foam, which comprises the following steps:
grinding the gravity tailings obtained through gravity separation to enable the particle size of particles with the granularity of less than 0.074mm to account for 70% -85%, so as to obtain a ground mineral material; wherein the mass fraction of tin element in the gravity tailings is 0.6% -0.9%, and the mass fraction of sulfur element is 5.9% -6.9%;
Removing particles with the granularity lower than 0.01-0.02 mm in the ore grinding material, adding a first regulator and a second regulator into the ore grinding material, and regulating the pH value of the mixed material to 6-8 to obtain a material to be floated; the first regulator comprises at least one of water glass and sodium pyrophosphate; the second regulator comprises at least one of sodium carboxymethyl cellulose and sodium dodecyl sulfate;
Mixing the material to be floated with a sulfide ore flotation collector and a foaming agent, and carrying out primary flotation roughing through a flotation machine to obtain roughing concentrate and roughing tailings;
The roughing tailings are subjected to three scavenging by the flotation machine, and scavenging concentrate obtained by the three scavenging is sequentially returned to the upper working procedure to form circulation;
And carrying out three blank concentration on the rougher concentrate through a cyclone-static flotation column to obtain sulfur concentrate and sulfur-containing tin middlings, and mixing the sulfur-containing tin middlings with the tin-containing tailings obtained by three scavenging for standby.
Preferably, the mass of the first regulator added into each ton of the ore grinding material is 800-1000 g.
Preferably, the mass of the second regulator added in each ton of the ore grinding material is 1200-1800g.
Preferably, after the pH of the mixture is adjusted to 6-8, stirring is carried out for 5-10 min.
Preferably, the sulphide ore flotation collector comprises the following components in percentage by mass: 1-2 butyl xanthate and amyl xanthate.
Preferably, in the primary flotation roughing process, the mass of the sulphide ore flotation collector added into each ton of the material to be floated is 50-400 g.
Preferably, the foaming agent comprises at least one of terpineol and alkyl sulphonic acid.
Preferably, in the primary flotation roughing process, the mass of the foaming agent added into each ton of the material to be floated is 10-60 g.
Preferably, in the first scavenging and the second scavenging in the three scavenging processes, the mass of the sulphide ore flotation collector added into each ton of rougher tailings is 50-400 g.
Preferably, in the first scavenging and the second scavenging in the three scavenging processes, the mass of the foaming agent added into each ton of roughing tailings is 10-60 g.
Preferably, in three blank refining, in each blank refining process, the mass of the sulphide ore flotation collector added into each ton of rougher concentrate is 30-100 g.
Preferably, the circulation pressure of the cyclone-static flotation column is 0.15-0.22 mpa, the air charging amount is 1200-4000L/h, and the thickness of a foam layer is 5-15 cm.
Preferably, particles smaller than 0.01-0.02 mm in the ground mineral aggregate are removed through a cyclone;
The ore feeding pressure of the cyclone is 0.05-0.15 mpa.
Preferably, the mass fraction of tin element in the sulfur concentrate is less than or equal to 0.25%.
Preferably, the recovery rate of tin element in the sulfur concentrate is less than or equal to 2.65 percent.
The invention also provides application of the method for reducing the tin content in the desulfurization flotation froth in the recovery of cassiterite.
Compared with the prior art, the invention has the beneficial effects that:
(1) According to the method for reducing the tin content in the desulfurization flotation froth, the particles with the size less than 0.01-0.02 mm in the ground ore material are removed before flotation, the first regulator and the second regulator are added, the pH value is regulated, and meanwhile, the flotation machine and the flotation column are adopted for combined separation, so that the tin content in the desulfurization flotation froth can be effectively reduced, namely the cassiterite content in sulfur concentrate obtained after desulfurization flotation is reduced. Solves the serious problem of the desulfurization flotation foam tin inclusion.
(2) According to the method for reducing the tin content in the desulfurization flotation foam, the particles smaller than 0.01-0.02 mm in the ore grinding material are removed before flotation, so that the interference of fine mineral particles on flotation is reduced, and the tin element content in sulphide ores is reduced.
(3) The method for reducing the tin content in the desulfurization flotation froth provided by the invention is simple in flow, and can obviously reduce the tin content in the desulfurization flotation froth, namely effectively reduce the tin content in the sulfur concentrate and the tin recovery rate, wherein the mass fraction of tin element in the sulfur concentrate is reduced to below 0.25%, and the tin recovery rate is reduced to below 2.65%, so that not only is the tin resource loss effectively reduced, but also the quality of the sulfide ore is improved, the subsequent process flow is reduced, and the subsequent treatment cost of the sulfide ore is reduced.
