CN115181998A - Method for recovering copper and high-purity silicon powder from organic silicon waste contact - Google Patents

Abstract

The invention discloses a method for recovering copper and high-purity silicon powder from organic silicon waste contacts, which comprises the following steps: adding the organic silicon waste contact, the sulfuric acid solution A and the regulator into an air floatation mechanical stirring coupling leaching tank, then introducing air and mechanically stirring for oxidizing leaching to obtain leaching slurry; carrying out solid-liquid separation on the leaching slurry to obtain copper-containing leaching solution and leaching residue, and washing, press-filtering and neutralizing the leaching residue to obtain silicon powder; adjusting the pH value of the copper-containing leaching solution to 1.5-2.0, then adding a copper extractant into the copper-containing leaching solution for extraction, and separating to obtain a copper extraction residual solution and a copper-containing organic phase; adding a sulfuric acid solution B into the copper-containing organic phase for back extraction to obtain a back-extracted copper sulfate solution and a regenerated organic phase; and carrying out copper electrodeposition on the back-extraction copper sulfate solution to obtain cathode copper. The whole process of the invention has mild reaction conditions, environmental protection to equipment, low energy consumption and wide applicability, the recovery rates of copper and silicon powder are both more than 95%, the purity of cathode copper is more than 99.95%, and the purity of silicon powder is more than 98%.

Description

A method for recovering copper and high-purity silicon powder from organic silicon waste contact body

technical field

The 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 organic silicon waste contact bodies.

Background technique

Silicone materials have the characteristics of electrical insulation resistance, high and low temperature resistance, radiation resistance, flame retardant, corrosion resistance, hydrophobicity, physiological inertia, non-toxic and tasteless, etc. They are widely used in construction, textile, electrical and electronic, light industry, medical treatment, automobile and other industries. At present, as the most important monomer material for the synthesis of organosilicon products, methylchlorosilane has become the foundation and pillar of the organosilicon industry, while the production of methylchlorosilane mainly adopts the direct method (Rochow method), namely, monochloromethane ( _CH3 Cl) and silicon powder are added into the fluidized bed reactor, and react directly under the action of ternary copper catalyst to generate methylchlorosilane. In this process, as the reaction goes on for a long time, the excessive deposits on the surface of the catalyst copper powder will reduce its reactivity, thereby reducing the yield of organosilicon monomers. In order to ensure the continuous and stable reaction of the reaction, it is necessary to discharge the remaining silicon powder and catalyst from the reactor to form industrial waste residues, namely waste organosilicon bodies.

The main components of organic silicon waste contact body are silicon powder, copper powder, carbon powder and iron, etc. Their content in waste contact body is 65%-75%, 10%-15%, 1%-5%, 0.2%, respectively. %～2%. In the production process of organosilicon monomers, the emission of waste contacts accounts for about 7% to 10% of the total monomers. With the continuous expansion of the production scale of silicone, the amount of waste contact body emissions will continue to increase. The massive accumulation of silicone waste contacts not only poses a certain safety hazard, but also brings serious pollution to the surrounding environment, and is also a large waste of resources.

In order to recover silicon powder and copper from organic silicon waste contact bodies, a lot of researches have been carried out by the predecessors. Chinese patent CN102943177A discloses a method for recovering copper and silicon powder from organosilicon waste residue. In this process, the organosilicon waste residue and concentrated sulfuric acid are mixed, heated and matured, and then immersed in water. Therefore, it is difficult to mix the slurry and the operation is complicated. It has defects such as high equipment requirements, high energy consumption, and low purity of silicon powder. Chinese patent CN104843721A discloses a method for recycling waste organosilicon contact bodies. In this process, the waste organosilicon contact bodies are successively subjected to calcination, leaching in an oxidant-containing ammonia-ammonium salt mixed solution, and immersion in an acid solution to obtain high-quality organic silicon. Pure silicon powder, but also has the defect of high energy consumption.

Therefore, it is extremely important to provide an economical, environmentally friendly, low energy consumption, no corrosion to equipment, and high purity and yield of silicon powder and copper. significance.

SUMMARY OF THE INVENTION

The object of the present invention is to overcome the above-mentioned technical deficiencies, propose a method for recovering copper and high-purity silicon powder from the waste organosilicon contact body, and solve the problem of recovering copper and silicon powder from the waste organosilicon contact body in the prior art. There are technical problems such as serious equipment corrosion, difficult slurry mixing, high energy consumption and low purity of silicon powder.

