CN1594608A - Method for extracting platinum-palladium and base metal from platinum metal sulphide ore - Google Patents

Method for extracting platinum-palladium and base metal from platinum metal sulphide ore Download PDF

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CN1594608A
CN1594608A CNA2004100401018A CN200410040101A CN1594608A CN 1594608 A CN1594608 A CN 1594608A CN A2004100401018 A CNA2004100401018 A CN A2004100401018A CN 200410040101 A CN200410040101 A CN 200410040101A CN 1594608 A CN1594608 A CN 1594608A
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platinum
digestion
liquid
palladium
solid
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CN1328398C (en
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陈景
黄琨
陈奕然
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Kunming Institute of Precious Metals
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Kunming Institute of Precious Metals
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    • 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 relates to a whole-wet method for processing platinum metals containing sulphur ore and a method for extracting platinum metals and Cu, Ni, Co valent metal from the sulphur ore. The method comprises: (1) pressurized oxidation soaking and boiling, (2) leaching Cu, Ni, Co, Fe heavy non-ferrous metal from pressurized soaking and boiling dreg under the atmospheric pressure with the acid, (3) leaching platinum family metal under the atmospheric pressure with the acid and the oxidant from acid pickling dregs, (4) Concentrating and fining platinum family metal with the traditional process.The invention has a simple technical process, non- poison polluted and the strong material compatibility characteristic. Its platinum, palladium returns-ratio achieved Pt>94%, Pd>96%. The copper, the nickel, the cobalt leaching rate achieved is above 98%.

Description

The platinum metals sulphide ores extracts the method for platinum palladium and base metal
Technical field
The present invention relates to the full wet processing of a kind of employing and handle low-grade platinum metals sulphide ores or its flotation concentrate, extract the method for platinum metals and base metal, particularly extract the method for platinum, palladium and copper, nickel, cobalt valuable metal.
Background technology
The tradition of platinum group metallic copper Ni sulphide mine is smelted extraction process and is all adopted the enrichment of pyrometallurgical smelting technology usually earlier.Its process system with the selecting and smelting technology of heavy non-ferrous metal as carrier.Flotation concentrate is earlier after roasting or oven dry, with the low sulfonium of output copper nickel behind electric furnace or the flash stove matte smelting divided silicon hydrochlorate, the platinum metals is trapped in the low sulfonium, low then sulfonium obtains the higher high sulfonium of precious metal grade through oxygen blowing, handle high sulfonium with the method for hydrometallurgy again, constantly heavy non-ferrous metal such as separating nickel, copper, cobalt obtain the concentration of precious metal thing, also claim the precious metal concentrate, that carries out at last precious metal again is separated from each other the purification refining.The tradition pyrometallurgical smelting process is for extracting the platinum metals, and flow process is too tediously long, and technical sophistication be difficult to obtain higher metal recovery rate, and environmental pollution is serious.When heavy non-ferrous metal grades such as the copper of association, nickel are on the low side, the pyrometallurgical smelting difficulty, the technology cost up, economic benefit is affected.And application HCl+Cl 2When the platinum metals sulphide ores is directly handled in the wet oxidation acidleach, must treat all heavy non-ferrous metal sulfide minerals and CaO, MgO, Al 2O 3Behind whole molten the finishing of oxide compound, precious metal could dissolve, and the reagent consumption is very big, the equipment anticorrosion difficulty, and the solution composition complexity, environmental pollution is serious, and from economy and technical standpoint analysis, its use value is subjected to bigger restriction.
Pressurization is leached as a kind of non-ferrous extractive metallurgy technology, has with the air or the oxygen-rich air of cheapness and makes oxygenant, and speed of response is fast, and flow process is short, operating environment close friend, advantage such as construction investment is little.Be used to handle not the heavy non-ferrous metal sulphide ores and the difficult-treating gold mine of platinum group metal, developed into quite sophisticated modern metallurgical industry new technology in the world.
