Improved treatment method for laterite-nickel ore

Abstract

The invention provides an improved treatment method for laterite-nickel ore. The improved treatment method comprises the following steps: S1, carrying out acid leaching on the laterite-nickel ore, and then filtering and washing to obtain a leached solution and first leached residues; step S2, the step S2 is selected from any one of a step S2-1, a step S2-2 and a step S2-3; s3, performing first-stage nickel and cobalt precipitation and dense filtration on the aluminum and scandium removed liquid or the iron and aluminum removed liquid by adopting a precipitator to obtain first-stage nickel and cobalt precipitation liquid and a nickel cobalt hydroxide product; and S4, carrying out second-stage nickel-cobalt precipitation on the first-stage nickel-cobalt precipitation solution by adopting a nickel-cobalt precipitation neutralizer and an oxidizing agent to obtain a magnesium sulfate manganese solution and nickel-cobalt-manganese slurry. In the traditional process, ferrous iron is oxidized by using compressed air, so that energy is wasted. According to the method, the manganese-containing substance is adopted as the oxidizing agent, ferrous iron is oxidized into ferric iron, the problems that the ferrous iron is low in oxidation rate under the low pH and compressed air is wasted are solved, and the scandium recovery rate is increased.

Description

Technical Field

[0001] The present invention relates to the technical field of laterite nickel ore, and in particular, to an improved treatment method for laterite nickel ore. Background Art

[0002] At present, laterite nickel ore has become the main raw material in the EV battery industrial chain. Among them, the high-pressure leaching process is the mainstream process for producing nickel-cobalt intermediate products at present. The main process is: high-pressure leaching - pre-neutralization - two-stage iron and aluminum removal - two-stage nickel and cobalt precipitation - tailing slag neutralization. This process is a patented technology of China Enfi and is widely used by enterprises such as Ruimu, Huayou, and Liqin.

[0003] However, the biggest problem with this process lies in:

[0004] (1) In the iron and aluminum removal stage, compressed air and oxygen are introduced for the oxidation of divalent iron. However, when the pH is relatively low, the oxidation rate of divalent iron is poor, the efficiency is low, and the utilization rate of compressed air is low <3%, wasting a large amount of electric energy.

[0005] (2) Iron cannot be recycled, and the slag rate is relatively high. Basically, about 1.2t of slag is produced from 1 ton of laterite nickel ore. This slag cannot be recycled. If a tailing pond is used, it will pose a huge hidden danger to environmental safety.

[0006] (3) After iron is leached, it exists in the form of a mixture of divalent iron and trivalent iron. The pH for the oxidation and precipitation of divalent iron is relatively high, generally in the second-stage iron and aluminum removal (the end-point pH is around 4.8) to be removed completely, resulting in the simultaneous precipitation of iron, aluminum, and scandium. The mixture of iron, aluminum, and scandium causes aluminum and scandium to be unable to be recycled. Summary of the Invention

[0007] The main object of the present invention is to provide an improved treatment method for laterite nickel ore to solve the problem of high cost caused by the extensive use of compressed air and oxygen for two-stage iron and aluminum removal in the process of preparing nickel-cobalt hydroxide in the prior art.

[0008] In order to achieve the above object, according to one aspect of the present invention, an improved treatment method for laterite nickel ore is provided. The laterite nickel ore is a mixed ore of limonite-type laterite nickel ore and residual ore-type laterite nickel ore in any proportion. The improved treatment method includes: Step S1, acid leaching the laterite nickel ore and then filtering and washing to obtain a post-leaching solution and a first leaching residue; Step S2, Step S2 is selected from any one of Step S2-1, Step S2-2, and Step S2-3; Step S2-1: Using a manganese-containing substance to oxidize and remove iron from the post-leaching solution to obtain an iron-oxidized and removed ore pulp; using an iron-removing neutralizing agent to sequentially perform neutralizing iron removal and liquid-solid separation on the iron-oxidized and removed ore pulp to obtain an iron-removing residue, using an aluminum-washing alkaline solution to perform aluminum-washing treatment on the iron-removing residue to obtain a liquid phase and a high-iron slag product; using a scandium-aluminum-precipitating neutralizing agent to perform scandium-aluminum precipitation on the liquid phase to obtain a scandium-rich aluminum slag and a post-scandium-aluminum removal solution; Step S2-2: Using a manganese-containing substance to oxidize and remove iron from the post-leaching solution to obtain an iron-oxidized and removed ore pulp; using a pre-neutralizing agent to sequentially perform pre-neutralization and liquid-solid separation on the iron-oxidized and removed ore pulp to obtain a post-neutralization residue, washing the post-neutralization residue to obtain a liquid phase and a second leaching residue; using a first-stage iron-aluminum-removing neutralizing agent to perform first-stage iron-aluminum removal on the liquid phase to obtain an open-circuit iron-aluminum slag and a first-stage post-iron-aluminum removal solution, using a second-stage iron-aluminum-removing neutralizing agent to perform second-stage iron-aluminum removal on the first-stage post-iron-aluminum removal solution to obtain a second-stage iron-aluminum slag and a post-iron-aluminum removal solution; returning the second-stage iron-aluminum slag to the iron-oxidizing and removing step; Step S2-3: Performing cyclic leaching on the post-leaching solution to obtain a cyclic leaching ore pulp; using a pre-neutralizing agent to sequentially perform pre-neutralization and liquid-solid separation on the cyclic leaching ore pulp to obtain a post-neutralization residue, washing the post-neutralization residue to obtain a liquid phase and a second leaching residue; using a first-stage iron-aluminum-removing neutralizing agent to perform first-stage iron-aluminum removal on the liquid phase to obtain an open-circuit iron-aluminum slag and a first-stage post-iron-aluminum removal solution, using a manganese-containing substance to perform second-stage iron-aluminum removal on the first-stage post-iron-aluminum removal solution to obtain a second-stage iron-aluminum slag and a post-iron-aluminum removal solution; returning the second-stage iron-aluminum slag to the cyclic leaching step; Step S3, using a precipitating agent to perform first-stage nickel-cobalt precipitation and thickening filtration on the post-scandium-aluminum removal solution or the post-iron-aluminum removal solution to obtain a first-stage post-nickel-cobalt precipitation solution and a nickel-cobalt hydroxide product; Step S4, using a nickel-cobalt-precipitating neutralizing agent and an oxidizing agent to perform second-stage nickel-cobalt precipitation on the first-stage post-nickel-cobalt precipitation solution to obtain a magnesium sulfate manganese solution and a nickel-cobalt-manganese slurry.

[0009] Further, the above-mentioned manganese-containing substance is selected from any one or more of nickel-cobalt-manganese slurry, manganese dioxide, potassium permanganate, sodium permanganate, pyrolusite, manganese sesquioxide, and manganese tetroxide.

[0010] Further, in the above-mentioned Step S2-1, the molar ratio of manganese in the manganese-containing substance to divalent iron in the post-leaching solution is 0.1 to 10:1; and / or, the temperature for iron oxidation and removal is 25°C to 100°C, and the time for iron oxidation and removal is 0.1 h to 5 h.

[0011] Further, in the above step S2-1, the end point pH of neutralization and iron removal is 2.8 to 3.5, the temperature of neutralization and iron removal is 25°C to 100°C, and the time of neutralization and iron removal is 0.5 h to 8 h; the iron removal neutralizing agent is selected from any one or more of sodium carbonate, sodium bicarbonate, potassium carbonate, potassium bicarbonate, magnesium carbonate, magnesium bicarbonate, ammonium carbonate, ammonium bicarbonate, calcium oxide, magnesium oxide, sodium hydroxide, potassium hydroxide, ammonia water, calcium hydroxide, magnesium hydroxide, calcium carbonate, calcium bicarbonate, limestone, bitter earth powder, magnesite, dolomite, and marble.

