CN104611558A - Method for recovering nickel, cobalt, iron and silicon from laterite-nickel ore through united leaching technology - Google Patents
Method for recovering nickel, cobalt, iron and silicon from laterite-nickel ore through united leaching technology Download PDFInfo
- Publication number
- CN104611558A CN104611558A CN201410845411.0A CN201410845411A CN104611558A CN 104611558 A CN104611558 A CN 104611558A CN 201410845411 A CN201410845411 A CN 201410845411A CN 104611558 A CN104611558 A CN 104611558A
- Authority
- CN
- China
- Prior art keywords
- nickel
- iron
- leaching
- cobalt
- limonite
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- 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
Landscapes
- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention discloses a method for recovering nickel, cobalt, iron and silicon from a laterite-nickel ore through a united leaching technology. The method comprises the following steps: adding heated saprolite ore pulp and a concentrated sulfuric acid to a double-helix shoving reactor; dissolving reaction materials into water, performing solid-liquid separation, washing filter residues so as to obtain constant-pressure leached residues, constant-pressure leached liquor and washing liquor; making the washing liquor and the limonite into limonite pulp, heating the limonite pulp and the constant-pressure leached liquor respectively, adding the limonite pulp and the constant-pressure leached liquor which are heated in a pressurized pipeline reactor to be pressurized and leached, hydrolyzing Fe<3+> in the constant-pressure leached liquor so as to release the acid, and then leaching the limonite; lowering the temperature for solid-liquid separation so as to obtain pressurized and leached residues and pressurized and leached liquor; removing impurities which do not belong to the nickel and the cobalt from the pressurized and leached liquor, and recovering the nickel and/or the cobalt by an existing method; washing the pressurized and leached residues through a sodium carbonate solution, and drying the washed pressurized and leached residues so as to obtain powdered iron; sieving and processing the constant-pressure leached residues so as to obtain silicon dioxide and building sand. The method disclosed by the invention has the advantages that the leaching time is short, the leaching efficiency of the nickel is high, the acid consumption is low, and the iron and part of the silicon can be effectively recovered.
Description
Technical field
The present invention relates to the hydrometallurgical processes technical field of red soil nickel ore, be specifically related to a kind of method being reclaimed nickel, cobalt, iron and silicon by combined leaching process from red soil nickel ore.
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.Nickel contained by the layer that weathering is lighter is generally contained in various magnesium silicate minerals more, such as serpentine.A lot of other may be had in incomplete zone of weathering to contain the silicate minerals of nickel.The height of part weathering is commonly referred to saprolite or noumeite containing magnesium ribbon.Its iron generally containing low ratio and a high proportion of silicon and magnesium.In some mineral deposits, also have the another kind of main band containing nontonite clays be usually between limonite and saprolite, be called transition ore deposit." low-grade laterite " refers to the laterite not having saprolite ore deposit, the laterite be namely made up of limonite and transition ore deposit.Under normal circumstances, limonite is the chief component of red soil nickel ore, accounts for the 65%-75% of laterite total amount; Saprolite accounts for 15%-25%; Transition ore deposit accounts for 10%.From red soil nickel ore, reclaim nickel, the where the shoe pinches of cobalt 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 current red soil nickel ore can be divided into thermal process and the large class of wet processing two usually.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.Heap Leaching leaching yield is lower, is only applicable to the laterite processing high Mg content; Reduction roasting-ammonia leaching technique due to energy consumption higher, technical process is long and less to be used; Normal pressure acidleach technological operation is simple, does not need to use expensive autoclave, but it is comparatively large that mineral will be made to dissolve then required sour consumption completely, and containing each metal ion species in leach liquor, makes the follow-up separation circuit that macerates become complicated.High pressure acidleach (HPAL) technique uses sulfuric acid to leach red soil nickel ore under high temperature (250 DEG C) and high pressure (50MPa).Under high temperature, condition of high voltage, the metalliferous mineral in ore almost dissolves completely.The iron dissolved is hydrolyzed to rapidly rhombohedral iron ore (Fe under adopted high temperature
20
3) precipitation, nickel, cobalt etc. stay in the solution, and the leaching residue of iron content and silicon is by a series of washing concentrating after cooling, namely concentrated in so-called counter-current decantation washing (CCD) loop and be separated from the solution of nickeliferous, cobalt.Therefore the main purpose of extract technology is reached--nickel is separated with iron.
The advantage of high pressure Ore Leaching (HPAL) technique is: nickel, cobalt leaching yield are high; Speed of response is fast, the reaction times is short; Iron does not consume sulfuric acid in theory in acidleach process and hydrolysate is rhombohedral iron ore (Fe
20
3) precipitation.But the shortcoming of high pressure Ore Leaching (HPAL) technique is also very outstanding: be first that it needs the autoclave of complicated high temperature, high pressure and relevant equipment, its I&M is all very expensive; Two is that the sulfuric acid of high pressure acidleach (HPAL) processes expend is more than the sulfuric acid needed for the non-ferrous metal components stoichiometrically dissolved in ore.Because most sulfate ion provided by sulfuric acid is connected to form hydrogen sulfate ion (HSO under high pressure acidleach condition
4 -).That is sulfuric acid dissociation under high pressure acidleach condition discharges a proton (H+).Leach liquor cooling and in and time, hydrogen sulfate ion resolves into sulfate radical (SO
4 2-) and another proton.Because after this proton (acid) is inabundant for leaching, and cause excessive sulfuric acid in subsequent disposal to be carried out with and consume neutralizing agent; Three is raw materials that HPAL technique is only limited to that process is mainly limonite class, because the existence of saprolite can cause rolling up of sulfuric acid consumption.This is because the Mg content of magnesium in saprolite is higher caused; Four be HPAL technique in the easy fouling of operational process mesohigh still, need periodic shut down to clear up, working rate is low; Five is leach the quantity of slag greatly, and is the mixing slag of silicon and iron, can not cost-effectively develop.
