CN115786713A - Method and system for recovering silver and aluminum from retired solar cell panel - Google Patents
Method and system for recovering silver and aluminum from retired solar cell panel Download PDFInfo
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- CN115786713A CN115786713A CN202211626139.8A CN202211626139A CN115786713A CN 115786713 A CN115786713 A CN 115786713A CN 202211626139 A CN202211626139 A CN 202211626139A CN 115786713 A CN115786713 A CN 115786713A
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Abstract
The invention relates to the field of solid waste recycling treatment, and particularly discloses a method and a system for recycling silver and aluminum from a retired solar cell panel. According to the invention, the silver and the aluminum in the waste solar cell panel are leached by using the mixed solution of methanesulfonic acid and hydrogen peroxide through the heat treatment system, the acid leaching system, the chlorination silver-precipitating system and the crude silver powder recovery system, so that the leaching efficiency is high, and toxic and harmful gases are not generated. The high-efficiency recovery of silver and aluminum is realized, and the leaching agent can be recycled.
Description
Technical Field
The invention relates to the field of solid waste recycling treatment, in particular to a method and a system for recycling silver and aluminum from a retired solar cell panel.
Background
With the increasing global warming trend and the exhaustion of fossil fuels, people increasingly pay attention to clean energy sources such as wind energy, solar energy, geothermal energy, tidal energy and the like. Solar photovoltaic power generation systems (photovoltaics) which are important branches of clean energy are greatly developed and applied.
By the end of 2019, the global photovoltaic new charging amount is 120GW, the global photovoltaic cumulative charging amount is 615GW, and the global photovoltaic cumulative charging amount is increased to 745GW in 2020. According to the estimation of the International Energy Agency (IEA), the global photovoltaic accumulated loading is expected to reach 1 721GW by the end of 2030.
In China, under the double promotion of national policy guidance and market demand, the photovoltaic industry in China not only has rapid technical development, but also has rapid increase of yield in order to realize the ambitious goals of carbon peak reaching and carbon neutralization. According to the report of a Chinese photovoltaic industry route map (2019 edition), the photovoltaic loading capacity of 30GW is newly added nationwide in 2019, the cumulative grid-connected capacity reaches 204GW, the first GW is all the world, and the total mass of the existing photovoltaic module is about 1350 ten thousand t. Among the numerous types of photovoltaic modules, crystalline silicon type photovoltaic modules dominate. The theoretical life of a typical crystalline silicon-type photovoltaic module is 25-30 years, but the outdoor environment accelerates the aging of the photovoltaic module, resulting in a substantial reduction in its actual service life. The peak time to first scrap of photovoltaic modules has begun in 2012. International renewable energy center (IRENA) predicted that worldwide retired photovoltaic modules would reach 7800 ten thousand tons in 2050, while domestic retired photovoltaic modules would include 197 ten thousand tons of glass, 46 ten thousand tons of aluminum, 11.1 ten thousand tons of silicon, 1080 tons of silver, 16236 tons of copper in 2030. The retired photovoltaic module contains a large amount of valuable elements (aluminum, silicon, silver, copper and the like), and resource waste and environmental pollution are caused by improper disposal.
At present, pretreatment is mostly adopted to separate a silicon plate and glass from silver recovered from a retired photovoltaic module, and then inorganic acid such as nitric acid and hydrofluoric acid is adopted to leach silver at a positive electrode and aluminum at a negative electrode of the silicon plate. The inorganic acid leaching can obtain better metal leaching rate, particularly, hydrofluoric acid can effectively remove a silicon nitride anti-reflection layer on the surface of a silicon plate, and the method has remarkable advantages for improving the recovery rate and the quality of the polycrystalline silicon substrate. Nitric acid is volatile and has strong oxidizing properties, and toxic NOx is produced during leaching. Hydrofluoric acid is volatile and toxic, and presents a potential safety risk to operators.
Disclosure of Invention
The invention aims to provide a method and a system for recycling silver and aluminum from a retired solar cell panel, so as to solve the problem that in the prior art, volatile liquid with high toxicity exists during recycling, and potential safety risks exist to operators.
