CN101942568B - Method for recovering noble metal from waste computer and fittings thereof - Google Patents
Method for recovering noble metal from waste computer and fittings thereof Download PDFInfo
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- CN101942568B CN101942568B CN2010105232204A CN201010523220A CN101942568B CN 101942568 B CN101942568 B CN 101942568B CN 2010105232204 A CN2010105232204 A CN 2010105232204A CN 201010523220 A CN201010523220 A CN 201010523220A CN 101942568 B CN101942568 B CN 101942568B
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- 239000002699 waste material Substances 0.000 title claims abstract description 27
- 238000000034 method Methods 0.000 title claims abstract description 26
- 229910000510 noble metal Inorganic materials 0.000 title abstract 4
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims abstract description 46
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 claims abstract description 32
- 229910052737 gold Inorganic materials 0.000 claims abstract description 32
- 239000010931 gold Substances 0.000 claims abstract description 32
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims abstract description 27
- 229910017604 nitric acid Inorganic materials 0.000 claims abstract description 27
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 claims abstract description 24
- 229910052763 palladium Inorganic materials 0.000 claims abstract description 23
- 229910052709 silver Inorganic materials 0.000 claims abstract description 19
- 239000004332 silver Substances 0.000 claims abstract description 19
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 claims abstract description 18
- NICDRCVJGXLKSF-UHFFFAOYSA-N nitric acid;trihydrochloride Chemical compound Cl.Cl.Cl.O[N+]([O-])=O NICDRCVJGXLKSF-UHFFFAOYSA-N 0.000 claims abstract description 16
- 235000019270 ammonium chloride Nutrition 0.000 claims abstract description 12
- 238000002386 leaching Methods 0.000 claims abstract description 12
- 238000011084 recovery Methods 0.000 claims abstract description 12
- 238000000053 physical method Methods 0.000 claims abstract description 4
- 238000006243 chemical reaction Methods 0.000 claims description 39
- 239000010970 precious metal Substances 0.000 claims description 38
- 239000000706 filtrate Substances 0.000 claims description 21
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 18
- 238000005868 electrolysis reaction Methods 0.000 claims description 17
- 239000008151 electrolyte solution Substances 0.000 claims description 15
- SQGYOTSLMSWVJD-UHFFFAOYSA-N silver(1+) nitrate Chemical compound [Ag+].[O-]N(=O)=O SQGYOTSLMSWVJD-UHFFFAOYSA-N 0.000 claims description 13
- 239000000843 powder Substances 0.000 claims description 12
- 238000003756 stirring Methods 0.000 claims description 12
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 8
- 239000010946 fine silver Substances 0.000 claims description 8
- 230000035484 reaction time Effects 0.000 claims description 8
- 239000000047 product Substances 0.000 claims description 7
- 229910001961 silver nitrate Inorganic materials 0.000 claims description 7
- 239000000243 solution Substances 0.000 claims description 7
- 229910003803 Gold(III) chloride Inorganic materials 0.000 claims description 6
- RJHLTVSLYWWTEF-UHFFFAOYSA-K gold trichloride Chemical compound Cl[Au](Cl)Cl RJHLTVSLYWWTEF-UHFFFAOYSA-K 0.000 claims description 6
- 229940076131 gold trichloride Drugs 0.000 claims description 6
- 230000005484 gravity Effects 0.000 claims description 6
- 238000007885 magnetic separation Methods 0.000 claims description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 6
- 238000001556 precipitation Methods 0.000 claims description 5
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 claims description 5
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 4
- 239000012535 impurity Substances 0.000 claims description 3
- 238000005555 metalworking Methods 0.000 claims description 3
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 claims description 3
- 238000012856 packing Methods 0.000 claims description 2
- 239000004033 plastic Substances 0.000 claims description 2
- 229920003023 plastic Polymers 0.000 claims description 2
- 239000000356 contaminant Substances 0.000 claims 1
- 238000012216 screening Methods 0.000 claims 1
- ONVGIJBNBDUBCM-UHFFFAOYSA-N silver;silver Chemical compound [Ag].[Ag+] ONVGIJBNBDUBCM-UHFFFAOYSA-N 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 230000001376 precipitating effect Effects 0.000 abstract 1
- 238000006722 reduction reaction Methods 0.000 description 9
- 238000007670 refining Methods 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- BFKJFAAPBSQJPD-UHFFFAOYSA-N tetrafluoroethene Chemical group FC(F)=C(F)F BFKJFAAPBSQJPD-UHFFFAOYSA-N 0.000 description 4
- 229910000906 Bronze Inorganic materials 0.000 description 3