U.S. Patent No. 4,097,575 describe the improvement to HPAL technique, be included in the high pressure that limonite occurs in described autoclave to leach, the discharge that high pressure leaches be used in less than about 820 DEG C roastings, and the stronger saprolite ore deposit roasting sand of the reactive behavior of sulfuric acid in and excessive acid, the nickel contained in saprolite ore deposit in this N-process dissolves in a large number.The advantage of this technique is that it utilizes the sulfuric acid added in limonite pressure leaching process better, decrease the consumption for the treatment of the Wingdale of autoclave discharge liquid or the neutralization reagent of other costlinesses, and obtain the ability that the limonite component in red soil nickel ore body and saprolite component are processed.But this technique still needs the leaching using expensive autoclave for limonite, and needs to carry out calcination process to saprolite ore deposit, and this treatment process is all very expensive in fund input and running cost.
U.S. Patent No. 6,379,636 B2 describe U.S. Patent No. 4, and 097, the further improvement of the technique described in 575, eliminates saprolite calcination steps, and acid excessive during saprolite raw ore is used for and in autoclave discharge solution.In addition, can add more acid in relief liquor can leaching content with what increase saprolite.But this technique still needs to use expensive autoclave.
In order to avoid using expensive autoclave, developing the laterite nickel resources of saprolite and limonite simultaneously, there has been proposed the normal pressure acidleach technology that some improve.If publication number is the patent of invention of CN101273146A, propose the two step normal pressure leach extraction methods in lixiviate saprolite ore deposit after simultaneously lixiviate limonite and saprolite ore deposit or first lixiviate limonite, this method has the advantage not using autoclave, but propose in the flow process described in this application when processing to remove Fe and/or A1 to infusion solution, to need to add in neutralizing agent and residual acid in leach liquor, most of iron is deposited as ferric hydroxide, and this can cause loss and the slurry filtration difficulty of the valuable elements such as nickel cobalt.And for example publication number is the patent of invention of CN101541985A, proposes the method for the mixture in a kind of normal pressure leaching limonite and saprolite ore deposit, but its iron precipitated product is jarosite, containing sulfate radical in jarosite, therefore can increase the acid consumption of leaching process; And jarosite is a kind of compound of thermodynamic instability, can sulfuric acid be discharged when heap sum is deposited, thus cause environmental pollution.For another example publication number is the patent of invention of CN101006190A, the method of the mixture proposing a kind of concentrated acid process limonite and saprolite ore deposit then water leaching nickel cobalt, the deposition of iron thing that this method produces is ferric oxide except jarosite or oxyhydroxide, but the extraction time of this application needs 12-48h, extraction time is longer, cause process cycle longer, production cost rises.
For another example publication number is the patent of invention of CN102206749A, propose one and first use sulfuric acid leaching limonite, use a leach liquor lixiviate saprolite ore deposit again, rear section (or all) secondary leach liquor return the circulation normal-pressure leaching method once leaching limonite again, the method possesses can process the higher advantage of limonite and saprolite ore deposit and nickel cobalt leaching yield simultaneously, but technical process is comparatively complicated, the shortcoming of sulfuric acid consumption higher (mean value is about 0.7g acid/1.0g ore deposit), and saprolite ore deposit used amount is more than 1.5 times of limonite amount, form with the mine belt of laterite and contradict.For another example publication number is the patent of invention of CN101001964A, propose and a kind ofly first under normal pressure (100 DEG C-105 DEG C), leach limonite with enough sulfuric acid, then use the normal pressure leaching ore pulp of limonite and saprolite ore pulp to leach the method extracting nickel, cobalt under middle pressure (about 0.5MPa, 150 DEG C).The advantage of the method is: can process limonite and saprolite ore deposit simultaneously; Avoid using expensive autoclave and achieve the higher nickel leaching yield in saprolite ore deposit with relatively simple pressure exerting device under middle pressure condition.But the method exists following shortcoming and defect: first the time of normal pressure leaching limonite is longer, be generally more than 4 hours, therefore required normal pressure leaching equipment is huge; Two is that acid consumption is higher, total acid/ore=0.6/1, although this acid consumes index far below normal pressure acidleach far above high pressure acidleach; Three are saprolite ore deposit used amounts is 1 times of limonite amount, and this mine belt that is same and laterite forms and contradicts, it is well known that in red soil nickel ore bed, and limonite amount: saprolite ore deposit measures >=2: 1.
In a word, in the patent of invention of above-mentioned 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; HPAL technique is only limited to the raw material that process is mainly limonite class; HPAL technique is in the easy fouling of operational process mesohigh still, and need periodic shut down to clear up, working rate is low.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 object of the invention is to solve the technical problem existed in prior art, providing a kind of and by combined leaching process sulfuric acid normal pressure leaching carried out to the saprolite ore deposit composition in red soil nickel ore and with normal pressure leaching liquid, limonite component carried out to the method for the recovery nickel of pressure leaching, cobalt, iron and silicon.
In order to achieve the above object, the present invention is by the following technical solutions: a kind of method being reclaimed nickel, cobalt, iron and silicon by combined leaching process from red soil nickel ore, comprise the following steps: (a) adds water obtained saprolite ore pulp in saprolite ore deposit, saprolite ore pulp is heated to 60 DEG C-100 DEG C, the vitriol oil is heated to 150 DEG C-200 DEG C, in duplex pusher reactor, add the saprolite ore pulp after heating and the vitriol oil, react to dissolve solubility non-ferrous metal and soluble iron in saprolite ore deposit; B () carries out water-soluble rear solid-liquid separation to reaction mass and residue washing obtains normal pressure leaching slag (A), normal pressure leaching liquid (B) and washings (E); C () makes limonite slurry with washings (E) and limonite, add in capstan reactor after limonite slurry and normal pressure leaching liquid (B) are heated to 95 DEG C-100 DEG C respectively, pressure be 1.5MPa-4.0Mpa, temperature be the condition of 150 DEG C-240 DEG C under pressure leaching 0.5-1.5 hour, the Fe in normal pressure leaching liquid (B)
3+be hydrolyzed to hematite precipitation and discharge acid and leach limonite again; D () is reduced temperature and carry out solid-liquid separation after 80 DEG C, obtain pressure leaching slag (C) and pressureleaching solution (D); By namely there being method to reclaim nickel and/or cobalt e () removes non-nickel cobalt impurity to pressureleaching solution (D) after; F () obtains Iron concentrate to pressure leaching slag (C) soda ash solution washing post-drying; G () obtains silicon-dioxide and building sand to normal pressure leaching slag (A) through screening process.
