Method for obtaining cassiterite concentrate by utilizing tin polymetallic ore
Through the linkage of processes such as cyclone desludge, sulfur flotation, grading, reselecting and flocculation settlement, the problem of low recovery rate of fine-grained cassiterite is solved, which improves the recovery rate of cassiterite and reduces costs.
Patent Information
- Application Number
- CN202510682497.8
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- Filing Date
- 2025-05-26
- Publication Date
- 2025-07-08
AI Technical Summary
In the prior art, the recovery rate of fine-grained cassiterite is low, especially during the sorting process of tin polymetallic ore. The fine-grained cassiterite is easily lost in the ore mud, resulting in a decrease in the recovery rate.
A linkage process of cyclone desludge, sulfur flotation, grading, reselecting, flocculation and settlement and multiple flotations is adopted. Different ore separation processes are adopted for coarse particles and fine particles, and the full recovery of tin is achieved by optimizing the treatment process of fine particles.
It improves the recovery rate of cassiterite, reduces the dosage of drugs, and reduces costs, achieving comprehensive recycling of valuable elements.
Smart Images
Figure CN120268554A_ABST
Abstract
Description
Technical Field
[0001] The present invention relates to the technical field of ore dressing, and in particular, to a method for obtaining cassiterite concentrate from tin polymetallic ore. Background Art
[0002] Tin polymetallic ore refers to a composite ore deposit mainly composed of tin (Sn) and associated with other valuable metals (such as zinc, lead, copper, tungsten, indium, silver, bismuth, etc.). Low tin grade, fine dissemination size, and complex associated relationship are typical characteristics of such tin polymetallic ores, such as Dachang zinc-tin polymetallic ore in Guangxi and Dulong copper-zinc-tin polymetallic ore in Wenshan, Yunnan. Recovering cassiterite from tin polymetallic ore can increase the added value of products.
[0003] At present, gravity separation is still the main method for recovering cassiterite in industry, but it is found in practice that the recovery effect of gravity separation on fine-grained cassiterite with a particle size less than 0.028 mm is poor. During the separation process of tin polymetallic ore, due to the brittleness of cassiterite and the fact that the tin separation operation is usually set after the flotation of sulfide ore, over-crushing of cassiterite is very likely to occur, and cassiterite is easily lost in the slime or tailings in the form of fine particles. Research shows that the "gravity-flotation" combined process is the most promising method for recovering fine-grained cassiterite, but it is found in production practice that serious slime interference and complex pulp environment have always been the main problems faced in the recovery of fine-grained cassiterite. To reduce the influence of slime on the flotation of cassiterite, in practice, fine-grained slime is generally removed preferentially by gravity separation to partially enrich tin and obtain tin concentrate with relatively high grade. Centrifugal concentrators, hydrocyclones, vibrating conical surface concentrators, etc. are commonly used desliming and pre-concentration equipment, but it is often found that some fine-grained cassiterite is also easily lost in the slime during gravity separation desliming, resulting in a decrease in the recovery rate of cassiterite. Since the specific surface area of tin-containing slime is large, the specific surface energy is high, the properties are complex and it is difficult to settle and treat alone, directly classifying it into the main process fine slime system will deteriorate the feed properties of the fine slime system and is not conducive to the recovery of subsequent operations.
[0004] Therefore, there is an urgent need to improve the cassiterite collection process to increase the recovery rate of fine-grained cassiterite.
[0005] In view of this, the present invention is specifically proposed. Summary of the Invention
[0006] The purpose of the present invention is to provide a method for obtaining cassiterite concentrate from tin polymetallic ore, aiming to solve the problem of low recovery rate of fine-grained cassiterite.
