CN103290213A - Process for recycling valuable metal from nickel laterite ores and simultaneously by-producing anhydrous calcium chloride - Google Patents
Process for recycling valuable metal from nickel laterite ores and simultaneously by-producing anhydrous calcium chloride Download PDFInfo
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Abstract
The invention discloses a process for comprehensively recycling valuable metal including nickel, cobalt, chromium, magnesium and the like from nickel laterite ores and simultaneously by-producing products including calcium chloride, calcium sulfate, sodium chloride and the like. A current method has a long technological process and more procedures, so that the investment is great; particularly, a technology of extracting for two times and leaching for three times is used in a leaching process, so that the great investment of equipment, funds and manpower is caused. The process disclosed by the invention is characterized in that the nickel laterite ores, recycled water and part of raffinate are added into a ball grinding mill to be subjected to ball grinding and pre-immersing reaction; a peracid leaching solution is pumped into an extraction and de-ironing working section from a peracid leaching solution storing groove to remove an iron element; part of extracted and de-ironed raffinate passes through a magnesium sinking working section to obtain a magnesium sinking solution with a main component of calcium chloride. According to the process disclosed by the invention, in a process of grinding ores, the aim of pre-leaching is realized, the time for a leaching reaction is shortened, the leaching rate of metal is improved, a technological process is shortened, and the investment cost of equipment is reduced.
Description
Technical field
The present invention relates to non-ferrous metal hydrometallurgy field, specifically a kind of from red soil nickel ore valuable metals such as comprehensive recovery nickel, cobalt, chromium, magnesium, the simultaneously technology of products such as by-product calcium chloride, calcium sulfate, sodium-chlor.
Background technology
The production method of calcium chloride can be divided into following several both at home and abroad at present:
(1) be raw material production calcium chloride with calcium carbonate and hydrochloric acid
This method is that raw material carries out acid-base neutralisation reaction with calcium carbonate and hydrochloric acid, and reacted ore pulp carries out solid-liquid separation, and filter residue is discarded, and filtrate neutralizes with milk of lime, regulates pH to 9.0-9.5, makes Al in the filtrate
3+, Mg
2+, Fe
3+Form Al (OH) Deng impurity
3, Mg (OH)
2, Fe (OH)
3Precipitation is removed from solution, in and the ore pulp press filtration after, filter residue is discarded, filtrate is increased to 68-69% through mass percent after the triple effect evaporation by 30-35%, enter flaker then and carry out film-making, mass percent is increased to 74% after the flake calcium chloride process fluidized bed drying, is the Calcium dichloride dihydrate product after the cooling, Calcium dichloride dihydrate is further drying and dewatering under 260 ℃ temperature, can make the anhydrous chlorides of rase calcium product.Also there is producer to adopt spraying fluidization drying-granulating technology, directly the calcium chloride solution of high density made the calcium chloride product through processes such as spraying, drying, granulation, coolings; Adopt this method technical process short and simple, the equipment less investment, product quality is higher, but owing to raw materials such as calcium carbonate and hydrochloric acid all need be bought, so production cost is higher.
(2) waste water that contains calcium chloride with alkali factory is raw material production calcium chloride
A kind of waste water that contains high calcium chloride concentration of output in the technological process of solvay soda process production soda ash, part producer utilizes these waste water to produce the calcium chloride product, detailed process is: the waste water that will contain 100g/L left and right sides calcium chloride is earlier sent into salt Tanaka and is carried out evaporation concentration, calcium chloride concentration is promoted to 300g/L, separate out part sodium-chlor product simultaneously, again this part calcium chloride solution is carried out the evaporative crystallization first time in evaporation equipment, further precipitated sodium chloride and magnesium chloride product, calcium chloride concentration rises to 450-500g/L simultaneously, centrifugation obtains clean calcium chloride solution and passes through evaporative crystallization for the second time again, when solution temperature rises to 170 ℃ of left and right sides solution sent into and carry out film-making in the flaker, mass percent is increased to 74% after the flake calcium chloride process fluidized bed drying, is the Calcium dichloride dihydrate product after the cooling.The further deep processing of Calcium dichloride dihydrate can make the anhydrous chlorides of rase calcium product.Adopt this method to produce calcium chloride product prime cost and concentrate in the heat energy consumption, consumption of raw and auxiliary materials is few, and comprehensive production cost is lower, but plant area's floor space is bigger, need possess certain condition and just can this method produce.
