CN111809059B - Zinc dross dechlorination process - Google Patents
Zinc dross dechlorination process Download PDFInfo
- Publication number
- CN111809059B CN111809059B CN202010441619.1A CN202010441619A CN111809059B CN 111809059 B CN111809059 B CN 111809059B CN 202010441619 A CN202010441619 A CN 202010441619A CN 111809059 B CN111809059 B CN 111809059B
- Authority
- CN
- China
- Prior art keywords
- copper
- leaching
- bismuth
- zinc
- 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
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
- 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
- C22B7/04—Working-up slag
-
- 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
-
- 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
-
- 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
-
- 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
-
- 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
- C22B7/006—Wet processes
- C22B7/008—Wet processes by an alkaline or ammoniacal leaching
-
- 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
Abstract
The invention relates to a zinc scum dechlorination process, which is characterized in that firstly, copper bismuth slag generated by separating rhenium from waste acid generated by acid preparation from copper smelting flue gas through copper sulfide precipitation and bismuth precipitation is subjected to dearsenification by an alkaline method, and alkaline leaching solution contains 20-40 g/L of arsenic and is used for preparing arsenic products; oxidizing and leaching the alkaline leaching residue in a sulfuric acid system, and performing solid-liquid separation to obtain a copper sulfate solution and a residue phase, wherein the bismuth content of the residue phase is up to 40-60% and the residue phase is used for recovering bismuth; adding zinc dross in half of the volume of the copper leaching solution, adding the other half of the copper leaching solution after complete reaction for neutralization reaction for dechlorination, performing solid-liquid separation to obtain a slag phase and a zinc sulfate solution, performing alkali washing on the slag phase, returning to the neutralization dechlorination process, sending the alkali washing solution to a water treatment system, and returning the zinc sulfate solution to the zinc electrodeposition process. The invention not only removes the chlorine in the zinc dross, but also opens the way for the arsenic and bismuth which are accumulated continuously during the copper smelting, solves the problem of resource waste caused by the piling up of the zinc dross produced by the wet zinc smelting, and realizes the resource utilization of the dross.
Description
Technical Field
The invention belongs to a wet metallurgy process in the metallurgy field, in particular to a zinc dross dechlorination process.
Background
At present, ammonium chloride is usually added in the fusion casting process of zinc cathode in the wet zinc smelting to break away zinc oxide films wrapping zinc particles and reduce the amount of zinc dross, but each 1 ten thousand tons of cathode zinc can be produced to produce 450 tons of zinc dross, wherein the zinc content is more than 80%. At present, zinc smelting enterprises remove chlorine in zinc dross through water washing and alkali washing, but the two methods consume a large amount of water and sodium carbonate, and the removal rate of chlorine by the water washing method is only 50%; the removal rate of chlorine in the fire dechlorination process can reach more than 99 percent, but the process has large investment, high energy consumption and large zinc loss, and chlorine enters a sulfuric acid system along with furnace gas to cause equipment corrosion and blockage of a ventilation device pipeline, so that the chlorine is mainly stockpiled or sold at low price at present to cause secondary resource waste and plant area environmental pollution. In addition, a large amount of copper-bismuth slag is generated in the process of extracting rhenium metal from waste acid generated in acid preparation by copper smelting flue gas through sulfuration fractional precipitation, at present, metal copper is recovered mainly through furnace returning smelting, and metal bismuth and arsenic are circulated in a closed loop in a system and are continuously enriched and enter an electrolyte along with anode copper, so that surface granulation and the like of cathode copper are easily caused, and the quality of the cathode copper is influenced. Therefore, the development and operation of the zinc dross dechlorination process which is simpler, more convenient and faster and has low investment and production cost is urgently needed.
Disclosure of Invention
The invention aims to provide a zinc dross dechlorination process which has the characteristics of short flow, simple and convenient operation, low investment, no secondary pollution and the like, can effectively remove chlorine in zinc dross and has important popularization value in industry.