[0007] The present invention is implemented as follows:
[0008] In a first aspect, the present invention provides a method for obtaining cassiterite concentrate from tin polymetallic ore, including:
[0009] Slurry preparation: Mix tin polymetallic ore and water to prepare slurry to obtain pulp;
[0010] Hydrocyclone desliming: The pulp is subjected to hydrocyclone classification to obtain a first overflow and a first sand deposit;
[0011] Sulphur flotation: The first sand deposit is mixed with sulphuric acid for pulp preparation, and then mixed with a first collector and a first frother for rough sulphur flotation to obtain sulphur concentrate and sulphur tailings;
[0012] Classification: The sulphur tailings are classified to obtain coarse particles and fine particles;
[0013] Gravity separation: The coarse particles are subjected to gravity separation to obtain cassiterite concentrate;
[0014] Flocculation sedimentation: The fine particles are subjected to flocculation sedimentation to obtain a second overflow and a second sand deposit; The second sand deposit is subjected to pulp preparation and then mixed with a second collector and a second frother for rough flotation to obtain sulphur flotation concentrate and sulphur flotation tailings;
[0015] Cassiterite flotation: The sulphur flotation tailings are subjected to pulp preparation and then mixed with a regulator, a third collector and a third frother for a first rough flotation to obtain a rough flotation concentrate and a rough flotation tailings; The rough flotation tailings are subjected to pulp preparation and then mixed with a fourth collector and a fourth frother for a second scavenging flotation to obtain a scavenging concentrate and a scavenging tailings. The scavenging concentrate is returned to the first rough flotation operation to form a closed circuit. The rough flotation concentrate is subjected to pulp preparation and then subjected to at least one blank cleaning to obtain cassiterite flotation concentrate.
[0016] In an alternative embodiment, during the sulphur flotation process, the first collector used is a mixture of sodium dialkyl sulphate and coconut oil alkylamine acetate, and the mass ratio of sodium dialkyl sulphate to coconut oil alkylamine acetate is 1:(3 - 6);
[0017] And / or, the addition amount of the first collector is 50 g / t - 100 g / t;
[0018] And / or, the pH of the pulp preparation with sulphuric acid added is 6 - 7;
[0019] And / or, the first frother is selected from at least one of pine oil and sodium dodecyl sulphate;
[0020] And / or, the addition amount of the first frother is 10 g / t - 60 g / t.
[0021] In an alternative embodiment, the particle size of the coarse particles is greater than or equal to the critical value, and the particle size of the fine particles is less than the critical value. The critical value is 0.070 mm - 0.080 mm;
[0022] And / or, the coarse particles are subjected to primary gravity separation using a spiral chute to obtain primary gravity separation coarse concentrate and primary gravity separation tailings; the primary gravity separation coarse concentrate is subjected to secondary gravity separation using a shaking table to obtain secondary gravity separation cassiterite concentrate and secondary gravity separation tailings, and the secondary gravity separation tailings are mixed with the fine particles for flocculation sedimentation.
[0023] In an alternative embodiment, the flocculant used in the flocculation sedimentation is obtained by reversible addition-fragmentation chain transfer polymerization from dimethylaminoethyl methacrylate, methyl methacrylate, and 7-acryloyloxy-4-methylcoumarin as raw materials;
[0024] And / or, the addition amount of the flocculant used in the flocculation sedimentation is 50 g / t - 300 g / t;
[0025] And / or, the flocculation sedimentation is carried out in an inclined plate sedimentation tank.
[0026] In an alternative embodiment, the mass fraction of the second sand sediment after pulp adjustment is 25% - 33%;
[0027] And / or, the second collector is selected from at least one of butyl xanthate and butylamine black medicine; the addition amount of the second collector is 100 g / t - 200 g / t;
[0028] And / or, the second frother is selected from at least one of pine oil and sodium dodecyl sulfate; the addition amount of the second frother is 20 g / t - 100 g / t.
[0029] In an alternative embodiment, the mass fraction of the sulfur flotation tailings after pulp adjustment is 20% - 25%;
[0030] And / or, the regulator is selected from at least one of lead nitrate and lead acetate; the addition amount of the regulator is 50 g / t - 3000 g / t;
[0031] And / or, the third collector is selected from at least one of ammonium salicylhydroxamate and benzohydroxamic acid; the addition amount of the third collector is 1000 g / t - 2000 g / t;
[0032] And / or, the third frother is selected from at least one of pine oil and sodium dodecyl sulfate; the addition amount of the third frother is 40 g / t - 110 g / t.
[0033] In an alternative embodiment, the mass fraction of the flotation rougher tailings after pulp adjustment is 18% - 24%;
[0034] And / or, the fourth collector is selected from at least one of ammonium salicylhydroxamate and tolylarsonic acid; the addition amount of the fourth collector is 300 g / t - 1200 g / t;
[0035] And / or, the fourth foaming agent is selected from at least one of pine oil and methyl isobutyl carbinol; the addition amount of the fourth foaming agent is 0 g / t - 50 g / t.
