CN102824962B - Reagent formula used for zinc leaching residue floatation process and application method of reagent formula - Google Patents
Reagent formula used for zinc leaching residue floatation process and application method of reagent formula Download PDFInfo
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Abstract
The invention relates to a reagent formula used for a zinc leaching residue floatation process and an application method of the reagent formula. The reagent is a floatation reagent which is added into floatation processes such as sulfurizing, rough floatation, scavenging and concentration. The reagent formula is characterized in that 1) one or two of sodium sulphide and sodium hydrosulfide are added into a sulfurizing process as a sulfurizing reagent; 2) in the rough floatation process, N,N-sodium diethyldithiocarbamate, butyl ammonium black powder and 25# black powder are added as lead mineral collecting agents, Y89 and (or) pentyl xanthate are added as silver mineral collecting agent(s); 3) in a scavenging process, one or two of sodium sulphide and sodium hydrosulfide are added as the sulfutizing agent(s), N,N-sodium diethyldithiocarbamate, butyl ammonium black powder and 25# black powder are added as the lead mineral collecting agents, and the Y89 and (or) pentyl xanthate are added as the silver mineral collecting agent(s); and 4) carboxymethylcellulose is added as a gangue inhibiting agent in a concentration process. After applying the reagent formula disclosed by the invention, by adopting one-time rougher floatation, one-time scavenging and one-time concentration, lead yield can reach up to more than 95% and lead tail run can reach 0.1-0.2%.
Description
Art
The present invention relates to a kind of floating agent formula and usage, especially a kind of reagent combination for zinc flotation of leached residue process and usage, belong to wet method selecting and smelting technology field.
Background technology
Zinc leaching slag is the leached mud of zinc hydrometallurgy leaching process output, is difficult to process and in reasons such as first processing method technological means are limited, zinc leaching slag is about 15-22%, leaded about 5-8% containing zinc, and argentiferous is about 30-300g/t due to Zn, Pb and Ag symbiosis.Zinc leaching slag zinc thing is based on zinc ferrite and zinc sulfate, and the plumbous thing of zinc leaching slag is based on sardinianite and lead silicate, and zinc leaching slag silver thing is based on silver sulfide and elemental silver.According to " reclaiming the method for zinc from the leached mud of dregs containing zinc " (ZL96118245.8) of the invention of Li Hong osmanthus, zinc leaching slag is reduced to 7-15% containing zinc, make process zinc soak slag technology and stepped into major step, but compared with a zinc resource zincblende, zinc leaching slag belongs to rich zinc resource.Therefore, the zinc in slag such as leaching such as zinc such as recovery such as method such as the employing of zinc hydrometallurgy enterprise high temperature high acidic oils and Rotary Kiln volatilization etc. and other valuable metal.Because energy consumption is high and the environmental pollution problem such as heavily, most zinc hydrometallurgy enterprises stop adopting Rotary Kiln technical finesse zinc to soak slag.Because of the zinc leaching slag after high temperature high acidic oils, still reach 3-5% containing zinc, along with the dilution day by day of a zinc resource and the rising day by day of cost of winning, this zinc leaching slag still belongs to rich zinc resource.Electricity zinc output and zinc soak slag output and are about 1:1, by world's electricity zinc output in 2011 1290.5 ten thousand tons of reckonings, world's zinc leaching slag is containing zinc total amount 38.7-64.5 ten thousand tons/year, leaded total amount 64.5-103.2 ten thousand tons/year, argentiferous total amount 516.2-3871.5 ton/year, zinc leaching slag remains a kind of secondary Zn, Pb and Ag resource having very much value of exploiting and utilizing.Therefore, the necessary method to formerly processing zinc leaching slag is improved.
Summary of the invention
The object of the invention is to, for existing zinc flotation of leached residue process, propose a kind of new reagent combination and usage, this reagent combination and usage effectively can extract metal values in zinc leaching slag, and medicament does not cause environmental pollution.
The present inventor is found by lot of experiments: zinc leaching slag contains the high reason of zinc, and one is that zinc ferrite mineral are wrapped up by sardinianite, prevents Leaching reaction to carry out; Two is low in first washing methods desorption zinc sulfate efficiency, cause zinc sulfate to be carried secretly by the absorption of zinc leaching slag, and then it is higher then higher containing zinc to cause zinc to soak lead-in-dreg.The reason of zinc leaching slag lead minerals and the difficult flotation of silver mineral, be that zinc sulfate parcel lead minerals and silver mineral surface form aquation covering, prevent medicament to effective absorption of lead minerals and silver mineral, and then it be higher containing zinc to cause zinc to soak slag, lead minerals and silver mineral flotation yield lower, lead concentrate containing zinc higher.