In order to achieve the purpose, the invention discloses a zinc dross dechlorination process, which is characterized by comprising the following steps:
step 1: the method comprises the steps of leaching copper-bismuth slag by a sodium hydroxide solution to realize separation of arsenic, copper, bismuth and the like, adding copper-bismuth slag generated by stepwise sulfurization and precipitation of contaminated acid generated in the acid preparation process by copper smelting flue gas into the sodium hydroxide solution in a rhenium extraction process, reacting for 15-60 min under the conditions that the mass ratio of sodium hydroxide to copper-bismuth slag is 3-7: 1, the reaction temperature is 50-80 ℃, the liquid-solid ratio is 3-6: 1L/kg, the stirring speed is 300rpm, and performing solid-liquid separation to obtain an alkali leaching solution and alkali leaching slag; the alkali leaching solution contains 20-40 g/L of arsenic and is used for preparing an arsenic product; carrying out oxidation acid leaching on the alkaline leaching residue to separate copper and bismuth;
step 2: oxidizing acid leaching the alkaline leaching residue obtained in the step 1 to separate copper and bismuth, and adding 70-150 g/L of 98% H in percentage by mass into the alkaline leaching residue obtained in the step 12SO4Reacting the solution for 20-90 min under the conditions that the liquid-solid ratio is 3-6: 1, the reaction temperature is 40-90 ℃, the stirring speed is 300rpm, and filtering to obtain copper leaching liquid and copper leaching slag, wherein the copper leaching slag contains 40-60% of bismuth and is used for recovering the bismuth;
and step 3: performing center returning reaction dechlorination, namely taking copper leaching solution with the volume of one half in the step 2, adding zinc dross according to 0.5-4 times of the mass of copper in the copper-bismuth slag, reacting for 40-120 min at the reaction temperature of 25-60 ℃ and at the stirring speed of 300rpm, then adding the other half of the copper leaching solution, reacting for 1-3 h at the reaction temperature of 50-95 ℃ and at the stirring speed of 300rpm, performing solid-liquid separation to obtain a slag phase and a zinc sulfate solution, and returning the slag phase to the center returning dechlorination process after alkali washing; the zinc sulfate solution contains less than 0.3g/L of chlorine and can return to zinc electrodeposition.
In the technical scheme of the zinc dross dechlorination process, the further preferable technical scheme is characterized in that:
1. in the step 1, the mass ratio of sodium hydroxide to copper-bismuth slag is 3:1, the reaction temperature is 60 ℃, the liquid-solid ratio is 3:1L/kg, and the reaction time is 30 min;
2. in the step 2, the liquid-solid ratio is 3:1, the reaction temperature is 40 ℃, and the reaction time is 20 min;
3. and 3, adding zinc dross which is 0.6 time of the mass of copper in the copper-bismuth slag, reacting at the temperature of 25 ℃ for 60min, then adding the other half of the copper-leaching solution, and reacting at the temperature of 50 ℃ for 1 h.
Compared with the prior art, the invention has the beneficial effects that: carrying out alkaline dearsenification-oxidation acid leaching on copper-bismuth slag generated by copper smelting to recover copper, so that not only can copper and open-circuit arsenic-bismuth be recovered, but also separation of arsenic, copper and bismuth and enrichment of bismuth are realized, and the grade of bismuth in the copper leaching slag reaches 40-60%; reducing partial copper leaching solution by using zinc scum as a reducing agent, adding the other half of the copper leaching solution after complete reaction, performing neutralization reaction for dechlorination, performing solid-liquid separation to obtain a slag phase and a zinc sulfate solution, performing alkali washing on the slag phase, returning the slag phase to the neutralization reaction for dechlorination, and sending the alkali washing solution to wastewater treatment, wherein the chlorine content of the zinc sulfate solution is less than 0.3 g/L. The method opens the circuit for arsenic and bismuth which are continuously accumulated in copper smelting, solves the problem of resource waste caused by stacking of zinc dross produced in zinc hydrometallurgy, and has the advantages of short flow, simple operation and no pollution.