- 238000000862 absorption spectrum Methods 0.000 description 3
- 239000010974 bronze Substances 0.000 description 3
- KUNSUQLRTQLHQQ-UHFFFAOYSA-N copper tin Chemical compound [Cu].[Sn] KUNSUQLRTQLHQQ-UHFFFAOYSA-N 0.000 description 3
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 230000008021 deposition Effects 0.000 description 2
- 238000006073 displacement reaction Methods 0.000 description 2
- 239000003792 electrolyte Substances 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 206010013786 Dry skin Diseases 0.000 description 1
- 229910045601 alloy Inorganic materials 0.000 description 1
- 239000000956 alloy Substances 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000008033 biological extinction Effects 0.000 description 1
- 238000005219 brazing Methods 0.000 description 1
- 230000001143 conditioned effect Effects 0.000 description 1
- 239000004020 conductor Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000007747 plating Methods 0.000 description 1
- 238000000247 postprecipitation Methods 0.000 description 1
- SATVIFGJTRRDQU-UHFFFAOYSA-N potassium hypochlorite Chemical compound [K+].Cl[O-] SATVIFGJTRRDQU-UHFFFAOYSA-N 0.000 description 1
- 238000010298 pulverizing process Methods 0.000 description 1
- 230000001698 pyrogenic effect Effects 0.000 description 1
- -1 silver ions Chemical class 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000001228 spectrum Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
Abstract
The invention discloses a method for recovering noble metal from waste computers and fittings thereof, which comprises the following procedures of a physical method processing procedure, a nitric acid leaching silver recovering procedure, a chloroazotic acid leaching gold recovering procedure and an ammonium chloride precipitating palladium recovering procedure. In the method of the invention, a full-wet process is adopted to recover the noble metal, so as to avoid the problems of high energy consumption and high pollution in the traditional fire method, and realize to recover the noble metal from the clamp plates in the waste computers with high efficiency, low pollution and low cost, wherein, the recovery of silver achieves 98.6%, the recovery of gold achieves 98.3%, and the recovery of palladium achieves 98.0%.
Description
Technical field
The present invention relates to a kind ofly, relate in particular to the method that from waste and old computer and accessory thereof, reclaims precious metal from containing the method that the precious metal waste reclaims precious metal.
Background technology
Along with popularizing and widespread use of computer, the computer of scrapping every year is increasing, contains precious metals such as gold and silver, palladium in waste and old computer and the accessory thereof.Wherein gold utensil have high anticorrosive and stable, and good electrical conductivity and thermal conductivity, be widely used in international reserve, jewelry is decorated and industry and science and technology on; Silver has good ductility, electroconductibility and thermal conduction, is widely used in conductor, system mirror and the sensitive materials of heat and electricity; Palladium is a more active metal in the precious metal, is widely used in the synthetic of electric slurry, plated material, catalyzer, brazing alloy and multiple contact material.China precious metal mineral products lack, and precious metal costs an arm and a leg, and therefore to realizing the regeneration of precious metal in the waste and old computer that contains precious metal and accessory such as the computer clamp, have crucial meaning to solving China's precious metal resource shortage.
At present, it is still immature both at home and abroad the precious metal waste from low levels to be reclaimed the technology of precious metal, also is in conceptual phase just, and major cause is that the various compositions in the waste are comparatively complicated, recovery technology is had relatively high expectations, also do not have very advantages of simplicity and high efficiency recovery method at present; Government is less relatively to the input of this respect besides, along with containing increasing year by year of precious metal waste, government and society are to the resource utilization of waste and old material and stop environmental pollution and more and more pay attention to, and therefore reclaim precious metal and have remarkable economical and social benefit from containing the precious metal waste.
Summary of the invention
For overcoming above-mentioned technological deficiency, the invention provides a kind of method that from waste and old computer and accessory thereof, reclaims precious metal, thereby realize the low cost of gold and silver in waste and old computer and the accessory thereof, palladium precious metal, high efficiency regeneration recovery.
