CN114990351B - Method for cooperatively treating zinc concentrate and copper white smoke dust - Google Patents
Method for cooperatively treating zinc concentrate and copper white smoke dust Download PDFInfo
- Publication number
- CN114990351B CN114990351B CN202210669026.XA CN202210669026A CN114990351B CN 114990351 B CN114990351 B CN 114990351B CN 202210669026 A CN202210669026 A CN 202210669026A CN 114990351 B CN114990351 B CN 114990351B
- Authority
- CN
- China
- Prior art keywords
- copper
- zinc
- leaching
- oxygen
- slag
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 239000011701 zinc Substances 0.000 title claims abstract description 161
- 239000010949 copper Substances 0.000 title claims abstract description 147
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 title claims abstract description 116
- 229910052802 copper Inorganic materials 0.000 title claims abstract description 114
- 229910052725 zinc Inorganic materials 0.000 title claims abstract description 113
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 title claims abstract description 108
- 238000000034 method Methods 0.000 title claims abstract description 47
- 239000000428 dust Substances 0.000 title claims abstract description 44
- 239000000779 smoke Substances 0.000 title claims abstract description 40
- 239000012141 concentrate Substances 0.000 title claims abstract description 37
- 238000002386 leaching Methods 0.000 claims abstract description 115
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims abstract description 89
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 75
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 75
- 239000001301 oxygen Substances 0.000 claims abstract description 75
- 239000002893 slag Substances 0.000 claims abstract description 64
- 239000002253 acid Substances 0.000 claims abstract description 52
- 229910052742 iron Inorganic materials 0.000 claims abstract description 33
- 239000000460 chlorine Substances 0.000 claims abstract description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 20
- 239000003792 electrolyte Substances 0.000 claims abstract description 18
- 239000002699 waste material Substances 0.000 claims abstract description 18
- 239000007788 liquid Substances 0.000 claims abstract description 17
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 12
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 12
- 238000001914 filtration Methods 0.000 claims abstract description 10
- 238000000227 grinding Methods 0.000 claims abstract description 8
- 238000007654 immersion Methods 0.000 claims abstract description 8
- 238000002156 mixing Methods 0.000 claims abstract description 4
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 28
- 230000008569 process Effects 0.000 claims description 28
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 27
- 229910052717 sulfur Inorganic materials 0.000 claims description 26
- 239000011593 sulfur Substances 0.000 claims description 26
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 16
- 238000006298 dechlorination reaction Methods 0.000 claims description 16
- 239000003546 flue gas Substances 0.000 claims description 16
- 238000009853 pyrometallurgy Methods 0.000 claims description 11
- 238000005266 casting Methods 0.000 claims description 9
- 238000005868 electrolysis reaction Methods 0.000 claims description 9
- 238000010791 quenching Methods 0.000 claims description 9
- 230000000171 quenching effect Effects 0.000 claims description 9
- 230000035484 reaction time Effects 0.000 claims description 9
- 229910052785 arsenic Inorganic materials 0.000 abstract description 71
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 abstract description 47
- 238000009854 hydrometallurgy Methods 0.000 abstract description 2
- 230000001376 precipitating effect Effects 0.000 abstract description 2
- 238000005188 flotation Methods 0.000 description 22
- 239000007787 solid Substances 0.000 description 15
- 230000000052 comparative effect Effects 0.000 description 12
- 239000002245 particle Substances 0.000 description 11
- BMWMWYBEJWFCJI-UHFFFAOYSA-K iron(3+);trioxido(oxo)-$l^{5}-arsane Chemical compound [Fe+3].[O-][As]([O-])([O-])=O BMWMWYBEJWFCJI-UHFFFAOYSA-K 0.000 description 10
- 238000011084 recovery Methods 0.000 description 10
- 238000006243 chemical reaction Methods 0.000 description 9
- 230000000694 effects Effects 0.000 description 9
- 230000001698 pyrogenic effect Effects 0.000 description 8
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 7
- 239000000203 mixture Substances 0.000 description 7
- 229910052751 metal Inorganic materials 0.000 description 6
- 239000002184 metal Substances 0.000 description 6
- 150000002739 metals Chemical class 0.000 description 6
- 238000000746 purification Methods 0.000 description 6
- 239000000047 product Substances 0.000 description 5
- 239000003513 alkali Substances 0.000 description 4
- 239000002244 precipitate Substances 0.000 description 4
- 238000001556 precipitation Methods 0.000 description 4
- HJTAZXHBEBIQQX-UHFFFAOYSA-N 1,5-bis(chloromethyl)naphthalene Chemical compound C1=CC=C2C(CCl)=CC=CC2=C1CCl HJTAZXHBEBIQQX-UHFFFAOYSA-N 0.000 description 3
- 241001536352 Fraxinus americana Species 0.000 description 3
- GOLCXWYRSKYTSP-UHFFFAOYSA-N arsenic trioxide Inorganic materials O1[As]2O[As]1O2 GOLCXWYRSKYTSP-UHFFFAOYSA-N 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 description 3
- 229910000360 iron(III) sulfate Inorganic materials 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000006386 neutralization reaction Methods 0.000 description 3
- JPVYNHNXODAKFH-UHFFFAOYSA-N Cu2+ Chemical compound [Cu+2] JPVYNHNXODAKFH-UHFFFAOYSA-N 0.000 description 2
- 238000003723 Smelting Methods 0.000 description 2
- 230000006978 adaptation Effects 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 229910001431 copper ion Inorganic materials 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000011946 reduction process Methods 0.000 description 2
- 238000007711 solidification Methods 0.000 description 2
- 230000008023 solidification Effects 0.000 description 2
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 1
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 1
- 239000005083 Zinc sulfide Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000003984 copper intrauterine device Substances 0.000 description 1
- 229910000365 copper sulfate Inorganic materials 0.000 description 1
- ARUVKPQLZAKDPS-UHFFFAOYSA-L copper(II) sulfate Chemical compound [Cu+2].[O-][S+2]([O-])([O-])[O-] ARUVKPQLZAKDPS-UHFFFAOYSA-L 0.000 description 1
