CN109055715B - Multi-element comprehensive recovery process for gold refining acidic wastewater - Google Patents

Multi-element comprehensive recovery process for gold refining acidic wastewater Download PDF

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CN109055715B
CN109055715B CN201810964101.9A CN201810964101A CN109055715B CN 109055715 B CN109055715 B CN 109055715B CN 201810964101 A CN201810964101 A CN 201810964101A CN 109055715 B CN109055715 B CN 109055715B
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刘晓勃
高文选
李毅飞
毛鹏飞
雒彩军
许海敏
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Lingbao Jinyuan Mining Co Ltd
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Abstract

A multi-element comprehensive recovery process for gold refining acidic wastewater comprises the following steps: (1) sending the gold refining acidic wastewater into a carbon adsorption tank for cyclic carbon adsorption until the gold grade in the liquid is lower than 0.2mg/L to obtain gold-loaded carbon, and sending the gold-loaded carbon to be analyzed; (2) liquid with gold grade lower than 0.2mg/L is sequentially sent into a No. 1 storage tank, a No. 2 storage tank and a No. 3 storage tank for metal ion replacement reaction, and supernatant in the No. 3 storage tank is discharged to a water treatment workshop for water treatment; drying the precipitate in the No. 3 storage tank at 600 +/-10 ℃ for 3.5-4.5 h, cooling mercury vapor into liquid mercury, and adding borax and soda ash into the dried slag for refining; (3) the refined slag is sent to ball milling and ore blending, the refined alloy is cast into an anode for electrolysis, pure copper is produced at the cathode after electrolysis, and anode mud is produced at the anode; the anode mud is chloridized to obtain gold and silver and waste residue, and the waste residue is returned to the primary refining.

Description

Multi-element comprehensive recovery process for gold refining acidic wastewater
Technical Field
The invention belongs to the field of wet metallurgy, and particularly relates to a multi-element comprehensive recovery process for gold refining acidic wastewater.
Background
In the non-ferrous metal industry, acid wastewater with low pH and containing heavy metals is generated in the processes of metal mining, mineral separation, smelting and the like, if the acid wastewater is not treated, basic facilities such as sewer pipelines, hydraulic structures and the like can be corroded, and the heavy metals in the acid wastewater can seriously pollute surface water, underground water or soil, influence the growth and the propagation of animals and plants and the growth of crops, and cause great harm to the environmental quality and the human health. The common treatment methods for heavy metal-containing acidic wastewater mainly comprise three types:
(1) heavy metal ions in the wastewater are removed through chemical reaction. Including chemical precipitation, redox, high molecular heavy metal collector methods, etc.;
(2) on the premise of not changing the chemical form of the heavy metal, the heavy metal is removed from the water body by the actions of adsorption, concentration, separation and the like. Including adsorption, ion exchange, membrane separation and other methods;
(3) the heavy metals in the wastewater are removed by organisms such as algae, fungi and bacteria through the actions of biological flocculation, biological adsorption, plant absorption and the like.
The chemical precipitation method is the method for removing heavy metals, which has the longest development time, mature process, most effectiveness and wide application range at present.
During the gold refining process, the conditions of acidic wastewater generated by I:
main elements of Au(mg/L) Ag(mg/L) Cu(g/L) Hg(mg/L)
Number of 0.2～3.0 10～30 0.5～2.5 0.2～2.0
The gold refining acid wastewater is discharged for about 4-6 times per month, and is discharged for about 40-60 m each time3And after the gold-containing liquid is discharged to an outdoor carbon adsorption tank for cyclic adsorption, the gold-containing grade of the liquid reaches the standard, and the liquid is discharged to a water treatment workshop for neutralization treatment. The treatment is time-consuming, more importantly, only gold is recovered, and heavy metal mercury and noble metal silver in the wastewater are not effectively recovered.
Disclosure of Invention
The invention aims to provide a multi-element comprehensive recovery process for gold refining acidic wastewater. The method effectively recovers gold, silver, copper and mercury in the acidic wastewater.