In order to achieve the purpose, the invention adopts the following technical scheme: the method for recovering silver and aluminum from the retired solar cell panel comprises the following steps:
(1) Disassembling, and separating the crystalline silicon plate from the cell panel assembly;
(2) Heat treatment, namely crushing the disassembled crystalline silicon plate to the particle size of 2-5 mm, heating to 500-600 ℃ in an inert atmosphere, preserving heat for 30-60 min, and reducing the temperature to normal temperature in the inert atmosphere;
(3) Acid leaching, namely adding methanesulfonic acid with the mass fraction of 30-45% and H with the mass fraction of 5-15% 2 O 2 The mixed solution is used for leaching silver and aluminum, the solid ratio of the leaching solution is 5:1-15 (liquid volume: solid mass, unit ml/g or L/kg), the leaching temperature is 60-75 ℃, and the leaching time is 1.5-3 h; filtering after leaching to obtain filtrate 1And filtering residue 1; adjusting the pH of the filtrate 1 to be =4 by using a NaOH solution with the mass fraction of 20% to remove aluminum, and filtering again to obtain a filtrate 2 and a filter residue 2; the filtrate 2 enters a chlorination silver precipitation system;
(4) Chloridizing and depositing silver, adding hydrochloric acid with the mass fraction of 10-20% into the filtrate 2 to deposit silver under the stirring state, and then filtering to obtain a filtrate 3 and a filter residue 3; filtrate 3 with methanesulfonic acid and H 2 O 2 Adjusting the components, returning to the silver leaching system in the step (3), extracting 30% of the total amount of the extracted components to a sodium methanesulfonate recovery unit after Na + in the silver leaching system reaches 35-45 g/L, and returning the generated methanesulfonic acid to the acid leaching system in the step (3); and the filter residue 3 enters a coarse silver powder recovery system.
The principle and the advantages of the scheme are as follows: in practical application, the invention can be directly classified and recycled after high-temperature pyrolysis, so that the additional value of the recycled substances is improved; the mixed solution of methanesulfonic acid and hydrogen peroxide is used for leaching silver and aluminum in the waste solar cell panel, so that the leaching efficiency is high, and toxic and harmful gases are not generated. The high-efficiency recovery of silver and aluminum is realized, and the leaching agent can be recycled. Nitric acid and hydrogen are leached by inorganic acid such as fluoric acid and the like to treat the waste solar cell panel, so that gaseous toxic substances NOx and HF are generated, a complex waste gas purification system is required to be matched, and the industrial application of the waste solar cell panel is limited. The invention is innovative in that the invention provides a method for preparing the compound of methanesulfonic acid and H 2 O 2 The complete process flow and the method for leaching the waste solar cell panel by the composite system respectively realize the recycling of silver and aluminum without generating toxic gas. And gives a complete process for the leaching of silver from waste solar panels by means of methane sulphonic acid and the post-treatment and separation of the leached products.
Preferably, as an improvement, the method also comprises (5) recovering the coarse silver powder, fully dissolving silver chloride in filter residue 3 by using ammonia water, controlling the pH of the solution to be = 11-12, adding hydrazine hydrate under the stirring state, controlling the adding amount of the hydrazine hydrate to be 30-40 g/L, and reducing for 60-90 min; filtering after reduction is finished to obtain filter residue 4 and filtrate 4, wherein the main component of the filter residue 4 is crude silver powder;
the filtrate 4 is sent to a wastewater treatment unit.
Preferably, as an improvement, in the step (2) heat treatment, the crystalline silicon plate is crushed to have a particle size of 2-5 mm, heated to 500 ℃ in an inert atmosphere, and kept for 30min.
Preferably, as an improvement, in the acid leaching in the step (3), 30 mass percent of methanesulfonic acid is used, and 5 mass percent of H is used 2 O 2 The silver and the aluminum are leached by the mixed solution, the solid ratio of the leaching solution is 5:1 (liquid volume: solid mass, unit ml/g or L/kg), the leaching temperature is 60 ℃, and the leaching time is 1.5h.