- 230000001627 detrimental effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000004070 electrodeposition Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 229910052595 hematite Inorganic materials 0.000 description 1
- 239000011019 hematite Substances 0.000 description 1
- 150000002505 iron Chemical class 0.000 description 1
- LIKBJVNGSGBSGK-UHFFFAOYSA-N iron(3+);oxygen(2-) Chemical compound [O-2].[O-2].[O-2].[Fe+3].[Fe+3] LIKBJVNGSGBSGK-UHFFFAOYSA-N 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000008520 organization Effects 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 239000002516 radical scavenger Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000006228 supernatant Substances 0.000 description 1
- NWONKYPBYAMBJT-UHFFFAOYSA-L zinc sulfate Chemical compound [Zn+2].[O-]S([O-])(=O)=O NWONKYPBYAMBJT-UHFFFAOYSA-L 0.000 description 1
- 229910000368 zinc sulfate Inorganic materials 0.000 description 1
- 229960001763 zinc sulfate Drugs 0.000 description 1
- 229910052984 zinc sulfide Inorganic materials 0.000 description 1
- DRDVZXDWVBGGMH-UHFFFAOYSA-N zinc;sulfide Chemical compound [S-2].[Zn+2] DRDVZXDWVBGGMH-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- 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
- C22B19/32—Refining zinc
-
- 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
- C22B15/0084—Treating solutions
- C22B15/0089—Treating solutions by chemical methods
- C22B15/0091—Treating solutions by chemical methods by cementation
-
- 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
-
- 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
- C22B30/00—Obtaining antimony, arsenic or bismuth
- C22B30/04—Obtaining arsenic
-
- 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
- C22B7/001—Dry processes
-
- 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
-
- 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
- C22B7/02—Working-up flue dust
-
- 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Manufacturing & Machinery (AREA)
- Metallurgy (AREA)
- Environmental & Geological Engineering (AREA)
- Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Inorganic Chemistry (AREA)
- Geochemistry & Mineralogy (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention belongs to the technical field of hydrometallurgy, and particularly relates to a method for removing arsenic and chlorine in a solution by cooperative treatment of zinc concentrate and copper white smoke dust. The method for cooperatively treating zinc concentrate and copper white smoke dust comprises the following steps: (1) Mixing zinc concentrate and copper white smoke dust, adding water, and grinding to obtain ore pulp; (2) Adding waste electrolyte into ore pulp, adjusting the molar ratio of acid zinc in the ore pulp to 0.8-1.1, performing oxygen pressure leaching, and filtering to obtain oxygen leaching liquid and oxygen leaching slag; (3) Zinc powder is added into the oxygen immersion liquid to remove copper, arsenic and chlorine to obtain copper slag and liquid after copper removal and chlorine removal. The zinc concentrate can be matched for treating up to 50% of white smoke dust, and the white smoke dust can be treated at one time with large quantity; the leaching rate of zinc and copper is high, wherein the zinc content can reach more than 98 percent, and the copper content can reach more than 95 percent, thereby achieving the purposes of efficiently leaching zinc and copper, and simultaneously reducing acid, precipitating iron and removing arsenic.
Description
Technical Field
The invention belongs to the technical field of hydrometallurgy, and particularly relates to a method for removing arsenic and chlorine in a solution by cooperative treatment of zinc concentrate and copper white smoke dust.
Background
The zinc concentrate oxygen pressure leaching has the advantages of high efficiency, energy saving, comprehensive recovery, good environmental protection effect and the like, and is widely applied, and smoke dust with higher arsenic content, which is generally called white smoke dust, contains 5-20% of copper, 6-20% of arsenic, valuable metals such as lead, zinc and the like, can be produced in the copper pyrometallurgy process. Because white dust contains high arsenic, arsenic in the white dust needs to be removed from a copper smelting system, and valuable metals are recovered. The method for removing arsenic from white smoke dust includes a fire method and a wet method, the method for removing arsenic from white smoke dust by fire treatment is based on low iron content of materials, arsenic can be reduced and volatilized into arsenic trioxide to be recovered as smoke dust, valuable metals such as lead and zinc volatilize into smoke dust along with arsenic, the separation effect of arsenic and valuable metals is poor, and meanwhile, the environment is protected. The wet treatment of white dust and dust for dearsenification generally adopts a copper leaching-copper precipitation-arsenic reduction process to achieve the aim of separating arsenic from valuable metals, and arsenic trioxide products can be obtained, but a large amount of sulfuric acid is produced in the copper precipitation and arsenic reduction processes, the acid is unbalanced, the excessive acid needs to be neutralized to produce a large amount of neutralization residues, and meanwhile, the arsenic trioxide products are difficult to sell and are required to be stored for a long time in a warehouse.
Disclosure of Invention
The invention aims to provide a method for removing arsenic and chlorine in a solution by cooperatively treating zinc concentrate and copper white smoke dust, which realizes arsenic solidification in slag instead of arsenic product discharge and solves the problem of harmless environmental protection of arsenic.
In order to solve the technical problems, the technical scheme of the invention is as follows:
a method for cooperatively treating zinc concentrate and copper white smoke dust comprises the following steps:
(1) Mixing zinc concentrate and copper white smoke dust, adding water, and grinding to obtain ore pulp;
(2) Adding waste electrolyte into ore pulp, adjusting the mole ratio of acid zinc in the ore pulp to be 0.8-1.1, then performing oxygen pressure leaching, and filtering to obtain oxygen leaching liquid and oxygen leaching slag;
(3) Zinc powder is added into the oxygen immersion liquid to remove copper and chlorine, so as to obtain copper slag and copper-removed and chlorine-removed liquid;
delivering sulfur from the oxygen leaching slag, recovering and producing sulfur and floatation tailings; and carrying out pyrometallurgy treatment on flotation tailings to obtain slag and flue gas.
