CN108048659B - Leaching method of zinc replacement slag - Google Patents
Leaching method of zinc replacement slag Download PDFInfo
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- CN108048659B CN108048659B CN201711172917.XA CN201711172917A CN108048659B CN 108048659 B CN108048659 B CN 108048659B CN 201711172917 A CN201711172917 A CN 201711172917A CN 108048659 B CN108048659 B CN 108048659B
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
- C22B7/006—Wet processes
- C22B7/007—Wet processes by acid leaching
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B15/00—Obtaining copper
- C22B15/0063—Hydrometallurgy
- C22B15/0065—Leaching or slurrying
- C22B15/0067—Leaching or slurrying with acids or salts thereof
- C22B15/0071—Leaching or slurrying with acids or salts thereof containing sulfur
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B19/00—Obtaining zinc or zinc oxide
- C22B19/20—Obtaining zinc otherwise than by distilling
- C22B19/22—Obtaining zinc otherwise than by distilling with leaching with acids
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B19/00—Obtaining zinc or zinc oxide
- C22B19/30—Obtaining zinc or zinc oxide from metallic residues or scraps
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
- C22B3/06—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic acid solutions, e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions
- C22B3/08—Sulfuric acid, other sulfurated acids or salts thereof
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/44—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes
- C22B3/46—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes by substitution, e.g. by cementation
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B41/00—Obtaining germanium
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B58/00—Obtaining gallium or indium
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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
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Abstract
The invention relates to a leaching method of zinc replacement slag, which comprises the following steps: first-stage leaching: pulping a solution containing 40-140g/L sulfuric acid and zinc replacement slag, carrying out oxygen pressure leaching after pulping, and carrying out solid-liquid separation to obtain a first-stage leachate and a first-stage leaching slag, wherein the first-stage leachate is used for recovering valuable metals; secondary leaching: pulping the solution containing 120-180g/L sulfuric acid and the first-stage leaching residue, performing oxygen pressure leaching after pulping, performing solid-liquid separation to obtain a second-stage leaching solution and a second-stage leaching residue, and returning the second-stage leaching solution to the first-stage leaching for pulping; three-stage leaching: pulping the sulfuric acid solution with the concentration of 140-250g/L and the second-stage leaching residue, stirring and leaching after pulping, performing solid-liquid separation to obtain a third-stage leaching solution and a third-stage leaching residue, and returning the third-stage leaching solution to the second-stage leaching for pulping. The leaching method of the zinc replacement slag has the advantages of high leaching rate, small environmental pollution, recyclable leaching solution and low treatment cost.
Description
Technical Field
The invention belongs to the technical field of wet metallurgy, and particularly relates to a leaching method of zinc replacement slag.
Background
At present, zinc hydrometallurgy mainly comprises two processes of conventional leaching and oxygen pressure leaching. The oxygen pressure leaching process has the advantages of high zinc leaching rate, simple process, less investment, environmental friendliness, high comprehensive recycling degree of associated metals and the like, and is widely applied to various sulfide mixed ores.
The oxygen pressure leaching process of zinc concentrate is to perform acid leaching of ore pulp under certain temperature and oxygen partial pressure conditions, to control leaching conditions to make zinc and associated metals enter sulfuric acid solution, and then to add zinc powder for replacement to make associated valuable metals precipitate and enrich to form zinc replacement slag with high added value. The zinc replacement slag is generally rich in 0.2-0.7% of valuable metal gallium, 0.1-0.8% of germanium, 0.01-0.2% of indium, 5-15% of copper, 5-20% of zinc, 3-10% of iron and 5-10% of impurity silicon dioxide.