Preferably, as an improvement, in the silver chloride precipitation in the step (4), hydrochloric acid with the concentration of 15% is added into the filtrate 2 for silver precipitation, and after the Na + in the silver chloride precipitation reaches 40g/L, 30% of the total amount is extracted and sent to a sodium methanesulfonate recovery unit.
Preferably, as an improvement, the filter residue 3 is fully dissolved with ammonia water to obtain silver chloride, the pH of the solution is controlled to be =11, the adding amount of hydrazine hydrate is controlled to be 30g/L, and the reduction time is 60min.
Preferably, as an improvement, the filter residue 3 is fully dissolved with ammonia water to obtain silver chloride, the pH of the solution is controlled to be =12, the adding amount of hydrazine hydrate is controlled to be 40g/L, and the reduction time is 90min.
Preferably, as an improvement, the filter residue 3 is fully dissolved with ammonia water to obtain silver chloride, the pH of the solution is controlled to be =11.4, the adding amount of hydrazine hydrate is controlled to be 35g/L, and the reduction time is 75min.
Silver-colored and aluminium system is retrieved to retired solar cell panel, its characterized in that includes:
disassembling the system, and separating the crystalline silicon plate from the cell panel assembly;
the heat treatment system is used for crushing the disassembled crystalline silicon plate to the particle size of 2-5 mm, heating the crushed crystalline silicon plate to 500-600 ℃ in an inert atmosphere, preserving the heat for 30-60 min, and reducing the temperature to the normal temperature in the inert atmosphere;
the acid leaching system uses methanesulfonic acid with the mass fraction of 30-45% and H with the mass fraction of 5-15% 2 O 2 The mixed solution is used for leaching silver and aluminum, the solid ratio of the leaching solution is 5:1-15 (liquid volume: solid mass, unit ml/g or L/kg), the leaching temperature is 60-75 ℃, and the leaching time is 1.5-3 h; filtering after leaching to obtain filtrate 1 and filter residue 1; adjusting the pH of the filtrate 1 to be =4 by using a NaOH solution with the mass fraction of 20% to remove aluminum, and filtering again to obtain a filtrate 2 and a filter residue 2; filter elementThe liquid 2 enters a chlorination silver precipitation system;
a chlorination silver precipitation system, wherein hydrochloric acid with the concentration of 10% -20% is added into the filtrate 2 to precipitate silver under the stirring state, and then the filtrate 3 and the filter residue 3 are obtained through filtration; filtrate 3 with methanesulfonic acid and H 2 O 2 Adjusting the components, returning to a leaching silver extraction system in the acid leaching system, extracting 30% of the total volume of filtrate 3 to send to a sodium methanesulfonate recovery unit after Na + in the silver extracting system reaches 35-45 g/L, and returning the generated methanesulfonic acid to the acid leaching system; and the filter residue 3 enters a coarse silver powder recovery system.
Preferably, in the coarse silver powder recovery system, the filter residue 3 is fully dissolved with ammonia water to obtain silver chloride, the pH of the solution is controlled to be = 11-12, hydrazine hydrate is added under the stirring state, the addition amount of the hydrazine hydrate is controlled to be 30-40 g/L, and the reduction time is 60-90 min; filtering after reduction is finished to obtain filter residue 4 and filtrate 4, wherein the main component of the filter residue 4 is crude silver powder; the filtrate 4 is sent to a wastewater treatment unit.
Drawings
Fig. 1 is a process flow diagram of a method for recovering silver and aluminum from a retired solar cell panel according to embodiment 1 of the present invention.
Detailed Description
The following is further detailed by way of specific embodiments:
example 1 is substantially as shown in figure 1:
(1) Dismantling
And the disassembly system separates components such as the aluminum frame, the junction box and the like from the crystalline silicon plate. The crystalline silicon plate is the main processing object of the present invention.
