A method for recovering copper and high-purity silicon powder from waste organosilicon contacts

Abstract

The present invention discloses a method for recovering copper and high-purity silicon powder from waste organosilicon contacts. The method comprises the following steps: adding waste organosilicon contacts, sulfuric acid solution A, and a regulator to an air flotation mechanically agitated coupled leaching tank, then introducing air and mechanically agitating for oxidation leaching to obtain a leaching slurry; separating the leaching slurry into a copper-containing leachate and a leaching residue; washing, filtering, and neutralizing the leaching residue to obtain silicon powder; adjusting the pH of the copper-containing leachate to 1.5-2.0, then adding a copper extractant to the copper-containing leachate for extraction, and separating the copper-extracted residual solution and a copper-containing organic phase; adding sulfuric acid solution B to the copper-containing organic phase for stripping to obtain a stripped copper sulfate solution and a regenerated organic phase; and subjecting the stripped copper sulfate solution to copper electrodeposition to obtain cathode copper. The entire process of the present invention has mild reaction conditions, is environmentally friendly to equipment, has low energy consumption, and is widely applicable. The recovery rates of copper and silicon powder are both above 95%, and the purity of the cathode copper is above 99.95%, and the purity of the silicon powder is above 98%.

Description

Technical Field

[0001] The present invention relates to the technical field of solid waste resource utilization, in particular to a method for recovering copper and high-purity silicon powder from waste organosilicon contacts. Background Art

[0002] Organosilicon materials boast properties such as electrical insulation, high and low temperature resistance, radiation resistance, flame retardancy, corrosion resistance, hydrophobicity, physiological inertness, and non-toxicity and odorlessness. They are widely used in industries such as construction, textiles, electronics, light industry, medical care, and the automotive industry. Currently, methylchlorosilane, the most important monomer for synthesizing organosilicon products, has become the foundation and pillar of the organosilicon industry. Methylchlorosilane production primarily utilizes the direct Rochow process, where monochloromethane (CH3Cl) and silicon powder are added to a fluidized bed reactor and react directly over a ternary copper catalyst to produce methylchlorosilane. Over time, excessive surface deposits on the copper catalyst reduce its reactivity, leading to a decrease in organosilicon monomer yield. To ensure continuous and stable reaction, the remaining silicon powder and catalyst must be removed from the reactor, forming industrial waste, or organosilicon waste.

[0003] The main components of waste silicone contacts are silicon powder, copper powder, carbon powder, and iron, with their respective contents at 65%-75%, 10%-15%, 1%-5%, and 0.2%-2%. During the production of organosilicon monomers, waste contact emissions account for approximately 7%-10% of the total monomer volume. As organosilicon production continues to expand, waste contact emissions will continue to increase. The accumulation of waste silicone contacts not only poses safety risks but also causes serious environmental pollution and represents a significant waste of resources.

[0004] Extensive research has been conducted to recover silicon powder and copper from waste organosilicon contacts. Chinese patent CN102943177A discloses a method for recovering copper and silicon powder from waste organosilicon residues. This process involves mixing the waste organosilicon residue with concentrated sulfuric acid, heating and aging it, and then immersing it in water. This process results in difficulties in slurry mixing, complex operation, high equipment requirements, high energy consumption, and low silicon powder purity. Chinese patent CN104843721A discloses a method for recovering waste organosilicon contacts. This process involves calcining the waste organosilicon contacts, leaching them in an oxidizing ammonia-ammonium salt mixed solution, and then soaking them in acid to obtain high-purity silicon powder. However, this process also suffers from high energy consumption.

[0005] Therefore, providing a harmless treatment process for waste silicone contacts that is economical, environmentally friendly, low in energy consumption, non-corrosive to equipment, and has high purity and yield of silicon powder and copper is of great significance to the development of my country's silicone industry. Summary of the Invention

[0006] The purpose of the present invention is to overcome the above-mentioned technical deficiencies and propose a method for recovering copper and high-purity silicon powder from waste silicone contacts, so as to solve the technical problems in the prior art of recovering copper and silicon powder from waste silicone contacts, such as severe equipment corrosion, difficulty in slurry mixing, high energy consumption and low purity of silicon powder.