The zinc replacement slag is treated by a pyrogenic volatilization or wet leaching method, wherein the pyrogenic volatilization is to send the replacement slag into equipment such as a rotary kiln, a side-blown furnace and the like for high-temperature treatment so as to volatilize valuable metals, and then sulfuric acid is used for leaching smoke dust, and although the technology of cremation volatilization is simple, the technology has large environmental pollution, high energy consumption and high cost because valuable metals are dispersed, and matched environmental protection facilities and the like need to be built; the wet treatment mostly adopts a sulfuric acid leaching process, the process flow can be used as a part of a zinc hydrometallurgy system to form system complementation and is environment-friendly, but the leaching rate of valuable metals is usually not high due to the difficulty of separation of metal germanium and the like caused by high silicon in the replacement slag.
Disclosure of Invention
Accordingly, an object of the present invention is to provide a method for leaching zinc-substituted slag, which has advantages of high leaching rate, low environmental pollution, recyclable leachate, and low treatment cost.
The technical scheme adopted by the invention is as follows:
a leaching method of zinc replacement slag sequentially comprises the following steps:
first-stage leaching: pulping the first-stage pulping liquid and the zinc replacement residues, carrying out oxygen pressure leaching on the pulped slurry, and carrying out solid-liquid separation on the leached slurry to obtain a first-stage leachate and a first-stage leaching residue, wherein the first-stage leachate is used for recovering valuable metals;
secondary leaching: pulping the second-stage pulping liquid and the first-stage leaching residues, carrying out oxygen pressure leaching on the pulped pulp, and carrying out solid-liquid separation on the leached pulp to obtain a second-stage leaching liquid and second-stage leaching residues;
three-stage leaching: pulping the three-stage pulping liquid and the two-stage leaching residue, leaching the pulped pulp under stirring, and performing solid-liquid separation on the leached pulp to obtain three-stage leaching liquid and three-stage leaching residue;
the first-stage slurry is a solution containing 40-140g/L sulfuric acid or a second-stage leaching solution; the second-stage slurry solution is a solution containing 120-180g/L sulfuric acid or a third-stage leaching solution; the three-stage slurry solution is a sulfuric acid solution with the concentration of 140-250 g/L.
The leaching method can leach and extract valuable metals of gallium (Ga), germanium (Ge), indium (In), copper (Cu), zinc (Zn) and iron (Fe) from zinc replacement slag, and after the three leaching stages are processed, the leaching rate of gallium is more than 98%, the leaching rate of germanium is more than 80%, the leaching rate of indium is more than 99%, the leaching rate of copper is more than 98%, the leaching rate of zinc is more than 95%, and the leaching rate of iron is more than 98%.
Wherein, the first-stage leaching and the second-stage leaching are oxygen pressure leaching, under a certain oxygen pressure condition, metals, metal oxides, metal sulfides and the like in the zinc replacement slag can fully react with sulfuric acid, and most valuable metal ions in the slag are leached; the third-stage leaching is agitation leaching, which mainly washes valuable metal ions carried in the slag into the third-stage leaching liquid, and enables the valuable metals which are not leached in the first-stage leaching and the second-stage leaching to be leached out to the maximum extent. The main chemical reactions that take place in the three leaching stages are as follows:
2Cu+2H2SO4+O2＝2CuSO4+2H2O
2Zn+2H2SO4+O2＝2ZnSO4+2H2O
Ga2O3+3H2SO4＝Ga2(SO4)3+3H2O
3GeS2+10O2＝Ge(SO4)2+4SO2+2GeO2
GeS2+Ge(SO4)2+2O2＝4SO2+2GeO2
GeO2+H2SO4＝GeSO4+2H2O
ZnO·GeO2+H2SO4＝H2GeO3+ZnSO4
FeO·GeO2+H2SO4＝H2GeO3+FeSO4
2In+3O2+6H2SO4＝2In2(SO4)3+6H2O
In2O3+3H2SO4＝In2(SO4)3+3H2O
according to the invention, the zinc replacement slag with the highest valuable metal content is leached by using the solution with the lowest sulfuric acid concentration, the primary leaching slag with the higher valuable metal content is leached by using the solution with the higher sulfuric acid concentration, and the secondary leaching slag with the low valuable metal content is leached by using the solution with the highest sulfuric acid concentration, so that the reaction can be controlled, the leaching difficulty is reduced, the valuable metals are fully leached section by section, and the utilization rate of the sulfuric acid solution is improved.