Technical scheme of the present invention is as described below:
A kind of method that reclaims precious metal from waste and old computer and accessory thereof comprises the steps:
(1) physical method treatment process: waste and old computer and accessory thereof are pulverized with pulverizer, carried out magnetic separation then, gravity treatment obtains containing precious metal powder;
(2) nitric acid leaches and reclaims silver-colored operation: precious metal powder is added nitric acid dissolve, filter, filtrate obtains thick silver through the copper powder displacement, and thick galactic longitude electrorefining obtains fine silver;
(3) chloroazotic acid leaches and reclaims the metal working preface: described nitric acid filter residue is leached with chloroazotic acid, obtain thick gold precipitation and filtrate through reduction, thick gold obtains the higher-grade gold through electrorefining;
(4) the heavy palladium of ammonium chloride reclaims the palladium operation: above-mentioned thick golden filtrate is added clorox and ammonium chloride, filter and obtain chlordeneization two ammino palladium products.
In the described step (1), pulverizer is selected the vertical and high-speed rotating disintegrator for use, pulverizes after magnetic separation removes de-iron equimagnetic impurity, impurity such as plastics are removed in gravity treatment, sieves with 50 orders～70 mesh standard sieves and obtains the screen underflow metal powder of attaching most importance to, and described standard sieve is preferably 60 orders.
In the described step (2), in the reactor of precious metal powder and water medium of packing into, keep certain stirring intensity, adding concentration in the reactor is 10%～30% dilute nitric acid solution, control is leached endpoint pH 1.0～3.0, and temperature of reaction is 50 ℃～90 ℃, after reaction finishes, filtration obtains filtrate and filter residue, filtrate keeps certain stirring intensity under 40 ℃～80 ℃ temperature, add the copper powder of 1.0～2.0 times of required theoretical amount of reaction, reaction 1h～5h filters and obtains thick silver; Do anode, make negative electrode with the fine silver version with thick silver, make electrolytic solution with Silver Nitrate, logical direct current carries out electrolysis, and silver nitrate concentration is 120～160g/l in the electrolytic solution, and concentration of nitric acid is 2～6g/l, and electrolysis temperature is 35 ℃～50 ℃, and cathode current density is 250～450A/m
2, bath voltage 1.5V～2.5V, homopolarity width between centers 100～160mm obtains fine silver through electrolytic refining.
Principal reaction is as follows:
In step (2), the concentration of nitric acid, consumption, temperature of reaction, stirring intensity, reaction times etc. all directly influence the leaching yield of silver in this step.Test-results shows: when the concentration of nitric acid is 15%, temperature of reaction is 60 ℃, and the reaction times is 3 hours, and the leaching yield of silver is 99.8%.Add in the copper powder reduction reaction, when copper powder is 1.2 times of theoretical amount, temperature of reaction is 70 ℃, and the reaction times is 2 hours, and the reduction ratio of silver is 99.6%.In thick electrorefining of silver, concentration of electrolyte, nitric acid content, electrolysis temperature, current density, bath voltage and homopolarity width between centers etc. are all influential to electrorefining, and experimental result shows, Silver Nitrate 150g/l in electrolytic solution, nitric acid 4g/l, 40 ℃ of electrolysis temperatures, cathode current density 300A/m
2, bath voltage 2.0V during homopolarity width between centers 120mm, obtains 99.8% fine silver through electrolytic refining.
In the described step (3), be that described chloroazotic acid consists of the 3:1 configuration by volume of concentrated hydrochloric acid, concentrated nitric acid with the filter residue adding chloroazotic acid of step (2), control is leached endpoint pH 1.0～3.0, temperature of reaction is 40 ℃～80 ℃, after reaction finishes, filters and obtains leach liquor and leached mud; Leach liquor keeps certain stirring intensity under 40 ℃～80 ℃ temperature, add the S-WAT of 1.0～2.0 times of theoretical amount, and reaction 1h～5h filters and obtains thick gold; Do anode, make negative electrode with the proof gold sheet with thick gold, make electrolytic solution with the muriate of gold, logical direct current carries out electrolysis, gold trichloride concentration is 250～500g/l in the electrolytic solution, concentration of hydrochloric acid is 150～200g/l, and electrolysis temperature is 40～70 ℃, and cathode current density is 400～700A/m
2, bath voltage is 0.4～0.8V, homopolarity width between centers is 80～120mm, obtains the higher-grade gold through electrolytic refining.
