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    • 专利摘要:
    SUMMARY The present invention provides a process for recovering valuable metals from slag from noble metal malting, comprising: melting the slag Than noble metal malt and a flux in a top-blast rotary smelting furnace to form lead-bismuth alloy, wherein the slag comprises Bi and Pb; electrolyzing the lead bismuth alloy at a current density of from 60 to 110 A / m2 to obtain lead cathode and lead anode; pure lead anode sludge to form bismuth and silver-zinc crust; and extract gold and silver separately Than silver zinc crust. By using a top-blast rotary smelting furnace as a smelting device and adjusting the flux ratio, the present invention enriches the precious metals gold, silver, bismuth, lead or the like, in the lead-bismuth alloy, sakertaller, containing gold, silver, bismuth and lead content in the reducing agent. the slag and thus increase the rich recovery rates of gold, silver, bismuth and lead from the slag tan noble metal malting.
    公开号:SE537159C2
    申请号:SE1251476
    申请日:2012-12-20
    公开日:2015-02-24
    发明作者:Songlin Zhou；Xiangtian Xie
    申请人:Xiangguang Copper Co Ltd；
    IPC主号:
    专利说明:

    TECHNICAL FIELD The present invention relates to the field of metallurgy recovery technology, in particular, to a process for recovering precious metals from slag from noble metal smelting.
    Background Precious metals possess unique physical and chemical properties, which are widely used in various fields, such as military industry, oil industry, chemical industry, organic synthesis, microelectronics technology, exhaust gas purification or the like, and play an irreplaceable role in modern high-tech industries. If the content of noble metals in the noble metal ore is in the order of grams / ton, the noble metal ore can be classified as a rich maim, and is considered valuable for all industrial exploitation. In certain smelting slag, which is formed during pyrometallurgical processing of noble metals, especially in smelting slag formed during pyrometallurgical processing of copper anode sludge and lead anode sludge, there are plenty of precious metals such as gold, silver, bismuth and lead. Examples include the molten slag, which is formed by pyrometallurgical processing of copper anode sludge and lead anode sludge with Kaldos malt furnace, the components: from 10 to 1000 g Au / h, from 0.05 to 4 (:) / 0 Ag, from 1 to 10% Bi, more than 10% Pb, Than 0 to 1.5% Cu, Than 0 to 4% Sb, and from 0 to 3% As, by weight. The molten slag formed from noble metals in pyrometallurgical processing has a relatively high content of precious metals, and is a good raw material for rich recovery of precious metals such as gold, silver, bismuth, lead or the like, and therefore recovery of slag -Iran noble metal malting is important to solve the problem of serious deficits in precious metal assets.
    Typically, slag returns to the lead nalting system, or copper smelting system, of a smelting plant for further recovery of gold and silver in the processes for treating noble metal smelting slag. However, neither the lead malt system, nor the copper malt system, can achieve a rich recovery of noble metals from slag than noble metal malting. For example, the lead malting system can only recover gold, silver and lead, without effective bismuth extraction, for a long recovery time and to a low recovery rate; while the copper malt system children can recycle gold and silver, but fail to recycle lead and bismuth, which also when returned to the copper malt system will cause a vicious circle due to lead in the large system affecting the copper malt system and copper electrolysis system. In addition, the process time is long and the recovery rate is low. The inventors wish to provide a process for recovering precious metals from slag Than noble metal smelting which richly recovers gold, silver, bismuth and lead from the slag from noble metal smelting with a high degree of recovery.
    Summary In view of this, the problem to be solved by the present invention is to provide a process for recovering precious metals from slag from noble metal malting, which richly recovers gold, silver, bismuth and lead from the slag from noble metal malting with a high degree of recovery.
    To solve the above technical problem, the present invention provides a process for recovering valuable metals from slag noble metal malting comprising the steps of: a) melting the slag from noble metal malting and a flux in a top-blast rotary smelting furnace to form a lead-bismuth alloy. the slag from noble metal malting comprises Au, Ag, Bi and Pb, the flux comprising 1 to 7 parts by weight of coke powder, 1 to 7 parts by weight of sodium carbonate, 0 to 7 parts by weight of quartz sand, 1 to 6 parts by weight of quicklime, 1 to 5 parts by weight of iron powder and 0 to 20 parts by weight of lead oxide, with respect to 100 parts by weight of the slag from noble metal smelting; and b) electrolyzing the resulting lead-bismuth alloy at a current density of Than 60 to 110 Ainn2 to form cathode lead and lead anode, respectively; C) purifying the lead anode sludge to form bismuth and silver-zinc crust, respectively; and d) extracting gold and silver separately from the silver-zinc crust.
    Preferably, the slag Than noble metal molten comprises the following elements in the following quantities thereof: tan 0.01 to 1% by weight of Yan Au; 2,577,159 Than 0.05 to 4% by weight of Ag; tan 1 to 10% by weight of Bi; mer an 10 wt% Pb; Than 0 to 1.5 wt% Cu; tan 0 to 4 wt% Sb; Than 0 to 3 wt% As.
    Preferably, step a) comprises in particular: melting the slag from noble metal malting and the flux in a top-blast rotary smelting furnace to form a lead-bismuth alloy, reducing slag, copper slag, arsenic-antimony slag and smoke dust. The slag from noble metal smelting includes Au, Ag, Bi and Pb. The particle size of the slag from noble metal melting is between 50 and 100 mesh and the melting temperature is between 850 and 1300 ° C. The gold content and the silver content in the reducing slag are regulated to be less than 1 g / h and less than 100 g / h, respectively. The flux comprises 1 to 7 parts by weight of coke powder, 1 to 7 parts by weight of sodium carbonate, 0 to 7 parts by weight of quartz sand, 1 to 6 parts by weight of quicklime, 1 to 5 parts by weight of iron powder and Than 0 to 20 parts by weight of lead oxide, with respect to 100 parts by weight of slag.
    Preferably, step b) comprises in particular: with the lead-bismuth alloy as the anode, a lead cathode plate as the cathode, and a liquid mixture of lead fluorosilicate and fluorosilicic acid as electrolyte, electrolyzing the resulting lead-bismuth alloy at a current density of Than 60 to 110 A / m to form cathode lead and lead anode sludge, respectively.
    Preferably, step c) comprises in particular: letting the lead anode sludge, in succession, be subjected to copper removal treatment, arsenic antimony removal treatment, basic purification, addition of zinc to remove silver and chlorinating purification treatment to form wilt liquor, and added caustic soda and potassium nitrate to to form bismuth and 30 silver-zinc crust.
    Preferably, step d) comprises in particular that: dl) letting the silver-zinc crust be subjected to vacuum distillation treatment and then condensation to form noble metal-rich lead alloy and zinc; blow the noble metal-rich lead alloy with a top-blast rotary narrowing furnace to form gold-silver alloy; and electrolyzing the gold-silver alloy to form gold and silver. Preferably, the vacuum distillation temperature is between 600 and 900 ° C, and the condensation temperature is between 350 and 500 ° C in step dl). Preferably, step d3) comprises in particular: with the gold-silver alloy as the anode, a stainless steel cathode plate as the cathode, and an aqueous solution of silver nitrate and nitric acid as the electrolyte, electrolyzing the gold-silver alloy by feeding direct current (DC) to an electrolytic cell for to form silver and silver anode sludge; the silver anode sludge is subsequently subjected to leaching treatment with a dilute hydrochloric acid, leaching to separate hydrochloric acid and chlorine gas, to form a filtrate; and mixing the filtrate with sodium bisulfite to obtain gold after reaction. Preferably, the zinc obtained in step dl) is used in the purification treatment of lead anode sludge in step c).