[0012] Further, in the above step S2-1, the mass concentration of the aluminum washing lye is 0.1 wt% to 40 wt%, and the dosage of the aluminum washing lye is 0.8 to 8 times the stoichiometric ratio of aluminum element in the iron removal slag; and / or the temperature of the aluminum washing treatment is 25°C to 100°C, and the time of the aluminum washing treatment is 0.5 h to 8 h; and / or, the magnesium sulfate and manganese solution is returned to step S2-1 as the aluminum washing lye.

[0013] Further, in the above step S2-1, the end point pH of aluminum and scandium precipitation treatment is 4.5 to 5.2, the temperature of aluminum and scandium precipitation treatment is 25°C to 100°C, and the time of aluminum and scandium precipitation treatment is 0.5 h to 8 h; and / or the aluminum and scandium precipitation neutralizing agent is selected from any one or more of sodium carbonate, sodium bicarbonate, potassium carbonate, potassium bicarbonate, magnesium carbonate, magnesium bicarbonate, ammonium carbonate, ammonium bicarbonate, calcium oxide, magnesium oxide, sodium hydroxide, potassium hydroxide, ammonia water, calcium hydroxide, magnesium hydroxide, calcium carbonate, calcium bicarbonate, limestone, bitter earth powder, magnesite, dolomite, and marble.

[0014] Further, the above step S2-1 further includes: successively performing drying and roasting treatments on the iron slag obtained by the aluminum washing treatment to obtain a high-iron slag product; wherein, the temperature of the roasting treatment is 500°C to 1200°C, the time of the roasting treatment is 1 min to 5 h, and the iron content in the high-iron slag product is 55% to 65%.

[0015] Further, in the above step S2-2, the temperature of oxidation and iron removal is 25°C to 100°C, and the time of oxidation and iron removal is 0.1 h to 5 h.

[0016] Further, in the above step S2-2, the pre-neutralizing agent, the first-stage iron and aluminum removal neutralizing agent, and the second-stage iron and aluminum removal neutralizing agent are each independently selected from any one or more of sodium carbonate, sodium bicarbonate, potassium carbonate, potassium bicarbonate, magnesium carbonate, magnesium bicarbonate, ammonium carbonate, ammonium bicarbonate, calcium oxide, magnesium oxide, sodium hydroxide, potassium hydroxide, ammonia water, calcium hydroxide, magnesium hydroxide, calcium carbonate, calcium bicarbonate, limestone, bitter earth powder, magnesite, dolomite, and marble; and / or, the end point pH of the pre-neutralization is 1-2, the temperature of the pre-neutralization is 25°C to 100°C, and the time of the pre-neutralization is 0.5 h to 8 h; and / or, the end point pH of the first-stage iron and aluminum removal is 3-4, the temperature of the first-stage iron and aluminum removal is 25°C to 100°C, and the time of the first-stage iron and aluminum removal is 0.5 h to 8 h; and / or, the end point pH of the second-stage iron and aluminum removal is 4-5, the temperature of the second-stage iron and aluminum removal is 25°C to 100°C, and the time of the second-stage iron and aluminum removal is 0.5 h to 8 h.

[0017] Further, in the above step S2-3, the molar ratio of manganese in the manganese-containing substance to ferrous iron in the liquid after the first-stage iron and aluminum removal is 0.1-10:1.

[0018] Further, in the above step S2-3, the pre-neutralizing agent and the first-stage iron and aluminum removal neutralizing agent are each independently selected from any one or more of sodium carbonate, sodium bicarbonate, potassium carbonate, potassium bicarbonate, magnesium carbonate, magnesium bicarbonate, ammonium carbonate, ammonium bicarbonate, calcium oxide, magnesium oxide, sodium hydroxide, potassium hydroxide, ammonia water, calcium hydroxide, magnesium hydroxide, calcium carbonate, calcium bicarbonate, limestone, bitter earth powder, magnesite, dolomite, and marble; and / or, the end point pH of the pre-neutralization is 1-2, the temperature of the pre-neutralization is 25°C to 100°C, and the time of the pre-neutralization is 0.5 h to 8 h; and / or, the end point pH of the first-stage iron and aluminum removal is 3-4, the temperature of the first-stage iron and aluminum removal is 25°C to 100°C, and the time of the first-stage iron and aluminum removal is 0.5 h to 8 h; and / or, the end point pH of the second-stage iron and aluminum removal is 4-5, the temperature of the second-stage iron and aluminum removal is 25°C to 100°C, and the time of the second-stage iron and aluminum removal is 0.1 h to 5 h.

[0019] Further, in the above step S3, the end point pH of the first-stage nickel and cobalt precipitation is 7.0-8.0, the temperature of the first-stage nickel and cobalt precipitation is 25°C to 100°C, and the time of the first-stage nickel and cobalt precipitation is 0.5 h to 8 h; the precipitating agent is selected from any one or more of magnesium oxide, sodium hydroxide, and calcium hydroxide.

[0020] Further, in the above step S4, the end point pH of the second-stage precipitation of nickel and cobalt is 8.0 - 9.0, the temperature of the second-stage precipitation of nickel and cobalt is 25°C - 100°C, and the time of the second-stage precipitation of nickel and cobalt is 0.5 h - 8 h; and / or, the nickel and cobalt precipitation neutralizing agent is selected from any one or more of sodium carbonate, sodium bicarbonate, potassium carbonate, potassium bicarbonate, magnesium carbonate, magnesium bicarbonate, ammonium carbonate, ammonium bicarbonate, calcium oxide, magnesium oxide, sodium hydroxide, potassium hydroxide, ammonia water, calcium hydroxide, magnesium hydroxide, calcium carbonate, and calcium bicarbonate; and / or, the oxidizing agent is selected from any one or more of a mixture of sulfur dioxide and oxygen, oxygen, compressed air, oxygen-enriched air, hydrogen peroxide, sodium persulfate, potassium persulfate, and potassium permanganate.

[0021] Further, in the above step S1, the temperature of the acid leaching is 80°C - 280°C, the time of the acid leaching is 0.1 - 10 h, and the acid-to-ore ratio of the acid leaching is 200 - 400 kg / t ore.

[0022] Further, the above improved treatment method further includes: performing an aluminum leaching treatment on the scandium-rich aluminum slag with an aluminum leaching alkali solution to obtain a scandium-rich slag product and a post-aluminum leaching solution; wherein, the mass concentration of the aluminum leaching alkali solution is 0.1 wt% - 40 wt%, and the dosage of the aluminum leaching alkali solution is 0.8 - 8 times the stoichiometric ratio of the aluminum element in the scandium-rich aluminum slag; and / or, the temperature of the aluminum leaching treatment is 25°C - 100°C, and the time of the aluminum leaching treatment is 0.5 h - 8 h; and / or, the post-aluminum leaching solution is recycled and used as the aluminum leaching alkali solution.