Detailed Description
The following will clearly and completely describe the technical solutions in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Embodiment 1, a zinc dross dechlorination process, comprising the steps of, step 1: the method comprises the steps of leaching copper-bismuth slag by a sodium hydroxide solution to realize separation of arsenic, copper, bismuth and the like, adding copper-bismuth slag generated by stepwise sulfurization and precipitation of contaminated acid generated in the acid preparation process by copper smelting flue gas into the sodium hydroxide solution in a rhenium extraction process, reacting for 15-60 min under the conditions that the mass ratio of sodium hydroxide to copper-bismuth slag is 3-7: 1, the reaction temperature is 50-80 ℃, the liquid-solid ratio is 3-6: 1L/kg, the stirring speed is 300rpm, and performing solid-liquid separation to obtain an alkali leaching solution and alkali leaching slag; the alkali leaching solution contains 20-40 g/L of arsenic and is used for preparing an arsenic product; carrying out oxidation acid leaching on the alkaline leaching residue to separate copper and bismuth; step 2: oxidizing acid leaching the alkaline leaching residue obtained in the step 1 to separate copper and bismuth, and adding 70-150 g/L of 98% H in percentage by mass into the alkaline leaching residue obtained in the step 12SO4Reacting the solution for 20-90 min under the conditions that the liquid-solid ratio is 3-6: 1, the reaction temperature is 40-90 ℃, the stirring speed is 300rpm, and filtering to obtain copper leaching liquid and copper leaching slag, wherein the copper leaching slag contains 40-60% of bismuth and is used for recovering the bismuth; and step 3: performing center returning reaction dechlorination, namely taking copper leaching solution with the volume of one half in the step 2, adding zinc dross according to 0.5-4 times of the mass of copper in the copper-bismuth slag, reacting for 40-120 min at the reaction temperature of 25-60 ℃ and at the stirring speed of 300rpm, then adding the other half of the copper leaching solution, reacting for 1-3 h at the reaction temperature of 50-95 ℃ and at the stirring speed of 300rpm, performing solid-liquid separation to obtain a slag phase and a zinc sulfate solution, and returning the slag phase to the center returning dechlorination process after alkali washing; the zinc sulfate solution contains less than 0.3g/L of chlorine and can return to zinc electrodeposition. The zinc dross comprises the following main chemical components: zn 60-85%, Cl 1-5%, and Fe0.001-0.032%; the copper-bismuth slag comprises the following main chemical components: 10-25% of As, 8-15% of Cu, 20-45% of Bi and 11-16% of S. The sodium hydroxide, the hydrogen peroxide and the sulfuric acid used in the invention are all industrial grade.
Example 2, the zinc dross dechlorination process of example 1, comprises: in the step 1, the mass ratio of the sodium hydroxide to the copper-bismuth slag is 3:1, the reaction temperature is 60 ℃, the liquid-solid ratio is 3:1L/kg, and the reaction time is 30 min.
Example 3, zinc dross dechlorination process according to example 1 or 2: in the step 2, the liquid-solid ratio is 3:1, the reaction temperature is 40 ℃, and the reaction time is 20 min.
Example 4, the zinc dross dechlorination process of example 1, 2 or 3 is carried out by: and 3, adding zinc dross which is 0.6 time of the mass of copper in the copper-bismuth slag, reacting at the temperature of 25 ℃ for 60min, then adding the other half of the copper-leaching solution, and reacting at the temperature of 50 ℃ for 1 h.
Example 5, (1) dearsenification by alkaline process, leaching of copper bismuth slag with sodium hydroxide solution to realize separation of arsenic from copper, bismuth, etc.: adding copper-bismuth slag generated by stepwise sulfurizing and precipitating contaminated acid generated in the acid making process by copper smelting flue gas into a sodium hydroxide solution in a rhenium extraction procedure, reacting for 15-60 min under the conditions that the mass ratio of sodium hydroxide to copper-bismuth slag is 3:1, the reaction temperature is 50-80 ℃, the liquid-solid ratio is 3:1L/kg, and the stirring speed is 300rpm, and carrying out solid-liquid separation to obtain an alkali leaching solution and alkali leaching slag; the alkaline leaching solution contains 32.5g/L arsenic and is used for preparing arsenic products.
(2) Oxidizing acid leaching, and separating copper and bismuth from alkaline leaching residues through oxidizing acid leaching: 70 g/L98% (wt) H is added into the alkaline leaching residue2SO4And (3) reacting the solution for 20min under the conditions that the liquid-solid ratio is 3:1, the reaction temperature is 40 ℃, the stirring speed is 300rpm, and filtering to obtain copper leaching solution and copper leaching slag, wherein the bismuth content of the copper leaching slag is 45.83 percent and the copper leaching slag is used for recovering bismuth.
(3) Performing center returning reaction dechlorination, grinding zinc dross to the granularity of-160 meshes, taking half volume of copper leaching solution, adding zinc dross according to 0.3 time of the mass of copper in copper-bismuth slag, adding the zinc dross at the reaction temperature of 25 ℃ and the stirring speed of 300rpm for 40min, adding the other half volume of copper leaching solution into the reduction mixed solution, reacting for 1h at the reaction temperature of 50 ℃ and the stirring speed of 300rpm, performing solid-liquid separation to obtain a slag phase and a zinc sulfate solution, wherein the chlorine content of the zinc sulfate solution is 0.27g/L, and returning to the zinc electrodeposition process. And after the slag phase is subjected to alkali washing, returning to the neutralization reaction for dechlorination, and sending an alkali washing solution to wastewater treatment.
