CN116422457A - Method for recycling fine-grained cassiterite - Google Patents
Method for recycling fine-grained cassiterite Download PDFInfo
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- CN116422457A CN116422457A CN202310086467.1A CN202310086467A CN116422457A CN 116422457 A CN116422457 A CN 116422457A CN 202310086467 A CN202310086467 A CN 202310086467A CN 116422457 A CN116422457 A CN 116422457A
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- sand
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- cassiterite
- tin
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- XOLBLPGZBRYERU-UHFFFAOYSA-N tin dioxide Chemical compound O=[Sn]=O XOLBLPGZBRYERU-UHFFFAOYSA-N 0.000 title claims abstract description 78
- 238000000034 method Methods 0.000 title claims abstract description 37
- 238000004064 recycling Methods 0.000 title claims abstract description 9
- 239000004576 sand Substances 0.000 claims abstract description 83
- 239000012141 concentrate Substances 0.000 claims abstract description 51
- ATJFFYVFTNAWJD-UHFFFAOYSA-N Tin Chemical compound [Sn] ATJFFYVFTNAWJD-UHFFFAOYSA-N 0.000 claims abstract description 45
- 238000007885 magnetic separation Methods 0.000 claims abstract description 34
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims abstract description 32
- 238000011084 recovery Methods 0.000 claims abstract description 12
- 238000004519 manufacturing process Methods 0.000 claims abstract description 10
- 238000004062 sedimentation Methods 0.000 claims abstract description 8
- 239000002002 slurry Substances 0.000 claims abstract description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 5
- 238000005188 flotation Methods 0.000 claims description 53
- 230000008719 thickening Effects 0.000 claims description 31
- 238000004537 pulping Methods 0.000 claims description 10
- TUZCOAQWCRRVIP-UHFFFAOYSA-N butoxymethanedithioic acid Chemical compound CCCCOC(S)=S TUZCOAQWCRRVIP-UHFFFAOYSA-N 0.000 claims description 7
- 239000003153 chemical reaction reagent Substances 0.000 claims description 7
- 229910000365 copper sulfate Inorganic materials 0.000 claims description 7
- ARUVKPQLZAKDPS-UHFFFAOYSA-L copper(II) sulfate Chemical compound [Cu+2].[O-][S+2]([O-])([O-])[O-] ARUVKPQLZAKDPS-UHFFFAOYSA-L 0.000 claims description 7
- 239000002245 particle Substances 0.000 claims 5
- 230000008569 process Effects 0.000 abstract description 11
- 208000005156 Dehydration Diseases 0.000 abstract description 8
- 230000018044 dehydration Effects 0.000 abstract description 8
- 238000006297 dehydration reaction Methods 0.000 abstract description 8
- 238000007667 floating Methods 0.000 abstract description 4
- 230000005484 gravity Effects 0.000 abstract description 4
- 238000000926 separation method Methods 0.000 abstract description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 abstract description 2
- 239000011593 sulfur Substances 0.000 abstract description 2
- 229910052717 sulfur Inorganic materials 0.000 abstract description 2
- 238000010835 comparative analysis Methods 0.000 description 3
- 238000003756 stirring Methods 0.000 description 3
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000010419 fine particle Substances 0.000 description 2
- 229910052500 inorganic mineral Inorganic materials 0.000 description 2
- 239000011707 mineral Substances 0.000 description 2
- 239000011701 zinc Substances 0.000 description 2
- 229910052725 zinc Inorganic materials 0.000 description 2
- 229910021532 Calcite Inorganic materials 0.000 description 1
- 229910052964 arsenopyrite Inorganic materials 0.000 description 1
- MJLGNAGLHAQFHV-UHFFFAOYSA-N arsenopyrite Chemical compound [S-2].[Fe+3].[As-] MJLGNAGLHAQFHV-UHFFFAOYSA-N 0.000 description 1
- 229910052951 chalcopyrite Inorganic materials 0.000 description 1
- DVRDHUBQLOKMHZ-UHFFFAOYSA-N chalcopyrite Chemical compound [S-2].[S-2].[Fe+2].[Cu+2] DVRDHUBQLOKMHZ-UHFFFAOYSA-N 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000008396 flotation agent Substances 0.000 description 1
- 229910052949 galena Inorganic materials 0.000 description 1