In recent years, the range of application of pressurization leaching-out technique progressively expands to the platinum group metal sulfide.Chinese patent application: publication number CN1417356A has reported a kind of method of extracting platinum metals and copper, nickel, cobalt from low-grade Pt-Pd sulfide flotation concentrate.At first adopt pressure oxidation acidleach or fiery wet method combined pre-treatment flotation concentrate, leach heavy non-ferrous metal copper, nickel, cobalt, leach the platinum metals with the pressure cyanide method then.Platinum, palladium leaching yield can reach Pt96%, Pd99%, and copper, nickel, cobalt leaching yield also reach more than 99%.Its advantage is reflected in the cupric sulfide nickel flotation concentrate of pressure oxidation acidleach technical finesse platiniferous palladium, can make sulphide ores all destroyed is vitriol, at high temperature then most of pyrrhosiderite and the hematite precipitation of forming of iron, help from pickling liquor, reclaiming copper and mickel, also help from leached mud, after follow-up pressure cyanide is handled, extracting platinum and palladium.But, make the application of this Technology be subjected to the influence of factors such as environment protection and operator safety protection, thereby increased the technology cost owing to use huge malicious prussiate.
Summary of the invention
The object of the invention provides a kind of technological operation is simply extracted platinum and palladium and weighed coloured valuable metal copper, nickel, cobalt from the sulphide ores of platinum group metal method.
The method of the extraction platinum from the sulphide ores of platinum group metal of foregoing invention purpose and palladium and heavy coloured valuable metal copper, nickel, cobalt comprises following several steps successively:
1. the digestion mineral aggregate pressurizes: mineral aggregate and digestion liquid were put into 50～250 ℃ of digestions of closed reactor 0.5～20 hour, and digestion liquid is selected from H 2SO 4, NaOH, water any, the weight ratio of this step mineral aggregate and this step digestion liquid is solid: liquid=1: 2～6 are filled with air, oxygen-rich air or pure oxygen gas in the reactor;
2. the solid slag that 1. obtains of 50～100 ℃ of digestion steps is 0.5～8 hour, and the digestion liquid that digestion is selected for use is HCl, H 2SO 4At least a, the weight ratio of the digestion liquid that the solid slag that 1. above-mentioned steps obtains and this step digestion are selected for use is solid: liquid=1: 2～6;
3. with the mixture solid slag that 2. the digestion step obtains under 40～100 ℃ of temperature of digestion liquid and oxygenant 0.5～8 hour, this step digestion liquid was selected from HCl, H 2SO 4, HCl and H 2SO 4Mixture, HCl and HNO 3Any of mixture, above-mentioned oxygenant is selected from H 2O 2, HClO 3, HClO, HNO 3, NaClO 3, NaClO, Na 2S 2O 8, chlorinated lime, Cl 2The solid-liquid weight ratio of the solid slag that 2. any of gas, above-mentioned steps obtain and this step digestion liquid is for solid: liquid=1: 2～6;
4. platinum, palladium during the leach liquor that 3. obtains with traditional enrichment, method of refining extraction step contains.
Behind each technical parameter, can further improve the productive rate of extract in the preferred technique scheme.
To step 1., its H 2SO 4, NaOH concentration be preferably 1wt%～40wt%, the gaseous tension in the reactor is preferably 1～5MPa.
To step 2., HCl, H 2SO 4Or the concentration of its mixture is preferably 5wt%～60wt%.
To step 3., digestion liquid HCl, H 2SO 4, HCl and H 2SO 4Mixture, HCl and HNO 3The concentration of mixture is preferably 5wt%～100wt%, oxygenant H 2O 2, HClO 3, HClO, HNO 3, NaClO 3, NaClO, Na 2S 2O 8, chlorinated lime, Cl 2The consumption of gas is preferably 0.5%～50% of solid slag weight that 2. step obtain.