According to above-mentioned research, the technical solution used in the present invention is: a kind of reagent combination for zinc flotation of leached residue process, described medicament, is in sulfuration, roughly selects, scans and the floating agent that adds respectively in selected floatation process, it is characterized in that:
1) one or both vulcanizing agents in vulcanized sodium or NaHS are added in sulfidation;
2) add diethyldithiocarbamate, butyl ammonium aerofloat, 25 ﹟ black powder as lead minerals collecting agent in rougher process, add Y89 and (or) penta xanthate as silver mineral collecting agent;
3) add one or both vulcanizing agents in vulcanized sodium or NaHS in the process of scanning, add diethyldithiocarbamate, butyl ammonium aerofloat, 25 ﹟ black powder as lead minerals collecting agent, add Y89 and (or) penta xanthate as silver mineral collecting agent;
4) carboxymethyl cellulose is added as gangue inhibitor at refining process.
A kind of usage of the reagent combination for zinc flotation of leached residue process is:
1) add vulcanizing agent in sulfidation, vulcanizing agent medicament and weight proportion thereof are: vulcanized sodium or NaHS (4-20kg);
2) add lead minerals collecting agent and silver mineral collecting agent in the preposition process of sizing mixing of one roughing, lead minerals collecting agent and silver mineral collecting agent medicament and weight proportion thereof are: diethyldithiocarbamate (200-300g/t), butyl ammonium aerofloat (50-100g/t); 25 ﹟ black powder (25-50g/t), Y89(40-50g/t), penta xanthate (40-50g/t);
3) add vulcanizing agent, lead minerals collecting agent and silver mineral collecting agent in the preposition process of sizing mixing of once purging selection, vulcanizing agent, lead minerals collecting agent and silver mineral collecting agent medicament and weight proportion thereof are: vulcanized sodium (300-500g/t), diethyldithiocarbamate (50-100g/t), butyl ammonium aerofloat (25-50g/t), 25 ﹟ black powder (10-20g/t), Y89(20-25g/t), penta Huang (20-25g/t);
4) add gangue inhibitor in the preposition process of sizing mixing of primary cleaning, gangue inhibitor medicament and weight proportion thereof are: carboxymethyl cellulose (50-200g/t).
Further, when Treatment of Copper zinc leaching slag, ethyl ammonia sulfate (50-200g/t) is increased in the preposition process of sizing mixing of one roughing, ethyl ammonia sulfate (50-100g/t) is increased in the preposition process of sizing mixing of once purging selection, sodium thioglycolate (20-100g/t) is increased in the preposition process of sizing mixing of primary cleaning, the primary cleaner tailing slurry of output is copper concentrate, implements open circuit process to copper concentrate.
Further, process not argentiferous zinc leaching slag time, do not add Y89 and (or) penta xanthate in the preposition process of sizing mixing of one roughing, do not add Y89 and (or) penta xanthate in the preposition process of sizing mixing of once purging selection.
Advantage of the present invention is:
1) technological process is short, and equipment investment is little, and the high and cost recovery of zinc, lead, silver-colored yield significantly reduces.
2) can independent operating mode or in conjunction with zinc hydrometallurgy enterprise at first production factors mode process zinc leaching slag.
Accompanying drawing explanation
Fig. 1 is a kind of ultrasonic dressing and smelting process processing zinc leaching slag.
Fig. 2 is the ultrasonic dressing and smelting process of a kind of Treatment of Copper zinc leaching slag.
In Fig. 1,1, zinc leaching slag; 2, ore mill; 3, ore pulp after ore grinding; 4, electrodeposition waste liquid (or industrial sulphuric acid); 5, hydrogen peroxide; 6, filter; 7, solution of zinc sulfate; 8, filter; 9, supersound washing filtrate; 10, ultrasonic leaching is preposition size mixing after liquid; 11, liquid after ultrasonic leaching; 12, ultrasonic leaching filter residue; 13, hot water; 14, supersound washing is preposition size mixing after liquid; 15, liquid after supersound washing; 16, medicament; 17, supersound washing filter residue; 18, paste mixer; 19, ultrasonic leaching machine; 20, medicament; 21, paste mixer; 22, ultrasonic washer; 23, paste mixer; 24, one roughing concentrate slurry; 25, one roughing is preposition size mixing after ore pulp; 26, medicament; 27, ore pulp after ultrasonic vulcanization; 28, ultrasonic vulcanization is preposition size mixing after ore pulp; 29, once purging selection concentrate slurry; 30, one roughing Tailings Slurry; 31, air flotation machine; 32, ore pulp after the preposition ultrasonic disperse of one roughing; 33, ultrasonic disperse machine; 34, paste mixer; 35, ultrasonic vulcanization machine; 36, once purging selection Tailings Slurry; 37, air flotation machine; 38, ore pulp after the preposition ultrasonic disperse of once purging selection; 39, ultrasonic disperse machine; 40, bulk concentrate slurry; 41, medicament; 42, primary cleaning is preposition size mixing after ore pulp; 43, dewatered tailings; 44, filter; 45, tail water; 46, paste mixer; 47, ultrasonic disperse machine; 48, ore pulp after the preposition ultrasonic disperse of primary cleaning; 49, air flotation machine; 50, primary cleaner tailing slurry; 51, lead concentrate.