[0023] Applying the technical solution of the present application, in the traditional process, compressed air is used to oxidize ferrous iron, with low efficiency and a utilization rate of less than 3%, resulting in energy waste. The present application uses a manganese-containing substance as an oxidizing agent to oxidize ferrous iron to ferric iron, which not only solves the problems of slow oxidation rate of ferrous iron at low pH and waste of compressed air, improves the oxidation efficiency and the utilization rate of manganese, but also enables ferric iron to precipitate at a lower pH, thereby reducing the precipitation of aluminum and scandium, achieving the effective separation of iron from aluminum and scandium, and improving the recovery rate of scandium. In addition, there are a total of four specific implementation methods for oxidizing ferrous iron to ferric iron, which can be specifically referred to Figures 1 to 4 , and the process differences are reflected in step S2. It can be seen that the main effects of the above improved treatment method for laterite nickel ore are as follows: significantly improving the oxidation efficiency of ferrous iron and the utilization rate of manganese, reducing the use of compressed air or oxygen, reducing power consumption, and lowering production costs; effectively recovering iron, reducing the slag rate, reducing the use of tailing ponds, and greatly reducing the potential safety hazards and pollution to the environment; achieving the effective separation of iron from aluminum and scandium, improving the recovery rates of scandium and aluminum, and at the same time, the recovery rates of nickel and cobalt and the product quality are also improved; the four process routes provided by this method enhance the adaptability and flexibility of the process. BRIEF DESCRIPTION OF THE DRAWINGS

[0024] The accompanying drawings forming a part of this application are used to provide a further understanding of the present invention. The schematic embodiments of the present invention and their descriptions are used to explain the present invention and do not constitute an improper limitation of the present invention. In the drawings:

[0025] Figure 1 Shows a process flow chart of an improved treatment method for laterite nickel ore according to Embodiment 1 of the present invention;

[0026] Figure 2 Shows a process flow chart of an improved treatment method for laterite nickel ore according to Embodiment 2 of the present invention;

[0027] Figure 3 Shows a process flow chart of an improved treatment method for laterite nickel ore according to Embodiment 3 of the present invention;

[0028] Figure 4 Shows a process flow chart of an improved treatment method for laterite nickel ore according to Embodiment 4 of the present invention. Detailed implementation manners

[0029] It should be noted that, without conflict, the embodiments in this application and the features in the embodiments can be combined with each other. The present invention will be described in detail below with reference to the drawings and in combination with the embodiments.

[0030] As described in the background art section, in the prior art process for preparing nickel cobalt hydroxide, there are problems such as high cost due to the extensive use of compressed air and oxygen for two-stage iron and aluminum removal. To solve the above problems, the present invention provides an improved treatment method for laterite nickel ore.

[0031] In a typical implementation manner of this application, an improved treatment method for laterite nickel ore is provided. The laterite nickel ore is a mixed ore of limonite-type laterite nickel ore and residual ore-type laterite nickel ore in any proportion. Refer to Figures 1 to 4, the improved treatment method includes: Step S1, acid-leaching and then filtering and washing the laterite nickel ore to obtain a post-leaching solution and a first leaching residue; Step S2, Step S2 is selected from any one of Step S2-1, Step S2-2, and Step S2-3; Step S2-1: Using a manganese-containing substance to oxidize and remove iron from the post-leaching solution to obtain an iron-oxidized and removed ore pulp; using an iron-removing neutralizing agent to sequentially perform neutralizing iron removal and liquid-solid separation on the iron-oxidized and removed ore pulp to obtain an iron-removed residue, using an aluminum-washing alkali solution to perform aluminum-washing treatment on the iron-removed residue to obtain a liquid phase and a high-iron slag product; using a scandium-aluminum-precipitating neutralizing agent to perform scandium-aluminum precipitation on the liquid phase to obtain a scandium-rich aluminum slag and a post-scandium-aluminum-removal solution; Step S2-2: Using a manganese-containing substance to oxidize and remove iron from the post-leaching solution to obtain an iron-oxidized and removed ore pulp; using a pre-neutralizing agent to sequentially perform pre-neutralization and liquid-solid separation on the iron-oxidized and removed ore pulp to obtain a post-neutralization residue, washing the post-neutralization residue to obtain a liquid phase and a second leaching residue; using a first-stage iron-aluminum-removing neutralizing agent to perform first-stage iron-aluminum removal on the liquid phase to obtain an open-circuit iron-aluminum slag and a first-stage post-iron-aluminum-removal solution, using a second-stage iron-aluminum-removing neutralizing agent to perform second-stage iron-aluminum removal on the first-stage post-iron-aluminum-removal solution to obtain a second-stage iron-aluminum slag and a post-iron-aluminum-removal solution; returning the second-stage iron-aluminum slag to the iron-oxidation and removal step; Step S2-3: Performing cyclic leaching on the post-leaching solution to obtain a cyclic leaching ore pulp; using a pre-neutralizing agent to sequentially perform pre-neutralization and liquid-solid separation on the cyclic leaching ore pulp to obtain a post-neutralization residue, washing the post-neutralization residue to obtain a liquid phase and a second leaching residue; using a first-stage iron-aluminum-removing neutralizing agent to perform first-stage iron-aluminum removal on the liquid phase to obtain an open-circuit iron-aluminum slag and a first-stage post-iron-aluminum-removal solution, using a manganese-containing substance to perform second-stage iron-aluminum removal on the first-stage post-iron-aluminum-removal solution to obtain a second-stage iron-aluminum slag and a post-iron-aluminum-removal solution; returning the second-stage iron-aluminum slag to the cyclic leaching step; Step S3, using a precipitating agent to perform first-stage nickel-cobalt precipitation and thickening filtration on the post-scandium-aluminum-removal solution or the post-iron-aluminum-removal solution to obtain a first-stage post-nickel-cobalt-precipitation solution and a nickel-cobalt hydroxide product; Step S4, using a nickel-cobalt-precipitating neutralizing agent and an oxidizing agent to perform second-stage nickel-cobalt precipitation on the first-stage post-nickel-cobalt-precipitation solution to obtain a magnesium sulfate manganese solution and a nickel-cobalt-manganese pulp.

[0032] The traditional process uses compressed air to oxidize divalent iron, with low efficiency and a utilization rate of less than 3%, resulting in energy waste. This application uses a manganese-containing substance as an oxidizing agent to oxidize divalent iron into trivalent iron, which not only solves the problems of slow oxidation rate of divalent iron at low pH and waste of compressed air, improves the oxidation efficiency and the utilization rate of manganese, but also enables trivalent iron to precipitate at a lower pH, thereby reducing the precipitation of aluminum and scandium, achieving the effective separation of iron from aluminum and scandium, and improving the recovery rate of scandium. In addition, there are a total of four specific implementation methods for oxidizing divalent iron into trivalent iron, which can be specifically referred to Figures 1 to 4, the difference in process is reflected in step S2. It can be seen that the main effects of the improved treatment method of laterite nickel ore are: significantly improving the efficiency of ferrous iron oxidation and the utilization rate of manganese, reducing the use of compressed air or oxygen, reducing power consumption, and reducing production costs; by effectively recovering iron, reducing the slag rate, reducing the use of tailings ponds, and greatly reducing safety hazards and pollution to the environment; achieving effective separation of iron and aluminum scandium, improving the recovery rate of scandium and aluminum, and at the same time improving the recovery rate of nickel and cobalt and product quality; this method provides four process routes to enhance the adaptability and flexibility of the process.

[0033] In one embodiment of the present application, the manganese-containing substance is selected from any one or more of nickel-cobalt-manganese slurry, manganese dioxide, potassium permanganate, sodium permanganate, pyrolusite, manganese trioxide and manganese tetraoxide.

[0034] On the one hand, the manganese in the above high-priced manganese-containing substances has a strong oxidation performance, which can oxidize divalent iron to trivalent iron, accelerate the oxidation reaction, and improve the oxidation efficiency. On the other hand, the use of manganese-containing substances of different sources and properties as oxidants can provide greater flexibility and adaptability for the process. On the other hand, the oxidation process of manganese-containing substances usually produces less greenhouse gas emissions and energy consumption, which helps to reduce the impact of the entire process on the environment, making it more green and sustainable. In addition, compared to nickel-cobalt-manganese slurry as manganese-containing substances, manganese dioxide, potassium permanganate, sodium permanganate, pyrolusite, manganese trioxide and manganese tetraoxide can reduce the risk of manganese-containing substances introducing impurities, but, compared to manganese-containing substances, manganese dioxide, potassium permanganate, sodium permanganate, pyrolusite, manganese trioxide and manganese tetraoxide, etc. are more expensive. The second application preferably uses nickel-cobalt-manganese slurry as a manganese-containing substance, which can not only reduce costs, but also reduce the storage difficulty and post-processing energy consumption of nickel-cobalt-manganese slurry.

