CN110983060B - Method for resource utilization of arsenic filter cake and white smoke - Google Patents
Method for resource utilization of arsenic filter cake and white smoke Download PDFInfo
- Publication number
- CN110983060B CN110983060B CN201911254668.8A CN201911254668A CN110983060B CN 110983060 B CN110983060 B CN 110983060B CN 201911254668 A CN201911254668 A CN 201911254668A CN 110983060 B CN110983060 B CN 110983060B
- Authority
- CN
- China
- Prior art keywords
- white smoke
- leaching
- pressure
- arsenic
- filter cake
- 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
Images
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
- C22B7/02—Working-up flue dust
-
- 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
- C22B61/00—Obtaining metals not elsewhere provided for in this subclass
-
- 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
-
- 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 discloses a method for resource utilization of arsenic filter cakes and white smoke dust, and belongs to the technical field of comprehensive utilization of non-ferrous metal smelting resources. The method comprises the following steps: a. leaching white smoke dust; b. cooling and filtering, namely filtering the feed liquid obtained in the step a to respectively obtain lead-rich slag and white smoke dust leachate; c. b, performing pressure leaching on the arsenic filter cake, pulping the arsenic filter cake and the white smoke leachate obtained in the step b, performing pressure leaching in a high-pressure kettle, filtering after the reaction is finished to obtain leachate and high-pressure slag, wherein the high-pressure slag is rich in copper and sulfur and is used as a raw material to return to a smelting system for batching; d. reducing the leaching solution obtained in the step c by using sulfur dioxide to obtain reduced solution and crude As2O3Crystallizing; e. coarse As2O3Transferring the crystals into a crystallization tank, stirring and washing with purified water, controlling the washing temperature to be 20-60 ℃, and filtering and drying to obtain national standard grade-1 arsenic trioxide; f. and d, recovering rhenium from the reduced liquid obtained in the step d through an ion exchange process or an extraction process to obtain an ammonium rhenate product and a reduction final liquid, and returning the reduction final liquid to the white smoke for leaching.
Description
Technical Field
The invention relates to a method for resource utilization of arsenic filter cakes and white smoke dust, and belongs to the technical field of comprehensive utilization of non-ferrous metal smelting resources.
Background
The white smoke dust is collected in an electric dust collection process in a copper smelting process, contains elements such as copper, lead, zinc, arsenic, bismuth, antimony, gold, silver and the like, and is required to be opened from a system and separately recycled in order to ensure the normal operation of production and prevent the furnace condition from being deteriorated and even the quality of electrolytic copper products from being influenced due to the cyclic accumulation of harmful impurities such as lead, arsenic, antimony, bismuth and the like. The treatment method of the white smoke dust mainly comprises two main types: the pyrogenic process is characterized in that the pyrogenic process is prepared by mixing with other lead-containing raw materials and then carrying out reduction smelting to produce crude lead and lead copper matte, arsenic is enriched in soot, and secondary pollution is generated in the smelting process. The wet process is to make lead, bismuth, gold, silver and the like enriched in leaching slag through acid leaching, elements such as copper and arsenic enter a solution, copper is recovered through extraction electrodeposition process or replacement process and the like, and arsenic is solidified in the form of calcium arsenate and ferric arsenate.
The arsenic filter cake is arsenic sulfide slag obtained by performing sulfuration dearsenification on open-circuit waste acid in the process of washing and purifying copper smelting flue gas, and the main component of the arsenic sulfide slag is arsenic sulfide. The disposal method of arsenic-containing materials mainly comprises two main types: one is harmless disposal, and the arsenic is stored by calcium arsenate and ferric arsenate with stable performance; the other is resource utilization, namely, the arsenic-containing material is comprehensively utilized to prepare an arsenic product, and valuable metals such as copper, rhenium, bismuth and the like are comprehensively recovered, and the typical production process comprises the following steps: acid oxidation leaching under high pressure oxygen (or compressed air) condition, oxidizing arsenic in arsenic sulfide into + 5-valent arsenic acid, filtering, and adding SO2The arsenic acid with the valence of +5 is reduced into arsenous acid with the valence of +3, and the arsenous acid can be precipitated and decomposed to obtain arsenic trioxide due to low solubility.
Disclosure of Invention
The invention aims to provide a method for resource utilization of an arsenic filter cake and white smoke.
