WO2022036775A1 - 一种从红土镍矿中回收多种有价金属及酸碱双介质再生循环的方法 - Google Patents

一种从红土镍矿中回收多种有价金属及酸碱双介质再生循环的方法 Download PDF

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WO2022036775A1
WO2022036775A1 PCT/CN2020/114550 CN2020114550W WO2022036775A1 WO 2022036775 A1 WO2022036775 A1 WO 2022036775A1 CN 2020114550 W CN2020114550 W CN 2020114550W WO 2022036775 A1 WO2022036775 A1 WO 2022036775A1
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acid
scandium
ore
reaction
nickel
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PCT/CN2020/114550
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French (fr)
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王成彦
马保中
赵林
陈永强
但勇
金长浩
赵澎
高波
赵顶
姜静
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四川顺应动力电池材料有限公司
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Priority to CU2023000008A priority Critical patent/CU20230008A7/es
Priority to AU2020463690A priority patent/AU2020463690B2/en
Publication of WO2022036775A1 publication Critical patent/WO2022036775A1/zh

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    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
    • C22B3/06—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic acid solutions, e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions
    • C22B3/065—Nitric acids or salts thereof
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B21/00—Nitrogen; Compounds thereof
    • C01B21/20—Nitrogen oxides; Oxyacids of nitrogen; Salts thereof
    • C01B21/38—Nitric acid
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
    • C01F5/00—Compounds of magnesium
    • C01F5/02—Magnesia
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
    • C01F7/00—Compounds of aluminium
    • C01F7/02—Aluminium oxide; Aluminium hydroxide; Aluminates
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B21/00—Obtaining aluminium
    • C22B21/0015—Obtaining aluminium by wet processes
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B23/00—Obtaining nickel or cobalt
    • C22B23/04—Obtaining nickel or cobalt by wet processes
    • C22B23/0407—Leaching processes
    • C22B23/0415—Leaching processes with acids or salt solutions except ammonium salts solutions
    • C22B23/0438—Nitric acids or salts thereof
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B23/00—Obtaining nickel or cobalt
    • C22B23/04—Obtaining nickel or cobalt by wet processes
    • C22B23/0453—Treatment or purification of solutions, e.g. obtained by leaching
    • C22B23/0461—Treatment or purification of solutions, e.g. obtained by leaching by chemical methods
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B26/00—Obtaining alkali, alkaline earth metals or magnesium
    • C22B26/20—Obtaining alkaline earth metals or magnesium
    • C22B26/22—Obtaining magnesium
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
    • C22B3/44—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B47/00—Obtaining manganese
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B59/00—Obtaining rare earth metals
    • 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

Definitions

  • the invention belongs to the intersecting field of metallurgy and chemical industry, and particularly relates to a process method for recovering various valuable metals from laterite nickel ore and regenerating and recycling acid and alkali dual media.
  • Aluminum, nickel and cobalt metals are commonly used metals in industrial and civil industries, especially nickel metals, which are mainly used in stainless steel, alloy steel and special alloys. With the continuous reduction of nickel sulfide ore resources, and cobalt associated with laterite nickel ore, efficient and economical extraction of valuable metals from laterite nickel ore has become the focus of research.
  • the processing technology of laterite nickel ore is mainly divided into fire method and wet method.
  • the fire method is mainly suitable for the treatment of nickel sulfide ore and laterite nickel ore with high nickel content; the wet method is suitable for the treatment of limonite-type laterite nickel ore and other minerals with low nickel content.
  • the wet method has the advantages of low energy consumption, low cost and low pollution. And the advantages of recycling cobalt at the same time.
  • the wet process for refining laterite nickel ore is mainly normal pressure acid leaching and pressurized acid leaching process.
  • elements such as Co, Mn, Al, Fe, Mg, etc. will exist in the acid leaching solution.
  • the prior art The extraction of metal elements in the acid leaching solution is often to add alkaline substances, such as magnesium oxide, to the leaching solution, adjust the pH value of the solution, first precipitate and separate the impurity aluminum hydroxide iron slag at pH 3-4, and then separate the impurities at pH 7-9.
  • the crude nickel cobalt manganese hydroxide is precipitated, and then the final products of nickel and cobalt, such as nickel sulfate, cobalt sulfate, electrolytic nickel, and electrolytic cobalt, are purified by combining the acid leaching process with extraction, electrolysis, evaporation concentration and other technologies.
  • nickel and cobalt such as nickel sulfate, cobalt sulfate, electrolytic nickel, and electrolytic cobalt
  • the appearance of aluminum hydroxide flocculation often occurs, which makes the filterability of aluminum hydroxide slag difficult, and the precipitated aluminum hydroxide slag will entrain more nickel and cobalt metals. elements, resulting in a certain loss in the recovery of nickel and cobalt metals.
  • nitric acid is expensive, and a large amount of alkali (MgO) is used for pH adjustment.
  • Chinese patent CN108950205B discloses a method of using alkaline substances calcium carbonate and magnesium carbonate to grind finely and mix them with water, and then control the flow rate and add the acid leaching solution into the stirring tank at the same time, control the pH value of the solution, and homogeneously precipitate aluminum iron slag, Although this method can improve the filtration performance of the precipitate to a certain extent, the content of nickel-cobalt metal entrained in the precipitate is also about 1-2%, resulting in the loss of nickel-cobalt metal recovery.
  • the present invention provides a method for recovering various valuable metals and acid-base dual medium regeneration cycle from laterite nickel ore.
  • adding alkaline substances to precipitate aluminum and nickel-cobalt separation process due to the formation of aluminum hydroxide flocculent precipitation, the recovery has problems of poor filterability and entrainment of nickel-cobalt metal in aluminum slag, which improves the total recovery of nickel-cobalt metal. Rate.
  • the magnesium nitrate solution after precipitating AlNiCoMnMnSc is evaporated and concentrated to obtain magnesium nitrate crystals for subsequent decomposition and regeneration of magnesium nitrate to obtain acid (nitric acid) and alkali (magnesium oxide), realizing the acid-base dual medium regeneration cycle.
  • the raw material of this process has strong adaptability and is especially suitable for the treatment of limonite laterite nickel ore with high aluminum content.
  • a method for recovering multiple valuable metals and acid-base dual medium regeneration cycle from laterite nickel ore comprising the following steps:
  • scandium salt is produced by extracting scandium, back extraction, and crystallization, and the solution after extracting scandium is used for the preparation of nickel-cobalt-manganese ternary material, or by fractional extraction, back-extraction, and crystallization, Production of nickel, cobalt and manganese products.
  • the laterite nickel ore described in step (1) is a typical limonite-type high iron and low nickel ore, and the mass fraction of its chemical composition is: Ni is 0.5-2.0%; Co is 0.05-0.20%; Fe is 35 ⁇ 55%; Al is 0.5-5.0%; Mn is 0.1-3.0%; Mg is 0.50-5.0%; Sc is 30-130 g/t.
  • the concentration of the nitric acid in the step (1) is 120-230 g/L, and the solid-liquid ratio of the mineral powder mixed with the nitric acid is 1:0.5-1:5 g/ml.
  • the autoclave is equipped with a stirring device, and the pulp is stirred during the leaching process, and the stirring speed is 150-250 rpm; the leaching temperature of the leaching reaction is 160-220 ° C, and the leaching time is 0.5 ⁇ 3h.
  • step (2) magnesium oxide is added to the pulp for pre-neutralization to adjust its pH value to 2.5-3.5.
  • step (3) magnesium oxide is added to the overflow liquid to adjust its pH value to 7.0 ⁇ 10.0; the reaction temperature of the precipitation reaction is 40 ⁇ 100°C, and the reaction time is 0.5 ⁇ 3.5h.