The method of the low-grade red soil nickel ore of wet processing is both at home and abroad at present:
(1) normal pressure sulfuric acid leaching: this method is to be leaching agent with sulfuric acid, controls reaction conditionss such as certain liquid-solid ratio, acidity, temperature, under normal pressure metals such as nickel, cobalt, iron, magnesium is leached from mineral aggregate; Adding neutralizing agent (Wingdale, calcium hydroxide or other alkaline matter) then removes impurity such as iron, aluminium, silicon, obtain nickel sulfate solution after the press filtration of removal of impurities ore pulp and scrap slag, scrap slag and efflux behind washery slag, nickel sulfate solution then uses sodium hydroxide (perhaps calcium hydroxide, magnesium hydroxide) to sink nickel reactant; The nickel slag that obtains is molten through acid, obtain the deep processed product of nickel cobalt behind the abstraction impurity removal; Liquid evaporative crystallization reclaim(ed) sulfuric acid magnesium behind the heavy nickel perhaps directly adds alkaline matter (Wingdale, calcium hydroxide, yellow soda ash etc.) and carries out precipitation process, and liquid effluxes after the processing that obtains.This treatment process is owing to be metal target with nickel, cobalt and a spot of magnesium only, and the rate of recovery of magnesium is low, the acid and alkali consumption height, and the quantity of slag is big and can't fully utilize, thereby causes production cost high.
(2) high pressure sulfuric acid leaching: this method is to be leaching agent with sulfuric acid, and control certain reaction temperature is handled laterite under the pressurization situation.Pressurized acid leaching technology starts from the hair Ah (MOA) of Cuba's the 1950's the earliest, Australian Mu Lin-Mu Lin after the nineties in 20th century, Bu Long, examining pressurized acid leaching factories such as gas goes into operation in succession, but many problems are appearring aspect technology and the equipment, the basic procedure of this technology is that ore enters autoclave through high pressure (4-5MPa) through after the broken slurrying, high temperature (230-260 ℃) is acid to be leached, carry out liquid-solid separation after the leaching, then leach liquor is neutralized, deironing, liquid carries out the separation of nickel cobalt by extraction after the deironing, also can further smelt according to different needs obtain different nickel cobalt products; The rate of recovery of this technology nickel cobalt can reach more than 90%, but this technology investment cost is big, relatively stricter to the requirement of equipment and material, because impurity such as magnesium are bigger for the influence of sulfuric acid consumption, so being fit to handle, this technology contains magnesium less than 10%, particularly less than 5% red soil nickel ore.In addition, in this technology operational process, equipment is prone to scale formation, production is affected greatly, and the cost of equipment maintenance height, slag can't rationally utilize, and the existence of these a series of problems makes the large-area applications of this method promote and has been subjected to certain influence.
(3) reduction roasting-ammonia leaching method: therefore reduction roasting-ammonia leaching technology claim the Caron flow process again by professor's Caron invention, and wherein, ammonia soaks and adopts NH in the process
3And CO
2Nickel in the roasted ore and cobalt are converted into ammonia complex enter solution, the advantage of this technology is that reagent can recycle, consumption is little, shortcoming is that the nickel cobalt rate of recovery is low, the nickel cobalt rate of recovery is respectively about 75% and 60%, and because mineral aggregate need be dried roasting, energy consumption is bigger, can not realize the comprehensive reutilization of resource.