[0036] In an alternative embodiment, the mass fraction of the rougher concentrate after pulp adjustment is 5% - 10%;
[0037] And / or, the blank cleaning is performed three times.
[0038] In an alternative embodiment, during the cassiterite flotation process, the middlings at each stage of flotation are returned to the previous operation to form a closed circuit.
[0039] In an alternative embodiment, the mass fraction of the pulp obtained after mixing the tin-polymetallic ore and water for pulp adjustment is 30% - 40%.
[0040] The present invention has the following beneficial effects: The present invention first performs hydrocyclone desliming and sulfur flotation to obtain a sulfur concentrate product, and then adopts a combined process of classification - flotation - gravity separation - flocculation - flotation for the sulfur tailings. Different ore separation processes are used for coarse particles and fine particles. By optimizing the treatment process of fine particles, tin is fully recovered, realizing the comprehensive recovery of valuable elements. The process provided by the present invention can reduce the dosage of reagents under the same process conditions, with a higher cassiterite recovery rate and lower cost. BRIEF DESCRIPTION OF THE DRAWINGS
[0041] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the following will briefly introduce the drawings required for the embodiments. It should be understood that the following drawings only show some embodiments of the present invention, and therefore should not be regarded as limiting the scope. For those of ordinary skill in the art, other related drawings can be obtained based on these drawings without creative efforts.
[0042] Figure 1 It is a process flow diagram provided for the embodiments of the present invention. DETAILED DESCRIPTION OF THE EMBODIMENTS
[0043] To make the objectives, technical solutions, and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below. Those not specified in the embodiments are carried out according to conventional conditions or conditions recommended by the manufacturer. The reagents or instruments not specified by the manufacturer are all conventional products that can be obtained through commercial purchase.
[0044] An embodiment of the present invention provides a method for obtaining cassiterite concentrate from tin-polymetallic ore, as Figure 1 shown, the steps are as follows:
[0045] S1. Pulp adjustment
[0046] Mix the tin polymetallic ore with water to make pulp, and mix evenly by stirring or other means to obtain pulp with a certain concentration.
[0047] In some embodiments, the mass fraction of the pulp obtained after mixing the tin polymetallic ore with water is 30%-40%, such as 30%, 32%, 35%, 38%, 40%, etc. Specifically, by controlling the amount of water added, the mass fraction of the pulp meets the requirements to facilitate the subsequent cyclone desliming operation.
[0048] S2. Cyclone desliming
[0049] Perform hydrocyclone classification on the pulp, the fine particles overflow, and the coarse particles are enriched at the bottom to obtain the first overflow and the first sand deposit (i.e., underflow). The first overflow basically does not contain valuable metals such as tin and is output as waste.
[0050] S3. Sulfur flotation
[0051] Mix the first sand deposit with sulfuric acid to make pulp, control the pH value to be 6-7, and then mix with the first collector and the first frother for rough sulfur flotation to obtain sulfur concentrate and sulfur tailings. Specifically, rough sulfur flotation is a process of separating and enriching sulfide minerals by foam flotation method. Under the action of the first collector and the first frother, sulfur minerals can be separated, and sulfur concentrate products such as pyrite can be output. Using sulfuric acid to make pulp acidic can better enrich sulfide minerals. Specifically, the pH value after mixing with sulfuric acid can be 6.0, 6.3, 6.5, 6.8, 7.0, etc.
[0052] In some embodiments, during the sulfur flotation process, the first collector used is a mixture of sodium dialkyl sulfate and coconut oil alkylamine acetate, and the mass ratio of sodium dialkyl sulfate to coconut oil alkylamine acetate is 1:(3-6), such as 1:3, 1:4, 1:5, 1:6, etc. By adjusting the type of the first collector, the sulfur separation effect is improved, and sulfur minerals are better enriched in the sulfur concentrate. The addition amount of the first collector is 50 g / t - 100 g / t, such as 50 g / t, 60 g / t, 70 g / t, 80 g / t, 90 g / t, 100 g / t, etc.
[0053] In some embodiments, the first frother is selected from at least one of pine oil and sodium dodecyl sulfate, and the first frother can be any one or several of the above. The addition amount of the first frother is 10 g / t - 60 g / t, such as 10 g / t, 20 g / t, 30 g / t, 40 g / t, 50 g / t, 60 g / t, etc.