  • step (4) the reaction temperature of adding alkali to dissolve the first precipitation filter residue is 140-200 ° C, the reaction time is 1-4 h, and the pH value range of the reaction is 12.5-14.0; the alkali used includes sodium hydroxide and Any of potassium hydroxide and combinations thereof.
  • step (4) also includes adding carbon dioxide or aluminum hydroxide seed crystals to the liquid after filtration of the second precipitation filter residue to obtain an aluminum hydroxide product.
  • reaction temperature of dissolving the second precipitation filter residue with sulfuric acid in step (5) is 30-100° C.
  • the reaction time is 1.0-2.5h
  • the pH range of the reaction is 0.5-3.5.
  • the scandium salt described in step (5) includes any form in scandium oxalate, scandium nitrate, and scandium chloride, but is not limited to these types, so it is collectively referred to as scandium salt.
  • step (5) also includes that the produced scandium salt is heated and decomposed to obtain scandium oxide, the heating temperature is 300 °C ⁇ 800 °C, and the decomposition mode includes any one of calcination decomposition, spray decomposition, suspension boiling decomposition and combination thereof. ;
  • the product scandium oxide can be sold as a commodity.
  • the above-mentioned method also includes the regeneration cycle of the acid-base dual medium, and the steps are as follows:
  • the first precipitation filtrate obtains magnesium nitrate crystal through evaporation and concentration, and the magnesium nitrate crystal enters into the decomposition furnace for pyrolysis after being heated and melted to form high temperature dust gas;
  • Magnesium oxide powder is separated from the high-temperature dust and gas through the dust collection system, and the produced magnesium oxide is returned to the first precipitation process; a part of the NOx gas after the dust collection is heated by the combustion furnace and recycled to the decomposition furnace for nitric acid again.
  • Magnesium pyrolysis another part of NOx enters the nitric acid regeneration system, and condensed dilute nitric acid is obtained through exhaust heat exchange, deep dust removal, secondary cooling and condensation, and then the condensed acid is pumped into the absorption tower, and the gas that has not been condensed and absorbed passes through nitrogen oxides
  • the compressor is pressurized and concentrated, enters the absorption tower to prepare nitric acid, and the produced nitric acid is returned to the leaching process.
  • the decomposition method of the decomposition furnace described in step (6) includes any one of boiling decomposition, calcination decomposition, and spray decomposition, but is not limited to the above methods, and the decomposition temperature in the furnace is 400 ° C ⁇ 900 ° C; the high temperature Dust gas contains magnesium oxide, water vapor, NOx, and oxygen.
  • step (7) 20-95% of the NOx gas after dust collection is heated by the combustion furnace, and then recycled into the decomposition furnace for pyrolysis of magnesium nitrate.
  • the temperature is lowered to below 120°C in the cooling system to obtain a large amount of condensed acid, and the concentration of condensed acid is 20-35%; NOx is pressurized to about 4.0Mpa ⁇ 5.0Mpa, and sent to the absorption tower to absorb and prepare nitric acid.
  • the aforementioned condensing acid is used as the absorbent, and the exhaust gas after absorption is treated and discharged up to the standard.
  • the present invention avoids the problem of poor filterability of flocculent aluminum hydroxide in the traditional process, and the obtained aluminum hydroxide has a high purity in this process.
  • the acid and alkali used in the process can be regenerated and recycled, which reduces the purchase of auxiliary materials and reduces the direct processing cost.
  • the condensed acid formed in the process is used in the subsequent nitric acid regeneration system to prepare nitric acid, which turns waste acid into treasure, improves the efficiency of nitric acid regeneration, and reduces fixed investment and nitric acid regeneration cost.
  • Fig. 1 is a kind of process flow diagram of the present invention that reclaims multiple valuable metals and acid-base dual medium regeneration cycle method from laterite nickel ore.
  • the invention discloses a method for recovering various valuable metals from laterite nickel ore and regenerating and recycling acid-base dual media.
  • the method firstly crushes and finely ground the ore of laterite nickel ore to obtain ore powder, then configures it into slurry for high-pressure leaching of nitric acid, and the obtained leaching slurry is subjected to pH adjustment and intensive washing to achieve solid-liquid separation to obtain leaching slag and The leaching solution and the leaching slag are filtered and dried and then pelletized and sintered to obtain iron concentrate.
  • Magnesium oxide is added to the leaching solution to adjust the pH value of the solution, and the AlNiCoMnSc and a small amount of iron in the acid leaching solution are completely precipitated.
  • the pH value and reaction temperature of the solution are controlled to dissolve the precipitation alkali, and the aluminum hydroxide in the mixture is converted into aluminate ions and dissolved in the alkali solution, and is separated from the nickel-cobalt-manganese-scandium precipitation by filtration.
  • the aluminum hydroxide product is obtained by precipitation in the alkaline solution by adding carbon dioxide or aluminum hydroxide seeds.
  • the nickel-cobalt-manganese-scandium precipitation mixture is dissolved with sulfuric acid, after scandium extraction, back-extraction and crystallization, the produced scandium salt is heated and decomposed to obtain scandium oxide, which is sold as a commodity. After fractional extraction of manganese/cobalt/nickel, back extraction and crystallization, nickel, cobalt and manganese products are obtained.
  • the magnesium nitrate solution after precipitation of AlNiCoMnSc is evaporated and concentrated to obtain magnesium nitrate crystals, and the magnesium nitrate crystals are heated to melting, and then added to the decomposition furnace.
  • Magnesium nitrate melt is rapidly decomposed by heating to form magnesium oxide, NO x , O 2 and so on.
  • the dust-containing gas passes through the dust collection system to obtain high-purity active magnesium oxide.
  • a part of the NOx gas is heated by the combustion furnace and then enters the decomposition system again to pyrolyze the magnesium nitrate melt.
  • the other part of the NOx gas is cooled down and flows to the The nitric acid regeneration system produces nitric acid.
  • the gas entering the nitric acid regeneration system is subjected to exhaust heat exchange, deep dust removal, secondary cooling and condensation to obtain condensed dilute nitric acid.
  • the subsequent gas is pressurized and concentrated by the nitrogen oxide compressor and enters the absorption tower.
  • the condensed acid obtained by the previous condensation is pumped to the corresponding tray of the nitric acid absorption tower for the preparation of nitric acid after measuring the concentration.
  • the industrial nitric acid produced by the nitric acid regeneration system will be used for the front-end leaching process, and the obtained high-purity active magnesium oxide will be used for the pH adjustment of the front-end.
  • the process is efficient and simple, and avoids the formation of aluminum hydroxide flocculent precipitates in the process of adding alkaline substances to control the pH value of the nitric acid leaching solution of laterite nickel ore to precipitate aluminum and nickel-cobalt, resulting in poor filtration and aluminum slag in the recovery process.
  • the problem of entrainment of nickel-cobalt metal, so the overall recovery of nickel-cobalt metal is improved.
  • the magnesium nitrate solution after precipitating AlNiCoMnSc is evaporated and concentrated to obtain magnesium nitrate crystals for subsequent decomposition and regeneration of magnesium nitrate to obtain acid (nitric acid) and alkali (magnesium oxide), realizing the acid-base dual medium regeneration cycle.
  • the raw material of the process has strong adaptability, and is especially suitable for the treatment of limonite-type laterite nickel ore with high aluminum content.
  • the laterite-nickel ore ore containing 0.6% nickel, 0.05% cobalt, 48% iron, 1.3% aluminum, 0.15% manganese, 0.6% magnesium and 43 g/t scandium is crushed and finely ground to obtain ore powder as a raw material for later use.