Further, in described step (a), the granularity in saprolite ore deposit is-80 orders, and the granularity of limonite is-80 orders.
Further, in described step (a), the mass ratio of saprolite ore deposit and water is 1:1.2-1:1.
Further, in described step (a), the mass ratio of saprolite ore pulp and the vitriol oil is 2:1-2.2:1, and the reaction times is 1-12 minute.
Further, time water-soluble in described step (b), the mass ratio of reaction mass and water is 1:1.2-1:1.
Further, proportioning when washings (E) and limonite make limonite slurry in described step (c) is 2L:1Kg.
Further, in limonite slurry, add normal pressure leaching liquid (B) in described step (c) makes reaction mass final ph be 0.5-1.5.
Further, in described step (f), the massfraction of soda ash solution is 10%, and bake out temperature is 120 DEG C-150 DEG C.
Further, in described step (b), normal pressure leaching slag (A) is white residue, and its dioxide-containing silica is 65%-90%.
Further, obtain pressure leaching slag (C) in described step (d) for rhombohedral iron ore slag, wherein iron level is 58%-65%.
Wherein, the first step is in saprolite acidleach process, the vitriol oil of saprolite ore pulp and q.s fully mixes fast, the heat of dilution that water in the vitriol oil and ore pulp produces makes temperature of charge raise to impel the metal (nickel, cobalt, iron, magnesium, chromium, aluminium etc.) in saprolite ore deposit and sulfuric acid rapid reaction to generate metal sulfate, and a large amount of reaction heat makes temperature of charge be increased to 95 DEG C-120 DEG C further to ensure to react and carry out fully and completely simultaneously.Silicon-dioxide and the unreacted iron of minute quantity and non-ferrous metal are formed and leach residue.Second step is the water-soluble of normal pressure acidleach material and solid-liquid separation process, for some time placed by the normal pressure leaching material of the first step, loose cellular solid-state lotion is formed in temperature-fall period, add the water that can ensure that metal sulfate all dissolves and stir, metal sulfate is all dissolved and enters solution, after carrying out solid-liquid separation and residue washing, obtain normal pressure leaching slag (A), normal pressure leaching liquid (B) and washings (E).3rd step is the process that normal pressure leaching immersion goes out limonite, and normal pressure leaching liquid and limonite slurry are added pressure leaching in autoclave, the Fe in filtrate
3+be hydrolyzed to hematite precipitation and discharge acid and leach limonite again, during reaction, pressure is 1.5MPa-4.0Mpa, temperature of reaction is 150 DEG C-240 DEG C, can not only ensure that the hydrolysate of iron ion is that rhombohedral iron ore also has fast hydrolysis rate and higher nickel cobalt leaching yield and leaching velocity.4th step is lowered the temperature by pressure leaching material and obtains pressure leaching slag (C) and pressureleaching solution (D) after carrying out solid-liquid separation, wherein pressure leaching slag (C) main component is rhombohedral iron ore, iron level is very high, and pressureleaching solution (D) nickel concentration is higher and iron/nickel ratio is lower.
Hinge structure of the present invention has following beneficial effect:
1, achieve and a kind ofly by combined leaching process sulfuric acid normal pressure leaching carried out to the saprolite ore deposit composition in red soil nickel ore and with normal pressure leaching liquid, limonite component carried out to the recovery nickel of pressure leaching, cobalt, the method of iron and silicon, overcome traditional deficiency adopting thermal process and wet processing process respectively, eliminate the shortcoming of existing 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 existing high pressure acidleach, particularly in technological process, very naturally easily the main component ironworking of red soil nickel ore is become Iron concentrate, part silicon is recovered as higher-grade silica product, waste residue amount is made to be reduced to about 5 percent of raw ore amount.Compared with high pressure Ore Leaching (HPAL) technique, pressure leaching of the present invention carries out under 1.5MPa-4.0Mpa, than mild condition many of high pressure acidleach 4.5MPa-5.0MPa, compared with normal pressure acidleach, the normal pressure leaching time of the present invention is 1-12 minute, and existing normal pressure leaching time is generally 240 minutes to 2400 minutes, corresponding normal pressure pickling equipment investment of the present invention is much smaller than existing normal pressure pickling equipment investment.
2, sulfuric acid consumption of the present invention not only consumes far below the acid of existing normal pressure acidleach, and consume lower than the acid of existing high pressure acidleach, the acid consumption of existing normal pressure acidleach is 2.57-3.33 times that the present invention's acid consumes, and the acid consumption of existing high pressure acidleach is 1.39-1.71 times of the present invention's acid consumption.Under high pressure acidleach condition, most sulfate ion provided by sulfuric acid is connected to form hydrogen sulfate ion (HSO
4 -), that is sulfuric acid dissociation under high pressure acidleach condition discharges a proton (H+), leach liquor cooling and in and time, hydrogen sulfate ion resolves into sulfate radical (SO
4 2-) and another proton, because after this proton (acid) is inabundant for leaching, and cause excessive sulfuric acid in subsequent disposal to be carried out and and consume neutralizing agent.And in method of the present invention, although need to consume more sulfuric acid and iron reaction generation ferric sulfate in the saprolite ore deposit normal pressure leaching stage, then do not need separately to add sulfuric acid in limonite pressure leaching stage, but rely on Fe
3+the proton (acid) being hydrolyzed to hematite precipitation release leaches limonite, avoiding problems because of hydrogen sulfate ion (HSO
4 -) and cause the defect that acid-utilising rate is low, and significantly can reduce the consumption of follow-up neutralizing agent.In addition, existing high pressure acid leaching process ore pulp and the vitriol oil is directly added autoclave leach, and in autoclave, regional area sulfuric acid concentration is very high, is easy to generate the fouling such as ferric subsulfate and alum, and the pressure leaching stage of the present invention does not have adding of the vitriol oil, the generation of foulant can be avoided.