[0054] S4. Classification
[0055] The sulfur tailings are classified to obtain coarse particles and fine particles, so as to enrich tin according to the different characteristics of the coarse particles and fine particles.
[0056] In some embodiments, the particle size of the coarse particles is greater than or equal to the critical value, and the particle size of the fine particles is less than the critical value. The critical value is 0.070 mm - 0.080 mm, such as 0.070 mm, 0.072 mm, 0.074 mm, 0.076 mm, 0.078 mm, 0.080 mm, etc.
[0057] S5. Gravity separation
[0058] The coarse particles obtained in S4 are used to obtain cassiterite concentrate by gravity separation. The coarse particles have a relatively large density, and tin can be enriched by gravity separation.
[0059] In some embodiments, the coarse particles are subjected to primary gravity separation using a spiral chute to obtain primary gravity separation rough concentrate and primary gravity separation tailings; the primary gravity separation rough concentrate is subjected to secondary gravity separation using a shaking table to obtain secondary gravity separation cassiterite concentrate and secondary gravity separation tailings, and the secondary gravity separation tailings are mixed with the fine particles for flocculation sedimentation. Through the two-stage gravity separation process, the purity of the cassiterite concentrate is improved.
[0060] In the preferred embodiments, both the primary gravity separation and the secondary gravity separation are carried out by shaking table gravity separation to improve the enrichment effect of tin.
[0061] S6. Flocculation sedimentation
[0062] The fine particles are subjected to flocculation sedimentation to obtain a second overflow (i.e., recycled water) and a second sediment; the second sediment is slurried and then mixed with a second collector and a second frother for rough flotation to obtain sulfur flotation concentrate (i.e., sulfur concentrate) and sulfur flotation tailings. After the fine particles are mixed with water, a flocculant, etc. and then subjected to flocculation sedimentation, metals such as tin are deposited, and fine mud impurities, etc. enter the second overflow and are removed. The second sediment is subjected to sulfur flotation to output sulfur flotation concentrate products, and at the same time, the sulfur flotation tailings enter the next stage.
[0063] In some embodiments, the flocculant used in the flocculation sedimentation is prepared from dimethylaminoethyl methacrylate, methyl methacrylate, and 7-acryloyloxy-4-methylcoumarin through reversible addition-fragmentation chain transfer polymerization. The synthesized coumarin-containing amphiphilic block copolymer can be used as a novel pH- and light-responsive flocculant. Using the flocculant provided by the embodiments of the present invention can further improve the flocculation effect and the enrichment effect of sulfur, tin, etc. The addition amount of the flocculant used in the flocculation sedimentation is 50 g / t - 300 g / t, such as 50 g / t, 80 g / t, 100 g / t, 150 g / t, 200 g / t, 250 g / t, 300 g / t, etc. Within this dosage range, the recovery rate of sulfur can be improved. The flocculation sedimentation can be carried out in an inclined plate sedimentation tank, but is not limited thereto.
[0064] In some embodiments, the mass fraction after the second desilting and pulp conditioning is 25%-33%, such as 25%, 28%, 30%, 33%, etc. The second collector is selected from at least one of butyl xanthate and ammonium butyl dithiophosphate, and the second collector can be any one or several of the above; the addition amount of the second collector is 100 g / t - 200 g / t, such as 100 g / t, 130 g / t, 150 g / t, 180 g / t, 200 g / t, etc.
[0065] Further, the second frother is selected from at least one of pine oil and sodium dodecyl sulfate, and the second frother can be any one or several of the above; the addition amount of the second frother is 20 g / t - 100 g / t, such as 20 g / t, 50 g / t, 80 g / t, 100 g / t, etc.
[0066] S7. Cassiterite flotation
[0067] The sulfur flotation tailings are pulp-conditioned and then mixed with a regulator, a third collector, and a third frother for a primary flotation roughing (i.e., roughing of fine cassiterite) to obtain a flotation roughing concentrate and a flotation roughing tailings; the flotation roughing tailings are pulp-conditioned and then mixed with a fourth collector and a fourth frother for a secondary flotation scavenging (i.e., scavenging I and scavenging II) to obtain a scavenging concentrate and a scavenging tailings. The scavenging concentrate is returned to the primary flotation roughing operation to form a closed circuit. The flotation roughing concentrate is pulp-conditioned and then subjected to at least one blank cleaning to obtain a cassiterite flotation concentrate. By means of primary flotation roughing, secondary flotation scavenging, blank cleaning, etc., the recovery rate of tin can be significantly improved, and at the same time, the purity of the cassiterite flotation concentrate can be increased.
