CN102690947A - Smelting process of silver concentrate - Google Patents
Smelting process of silver concentrate Download PDFInfo
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- CN102690947A CN102690947A CN2012101630983A CN201210163098A CN102690947A CN 102690947 A CN102690947 A CN 102690947A CN 2012101630983 A CN2012101630983 A CN 2012101630983A CN 201210163098 A CN201210163098 A CN 201210163098A CN 102690947 A CN102690947 A CN 102690947A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
Abstract
The invention discloses a smelting process of a silver concentrate. The smelting process comprises the following steps: roasting the silver concentrate generated by a floatation process, carrying out sulfuric acid leaching and thiourea leaching, wherein silver deposition is performed by a copper replacement method corresponding to sulfuric acid leaching liquid, and silver-gold deposition is performed by an electrodeposition silver-gold deposition method corresponding to thiourea leaching liquid, and at last, smelting silver and gold metals generated by copper replacement silver deposition and electrodeposition silver-gold deposition to generate silver ingots and gold ingots. An ignition lost rate for roasting the silver concentrate reaches 50-55%. Through low-temperature roasting, valued metals such as silver and the like are enriched, so that the subsequent entity treatment quantity is correspondingly reduced to facilitate recycling the silver in the next step. Through two-step leaching of the sulfuric acid leaching and the thiourea leaching, the silver leaching rate is higher, leaching liquid-solid ratio is low, the leaching liquid concentration is high, and the investment of the device is less; meanwhile, the smelting process is beneficial to reducing environmental pollution and reducing safety hidden trouble.
Description
Technical field
The invention belongs to the technical field of smelting of non-ferrous metal, relate to a kind of smelting technology of silver preparation concentrate specifically.
Background technology
Produce great amount of high-temperature peracid leached mud (be called for short height and soak slag) in the zinc hydrometallurgy peracid extract technology production process; Height soaks valuable metals such as argentiferous in the slag, zinc, lead, copper, gold; Valuable metal content is low; About the average 200g/T of slag argentiferous, wherein zinc 5-6%, leaded 2-3%, cupric 0.3-0.4%, the height of present domestic high temperature peracid extract technology output soak slag and have reached annual more than 1,500,000 tons.Soak valuable metals such as silver in the slag, zinc, copper, gold for reclaiming height, improve the business economic benefit, reduce the pollution of waste sludge discharge, generally all take floatation process to reclaim the high silver in the slag that soaks environment.Reclaim the high silver in the slag that soaks through floatation process, investment is supported, is polluted less, cost is low, improves Enterprises'Competitiveness and resource utilization has obtained effect preferably for zinc hydrometallurgy enterprise.
In order further to improve the business economic benefit; Improve the market competitiveness of enterprise, operational path is economically and reasonably selected by enterprise on the basis of flotation silver preparation concentrate; Silver preparation concentrate is smelted; Produce silver ingot and ingot, and comprehensively reclaim valuable metals such as zinc in the silver preparation concentrate, copper, improve value-added content of product and have remarkable economic efficiency and social benefit.
At present, the valuable metal modes such as silver that reclaim both at home and abroad in the silver preparation concentrate are divided two types, i.e. direct method and indirect method.So-called direct method be exactly with the flotation silver preparation concentrate as main raw material, the method that the technology of selecting to suit is smelted valuable metals such as silver in the flotation silver preparation concentrate.Indirect method be exactly with the flotation silver preparation concentrate as less important raw material, add concentrate with the mode of batching, in copper, the plumbous anode sludge of smelting, reclaim silver.
1, direct method
According to the difference of the comprehensive way of recycling of flotation silver preparation concentrate, the special emphasis that valuable metals such as silver in the flotation silver preparation concentrate are reclaimed is different.Mainly contain following several kinds of technologies at present both at home and abroad;
(1) cyanide process; Being primarily aimed at auriferous silver preparation concentrate, is leaching agent with the sodium cyanide, sodium cyanide mass concentration 0.8%; PH10～12; Extraction time 36 hours.From leach liquor, reclaim silver with zinc replacement, again the substitute melting is produced silver ingot.
(2) thiocarbamide method; Be primarily aimed at the low silver preparation concentrate of cupric, leaching condition: PH1.5～2.0; Thiocarbamide mass concentration 10g/L; Liquid-solid ratio 10: 1; 40～60 ℃ of temperature; Extraction time 2 hours.From leach liquor, reclaim silver with zinc replacement, again the substitute melting is produced silver ingot.
(3) chlorination; Be primarily aimed at cupric height, leaded high concentrate, leaching condition: PH1.5～2.0; Sodium-chlor mass concentration 280-300g/L; 80～90 ℃ of temperature; Extraction time 2 hours.Reclaim silver, plumbous, copper from leach liquor again.