  • the obtained mineral powder, nitric acid, and water are fully stirred and mixed in a slurry tank with a liquid-solid ratio (1:5g/mL) and an initial acid concentration (120g/L) to form a pulp, and then the pulp is pumped into the nitric acid.
  • Leaching is carried out in an autoclave.
  • the leaching temperature was 160° C.
  • the leaching time was 1 h
  • the stirring speed was 170 rpm.
  • magnesium oxide was added to the pulp to pre-neutralize to adjust the pH to 2.5, and then the pulp was densely washed to obtain underflow and overflow.
  • the bottom stream is filtered and dried to carry out pelletizing and sintering process to obtain iron concentrate with iron content of 54%, and magnesium oxide is added to the overflow liquid for precipitation reaction.
  • the reaction temperature was controlled to be 65° C.
  • the pH value of the solution was 7.0
  • the first precipitation filter residue was obtained by filtration.
  • add sodium hydroxide solution to the first precipitation filter residue, control the pH value of the reaction solution to be 12.5, and control the reaction temperature to be 140 ° C.
  • the second precipitation filter residue is mixed with sulfuric acid solution, and the pH of the reaction solution is controlled to be 2.0, and the reaction temperature is 80 ° C.
  • nickel sulfate, cobalt, manganese, and scandium solutions are obtained by filtration, and then scandium extraction, back extraction, Crystallization, the produced scandium oxalate, the scandium oxalate is calcined and decomposed at a temperature of 650°C to obtain Sc 2 O 3 with a content of 98%, which is sold as a commercial product.
  • the liquid is subjected to fractional extraction of manganese/cobalt/nickel and crystallization to obtain nickel sulfate solution, cobalt sulfate solution, manganese sulfate solution and scandium salt solution. .
  • the first precipitation filtrate was evaporated and concentrated to obtain magnesium nitrate crystals, which were heated and melted and then introduced into a decomposition furnace. The temperature in the decomposition furnace was 450°C. Magnesium nitrate is rapidly decomposed into nitrogen oxide gas, water vapor, magnesium oxide and oxygen in the decomposition furnace.
  • the obtained condensed acid is pumped into the corresponding tray of the absorption tower, and finally the regenerated nitric acid with a concentration of 48% is obtained at the bottom of the tower, and the absorbed tail gas is treated and discharged up to the standard.
  • the laterite-nickel ore containing 0.87% nickel, 0.085% cobalt, 49% iron, 1.9% aluminum, 0.9% manganese, 1.3% magnesium and 66g/t scandium is crushed and finely ground to obtain ore powder as raw material for later use.
  • the obtained mineral powder, nitric acid, and water are fully stirred and mixed in a slurry tank with a liquid-solid ratio (1:2g/mL) and an initial acid concentration (150g/L) to make a pulp, and then the pulp is pumped into the nitric acid.
  • Leaching is carried out in an autoclave.
  • the leaching temperature was 180° C.
  • the leaching time was 2 h
  • the stirring speed was 180 rpm.
  • magnesium oxide was added to the pulp to pre-neutralize to adjust the pH to 2.5, and then the pulp was densely washed to obtain underflow and overflow.
  • the bottom stream is filtered and dried for pelletizing and sintering to obtain iron concentrate with an iron content of 59%.
  • the magnesium oxide was added to the overflow liquid to carry out the precipitation reaction, the reaction temperature was controlled to be 80° C., and the pH value of the solution was 8.0. After 1 h of precipitation reaction, the first precipitation residue was obtained by filtration.
  • the closed reaction kettle add sodium hydroxide solution to the first precipitation filter residue, control the pH value of the reaction solution to be 13.0, control the reaction temperature to 160 ° C, and after the reaction for 3h, filter to obtain the second precipitation filter residue and filtrate.
  • the filtrate was subjected to precipitation treatment by carbon fractionation, and the precipitated aluminum hydroxide was obtained by filtration.
  • the second precipitation filter residue is mixed with the sulfuric acid solution, and the pH of the reaction solution is controlled to be 1.0, and the reaction temperature is 40 ° C.
  • the nickel sulfate, cobalt, manganese and scandium solutions are obtained by filtration, and then the scandium is extracted and crystallized to produce
  • the resulting scandium nitrate was calcined and decomposed at a temperature of 500° C. to obtain Sc 2 O 3 with a content of 97%, which was sold as a commercial product.
  • the liquid is subjected to fractional extraction of manganese/cobalt/nickel and crystallization to obtain nickel sulfate solution, cobalt sulfate solution, manganese sulfate solution and scandium salt solution. .
  • the first precipitation filtrate was evaporated and concentrated to obtain magnesium nitrate crystals, which were heated and melted and then introduced into a decomposition furnace.
  • the temperature in the decomposition furnace was 500°C.
  • Magnesium nitrate is rapidly decomposed into nitrogen oxide gas, water vapor, magnesium oxide and oxygen in the decomposition furnace.
  • high-purity active magnesium oxide with a content of more than 94.3% is obtained, and 60% of the gas after dust collection is heated in a combustion furnace, and then enters the decomposition furnace again for heating and decomposition of magnesium nitrate.
  • the other part of the gas is deeply dedusted and then cooled to reduce the temperature to 100°C to obtain condensed nitric acid with a concentration of 27%.
  • the residual gas is pressurized to 4.2Mpa by the nitrogen oxide compressor and then introduced into the absorption tower.
  • the obtained condensed acid is pumped into the corresponding plate of the absorption tower, and finally the regenerated nitric acid with a concentration of 49% is obtained at the bottom of the tower, and the absorbed tail gas is treated and discharged up to the standard.
  • the laterite-nickel ore ore containing 1.0% nickel, 0.11% cobalt, 45% iron, 2.7% aluminum, 1.5% manganese, 2.7% magnesium and 85g/t scandium is crushed and finely ground to obtain ore powder as a raw material for later use.
  • the obtained mineral powder, nitric acid, and water are fully stirred and mixed in a slurry tank with a liquid-solid ratio (1:3g/mL) and an initial acid concentration (180g/L) to form a pulp, and then the pulp is pumped into the nitric acid.
  • Leaching is carried out in an autoclave.
  • the leaching temperature was 170°C
  • the leaching time was 3h
  • the stirring speed was 190rpm.
  • magnesium oxide was added to the pulp to pre-neutralize to adjust the pH to 3.0, and then the pulp was densely washed to obtain underflow and overflow.
  • the bottom stream is filtered and dried for pelletizing and sintering to obtain iron concentrate with an iron content of 56%.
  • the magnesium oxide was added to the overflow liquid to carry out the precipitation reaction, the reaction temperature was controlled to be 70° C., and the pH value of the solution was 7.5.
  • the first precipitation filter residue was obtained by filtration. Then in a closed reaction kettle, add sodium hydroxide solution to the first precipitation filter residue, control the pH value of the reaction solution to be 14.0, and control the reaction temperature to be 180 ° C.
  • the second precipitation filter residue is mixed with the sulfuric acid solution, and the pH of the reaction solution is controlled to be 0.5, and the reaction temperature is 60 ° C.
  • the nickel sulfate, cobalt, manganese, and scandium solutions are obtained by filtration, and then scandium extraction and crystallization are performed to produce
  • the resulting scandium chloride is calcined and decomposed at a temperature of 800° C. to obtain Sc 2 O 3 with a content of 99%, which is sold as a commercial product.
  • the liquid is subjected to fractional extraction of manganese/cobalt/nickel and crystallization to obtain nickel sulfate solution, cobalt sulfate solution, manganese sulfate solution and scandium salt solution. .