    Preferably, the recovery rate is higher than 9 (:) / 0 for gold, higher than 95 15% for silver, higher than 90% for lead, and higher than 90 (:) / 0 for bismuth.
    The present invention provides a process for recovering precious metals from noble metal smelting slag, comprising the steps of: smelting the noble metal smelting slag and a flux in a top-blast rotary smelting furnace to form a lead-viscous alloy, the slag from noble metal smelting, , Bi and Pb; electrolyzing the lead-bismuth alloy at a current density of from 60 to 110 A / m2 to form lead cathode and lead anode, respectively; pure lead anode sludge to form bismuth and zinc-silver crust; and extract gold and silver separately from the ziverzinc crust. In accordance with the state of the art, the present invention enables the precious metals such as gold, silver, bismuth, lead, or the like, to be abundant in lead-bismuth alloy, and that the content of gold, silver, bismuth and lead may be added to the reducing slag. , and damned that the rich recovery rate of gold, silver, bismuth and lead from the slag from noble metal smelting can increase, by using a topblast rotating smelting furnace as a smelting device and adjusting the flux ratio. The experimental results show that the process of the present invention can reach a recovery rate of higher than 9 (:) / 0 for gold, higher than 95 (:) / 0 for silver, higher than 90 (:) / 0 for lead, and higher an 90% f6r bismuth. BRIEF DESCRIPTION OF THE DRAWINGS Figure 1 shows a flow chart for the recovery of precious metals from the slag Than noble metal malt shown in Example 1 of the present invention.
    Detailed Description The technical solutions in the examples of the present invention will be described clearly and in detail below. The described embodiments are only to further illustrate the features and advantages of the present invention, and not to limit the claims of the present invention. All other embodiments conceived by the person skilled in the art, without creative work, and which are based on the embodiments of the present invention, fall within the scope of the invention.
    The present invention provides a process for recovering valuable metals from slag noble metal forming comprising the steps of: a) melting the slag Than noble metal malt and a flux in a topblast rotary smelting furnace to form a lead-bismuth alloy, the slag comprising Than noble metal. Ag, Bi and Pb, and wherein the flux comprises 1 to 7 parts by weight of baking powder, 1 to 7 parts by weight of sodium carbonate, 0 to 7 parts by weight of quartz sand, 1 to 6 parts by weight of quicklime, 1 to 5 parts by weight of iron powder and 0 to 20 parts by weight of lead oxide. 100 parts by weight of slag Than noble metal malting; and b) electrolyzing the lead-bismuth alloy at a current density of Than 60 to 1 A / m 2 to form the lead cathode and lead anode, respectively; c) purifying the lead anode slurry to form bismuth and silver-zinc crust; and d) extracting gold and silver separately from the silver-zinc crust.
    In the above recovery process, the present invention enriches the precious metals gold, silver, bismuth, lead, or the like, in lead-bismuth alloy, and Or the content of gold, silver, bismuth and lead added to the reducing slag, thereby increasing the rich recovery rate. of gold, silver, bismuth and lead from the slag from noble metal smelting by using a top-blast rotary smelting furnace as a smelting device and adjusting the flux ratio.
    The slag from noble metal smelting used in the present invention is preferably a smelting slag formed by pyrone metallurgical processing of copper anode sludge and lead anode sludge which are rich in precious metals such as gold, silver, bismuth, lead, or the like, or more preferably melted. in pyrometallurgical processing of copper anode sludge and lead anode sludge with Kaldos malt furnace. Preferably, the slag from noble metal smelting comprises the following elements in the following amounts thereof: from 0.01 to 1% by weight of Au; Than 0.05 to 4% by weight of Ag; from 1 to 10% by weight of Bi; more than 10% by weight of Pb; Than 0 to 1.5% by weight of Cu; Than 0 to 4% by weight Sb; and Than 0 to 3% by weight of As.
    First, the slag from noble metal smelting is treated with a top-blast rotary smelting furnace to form lead-bismuth alloy. Step a) comprises in particular: melting the slag Than noble metal malting and a flux in a top-blast rotary smelting furnace to form a lead-bismuth alloy, reducing slag, copper choke, arsenic-antimondrous smoker and smoke dust. The slag Than noble metal smelting includes Au, Ag, Bi and Pb. The particle size of the slag from noble metal smelting is between 50 and 100 mesh. The melting temperature is between 850 and 1300 ° C, preferably between 850 and 1100 ° C. The gold content and the silver content in the reducing slag are regulated to be less than 1 g / h and less than 100 g / h, respectively. The flux comprises 1 to 7 parts by weight of baking soda, 1 to 7 parts by weight of sodium carbonate, 0 to 7 parts by weight of quartz sand, 1 to 6 parts by weight of quicklime, 1 to 5 parts by weight of iron powder and 0 to 20 parts by weight of lead oxide, with respect to 100 parts by weight of slag. According to a preferred embodiment, the flux comprises 2 to 6 parts by weight of baking powder, 2 to 6 parts by weight of sodium carbonate, 0 to 5 parts by weight of quartz sand, 2 to 5 parts by weight of quicklime, 2 to 4 parts by weight of iron powder and 2 to 15 parts by weight of lead oxide. By controlling the particle size of the slag from noble metal melting, the present invention guarantees material transfer and saves time and energy for melting the materials. In real time, the flux ratio above and the reaction tin temperature help to ensure an increase in the rich recovery rate and maintaining a low level of gold, silver, bismuth and lead in the slag.
    In the process of melting slag from noble metal smelting to form lead bismuth alloy, it is preferable to introduce natural gas to carry out smelting. Natural gas is a unit in unit consumption of from 80 to 100 Nm3 / ton of slag, which enables low energy consumption. The top-blast rotary kiln used in the present invention is not particularly limited, and the top-blast rotary kiln selected by those skilled in the art can be adapted. In particular, the top-blast rotary kiln is a round kiln with refractory brick lining, which can be rotated about an axis line and also tilted up and down, whereby fuel lance and converting lance can be fed into Than kiln. top. In the smelting process where a top-blast rotary smelting furnace is used, the process smoke is released after it has passed through a water-cooled flue gas duct - high efficiency spray gas purifier - water-electric defroster - air blower - absorption tower, whereby the final dust content in the discharged less smoke is preferred. mg / Nm3f6r to meet the environmental protection requirements. The top blast rotary kiln can also operate continuously and is equipped with an autonomous feed system and DCS control system, which guarantees that the method according to the present invention has properties such as a high degree of automation.
    After obtaining lead-bismuth alloy, it is subjected to electrolysis.