Detailed Description
The technical solutions of the present invention will be clearly and completely described in conjunction with the following detailed description, but it will be understood by those skilled in the art that the examples described below are some examples of the present invention, but not all examples, which are merely illustrative of the present invention and should not be construed as limiting the scope of the present invention. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention. The specific conditions are not noted in the examples and are carried out according to conventional conditions or conditions recommended by the manufacturer. The reagents or apparatus used were conventional products commercially available without the manufacturer's attention.
In the present invention, unless specifically stated otherwise, the terms "first", "second", "third", "fourth", etc. are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or quantity or as implicitly indicating the importance or quantity of the indicated technical feature. Moreover, the terms "first," "second," "third," "fourth," and the like are used for non-exhaustive list description purposes only, and are not to be construed as limiting the number of closed forms.
The terms "comprising" and "including" as used herein mean open ended or closed ended, unless otherwise noted. For example, the terms "comprising" and "comprises" may mean that other components not listed may be included or included, or that only listed components may be included or included.
In the present invention, "one or more" or "at least one" means any one, any two or more of the listed items unless specifically stated otherwise. Wherein "several" means any two or more.
In a first aspect, the invention provides a method for reducing tin content in desulfurization flotation froth based on a selective washing (beneficiation) process, which has simple means, low carbon and short flow, and specifically comprises the following steps:
Grinding the gravity tailings obtained through gravity separation, so that the particle ratio of particles with the granularity of less than 0.074mm is 70% -85%, including but not limited to any one point value or any range value between any two points of 70%, 72%, 73%, 75%, 78%, 80%, 82%, 84% and 85%, and obtaining the grinding material.
Wherein, the purpose of grinding is: through the adjustment of the grinding medium and the grinding time, the dissociation degree of minerals is increased, so that cassiterite is fully separated from sulphide ores, and coordination bonds on the surface of the sulphide ores, which interact with flotation agents, are increased; on the other hand, the exposed surface of the cassiterite is selectively changed, the adsorption of the flotation reagent on the surface of the cassiterite is reduced, the selective adsorption of the reagent on the surface of the ore is realized, and the content of the cassiterite in the sulfide ore foam is realized.
The grinding may be performed by any grinding apparatus, such as a ball mill, but is not limited thereto.
Wherein the mass fraction of tin element in the gravity tailings is 0.6% -0.9%, including but not limited to any one point value or any range value between any two of 0.6%, 0.65%, 0.67%, 0.69%, 0.7%, 0.72%, 0.75%, 0.78%, 0.8%, 0.82%, 0.84%, 0.9%; the mass fraction of the sulfur element is 5.9% -6.9%, including but not limited to any one point value or a range value between any two of 5.9%, 5.91%, 6%, 6.1%, 6.2%, 6.3%, 6.4%, 6.5%, 6.6%, 6.7%, 6.8%, 6.88% and 6.9%.
And then removing particles with the granularity lower than 0.01-0.02 mm (including but not limited to point values of any one of 0.02mm, 0.019mm, 0.018mm, 0.017mm, 0.016mm, 0.015mm, 0.013mm, 0.012mm and 0.01mm or range values between any two), adding a first regulator and a second regulator into the ground mineral, and adjusting the pH of the mixed material to 6-8 (including but not limited to point values of any one of 6, 6.3, 6.5, 6.8, 7, 7.2, 7.5, 7.8 and 8 or range values between any two) to obtain the material to be floated.
The purpose of removing particles with the granularity lower than 0.01-0.02 mm in the ore grinding material is as follows: the interference of fine-grain mineral particles on flotation is reduced, and the tin content in sulfide ore foam is reduced. If the particle size of the removed particles is too large, fine-grained cassiterite is mixed into the sulfide ore foam, and the resource utilization rate of the cassiterite is reduced.
The first regulator comprises at least one of water glass and sodium pyrophosphate; the second regulator includes at least one of sodium carboxymethyl cellulose and sodium dodecyl sulfate. Wherein the first regulator and the second regulator play roles of: the agglomeration of the fine-grain cassiterite is reduced, and the floatability of the cassiterite is weakened.
The purpose of adjusting the pH of the mixed material to 6-8 is that: the oxide film on the surface of the sulphide ore is reduced, and the floatability of the sulphide ore is increased.
In some embodiments, the pH of the mixture is adjusted to 6-8 with an acid, such as hydrochloric acid, but not limited thereto.