(2) Thermal treatment
And crushing the disassembled cell panel to a particle size of 2mm, heating to 500 ℃ in an inert atmosphere, preserving heat for 30min, and reducing the temperature to normal temperature in the inert atmosphere.
(3) Acid leaching system
Using methanesulfonic acid with the mass fraction of 30 percent and H with the mass fraction of 5 percent 2 O 2 The silver and the aluminum are leached by the mixed solution, the solid ratio of the leaching solution is 5:1 (liquid volume: solid mass, unit ml/g or L/kg), the leaching temperature is 60 ℃, and the leaching time is 1.5h. And filtering after leaching is finished to obtain filtrate 1 and filter residue 1.
Filtrate 1 was adjusted to pH =4 with NaOH to remove aluminum and then filtered again to give filtrate 2 and residue 2. And (4) feeding the filtrate 2 into a chlorination silver precipitation system.
(4) Chloridizing silver-precipitating system
Adding hydrochloric acid with the mass fraction of 10% -20% into the filtrate 2 under the stirring state for silver precipitation, and then filtering to obtain filtrate 3 and filter residue 3.
Filtrate 3 with methanesulfonic acid and H 2 O 2 And adjusting the components, returning to a leaching silver extraction system, extracting 30% of the total volume of filtrate 3 to a sodium methanesulfonate recovery unit after Na + in the silver extraction system reaches 40g/L, and returning the generated methanesulfonic acid to an acid leaching system. The main component of the filter residue 3 is silver chloride, and the filter residue enters a coarse silver powder recovery system.
(5) Coarse silver powder recovery system
And (3) fully dissolving silver chloride in filter residue 3 by using ammonia water, controlling the pH of the solution to be =11, adding hydrazine hydrate under the stirring state, controlling the adding amount of the hydrazine hydrate to be 30g/L, and reducing for 60min. And filtering after reduction is finished to obtain filter residue 4 and filtrate 4, wherein the main component of the filter residue 4 is crude silver powder. The filtrate 4 is sent to a wastewater treatment unit.
The invention can be directly classified and recycled after high-temperature pyrolysis, so that the additional value of the recycled substances is improved; the mixed solution of methanesulfonic acid and hydrogen peroxide is used for leaching silver and aluminum in the waste solar cell panel, so that the leaching efficiency is high, and toxic and harmful gases are not generated. The high-efficiency recovery of silver and aluminum is realized, and the leaching agent can be recycled. Since nitric acid and hydrogen are leached by inorganic acids such as hydrofluoric acid and the like to treat the waste solar cell panel, gaseous toxic substances NOx and HF are generated, a complex waste gas purification system needs to be matched, and the industrial application of the waste gas purification system is limited. The invention is innovative in that the invention provides a method for preparing the compound of methanesulfonic acid and H 2 O 2 The complete process flow and the method for leaching the waste solar cell panel by the composite system respectively realize the recycling of silver and aluminum without generating toxic gas. And gives a complete process of post-treatment and separation of the leaching of silver from the waste solar panels by means of methane sulphonic acid and the leaching products.
Example two
(1) Dismantling
And the disassembly system separates components such as the aluminum frame, the junction box and the like from the crystalline silicon plate. The crystalline silicon plate is the main processing object of the present invention.
(2) Thermal treatment
And crushing the disassembled battery plate to a particle size of 5mm, heating to 600 ℃ in an inert atmosphere, preserving heat for 60min, and reducing the temperature to normal temperature in the inert atmosphere.
(3) Acid leaching system
Using methanesulfonic acid with the mass fraction of 45% and H with the mass fraction of 15% 2 O 2 The mixed solution of the silver and the aluminum is used for leaching silver and aluminum, the solid ratio of the leaching solution is 15 (liquid volume: solid mass, unit ml/g or L/kg), the leaching temperature is 75 ℃, and the leaching time is 3 hours. And filtering after leaching is finished to obtain filtrate 1 and filter residue 1.
The filtrate 1 is adjusted to pH =5 with a 20% by mass NaOH solution to remove aluminum, and then filtered again to obtain a filtrate 2 and a residue 2. And (4) feeding the filtrate 2 into a chlorination silver precipitation system.