The invention provides a method for recovering copper and high-purity silicon powder from organic silicon waste contact bodies, comprising the following steps:

Oxidative acid leaching: Add organic silicon waste contact body, sulfuric acid solution A and adjusting agent to the air flotation mechanical stirring coupling leaching tank, introduce air into the air flotation mechanical stirring coupling leaching tank, and continuously operate the slag scraper to scrape the surface air flotation layer, mechanical stirring to carry out oxidative leaching to obtain leaching slurry;

Solid-liquid separation: the above-mentioned leaching slurry is solid-liquid separated to obtain copper-containing leaching solution and leaching slag, and the leaching slag is washed, filtered, and neutralized to obtain silicon powder;

Copper extraction: the above-mentioned copper-containing leaching solution is adjusted to a pH value of 1.5 to 2.0, then copper extractant is added to the above-mentioned copper-containing leaching solution for extraction, and the aqueous phase and the organic phase are separated to obtain the copper-extracted residual liquid and the copper-containing organic phase;

Copper stripping: adding sulfuric acid solution B to the above-mentioned copper-containing organic phase for stripping, and separating the stripping copper sulfate solution and the regenerated organic phase;

Copper electrodeposition: copper electrodeposition is performed on the back-extracted copper sulfate solution to obtain cathode copper.

Compared with the prior art, the beneficial effects of the present invention include:

The invention provides a method for recovering copper and high-purity silicon powder from organic silicon waste contact bodies, which does not introduce chemical oxidants, reducing agents and roasting processes, has fast mixing of slurry, high production efficiency and silicon powder purity, and is equipment-friendly. This process is of great significance to the comprehensive utilization of organosilicon waste contacts. The whole process of the invention has mild reaction conditions, environmental protection for equipment, low energy consumption and wide applicability, the recovery rates of copper and silicon powder are both above 95%, and the purity of the obtained cathode copper is above 99.95%, and the purity of silicon powder is 98%. %above.

Description of drawings

1 is a process flow diagram of an embodiment of the method for recovering copper and high-purity silicon powder from organic silicon waste contact bodies provided by the present invention.

Detailed ways

In order to make the objectives, technical solutions and advantages of the present invention clearer, 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, but not to limit the present invention.

The invention provides a method for recovering copper and high-purity silicon powder from organic silicon waste contact bodies, comprising the following steps:

S1. Oxidative acid leaching: Add organic silicon waste contact body, sulfuric acid solution A and adjuster to the air flotation mechanical stirring coupling leaching tank, introduce air into the air flotation mechanical stirring coupling leaching tank, and continuously operate the scraper to scrape the surface Air flotation layer, mechanical stirring to carry out oxidative leaching to obtain leaching slurry. The main chemical reactions in the leaching process are as follows:

H ₂ SO ₄ +CuO=CuSO ₄ +H ₂ O

H ₂ SO ₄ +Cu ₂ O=CuSO ₄ +Cu+H ₂ O

2H ₂ SO ₄ +2Cu+O ₂ =2CuSO ₄ +2H ₂ O

S2. Solid-liquid separation: the above-mentioned leaching slurry is solid-liquid separated to obtain copper-containing leaching solution and leaching slag, and the leaching slag is washed, filtered, and neutralized to obtain silicon powder.

S3, copper extraction: the above-mentioned copper-containing leaching solution is adjusted to a pH value of 1.5 to 2.0, then a copper extractant is added to the copper-containing leaching solution for extraction, and the aqueous phase and the organic phase are separated to obtain a copper-extracted residual liquid and a copper-containing organic phase.

S4, copper stripping: adding sulfuric acid solution B to the above-mentioned copper-containing organic phase for stripping, and separating the stripping copper sulfate solution and the regenerated organic phase.

S5, copper electrodeposition: copper electrodeposition is performed on the above-mentioned back-extracted copper sulfate solution to obtain cathode copper.

The invention uses the air flotation mechanical stirring and coupling leaching tank as the leaching equipment. On the one hand, air is filled in the leaching process to replace the addition of chemical oxidants, which not only reduces the production cost, but also has weak corrosion to the equipment and eliminates the need for the production process. The safety hazard brought by chemical oxidants; on the other hand, the coupling effect produced by the synergy of airflow agitation and mechanical agitation makes it possible to obtain a higher copper leaching rate at a lower sulfuric acid concentration and a shorter leaching time, which greatly improves the production efficiency. At the same time, the slag scraper in the air flotation mechanical stirring coupling leaching tank can scrape off the carbon powder floating to the water surface and improve the purity of the silicon powder.