[0035] In one embodiment of the present application, in the above step S2-1, the molar ratio of manganese in the manganese-containing substance to divalent iron in the leaching solution is 0.1 to 10:1; and / or the temperature for oxidative iron removal is 25°C to 100°C, and the time for oxidative iron removal is 0.1h to 5h.

[0036] Controlling the molar ratio of manganese in the manganese-containing substance to ferrous iron in the leached solution helps control the potential at which ferrous iron is oxidized to ferric iron to be no higher than 400 mV, thereby helping to make the oxidation of ferrous iron to ferric iron more complete and minimizing the occurrence of side reactions.

[0037] As the temperature increases, the rate of the oxidation reaction accelerates, which helps to shorten the time required to reach the desired degree of oxidation and improve production efficiency. However, excessively high temperatures may lead to side reactions and additional energy consumption. By controlling the upper temperature limit at 100 °C, it helps to keep the reaction proceeding in a controllable and efficient state. Preferably, the above oxidation time can not only promote the full progress of the reaction but also reduce unnecessary waiting, enhancing overall productivity. Controlling the above temperature and time comprehensively can reduce energy consumption, heat loss, and equipment wear, which is beneficial to energy conservation, emission reduction, and cost reduction of production. Further, preferably, the molar ratio of manganese in the manganese-containing substance to divalent iron in the post-leaching solution is 1-5:1; the temperature for iron removal by oxidation is 40 °C - 80 °C, and the time for iron removal by oxidation is 1 h - 2 h

[0038] In one embodiment of the present application, in the above step S2-1, the end point pH of iron removal by neutralization is 2.8 - 3.5, the temperature for iron removal by neutralization is 25 °C - 100 °C, and the time for iron removal by neutralization is 0.5 h - 8 h; the iron removal neutralizing agent is selected from any one or more of sodium carbonate, sodium bicarbonate, potassium carbonate, potassium bicarbonate, magnesium carbonate, magnesium bicarbonate, ammonium carbonate, ammonium bicarbonate, calcium oxide, magnesium oxide, sodium hydroxide, potassium hydroxide, ammonia water, calcium hydroxide, magnesium hydroxide, calcium carbonate, calcium bicarbonate, limestone, bitter earth powder, magnesite, dolomite, and marble

[0039] Since a manganese-containing substance is used to oxidize and remove iron from the post-leaching solution, divalent iron ions are fully oxidized to trivalent iron ions, so that iron removal by neutralization can be carried out within the above relatively low pH range, enabling trivalent iron ions to effectively precipitate to form iron hydroxide, while other metals (such as aluminum and scandium) remain in a dissolved state at this pH, thus achieving the preliminary separation of metals. The temperature for iron removal by neutralization being 25 °C - 100 °C can accelerate the precipitation reaction rate of trivalent iron, shorten the reaction time, and improve production efficiency. The preferred time for iron removal by neutralization can ensure the full precipitation of trivalent iron, while avoiding the waste of energy and time caused by excessive operation, balancing efficiency and effect. Different neutralizing agents have different chemical properties and costs. According to the actual situation of the process, selecting a neutralizing agent with good compatibility with the pulp system and lower cost can optimize the precipitation effect and control production costs at the same time. Further, preferably, the temperature for iron removal by neutralization is 30 °C - 80 °C, and the time for iron removal by neutralization is 1 h - 5 h

[0040] In one embodiment of the present application, in the above step S2-1, the mass concentration of the aluminum-washing alkali solution is 0.1 wt% - 40 wt%, and the dosage of the aluminum-washing alkali solution is 0.8 - 8 times the stoichiometric ratio of aluminum element in the iron removal slag; and / or the temperature for aluminum-washing treatment is 25 °C - 100 °C, and the time for aluminum-washing treatment is 0.5 h - 8 h; and / or, the magnesium sulfate manganese solution is returned to step S2-1 as the aluminum-washing alkali solution

[0041] A higher caustic solution mass concentration can accelerate the dissolution process but may increase chemical costs and energy consumption; while a lower concentration, although having a lower cost, may require a longer processing time. Selecting the mass concentration of the above-mentioned aluminum washing caustic solution can effectively dissolve metals such as aluminum and scandium, while reducing the dissolution of other metals (such as iron, nickel, and cobalt), achieving selective aluminum washing, and balancing costs and processing efficiency. Excessive caustic solution may introduce unwanted impurities, affecting the quality and purity of subsequent metal recovery. Controlling the dosage of the aluminum washing caustic solution within the range where the stoichiometric ratio of aluminum element in the iron removal slag is within the above range can not only ensure the complete dissolution of metals such as aluminum and scandium, improving the recovery rate; but also help reduce the risk of impurities introduced by excessive caustic solution. Temperature control is crucial. Too high a temperature or too long a time may promote the dissolution of non-target metals or cause the formation of complex compounds of metals in the solution, affecting subsequent separation and recovery. Selecting within the above temperature and time range helps the effective dissolution of aluminum and scandium, while reducing the risk of unnecessary side reactions. Returning the magnesium sulfate and manganese solution to step S2-1 as the aluminum washing caustic solution helps reduce costs and achieve secondary utilization of waste. Further, preferably, the mass concentration of the aluminum washing caustic solution is 3wt% - 20wt%, and the dosage of the aluminum washing caustic solution is 1 - 5 times the stoichiometric ratio of aluminum element in the iron removal slag; and / or the temperature of the aluminum washing treatment is 30°C - 90°C, and the time of the aluminum washing treatment is 1h - 5h.

[0042] In an embodiment of the present application, in the above step S2-1, the end point pH of the aluminum and scandium precipitation treatment is 4.5 - 5.2, the temperature of the aluminum and scandium precipitation treatment is 25°C - 100°C, and the time of the aluminum and scandium precipitation treatment is 0.5h - 8h; and / or, the aluminum and scandium neutralizing agent is selected from any one or more of sodium carbonate, sodium bicarbonate, potassium carbonate, potassium bicarbonate, magnesium carbonate, magnesium bicarbonate, ammonium carbonate, ammonium bicarbonate, calcium oxide, magnesium oxide, sodium hydroxide, potassium hydroxide, ammonia water, calcium hydroxide, magnesium hydroxide, calcium carbonate, calcium bicarbonate, limestone, bitter earth powder, magnesite, dolomite, and marble.

[0043] Too high a pH will cause the coprecipitation of metals such as nickel and cobalt, while too low a pH may not completely precipitate aluminum and scandium. Selecting the above pH range can maximize the avoidance of coprecipitation of non-target metals, thereby reducing the complexity and cost of subsequent processing. Temperature control helps inhibit unwanted side reactions, such as the reaction of forming complex compounds between metals, ensuring the precipitation purity and selectivity of aluminum and scandium. Controlling the temperature and time of the aluminum and scandium precipitation treatment within the above range helps maximize the balance between production speed and precipitation effect. Different aluminum and scandium neutralizing agents have different basic strengths and reaction characteristics. According to actual operation needs, selecting a suitable aluminum and scandium neutralizing agent from the above types can optimize the aluminum and scandium precipitation effect and improve the metal recovery rate.

[0044] In one embodiment of the present application, the above step S2-1 further includes: sequentially drying and roasting the iron slag obtained by the aluminum washing treatment to obtain a high-iron slag product; wherein, the temperature of the roasting treatment is 500°C to 1200°C, the time of the roasting treatment is 1 minute to 5 hours, and the iron content in the high-iron slag product is 55% to 65%.