- 229910052973 jamesonite Inorganic materials 0.000 description 1
- XCAUINMIESBTBL-UHFFFAOYSA-N lead(ii) sulfide Chemical compound [Pb]=S XCAUINMIESBTBL-UHFFFAOYSA-N 0.000 description 1
- -1 marmatite Inorganic materials 0.000 description 1
- 229910052976 metal sulfide Inorganic materials 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052683 pyrite Inorganic materials 0.000 description 1
- 239000011028 pyrite Substances 0.000 description 1
- NIFIFKQPDTWWGU-UHFFFAOYSA-N pyrite Chemical compound [Fe+2].[S-][S-] NIFIFKQPDTWWGU-UHFFFAOYSA-N 0.000 description 1
- 229910052952 pyrrhotite Inorganic materials 0.000 description 1
- 239000010453 quartz Substances 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- 229910052950 sphalerite Inorganic materials 0.000 description 1
- 229910052969 tetrahedrite Inorganic materials 0.000 description 1
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03B—SEPARATING SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS
- B03B7/00—Combinations of wet processes or apparatus with other processes or apparatus, e.g. for dressing ores or garbage
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03B—SEPARATING SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS
- B03B9/00—General arrangement of separating plant, e.g. flow sheets
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C—MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C1/00—Magnetic separation
- B03C1/02—Magnetic separation acting directly on the substance being separated
- B03C1/30—Combinations with other devices, not otherwise provided for
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- Manufacture And Refinement Of Metals (AREA)
Abstract
The method for recycling fine-grained cassiterite comprises the steps of firstly collecting overflow water of a production line, entering a dense pond for sedimentation, entering a dehydration bucket for desliming after sand setting of the dense pond is obtained, obtaining primary dehydration bucket for sand setting, then mixing slurry, performing sulphide ore floatation, desliming by using a cyclone after obtaining sulphide ore floatation tailings, entering the dehydration bucket for secondary desliming after sand setting of the cyclone, mixing slurry after sand setting of the secondary dehydration bucket, performing floatation, obtaining floatation concentrate, performing magnetic separation, entering a shaking table for reselection after obtaining magnetic separation tailings, and obtaining the shaking table cassiterite concentrate with the raw ore tin recovery rate of 5-7% and the tin grade of more than 46%. The method adopts a combined process of desliming, sulfur floating, desliming, tin floating, magnetic separation and gravity separation to recycle the fine-grained cassiterite, and has high cassiterite recovery rate and stable product quality.
Description
Technical Field
The invention belongs to the technical field of fine-particle-level cassiterite ore dressing recovery, and particularly relates to a method for recovering fine-particle cassiterite.
Background
Wujin (Fine mud cassiterite flotation Process research, university of Shanghai second Industrial university, 2000 (2), 66-72) on the fine mud cassiterite of car and river concentrating mills, which is a classified overflow of twice gravity tailings. Because the mud content in flotation ore feeding is larger, the two process flows of desliming, tin flotation and desulfurization, desliming and tin flotation are compared aiming at the fine mud cassiterite, and the latter flow is more economic and reasonable and the concentrate quality is higher. However, the process also adopts a single flotation process for the flotation of cassiterite, and has a relatively large dependence on flotation agents.
Because of the low efficiency of reselection to fine-grained cassiterite, the direction of research has focused mainly on single flotation technology. Although some of the processes adopt pretreatment before cassiterite separation or combined process flows, the problems of high flotation cost or poor rationality are not solved.