In the present invention, the adjusting agent is added in the process of oxidative acid leaching of waste organosilicon contact bodies. On the one hand, the slurry is quickly and fully mixed evenly, thereby accelerating the leaching of copper and improving the production efficiency; The powder floats to the water surface under the action of bubble buoyancy, and then is scraped off by scraper equipment, thereby realizing the separation of carbon powder and silicon powder and the significant improvement of the purity of silicon powder.

Compared with the traditional replacement method to produce sponge copper, the invention adopts the copper extraction-electrowinning process, on the one hand, it can avoid the problem of treating acidic wastewater containing ferrous sulfate in the traditional replacement process, so that it is more environmentally friendly and environmentally friendly; on the other hand In the whole process flow, both the raffinate and the regenerated organic phase can be recycled, which significantly reduces the production cost and has high economic benefits.

In the present invention, the specific structure of the air flotation mechanical stirring coupling leaching tank is not limited, and those skilled in the art can choose according to the actual situation. For example, its structure can be similar to that of a fully automatic coagulation and air flotation stirring and adjusting device disclosed in Chinese Patent CN208898535U.

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-to-liquid ratio of the organosilicon waste contact body to the sulfuric acid solution A is 1 kg: (3-6 ) L, further 1 kg: (3-5) L.

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

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 hours, and further 1.5-2 hours.

Preferably, the oxidative leaching is carried out by continuously feeding air into the air flotation mechanical stirring coupled leaching tank and mechanically stirring. Further, the inflow velocity of air is 0.1 to 10 m ³ /min, further 1 to 3 m ³ /min, and further 2 m ³ /min.

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

Preferably, in the above step S3, the copper extractant is composed 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 20%-30%; copper extraction stages are 3-4, extraction time is 3-4min, and copper extraction ratio O/A is 1:(1-2).

Preferably, in the above-mentioned step S3, the above-mentioned copper-extracted residual liquid is returned to the air-flotation mechanical stirring coupling leaching tank in the step S1 for recycling.

Preferably, in the above-mentioned step S4, the mass concentration of sulfuric acid in the above-mentioned sulfuric acid solution B is 300～400g/L; It is (1-2):1, and it is (1.5-2):1 further.

Preferably, in the above step S4, the concentration of Cu ²⁺ in the obtained back-extracted copper sulfate solution is 30-50 g/L.

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

Preferably, in the above step S5, the electrowinning cell uses the lead plate as the anode and the copper sheet as the cathode, the electrowinning current density is 200-400A/m ² , further 300-400A/m ² ; the cell voltage is 2.0-3.5V, further It is 2.5～2.8V; the electrowinning time is 12～36h, and further is 24～36h.

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

In order to avoid repetition, some raw materials or parameters involved in the following examples and comparative examples of the present invention are described uniformly as follows, and will not be repeated in the specific examples:

The main chemical composition of silicone waste contact body is Si 65%～80%, CuO 10%～15%, _{Fe2O3 2} %～5%, _{Al2O3 1} %～4%, C 1%～5% , the balance is other element oxides and loss on ignition.

Example 1

A method for recovering copper and high-purity silicon powder from organic silicon waste contact bodies, comprising the following steps:

(1) Oxidative acid leaching: Accurately weigh 1kg of organosilicon waste contact body, 4L of 150g/L sulfuric acid solution and 1.5g of sodium hexametaphosphate, and add them to a 6L air flotation mechanical stirring coupled leaching tank with continuous air (2m ³ /min) and continue to run the scraper to scrape off the surface air flotation layer, and mechanically stir for 2 hours to obtain the leaching slurry.

(2) Solid-liquid separation: solid-liquid separation of the leaching slurry obtained in step (1) to obtain leaching slag and copper-containing leaching solution. At this time, the ^Cu concentration in the copper-containing leaching solution is 23.83 g/L, and the leaching slag is washed and filtered by pressure. , neutralized silicon powder, the purity and recovery rate of silicon powder were 98.2% and 95.5%, respectively.

(3) Copper extraction: the copper-containing leaching solution obtained in step (2) was adjusted to pH 2.0 by 20wt.% NaOH solution, at room temperature, the concentration of extractant N902 was 30%, and the extraction ratio was O/A=1:1 , 3-stage countercurrent extraction was performed under the condition that the extraction time was 3 min. After the extraction is completed, the copper-extracted residual liquid and the copper-containing organic phase are separated and separated, and the Cu ²⁺ concentration in the copper-extracted residual liquid is 0.47g/L, and returns to step (1) air flotation mechanical stirring coupled leaching groove.

(4) copper stripping: the copper-containing organic phase obtained in step (3) is stripped using a sulfuric acid solution of 400 g/L as a stripping agent, and the stripping ratio is O/A=2:1, and the stripping time is 2min. 3-stage countercurrent stripping was carried out under the conditions of 300°C, and after sufficient standing for stratification, the stripping copper sulfate solution and the regenerated organic phase were separated, wherein the ^Cu concentration in the stripped copper sulfate solution was 47.18g/L, and the regenerated organic phase returned to Step (3) is used for the extraction of copper-containing leaching solution.

(5) copper electrowinning: carry out a copper electrowinning experiment with the back-extracted copper sulfate solution obtained in step (4), the electrowinning experimental device is a small single electrolytic cell, the anode is a lead plate, the cathode is a copper sheet, and the current density is 300A/m ² , cell voltage 2.6V, electrowinning time 24h. The cathode copper plate is obtained by electrowinning, and the copper purity reaches 99.95%, which meets the No. 1 standard cathode copper, and the copper recovery rate is 95.8%.

The relevant experimental data are shown in Table 1.

Relevant experimental data (g/L) of each solution in Table 1 Example 1

name Copper ion concentration Iron ion concentration Chloride concentration Copper Leachate 23.83 1.89 0.043 Copper extraction residue 0.47 1.88 0.040 Back-extraction of copper sulfate solution 47.18 0.024 0.014

Example 2

A method for recovering copper and high-purity silicon powder from organic silicon waste contact bodies, comprising the following steps:

(1) Oxidative acid leaching: 1kg of organosilicon waste contact body, 5L of 120g/L sulfuric acid solution and 1g of sodium lignosulfonate were added to 8L of air flotation mechanical stirring coupling leaching tank and continuously filled with air (2m ³ /min) and The slag scraper was continuously operated to scrape off the surface air flotation layer, and the leaching slurry was obtained by mechanical stirring for 1.5 hours.

(2) Solid-liquid separation: solid-liquid separation of the leaching slurry obtained in step (1) to obtain leaching slag and copper-containing leaching solution. At this time, the Cu ²⁺ concentration in the copper-containing leaching solution is 19.12 g/L, and the leaching slag is washed and filtered by pressure. , neutralized to obtain silicon powder, the purity and recovery of silicon powder were 98.6% and 95.2%.

(3) Copper extraction: the copper-containing leaching solution obtained in step (2) was adjusted to pH 1.8 by 20wt.% NaOH solution, at room temperature, the concentration of extractant BK992 was 30%, and the extraction ratio was O/A=1:1 , 3-stage countercurrent extraction was performed under the condition that the extraction time was 3 min. After the extraction is completed, after fully standing for stratification, the copper-extracted residual liquid and the copper-containing organic phase are separated, and the Cu ²⁺ concentration in the copper-extracted residual liquid is 0.23g/L, and returns to step (1) air flotation mechanical stirring coupled leaching in the slot.

(4) Copper back extraction: the copper-containing organic phase obtained in step (3) is back extracted by using 400g/L sulfuric acid solution as back extraction agent, and the back extraction ratio O/A=2:1, back extraction time 2min 3-stage countercurrent stripping was carried out under the conditions of 300 °C, and after sufficient standing for stratification, the stripped copper sulfate solution and the regenerated organic phase were separated, wherein the ^Cu concentration in the stripped copper sulfate solution was 38.08 g/L, and the regenerated organic phase returned to Step (3) is used for copper-containing leachate extraction.

(5) copper electrowinning: carry out a copper electrowinning experiment with the back-extracted copper sulfate solution obtained in step (4), the electrowinning experimental device is a small single electrolytic cell, the anode is a lead plate, the cathode is a copper sheet, and the current density is 400A/m ² , the cell voltage is 2.8V, and the electrowinning time is 36h. The cathode copper plate is obtained by electrowinning, and the copper purity reaches 99.95%, which conforms to the No. 1 standard cathode copper, and the copper recovery rate is 96.3%.

The relevant experimental data are shown in Table 2.

The relevant experimental data (g/L) of each solution in the embodiment 2 of table 2

name Copper ion concentration Iron ion concentration Chloride concentration Copper Leachate 19.12 1.53 0.038 Copper extraction residue 0.23 1.51 0.036 Back-extraction of copper sulfate solution 38.08 0.020 0.012

Example 3

A method for recovering copper and high-purity silicon powder from organic silicon waste contact bodies, comprising the following steps:

(1) Oxidative acid leaching: add 2kg of organosilicon waste contact body, 6L of 180g/L sulfuric acid solution and 2g of modifiers (0.5g of tannic acid and 1.5g of sodium silicate) into 10L of air flotation mechanical stirring coupled leaching The tank was continuously filled with air (2m ³ /min) and the slag scraper was continuously operated to scrape off the surface air flotation layer, and the leaching slurry was obtained by mechanical stirring for 2 hours.

(2) Solid-liquid separation: solid-liquid separation of the leaching slurry obtained in step (1) to obtain leaching slag and copper-containing leaching solution. At this time, the ^Cu concentration in the copper-containing leaching solution is 31.35 g/L, and the leaching slag is washed and filtered by pressure. , and neutralized to obtain silicon powder, and the purity and recovery rate of silicon powder are 98.0% and 95.8%, respectively.

(3) Copper extraction: the copper-containing leaching solution obtained in step (2) was adjusted to pH 2.0 by 20wt.% NaOH solution, at room temperature, the concentration of extractant N902 was 30%, and the extraction ratio was O/A=1:1 , 3-stage countercurrent extraction was performed under the condition that the extraction time was 4 min. After the extraction is completed, after fully standing for stratification, the copper-extracted residual liquid and the copper-containing organic phase are separated, and the Cu ²⁺ concentration in the copper-extracted residual liquid is 0.41 g/L, and returns to step (1) air flotation mechanical stirring coupled leaching in the slot.

(4) Copper stripping: the copper-containing organic phase obtained in step (3) was stripped using 400 g/L sulfuric acid solution as stripping agent, and the ratio of O/A in stripping was 1.5:1, and stripping time was 3min. 3-stage counter-current stripping was carried out under the conditions of 300 °C, and after sufficient standing for stratification, the stripped copper sulfate solution and the regenerated organic phase were separated, wherein the ^Cu concentration in the stripped copper sulfate solution was 46.65 g/L, and the regenerated organic phase returned to Step (3) is used for copper-containing leachate extraction.

(5) copper electrowinning: the copper sulfate solution obtained in the step (4) is subjected to a copper electrowinning experiment, the electrowinning experimental device is a small single electrolytic cell, the anode is a lead plate, the cathode is a copper sheet, and the current density is 300A/ m ² , the cell voltage is 2.5V, and the electrowinning time is 24h. The cathode copper plate is obtained by electrowinning, and the copper purity reaches 99.95%, which meets the No. 1 standard cathode copper, and the copper recovery rate is 95.5%.

The relevant experimental data are shown in Table 3.

The relevant experimental data (g/L) of each solution in the embodiment 3 of table 3

name Copper ion concentration Iron ion concentration Chloride concentration Copper Leachate 31.35 2.67 0.055 Copper extraction residue 0.41 2.65 0.054 Back-extraction of copper sulfate solution 46.65 0.028 0.015

Comparative Example 1

Except that in step (1), an ordinary mechanical stirring tank is used instead of the air flotation mechanical stirring and coupling leaching tank, and the air is continuously charged (2m ³ /min) (without a slag scraper), the rest are the same as those in Example 1.

The relevant experimental data (g/L) of each solution in Table 4 Comparative Example 1

name Copper ion concentration Iron ion concentration Chloride concentration Copper Leachate 21.47 1.96 0.040 Copper extraction residue 0.40 1.94 0.036 Back-extraction of copper sulfate solution 42.51 0.025 0.013

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 was obtained by electrowinning, and the copper purity reached 99.95%, which met the GB/T 467-2010 No. 1 standard cathode copper quality standard. The copper recovery was 84.47%.

Comparative Example 2

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

The relevant experimental data are shown in Table 5.

The relevant experimental data (g/L) of each solution in Table 5 Comparative Example 2

name Copper ion concentration Iron ion concentration Chloride concentration Copper Leachate 22.54 1.82 0.045 Copper extraction residue 0.45 1.80 0.038 Back-extraction of copper sulfate solution 44.63 0.023 0.014

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 was obtained by electrowinning, and the copper purity reached 99.95%, which met the GB/T 467-2010 No. 1 standard cathode copper quality standard. The copper recovery was 90.59%.

The specific embodiments of the present invention described above do not limit the protection scope of the present invention. Any other corresponding changes and modifications made according to the technical concept of the present invention shall be included in the protection scope of the claims of the present invention.

Claims (10)

1. a method for recovering copper and high-purity silicon powder from organosilicon waste contact body, is characterized in that, comprises the following steps: Oxidative acid leaching: Add organic silicon waste contact body, sulfuric acid solution A and modifier to the air flotation mechanical stirring coupling leaching tank, introduce air into the air flotation mechanical stirring coupling leaching tank, and continuously operate the slag scraper to scrape the surface Air flotation layer, mechanical stirring to carry out oxidative leaching to obtain leaching slurry; Solid-liquid separation: solid-liquid separation of the leaching slurry to obtain copper-containing leaching solution and leaching slag, and the leaching slag is washed, filtered, and neutralized to obtain silicon powder; Copper extraction: adjusting the pH of the copper-containing leaching solution to 1.5 to 2.0, then adding a copper extractant to the copper-containing leaching solution for extraction, and separating the aqueous phase and the organic phase to obtain a copper-extracted residue and a copper-containing organic phase; Copper stripping: adding sulfuric acid solution B to the copper-containing organic phase for stripping, and separating the stripping copper sulfate solution and the regenerated organic phase; Copper electrodeposition: copper electrodeposition is performed on the back-extracted copper sulfate solution to obtain cathode copper. 2. The method for recovering copper and high-purity silicon powder from organosilicon waste contact bodies according to claim 1, wherein the mass concentration of sulfuric acid in the sulfuric acid solution A is 100-200 g/L, and the organosilicon The solid-liquid ratio of the waste contact body to the sulfuric acid solution A is 1kg: (3-6)L. 3. the method for recovering copper and high-purity silicon powder from organosilicon waste contact body according to claim 1, is characterized in that, described regulator is sodium hexametaphosphate, tannic acid, sodium silicate, lignosulfonic acid At least one of sodium; the mass ratio of the regulator to the organosilicon waste contact body is 500-2000g:1t. 4. The method for recovering copper and high-purity silicon powder from organosilicon waste contact bodies according to claim 1, wherein the temperature of the oxidative acid leaching is 25 to 40°C, and the time of the oxidative acid leaching is 1 to 2 hours. 5. the method for recovering copper and high-purity silicon powder from organosilicon waste contact body according to claim 1, is characterized in that, described copper extraction agent is made up of extraction agent and thinner, and described extraction agent is M5640, In any one of BK992 and N902, the diluent is sulfonated kerosene. 6. The method for recovering copper and high-purity silicon powder from organosilicon waste contact bodies according to claim 5, wherein the volume concentration of the extraction agent in the copper extraction agent is 20% to 30%; The number is 3 to 4, the extraction time is 3 to 4 minutes, and the O/A ratio of copper extraction is 1: (1 to 2). 7 . The method for recovering copper and high-purity silicon powder from organosilicon waste contact bodies according to claim 1 , wherein the copper-extracted residual liquid is returned to the air flotation mechanical stirring coupling leaching tank for recycling. 8 . 8. The method for recovering copper and high-purity silicon powder from organosilicon waste contact bodies according to claim 1, wherein the mass concentration of sulfuric acid in the sulfuric acid solution B is 300 to 400 g/L; The number of stages is 2-3, the back-extraction time is 2-3min, and the ratio of back-extraction to O/A is (1-2):1. 9 . The method for recovering copper and high-purity silicon powder from organosilicon waste contact bodies according to claim 1 , wherein the regenerated organic phase is returned to the copper extraction step to be recycled for the extraction of copper-containing leachate. 10 . 10. The method for recovering copper and high-purity silicon powder from organosilicon waste contact bodies according to claim 1, wherein the electroplating cell uses a lead plate as an anode, a copper sheet as a cathode, and the electroplating current density is 200 ～400A/m ² , the cell voltage is 2.0～3.5V, and the electrowinning time is 12～36h.

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