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INVENTION
Russian Federation Patent RU2095443
Method of extracting precious metals from solutions
Name of the inventor: Gurov VA .; Ivanov VS
The name of the patentee: Open Joint Stock Company "Management of the Intergovernmental ore innovative program"
Address for correspondence:
Starting date of the patent: 1996.09.03
Usage: hydrometallurgy of precious metals and can be used to extract them from the productive solutions leaching of ores and industrial waste water.
The inventive method comprises periodically alternating cycles noble metal adsorption on ion exchangers and ion exchangers processing solution containing a reducing agent in the form of noble metal counter ion exchangers functional groups. The method allows to increase the saturation of the noble metal ion exchange resins.
DESCRIPTION OF THE INVENTION
The invention relates to a hydrometallurgical precious metals and can be used for extracting precious metals from the leaching solution produktcionnyh ores and materials, from the waste water and industrial discharges beneficiation of ores, for the separation and purification of noble metals from impurities.
There is a method of extracting precious metals, particularly silver, from a solution of silver nitrate in the amphoteric ion exchanger grade TSA in Na + -form (AB Davankov, VM and Laufer LA Shits "ZHPH", 1957 m. 30 vyp.6, s.839-844). After sorption cycle of silver ion exchanger was treated with hydroquinone and again led sorption.
A disadvantage of the method is the poor saturation of the ion exchanger with the noble metal adsorption from dilute solutions it due to the use for the treatment of the ion exchanger reductant solution of hydroquinone in nonionic form.
The closest to the invention is a process for the recovery of precious metals, particularly silver, from a solution of silver nitrate on a strong cation exchanger KU-2 (AB Davankov and VM Laufer "Math. University. Non-ferrous metallurgy", of N 4 for 1961 g, s.121-123 and "Factory laboratory", t.22, vyp.7 for 1956, s.788-789). There are periodically alternated sorption cycles and silver electrowinning phase of its recovery in case of the ion exchanger in a solution or a reducing exchanger treatment, sodium hydrosulfite otherwise.
The disadvantage of this method is low and the saturation of the ion exchanger noble metal from the processing of the ion exchanger with a solution containing a reducing agent, sulfite ion, not in the form of counter cation functional groups.
The aim of the invention is to increase the saturation of ion exchangers in sorption of precious metals from solutions.
The objective is achieved by the alternation of cycles of sorption of precious metals and processing of ion exchangers with a solution of noble metals are ion exchangers reductant processing solution containing a reducing agent in the form of functional groups counterion ion exchangers.
Summary of the invention is as follows. If sorption of silver cations in the cation they bind a functional group of the resin as a counter, displacing the cations in the solution, which was charged to the ion exchanger sorption. When processing cycle after cation sorption sodium bisulfite solution is a restoration of silver ions to the metallic state and the deposition of the noble metal in the resin phase. Place silver occupy functional groups of the ion exchanger, for example, Na + ions or other cations contained in the solution to be sorbed. At high salt content and the low concentration of precious metal recovered in the solution to be sorbed, it is usually the case, the saturation of the ion exchanger in the noble metal adsorption cycle becomes very low. As a result, it is often necessary to alternate operation of adsorption and processing of the resin solution of a reducing agent. If the ion exchanger, in this case the cation resin, treated with a solution containing a reducing agent in an appropriate amount to form the counterion of the functional groups of the ion exchanger, i.e. in this case in the form of a cation, then the reducing agent will not only restore the silver, but it takes place on the functional groups. For example, if the cation process tin chloride solution (II), the Sn 2+ cations restore the silver to the metallic state and, as counterions, the cationic charge in the Sn 2+ -form. As a result, during the subsequent adsorption of silver cations to be exchanged not only with Sn 2+ cations on functional groups, but also to recover and deposited in the exchanger phase sorption cycle. Thus, in the sorption process will occur and the ion exchange silver recovery and the ion exchanger phase. Because of these circumstances increase the selectivity of the resin to precious metals and to increase the saturation of the ion exchanger. Addition salts of tin (II) in this case may be treated with cation exchanger with a solution of hydrazine or hydroxylamine salts, reducing agent containing silver to form a cation. If the noble metal is present in solution in the anionic form, such as chloride complexes, and the adsorption is carried out on an anion exchanger, the post-treatment of the anion exchanger with a solution containing a reducing agent in the form of counter ions of functional groups of the ion exchanger, for example sodium hydrosulfite, lead to the same result. HSO ions -3 restore the noble metal and the charge of the anion in HSO -3-form. In the subsequent adsorption will occur and the ion exchange and recovery of the noble metal in the anion exchanger phase, and increase the saturation of the ion exchanger.
Thus, if the periodic alternation of precious metal sorption cycles and processing of ion exchangers with a solution of a reducing agent of precious metals processing of ion exchangers lead solution containing a reducing agent in the form of a counter functional groups of ion exchangers, the saturation of the noble metal ion exchange resins will increase and the goal is reached.
According to the well-known and offers the option of in vitro sorption carried silver from silver nitrate solution to the cation exchanger KU-2-8. A portion of the cation exchanger placed in a column and the filtered solution until the resin saturation. Next, the cation exchanger was treated with silver solution and reducing agent, a second sorption cycle. According to the residual silver concentration in the solution was determined by the amount of sorbed silver recovery and cation saturation of noble metal. The silver concentration in the feed solution was 30 mg / l. According to an embodiment known cation exchanger with a solution of sodium bisulfite at a concentration of 52 g / l, equivalent to the reducing capacity of silver of 1 g-eq / l. According to the proposed embodiment cation exchanger with a solution of tin chloride (II) with a concentration of 95g / l, equivalent to the reducing capacity of silver and 1 g-eq / l. The results are shown in the table.
From the table it follows that the treatment of the cation exchanger with a solution of tin chloride (II), containing a reducing agent in the form of the counterion of the functional groups of the ion exchanger, in comparison with the treatment with sodium bisulfite solution, the residual silver concentration decreased to a greater degree and saturation cation silver has increased from 143 to 246mg / g of the resin.
CLAIM
Method of extracting precious metals from solutions comprising periodic alternation of cycles noble metal adsorption on ion exchangers and ion exchangers processing solution noble metal reducing agent, characterized in that the ion exchangers are processing solution containing a reducing agent in the form of functional groups counterion ion exchangers.
print version
Publication date 05.12.2006gg
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