The desulfurization flotation of the invention adopts a flotation machine and a flotation column to combine and separate. Specifically, the material to be floated is mixed with a sulphide ore floatation collector and a foaming agent, and primary floatation roughing is carried out through a floatation machine, so that roughing concentrate and roughing tailings are obtained.
Wherein, sulphide ore flotation collector plays the effect: the polar groups on the surface of the collector are selectively coordinated with coordination bonds on the surface of the minerals, so that the floatability of the sulphide ores is improved, and the loss of the sulphide ores in the tailings is reduced.
The foaming agent has the following functions: increasing mineralization floatability.
And then, carrying out three scavenging on the roughing tailings through the flotation machine so as to remove sulfide minerals, and sequentially returning scavenging concentrate obtained by the three scavenging to an upper working procedure to form circulation.
And carrying out three blank concentration on the roughing concentrate through a cyclone-static flotation column to obtain sulfur concentrate and sulfur-containing tin middlings, mixing the sulfur-containing tin middlings and tin-containing tailings obtained through three scavenging for standby, and entering a subsequent separation operation.
Wherein the blank beneficiation does not add a flotation reagent, e.g., neither a flotation collector nor a frother.
By performing the blank concentration three times, the quality of the concentrate can be increased, and the impurities in the concentrate or the intergrowth of the minerals containing the impurities are abandoned.
According to the method for reducing the tin content in the desulfurization flotation foam, the particles with the particle size smaller than 0.01-0.02 mm in the ground ore material are removed before flotation, the first regulator and the second regulator are added, the pH value is regulated, and meanwhile, the floatation machine and the floatation column are adopted for combined separation, so that the cassiterite content in sulfur concentrate obtained after desulfurization flotation can be effectively reduced.
Furthermore, the invention adopts the cyclone-static flotation column to carry out further carefully choosing operation on the basis of pre-choosing of the flotation machine, can adapt to a flotation ore pulp system rich in micro-particles, has higher choosing efficiency and obviously reduces tin inclusion of sulphide ores.
In some specific embodiments, the mass of the first regulator added in each ton of the grinding material is 800-1000 g; including but not limited to a point value of any one of 800g, 850g, 900g, 950g, 1000g, or a range value between any two.
In some embodiments, the mass of the second conditioning agent added per ton of the mill feed is 1200-1800 g, including but not limited to a point value of any one of 1200g, 1300g, 1400g, 1500g, 1600g, 1700g, 1800g, or a range value between any two.
The first regulator and the second regulator with the above dosage can effectively reduce the tin content in the sulphide ore concentrate.
In some specific embodiments, after the pH of the mixture is adjusted to 6-8, stirring is performed for 5-10 min, including, but not limited to, any one point value or any range value between any two of 5min, 6min, 7min, 8min, 9min, and 10 min.
After the pH is regulated, stirring is carried out, so that an oxide layer on the surface of the sulfide ore can be reduced, and the adsorption effect of the sulfide ore and the medicament can be increased.
In some specific embodiments, the sulphide ore flotation collector comprises the following components in mass ratio of 3-4: 1-2 butyl xanthate and amyl xanthate, e.g., 3:1, 3:2, 4:1 or 4:2.
Meanwhile, butyl xanthate and amyl xanthate are mixed for use, so that the floatability of the lead-containing mineral can be improved, and the recovery rate of lead-containing sulfide can be improved.
In some specific embodiments, in the primary flotation roughing process, the mass of the sulphide ore flotation collector added into each ton of the material to be floated is 50-400 g; including but not limited to a point value of any one of 50g, 70g, 80g, 100g, 120g, 150g, 180g, 200g, 230g, 250g, 280g, 400g, or a range value therebetween.
In some embodiments, the foaming agent comprises at least one of a pinitol oil and an alkyl sulfonic acid.
In some specific embodiments, in the process of primary flotation roughing, the mass of the foaming agent added in each ton of the material to be floated is 10-60 g, including but not limited to a point value of any one of 10g, 20g, 30g, 40g, 50g and 60g or a range value between any two.
In some specific embodiments, in the first scavenging and the second scavenging in the three scavenging, the mass of the sulphide flotation collector added into each ton of the rougher tailings is 50-400 g; including but not limited to a point value of any one of 50g, 70g, 80g, 100g, 120g, 150g, 180g, 200g, 230g, 250g, 280g, 400g, or a range value therebetween.
In some specific embodiments, in the first scavenging and the second scavenging of the three scavenging processes, the mass of the foaming agent added in each ton of the roughing tailings is 10-60 g, including but not limited to a point value of any one of 10g, 20g, 30g, 40g, 50g and 60g or a range value between any two.