The technical scheme adopted by the invention for solving the technical problems is as follows: a method for resource utilization of arsenic filter cakes and white smoke dust comprises the following steps:
a. white smoke leaching
Leaching the white smoke dust in a leaching tank by using a reduction final solution(waste acid stock solution is used in the first liquid preparation, and the waste acid stock solution is SO2The acidity of the waste sulfuric acid solution produced in the flue gas washing and purifying process is 80-150 g/L)) for leaching, wherein the leaching conditions are as follows: the reaction is carried out for 1-4 h at normal pressure and a liquid-solid ratio of 3-7: 1, at a temperature of 60-90 ℃, at a sulfuric acid acidity of 80-150 g/L, and after the reaction is finished, filtering;
b. cooling and filtering
Filtering the feed liquid obtained in the step a to respectively obtain a solid lead bismuth material (hereinafter referred to as lead-rich slag) and a white smoke leachate, wherein the lead-rich slag is used as a lead extraction raw material for sale, and the white smoke leachate is used for pressure leaching of an arsenic filter cake;
c. pressure leaching of arsenic filter cake
B, mixing the white smoke dust leachate obtained in the step b with an arsenic filter cake, and then carrying out pressure leaching in a high-pressure kettle, wherein the reaction conditions are controlled as follows: oxygen (or compressed air) pressure is 0.5-1.5 MPa, temperature is 80-150 ℃, acidity is 60-150 g/L, liquid-solid ratio is 8-13: 1, reaction time is 2-5 h, after the reaction is finished, pressure is slowly released, meanwhile, a cooling coil is started to feed water for cooling, when the temperature is reduced to 40-60 ℃ and the reading of a pressure gauge is zero, filtration is carried out to obtain leachate and high-pressure slag, and the high-pressure slag is rich in copper and sulfur and is used as a raw material to return to a smelting system for batching;
d. reduction of sulfur dioxide
C, transferring the leachate obtained in the step c into a reduction tank, and introducing SO at normal temperature2Reducing the gas for 4-12 h, and performing SO treatment after the reduction is finished2After desorption, the solution is filtered to obtain reduced solution and crude As2O3Crystallizing;
e. the crude As obtained in step d2O3Transferring the crystals into a crystallization tank, stirring and washing with purified water, controlling the washing temperature to be 20-60 ℃, and filtering and drying to obtain national standard grade-1 arsenic trioxide;
f. and d, recovering rhenium from the reduced liquid obtained in the step d through an ion exchange process or an extraction process to obtain an ammonium rhenate product and a reduction final liquid, and returning the reduction final liquid to the white smoke for leaching.
In the step c, if the copper content of the raw material or the leachate is high, the leaching pressure can be properly reduced and controlled to be 0.6-0.85 MPa when the copper needs to be kept in the high-pressure slag as much as possible.
And c, after the reaction is finished, relieving the pressure of the autoclave and cooling to 40-60 ℃, namely after the reaction is finished, closing the air inlet valve, opening the pressure relief valve to gradually relieve the pressure until the reading of the pressure gauge is 0, and simultaneously, opening coil cooling water in the autoclave to cool until the temperature of the feed liquid in the autoclave is lower than 60 ℃.
And in the step c, the high-pressure slag is directly returned to the copper smelting system, namely the obtained high-pressure slag containing copper and sulfur and other copper concentrate raw materials are mixed according to the smelting requirement.
In said step d, SO2The desorption is that after the reduction reaction is finished, the feed liquid is continuously stirred to ensure that SO in the feed liquid2The gas is volatilized and released, is pumped out by a fan and is sent back to the acid making system.
In the step f, the liquid after reduction contains rhenium, and the ammonium rhenate product is prepared by recovering through an ion exchange or extraction process, which is the existing mature production process.
The main chemical reactions involved in the invention are as follows:
(1) pressure oxidation leaching process
As2S3+3CuSO4+4H2O＝2HAsO2+3CuS↓+3H2SO4
2As2S3+6H2O+5O2＝4H3AsO4+6S↓
2CuS+2H2SO4+O2＝2CuSO4+2S↓+2H2O
2HAsO2+O2+2H2O＝2H3AsO4
(2) Reduction crystallization process
H3AsO4+SO2＝HAsO2+H2SO4
2HAsO2＝As2O3↓+H2O
The arsenic filter cake comprises the following main components in percentage by mass: 5-50% of arsenic, 0.1-10% of copper, 20-50% of sulfur and 0.03-0.3% of rhenium.