Example 6, (1) dearsenification by alkaline process, leaching of copper bismuth slag with sodium hydroxide solution to realize separation of arsenic from copper, bismuth, etc.: adding copper-bismuth slag generated by stepwise sulfurizing and precipitating contaminated acid generated in the acid making process by copper smelting flue gas into a sodium hydroxide solution, reacting for 30min under the conditions that the mass ratio of sodium hydroxide to copper-bismuth slag is 4:1, the reaction temperature is 60 ℃, the liquid-solid ratio is 4:1L/kg, and the stirring speed is 300rpm, and carrying out solid-liquid separation to obtain an alkali leaching solution and alkali leaching slag; the alkaline leaching solution contains 36.2g/L arsenic and is used for preparing arsenic products.
(2) Oxidizing acid leaching, and separating copper and bismuth from alkaline leaching residues through oxidizing acid leaching: 100 g/L98% (wt) H is added into the alkaline leaching residue2SO4And reacting the solution for 60min under the conditions that the liquid-solid ratio is 4:1, the reaction temperature is 40-90 ℃, the stirring speed is 300rpm, and filtering to obtain copper leaching solution and copper leaching slag, wherein the bismuth content of the copper leaching slag is 56.84 percent and is used for recovering bismuth.
(3) Performing center returning reaction dechlorination, grinding zinc dross to the granularity of-180 meshes, taking half volume of copper leaching solution, adding zinc dross according to 0.6 time of the mass of copper in copper-bismuth slag, adding the other half volume of copper leaching solution into the reduction mixed solution after 80min at the reaction temperature of 35 ℃ and the stirring speed of 300rpm, reacting for 2h at the reaction temperature of 75 ℃ and the stirring speed of 300rpm, performing solid-liquid separation to obtain a slag phase and a zinc sulfate solution, wherein the chlorine content of the zinc sulfate solution is 0.23g/L, and returning to the zinc electrodeposition process; and after the slag phase is subjected to alkali washing, returning to the neutralization reaction for dechlorination, and sending an alkali washing solution to wastewater treatment.
Example 7, (1) dearsenification by alkaline process, leaching of copper bismuth slag with sodium hydroxide solution to realize separation of arsenic from copper, bismuth, etc.: adding copper-bismuth slag generated by stepwise sulfurizing and precipitating contaminated acid generated in the acid preparation process by the copper smelting flue gas through the contaminated acid in a rhenium extraction process into a sodium hydroxide solution, reacting for 60min under the conditions that the mass ratio of sodium hydroxide to copper-bismuth slag is 7:1, the reaction temperature is 80 ℃, the liquid-solid ratio is 6:1L/kg, and the stirring speed is 300rpm, and carrying out solid-liquid separation to obtain an alkali leaching solution and alkali leaching slag; the alkaline leaching solution contains 37.8g/L arsenic and is used for preparing arsenic products.
(2) Oxidizing acid leaching, and separating copper and bismuth from alkaline leaching residues through oxidizing acid leaching: 150 g/L98% (wt) H is added into the alkaline leaching residue2SO4The solution is reacted for 90min under the conditions that the liquid-solid ratio is 6:1, the reaction temperature is 90 ℃, the stirring speed is 300rpm, and the copper leaching can be obtained after filtrationThe liquid and the copper leaching slag contain 58.46 percent of bismuth and are used for recovering the bismuth.
(3) Performing center returning reaction dechlorination, grinding zinc scum to the granularity of-200 meshes, taking half volume of copper leaching solution, adding zinc scum which is 1 time of the mass of copper in copper-bismuth slag, adding the zinc scum into the copper leaching solution after 120min at the reaction temperature of 50 ℃ and the stirring speed of 300rpm, adding the other half volume of copper leaching solution to reduce the mixed solution, reacting for 3h at the reaction temperature of 95 ℃ and the stirring speed of 300rpm, performing solid-liquid separation to obtain a slag phase and a zinc sulfate solution, wherein the chlorine content of the zinc sulfate solution is 0.29g/L, and returning to the zinc electrodeposition process; and after the slag phase is subjected to alkali washing, returning to the neutralization reaction for dechlorination, and sending an alkali washing solution to wastewater treatment.