In addition, also have roasting → leaching → pyrogenic processes such as displacement → melting, wet method combined technology and other certain methods.
In a word, the special emphasis and the phase structure thereof that reclaim according to valuable metals such as silver in the flotation silver preparation concentrate determine concrete technical process.Direct method is primarily aimed at does not have copper, the plumbous enterprise that smelts, and at home and abroad the production capacity ratio is less.
2, indirect method
The flotation silver preparation concentrate is added copper, lead ore concentrate with the mode of preparing burden, in copper, plumbous technological process of smelting, reclaim.At present, silver preparation concentrate is smelted the main indirect method technology that adopts both at home and abroad.With Zhuzhou Smelter, Henan, Henan light gold lead be the enterprise of representative because plumbous the smelting all arranged itself, therefore, all adopt this mode; And the enterprise that does not have lead to smelt, the mode of mainly taking to sell silver preparation concentrate.
Summary of the invention
The present invention is in order to overcome the deficiency that prior art exists, provide a kind of facility investment few, do not have potential safety hazard, reduce environmental pollution, the smelting technology of economic benefit is high, silver ingot purity is high silver preparation concentrate.
The present invention realizes through following technical scheme: a kind of smelting technology of silver preparation concentrate, it comprises the steps:
(1) sinter process: adopt fluidizing reactor that silver preparation concentrate is carried out oxidizing roasting and produce calcining, baking flue gas feeds acid making system relieving haperacidity with pipeline;
(2) extract technology: (a) sulfuric acid leaches: calcining is leached through sulfuric acid produce sulphuric leachate and sulfuric acid leached mud; (b) thiocarbamide leaches: the sulfuric acid leached mud is leached through thiocarbamide produce thiocarbamide leach liquor and waste residue;
(3) heavy silver process: (a) the heavy silver of copper displacement: sulphuric leachate is adopted the heavy silver of copper method of replacing, send copper zinc recovery system further to reclaim copper and zinc through the liquid after the heavy silver of copper displacement; (b) the heavy silver gold of electrodeposition: the method for the heavy silver gold of thiocarbamide leach liquor employing electrodeposition is heavy silver-colored and golden, send Waste Water Treatment through the heavy silver gold of electrodeposition liquid afterwards;
(4) silver-colored gold refining: will pass through copper displacement heavy silver and metal silver-colored and that the heavy silver gold of electrodeposition produces and carry out melting, output silver ingot and ingot.
Described sinter process, the maturing temperature that silver preparation concentrate is carried out oxidizing roasting is 550～650 ℃, roasting time is 3～4 hours.
Described sulfuric acid leaches: solid-to-liquid ratio 1: 3～7, beginning acid 30～100g/L, eventually sour 5～30g/L, 60 ℃～90 ℃ of temperature of reaction, 2～6 hours reaction times; Described thiocarbamide leaches: solid-to-liquid ratio 1: 4～12, pH value 1.5～2.0,40 ℃～60 ℃ of temperature of reaction, 2～6 hours reaction times.
The invention has the beneficial effects as follows:
(1) silver preparation concentrate calorific value 2455 kcal/kg, silver preparation concentrate autogenous roasting is feasible.The roasting silver preparation concentrate burns the mistake rate and reaches 50～55%.Roasting not only makes valuable metal enrichments such as silver, makes the corresponding reduction of follow-up treatment capacity in kind, helps next step silver-colored recovery.
(2) baking flue gas feeds existing acid making system with pipeline, can reduce environmental pollution, has also realized the utilization again of resource simultaneously.
(3) calcining leaches silver, copper and zinc through sulfuric acid, obtains the leach liquor of argentiferous, copper, zinc, obtains silver-colored enriched substance through heavy silver and gives next step refining, and heavy silver back liquid send and reclaims copper zinc between integrated car.Behind sulfuric acid leaching silver, copper and the zinc, making the difficult silver that leaches in leached mud, obtain enrichment better, is that stepping recovery silver has been created better condition.
(4) can add cheap oxygenant in the thiocarbamide method leaching process, thiocarbamide can be recycled simultaneously, correspondingly can reduce cost.
(5) extract technology is taked twice leaching, and silver leaching rate is higher.
(6) in extract technology, the leaching liquid-solid ratio is low, leach liquor concentration high, and investment of devices is few.
(7) heavy silver process helps improving the purity of silver, reduces the refining difficulty.
(8) help reducing environmental pollution, reduce potential safety hazard.
Description of drawings
Fig. 1 is the smelting technology schema of silver preparation concentrate of the present invention.
Embodiment
Below in conjunction with accompanying drawing the present invention is described in detail.