To step oxygenant H 3. 2O 2, HClO 3, HClO, HNO 3, NaClO 3, NaClO, Na 2S 2O 8, in this step digestion liquid of the selected direct adding of chlorinated lime, oxygenant Cl 2In the digestion liquid of selected continuous this step of directly feeding of gas.
Further preferred steps consolidating in 1.: liquid=1: 3～5, step consolidating in 2.: liquid=1: 3～5, step consolidating in 3.: liquid=1: 3～5.
Can also preferred steps H in 1. 2SO 4Concentration is 15wt%～25wt%, and gaseous tension is 1～3MPa oxygen in the reactor, and digestion temperature is 180～200 ℃, and the digestion time is 8～15 hours.
Also can preferred steps H in 2. 2SO 4Concentration is 20wt%～50wt%, and digestion temperature is 80～100 ℃, 4～6 hours digestion time.
Can also preferred steps HCl concentration in 3. be 50wt%～100wt%, described digestion temperature is 80～100 ℃, 4～6 hours described digestion time.
Chlorinated lime in the technique scheme is meant Ca (ClO) 2CaCl 22H 2O.
In the technique scheme, step HCl and H 2. 2SO 4In the mixture, 0＜HCl concentration＜60wt%, 0＜H 2SO 4Concentration＜60wt%; Step HCl and H 3. 2SO 4In the mixture, 0＜HCl concentration＜100wt%, 0＜H 2SO 4Concentration＜100wt%; Step HCl and HNO 3. 3In the mixture, 0＜HCl concentration＜100wt%, 0＜HNO 3Concentration＜100wt%.
State on the implementation in the technical scheme process, because the oxygen in the step gas 1. participates in reaction process, so the gaseous tension in the reactor selects to remain a certain steady state value selected in appropriate technical solution gaseous tension parameter area.Help reaction like this and normally carry out, guarantee to obtain higher leaching yield, realize that simultaneously rapid extraction reclaims heavy non-ferrous metal copper, nickel, the cobalt in the mineral aggregate.
In the technique scheme, 1. step contains the leach liquor of copper, nickel, cobalt respective compound with the 2. equal output of step, available traditional method, and as solvent extraction, copper, nickel, cobalt in the difference Separation and Recovery digestion liquid.
In the technique scheme, step oxygenant 3. can with digestion liquid synchronized mixes, also can be in temperature-rise period substep add in the digestion liquid.
In the technique scheme, step traditional enrichment, method of refining 4. can be substitution method, ion exchange method, solvent extration or chromatograph absorption method.Substitution method can use metal replacements such as powdery, sheet or blocky Zn, Mg, Al, Fe or Cu to obtain platinum, palladium.Ion exchange method comprises various anionite-exchange resin absorption and obtains platinum, palladium.Solvent extration mainly is to obtain the platinum palladium with quaternary ammonium salt, tertiary amine, TRPO or TBP extraction.Use traditional method of refining output platinum metals product again through the platinum metals enriched substance that above-mentioned any enrichment obtains.
The present invention is to the pressure oxidation acidleach pre-treatment slag of platinum group metal sulfide, adopt atmospheric pressure oxidation acidleach platinum metals, saved the high-temperature cyanidation process, thereby the potential hazard of having avoided using huge malicious prussiate and environment and operator being existed, and shortened technical process, adopt normal pressure leaching-out technique means greatly to reduce and implement Financial cost of the present invention.Process program technology maturation of the present invention, simple to operate, the equipment used maintenance and management is easy.Adopt the present invention to handle the platinum group metal sulfide, platinum, palladium recovery rate can reach Pt＞94%, Pd＞96%, and copper, nickel, cobalt leaching yield reach more than 98%.Invention has the adaptable characteristics of material.
The present invention can be used for handling the Cu, Ni and Co sulfide content below 15%, the low-grade platinum metals sulphide ores of platinum metals content below 0.05%, be more suitable for handling its flotation concentrate, simultaneously also be suitable for handling other material of platinum group metal, for example platinum group burning ore deposit, the anode sludge, smelting intermediates etc.The present invention all has no special requirements to employed each chemical reagent of reactant gases that comprises, above commercial reagent of technical pure or gas can satisfy the technical scheme requirement.