[0045] A large amount of iron slag produced by the existing process cannot be effectively recycled, with a high slag rate, posing a threat to environmental safety. By controlling specific conditions, this method realizes the efficient recycling of iron, and converts the iron slag into a high-iron product through roasting, reducing the slag rate and alleviating the environmental pressure.

[0046] In one embodiment of the present application, in the above step S2-2, the temperature for iron removal by oxidation is 25°C to 100°C, and the time for iron removal by oxidation is 0.1 hour to 5 hours.

[0047] Performing iron removal by oxidation within the above temperature and time ranges for iron removal by oxidation helps to find the best balance between the oxidation effect and energy consumption. Further, preferably, the temperature for iron removal by oxidation is 40°C to 90°C, and the time for iron removal by oxidation is 1 hour to 4 hours.

[0048] In one embodiment of the present application, in the above step S2-2, the pre-neutralizing agent, the first-stage iron and aluminum removal neutralizing agent, and the second-stage iron and aluminum removal neutralizing agent are each independently selected from any one or more of sodium carbonate, sodium bicarbonate, potassium carbonate, potassium bicarbonate, magnesium carbonate, magnesium bicarbonate, ammonium carbonate, ammonium bicarbonate, calcium oxide, magnesium oxide, sodium hydroxide, potassium hydroxide, ammonia water, calcium hydroxide, magnesium hydroxide, calcium carbonate, calcium bicarbonate, limestone, bitter earth powder, magnesite, dolomite, and marble; and / or, the end point pH of the pre-neutralization is 1 to 2, the temperature of the pre-neutralization is 25°C to 100°C, and the time of the pre-neutralization is 0.5 hour to 8 hours; and / or, the end point pH of the first-stage iron and aluminum removal is 3 to 4, the temperature of the first-stage iron and aluminum removal is 25°C to 100°C, and the time of the first-stage iron and aluminum removal is 0.5 hour to 8 hours; and / or, the end point pH of the second-stage iron and aluminum removal is 4 to 5, the temperature of the second-stage iron and aluminum removal is 25°C to 100°C, and the time of the second-stage iron and aluminum removal is 0.5 hour to 8 hours.

[0049] Different neutralizing agents may have different effects on the precipitation behavior of metal ions in solution. Selecting an appropriate neutralizing agent can achieve the selective precipitation of metals such as iron, aluminum, and scandium, which helps to improve the recovery rate and purity of metals. The pre-neutralization process can cause some metal ions to start precipitating by controlling the end-point pH, laying the foundation for more refined metal separation in the subsequent process. The temperature and time of pre-neutralization can ensure that all metal ions to be precipitated react fully, avoiding metal residues from affecting the subsequent treatment process. By precisely controlling the end-point pH of the first-stage iron and aluminum removal, a large amount of iron can be removed while reducing the co-precipitation of aluminum and scandium, improving the metal separation efficiency. By adjusting the end-point temperature and time of the first-stage iron and aluminum removal, the composition of the precipitate can be optimized, reducing unnecessary by-products and improving the economic benefits of metal recovery. As a further metal separation step, the second-stage iron and aluminum removal can achieve more precise metal separation by controlling the end-point pH, temperature, and time of the second-stage iron and aluminum removal. Especially for trace iron that is difficult to completely remove, the loss of aluminum and scandium can be minimized, and their recovery rate can be improved.

[0050] In an embodiment of the present application, in the above step S2-3, the molar ratio of manganese in the manganese-containing substance to ferrous iron in the solution after the first-stage iron and aluminum removal is 0.1-10:1.

[0051] Manganese in the manganese-containing substance acts as an oxidant and can effectively oxidize ferrous iron to ferric iron. By controlling the molar ratio of manganese to ferrous iron within the above range, this oxidation process can be optimized, avoiding excessive consumption or deficiency of manganese, ensuring the completeness and high efficiency of the oxidation reaction, and thus improving the precipitation and removal efficiency of iron. Further, it is preferably that the molar ratio of manganese in the manganese-containing substance to ferrous iron in the solution after the first-stage iron and aluminum removal is 1-6:1.

[0052] In an embodiment of the present application, in the above step S2-3, the pre-neutralizing agent and the first-stage iron and aluminum neutralizing agent are each independently selected from any one or more of sodium carbonate, sodium bicarbonate, potassium carbonate, potassium bicarbonate, magnesium carbonate, magnesium bicarbonate, ammonium carbonate, ammonium bicarbonate, calcium oxide, magnesium oxide, sodium hydroxide, potassium hydroxide, ammonia water, calcium hydroxide, magnesium hydroxide, calcium carbonate, calcium bicarbonate, limestone, magnesia powder, magnesite, dolomite, and marble; and / or, the end-point pH of the pre-neutralization is 1-2, the temperature of the pre-neutralization is 25°C-100°C, the time of the pre-neutralization is 0.5 h-8 h; and / or, the end-point pH of the first-stage iron and aluminum removal is 3-4, the temperature of the first-stage iron and aluminum removal is 25°C-100°C, the time of the first-stage iron and aluminum removal is 0.5 h-8 h; and / or, the end-point pH of the second-stage iron and aluminum removal is 4-5, the temperature of the second-stage iron and aluminum removal is 25°C-100°C, the time of the second-stage iron and aluminum removal is 0.1 h-5 h.

[0053] Due to differences in their chemical properties, different neutralizing agents can affect the precipitation selectivity of metal ions in a solution. Selecting an appropriate neutralizing agent can achieve the selective precipitation of metals, which helps improve the recovery rate and purity of metals. The end-point pH value of pre-neutralization directly affects the initial distribution of metal ions in the solution. The above end-point pH value of pre-neutralization helps to preliminarily separate some easily precipitated metals in advance, improving the pertinence and efficiency of subsequent treatment. Controlling the end-point pH of the first-stage iron and aluminum removal and the end-point pH of the second-stage iron and aluminum removal is the key to effectively separating iron from aluminum and scandium. A lower pH value (such as after pre-neutralization) helps to preferentially precipitate iron. As the pH value gradually increases, metals such as aluminum and scandium begin to precipitate. By controlling the pH value in stages, the orderly separation of metals can be achieved, reducing the loss of aluminum and scandium. Selecting the above temperature and time helps to balance the precipitation rates and side reactions of the pre-neutralizing agent, the first-stage iron and aluminum removal, and the second-stage iron and aluminum removal.

[0054] In an embodiment of the present application, in the above step S3, the end-point pH of the first-stage nickel and cobalt precipitation is 7.0 - 8.0, the temperature of the first-stage nickel and cobalt precipitation is 25°C - 100°C, and the time of the first-stage nickel and cobalt precipitation is 0.5 h - 8 h; the precipitating agent is selected from any one or more of magnesium oxide, sodium hydroxide, and calcium hydroxide.

[0055] Within the above end-point pH range of the first-stage nickel and cobalt precipitation, the precipitation selectivity of nickel and cobalt ions is relatively high, which can effectively separate nickel and cobalt compounds from the solution, while avoiding the premature precipitation of other metals (such as manganese), thereby improving the purity and recovery rate of nickel and cobalt products. Moderately increasing the temperature of the first-stage nickel and cobalt precipitation can accelerate the ion movement rate and improve the precipitation efficiency. However, too high a temperature may trigger unnecessary side reactions, such as accelerating hydrolysis or promoting the oxidation of certain metals. Selecting the above temperature can not only ensure the reaction rate and completeness but also reduce the energy consumption during the heating process. A shorter time may not be sufficient for all nickel and cobalt ions to precipitate completely, while too long a time may increase energy consumption and production costs. The above time for the first-stage nickel and cobalt precipitation helps to balance the complete precipitation efficiency of nickel and cobalt ions and the energy consumption.

[0056] In an embodiment of the present application, in the above step S4, the end-point pH of the second-stage nickel and cobalt precipitation is 8.0 - 9.0, the temperature of the second-stage nickel and cobalt precipitation is 25°C - 100°C, and the time of the second-stage nickel and cobalt precipitation is 0.5 h - 8 h; and / or, the nickel and cobalt neutralizing agent is selected from any one or more of sodium carbonate, sodium bicarbonate, potassium carbonate, potassium bicarbonate, magnesium carbonate, magnesium bicarbonate, ammonium carbonate, ammonium bicarbonate, calcium oxide, magnesium oxide, sodium hydroxide, potassium hydroxide, ammonia water, calcium hydroxide, magnesium hydroxide, calcium carbonate, and calcium bicarbonate; and / or, the oxidizing agent is selected from any one or more of a mixture of sulfur dioxide and oxygen, oxygen, compressed air, oxygen-enriched air, hydrogen peroxide, sodium persulfate, potassium persulfate, and potassium permanganate.

[0057] The end-point pH of the two-stage precipitation of nickel and cobalt enhances the selective precipitation of nickel and cobalt ions, which helps to form purer nickel and cobalt products. At the same time, it inhibits the possibility of other metals (such as manganese, aluminum, scandium, etc.) precipitating under the same conditions (by-products such as aluminum hydroxide, scandium hydroxide, etc.), thereby improving the recovery rate and purity of nickel and cobalt. The selection of temperature and time for the two-stage precipitation of nickel and cobalt helps to balance the complete precipitation efficiency and effect of nickel and cobalt ions. Selecting the above precipitants helps to improve the precipitation efficiency and selectivity of nickel and cobalt and reduce the co-precipitation of other unwanted metal ions. During the two-stage precipitation of nickel and cobalt, the oxidant aims to oxidize certain low-valent metals in the solution so that they precipitate at a higher pH value. The synergistic cooperation of the above precipitants and oxidants makes the selective precipitation effect of nickel and cobalt ions in the two-stage precipitation of nickel and cobalt better.

[0058] In an embodiment of the present application, in the above step S1, the temperature of the acid leaching is 80°C to 280°C, the time of the acid leaching is 0.1 to 10 h, and the acid-to-ore ratio of the acid leaching is 200 to 400 kg / t of ore.

[0059] The acceleration of the acid leaching reaction rate helps to improve the leaching efficiency of metals such as nickel and cobalt in laterite nickel ore. The temperature and time of the acid leaching can prompt metal ions to dissolve into the solution faster and more fully from the ore, thereby increasing the raw material concentration for subsequent metal recovery. A higher acid-to-ore ratio can increase the concentration of acid in the solution and promote the dissolution of metal ions, but at the same time, it will also increase the consumption of acid and the cost of treating acidic waste liquid. By optimizing the acid-to-ore ratio, unnecessary acid usage can be reduced, thereby reducing energy consumption, including the energy in the heating and stirring processes.

[0060] In an embodiment of the present application, the above improved treatment method further includes: using an aluminum leaching alkaline solution to perform aluminum leaching on the scandium-rich aluminum slag to obtain a scandium-rich slag product and a post-aluminum leaching solution; wherein, the mass concentration of the aluminum leaching alkaline solution is 0.1 wt% to 40 wt%, and the dosage of the aluminum leaching alkaline solution is 0.8 to 8 times the stoichiometric ratio of aluminum element in the scandium-rich aluminum slag; and / or, the temperature of the aluminum leaching treatment is 25°C to 100°C, and the time of the aluminum leaching treatment is 0.5 h to 8 h; and / or, the post-aluminum leaching solution is recycled and used as the aluminum leaching alkaline solution.

[0061] When the mass concentration of the aluminum leaching alkali solution is within the above range, the aluminum element in the scandium-rich aluminum slag can be efficiently dissolved, thereby improving the recovery rate of aluminum. When the dosage of the aluminum leaching alkali solution is within the range of the stoichiometric ratio of the aluminum element in the scandium-rich aluminum slag, it can ensure the full dissolution of aluminum while avoiding the excessive dissolution of scandium, realizing the effective separation of aluminum and scandium. Appropriate temperature and time can reduce the occurrence of side reactions, such as avoiding the dissolution of other metal ions such as scandium and iron, maintaining the purity of the solution after aluminum leaching, and reducing the complexity of subsequent separation treatment. Further, it is preferred that the mass concentration of the aluminum leaching alkali solution is 1 wt% to 15 wt%, and the dosage of the aluminum leaching alkali solution is 1 to 5 times the stoichiometric ratio of the aluminum element in the scandium-rich aluminum slag; and / or, the temperature of the aluminum leaching treatment is 30°C to 90°C, and the time of the aluminum leaching treatment is 1 h to 5 h.

[0062] The nickel content in the raw laterite nickel ore is 0.8 - 1.5 wt%, the cobalt content is 0.01 - 0.3 wt%, the iron content is 40 - 45 wt%, the magnesium content is 0.5 - 5 wt%, the manganese content is 0.5 - 2 wt%, the aluminum content is 0.5 - 4 wt%, and the scandium content is 20 - 80 ppm.

[0063] The concentration levels of various metal ions in the raw laterite nickel ore will affect the difficulty and cost of the subsequent iron removal process. Controlling the concentration of each metal ion within the above range helps to optimize the subsequent precipitation conditions, reduce the interference of iron precipitation on the recovery of nickel and cobalt, and thus improve the recovery rate and purity of the target metals.

[0064] In the preferred embodiment of the present application, through the above preparation process, the nickel content in the nickel-cobalt hydroxide product is 39 - 45 wt%, and the cobalt content is 3 - 5 wt%, thereby improving its utilization value.

[0065] The following further describes the present application in detail with specific examples, and these examples should not be construed as limiting the scope claimed by the present application.

[0066] Example 1

[0067] Refer to Figure 1 the improved treatment method process flow chart of laterite nickel ore to improve the laterite nickel ore, specifically as follows:

[0068] The raw material is limonite-type laterite nickel ore with a nickel content of 1.2%, a cobalt content of 0.12 wt%, an iron content of 45%, a magnesium content of 2%, a manganese content of 0.8 wt%, an aluminum content of 1.5%, and a scandium content of 40 ppm. After high-pressure sulfuric acid leaching with an acid-to-ore ratio of 250 kg / t ore, a temperature of 255 °C, and a leaching time of 1 h, filtration and washing are carried out after leaching to obtain the post-leaching solution and the first leaching residue. The temperature of the post-leaching solution is 90 °C, which is fed into the second-stage nickel-cobalt-manganese slurry (nickel-cobalt-manganese slurry) for iron oxidation removal to obtain the iron-oxidized removal slurry. The manganese-to-iron ratio (the molar ratio of the second-stage nickel-cobalt-manganese slurry to divalent iron in the post-leaching solution) is 1:1, the treatment time is 1 h, and the potential is 400 mV. Magnesium oxide is continuously used to neutralize and remove iron from the iron-oxidized removal slurry, with the end-point pH controlled at 3.3 and the time being 3 h. The iron removal rate is 99.8%. After filtration, the iron-removed residue is obtained. The iron-removed residue cake is treated with sodium hydroxide solution to wash aluminum, with a temperature of 90 °C, a dosage coefficient of sodium hydroxide solution (20 wt%) of 3 (the dosage of sodium hydroxide solution is 3 times the stoichiometric ratio of aluminum element in the iron-removed residue), and a time of 3 h. After washing away aluminum, a liquid phase and a cake are obtained. The cake is dried and calcined at 800 °C for 2 h to obtain a high-iron slag product, hematite, with an iron content of 63%. Magnesium oxide is added to the liquid phase for aluminum-scandium precipitation treatment, with the end-point pH controlled at 4.8 and the time being 3 h to obtain a scandium-rich aluminum slag and a post-aluminum-scandium-removal solution. The scandium-rich aluminum slag is leached with sodium hydroxide solution at a temperature of 90 °C, a dosage coefficient of sodium hydroxide solution (the dosage of sodium hydroxide solution is 4 times the stoichiometric ratio of aluminum element in the scandium-rich aluminum slag) of 4, and a time of 3 h to obtain a scandium-rich slag product and a post-aluminum-leaching solution. The post-aluminum-leaching solution is used to produce aluminum hydroxide. Sodium hydroxide is used for the first-stage precipitation of nickel and cobalt from the post-aluminum-scandium-removal solution at a temperature of 65 °C and a time of 3 h, with the end-point pH controlled at 8.0 to obtain an MHP product and a first-stage post-nickel-cobalt-precipitation solution. Magnesium oxide is used to neutralize the first-stage post-nickel-cobalt-precipitation solution. At the same time, compressed air is introduced for the second-stage precipitation of nickel and cobalt at a temperature of 65 °C and a time of 3 h, with the end-point pH controlled at 8.5. After precipitation, thickening is carried out to obtain a magnesium sulfate-manganese solution and a nickel-cobalt-manganese slurry. The nickel-cobalt-manganese slurry at the thickening underflow is returned to the above iron oxidation removal step.

[0069] Example 2

[0070] Refer to Figure 2 the process flow chart of the improved treatment method of laterite nickel ore to carry out improved treatment on laterite nickel ore, specifically as follows:

[0071] The raw material is limonite-type laterite nickel ore with a nickel content of 1.2%, a cobalt content of 0.12 wt%, an iron content of 45%, a magnesium content of 2%, a manganese content of 0.8 wt%, an aluminum content of 1.5%, and a scandium content of 40 ppm. Through high-pressure sulfuric acid leaching, secondary nickel-cobalt-manganese ore pulp (nickel-cobalt-manganese pulp) is introduced during the leaching process. The acid-to-ore ratio is 250 kg / t ore, the temperature is 255 °C, and the leaching time is 1 h. After leaching, filtration and washing are carried out to obtain the post-leaching solution and the first leaching residue. The temperature of the post-leaching solution is 90 °C, and oxidation for iron removal is carried out to obtain the oxidized iron-removed ore pulp. The manganese-to-iron ratio is 1:1, the treatment time is 1 h, and the potential is 400 mV. Then, magnesia is continuously used to neutralize and remove iron from the oxidized iron-removed ore pulp, with the end-point pH controlled at 3.3 and the time of 3 h. The iron removal rate is 99.8%. After filtration, the iron-removed residue is obtained. The iron-removed residue cake is treated with sodium hydroxide solution for aluminum washing at a temperature of 90 °C. The dosage coefficient of the sodium hydroxide solution is 3, and the time is 3 h to wash away aluminum, obtaining the liquid phase and the cake. The cake is dried and calcined at 800 °C for 2 h to obtain the high-iron slag product hematite with an iron content of 63%. Magnesia is added to the liquid phase for aluminum and scandium precipitation, with the end-point pH controlled at 4.8 and the time of 3 h, obtaining the scandium-rich aluminum slag and the post-aluminum and scandium-removed solution. The scandium-rich aluminum slag cake is leached with sodium hydroxide solution at a temperature of 90 °C. The dosage coefficient of the sodium hydroxide solution is 4, and the time is 3 h to obtain the scandium-rich slag product and the post-aluminum leaching solution. The post-aluminum leaching solution is used to produce aluminum hydroxide. Sodium hydroxide is used for primary nickel-cobalt precipitation from the post-aluminum and scandium-removed solution at a temperature of 65 °C and a time of 3 h, with the end-point pH controlled at 8.0, obtaining the MHP product and the primary nickel-cobalt precipitation post-solution. Magnesia is used to neutralize the primary nickel-cobalt precipitation post-solution. At the same time, compressed air is introduced for secondary nickel-cobalt precipitation at a temperature of 65 °C and a time of 3 h, with the end-point pH controlled at 8.5. After precipitation, thickening is carried out to obtain the magnesium sulfate and manganese solution and the nickel-cobalt-manganese pulp. The thickened underflow nickel-cobalt-manganese pulp is returned to the above-mentioned oxidized iron-removal step.

[0072] Example 3

[0073] Refer to Figure 3 the improved treatment process flow chart of laterite nickel ore to carry out improved treatment on laterite nickel ore, specifically as follows:

[0074] The raw material used is limonite-type laterite nickel ore, with a nickel content of 1.2%, a cobalt content of 0.12 wt%, an iron content of 45%, a magnesium content of 2%, a manganese content of 0.8 wt%, an aluminum content of 1.5%, and a scandium content of 40 ppm. After high-pressure sulfuric acid leaching, the acid-to-ore ratio is 250 kg / t ore, the temperature is 255 °C, the leaching time is 1 h. After leaching, filtration and washing are carried out to obtain the post-leaching solution and the first leaching residue. The temperature of the post-leaching solution is 90 °C, which is fed into the second-stage nickel-cobalt-manganese slurry (nickel-cobalt-manganese slurry) for iron oxidation removal to obtain the iron-oxidation-removal slurry, with a manganese-to-iron ratio of 1:1, a treatment time of 1 h, and a potential of 400 mV. Then, magnesium oxide is continuously used to pre-neutralize the iron-oxidation-removal slurry, with the end-point pH controlled at 1.0 and a time of 3 h. After filtration, the post-neutralization residue is obtained, and the post-neutralization residue is washed with sodium hydroxide solution at a temperature of 90 °C, with the dosage coefficient of the sodium hydroxide solution being 3 and a time of 3 h to obtain the liquid phase and the second leaching residue. Magnesium oxide is added to carry out the first-stage iron and aluminum removal on the liquid phase, with the end-point pH controlled at 3.0 and a time of 3 h to obtain the open-circuit iron and aluminum slag and the first-stage iron and aluminum removal post-liquid. Magnesium oxide is added to the first-stage iron and aluminum removal post-liquid to carry out the second-stage iron and aluminum removal, with the end-point pH controlled at 4.0 and a time of 3 h to obtain the second-stage iron and aluminum slag and the iron and aluminum removal post-liquid. The second-stage iron and aluminum slag is returned to the iron oxidation removal step. Sodium hydroxide is used to carry out the first-stage nickel and cobalt precipitation on the iron and aluminum removal post-liquid at a temperature of 65 °C, with a time of 3 h and the end-point pH controlled at 8.0 to obtain the MHP product and the first-stage nickel and cobalt precipitation post-liquid. Magnesium oxide is used to neutralize the first-stage nickel and cobalt precipitation post-liquid. At the same time, compressed air is introduced for the second-stage nickel and cobalt precipitation at a temperature of 65 °C, with a time of 3 h and the end-point pH controlled at 8.5. After precipitation, thickening is carried out to obtain the magnesium sulfate and manganese solution and the nickel-cobalt-manganese slurry. The thickened underflow nickel-cobalt-manganese slurry is returned to the above iron oxidation removal step.