In Fig. 2,52, preposition ultrasonic leaching system; 53, rearmounted ultrasonic flotation system.
Detailed description of the invention
Below in conjunction with drawings and Examples, the invention will be further described, but protection scope of the present invention is not limited to the scope described by embodiment.
embodiment one:a kind of ultrasonic dressing and smelting process processing zinc leaching slag
As can be seen from Fig. 1 and 2, the present invention is a kind of ultrasonic dressing and smelting process processing zinc leaching slag.Preposition ultrasonic leaching system 52, is made up of ore mill 2, paste mixer 18, ultrasonic leaching machine 19, filter 6, paste mixer 21, ultrasonic washer 22, filter 8; Rearmounted ultrasonic flotation system 53, is made up of paste mixer 23, ultrasonic vulcanization machine 35, paste mixer 34, ultrasonic disperse machine 33, air flotation machine 31, ultrasonic disperse machine 39, air flotation machine 37, paste mixer 46, ultrasonic disperse machine 47, air flotation machine 49, filter 44.Its know-why and the course of work are:
Zinc leaching slag 1 prepare burden by solid-to-liquid ratio 2:1 with hot water 13, enters ore mill 2, and it is that-0.074mm accounts for ore pulp 3 after the ore grinding of 90-100% that output zinc soaks slag 1 granularity.
After ore grinding ore pulp 3 enter stir paste mixer 18 size mixing.Solvent of sizing mixing comprises Zinc electrolysis waste liquid (or industrial sulphuric acid) 4 and supersound washing filtrate 9.Solid-to-liquid ratio of sizing mixing is 1:3, initial p H1-2.5, adjusting slurry temperature control 70-90 DEG C, hydrogen peroxide consumption 10-40ml/L, after sizing mixing 5-30 minute, the ultrasonic leaching of output is preposition size mixing after liquid 10.
Ultrasonic leaching is preposition size mixing after liquid 10 pump into one-way flow in U-shaped tubular ultrasonic leaching machine 19.Ultrasonic leaching machine 19 the ultrasonic leaching of one-way flow is preposition size mixing after form effective sound intensity in liquid 10 and be greater than 1w/cm
2ultrasonic sound field, the particle flux that this ultrasonic sound field causes 400 meters of flow velocitys per second clashes into zinc leaching slag 1 surface, the zinc leaching surperficial newborn covering of slag 1 (as Iron Oxide Minerals and zinc sulfate covering) and self covering (as zinc ferrite covering) is degraded in strengthening, to set granularity, concentration, liquid temperature, PH, pulp potential ultrasonic leaching preposition size mixing after liquid 10 implement ultrasonic leaching.Ultrasonic leaching is after 1-5 minute, and the zinc ferrite in zinc leaching slag 1 is decomposed, and output comprises liquid 11 after the ultrasonic leaching of ionic state zinc sulfate and solid oxide iron mineral.
Liquid 11 after ultrasonic leaching, pumps into filter 6 under liquid temperature >=70 DEG C, PH≤5.2 condition.Filter process does not have basic zinc sulfate crystallization to generate, thus stops ultrasonic leaching filter residue 12 surface to form basic zinc sulfate aquation covering.The ultrasonic leaching filtrate of filter 6 output is solution of zinc sulfate 7, with pipeline or the process of chute conveying cleaning system.
Enter the ultrasonic leaching filter residue 12 stirring paste mixer 21, its solvent of sizing mixing is hot water 13, solid-to-liquid ratio is that 1:3-4(is obvious, reduce the preposition process solid-to-liquid ratio of sizing mixing of supersound washing to 1:8-10, then clean result is better), liquid temperature 70-90 DEG C, after sizing mixing 5-30 minute, output supersound washing is preposition size mixing after liquid 14.
Supersound washing is preposition size mixing after liquid 14 pump into one-way flow in U-tube formula ultrasonic washer 22.Ultrasonic washer 22 the supersound washing of one-way flow is preposition size mixing after form effective sound intensity in liquid 14 and be greater than 1w/cm
2ultrasonic sound field, this ultrasonic sound field causes the particle flux of 400 meters of flow velocitys per second and clashes into ultrasonic leaching filter residue 12 surface, makes the zinc sulfate desorption being adsorbed on ultrasonic leaching filter residue 12 surface enter in hot water 13, liquid 15 after output supersound washing.