Embodiment
Select for use the low-grade Pt-Pd sulphide ores through the flotation concentrate of floating and enriching as the technical solution of the present invention process object.This kind flotation concentrate sulfur-bearing is about 15%, belongs to sulphide ores, and the Pt+Pd grade can reach 70～100g/t, but Cu and Ni grade are respectively＜5%, SiO 2Content is 26%, and MgO content is near 20%.The platinum palladium flotation concentrate material that experiment is handled is the toner powder darkly, and the sample quartering analytical results is listed in table 1.
Table 1 platinum palladium flotation concentrate multielement chemical analysis results (Pt, Pd:g/t, other element: wt%)
Element ??Pt ??Pd ??Cu ??Fe ??Ni ??Co ???S ??SiO 2 ?CaO ?MgO
Content ?32.14 ?50.31 ??3.77 ?15.32 ?3.55 ?0.24 ?14.15 ?25.97 ?2.89 ?18.56
Embodiment 1
1. get mineral aggregate 500 grams in the table 1, with weight percent concentration 20%H 2SO 4Aqueous solution, the furnishing pulpous state is put into reactor.Mineral aggregate and H 2SO 4Aqueous solution solid-liquid weight ratio is 1: 4.Be heated to 200 ℃ of temperature, reacted 10 hours, gas is oxygen in the preceding reactor of heating, and the gaseous tension in the reaction process control reactor is constant to be 2.0MPa.
2. the acid leaching residue that 1. step is obtained under normal pressure with the H of weight percent concentration 20% 2SO 4Aqueous solution, solid-liquid weight ratio are 1: 4, and temperature of reaction is 90 ℃, 6 hours reaction times.
3. the acid leaching residue that 2. step is obtained is put into reactor, sizes mixing with weight percent concentration 50%HCl aqueous solution, and the solid-liquid weight ratio is 1: 5, is heated to 90 ℃ of temperature, adds weight and be the NaClO of the acid leaching residue 10% that 2. step obtain 3, normal pressure reacted 6 hours down.
4. the leach liquor zinc dust precipitation that 3. step is obtained obtains separating the purification platinum metals with traditional technology again behind the concentration of precious metal thing.
Platinum, palladium leaching yield are respectively: Pt97.07%, Pd98.90%.
Copper, nickel, cobalt leaching yield are respectively: Cu98.0%, Ni98.6%, Co98.5%.
Embodiment 2
1. get mineral aggregate 500 grams in the table 1, with weight percent concentration 15%H 2SO 4Aqueous solution, the furnishing pulpous state is put into reactor.Mineral aggregate and H 2SO 4Aqueous solution solid-liquid weight ratio is 1: 5.Be heated to 200 ℃ of temperature, reacted 15 hours, gas is oxygen in the preceding reactor of heating, and the constant system pressure of reaction process is 3.0MPa.
2. the acid leaching residue that 1. step is obtained under normal pressure with the HCl aqueous solution of concentration expressed in percentage by weight 20%, the solid-liquid weight ratio is 1: 4, temperature of reaction is 50 ℃, 4 hours reaction times;
3. the acid leaching residue that 2. step is obtained is put into reactor, mixes with weight percent concentration 100%HCl solution and sizes mixing, and the solid-liquid weight ratio is 1: 5, is heated to 40 ℃ of temperature, adds weight and be the H of the acid leaching residue 40% that 2. step obtain 2O 2, normal pressure reacted 4 hours down.
4. the leach liquor zinc dust precipitation that 3. step is obtained obtains separating the purification platinum metals with traditional technology again behind the concentration of precious metal thing.
Platinum, palladium leaching yield are respectively: Pt94.55%, Pd9730%.
Copper, nickel, cobalt leaching yield are respectively: Cu99.0%, Ni99.0%, Co98.5%.