Principal reaction is as follows:
The consumption of chloroazotic acid, temperature of reaction, stirring intensity, reaction times, solid-to-liquid ratio etc. all directly influence the leaching yield of gold in the step (3), test-results shows, the chloroazotic acid consumption is 1.5 times of theoretical amount, temperature of reaction is 70 ℃, liquid-solid ratio is 4:1, reaction times is 4 hours, and the leaching yield of gold is 99.6%; During with S-WAT reduction gold, sulfurous acid consumption, temperature of reaction, reduction pH value etc. have a direct impact the reduction ratio of gold, and experimental result surface sulfurous acid consumption is 1.5 times of theoretical amount, temperature of reaction is 60 ℃, reduction pH value is 4.0, and the recovery time is 3 hours, and the reduction ratio of gold is 99.4%; During thick golden electrolytic refining, concentration of electrolyte, nitric acid content, electrolysis temperature, current density, bath voltage and homopolarity width between centers etc. are all influential to electrorefining, the experimental result surface, in electrolytic solution, contain gold trichloride 400g/l, hydrochloric acid 180g/l, 55 ℃ of electrolysis temperatures, cathode current density 550A/m
2, bath voltage 0.6V, homopolarity width between centers 100mm obtains 99.9% higher-grade gold through electrolytic refining
In the described step (4), be that the thick golden filtrate in the step (3) is added clorox and ammonium chloride, regulate the pH value 1.0～4.0 with ammoniacal liquor, reaction obtained chlordeneization two ammino palladium products in 3 hours under 40 ℃～80 ℃ temperature.
Principal reaction is as follows:
The consumption of ammonium chloride in the step (4), precipitation pH value, temperature of reaction etc. all influence the deposition rate of palladium, and experimental result shows that ammonium chloride is 1.6 times of theoretical amount, and precipitation pH value is 3.5, and temperature of reaction is 80 ℃, and the reaction times is 3 hours, and the deposition rate of palladium is 99.5%.
Among the present invention, adopt full wet processing to reclaim precious metal, avoided high energy consumption in traditional pyrogenic process, high pollution problem, realized that high-level efficiency, low pollution, low cost reclaim precious metal from waste and old computer clamp.Wherein Yin the rate of recovery reaches 98.6%, and the rate of recovery of gold reaches 98.3%, and the rate of recovery of palladium reaches 98.0%.
Description of drawings
Fig. 1 is a recovery process flow sheet of the present invention.
Embodiment
The precious metal that reclaims from waste and old computer and accessory thereof of the present invention reclaims process flow sheet as shown in Figure 1, comprise the steps: (1) physical method treatment process: waste and old computer and accessory thereof are pulverized with pulverizer, carried out magnetic separation then, gravity treatment obtains containing precious metal powder; (2) nitric acid leaches and reclaims silver-colored operation: precious metal powder is added nitric acid dissolve, filter, filtrate obtains thick silver through the copper powder displacement, and thick galactic longitude electrorefining obtains fine silver; (3) chloroazotic acid leaches and reclaims the metal working preface: described nitric acid filter residue is leached with chloroazotic acid, obtain thick gold precipitation and filtrate through reduction, thick gold obtains the higher-grade gold through electrorefining; (4) the heavy palladium of ammonium chloride reclaims the palladium operation: above-mentioned thick golden filtrate is added potassium hypochlorite and ammonium chloride, filter and obtain chlordeneization two ammino palladium products.
Below in conjunction with accompanying drawing 1, the present invention is described in detail by specific embodiment.
Embodiment 1:
Get waste and old computer clamp 100kg, adopt the vertical and high-speed rotating disintegrator, the pulverizing time was made as 10 minutes, pulverized after sieve with 60 mesh standard sieves after magnetic separation and the gravity treatment, and screen underflow obtains containing precious metal powder 20.5kg; Receive detection, cupric 13kg, golden 0.05kg, silver-colored 1kg, palladium 0.04kg in the precious metal powder through atom extinction spectrum.
Embodiment 2:
Get precious metal powder 10kg among the embodiment 1, join in 100 liters the reactor of liner tetrafluoroethylene, add 40 premium on currency, temperature of reaction kettle is set at 60 ℃, stirring velocity is transferred to 120 rev/mins, continuous adding concentration is rare nitric acid of 15% in the past then still, the nitric acid flow is 2.0 liters/hour, when pH of leaching solution is 2.0, stop to add nitric acid, filter leach liquor, wash filter residue with less water, with filtrate constant volume to 50 liter, detecting concentration of silver ions through atomic absorption spectrum is 9.96 grams per liters, and the leaching yield of silver is 99.0%; Filtrate adds the copper powder of 1.2 times of reaction theory amounts under 70 ℃ of temperature, reaction 2h filters and obtains thick silver; The Silver Nitrate mass concentration is 150g/l in the electrolytic solution, and concentration of nitric acid is 4g/l, and electrolysis temperature is 40 ℃, and cathode current density is 300A/m
2, bath voltage 2.0V, homopolarity width between centers 120mm, the purity that obtains silver through electrolytic refining is 99.2%.