After supersound washing liquid 15 liquid temperature 70-90 DEG C, pump into filter 8 under the condition of PH≤5.2, filter process does not have basic zinc sulfate crystallization and generates, and then effectively stops supersound washing filter residue 17 pairs of zinc sulfate to produce absorption to carry secretly.Supersound washing filtrate 9 gravity flow of filter 8 output enters paste mixer 18 and sizes mixing, and supersound washing filter residue 17, as the raw material of rearmounted ultrasonic flotation system 53, enters and stirs paste mixer 23.Complete the preposition ultrasonic leaching process of zinc leaching slag 1 thus.
Supersound washing filter residue 17 is prepared burden by solid-to-liquid ratio 1:2-3 with hot water 13 in stirring paste mixer 23, at slurry temperature 60-70 DEG C, medicament 16(is as vulcanized sodium) under the condition of addition 4-20kg/t, stir the 3-8 minute that sizes mixing, output ultrasonic vulcanization is preposition size mixing after ore pulp 28.
Ultrasonic vulcanization is preposition size mixing after ore pulp 28 pump into one-way flow in U-tube formula ultrasonic vulcanization machine 35.Ultrasonic vulcanization machine 35 the ultrasonic vulcanization of one-way flow is preposition size mixing after form effective sound intensity in ore pulp 28 and be greater than 1w/cm
2ultrasonic sound field, the particle flux that this ultrasonic sound field causes 400 meters of flow velocitys per second clashes into supersound washing filter residue 17 surface, the ultra-fine gangue sludge being deposited on supersound washing filter residue 17 surface is removed by high-efficient cleaning, medicament 16(is vulcanized sodium or NaHS, addition is 4-20kg) be preferably deposited in lead minerals and silver mineral surface, the lead minerals making hydrophobicity lower and silver mineral surface modification are the sulfide cladding surface that hydrophobicity is higher.Ultrasonic vulcanization 3 minutes under the condition of slurry temperature 60-70 DEG C, completes the sulfidation that supersound washing filter residue 17 lead minerals and silver mineral surface modification are sulfide covering, ore pulp 27 after output ultrasonic vulcanization.
After ultrasonic vulcanization, ore pulp 27 enters to stir in paste mixer 34 and carries out that one roughing is preposition sizes mixing.This process of sizing mixing is intended to utilize medicament 26 to implement to be modified as the selective absorption after sulfide covering and deposition to lead minerals and silver mineral, improves the hydrophobicity on lead minerals and silver mineral surface further.Medicament 26 is: diethyldithiocarbamate (200-300g/t), butyl ammonium aerofloat (50-100g/t); 25 ﹟ black powder (25-50g/t), Y89(40-50g/t), penta xanthate (40-50g/t).After sizing mixing 3-5 minute, output one roughing is preposition size mixing after ore pulp 25.
One roughing is preposition size mixing after ore pulp 25 pump into one-way flow in U-tube formula ultrasonic disperse machine 33.Ultrasonic disperse machine 33 the one roughing of one-way flow is preposition size mixing after form effective sound intensity in ore pulp 25 and be greater than 1w/cm
2ultrasonic sound field, the particle flux that this ultrasonic sound field causes 400 meters of flow velocitys per second clashes into supersound washing filter residue 17 and medicament 26, the ultra-fine gangue sludge being deposited on lead minerals and silver mineral modified sulphur compound cladding surface is removed by high-efficient cleaning, medicament 26 one roughing is preposition size mixing after high efficiency dispersion in ore pulp 25.After the preposition ultrasonic disperse 0.5-1 of one roughing minute, medicament 26 is firmly deposited on the modified sulphur compound cladding surface of supersound washing filter residue 17 lead minerals and silver mineral, efficiently completes creation sufficient and necessary condition for rearmounted bubble mineralization process.
After the preposition ultrasonic disperse of one roughing, ore pulp 32 enters in air flotation machine 31.Air flotation machine 31 adopts cored screw rotor structure to implement bubble and produces and mineralization process, adopts the mode of N bar helical duct shunting Tailings Slurry to implement gas solid separation process, is passing into pressure 0.3MPa, flow 3-4m
3under/h airflow conditions, pass into air stream in cored screw rotor, form N number of spiral gas field, N gas-liquid mixed is implemented to ore pulp 32 after the preposition ultrasonic disperse of one roughing, after making the preposition ultrasonic disperse of one roughing, in ore pulp 32, is attached to bubble surface fast by the lead minerals of the abundant parcel of medicament 26 and silver mineral particle.Mineral laden bubble with not by the gangue particle that bubble adsorbs, the gas solid separation region in air flotation machine 31 completes gas solid separation: mineral laden bubble emersion mineral syrup liquid, flow out air flotation machine 31, output one roughing concentrate slurry 24; Gangue particle, through being located at the N bar helical duct shunting of air flotation machine 31 cell body inwall, flows out from the Tailings Slurry outlet bottom air flotation machine 31, output one roughing Tailings Slurry 30.