  • the first precipitation filtrate was evaporated and concentrated to obtain magnesium nitrate crystals, which were heated and melted and then introduced into a decomposition furnace. The temperature in the decomposition furnace was 600°C. Magnesium nitrate is rapidly decomposed into nitrogen oxide gas, water vapor, magnesium oxide and oxygen in the decomposition furnace.
  • the obtained condensed acid is pumped into the corresponding tray of the absorption tower, and finally the regenerated nitric acid with a concentration of 53% is obtained at the bottom of the tower, and the absorbed tail gas is treated and discharged up to the standard.
  • the laterite-nickel ore ore containing 1.5% nickel, 0.14% cobalt, 43% iron, 3.5% aluminum, 2.1% manganese, 3.6% magnesium and 91 g/t scandium is crushed and finely ground to obtain ore powder as a raw material for later use.
  • the obtained mineral powder, nitric acid, and water are fully stirred and mixed in a slurry tank with a liquid-solid ratio (1:4g/mL) and an initial acid concentration (200g/L) to form a pulp, and then the pulp is pumped into the nitric acid.
  • Leaching is carried out in an autoclave.
  • the leaching temperature was 190° C.
  • the leaching time was 2.5 h
  • the stirring speed was 200 rpm.
  • magnesium oxide was added to the pulp to pre-neutralize to adjust the pH to 2.5, and then the pulp was densely washed to obtain underflow and overflow.
  • the bottom stream is filtered and dried for pelletizing and sintering to obtain iron concentrate with an iron content of 53%.
  • the magnesium oxide was added to the overflow liquid to carry out the precipitation reaction, the reaction temperature was controlled to be 55°C, and the pH value of the solution was 9.0.
  • the first precipitation residue was obtained by filtration. Then, in a closed reaction kettle, add sodium hydroxide solution to the first precipitation filter residue, control the pH value of the reaction solution to be 14.0, and control the reaction temperature to be 170° C.
  • the second precipitation filter residue is mixed with the sulfuric acid solution, and the pH of the reaction solution is controlled to be 3.0, and the reaction temperature is 70 ° C.
  • the nickel sulfate, cobalt, manganese and scandium solutions are obtained by filtration, and then the scandium is extracted and crystallized to produce a solution.
  • the scandium oxalate is calcined and decomposed at a temperature of 650 ° C to obtain Sc 2 O 3 with a content of 99%, which is sold as a commercial product.
  • the liquid is subjected to fractional extraction of manganese/cobalt/nickel and crystallization to obtain nickel sulfate solution, cobalt sulfate solution, manganese sulfate solution and scandium salt solution. .
  • the first precipitation filtrate was evaporated and concentrated to obtain magnesium nitrate crystals, which were heated and melted and then introduced into a decomposition furnace. The temperature in the decomposition furnace was 700°C. Magnesium nitrate is rapidly decomposed into nitrogen oxide gas, water vapor, magnesium oxide and oxygen in the decomposition furnace.
  • the obtained condensed acid is pumped into the corresponding tray of the absorption tower, and finally the regenerated nitric acid with a concentration of 55% is obtained at the bottom of the tower, and the absorbed tail gas is treated and discharged up to the standard.
  • the laterite-nickel ore ore containing 1.8% nickel, 0.19% cobalt, 38% iron, 4.3% aluminum, 2.7% manganese, 4.5% magnesium and 119g/t scandium is crushed and finely ground to obtain ore powder as a raw material for later use.
  • the obtained mineral powder, nitric acid, and water are fully stirred and mixed in the slurry tank at the liquid-solid ratio (1:0.5g/mL) and the initial acid concentration (130g/L) to make the pulp, and then the pulp is pumped into the Leaching is carried out in a nitric acid autoclave.
  • the leaching temperature was 220° C.
  • the leaching time was 0.5 h
  • the stirring speed was 200 rpm.
  • magnesium oxide was added to the pulp to pre-neutralize to adjust the pH to 3.5, and then the pulp was thickly washed to obtain underflow and overflow.
  • the bottom stream is filtered and dried for pelletizing and sintering to obtain iron concentrate with an iron content of 50%.
  • the magnesium oxide was added to the overflow liquid to carry out the precipitation reaction, the reaction temperature was controlled to be 90° C., and the pH value of the solution was 10.0. After the precipitation reaction for 1.0 h, the first precipitation filter residue was obtained by filtration.
  • the closed reaction kettle add sodium hydroxide solution to the first precipitation filter residue, control the pH value of the reaction solution to be 12.5, control the reaction temperature to be 200 ° C, and after the reaction for 2 hours, filter to obtain the second precipitation filter residue and filtrate.
  • the filtrate was subjected to precipitation treatment by carbon fractionation, and the precipitated aluminum hydroxide was obtained by filtration.
  • the second precipitation filter residue is mixed with the sulfuric acid solution, and the pH of the reaction solution is controlled to be 0.5, and the reaction temperature is 65 ° C.
  • the nickel sulfate, cobalt, manganese and scandium solutions are obtained by filtration, and then the scandium is extracted and crystallized to produce a solution.
  • the scandium oxalate is calcined and decomposed at a temperature of 700 ° C to obtain Sc 2 O 3 with a content of 99%, which is sold as a commercial product.
  • the liquid is subjected to fractional extraction of manganese/cobalt/nickel and crystallization to obtain nickel sulfate solution, cobalt sulfate solution, manganese sulfate solution, and scandium salt solution. .
  • the first precipitation filtrate was evaporated and concentrated to obtain magnesium nitrate crystals, which were heated and melted and then introduced into a decomposition furnace. The temperature in the decomposition furnace was 850°C.
  • Magnesium nitrate is rapidly decomposed into nitrogen oxide gas, water vapor, magnesium oxide and oxygen in the decomposition furnace. After dust collection, high-purity active magnesium oxide with a content of more than 99% is obtained, and 20% of the gas after dust collection is heated in a combustion furnace, and then enters the decomposition furnace again for heating and decomposition of magnesium nitrate. The other part of the gas is cooled down to 60°C after deep dust removal to obtain condensed nitric acid with a concentration of 31%. The residual gas is pressurized to 5.0Mpa by the nitrogen oxide compressor and then introduced into the absorption tower.
  • the obtained condensed acid is pumped into the corresponding tray of the absorption tower, and finally the regenerated nitric acid with a concentration of 56% is obtained at the bottom of the tower, and the absorbed tail gas is treated and discharged up to the standard.

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Abstract

一种从红土镍矿中回收多种有价金属及酸碱双介质再生循环的方法，首先将红土镍矿原矿细磨得到矿粉，配置成浆后进行硝酸浸出，浸出渣经球团烧结工艺得到铁精矿；调节浸出液pH值，将铝镍钴锰钪及少量铁完全沉淀出来，将沉淀碱溶解，实现铝分离；镍钴锰钪沉淀混合物酸解后分级萃取，得到钪、镍、钴、锰产品；沉淀铝镍钴锰钪后的硝酸镁溶液经蒸发浓缩得到硝酸镁晶体用于后续硝酸镁分解再生获得酸和碱，实现酸碱双介质再生循环。该方法避免了在红土镍矿酸浸液加入碱性物质沉淀铝与镍钴分离过程中，由于氢氧化铝絮状沉淀的生成导致回收出现过滤性差及铝渣中夹带镍钴金属的问题，提高了镍钴金属总回收率。

Description

一种从红土镍矿中回收多种有价金属及酸碱双介质再生循环的方法 技术领域
本发明属于冶金和化工的交叉领域，具体涉及一种从红土镍矿中回收多种有价金属及酸碱双介质再生循环的工艺方法。
背景技术
铝、镍、钴金属是工业与民用行业中很常用的金属，特别是镍金属，主要用于不锈钢、合金钢和特种合金等。随着硫化镍矿资源的不断减少，而红土镍矿伴生钴，从红土镍矿中高效、经济提取有价金属已成为研究焦点。红土镍矿处理工艺主要分为火法和湿法。火法主要适用于处理硫化镍矿和含镍品位较高的红土镍矿；湿法适合处理褐铁型红土镍矿等含镍较低的矿物，湿法具有能耗小、成本低、污染小及可同时回收钴等优势。
现在对红土镍矿进行提炼的湿法工艺主要是常压酸浸与加压酸浸工艺，无论哪种方法，酸浸液中都会存在Co、Mn、Al、Fe、Mg等元素，现有技术对酸浸液中金属元素的提取往往是在浸出液中加入碱性物质，例如氧化镁，调整溶液pH值，先在pH 3～4沉淀分离出杂质氢氧化铝铁渣，然后在pH 7～9沉淀出产品粗制氢氧化镍钴锰，然后使用酸浸工艺与萃取、电解、蒸发浓缩等技术结合，提纯出镍钴的最终产品，如硫酸镍、硫酸钴、电解镍、电解钴。但是在沉淀分离出铝金属的过程中，常常会出现氢氧化铝絮状沉淀的出现导致氢氧化铝渣的过滤性较难的问题，而且沉淀氢氧化铝渣会夹带较多的镍、钴金属元素，导致镍钴金属的回收产生一定的损失。并且硝酸价格昂贵，pH调节要使用大量的碱(MgO),如果不考虑回收该工艺经济效益显著下降。
中国专利CN108950205B公开了一种采用碱性物质碳酸钙与碳酸镁磨细与水混合均匀，然后控制流速与酸浸液同时加入搅拌槽中，控制溶液的pH值，均相沉淀出铝铁渣，此方法虽然能够在一定程度上改善了沉淀物的过滤性能，但沉淀物中夹带的镍钴金属的含量也有1～2％左右，造成镍钴金属的回收损失。
发明内容
针对现有技术中存在的缺陷与不足，本发明提供了一种从红土镍矿中回收多种有价金属及酸碱双介质再生循环的方法，该工艺流程高效简洁，避免了在红土镍矿硝酸 浸出液中，加入碱性物质沉淀铝与镍钴分离过程中，由于氢氧化铝絮状沉淀的生成导致回收出现过滤性差和铝渣中夹带镍钴金属的问题，提高了镍钴金属的总回收率。同时，沉淀铝镍钴锰钪后的硝酸镁溶液经过蒸发浓缩得到硝酸镁晶体用于后续硝酸镁分解再生获得酸(硝酸)和碱(氧化镁)，实现了酸碱双介质再生循环。该工艺原料适应性强，特别适用于含铝较高的褐铁型红土镍矿的处理。
本发明是通过以下技术方案实现的：
一种从红土镍矿中回收多种有价金属及酸碱双介质再生循环的方法，包括以下步骤：
(1)将红土镍矿原矿破碎并细磨得到矿粉，将矿粉与硝酸混合并充分搅拌制成矿浆；
(2)将矿浆泵入高压釜中进行浸出反应，反应结束后预中和调节矿浆的pH值，之后矿浆经过多级浓密洗涤得到底流和溢流液；
(3)底流经过滤干燥，进行球团烧结得到铁精矿，溢流液调节pH值后进行沉淀反应，反应结束后，酸浸液中的铝、镍、钴、锰、钪及少量铁完全沉淀出来，与硝酸镁溶液分离，过滤得到第一沉淀滤渣；
(4)将第一沉淀滤渣加碱溶解，将滤渣中的氢氧化铝转化为铝酸根离子溶于碱液中，过滤得到第二沉淀滤渣。在过滤后液中加入二氧化碳或氢氧化铝晶种沉淀获得氢氧化铝产品；
(5)第二沉淀滤渣用硫酸溶解后，经萃钪、反萃、结晶生产得到钪盐，萃钪后液用于镍钴锰三元材料的制备，或经分级萃取、反萃、结晶，生产镍、钴、锰产品。
进一步的，步骤(1)中所述红土镍矿为典型的褐铁矿型高铁低镍矿石，其化学组成的质量分数为：Ni为0.5～2.0％；Co为0.05～0.20％；Fe为35～55％；Al为0.5～5.0％；Mn为0.1～3.0％；Mg为0.50～5.0％；Sc为30～130g/t。
进一步的，步骤(1)中所述硝酸的浓度为120～230g/L，矿粉与硝酸混合的固液比为1:0.5-1:5g/ml。
进一步的，步骤(2)中所述高压釜带有搅拌装置，在浸出过程中对矿浆进行搅拌，搅拌速率为150-250rpm；所述浸出反应的浸出温度为160～220℃，浸出时间为0.5～3h。
进一步的，步骤(2)中向矿浆中加入氧化镁预中和调节其pH值至2.5～3.5。
进一步的，步骤(3)中向溢流液中加入氧化镁调节其pH值至7.0～10.0；所述沉 淀反应的反应温度为40～100℃，反应时间为0.5～3.5h。
进一步的，步骤(4)中将第一沉淀滤渣加碱溶解的反应温度为140～200℃，反应时间1～4h，反应的pH值范围为12.5～14.0；所使用的碱包括氢氧化钠和氢氧化钾中任何一种及其组合形式。
进一步的，步骤(4)还包括向第二沉淀滤渣过滤后液中加入二氧化碳或氢氧化铝晶种沉淀获得氢氧化铝产品。
进一步的，步骤(5)第二沉淀滤渣用硫酸溶解的反应温度为30～100℃，反应时间为1.0～2.5h，反应的pH范围为0.5～3.5。
进一步的，步骤(5)所述钪盐包括草酸钪、硝酸钪、氯化钪中任一种形式，但不局限于这几种，因此统称为钪盐。
进一步的，步骤(5)还包括生产出的钪盐经加热分解得到氧化钪，加热温度为300℃～800℃，分解方式包括煅烧分解、喷雾分解、悬浮沸腾分解中任意一种及其组合形式；产物氧化钪可以作为商品出售。
上述方法还包括酸碱双介质的再生循环，步骤如下：
(6)第一沉淀滤液经蒸发浓缩得到硝酸镁晶体，所述硝酸镁晶体加热熔化后进入分解炉热解，形成高温尘气；
(7)高温尘气经收尘系统后分离出氧化镁粉体，产出的氧化镁返回第一沉淀工序；收尘后一部分NO x气体经燃烧炉加热，再次循环到分解炉内用于硝酸镁的热解，另一部分NO x进入硝酸再生系统，经尾气换热、深度除尘、二次降温冷凝获得冷凝稀硝酸，再将冷凝酸泵入至吸收塔，未被冷凝吸收的气体经过氧化氮压缩机加压增浓，进入吸收塔制备硝酸，产出的硝酸返回浸出工序。
进一步的，步骤(6)中所述分解炉的分解方式包括沸腾分解、煅烧分解、喷雾分解中任何一种但不局限于上述方式，炉内的分解温度为400℃～900℃；所述高温尘气包含氧化镁、水蒸气、NOx、氧气。
进一步的，步骤(7)中收尘后20～95％的NO x气体经燃烧炉加热，再次循环到分解炉内用于硝酸镁的热解。
进一步的，步骤(7)中进入硝酸再生系统的NO x经过深度除尘后，至冷却系统将温度下降至120℃以下，获得大量冷凝酸，冷凝酸浓度为20～35％；未被冷凝吸收的NO x经加压至约4.0Mpa～5.0Mpa，送入吸收塔吸收制备硝酸，该过程用前述的冷凝酸作为吸收剂，吸收后的尾气经处理后达标排出。
本发明技术方案具有如下有益效果：
(1)本发明避免了传统工艺过程中存在絮状氢氧化铝过滤性差的问题，并且本工艺所得氢氧化铝纯度高。
(2)全程镍钴金属的总回收率得到了提升，进一步增加了本工艺的经济效益。
(3)实现了铝钪的高效分离与回收，应用前景广阔。
(4)过程使用的酸碱都可以可再生循环，减小辅料的采购，降低直接加工成本。
(5)过程中形成的冷凝酸用到后续硝酸再生系统制备硝酸，将废酸变废为宝，提高了硝酸再生的效率，减小了固定投资以及硝酸再生成本。
附图说明
图1是本发明一种从红土镍矿中回收多种有价金属及酸碱双介质再生循环方法的工艺流程意图。
具体实施方式
下面结合附图及具体实施例对本发明作进一步的详细说明，但本发明的保护范围并不限于所述内容。
本发明公开了一种从红土镍矿中回收多种有价金属及酸碱双介质再生循环的方法。如图1所示，该方法首先将红土镍矿原矿经破碎与细磨得到矿粉，然后配置成浆进行硝酸高压浸出，得到的浸出浆经过pH调节、浓密洗涤实现固液分离得到浸出渣和浸出液，浸出渣经过滤烘干后进行球团烧结工艺得到铁精矿。浸出液中添加氧化镁调整溶液的pH值，将酸浸液中的铝镍钴锰钪及少量铁完全沉淀出来。然后控制溶液的pH值、反应温度，将沉淀碱溶解，混合物中的氢氧化铝转为铝酸根离子溶于碱液中，经过滤与镍钴锰钪沉淀分离。在碱性溶液通过加入二氧化碳或氢氧化铝晶种，沉淀获得氢氧化铝产品。镍钴锰钪沉淀混合物用硫酸溶解后，经萃钪、反萃、结晶后，生产出的钪盐经过加热分解得到氧化钪作为商品出售。后经过分级萃取锰/钴/镍、反萃、结晶，得到的镍、钴、锰产品。
沉淀铝镍钴锰钪后的硝酸镁溶液经过蒸发浓缩得到硝酸镁晶体，将硝酸镁晶体加热至熔化，再加入到分解炉中。硝酸镁熔体受热快速分解形成氧化镁、NO x、O 2等。该含尘气体经过收尘系统得到高纯活性氧化镁，收尘后一部分NO x气体经过燃烧炉加热后再次进入分解系统内用以热解硝酸镁熔体，另一部分NO x气体经过降温，流向硝酸再生系统制备硝酸。进入硝酸再生系统的气体经过尾气换热、深度除尘、二次降温 冷凝获得冷凝稀硝酸。后续气体经过氧化氮压缩机加压增浓、进入吸收塔。前面冷凝所获得的冷凝酸，在测量浓度后泵入到硝酸吸收塔相应的塔板上用于硝酸制备。硝酸再生系统产生的工业硝酸将用于前端浸出工序，所得到的高纯活性氧化镁用于前段pH调试。
该工艺过程高效简洁，避免了在红土镍矿硝酸浸出液中，加入碱性物质控制pH值沉淀铝与镍钴分离过程中，氢氧化铝絮状沉淀的生成，导致回收出现过滤性差和铝渣中夹带镍钴金属的问题，因此镍钴金属的总回收率提高。沉淀铝镍钴锰钪后的硝酸镁溶液经过蒸发浓缩得到硝酸镁晶体用于后续硝酸镁分解再生获得酸(硝酸)和碱(氧化镁)，实现了酸碱双介质再生循环。并且该工艺原料适应性强，特别适用于含铝较高的褐铁型红土镍矿的处理。
实施例1
将含镍0.6％、钴0.05％、铁48％、铝1.3％、锰0.15％、镁0.6％、钪43g/t的红土镍矿原矿矿石进行破碎与细磨，得到矿粉作为原料备用。将所得的矿粉、硝酸、水以液固比(1:5g/mL)和初始酸浓度(120g/L)，在浆化槽内充分搅拌混合制成矿浆，然后再将矿浆泵入到硝酸加压釜内进行浸出。浸出温度为160℃，浸出时间为1h，搅拌速度为170rpm。反应结束后在矿浆中加入氧化镁预中和调节pH至2.5，之后矿浆通过浓密洗涤得到底流和溢流液。底流经过滤干燥进行球团与烧结工艺，得到含铁量54％的铁精矿，将氧化镁加入溢流液中进行沉淀反应。控制反应温度为65℃，溶液的pH值为7.0，沉淀反应1.5h后，过滤得到第一沉淀滤渣。然后在密闭反应釜中，向第一沉淀滤渣中加入氢氧化钠溶液，并控制反应溶液pH值为12.5，控制反应温度为140℃，反应1h后，过滤得到第二沉淀滤渣和滤液。将滤液通过碳分法进行沉淀处理，过滤得到氢氧化铝沉淀。将第二沉淀滤渣与硫酸溶液进行混合，并控制反应溶液pH为2.0，反应温度为80℃，反应1.5h后，过滤得到硫酸镍、钴、锰、钪溶液，然后进行萃钪、反萃、结晶，生产出的草酸钪，草酸钪在650℃的温度下煅烧分解，得到含量为98％的Sc 2O 3，作为商品出售。萃钪后液经分级萃取锰/钴/镍、结晶，得到硫酸镍溶液、硫酸钴溶液、硫酸锰溶液、钪盐溶液，分别对每种溶液进行蒸发浓缩处理，得到的镍、钴、锰产品。将第一沉淀滤液进行蒸发浓缩得到硝酸镁晶体，将其加热熔化后导入至分解炉，分解炉内的温度为450℃。硝酸镁在分解炉内迅速分解为氧化氮气体、水蒸气、氧化镁、氧气。后经过收尘得到含量大于92.3％的高纯活性氧化镁，收尘后的80％气体经过燃烧炉加热后，再次进入分解炉加热分解硝酸镁。另一部分气体经深度除尘后 经降温使温度下降到40℃，获得浓度为33％的冷凝硝酸。剩余气体经氧化氮压缩机加压到4.1Mpa后导入到吸收塔内。同时将获得的冷凝酸泵入吸收塔相应的塔板上，最终在塔底获得浓度为48％的再生硝酸，吸收后的尾气经处理后达标排放。
实施例2
将含镍0.87％、钴0.085％、铁49％、铝1.9％、锰0.9％、镁1.3％、钪66g/t的红土镍矿原矿矿石进行破碎与细磨，得到矿粉作为原料备用。将所得的矿粉、硝酸、水以液固比(1:2g/mL)和初始酸浓度(150g/L)，在浆化槽内充分搅拌混合制成矿浆，然后再将矿浆泵入到硝酸加压釜内进行浸出。浸出温度为180℃，浸出时间为2h，搅拌速度为180rpm。反应结束后在矿浆中加入氧化镁预中和调节pH至2.5，之后矿浆通过浓密洗涤得到底流和溢流液。底流经过滤干燥进行球团与烧结工艺，得到含铁量59％的铁精矿。将氧化镁加入溢流液中进行沉淀反应，控制反应温度为80℃，溶液的pH值为8.0。沉淀反应1h后，过滤得到第一沉淀滤渣。然后在密闭反应釜中，向第一沉淀滤渣中加入氢氧化钠溶液，并控制反应溶液pH值为13.0，控制反应温度为160℃，反应3h后，过滤得到第二沉淀滤渣和滤液。将滤液通过碳分法进行沉淀处理，过滤得到氢氧化铝沉淀。将第二沉淀滤渣与硫酸溶液进行混合，并控制反应溶液pH为1.0，反应温度为40℃，反应2.0h后，过滤得到硫酸镍、钴、锰、钪溶液，然后进行萃钪、结晶，生产出的硝酸钪在500℃的温度下煅烧分解，得到含量为97％的Sc 2O 3，作为商品出售。萃钪后液经分级萃取锰/钴/镍、结晶，得到硫酸镍溶液、硫酸钴溶液、硫酸锰溶液、钪盐溶液，分别对每种溶液进行蒸发浓缩处理，得到的镍、钴、锰产品。将第一沉淀滤液进行蒸发浓缩得到硝酸镁晶体，将其加热熔化后导入至分解炉，分解炉内的温度为500℃。硝酸镁在分解炉内迅速分解为氧化氮气体、水蒸气、氧化镁、氧气。后经过收尘得到含量大于94.3％的高纯活性氧化镁，收尘后的60％气体经过燃烧炉加热后，再次进入分解炉加热分解硝酸镁。另一部分气体经深度除尘后经降温使温度下降到100℃，获得浓度为27％的冷凝硝酸。剩余气体经氧化氮压缩机加压到4.2Mpa后导入到吸收塔内。同时将获得的冷凝酸泵入吸收塔相应的塔板上，最终在塔底获得浓度为49％的再生硝酸，吸收后的尾气经处理后达标排放。
实施例3
将含镍1.0％、钴0.11％、铁45％、铝2.7％、锰1.5％、镁2.7％、钪85g/t的红土镍矿原矿矿石进行破碎与细磨，得到矿粉作为原料备用。将所得的矿粉、硝酸、水以液固比(1:3g/mL)和初始酸浓度(180g/L)，在浆化槽内充分搅拌混合制成矿浆，然后 再将矿浆泵入到硝酸加压釜内进行浸出。浸出温度为170℃，浸出时间为3h，搅拌速度为190rpm。反应结束后在矿浆中加入氧化镁预中和调节pH至3.0，之后矿浆通过浓密洗涤得到底流和溢流液。底流经过滤干燥进行球团与烧结工艺，得到含铁量56％的铁精矿。将氧化镁加入溢流液中进行沉淀反应，控制反应温度为70℃，溶液的pH值为7.5。沉淀反应3.0h后，过滤得到第一沉淀滤渣。然后在密闭反应釜中，向第一沉淀滤渣中加入氢氧化钠溶液，并控制反应溶液pH值为14.0，控制反应温度为180℃，反应2h后，过滤得到第二沉淀滤渣和滤液。将滤液通过碳分法进行沉淀处理，过滤得到氢氧化铝沉淀。将第二沉淀滤渣与硫酸溶液进行混合，并控制反应溶液pH为0.5，反应温度为60℃，反应2.5h后，过滤得到硫酸镍、钴、锰、钪溶液，然后进行萃钪、结晶，生产出的氯化钪，氯化钪在800℃的温度下煅烧分解，得到含量为99％的Sc 2O 3，作为商品出售。萃钪后液经分级萃取锰/钴/镍、结晶，得到硫酸镍溶液、硫酸钴溶液、硫酸锰溶液、钪盐溶液，分别对每种溶液进行蒸发浓缩处理，得到的镍、钴、锰产品。将第一沉淀滤液进行蒸发浓缩得到硝酸镁晶体，将其加热熔化后导入至分解炉，分解炉内的温度为600℃。硝酸镁在分解炉内迅速分解为氧化氮气体、水蒸气、氧化镁、氧气。后经过收尘得到含量大于98.2％的高纯活性氧化镁，收尘后的50％气体经过燃烧炉加热后，再次进入分解炉加热分解硝酸镁。另一部分气体经深度除尘后经降温使温度下降到80℃，获得浓度为30％的冷凝硝酸。剩余气体经氧化氮压缩机加压到4.5Mpa后导入到吸收塔内。同时将获得的冷凝酸泵入吸收塔相应的塔板上，最终在塔底获得浓度为53％的再生硝酸，吸收后的尾气经处理后达标排放。
实施例4
将含镍1.5％、钴0.14％、铁43％、铝3.5％、锰2.1％、镁3.6％、钪91g/t的红土镍矿原矿矿石进行破碎与细磨，得到矿粉作为原料备用。将所得的矿粉、硝酸、水以液固比(1:4g/mL)和初始酸浓度(200g/L)，在浆化槽内充分搅拌混合制成矿浆，然后再将矿浆泵入到硝酸加压釜内进行浸出。浸出温度为190℃，浸出时间为2.5h，搅拌速度为200rpm。反应结束后在矿浆中加入氧化镁预中和调节pH至2.5，之后矿浆通过浓密洗涤得到底流和溢流液。底流经过滤干燥进行球团与烧结工艺，得到含铁量53％的铁精矿。将氧化镁加入溢流液中进行沉淀反应，控制反应温度为55℃，溶液的pH值为9.0。沉淀反应2.5h后，过滤得到第一沉淀滤渣。然后在密闭反应釜中，向第一沉淀滤渣中加入氢氧化钠溶液，并控制反应溶液pH值为14.0，控制反应温度为170℃，反应1h后，过滤得到第二沉淀滤渣和滤液。将滤液通过碳分法进行沉淀处理，过滤得 到氢氧化铝沉淀。将第二沉淀滤渣与硫酸溶液进行混合，并控制反应溶液pH为3.0，反应温度为70℃，反应3h后，过滤得到硫酸镍、钴、锰、钪溶液，然后进行萃钪、结晶，生产出的草酸钪，草酸钪在650℃的温度下煅烧分解，得到含量为99％的Sc 2O 3，作为商品出售。萃钪后液经分级萃取锰/钴/镍、结晶，得到硫酸镍溶液、硫酸钴溶液、硫酸锰溶液、钪盐溶液，分别对每种溶液进行蒸发浓缩处理，得到的镍、钴、锰产品。将第一沉淀滤液进行蒸发浓缩得到硝酸镁晶体，将其加热熔化后导入至分解炉，分解炉内的温度为700℃。硝酸镁在分解炉内迅速分解为氧化氮气体、水蒸气、氧化镁、氧气。后经过收尘得到含量大于98.8％的高纯活性氧化镁，收尘后的40％气体经过燃烧炉加热后，再次进入分解炉加热分解硝酸镁。另一部分气体经深度除尘后经降温使温度下降到50℃，获得浓度为31.9％的冷凝硝酸。剩余气体经氧化氮压缩机加压到4.7Mpa后导入到吸收塔内。同时将获得的冷凝酸泵入吸收塔相应的塔板上，最终在塔底获得浓度为55％的再生硝酸，吸收后的尾气经处理后达标排放。
实施例5