The white smoke dust comprises the following main components: 3-25% of copper, 5-20% of arsenic, 1-8% of zinc, 8-40% of lead, 1-15% of bismuth, 8-15% of sulfur, 1-5 g/t of gold and 50-300 g/t of silver.
Compared with the prior art, the invention has the following advantages:
realizing the resource utilization of the arsenic filter cake and the white smoke; the recovery rate of valuable elements such as copper, arsenic, rhenium, sulfur and the like is high, and lead, bismuth, gold and silver elements in the white smoke dust are enriched after being leached out and can be used as raw materials for lead and bismuth production; the whole process of the method is in closed cycle, and secondary pollution is avoided.
Drawings
FIG. 1 is a process flow diagram of the present invention.
Detailed Description
The invention is further described with reference to the following figures and detailed description.
A method for resource utilization of arsenic filter cakes and white smoke dust comprises the following steps:
a. white smoke leaching
The leaching of the white smoke dust is carried out in a leaching tank by using a reduction final solution (a waste acid stock solution is used in the first solution preparation, and the waste acid stock solution is SO2The acidity of the waste sulfuric acid solution produced in the flue gas washing and purifying process is 80-150 g/L)) for leaching, wherein the leaching conditions are as follows: the reaction is carried out for 1-4 h at normal pressure and a liquid-solid ratio of 3-7: 1, at a temperature of 60-90 ℃, at a sulfuric acid acidity of 80-150 g/L, and after the reaction is finished, filtering;
b. cooling and filtering
B, filtering the feed liquid obtained in the step a to respectively obtain lead-rich slag and white smoke leachate, wherein the lead-rich slag is used as a lead extraction raw material for sale, and the white smoke leachate is used for pressure leaching of an arsenic filter cake;
c. pressure leaching of arsenic filter cake
B, mixing the white smoke dust leachate obtained in the step b with an arsenic filter cake, and then carrying out pressure leaching in a high-pressure kettle, wherein the reaction conditions are controlled as follows: oxygen (or compressed air) pressure is 0.5-1.5 MPa, temperature is 80-150 ℃, acidity is 60-150 g/L, liquid-solid ratio is 8-13: 1, reaction time is 2-5 h, after the reaction is finished, pressure is slowly released, meanwhile, a cooling coil is started to feed water for cooling, when the temperature is reduced to 40-60 ℃ and the reading of a pressure gauge is zero, filtration is carried out to obtain leachate and high-pressure slag, and the high-pressure slag is rich in copper and sulfur and is used as a raw material to return to a smelting system for batching;
d. reduction of sulfur dioxide
C, transferring the leachate obtained in the step c into a reduction tank, and introducing SO at normal temperature2Reducing the gas for 4-12 h, and performing SO treatment after the reduction is finished2After desorption, the solution is filtered to obtain reduced solution and crude As2O3Crystallizing;
e. the crude As obtained in step d2Transferring the O3 crystal into a crystallization tank, stirring and washing with purified water, controlling the water washing temperature to be 20-60 ℃, and filtering and drying to obtain national standard grade-1 arsenic trioxide;
f. and d, recovering rhenium from the reduced liquid obtained in the step d through an ion exchange process or an extraction process to obtain an ammonium rhenate product and a reduction final liquid, and returning the reduction final liquid to the white smoke for leaching.
The following examples are provided to illustrate the present invention and are not intended to limit the scope of the present invention.