Disclosure of Invention
Aiming at the problems of single flotation technology, high flotation cost or poor rationality in the prior art, the invention provides a method for recycling fine-grained cassiterite, and the method has stable quality and high recycling rate of tin concentrate. The specific scheme is as follows:
the method for recycling fine-grain cassiterite comprises the steps of firstly collecting overflow water of a production line, entering a thickening tank for sedimentation, entering a dewatering hopper for desliming after sand setting of the thickening tank is obtained, obtaining primary dewatering hopper for sand setting, then mixing slurry, and carrying out cyclone desliming after sulphide ore flotation tailings are obtained, entering a dewatering hopper for secondary desliming after sand setting of the cyclone is obtained, mixing slurry and carrying out flotation after sand setting of the secondary dewatering hopper, obtaining flotation concentrate, carrying out magnetic separation after obtaining magnetic separation tailings, entering a shaking table for gravity separation, and obtaining shaking table cassiterite concentrate with a raw ore tin recovery rate of 5-7% and a tin grade of 46%, wherein the method comprises the following specific steps:
(1) Collecting overflow water of each operation point of the production line, entering a thickening tank with the diameter of 30 meters for sedimentation to obtain thickening tank sand and thickening tank overflow, entering the thickening tank sand into a dewatering hopper for desliming to obtain primary dewatering hopper sand and primary dewatering hopper overflow, and returning the primary dewatering hopper overflow to the thickening tank with the diameter of 30 meters to form closed circulation;
(2) Setting sand and pulping the primary dewatering hopper obtained in the step (1) until the pulp concentration is 40-48%, and sequentially adding copper sulfate, butyl xanthate and No. 2 oil to carry out sulphide ore floatation to obtain sulphide ore concentrate and sulphide ore tailings;
(3) Desliming the sulfide ore tailings obtained in the step (2) by using a cyclone to obtain cyclone overflow and cyclone sand setting, and desliming the cyclone sand setting again by using a dewatering bucket to obtain secondary dewatering bucket sand setting and secondary dewatering bucket overflow;
(4) Setting sand and pulping the secondary dewatering hopper in the step (3) until the pulp concentration is 25-35%, sequentially adding a flotation reagent BY-9 of 120-190 g/t and No. 2 oil of 20-60 g/t, and carrying out flotation to obtain flotation concentrate and flotation tailings;
(5) Carrying out magnetic separation on the flotation concentrate obtained in the step (4) under the condition that the magnetic field strength is 250mT, so as to obtain magnetic separation concentrate and magnetic separation tailings;
(6) And (3) separating the magnetic separation tailings obtained in the step (5) into a shaking table to obtain shaking table concentrate, shaking table middlings and shaking table tailings, taking the shaking table concentrate as a tin product to go out of a warehouse, and returning the shaking table middlings to a cyclone to operate so as to form closed circulation.
Further, the grain size of the dense pool sand in the step (1) is more than 85 percent in terms of mass percent, the grain size is 40-45 percent in terms of-0.074 mm, the grain size of the primary dewatering hopper sand setting is 35-40 percent in terms of-0.010 mm, and the tin grade of the primary dewatering hopper sand setting ore is 0.21-0.29 percent.
Further, in the step (2), copper sulfate is 20-60 g/t, butyl xanthate is 20-50 g/t, no. 2 oil is 30-60 g/t, and the sulfide ore tailings contain 0.27-0.32% of tin.
Further, the cyclone sand setting in the step (3) accounts for 18-23% in terms of mass of granularity of-0.010 mm, the secondary dehydration bucket sand setting accounts for 14-18% in terms of mass of granularity of-0.010 mm, and the secondary dehydration bucket sand setting grade is 0.33-0.35%.
Further, the flotation reagent BY-9 in the step (4) is 120-190 g/t, the No. 2 oil is 20-60 g/t, and the flotation concentrate contains 3.71-4.5% of tin.
Further, the magnetic separation tailings in the step (5) contain 3.96-5.1% of tin.
