CN101658819A - Multielement composite recovery process - Google Patents
Multielement composite recovery process Download PDFInfo
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- CN101658819A CN101658819A CN200910017384A CN200910017384A CN101658819A CN 101658819 A CN101658819 A CN 101658819A CN 200910017384 A CN200910017384 A CN 200910017384A CN 200910017384 A CN200910017384 A CN 200910017384A CN 101658819 A CN101658819 A CN 101658819A
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Abstract
The invention relates to a multielement composite recovery process, which consists of lead concentrate recovery, copper-zinc concentrate recovery and sulphur concentrate recovery. The main process forfloatation comprises primary crude selection, secondary filtration and secondary fine recovery, and thereby the multielement composite recovery process is simple, has high recovery efficiency, and isparticularly suitable for recovering copper, lead, zinc, sulphur and other valuable elements.
Description
Technical field:
The present invention relates to a kind of technology of comprehensive recovery, the technology that particularly a kind of multielement composite reclaims.
Background technology:
The method that China adopts the refined gold ore cyaniding extraction of gold process directly to produce gold accounts for the half of the country that gold industry is produced.But contain valuable elements such as a large amount of copper, lead, zinc in the cyanidation tailings, at present, domestic most of cyanide plant do not possess the multielement composite recovering condition, cause a large amount of wastings of resources, though, there is part producer that these elements are reclaimed now, but, its complex process, the rate of recovery is low.
Summary of the invention:
Purpose of the present invention be exactly to provide a kind of and economize on resources, technology that technology is simple, the rate of recovery is high multielement composite reclaims.
The object of the present invention is achieved like this: the technology that a kind of multielement composite reclaims is characterized in that it has following steps to finish:
(1) lead concentrate reclaims: cyanidation tailings is squeezed in the filter press dashpot through peristaltic pump, take off through plate and frame type filter-press and to contain the cyanogen lean solution, produce filter cake, lean solution is returned cyanidation system, and filter cake is delivered to dashpot by belt and sizes mixing, and adds diethyldithiocarbamate, the ratio of diethyldithiocarbamate and filter cake is that filter cake per ton adds diethyldithiocarbamate 4.5-5.5g, the ore pulp that mixes up flows automatically in the inflation agitated flotation cell, through one thick, two sweep, behind two cleaner flotations, flotation obtains lead concentrate;
(2) copper zinc concentrate, sulphur concentrate reclaim: the tailings behind the flotation of lead concentrate is squeezed into activated bath by the slag stock pump and is added the hydrogen peroxide activation, the hydrogen peroxide soak time is 25-35 minute, add xanthate and Z200 again, ore pulp flows in the inflation agitated flotation cell, through one thick, two sweep, behind two cleaner flotations, obtain the copper zinc concentrate, its mine tailing is as final sulphur concentrate.
The present invention compared with prior art has the following advantages:
Because the method that adopts segmentation to reclaim, promptly reclaim the method that lead concentrate, back reclaim copper zinc concentrate, sulphur concentrate earlier, thereby, economize on resources, technology is simple, the rate of recovery is high.
The specific embodiment:
Embodiment one:
The cyanidation tailings that is numbered Al batch is handled.This tailings is 600 tons, and copper content is 0.31%, lead content is 0.71%, zinc content is 0.68%, sulfur content is 27.49%.Cyanidation tailings is squeezed into Ф 3*4 filter press dashpot through the 2RGB75 peristaltic pump, take off through the XAZ240 plate and frame type filter-press and to contain the cyanogen lean solution, lean solution is returned cyanidation system, filter cake is delivered to Ф 2*2 dashpot by belt and sizes mixing, after adding diethyldithiocarbamate, flow automatically in the BSK-4 inflation agitated flotation cell, through one thick, two sweep, behind two cleaner flotations, diffeential floatation obtains lead concentrate; Its tailings is squeezed into Ф 4*5 activated bath by 65EGB slag stock pump and is activated through hydrogen peroxide, after adding xanthate and Z200, flow into certainly in the BSK-4 inflation agitated flotation cell, through one thick, two sweep, behind two cleaner flotations, obtain copper and zinc bulk concentrate, its mine tailing is as final sulphur ore deposit.