Taking arsenic filter cakes and white smoke dust leachate of a certain domestic copper smelting enterprise as an example, the main components of the raw materials are as follows:
formulation of white smoke and arsenic filter cake in certain enterprise (%)
| Name (R) | Cu | As | Zn | S | Pb | Bi | Re | Au(g/t) | Ag(g/t) |
| White smoke and dust | 9.34 | 10.82 | 3.33 | 10.49 | 9.86 | 3.31 | - | 3.8 | 102.98 |
| Arsenic filter cake | 0.11 | 37.08 | - | 46.9 | 2.6 | 0.3 | 0.18 | - | - |
Example 1
1. White smoke leaching
Leaching white smoke dust at the reaction temperature of 80 ℃, the reaction time of 2h, the liquid-solid ratio of 4: 1 and the acidity of 80g/L, and filtering after the reaction is finished to obtain white smoke dust leachate and lead-rich slag, wherein the related components are shown in the following table:
| name (R) | Cu | As | H2SO4 | Pb | Bi | Zn | Au | Ag |
| White smoke dust lixivium (g/L) | 14.15 | 14.20 | 75.3 | - | - | 3.5 | - | - |
| Lead-rich slag (%) | 3.02 | 5.38 | - | 25.56 | 5.41 | 1.26 | 6.02 | 123.83 |
2. Pressure leaching of arsenic filter cake
Mixing and pulping the white smoke dust leachate and the arsenic filter cake, and transferring the mixture into a high-pressure kettle for pressure leaching, wherein the reaction conditions are controlled as follows: oxygen (or compressed air) pressure is 0.6MPa, temperature is 90-115 ℃, acidity is 80g/L, liquid-solid ratio is 10: 1, reaction time is 3h, after the reaction is finished, pressure is slowly released, meanwhile, a cooling coil is started to feed water for cooling, when the temperature is reduced to 60 ℃ and the reading of a pressure gauge is zero, filtration is carried out to obtain leachate and high-pressure slag, and the components are shown in the following table:
| name (R) | Cu | As | Re | S |
| Lixivium (g/L) | 0.84 | 35.14 | 164.0mg/L | - |
| High pressure slag (%) | 9.98 | 4.25 | 0.078 | 70.44 |
3. Reduction crystallization
Cooling the leaching solution to normal temperature, and introducing SO2Reducing the gas for 11h to obtain reduced liquid and As2O3The composition of the crude crystalline, reduced liquid is shown in the following table:
| name (R) | Cu | As | Re | H2SO4 |
| Reduced liquid (g/L) | 0.91 | 15.14 | 174.0mg/L | 85.2 |
4.As2O3Washing and refining
As is2O3Stirring and washing the coarse crystals with purified water at 60 ℃, filtering and drying to obtain finished As products2O3Crystals, the main constituents of which are shown in the following table:
| name (R) | As2O3 | Cu | Zn | Fe | Pb | Bi |
| As2O3Product (%) | 99.65 | 0.0035 | 0.0008 | 0.0017 | 0.00045 | 0.0003 |
Example 2
1. White smoke leaching
Leaching white smoke dust at the reaction temperature of 85 ℃, the reaction time of 2 hours, the liquid-solid ratio of 5: 1 and the acidity of 120g/L, and filtering after the reaction is finished to obtain white smoke dust leachate and lead-rich slag, wherein the related components are shown in the following table:
| name (R) | Cu | As | H2SO4 | Pb | Bi | Zn | Au | Ag |
| White smoke dust lixivium (g/L) | 15.25 | 14.78 | 114.3 | - | - | 4.5 | - | - |
| Lead-rich slag (%) | 1.89 | 2.43 | - | 32.64 | 8.98 | 1.08 | 10.76 | 237.98 |
2. Pressure leaching of arsenic filter cake
Mixing and pulping the white smoke dust leachate and the arsenic filter cake, and transferring the mixture into a high-pressure kettle for pressure leaching, wherein the reaction conditions are controlled as follows: the method comprises the following steps of (1) enabling oxygen pressure to be 1.05MPa, enabling the temperature to be 95-120 ℃, enabling acidity to be 110g/L, enabling liquid-solid ratio to be 10: 1, enabling reaction time to be 3h, after reaction is finished, slowly releasing pressure, simultaneously starting a cooling coil to feed water for cooling, and filtering when the temperature is reduced to 60 ℃ and the reading of a pressure gauge is zero to obtain leachate and high-pressure slag, wherein the components of the leachate and the high-pressure slag are shown in:
| name (R) | Cu | As | Re | S |
| Lixivium (g/L) | 7.45 | 45.9 | 179.8mg/L | - |
| High pressure slag (%) | 4.35 | 2.76 | 0.058 | 79.25 |
3. Reduction crystallization
Cooling the leaching solution to normal temperature, and introducing SO2Reducing the gas for 10 hours to obtain reduced liquid and As2O3The composition of the crude crystalline, reduced liquid is shown in the following table:
| name (R) | Cu | As | Re | H2SO4 |
| Reduced liquid (g/L) | 7.58 | 14.52 | 182.0mg/L | 113.5 |
4.As2O3Washing and refining
As is2O3Stirring and washing the coarse crystals with purified water at 60 ℃, filtering and drying to obtain finished As products2O3Crystals, the main constituents of which are shown in the following table.