The solution used in the three leaching sections is reasonably arranged according to the sulfuric acid concentration gradient of 40-140g/L, 120-180g/L and 140-250g/L, so that the sulfuric acid concentration of the second-section leaching solution can meet the requirement of the first-section leaching and can be directly returned to the first-section leaching for use, and the sulfuric acid concentration of the third-section leaching solution can meet the requirement of the second-section leaching and can be directly returned to the second-section leaching for use, thereby forming a three-section countercurrent leaching process, further improving the utilization rate of the sulfuric acid solution and reducing the treatment cost. The first-stage leaching solution is rich in valuable metal ions and is sent to a separation and enrichment working section for recovering the valuable metals, the third-stage leaching solution uses a high-concentration sulfuric acid solution which is input from the outside of the system and does not contain the valuable metal ions, the valuable metal ions carried in the second-stage leaching slag can be thoroughly washed out, the valuable metals which are not leached in the slag can be leached out to the maximum extent, and the leaching rate is effectively improved.
Compared with a pyrogenic process volatilization process, the method disclosed by the invention has the advantages that the zinc replacement slag is leached by adopting a sulfuric acid wet method, the environmental pollution is less, matched environment-friendly facilities do not need to be built, and the energy consumption is lower. Compared with the common one-stage wet leaching process, the three-stage countercurrent leaching process is adopted, so that the higher leaching rate can be achieved, and the leachate can be recycled, thereby being beneficial to reducing the treatment cost.
Further, in the first-stage leaching, 1-6 liters of first-stage slurry is used for pulping every 1 kg of zinc replacement slag, and the concentration of sulfuric acid in the obtained first-stage leaching solution is 5-30 g/L.
Further, in the first-stage leaching, the slurried slurry is pumped into an oxygen pressure pump for oxygen pressure leaching, and the flow of oxygen introduced into an oxygen pressure kettle is 20-120Nm3The pressure in the kettle is 0.1-0.5Mpa, the leaching temperature is 60-140 ℃, and the leaching time is 1-6 hours.
Further, in the second-stage leaching, 1-10 liters of second-stage slurry liquid is used for pulping every 1 kg of first-stage leaching slag, and the concentration of sulfuric acid in the obtained second-stage leaching liquid is 40-140 g/L.
Further, in the second-stage leaching, the slurried slurry is pumped into an oxygen pressure pump for oxygen pressure leaching, and the flow of oxygen introduced into an oxygen pressure kettle is 20-120Nm3The pressure in the kettle is 0.1-0.5Mpa, the leaching temperature is 60-140 ℃, and the leaching time is 1-6 hours.
Further, in the three-stage leaching, 1-10 liters of three-stage slurry liquid is used for slurrying every 1 kg of two-stage leaching slag, and the concentration of sulfuric acid in the obtained three-stage leaching liquid is 120-180 g/L.
Further, in three-stage leaching, slurried slurry is pumped into a stirring barrel to be leached under stirring, the leaching temperature is 60-90 ℃, and the leaching time is 1-6 hours.
Through reasonably setting the technological parameters of the liquid-solid ratio of the slurrying liquid to the slag leached by each section, the leaching temperature, the leaching time and the like, the reactions of all the sections can be controlled to be smoothly carried out, the sulfuric acid concentration of the leachate of each section is ensured to be maintained in an appropriate range, the normal continuous leaching production is facilitated, the smooth operation of a leaching system is ensured, and the leaching rate is improved.
Further, the method also comprises a pretreatment step before the first-stage leaching, wherein the pretreatment step comprises the following steps: baking the zinc replacement slag in oxygen-containing atmosphere, and grinding for later use after baking.