Based on the purpose, the invention adopts the following technical scheme:
a multi-element comprehensive recovery process for gold refining acidic wastewater comprises the following steps:
(1) sending the gold refining acidic wastewater into a carbon adsorption tank for cyclic carbon adsorption until the gold grade in the liquid is lower than 0.2mg/L, simultaneously obtaining gold-loaded carbon, and sending the gold-loaded carbon to be analyzed;
(2) liquid with the gold grade lower than 0.2mg/L is sequentially sent into a No. 1 storage tank, a No. 2 storage tank and a No. 3 storage tank (two storage tanks are just enough, and 3 storage tanks can be treated more thoroughly) at the flow rate of 1.0-2.0 m/s for reaction, and supernatant in the No. 3 storage tank is discharged to a water treatment workshop for water treatment; drying the precipitate in the No. 3 storage tank at 600 +/-10 ℃ for 3.5-4.5 h, cooling mercury vapor into liquid mercury, and adding borax and soda ash into the dried slag for refining;
(3) the refined slag is sent to ball mill and ore blending, the alloy after the refining is poured into an anode, and the component of the electrolyte is Cu2+35～40g/L，H+190～230g/L ，SO4 2-225-270 g/L, current density of 150-190A/m2Electrolyzing for 18-22 hours under the condition that the cell voltage is 1.8-2.2V, wherein pure copper is produced at a cathode after electrolysis, and anode mud is produced at an anode; the anode mud is chloridized to obtain gold and silver and waste residue, and the waste residue is returned to the primary refining.
Further, the volumes of the No. 1, the No. 2 storage tanks and the No. 3 storage tank are all 80m, the processing time of the liquid in each storage tank is 1.5-2 hours, the No. 1 storage tank can replace about 65% of the total mass of the metal contained in the liquid, the No. 2 storage tank can replace about 25% of the total mass of the metal contained in the liquid, and the No. 3 storage tank can replace about 5% of the total mass of the metal contained in the liquid.
Further, adding the precipitate of the previous No. 2 storage tank into the No. 1 storage tank, adding the precipitate of the previous No. 3 storage tank into the No. 2 storage tank, and adding iron powder and Na into the No. 3 storage tank2S (iron powder is used for carrying out replacement reaction with some metal ions to replace a part of metal, mainly replacing gold, silver, copper and mercury in liquid, and Na is added2The purpose of S is S2-And a portion of the metal forms sulfide precipitates, such as changing Hg to HgS. ).
Preferably, 60m is treated in step (1)3When the acid wastewater is refined by gold, 10-15 kg of the precipitate of the previous No. 2 storage tank needs to be added into the No. 1 storage tank, 20-25 kg of the precipitate of the previous No. 3 storage tank needs to be added into the No. 2 storage tank, and 20-25 kg of iron powder and Na are added into the No. 3 storage tank2S10-15 kg, if the precipitates in the No. 2 and No. 3 storage tanks are insufficient, iron powder and sodium sulfide can be used for replacing the precipitates, but the mass of the iron powder and the sodium sulfide added into the No. 1 storage tank and the No. 2 storage tank is half of the dosage of the No. 3 storage tank. Iron powder is purchased in the market, and the-200 meshes are required to account for more than 75wt% (namely, the particle size is less than 0.074mm and accounts for more than 75%).
Further, the concrete process of the refining is as follows: the method comprises the steps of proportioning the dried slag, borax and calcined soda according to the mass ratio of 1:0.3:0.2 (the addition of the borax and the calcined soda is used for reducing the melting point of the slag in the smelting process and improving the fluidity of molten slag), adding the mixture into an intermediate frequency furnace to carry out smelting at 1800-1900 ℃ to obtain a smelting solution, pouring the smelting solution into a squatting pot, cooling, taking out an alloy formed at the lower part of the squatting pot, putting the alloy into the intermediate frequency furnace again to melt, and pouring molten metal into the anode size required by electrolytic copper.