[0068] In some embodiments, the mass fraction after the sulfur flotation tailings are pulp-conditioned is 20%-25%, such as 20%, 21%, 22%, 23%, 24%, 25%, etc. The regulator is selected from at least one of lead nitrate and lead acetate, and the regulator can be any one or several of the above; the addition amount of the regulator is 50 g / t - 3000 g / t, such as 50 g / t, 100 g / t, 500 g / t, 1000 g / t, 1500 g / t, 2000 g / t, 2500 g / t, 3000 g / t, etc.
[0069] Further, the third collector is selected from at least one of ammonium salicylhydroxamate and benzohydroxamic acid, and the third collector can be any one or several of the above; the addition amount of the third collector is 1000 g / t - 2000 g / t, such as 1000 g / t, 1300 g / t, 1500 g / t, 1800 g / t, 2000 g / t, etc. The third foaming agent is selected from at least one of pine oil and sodium dodecyl sulfate, and the third foaming agent can be any one or several of the above; the addition amount of the third foaming agent is 40 g / t - 110 g / t, such as 40 g / t, 60 g / t, 80 g / t, 100 g / t, 110 g / t, etc.
[0070] Further, the mass fraction of the rougher flotation tailings after pulp adjustment is 18% - 24%, such as 18%, 20%, 22%, 24%, etc. The fourth collector is selected from at least one of ammonium salicylhydroxamate and arsonic acid, and the fourth collector can be any one or several of the above; the addition amount of the fourth collector is 300 g / t - 1200 g / t, such as 300 g / t, 500 g / t, 800 g / t, 1000 g / t, 1200 g / t, etc. The fourth foaming agent is selected from at least one of pine oil and methyl isobutyl carbinol, and the fourth foaming agent can be any one or several of the above; the addition amount of the fourth foaming agent is 0 g / t - 50 g / t, such as 0 g / t, 5 g / t, 10 g / t, 20 g / t, 30 g / t, 40 g / t, 50 g / t, etc.
[0071] Further, the mass fraction of the rougher flotation concentrate after pulp adjustment is 5% - 10%, such as 5%, 6%, 7%, 8%, 9%, 10%, etc. The number of blank cleaning operations can be three (i.e., cleaning I, cleaning II, and cleaning III), and blank cleaning means cleaning without adding a collector and a foaming agent.
[0072] In some embodiments, during the cassiterite flotation process, the intermediate concentrates from each stage of flotation are returned to the previous operation to form a closed circuit to improve the recovery rate of the raw materials. "Intermediate concentrate of flotation" refers to the tailings generated in each flotation operation during the operation process.
[0073] The features and properties of the present invention will be further described in detail below in conjunction with embodiments.
[0074] Example 1
[0075] This example provides a method for obtaining cassiterite concentrate from a tin-polymetallic ore. Using a tin-polymetallic ore in a certain place in Inner Mongolia as the raw material, the main mineral components of the ore are cassiterite, pyrite, chalcopyrite, quartz, muscovite, biotite, chlorite, kaolinite, dolomite, etc. The average grades of the main valuable elements tin, copper, and sulfur in the ore are 0.86%, 0.36%, and 5.52%, respectively. The method mainly includes the following steps:
[0076] (1) Pulp preparation: Add water to the feedstock to adjust the pulp concentration to 30% (mass fraction, the same below).
[0077] (2) Hydrocyclone classification: Use a hydrocyclone of model FX-125 (the same below) to perform hydrocyclone classification on the material in step (1) to obtain hydrocyclone overflow and hydrocyclone sand.
[0078] (3) Sulfur flotation: Add sulfuric acid to the hydrocyclone sand for pulp preparation, control the pH value to 6, and sequentially add 50 g / t of collector (a mixture of sodium dialkyl sulfate and coconut oil alkylamine acetate, with a mass ratio of 1:3) and 10 g / t of frother pine oil for rough sulfur flotation to obtain sulfur concentrate and sulfur tailings.
[0079] (4) Classification: Classify the sulfur scavenging tailings into two particle sizes of +0.074 mm and -0.074 mm.