In the baking treatment of the pretreatment, oxygen is utilized to oxidize metallic zinc, copper, iron and the like in the zinc replacement slag into metallic oxides, so that the subsequent sulfuric acid solution is conveniently leached, part of slag is agglomerated after being baked at high temperature, and the agglomeration can be broken by grinding treatment, so that the slurrying effect is improved, the surface area of the material can be increased, and the improvement of the leaching rate is greatly facilitated.
Further, the baking temperature of the pretreatment is 250-700 ℃, the baking time is 2-8 hours, and the grinding particle size is 50-300 μm.
Further, the zinc replacement slag contains, by mass, 0.2-0.7% of gallium, 0.1-0.8% of germanium, 0.01-0.2% of indium, 5-15% of copper, 5-20% of zinc, 3-10% of iron, and 5-10% of silicon dioxide.
For a better understanding and practice, the invention is described in detail below with reference to the accompanying drawings.
Drawings
Fig. 1 is a process flow diagram of the leaching method of zinc replacement slag of the present invention.
Detailed Description
Example 1
As shown in fig. 1, in this embodiment, the zinc replacement slag is leached, and the zinc replacement slag contains, by mass, 0.45% of gallium, 0.45% of germanium, 0.1% of indium, 8% of copper, 16.9% of zinc, 3% of iron, and 10.3% of silicon dioxide, and the specific steps are as follows:
(1) pretreatment: baking the zinc replacement slag in an oxygen-containing atmosphere at the baking temperature of 300 ℃ for 2 hours, and grinding the baked zinc replacement slag by a grinder until the particle size is 200 meshes for later use.
(2) First-stage leaching: the pretreated zinc replacement slag was slurried with 3 liters of a solution containing 100g/L sulfuric acid or a secondary leach solution per 1 kg. Pumping the slurried slurry into an oxygen autoclave for leaching, wherein the flow of oxygen introduced into the oxygen autoclave is 20-120Nm3The pressure in the kettle is 0.2Mpa, the leaching temperature is 80 ℃, and the leaching time is 2 hours. And then carrying out solid-liquid separation on the leaching slurry to obtain a first-stage leaching solution and a first-stage leaching residue, wherein the first-stage leaching solution is sent to a separation and enrichment working section for recovering valuable metals, and the concentration of sulfuric acid contained in the first-stage leaching solution is 8 g/L.
(3) Secondary leaching: the first leaching residue (1 kg) was slurried with 8 liters of a solution containing 121g/L sulfuric acid or a three-stage leaching solution. Pumping the slurried slurry into an oxygen autoclave for leaching, wherein the flow of oxygen introduced into the oxygen autoclave is 20-120Nm3The pressure in the kettle is 0.2Mpa, the leaching temperature is 90 ℃, and the leaching time is 6 hours. And then carrying out solid-liquid separation on the leached slurry to obtain a second-stage leachate and second-stage leached residues, wherein the second-stage leachate is returned to the first-stage leaching for slurrying, and the concentration of sulfuric acid contained in the second-stage leachate is 98 g/L.
(4) Three-stage leaching: the two-stage leaching residue of 1 kg is pulped by using 10 liters of sulfuric acid solution with the concentration of 140 g/L. Pumping the pulped slurry into a stirring barrel to be leached under stirring, wherein the leaching temperature is 90 ℃, and the leaching time is 4 hours. And then carrying out solid-liquid separation on the leached slurry to obtain three-stage leachate and three-stage leached residues, returning the three-stage leachate to the second-stage leaching for slurrying, wherein the concentration of sulfuric acid contained in the three-stage leachate is 125g/L, and piling or retreating the three-stage leached residues.
After the pretreatment and the treatment of the three leaching stages, the leaching rate of gallium in the zinc replacement slag reaches 98.9%, the leaching rate of germanium reaches 81.5%, the leaching rate of indium reaches 99.6%, the leaching rate of copper reaches 98.2%, the leaching rate of zinc reaches 95.1%, and the leaching rate of iron reaches 98.8%.