In the zinc oxygen pressure leaching process, the molar ratio of acid zinc is too large, namely, the starting acid is higher, so that after oxygen pressure leaching, the final acid is higher, and Fe (OH) is difficult to form 3 So that ferric arsenate cannot be formed and the subsequent purification process can causeThe alkali forming consumption is high. In addition, the leaching rate of Zn and Cu is not obviously improved due to the excessively high molar ratio of zinc acid, but the leaching of other impurity elements is increased, so that the purity of the product is reduced, and the purification load is increased. However, if the molar ratio of zinc acid is too low, the leaching rate of Zn and Cu is not high due to insufficient acid for reaction.
Preferably, the zinc concentrate comprises the following main components in percentage by mass: 40 to 55 percent of Zn, 1 to 15 percent of Fe, 0.1 to 1 percent of Cu and 0.05 to 0.5 percent of As.
Preferably, the copper white smoke dust comprises the following main components in percentage by mass: 5-18% of Cu, 1-5% of Zn, 6-20% of As and 1-5% of Fe.
Preferably, in the step (1), the mass ratio of the zinc concentrate to the copper white smoke is 1 (30% -50%).
The addition amount of white smoke dust is small, so that the amount of As entering the solution is small, on one hand, the amount of copper white smoke dust which can be treated is small, and on the other hand, the iron which is precipitated As arsenic in the leaching solution is small, so that the content of residual iron in the leaching solution is still high, and the combined action of the arsenic precipitation and the iron precipitation is not achieved. If the addition amount is too large, the arsenic content of the solution is too high, and the iron in the system is insufficient to remove arsenic, so that two impurities cannot be treated at the same time.
The highest proportion of white dust is about 50%, and the leached iron is combined with As of the white dust to generate ferric arsenate mainly according to the content of iron carried in zinc concentrate and the white dust.
When the white smoke dust is excessively added, the As content is excessive, iron carried in zinc concentrate is insufficient to satisfy the requirement that As is settled to generate ferric arsenate, and a large load is caused for removing arsenic in a subsequent system.
In addition, the zinc grade of the oxygen autoclave is reduced by adding the white ash, so that the zinc concentration in the leaching solution is reduced, and the white ash is not easy to be added too much, so that the reduction of the zinc concentration in an original zinc system is avoided.
Preferably, in the step (1), the mass concentration of the pulp solid is 65-70%, and the particle size 90% is less than 44 μm.
The control of the ore pulp concentration is to ensure that the zinc concentrate is finely ground to a target particle size range in the grinding stage to obtain higher leaching rates of Zn and Cu.
The granularity is a parameter which has larger influence on the leaching effect in the wet leaching process, and too small granularity can naturally improve the leaching efficiency, but the lifting amplitude is not large, and the energy consumption is larger; too large a particle size is detrimental to zinc leaching.
Preferably, in the step (2), oxygen with a concentration of 99% is introduced into the oxygen pressure leaching.
The oxygen pressure leaching process requires a high oxygen potential, the higher the oxygen concentration, the more advantageous the leaching of zinc.
Preferably, in the step (2), the temperature is controlled to be 145-155 ℃ and the pressure is controlled to be 1.0-1.2 Mpa in the oxygen pressure leaching process, and the reaction time is 100-120 min.
The temperature, pressure and time interval can ensure the leaching rate of zinc and reduce the oxidation of sulfur, and most of sulfur in leaching slag exists in the form of sulfur. The high leaching rate of zinc can be ensured due to the fact that the temperature is too high, the pressure is too high and the reaction time is prolonged, but oxidation of sulfur is increased, so that the conversion rate of sulfur is reduced, the final acid is improved, and the alkali consumption for neutralization in the subsequent purification is greatly improved.
If these parameters are too small, the zinc leaching rate is insufficient.
Therefore, reasonable temperature, pressure and time parameters need to be controlled.
Preferably, in the step (2), after oxygen pressure leaching, the reacted ore pulp is cooled and depressurized through a flash tank and filtered.
The temperature of ore pulp is 150 ℃ below zero, the pressure of solution is 1.0MPa, and conventional filter equipment cannot be adopted without reducing the temperature and the pressure.
Preferably, in step (2), the filtration is a dense filtration.
The method is characterized in that supernatant fluid is subjected to iron removal, purification and electrodeposition processes, and underflow is subjected to sulfur recovery. If the plate frame is adopted for filtering, the sulfur recovery process is also needed after the slurry mixing.
Preferably, in the step (3), the addition amount of zinc powder is 2-5 times of Cu content (mass) of the leaching solution.
Preferably, in the step (3), the conditions of adding zinc powder for copper removal and dechlorination are that the pH is 1.0-1.5, the temperature is 70-80, and the reaction time is 3-4 hours.
The purpose of step (3) is to deeply remove the Cu content of the leachate by adding a copper scavenger, i.e. zinc powder.
First, as is removed by the formation of ferric arsenate precipitate by combination with Fe during oxygen pressure leaching, where the main impurity in the oxygen leach is copper. The principle of copper precipitation and dechlorination of Zn powder is reaction (6) and reaction (7), in addition, zn powder can react with acid, the pH value range of the reaction is controlled, the acidity of oxygen pressure leaching liquid is ensured to be very low, and the consumption of zinc powder directly reacted with acid is very low, namely about 5 g/L. And then, controlling the pH value, the temperature and the reaction time of the solution to remove copper in the solution.
When the pH is less than 1, the consumption of the zinc powder and the acid is too large, so that the addition of the zinc powder is insufficient, the copper removal effect is not obvious, and when the pH is more than 1.5, the chlorine removal effect can be influenced after the zinc powder is added.
Too low temperature and time control result in poor removal effect, too high energy consumption and insignificant increase in removal effect.
Preferably, in the step (3), copper slag is returned to copper pyrometallurgy; and (3) delivering the solution after copper removal and dechlorination to remove iron and purify, and carrying out electrolysis and casting to produce the electro-zinc.
Preferably, in the step (2), after sulfur is recovered from the oxygen leaching slag through floatation, the floatation tailings are sent to a pyrometallurgical system, and the pyrometallurgical slag is subjected to water quenching to obtain harmless slag; and sending the flue gas to acid to produce sulfuric acid.