[0080] (5) Gravity separation: Use a spiral chute to perform primary gravity separation on the +0.074 mm particle size to obtain primary gravity separation rough concentrate and primary gravity separation tailings; use a shaking table to perform secondary gravity separation on the primary gravity separation rough concentrate to obtain secondary gravity separation cassiterite concentrate and secondary gravity separation tailings, and mix the secondary gravity separation tailings with the fine particles for flocculation sedimentation.
[0081] (6) Flocculation sedimentation for de-sludging: Perform flocculation sedimentation on the -0.074 mm in step (4) in an inclined plate sedimentation tank (the dosage of the flocculant is 50 g / t) to obtain overflow and sand; the sand is adjusted to a pulp concentration of 25%, and 100 g / t of collector butyl xanthate and 20 g / t of frother pine oil are sequentially added for rough flotation to obtain sulfur flotation concentrate and sulfur flotation tailings; among them, the preparation process of the flocculant used is as follows: Mix 5 g of dimethylaminoethyl methacrylate, 50 g of methyl methacrylate, and 30 g of 7-acryloyloxy-4-methylcoumarin, and polymerize at 50 °C for 24 h.
[0082] (7) Cassiterite flotation: Adjust the pulp concentration of the sulfur flotation tailings to 20%, sequentially add 50 g / t of regulator (lead nitrate), 1000 g / t of collector (ammonium salicylhydroxamate), and 40 g / t of frother pine oil for primary rough flotation to obtain rough flotation concentrate and rough flotation tailings; add water to the rough flotation tailings to adjust the pulp concentration to 18%, add 300 g / t of collector (ammonium salicylhydroxamate) and 15 g / t of frother pine oil for secondary scavenging flotation to obtain scavenging concentrate and scavenging tailings, and return the scavenging concentrate to the primary rough flotation operation to form a closed circuit; adjust the pulp concentration of the rough flotation concentrate to 5% with water and perform three blank cleaning operations to obtain cassiterite flotation concentrate; the middlings in each stage of flotation are returned to the upper-stage operation to form a closed circuit.
[0083] In the above steps, through the linked process of classification - flotation - gravity separation - flocculation - flotation, sulfur flotation concentrate and sulfur flotation tailings are obtained; the sulfur flotation tailings are adjusted to a pulp concentration of 20%, and through one rough selection, two scavenging selections and three blank cleaning selections, cassiterite flotation concentrate is obtained, with a tin grade of 6% and a tin recovery rate of 75.25%.
[0084] Example 2
[0085] This example provides a method for obtaining cassiterite concentrate from a tin polymetallic ore. A tin polymetallic ore in a certain place in Guangxi is used. The main mineral components of the ore are cassiterite, pyrite, chalcopyrite, quartz, muscovite, biotite, chlorite, kaolinite and dolomite, etc. The average grades of the main valuable elements tin, copper and sulfur in the ore are 0.75%, 0.44% and 6.32% respectively. It mainly includes the following steps:
[0086] (1) Pulp adjustment: Add water to the feed to adjust the pulp concentration to 35%;
[0087] (2) Hydrocyclone desliming: The material in step (1) is subjected to hydrocyclone classification to obtain hydrocyclone overflow and hydrocyclone sand;
[0088] (3) Sulfur flotation: Add sulfuric acid to the hydrocyclone sand for pulp adjustment, control the pH value to 7, and sequentially add 80 g / t of collector (a mixture of sodium dialkyl sulfate and coconut oil alkylamine acetate, with a mass ratio of 1:4.5) and 45 g / t of frother pine oil for rough sulfur flotation to obtain sulfur concentrate and sulfur tailings;
[0089] (4) Classification: The sulfur scavenging tailings are classified into two particle sizes of +0.074 mm and -0.074 mm;
[0090] (5) Gravity separation: The +0.074 mm particle size is subjected to one - stage gravity separation using a spiral chute to obtain primary gravity separation rough concentrate and primary gravity separation tailings; the primary gravity separation rough concentrate is subjected to secondary gravity separation using a shaking table to obtain secondary gravity separation cassiterite concentrate and secondary gravity separation tailings, and the secondary gravity separation tailings are mixed with the fine particles for flocculation sedimentation;
[0091] (6) Flocculation sedimentation: The -0.074 mm in step (4) is subjected to flocculation sedimentation in an inclined - plate sedimentation tank (the dosage of the flocculant is 150 g / t, and the flocculant preparation process is the same as that in Example 1) to obtain overflow and sand; the sand is adjusted to a pulp concentration of 28%, and 200 g / t of collector butyl xanthate and 100 g / t of frother pine oil are sequentially added for rough flotation to obtain sulfur flotation concentrate and sulfur flotation tailings;
[0092] (7) Cassiterite flotation: The tailings of sulfur flotation are adjusted to a pulp concentration of 22%, and 3000 g / t of regulator (lead acetate) is added in sequence, 2000 g / t of collector (ammonium salicylhydroxamate) and 110 g / t of frother pine oil are added, and a primary rough flotation is carried out to obtain a rough flotation concentrate and a rough flotation tailings; the pulp concentration of the rough flotation tailings after adding water for pulp adjustment is 24%, 1200 g / t of collector (ammonium salicylhydroxamate) and 50 g / t of frother pine oil are added for a secondary scavenging flotation to obtain a scavenging concentrate and a scavenging tailings, and the scavenging concentrate is returned to the primary rough flotation operation to form a closed circuit; the pulp concentration of the rough flotation concentrate after adding water for pulp adjustment is 10%, and a tertiary blank cleaning is carried out to obtain a cassiterite flotation concentrate; the middlings of each stage of flotation are returned to the previous operation to form a closed circuit.