Tailings is after filter-press dehydration is sized mixing, and concentration is 22%, and the diethyldithiocarbamate consumption joins in the ore pulp according to the standard of 5g/t, through one thick, two sweep, two cleaner flotations obtain lead concentrate, grade is 41%, the rate of recovery is 56.36%; The floating tail of lead concentrate added the hydrogen peroxide activation of 9-10kg/t after 30 minutes, added butyl xanthate, the 40-50g/tZ200 of 10g/t, through after the flotation, obtain copper and zinc bulk concentrate, copper content is 9.60%, and zinc content is 25.12%, its mine tailing is as final sulphur ore deposit, and the content of sulphur is 29.14%; The bulk concentrate dehydration is sized mixing, and concentration is 10%, adds 10kg/t zinc sulfate and 3kg/t Cymag and suppresses the zinc stirring after 60 minutes, adds the Z200 of 30g/t, after flotation, obtains copper concentrate and zinc concentrate respectively, and its content is respectively copper 16.66%, zinc 45.21%.
Embodiment two:
The cyanidation tailings that is numbered A2 batch is handled.This tailings is 600 tons, and copper content is 0.29%, lead content is 0.69%, zinc content is 0.78%, sulfur content is 28.63%.Cyanidation tailings is squeezed into Ф 3*4 filter press dashpot through the 2RGB75 peristaltic pump, take off through the XAZ240 plate and frame type filter-press and to contain the cyanogen lean solution, lean solution is returned cyanidation system, filter cake is delivered to Ф 2*2 dashpot by belt and sizes mixing, after adding diethyldithiocarbamate, flow automatically in the BSK-4 inflation agitated flotation cell, through one thick, two sweep, behind two cleaner flotations, diffeential floatation obtains lead concentrate; Its tailings is squeezed into Ф 4*5 activated bath by 65EGB slag stock pump and is activated through hydrogen peroxide, after adding xanthate and Z200, flow into certainly in the BSK-4 inflation agitated flotation cell, through one thick, two sweep, behind two cleaner flotations, obtain copper and zinc bulk concentrate, its mine tailing is as final sulphur ore deposit.
Tailings is after filter-press dehydration is sized mixing, and concentration is 22%, and the diethyldithiocarbamate consumption joins in the ore pulp according to the standard of 5g/t, through one thick, two sweep, two cleaner flotations obtain lead concentrate, grade is 40.91%, the rate of recovery is 55.27%; The floating tail of lead concentrate added the hydrogen peroxide activation of 9-10kg/t after 30 minutes, added butyl xanthate, the 40-50g/tZ200 of 10g/t, through after the flotation, obtain copper and zinc bulk concentrate, copper content is 8.90%, and zinc content is 27.53%, its mine tailing is as final sulphur ore deposit, and the content of sulphur is 28.74%; The bulk concentrate dehydration is sized mixing, and concentration is 10%, adds 10kg/t zinc sulfate and 3kg/t Cymag and suppresses the zinc stirring after 59 minutes, adds the Z200 of 30g/t, after flotation, obtains copper concentrate and zinc concentrate respectively, and its content is respectively copper 15.94%, zinc 43.75%.
Embodiment three:
The cyanidation tailings that is numbered A3 batch is handled.This tailings is 800 tons, and copper content is 0.30%, lead content is 0.74%, zinc content is 0.81%, sulfur content is 25.47%.Cyanidation tailings is squeezed into Ф 3*4 filter press dashpot through the 2RGB75 peristaltic pump, take off through the XAZ240 plate and frame type filter-press and to contain the cyanogen lean solution, lean solution is returned cyanidation system, filter cake is delivered to Ф 2*2 dashpot by belt and sizes mixing, after adding diethyldithiocarbamate, flow automatically in the BSK-4 inflation agitated flotation cell, through one thick, two sweep, behind two cleaner flotations, diffeential floatation obtains lead concentrate; Its tailings is squeezed into Ф 4*5 activated bath by 65EGB slag stock pump and is activated through hydrogen peroxide, after adding xanthate and Z200, flow into certainly in the BSK-4 inflation agitated flotation cell, through one thick, two sweep, behind two cleaner flotations, obtain copper and zinc bulk concentrate, its mine tailing is as final sulphur ore deposit.
Tailings is after filter-press dehydration is sized mixing, and concentration is 21%, and the diethyldithiocarbamate consumption joins in the ore pulp according to the standard of 5g/t, through one thick, two sweep, two cleaner flotations obtain lead concentrate, grade is 44.38%, the rate of recovery is 55.69%; The floating tail of lead concentrate added the hydrogen peroxide activation of 9-10kg/t after 30 minutes, added butyl xanthate, the 40-50g/tZ200 of 10g/t, through after the flotation, obtain copper and zinc bulk concentrate, copper content is 9.11%, and zinc content is 26.98%, its mine tailing is as final sulphur ore deposit, and the content of sulphur is 28.58%; The bulk concentrate dehydration is sized mixing, and concentration is 10%, adds 10kg/t zinc sulfate and 3kg/t Cymag and suppresses the zinc stirring after 65 minutes, adds the Z200 of 30g/t, after flotation, obtains copper concentrate and zinc concentrate respectively, and its content is respectively copper 15.97%, zinc 43.67%.