The invention is further explained as follows:
according to the method, zinc concentrate oxygen pressure leaching is adopted to match with copper white smoke dust, zinc and copper in materials are leached into zinc sulfate and copper sulfate solutions, sulfur is mostly converted into elemental sulfur, iron leached from zinc concentrate and arsenic in white smoke dust are combined to generate ferric arsenate precipitate, copper ions entering the solution can remove copper and chlorine in the solution in the subsequent copper removal process, and the main chemical reaction principle is as follows:
2ZnFeS+5H 2 SO 4 +2.5O 2 →2ZnSO 4 +Fe 2 (SO 4 ) 3 +5H 2 O+2S 0 (1)
CuSO 4 (s)→Cu 2+ (aq)+SO 4 2- (aq) (2)
Fe 2 (SO 4 ) 3 +(x+3)H 2 O→Fe 2 O 3 ·xH 2 O+3H 2 SO 4 (3)
2H 3 AsO 3 +O 2 →2H 3 AsO 4 (4)
H 3 AsO 4 +Fe(OH) 3 →FeAsO 4 ↓+3H 2 O (5)
Cu 2+ +Zn→Cu↓+Zn 2+ (6)
2Cu 2+ +2Cl - +nZn→Cu 2 Cl 2 ↓+nZn 2+ (7)
in the invention, copper white dust is added in the oxygen pressure leaching of zinc concentrate, so the treatment process is obviously affected. The concrete steps are as follows:
1. for the acid zinc ratio, in the application, in the process of synergizing leaching of zinc concentrate and copper white smoke dust, in order to ensure higher leaching rates of zinc and copper, the control range of the acid zinc molar ratio of the conventional zinc concentrate is higher.
2. The conventional zinc concentrate oxygen pressure leaching adopts a two-stage process, namely the acid is difficult to balance, namely when the leaching rate of Zn is high, the sulfuric acid content in the leaching solution is too high, so that the subsequent neutralization use of alkali is large, and therefore, the zinc sulfide concentrate is treated by adopting a two-stage oxygen pressure leaching process. The invention adopts the copper white dust, and the sulfuric acid in the solution is neutralized by the copper white dust which is matched with the copper white dust while the high-efficiency leaching of zinc is satisfied, so that the leaching solution can be directly subjected to the subsequent purification process, one section of working procedures can be directly omitted, the alkali consumption is small, and the invention meets the production requirements of industrial green energy conservation.
Because the zinc concentrate contains very little arsenic, the iron carried in the zinc concentrate and the arsenic carried in the copper white ash are combined to generate ferric arsenate for removing arsenic, and the oxygen immersion liquid contains only about 0.1g/L arsenic after arsenic removal.
The invention has the advantages and technical effects that:
(1) The zinc concentrate can be matched for treating up to 50% of white smoke dust, the copper and arsenic of the mixed material are high, wherein the copper can reach 5%, the arsenic can reach 6%, and the white smoke dust can be treated at one time with large quantity;
(2) The leaching rate of zinc and copper is high, wherein the zinc can reach more than 98 percent, the copper can reach more than 95 percent, and H-containing can be obtained 2 SO 4 5～8g/L，Fe 2～3g/L，Cu 10g/L，As<0.1g/L oxygen immersion liquid, thereby achieving the purposes of efficiently leaching zinc and copper, and simultaneously reducing acid, precipitating iron and removing arsenic;
(3) Copper ions and zinc powder in the solution are utilized to efficiently remove copper and chlorine in the solution;
(4) The floatation tailings are smelted by a pyrogenic process, so that arsenic is solidified in the slag along with iron to be changed into harmless slag, the aim of discharging arsenic in the arsenic solidification slag instead of arsenic products is fulfilled, and the harmless environmental protection problem of arsenic is solved.
Drawings
FIG. 1 is a process flow diagram of the present invention.
Detailed Description
The present invention will be described in further detail by way of examples, but the scope of the present invention is not limited to the above.
Example 1
According to the process flow of FIG. 1, 9t zinc concentrate (Zn 48%, fe 10%, cu 0.3% and As 0.1%) and white smoke 4t (Zn 2%, fe 3%, cu 17% and As 10%) are mixed to obtain a mixture 13t (Zn 34%, fe 8%, cu 5% and As 3%), water is added to grind the mixture to obtain ore pulp with solid mass concentration of 65-70% and particle size of 90% less than 44 μm, and the ore pulp is fed into an autoclave, and waste electrolyte (acidity of 160-180 g/L H is added 2 SO 4 ) The molar ratio of zinc acid is controlled by adding waste electrolyte, 99% pure oxygen is introduced to carry out oxygen pressure leaching, the molar ratio of zinc acid is controlled to be 0.9, the temperature is 145 ℃ and the pressure is 1.2Mpa, and the reaction is carried outAfter 100min, obtaining 70m oxygen immersion liquid after dense filtration 3 (Zn 107g/L，Fe 2g/L，Cu 10g/L，As 0.07g/L，Cl 0.4g/L，H 2 SO 4 5.2 g/L), zinc leaching rate is 98.2%, copper leaching rate is 96%. Adding zinc powder twice the sum of Cu mass into oxygen leaching solution, controlling pH to 1.2, temperature to 70 ℃, and reacting for 3 hours to obtain solution 70m after copper removal and dechlorination 3 (Zn 122g/L, fe 2.0g/L, cu 0.07g/L, as 0.04g/L, cl 0.1 g/L) and copper slag. And (3) delivering the solution after copper removal and dechlorination to remove iron and purify, and carrying out electrolysis and casting to produce the electro-zinc. Copper slag 0.89t (Cu 78%) is returned to copper pyrometallurgy. The oxygen leaching slag is sent to a flotation process for sulfur recovery to obtain flotation tailings and sulfur, the flotation tailings are smelted by a pyrogenic process to obtain slag 3.0t (Zn 1.2%, fe 28%, cu 0.6% and As 10%) and flue gas, and the slag is sent to water quenching to obtain solid arsenic harmless slag; and sending the flue gas to acid to produce sulfuric acid.
