CN105063352A - Limonite hydrometallurgy process - Google Patents
Limonite hydrometallurgy process Download PDFInfo
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- CN105063352A CN105063352A CN201410845323.0A CN201410845323A CN105063352A CN 105063352 A CN105063352 A CN 105063352A CN 201410845323 A CN201410845323 A CN 201410845323A CN 105063352 A CN105063352 A CN 105063352A
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Abstract
The present invention discloses a limonite hydrometallurgy process, and belongs to the field of metallurgy. According to the process, washing grading is performed on limonite to obtain high-silicon-magnesium ore and low-silicon-magnesium and high-iron ore; the high-silicon-magnesium ore slurry and sufficient concentrated sulfuric acid are concurrently added to a twin screw material pushing reactor so as to dissolve most of soluble non-ferrous metals and soluble iron; solid-liquid separation is performed to obtain normal pressure leaching residue and a normal pressure leaching solution; the normal pressure leaching solution and the low-silicon-magnesium and high-iron ore slurry are added to a pressurization kettle according to a certain ratio to be subjected to pressurization leaching; solid-liquid separation is performed to obtain pressurization leaching residue and a pressurization leaching solution; and the pressurization leaching solution filtrate is purified to obtain the iron fine powder product. According to the present invention, the process has advantages of high nickel and cobalt leaching rate, low sulfuric acid consumption, short reaction time and high production efficiency; the pressurization leaching equipment is the medium-low pressure equipment, such that the disadvantages of high price and easy scaling of the high pressure kettle are avoided; and the main component iron in the ore can be economically and effectively recovered and effectively utilized, and the waste residue is less.
Description
Technical field
The high silicon magnesium ore deposit composition that the present invention relates to limonite carries out sulfuric acid normal pressure leaching and with normal pressure leaching liquid, low silicon magnesium height ferrous components is carried out to the technique of pressure leaching, belongs to field of metallurgy, specifically a kind of hydrometallurgical processes of limonite.
Background technology
Laterite is by nickeliferous peridotites at the torrid zone or the nickel oxide ore that goes bad through extensive long-term weathering leaching of subtropical zone, and owing to there is the difference of geographical position, weather condition and rate of decay, laterite type is all over the world incomplete same.
Efflorescence generally produces bedded deposit, wherein also exists completely or sedentary product the most thoroughly near surface, along with degree of depth increase fades to the lighter sedentary product of degree, and finally terminates as unweathered rock at certain darker depth.
Most of nickel that height waste mantle is contained usually is trickle to be distributed in pyrrhosiderite particle in small, broken bits.This layer is commonly referred to limonite, and it generally contains silicon and the magnesium of a high proportion of iron and low ratio.
Under normal circumstances, limonite is the chief component of red soil nickel ore, accounts for 65% ~ 75% of laterite total amount; Saprolite accounts for 15% ~ 25%; Transition ore deposit accounts for 10%.
The where the shoe pinches reclaiming nickel (cobalt) from laterite nickel is, usually not by the useful component of the abundant enriching nickel of physics mode before carrying out chemical treatment separating metal useful component (as nickel and cobalt), namely cannot carry out enrichment by the technology of ore dressing, this makes the processing cost of red soil nickel ore very high.And due to different mineral and chemical constitution in limonite and saprolite ore deposit, these ores are unsuitable for using same treatment technology to process usually.Finding the method for the cost reducing process red soil nickel ore in decades always.
The treatment process of red soil nickel ore can be divided into thermal process and the large class of wet processing two.Fire metallurgy process is applicable to process saprolite ore deposit.This technique can only produce ferronickel usually, can not Call Provision, and its application is restricted.Hydrometallurgical processes is applicable to process limonite.Hydrometallurgical technology comprise high pressure acidleach and reducing roasting ammonia leaching and occur in recent years as normal pressure acidleach, heap leaching method etc.