[0007] The present invention provides a method for recovering copper and high-purity silicon powder from waste organosilicon contacts, comprising the following steps:

[0008] Oxidative acid leaching: Add the waste organosilicon contact, sulfuric acid solution A and the adjusting agent into the air flotation mechanical stirring coupled leaching tank, introduce air into the air flotation mechanical stirring coupled leaching tank and continuously operate the scraper to scrape off the surface floating layer, and then perform oxidative leaching with mechanical stirring to obtain a leaching slurry;

[0009] Solid-liquid separation: the leaching slurry is separated into solid and liquid to obtain copper-containing leachate and leach residue, and the leach residue is washed, filtered, and neutralized to obtain silicon powder;

[0010] Copper extraction: adjusting the pH value of the copper-containing leachate to 1.5-2.0, then adding a copper extractant to the copper-containing leachate for extraction, and separating the aqueous phase and the organic phase to obtain a copper extraction residue and a copper-containing organic phase;

[0011] Copper stripping: adding sulfuric acid solution B to the copper-containing organic phase for stripping, and separating the stripped copper sulfate solution and the regenerated organic phase;

[0012] Copper electrowinning: The stripped copper sulfate solution is subjected to copper electrowinning to obtain cathode copper.

[0013] Compared with the prior art, the present invention has the following beneficial effects:

[0014] The present invention provides a process for recovering copper and high-purity silicon powder from waste organosilicon contactors that eliminates the need for chemical oxidants, reducing agents, or calcination steps, achieves rapid slurry mixing, achieves high production efficiency and silicon powder purity, and is equipment-friendly. This process is of great significance for the comprehensive utilization of waste organosilicon contactors. The entire process of the present invention features mild reaction conditions, is environmentally friendly, has low energy consumption, and offers wide applicability. The recovery rates for both copper and silicon powder exceed 95%, and the resulting cathode copper has a purity exceeding 99.95%, while the silicon powder purity exceeds 98%. BRIEF DESCRIPTION OF THE DRAWINGS

[0015] Figure 1 The present invention provides a process flow chart of a method for recovering copper and high-purity silicon powder from waste organic silicon contacts. DETAILED DESCRIPTION

[0016] In order to make the purpose, technical solutions and advantages of the present invention more clearly understood, the present invention will be further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are only used to explain the present invention and are not intended to limit the present invention.

[0017] The present invention provides a method for recovering copper and high-purity silicon powder from waste organosilicon contacts, comprising the following steps:

[0018] S1. Oxidative acid leaching: Add the waste organosilicon contactors, sulfuric acid solution A and the regulator into the flotation-mechanical stirring coupled leaching tank. Air is introduced into the flotation-mechanical stirring coupled leaching tank and the scraper is continuously operated to scrape off the surface flotation layer. The leaching is carried out by mechanical stirring to obtain the leaching slurry. The main chemical reactions during the leaching process are as follows:

[0019] H2SO4+CuO=CuSO4+H2O

[0020] H2SO4+Cu2O=CuSO4+Cu+H2O

[0021] 2H2SO4+2Cu+O2=2CuSO4+2H2O

[0022] S2. Solid-liquid separation: The leaching slurry is separated into solid and liquid to obtain copper-containing leachate and leaching residue, and the leaching residue is washed, filtered, and neutralized to obtain silicon powder.

[0023] S3, copper extraction: adjusting the pH value of the copper-containing leachate to 1.5-2.0, then adding a copper extractant to the copper-containing leachate for extraction, and separating the aqueous phase and the organic phase to obtain a copper-extracted residual solution and a copper-containing organic phase.

[0024] S4. Copper stripping: adding sulfuric acid solution B to the copper-containing organic phase for stripping, and separating to obtain stripped copper sulfate solution and regenerated organic phase.