    In particular, step b) comprises: using the lead-visne alloy as the anode, a lead cathode plate as the cathode, and a liquid mixture of lead fluorosilicate and fluorosilicic acid as the electrolyte, electrolyzing the resulting lead viscous alloy at a strand density of from 60 to 110 A / nn 2 to form cathode lead and lead anode sludge, respectively. The current density is preferably between 70 and 100 A / m2, and more preferably between 80 and 100 A / m2. More preferably, the following parannets are regulated in the invention: (1) the lead bismuth alloy prepared in step a) preferably has more than 90% of the sum of lead and bismuth, where the bismuth content is between 8 and 30%, the copper content is less than 0.4 %, and the antinnone content is between 0.5 and 1.5%; (2) the current density of the cathode: 60 - 110 A / m2; (3) unipolar distance: concentric distance is 70 - 100 mm; (4) additives: 13-naphthol and drawstring; (5) fresh solution for circulation: in the fresh acid solution, the concentration of free acid on tan is 200 to 300 g / l and the concentration of lead ions on than is 200 to 300 g / l; and (6) electrolysis products: cathode lead containing 99.94% lead, anode residue (which returns to anode casting) and lead anode sludge.
    Among the electrolysis products, cathode lead has a relatively high content of lead, ie lead recovery is carried out. In addition, the lead anode sludge formed during electrolysis is subjected to purification treatment. Step c) preferably comprises: c1) allowing the lead anode sludge, in succession, to be subjected to copper removal treatment, arsenic antimony removal treatment, basic purification, addition of zinc to remove silver and chlorinating purification treatment to form bismuth liquor, and c2) added caustic soda and potassium nitrate to the bismuth liquor, to form bismuth and silver-zinc crust after reaction. Lead anode sludge has a relatively high content of bismuth, which is also called raw bismuth. Before removing copper, first perform a step of filling and smelting, in particular the lead anode sludge (raw bismuth) is filled into a first purification kettle, and melted at 500 to 600 ° C for 4 hours, and the smelting slag is removed when the temperature rises to 600 ° C.
    According to the present embodiment, in step c): (1) the copper removal treatment comprises in particular that: the property that the solubility of copper in bismuth liquor varies with temperature is utilized in the first refining kettle by, in the first refining kettle, regulating the temperature to 500 ° C so that the copper transferred to a refractory compound or eutectic solid solution in the form of a clean sun can be removed. It medic & that 50 (:) / 0 of the copper can be removed by the above-mentioned smelting. However, since the residual copper content may still be more than 0.3 "Yo, additional sulfur is added during stirring to remove copper. During the addition of sulfur, the temperature is controlled to be from 280 to 3 ° C. By using the property of copper-containing sulphide, which is formed from sulfur and copper, is insoluble in bismuth liquor and has a low density, copper-containing sulphide can be removed, and residual copper can be removed in the subsequent process.Finally, when the temperature rises to 650 ° C, compressed air is biased into to oxidize the remaining sulfur to SO2 gas, thus completing the copper removal process. (2) In the arsenic antimony removal treatment, blowing-oxidation purification is preferably used to remove arsenic and antimony, in particular: arsenic and antimony are removed by oxidation. Due to the large difference between the free enthalpies of the oxides of arsenic and antimony and the free enthalpy lpin for bismuth oxide, compressed air is biased in to preferably oxidize arsenic and antimony to arsenic oxide and antimony oxide while bismuth liquor evaporates when the temperature rises to 680-750 ° C, thereby removing arsenic and antimony. Preferably, the reaction is carried out for 6 hours until the evaporated white smoke becomes thin, and then the foam is removed. If the foam is thin, an appropriate amount of caustic soda or wood waste can be added to dry out the foam, which facilitates removal of the foam.
    The step of basic purification comprises in particular that: Transfer the bismuth liquor to a second purification kettle Than the first purification kettle through a bismuth pump to subject it to a basic purification after the arsenic and antimony removal by oxidation purification; wherein oxides of tellurium and tin react with caustic soda to generate sodium tellurite and sodium selenite with low melting temperatures, which take the form of foam, and thus can be removed in the basic purification. This procedure involves two steps. The first step is telluric removal: when the temperature of the bismuth drops to 500-520 ° C, caustic soda is added several times so that its weight corresponds to a total of 1.5-2 ° A of the weight of the bismuth lye; after melting, compressed air is biased in with stirring to carry out the reaction for 6-10 hours until the foam does not become dry, and at this point the tellurium content has already decreased to about 0.05%. The second step is tin removal: as the temperature of the bismuth liquor drops to 450 ° C, NaOH and NaCl are filled in and melted, with NaOH and NaCl tacking the surface of the bismuth liquor; compressed air is biased into the resulting solution for 20 minutes with stirring, and then NaNO 3 is charged; blowing is continued for another 30 minutes, after which the foam is removed.
    The step of filling zinc to remove silver comprises in particular that: the bismuth liquor is transferred to a third purification kettle from the second purification kettle via a withering nozzle, after basic purification, to subject it to an addition of zinc to remove silver. The process is carried out at a low temperature of 420-500 ° C. Addition of zinc to remove silver is based on the fact that the stable refractory compound sun can be removed as skunn, due to low density, formed by reaction between zinc and silver. The degree of silver removal has a great influence on the quality of the purified wilt and the degree of recovery. The process is terminated when the bismuth liquor contains less than 0.003% silver. The resulting gold-silver-zinc crust returns to the Kaldosmalt oven for further treatment. (5) The chlorinating purification treatment comprises in particular that the bismuth liquor is transferred to a fourth purification kettle Than the third purification kettle via a bismuth pump, after the addition of zinc to remove silver. The chlorine gas is forced into the fourth purification kettle through a glass tube inserted in the bismuth liquor. Chlorine can react with the lead in the bismuth to form PbCl2, which has a density of 2.91 g3m3 and is lower than that of the bismuth, which is 10 g / cm3; thus, PbCl2 can be removed as an off-white foam.
    After the above steps (1) to (5) are completed, caustic soda and potassium nitrate are added to the bismuth liquor.
    In particular, after the chlorinating purification, the bismuth liquor is transferred to a fifth purification kettle Than the fourth purification kettle via a bismuth pump. Caustic soda and potassium nitrate were added to remove minor amounts of Cl, Zn, As, Sb, Pb and Te. Finally, bismuth liquor is obtained with 99.99% purity and cast into ingots, whereby bismuth extraction is carried out.
    According to the present invention, step d) comprises in particular: dl) subjecting the silver-zinc crust prepared in the preceding step to vacuum distillation treatment to form noble metal-rich lead alloy and zinc after condensation; d2) blowing the noble metal-rich alloy with a top-blast rotary narrowing furnace to form a gold-silver alloy; and d3) electrolyzing the gold-silver alloy to form gold and silver; wherein the tin temperature for the vacuum distillation is between 600 and 900 ° C, and the condensation temperature is between 350 and 500 ° C in step dl).