The above description is only for the preferred embodiments of the present invention, but the protection scope of the present invention is not limited thereto, and any person skilled in the art can substitute or change the technical solution of the present invention and the inventive concept thereof within the scope of the present invention.
Claims (4)
1. The zinc dross dechlorination process is characterized by comprising the following steps of:
step 1: performing arsenic removal by an alkaline method, leaching copper-bismuth slag by a sodium hydroxide solution to realize separation of arsenic, copper and bismuth, adding copper-bismuth slag generated by stepwise sulfurization precipitation of contaminated acid generated in the acid preparation process by copper smelting flue gas into the sodium hydroxide solution, reacting for 15-60 min under the conditions that the mass ratio of sodium hydroxide to copper-bismuth slag is 3-7: 1, the reaction temperature is 50-80 ℃, the liquid-solid ratio is 3-6: 1L/kg, the stirring speed is 300rpm, and performing solid-liquid separation to obtain an alkali leaching solution and alkali leaching slag; the alkali leaching solution contains 20-40 g/L of arsenic and is used for preparing an arsenic product; carrying out oxidation acid leaching on the alkaline leaching residue to separate copper and bismuth;
step 2: oxidizing acid leaching the alkaline leaching residue obtained in the step 1 to separate copper and bismuth, and adding 70-150 g/L of 98% H in percentage by mass into the alkaline leaching residue obtained in the step 12SO4Reacting the solution for 20-90 min under the conditions that the liquid-solid ratio is 3-6: 1, the reaction temperature is 40-90 ℃, the stirring speed is 300rpm, filtering to obtain copper leaching liquid and copper leaching slag, wherein the bismuth content of the copper leaching slag is 40-60%,used for recovering bismuth;
and step 3: performing center returning reaction dechlorination, namely taking copper leaching solution with the volume of one half in the step 2, adding zinc scum with the mass of 0.5-4 times that of copper in copper-bismuth slag, reacting for 40-120 min at the reaction temperature of 25-60 ℃ and at the stirring speed of 300rpm, then adding the other half of the copper leaching solution, reacting for 1-3 h at the reaction temperature of 50-95 ℃ and at the stirring speed of 300rpm, performing solid-liquid separation to obtain a slag phase and a zinc sulfate solution, and returning the slag phase to the center returning dechlorination process after alkali washing; the zinc sulfate solution contains less than 0.3g/L of chlorine and returns to zinc electrodeposition.
2. The zinc dross dechlorination process of claim 1, wherein: in the step 1, the mass ratio of the sodium hydroxide to the copper-bismuth slag is 3:1, the reaction temperature is 60 ℃, the liquid-solid ratio is 3:1L/kg, and the reaction time is 30 min.
3. The zinc dross dechlorination process of claim 1, wherein: in the step 2, the liquid-solid ratio is 3:1, the reaction temperature is 40 ℃, and the reaction time is 20 min.
4. The zinc dross dechlorination process of claim 1, wherein: and 3, adding zinc dross which is 0.6 time of the mass of copper in the copper-bismuth slag, reacting at the temperature of 25 ℃ for 60min, then adding the other half of the copper-leaching solution, and reacting at the temperature of 50 ℃ for 1 h.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010441619.1A CN111809059B (en) | 2020-05-22 | 2020-05-22 | Zinc dross dechlorination process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010441619.1A CN111809059B (en) | 2020-05-22 | 2020-05-22 | Zinc dross dechlorination process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN111809059A CN111809059A (en) | 2020-10-23 |
| CN111809059B true CN111809059B (en) | 2022-05-03 |
Family
ID=72848471
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202010441619.1A Active CN111809059B (en) | 2020-05-22 | 2020-05-22 | Zinc dross dechlorination process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111809059B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113584313B (en) * | 2021-07-28 | 2023-03-17 | 云南驰宏资源综合利用有限公司 | Method for producing coarse copper powder from high-arsenic copper bismuth slag |
| CN115724442B (en) * | 2022-11-04 | 2024-03-19 | 西北矿冶研究院 | Preparation method of lead thiocyanate |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002249827A (en) * | 2001-02-26 | 2002-09-06 | Nippon Mining & Metals Co Ltd | Treatment method for electrolytic cement copper |