3, it is large that existing high pressure acid leaching process and normal pressure acid leaching process leach the quantity of slag, its leached mud is the mixing slag of silicon and iron, can not cost-effectively develop, specifically, due to the silicon-dioxide in leached mud and ferric oxide, pyrrhosiderites etc. are the fine particles that reaction generates, their mutual " growths " together, be difficult to by methods such as simple magnetic separation, they are separated, therefore the economic benefit that the leached mud utilizing existing high pressure acid leaching process and normal pressure acid leaching process to obtain develops 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 to process.And the main component iron in ore deposit and part silicon very naturally can be able to cost-effective recycling easily by method of the present invention in technological process.According to method of the present invention, in the normal pressure leaching stage, in saprolite ore deposit, iron and non-ferrous metal and sulfuric acid reaction generate vitriol and enter solution, silicon forms silicon-dioxide and becomes leaching residue, the 30-50% that the normal pressure leaching quantity of slag only has saprolite ore deposit to measure after solid-liquid separation, the 8-15% accounting for red soil nickel ore total amount, in normal pressure leaching slag, dioxide-containing silica reaches 80-85%; In the pressure leaching stage, the Fe in normal pressure leaching liquid
3+all generate rhombohedral iron ore with the iron in limonite and a small amount of silicon becomes leaching residue, after solid-liquid separation, in pressure leaching slag, iron level is up to 58-65%, and namely simple process can be used as Iron concentrate and sell.
4, nickel leaching yield of the present invention is not only far above the nickel leaching yield of existing normal pressure acidleach, and higher than the nickel leaching yield of existing high pressure acidleach.The nickel leaching yield of existing normal pressure acidleach is 70-85%, and the nickel leaching yield of existing high pressure acidleach is 90-93%, and nickel leaching yield of the present invention is more than 95%.
Accompanying drawing explanation
fig. 1 is schematic flow sheet of the present invention.
Embodiment
Use in following embodiment 1
#, 2
#with 3
#ore from laterite mineral deposit, New Caledonia, 4
#with 5
#ore is from Indonesia's laterite mineral deposit, and the main component of ore is in table 1.Saprolite ore deposit and limonite are broken and be ground to granularity for-80 orders before for experiment.
The main component table of table 1 ore
Below in conjunction with specific embodiment, the invention will be further described.
Embodiment 1
Get 500Kg 2
#saprolite ore deposit (doing) adds 500Kg water and makes saprolite ore pulp, preparing 500Kg massfraction is the vitriol oil of 98%, saprolite ore pulp is heated to 60 DEG C, the saprolite ore pulp after heating and the vitriol oil synchronously to add the opening for feed of duplex pusher reactor by the vitriol oil with mortar pump and vitriol oil pump after being heated to 200 DEG C, saprolite ore pulp and the vitriol oil are forced into rapid reaction in duplex pusher reactor and, to dissolve solubility non-ferrous metal and soluble iron, react and reaction mass is released duplex pusher reactor after 1 minute after short mix.Be cooled to less than 60 DEG C, the reaction mass simple crushing of loose cellular solid-state lotion is fallen back in leaching tank, add 1500Kg water, stirring carries out water-soluble in 30 minutes, water-soluble gained slurry is pumped in plate-and-frame filter press and carries out solid-liquid separation and residue washing, obtain normal pressure leaching slag (A1) 185Kg(do), normal pressure leaching liquid (B1) 1480L and washings (E1) 1200L.The composition of normal pressure leaching slag (A1), normal pressure leaching liquid (B1) and washings (E1) is in Table 1-1, table 1-2 and table 1-3.
Get 30Kg1
#limonite (doing), add washings (E1) 60L and be mixed with limonite slurry, add in the circulation tank of capstan reactor after limonite slurry being heated to 95 DEG C, in the circulation tank of capstan reactor, add the normal pressure leaching liquid (B1) being heated to 95 DEG C again makes reaction mass final ph be 0.5, force (forcing) pump is opened after sealing circulation tank, open the hot oil heater of capstan reactor simultaneously, control temperature heats, pressure be 1.5MPa, temperature be the condition of 240 DEG C under pressure leaching 50 minutes, the Fe in normal pressure leaching liquid (B1)
3+be hydrolyzed to hematite precipitation and discharge acid and leach limonite again; From the circulation tank of capstan reactor, shift out reaction paste after being cooled to 85 DEG C carry out solid-liquid separation and wash filter residue, obtain pressure leaching slag (C1) 28Kg(to do), pressureleaching solution (D1) 76L and washings (F1) 46L, by namely there being method reclaim nickel and/or cobalt after removing non-nickel cobalt impurity to pressureleaching solution (D1).The composition of pressure leaching slag (C1), pressureleaching solution (D1) and washings (F1) is in Table 1-4, table 1-5 and table 1-6.
Get 300g pressure leaching slag (C1) and add that to fill 1000ml massfraction be in the beaker of the soda ash solution of 10%, be heated to 60 DEG C and stir 30 minutes, solid-liquid separation is also dried after washing leaching cake under temperature is 120 DEG C of conditions, obtains rhombohedral iron ore (G1) 295g.Rhombohedral iron ore (G1) composition is in Table 1-7.
Get 300g normal pressure leaching slag (A1) and carry out hydrocyclone separation technology, obtain-100 order silicon dioxide powder (H1) 145g and+100 order fine sand (I1) 150g.Silicon dioxide powder (H1) and fine sand (I1) composition are in Table 1-8 and table 1-9.
