CN102108519A - Method for recovering zinc and aluminum by simultaneously electrolyzing hot-dipped zinc and aluminum slag through ionic membrane - Google Patents
Method for recovering zinc and aluminum by simultaneously electrolyzing hot-dipped zinc and aluminum slag through ionic membrane Download PDFInfo
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- CN102108519A CN102108519A CN2010106052603A CN201010605260A CN102108519A CN 102108519 A CN102108519 A CN 102108519A CN 2010106052603 A CN2010106052603 A CN 2010106052603A CN 201010605260 A CN201010605260 A CN 201010605260A CN 102108519 A CN102108519 A CN 102108519A
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Abstract
The invention relates to a method for recovering zinc and aluminum by simultaneously electrolyzing hot-dipped zinc and aluminum slag through an ionic membrane. An anode for electrolysis is a fused cast plate of the hot-dipped zinc and aluminum slag, and a cathode is a stainless steel plate. A diaphragm of an electrolyzer is an anion-exchange membrane. Anode solution is ammonium chloride solution and cathode solution is zinc ion-containing ammoniacal solution. During electrolysis, the current density range is 100 to 800A.m<-2>, and the electrolyzer voltage range is 0.5 to 5V. The current efficiency of the anode and the cathode can reach 99 percent. The method has the advantages that: electrolyte containing zinc ions and aluminum ions is obtained in an anode chamber; meanwhile, high-purity zinc metal can be obtained at the cathode, and the energy consumption of electrowinning zinc is reduced; and the electrolyte in the anode chamber is purified and then can be used for preparing aluminum hydroxide, mother solution can be used as electrolyte for electrowinning zinc, and the hot-dipped zinc and aluminum slag is comprehensively recycled.
Description
Technical field
The present invention relates to the Non-ferrous Metallurgy field, specifically a kind of ionic membrane electrolysis simultaneously hot dip zinc-aluminium slag reclaims the method for zinc and aluminium.
Background technology
The smelting of zinc has two kinds of pyrometallurgical smelting and hydrometallurgies.Hydrometallurgy has that throughput is big, efficient is high, operational condition is good, environmental pollution is little and valuable metal is comprehensive reclaims advantages such as good, is widely adopted.But the zinc electrodeposition process energy consumption in the zinc hydrometallurgy is huge, account for 80% of zinc hydrometallurgy total energy consumption, its major cause is to adopt the lead 2-base alloy anode in the high-concentration sulfuric acid electrolyte system always, its overpotential for oxygen evolution reaches 1V, increase the nearly 1000kWh/t zinc of useless power consumption thus, account for 30% of zinc electrodeposition total energy consumption (about 3200kWh/t zinc).In addition, the lead 2-base alloy anode density is big, intensity is low, flexible creep and cause short circuit, reduces current efficiency, increases energy consumption; Lead 2-base alloy anodic plumbic oxide passive film is loose porous, the formation anode sludge that easily comes off, and pollute cathode zinc, reduce quality product.Though ZnCl
2-NH
3-NH
4Energy consumption decreases in the Cl electrolysis of solutions system, but anode still uses inert anode, does not make full use of electric energy.The electrodeposition process of improvement and raising zinc hydrometallurgy can be saved energy and reduce the cost, be reduced production costs.
In hot galvanizing process, zinc and bauxite resource content are extremely abundant in the slag.Can enlarge work-ing life, the reduction production energy consumption of zinc resource for the electrowinning zinc anode with the hot galvanizing residue.Data shows, is producing the total expenses of zinc from the zinc primary ore, and energy cost has accounted for 20%, if adopt cadmia waste material production metallic zinc, the energy consumption that its energy loss-rate is produced the zinc metal with primary zinc ore reduces about 60%～72%.Simultaneously, low owing to the raw mineral materials grade, composition is complicated if with primary zinc ore zinc concentrate, thereby technical process is long, and the production technology complexity, " three wastes " that produce in the production are many.The content of zinc is up to more than 85% in the cadmia that has, and the raw material grade is higher, and technical process is shorter, thereby can reduce pollution to environment with cadmia direct production metallic zinc, reduces the quantity discharged of the three wastes.