| Name (R) | As2O3 | Cu | Zn | Fe | Pb | Bi |
| As2O3Product (%) | 99.75 | 0.0045 | 0.0006 | 0.0013 | 0.00035 | 0.0002 |
Example 3
1. White smoke leaching
Leaching the white smoke dust by using the reduced solution under the conditions of reaction temperature of 80 ℃, reaction time of 2h, liquid-solid ratio of 4: 1 and acidity of 100g/L, and filtering after the reaction is finished to obtain white smoke dust leachate and lead-rich slag, wherein the related components are shown in the following table:
| name (R) | Cu | As | H2SO4 | Re(mg/L) | Pb | Bi | Zn | Au | Ag |
| Liquid after reduction | 6.05 | 13.8 | 102.5 | 135.6 | - | - | - | - | - |
| White smoke dust lixivium (g/L) | 21.03 | 27.4 | 95.7 | 128.3 | - | - | 5.7 | - | - |
| Lead-rich slag (%) | 2.38 | 4.39 | - | - | 29.46 | 8.53 | 1.13 | 9.67 | 181.78 |
2. Pressure leaching of arsenic filter cake
Mixing and pulping the white smoke dust leachate and the arsenic filter cake, and transferring the mixture into a high-pressure kettle for pressure leaching, wherein the reaction conditions are controlled as follows: oxygen (or compressed air) pressure is 0.80MPa, temperature is 90-120 ℃, acidity is 100g/L, liquid-solid ratio is 10: 1, reaction time is 3h, after the reaction is finished, pressure is slowly released, meanwhile, a cooling coil is started to feed water for cooling, when the temperature is reduced to 60 ℃ and the reading of a pressure gauge is zero, filtration is carried out to obtain leachate and high-pressure slag, and the components are shown in the following table:
| name (R) | Cu | As | Re | S |
| Lixivium (g/L) | 3.26 | 54.45 | 285.0mg/L | - |
| High pressure slag (%) | 12.47 | 6.07 | 0.072 | 62.4 |
3. Reduction crystallization
Cooling the leaching solution to normal temperature, and introducing SO2Reducing the gas for 10 hours to obtain reduced liquid and As2O3The composition of the crude crystalline, reduced liquid is shown in the following table:
| name (R) | Cu | As | Re | H2SO4 |
| Reduced liquid (g/L) | 3.52 | 14.39 | 293.2mg/L | 103.5 |
4.As2O3Washing and refining
As is2O3Stirring and washing the coarse crystals with purified water at 60 ℃, filtering and drying to obtain finished As products2O3Crystals, the main constituents of which are shown in the following table:
| name (R) | As2O3 | Cu | Zn | Fe | Pb | Bi |
| As203Product (%) | 99.60 | 0.0055 | 0.0009 | 0.0015 | 0.0004 | 0.0003 |
Claims (4)
1. A method for resource utilization of arsenic filter cakes and white smoke dust is characterized by comprising the following steps: the method comprises the following steps:
a. white smoke leaching
The leaching of the white smoke dust is carried out in a leaching tank, a reduction final solution is used, a waste acid stock solution is used for leaching when a solution is prepared for the first time, and the leaching conditions are as follows: normal pressure, liquid-solid ratio 3-7: 1. the temperature is 60-90 ℃, the sulfuric acid acidity is 80-150 g/L, the reaction time is 1-4 h, and after the reaction is finished, filtration is carried out;
b. cooling and filtering
Filtering the feed liquid obtained in the step a to respectively obtain lead-rich slag and white smoke dust leachate;
c. pressure leaching of arsenic filter cake
B, mixing the white smoke dust leachate obtained in the step b with an arsenic filter cake, and then carrying out pressure leaching in a high-pressure kettle, wherein the reaction conditions are controlled as follows: oxygen or compressed air with the pressure of 0.5-1.5 MPa, the temperature of 80-150 ℃, the acidity of 60-150 g/L and the liquid-solid ratio of 8-13: 1. the reaction time is 2-5 h, after the reaction is finished, slowly releasing pressure, starting a cooling coil pipe for water inlet cooling, and filtering when the temperature is reduced to 40-60 ℃ and the reading of a pressure gauge is zero to obtain a leaching solution and high-pressure slag, wherein the high-pressure slag is rich in copper and sulfur and is used as a raw material to return to a smelting system for batching;
the main chemical reaction is as follows:
d. reduction of sulfur dioxide
C, transferring the leachate obtained in the step c into a reduction tank, and introducing SO at normal temperature2Reducing the gas for 4-12 h, and performing SO treatment after the reduction is finished2After desorption, the solution is filtered to obtain reduced solution and crude As2O3Crystallizing;
the main chemical reaction is as follows:
H3AsO4 + SO2=HAsO2+H2SO4
e. the crude As obtained in step d2O3Transferring the crystals into a crystallization tank, stirring and washing with purified water, controlling the washing temperature to be 20-60 ℃, and filtering and drying to obtain national standard grade-1 arsenic trioxide;
f. and d, recovering rhenium from the reduced liquid obtained in the step d through an ion exchange process or an extraction process to obtain an ammonium rhenate product and a reduction final liquid, and returning the reduction final liquid to the white smoke for leaching.