Calculate nickel, cobalt leaching yield, slag rate and acid consumption data as follows:
Normal pressure acidleach nickel leaching yield: 98.8%; Normal pressure acidleach cobalt leaching yield: 97.6%.
Pressure leaching nickel leaching yield: 95.6%; Pressure leaching cobalt leaching yield: 94.1%.
Amount to nickel leaching yield 96.9%; Cobalt leaching yield 94.8%.
Iron recovery >96%.
Sulfuric acid consumption: 250Kg sulfuric acid/t ore deposit.
Amount to slag rate: 46g white residue/1000g red soil nickel ore.
Embodiment 2
Get 500Kg 5
#saprolite ore deposit (doing) adds 600Kg water and makes saprolite ore pulp, preparing 500Kg massfraction is the vitriol oil of 98%, saprolite ore pulp is heated to 100 DEG C, the saprolite ore pulp after heating and the vitriol oil synchronously to add the opening for feed of duplex pusher reactor by the vitriol oil with mortar pump and vitriol oil pump after being heated to 150 DEG C, saprolite ore pulp and the vitriol oil are forced into rapid reaction in duplex pusher reactor and, to dissolve solubility non-ferrous metal and soluble iron, react and reaction mass is released duplex pusher reactor after 12 minutes after short mix.Be cooled to less than 60 DEG C, the reaction mass simple crushing of loose cellular solid-state lotion is fallen back in leaching tank, add 1920Kg water, stirring carries out water-soluble in 30 minutes, water-soluble gained slurry is pumped in plate-and-frame filter press and carries out solid-liquid separation and residue washing, obtain normal pressure leaching slag (A2) 230Kg(do), normal pressure leaching liquid (B2) 1500L and washings (E2) 1350L.The composition of normal pressure leaching slag (A2), normal pressure leaching liquid (B2) and washings (E2) is in Table 2-1, table 2-2 and table 2-3.
Get 40Kg4
#limonite (doing), add washings (E2) 80L and be mixed with limonite slurry, add in the circulation tank of capstan reactor after limonite slurry being heated to 100 DEG C, in the circulation tank of capstan reactor, add the normal pressure leaching liquid (B2) being heated to 100 DEG C again makes reaction mass final ph be 1.5, force (forcing) pump is opened after sealing circulation tank, open the hot oil heater of capstan reactor simultaneously, control temperature heats, pressure be 4.0MPa, temperature be the condition of 150 DEG C under pressure leaching 30 minutes, the Fe in normal pressure leaching liquid (B2)
3+be hydrolyzed to hematite precipitation and discharge acid and leach limonite again; From the circulation tank of capstan reactor, shift out reaction paste after being cooled to 85 DEG C carry out solid-liquid separation and wash filter residue, obtain pressure leaching slag (C2) 34Kg(to do), pressureleaching solution (D2) 94L and washings (F2) 55L, by namely there being method reclaim nickel and/or cobalt after removing non-nickel cobalt impurity to pressureleaching solution (D2).The composition of pressure leaching slag (C2), pressureleaching solution (D2) and washings (F2) is in Table 2-4, table 2-5 and table 2-6.
Get 300g pressure leaching slag (C2) and add that to fill 1000ml massfraction be in the beaker of the soda ash solution of 10%, be heated to 60 DEG C and stir 30 minutes, solid-liquid separation is also dried after washing leaching cake under temperature is 120 DEG C of conditions, obtains rhombohedral iron ore (G2) 295g.Rhombohedral iron ore (G2) composition is in Table 2-7.
Get 300g normal pressure leaching slag (A2) and carry out hydrocyclone separation technology, obtain-100 order silicon dioxide powder (H1) 143g and+100 order fine sand (I1) 151g.Silicon dioxide powder (H2) and fine sand (I2) composition are in Table 2-8 and table 2-9.
Calculate nickel, cobalt leaching yield, slag rate and acid consumption data as follows:
Normal pressure acidleach nickel leaching yield: 98.1%; Normal pressure acidleach cobalt leaching yield: 93.5%.
Pressure leaching nickel leaching yield: 94.6%; Pressure leaching cobalt leaching yield: 92.1%.
Amount to nickel leaching yield 95.5%; Cobalt leaching yield 93.1%.
Iron recovery >96%.
Sulfuric acid consumption: 180Kg sulfuric acid/t ore deposit.
Amount to slag rate: 46.3g white residue/1000g red soil nickel ore.
Embodiment 3
The normal pressure acid leaching stage of the present embodiment is identical with embodiment 1, in the pressure leaching stage by 1
#new noise made in coughing or vomiting limonite has changed 4 into
#indonesia's limonite.
Get 30Kg4
#limonite (doing), add washings (E1) 60L and be mixed with limonite slurry, add in the circulation tank of capstan reactor after limonite slurry being heated to 95 DEG C, in the circulation tank of capstan reactor, add the normal pressure leaching liquid (B1) being heated to 95 DEG C again makes reaction mass final ph be 1.0, force (forcing) pump is opened after sealing circulation tank, open the hot oil heater of capstan reactor simultaneously, control temperature heats, pressure be 2.0MPa, temperature be the condition of 223 DEG C under pressure leaching 60 minutes, the Fe in normal pressure leaching liquid (B1)
3+be hydrolyzed to hematite precipitation and discharge acid and leach limonite again; From the circulation tank of capstan reactor, shift out reaction paste after being cooled to 85 DEG C carry out solid-liquid separation and wash filter residue, obtain pressure leaching slag (C3) 29Kg(to do), pressureleaching solution (D3) 76L and washings (F3) 44L, by namely there being method reclaim nickel and/or cobalt after removing non-nickel cobalt impurity to pressureleaching solution (D3).The composition of pressure leaching slag (C3), pressureleaching solution (D3) and washings (F3) is in Table 3-1, table 3-2 and table 3-3.