Summary of the invention
Technical problem to be solved by this invention is low at the rate of recovery of zinc, power consumption is big, proposing a kind of is anode with hot dip zinc-aluminium slag, when obtaining containing zine ion and aluminum ions electrolytic solution, anode obtains the ionic membrane electrolysis simultaneously hot dip zinc-aluminium slag recovery zinc of metallic zinc and the method for aluminium at negative electrode
The technical scheme that the present invention solves the problems of the technologies described above employing is: a kind of ionic membrane electrolysis simultaneously hot dip zinc-aluminium slag reclaims the method for zinc and aluminium, use ion-exchange membrane that electrolyzer is divided into anolyte compartment and cathode compartment, anode and negative electrode, anolyte and corresponding respectively anolyte compartment and the cathode compartment of placing of catholyte, anolyte is the ammonium chloride solution of concentration 10～80g/L, catholyte is the ammonia solution that contains zine ion, and it consists of: Zn
2+Concentration 30～150g/L, it is 7.5～10 that ammoniacal liquor is regulated pH; In current density is 100～800A/m
2The time, logical direct current electrolysis, the temperature of electrolytic solution is 10～60 ℃ during electrolysis, when the anolyte compartment obtains containing zine ion and aluminum ions electrolytic solution, obtains metallic zinc at cathode compartment; The anode principal reaction is the electrochemical dissolution reaction of hot dip zinc-aluminium slag, and the negative electrode principal reaction is the electrochemical deposition reaction of precipitating metal zinc.
Described ion-exchange membrane is an anion-exchange membrane.Described anode is a hot dip zinc-aluminium slag founding plate, and negative electrode is a stainless steel plate.The distance of described negative electrode and ion-exchange membrane, anode and ion-exchange membrane is 5～50mm, and electrode distance is 10～100mm.
Advantage of the present invention is: because the use of ion-exchange membrane when the anolyte compartment obtains containing zine ion, aluminum ions electrolytic solution, also can obtain high-purity zinc at cathode compartment, reduce the energy consumption of electrowinning zinc.By adjustment to different electrolytes concentration, the meltage and the anodic current efficiency of hot dip zinc-aluminium slag have been improved, anolyte compartment's electrolytic solution can prepare aluminium hydroxide after purifying, mother liquor can be used as the electrolytic solution of electrowinning zinc, has reached the comprehensive reutilization to hot dip zinc-aluminium slag.
Embodiment
A kind of ionic membrane electrolysis simultaneously hot dip zinc-aluminium slag reclaims the method for zinc and aluminium, use ion-exchange membrane that electrolyzer is divided into anolyte compartment and cathode compartment, anode and negative electrode, anolyte and corresponding respectively anolyte compartment and the cathode compartment of placing of catholyte, anolyte is the ammonium chloride solution of concentration 10～80g/L, catholyte is the ammonia solution that contains zine ion, and it consists of: Zn
2+Concentration 30～150g/L, it is 7.5～10 that ammoniacal liquor is regulated pH; In current density is 100～800A/m
2The time, logical direct current electrolysis, the temperature of electrolytic solution is 10～60 ℃ during electrolysis, when the anolyte compartment obtains containing zine ion and aluminum ions electrolytic solution, obtains metallic zinc at cathode compartment; The anode principal reaction is the electrochemical dissolution reaction of hot dip zinc-aluminium slag, and the negative electrode principal reaction is the electrochemical deposition reaction of precipitating metal zinc.
Below in conjunction with embodiment technology contents of the present invention is described in further detail
Embodiment 1
A kind of ionic membrane electrolysis simultaneously hot dip zinc-aluminium slag reclaims the method for zinc and aluminium: anode is a hot dip zinc-aluminium slag founding plate, and negative electrode is a stainless steel plate; Electrolyzer yin, yang the two poles of the earth are the plate and frame structure; Electrode diaphragm is an anion-exchange membrane; Electrode distance is 60mm; Current density is 300A/m
2
The ammonium chloride solution of measuring 500mL concentration and be 40g/L is an anolyte; Other measures 500mL Zn
2+Concentration is that the ammonia solution of 40g/L is a catholyte, and pH is 9; Electrolysis 1h when temperature is 25 ℃, the result is: current efficiency 99.50%, average groove is pressed 1.6V.