Embodiment 3
1. get mineral aggregate 500 grams in the table 1, with weight percent concentration 25%H 2SO 4Aqueous solution, the furnishing pulpous state is put into reactor.Flotation concentrate and H 2SO 4Aqueous solution solid-liquid weight ratio is 1: 3.Be heated to 180 ℃ of temperature, reacted 8 hours, gas is oxygen in the preceding reactor of heating, and the constant system pressure of reaction process is 2.5MPa.
2. the acid leaching residue that 1. step is obtained under normal pressure is 20% HCl+H with concentration expressed in percentage by weight 2SO 4Aqueous solution, solid-liquid weight ratio are 1: 4, and temperature of reaction is 80 ℃, react 4 hours.
3. the acid leaching residue that 2. step is obtained is put into reactor, mixes with weight percent concentration 50%HCl solution and sizes mixing, and the solid-liquid weight ratio is 1: 4, is heated to 80 ℃ of temperature, adds weight percent concentration 15%NaClO, and normal pressure reacted 8 hours down.
4. the leach liquor zinc dust precipitation that 3. step is obtained obtains separating the purification platinum metals with traditional technology again behind the concentration of precious metal thing.
Platinum, palladium leaching yield are respectively: Pt94.0%, Pd96.5%.
Copper, nickel, cobalt leaching yield are respectively: Cu99.0%, Ni99.0%, Co98.5%.
Embodiment 4
1. get mineral aggregate 500 grams in the table 1, with weight percent concentration 15%NaOH aqueous solution, the furnishing pulpous state is put into reactor.Flotation concentrate and NaOH aqueous solution solid-liquid weight ratio are 1: 5.Be heated to 200 ℃ of temperature, reacted 20 hours, gas is oxygen in the preceding reactor of heating, and the constant system pressure of reaction process is 2.5MPa.
2. 1.) leached mud of Huo Deing under normal pressure is 50% H with concentration expressed in percentage by weight with step 2SO 4Aqueous solution, solid-liquid weight ratio are 1: 4, and temperature of reaction is 70 ℃, react 6 hours.
3. the leached mud that 2. step is obtained is put into reactor, with weight percent concentration 50%HCl+H 2SO 4Solution mixes sizes mixing, and the solid-liquid weight ratio is 1: 4, is heated to 80 ℃ of temperature, adds weight and be the HClO of the acid leaching residue 50% that 2. step obtain 3, normal pressure reacted 8 hours down.
4. the leach liquor zinc dust precipitation that 3. step is obtained obtains separating the purification platinum metals with traditional technology again behind the concentration of precious metal thing.
Platinum, palladium leaching yield are respectively: Pt95.7%, Pd96.0%.
Copper, nickel, cobalt leaching yield are respectively: Cu98.6%, Ni99.0%, Co99.2%.
Embodiment 5
1. get mineral aggregate 500 grams in the table 1, with weight percent concentration 20%H 2SO 4Aqueous solution, the furnishing pulpous state is put into reactor.Flotation concentrate and H 2SO 4Aqueous solution solid-liquid weight ratio is 1: 4.Be heated to 200 ℃ of temperature, reacted 10 hours, gas is oxygen in the preceding reactor of heating, and the constant system pressure of reaction process is 2.0MPa.
2. the acid leaching residue that 1. step is obtained under normal pressure with the H of weight percent concentration 30% 2SO 4Aqueous solution, solid-liquid weight ratio are 1: 4, and temperature of reaction is 90 ℃, 6 hours reaction times.
3. the acid leaching residue that 2. step is obtained is put into reactor, sizes mixing with weight percent concentration 100%HCl aqueous solution, and the solid-liquid weight ratio is 1: 5, is heated to 90 ℃ of temperature, feeds Cl in digestion liquid continuously 2, take out sample with sampler in the reaction process and send chemical analysis, with platinum metals leaching yield＞90% as reaction end.