    The purpose of converting the lead alloy in step d2) is to obtain a gold-silver alloy having a purity higher than 98 (Y0, and thus meet the requirement for silver electrolysis technology. Step d3) includes in particular that with the gold-silver alloy as an anode, a stainless steel cathode plate which cathode, the aqueous solution of silver nitrate and nitric acid as electrolyte, electrolyzing the gold-silver alloy by feeding direct current (DC) through an electrolytic cell to form silver and silver anode sludge; The lazy silver anode solution, at -160, is subjected to leaching treatment with dilute hydrochloric acid, leaching treatment with hydrochloric acid and chlorine gas to form a filtrate, and mixing the filtrate with sodium bisulfite to obtain gold sand after reaction. Preferably, the golden sand is cast into gold bars.
    In a preferred embodiment, it also comprises that the zinc formed in step d1) is used for purification treatment of lead anode sludge in step c). and thus zinc recovery is carried out. As can be seen in the above embodiment, the present invention enriches valuable metals such as gold, silver, bismuth, lead, or the like, in a lead-bismuth alloy, and makes the content of gold, silver, bismuth and lead added to the reducing slag. and thereby increases the rich recovery rate of gold, silver, bismuth and lead in the slag tan noble metal malting by using a top-blast rotary smelting furnace as a smelting device and adjusting the flux ratio. The experimental results show that the process of the present invention can reach a recovery rate of higher than 95% for gold, higher than 95 (:) / 0 for silver, higher than 90 (:) / 0 for lead, and higher than 90 (: ) / 0 for bismuth.
    To further illustrate the technical solutions of the present invention, preferred embodiments of the invention will be described in connection with the examples below. However, these descriptions are merely to illustrate the features and advantages of the invention, rather than to limit the appended claims. Example 53 Example 1 Figure 1 shows a flow chart of the process for recovering valuable metals from slag from noble metal smelting according to an embodiment of the present invention.
    Table 1. The raw materials and their contents in the slag from precious metal smelting in Example 1.
    Amne Au Ag Bi Pb Cu Sb As 5i02 Content 500 g / h 1% 6.4 (:) / 0 45% 0.3% 1 (:) / 0 1% 10% Lead-bismuth alloy formed from slag from noble metal smelting Nagra the substances and contents thereof in slag Than noble metal malt used in Example 1 are shown in Table 1. The slag from noble metal malt is ground to 100 mesh via two-step crushing, and then the mama slag Than noble metal malt is fed to an upper container of a topblast rotary smelting furnace by means of pne transport. Materials inside the Upper Container, such as slag from noble metal smelting and a flux such as quartz, sodium carbonate, quicklime, coke powder, and lead oxide, are automatically fed into the top-blast rotary smelting furnace through a mechanical feed system. The reducing melting is carried out at 850-1300 ° C by inserting a combustion lance. After the melting is completed, the slag is discharged, hot lead-bismuth alloy is formed and kept in a lead bismuth alloy purification furnace to remove copper, and after removal of As and Sb, a purified lead-bismuth alloy fluid is obtained, which can then be cast into a lead-bismuth alloy anode plate. an anode casting machine.
    The flux comprises: 7% coke powder, 7% sodium carbonate, 6 (:) / 0 quicklime, 3% iron powder, 0 (:) / 0 lead oxide, and 0 (:) / 0 quartz sand (with respect to the mass of the slag Than noble metal malt) .
    Main smelting products: lead-bismuth alloy, reducing slag, copper choke, arsenic-antimondrode and smoke dust. The reducing slag contains 0.95 g gold / h and 80 g silver / h, and has a unit consumption of natural gas of 80 Nm3 / h slag. The resulting lead-bismuth alloy contains more than 90.94 `) / 0 of the sum of Pb and Bi. 12 537 159 The exhaust gas is emitted after passing through a water - cooled flue gas duct - high efficiency spray gas purifier - water electric defroster - air blower - absorption tower, and the final dust content of the discharged exhaust gas is less than 2 mg / Nm3.
    Electrolysis purification of the lead-bismuth alloy The electrolysis was performed using the lead-bismuth alloy son anode, a lead cathode plate as cathode, a liquid mixture of lead fluorosilicate and fluorosilicic acid as electrolyte, and feeding direct current (DC) to an electrolytic cell. (1) Composition of the lead-bismuth alloy Table 2. The composition of the lead-bismuth alloy obtained in Example 1.
    Pb Bi Cu As Sb Sn Au Ag 79.6% 11.38% 0.2% 0.24% 1.07% 0.26% 930 g / h 1.8% Cathode current density The current density is low, namely, 80 A / m2.
    Distance between the cobblestones 15 90 mm.
    Additives p-naphthol.
    Fresh solution for circulation In the fresh acid solution, the concentration of free acid is 300 g / I and the concentration of lead ions is 300 g / I.
    Electrolysis products Cathode lead containing 99.94% lead, anode residue (which returns to anode casting) and lead anode sludge.
    Lead anode sludge treatment The lead anode sludge formed by electrolysis of lead-bismuth alloy is dried, and the dried lead anode sludge is fed into an electric smelting furnace for smelting, copper removal, arsenic-antinnone removal, basic purification, addition of zinc for silver removal, chlorination and chlorination. purified bismuth and silver-zinc crust. (1) Feeding and melting 13 537 159 The raw bismuth is fed into a first purification kettle, and melted at 500 to 600 ° C for 4 hours, and the melting slag is emptied when the temperature rises to 600 ° C.
    Copper removal process By utilizing the property that the solubility of copper in bismuth liquor varies with temperature, the temperature in the first purification kettle is regulated to be 500 ° C so that the copper is converted into a refractory compound or a eutectic solid solution in the form of foam, which is then removed. Thus, 50 (:) / 0 of the cup can be removed by the melting above. However, since the residual copper content is still higher than 0.3%, sulfur is also added with stirring to remove copper. During the addition of sulfur, the temperature is regulated to 300 ° C. By utilizing the property that copper-containing sulphide formed from sulfur and copper is insoluble in bismuth liquor and has a low density, copper-containing sulphide is removed, and residual copper is removed in the following process. Finally, when the temperature rises to 650 ° C, compressed air is biased in to oxidize residual sulfur to SO 2 gas. Damned, the copper removal procedure is completed.
    Arsenic and antimony removal by blowing-oxidation purification In the first purification kettle, arsenic and antimony are removed by oxidation purification. Due to the large differences in free enthalpy of arsenic and antimony oxides and bismuth oxide free enthalpy, compressed air is biased in when the temperature rises to 680-750 ° C, to preferentially oxidize arsenic and antimony to arsenic oxide and antimony oxide while evaporating bismuth oxide. , and thus arsenic and antimony are removed. Preferably, the reaction is carried out for 6 hours until the evaporated white smoke becomes thin, after which the foam is removed. If the foam is thin, an appropriate amount of caustic soda or wood waste can be added to dry out the foam, which will facilitate the removal of the foam.