Further, the chlorination process is as follows:
a. acid leaching: adding hydrochloric acid and water into a reaction kettle according to the volume ratio of 2:1 to obtain a dilute hydrochloric acid solution, adding anode mud, wherein the mass ratio of the anode mud to the dilute hydrochloric acid solution is 1: 2.5-4.5, leaching at 85-95 ℃ for 2.5-3.5 hours, and separating residues and liquids;
b. chlorination: adding hydrochloric acid and water into a reaction kettle according to the volume ratio of 2:1 to obtain a dilute hydrochloric acid solution, heating to 80 ℃ under stirring, adding the slag separated in the step a, keeping the temperature below 80 ℃, adding sodium chlorate, wherein the dosage of the sodium chlorate is 1.5-2.5 times of the mass of the gold in the anode mud, stirring to react for 2-4 hours at 90-95 ℃, standing for 15-30 minutes after the reaction is finished, starting slag-liquid separation, automatically flowing the liquid into a reduction reaction kettle, and adding iron powder into the slag to replace silver;
c. reduction: the liquid flowing into the reduction reaction kettle automatically is stirred and heated, sodium sulfite is added when the temperature is raised to more than 85 ℃ for reduction, the adding amount of the sodium sulfite is 1.5 to 2.5 times of the mass of the gold in the liquid, when the content of the gold in the supernatant is below 3mg/L, the reaction can be stopped, solid-liquid separation is carried out, the liquid is sent to carbon adsorption, the solid is gold powder, and the gold powder is added into an intermediate frequency furnace after being dried to be smelted into gold ingots.
Further, the concentration of the hydrochloric acid is 29-35 wt%.
The invention simultaneously recovers four elements of gold, silver, copper and mercury from the gold refining acid wastewater, has reasonable layout and high recovery rate of various elements, establishes No. 1, No. 2 and No. 3 storage tanks, thereby leading metal ions in waste acid to be fully replaced or precipitated, and decomposes HgS into Hg steam by drying at 600 +/-10 ℃ for 3.5-4.5 h, thereby effectively recovering Hg.
After the process is improved, about 3.8 tons of copper, about 1.5 tons of mercury, about 3kg of gold and about 15kg of silver can be recovered from the gold refining acidic discharged wastewater every year, and the economic value is about 120 ten thousand yuan.
Drawings
FIG. 1 is a process flow diagram of the present invention.
Detailed Description
The technical solutions of the present invention are further described in detail below with reference to specific embodiments and drawings, but the scope of the present invention is not limited thereto.
Example 1
A multi-element comprehensive recovery process for gold refining acid wastewater (with a pH value of 1-2, 2.0mg/L of Au, 30mg/L of Ag, 2.0g/L of Cu and 2.0mg/L of Hg) is shown in figure 1 and comprises the following steps:
(1) refining gold with acid wastewater of 60m3Sending into a carbon adsorption tank (the adsorption tank is filled with apricot kernel carbon for 3 tons at a time, the operation lasts for about one year, the adsorption period exceeds 3 days, and the gold grade reaches 1500 g/ton), performing circulating carbon adsorption until the gold grade in the liquid reaches 0.10mg/L, simultaneously obtaining gold-loaded carbon, and sending the gold-loaded carbon to analysis;
(2) sequentially feeding the liquid with the gold grade of 0.10mg/L into No. 1, No. 2 and No. 3 storage tanks (the volume of each storage tank is 80 m) at the flow rate of 2m/s for metal ion replacement reaction, adding 10kg of precipitate of the previous No. 2 storage tank into the No. 1 storage tank (the precipitate of the No. 1 storage tank is recycled once per month, the recycled precipitate is put into a titanium tank and sent into an industrial resistance furnace), adding 25kg of precipitate of the previous No. 3 storage tank into the No. 2 storage tank, and adding 25kg of iron powder and Na into the No. 3 storage tank2S15 kg, the treatment time of the liquid in each storage tank is 2 hours, about 65% of the total mass of the metal contained in the liquid can be replaced by the storage tank No. 1, about 25% of the total mass of the metal contained in the liquid can be replaced by the storage tank No. 2, and about 5% of the total mass of the metal contained in the liquid can be replaced by the storage tank No. 3.