Embodiment 1: as shown in Figure 1, and a kind of smelting technology of silver preparation concentrate, it comprises the steps:
(1) sinter process: adopt fluidizing reactor that silver preparation concentrate is carried out oxidizing roasting and produce calcining, 600 ℃ of maturing temperatures, 3.5 hours time; Baking flue gas feeds acid making system relieving haperacidity with pipeline;
(2) extract technology: (a) sulfuric acid leaches: calcining is leached through sulfuric acid produce sulphuric leachate and sulfuric acid leached mud, solid-to-liquid ratio 1: 6, the sour 50g/L that begins, whole sour 10g/L, 68 ℃ of temperature of reaction, 2.5 hours reaction times; (b) thiocarbamide leaches: the sulfuric acid leached mud is leached generation thiocarbamide leach liquor and waste residue, solid-to-liquid ratio 1: 6, pH value 1.6,50 ℃ of temperature of reaction, 5 hours reaction times through thiocarbamide;
(3) heavy silver process: (a) the heavy silver of copper displacement: sulphuric leachate is adopted the heavy silver of copper method of replacing, send copper zinc recovery system further to reclaim copper and zinc through the liquid after the heavy silver of copper displacement; (b) the heavy silver gold of electrodeposition: the method for the heavy silver gold of thiocarbamide leach liquor employing electrodeposition is heavy silver-colored and golden, send Waste Water Treatment through the heavy silver gold of electrodeposition liquid afterwards;
(4) silver-colored gold refining: will pass through copper displacement heavy silver and metal silver-colored and that the heavy silver gold of electrodeposition produces and carry out melting, output silver ingot and ingot.
Embodiment 2: other step is identical with embodiment 1, and difference is:
In sinter process step (1): the 3.8 hours oxidizing roasting time under 560 ℃ of conditions;
In extract technology step (2): (a) sulfuric acid leaches: calcining is leached through sulfuric acid produce sulphuric leachate and sulfuric acid leached mud, solid-to-liquid ratio 1: 5, the sour 70g/L that begins, whole sour 15g/L, 75 ℃ of temperature of reaction, 4 hours reaction times; (b) thiocarbamide leaches: the sulfuric acid leached mud is leached generation thiocarbamide leach liquor and waste residue, solid-to-liquid ratio 1: 8, pH value 1.8,55 ℃ of temperature of reaction, 3 hours reaction times through thiocarbamide.
Embodiment 3: other step is identical with embodiment 1, and difference is:
In sinter process step (1): the 3.2 hours oxidizing roasting time under 620 ℃ of conditions;
In extract technology step (2): (a) sulfuric acid leaches: calcining is leached through sulfuric acid produce sulphuric leachate and sulfuric acid leached mud, solid-to-liquid ratio 1: 4, the sour 90g/L that begins, whole sour 25g/L, 82 ℃ of temperature of reaction, 3 hours reaction times; (b) thiocarbamide leaches: the sulfuric acid leached mud is leached generation thiocarbamide leach liquor and waste residue, solid-to-liquid ratio 1: 10, pH value 1.7,45 ℃ of temperature of reaction, 4 hours reaction times through thiocarbamide.
Claims (3)
1. the smelting technology of a silver preparation concentrate, it comprises the steps:
(1) sinter process: adopt fluidizing reactor that silver preparation concentrate is carried out oxidizing roasting and produce calcining, baking flue gas feeds acid making system relieving haperacidity with pipeline;
(2) extract technology: (a) sulfuric acid leaches: calcining is leached through sulfuric acid produce sulphuric leachate and sulfuric acid leached mud; (b) thiocarbamide leaches: the sulfuric acid leached mud is leached through thiocarbamide produce thiocarbamide leach liquor and waste residue;
(3) heavy silver process: (a) the heavy silver of copper displacement: sulphuric leachate is adopted the heavy silver of copper method of replacing, send copper zinc recovery system further to reclaim copper and zinc through the liquid after the heavy silver of copper displacement; (b) the heavy silver gold of electrodeposition: the method for the heavy silver gold of thiocarbamide leach liquor employing electrodeposition is heavy silver-colored and golden, send Waste Water Treatment through the heavy silver gold of electrodeposition liquid afterwards;
(4) silver-colored gold refining: will pass through copper displacement heavy silver and metal silver-colored and that the heavy silver gold of electrodeposition produces and carry out melting, output silver ingot and ingot.
2. the smelting technology of silver preparation concentrate according to claim 1 is characterized in that: described sinter process, and the maturing temperature that silver preparation concentrate is carried out oxidizing roasting is 550～650 ℃, roasting time is 3～4 hours.