| CN101633982A (en) * | 2009-08-15 | 2010-01-27 | 蒙自矿冶有限责任公司 | Method for circularly removing chlorine in zinc sulphate solution by copper slag |
| CN102586604A (en) * | 2011-01-18 | 2012-07-18 | 郴州市金贵银业股份有限公司 | Technology for wet-processing anode mud containing arsenic and lead |
| CN103397180A (en) * | 2013-08-07 | 2013-11-20 | 江西铜业股份有限公司 | Method for recovering tellurium, bismuth, antimony, and copper from complex material |
| CN104404254A (en) * | 2014-12-22 | 2015-03-11 | 湖南水口山有色金属集团有限公司 | Dechlorinating method |
| CN110616325A (en) * | 2019-08-19 | 2019-12-27 | 西北矿冶研究院 | Method for separating and recovering copper and bismuth in rhenium leaching residues |
-
2020
- 2020-05-22 CN CN202010441619.1A patent/CN111809059B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002249827A (en) * | 2001-02-26 | 2002-09-06 | Nippon Mining & Metals Co Ltd | Treatment method for electrolytic cement copper |
| CN101633982A (en) * | 2009-08-15 | 2010-01-27 | 蒙自矿冶有限责任公司 | Method for circularly removing chlorine in zinc sulphate solution by copper slag |
| CN102586604A (en) * | 2011-01-18 | 2012-07-18 | 郴州市金贵银业股份有限公司 | Technology for wet-processing anode mud containing arsenic and lead |
| CN103397180A (en) * | 2013-08-07 | 2013-11-20 | 江西铜业股份有限公司 | Method for recovering tellurium, bismuth, antimony, and copper from complex material |
| CN104404254A (en) * | 2014-12-22 | 2015-03-11 | 湖南水口山有色金属集团有限公司 | Dechlorinating method |
| CN110616325A (en) * | 2019-08-19 | 2019-12-27 | 西北矿冶研究院 | Method for separating and recovering copper and bismuth in rhenium leaching residues |
Also Published As
| Publication number | Publication date |
|---|---|
| CN111809059A (en) | 2020-10-23 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN111278998A (en) | Method for recovering cobalt, lithium and other metals from spent lithium-based batteries and other feeds | |
| CN100572573C (en) | From clean melt cinder of wet-process zinc metallurgy, reclaim the method for copper | |
| CN109110826B (en) | Production method of battery-grade nickel sulfate | |
| CN101994007B (en) | Method for removing sulfur from waste lead-acid storage battery gypsum mud by using magnesium chloride | |
| CN111945002B (en) | Method for removing copper from waste lithium batteries by recovery wet process | |
| CN109022793B (en) | Method for selectively leaching lithium from waste powder of cathode material containing at least one of cobalt, nickel and manganese | |
| CN111575491B (en) | Resource comprehensive utilization method for purifying cobalt-nickel slag by zinc hydrometallurgy arsenic salt | |
| CN109897966B (en) | Efficient resource utilization method for secondary zinc oxide raw material | |
| CN111809059B (en) | Zinc dross dechlorination process | |
| CN107354484A (en) | Method for removing chlorine in zinc electrolysis waste liquid | |
| CN103290221A (en) | Method for recovering copper, arsenium and antimony from black copper sludge | |
| CN110923462A (en) | Resourceful treatment method for white smoke | |
| CN106755996A (en) | A kind of lead copper matte synthetical recovery processing method | |
| CN109439916A (en) | A kind of method of the wet-treating containing cadmium fumes | |
| CN110747344A (en) | Preparation and regeneration method of circulating copper salt dechlorinating agent | |
| CN108199106B (en) | Recovery process of waste materials in production process of nickel-cobalt-manganese ternary precursor | |
| CN112553468B (en) | Method for producing high-purity manganese sulfate by adopting metal manganese anode mud | |
| CN113025828A (en) | Heavy metal recovery method and vulcanization precipitation method for magnesium-containing wastewater | |
| CN102690951A (en) | Method for removing lead and antimony from alkaline-leaching dearsenification solution of lead anode slime | |
| CN108486379A (en) | The efficient separation method of arsenic and alkali in a kind of arsenic alkaline slag | |
| CN109055748B (en) | Defluorination chlorine agent and preparation method thereof and method for defluorination chlorine using same | |
| CN109055764B (en) | Comprehensive recovery method of high-chlorine low-zinc material | |
| CN103233129A (en) | Wet-process open treatment method of arsenic in copper ashes | |
| CN103496676A (en) | Method for recovering selenium from acid mud wastes of acid production with copper smelting smoke | |
| CN114606388B (en) | Method for leaching arsenic-containing copper smelting smoke dust and synchronously removing arsenic |
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 |