将含镍1.8％、钴0.19％、铁38％、铝4.3％、锰2.7％、镁4.5％、钪119g/t的红土镍矿原矿矿石进行破碎与细磨，得到矿粉作为原料备用。将所得的矿粉、硝酸、水以液固比(1:0.5g/mL)和初始酸浓度(130g/L)，在浆化槽内充分搅拌混合制成矿浆，然后再将矿浆泵入到硝酸加压釜内进行浸出。浸出温度为220℃，浸出时间为0.5h，搅拌速度为200rpm。反应结束后在矿浆中加入氧化镁预中和调节pH至3.5，之后矿浆通过浓密洗涤得到底流和溢流液。底流经过滤干燥进行球团与烧结工艺，得到含铁量50％的铁精矿。将氧化镁加入溢流液中进行沉淀反应，控制反应温度为90℃，溶液的pH值为10.0。沉淀反应1.0h后，过滤得到第一沉淀滤渣。然后在密闭反应釜中，向第一沉淀滤渣中加入氢氧化钠溶液，并控制反应溶液pH值为12.5，控制反应温度为200℃，反应2h后，过滤得到第二沉淀滤渣和滤液。将滤液通过碳分法进行沉淀处理，过滤得到氢氧化铝沉淀。将第二沉淀滤渣与硫酸溶液进行混合，并控制反应溶液pH为0.5，反应温度为65℃，反应3h后，过滤得到硫酸镍、钴、锰、钪溶液，然后进行萃钪、结晶，生产出的草酸钪，草酸钪在700℃的温度下煅烧分解，得到含量为99％的Sc 2O 3，作为商品出售。萃钪后液经分级萃取锰/钴/镍、结晶，得到硫酸镍溶液、硫酸钴溶液、硫酸锰溶液、钪盐溶液，分别对每种溶液进行蒸发浓缩处理，得到的镍、钴、锰产品。将第一沉淀滤液进行蒸发浓缩得到硝酸镁晶体，将其加热熔化后导入至分解炉，分解炉内的温度为850℃。硝酸镁在分解炉内迅速分解为氧化氮气体、水蒸气、氧化镁、氧 气。后经过收尘得到含量大于99％的高纯活性氧化镁，收尘后的20％气体经过燃烧炉加热后，再次进入分解炉加热分解硝酸镁。另一部分气体经深度除尘后经降温使温度下降到60℃，获得浓度为31％的冷凝硝酸。剩余气体经氧化氮压缩机加压到5.0Mpa后导入到吸收塔内。同时将获得的冷凝酸泵入吸收塔相应的塔板上，最终在塔底获得浓度为56％的再生硝酸，吸收后的尾气经处理后达标排放。
以上所述，仅为本发明较佳的具体实施方式，但本发明的保护范围并不局限于此，任何熟悉本技术领域的技术人员在本发明披露的技术范围内，可轻易想到的变化或替换，都应涵盖在本发明的保护范围之内。因此，本发明的保护范围应该以权利要求书的保护范围为准。

Claims (10)

  1. 一种从红土镍矿中回收多种有价金属及酸碱双介质再生循环的方法，包括以下步骤：
    (1)将红土镍矿原矿破碎并细磨得到矿粉，将矿粉与硝酸混合并充分搅拌制成矿浆；
    (2)将矿浆泵入高压釜中进行浸出反应，反应结束后预中和调节矿浆的pH值，之后矿浆经过多级浓密洗涤得到底流和溢流液；
    (3)底流经过滤干燥，进行球团烧结得到铁精矿，溢流液调节pH值后进行沉淀反应，反应结束后，酸浸液中的铝、镍、钴、锰、钪及少量铁完全沉淀出来，与硝酸镁溶液分离，过滤得到第一沉淀滤渣；
    (4)将第一沉淀滤渣加碱溶解，将滤渣中的氢氧化铝转化为铝酸根离子溶于碱液中，过滤得到第二沉淀滤渣，在过滤后液中加入二氧化碳或氢氧化铝晶种沉淀获得氢氧化铝产品；
    (5)第二沉淀滤渣用硫酸溶解后，经萃钪、反萃、结晶生产得到钪盐，萃钪后液用于镍钴锰三元材料的制备，或经分级萃取、反萃、结晶，生产镍、钴、锰产品。
  2. 如权利要求1所述从红土镍矿中回收多种有价金属及酸碱双介质再生循环的方法，其特征在于，步骤(1)中所述红土镍矿为褐铁矿型高铁低镍矿石，其化学组成的质量分数为：Ni为0.5～2.0％；Co为0.05～0.20％；Fe为35～55％；Al为0.5～5.0％；Mn为0.1～3.0％；Mg为0.50～5.0％；Sc为30～130g/t；所述硝酸的浓度为120～230g/L，矿粉与硝酸混合的固液比为1:0.5-1:5g/ml。
  3. 如权利要求1所述从红土镍矿中回收多种有价金属及酸碱双介质再生循环的方法，其特征在于，步骤(2)中所述高压釜带有搅拌装置，在浸出过程中对矿浆进行搅拌，搅拌速率为150-250rpm；所述浸出反应的浸出温度为160～220℃，浸出时间为0.5～3h；浸出反应结束后向矿浆中加入氧化镁预中和调节其pH值至2.5～3.5。
  4. 如权利要求1所述从红土镍矿中回收多种有价金属及酸碱双介质再生循环的方法，其特征在于，步骤(3)中向溢流液中加入氧化镁调节其pH值至7.0～10.0；所述沉淀反应的反应温度为40～100℃，反应时间为0.5～3.5h。
  5. 如权利要求1所述从红土镍矿中回收多种有价金属及酸碱双介质再生循环的方法，其特征在于，步骤(4)中将第一沉淀滤渣加碱溶解的反应温度为140～200℃，反应时间1～4h，反应的pH值范围为12.5～14.0；所使用的碱包括氢氧化钠和氢氧化 钾中任何一种及其组合形式；向第二沉淀滤渣过滤后液中加入二氧化碳或氢氧化铝晶种沉淀获得氢氧化铝产品。
  6. 如权利要求1所述从红土镍矿中回收多种有价金属及酸碱双介质再生循环的方法，其特征在于，步骤(5)第二沉淀滤渣用硫酸溶解的反应温度为30～100℃，反应时间为1.0～2.5h，反应的pH范围为0.5～3.5；所述钪盐包括草酸钪、硝酸钪、氯化钪中任一种形式。
  7. 如权利要求1所述从红土镍矿中回收多种有价金属及酸碱双介质再生循环的方法，其特征在于，步骤(5)还包括生产出的钪盐经加热分解得到氧化钪，加热温度为300℃～800℃，分解方式包括煅烧分解、喷雾分解、悬浮沸腾分解中任意一种及其组合形式。
  8. 如权利要求1-7任一所述从红土镍矿中回收多种有价金属及酸碱双介质再生循环的方法，其特征在于，还包括酸碱双介质的再生循环方法，步骤如下：
    (6)第一沉淀滤液经蒸发浓缩得到硝酸镁晶体，所述硝酸镁晶体加热熔化后进入分解炉热解，形成高温尘气；
    (7)高温尘气经收尘系统后分离出氧化镁粉体，产出的氧化镁返回第一沉淀工序；收尘后一部分NO x气体经燃烧炉加热，再次循环到分解炉内用于硝酸镁的热解，另一部分NO x进入硝酸再生系统，经尾气换热、深度除尘、二次降温冷凝获得冷凝稀硝酸，再将冷凝酸泵入至吸收塔，未被冷凝吸收的气体经过氧化氮压缩机加压增浓，进入吸收塔制备硝酸，产出的硝酸返回浸出工序。
  9. 如权利要求8所述从红土镍矿中回收多种有价金属及酸碱双介质再生循环的方法，其特征在于，步骤(6)中所述分解炉的分解方式包括沸腾分解、煅烧分解、喷雾分解中任何一种，炉内的分解温度为400℃～900℃；所述高温尘气包含氧化镁、水蒸气、NOx、氧气。
  10. 如权利要求8所述从红土镍矿中回收多种有价金属及酸碱双介质再生循环的方法，其特征在于，步骤(7)中收尘后20～95％的NO x气体经燃烧炉加热，再次循环到分解炉内用于硝酸镁的热解；进入硝酸再生系统的NO x至冷却系统将温度下降至120℃以下，获得冷凝稀硝酸，所述冷凝稀硝酸的浓度为20～35％；未被冷凝吸收的NO x经加压至4.0Mpa～5.0Mpa，送入吸收塔吸收制备硝酸，该过程用前述冷凝稀硝酸作为吸收剂，吸收后的尾气经处理后达标排出。
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