Utilize the one roughing gas solid separation region of air flotation machine 31 to add medicament 20, one roughing Tailings Slurry 30 is sized mixing.Medicament 20 is: vulcanized sodium (300-500g/t), diethyldithiocarbamate (50-100g/t), butyl ammonium aerofloat (25-50g/t), 25 ﹟ black powder (10-20g/t), Y89(20-25g/t), penta Huang (20-25g/t).Process of sizing mixing and the one roughing gas solid separation process of one roughing Tailings Slurry 30 are same process.
One roughing Tailings Slurry 30 enters ultrasonic disperse machine 39, after going through that roughly the same one roughing is preposition and sizing mixing ore pulp 25 ultrasonic disperse process after, ore pulp 38 after the preposition ultrasonic disperse of output once purging selection.
After the preposition ultrasonic disperse of once purging selection, ore pulp 38 enters air flotation machine 37, after going through the floatation process of ore pulp 32 after the preposition ultrasonic disperse of roughly the same one roughing, and output once purging selection concentrate slurry 29 and once purging selection Tailings Slurry 36.
One roughing concentrate slurry 24 and once purging selection concentrate slurry 29, can conflux for bulk concentrate slurry 40, enters to stir in paste mixer 46 to carry out that primary cleaning is preposition sizes mixing.This process of sizing mixing adds medicament 41, and medicament 41 is carboxymethyl cellulose (50-200g/t).After sizing mixing 3-5 minute, output primary cleaning is preposition size mixing after ore pulp 42.
Primary cleaning is preposition size mixing after ore pulp 42 pump into ultrasonic disperse machine 47, after going through that roughly the same one roughing is preposition and sizing mixing ore pulp 25 and one roughing Tailings Slurry 30 ultrasonic disperse process after, ore pulp 48 after the preposition ultrasonic disperse of output primary cleaning.
After the preposition ultrasonic disperse of primary cleaning, ore pulp 48 enters air flotation machine 49, after going through the floatation process of ore pulp 38 after ore pulp 32 and the preposition ultrasonic disperse of once purging selection after the preposition ultrasonic disperse of roughly the same one roughing, output primary cleaning concentrate slurry and lead concentrate 51 and primary cleaner tailing slurry 50.
Once purging selection Tailings Slurry 36 enters filter 44, output dewatered tailings 43 and tail water 45.Tail water 45 is middle warm water, returns paste mixer 23 pairs of supersound washing filter residues 17 and implement to size mixing after heating.Complete the rearmounted ultrasonic flotation process of supersound washing filter residue 17 thus.
The air flotation machine that the present invention adopts, open in the patents of invention such as PCT/CN2011/078154 and CN102441494A, but do not repel the application at first air flotation machine.In know-why and the course of work of first air flotation machine, be well-known.
As can be seen from Fig. 1 and 2, size mixing in process the ultrasonic leaching of preposition ultrasonic leaching system 52 is preposition, Leaching reaction starts, extend the preposition process time of sizing mixing of ultrasonic leaching, the ultrasonic leaching process time can correspondingly shorten, otherwise the ultrasonic leaching process time can correspondingly extend.The design parameter of process of sizing mixing, depends on that reaching setting slurry temperature, acidity, solid-to-liquid ratio and medicament adds the factors such as deadline, especially warming up pulp time factor.
As can be seen from Fig. 1 and 2, the Main Function of hydrogen peroxide 5, it is the strong oxidizer effect under setting leaching environment, by disproportionation current potential, oxidation is implemented to zinc leaching slag institute's sulfur compound and ferrous iron, pulp potential under adjustment leaching environment is in zinc ferrite can not the pulp potential of stable existence, and then effectively eliminates zinc sulfate aquation covering.The addition manner of hydrogen peroxide 5 is uniformly continous addition manner.The addition manner of assault formula, will cause it to consume meaningless increase.
It can also be seen that from Fig. 1 and 2, the degree of association of flotation effect and air flotation machine functional structure is very large, bubble produces and mineralization process effect, and gas solid separation process effect, when using the air flotation machine of difference in functionality structure, cause different roughly selecting number of times thus, scan number of times, concentration times and empty flow parameter, be completely possible.The air flotation machine 31,37,49 that the present invention adopts, its bubble produces and mineralization process, is to produce and mineralization process based on the bubble under N number of spiral gas field action; Its gas solid separation process is the gas solid separation process based on adopting N bar helical duct shunting mine tailing.
embodiment two:a kind of ultrasonic dressing and smelting process of Treatment of Copper zinc leaching slag
As can be seen from Figure 2, the present invention is the ultrasonic dressing and smelting process of a kind of Treatment of Copper zinc leaching slag, its engineering design and embodiment one are substantially identical, and difference is: in the medicament 26 that the preposition process of sizing mixing of one roughing adds, and increase ethyl ammonia sulfate (50-200g/t); In the medicament 20 that the preposition process of sizing mixing of once purging selection adds, increase ethyl ammonia sulfate (50-100g/t); In the medicament 41 that the preposition process of sizing mixing of primary cleaning adds, increase sodium thioglycolate (20-100g/t); Primary cleaner tailing slurry 50 is copper concentrate, and copper concentrate implements open circuit process.