In a word, in the patent of invention of laterite nickel ore hydrometallurgical, the shortcoming of the high pressure acid leaching process of high pressure acidleach (HPAL) technique and improvement is: need the autoclave of complicated high temperature, high pressure and relevant equipment, its I&M is all very expensive; The sulfuric acid of HPAL processes expend is more than the sulfuric acid needed for the non-ferrous metal components stoichiometrically dissolved in ore.The shortcoming of the normal pressure acid leaching process of normal pressure acid leaching process and improvement is: sulfuric acid consumption is high; Nickel, cobalt leaching yield are low; Long reaction time, required equipment is huge.It is that to leach the quantity of slag large that high pressure acidleach comprises common drawback that the high pressure acid leaching process of improvement and normal pressure acid leaching process comprise the normal pressure acid leaching process of improvement, and is the mixing slag of silicon and iron, and the main component iron of laterite can not cost-effectively be developed.Although be referred to the recycling of leached mud in the patent of invention of CN102206749A, but because the silicon-dioxide in slag and ferric oxide, pyrrhosiderite etc. are the fine particles of reaction generation, their mutual " growths " together, be difficult to by methods such as simple magnetic separation, they are separated, therefore the economic benefit of above-mentioned leached mud exploitation is very poor, useless solid process can only be worked as, even must work as danger waste residue for the leached mud that nickel leaching yield is lower and process.
Summary of the invention
The present invention seeks to the shortcoming eliminating or alleviate high pressure Ore Leaching technique, obtain the nickel higher than known normal pressure leaching technique and the cobalt rate of recovery simultaneously and reclaim speed faster, the acid consumption lower than high pressure acidleach.Particularly in technological process, very naturally easily the main component ironworking of laterite is become Iron concentrate, make waste residue amount be reduced to about 1/10th of raw ore amount.
For achieving the above object, the hydrometallurgical processes of a kind of limonite of the present invention, implementation step is as follows:
A. get limonite ore washing classification, mineral thicker for the particles such as the gravel in limonite, sandstone are separated from raw ore, obtain high silicon magnesium ore and low silicon magnesium ore;
B. high silicon magnesium ore is added water and prepare high silicon magnesium ore ore pulp, stand-by;
C. in duplex pusher reactor, synchronously add high silicon magnesium ore ore pulp that step b prepares be heated to 60 ~ 100 DEG C and enough high-concentration inorganic acids are heated to 150 ~ 200 DEG C, total overall reaction used time 10min is released upon mixing by duplex pusher reactor, the material released by duplex pusher reactor is loose cellular solid-state lotion, stand-by;
What d. obtained by step c carries out simple crushing in loose cellular solid-state lotion, and fragmentation is fallen back in leaching tank, adds the water with loose cellular solid-state lotion equal weight, carries out water-soluble step, stirs 25 ~ 35min;
E. water-soluble step gained slurry is pumped into plate-and-frame filter press and carry out solid-liquid separation and residue washing, obtain normal pressure acidleach filter residue A, normal pressure acidleach liquor B and washings E;
F. take the low silicon magnesium ore that step a obtains, add after washings E is mixed with low silicon magnesium ore ore pulp and move in autoclave, then in autoclave, add normal pressure acidleach liquor B, make solution ph be 0.5 ~ 1.5; Controlling its temperature range after sealing pressing still is 150 ~ 240 DEG C, stops heating and cooling after continuing thermostatically heating 30 ~ 60min; From autoclave, shift out reaction paste after being cooled to 80 DEG C carry out solid-liquid separation and wash filter residue, obtain pressure leaching slag C, pressureleaching solution D and washings F;
G. get 300g pressure leaching slag C to add in the container filling 1000ml, 10% sodium carbonate solution, be heated to 25 ~ 60 DEG C and stir 10 ~ 30min; Solid-liquid separation washing leaching cake, oven dry, obtain rhombohedral iron ore G.
During described limonite ore washing classification, by ore reduction to 80 order.