4. the leach liquor zinc dust precipitation that 3. step is obtained obtains separating the purification platinum metals with traditional technology again behind the concentration of precious metal thing.
Platinum, palladium leaching yield are respectively: Pt95.2%, Pd97.5%.
Copper, nickel, cobalt leaching yield are respectively: Cu98.0%, Ni98.6%, Co98.5%.
Embodiment 6
1. getting mineral aggregate 500 grams in the table 1, is that 2000 water that restrain mix with weight, and the furnishing pulpous state is put into reactor.Be heated to 200 ℃ of temperature, reacted 18 hours, gas is oxygen in the preceding reactor of heating, and the constant system pressure of reaction process is 3.0MPa.
2. the leached mud that 1. step is obtained under normal pressure is 20% HCl aqueous solution with concentration expressed in percentage by weight, and the solid-liquid weight ratio is 1: 4, and temperature of reaction is 100 ℃, reacts 4 hours.
3. the leached mud that 2. step is obtained is put into reactor, with weight percent concentration 50%HCl+HNO 3Solution mixes sizes mixing, and the solid-liquid weight ratio is 1: 4, is heated to 60 ℃ of temperature, and normal pressure reacted 4 hours down.
4. the leach liquor solvent extraction that 3. step is obtained obtains separating the purification platinum metals with traditional technology again behind the concentration of precious metal thing with zinc dust precipitation from strip liquor.
Platinum, palladium leaching yield are respectively: Pt95.4%, Pd96.2%.
Copper, nickel, cobalt leaching yield are respectively: Cu98.6%, Ni99.0%, Co99.2%.
Embodiment 7
1. get mineral aggregate 500 grams in the table 1, with weight percent concentration 20%H 2SO 4Aqueous solution, the furnishing pulpous state is put into reactor.Flotation concentrate and H 2SO 4Aqueous solution solid-liquid weight ratio is 1: 4.Be heated to 200 ℃ of temperature, reacted 10 hours, gas is oxygen in the preceding reactor of heating, and the constant system pressure of reaction process is 2.0MPa.
2. the acid leaching residue that 1. step is obtained under normal pressure with the H of weight percent concentration 30% 2SO 4Aqueous solution, solid-liquid weight ratio are 1: 4, and temperature of reaction is 90 ℃, 6 hours reaction times.
3. the leached mud that 2. step is obtained is put into reactor, with weight percent concentration 50%H 2SO 4Solution mixes sizes mixing, and the solid-liquid weight ratio is 1: 6, is heated to 100 ℃ of temperature, adds weight and be the NaClO of the acid leaching residue 10% that 2. step obtain 3, normal pressure reacted 8 hours down.
4. the leach liquor zinc dust precipitation that 3. step is obtained obtains separating the purification platinum metals with traditional technology again behind the concentration of precious metal thing.
Platinum, palladium leaching yield are respectively: Pt94.5%, Pd95.2%.
Copper, nickel, cobalt leaching yield are respectively: Cu98.6%, Ni99.0%, Co99.2%.
Embodiment 8
1. get mineral aggregate 500 grams in the table 1, with weight percent concentration 15%NaOH aqueous solution, the furnishing pulpous state is put into reactor.Flotation concentrate and NaOH aqueous solution solid-liquid weight ratio are 1: 5.Be heated to 200 ℃ of temperature, reacted 20 hours, gas is oxygen in the preceding reactor of heating, and the constant system pressure of reaction process is 2.5MPa.
2. the leached mud that 1. step is obtained under normal pressure is 50% HCl aqueous solution with concentration expressed in percentage by weight, and the solid-liquid weight ratio is 1: 4, and temperature of reaction is 70 ℃, reacts 6 hours.
3. the leached mud that 2. step is obtained is put into reactor, with weight percent concentration 95%HCl+HNO 3Solution mixes sizes mixing, and the solid-liquid weight ratio is 1: 4, is heated to 100 ℃ of temperature, and normal pressure reacted 2 hours down.
4. the leach liquor solvent extraction that 3. step is obtained obtains separating the purification platinum metals with traditional technology again behind the concentration of precious metal thing with zinc dust precipitation from strip liquor.
Platinum, palladium leaching yield are respectively: Pt96.4%, Pd97.0%.
Copper, nickel, cobalt leaching yield are respectively: Cu98.6%, Ni99.0%, Co99.2%.

Claims (9)

1. method of extracting platinum, palladium, copper, nickel, cobalt from the sulphide ores of platinum group metal comprises following process steps successively:
1. the digestion mineral aggregate pressurizes: mineral aggregate and digestion liquid were put into 50～250 ℃ of digestions of closed reactor 0.5～20 hour, and described digestion liquid is selected from H 2SO 4, NaOH, water any, the weight ratio of described mineral aggregate and described digestion liquid is solid: liquid=1: 2～6 are filled with air, oxygen-rich air or pure oxygen gas in the described reactor;
2. the solid slag that 1. obtains of 50～100 ℃ of digestion steps is 0.5～8 hour, and the digestion liquid that described digestion is selected for use is HCl, H 2SO 4Or its mixture, the weight ratio of the digestion liquid that solid slag that 1. described step obtains and described digestion are selected for use is solid: liquid=1: 2～6;
3. with the mixture solid slag that 2. the digestion step obtains under 40～100 ℃ of temperature of digestion liquid and oxygenant 0.5～8 hour, described digestion liquid was selected from HCl, H 2SO 4, HCl and H 2SO 4Mixture, HCl and HNO 3Any of mixture, described oxygenant is selected from H 2O 2, HClO 3, HClO, HNO 3, NaClO 3, NaClO, Na 2S 2O 8, chlorinated lime, Cl 2Any of gas, the solid-liquid weight ratio of solid slag that 2. described step obtains and described digestion liquid is for solid: liquid=1: 2～6;
4. platinum, the palladium in the leach liquor that 3. obtains with traditional enrichment, method of refining extraction step.
2. the method for extracting platinum, palladium, copper, nickel, cobalt from the sulphide ores of platinum group metal as claimed in claim 1 is characterized in that the 1. described H of step 2SO 4, NaOH concentration be 1wt%～40wt%, the gaseous tension in the described reactor is 1～5MPa.
3. the method for extracting platinum and palladium and copper, nickel, cobalt from the sulphide ores of platinum group metal as claimed in claim 1 is characterized in that the 2. described HCl of step, H 2SO 4Or the concentration of its mixture is 5wt%～60wt%.
4. the method for extracting platinum, palladium, copper, nickel, cobalt from the sulphide ores of platinum group metal as claimed in claim 1 is characterized in that the 3. described digestion liquid of step HCl, H 2SO 4, HCl and H 2SO 4Mixture, HCl and HNO 3The concentration of mixture is 5wt%～100wt%, described oxygenant H 2O 2, HClO 3, HClO, HNO 3, NaClO 3, NaClO, Na 2S 2O 8, chlorinated lime, Cl 2The consumption of gas is 0.5%～50% of the solid slag weight that 2. obtains of described step.
5. the method for extracting platinum, palladium, copper, nickel, cobalt from the sulphide ores of platinum group metal as claimed in claim 4 is characterized in that the 3. described oxygenant H of step 2O 2, HClO 3, HClO, HNO 3, NaClO 3, NaClO, Na 2S 2O 8, chlorinated lime is introduced directly in the described digestion liquid described oxygenant Cl 2Gas is directly fed in the described digestion liquid continuously.
6. as the described method of from the sulphide ores of platinum group metal, extracting platinum, palladium, copper, nickel, cobalt of one of claim 1 to 5, it is characterized in that step is 1. described solid: liquid=1: 3～5, step is 2. described solid: liquid=1: 3～5, step are 3. described solid: liquid=1: 3～5.