The zinc leaching slag 1 of the ultrasonic flotation and metallurgy method Treatment of Copper 0.8% of application the present embodiment, obtains the supersound washing filter residue 17 of cupric 2.4% at preposition ultrasonic leaching system 52, obtain the primary cleaner tailing slurry 50 of cupric 12-15% in rearmounted ultrasonic flotation system 53.Subsequent treatment (such as increasing a copper concentrate selected) is implemented to primary cleaner tailing slurry 50 open circuit, then can obtain the copper concentrate of commerical grade grade.
Obviously, under the ultrasonic dressing and smelting process condition of the present embodiment, the partial oxidation copper mineral in cupric zinc leaching slag 1, inevitably by leaching section, enters in solution of zinc sulfate 7.Adjust ultrasonic leaching process condition, the ratio that copper mineral enters solution of zinc sulfate 7 and primary cleaner tailing slurry 50 can be changed.Therefore, the present invention is applied to the process of zinc-lead oxide copper mine, zinc oxide copper mine, can realize zinc lead bronze or zinc-copper is efficiently separated, output solution of zinc sulfate, copper concentrate, adopts zinc dust precipitation process then output copper sponge to solution of zinc sulfate.
embodiment three:a kind of ultrasonic dressing and smelting process processing not argentiferous zinc leaching slag
As can be seen from Figure 2, the present invention is a kind of ultrasonic dressing and smelting process processing not argentiferous zinc leaching slag, and its engineering design and embodiment one are substantially identical, and difference is: do not need to add Y89 and (or) penta xanthate at floatation process.The Pb-Zn deposits in Zn, Pb and Ag symbiosis or half a lifetime is very general in lead zinc sulphur ore resource, but in the lead zinc sulphur ore of Chinese Xiangxi Region, silver containing mineral hardly.In plumbous Zinc oxide, also there is a lot of led-zinc-silver deposit that argentiferous or argentiferous are very not low.The zinc leaching slag of application the present embodiment process not argentiferous, is conducive to saving reagent cost.
Can be found out by above-described embodiment, the present invention relates to a kind of reagent combination for zinc flotation of leached residue process, described medicament, be in sulfuration, roughly select, scan and the floating agent that adds respectively in selected floatation process, it is characterized in that:
1) one or both vulcanizing agents in vulcanized sodium or NaHS are added in sulfidation;
2) add diethyldithiocarbamate, butyl ammonium aerofloat, 25 ﹟ black powder as lead minerals collecting agent in rougher process, add Y89 and (or) penta xanthate as silver mineral collecting agent;
3) add one or both vulcanizing agents in vulcanized sodium or NaHS in the process of scanning, add diethyldithiocarbamate, butyl ammonium aerofloat, 25 ﹟ black powder as lead minerals collecting agent, add Y89 and (or) penta xanthate as silver mineral collecting agent;
4) carboxymethyl cellulose is added as gangue inhibitor at refining process.
A kind of usage of the reagent combination for zinc flotation of leached residue process is:
1) add vulcanizing agent in sulfidation, vulcanizing agent medicament and weight proportion thereof are: vulcanized sodium or NaHS (4-20kg);
2) add lead minerals collecting agent and silver mineral collecting agent in the preposition process of sizing mixing of one roughing, lead minerals collecting agent and silver mineral collecting agent medicament and weight proportion thereof are: diethyldithiocarbamate (200-300g/t), butyl ammonium aerofloat (50-100g/t); 25 ﹟ black powder (25-50g/t), Y89(40-50g/t), penta xanthate (40-50g/t);
3) add vulcanizing agent, lead minerals collecting agent and silver mineral collecting agent in the preposition process of sizing mixing of once purging selection, vulcanizing agent, lead minerals collecting agent and silver mineral collecting agent medicament and weight proportion thereof are: vulcanized sodium (300-500g/t), diethyldithiocarbamate (50-100g/t), butyl ammonium aerofloat (25-50g/t), 25 ﹟ black powder (10-20g/t), Y89(20-25g/t), penta Huang (20-25g/t);
4) add gangue inhibitor in the preposition process of sizing mixing of primary cleaning, gangue inhibitor medicament and weight proportion thereof are: carboxymethyl cellulose (50-200g/t).