Comparative example 1
Adding water into 13t zinc concentrate (Zn 48%, fe 10%, cu 0.3% and As 0.1%), grinding to obtain pulp with solid mass concentration of 65-70% and particle size of 90% less than 44 μm, feeding into autoclave, adding waste electrolyte (acidity 160-180 g/L H) 2 SO 4 ) Controlling the molar ratio of zinc acid by adding waste electrolyte, introducing 99% pure oxygen to perform oxygen pressure leaching, controlling the molar ratio of zinc acid to 0.9, controlling the temperature to 145 ℃, controlling the pressure to 1.2Mpa, reacting for 100min, and obtaining 70m oxygen leaching solution after dense filtration 3 (Zn 132g/L，Fe 2g/L，Cu 0.5g/L，As 0.2g/L，Cl 0.4g/L，H 2 SO 4 30 g/L), zinc leaching rate is 98%, copper leaching rate is 95.6%.
In this comparative example, although the leaching rate of zinc is not affected to a large extent, the sulfuric acid concentration in the oxygen immersion liquid is as high as 30g/L, which would seriously affect the subsequent treatment of the oxygen immersion liquid.
Comparative example 2:
adding water into 13t white smoke dust (Zn 2%, fe 3%, cu 17% and As 10%), grinding to obtain pulp with solid mass concentration of 65-70% and particle size of 90% less than 44 μm, feeding into autoclave, adding sulfuric acid solution of ferric sulfate (Fe 10 g/L), adding oxygen with purity of 99% for ensuring acid-zinc ratioOxygen pressure leaching, controlling the molar ratio of zinc acid to 0.9, the temperature to 145 ℃, the pressure to 1.2Mpa, and the reaction time to 100min to obtain 70m oxygen leaching solution 3 (Zn 3.5g/L，Fe 1g/L，Cu30g/L，As 9g/L，Cl 0.2g/L，H 2 SO 4 6 g/L), zinc leaching rate is 92.3%, copper leaching rate is 96.2%.
Adding zinc powder with the mass twice of that of Cu into the oxygen leaching solution, controlling the pH value to be 1.2, controlling the temperature to be 70 ℃ and reacting for 3 hours to obtain a solution 70m after copper removal and dechlorination 3 (Zn 84.6g/L, fe 1g/L, cu 0.12g/L, as 7.5g/L, cl 0.1 g/L) and copper slag. And (3) removing copper, arsenic and chlorine, and delivering the solution to iron removal purification, electrolysis and casting to produce the electro-zinc. 2.7t (Cu 78%) of copper slag is returned to copper pyrometallurgy. The oxygen leaching slag is sent to a flotation process for sulfur recovery to obtain flotation tailings and sulfur, the flotation tailings are smelted by a pyrogenic process to obtain slag and flue gas, and the slag is sent to water quenching to obtain arsenic-fixing harmless slag; and sending the flue gas to acid to produce sulfuric acid.
In this comparative example, an acid solution of ferric sulfate was added in an amount of 10g/L (this content was substantially identical to the iron content in the leachate after co-leaching in example 1). This iron content was insufficient, so that in the same case, 9g/L of As still remained after oxygen pressure leaching.
If the arsenic in the copper white dust with the same weight needs to be fully settled, the inventor verifies that the iron content of the added ferric sulfate needs to be 30g/L, so that the As in the white dust can be removed to a similar low content.
Comparative example 3
9t zinc concentrate (Zn 48%, fe 10%, cu 0.3%, as 0.1%) and white smoke 4t (Zn 2%, fe 3%, cu 17%, as 10%) are mixed to obtain a mixture 13t (Zn 34%, fe 8%, cu 5%, as 3%), water is added to grind to obtain pulp with solid mass concentration of 65-70%, particle size of 90% is less than 44 μm, the pulp is fed into an autoclave, waste electrolyte is added, and waste electrolyte (acidity is 160-180 g/L H) 2 SO 4 ) Controlling the molar ratio of zinc acid by adding waste electrolyte, introducing 99% pure oxygen to perform oxygen pressure leaching, controlling the molar ratio of zinc acid to 0.9, controlling the temperature to 120 ℃, controlling the pressure to 0.4Mpa, and reacting for 100min to obtain 70m oxygen leaching solution 3 (Zn 95g/L，Fe 9g/L，Cu 9g/L，As 4.5g/L，Cl 0.4g/L，H 2 SO 4 10 g/L), zinc leaching rate is 80%, copper leaching rate is 88%.
Adding zinc powder with the mass twice of that of Cu into the oxygen leaching solution, controlling the pH value to be 1.2, controlling the temperature to be 70 ℃ and reacting for 3 hours to obtain a solution 70m after copper removal and dechlorination 3 (Zn 122g/L, fe 7.0g/L, cu 2g/L, as 3.5g/L, cl 0.1 g/L) and copper slag. And (3) delivering the solution after copper removal and dechlorination to remove iron and purify, and carrying out electrolysis and casting to produce the electro-zinc. Copper slag 0.64t (Cu 77%) is returned to copper pyrometallurgy. The oxygen leaching slag is sent to a flotation process for sulfur recovery to obtain flotation tailings and sulfur, the flotation tailings are smelted by a pyrogenic process to obtain slag 4.0t (Zn 1.8%, fe 22%, cu 0.6% and As 0.3%) and flue gas, and the slag is sent to water quenching to obtain solid arsenic harmless slag; and sending the flue gas to acid to produce sulfuric acid.
This comparative example shows that the temperature is lower than the claimed temperature range, the leaching rate of zinc and copper is low, the oxygen pressure leaching solution Fe is high, and the As content is high. The main reason is that Fe of the oxygen pressure leaching solution is ferrous iron (Fe 2+ ) It is difficult to combine with As to form ferric arsenate, so that the arsenic removal effect is not obvious.