(4) Chloridizing silver-precipitating system
Adding hydrochloric acid with the mass fraction of 20% into the filtrate 2 under stirring for silver precipitation, and then filtering to obtain filtrate 3 and filter residue 3.
(5) Coarse silver powder recovery system
And (3) sufficiently dissolving silver chloride in the filter residue 3 by using ammonia water, controlling the pH of the solution to be =12, adding hydrazine hydrate under the stirring state, controlling the adding amount of the hydrazine hydrate to be 40g/L, and reducing for 90min. And filtering after reduction is finished to obtain filter residue 4 and filtrate 4, wherein the main component of the filter residue 4 is crude silver powder. The filtrate 4 is sent to a wastewater treatment unit.
The invention can be directly classified and recycled after high-temperature pyrolysis, so that the additional value of the recycled substances is improved; the mixed solution of methanesulfonic acid and hydrogen peroxide is used for leaching silver and aluminum in the waste solar cell panel, so that the leaching efficiency is high, and toxic and harmful gases are not generated. Realize the high-efficiency recovery of silver and aluminum and leachingThe discharged agent can be recycled. Nitric acid and hydrogen are leached by inorganic acid such as fluoric acid and the like to treat the waste solar cell panel, so that gaseous toxic substances NOx and HF are generated, a complex waste gas purification system is required to be matched, and the industrial application of the waste solar cell panel is limited. The invention is innovative in that methanesulfonic acid + H is given 2 O 2 The complete process flow and the method for leaching the waste solar cell panel by the composite system respectively realize the recycling of silver and aluminum without generating toxic gas. And gives a complete process of post-treatment and separation of the leaching of silver from the waste solar panels by means of methane sulphonic acid and the leaching products.
EXAMPLE III
(1) Dismantling
And the disassembly system separates components such as the aluminum frame, the junction box and the like from the crystalline silicon plate. The crystalline silicon plate is the main processing object of the present invention.
(2) Thermal treatment
And crushing the disassembled battery plate to a particle size of 3mm, heating to 550 ℃ in an inert atmosphere, preserving heat for 40min, and reducing the temperature to normal temperature in the inert atmosphere.
(3) Acid leaching system
Using methanesulfonic acid with the mass fraction of 38% and H with the mass fraction of 10% 2 O 2 The silver and aluminum are leached by the mixed solution, the solid ratio of the leaching solution is 10 (liquid volume: solid mass, unit ml/g or L/kg), the leaching temperature is 70 ℃, and the leaching time is 2 hours. And filtering after leaching is finished to obtain filtrate 1 and filter residue 1.
The filtrate 1 was adjusted to pH =4.5 with a 20% by mass NaOH solution to remove aluminum, and then filtered again to obtain filtrate 2 and residue 2. And (4) feeding the filtrate 2 into a chlorination silver precipitation system.
(4) Silver system is sunk in chlorination
Adding hydrochloric acid with the mass fraction of 20% into the filtrate 2 under stirring for silver precipitation, and then filtering to obtain filtrate 3 and filter residue 3.
(5) Coarse silver powder recovery system
And (3) fully dissolving silver chloride in the filter residue 3 by using ammonia water, controlling the pH of the solution to be =11.4, adding hydrazine hydrate under the stirring state, controlling the adding amount of the hydrazine hydrate to be 35g/L, and reducing for 70min. And filtering after reduction is finished to obtain filter residue 4 and filtrate 4, wherein the main component of the filter residue 4 is crude silver powder. The filtrate 4 is sent to a wastewater treatment unit.