Embodiment 2
A kind of ionic membrane is the method for electrolytic recovery hot dip zinc-aluminium slag simultaneously, and cell construction, electrode diaphragm, electrode distance are with embodiment 1, and current density is 400A/m
2
The ammonium chloride solution of measuring 500mL concentration and be 60g/L is an anolyte; Other measures 500mL Zn
2+Concentration is that the ammonia solution of 60g/L is a catholyte, and pH is 8; Electrolysis 2h when temperature is 25 ℃, the result is: current efficiency 99.18%, average groove is pressed 1.35V.
Embodiment 3
A kind of ionic membrane is the method for electrolytic recovery hot dip zinc-aluminium slag simultaneously, and cell construction, electrode diaphragm, electrode distance are with embodiment 1, and current density is 600A/m
2
The ammonium chloride solution of measuring 500mL concentration and be 60g/L is an anolyte; Other measures 500mL Zn
2+Concentration is that the ammonia solution of 60g/L is a catholyte, and pH is 9; Electrolysis 8h when temperature is 25 ℃, the result is: current efficiency 99.28%, average groove is pressed 1.55V.
Embodiment 4
A kind of ionic membrane is the method for electrolytic recovery hot dip zinc-aluminium slag simultaneously, and cell construction, electrode diaphragm, electrode distance are with embodiment 1, and current density is 400A/m
2
The ammonium chloride solution of measuring 500mL concentration and be 60g/L is an anolyte; Other measures 500mL Zn
2+Concentration is that the ammonia solution of 80g/L is a catholyte, and pH is 9; Electrolysis 4h when temperature is 25 ℃, the result is: current efficiency 99.16%, average groove is pressed 1.45V.
Embodiment 5
A kind of ionic membrane is the method for electrolytic recovery hot dip zinc-aluminium slag simultaneously, and cell construction, electrode diaphragm are with embodiment 1, and electrode distance is 80mm, and current density is 500A/m
2
The ammonium chloride solution of measuring 500mL concentration and be 80g/L is an anolyte; Other measures 500mL Zn
2+Concentration is that the ammonia solution of 60g/L is a catholyte, and pH is 8; Electrolysis 4h when temperature is 25 ℃, the result is: current efficiency 99.10%, average groove is pressed 1.45V.
Embodiment 6
A kind of ionic membrane is the method for electrolytic recovery hot dip zinc-aluminium slag simultaneously, and cell construction, electrode diaphragm, electrode distance are with embodiment 1, current density 500A/m
2
The ammonium chloride solution of measuring 500mL concentration and be 60g/L is an anolyte; Other measures 500mL Zn
2+Concentration is that the ammonia solution of 60g/L is a catholyte, and pH is 8; Electrolysis 4h when temperature is 40 ℃, the result is: current efficiency 99.50%, average groove is pressed 1.41V.
Embodiment 7
A kind of ionic membrane is the method for electrolytic recovery hot dip zinc-aluminium slag simultaneously, and cell construction, electrode diaphragm be with embodiment 1, electrode distance 60mm, current density 500A/m
2
The ammonium chloride solution of measuring 500mL concentration and be 60g/L is an anolyte; Other measures 500mL Zn
2+Concentration is that the ammonia solution of 60g/L is a catholyte, and pH is 9; Electrolysis 4h when temperature is 50 ℃, the result is: current efficiency 99.05%, average groove is pressed 1.44V.
Claims (4)
1. ionic membrane electrolysis simultaneously hot dip zinc-aluminium slag reclaims the method for zinc and aluminium, it is characterized in that: use ion-exchange membrane that electrolyzer is divided into anolyte compartment and cathode compartment, anode and negative electrode, anolyte and corresponding respectively anolyte compartment and the cathode compartment of placing of catholyte, anolyte is the ammonium chloride solution of concentration 10～80g/L, catholyte is the ammonia solution that contains zine ion, and it consists of: Zn
2+Concentration 30～150g/L, it is 7.5～10 that ammoniacal liquor is regulated pH; In current density is 100～800A/m
2The time, logical direct current electrolysis, the temperature of electrolytic solution is 10～60 ℃ during electrolysis, when the anolyte compartment obtains containing zine ion and aluminum ions electrolytic solution, obtains metallic zinc at cathode compartment; The anode principal reaction is the electrochemical dissolution reaction of hot dip zinc-aluminium slag, and the negative electrode principal reaction is the electrochemical deposition reaction of precipitating metal zinc.