Comparative example 4
9t zinc concentrate (Zn 48%, fe 10%, cu 0.3%, as 0.1%) and white smoke 4t (Zn 2%, fe 3%, cu 17%, as 10%) are mixed to obtain a mixture 13t (Zn 34%, fe 8%, cu 5%, as 3%), water is added to grind to obtain pulp with solid mass concentration of 65-70%, particle size of 90% is less than 44 μm, the pulp is fed into an autoclave, waste electrolyte is added, and waste electrolyte (acidity is 160-180 g/L H) 2 SO 4 ) Controlling the molar ratio of zinc acid by adding waste electrolyte, introducing 99% pure oxygen to perform oxygen pressure leaching, controlling the molar ratio of zinc acid to 0.9, controlling the temperature to 170 ℃, controlling the pressure to 1.5Mpa, and reacting for 100min to obtain 70m oxygen leaching solution 3 (Zn 107g/L，Fe 2g/L，Cu 10g/L，As 4.3g/L，Cl 0.4g/L，H 2 SO 4 55 g/L), zinc leaching rate is 98.3%, copper leaching rate is 96.2%.
Adding zinc powder with the mass twice of that of Cu into the oxygen leaching solution, controlling the pH value to be 1.2, controlling the temperature to be 70 ℃ and reacting for 3 hours to obtain a solution 70m after copper removal and dechlorination 3 (Zn 136g/L, fe 2.0g/L, cu0.1 g/L, as 3.4g/L, cl 0.1 g/L) andcopper slag. And (3) delivering the solution after copper removal and dechlorination to remove iron and purify, and carrying out electrolysis and casting to produce the electro-zinc. 12.7t (Cu 78%) of copper slag is returned to copper pyrometallurgy. The oxygen leaching slag is sent to a flotation process for sulfur recovery to obtain flotation tailings and sulfur, the flotation tailings are smelted by a pyrogenic process to obtain slag 2.8t (Zn 1.1%, fe 26%, cu 0.2% and As 4%) and flue gas, and the slag is sent to water quenching to obtain solid arsenic harmless slag; and sending the flue gas to acid to produce sulfuric acid.
In this comparative example, the temperature is higher than the claimed temperature range, and the leaching rate of zinc and copper is still higher and basically unchanged.
The oxygen pressure leachate has low Fe content but still high As content, mainly because the dissolved Fe forms Fe 2 O 3 Into the slag phase, i.e. iron is removed As hematite, which part of the Fe can no longer combine with As to form ferric arsenate precipitates.
Comparative example 5
9t zinc concentrate (Zn 48%, fe 10%, cu 0.3% and As 0.1%) and white smoke 4t (Zn 2%, fe 3%, cu 17% and As 10%) are mixed to prepare a mixture 13t (Zn 34%, fe 8%, cu 5% and As 3%) which is added with water to grind to obtain pulp with solid mass concentration of 65-70% and particle size of 90% smaller than 44 mu m, and the pulp is fed into an autoclave, waste electrolyte is added, and waste electrolyte (acidity 160-180 g/L H) 2 SO 4 ) Controlling the molar ratio of zinc acid by adding waste electrolyte, introducing 99% pure oxygen to perform oxygen pressure leaching, controlling the molar ratio of zinc acid to 0.6, controlling the temperature to 145 ℃, controlling the pressure to 1.2Mpa, reacting for 100min, and obtaining 70m oxygen leaching solution after dense filtration 3 (Zn 98.2g/L，Fe 3g/L，Cu 9.3g/L，As 1.7g/L，Cl 0.4g/L，H 2 SO 4 5.5 g/L), zinc leaching rate is 84.2%, copper leaching rate is 85%. Adding zinc powder (the addition amount is 2 times of the mass of Cu) into the oxygen leaching solution, controlling the pH value to be 1.2, controlling the temperature to be 70 ℃, and reacting for 3 hours to obtain a solution 70m after copper removal and dechlorination 3 (Zn 131g/L, fe 3g/L, cu 0.5g/L, as1.2g/L, cl 0.1 g/L) and copper slag. And (3) delivering the solution after copper removal and dechlorination to remove iron and purify, and carrying out electrolysis and casting to produce the electro-zinc. And 0.8t (Cu 77%) of copper slag is returned to copper pyrometallurgy. The oxygen leaching slag is sent to a flotation process for sulfur recovery, and then flotation tailings and sulfur are obtained, and the flotation tailings are smelted by a pyrogenic process4.1t (Zn 1.6%, fe 24%, cu 0.6%, as 7%) of slag and smoke are obtained, and the slag is sent to water quenching to obtain arsenic-fixing harmless slag; and sending the flue gas to acid to produce sulfuric acid.
In the comparative example, the molar ratio of zinc acid is lower than the molar ratio range of zinc acid in the claims, and the leaching rate of zinc and copper is lower.
The oxygen pressure leaching solution has higher Fe and As, and the main reason is that the molar ratio of acid zinc is reduced, so that the amount of acid participating in the reaction is reduced, and the content of Zn, cu and Fe in the leaching solution is reduced, thus the leaching rate of Cu and Zn is reduced. The reduction of Fe reduces the formation of ferric arsenate precipitate by combining with As, so that the Fe and As contents in the oxygen pressure leaching solution are still slightly higher.
Comparative example 6
9t zinc concentrate (Zn 48%, fe 10%, cu 0.3% and As 0.1%) and white smoke 4t (Zn 2%, fe 3%, cu 17% and As 10%) are prepared into a mixture 13t (Zn 34%, fe 8%, cu 5% and As 3%), water is added for grinding to obtain pulp solid with mass concentration of 65-70%, particle size of 90% is smaller than 44 μm, the pulp solid is sent into an autoclave, waste electrolyte is added, 99% pure oxygen is introduced for oxygen pressure leaching, the mole ratio of zinc acid is controlled to be 1.5, the temperature is 145 ℃, the pressure is 1.2Mpa, the reaction time is 100min, and the oxygen leaching liquid is obtained after dense filtration, the oxygen leaching liquid is 70m 3 (Zn 107g/L，Fe 11g/L，Cu 8.9g/L，As 4.2g/L，Cl 0.4g/L，H 2 SO 4 48 g/L), zinc leaching rate is 98.4%, copper leaching rate is 96.2%. Adding zinc powder (the addition amount is 2 times of the mass of Cu) into the oxygen leaching solution, controlling the pH value to be 1.2, controlling the temperature to be 70 ℃, and reacting for 3 hours to obtain a solution 70m after copper removal and dechlorination 3 (Zn 146g/L, fe 10g/L, cu 0.6g/L, as 2.9g/L, cl 0.1 g/L) and copper slag. And (3) delivering the solution after copper removal and dechlorination to remove iron and purify, and carrying out electrolysis and casting to produce the electro-zinc. Copper slag 0.84t (Cu 68%) is returned to copper pyrometallurgy. The oxygen leaching slag is sent to a flotation process for sulfur recovery to obtain flotation tailings and sulfur, the flotation tailings are smelted by a pyrogenic process to obtain slag 2.7t (Zn 1.2%, fe16%, cu 0.6% and As 0.3%) and flue gas, and the slag is sent to water quenching to obtain solid arsenic harmless slag; and sending the flue gas to acid to produce sulfuric acid.