The weight percent of the high silicon magnesium ore ore pulp in described step and low silicon magnesium ore ore pulp is 50 ~ 60wt%.
Described high-concentration inorganic acid to be concentration be 98% sulfuric acid.
After described step f sealing pressing still, control temperature heating is preferably 210 ~ 240 DEG C.
During described step f reaction, pH value is preferably 1.0.
In described wherein step e, normal pressure leaching slag A is white residue, and its dioxide-containing silica is 65 ~ 90%.
Obtaining pressure leaching slag C in described wherein step f is rhombohedral iron ore slag, and wherein iron level is 58 ~ 65%.
The hydrometallurgical processes of a kind of limonite of the present invention, its beneficial effect is: this technique is carried out under 1.5 ~ 3.0MPa by pressure leaching, and pressure condition is gentle, such that technological operation is simple, maintenance of the equipment is simple, the time used is short, efficiency is high; And do not need separately to add sulfuric acid in limonite pressure leaching stage, sulfuric acid consumption is low; Pressure leaching is medium/low-voltage equipment, avoids the shortcoming of autoclave apparatus expensive, easily fouling; Fe in normal pressure leaching liquid
3+rhombohedral iron ore is all generated and a small amount of silicon becomes leaching residue with the iron in low silicon magnesium height iron ore, after solid-liquid separation, in pressure leaching slag, iron level is higher, can reach 58 ~ 65%, makes subsequent production simple process, waste residue amount is few and can effectively utilize, and achieves and utilizes the Efficient Development of limonite.
Accompanying drawing explanation
Fig. 1 is process flow sheet of the present invention.
Embodiment
Below in conjunction with the accompanying drawing in the embodiment of the present invention, be clearly and completely described the technical scheme in the embodiment of the present invention, obviously, described embodiment is only the scope of the bright protection of the present invention.
Embodiment 1
One, get limonite ore washing classification, mineral thicker for the particles such as the gravel in limonite, sandstone are separated from raw ore, obtain high silicon magnesium ore and low silicon magnesium ore;
Two, by+80 objects 2
#the high silicon magnesium ore deposit 500kg 500kg that adds water prepares the ore pulp of 50wt%, stand-by;
Three, in duplex pusher reactor, synchronously add the ore pulp being heated to 60 DEG C that the 450kg98% vitriol oil being heated to 150 DEG C and step 2 prepare 50wt%, total overall reaction used time 10min is released upon mixing by duplex pusher reactor, the material released by duplex pusher reactor is loose cellular solid-state lotion, stand-by;
What four, step 3 obtained carries out simple crushing in loose cellular solid-state lotion, and fragmentation is fallen back in leaching tank, adds the water with loose cellular solid-state lotion equal weight, carries out water-soluble step, stirs 10min;
Five, water-soluble step gained slurry is pumped into plate-and-frame filter press and carry out solid-liquid separation and residue washing; Obtain normal pressure acidleach filter residue (A1) 175kg, normal pressure acidleach filtrate (B1) 1480L and washings (E1) 1130L; The composition of above-mentioned raw materials is in Table 1-1, table 1-2 and table 1-3;
Six ,+80 orders 3 that step one obtains are taken
#low silicon magnesium ore deposit 4000g, adds after washings 8000ml is mixed with 60wt% ore pulp and moves in autoclave, then in autoclave, add the obtained normal pressure acidleach liquor B 3000ml of step 5, makes solution ph be 0.5; After sealing pressing still, control pressure is 1.5MPa, stops heating and cooling after continuing thermostatically heating 55min when control temperature is 225 DEG C; From autoclave, shift out reaction paste after being cooled to 80 DEG C carry out solid-liquid separation and wash filter residue, obtain pressure leaching slag (C1) 3600g, pressureleaching solution (D1) 9380ml and washings (F1) 5460ml; The C1 composition of above-mentioned raw materials in Table 1-4, D1 composition in Table 1-5;
Seven, get 300g pressure leaching slag (C1) to add in the container filling 1000ml, 10% sodium carbonate solution, be heated to 60 DEG C and stir 30min; Solid-liquid separation washing leaching cake, oven dry, obtain rhombohedral iron ore (G1) 290g.