The invention can be directly classified and recycled after high-temperature pyrolysis, so that the additional value of recycled substances is improved; the mixed solution of methanesulfonic acid and hydrogen peroxide is used for leaching silver and aluminum in the waste solar cell panel, so that the leaching efficiency is high, and toxic and harmful gases are not generated. The high-efficiency recovery of silver and aluminum is realized, and the leaching agent can be recycled. Nitric acid and hydrogen are leached by inorganic acid such as fluoric acid and the like to treat the waste solar cell panel, so that gaseous toxic substances NOx and HF are generated, a complex waste gas purification system is required to be matched, and the industrial application of the waste solar cell panel is limited. The invention is innovative in that methanesulfonic acid + H is given 2 O 2 The complete process flow and the method for leaching the waste solar cell panel by the composite system respectively realize the recycling of silver and aluminum without generating toxic gas. And gives a complete process of post-treatment and separation of the leaching of silver from the waste solar panels by means of methane sulphonic acid and the leaching products.
The above description is only an example of the present invention, and the general knowledge of the known specific technical solutions and/or characteristics and the like in the solutions is not described herein too much. It should be noted that, for those skilled in the art, variations and modifications can be made without departing from the technical solution of the present invention, and unless otherwise specifically stated or limited, the terms "mounted," "connected," "fixed," and the like are to be construed broadly, and for example, may be fixedly connected, detachably connected, or integrally connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations. The scope of the claims of the present application shall be determined by the contents of the claims, and the description of the embodiments and the like in the specification shall be used to explain the contents of the claims.
Claims (10)
1. The method for recycling the silver and the aluminum from the retired solar cell panel is characterized by comprising the following steps of:
(1) Disassembling, and separating the crystalline silicon plate from the cell panel assembly;
(2) Heat treatment, namely crushing the disassembled crystalline silicon plate to the particle size of 2-5 mm, heating to 500-600 ℃ in an inert atmosphere, preserving heat for 30-60 min, and reducing the temperature to normal temperature in the inert atmosphere;
(3) Acid leaching, namely adding methanesulfonic acid with the mass fraction of 30-45% and H with the mass fraction of 5-15% 2 O 2 The silver and the aluminum are leached by the mixed solution, the solid ratio of the leaching solution is 5:1-15, the leaching temperature is 60-75 ℃, and the leaching time is 1.5-3 h; filtering after leaching to obtain filtrate 1 and filter residue 1; adjusting the pH of the filtrate 1 to be =4 by using NaOH with the mass fraction of 20% to remove aluminum, and filtering again to obtain filtrate 2 and filter residue 2; the filtrate 2 enters a chlorination silver precipitation system;
(4) Chloridizing and depositing silver, adding hydrochloric acid with the mass fraction of 10% -20% into the filtrate 2 to deposit silver under the stirring state, and then filtering to obtain a filtrate 3 and a filter residue 3; filtrate 3 with methanesulfonic acid and H 2 O 2 Adjusting components, returning to the silver leaching system in the step (3), extracting 30% of the total volume of the filtrate 3 to send to a sodium methanesulfonate recovery unit after Na + in the silver leaching system reaches 35-45 g/L, and returning the generated methanesulfonic acid to the acid leaching system in the step (3); and the filter residue 3 enters a coarse silver powder recovery system.
2. The method of decommissioning solar panels as claimed in claim 1, wherein the method comprises: recovering the coarse silver powder, fully dissolving silver chloride in the filter residue 3 by using ammonia water, controlling the pH of the solution to be = 11-12, adding hydrazine hydrate under the stirring state, controlling the adding amount of the hydrazine hydrate to be 30-40 g/L, and reducing for 60-90 min; filtering after reduction is finished to obtain filter residue 4 and filtrate 4, wherein the main component of the filter residue 4 is crude silver powder; the filtrate 4 is sent to a wastewater treatment unit.
3. The method of decommissioning solar panels as claimed in claim 1, wherein the method comprises the following steps: in the step (2) of heat treatment, the crystalline silicon plate is crushed to the particle size of 2-5 mm, heated to 500 ℃ in an inert atmosphere and kept for 30min.
4. The method of decommissioning solar panels as claimed in claim 1, wherein the method comprises: in the acid leaching in the step (3), methanesulfonic acid with the mass fraction of 30% is used, and H with the mass fraction of 5% is added 2 O 2 The silver and the aluminum are leached by the mixed solution, the solid ratio of the leaching solution is 5:1, the leaching temperature is 60 ℃, and the leaching time is 1.5h.