In this comparative example, the molar ratio of zinc acid is higher than the range of the molar ratio of zinc acid in the claims, and the leaching rates of zinc and copper are extremely higher than those in example 1A small rise. The main reason is that the molar ratio of acid zinc is increased, the acid quantity participating in the reaction is increased, and the leaching of Zn, cu and Fe in the leaching solution is facilitated. However, the problem is that the final acid is raised, so that the dissolved Fe cannot generate Fe (OH) 3 Further, it is not possible to combine with As in the solution to produce ferric arsenate. Therefore, the concentration of Fe and As in the oxygen pressure leaching solution is higher.
Example 2
9t zinc concentrate (Zn 48%, fe 10%, cu 0.3% and As 0.1%) and white smoke 4t (Zn 10%, fe 2%, cu 7% and As 15%) are prepared into a mixture 13t (Zn 36%, fe 8%, cu 2% and As 5%), water is added for grinding to obtain pulp with solid mass concentration of 65-70%, particle size of 90% is smaller than 44 mu m, the pulp is sent into an autoclave, waste electrolyte is added, 99% pure oxygen is introduced for oxygen pressure leaching, the mole ratio of acid zinc is controlled to be 1.0, the temperature is 150 ℃, the pressure is 1.0MPa, the reaction time is 120min, and the oxygen leaching solution is obtained with 70m 3 (Zn 110g/L，Fe 2.0g/L，Cu 4g/L，As 0.08g/L，Cl 0.4g/L，H 2 SO 4 5.4 g/L), zinc leaching rate is 98.5%, copper leaching rate is 95%. Adding zinc powder with Cu quality three times into oxygen leaching solution, controlling pH to 1.0, temperature to 80 ℃, and reacting for 3.5h to obtain copper-removing dechlorinated solution 70m 3 (126 g/L of Zn, 2.0g/L of Fe, 0.06g/L of Cu, 0.05g/L of As and 0.2g/L of Cl) and copper slag. And (3) delivering the solution after copper removal and dechlorination to remove iron and purify, and carrying out electrolysis and casting to produce the electro-zinc. Copper slag 0.37t (Cu 74%) is returned to copper pyrometallurgy. The oxygen leaching slag is sent to a flotation process for sulfur recovery to obtain flotation tailings and sulfur, the flotation tailings are smelted by a pyrogenic process to obtain slag 2.9t (Zn 1.0%, fe 29%, cu 0.4% and As 17%) and flue gas, and the slag is sent to water quenching to obtain solid arsenic harmless slag; and sending the flue gas to acid to produce sulfuric acid.
The method for removing arsenic from copper smelting smoke dust and recycling valuable metals provided by the invention is described in detail. The principles and embodiments of the present invention have been described herein with reference to specific examples, but the above examples are merely intended to aid in the organization of the methods and core concepts of the invention. It should be noted that it will be apparent to those skilled in the art that various modifications and adaptations of the invention can be made without departing from the principles of the invention and these modifications and adaptations are intended to be within the scope of the invention as defined in the following claims.
Claims (3)
1. The method for cooperatively treating zinc concentrate and copper white smoke is characterized by comprising the following steps of:
(1) Mixing zinc concentrate and copper white smoke dust, adding water, and grinding to obtain ore pulp;
(2) Adding waste electrolyte into ore pulp, adjusting the molar ratio of acid zinc in the ore pulp to 0.8-1.1, performing oxygen pressure leaching, and filtering to obtain oxygen leaching liquid and oxygen leaching slag;
(3) Zinc powder is added into the oxygen immersion liquid to remove copper and chlorine, so as to obtain copper slag and copper-removed and chlorine-removed liquid;
the zinc concentrate comprises the following main components in percentage by mass: 40-55% of Zn, 1-15% of Fe, 0.1-1% of Cu and 0.05-0.5% of As;
the copper white smoke dust comprises the following main components in percentage by mass: 5-18% of Cu, 1-5% of Zn, 6-20% of As and 1-5% of Fe;
in the step (1), the mass ratio of the zinc concentrate to the copper white smoke dust is 1 (30% -50%);
in the step (2), the temperature is controlled to be 145-155 ℃ and the pressure is controlled to be 1.0-1.2 mpa in the oxygen pressure leaching process, and the reaction time is 100-120 min;
in the step (3), the addition amount of zinc powder is 2-5 times of the mass of Cu;
in the step (3), zinc powder is added to remove copper and chlorine under the conditions of pH 1.0-1.5, temperature 70-80 ℃ and reaction time 3-4 h.
2. The method of claim 1, wherein in step (3), the copper slag is returned to the copper pyrometallurgy; and (3) delivering the solution after copper removal and dechlorination to remove iron and purify, and carrying out electrolysis and casting to produce the electro-zinc.