Get 300g pressure leaching slag (C3) and add that to fill 1000ml massfraction be in the beaker of the soda ash solution of 10%, be heated to 60 DEG C and stir 30 minutes, solid-liquid separation is also dried after washing leaching cake under temperature is 130 DEG C of conditions, obtains rhombohedral iron ore (G3) 295g.Rhombohedral iron ore (G3) composition is in Table 3-4.
Get 300g normal pressure leaching slag (A1) and carry out hydrocyclone separation technology, obtain-100 order silicon dioxide powder (H1) 145g and+100 order fine sand (I1) 150g.
Calculate nickel, cobalt leaching yield, slag rate and acid consumption data as follows:
Pressure leaching nickel leaching yield: 95.4%; Pressure leaching cobalt leaching yield: 93.2%.
Amount to nickel leaching yield 96.6%; Cobalt leaching yield 93.3%.
Iron recovery >96%.
Sulfuric acid consumption: 250Kg sulfuric acid/t ore deposit.
Amount to slag rate: 92.5g white residue/1000g red soil nickel ore.
Embodiment 4
The normal pressure acid leaching stage of the present embodiment is identical with embodiment 2, in the pressure leaching stage by 4
#indonesia's limonite has changed 1 into
#new noise made in coughing or vomiting limonite.
Get 40Kg1
#limonite (doing), add washings (E1) 80L and be mixed with limonite slurry, add in the circulation tank of capstan reactor after limonite slurry being heated to 100 DEG C, in the circulation tank of capstan reactor, add the normal pressure leaching liquid (B1) being heated to 100 DEG C again makes reaction mass final ph be 1.5, force (forcing) pump is opened after sealing circulation tank, open the hot oil heater of capstan reactor simultaneously, control temperature heats, pressure be 3MPa, temperature be the condition of 185 DEG C under pressure leaching 45 minutes, the Fe in normal pressure leaching liquid (B1)
3+be hydrolyzed to hematite precipitation and discharge acid and leach limonite again; From the circulation tank of capstan reactor, shift out reaction paste after being cooled to 85 DEG C carry out solid-liquid separation and wash filter residue, obtain pressure leaching slag (C4) 38Kg(to do), pressureleaching solution (D4) 94L and washings (F4) 55L, by namely there being sulfide precipitation method reclaim nickel and/or cobalt after removing non-nickel cobalt impurity to pressureleaching solution (D4).The composition of pressure leaching slag (C4), pressureleaching solution (D4) and washings (F4) is in Table 4-1, table 4-2 and table 4-3.
Get 300g pressure leaching slag (C4) and add that to fill 1000ml massfraction be in the beaker of the soda ash solution of 10%, be heated to 60 DEG C and stir 30 minutes, solid-liquid separation is also dried after washing leaching cake under temperature is 140 DEG C of conditions, obtains rhombohedral iron ore (G4) 295g.Rhombohedral iron ore (G4) composition is in Table 4-4.
Get 300g normal pressure leaching slag (A2) and carry out hydrocyclone separation technology, obtain-100 order silicon dioxide powder (H2) 143g and+100 order fine sand (I2) 151g.
Calculate nickel, cobalt leaching yield, slag rate and acid consumption data as follows:
Pressure leaching nickel leaching yield: 95.1%; Pressure leaching cobalt leaching yield: 93.7%.
Amount to nickel leaching yield 96.9%; Cobalt leaching yield 94.4%.
Iron recovery >96%.
Sulfuric acid consumption: 180Kg sulfuric acid/t ore deposit.
Amount to slag rate: 92.0g white residue/1000g red soil nickel ore.
Embodiment 5 (reference examples)
The normal pressure acid leaching stage of the present embodiment is identical with embodiment 1, in the pressure leaching stage by 1
#new noise made in coughing or vomiting limonite has changed 3 into
#new Ka Guodukuang.
Get 30Kg3
#transition ore deposit (doing), add washings (E1) 60L and be mixed with transition ore pulp, add after transition ore pulp is heated to 95 DEG C in the circulation tank of capstan reactor, in the circulation tank of capstan reactor, add the normal pressure leaching liquid (B1) being heated to 95 DEG C again makes reaction mass final ph be 1.0, force (forcing) pump is opened after sealing circulation tank, open the hot oil heater of capstan reactor simultaneously, control temperature heats, pressure be 2.0MPa, temperature be the condition of 223 DEG C under pressure leaching 60 minutes, the Fe in normal pressure leaching liquid (B1)
3+be hydrolyzed to hematite precipitation and discharge acid and leach transition ore deposit again; From the circulation tank of capstan reactor, shift out reaction paste after being cooled to 85 DEG C carry out solid-liquid separation and wash filter residue, obtain pressure leaching slag (C5) 29Kg(to do), pressureleaching solution (D5) 76L and washings (F5) 47L, by namely there being sulfide precipitation method reclaim nickel and/or cobalt after removing non-nickel cobalt impurity to pressureleaching solution (D5).The composition of pressure leaching slag (C5), pressureleaching solution (D5) and washings (F5) is in Table 5-1, table 5-2 and table 5-3.
Get 300g pressure leaching slag (C5) and add that to fill 1000ml massfraction be in the beaker of the soda ash solution of 10%, be heated to 60 DEG C and stir 30 minutes, solid-liquid separation is also dried after washing leaching cake under temperature is 120 DEG C of conditions, obtains rhombohedral iron ore (G5) 293g.Rhombohedral iron ore (G5) composition is in Table 5-4.
Calculate nickel, cobalt leaching yield, slag rate and acid consumption data as follows:
Pressure leaching nickel leaching yield: 94.7%; Pressure leaching cobalt leaching yield: 92.5%.
Amount to nickel leaching yield 95.4%; Cobalt leaching yield 93.6%.
Iron recovery >96%.
Sulfuric acid consumption: 250Kg sulfuric acid/t ore deposit.
Amount to slag rate: 92.0g white residue/1000g red soil nickel ore.