Embodiment 3:
Whole filter residues of getting embodiment 2 join in 30 liters the reactor of liner tetrafluoroethylene, add 10 premium on currency, temperature of reaction kettle is set at 70 ℃, stirring velocity is transferred to 120 rev/mins, in still, constantly add wang aqueous solution then, chloroazotic acid consists of concentrated hydrochloric acid, concentrated nitric acid is the 3:1 configuration by volume, and the chloroazotic acid add-on is 0.1 liter/hour, stops to add chloroazotic acid when pH of leaching solution is 2.5, filter leach liquor, wash filter residue with less water,, detect the content of GOLD FROM PLATING SOLUTION and palladium with atomic absorption spectrum filtrate constant volume to 12 liter, gold is: 2.01g/l, palladium is 1.60g/l, and the leaching yield of gold is 98.7%, and the leaching yield of palladium is 98.4%.
Embodiment 4:
The filtrate of the foregoing description 3 is joined in the reactor of 30 liters of liner tetrafluoroethylene, temperature of reaction kettle is set at 60 ℃, stirring velocity is transferred to 120 rev/mins, with ammoniacal liquor regulator solution pH value is 4.0, in reactor, add the 50g S-WAT then, reacted 3 hours, filter thick bronze and filtrate, wash thick bronze with less water after, be anode with thick bronze, the proof gold sheet is made negative electrode, gold trichloride is an electrolytic solution, and gold trichloride concentration is 400g/l in the control electrolytic solution, and concentration of hydrochloric acid is 180g/l, electrolysis temperature is 55 ℃, and cathode current density is 550A/m
2, bath voltage is 0.6V, homopolarity width between centers is 100mm, is 99.9% through the golden purity of the electrolysis of electrorefining gained.
Embodiment 5:
Thick golden filtrate among the embodiment 4 is joined in the reactor of 30 liters of liner tetrafluoroethylene, temperature of reaction kettle is set at 80 ℃, stirring velocity is transferred to 120 rev/mins, adds the ammonium chloride of 50g then, and ammoniacal liquor conditioned reaction pH value is about 3.5, reacted 3 hours, filter gained chlordeneization two ammino palladiums,, placed 100 ℃ of air dry oven inner dryings 3 hours with less water washing gained post precipitation, promptly get chlordeneization two ammino palladium products, the purity that detects products obtained therefrom with atomic absorption spectrum is 99.6%.
In sum; although the present invention is described in detail by specific embodiment; but persons skilled in the art should be understood that; the foregoing description only is the description to the preferred embodiments of the present invention; but not limiting the scope of the invention; persons skilled in the art are in the disclosed technical scope of the present invention, and the variation that can expect easily is all within protection scope of the present invention.
Claims (5)
1. a method that reclaims precious metal from waste and old computer and accessory thereof is characterized in that, comprises the steps:
(1) physical method treatment process: waste and old computer and accessory thereof are pulverized with pulverizer, carried out magnetic separation then, gravity treatment gets
To precious metal powder;
(2) nitric acid leaches and reclaims silver-colored operation: in the reactor of precious metal powder and water medium of packing into, keep certain stirring intensity, adding mass concentration in the reactor is 10%～30% dilute nitric acid solution, and control is leached endpoint pH 1.0～3.0, temperature of reaction is 50 ℃～90 ℃, after reaction finishes, filter and obtain filtrate and filter residue, filtrate is under 40 ℃～80 ℃ temperature, keep certain stirring intensity, the copper powder that adds 1.0～2.0 times of theoretical amount, reaction lh～5h filters and obtains thick silver; Do anode, make negative electrode with the fine silver version with thick silver, make electrolytic solution with Silver Nitrate, logical direct current carries out electrolysis, and silver nitrate concentration is 120～160g/l in the electrolytic solution, and concentration of nitric acid is 2～6g/l, and electrolysis temperature is 35 ℃～50 ℃, and cathode current density is 250～450A/m
2, bath voltage 1.5V～2.5V, homopolarity width between centers l00～160mm obtains fine silver through electrorefining;