The 1# ore used in described embodiment is from laterite mineral deposit, New Caledonia, and washing classification obtains 2# and 3# ore; 4# ore is from Philippines's laterite mineral deposit, and washing classification obtains 5# and 6# ore.The main component of ore is in table 1.
To sum up experimental data draws, based on the component content of residue, calculates nickel, cobalt leaching yield, slag rate and acid consumption data as follows:
Normal pressure acidleach nickel leaching yield: 98.78%; Normal pressure acidleach cobalt leaching yield: 97.66.
Pressure leaching nickel leaching yield: 95.11%; Pressure leaching cobalt leaching yield: 93.07.
Amount to nickel leaching yield 95.78%; Cobalt leaching yield 94.00%.
Iron recovery >96%.
Sulfuric acid consumption: 180Kg sulfuric acid/t ore deposit.
Amount to slag rate: 70.0g white residue/1000g laterite.
Embodiment 2
One, get limonite ore washing classification, mineral thicker for the particles such as the gravel in limonite, sandstone are separated from raw ore, cross 80 mesh sieves, obtain+80 object ores and-80 object ores;
Two, by+80 orders 5
#high silicon magnesium ore deposit adds water and prepares the ore pulp of 50wt%, stand-by;
Three, in duplex pusher reactor, synchronously add the ore pulp being heated to 60 DEG C that the 450kg98% vitriol oil being heated to 150 DEG C and step 2 prepare 50wt%, total overall reaction used time 10min is released upon mixing by duplex pusher reactor, the material released by duplex pusher reactor is loose cellular solid-state lotion, stand-by;
What four, step 3 obtained carries out simple crushing in loose cellular solid-state lotion, and fragmentation is fallen back in leaching tank, adds the water with loose cellular solid-state lotion equal weight, carries out water-soluble step, stirs 30min;
Five, water-soluble step gained slurry is pumped into plate-and-frame filter press and carry out solid-liquid separation and residue washing; Obtain normal pressure acidleach filter residue (A2) 220kg, normal pressure acidleach filtrate (B2) 1490kg and washings (E2) 1100L;
Six, take the low silicon magnesium ore deposit 4000g of+80 order 6# that step one obtains, add after washings 8000ml is mixed with 60wt% ore pulp and move in autoclave, then in autoclave, add the obtained normal pressure acidleach liquor B 3000ml of step 5, make solution ph be 1.5; After sealing pressing still, control pressure is 2.0MPa, stops heating and cooling after continuing thermostatically heating 60min when control temperature is 228 DEG C; From autoclave, shift out reaction paste after being cooled to 80 DEG C carry out solid-liquid separation and wash filter residue, obtain pressure leaching slag (C2) 3150g, pressureleaching solution (D2) 9370ml and washings (F2) 5480ml; F2 composition is in Table 2-6;
Seven, get 300g pressure leaching slag (C2) to add in the container filling 1000ml, 10% sodium carbonate solution, be heated to 60 DEG C and stir 30min; Solid-liquid separation washing leaching cake, oven dry, obtain rhombohedral iron ore (G2) 296g; Rhombohedral iron ore (G2) composition is in Table 2-7.
To sum up experimental data draws, based on the component content of residue, calculates nickel, cobalt leaching yield, slag rate and acid consumption data as follows:
Normal pressure acidleach nickel leaching yield: 99.01%; Normal pressure acidleach cobalt leaching yield: 95.47%.
Pressure leaching nickel leaching yield: 94.74%; Pressure leaching cobalt leaching yield: 92.61%.
Amount to nickel leaching yield 95.37%; Cobalt leaching yield 93.17%.