Further, when Treatment of Copper zinc leaching slag, ethyl ammonia sulfate (50-200g/t) is increased in the preposition process of sizing mixing of one roughing, ethyl ammonia sulfate (50-100g/t) is increased in the preposition process of sizing mixing of once purging selection, sodium thioglycolate (20-100g/t) is increased in the preposition process of sizing mixing of primary cleaning, the primary cleaner tailing slurry of output is copper concentrate, implements open circuit process to copper concentrate.
Further, process not argentiferous zinc leaching slag time, do not add Y89 and (or) penta xanthate in the preposition process of sizing mixing of one roughing, do not add Y89 and (or) penta xanthate in the preposition process of sizing mixing of once purging selection.
For a long time, ore dressing brainstrust has neglected the negative effect of solvable zinc sulfate under flotation environment, and existing ion flotation technique study rests on ionic state noble metal recovery field, so, study from the angle of method for floating merely, almost have no chance to find economy high efficiente callback zinc to soak technical method and the compounding method for medicament of slag lead minerals and silver mineral.The present invention is also based on a kind of compounding method for medicament contained by zinc leaching slag after the efficient desorption of zinc sulfate.
The present inventor soaks the mineral such as slag, refractory oxidized leadzinc ore, difficult choosing oxidation lead skim to zinc, carry out floatation process test to find, diethyldithiocarbamate and butyl ammonium aerofloat is adopted to make lead minerals collecting agent, plumbous yield can reach more than 90%, but after increasing by 25 ﹟ black powder, plumbous yield can reach more than 95%, and the plumbous tail that runs is reduced to 0.1%.Refining process adopts the gangue inhibitors such as starch, waterglass, calgon, and inhibition is all not as carboxymethyl cellulose.Obviously, adjustment butyl ammonium aerofloat consumption, adopts 2# oil (mixtures of terpenic oil and petrochemical industry intermediate products) foaming agent as a supplement, also can reach or close to flotation effect of the present invention.Be used alone Y89 or penta xanthate, adjustment consumption, zinc flotation of leached residue effect is also rather close.
The present inventor also confirms from test, and for leaded more than 20% zinc leaching slag, adopt the mixed lead concentrate of one roughing, once purging selection output, namely leaded grade reaches more than 35%, and once purging selection mine tailing is leaded is reduced to 0.1-0.2%.
Claims (5)
1., for a reagent combination for zinc flotation of leached residue process, described medicament, is in sulfuration, roughly selects, scans and the floating agent that adds respectively in selected floatation process, it is characterized in that:
1) a kind of vulcanizing agent in vulcanized sodium or NaHS is added in sulfidation;
2) add diethyldithiocarbamate, butyl ammonium aerofloat, 25 ﹟ black powder as lead minerals collecting agent in rougher process, add Y89 and penta xanthate as silver mineral collecting agent;
3) add a kind of vulcanizing agent in vulcanized sodium or NaHS in the process of scanning, add diethyldithiocarbamate, butyl ammonium aerofloat, 25 ﹟ black powder as lead minerals collecting agent, add Y89 and penta xanthate as silver mineral collecting agent;
4) carboxymethyl cellulose is added as gangue inhibitor at refining process;
Described reagent combination and using method thereof is:
1) add vulcanizing agent in sulfidation, vulcanizing agent medicament and weight proportion thereof are: vulcanized sodium or NaHS 4-20kg/t;
2) add lead minerals collecting agent and silver mineral collecting agent in the preposition process of sizing mixing of one roughing, lead minerals collecting agent and silver mineral collecting agent medicament and weight proportion thereof are: diethyldithiocarbamate 200-300g/t, butyl ammonium aerofloat 50-100g/t; 25 ﹟ black powder 25-50g/t, Y8940-50g/t, penta xanthate 40-50g/t;
3) add vulcanizing agent, lead minerals collecting agent and silver mineral collecting agent in the preposition process of sizing mixing of once purging selection, vulcanizing agent, lead minerals collecting agent and silver mineral collecting agent medicament and weight proportion thereof are: vulcanized sodium 300-500g/t, diethyldithiocarbamate 50-100g/t, butyl ammonium aerofloat 25-50g/t, 25 ﹟ black powder 10-20g/t, Y8920-25g/t, penta yellow 20-25g/t;
4) add gangue inhibitor in the preposition process of sizing mixing of primary cleaning, gangue inhibitor medicament and weight proportion thereof are: carboxymethyl cellulose 50-200g/t.
2. as claimed in claim 1 for the reagent combination of zinc flotation of leached residue process, it is characterized in that: when Treatment of Copper zinc leaching slag, ethyl ammonia sulfate 50-200g/t is increased in the preposition process of sizing mixing of one roughing, ethyl ammonia sulfate 50-100g/t is increased in the preposition process of sizing mixing of once purging selection, sodium thioglycolate 20-100g/t is increased in the preposition process of sizing mixing of primary cleaning, the primary cleaner tailing slurry of output is copper concentrate, implements open circuit process to copper concentrate.