2. a kind of ionic membrane according to claim 1 electrolysis simultaneously hot dip zinc-aluminium slag reclaims the method for zinc and aluminium, and it is characterized in that: ion-exchange membrane is an anion-exchange membrane.
3. a kind of ionic membrane according to claim 1 electrolysis simultaneously hot dip zinc-aluminium slag reclaims the method for zinc and aluminium, and it is characterized in that: anode is a hot dip zinc-aluminium slag founding plate, and negative electrode is a stainless steel plate.
4. a kind of ionic membrane according to claim 1 electrolysis simultaneously hot dip zinc-aluminium slag reclaims the method for zinc and aluminium, and it is characterized in that: the distance of negative electrode and ion-exchange membrane, anode and ion-exchange membrane is 5～50mm, and electrode distance is 10～100mm.
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| Application Number | Priority Date | Filing Date | Title |
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| CN2010106052603A CN102108519A (en) | 2010-12-14 | 2010-12-14 | Method for recovering zinc and aluminum by simultaneously electrolyzing hot-dipped zinc and aluminum slag through ionic membrane |
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| CN2010106052603A CN102108519A (en) | 2010-12-14 | 2010-12-14 | Method for recovering zinc and aluminum by simultaneously electrolyzing hot-dipped zinc and aluminum slag through ionic membrane |
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| CN102108519A true CN102108519A (en) | 2011-06-29 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102433569A (en) * | 2011-12-06 | 2012-05-02 | 中南大学 | Method for electrolyzing high-alkali gangue type low-grade zinc oxide ore leachate treated by ammonia leaching process |
| CN102839389A (en) * | 2012-09-26 | 2012-12-26 | 兰州交通大学 | Novel production method of electro-depositing and refining metal chloride by membrane process |
| CN116103517A (en) * | 2023-02-03 | 2023-05-12 | 哈尔滨工业大学（威海） | Extraction solvent and extraction method for extracting and separating titanium and/or iron from acidic solution containing titanium and/or iron |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101054686A (en) * | 2007-02-14 | 2007-10-17 | 浙江工业大学 | Process for purifying zinc from casting zinc residue |
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2010
- 2010-12-14 CN CN2010106052603A patent/CN102108519A/en active Pending
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101054686A (en) * | 2007-02-14 | 2007-10-17 | 浙江工业大学 | Process for purifying zinc from casting zinc residue |
Non-Patent Citations (1)
| Title |
|---|
| XIULIAN REN等: "The recovery of zinc from hot galvanizing slag in an anion-exchange membrane electrolysis reactor", 《JOURNAL OF HAZARDOUS MATERIALS》 * |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102433569A (en) * | 2011-12-06 | 2012-05-02 | 中南大学 | Method for electrolyzing high-alkali gangue type low-grade zinc oxide ore leachate treated by ammonia leaching process |
| CN102433569B (en) * | 2011-12-06 | 2014-11-05 | 中南大学 | Method for electrolyzing high-alkali gangue type low-grade zinc oxide ore leachate treated by ammonia leaching process |
| CN102839389A (en) * | 2012-09-26 | 2012-12-26 | 兰州交通大学 | Novel production method of electro-depositing and refining metal chloride by membrane process |
| WO2014048050A1 (en) * | 2012-09-26 | 2014-04-03 | 兰州交通大学 | Production method of electro-depositing and refining metal chloride by membrane process and preparation method for cation selective diaphragm used therein |
| CN102839389B (en) * | 2012-09-26 | 2015-06-03 | 兰州交通大学 | Novel production method of electro-depositing and refining metal chloride by membrane process |
| EP3002349A1 (en) * | 2012-09-26 | 2016-04-06 | Lanzhou Jiaotong University | Membrane process of electro-depositing and refining metal chloride and preparation of cation selective membrane |
| CN116103517A (en) * | 2023-02-03 | 2023-05-12 | 哈尔滨工业大学（威海） | Extraction solvent and extraction method for extracting and separating titanium and/or iron from acidic solution containing titanium and/or iron |
| CN116103517B (en) * | 2023-02-03 | 2024-04-26 | 哈尔滨工业大学（威海） | Extraction solvent and extraction method for extracting and separating titanium and/or iron from acidic solution containing titanium and/or iron |
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Application publication date: 20110629 |