[0025] S5. Copper electrowinning: subjecting the stripped copper sulfate solution to copper electrowinning to obtain cathode copper.

[0026] The present invention uses an air flotation-mechanical stirring coupled leaching tank as leaching equipment. On the one hand, air is filled into the leaching process to replace the addition of chemical oxidants, which not only reduces production costs, but also reduces corrosion to equipment and eliminates the safety hazards caused by chemical oxidants in the production process. On the other hand, the coupling effect of air flow agitation and mechanical stirring synergistically achieves a higher copper leaching rate at a lower sulfuric acid concentration and a shorter leaching time, which greatly improves production efficiency. At the same time, a scraper in the air flotation-mechanical stirring coupled leaching tank can scrape off carbon powder floating to the water surface, thereby improving the purity of silicon powder.

[0027] The present invention adds a regulator during the oxidative acid leaching process of waste silicone contacts. On the one hand, the slurry is quickly and fully mixed, thereby accelerating the leaching of copper and improving production efficiency; on the other hand, it helps the carbon powder attached to the surface of the silicon powder to float to the water surface under the action of the buoyancy of bubbles and then be scraped off by the scraper equipment, thereby achieving carbon powder-silicon powder separation and significantly improving the purity of the silicon powder.

[0028] Compared with the traditional replacement method for producing sponge copper, the present invention adopts the copper extraction-electrodeposition process. On the one hand, it can avoid the problem of treating acidic wastewater containing ferrous sulfate generated in the traditional replacement process, thereby being more environmentally friendly and environmentally friendly; on the other hand, in the entire process flow, both the raffinate and the regenerated organic phase can be recycled, which significantly reduces the production cost and has higher economic benefits.

[0029] In the present invention, the specific structure of the flotation-mechanical stirring coupled leaching tank is not limited, and those skilled in the art can select it according to actual conditions. For example, its structure can be similar to the structure of a fully automatic coagulation flotation stirring adjustment device disclosed in Chinese patent CN208898535U.

[0030] Preferably, in the above step S1, the mass concentration of sulfuric acid in the sulfuric acid solution A is 100-200 g / L, further 120-180 g / L; the solid-liquid ratio of the waste organosilicon contact body to the sulfuric acid solution A is 1 kg: (3-6) L, further 1 kg: (3-5) L.

[0031] Preferably, in the above step S1, the regulator is at least one of sodium hexametaphosphate, tannic acid, sodium silicate, and sodium lignosulfonate; and the mass ratio of the regulator to the waste organosilicon contact body is 500-2000 g:1 t, further 1000-2000 g:1 t.

[0032] Preferably, in the above step S1, the temperature of the oxidative acid leaching is 25-40° C., and the time of the oxidative acid leaching is 1-2 h, further 1.5-2 h.

[0033] Preferably, air is continuously introduced into the flotation-mechanical stirring coupled leaching tank and mechanically stirred to perform oxidation leaching. Furthermore, the air introduction speed is 0.1 to 10 m / s. 3 / min, further 1~3m 3 / min, further 2m 3 / min.

[0034] Preferably, in step S3, the pH value of the copper-containing leachate is adjusted to 1.5 to 2.0 with an alkaline solution. In some embodiments of the present invention, the alkaline solution is a sodium carbonate solution or a sodium hydroxide solution with a mass concentration of 10 to 30 wt.%.

[0035] Preferably, in the above step S3, the copper extractant consists of an extractant and a diluent, and the extractant is any one of M5640, BK992, and N902, and the diluent is sulfonated kerosene; the volume concentration of the extractant in the copper extractant is 20% to 30%; the copper extraction stage is 3 to 4 stages, the extraction time is 3 to 4 minutes, and the copper extraction phase O / A ratio is 1:(1 to 2).

[0036] Preferably, in the above step S3, the copper extraction residual solution is returned to the air flotation mechanical stirring coupled leaching tank in step S1 for recycling.

[0037] Preferably, in the above step S4, the mass concentration of sulfuric acid in the above sulfuric acid solution B is 300-400 g / L; the copper stripping stage is 2-3 stages, the stripping time is 2-3 min, and the stripping phase ratio O / A is (1-2):1, further (1.5-2):1.