THE ADVANTAGES OF THE PRESENT INVENTION
(1) The method for recycling the fine-grain cassiterite carries out desliming operation of a dense pond with the phi of 30 meters and desliming operation of a dehydration bucket before desulfurization flotation, removes ore slimes with the diameter of less than-0.010 mm, reduces the interference of the ore slimes on the floatation of sulphide ores, and creates a good environment for the floatation of sulphide ores.
(2) Before the cassiterite flotation, the method for recycling the fine-grain cassiterite carries out the desliming operation of the phi 250 cyclone and the desliming operation of the dehydration bucket, removes ore slimes below-0.010 mm, reduces the interference of the ore slimes on the cassiterite flotation, and provides a good ore pulp environment for the cassiterite flotation.
(3) Before the method for recovering the fine-grain cassiterite is carried out by the operation of the shaking table, the magnetic separation operation is carried out to remove the magnetic minerals in the ore, and good selection conditions are provided for the shaking table selection of the cassiterite.
(4) The method for recovering the fine-grain cassiterite adopts a combined process of desliming, sulfur floating, desliming, tin floating, magnetic separation and gravity separation to recover the fine-grain cassiterite, and compared with the original ore, the method has the advantages of 5-7% of tin recovery rate, more than 46% of tin grade, high cassiterite recovery rate and stable product quality.
Drawings
FIG. 1 is a process flow diagram of the present invention.
Detailed Description
It should be noted that the following description is not intended to limit the scope of the invention.
Example 1
The main mineral composition of the multi-metal sulfide ore of cassiterite in Guangxi province of China is cassiterite, marmatite, jamesonite, pyrite, pyrrhotite, arsenopyrite, galena, sphalerite, chalcopyrite, tetrahedrite, quartz, calcite and the like.
As shown in fig. 1, the specific steps of the method for recovering fine-grained cassiterite of this example 1 are as follows:
(1) Collecting overflow of each operation point of the production line, and entering a thickening tank with the diameter of 30 m for sedimentation to obtain thickening tank sand and overflow of the thickening tank, wherein the thickening tank sand accounts for 91.7% with the granularity of-0.074 mm and 42% with the granularity of-0.010 mm by mass; the sand setting of the thickening tank enters a dewatering hopper to be desliming again, so as to obtain sand setting of the primary dewatering hopper and overflow of the primary dewatering hopper, wherein the granularity of the sand setting of the primary dewatering hopper is-0.010 mm accounting for 35% by mass, and the overflow of the primary dewatering hopper returns to the thickening tank with the diameter of 30 m to form closed circulation, wherein the tin grade of the sand setting ore of the primary dewatering hopper is 0.21%;
(2) Setting sand and pulping the primary dewatering hopper obtained in the step (1) until the pulp concentration is 42.3%, and sequentially adding 25g/t of copper sulfate, 32g/t of butyl xanthate and 35g/t of No. 2 oil for sulphide ore floatation to obtain sulphide ore concentrate and sulphide ore tailings, wherein the sulphide ore tailings contain 0.27% of tin;
(3) Feeding the flotation sulfide ore tailings obtained in the step (2) into a phi 250 cyclone with the model number for desliming to obtain cyclone sand setting and cyclone overflow, wherein the cyclone sand setting accounts for 20% with the mass percent of-0.010 mm; the cyclone sand setting enters a dewatering hopper to be desliming again, so as to obtain secondary dewatering hopper sand setting and overflow of the secondary dewatering hopper, wherein the secondary dewatering hopper sand setting accounts for 17% in terms of mass percent of granularity of-0.010 mm, and the grade of the secondary dewatering hopper sand setting is 0.33%;
(4) Setting sand and pulping the secondary dewatering hopper obtained in the step (3) until the concentration of ore pulp is 26.3%, sequentially adding a flotation reagent BY-9 of 124g/t and No. 2 oil of 36g/t, stirring, and performing flotation to obtain flotation concentrate and flotation tailings, wherein the flotation concentrate contains 3.71% of tin;
(5) Carrying out magnetic separation on the flotation concentrate obtained in the step (4) under the condition that the magnetic field intensity is 250mT to obtain magnetic separation concentrate and magnetic separation tailings, wherein the tin content of the magnetic separation tailings is 3.96%;
(6) And (3) separating the magnetic separation tailings obtained in the step (5) into a shaking table to obtain shaking table concentrate, shaking table middlings and shaking table tailings, taking the shaking table concentrate as a tin product, leaving the shaking table concentrate as a warehouse, wherein the shaking table concentrate contains 46.81% of tin, and the recovery rate of raw ore is 5.32%, and the shaking table middlings are returned to a phi 250 cyclone to operate to form closed circulation.
Example 2
As shown in fig. 1, the ore properties of example 2 are the same as those of example 1, and the specific steps of the method for recovering fine-grained cassiterite of this example 2 are as follows:
(1) Collecting overflow of each operation point of the production line, and entering a thickening tank with the diameter of 30 m for sedimentation to obtain thickening tank sand and overflow of the thickening tank, wherein the thickening tank sand accounts for 86.5% with the granularity of-0.074 mm and 45% with the granularity of-0.010 mm by mass; the sand setting of the thickening tank enters a dewatering hopper to be desliming again, so as to obtain sand setting of the primary dewatering hopper and overflow of the primary dewatering hopper, wherein the granularity of the sand setting of the primary dewatering hopper is 40% in terms of mass percent of-0.010 mm, and the overflow of the primary dewatering hopper returns to the thickening tank with phi of 30 m to form closed circulation, wherein the tin grade of the sand setting ore of the primary dewatering hopper is 0.29%;
(2) Setting sand and pulping the primary dewatering hopper obtained in the step (1) until the pulp concentration is 48%, sequentially adding 41g/t of copper sulfate, 50g/t of butyl xanthate and 58g/t of No. 2 oil for sulphide ore floatation to obtain sulphide ore concentrate and sulphide ore tailings, wherein the sulphide ore tailings contain 0.32% of tin;
(3) Feeding the flotation sulfide ore tailings obtained in the step (2) into a phi 250 cyclone for desliming to obtain cyclone sand setting and cyclone overflow, wherein the cyclone sand setting accounts for 23% with the mass percent of-0.010 mm; the cyclone sand setting enters a dewatering hopper to be desliming again, so as to obtain secondary dewatering hopper sand setting and overflow of the secondary dewatering hopper, wherein the secondary dewatering hopper sand setting accounts for 18% in terms of mass percent of granularity of-0.010 mm, and the grade of the secondary dewatering hopper sand setting is 0.35%;
(4) Setting sand and pulping the secondary dewatering hopper obtained in the step (3) until the concentration of ore pulp is 32%, sequentially adding a flotation reagent BY-9 of 180g/t and No. 2 oil of 60g/t, and carrying out flotation after stirring to obtain flotation concentrate and flotation tailings, wherein the flotation concentrate contains 4.5% of tin;
(5) Carrying out magnetic separation on the flotation concentrate obtained in the step (4) under the condition that the magnetic field intensity is 250mT to obtain magnetic separation concentrate and magnetic separation tailings, wherein the magnetic separation tailings contain 5.1% of tin;
(6) And (3) separating the magnetic separation tailings obtained in the step (5) into a shaking table to obtain shaking table concentrate, shaking table middlings and shaking table tailings, taking the shaking table concentrate as a tin product, leaving the shaking table concentrate as a warehouse, wherein the shaking table concentrate contains 48.21% of tin, and returning the shaking table middlings to the phi 250 cyclone to operate to form closed circulation for the raw ore recovery rate of 6.91%.
Example 3
As shown in fig. 1, the ore properties of this example 3 are the same as those of example 1, and the specific steps of the method for recovering fine-grained cassiterite of this example 3 are as follows:
(1) Collecting overflow of each operation point of the production line, and entering a thickening tank with the diameter of 30 m for sedimentation to obtain thickening tank sand and overflow of the thickening tank, wherein the mass of the thickening tank sand is-0.074 mm and 90.2%, and the mass of the thickening tank sand is-0.010 mm and 45%; the sand setting of the thickening tank enters a dewatering hopper to be desliming again, so as to obtain sand setting of the primary dewatering hopper and overflow of the primary dewatering hopper, wherein the sand setting of the primary dewatering hopper accounts for 41 percent in terms of mass percent with granularity of-0.010 mm, and the overflow of the primary dewatering hopper returns to the thickening tank with phi of 30 meters to form closed circulation, wherein the tin grade of the sand setting ore of the primary dewatering hopper is 0.27 percent;
(2) Setting sand and pulping the primary dewatering hopper obtained in the step (1) until the pulp concentration is 45.3%, sequentially adding 53g/t of copper sulfate, 39g/t of butyl xanthate and 45g/t of No. 2 oil for sulphide ore floatation to obtain sulphide ore concentrate and sulphide ore tailings, wherein the sulphide ore tailings contain 0.28% of tin;
(3) Feeding the flotation sulfide ore tailings obtained in the step (2) into a phi 250 cyclone for desliming to obtain cyclone sand setting and cyclone overflow, wherein the cyclone sand setting accounts for 20% with the mass percent of-0.010 mm; the cyclone sand setting enters a dewatering hopper to be desliming again, so as to obtain secondary dewatering hopper sand setting and overflow of the secondary dewatering hopper, wherein the secondary dewatering hopper sand setting accounts for 15% in terms of mass percent of-0.010 mm, and the grade of the secondary dewatering hopper sand setting is 0.34%;
(4) Setting sand and pulping the secondary dewatering hopper obtained in the step (3) until the concentration of ore pulp is 29%, sequentially adding a flotation reagent BY-9 of 170g/t and No. 2 oil of 46g/t, stirring, and performing flotation to obtain flotation concentrate and flotation tailings, wherein the flotation concentrate contains 4.21% of tin;
(5) Carrying out magnetic separation on the flotation concentrate obtained in the step (4) under the condition that the magnetic field intensity is 250mT to obtain magnetic separation concentrate and magnetic separation tailings, wherein the magnetic separation tailings contain 4.39% of tin;
(6) And (3) separating the magnetic separation tailings obtained in the step (5) into a shaking table to obtain shaking table concentrate, shaking table middlings and shaking table tailings, taking the shaking table concentrate as a tin product, leaving the shaking table concentrate as a warehouse, wherein the tin content in the shaking table concentrate is 49.54%, the recovery rate of raw ore is 6.37%, and the shaking table middlings are returned to the phi 250 cyclone to operate to form closed circulation.
The comparative analysis of lead and zinc production indexes of the process and the prior art are shown in Table 1.
TABLE 1 comparative analysis Table of lead and zinc production index of the process and the prior art
As can be seen from the comparative analysis of Table 1, the recovery rate of raw ore tin obtained by the method is 0.52-2.11% higher than that of the prior art, the grade of concentrate tin is 1.21-3.94% higher than that of the prior art, and the recovery rate of raw ore tin obtained by the method and the grade of concentrate tin are higher than that of the prior art.
In view of the foregoing, it is intended that the present invention should not be limited to the preferred embodiments of the present invention, but that all modifications, equivalents, and improvements made within the spirit and principles of the present invention be included within the scope of the present invention.