    Basic purification The bismuth liquor is transferred to a second purification kettle from the first purification kettle through a bismuth punch, after arsenic and antimony removal by oxidation purification, to subject it to alkaline purification; wherein oxides of tellurium and tin react with solid caustic soda in the basic purification to form sodium tellurite and sodium selenite with low melting points, in that tellurium oxide and tin oxide react with solid caustic soda, which take the form of foam, and thus can be removed. This procedure involves two steps. The first step is 14 537 159 tellurium removal: when the temperature of the bismuth liquor drops to 500-520 ° C, solid caustic soda is added several times so that its weight corresponds to a total of 1.5-2% of the weight of the bismuth liquor; after cooling, compressed air is biased in with stirring to carry out the reaction for 6-10 hours until the foam no longer dries, and at this point the tellurium content has already decreased to about 0.05%. The second step is tin removal: as the temperature of the bismuth liquor drops to 450 ° C, NaOH and NaCl are added and melted, which thank the surface of the bismuth liquor; whereby compressed air is biased into the resulting solution for 20 minutes with stirring, and then NaNO 3 is added; the blowing continues for another 30 minutes, after which the foam is removed.
    Addition of zinc for silver removal The bismuth leaches a third cleaning kettle from the second cleaning kettle via a bismuth pump, after basic purification, to expose it to the step of adding zinc for silver removal. The process is carried out at a low temperature of 450 ° C. Addition of zinc for silver removal is based on the fact that the stable refractory compound, sun can be removed sun due to low density, formed by reaction between zinc and silver. The degree of silver removal has a great influence on the quality of the purified bismuth and the degree of recovery. The preform is terminated when the bismuth liquor contains less than 0.003 (:) / 0 silver. The resulting gold-silver-zinc crust returns to the Kaldosmalt furnace for further treatment.
    Chlorinating purification The bismuth is transferred to a fourth purification kettle from the third purification kettle via a bismuth pump, after the addition of zinc for silver removal. The chlorine gas is forced into the fourth purification kettle through a glassy tube inserted into the bismuth liquor. Chlorine can react with lead in the bismuth to form PbCl2, which has a density of 2.91 g / cm3 and store the same for the bismuth, i.e. 10 gicm3; thus, PbCl2 can be removed as an off-white skin.
    Final purification The bismuth is transferred to a fifth purification kettle from the fourth purification kettle via a bismuth pump, after the chlorinating purification. Caustic soda and potassium nitrate were added to remove minor amounts of Cl, Zn, As, Sb, Pb and Te. Finally, bismuth liquor is obtained with 99.99% purity and then cast into ingots, whereby the bismuth extraction is carried out. 537 159 Processing of gold-silver-zinc crust Table 3. Some substances and their contents in the gold-silver-zinc crust obtained in Example 1.
    Pb Bi Cu As Sb Zn Au Ag 2.2% 10.3 (:) / 0 0.39 (:) / 0 0.47 (1/0 0.56% 53.4 (:) / 0 1.2 % 19.8 (:) / 0 After liquid bismuth is pressed out via a press, the gold-silver-zinc crust is transferred to a vacuum distillation smelting furnace for zinc removal, under the conditions with a negative pressure of 2 kPa, a distillation smelting furnace temperature of 800 ° C and a condenser temperature of 480 ° C, a noble metal-rich lead alloy and zinc and blue powder are formed with a purity of 98.4%, and the zinc and blue powder return to the process where zinc has been added to remove silver in the lead anode sludge treatment.
    After the noble metal-rich lead alloy is blasted via the top-blasted rotary smelting furnace, a gold-silver alloy is formed with a sum of gold and silver of more than 98%. The electrolysis is carried out with the gold-silver alloy as the anode, a stainless steel cathode plate as the cathode, an aqueous solution of silver nitrate and nitric acid as the electrolyte, and the supply of direct current (DC) to an electrolytic cell. The electrolysis treatment forms silver cathode, residual anode and silver anode sludge. 99.99 (:) / 0 (purity) of the silver ingots is obtained by casting the silver cathode.
    Silver anode sludge has been subjected to lacquer treatment with dilute hydrochloric acid solution to remove most of the contaminants. Then hydrochloric acid and chlorine gas are used to leach out and dissolve the anode lime, and then only the formed silver chloride and some insoluble pollutants fall out. Sodium bisulfite is then used to precipitate gold from the filtrate. The precipitated gold sand is filtered, washed and dried to form gold sand with 99.99% (purity), whereby 99.99 .mu.l / 0 (purity) of the gold bars are obtained by casting the gold sand.
    Recovery rates of precious metals and associated parameters in this example are shown in Table 4. 16 537 159 Table 4. Recovery radar of precious metals and performance parameters Example 1.
    Number Item Unit Result 1 Recycling rate of lead% 90 2 Recycling rate of bismuth% 90 3 Recycling rate of gold% 9 4 Recycling rate of silver% 9 Lead in slag% <3 6 Bismuth in slag% <0.1 7 Silver in slag g / h <100 8 Gold in slag g / h <1 9 Unit consumption of natural gas Nm3 / h 80-100 Unit consumption of zinc Kg / h bismuth <11 Dust in emitted smoke mg / Nm3 <2 Example 2 Table 5. Na ra substances and their contents in slag from precious metal smelting in Example 2.
    Amne Au Ag Bi Pb Cu Sb As Si02 Content 100 g / h 0.4% 8% (1/0 0.3% 1.2% 1.8% 5% Lead-bismuth alloy formed from slag from noble metal malting Slag from noble metal malting is ground to 70 mesh via two-step crushing, and then the ground slag from noble metal malt is passed to an upper container of a top-blast rotary steel furnace as by pneumatic transport.The material inside the upper container, such as slag from noble metal malt and flux such as carbonaceous quartz, sodium sulphate, quartz , and lead oxide, are automatically fed into the top-blast rotary smelting furnace, on the basis of a feed ratio, through a mechanical feed system.The reducing smelting is carried out at 850-1100 ° C by inserting a combustion lance. is finished, the slag is removed, and hot raw lead-bismuth alloy is formed, then the raw lead-bismuth alloy is kept in a lead-bismuth alloy purification furnace to remove copper, and after removal of As and Sb, a purified lead-bismuth alloy fluid is obtained, which is then cast into a lead-bismuth alloy anode plate in an anode casting machine.
    The flux comprises: 17,537,159 4% coke powder, 2% sodium carbonate, 7% quicklime, 3% iron powder, 10% lead oxide, and 0% quartz sand (with respect to the pulp, the slag is from noble metal malting).
    Main smalt products are: lead-bismuth alloy, reducing slag, copper choke, arsenic-antimondrode and smoke and dust. The reducing slag contains 0.6 g gold / h and 98 g silver / h, with a unit consumption of natural gas of 80 Nm3 / h slag. The resulting lead bismuth alloy contains more than 90.94% of the sum of Pb and Bi. The smoke is released after it has passed through a water-cooled flue gas duct - high-efficiency spray gas purifier - water-electric defroster - air blower - absorption tower, and the final dust content in the emitted smoke is less than 2 ring / Nm3.
    Electrolysis purification of the lead-bismuth alloy The electrolysis is accomplished by using the lead-bismuth alloy as the anode, a lead cathode plate son cathode, a liquid mixture of lead fluorosilicate and fluorosilicic acid as the electrolyte, and feeding direct current (DC) to an electrolytic cell. (1) Composition of the lead-bismuth alloy Table 6. The composition of the lead-bismuth alloy obtained in Example 2.
    Pb Bi Cu As Sb Sn Au Ag 76.5% 16% 0.3% 0, 32% 1.3% 0.35% 198 g / h 0.8% (2) Cathode current density The current density is low, namely, 60 A / m2.