In some specific embodiments, in three blank refinements, the mass of the sulphide ore flotation collector added in each ton of the rougher concentrate is 30-100 g in each blank refinement process, including but not limited to a point value of any one of 30g, 40g, 50g, 60g, 70g, 80g, 90g, 100g or a range value between any two.
In some specific embodiments, the circulating pressure of the cyclone-static flotation column is 0.15-0.22 Mpa, including but not limited to a point value of any one of 0.15Mpa, 0.16Mpa, 0.17Mpa, 0.19Mpa, 0.2Mpa, 0.21Mpa, 0.22Mpa, or a range value between any two of them; the inflation amount is 1200-4000L/h, including but not limited to any one point value or any range value between two points in 1200L/h、1300L/h、1500L/h、1800L/h、2000L/h、2200L/h、2500L/h、2800L/h、3000L/h、3300L/h、3500L/h、3800L/h、4000L/h; the thickness of the foam layer is 5-15 cm, including but not limited to a point value of any one of 5cm, 7cm, 8cm, 10cm, 12cm, 14cm, 15cm or a range value between any two.
The cyclone-static flotation column adopts the circulating pressure, the aeration quantity and the foam layer thickness, so that the mineralization degree of foam can be improved, the secondary enrichment of minerals in the foam layer is realized, and the loading quantity of tin-containing minerals is reduced.
In some specific embodiments, the particles less than 0.01-0.02 mm in the grinding material are removed by a cyclone, but not limited thereto.
The cyclone has the advantage of high-efficiency separation of fine-grained minerals, and can realize high-efficiency separation of minerals with the particle size of less than 0.01-0.02 mm in raw materials.
In some specific embodiments, the feeding pressure of the cyclone is 0.05-0.15 Mpa, including but not limited to any one of 0.05Mpa, 0.08Mpa, 0.10Mpa, 0.12Mpa, 0.14Mpa, 0.15Mpa, or a range between any two.
In some specific embodiments, the mass fraction of tin in the sulfur concentrate is less than or equal to 0.25%, including, but not limited to, a point value of any one of 0.25%, 0.24%, 0.22%, 0.20%, 0.18%, 0.15%, 0.12%, 0.10%, 0.08%, 0.07%, or a range value between any two.
In some embodiments, the recovery of tin element in the sulfur concentrate is less than or equal to 2.65%, including but not limited to a point value of any one of 2.56%, 2.5%, 2.3%, 2.1%, 2%, 1.8%, 1.5%, 1.3%, 1.27%, or a range value between any two.
The method for reducing the tin content in the desulfurization flotation froth can effectively reduce the tin content in the sulfur concentrate.
In a second aspect, the invention provides the use of the method for reducing the tin content of desulphurised flotation froth in the recovery of cassiterite.
The method can obviously reduce the tin content in the sulfide ore foam, namely effectively reduce the cassiterite content in the sulfur concentrate obtained after desulfurization and flotation.
Embodiments of the present invention will be described in detail below with reference to examples, but it will be understood by those skilled in the art that the following examples are only for illustrating the present invention and should not be construed as limiting the scope of the present invention. The specific conditions are not noted in the examples and are carried out according to conventional conditions or conditions recommended by the manufacturer. The reagents or apparatus used were conventional products commercially available without the manufacturer's attention.
Example 1
The method for reducing the tin content in the desulfurization flotation foam based on the selective washing process provided by the embodiment comprises the following steps:
(1) Grinding the gravity tailings of the shaking table through a ball mill to enable the proportion of particles with the granularity lower than 0.074mm to be 73.50%, and obtaining the grinding material. The gravity concentration tailings of the shaking table are tin polymetallic ores in Guangxi places, the main mineral components of the ores are cassiterite, pyrite, quartz, calcite and the like, the mass fraction of tin element in the gravity concentration tailings of the shaking table is 0.67%, and the mass fraction of sulfur element in the gravity concentration tailings of the shaking table is 6.62%.
(2) And (3) feeding the ground ore obtained in the step (1) into a cyclone to remove fine particles with the granularity lower than 0.019mm, enabling overflow of the cyclone to enter a sloping plate thickener, enabling underflow of the cyclone to enter subsequent flotation operation, and enabling ore feeding pressure of the cyclone to be 0.10Mpa.