3. The method according to claim 1, wherein in the step (2), after sulfur is recovered from the oxygen leaching slag by floatation, the floatation tailings are sent to a pyrometallurgical system, and the pyrometallurgical slag is subjected to water quenching to obtain harmless slag; and sending the flue gas to acid to produce sulfuric acid.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210669026.XA CN114990351B (en) | 2022-06-14 | 2022-06-14 | Method for cooperatively treating zinc concentrate and copper white smoke dust |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210669026.XA CN114990351B (en) | 2022-06-14 | 2022-06-14 | Method for cooperatively treating zinc concentrate and copper white smoke dust |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN114990351A CN114990351A (en) | 2022-09-02 |
| CN114990351B true CN114990351B (en) | 2024-01-30 |
Family
ID=83034467
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202210669026.XA Active CN114990351B (en) | 2022-06-14 | 2022-06-14 | Method for cooperatively treating zinc concentrate and copper white smoke dust |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN114990351B (en) |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4244734A (en) * | 1979-07-19 | 1981-01-13 | Hazen Research, Inc. | Process for recovering metal values from materials containing arsenic |
| JPH04311541A (en) * | 1991-04-08 | 1992-11-04 | Akita Seiren Kk | Wet-type treating method for zinc concentration and zinc leaching residue at the same time |
| CN105603186A (en) * | 2016-01-24 | 2016-05-25 | 李家元 | Technology for efficiently and selectively separating zinc in zinc sulfide concentrate |
| CN105734300A (en) * | 2014-12-08 | 2016-07-06 | 云南云铜锌业股份有限公司 | Method for recovering copper from copper dust and immobilizing arsenic from copper dust into scorodite |
| CN113684368A (en) * | 2021-08-29 | 2021-11-23 | 中南大学 | Method for co-processing arsenic sulfide slag and arsenic-containing smoke dust in copper smelting |
| CN114561547A (en) * | 2022-03-14 | 2022-05-31 | 昆明理工大学 | Method for comprehensively recovering valuable metals in high-zinc copper smelting smoke dust |
| CN114592129A (en) * | 2022-03-14 | 2022-06-07 | 昆明理工大学 | Method for comprehensively recovering valuable metals in high-copper-content smelting smoke dust |
| CN114606388A (en) * | 2022-03-14 | 2022-06-10 | 昆明理工大学 | Method for leaching arsenic-containing copper smelting smoke and synchronously removing arsenic |
-
2022
- 2022-06-14 CN CN202210669026.XA patent/CN114990351B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4244734A (en) * | 1979-07-19 | 1981-01-13 | Hazen Research, Inc. | Process for recovering metal values from materials containing arsenic |
| JPH04311541A (en) * | 1991-04-08 | 1992-11-04 | Akita Seiren Kk | Wet-type treating method for zinc concentration and zinc leaching residue at the same time |
| CN105734300A (en) * | 2014-12-08 | 2016-07-06 | 云南云铜锌业股份有限公司 | Method for recovering copper from copper dust and immobilizing arsenic from copper dust into scorodite |
| CN105603186A (en) * | 2016-01-24 | 2016-05-25 | 李家元 | Technology for efficiently and selectively separating zinc in zinc sulfide concentrate |
| CN113684368A (en) * | 2021-08-29 | 2021-11-23 | 中南大学 | Method for co-processing arsenic sulfide slag and arsenic-containing smoke dust in copper smelting |
| CN114561547A (en) * | 2022-03-14 | 2022-05-31 | 昆明理工大学 | Method for comprehensively recovering valuable metals in high-zinc copper smelting smoke dust |
| CN114592129A (en) * | 2022-03-14 | 2022-06-07 | 昆明理工大学 | Method for comprehensively recovering valuable metals in high-copper-content smelting smoke dust |
| CN114606388A (en) * | 2022-03-14 | 2022-06-10 | 昆明理工大学 | Method for leaching arsenic-containing copper smelting smoke and synchronously removing arsenic |
Also Published As
| Publication number | Publication date |
|---|---|
| CN114990351A (en) | 2022-09-02 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102994747B (en) | Technology for recovering metallic copper from high-lead copper matte | |
| US4004991A (en) | Two-stage pressure leaching process for zinc and iron bearing mineral sulphides | |
| CA2856341A1 (en) | Method for producing high-purity nickel sulfate | |
| CN110438344A (en) | The method of separation of Cu and Co recycling | |
| CN105543479B (en) | A kind of comprehensive recovering process of bismuth matte | |
| CN111647754A (en) | Comprehensive utilization method of zinc-containing dust and sludge in steel plant | |
| CN113846214B (en) | Method for treating zinc-containing material in zinc hydrometallurgy production | |
| CN112410555B (en) | Comprehensive recovery method for flotation silver concentrate from zinc hydrometallurgy acidic leaching residue | |
| CN105200242B (en) | A kind of method that cadmium is reclaimed from containing arsenic refining lead oxygen bottom blown furnace cigarette ash | |
| CN108588425B (en) | Treatment method of cobalt-nickel metallurgy wastewater slag | |
| CN111748690B (en) | Method for purifying and deironing hydrometallurgy leaching solution based on hydrothermal lattice transformation | |
| CN115044778B (en) | Method for leaching zinc oxide and copper white smoke dust in mixed mode | |
| CA1097507A (en) | Process of treating residues from the leaching of roasted zinc blende | |
| CN110585865B (en) | Method for treating zinc smelting sulfur dioxide flue gas by using zinc hydrometallurgy iron-containing precipitation slag | |
| CN114606400B (en) | Treatment method of high-iron arsenic-zinc-containing leaching residues | |
| CN111235404A (en) | Impurity removal method for producing cobalt hydroxide from copper raffinate | |
| WO2020062145A1 (en) | Oxygen pressure leaching method for copper sulfide concentrate and copper smelting method | |
| CN1800422A (en) | Method for processing cobalt copper alloy | |
| CN114990351B (en) | Method for cooperatively treating zinc concentrate and copper white smoke dust | |
| CN109913647B (en) | Wet processing method for recovering copper and zinc in bismuth middling | |
| CN114214520B (en) | Copper-containing refractory material waste-free environment-friendly recovery method | |
| CN109576500A (en) | A kind of technique for extracting metallic zinc from the height cigarette ash of zinc containing chlorine | |
| CN114934192B (en) | Method for cooperatively leaching zinc concentrate and arsenic sulfide slag | |
| Monhemius | The electrolytic production of zinc | |
| CN115011810A (en) | Leaching process for improving copper recovery rate in zinc roasted ore |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |