Extraction method of nickel from oxidised nickel ores
SUBSTANCE: method involves heap leaching of nickel with sulphuric acid solution, neutralisation of production solution, sorption of nickel on ionite from it, processing of strippant so that nickel is obtained, supply of raffinate solution for heap leaching of ore during its revolution and circulation. At that, some part of raffinate is subject to neutralisation with lime milk and its cleaning from impurities of iron, manganese and magnesium by directing in the form of neutralised pulp to waste heap for deposition of iron, manganese and magnesium on it with further mixing with the main volume of cycling solution of raffinate and final strengthening with sulphuric acid. Volume of some part of raffinate, which is subject to neutralisation and cleaning, as per the amount of iron, manganese and magnesium, corresponds to their transition to production solution during leaching of nickel from the ore during circulation of cycling solution.
EFFECT: simplifying the utilisation process of iron, manganese and magnesium and heap leaching process of nickel.
1 dwg, 1 tbl
The invention relates to metallurgy, and in particular to methods of extraction of Nickel from laterite Nickel ores of ferrous and magnesium types.
As a prototype of the selected method of extraction of Nickel from Ni-Fe-Mg lateritic ores containing large amounts of magnesium (U.S. patent No. 5571308), in which magnesia ore processed by heap leaching with sulfuric acid followed by neutralization productive solution and then the sorption of Nickel on the selective ion exchangers resin. Desorbed with high Nickel content is sent for further processing by removing the cathode of Nickel by way of electrowinning, and a portion of the raffinate is subjected to neutralization with lime milk and purification from impurities of iron, manganese and magnesium by sending in the form of neutralized slurry to waste a bunch for deposition on iron, manganese and magnesium, followed by mixing with the main volume of the working solution of the raffinate and doripenem sulfuric acid.
The disadvantages of this method are the utilization of the magnesium-containing solution, burial precipitate iron hydroxide and the need for continued stabilization of the volume of leach solution by adding water to compensate for the volume withdrawn from circulation solution of magnesium sulfate and hydroxide of iron.
Tasks which is aimed at solving the claimed invention, are simplifying the utilization of iron, manganese and magnesium and the whole process of heap leaching of Nickel.
This task is solved in that in the method of extraction of Nickel from laterite Nickel ores, including heap leaching of Nickel sulfuric acid solution, followed by neutralization productive solution and sorption of Nickel on the ion exchanger, the processing decorate, neutralizing part of the raffinate and the precipitation of the iron, part of the raffinate is sent to waste a bunch for the deposition of iron, manganese and magnesium, and the volume part of the raffinate subjected to neutralization and purification, the amount of iron, manganese and magnesium must comply with their transition into productive solution in the leaching of Nickel from the ore during circulation of the circulating solution.
The method was carried out as follows.
The pregnant solution after sulfuric acid heap leaching of magnesium or ferrous ores containing Nickel, cobalt, iron, magnesium, manganese and concomitant impurities, is fed to the operation of selective sorption of Nickel and cobalt on the ionite chelate resin type, such as DOWEX M4195. Sorption on ion exchangers chelate resin type allows you to selectively adsorb Nickel and clear it from magnesium, manganese and partly of iron. Desorbed, reduced in volume in dozens of times in relation to the original productive R is the target and containing up to 60 g/l of Nickel and 5-6 g/l of iron, after hydrolytic purification from iron is supplied to the processing solution to produce cathode Nickel method electrowinning or certified Nickel sulfate.
The precipitate of iron hydroxide formed when cleaning decorate is routed to a waste pile for the co-disposal of waste space career when his reinstatement.
Part of the raffinate is subjected to neutralization with lime milk and purification from impurities of iron, manganese and magnesium by sending in the form of neutralized slurry to waste a bunch for deposition on iron, manganese and magnesium, followed by mixing with the main volume of the working solution of the raffinate and doripenem sulfuric acid. The hydroxides of iron, magnesium and manganese deposited on the ore material waste heap together and stored in the waste space quarry oxidized Nickel ore and reclamation.
And the volume part of the raffinate subjected to neutralization and purification, the amount of iron, manganese and magnesium must comply with their transition into productive solution in the leaching of Nickel from the ore during circulation of the circulating solution.
The solution after the precipitation of hydroxides of iron, manganese and magnesium on the waste pile is mixed with a basic solution doubleplays sulfuric acid is served on a heap leach ore (see the drawing).
This allows you to stabilize the circulating washing solution according to the content of iron, magnesium and manganese without filtering and organization of the special landfills for precipitation of the hydroxides of iron, magnesium and manganese.
Stabilization productive working solutions on the content of impurities in the feed portion of the raffinate after neutralization at the spent ore material to be excluded from the process technology filtration precipitation of hydroxides and their deposition on the spent ore material is confirmed by experiments on percolation leaching conducted on the averaged core samples taken from the field of oxidized Nickel ores "Kungur".
The chemical composition of magnesium ore, %:
Table 1 shows the contents of the elements in a productive working solutions percolation leaching after sorption of Nickel on ionite resin DOWEX M when circulation of the solution without precipitation of hydroxides on used material heap and neutralize 50% of these solutions and applying them on the used material percolation columns.
Leaching and circulation leach solution leaving the first column, made be the neutralization and removal of impurities.
The second column.
The sulfuric acid solution in an amount of 10 liters with a sulfuric acid concentration of 100 g/l was fed into the top of the second column on the surface of the ore at a speed of 5 liters per hour/m2. Leaching was carried out for 15 days. The total time of passage of the solution through the ore layer 3 nights. The sorption of Nickel from the pregnant solution produced on the resin DOWEX M4195. The raffinate was subjected to neutralization with lime milk and was applied to the surface of the ore in the waste percolation column. Then neutralized raffinate leaving the waste column, were analyzed for the presence of impurities and doreplace sulfuric acid to 100 g/L. then doubleplay solution was again applied to the surface of the ore to leach Nickel.
From the above example shows that the removal of impurities from the raffinate possible without the process of separation of the liquid and solid phase by filtration. Enough to supply the neutralized slurry with hydroxides on the surface of the ore in the waste percolation column. This provides stabilization of the salt composition productive solution that allows you to more effectively manage the process of sorption of Nickel.
|The method of heap leaching||The current pls, g/l|
|Ni||Co||Fe||Mg||Mn||The leaching time, the day|
|Percolation leaching without neutralizing the circulating solution|
|1. 1st productive solution||0,1||0,05||3,1||5,2||0,3||3|
|2. Working solution -1||0,1||0,06||6,9||14,8||0,7||6|
|3. Working solution 2||0,1||0,06||7,2||16,1||0,8||9|
|4. About the commander solution 3||0,1||0,07||8,7||18,3||1,1||12|
|5. Working solution - 4||0,1||0,08||10,3||20,5||1,3||15|
|Percolation leaching with neutralization and flow of the circulating solution to waste percolation column.|
|1. 1st productive solution||0,1||0,05||3,1||5,2||0,3||3|
|2. The circulating solution 1||0,1||0,05||2,9||5,2||0,2||6|
|3. Working solution 2||0,1||0,03||2,7||a 4.9||0,3||9|
|4. Working solution - 3||0,1||0,04||2,2||5,3||0,4||12|
|5. Working solution - 4||0,1||0,03||1,7||5,0||0,2||15|
The method of extraction of Nickel from laterite Nickel ores, including heap leaching of Nickel sulfuric acid solution, neutralizing productive solution, sorption of Nickel on the ion exchanger, the processing decorate obtaining Nickel, feed raffinate solution in heap leaching of ore in its turnover and circulation, characterized in that a portion of the raffinate is subjected to neutralization with lime milk and purification from impurities of iron, manganese and magnesium by sending in the form of neutralized slurry to waste a bunch for deposition therein jelly is a, manganese and magnesium, followed by mixing with the main volume of the working solution of the raffinate and doripenem sulfuric acid, the volume part of the raffinate subjected to neutralization and purification, the amount of iron, manganese and magnesium corresponds to their transition into productive solution in the leaching of Nickel from the ore during circulation of the circulating solution.
SUBSTANCE: method of enriching anatase mechanical concentrates involves burning (1) an anatase concentrate in a fluidised bed furnace or a drum furnace; reducing (2) the burnt product in the fluidised bed furnace or drum furnace using a hydrogen or natural gas as a reducing agent; dry and wet separation (3) of the reduced product in a weak magnetic field in magnetic separators fitted with a permanent magnet and a drum, where the magnetic fraction formed during reduction is discarded; dry separation (4) in a strong, high-gradient magnetic field of the magnetic fraction obtained during separation in a weak magnetic field in roller or drum separators with a rare-earth permanent magnet, with extraction of silicates, secondary phosphates, monazite, calzirtite, zircolinite and uranium and thorium-containing minerals; leaching (5) of the magnetic fraction obtained from separation in strong magnetic field in mixing tanks or fluidised bed columns, with a hydrochloric acid solution; filtering the leached product on a belt filter; drying of the filtered product in a rotary drier or fluidised bed drier; oxidation (6) of the dried product in the drum furnace or fluidised bed furnace; fast cooling of the oxidised product in water or compressed air in a drum cooling device or by immersing in water; leaching (7) the fast-cooled product in mixing tanks or columns, or with hydrochloric acid or sulphuric acid; filtering the product from the second leaching (7) on a belt filter; and drying of the filtered product in a rotary or fluidised bed drier; and final dry separation (8) of the product of the second leaching in a strong, high-gradient magnetic field in roller or drum separators with a rare-earth permanent magnet, while discarding the magnetic fraction and extracting the non-magnetic fraction as the final product (P), i.e. the synthetic rutile.
EFFECT: invention enables to obtain synthetic rutile with low content of rare-earth and radioactive elements while lowering production costs.
28 cl, 3 dwg, 4 tbl, 4 ex
SUBSTANCE: procedure consists in crushing and crumbling gold containing ore to size 60 % of class minus 0.063 mm, in gravitation concentration in centrifugal concentrators with successive refinement of crude gold containing concentrate on tables concentrators to production of gold containing concentrate. Collective copper concentrate is extracted from gravitation rejects by collective flotation of sulphide and oxidised minerals of copper. Collective copper concentrate is subjected to leaching at mixing with water solution of sulphuric acid at concentration not less 2 g/l with ozone at concentration in ozone-oxygen gas mixture over 85 g/l, hydrogen peroxide and ions of oxidised iron with concentration not less 2 g/l. Further, solid phase of concentrate leaching is dehydrated and washed, copper is extracted from copper containing solutions and copper and silver are extracted by flotation from solid phase of concentrate leaching.
EFFECT: increased extraction of metals from gold containing sulphide-oxidised copper ore.
6 cl, 2 dwg, 1 tbl, 1 ex
SUBSTANCE: procedure for extraction of rhenium consists in leaching rhenium from catalyst with diluted solution of sulphuric acid, in sorption of rhenium on low-base anionite and in its de-sorption with solution of ammonia. Also, sodium thiosulphate at amount of 0.002-0.01 mole/l is added into diluted solution of sulphuric acid before rhenium leaching. Upon rhenium extraction non-dissolved residue is directed to extraction of platinum by known procedures.
EFFECT: reduced expenditures for extraction and purification of rhenium; reduced amount of platinum in material-in-process due to reduced extraction of platinum into solution of selective rhenium leaching.
1 tbl, 2 ex
SUBSTANCE: procedure for processing mixed copper ore consists in ore crushing and crumbling. Further, crumbled ore is leached with solution of sulphuric acid of concentration 10-40 g/dm3 and mixed during 10-60 min at contents of solid phase 10-70 %. Upon leaching cake of ore leaching is dehydrated and flushed. Further, flush water is added to a liquid phase of ore leaching and solid suspensions are released from joined copper containing solution. Copper is extracted from copper containing solution and there is produced cathode copper. Flotation of copper minerals from leaching cake is performed at value of pH 2.0-6.0 and there is produced flotation concentrate.
EFFECT: raised extraction of copper into commodity products, reduced consumption of reagents for flotation, increased rate of flotation, and reduced expenditures for crumbling.
8 cl, 1 dwg, 2 ex
SUBSTANCE: procedure for processing sulphide mineral products using bacteria for extraction of metals consists in vat leaching crumbled sulphide mineral products in not less, than two serially connected vats and in mixing with solution of sulphuric acid at value of pH below 1.8, contents of solid phase 10-60%, concentration of ions of trivalent iron over 3 g/l, and temperature 50-99°C. Pulp is withdrawn from the last vat, is divided into solid and liquid phases and solid phase is returned to leaching into the first vat. Bacterial oxidation of iron in a liquid phase is performed in a separate reactor at value of pH 1.4-2.2, and temperature to 90°C with aeration and with addition of elements for bacteria feeding. Upon iron oxidation liquid phase is returned to the leaching vats. Metals are extracted from leaching phases.
EFFECT: increased extraction of metals and rate of process.
11 cl, 1 dwg, 2 ex
SUBSTANCE: procedure for extracting metals of platinum group consists in sulphatisation of source raw stock using oxidant and in successive water leaching. As source raw stock there are used chromites. Chromites are sulphidised at liquid: solid ratio =4:1-6:1 in water solution of sulphuric acid with concentration 85-93 % wt at temperature 150-170°C. As oxidant there is used chromium oxide CrO3 taken at amount of 70-80 % wt of iron contents in chromite.
EFFECT: raised complexity of raw stock utilisation and increased extraction of platinum metals.
1 tbl, 5 ex
SUBSTANCE: procedure consists in processing wastes with sulphuric acid at raised temperature, in supplying hydrogen peroxide, in introducing rhenium, nickel and cobalt into leaching solution and in concentrating tungsten, niobium and tantalum in insoluble residue. Further, solution is separated from insoluble residue; extraction of rhenium from solution is leached with secondary aliphatic alcohol. Extract is washed and rhenium is re-extracted with leaching solution upon extraction. Hydrogen peroxide is supplied after main part of nickel and cobalt have passed into solution at maintaining redox potential in interval of 0.50-0.75 V relative to a saturated chlorine-silver electrode, while extraction of rhenium, extract washing and rhenium re-extraction are carried out on 2-5 steps.
EFFECT: increased extraction of rhenium at reduced consumption of oxidant, increased safety of procedure due to separated in time operations followed with release of hydrogen and oxygen.
6 cl, 4 ex
SUBSTANCE: procedure consists in underground leaching nickel with solution of sulphuric acid and in pumping product solution out. Further, acidity of product solution is reduced, and nickel is sorbed on ionite resin with its following desorption. Upon desorption raffinate of nickel sorption is made-up with sulphuric acid and directed to leaching as leaching solution. Also, excessive sulphuric acid is sorbed on separate ionite with following desorption for reduction of product solution acidity. Upon nickel sorption raffinate is made-up with sulphuric acid and with sulphuric acid after operation of its desorption.
EFFECT: simplification of process, increased ecological safety and reduced consumption of sulphuric acid.
1 dwg, 1 tbl
SUBSTANCE: method involves leaching using an aqueous leaching agent containing sulphuric acid. The leaching agent also contains one or more alkane sulphonic acids with a propyl, ethyl or methyl residue, in weight ratio of alkane sulphonic acid to sulphuric acid between 1:1000 and 1:1 and/or a mixture of one or more salts of alkane sulphonic acids with a propyl, ethyl or methyl residue and sulphuric acid in weight ratio of the salt of alkane sulphonic acid to sulphuric acid between 1:9 and 1:99. Concentration of sulphuric acid in the leaching agent is between 0.1 wt % and 50 wt %. The leaching agent contains 0.001-50 wt % alkane sulphonic acid. The metal-containing compound contains copper, titanium, CaF2, zinc, lead, molybdenum, antimony, bismuth, mercury, cobalt, nickel, aluminium, lanthanum, lanthanide or uranium. The leaching agent can contain one or more nonionic, anionic, cationic or amphoteric surfactants.
EFFECT: high output of metal ions into the solution.
13 cl, 4 tbl, 2 ex
SUBSTANCE: procedure consists in sulphuric acid leaching of uranium. Also source material of 0.1-0.3 mm dimension is subjected to sulphuric acid leaching in autoclave till over 95% of uranium is transited to solution and till degree of pyrite oxidation reaches not less, than 50%. Upon separation of uranium containing solution from a solid phase in form of a cake the latter is conditioned by flotation of valuable metals with sulphydric collector and oxy-ethylated compound at pH 2.5-7.0 thus producing concentrate of valuable metals.
EFFECT: high degree of decomposition of persistent minerals of uranium and pyrite oxidation associating silver and gold and efficient extraction of uranium into water phase and valuable metals into floated concentrate.
17 cl, 1 dwg, 7 tbl, 5 ex
SUBSTANCE: conversion method of non-ferrous metal salt involves counterflow extraction of metal from solution of its converted salt with the use as cation-exchange extractant in salt form of solution of organophosphorus acid in inert diluter and re-extraction of non-ferrous metal with converting acid so that re-extract containing converted salt of non-ferrous metal is obtained. As non-ferrous metal there used is cobalt or nickel; extraction is performed from solution of converted salt of cobalt or nickel at concentration of cobalt or nickel in solution 65-80 g/l and pH 4-7 with the use as cation-exchange extractant of 20-50% solution of organophosphorus acid in sodium, potassium or ammonia form. Re-extraction is performed with 0.5-2.0 M solution of converting acid. Number of non-ferrous metals to which the proposed method is applied can also include copper and zinc.
EFFECT: increasing conversion degree at minimum content of impurities and enlarging the range of obtained salts of non-ferrous metals.
5 cl, 8 ex
SUBSTANCE: procedure consists in electrolysis with asymmetrical alternate current of 50 Hz frequency at heating in alkali medium. Electrolysis is carried out at density of current of anode and cathode half-periods 2.5 A/cm2 and 0.5…2 A/cm2 correspondingly, while size of parts of produced nickel oxide is 9…20 nm.
EFFECT: production of ultra-micro-dispersed powder of nickel oxide applicable for usage in catalytic production of nano carbon materials by pyrolysis of hydrocarbon raw stock.
2 cl, 4 ex
SUBSTANCE: procedure for production of nano-structured agglomerate of metal cobalt consists in interaction of solutions of cobalt salt of general formula CoX2, where X2 are chlorides, nitrates and/or sulphides with reagents and in reduction at higher temperature. A stabilising agent is introduced into solution before reaction of solutions of cobalt salts with reagents. As a stabilising agent there is used sodium-potassium tartrate. Simultaneously introduced alkali in form of NaOH or KOH are used as reagents at interaction and reduction, while as a reducing agent there is used hydrazine hydrate.
EFFECT: production of new nano structured fractal agglomerates of metal cobalt by simple method under soft process conditions; production of target product of high purity.
7 cl, 4 dwg, 5 ex
SUBSTANCE: procedure consists in sorption of cobalt on complex forming ionite from manganese containing solution and of desorption of cobalt from ionite. Desorption of cobalt is performed with solution with pH value=4.5÷5.5 containing ions of copper and(or) nickel possessing higher affinity to functional groups of ionite, than cobalt.
EFFECT: reduced amount of solution processing stages, reduced consumption of reagents and process equipment, increased efficiency and reduction of process cost.
1 dwg, 1 ex
SUBSTANCE: there are performed following stages: ore leaching at presence of hydrochloric acid with formation of soluble chloride of metal in solution for leaching, addition of sulphuric acid and/or sulphur dioxide into solution for leaching, regeneration of solid sulphate of metal or sulphate of metal from solution for leaching, regeneration of hydrochloric acid and continuous transformation of at least part of hydrochloric acid from solution into vaporous phase. Further, vaporous hydrochloric acid is absorbed and returned to the leaching stage. The sulphuric acid and/or sulphur dioxide are added to solution for leaching during process of leaching or after it. Valuable metal is usually chosen from group including Zn, Cu, Ti, Al, Cr, Ni, Co, Mn, Fe, Pb, Na, K, Ca, metals of platinum group and gold. Metal in sulphate of metal or sulphite of metal corresponds to valuable metal or less valuable metal in comparison with metal leached from ore, for example, magnesium.
EFFECT: raised efficiency of procedure.
14 cl, 27 dwg, 1 tbl
SUBSTANCE: procedure consists in following stages: ore leaching at presence of hydrochloric acid with production of soluble metal chloride in solution for leaching, addition of sulphuric acid into solution for leaching, extraction of metal sulphate from solution for leaching and regeneration of hydrochloric acid. As ore there is used oxide ore of non-ferrous metal, such as oxide zinc ore, laterite nickel ore such as saprolite or limonite, sulphide ore or titanium ore. Valuable metal is chosen from group including Zn, Cu, Ti, Al, Cr, Ni, Co, Mn, Fe, Pb, Na, K, Ca, metals of platinum group and gold. Valuable metal or less valuable metal, such as magnesium, can be metal in composition of metal sulphite. Regenerated hydrochloric acid is directed into re-circulation system into process of leaching.
EFFECT: raised efficiency of procedure.
40 cl, 36 dwg, 5 tbl
SUBSTANCE: procedure for processing final tailings of galvanic production consists in crumbling, leaching, separation of solution from sedimentation and in extracting heavy non-ferrous metals from produced solution. Also, final tailings are crumbled with mechanic-chemical activation by wet crumbling in form of pulp suspension at pH≤3 and ratio s (solid): l (liquid) = 1:(0.4-1) and temperature 60-90°C.
EFFECT: reduced harmful environmental impact and power expenditures due to elimination of thermal treatment stage at processing final tailings; raised efficiency of extraction of heavy metal compounds.
3 tbl, 1 ex
SUBSTANCE: there are used soluble and insoluble anodes connected to separate sources of current for control over soluble anode dissolution during process of electrolysis and concentration of ions of metal in solution by means of correcting ratio of anode strengths of current of soluble and insoluble anodes at constant value of cathode density of current. Also, constant value of cathode density of current is achieved by constant area of cathode and sum of current strength on the soluble and insoluble anodes.
EFFECT: avoiding labour-intense operation of correction of electrolyte due to equalising cathode and anode current outputs at production of powders of metal.
8 dwg, 3 ex
SUBSTANCE: procedure consists in leaching at atmospheric or raised pressure, in production of effluent and in utilisation of ion-exchanging resins for absorption and extraction of nickel and cobalt. Before extraction of nickel and cobalt effluent in form of solution or pulp is treated with cation or chelate resin possessing selectivity relative to extraction of iron, aluminium and copper for their removal; it also increases pH of solution.
EFFECT: elimination of neutralisation stage of solution, efficient purification of effluent, prevention of nickel losses and avoiding division of solid and fluid phase of formed pulp at laterite ore leaching.
6 cl, 2 dwg
SUBSTANCE: procedure consists in leaching with chloride solution at supply of chlorine, in purification of solution from copper and in production of copper sulphide cake, in extracting concentrate of precious metals and in electro-extraction of nickel from solution. Prior to leaching matte is separated to a sulphide and metallised fractions. The sulphide fraction is subjected to leaching with chloride solution with supply of chlorine. The metallised fraction produced at separation of matte is added into pulp produced at leaching thus performing purification of solution from copper and its withdrawal to copper sulphide cake. Upon purification of solution from copper solution is purified from iron, zinc and cobalt. Copper sulphide cake is roasted and produced cinder is leached. Solution is directed to electro-extraction of copper, while concentrate of precious metals and chamber product are extracted from residue by flotation.
EFFECT: reduced material and operational expenditures and losses of non-ferrous and precious metals.
2 cl, 12 ex, 2 dwg
FIELD: metallurgy, in particular complex metal recovery from oxidized ore.
SUBSTANCE: claimed method includes granulation with sulfuric acid. Obtained granules are sulfated at 250-4500C for 1-2 h in one or two steps. Then leaching of nickel and other metal sulfates are carried out followed by metal recovery using known methods. Invention is useful in reprocessing of oxidized nickel-cobalt ores, as well as laterite ores containing nickel, cobalt, and copper, and iron-manganese nickel-containing nodules.
EFFECT: high yield nickel recovery; inexpensive and usable equipment.
3 cl, 3 tbl, 4 ex