(3) Feeding the underflow of the cyclone into a stirring barrel for pulp mixing treatment: 1000g/t water glass and 1800g/t sodium carboxymethyl cellulose (namely 1000g of water glass and 1800g of sodium carboxymethyl cellulose are added into each ton of ground mineral material), then hydrochloric acid is used for regulating the pH value of ore pulp to 6, and stirring is carried out for 8min, so as to obtain the material to be floated.
(4) Adding 150g/t sulfide ore flotation collector butyl xanthate and amyl xanthate into the material to be floated obtained in the step (3), wherein the mass ratio of the butyl xanthate to the amyl xanthate is 3: and 2, adding 60g/t foaming agent pinitol oil, and carrying out primary flotation roughing through a flotation machine to obtain roughing concentrate and roughing tailings.
(5) And (3) carrying out three scavenging on the roughing tailings obtained in the step (4) through a flotation machine to remove sulfide minerals, and sequentially returning scavenging concentrate obtained in the three scavenging to an upper-level operation to form circulation, wherein in each scavenging, the mass of a sulfide ore floatation collector butyl xanthate and amyl xanthate (in the mass ratio of the step (4)) is 100g, and the mass of the pinitol oil is 60g.
(6) And (3) carrying out three blank concentration on the roughing concentrate obtained in the step (4) through a cyclone-static flotation column to obtain sulfur concentrate and sulfur-tin-containing middlings, and mixing the sulfur-tin-containing middlings and tin-containing tailings obtained through three scavenging to enter a subsequent separation operation. Wherein, 100g of sulphide ore flotation collector is added into each ton of rougher concentrate in each blank concentration process. The circulation pressure of the cyclone-static flotation column is 0.22Mpa, the aeration quantity is 1800L/h, and the thickness of a foam layer is 15cm.
The mass fraction of tin element in the sulfur concentrate obtained in this example was 0.24%, and the recovery rate of tin element in the sulfur concentrate was 1.89%.
The mass fraction of tin element in each example of the present invention and each comparative example was measured by a pyrometallurgical titration process.
Recovery of tin element in sulfur concentrate = (mass of sulfur concentrate x mass fraction of tin element in sulfur concentrate)/(mass of concentrator gravity tailings x mass fraction of tin element in concentrator gravity tailings) ×100%.
Example 2
The method for reducing the tin content in the desulfurization flotation foam based on the selective washing process provided by the embodiment comprises the following steps:
(1) Grinding the gravity tailings of the shaking table through a ball mill to make the proportion of particles with the granularity lower than 0.074mm be 80%, thus obtaining the grinding material. The gravity concentration tailings of the shaking table are tin polymetallic ores in a certain place in Yunnan, the main mineral components of the ores are cassiterite, pyrite, quartz, muscovite, kaolinite and the like, the mass fraction of tin element in the gravity concentration tailings of the shaking table is 0.84%, and the mass fraction of sulfur element in the gravity concentration tailings of the shaking table is 5.91%.
(2) And (3) feeding the ground ore obtained in the step (1) into a cyclone to remove fine particles with the granularity lower than 0.019mm, enabling the overflow of the cyclone to enter a sloping plate thickener, enabling the underflow of the cyclone to enter the subsequent flotation operation, and enabling the ore feeding pressure of the cyclone to be 0.12Mpa.
(3) Feeding the underflow of the cyclone into a stirring barrel for pulp mixing treatment: 800g/t water glass and 1550g/t sodium carboxymethyl cellulose are added, then hydrochloric acid is used for adjusting the pH value of ore pulp to 6, and stirring is carried out for 5min, so that the material to be floated is obtained.
(4) And (3) adding 300g/t sulfide ore flotation collectors butyl xanthate and amyl xanthate into the material to be subjected to flotation obtained in the step (3), wherein the mass ratio of the butyl xanthate to the amyl xanthate is 3:1, adding 15g/t foaming agent pinitol oil, and carrying out primary flotation roughing through a flotation machine to obtain roughing concentrate and roughing tailings.
(5) And (3) carrying out three scavenging on the roughing tailings obtained in the step (4) through a flotation machine to remove sulfide minerals, and sequentially returning scavenging concentrate obtained in the three scavenging to an upper-level operation to form circulation, wherein in each scavenging, the mass of a sulfide ore flotation collector butyl xanthate and amyl xanthate (the mass ratio of butyl xanthate to amyl xanthate) is 200g and the mass of the pinitol oil is 15g in each ton of roughing tailings.
(6) And (3) carrying out three blank concentration on the roughing concentrate obtained in the step (4) through a cyclone-static flotation column to obtain sulfur concentrate and sulfur-tin-containing middlings, and mixing the sulfur-tin-containing middlings and tin-containing tailings obtained through three scavenging to enter a subsequent separation operation. Wherein 80g of sulphide ore flotation collector is added into each ton of rougher concentrate in each blank concentration process. The circulation pressure of the cyclone-static flotation column is 0.15Mpa, the aeration quantity is 1200L/h, and the thickness of the foam layer is 5cm.
The mass fraction of tin element in the sulfur concentrate obtained in this example was 0.21%, and the recovery rate of tin element in the sulfur concentrate was 1.27%.
Example 3
The method for reducing the tin content in the desulfurization flotation foam based on the selective washing process provided by the embodiment comprises the following steps:
(1) Grinding the gravity tailings of the shaking table through a ball mill to enable the proportion of particles with the granularity lower than 0.074mm to be 85%, and obtaining the grinding material. The gravity concentration tailings of the shaking table are tin polymetallic ores in a certain place in Guizhou, the main mineral components of the ore are cassiterite, pyrite, a small amount of sphalerite, quartz, kaolinite, dolomite and the like, the mass fraction of tin element in the gravity concentration tailings of the shaking table is 0.75%, and the mass fraction of sulfur element in the gravity concentration tailings of the shaking table is 6.88%.
(2) And (3) feeding the ground ore obtained in the step (1) into a cyclone to remove fine particles with the granularity lower than 0.019mm, enabling the overflow of the cyclone to enter a sloping plate thickener, enabling the underflow of the cyclone to enter the subsequent flotation operation, and enabling the ore feeding pressure of the cyclone to be 0.15Mpa.
(3) Feeding the underflow of the cyclone into a stirring barrel for pulp mixing treatment: adding 800g/t sodium pyrophosphate and 1200g/t sodium dodecyl sulfate, then adjusting the pH value of the ore pulp to 6 by using hydrochloric acid, and stirring for 8min to obtain the material to be floated.
(4) Adding 350g/t sulfide ore flotation collector butyl xanthate and amyl xanthate into the material to be floated obtained in the step (3), wherein the mass ratio of the butyl xanthate to the amyl xanthate is 4:1, adding 60g/t foaming agent alkyl sulfonic acid, and carrying out primary flotation roughing through a flotation machine to obtain roughing concentrate and roughing tailings.
(5) And (3) carrying out three scavenging on the roughing tailings obtained in the step (4) through a flotation machine to remove sulfide minerals, and sequentially returning scavenging concentrate obtained in the three scavenging to an upper-level operation to form circulation, wherein in each scavenging, the mass of a sulfide ore flotation collector butyl xanthate and amyl xanthate (the mass ratio of butyl xanthate to amyl xanthate) is 150g and the mass of alkylsulfonic acid is 60g in each ton of roughing tailings.
(6) And (3) carrying out three blank concentration on the roughing concentrate obtained in the step (4) through a cyclone-static flotation column to obtain sulfur concentrate and sulfur-tin-containing middlings, and mixing the sulfur-tin-containing middlings and tin-containing tailings obtained through three scavenging to enter a subsequent separation operation. Wherein, 100g of sulphide ore flotation collector is added into each ton of rougher concentrate in each blank concentration process. The circulation pressure of the cyclone-static flotation column is 0.22Mpa, the aeration quantity is 2000L/h, and the thickness of the foam layer is 5cm.
The mass fraction of tin element in the sulfur concentrate obtained in this example was 0.18%, and the recovery rate of tin element in the sulfur concentrate was 1.32%.
Example 4
The method for reducing tin content in desulfurization flotation froth based on the selective washing process provided in this example is basically the same as that in example 3, except that in step (2), the ground mineral aggregate is fed into a cyclone to remove fine particles with a particle size of less than 0.01 mm.
The mass fraction of tin element in the sulfur concentrate obtained in this example was 0.10%, and the recovery rate of tin element in the sulfur concentrate was 2.17%.
Example 5
The method for reducing tin content in desulphurized flotation froth based on the selective washing process provided in this example is basically the same as in example 3, except that in step (3), hydrochloric acid is used to adjust the pH of the pulp to 7.
The mass fraction of tin element in the sulfur concentrate obtained in this example was 0.092%, and the recovery rate of tin element in the sulfur concentrate was 2.65%.
Example 6
The method for reducing tin content in desulphurized flotation froth based on the selective washing process provided in this example is basically the same as in example 3, except that in step (3), hydrochloric acid is used to adjust the pH of the pulp to 8.
The mass fraction of tin element in the sulfur concentrate obtained in this example was 0.089%, and the recovery rate of tin element in the sulfur concentrate was 1.51%.
Example 7
The method for reducing tin content in desulfurization flotation froth based on the selective washing process provided in this embodiment is basically the same as that of embodiment 3, except that in step (6), the circulation pressure of the cyclone-static flotation column is 0.20Mpa, the aeration amount is 3500L/h, and the froth layer thickness is 10cm.
The mass fraction of tin element in the sulfur concentrate obtained in this example was 0.14%, and the recovery rate of tin element in the sulfur concentrate was 1.63%.
Comparative example 1
The method for reducing the tin content in the desulfurization flotation froth based on the selective washing process provided in this comparative example is basically the same as that in example 3, except that step (2) is not performed, i.e., the mill mineral obtained in step (1) is directly placed in a stirring tank to perform the size mixing treatment.
The mass fraction of tin element in the sulfur concentrate obtained in this comparative example was 0.38%, and the recovery rate of tin element in the sulfur concentrate was 6.24%.
Comparative example 2
The method for reducing tin content in desulphurized flotation froth based on the selective washing process provided in this comparative example was essentially the same as in example 3, except that the grinding in step (1) was performed with a 60% particle fraction of less than 0.074 mm.
The mass fraction of tin element in the sulfur concentrate obtained in this comparative example was 0.42%, and the recovery rate of tin element in the sulfur concentrate was 6.34%.
Comparative example 3
The method for reducing tin content in desulphurized flotation froth based on the selective washing process provided in this comparative example is essentially the same as in example 3, except that in step (2) the mill base is fed into a cyclone to remove fines having a particle size below 0.03 mm.
The mass fraction of tin element in the sulfur concentrate obtained in this comparative example was 0.42%, and the recovery rate of tin element in the sulfur concentrate was 5.87%.
Comparative example 4
The method for reducing tin content in desulphurized flotation froth based on the selective washing process provided in this comparative example is essentially the same as in example 3, except that in step (3), the pH is not adjusted.
The mass fraction of tin element in the sulfur concentrate obtained in this comparative example was 0.48%, and the recovery rate of tin element in the sulfur concentrate was 7.05%.
Comparative example 5
The method for reducing tin content in desulphurized flotation froth based on the selective washing process provided in this comparative example is essentially the same as in example 3, except that in step (3) hydrochloric acid is used to adjust the pH of the pulp to 5.
The mass fraction of tin element in the sulfur concentrate obtained in this comparative example was 0.51%, and the recovery rate of tin element in the sulfur concentrate was 7.32%.
Comparative example 6
The method for reducing tin content in the desulphurized flotation froth based on the selective washing process provided in this comparative example is essentially the same as in example 3, except that in step (3), sodium pyrophosphate is replaced by sodium lauryl sulfate of equal mass (i.e. sodium pyrophosphate is not added).
The mass fraction of tin element in the sulfur concentrate obtained in this comparative example was 0.46%, and the recovery rate of tin element in the sulfur concentrate was 6.87%.
Comparative example 7
The method for reducing tin content in the desulphurized flotation froth based on the selective washing process provided in this comparative example is essentially the same as in example 3, except that in step (3) sodium dodecyl sulfate is replaced by sodium pyrophosphate of equal mass (i.e. sodium dodecyl sulfate is not added).
The mass fraction of tin element in the sulfur concentrate obtained in this comparative example was 0.47%, and the recovery rate of tin element in the sulfur concentrate was 7.92%.
Comparative example 8
The method for reducing tin content in desulphurized flotation froth based on the flotation process provided in this comparative example is essentially the same as in example 3, except that in step (4) one flotation rougher is performed by means of a cyclone-static flotation column and in step (5) three scavenging is performed by means of a cyclone-static flotation column.
The mass fraction of tin element in the sulfur concentrate obtained in this comparative example was 0.58%, and the recovery rate of tin element in the sulfur concentrate was 6.67%.
Comparative example 9
The method for reducing tin content in desulphurized flotation froth based on the flotation process provided in this comparative example is essentially the same as in example 3, except that in step (6) three blank beneficiations are performed by the flotation machine.
The mass fraction of tin element in the sulfur concentrate obtained in this comparative example was 0.54%, and the recovery rate of tin element in the sulfur concentrate was 7.84%.
As can be seen from the results of the comparative examples, by adopting the method for reducing the tin content in the desulfurization flotation froth by the selective washing process provided by the invention, the tin content in the desulfurization flotation froth can be obviously reduced, namely the tin content in the sulfur concentrate is effectively reduced, wherein the recovery rate of tin element in the sulfur concentrate is reduced to below 2.65%, and the recovery rate of tin element in the sulfur concentrate is only 1.27%, thereby not only effectively reducing the tin resource loss, but also improving the quality of the sulfide ore, reducing the subsequent process flow and reducing the subsequent treatment cost of the sulfide ore.