5. The method of decommissioning solar panels as claimed in claim 1, wherein the method comprises: in the step (4), during silver precipitation by chlorination, 15% by mass of hydrochloric acid is added into the filtrate for silver precipitation, and 30% of the total volume of the filtrate is extracted and sent to a sodium methanesulfonate recovery unit after Na + in the filtrate reaches 40 g/L.
6. The method of decommissioning solar panels of claim 2, wherein the method comprises: and (3) fully dissolving silver chloride in filter residue 3 by using ammonia water, controlling the pH of the solution to be =11, controlling the adding amount of hydrazine hydrate to be 30g/L, and reducing for 60min.
7. The method of decommissioning solar panels of claim 2, wherein the method comprises: and (3) sufficiently dissolving silver chloride in the filter residue 3 by using ammonia water, controlling the pH of the solution to be =12, controlling the adding amount of hydrazine hydrate to be 40g/L, and reducing for 90min.
8. The method of decommissioning solar panels of claim 2, wherein the method comprises: and (3) sufficiently dissolving silver chloride in the filter residue 3 by using ammonia water, controlling the pH of the solution to be =11.4, controlling the adding amount of hydrazine hydrate to be 35g/L, and reducing for 75min.
9. The decommissioned solar panel silver and aluminum recovery system according to claim 1, comprising:
disassembling the system, and separating the crystalline silicon plate from the battery plate assembly;
the heat treatment system is used for crushing the disassembled crystalline silicon plate to the particle size of 2-5 mm, heating the crystalline silicon plate to 500-600 ℃ in an inert atmosphere, preserving the heat for 30-60 min, and reducing the temperature to the normal temperature in the inert atmosphere;
the acid leaching system uses methanesulfonic acid with the mass fraction of 30-45% and H with the mass fraction of 5-15% 2 O 2 The silver and the aluminum are leached by the mixed solution, the solid ratio of the leaching solution is 5:1-15, the leaching temperature is 60-75 ℃, and the leaching time is 1.5-3 h; filtering after leaching to obtain filtrate 1 and filter residue 1; adjusting the pH of the filtrate 1 to be =4 by using a NaOH solution with the mass fraction of 20% to remove aluminum, and filtering again to obtain a filtrate 2 and a filter residue 2; the filtrate 2 enters a chlorination silver precipitation system;
a chlorination silver precipitation system, wherein hydrochloric acid with the concentration of 10% -20% is added into the filtrate 2 to precipitate silver under the stirring state, and then the filtrate 3 and the filter residue 3 are obtained through filtration; filtrate 3 with methanesulfonic acid and H 2 O 2 Adjusting components, returning to a leaching silver extraction system in the acid leaching system, extracting 30% of the total amount to send to a sodium methanesulfonate recovery unit after Na + in the silver extracting system reaches 35-45 g/L, and returning the generated methanesulfonic acid to the acid leaching system; and the filter residue 3 enters a coarse silver powder recovery system.
10. The system for the decommissioning of solar panels for the recovery of silver and aluminum according to claim 9, wherein: in the crude silver powder recovery system, the filter residue 3 is fully dissolved with ammonia water to obtain silver chloride, the pH of the solution is controlled to be = 11-12, hydrazine hydrate is added under the stirring state, the addition amount of the hydrazine hydrate is controlled to be 30-40 g/L, and the reduction time is 60-90 min; filtering after reduction is finished to obtain filter residue 4 and filtrate 4, wherein the main component of the filter residue 4 is crude silver powder; the filtrate 4 is sent to a wastewater treatment unit.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117587249A (en) * | 2023-12-28 | 2024-02-23 | 横峰县凯怡实业有限公司 | Method for preparing silver powder by utilizing silver-containing waste |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN117587249A (en) * | 2023-12-28 | 2024-02-23 | 横峰县凯怡实业有限公司 | Method for preparing silver powder by utilizing silver-containing waste |
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