Iron recovery >96%.
Sulfuric acid consumption: 180Kg sulfuric acid/t ore deposit.
Amount to slag rate: 88.0g white residue/1000g laterite.
Embodiment 3
One, get limonite ore washing classification, mineral thicker for the particles such as the gravel in limonite, sandstone are separated from raw ore, cross 80 mesh sieves, obtain+80 object ores and-80 object ores;
Two, by+80 objects 2
#the high silicon magnesium ore deposit 500kg 500kg that adds water prepares the ore pulp of 50wt%, stand-by;
Three, in duplex pusher reactor, synchronously add the ore pulp being heated to 60 DEG C that the 450kg98% vitriol oil being heated to 150 DEG C and step 2 prepare 50wt%, total overall reaction used time 10min is released upon mixing by duplex pusher reactor, the material released by duplex pusher reactor is loose cellular solid-state lotion, stand-by;
What four, step 3 obtained carries out simple crushing in loose cellular solid-state lotion, and fragmentation is fallen back in leaching tank, adds the water with loose cellular solid-state lotion equal weight, carries out water-soluble step, stirs 10min;
Five, water-soluble step gained slurry is pumped into plate-and-frame filter press and carry out solid-liquid separation and residue washing; Obtain normal pressure acidleach filter residue (A3) 175kg, normal pressure acidleach filtrate (B3) 1480L and washings (E3) 1130L; The composition of above-mentioned raw materials is in Table 1-1, table 1-2 and table 1-3;
Six ,+80 orders 6 that step one obtains are taken
#low silicon magnesium ore deposit 4000g, adds after washings 8000ml is mixed with 60wt% ore pulp and moves in autoclave, then in autoclave, add the obtained normal pressure acidleach liquor B 3000ml of step 5, makes solution ph be 1.0; After sealing pressing still, control pressure is 3.0MPa, stops heating and cooling after continuing thermostatically heating 60min when control temperature is 225 DEG C; From autoclave, shift out reaction paste after being cooled to 80 DEG C carry out solid-liquid separation and wash filter residue, obtain pressure leaching slag (C3) 3190g, pressureleaching solution (D3) 9390ml and washings (F3) 5420ml; The composition of above-mentioned raw materials is in Table 3-1, table 3-2 and table 3-3;
Seven, get 300g pressure leaching slag (C3) to add in the container filling 1000ml, 10% sodium carbonate solution, be heated to 60 DEG C and stir 30min; Solid-liquid separation washing leaching cake, oven dry, obtain rhombohedral iron ore (G3) 299g.Rhombohedral iron ore (G3) composition is in Table 3-4.
To sum up experimental data draws, based on the component content of residue, calculates nickel, cobalt leaching yield, slag rate and acid consumption data as follows:
Pressure leaching nickel leaching yield: 95.36%; Pressure leaching cobalt leaching yield: 93.34%.
Amount to nickel leaching yield 95.97%; Cobalt leaching yield 94.71%.
Iron recovery >96%.
Sulfuric acid consumption: 180Kg sulfuric acid/t ore deposit.
Amount to slag rate: 70.0g white residue/1000g laterite.