3., as claimed in claim 1 for the reagent combination of zinc flotation of leached residue process, it is characterized in that: process not argentiferous zinc leaching slag time, do not add Y89 and penta xanthate in the preposition process of sizing mixing of one roughing, do not add Y89 and penta xanthate in the preposition process of sizing mixing of once purging selection.
4. as claimed in claim 2 for the reagent combination of zinc flotation of leached residue process, it is characterized in that: described zinc leaching slag, is the zinc leaching slag after adopting flotation and metallurgy method desorption zinc sulfate covering.
5. as claimed in claim 2 for the reagent combination of zinc flotation of leached residue process, it is characterized in that: zinc leaching lead-in-dreg grade higher than 20% time, the lead concentrate of one roughing process output and the lead concentrate of once purging selection process output mix, namely the lead concentrate of leaded more than 35% is become, and once purging selection mine tailing is leaded is reduced to 0.1-0.2%, thus remove primary cleaning process from.
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| CN103551256B (en) * | 2013-11-06 | 2015-12-30 | 湖南华麒资源环境科技发展有限公司 | A kind of activator of zinc hydrometallurgy acid leaching ore pulp silver floatation |
| CN104624388A (en) * | 2013-11-13 | 2015-05-20 | 甘肃中盛矿业有限责任公司 | Agent improvement method used in silver and zinc compound ore flotation process |
| CN103657860B (en) * | 2013-12-11 | 2015-09-30 | 广西大学 | The method of reverse flotation enrichment zinc silicate mineral in acid condition |
| CN103721857B (en) * | 2013-12-31 | 2015-10-21 | 广西大学 | A kind of preparation method of willemite thing collecting agent |
| CN103831172B (en) * | 2014-03-28 | 2015-02-11 | 西藏华钰矿业股份有限公司 | Method for improving antimony, lead and associated silver flotation recovery rate by adopting combination collecting agent |
| CN104532295B (en) * | 2015-01-08 | 2016-08-24 | 花垣县宏达边城科技有限公司 | The recovery process of valuable metal and the electrolysis bath used thereof in electrolytic zinc leached mud |
| CN104785356A (en) * | 2015-03-26 | 2015-07-22 | 云南永昌铅锌股份有限公司 | Method and system for processing leaching residues of zinc hydrometallurgy |
| CN104841564B (en) * | 2015-05-15 | 2017-08-18 | 西北矿冶研究院 | Lead-silver residue flotation combined collecting agent and application process thereof |
| CN107626441B (en) * | 2017-10-20 | 2019-12-03 | 中国科学院过程工程研究所 | Recycle the beneficiation method and beneficiation reagent of copper in copper slag |
| CN108906332A (en) * | 2018-07-27 | 2018-11-30 | 广西大学 | A kind of zinc sulfide ore method for floating |
| CN109939831B (en) * | 2019-04-03 | 2024-04-26 | 成都市锐晨科技有限公司 | Automatic control heating and vulcanizing system for lead zinc oxide ores |
| CN112138855B (en) * | 2020-08-10 | 2021-12-28 | 西部矿业股份有限公司 | Method for recycling zinc oxygen pressure leaching sulfur flotation tailings |
| CN115445776B (en) * | 2022-08-11 | 2023-05-26 | 昆明理工大学 | Separation method applied to copper-lead bulk concentrate |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101451185A (en) * | 2007-11-28 | 2009-06-10 | 灵宝市金源矿业有限责任公司 | Comprehensive recovery method for ferro-sulphur ore containing copper, zinc and iron multi-metal |
| CN101690915A (en) * | 2009-09-30 | 2010-04-07 | 北京矿冶研究总院 | Method for separating copper-lead sulfide minerals |
| CN101693224A (en) * | 2009-09-30 | 2010-04-14 | 北京矿冶研究总院 | Method for separating copper-zinc sulfide minerals |
| CN101972703A (en) * | 2010-10-27 | 2011-02-16 | 株洲市湘麒科技开发有限公司 | Beneficiation method for recovering zinc, lead and silver from zinc leaching residue |
-
2012
- 2012-09-17 CN CN201210343398.XA patent/CN102824962B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101451185A (en) * | 2007-11-28 | 2009-06-10 | 灵宝市金源矿业有限责任公司 | Comprehensive recovery method for ferro-sulphur ore containing copper, zinc and iron multi-metal |
| CN101690915A (en) * | 2009-09-30 | 2010-04-07 | 北京矿冶研究总院 | Method for separating copper-lead sulfide minerals |
| CN101693224A (en) * | 2009-09-30 | 2010-04-14 | 北京矿冶研究总院 | Method for separating copper-zinc sulfide minerals |
| CN101972703A (en) * | 2010-10-27 | 2011-02-16 | 株洲市湘麒科技开发有限公司 | Beneficiation method for recovering zinc, lead and silver from zinc leaching residue |
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