    Distance between the cobblestones 90 mm.
    Additives 25 Draglinn.
    Fresh solution for circulation In the fresh acid solution, the concentration of free acid is 300 g / I and the concentration of lead ions is 300 g / I.
    Electrolysis products Cathode lead containing 99.94% lead, anode residue (which returns to anode casting) and lead anode sludge. 18 537 159 Lead anode sludge treatment The lead anode sludge formed by electrolysis of lead-bismuth alloy is dried, and the dried lead anode sludge is fed into an electric smelting furnace for smelting, copper removal, arsenic-antimony removal, basic purification, addition of zinc, silver purification and silver purification. to produce purified bismuth and silver-zinc crust.
    Feeding and melting The raw bismuth is fed into a first purification kettle, and melted at 500 to 600 ° C for 5 hours, and the melting slag is removed when the temperature rises to 600 ° C.
    Copper removal process By utilizing the property that the solubility of copper in bismuth liquor varies with temperature, the temperature in the first purification kettle is regulated to be 500 ° C so that the copper is converted into a refractory compound or a eutectic solid solution in the form of foam, which is consequently removed. Thus, 50% of the copper can be removed through the melt above. However, sulfur was also added with stirring to remove copper since the residual copper content is still higher than 0.3%. During the addition of sulfur, the temperature is regulated to 280-330 ° C. Through the use of the property that copper-containing sulphide, which is formed from sulfur and copper, is insoluble in bismuth liquor and has a low density, copper-containing sulphide is removed and residual copper is removed in the following process. Finally, when the temperature rises to 650 ° C, compressed air is biased in to oxidize residual sulfur to SO 2 gas. This completes the copper removal process. (3) Arsenic and antinone removal by blowing-oxidation purification In the first purification kettle, arsenic and antimony are removed by oxidation purification. Due to the large differences in free enthalpy of arsenic and antimony oxides and free enthalpy of viscous nut oxide, compressed air is biased in when the temperature rises to 680-750 ° C, to preferentially oxidize arsenic and antimony to arsenic oxide and antimony oxide while evaporating bismuth liquor. , and damned arsenic and antimony are removed. Preferably, the reaction is carried out for 6 hours until the evaporated white smoke becomes thin, after which the foam is removed. If the foam is thin, an appropriate amount of caustic soda or wood waste can be added to dry out the foam, which will facilitate the removal of the foam. (4) Basic purification 19 537 159 The bismuth liquor is transferred to a second purification cauldron from the first purification cauldron by means of a bismuth pump, after removal of arsenic and antimony by oxidative purification, to subject it to alkaline purification; wherein oxides of tellurium and tin react with solid caustic soda, in the basic purification, to form sodium tellurite and sodium selenite with low melting points, which take the form of foam, and thus can be removed. This procedure involves two steps. The first step is tellurium removal: when the temperature of the bismuth liquor drops to 500-520 ° C, solid caustic soda is added several times so that its weight corresponds to a total of 1.5-2 (:) / 0 of the weight of the bismuth liquor; after melting, compressed air is biased in with stirring to carry out the reaction for 7 hours until the foam no longer dries, and at this point the tellurium content has already decreased to about 0.05%. The second step is tin removal: as the temperature of the bismuth liquor drops to 450 ° C, NaOH and NaCl are added and melted, which thank the surface of the bismuth liquor; compressed lufit is biased into the resulting solution for 15-20 minutes with stirring, and then NaNO 3 is added; the blowing continues for another 30 minutes, after which the foam is removed.
    Addition of zinc for silver removal The bismuth is transferred to a third purification kettle from the second purification kettle through a wilt nozzle pump, after basic purification, to subject it to the step of adding zinc for silver removal. The process is carried out at a low temperature of 420-500 ° C. Addition of zinc for silver removal is based on the fact that a stable refractory compound is formed by reaction between zinc and silver and that the stable refractory compound can be removed as a foam due to low density. The degree of silver removal has a great influence on the quality of the purified bismuth and the degree of recovery. The preform is terminated when the bismuth liquor contains less than 0.003% silver. The resulting gold-silver-zinc crust returns to the Kaldosnnal kiln for further treatment.
    Chlorinated purification The bismuth liquor is transferred to a fourth purification kettle -Iran the third purification kettle through a bismuth punch, after adding zinc for silver removal. The chlorine gas is introduced into the fourth purification kettle via a glass tube which is inserted into the bismuth liquor. Chlorine can react with lead in the bismuth to form PbCl2, which has a density of 2.91 gicm3 and is lower than that of the bismuth, i.e. 10 g / cm 3; thus, PbCl2 can be removed as an off-white foam.
    Final purification 537 159 The bismuth is transferred to a fifth purification kettle from the fourth purification kettle through a bismuth pump, after the chlorinating purification. Caustic soda and potassium nitrate were added to remove minor amounts of Cl, Zn, As, Sb, Pb and Te. Finally, bismuth liquor is obtained with 99.99 (:) / 0 purity and then cast into ingots, whereby the bismuth extraction is carried out.
    Processing of gold-silver-zinc crust Table 7. Some substances and their contents in the gold-silver-zinc crust obtained in Example 2.
    Pb Bi Cu As Sb Zn Au Ag 2.67% 10.0% 0.67% 0.32% 0.53% 45.87% 1.16% 23.25% After liquid bismuth is squeezed out via a presser transferred the gold-silver zinc crust for a vacuum distillation smelting furnace for zinc removal. Under the conditions with a negative pressure of 1.5 kPa, a distillation molten kiln temperature of 780 ° C and a condenser temperature of 480 ° C, noble metal-rich lead alloy and blue powder and zinc with a purity of 98.3% are formed. The zinc and the blue powder return to the process where zinc has been added to remove silver in the lead anode sludge treatment.
    After the noble metal-rich lead alloy is biased via the top-blasted rotary smelting furnace, a gold-silver alloy is formed with a sum of gold and silver of more than 98%. The electrolysis is carried out with the gold-silver alloy as the anode, a stainless steel cathode plate as the cathode, an aqueous solution of silver nitrate and nitric acid as the electrolyte, and the supply of direct current (DC) to an electrolytic cell. The electrolysis treatment forms silver cathode, residual anode and silver anode sludge. 99.99 (10-inch silver ingots are obtained by casting the silver cathode.
    Silver anode sludge has been subjected to lacquer treatment with dilute hydrochloric acid solution to remove most of the contaminants. Then hydrochloric acid and chlorine gas are used to leach out and dissolve the anode lime, and only the silver chloride formed and some insoluble impurities fall out. Sodium bisulfite is then used to precipitate gold from the filtrate. The precipitated gold sand is filtered, washed and dried to form 99.99% gold sand, whereby 99.99 (:) 0-ounces of gold ingots are obtained by casting the gold sand. 21 537 159 Example 3 Table 8. The raw materials and their contents in slag from precious metal smelting in Example 3.