[0038] Preferably, in the above step S4, the Cu 2+ The concentration is 30-50g / L.

[0039] Preferably, in the above step S4, the regenerated organic phase is returned to step S3 for recycling to be used for extraction of the copper-containing leachate.

[0040] Preferably, in the above step S5, the electrolytic cell uses a lead plate as an anode and a copper sheet as a cathode, and the electrolytic current density is 200 to 400 A / m 2 , further to 300~400A / m 2 ; The cell voltage is 2.0~3.5V, further to 2.5~2.8V; the electrolysis time is 12~36h, further to 24~36h.

[0041] Unless otherwise specified, the raw materials, reagents, instruments and equipment used in the present invention can be purchased from the market or prepared by existing methods.

[0042] To avoid repetition, some of the raw materials or parameters involved in the following embodiments and comparative examples of the present invention are described as follows, and are not repeated in the specific examples:

[0043] The main chemical components of waste silicone contacts are Si 65% to 80%, CuO 10% to 15%, Fe2O3 2% to 5%, Al2O3 1% to 4%, C 1% to 5%, and the remainder is oxides of other elements and loss on ignition.

[0044] Example 1

[0045] A method for recovering copper and high-purity silicon powder from waste organosilicon contacts comprises the following steps:

[0046] (1) Oxidative acid leaching: Accurately weigh 1 kg of waste silicone contact, 4 L of 150 g / L sulfuric acid solution and 1.5 g of sodium hexametaphosphate, add them into a 6 L air flotation mechanical stirring coupled leaching tank and continuously fill with air (2 m 3 / min) and continuously operate the scraper to scrape off the surface air floating layer, and leaching was carried out with mechanical stirring for 2 h to obtain a leaching slurry.

[0047] (2) Solid-liquid separation: The leaching slurry obtained in step (1) is separated into solid and liquid to obtain leaching residue and copper-containing leachate. At this time, the copper-containing leachate contains Cu 2+ The concentration is 23.83 g / L. The leached residue is washed, filtered, and neutralized to obtain silicon powder. The purity and recovery rate of the silicon powder are 98.2% and 95.5% respectively.

[0048] (3) Copper extraction: The copper-containing leachate obtained in step (2) was adjusted to pH 2.0 by 20wt.% NaOH solution, and subjected to three-stage countercurrent extraction at room temperature, with an extractant N902 concentration of 30%, an extracting phase ratio O / A=1:1, and an extraction time of 3min. After the extraction was completed, the copper-containing residual solution and the copper-containing organic phase were separated after sufficient standing and stratification. The Cu in the copper-containing residual solution was 0.0447 W / m. 2+ The concentration is 0.47 g / L, and the mixture is returned to the flotation mechanical stirring coupled leaching tank in step (1).

[0049] (4) Copper stripping: The copper-containing organic phase obtained in step (3) is stripped using 400 g / L sulfuric acid solution as a stripping agent, and three-stage countercurrent stripping is performed under the conditions of stripping phase ratio O / A=2:1 and stripping time of 2 min. After sufficient standing and stratification, the stripped copper sulfate solution and the regenerated organic phase are separated, wherein the copper in the stripped copper sulfate solution is 2+ The concentration is 47.18 g / L, and the regenerated organic phase is returned to step (3) for extraction of copper-containing leachate.

[0050] (5) Copper electrowinning: The stripped copper sulfate solution obtained in step (4) was subjected to a copper electrowinning experiment. The electrowinning experimental device was a small single electrolytic cell, the anode was a lead plate, the cathode was a copper sheet, and the current density was 300 A / m 2 The cell voltage was 2.6V and the electrowinning time was 24 hours. The cathode copper plate obtained by electrowinning had a copper purity of 99.95%, meeting the No. 1 standard for cathode copper, and a copper recovery rate of 95.8%.

[0051] Relevant experimental data are shown in Table 1.