Embodiment 4
One, get limonite ore washing classification, mineral thicker for the particles such as the gravel in limonite, sandstone are separated from raw ore, cross 80 mesh sieves, obtain+80 object ores and-80 object ores;
Two, by+80 orders 5
#high silicon magnesium ore deposit adds water and prepares the ore pulp of 50wt%, stand-by;
Three, in duplex pusher reactor, synchronously add the ore pulp being heated to 60 DEG C that the 450kg98% vitriol oil being heated to 150 DEG C and step 2 prepare 50wt%, total overall reaction used time 10min is released upon mixing by duplex pusher reactor, the material released by duplex pusher reactor is loose cellular solid-state lotion, stand-by;
What four, step 3 obtained carries out simple crushing in loose cellular solid-state lotion, and fragmentation is fallen back in leaching tank, adds the water with loose cellular solid-state lotion equal weight, carries out water-soluble step, stirs 30min;
Five, water-soluble step gained slurry is pumped into plate-and-frame filter press and carry out solid-liquid separation and residue washing; Obtain normal pressure acidleach filter residue (A2) 220kg, normal pressure acidleach filtrate (B2) 1490kg and washings (E2) 1100L;
Six, take the low silicon magnesium ore deposit 4000g of+80 order 3# that step one obtains, add after washings 8000ml is mixed with 50wt% ore pulp and move in autoclave, then in autoclave, add the obtained normal pressure acidleach liquor B 3000ml of step 5, make solution ph be 1.5; After sealing pressing still, control pressure is 4.0MPa, stops heating and cooling after continuing thermostatically heating 60min when control temperature is 230 DEG C; From autoclave, shift out reaction paste after being cooled to 80 DEG C carry out solid-liquid separation and wash filter residue, obtain pressure leaching slag (C4) 3510g, pressureleaching solution (D4) 9360ml and washings (F4) 5490ml; The composition of above-mentioned raw materials is in Table 4-1, table 4-2 and table 4-3;
Seven, get 300g pressure leaching slag (C4) to add in the container filling 1000ml, 10% sodium carbonate solution, be heated to 60 DEG C and stir 30min; Solid-liquid separation washing leaching cake, oven dry, obtain rhombohedral iron ore (G4) 293g; Rhombohedral iron ore (G4) composition is in Table 4-4.
To sum up experimental data draws, based on the component content of residue, calculates nickel, cobalt leaching yield, slag rate and acid consumption data as follows:
Pressure leaching nickel leaching yield: 94.76%; Pressure leaching cobalt leaching yield: 93.02%.
Amount to nickel leaching yield 95.36%; Cobalt leaching yield 93.28%.
Iron recovery >96%.
Sulfuric acid consumption: 180Kg sulfuric acid/t ore deposit.
Amount to slag rate: 88.0g white residue/1000g laterite.
In above embodiment, embodiment 1 and the embodiment 2 high silicon magnesium ore deposit in the limonite of same mineral deposit and the combination of low silicon magnesium ore deposit; Embodiment 3 and the embodiment 4 high silicon magnesium ore deposit in the limonite of different mineral deposits and the combination of low silicon magnesium ore deposit.From analytical data, the technical indicator such as nickel (cobalt) leaching yield, sulfuric acid consumption etc. of four embodiments is all better, the iron level of the pressure leaching slag that four embodiments obtain is all more than 63%, and the rhombohedral iron ore iron level of recovery is all about 63%, and iron recovery is more than 96%.
The foregoing is only preferred embodiment of the present invention, not in order to limit the present invention, within the spirit and principles in the present invention all, any amendment done, equivalent replacement, improvement etc., all should be included within protection scope of the present invention.