7. the method for extracting platinum, palladium, copper, nickel, cobalt from the sulphide ores of platinum group metal as claimed in claim 6 is characterized in that the 1. described H of step 2SO 4Concentration is 15wt%～25wt%, and gaseous tension is 1～3MPa oxygen in the described reactor, and described digestion temperature is 180～200 ℃, and the described digestion time is 8～15 hours.
8. the method for extracting platinum, palladium, copper, nickel, cobalt from the sulphide ores of platinum group metal as claimed in claim 6 is characterized in that the 2. described H of step 2SO 4Concentration is 20wt%～50wt%, and described digestion temperature is 80～100 ℃, 4～6 hours described digestion time.
9. the method for from the sulphide ores of platinum group metal, extracting platinum, palladium, copper, nickel, cobalt as claimed in claim 6, it is characterized in that the 3. described HCl concentration of step is 50wt%～100wt%, described digestion temperature is 80～100 ℃, 4～6 hours described digestion time.
CNB2004100401018A 2004-06-26 2004-06-26 Method for extracting platinum-palladium and base metal from platinum metal sulphide ore Active CN1328398C (en)

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ZA200505141A ZA200505141B (en) 2004-06-26 2005-06-24 Hydrometallurgical leaching method for extracting platinum, palladium, copper and nickel from the sulfide flotation concentrates containing platinum metals

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CN103436711A (en) * 2013-08-22 2013-12-11 中南大学 Method for enriching gold in gold cyanide sludge
CN103492592A (en) * 2011-02-03 2014-01-01 西铂有限公司 Refining of platinum group metals concentrates
CN103572066A (en) * 2013-11-11 2014-02-12 广州有色金属研究院 Method for enriching platinum family elements from platinum family concentrate
CN104263958A (en) * 2014-08-30 2015-01-07 广东省工业技术研究院(广州有色金属研究院) Method for separating copper, nickel or cobalt and platinum family elements from platinum family concentrates
CN106244820A (en) * 2016-08-29 2016-12-21 金川集团股份有限公司 A kind of method of chlorine pressure rapid solution complexity rare precious metal concentrate
CN107475512A (en) * 2017-08-30 2017-12-15 江西铜业股份有限公司 A kind of method of comprehensive exploitation low-grade Pt-Pd concentrate
CN113802008A (en) * 2021-09-16 2021-12-17 兰州大学 Method for treating waste liquid containing platinum group noble metal

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CN1234889C (en) * 2001-11-07 2006-01-04 昆明贵金属研究所 Extraction of platinum family metals and Cu, Ni and Co from sulfide ore or floated concentrate of platinum family metals
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CN101509077B (en) * 2009-02-19 2010-08-25 昆明贵金属研究所 Method for extracting platinum, palladium, rhodium from automotive catalyst of ore phase reconstruction
CN103492592A (en) * 2011-02-03 2014-01-01 西铂有限公司 Refining of platinum group metals concentrates
CN103436711A (en) * 2013-08-22 2013-12-11 中南大学 Method for enriching gold in gold cyanide sludge
CN103572066A (en) * 2013-11-11 2014-02-12 广州有色金属研究院 Method for enriching platinum family elements from platinum family concentrate
CN104263958A (en) * 2014-08-30 2015-01-07 广东省工业技术研究院(广州有色金属研究院) Method for separating copper, nickel or cobalt and platinum family elements from platinum family concentrates
CN104263958B (en) * 2014-08-30 2016-04-20 广东省工业技术研究院(广州有色金属研究院) A kind of method being separated Cu, Ni and Co and platinum family element from platinum family concentrate
CN106244820A (en) * 2016-08-29 2016-12-21 金川集团股份有限公司 A kind of method of chlorine pressure rapid solution complexity rare precious metal concentrate
CN107475512A (en) * 2017-08-30 2017-12-15 江西铜业股份有限公司 A kind of method of comprehensive exploitation low-grade Pt-Pd concentrate
CN113802008A (en) * 2021-09-16 2021-12-17 兰州大学 Method for treating waste liquid containing platinum group noble metal

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