Chinese patent application numbers 200810058077.9 discloses a kind of salt acid system extracts the nickel cobalt from red soil nickel ore method, and this method has used hydrochloric acid as leaching agent in the red soil nickel ore leaching process; The mode that mineral aggregate leaches is the leaching of uniting of dump leaching, dip, agitation leach or these several modes; Adopt the way of magnetic separation that the iron ore concentrate in the leached mud is reclaimed, the tailings after the magnetic separation is stored up; Leach the leach liquor that obtains after the solid-liquid separation on ore pulp (thickener, flame filter press etc.) and carry out the coprecipitated nickel hydroxide cobalt with sulfide (potassium sulphide, sodium sulphite etc.), sodium hydroxide or yellow soda ash; Reclaim hydrochloric acid in the tail washings of heavy nickel, the way of employing is fluidized bed process, spray roasting or spent acid distillation, reclaims metal oxide simultaneously, and the hydrochloric acid of recovery is got back in the leaching process of ore, realizes the closed cycle utilization of hydrochloric acid.In the method, used slag washing water to absorb the hydrogenchloride of output in the spray roasting process, and this is contained acid solution turned back in the leaching process; Iron ore concentrate in the slag is reclaimed, because metals such as Fe, Co, Ni exist with the form of compound association in laterite, so that the heavy metal content in the iron ore concentrate that reclaims is higher, can not satisfy the service requirements of iron ore concentrate, so infeasible with this method recovery iron ore concentrate; Tailings is stored up processing, still is a problem in the utilization of tailings; Use sulfide (potassium sulphide, sodium sulphite etc.), sodium hydroxide or yellow soda ash to carry out the coprecipitated nickel hydroxide cobalt, cost of supplementary product is high, and uses the heavy nickel cobalt of sulfide, and the precipitate particles that obtains is thinner, and solid-liquid separation is difficulty quite; Hydrochloric acid after adopting fluidized bed process, spray roasting or spent acid distillation to heavy nickel in the liquid reclaims, reclaim metal oxide simultaneously, because the nickel grade of red soil nickel ore is lower, make a wet method factory that produces 10000 tons of nickel per year, the nearly 10000m of liquid measure behind one day the heavy nickel
3, so huge amount of solution adopts this method to reclaim hydrochloric acid, on the energy consumption, equipment drops into and goes up, all be quite huge in the manning, the height of cost is well imagined; In sum, there are serious problems in this method in industrial applications.
Chinese patent application numbers 201210202583.7 disclose a kind of from red soil nickel ore the method for comprehensively recovering valuable metal.This method has been divided into irony ore deposit and magnesia ore deposit with mineral aggregate in the processing of mineral aggregate; In the red soil nickel ore leaching process, used sulfuric acid as leaching agent; Adopted in one section peracid agitation leach and two sections and the mode of agitation leach leaches laterite, the slag that peracid leaches send cement mill or the brickmaking factory to handle through behind the washery slag; Adopt the way of extraction to carry out deironing, deironing is divided into single extraction and reextraction, the anti-iron liquid that obtains in twice extraction process is delivered to the spray roasting stove and is carried out pyrolytic decomposition and handle, generate the iron oxide red product and reclaim hydrochloric acid simultaneously, the hydrochloric acid that reclaims is used for the back extraction process of extraction deironing, the raffinate that the single extraction deironing obtains is back to the peracid leaching process, and the raffinate of reextraction deironing enters receives chromium workshop section, has realized sour comprehensive utilization; Use the heavy nickel slag of secondary, magnesium hydroxide or the milk of lime receipts chromium that neutralizes; Use milk of lime or magnesium hydroxide to carry out once and the heavy nickel of secondary; Use ammoniacal liquor or milk of lime to sink magnesium; In the process of heavy nickel and heavy magnesium with milk of lime, used the specific equipment separator column to carry out separating of nickel hydroxide (magnesium) and calcium sulfate, obtained the product of calcium sulfate; Do not have other foreign ion behind the heavy magnesium in this method in the liquid, use as the reuse water retrieval system; Use the carbonic acid gas carborization that calcium in the magnesium hydroxide has been carried out degree of depth separation in this method, made the higher magnesium products of purity.There is following problem in this method: flow process is long, operation is more, causes investment bigger, particularly in the process that leaches, has used the technology of twice extraction, three leachings, has caused the input of large number quipments, fund and manpower; Fail to propose more economical and realistic plan more in the utilization of slag; Adopt spray method to reclaim hydrochloric acid, energy consumption is higher; Used sulfuric acid as acid source, with milk of lime as alkali source, the defective that this soda acid source is selected be with milk of lime receive chromium, with the heavy nickel of milk of lime and in the product of the heavy magnesium of milk of lime more or less be entrained with calcium sulfate, the disadvantageous effect that the existence of this part calcium sulfate brings has following two aspects: the one, caused the purity drop of product, the 2nd, the calcium sulfate dissolving enters into leach liquor in the molten process of acid, calcium ion wherein can affect greatly technology in workshop section's foulings such as extractions subsequently.In sum, this method also has more needs to improve improved place in industrial applications.
Summary of the invention
Technical problem to be solved by this invention is to overcome the defective that above-mentioned prior art exists, provide a kind of from being that raw material is in valuable metals such as comprehensive recovery nickel, cobalt, chromium, magnesium, iron with red soil nickel ore, hydrochloric acid and milk of lime, the technology of products such as by-product calcium chloride, calcium sulfate, sodium-chlor, it carries out ball milling preimpregnation reaction under hydrochloric acid system, with shortened process; The by-product multiple product is to reduce production costs.
For this reason, the present invention adopts following technical scheme: the technology of by-product Calcium Chloride Powder Anhydrous when reclaiming valuable metal from red soil nickel ore, it is characterized in that: carry out ball milling preimpregnation reaction in red soil nickel ore, reuse water and the part raffinate adding ball mill, the solid content in the control ball mill is at 20-50%; Mineral aggregate after ball milling leaches pumps into and carries out classification in the swirler, makes particle diameter≤100 purpose mineral aggregates enter in the overflow ore pulp, continues ball milling in the ball mill and the thicker mineral aggregate of another part particle is turned back to; The overflow ore pulp enters and continues to participate in leaching reaction in the leaching vat, add hydrochloric acid and reuse water, after the leaching reaction is finished, ore pulp pumps into and carries out solid-liquid separation in the washery slag pressure filter, the leached mud of gained washs in pressure filter, washing lotion is reuse water, and the slag washing water of gained is mixed into high acid leaching liquor storage tank with leaching filtrate; Slag part after the washing is as high silica flour product, and another part carries out alkali with sodium hydroxide and soaks, and produces the white carbon black product;
High acid leaching liquor pumps into extraction deironing workshop section from high acid leaching liquor storage tank, carry out removing of ferro element, obtain the anti-iron liquid of peracid with the back extraction of 6-7N hydrochloric acid, the anti-iron liquid of described peracid makes high density chlorination ferrous solution through depickling, the back extraction process of extraction iron removal is returned in isolated acid, realizes the comprehensive utilization of residual acid; Contain acid in the raffinate of extraction deironing, its part is returned the ball milling prepreg process and is used as acid medium, and another part enters dechromisation workshop section, enters heavy nickel workshop section, heavy magnesium workshop section successively afterwards;
Major ingredient is calcium chloride in the liquid behind the heavy magnesium that heavy magnesium workshop section obtains, its part turns back in the system as reuse water, a part is opened a way to calcium chloride evaporation concentration workshop section, produce the calcium chloride product, liquid and metabisulfite solution prepared in reaction calcium sulfate product behind some heavy magnesium, the surplus liquid that has reacted then pumps into the salt pan and shines sodium-chlor product processed, thereby realizes the complete utilization of calcium chloride.
The leaching process of red soil nickel ore by traditional dump leaching, stir mode such as soak and change the mode that ball milling leaches into, namely in ball mill, realize ore grinding and leach two processes; After ball milling leaches, be the effect that guarantees to leach, leaching process increases leaching vat and leaches.
The invention solves the following problem that prior art exists: (1) leaching process long flow path, the problem that equipment is many, investment is big; (2) the low-cost recovery problem of residual acid in the anti-iron liquid; (3) problem of complex utilization of leached mud; (4) chromium hydroxide, nickel, magnesium improve purity problem; (5) calcium chloride product low cost production problem.
Replenish as the further of technique scheme:
The anti-iron liquid of described peracid is handled with film or the depickling reaction is carried out in distillation, and described film is for to have permselective film to positively charged ion, and film can obtain two kinds of solution after handling, and a kind of is the iron(ic) chloride liquid of low acid, and a kind of is the solution that contains acid.
When participate in leaching reaction in leaching vat, the liquid-solid ratio of control reaction is 3-7:1, temperature of reaction 80-100 ℃, and reaction times 1-3h, slag is nickeliferous≤and 0.1%.
In ball milling preimpregnation reaction, the pH of control ore pulp is at 0.5-1.5, slurry temperature≤70 ℃ behind the control ball milling.
Precipitate chromium in the extraction deironing raffinate with milk of lime, reclaim the chromium hydroxide product, chromium hydroxide washs with reuse water, washes back liquid and enters into liquid behind the dechromisation.
Liquid carries out one section heavy nickel with milk of lime behind the described dechromisation, and one section heavy nickel slag makes the nickel hydroxide product with steam condensate or tap water after washing, and washing lotion enters behind one section heavy nickel in the liquid; Liquid carries out the heavy nickel of secondary with milk of lime behind one section heavy nickel, is back to the leaching vat leaching section after the heavy nickel slag of the secondary that press filtration obtains is sized mixing with reuse water; Liquid sinks magnesium with milk of lime behind two sections heavy nickel, and press filtration obtains liquid behind magnesium hydroxide slag and the heavy magnesium, and the magnesium hydroxide slag obtains magnesium hydroxide products after with steam condensate or tap water washing, and washing back liquid effluxes.
Metal ion and residual acid such as Cr, the Fe in the extremely heavy chromium workshop section of the open circuit raffinate, Ni, Co, Mg all use milk of lime to carry out neutralization precipitation, realize calcium ion and the exchange of each metal ion in solution.
The reuse water that turns back in the system uses as leaching reaction water, milk of lime preparation water, leached mud slag washing water and the two sections heavy nickel slags water of sizing mixing.
The ball mill of selecting for use is through rotproofing, the equal abrasion-proof corrosion-proof of the liner plate of selecting for use and abrading-ball.
The beneficial effect that the present invention has: the application of (1) ball milling leaching-out technique, realized in ore grinding, carry out the purpose of preextraction, shortened the time of leaching reaction, improved the leaching yield of metal, shortened technical process, reduced the facility investment expense; (2) use membrane technology or distillation depickling technology that the residual acid in the anti-iron liquid of peracid is separated, realized that the residual acid in the anti-iron liquid is reclaimed cheaply, and the low cost production problem of high-purity high density chlorination iron product; (3) by-product of calcium chloride, sodium-chlor has been shared the cost of soda acid auxiliary material, has reduced the nickel production cost; (4) production of white carbon black has solved the problem that slag muck is put, and has improved the added value of slag, has shared the nickel production cost.
The invention will be further described below in conjunction with specification drawings and specific embodiments.
Description of drawings
Fig. 1 is process flow sheet of the present invention.
Embodiment
As shown in Figure 1, carry out ball milling preimpregnation reaction in red soil nickel ore, reuse water and the part raffinate adding ball mill, solid content in the control ball mill is at 20-50%, the pH of control reaction ore pulp is at 0.5-1.5, slurry temperature≤70 ℃ behind the control ball milling, mineral aggregate after ball milling leaches pumps into and carries out classification in the swirler, makes particle diameter≤100 purpose mineral aggregates enter into the overflow ore pulp, continue ball milling in the ball mill and the thicker mineral aggregate of another part particle is turned back to.
The overflow ore pulp enters and continues to participate in leaching reaction in the leaching vat, add an amount of hydrochloric acid and reuse water, the liquid-solid ratio 3-7:1 of control reaction, control temperature of reaction 〉=80 ℃, control reaction times 2h, control slag nickeliferous≤0.1%, after the leaching reaction was finished, ore pulp pumped into and carries out solid-liquid separation in the washery slag pressure filter, and leached mud washs in pressure filter, washing lotion is reuse water, and slag washing water is mixed into high acid leaching liquor storage tank with leaching filtrate; Slag part after the washing is as high silica flour export trade, and another part carries out alkali with sodium hydroxide and soaks, and produces the white carbon black product.
Leach liquor pumps into extraction deironing workshop section from high acid leaching liquor storage tank, carry out removing of ferro element, obtains the anti-iron liquid of peracid with the back extraction of 6-7N hydrochloric acid; Contain acid in the raffinate of extraction deironing, its part is returned the ball milling leaching process and is used as acid medium, and another part enters dechromisation workshop section; The anti-iron liquid of peracid is handled with film or the residual acid in the anti-iron liquid of peracid is separated in the distillation depickling, realized that the residual acid in the anti-iron liquid reclaims cheaply, the hydrochloric acid of returning turns back in the leading portion extraction back extraction process, has realized the reasonable utilization of residual acid in the anti-iron liquid.
Precipitate chromium in the extraction deironing raffinate with milk of lime, reclaim the chromium hydroxide product, chromium hydroxide washs with reuse water, washes back liquid and enters into liquid behind the dechromisation; Liquid carries out one section heavy nickel with milk of lime behind the dechromisation, and one section heavy nickel slag makes the nickel hydroxide product with steam condensate or tap water after washing, and nickel hydroxide is handled the related products that can make cobalt nickel through further deep processing, and washing lotion enters behind one section heavy nickel in the liquid; Liquid carries out the heavy nickel of secondary with milk of lime behind one section heavy nickel, is back to the leaching vat leaching section after the heavy nickel slag of the secondary that press filtration obtains is sized mixing with reuse water; Liquid sinks magnesium with milk of lime behind two sections heavy nickel, and press filtration obtains liquid behind magnesium hydroxide slag and the heavy magnesium, and the magnesium hydroxide slag obtains magnesium hydroxide products after with steam condensate or tap water washing; Behind the heavy magnesium in the liquid major ingredient be calcium chloride, its part turns back in the system as reuse water, use as leaching water, milk of lime preparation water, leached mud slag washing water and the two sections heavy nickel slags water of sizing mixing of sizing mixing, a part is opened a way to calcium chloride evaporation concentration workshop section, produce the calcium chloride product, behind some heavy magnesium liquid can with metabisulfite solution prepared in reaction calcium sulfate product, the surplus liquid that has reacted then can pump into the salt pan and shine sodium-chlor product processed and use, thus the complete utilization of realization calcium chloride.
Supplementary notes: the pH control of (1) dechromisation reaction is at 3.5-4.5, and temperature is controlled at 40-60 ℃, and the reaction times is controlled at 2-3h; The pH control of (2) one sections heavy nickel reactants is at 7.5-8.5, and temperature is controlled at 40-60 ℃, and the reaction times is controlled at 2-3h; The pH control of (3) two sections heavy nickel reactants is at 8.5-9.5, and temperature is controlled at 40-60 ℃, and the reaction times is controlled at 2-3h; (4) pH of heavy reactive magnesium control is at 10.0-11.0, and temperature is controlled at 40-60 ℃, and the reaction times is controlled at 2-3h.
Claims (9)
1. the technology of by-product Calcium Chloride Powder Anhydrous when reclaiming valuable metal from red soil nickel ore is characterized in that: carry out ball milling preimpregnation reaction in red soil nickel ore, reuse water and the part raffinate adding ball mill, the solid content in the control ball mill is at 20-50%; Mineral aggregate after ball milling leaches pumps into and carries out classification in the swirler, makes particle diameter≤100 purpose mineral aggregates enter in the overflow ore pulp, continues ball milling in the ball mill and the thicker mineral aggregate of another part particle is turned back to; The overflow ore pulp enters and continues to participate in leaching reaction in the leaching vat, add hydrochloric acid and reuse water, after the leaching reaction is finished, ore pulp pumps into and carries out solid-liquid separation in the washery slag pressure filter, the leached mud of gained washs in pressure filter, washing lotion is reuse water, and the slag washing water of gained is mixed into high acid leaching liquor storage tank with leaching filtrate; Slag part after the washing is as high silica flour product, and another part carries out alkali with sodium hydroxide and soaks, and produces the white carbon black product;
High acid leaching liquor pumps into extraction deironing workshop section from high acid leaching liquor storage tank, carry out removing of ferro element, obtain the anti-iron liquid of peracid with the back extraction of 6-7N hydrochloric acid, the anti-iron liquid of described peracid makes high density chlorination ferrous solution through depickling, and the back extraction process of extraction iron removal is returned in isolated acid; Contain acid in the raffinate of extraction deironing, its part is returned the ball milling prepreg process and is used as acid medium, and another part enters dechromisation workshop section, enters heavy nickel workshop section, heavy magnesium workshop section successively afterwards;
Major ingredient is calcium chloride in the liquid behind the heavy magnesium that heavy magnesium workshop section obtains, its part turns back in the system as reuse water, a part is opened a way to calcium chloride evaporation concentration workshop section, produce the calcium chloride product, liquid and metabisulfite solution prepared in reaction calcium sulfate product behind some heavy magnesium, the surplus liquid that has reacted then pump into the salt pan and shine sodium-chlor product processed.
2. technology according to claim 1 is characterized in that, the anti-iron liquid of described peracid is handled with film or the depickling reaction is carried out in distillation, and described film is for to have permselective film to positively charged ion.
3. technology according to claim 2 is characterized in that, the pH value of control depickling is at 2-6.
4. according to claim 1,2 or 3 described technologies, it is characterized in that when participate in leaching reaction in leaching vat, the liquid-solid ratio of control reaction is 3-7:1, temperature of reaction 80-100 ℃, reaction times 1-3h, slag is nickeliferous≤and 0.1%.
5. according to claim 1,2 or 3 described technologies, it is characterized in that in ball milling preimpregnation reaction, the pH of control ore pulp is at 0.5-1.5, slurry temperature≤70 ℃ behind the control ball milling.
6. according to claim 1,2 or 3 described technologies, it is characterized in that, precipitate chromium in the extraction deironing raffinate with milk of lime, reclaim the chromium hydroxide product, chromium hydroxide washs with reuse water, washes back liquid and enters into liquid behind the dechromisation.
7. technology according to claim 6 is characterized in that, liquid carries out one section heavy nickel with milk of lime behind the described dechromisation, and one section heavy nickel slag makes the nickel hydroxide product with steam condensate or tap water after washing, and washing lotion enters behind one section heavy nickel in the liquid; Liquid carries out the heavy nickel of secondary with milk of lime behind one section heavy nickel, is back to the leaching vat leaching section after the heavy nickel slag of the secondary that press filtration obtains is sized mixing with reuse water; Liquid sinks magnesium with milk of lime behind two sections heavy nickel, and press filtration obtains liquid behind magnesium hydroxide slag and the heavy magnesium, and the magnesium hydroxide slag obtains magnesium hydroxide products after with steam condensate or tap water washing, and washing back liquid effluxes.
8. technology according to claim 1 is characterized in that, the reuse water that turns back in the system uses as leaching reaction water, milk of lime preparation water, leached mud slag washing water and the two sections heavy nickel slags water of sizing mixing.
9. technology according to claim 1 is characterized in that, the ball mill of selecting for use is through rotproofing, the equal abrasion-proof corrosion-proof of the liner plate of selecting for use and abrading-ball.
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| CN103820640A (en) * | 2014-03-12 | 2014-05-28 | 胡雷 | Method for extracting iron from laterite nickel ore by adopting wet process |
| CN105296744A (en) * | 2015-10-26 | 2016-02-03 | 广西银亿再生资源有限公司 | Method for laterite-nickel ore resourceful treatment and comprehensive recycling |
| CN106315630A (en) * | 2016-08-30 | 2017-01-11 | 荆门市格林美新材料有限公司 | Method for preparing high-purity flame-retardant magnesium hydroxide through recovery from heavy-metal sludge |
| CN106674590A (en) * | 2016-12-26 | 2017-05-17 | 荆门市格林美新材料有限公司 | Method for recycling aluminum and magnesium from sludge and preparing composite flame retardant |
| CN106673025A (en) * | 2016-11-18 | 2017-05-17 | 江苏仁欣环保科技有限公司 | Technological method for producing magnesium hydroxide by utilization of magnesium-containing wastewater generated by laterite nickel ore wet-process |
| CN108754168A (en) * | 2018-04-20 | 2018-11-06 | 中国瑞林工程技术有限公司 | A kind of processing method of sulfur-bearing leached mud and its application |
| CN109536711A (en) * | 2018-11-06 | 2019-03-29 | 泰州华昊废金属综合利用有限公司 | The resource utilization processing system of Treatment of Metal Surface waste |
| CN112110495A (en) * | 2020-08-24 | 2020-12-22 | 斯瑞尔环境科技股份有限公司 | Method for producing flaky crystalline ferric chloride |
| CN112456523A (en) * | 2020-12-08 | 2021-03-09 | 山东理工大学 | Method for preparing high-purity magnesium chloride hexahydrate product by directly leaching magnesium element in magnesite |
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| CN103820640B (en) * | 2014-03-12 | 2015-12-30 | 胡雷 | A kind of method of wet underwater welding iron from red soil nickel ore |
| CN103820640A (en) * | 2014-03-12 | 2014-05-28 | 胡雷 | Method for extracting iron from laterite nickel ore by adopting wet process |
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| CN106315630A (en) * | 2016-08-30 | 2017-01-11 | 荆门市格林美新材料有限公司 | Method for preparing high-purity flame-retardant magnesium hydroxide through recovery from heavy-metal sludge |
| CN106673025A (en) * | 2016-11-18 | 2017-05-17 | 江苏仁欣环保科技有限公司 | Technological method for producing magnesium hydroxide by utilization of magnesium-containing wastewater generated by laterite nickel ore wet-process |
| CN106674590B (en) * | 2016-12-26 | 2018-04-20 | 荆门市格林美新材料有限公司 | The method that magnalium prepares composite flame-retardant agent is recycled from sludge |
| CN106674590A (en) * | 2016-12-26 | 2017-05-17 | 荆门市格林美新材料有限公司 | Method for recycling aluminum and magnesium from sludge and preparing composite flame retardant |
| CN108754168A (en) * | 2018-04-20 | 2018-11-06 | 中国瑞林工程技术有限公司 | A kind of processing method of sulfur-bearing leached mud and its application |
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| CN112110495A (en) * | 2020-08-24 | 2020-12-22 | 斯瑞尔环境科技股份有限公司 | Method for producing flaky crystalline ferric chloride |
| CN112456523A (en) * | 2020-12-08 | 2021-03-09 | 山东理工大学 | Method for preparing high-purity magnesium chloride hexahydrate product by directly leaching magnesium element in magnesite |
| CN112456523B (en) * | 2020-12-08 | 2022-06-17 | 山东理工大学 | Method for preparing high-purity magnesium chloride hexahydrate product by directly leaching magnesium element in magnesite |
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