Discharging the supernatant in the No. 3 storage tank to a water treatment workshop for water treatment; drying the precipitate in the No. 3 storage tank at 600 ℃ for 4h for demercuration (the boiling point of mercury is 356.73 ℃), cooling mercury vapor into liquid mercury, adding borax and sodium carbonate into the dried slag for refining, and comprising the following specific steps: mixing the dried slag, borax and sodium carbonate according to the mass ratio of 1:0.3:0.2, adding the mixture into an intermediate frequency furnace at 1900 ℃ for smelting to obtain a smelting solution, pouring the smelting solution into a squatting pot, cooling, taking out an alloy formed at the lower part of the squatting pot (the alloy is deposited at the lower part of the squatting pot by utilizing the gravity effect and the density of the slag and the alloy is different), putting the alloy into the intermediate frequency furnace again for smelting, and pouring the molten metal into an anode size required by electrolytic copper;
(3) the refined slag is sent to ball mill and ore blending, the alloy after the refining is poured into an anode, and the component of the electrolyte is Cu2+35g/L，H+220g/L，SO4 2-255g/L and the current density is 190A/m2Electrolyzing for 22 hours under the condition that the cell voltage is 2.2V, wherein pure copper (the purity Cu is more than or equal to 99.5%) is produced at a cathode after electrolysis, and anode mud (mainly gold and silver) is produced at an anode; the anode mud is chloridized to obtain gold and silver and waste residue, and the waste residue is returned to be refined;
the chlorination process comprises the following steps:
a. acid leaching: adding 600L of 30wt% hydrochloric acid and 300L of water into a reaction kettle to obtain a dilute hydrochloric acid solution, adding 300kg of anode mud, leaching for 3 hours at 90 ℃, and separating residues and liquids;
b. chlorination: adding 600L of 30wt% hydrochloric acid and 300L of water into a reaction kettle to obtain a dilute hydrochloric acid solution, heating to 50 ℃ under stirring, adding the separated slag material obtained in the step a, adding sodium chlorate when the temperature is raised to 80 ℃, wherein the dosage of the sodium chlorate is 2 times of the mass of the gold in the anode mud, stirring to react for 2.5 hours at 90 ℃, standing for 30 minutes after the reaction is finished, starting slag-liquid separation, automatically flowing the liquid into a reduction reaction kettle, adding the slag into a replacement kettle, adding iron powder to replace silver, and returning the generated waste slag to the primary refining;
c. reduction: the liquid flowing into a reduction reaction kettle automatically is heated under stirring, sodium sulfite is added when the temperature is raised to more than 85 ℃ for reduction, the addition amount of the sodium sulfite is 2 times of the mass of the gold in the liquid, when the content of the gold in the supernatant is below 3mg/L, the reaction can be stopped, solid-liquid separation is carried out, the gold in the liquid is 0.2mg/L, the silver is 10mg/L, the copper is 0.5g/L, the mercury is 0.2mg/L, the pH value is 3-4, the recovery rate of the gold is 96%, the recovery rate of the silver is 83%, the recovery rate of the copper is 93%, and the recovery rate; and (4) carrying out carbon adsorption on the liquid to obtain a solid, namely gold powder, drying the gold powder, and adding the dried gold powder into an intermediate frequency furnace to smelt a gold ingot.
According to the process steps, about 3.8 tons of copper, about 1.5 tons of mercury, about 3kg of gold and about 15kg of silver can be recovered from the gold refining acidic discharged wastewater every year, and the economic value is about 120 ten thousand yuan.
Example 2
A multi-element comprehensive recovery process for gold refining acid wastewater (with a pH value of 1-2, 3.0mg/L of Au, 20mg/L of Ag, 2.5g/L of Cu and 1.5mg/L of Hg), as shown in figure 1, comprises the following steps:
(1) refining gold with acid wastewater of 60m3Sending into a carbon adsorption tank (the adsorption tank is filled with apricot kernel carbon for 3 tons at a time, the operation lasts for about one year, the adsorption period exceeds 3 days, and the gold grade reaches 1500 g/ton), performing circulating carbon adsorption until the gold grade in the liquid reaches 0.15mg/L, simultaneously obtaining gold-loaded carbon, and sending the gold-loaded carbon to analysis;
(2) sequentially feeding the liquid with the gold grade of 0.15mg/L into No. 1, No. 2 and No. 3 storage tanks (the volume of each storage tank is 80 m) at the flow rate of 1m/s for metal ion replacement reaction, adding 15kg of precipitate of the previous No. 2 storage tank into the No. 1 storage tank (the precipitate of the No. 1 storage tank is recycled once per month, the recycled precipitate is put into a titanium tank and sent into an industrial resistance furnace), adding 20kg of precipitate of the previous No. 3 storage tank into the No. 2 storage tank, and adding 20kg of iron powder and Na into the No. 3 storage tank2S10 kg, the treatment time of the liquid in each tank was 1.5 hours, and the tank No. 1 replaced about 65% by mass of the total metal contained in the liquid, the tank No. 2 replaced about 25% by mass of the total metal contained in the liquid, and the tank No. 3 replaced about 5% by mass of the total metal contained in the liquid.