3. the smelting technology of silver preparation concentrate according to claim 1 and 2 is characterized in that: described sulfuric acid leaching: solid-to-liquid ratio 1: 3～7, beginning acid 30～100g/L, eventually sour 5～30g/L, 60 ℃～90 ℃ of temperature of reaction, 2～6 hours reaction times; Described thiocarbamide leaches: solid-to-liquid ratio 1: 4～12, pH value 1.5～2.0,40 ℃～60 ℃ of temperature of reaction, 2～6 hours reaction times.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012101630983A CN102690947A (en) | 2012-05-24 | 2012-05-24 | Smelting process of silver concentrate |
| CN2012104217850A CN103243349A (en) | 2012-05-24 | 2012-10-30 | Comprehensive zinc hydrometallurgy recovery system technique |
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| CN2012101630983A CN102690947A (en) | 2012-05-24 | 2012-05-24 | Smelting process of silver concentrate |
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| CN102690947A true CN102690947A (en) | 2012-09-26 |
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| CN2012101630983A Pending CN102690947A (en) | 2012-05-24 | 2012-05-24 | Smelting process of silver concentrate |
| CN2012104217850A Pending CN103243349A (en) | 2012-05-24 | 2012-10-30 | Comprehensive zinc hydrometallurgy recovery system technique |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104032145A (en) * | 2014-06-23 | 2014-09-10 | 贵州顶效开发区宏达金属综合回收有限公司 | Method for extracting and separating Ag and Cu from flotation silver concentrate |
| CN106676279A (en) * | 2017-01-13 | 2017-05-17 | 昆明理工大学 | Method for recycling silver through wet-process leaching |
| CN108070712A (en) * | 2017-12-15 | 2018-05-25 | 郴州市金贵银业股份有限公司 | The recovery method of valuable metal in a kind of silver electrolysis mother liquor purification slag |
| CN111778406A (en) * | 2019-08-27 | 2020-10-16 | 昆明理工大学 | Comprehensive utilization method of zinc roasting oxidation waste residue |
| CN112708772A (en) * | 2020-12-23 | 2021-04-27 | 紫金矿业集团股份有限公司 | Method for high-valued and synergistic dechlorination of zinc smelting intermediate material |
| CN113403483A (en) * | 2021-05-26 | 2021-09-17 | 来宾华锡冶炼有限公司 | Method for extracting silver from high-iron, high-tin and high-indium flotation silver concentrate |
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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 |
| CN111349794B (en) * | 2019-12-06 | 2022-04-12 | 中国船舶重工集团公司七五0试验场 | Automatic control method for lead-zinc ore smelting and selecting combined process |
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| CN100374589C (en) * | 2006-06-07 | 2008-03-12 | 祥云县飞龙实业有限责任公司 | Combined process for organic solvent extracting zinc and wet zinc refining |
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2012
- 2012-05-24 CN CN2012101630983A patent/CN102690947A/en active Pending
- 2012-10-30 CN CN2012104217850A patent/CN103243349A/en active Pending
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104032145A (en) * | 2014-06-23 | 2014-09-10 | 贵州顶效开发区宏达金属综合回收有限公司 | Method for extracting and separating Ag and Cu from flotation silver concentrate |
| CN104032145B (en) * | 2014-06-23 | 2015-07-29 | 贵州顶效开发区宏达金属综合回收有限公司 | The method of a kind of extraction and isolation Ag, Cu from flotation of silver concentrate |
| CN106676279A (en) * | 2017-01-13 | 2017-05-17 | 昆明理工大学 | Method for recycling silver through wet-process leaching |
| CN108070712A (en) * | 2017-12-15 | 2018-05-25 | 郴州市金贵银业股份有限公司 | The recovery method of valuable metal in a kind of silver electrolysis mother liquor purification slag |
| CN108070712B (en) * | 2017-12-15 | 2019-12-03 | 郴州市金贵银业股份有限公司 | A kind of silver is electrolysed the recovery method of valuable metal in mother liquor purification slag |
| CN111778406A (en) * | 2019-08-27 | 2020-10-16 | 昆明理工大学 | Comprehensive utilization method of zinc roasting oxidation waste residue |
| CN111778406B (en) * | 2019-08-27 | 2021-10-26 | 昆明理工大学 | Comprehensive utilization method of zinc roasting oxidation waste residue |
| CN112708772A (en) * | 2020-12-23 | 2021-04-27 | 紫金矿业集团股份有限公司 | Method for high-valued and synergistic dechlorination of zinc smelting intermediate material |
| CN113403483A (en) * | 2021-05-26 | 2021-09-17 | 来宾华锡冶炼有限公司 | Method for extracting silver from high-iron, high-tin and high-indium flotation silver concentrate |
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| CN103243349A (en) | 2013-08-14 |
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Application publication date: 20120926 |