Claims (8)
1. a hydrometallurgical processes for limonite, is characterized in that:
A. get limonite ore washing classification, mineral thicker for the particles such as the gravel in limonite, sandstone are separated from raw ore, obtain high silicon magnesium ore and low silicon magnesium ore;
B. high silicon magnesium ore is added water and prepare high silicon magnesium ore ore pulp, stand-by;
C. in duplex pusher reactor, synchronously add high silicon magnesium ore ore pulp that step b prepares be heated to 60 ~ 100 DEG C and enough high-concentration inorganic acids are heated to 150 ~ 200 DEG C, total overall reaction used time 10min is released upon mixing by duplex pusher reactor, the material released by duplex pusher reactor is loose cellular solid-state lotion, stand-by;
What d. obtained by step c carries out simple crushing in loose cellular solid-state lotion, and fragmentation is fallen back in leaching tank, adds the water with loose cellular solid-state lotion equal weight, carries out water-soluble step, stirs 25 ~ 35min;
E. water-soluble step gained slurry is pumped into plate-and-frame filter press and carry out solid-liquid separation and residue washing, obtain normal pressure acidleach filter residue A, normal pressure acidleach liquor B and washings E;
F. take the low silicon magnesium ore that step a obtains, add after washings E is mixed with low silicon magnesium ore ore pulp and move in autoclave, then in autoclave, add normal pressure acidleach liquor B, make solution ph be 0.5 ~ 1.5; Controlling its temperature range after sealing pressing still is 150 ~ 240 DEG C, stops heating and cooling after continuing thermostatically heating 30 ~ 60min; From autoclave, shift out reaction paste after being cooled to 80 DEG C carry out solid-liquid separation and wash filter residue, obtain pressure leaching slag C, pressureleaching solution D and washings F;
G. get 300g pressure leaching slag C to add in the container filling 1000ml, 10% sodium carbonate solution, be heated to 25 ~ 60 DEG C and stir 10 ~ 30min; Solid-liquid separation washing leaching cake, oven dry, obtain rhombohedral iron ore G.
2. the hydrometallurgical processes of a kind of limonite as claimed in claim 1, is characterized in that: during described limonite ore washing classification, by ore reduction to 80 order.
3. the hydrometallurgical processes of a kind of limonite as claimed in claim 1, is characterized in that: the weight percent of the high silicon magnesium ore ore pulp in described step and low silicon magnesium ore ore pulp is 50 ~ 60wt%.
4. the hydrometallurgical processes of a kind of limonite as claimed in claim 1, is characterized in that: described high-concentration inorganic acid to be concentration be 98% sulfuric acid.
5. the hydrometallurgical processes of a kind of limonite as claimed in claim 1, is characterized in that: after described step f sealing pressing still, control temperature heating is preferably 210 ~ 240 DEG C.
6. the hydrometallurgical processes of a kind of limonite as claimed in claim 1, is characterized in that: during described step f reaction, pH value is preferably 1.0.
7. the hydrometallurgical processes of a kind of limonite as claimed in claim 1, it is characterized in that: in described wherein step e, normal pressure leaching slag A is white residue, its dioxide-containing silica is 65 ~ 90%.
8. the hydrometallurgical processes of a kind of limonite as claimed in claim 1, is characterized in that: obtaining pressure leaching slag C in described wherein step f is rhombohedral iron ore slag, and wherein iron level is 58 ~ 65%.
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| JP2007077459A (en) * | 2005-09-15 | 2007-03-29 | Taiheiyo Kinzoku Kk | Method for recovering nickel or cobalt |
| CN101133171A (en) * | 2005-02-14 | 2008-02-27 | Bhp比利通Ssm技术有限公司 | Process for enhanced acid leaching of laterite ores |
| CN101356292A (en) * | 2005-11-10 | 2009-01-28 | 瓦利·德·利奥多斯公司 | Combined leaching process |
| CN101768665A (en) * | 2008-12-30 | 2010-07-07 | 厦门紫金矿冶技术有限公司 | Method for reducing acid consumption during heap leaching and high-pressure leaching of nickel laterite ore |
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- 2014-12-31 CN CN201410845323.0A patent/CN105063352A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101133171A (en) * | 2005-02-14 | 2008-02-27 | Bhp比利通Ssm技术有限公司 | Process for enhanced acid leaching of laterite ores |
| JP2007077459A (en) * | 2005-09-15 | 2007-03-29 | Taiheiyo Kinzoku Kk | Method for recovering nickel or cobalt |
| CN101356292A (en) * | 2005-11-10 | 2009-01-28 | 瓦利·德·利奥多斯公司 | Combined leaching process |
| CN101768665A (en) * | 2008-12-30 | 2010-07-07 | 厦门紫金矿冶技术有限公司 | Method for reducing acid consumption during heap leaching and high-pressure leaching of nickel laterite ore |
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Application publication date: 20151118 |