[0093] In the above steps, through the combined process of classification - flotation - gravity separation - flocculation - flotation, a sulfur flotation concentrate and sulfur flotation tailings are obtained; the sulfur flotation tailings are adjusted to a pulp concentration of 22%, and through a primary roughing, a secondary scavenging and a tertiary blank cleaning, a cassiterite flotation concentrate is obtained, with a tin grade of 5.80% and a tin recovery rate of 74.20%.
[0094] Example 3
[0095] The difference from Example 1 is only that: the collector used in step (3) is replaced with an equal amount of benzohydroxamic acid.
[0096] The results show that: the tin grade in the obtained cassiterite flotation concentrate is 4.8%, and the tin recovery rate of the process is 65.78%.
[0097] Example 4
[0098] The difference from Example 1 is only that: the collector used in step (3) is replaced with an equal amount of ammonium salicylhydroxamate and benzohydroxamic acid (mixed by mass ratio: 3:1).
[0099] The results show that: the tin grade in the obtained cassiterite flotation concentrate is 5.07%, and the tin recovery rate of the process is 68.33%.
[0100] Example 5
[0101] The difference from Example 1 is only that: the flocculant used in step (6) is replaced with an equal amount of 100 g / t of polyacrylamide.
[0102] The results show that: the tin grade in the obtained cassiterite flotation concentrate is 3.69%, and the tin recovery rate of the process is 49.68%.
[0103] Example 6
[0104] The difference from Example 1 is only that: the flocculant used in step (6) is replaced with an equal amount of 100 g / t of ferric chloride.
[0105] The results show that the tin grade in the obtained cassiterite flotation concentrate is 3.18%, and the tin recovery rate of the process is 45.29%.
[0106] Comparative Example 1
[0107] This comparative example provides a method for obtaining cassiterite concentrate from tin polymetallic ore. The difference from Example 1 is only that there is no flocculation sedimentation for mud removal.
[0108] The results show that the tin grade in the obtained cassiterite flotation concentrate is 2.18%, and the tin recovery rate of the process is 35.18%.
[0110] The above are only the preferred embodiments of the present invention and are not used to limit the present invention. For those skilled in the art, the present invention can have various changes and modifications. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention shall be included within the protection scope of the present invention.
Claims
1. A method for obtaining cassiterite concentrate from tin polymetallic ore, characterized in that, Including: Slurry preparation: Mixing stanniferous polymetallic ore and water to prepare slurry, obtaining pulp; Hydrocyclone desliming: Performing hydrocyclone classification on the pulp to obtain first overflow and first sand deposit; Sulphur flotation: Mixing the first sand deposit and sulfuric acid to prepare slurry, and then mixing with a first collector and a first frother to conduct rough sulphur flotation, obtaining sulphur concentrate and sulphur tailings; Classification: Classifying the sulphur tailings to obtain coarse particles and fine particles; Gravity separation: Obtaining cassiterite concentrate from the coarse particles by gravity separation; Flocculation sedimentation: Conducting flocculation sedimentation on the fine particles to obtain second overflow and second sand deposit; Mixing the second sand deposit to prepare slurry and then mixing with a second collector and a second frother to conduct rough flotation, obtaining sulphur flotation concentrate and sulphur flotation tailings; Cassiterite flotation: Mixing the sulphur flotation tailings to prepare slurry and then mixing with a regulator, a third collector and a third frother to conduct primary rough flotation, obtaining rough flotation concentrate and rough flotation tailings; Mixing the rough flotation tailings to prepare slurry and then mixing with a fourth collector and a fourth frother to conduct secondary scavenging flotation, obtaining scavenging concentrate and scavenging tailings, returning the scavenging concentrate to the primary rough flotation operation to form a closed circuit, mixing the rough flotation concentrate to prepare slurry and then conducting at least one blank cleaning to obtain cassiterite flotation concentrate.
2. The method according to claim 1, wherein During the process of the sulphur flotation, the first collector used is a mixture of sodium dialkyl sulfate and coconut oil alkylamine acetate, and the mass ratio of sodium dialkyl sulfate to coconut oil alkylamine acetate is 1:(3 - 6); And / or, the addition amount of the first collector is 50 g / t - 100 g / t; And / or, the pH of adding sulfuric acid to prepare slurry is 6 - 7; And / or, the first frother is selected from at least one of pine oil and sodium dodecyl sulfate; And / or, the addition amount of the first frother is 10 g / t - 60 g / t.
3. The method according to claim 1, wherein The particle size of the coarse particles is greater than or equal to the critical value, the particle size of the fine particles is less than the critical value, and the critical value is 0.070 mm - 0.080 mm; And / or, conducting primary gravity separation on the coarse particles using a spiral chute to obtain primary gravity separation rough concentrate and primary gravity separation tailings; Conducting secondary gravity separation on the primary gravity separation rough concentrate using a shaking table to obtain secondary gravity separation cassiterite concentrate and secondary gravity separation tailings, and mixing the secondary gravity separation tailings with the fine particles to conduct flocculation sedimentation.
4. The method according to claim 1 or 3, characterized in that, The flocculant used in the flocculation sedimentation is obtained by reversible addition-fragmentation chain transfer polymerization with dimethylaminoethyl methacrylate, methyl methacrylate and 7-acryloyloxy-4-methylcoumarin as raw materials; And / or, the addition amount of the flocculant used in the flocculation sedimentation is 50 g / t - 300 g / t; And / or, the flocculation sedimentation is carried out in an inclined plate sedimentation tank.
5. The method according to claim 1, characterized in that, The mass fraction of the second sand deposit after slurry preparation is 25% - 33%; And / or, the second collector is selected from at least one of butyl xanthate and ammonium butyl dithiophosphate; the addition amount of the second collector is 100 g / t - 200 g / t; And / or, the second frother is selected from at least one of pine oil and sodium dodecyl sulfate; the addition amount of the second frother is 20 g / t - 100 g / t.
6. The method according to claim 1, wherein The mass fraction of the sulfur flotation tailings after pulp mixing is 20%-25%; and / or, the regulator is selected from at least one of lead nitrate and lead acetate; the addition amount of the regulator is 50 g / t - 3000 g / t; and / or, the third collector is selected from at least one of ammonium salicylhydroxamate and benzohydroxamic acid; the addition amount of the third collector is 1000 g / t - 2000 g / t; and / or, the third foaming agent is selected from at least one of pine oil and sodium dodecyl sulfate; the addition amount of the third foaming agent is 40 g / t - 110 g / t.
7. The method according to claim 1, characterized in that, The mass fraction of the rough flotation tailings after pulp mixing is 18%-24%; and / or, the fourth collector is selected from at least one of ammonium salicylhydroxamate and tolylarsonic acid; the addition amount of the fourth collector is 300 g / t - 1200 g / t; and / or, the fourth foaming agent is selected from at least one of pine oil and methyl isobutyl carbinol; the addition amount of the fourth foaming agent is 0 g / t - 50 g / t.
8. The method according to claim 1, characterized in that, The mass fraction of the rough flotation concentrate after pulp mixing is 5%-10%; and / or, the blank cleaning is carried out three times.
9. The method according to claim 1, wherein During the cassiterite flotation process, the middlings at all levels of flotation are returned to the upper operation to form a closed circuit.
10. The method according to claim 1, characterized in that, The mass fraction of the pulp obtained by mixing the tin polymetallic ore and water for pulp mixing is 30%-40%.