In above embodiment, embodiment 1 and embodiment 2 saprolite in same mineral deposit and limonite combination; Embodiment 3 and embodiment 4 saprolite in different mineral deposit and limonite combination; As a comparison, embodiment 5 saprolite and the combination of transition ore deposit.From analytical data, the technical indicator such as nickel (cobalt) leaching yield, sulfuric acid consumption etc. of five embodiments is all better, but due to embodiment 5 employing is saprolite and the combination of transition ore deposit, therefore the iron level of pressure leaching slag is only 44.3%, iron almost cannot be recycled, and the iron level of the pressure leaching slag that other four embodiments obtain is all more than 58%, the rhombohedral iron ore iron content about 60% of recovery, the rate of recovery of iron is more than 96%.Amount to slag rate about 90.0g white residue/1000g red soil nickel ore, about slag rate is down to 46g white residue/1000g red soil nickel ore after reclaiming silicon-dioxide.
Claims (10)
1. from red soil nickel ore, reclaimed a method for nickel, cobalt, iron and silicon by combined leaching process, it is characterized in that: comprise the following steps:
A () adds water obtained saprolite ore pulp in saprolite ore deposit, saprolite ore pulp is heated to 60 DEG C-100 DEG C, the vitriol oil is heated to 150 DEG C-200 DEG C, in duplex pusher reactor, add the saprolite ore pulp after heating and the vitriol oil, react to dissolve solubility non-ferrous metal and soluble iron in saprolite ore deposit;
B () carries out water-soluble rear solid-liquid separation to reaction mass and residue washing obtains normal pressure leaching slag (A), normal pressure leaching liquid (B) and washings (E);
C () makes limonite slurry with washings (E) and limonite, add in capstan reactor after limonite slurry and normal pressure leaching liquid (B) are heated to 95 DEG C-100 DEG C respectively, pressure be 1.5MPa-4.0Mpa, temperature be the condition of 150 DEG C-240 DEG C under pressure leaching 0.5-1.5 hour, the Fe in normal pressure leaching liquid (B)
3+be hydrolyzed to hematite precipitation and discharge acid and leach limonite again;
D () is reduced temperature and carry out solid-liquid separation after 80 DEG C, obtain pressure leaching slag (C) and pressureleaching solution (D);
By namely there being method to reclaim nickel and/or cobalt e () removes non-nickel cobalt impurity to pressureleaching solution (D) after;
F () obtains Iron concentrate to pressure leaching slag (C) soda ash solution washing post-drying;
G () obtains silicon-dioxide and building sand to normal pressure leaching slag (A) through screening process.
2. a kind of method being reclaimed nickel, cobalt, iron and silicon by combined leaching process from red soil nickel ore according to claim 1, be is characterized in that: in described step (a), the granularity in saprolite ore deposit is-80 orders, and the granularity of limonite is-80 orders.
3. a kind of method being reclaimed nickel, cobalt, iron and silicon by combined leaching process from red soil nickel ore according to claim 1, be is characterized in that: in described step (a), the mass ratio of saprolite ore deposit and water is 1:1.2-1:1.
4. a kind of method being reclaimed nickel, cobalt, iron and silicon by combined leaching process from red soil nickel ore according to claim 1, it is characterized in that: in described step (a), the mass ratio of saprolite ore pulp and the vitriol oil is 2:1-2.2:1, and the reaction times is 1-12 minute.
5. a kind of method being reclaimed nickel, cobalt, iron and silicon by combined leaching process from red soil nickel ore according to claim 1, be is characterized in that: time water-soluble in described step (b), the mass ratio of reaction mass and water is 1:1.2-1:1.
6. a kind of method being reclaimed nickel, cobalt, iron and silicon by combined leaching process from red soil nickel ore according to claim 1, be is characterized in that: proportioning when washings (E) and limonite make limonite slurry in described step (c) is 2L:1Kg.
7. a kind of method being reclaimed nickel, cobalt, iron and silicon by combined leaching process from red soil nickel ore according to claim 1, be is characterized in that: in limonite slurry, add normal pressure leaching liquid (B) in described step (c) make reaction mass final ph be 0.5-1.5.
8. a kind of method being reclaimed nickel, cobalt, iron and silicon by combined leaching process from red soil nickel ore according to claim 1, be is characterized in that: in described step (f), the massfraction of soda ash solution is 10%, and bake out temperature is 120 DEG C-150 DEG C.
9. a kind of method being reclaimed nickel, cobalt, iron and silicon by combined leaching process from red soil nickel ore according to claim 1, it is characterized in that: in described step (b), normal pressure leaching slag (A) is white residue, and its dioxide-containing silica is 65%-90%.