Example 2
As shown in fig. 1, in this embodiment, the zinc replacement slag is leached, and the zinc replacement slag contains, by mass, 0.55% of gallium, 0.26% of germanium, 0.6% of indium, 6% of copper, 19.5% of zinc, 5% of iron, and 11.3% of silicon dioxide, and the specific steps are as follows:
(1) pretreatment: baking the zinc replacement slag in an oxygen-containing atmosphere at the baking temperature of 500 ℃ for 4 hours, and grinding the baked zinc replacement slag by a grinder until the granularity is 200 meshes for later use.
(2) First-stage leaching: the pretreated zinc replacement slag was slurried with 4 liters of a solution containing 140g/L sulfuric acid or a second leach solution per 1 kg. Pumping the slurried slurry into an oxygen autoclave for leaching, wherein the flow of oxygen introduced into the oxygen autoclave is 20-120Nm3The pressure in the kettle is 0.2Mpa, the leaching temperature is 80 ℃, and the leaching time is 2 hours. And then carrying out solid-liquid separation on the leaching slurry to obtain a first-stage leaching solution and a first-stage leaching residue, wherein the first-stage leaching solution is sent to a separation and enrichment working section for recovering valuable metals, and the concentration of sulfuric acid contained in the first-stage leaching solution is 30 g/L.
(3) Secondary leaching: the first leaching residue (1 kg) was slurried with 6 liters of a solution containing 180g/L sulfuric acid or a three-stage leaching solution. Pumping the slurried slurry into an oxygen autoclave for leaching, wherein the flow of oxygen introduced into the oxygen autoclave is 20-120Nm3The pressure in the kettle is 0.2Mpa, the leaching temperature is 80 ℃, and the leaching time is 6 hours. And then, carrying out solid-liquid separation on the leached slurry to obtain a second-stage leachate and second-stage leached residues, returning the second-stage leachate to the first-stage leaching for slurrying, wherein the concentration of sulfuric acid contained in the second-stage leachate is 140 g/L.
(4) Three-stage leaching: every 1 kg of the two-stage leaching residue is pulped by using 10 liters of sulfuric acid solution with the concentration of 200 g/L. Pumping the pulped slurry into a stirring barrel to be leached under stirring, wherein the leaching temperature is 80 ℃, and the leaching time is 6 hours. And then carrying out solid-liquid separation on the leaching slurry to obtain three-stage leaching liquid and three-stage leaching residues, returning the three-stage leaching liquid to the two-stage leaching for slurrying, wherein the concentration of sulfuric acid contained in the three-stage leaching liquid is 180g/L, and piling up or retreating the three-stage leaching residues.
After the pretreatment and the treatment of the three leaching stages, the leaching rate of gallium in the zinc replacement slag reaches 99.5%, the leaching rate of germanium reaches 82.9%, the leaching rate of indium reaches 99.6%, the leaching rate of copper reaches 99.4%, the leaching rate of zinc reaches 98.6%, and the leaching rate of iron reaches 98.9%.
The above-mentioned embodiments only express several embodiments of the present invention, and the description thereof is more specific and detailed, but not construed as limiting the scope of the invention. It should be noted that, for a person skilled in the art, several variations and modifications can be made without departing from the inventive concept, which falls within the scope of the present invention.
Claims (9)
1. A leaching method of zinc replacement slag is characterized in that: sequentially comprises the following steps:
pretreatment: baking the zinc replacement slag in an oxygen-containing atmosphere, and grinding for later use after baking;
first-stage leaching: pulping the first-stage pulping liquid and the zinc replacement residues, carrying out oxygen pressure leaching on the pulped slurry, and carrying out solid-liquid separation on the leached slurry to obtain a first-stage leachate and a first-stage leaching residue, wherein the first-stage leachate is used for recovering valuable metals;
secondary leaching: pulping the second-stage pulping liquid and the first-stage leaching residues, carrying out oxygen pressure leaching on the pulped pulp, and carrying out solid-liquid separation on the leached pulp to obtain a second-stage leaching liquid and second-stage leaching residues;
three-stage leaching: pulping the three-stage pulping liquid and the two-stage leaching residue, leaching the pulped pulp under stirring, and performing solid-liquid separation on the leached pulp to obtain three-stage leaching liquid and three-stage leaching residue;
the first-stage slurry is a solution containing 40-140g/L sulfuric acid or a second-stage leaching solution; the second-stage slurry solution is a solution containing 120-180g/L sulfuric acid or a third-stage leaching solution; the three-stage slurry solution is a sulfuric acid solution with the concentration of 140-250 g/L.