Discharging the supernatant in the No. 3 storage tank to a water treatment workshop for water treatment; drying the precipitate in the No. 3 storage tank at 600 ℃ for 4h for demercuration (the boiling point of mercury is 356.73 ℃), cooling mercury vapor into liquid mercury, adding borax and sodium carbonate into the dried slag for refining, and comprising the following specific steps: mixing the dried slag, borax and sodium carbonate according to the mass ratio of 1:0.3:0.2, adding the mixture into an intermediate frequency furnace at 1850 ℃ for smelting to obtain a smelting solution, pouring the smelting solution into a squatting pot, cooling, taking out an alloy formed at the lower part of the squatting pot (the alloy is deposited at the lower part of the squatting pot by utilizing the gravity effect and the density of the slag and the alloy is different), putting the alloy into the intermediate frequency furnace again for smelting, and pouring the molten metal into the anode size required by electrolytic copper;
(3) the refined slag is sent to ball mill and ore blending, the alloy after the refining is poured into an anode, and the electrolyte comprisesCu2+40g/L，H+200g/L，SO4 2-240g/L and a current density of 150A/m2Electrolyzing for 20 hours under the condition that the cell voltage is 2.0V, wherein pure copper (the purity Cu is more than or equal to 99.5%) is produced at a cathode after electrolysis, and anode mud (mainly gold and silver) is produced at an anode; the anode mud is chloridized to obtain gold and silver and waste residue, and the waste residue is returned to be refined;
the chlorination process comprises the following steps:
a. acid leaching: adding 600L of 30wt% hydrochloric acid and 300L of water into a reaction kettle to obtain a dilute hydrochloric acid solution, adding 300kg of anode mud, leaching for 3 hours at 90 ℃, and separating residues and liquids;
b. chlorination: adding 600L of 30wt% hydrochloric acid and 300L of water into a reaction kettle to obtain a dilute hydrochloric acid solution, heating to 50 ℃ under stirring, adding the separated slag material obtained in the step a, adding sodium chlorate when the temperature is raised to 80 ℃, wherein the dosage of the sodium chlorate is 2 times of the mass of the gold in the anode mud, stirring to react for 2.5 hours at 90 ℃, standing for 30 minutes after the reaction is finished, starting slag-liquid separation, automatically flowing the liquid into a reduction reaction kettle, adding the slag into a replacement kettle, adding iron powder to replace silver, and returning the generated waste slag to the primary refining;
c. reduction: the liquid flowing into a reduction reaction kettle automatically is heated under stirring, sodium sulfite is added when the temperature is raised to more than 85 ℃ for reduction, the addition amount of the sodium sulfite is 2 times of the mass of the gold in the liquid, when the content of the gold in the supernatant is below 3mg/L, the reaction can be stopped, solid-liquid separation is carried out, the gold in the liquid is 0.15mg/L, the silver is 8mg/L, the copper is 0.4g/L, the mercury is 0.15mg/L, the pH value is 3-4, the recovery rate of the gold is 98%, the recovery rate of the silver is 85%, the recovery rate of the copper is 95%, and the recovery rate; and (4) carrying out carbon adsorption on the liquid to obtain a solid, namely gold powder, drying the gold powder, and adding the dried gold powder into an intermediate frequency furnace to smelt a gold ingot.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.