2. The method for recycling arsenic filter cake and white smoke according to claim 1, wherein the method comprises the following steps: the arsenic filter cake comprises the following main components in percentage by mass: 5-50% of arsenic, 0.1-10% of copper, 20-50% of sulfur and 0.03-0.3% of rhenium.
3. The method for recycling arsenic filter cake and white smoke according to claim 1, wherein the method comprises the following steps: the white smoke dust comprises the following main components: 3-25% of copper, 5-20% of arsenic, 1-8% of zinc, 8-40% of lead, 1-15% of bismuth, 8-15% of sulfur, 1-5 g/t of gold and 50-300 g/t of silver.
4. The method for recycling arsenic filter cake and white smoke according to claim 1, wherein the method comprises the following steps: the waste acid stock solution system SO2And the acidity of the waste sulfuric acid solution produced in the flue gas washing and purifying process is 80-150 g/L.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911254668.8A CN110983060B (en) | 2019-12-09 | 2019-12-09 | Method for resource utilization of arsenic filter cake and white smoke |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911254668.8A CN110983060B (en) | 2019-12-09 | 2019-12-09 | Method for resource utilization of arsenic filter cake and white smoke |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN110983060A CN110983060A (en) | 2020-04-10 |
| CN110983060B true CN110983060B (en) | 2021-07-06 |
Family
ID=70091727
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201911254668.8A Active CN110983060B (en) | 2019-12-09 | 2019-12-09 | Method for resource utilization of arsenic filter cake and white smoke |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110983060B (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111573729B (en) * | 2020-04-14 | 2023-03-24 | 江西铜业股份有限公司 | System and method for preparing arsenic trioxide through continuous reduction |
| 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 |
| CN115261625A (en) * | 2022-07-29 | 2022-11-01 | 济源豫光有色冶金设计研究院有限公司 | Method for recovering copper and arsenic step by step in combined leaching of black copper mud and arsenic filter cake |
| CN115557533A (en) * | 2022-09-15 | 2023-01-03 | 林西金易来砷业有限公司 | Recycling method of arsenic sulfide slag |
| CN115747500A (en) * | 2022-11-14 | 2023-03-07 | 郴州金铖环保科技有限公司 | Method for cooperatively removing chlorine in strong-acid arsenic solution from high-arsenic silver-containing smelting slag |
| CN115821065A (en) * | 2022-12-21 | 2023-03-21 | 黑龙江紫金铜业有限公司 | Recycling method for recycling arsenic and leaching residues from black copper mud and arsenic filter cake |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4572822A (en) * | 1982-02-15 | 1986-02-25 | Dowa Mining Co., Ltd. | Method of recovering metals from industrial by-products |
| CN101037725A (en) * | 2007-02-06 | 2007-09-19 | 朱永文 | Method for treating arsenic pollution of copper smelt industry |
| CN103014355A (en) * | 2012-12-13 | 2013-04-03 | 马永涛 | Multi-metal comprehensive recycling process for copper smelting ash |
| CN103911508A (en) * | 2014-04-28 | 2014-07-09 | 北京矿冶研究总院 | Method for recovering rhenium from arsenic sulfide pressure leaching liquid |
| CN106086426A (en) * | 2016-08-15 | 2016-11-09 | 郴州金山冶金化工有限公司 | A kind of arsenic sulfide slag hyperbaric oxygen leaches resource utilization process continuously |
| CN109930004A (en) * | 2019-04-12 | 2019-06-25 | 江西铜业股份有限公司 | A kind of method of arsenic filter cake resource utilization |
-
2019
- 2019-12-09 CN CN201911254668.8A patent/CN110983060B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4572822A (en) * | 1982-02-15 | 1986-02-25 | Dowa Mining Co., Ltd. | Method of recovering metals from industrial by-products |
| CN101037725A (en) * | 2007-02-06 | 2007-09-19 | 朱永文 | Method for treating arsenic pollution of copper smelt industry |