[0052] Table 1 Experimental data of each solution in Example 1 (g / L)

[0053] name Copper ion concentration Iron ion concentration Chloride ion concentration Copper-containing leachate 23.83 1.89 0.043 Copper extraction residue 0.47 1.88 0.040 Stripping copper sulfate solution 47.18 0.024 0.014

[0054] Example 2

[0055] A method for recovering copper and high-purity silicon powder from waste organosilicon contacts comprises the following steps:

[0056] (1) Oxidative acid leaching: 1 kg of waste organosilicon contact, 5 L of 120 g / L sulfuric acid solution and 1 g of sodium lignosulfonate were added to an 8 L air flotation mechanical stirring coupled leaching tank and continuously filled with air (2 m 3 / min) and continuously operate the scraper to scrape off the surface floating layer, and leaching was carried out with mechanical stirring for 1.5 hours to obtain a leaching slurry.

[0057] (2) Solid-liquid separation: The leaching slurry obtained in step (1) is separated into solid and liquid to obtain leaching residue and copper-containing leachate. At this time, the copper-containing leachate contains Cu 2+ The concentration is 19.12 g / L. The leached residue is washed, filtered and neutralized to obtain silicon powder. The purity and recovery rate of the silicon powder are 98.6% and 95.2% respectively.

[0058] (3) Copper extraction: The copper-containing leachate obtained in step (2) was adjusted to pH 1.8 by 20wt.% NaOH solution, and subjected to three-stage countercurrent extraction at room temperature, with the concentration of extractant BK992 being 30%, the extraction phase ratio O / A being 1:1, and the extraction time being 3min. After the extraction was completed, the copper extraction residual solution and the copper-containing organic phase were separated after sufficient standing and stratification. The Cu in the copper extraction residual solution was 0.01% and 0.01% respectively. 2+ The concentration is 0.23 g / L, and it is returned to the flotation mechanical stirring coupled leaching tank in step (1).

[0059] (4) Copper stripping: The copper-containing organic phase obtained in step (3) is stripped using 400 g / L sulfuric acid solution as a stripping agent, and three-stage countercurrent stripping is performed under the conditions of stripping phase ratio O / A=2:1 and stripping time of 2 min. After sufficient standing and stratification, the stripped copper sulfate solution and the regenerated organic phase are separated, wherein the copper in the stripped copper sulfate solution is 2+ The concentration is 38.08 g / L, and the regenerated organic phase is returned to step (3) for extraction of copper-containing leachate.

[0060] (5) Copper electrowinning: The stripped copper sulfate solution obtained in step (4) was subjected to a copper electrowinning experiment. The electrowinning experimental device was a small single electrolytic cell, the anode was a lead plate, the cathode was a copper sheet, and the current density was 400 A / m 2 The cell voltage was 2.8V and the electrowinning time was 36 hours. The cathode copper plate obtained by electrowinning had a copper purity of 99.95%, meeting the No. 1 standard for cathode copper, and a copper recovery rate of 96.3%.

[0061] Relevant experimental data are shown in Table 2.

[0062] Table 2 Experimental data of each solution in Example 2 (g / L)

[0063] name Copper ion concentration Iron ion concentration Chloride ion concentration Copper-containing leachate 19.12 1.53 0.038 Copper extraction residue 0.23 1.51 0.036 Stripping copper sulfate solution 38.08 0.020 0.012

[0064] Example 3

[0065] A method for recovering copper and high-purity silicon powder from waste organosilicon contacts comprises the following steps:

[0066] (1) Oxidative acid leaching: 2 kg of waste organosilicon contactors, 6 L of 180 g / L sulfuric acid solution and 2 g of regulator (0.5 g of tannic acid and 1.5 g of sodium silicate) were added to a 10 L air flotation mechanical stirring coupled leaching tank and continuously filled with air (2 m 3 / min) and continuously operate the scraper to scrape off the surface air floating layer, and leaching was carried out with mechanical stirring for 2 h to obtain a leaching slurry.

[0067] (2) Solid-liquid separation: The leaching slurry obtained in step (1) is separated into solid and liquid to obtain leaching residue and copper-containing leachate. At this time, the copper-containing leachate contains Cu 2+ The concentration is 31.35 g / L. The leached residue is washed, filtered and neutralized to obtain silicon powder. The purity and recovery rate of the silicon powder are 98.0% and 95.8% respectively.

[0068] (3) Copper extraction: The copper-containing leachate obtained in step (2) was adjusted to pH 2.0 by 20wt.% NaOH solution, and subjected to three-stage countercurrent extraction at room temperature, with an extractant N902 concentration of 30%, an extracting phase ratio O / A=1:1, and an extraction time of 4 minutes. After the extraction was completed, the copper-containing residual solution and the copper-containing organic phase were separated after sufficient standing and stratification. The Cu in the copper-containing residual solution was 0.0447 W / m. 2+ The concentration is 0.41 g / L, and it is returned to the flotation mechanical stirring coupled leaching tank in step (1).

[0069] (4) Copper stripping: The copper-containing organic phase obtained in step (3) is stripped using 400 g / L sulfuric acid solution as a stripping agent, and three-stage countercurrent stripping is performed under the conditions of stripping phase ratio O / A=1.5:1 and stripping time of 3 min. After sufficient standing and stratification, the stripped copper sulfate solution and the regenerated organic phase are separated, wherein the copper in the stripped copper sulfate solution is 2+ The concentration is 46.65 g / L, and the regenerated organic phase is returned to step (3) for extraction of copper-containing leachate.

[0070] (5) Copper electrowinning: The copper sulfate solution obtained in step (4) was subjected to a copper electrowinning experiment. The electrowinning experimental device was a small single electrolytic cell, the anode was a lead plate, the cathode was a copper sheet, and the current density was 300 A / m 2 The cell voltage was 2.5V and the electrowinning time was 24 hours. The cathode copper plate obtained by electrowinning had a copper purity of 99.95%, meeting the No. 1 standard for cathode copper, and a copper recovery rate of 95.5%.

[0071] Relevant experimental data are shown in Table 3.

[0072] Table 3 Experimental data of each solution in Example 3 (g / L)

[0073] name Copper ion concentration Iron ion concentration Chloride ion concentration Copper-containing leachate 31.35 2.67 0.055 Copper extraction residue 0.41 2.65 0.054 Stripping copper sulfate solution 46.65 0.028 0.015

[0074] Comparative Example 1

[0075] In addition, in step (1), a common mechanical stirring tank is used instead of an air flotation mechanical stirring coupled leaching tank, and air is continuously filled (2m 3 / min) (without scraper), the rest are consistent with Example 1.

[0076] Table 4 Related experimental data of each solution in Comparative Example 1 (g / L)

[0077] name Copper ion concentration Iron ion concentration Chloride ion concentration Copper-containing leachate 21.47 1.96 0.040 Copper extraction residue 0.40 1.94 0.036 Stripping copper sulfate solution 42.51 0.025 0.013

[0078] The recovery rate and purity of the silicon powder recovered under the experimental conditions were 96.2% and 88.96%, respectively. The cathode copper sheet obtained by electrowinning had a copper purity of 99.95%, meeting the cathode copper quality standard of GB / T 467-2010 No. 1, and the copper recovery rate was 84.47%.

[0079] Comparative Example 2

[0080] Except that no adjusting agent is added in step (1), the other conditions are the same as those in Example 1.

[0081] Relevant experimental data are shown in Table 5.

[0082] Table 5 Related experimental data of each solution in Comparative Example 2 (g / L)

[0083] name Copper ion concentration Iron ion concentration Chloride ion concentration Copper-containing leachate 22.54 1.82 0.045 Copper extraction residue 0.45 1.80 0.038 Stripping copper sulfate solution 44.63 0.023 0.014

[0084] The recovery rate and purity of the silicon powder recovered under the experimental conditions were 95.0% and 92.05%, respectively. The cathode copper sheet obtained by electrowinning had a copper purity of 99.95%, meeting the cathode copper quality standard of GB / T 467-2010 No. 1, and the copper recovery rate was 90.59%.

[0085] The specific embodiments of the present invention described above do not limit the scope of protection of the present invention. Any other corresponding changes and modifications made based on the technical concept of the present invention should be included in the scope of protection of the claims of the present invention.

Claims

1. A method for recovering copper and high-purity silicon powder from waste organosilicon contacts, characterized in that: The following steps are involved: Oxidative acid leaching: adding the waste organosilicon contact, sulfuric acid solution A and the adjusting agent into an air flotation mechanical stirring coupled leaching tank, introducing air into the air flotation mechanical stirring coupled leaching tank and continuously operating a scraper to scrape off the surface air flotation layer, and mechanically stirring to perform oxidative leaching to obtain a leaching slurry; Solid-liquid separation: separating the leaching slurry into a solid-liquid state to obtain a copper-containing leachate and a leach residue, and washing, filtering, and neutralizing the leach residue to obtain silicon powder; Copper extraction: adjusting the pH value of the copper-containing leachate to 1.5-2.0, then adding a copper extractant to the copper-containing leachate for extraction, and separating the aqueous phase and the organic phase to obtain a copper extraction residue and a copper-containing organic phase; Copper stripping: adding sulfuric acid solution B to the copper-containing organic phase for stripping, and separating to obtain stripped copper sulfate solution and regenerated organic phase; Copper electrowinning: subjecting the stripped copper sulfate solution to copper electrowinning to obtain cathode copper; wherein, The regulator is at least one of sodium hexametaphosphate, tannic acid, sodium silicate, and sodium lignosulfonate; and the mass ratio of the regulator to the waste organosilicon contact body is 500-2000 g:1 t.

2. The method for recovering copper and high-purity silicon powder from waste organosilicon contacts according to claim 1, characterized in that: The mass concentration of sulfuric acid in the sulfuric acid solution A is 100-200 g / L, and the solid-liquid ratio of the waste organosilicon contact body to the sulfuric acid solution A is 1 kg: (3-6) L.

3. The method for recovering copper and high-purity silicon powder from waste organosilicon contacts according to claim 1, characterized in that: The temperature of the oxidizing acid leaching is 25-40° C., and the time of the oxidizing acid leaching is 1-2 h.

4. The method for recovering copper and high-purity silicon powder from waste organosilicon contacts according to claim 1, characterized in that: The copper extractant consists of an extractant and a diluent, and the extractant is any one of M5640, BK992, and N902, and the diluent is sulfonated kerosene.

5. The method for recovering copper and high-purity silicon powder from waste organosilicon contacts according to claim 4, characterized in that: The volume concentration of the extractant in the copper extractant is 20% to 30%; the copper extraction stage is 3 to 4 stages, the extraction time is 3 to 4 minutes, and the copper extraction ratio O / A is 1: (1 to 2).

6. The method for recovering copper and high-purity silicon powder from waste organosilicon contacts according to claim 1, characterized in that: The copper extraction residual solution is returned to the air flotation mechanical stirring coupled leaching tank for recycling.

7. The method for recovering copper and high-purity silicon powder from waste organosilicon contacts according to claim 1, characterized in that: The mass concentration of sulfuric acid in the sulfuric acid solution B is 300-400 g / L; the copper stripping stage is 2-3 stages, the stripping time is 2-3 min, and the stripping phase ratio O / A is (1-2):

1.

8. The method for recovering copper and high-purity silicon powder from waste organosilicon contacts according to claim 1, characterized in that: The regenerated organic phase is returned to the copper extraction step and circulated for extraction of copper-containing leachate.

9. The method for recovering copper and high-purity silicon powder from waste organosilicon contacts according to claim 1, characterized in that: The electrolytic cell uses lead plate as anode and copper sheet as cathode, and the electrolytic current density is 200~400 A / m 2 , cell voltage 2.0~3.5 V, and electrolysis time 12~36 h.

Images