Claims (4)

1. A multi-element comprehensive recovery process for gold refining acidic wastewater is characterized by comprising the following steps: (1) feeding the gold refining acid wastewater with the pH value of 1-2 into a carbon adsorption tank for cyclic carbon adsorption until the gold grade in the liquid is lower than 0.2mg/L, simultaneously obtaining gold-loaded carbon, and feeding the gold-loaded carbon for analysis;
(2) the liquid with the gold grade lower than 0.2mg/L is sequentially sent into a No. 1 storage tank, a No. 2 storage tank and a No. 3 storage tank for reaction, the precipitate of the previous No. 2 storage tank is added into the No. 1 storage tank, the precipitate of the previous No. 3 storage tank is added into the No. 2 storage tank, and iron powder and Na are added into the No. 3 storage tank2S, discharging the supernatant in the No. 3 storage tank to a water treatment workshop for water treatment; drying the precipitate in the No. 3 storage tank at 600 +/-10 ℃ for 3.5-4.5 h, cooling mercury vapor into liquid mercury, and adding borax and soda ash into the dried slag for refining; treatment of 60m3When the acid wastewater is refined by gold, 10-15 kg of the precipitate of the previous No. 2 storage tank needs to be added into the No. 1 storage tank, 20-25 kg of the precipitate of the previous No. 3 storage tank needs to be added into the No. 2 storage tank, and 20-25 kg of iron powder and Na are added into the No. 3 storage tank2S10-15 kg, wherein the treatment time of the wastewater in each storage tank is 1.5-2 hours; the concrete process of the refining is as follows: adding the dried slag, borax and sodium carbonate into an intermediate frequency furnace according to the mass ratio of 1:0.3:0.2, smelting at 1800-1900 ℃ to obtain a smelting solution, pouring the smelting solution into a squatting pot, cooling, taking out an alloy formed at the lower part of the squatting pot, putting the alloy into the intermediate frequency furnace again for melting, and pouring molten metal into the size of an anode required by electrolytic copper;
(3) the refined slag is sent to ball mill and ore blending, the alloy after the refining is poured into an anode, and the component of the electrolyte is Cu2+35～40g/L，H+190～230g/L ，SO4 2-225-270 g/L, current density of 150-190A/m2Electrolyzing for 18-22 hours under the condition that the cell voltage is 1.8-2.2V, wherein pure copper is produced at a cathode after electrolysis, and anode mud is produced at an anode; the anode mud is chloridized to obtain gold and silver and waste residue, and the waste residue is returned to the primary refining.
2. The multi-element comprehensive recovery process of the gold refining acidic wastewater as recited in claim 1, wherein the iron powder has a particle size of less than 0.074mm and accounts for more than 75 wt%.
3. The multi-element comprehensive recovery process of the gold refining acidic wastewater as recited in claim 1, wherein the chlorination process comprises the following steps:
a. acid leaching: adding hydrochloric acid and water into a reaction kettle according to the volume ratio of 2:1 to obtain a dilute hydrochloric acid solution, adding anode mud, wherein the mass ratio of the anode mud to the dilute hydrochloric acid solution is 1: 2.5-4.5, leaching at 85-95 ℃ for 2.5-3.5 hours, and separating residues and liquids;
b. chlorination: adding hydrochloric acid and water into a reaction kettle according to the volume ratio of 2:1 to obtain a dilute hydrochloric acid solution, heating to 80 ℃ under stirring, adding the slag separated in the step a, keeping the temperature below 80 ℃, adding sodium chlorate, wherein the dosage of the sodium chlorate is 1.5-2.5 times of the mass of the gold in the anode mud, stirring to react for 2-4 hours at 90-95 ℃, standing for 15-30 minutes after the reaction is finished, starting slag-liquid separation, automatically flowing the liquid into a reduction reaction kettle, and adding iron powder into the slag to replace silver;
c. reduction: the liquid flowing into the reduction reaction kettle automatically is stirred and heated, sodium sulfite is added when the temperature is raised to more than 85 ℃ for reduction, the adding amount of the sodium sulfite is 1.5 to 2.5 times of the mass of the gold in the liquid, when the content of the gold in the supernatant is below 3mg/L, the reaction can be stopped, solid-liquid separation is carried out, the liquid is sent to carbon adsorption, the solid is gold powder, and the gold powder is added into an intermediate frequency furnace after being dried to be smelted into gold ingots.
4. The multi-element comprehensive recovery process for the gold refining acidic wastewater as recited in claim 3, wherein the concentration of the hydrochloric acid is 29-35 wt%.
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Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1718784A (en) * 2005-07-07 2006-01-11 孙涛 Method of recovery copper, nickel and noble metal in waste water and slag by combined technology of wet method and fire method
CN101451190A (en) * 2007-11-30 2009-06-10 灵宝市金源矿业有限责任公司 Novel method for separating gold and silver from gold mud
CN102286663A (en) * 2011-08-19 2011-12-21 北京矿冶研究总院 Treatment method of copper-containing gold mud

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1718784A (en) * 2005-07-07 2006-01-11 孙涛 Method of recovery copper, nickel and noble metal in waste water and slag by combined technology of wet method and fire method
CN101451190A (en) * 2007-11-30 2009-06-10 灵宝市金源矿业有限责任公司 Novel method for separating gold and silver from gold mud
CN102286663A (en) * 2011-08-19 2011-12-21 北京矿冶研究总院 Treatment method of copper-containing gold mud

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