    Amne Au Ag Bi Pb Cu Sb As Na2CO2 Content 20 g / h 0.2% 3% 10% 0.01% 1.6 `) / 0 1.5% 5% Lead-bismuth alloy formed from slag from noble metal melting Slag from noble metal malt is ground to 50 mesh via two-stage crushing, and then the ground slag is passed from noble metal malt to an upper container of a top-blast rotary steel furnace as by pneumatic transport. The material inside the upper container, such as slag from precious metal malting and fluxes such as quartz, sodium carbonate, quicklime, coke powder, and lead oxide, is automatically fed into the top-blast rotary smelting furnace, on the basis of a feed ratio, through a mechanical feed system. The reducing melting is performed at 850-1100 ° C by inserting a combustion gun. After the melting is completed, the slag is removed, forming hot lead-bismuth alloy. Thereafter, the hot raw lead-bismuth alloy is kept in a lead-bismuth alloy purification furnace to remove copper 1, As and Sb, and to obtain a purified lead-bismuth alloy liquid, which is then cast into a lead-bismuth alloy anode plate in an anode casting machine.
    The flux comprises: 6% coke powder, 1% sodium carbonate, 1 (:) / 0 quicklime, 3% iron powder,% lead oxide, and 7 (:) / 0 quartz sand (with respect to the mass of the slag from noble metal malting).
    The main narrow products are: lead-bismuth alloy, reducing slag, copper choke, arsenic-antimony saffron and smoke dust. The reducing slag contains 0.3 g gold It and 98 g silver It, with a unit consumption of natural gas of 96 Nm3 / h slag. The resulting lead-bismuth alloy contains more than 92.05% of the sum of Pb and Bi.
    The smoke is released after it has passed through a water - cooled flue gas duct - high efficiency spray gas purifier - water electric defroster 30 - air blower - absorption tower, and the final dust content of the emitted smoke is less than 2 nng / Nnn3. Electrolysis purification of the lead-bismuth alloy The electrolysis is accomplished by using the lead-bismuth alloy as the anode, a lead cathode plate as the cathode, a liquid mixture of lead fluorosilicate and fluorosilicic acid as the electrolyte, and feeding DC (DC) to an electrolysis cell. (1) Composition of the lead-bismuth alloy Table 9. The composition of the lead-bismuth alloy is obtained in Example 3.
    Pb Bi Cu As Sb Sn Au Ag 82.6% 9.45% 0.1 (:) / 0 0.52% 1.2% 0.25% 63 g / h 0.63% Cathode current density Current density is low, namely, 110 A / m2.
    Distance between the cobblestones 10 90 mm.
    Additives 8-naphthol.
    Fresh solution for circulation In the fresh acid solution, the concentration of free acid is 300 g / I and the concentration of lead ions is 300 g / I.
    Electrolysis products Cathode lead containing 99.97 (:) / 0 lead, anode residue (which returns to anode casting) and lead anode sludge.
    Lead anode sludge treatment The lead anode sludge formed by electrolysis of lead-bismuth alloy is dried, and the dried lead anode sludge is fed into an electric smelting furnace for smelting, copper removal, arsenic-antimony removal, basic purification, addition of zinc for final silver removal, silver removal. purified bismuth and silver-zinc crust. (1) Feeding and melting The raw bismuth is fed into a first purification kettle, and melted at 500 to 600 ° C for 4-6 hours, and the slag slag is removed when the temperature rises to 600 ° C. (2) Copper removal process By utilizing the property that the solubility of copper in welded liquor varies with temperature, the temperature in the first purification kettle is regulated to be 500 ° C so that the copper is converted into a refractory compound or a eutectic solid solution in the form of foam. , which is then removed. Thus, (:) / 0 of the cup can be removed by the melting above. However, in addition, sulfur was added with stirring to remove copper, since the residual copper content is still higher than 0.3%. During the addition of sulfur, the temperature is regulated to 280-330 ° C. By utilizing the property that copper-containing sulphide, which is formed from sulfur and copper, is insoluble in bismuth liquor and has a low density, copper-containing sulphide is removed and residual copper is removed in the following procedure. Finally, when the temperature rises to 650 ° C, compressed air is biased in to oxidize residual sulfur to SO 2 gas. This completes the copper removal process.
    Arsenic and antimony removal by blowing-oxidation purification In the first purification kettle, arsenic and antimony are removed by oxidation purification. Due to the large differences in free enthalpy of the oxides of arsenic and antimony and free enthalpy of bismuth oxide, compressed air is biased in when the temperature rises to 680-750 ° C, to preferentially oxidize arsenic and antimony to arsenic oxide and antinone oxide. , and thus the arsenic and antimony are removed. Preferably, the reaction is carried out for 4-10 hours until the evaporated white smoke becomes thin, after which the foam is removed. If the foam is thin, a caustic soda or wood waste can be added to dry out the foam, which will facilitate the removal of the foam.
    Basic purification The bismuth liquor is transferred to a second purification cauldron from the first purification cauldron, after arsenic and antimony removal by oxidation purification, through a bismuth pump to subject it to alkaline purification; wherein oxides of tellurium and tin react with solid caustic soda to form sodium tellurite and sodium selenite with low melting points, which take the form of foam, and thus can be removed. This procedure involves two steps. The first step is tellurium removal: when the temperature of the bismuth liquor drops to 500-520 ° C, solid caustic soda is added several times so that its weight corresponds to a total of 1.5-2% of the weight of the bismuth liquor; after cooling, compressed air is biased in with stirring to carry out the reaction for 6-10 hours until the foam no longer dries, and at this point the tellurium content has already decreased to about 0.05%. The second step is tin removal: when the temperature of the bismuth leach decreases to 450 ° C, NaOH and NaCl are added and melted, and tack the surface of the bismuth lye; whereby compressed air is biased into the solution formed for 20 minutes with stirring, and then NaNO 3 is added; the blowing continues for another 30 minutes, after which the foam is removed. (5) Addition of zinc for silver removal The bismuth is transferred to a third purification kettle from the second purification kettle through a bismuth pump, after basic purification, to subject it to the step of adding zinc for silver removal. The process is carried out at a low temperature of 420-500 ° C. Addition of zinc for silver removal is based on the fact that a stable refractory compound is formed by reaction between zinc and silver, and can be removed as foam due to low density. The degree of silver removal has a great influence on the quality of the purified bismuth and the degree of recovery. The preform is terminated when the bismuth liquor contains less than 0.003 (:) / 0 silver. The resulting gold-silver-zinc crust returns to the Kaldosmalt furnace for further treatment. (6) Chlorinated purification The bismuth liquor is transferred to a fourth purification cauldron from the third purification cauldron through a bismuth pump, after the addition of zinc for silver removal. The chlorine gas is introduced into the fourth purification kettle through a glass tube inserted into the bismuth liquor. Chlorine can react with lead in the bismuth to form PbCl2, which has a density of 2.91 g / cm3 and stores the same for the bismuth, i.e. 10 g / cm 3; thus, PbCl2 can be removed as an off-white foam. (7) Final purification The bismuth liquor is transferred to a fifth purification cauldron from the fourth purification cauldron through a bismuth pump, after the chlorinating purification. Caustic soda and potassium nitrate were added to remove minor amounts of Cl, Zn, As, Sb, Pb and Te. Finally, bismuth liquor is obtained with 99.99% purity and then cast into ingots, whereby the bismuth extraction is carried out.