10. a kind of method being reclaimed nickel, cobalt, iron and silicon by combined leaching process from red soil nickel ore according to claim 1, it is characterized in that: obtain pressure leaching slag (C) in described step (d) for rhombohedral iron ore slag, wherein iron level is 58%-65%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410845411.0A CN104611558B (en) | 2014-12-31 | 2014-12-31 | A kind of method reclaiming nickel, cobalt, ferrum and silicon by combined leaching process from lateritic nickel ore |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410845411.0A CN104611558B (en) | 2014-12-31 | 2014-12-31 | A kind of method reclaiming nickel, cobalt, ferrum and silicon by combined leaching process from lateritic nickel ore |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104611558A true CN104611558A (en) | 2015-05-13 |
| CN104611558B CN104611558B (en) | 2017-03-01 |
Family
ID=53146202
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410845411.0A Active CN104611558B (en) | 2014-12-31 | 2014-12-31 | A kind of method reclaiming nickel, cobalt, ferrum and silicon by combined leaching process from lateritic nickel ore |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104611558B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108396157A (en) * | 2018-03-15 | 2018-08-14 | 李宾 | A kind of method of laterite nickel ore by sulfuric acid leaching liquid and silica gel chelating resin purification production sulfuric acid nickel cobalt |
| CN116004983A (en) * | 2022-12-31 | 2023-04-25 | 贵州中伟资源循环产业发展有限公司 | Leaching method of sulfide minerals |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2872306A (en) * | 1956-05-29 | 1959-02-03 | Freeport Sulphur Co | Recovery of cobalt and nickel from ores |
| US2971836A (en) * | 1957-04-29 | 1961-02-14 | James D Hall | Separation of nickel and cobalt |
| US3093559A (en) * | 1958-06-20 | 1963-06-11 | Merwin G White | Treatment of lateritic ores |
| US3809549A (en) * | 1970-07-08 | 1974-05-07 | V Opratko | Acid leaching of lateritic ore |
| US3991159A (en) * | 1975-01-09 | 1976-11-09 | Amax Inc. | High temperature neutralization of laterite leach slurry |
| 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 |
| CN101778958A (en) * | 2007-08-07 | 2010-07-14 | Bhp比利通Ssm开发有限公司 | The method of normal pressure acid leaching of laterite |
| CN103614571A (en) * | 2013-10-09 | 2014-03-05 | 北京矿冶研究总院 | Combined leaching process of laterite-nickel ore |
-
2014
- 2014-12-31 CN CN201410845411.0A patent/CN104611558B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2872306A (en) * | 1956-05-29 | 1959-02-03 | Freeport Sulphur Co | Recovery of cobalt and nickel from ores |
| US2971836A (en) * | 1957-04-29 | 1961-02-14 | James D Hall | Separation of nickel and cobalt |
| US3093559A (en) * | 1958-06-20 | 1963-06-11 | Merwin G White | Treatment of lateritic ores |
| US3809549A (en) * | 1970-07-08 | 1974-05-07 | V Opratko | Acid leaching of lateritic ore |
| US3991159A (en) * | 1975-01-09 | 1976-11-09 | Amax Inc. | High temperature neutralization of laterite leach slurry |
| 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 |
| CN101778958A (en) * | 2007-08-07 | 2010-07-14 | Bhp比利通Ssm开发有限公司 | The method of normal pressure acid leaching of laterite |
| CN103614571A (en) * | 2013-10-09 | 2014-03-05 | 北京矿冶研究总院 | Combined leaching process of laterite-nickel ore |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108396157A (en) * | 2018-03-15 | 2018-08-14 | 李宾 | A kind of method of laterite nickel ore by sulfuric acid leaching liquid and silica gel chelating resin purification production sulfuric acid nickel cobalt |
| WO2019174103A1 (en) * | 2018-03-15 | 2019-09-19 | 李宾 | Method for producing nickel sulfate and cobaltous sulfate by purification of laterite nickel ore sulfuric acid leaching solution and silica gel chelate resin |
| CN116004983A (en) * | 2022-12-31 | 2023-04-25 | 贵州中伟资源循环产业发展有限公司 | Leaching method of sulfide minerals |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104611558B (en) | 2017-03-01 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN111777224B (en) | Method for comprehensively utilizing polymetallic acid wastewater of nonferrous metal mine | |
| CN104630500A (en) | Method for recovering nickel, cobalt, iron and silicon from laterite-nickel ore by combined leaching process | |
| CN104611548A (en) | Method for recovering nickel in low-grade laterite-nickel ore | |
| CN104831087A (en) | Method of recycling nickel, cobalt, iron and silicon from low-grade laterite nickel ore through combined leaching process | |
| CN104805306A (en) | New method for recovering nickel, cobalt and iron from low-grade laterite-nickel ore | |
| CN104831061A (en) | Method of recycling nickel, cobalt and iron from low-grade laterite-nickel ore | |
| CN104775025A (en) | Method for recovering nickel, cobalt, iron and silicon from laterite-nickel ore through combined leaching technology | |
| CN104651634A (en) | Method for recovering nickel, cobalt and iron from laterite-nickel ores | |
| CN104789797A (en) | A novel method of recovering nickel, cobalt, iron, silicon and magnesium from low-grade lateritic nickel ore | |
| CN104611558B (en) | A kind of method reclaiming nickel, cobalt, ferrum and silicon by combined leaching process from lateritic nickel ore | |
| CN104651609A (en) | Method for recovering nickel, cobalt and iron from laterite-nickel ores | |
| CN104805308A (en) | New method for recovering nickel, cobalt, iron, silicon and magnesium from low-grade laterite-nickel ore | |
| CN104789766A (en) | A method of recovering nickel, iron and silicon from lateritic nickel ore by a combined leaching process | |
| CN104775028A (en) | Method for recovering nickel, cobalt and iron from low grade laterite-nickel ore | |
| CN104630502A (en) | Method for recovering nickel, cobalt, iron and silicon from limonite by combined leaching process | |
| CN104630501A (en) | Method for recovering nickel, cobalt, iron and silicon from low-grade laterite-nickel ore by combined leaching process | |
| CN104611552A (en) | Method for extracting nickel from brown iron ore | |
| CN104611581A (en) | Method for extracting nickel from low-grade nickel laterite ore | |
| CN104611579A (en) | Method for recycling nickel from low-grade nickel laterite ore | |
| CN104630503A (en) | Method for recovering nickel, cobalt, iron and silicon from limonite by combined leaching process | |
| CN104630505A (en) | Method for recovering nickel, cobalt, iron and silicon from low-grade laterite-nickel ore by combined leaching process | |
| CN104805309A (en) | Method for recovering nickel, cobalt and iron from laterite-nickel ore | |
| CN104775024A (en) | Method for recovering nickel, cobalt and iron from laterite-nickel ore | |
| CN104762493A (en) | Method for treating laterite nickel ore through combination of normal-pressure acid leaching and medium-pressure leaching | |
| CN104805307A (en) | New method for recovering nickel, cobalt and iron from low-grade laterite-nickel ore |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20190215 Address after: 730101 Jinchuan Science and Technology Park, Peace Economic Development Zone, Yuzhong County, Lanzhou City, Gansu Province Patentee after: Gansu Jinchuan Nickel-Cobalt New Material Technology Innovation Center Co., Ltd. Address before: No. 98 Jinchuan Road, Jinchang, Gansu Patentee before: Jinchuan Group Co., Ltd. |
|
| TR01 | Transfer of patent right |