(3) chloroazotic acid leaches and reclaims the metal working preface: be the filter residue adding chloroazotic acid with step (2), described chloroazotic acid consists of the 3:l configuration by volume of concentrated hydrochloric acid, concentrated nitric acid, and control is leached endpoint pH 1.0～3.0, and temperature of reaction is 40 ℃～80 ℃, after reaction finishes, filter and obtain leach liquor and leached mud; Leach liquor keeps certain stirring intensity under 40 ℃～80 ℃ temperature, add the S-WAT of 1.0～2.0 times of theoretical amount, and reaction lh～5h filters and obtains thick gold precipitation and filtrate; Do anode, make negative electrode with the proof gold sheet with thick gold, make electrolytic solution with the muriate of gold, logical direct current carries out electrolysis, the gold trichloride mass concentration is 250～500g/l in the electrolytic solution, the hydrochloric acid mass concentration is 150～200g/l, and electrolysis temperature is 40～70 ℃, and cathode current density is 400 A～700A/m
2, bath voltage is 0.4～0.8V, homopolarity width between centers is 80～120mm, obtains the higher-grade gold through electrorefining;
(4) the heavy palladium of ammonium chloride reclaims the palladium operation: the thick golden filtrate in the step (3) is added clorox and ammonium chloride, regulate the pH value 1.0～4.0 with ammoniacal liquor, reaction was filtered and is obtained chlordeneization two ammino palladium products in 3 hours under 40 ℃～80 ℃ temperature, and described ammonium chloride is 1.6 times of theoretical amount.
2. as the described method that from waste and old computer and accessory thereof, reclaims precious metal of claim l, it is characterized in that: institute
State in the step (1), pulverizer is selected the vertical and high-speed rotating disintegrator for use, pulverizes after ferromegnetism impurity is removed in magnetic separation, gravity treatment removes
Go plastic contaminant, obtaining screen underflow with 50 orders～70 mesh standard sieves screening is precious metal powder.
3. the method that reclaims precious metal from waste and old computer and accessory thereof as claimed in claim 2 is characterized in that: institute
Stating standard sieve is 60 orders.
4. the method that reclaims precious metal from waste and old computer and accessory thereof as claimed in claim 1 is characterized in that: in the described step (2), adding mass concentration in the reactor is 15% dilute nitric acid solution, control leaching endpoint pH 1.0～
3.0 temperature of reaction is 60 ℃, the reaction times is 3h, after reaction finishes, filters and obtains filtrate and filter residue; Filtrate adds the copper powder of 1.2 times of theoretical amount under 70 ℃ of temperature, reaction 2h filters and obtains thick silver; Silver nitrate concentration is 150g/l in the electrolytic solution, and concentration of nitric acid is 4g/l, and electrolysis temperature is 40 ℃, and cathode current density is 300A/m
2, bath voltage 2.0V, homopolarity width between centers 120mm obtains fine silver through electrorefining.
5. the method that from waste and old computer and accessory thereof, reclaims precious metal as claimed in claim 1, it is characterized in that: chloroazotic acid consists of the 3:l configuration by volume of concentrated hydrochloric acid, concentrated nitric acid, consumption is 1.5 times of theoretical amount, and temperature of reaction is 70 ℃, and the reaction times is 4 hours; The S-WAT consumption is 1.5 times of theoretical amount, and temperature of reaction is 60 ℃, and reduction pH value is 4.0, and the recovery time is 3 hours; The gold trichloride mass concentration is 400g/l in the electrolytic solution, and the hydrochloric acid mass concentration is 180g/l, 55 ℃ of electrolysis temperatures, and cathode current density is 550A/m
2, bath voltage is 0.6V, homopolarity width between centers l00mm.
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| CN110484744B (en) * | 2019-08-26 | 2020-07-24 | 珠海格力电器股份有限公司 | Method for recovering precious metal from waste chip capacitor |
| WO2021161316A1 (en) | 2020-02-12 | 2021-08-19 | Bromine Compounds Ltd. | A process for recovering metals from recycled rechargeable batteries |
| CN113528849B (en) * | 2021-06-02 | 2022-12-23 | 云南滇金投资有限公司 | Method for extracting refined gold from palladium-silver-containing alloy gold |
| CN115491512A (en) * | 2021-06-17 | 2022-12-20 | 江苏宁达环保股份有限公司 | Method for extracting and recovering noble metal from cathode ray tube fluorescent powder |
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