    Processing of gold-silver-zinc crust Table 10. Nagra hearth and its contents in the gold-silver-zinc crust obtained in Exennpel 3.
    Pb Bi Cu As Sb Zn Au Ag 2, (:) / 0 8.9 (:) / 0 0.58 (:) / 0 0.32 (:) / 0 0.38 (:) / 0 42.1 % 0.62% 27, (:) / 0 537 159 After liquid bismuth is pressed out via a press, the gold-silver-zinc crust is transferred to a vacuum distillation melting furnace for zinc removal. Under the conditions with a negative pressure of 1.2 kPa, a distillation molten kiln temperature of 700 ° C and a condenser temperature of 450 ° C, noble metal-rich lead alloy and blue powder and zinc with a purity of 98.2% are formed. The zinc and the blue powder return to the process where zinc has been added to remove silver in the lead anode sludge treatment. After the noble metal-rich lead alloy is biased via the top-blasted rotary smelting furnace, a gold-silver alloy is formed with a sum of gold 10 and silver of more than 98%. The electrolysis is carried out with the gold-silver alloy as the anode, a stainless steel cathode plate as the cathode, an aqueous solution of silver nitrate and nitric acid as the electrolyte, and the supply of direct current (DC) to an electrolytic cell. The electrolysis treatment forms silver cathode, residual anode and silver anode sludge. 99.99% silver ingots are obtained by silver cathode casting.
    The silver anode sludge has been subjected to leaching treatment with dilute hydrochloric acid solution to remove the next of the contaminants. Then hydrochloric acid and chlorine gas are used to leach out and dissolve the anode lime, and only the silver chloride formed and some insoluble impurities fall out. Then sodium bisulfite is used to precipitate the gold tan filtrate. The precipitated gold sand is filtered, washed and dried to form 99.99 (:) 0-g gold sand, whereby 99.99 (:) 0-g gold bars are obtained by casting the gold sand.
    The above description with respect to the illustrated examples provides insight into, and application of, the present invention to those skilled in the art. It will be apparent to those skilled in the art to make various modifications of these embodiments in accordance with the general principles defined herein, without departing from the spirit and scope of the present invention. Therefore, the invention should not be limited to the examples herein, but should have the broadest scope in accordance with the principles and novel features set forth by this invention. 26
    权利要求:
    Claims (10)
    [1]
    A process for recovering precious metals from slag Than noble metal malting comprising the steps of: a) melting the slag from noble metal malting and a flux in a topblast rotating smelting furnace to form a lead-bismuth alloy, the slag Than noble metal malting comprising Au, Ag, Bi and Pb , and the flux comprises 1 to 7 parts by weight of coke powder, 1 to 7 parts by weight of sodium carbonate, 0 to 7 parts by weight of quartz sand, 1 to 6 parts by weight of quicklime, 1 to 5 parts by weight of iron powder and 0 to 20 parts by weight of lead oxide per 100 parts by weight of slag. b) electrolyzing the lead-bismuth alloy at a current density of from 60 to 110 A / m2 to form lead cathode and lead anode; C) pure lead anode sludge to form bismuth and silver-zinc crust; and d) extracting gold and silver Than silver-zinc crust.
    [2]
    Process according to claim 1, characterized in that the slag Than noble metal melting comprises: Than 0.01 to 1% by weight of Au; Than 0.05 to 4% by weight of Ag; from 1 to 10% by weight of Bi; less than 10% by weight of Pb; Than 0 to 1.5% by weight of Cu; from 0 to 4% by weight of Sb; and Than 0 to 3% by weight of As.
    [3]
    Process according to claim 1, characterized in that the slag from noble metal melting, reaches a particle size of between 50 and 100 mesh, and the flux is melted at a temperature of between 850 and 1300 ° C, in step a) to form lead. bismuth alloy, reducing stroke, copper choke, arsenic antimonde choke and smoke dust, the content of gold and silver in the reducing slag being regulated to be lower than 1 g gold / t and 100 g silver / t, respectively. 27,537,159
    [4]
    4. A process according to claim 1, characterized in that, in step b), the lead-bismuth alloy is used as the anode, a lead cathode plate as the cathode, and a liquid mixture of lead fluorosilicate and fluorosilicic acid as the electrolyte.
    [5]
    Process according to claim 1, characterized in that, in step c), bismuth liquor is formed in lead anode sludge, in succession, subjected to copper removal treatment, arsenic antimony removal treatment, basic purification, silver removal by zinc addition, and chlorinating purification treatment; and caustic soda and potassium nitrate were added to the bismuth liquor to form bismuth and silver-zinc crust after reaction.
    [6]
    A process according to claim 1, characterized in that step d) comprises dl) subjecting the silver-zinc crust to vacuum distillation treatment to form noble metallic lead alloy and zinc after condensation; d2) blowing the noble metal-rich lead alloy into the top-blasted rotary smelting furnace to form gold-silver alloy; and d3) electrolyzing the gold-silver alloy to form gold and silver.
    [7]
    Process according to Claim 6, characterized in that the vacuum distillation is carried out at a temperature of between 600 and 900 ° C, and that the condensation is carried out at a temperature of between 350 and 500 ° C, in step dl).
    [8]
    A method according to claim 6, characterized in that step d3) comprises: with the gold-silver alloy as an anode, with a stainless steel cathode plate as cathode and with an aqueous solution of silver nitrate and nitric acid as electrolyte, electrolyzing the gold-silver alloy by applying direct current (DC) to an electrolytic cell to form silver and silver anode sludge; exposed silver anode sludge, in succession, for leaching with dilute hydrochloric acid, and leaching with hydrochloric acid and chlorine gas, to form filtrate; and mixing the filtrate with sodium bisulfite to form gold after reaction
    [9]
    The method of claim 6, further comprising: using the zinc obtained in step d1) for the purification treatment of lead anode sludge in step c).
    [10]
    A method according to claim 1, characterized in that more than 95% gold, more than 9 (:) / 0 silver, more than 90 (:) / 0 lead and more than 90% bismuth are recovered. 29 537 159 slag from noble malt crushing and low-temperature vacuum distillation grinding blue powder enriched zinc (as filling (as atergarblyatergs for admixture cleaning) reducing smelting with top blast bismuth purging (blast furnace blasting with top blast ) the alloy reducing electrolysis of the gold-silver alloy slag) anode residue (which returns to lead-bismuth-alloy purification) precipitation of casting lead-purification of bismuth • ingots purified bismuth gold-silver-purification lead-bismuth-alloy anode electrolysis of lead-bismuth alloy • lead anode residue which leads to anode casting) lead anode sludge electrolytic silver casting silver ingots silver anode sludge gold ingots gold recovery gold zinc crust
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    同族专利:
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    CN102703719A|2012-10-03|
    SE1251476A1|2014-01-04|
    CA2798302C|2015-10-06|
    US20140008238A1|2014-01-09|
    CN102703719B|2014-03-05|
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    CN201210229667.XA|CN102703719B|2012-07-03|2012-07-03|Technology for recovering valuable metals from noble metal slag|
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