Claims (1)
- The technology that a kind of multielement composite reclaims is characterized in that it has following steps to finish:1, lead concentrate reclaims: cyanidation tailings is squeezed in the filter press dashpot through peristaltic pump, take off through plate and frame type filter-press and to contain the cyanogen lean solution, produce filter cake, lean solution is returned cyanidation system, and filter cake is delivered to dashpot by belt and sizes mixing, and adds diethyldithiocarbamate, the ratio of diethyldithiocarbamate and filter cake is that filter cake per ton adds diethyldithiocarbamate 4.5-5.5g, the ore pulp that mixes up flows automatically in the inflation agitated flotation cell, through one thick, two sweep, behind two cleaner flotations, flotation obtains lead concentrate;2, copper zinc concentrate, sulphur concentrate reclaim: the tailings behind the flotation of lead concentrate is squeezed into activated bath by the slag stock pump and is added the hydrogen peroxide activation, the hydrogen peroxide soak time is 25-35 minute, add xanthate and Z200 again, ore pulp flows in the inflation agitated flotation cell, through one thick, two sweep, behind two cleaner flotations, obtain the copper zinc concentrate, its mine tailing is as final sulphur concentrate.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910017384A CN101658819A (en) | 2009-08-03 | 2009-08-03 | Multielement composite recovery process |
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| CN200910017384A CN101658819A (en) | 2009-08-03 | 2009-08-03 | Multielement composite recovery process |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102513219A (en) * | 2011-12-19 | 2012-06-27 | 云南澜沧铅矿有限公司 | Beneficiation reagent for separating lead zinc ores from lead zinc sulphide ores containing carbon and beneficiation method |
| CN102513215A (en) * | 2011-12-09 | 2012-06-27 | 紫金矿业集团股份有限公司 | Method for separating gold, silver and other metals and sulfur from waste cyanide tailings by floatation |
| CN102784713A (en) * | 2012-07-18 | 2012-11-21 | 山东国大黄金股份有限公司 | Method for recycling multiple elements of liquid after cyanided tailing flotation |
| CN103255285A (en) * | 2013-05-17 | 2013-08-21 | 招金矿业股份有限公司金翅岭金矿 | Lead-zinc-silver mixed concentrate comprehensive recovering method |
| CN104080541A (en) * | 2012-01-27 | 2014-10-01 | 赢创德固赛有限公司 | Enrichment of metal sulfide ores by oxidant assisted froth flotation |
| CN107952577A (en) * | 2017-11-30 | 2018-04-24 | 长沙三博矿业科技有限公司 | Difficulty selects cyanidation tailings preprocess method |
-
2009
- 2009-08-03 CN CN200910017384A patent/CN101658819A/en active Pending
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102513215A (en) * | 2011-12-09 | 2012-06-27 | 紫金矿业集团股份有限公司 | Method for separating gold, silver and other metals and sulfur from waste cyanide tailings by floatation |
| CN102513219A (en) * | 2011-12-19 | 2012-06-27 | 云南澜沧铅矿有限公司 | Beneficiation reagent for separating lead zinc ores from lead zinc sulphide ores containing carbon and beneficiation method |
| CN104080541A (en) * | 2012-01-27 | 2014-10-01 | 赢创德固赛有限公司 | Enrichment of metal sulfide ores by oxidant assisted froth flotation |
| CN104080541B (en) * | 2012-01-27 | 2016-10-19 | 赢创德固赛有限公司 | The foam flotation method sulphide-rich Ore assisted by oxidant |
| CN102784713A (en) * | 2012-07-18 | 2012-11-21 | 山东国大黄金股份有限公司 | Method for recycling multiple elements of liquid after cyanided tailing flotation |
| CN102784713B (en) * | 2012-07-18 | 2013-12-04 | 山东国大黄金股份有限公司 | Method for recycling multiple elements of liquid after cyanided tailing flotation |
| CN103255285A (en) * | 2013-05-17 | 2013-08-21 | 招金矿业股份有限公司金翅岭金矿 | Lead-zinc-silver mixed concentrate comprehensive recovering method |
| CN103255285B (en) * | 2013-05-17 | 2014-10-22 | 招金矿业股份有限公司金翅岭金矿 | Lead-zinc-silver mixed concentrate comprehensive recovering method |
| CN107952577A (en) * | 2017-11-30 | 2018-04-24 | 长沙三博矿业科技有限公司 | Difficulty selects cyanidation tailings preprocess method |
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Application publication date: 20100303 |