Claims (6)
1. The method for recycling fine-grain cassiterite is characterized in that overflow water of a production line is firstly collected and enters a dense pond for sedimentation, sand setting of the dense pond is obtained, then enters a dewatering hopper for desliming, primary dewatering hopper sand setting is obtained, slurry mixing is carried out, sulfide ore floatation is carried out, after sulfide ore floatation tailings are obtained, cyclone sand setting is obtained, secondary desliming is carried out, secondary dewatering hopper sand setting is obtained, slurry mixing is carried out, flotation concentrate is obtained, magnetic separation is carried out, and after magnetic separation tailings are obtained, shaking table cassiterite concentrate with a raw ore tin recovery rate of 5-7% and a tin grade of more than 46% is obtained, and the method comprises the following specific steps:
(1) Collecting overflow water of each operation point of the production line, entering a thickening tank with the diameter of 30 meters for sedimentation to obtain thickening tank sand and thickening tank overflow, entering the thickening tank sand into a dewatering hopper for desliming to obtain primary dewatering hopper sand and primary dewatering hopper overflow, and returning the primary dewatering hopper overflow to the thickening tank with the diameter of 30 meters to form closed circulation;
(2) Setting sand and pulping the primary dewatering hopper obtained in the step (1) until the pulp concentration is 40-48%, and sequentially adding copper sulfate, butyl xanthate and No. 2 oil to carry out sulphide ore floatation to obtain sulphide ore concentrate and sulphide ore tailings;
(3) Desliming the sulfide ore tailings obtained in the step (2) by using a cyclone to obtain cyclone overflow and cyclone sand setting, and desliming the cyclone sand setting again by using a dewatering bucket to obtain secondary dewatering bucket sand setting and secondary dewatering bucket overflow;
(4) Setting sand and pulping the secondary dewatering hopper in the step (3) until the pulp concentration is 25-35%, and sequentially adding a flotation reagent BY-9 and No. 2 oil for flotation to obtain flotation concentrate and flotation tailings;
(5) Carrying out magnetic separation on the flotation concentrate obtained in the step (4) under the condition that the magnetic field strength is 250mT, so as to obtain magnetic separation concentrate and magnetic separation tailings;
(6) And (3) separating the magnetic separation tailings obtained in the step (5) into a shaking table to obtain shaking table concentrate, shaking table middlings and shaking table tailings, taking the shaking table concentrate as a tin product to go out of a warehouse, and returning the shaking table middlings to a cyclone to operate so as to form closed circulation.
2. The method for recovering fine-grained cassiterite according to claim 1, wherein the dense pool sand in the step (1) has a particle size of-0.074 mm of 85% or more, a particle size of-0.010 mm of 40 to 45%, a primary dewatering hopper sand particle size of-0.010 mm of 35 to 40%, and a primary dewatering hopper sand ore tin grade of 0.21 to 0.29% by mass.
3. The method for recovering fine-grained cassiterite according to claim 1, wherein the copper sulfate in the step (2) is 20-60 g/t, butyl xanthate is 20-50 g/t, no. 2 oil is 30-60 g/t, and the sulfide ore tailings contain 0.27-0.32% of tin.
4. The method for recovering fine cassiterite according to claim 1, wherein the cyclone sand setting in the step (3) is 18-23% in particle size of-0.010 mm by mass, the secondary dewatering hopper sand setting is 14-18% in particle size of-0.010 mm by mass, and the secondary dewatering hopper sand setting grade is 0.33-0.35%.
5. A method for recovering fine-grained cassiterite according to claim 1, characterized in that the flotation reagent BY-9 in step (4) is 120-190 g/t, the number 2 oil is 20-60 g/t, and the flotation concentrate contains 3.71-4.5% tin.
6. A method for recovering fine-grained cassiterite according to claim 1, characterized in that the magnetic separation tailings in step (5) contain 3.96-5.1% tin.
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| CN202310086467.1A CN116422457A (en) | 2023-02-09 | 2023-02-09 | Method for recycling fine-grained cassiterite |
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| CN202310086467.1A CN116422457A (en) | 2023-02-09 | 2023-02-09 | Method for recycling fine-grained cassiterite |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN117583116A (en) * | 2024-01-18 | 2024-02-23 | 中国矿业大学(北京) | Method for recycling low-grade fine-grain cassiterite and application thereof |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117583116A (en) * | 2024-01-18 | 2024-02-23 | 中国矿业大学(北京) | Method for recycling low-grade fine-grain cassiterite and application thereof |
| CN117583116B (en) * | 2024-01-18 | 2024-04-05 | 中国矿业大学(北京) | Method for recycling low-grade fine-grain cassiterite and application thereof |
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