2. The leaching method of zinc replacement slag according to claim 1, wherein: in the first-stage leaching, 1-6 liters of first-stage pulping liquid is used for pulping every 1 kg of zinc replacement slag, and the concentration of sulfuric acid in the obtained first-stage leaching liquid is 5-30 g/L.
3. The leaching method of zinc replacement slag according to claim 2, wherein: in the first-stage leaching, the slurried slurry is pumped into an oxygen pressure kettle for oxygen pressure leaching, and the flow of oxygen introduced into the oxygen pressure kettle is 20-120Nm3The pressure in the kettle is 0.1-0.5Mpa, the leaching temperature is 60-140 ℃, and the leaching time is 1-6 hours.
4. The leaching method of zinc replacement slag according to claim 3, wherein: in the second-stage leaching, 1-10 liters of second-stage slurry liquid is used for slurrying every 1 kg of first-stage leaching residues, and the concentration of sulfuric acid in the obtained second-stage leaching liquid is 40-140 g/L.
5. The leaching method of zinc replacement slag according to claim 4, wherein: in the second-stage leaching, the slurried slurry is pumped into an oxygen pressure kettle for oxygen pressure leaching, and the flow of oxygen introduced into the oxygen pressure kettle is 20-120Nm3The pressure in the kettle is 0.1-0.5Mpa, the leaching temperature is 60-140 ℃, and the leaching time is 1-6 hours.
6. The leaching method of zinc replacement slag according to claim 5, wherein: in the three-stage leaching, 1-10 liters of three-stage slurry liquid is used for slurrying every 1 kg of two-stage leaching slag, and the concentration of sulfuric acid in the obtained three-stage leaching solution is 120-180 g/L.
7. The method for leaching zinc replacement slag according to claim 6, wherein: in the three-stage leaching, the slurried slurry is pumped into a stirring barrel to be leached under stirring, the leaching temperature is 60-90 ℃, and the leaching time is 1-6 hours.
8. The leaching method of zinc replacement slag according to claim 7, wherein: the baking temperature of the pretreatment is 250-700 ℃, the baking time is 2-8 hours, and the grinding particle size is 50-300 μm.
9. The leaching method of zinc replacement slag according to claim 7, wherein: the zinc replacement slag comprises, by mass, 0.2-0.7% of gallium, 0.1-0.8% of germanium, 0.01-0.2% of indium, 5-15% of copper, 5-20% of zinc, 3-10% of iron and 5-10% of silicon dioxide.
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| CN100537796C (en) * | 2007-08-09 | 2009-09-09 | 株洲冶炼集团股份有限公司 | The method of leaching, enriching and reclaiming indium from lead-zinc smelting by-product zinc oxide |
| CN101550485B (en) * | 2008-04-02 | 2011-04-06 | 中国科学院过程工程研究所 | Oxidative pressure acid leaching method for processing purified waste residue in zinc hydrometallurgy process |
| CN102851496B (en) * | 2012-10-08 | 2013-12-18 | 来宾华锡冶炼有限公司 | Treatment method of high-indium high-iron zinc concentrate |
| CN106834692A (en) * | 2016-12-30 | 2017-06-13 | 贵州宏达环保科技有限公司 | The comprehensive recovering process of valuable metal in a kind of zinc dust precipitation slag |
| CN106834695A (en) * | 2017-01-14 | 2017-06-13 | 六盘水中联工贸实业有限公司 | A kind of method that germanium is extracted in the zinc replacement slag from smelting |
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