| CN103014355A (en) * | 2012-12-13 | 2013-04-03 | 马永涛 | Multi-metal comprehensive recycling process for copper smelting ash |
| CN103911508A (en) * | 2014-04-28 | 2014-07-09 | 北京矿冶研究总院 | Method for recovering rhenium from arsenic sulfide pressure leaching liquid |
| CN106086426A (en) * | 2016-08-15 | 2016-11-09 | 郴州金山冶金化工有限公司 | A kind of arsenic sulfide slag hyperbaric oxygen leaches resource utilization process continuously |
| CN109930004A (en) * | 2019-04-12 | 2019-06-25 | 江西铜业股份有限公司 | A kind of method of arsenic filter cake resource utilization |
Also Published As
| Publication number | Publication date |
|---|---|
| CN110983060A (en) | 2020-04-10 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN110983060B (en) | Method for resource utilization of arsenic filter cake and white smoke | |
| CN110093506B (en) | Method for efficiently extracting valuable metals from germanium-containing zinc leaching residues and reducing valuable metals | |
| CN110983059B (en) | Method for recovering copper and arsenic from copper smelting white smoke leachate and arsenic filter cake | |
| CN100572286C (en) | Utilize arsenic-containing waste water to prepare the method for white arsenic | |
| CN113684368A (en) | Method for co-processing arsenic sulfide slag and arsenic-containing smoke dust in copper smelting | |
| CN103643044B (en) | The direct extracting copper of a kind of Bellamya aeruginosa wet method, zinc technology | |
| CN101338368A (en) | Method for preprocessing anode sludge and recovering dissipated metal | |
| CN101037725A (en) | Method for treating arsenic pollution of copper smelt industry | |
| CN101328539A (en) | Oxidation oven ash hydrometallurgical leaching process | |
| CN113549766A (en) | Method for removing arsenic from lead smelting smoke dust and recovering valuable metals | |
| CN106119560A (en) | Zinc-cobalt separation method | |
| CN112708777B (en) | Method for recovering zinc sulfate from zinc-containing waste | |
| CN112725624A (en) | Method for efficiently recycling arsenic-cobalt-nickel-containing slag | |
| CN113621818A (en) | Method for co-processing copper smelting waste acid and arsenic-containing smoke dust | |
| CN114606400B (en) | Treatment method of high-iron arsenic-zinc-containing leaching residues | |
| CN110172583B (en) | Method for efficiently treating arsenic-containing soot in reduction mode | |
| CN104032131A (en) | Method for processing high-tin anode slurry | |
| CN111235404A (en) | Impurity removal method for producing cobalt hydroxide from copper raffinate | |
| AU1135600A (en) | Separation and concentration method | |
| CN104762483A (en) | Method for producing copper sulfate from copper-bismuth scum | |
| CN111979421A (en) | Method for comprehensively utilizing copper-containing arsenic-containing soot produced in copper smelting process | |
| CN1789445A (en) | Method for separating copper, arsenic and zinc from copper-smelting high-arsenic flue dust sulphuric acid leach liquor | |
| CN106636657A (en) | Method for pre-removing arsenic in arsenic-containing soot | |
| CN114214520B (en) | Copper-containing refractory material waste-free environment-friendly recovery method | |
| US5002748A (en) | Method for the preparation of copper arsenate |
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 | ||
| CP02 | Change in the address of a patent holder | ||
| CP02 | Change in the address of a patent holder |
Address after: 161000 No. 1, Fujing Road, Fularji district electric power office, Qiqihar City, Heilongjiang Province Patentee after: HEILONGJIANG ZIJIN COPPER INDUSTRY Co.,Ltd. Address before: 161000 Room 101, science and technology entrepreneurship center building, north end of Gongnong street, Fularji District, Qiqihar City, Heilongjiang Province Patentee before: HEILONGJIANG ZIJIN COPPER INDUSTRY Co.,Ltd. |