While the invention has been illustrated and described with reference to specific embodiments, it is to be understood that the above embodiments are merely illustrative of the technical aspects of the invention and not restrictive thereof; those of ordinary skill in the art will appreciate that: modifications may be made to the technical solutions described in the foregoing embodiments, or equivalents may be substituted for some or all of the technical features thereof, without departing from the spirit and scope of the present invention; such modifications and substitutions do not depart from the spirit of the corresponding technical solutions; it is therefore intended to cover in the appended claims all such alternatives and modifications as fall within the scope of the invention.
Claims (8)
1. A method for reducing tin content in desulfurization flotation froth, comprising the steps of:
grinding the gravity tailings obtained through gravity separation to enable the particle size of particles with the granularity of less than 0.074mm to account for 70% -85%, so as to obtain a ground mineral material; wherein the mass fraction of tin element in the gravity tailings is 0.6% -0.9%, and the mass fraction of sulfur element is 5.9% -6.9%;
Removing particles with the granularity lower than 0.01-0.02 mm in the ore grinding material, adding a first regulator and a second regulator into the ore grinding material, and regulating the pH value of the mixed material to 6-8 to obtain a material to be floated; the first regulator comprises at least one of water glass and sodium pyrophosphate; the second regulator comprises at least one of sodium carboxymethyl cellulose and sodium dodecyl sulfate;
Mixing the material to be floated with a sulfide ore flotation collector and a foaming agent, and carrying out primary flotation roughing through a flotation machine to obtain roughing concentrate and roughing tailings;
The roughing tailings are subjected to three scavenging by the flotation machine, and scavenging concentrate obtained by the three scavenging is sequentially returned to the upper working procedure to form circulation;
Performing three blank concentration on the rougher concentrate through a cyclone-static flotation column to obtain sulfur concentrate and sulfur-containing tin middlings, and mixing the sulfur-containing tin middlings with the tin-containing tailings obtained by three scavenging for later use;
The mass of the first regulator added into each ton of the ore grinding material is 800-1000 g; the mass of the second regulator added into each ton of the ore grinding material is 1200-1800g;
the sulphide ore flotation collector comprises the following components in percentage by mass: 1-2 of butyl xanthate and amyl xanthate;
the circulation pressure of the cyclone-static flotation column is 0.15-0.22 mpa, the air charging amount is 1200-4000L/h, and the thickness of a foam layer is 5-15 cm;
the mass fraction of tin element in the sulfur concentrate is less than or equal to 0.25%; the recovery rate of tin element in the sulfur concentrate is less than or equal to 2.65 percent.
2. The method for reducing the tin content in the desulfurization flotation froth according to claim 1, wherein the mixed material is stirred for 5 to 10 minutes after the pH of the mixed material is adjusted to 6 to 8.
3. The method for reducing the tin content in the desulfurization flotation froth according to claim 1, wherein the mass of the sulfide ore flotation collector added per ton of the material to be floated in the primary flotation rougher is 50 to 400g.
4. The method of reducing the tin content of a desulphurised flotation froth according to claim 1, comprising at least one of the following features (1) to (2):
(1) The foaming agent comprises at least one of terpineol and alkyl sulfonic acid;
(2) In the primary flotation roughing process, the mass of the foaming agent added into each ton of the material to be subjected to flotation is 10-60 g.
5. The method for reducing the tin content in the desulfurization flotation froth according to claim 1, wherein the mass of the sulfide ore flotation collector added in each ton of the rougher tailings is 50-400 g in the first scavenging and the second scavenging of the three scavenging processes;
And/or in the first scavenging and the second scavenging in the three scavenging processes, the mass of the foaming agent added into each ton of roughing tailings is 10-60 g.
6. The method for reducing the tin content in the desulfurization flotation froth according to claim 1, wherein in three blank refining steps, the mass of the sulfide ore flotation collector added to each ton of the rougher concentrate is 30-100 g in each blank refining process.
7. The method for reducing the tin content in the desulfurization flotation froth according to claim 1, wherein particles less than 0.01 to 0.02mm in the mill feed are removed by a cyclone;
The ore feeding pressure of the cyclone is 0.05-0.15 mpa.
8. Use of the method for reducing tin content in desulphurised flotation froth according to any of claims 1 to 7 for the recovery of cassiterite.
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