[0075] Example 4

[0076] Reference Figure 4 The laterite nickel ore is improvedly processed with reference to the process flow chart of the improved treatment method of laterite nickel ore as follows:

[0077] The raw material used is limonite-type laterite nickel ore, with a nickel content of 1.2%, a cobalt content of 0.12 wt%, an iron content of 45%, a magnesium content of 2%, a manganese content of 0.8 wt%, an aluminum content of 1.5%, and a scandium content of 40 ppm. After high-pressure sulfuric acid leaching, the acid-to-ore ratio is 250 kg / t ore, the temperature is 255 °C, and the leaching time is 1 h. After leaching, filtration and washing are carried out to obtain the post-leaching solution and the first leaching residue. The post-leaching solution is subjected to cyclic leaching at a temperature of 90 °C to obtain a cyclic leaching pulp; magnesia is continuously used to pre-neutralize the cyclic leaching pulp, the end-point pH is controlled at 1.0, and the time is 3 h. After filtration, the post-neutralization residue is obtained. The post-neutralization residue is washed with a sodium hydroxide solution at a temperature of 90 °C, the dosage coefficient of the sodium hydroxide solution is 3, and the time is 3 h to obtain a liquid phase and a second leaching residue. Magnesia is added to carry out primary iron and aluminum removal on the liquid phase, the end-point pH is controlled at 3.0, and the time is 3 h to obtain an open-circuit iron and aluminum residue and a liquid phase after primary iron and aluminum removal. The liquid phase after primary iron and aluminum removal is fed into a secondary nickel-cobalt-manganese pulp (nickel-cobalt-manganese slurry), the manganese-to-iron ratio is 1:1, the treatment time is 1 h, and the potential is 400 mV. The liquid phase after primary iron and aluminum removal is subjected to secondary iron and aluminum removal, the end-point pH is controlled at 1.0, and the time is 3 h to obtain a secondary iron and aluminum residue and a liquid phase after iron and aluminum removal. The secondary iron and aluminum residue is returned to the step of oxidative iron removal. Sodium hydroxide is used to carry out primary nickel and cobalt precipitation on the liquid phase after iron and aluminum removal at a temperature of 65 °C, the time is 3 h, and the end-point pH is controlled at 8.0 to obtain an MHP product and a liquid phase after primary nickel and cobalt precipitation. Magnesia is used to neutralize the liquid phase after primary nickel and cobalt precipitation. At the same time, compressed air is introduced to carry out secondary nickel and cobalt precipitation at a temperature of 65 °C, the time is 3 h, and the end-point pH is controlled at 8.5. After precipitation, thickening is carried out to obtain a magnesium sulfate and manganese solution and a nickel-cobalt-manganese pulp. The nickel-cobalt-manganese pulp at the thickening underflow is returned to the above-mentioned oxidative iron removal step.

[0078] Example 5

[0079] The difference from Example 1 is that the molar ratio of the secondary nickel-cobalt-manganese pulp to ferrous iron in the post-leaching solution is 5:1, and an MHP product is finally obtained.

[0080] Example 6

[0081] The difference from Example 1 is that the molar ratio of the secondary nickel-cobalt-manganese pulp to ferrous iron in the post-leaching solution is 0.5:1, and an MHP product is finally obtained.

[0082] Example 7

[0083] The difference from Example 1 is that for neutralization and iron removal, the end-point pH is controlled at 3.5, and an MHP product is finally obtained.

[0084] Example 8

[0085] The difference from Example 1 is that for neutralization and iron removal, the end-point pH is controlled at 3.8, and an MHP product is finally obtained.

[0086] Example 9

[0087] It is different from Example 1 in that the dosage coefficient of the sodium hydroxide solution (20 wt%) (the dosage of the sodium hydroxide solution is the stoichiometric ratio of aluminum element in the iron-removing slag) is 5, and finally the MHP product is obtained.

[0088] Example 10

[0089] It is different from Example 1 in that the dosage coefficient of the sodium hydroxide solution (20 wt%) (the dosage of the sodium hydroxide solution is the stoichiometric ratio of aluminum element in the iron-removing slag) is 0.8, and finally the MHP product is obtained.

[0090] Example 11

[0091] It is different from Example 1 in that magnesium oxide is added to carry out aluminum-scandium precipitation treatment on the liquid phase, and the end point pH is controlled at 5.2, and finally the MHP product is obtained.

[0092] Example 12

[0093] It is different from Example 1 in that magnesium oxide is added to carry out aluminum-scandium precipitation treatment on the liquid phase, and the end point pH is controlled at 4.3, and finally the MHP product is obtained.

[0094] Example 13

[0095] It is different from Example 1 in that the dosage of the sodium hydroxide solution is 1 times the stoichiometric ratio of aluminum element in the scandium-rich aluminum slag, and finally the MHP product is obtained.

[0096] Example 14

[0097] It is different from Example 1 in that the dosage of the sodium hydroxide solution is 0.8 times the stoichiometric ratio of aluminum element in the scandium-rich aluminum slag, and finally the MHP product is obtained.

[0098] Example 15

[0099] The difference from Example 1 is that limonite-type laterite nickel ore is used as the raw material, with a nickel content of 1.2%, a cobalt content of 0.12 wt%, an iron content of 45%, a magnesium content of 2%, a manganese content of 0.8 wt%, an aluminum content of 1.5%, and a scandium content of 40 ppm. After high-pressure sulfuric acid leaching, the acid-to-ore ratio is 250 kg / t ore, the temperature is 255 °C, and the leaching time is 1 h. After leaching, filtration and washing are carried out to obtain the post-leaching solution and the first leaching residue. The temperature of the post-leaching solution is 40 °C, which is fed into the second-stage nickel-cobalt-manganese slurry (nickel-cobalt-manganese slurry) for iron oxidation removal to obtain the iron-oxidized removal slurry. The manganese-to-iron ratio (the molar ratio of the second-stage nickel-cobalt-manganese slurry to ferrous iron in the post-leaching solution) is 5:1, the treatment time is 2 h, and the potential is 400 mV. Then, magnesium oxide is continuously used to neutralize and remove iron from the iron-oxidized removal slurry, and the end-point pH is controlled at 3.5 for 8 h. The iron removal rate is 99.8%. After filtration, the iron-removed residue is obtained. The iron-removed residue cake is washed with aluminum using a sodium hydroxide solution at a temperature of 80 °C. The dosage coefficient of the sodium hydroxide solution (30 wt%) (the dosage of the sodium hydroxide solution is 8 times the stoichiometric ratio of aluminum element in the iron-removed residue) is 8, and the time is 3 h to wash away aluminum, obtaining the liquid phase and the cake. The cake is dried and calcined at 1000 °C for 2 h to obtain the high-iron slag product hematite with an iron content of 65%. Magnesium oxide is added to the liquid phase for aluminum-scandium precipitation treatment, and the end-point pH is controlled at 5.0 for 8 h to obtain the scandium-rich aluminum slag and the post-aluminum-scandium removal solution. The scandium-rich aluminum slag is leached with a sodium hydroxide solution at a temperature of 80 °C. The dosage coefficient of the sodium hydroxide solution (the dosage of the sodium hydroxide solution is 8 times the stoichiometric ratio of aluminum element in the scandium-rich aluminum slag) is 8, and the time is 8 h to obtain the scandium-rich slag product and the post-aluminum leaching solution. The post-aluminum leaching solution is used to produce aluminum hydroxide. Sodium hydroxide is used for the first-stage precipitation of nickel and cobalt from the post-aluminum-scandium removal solution at a temperature of 65 °C for 3 h, and the end-point pH is controlled at 7.0 to obtain the MHP product and the first-stage post-precipitation nickel-cobalt solution. Magnesium oxide is used to neutralize the first-stage post-precipitation nickel-cobalt solution. At the same time, compressed air is introduced for the second-stage precipitation of nickel and cobalt at a temperature of 45 °C for 5 h, and the end-point pH is controlled at 9.0. After precipitation, thickening is carried out to obtain the magnesium sulfate-manganese solution and the nickel-cobalt-manganese slurry. The thickened underflow nickel-cobalt-manganese slurry is returned to the above iron oxidation removal step.

[0100] Example 16

[0101] The difference from Example 3 is that limonite-type laterite nickel ore is used as the raw material, with a nickel content of 1.2%, a cobalt content of 0.12 wt%, an iron content of 45%, a magnesium content of 2%, a manganese content of 0.8 wt%, an aluminum content of 1.5%, and a scandium content of 40 ppm. After high-pressure sulfuric acid leaching, the acid-to-ore ratio is 400 kg / t ore, the temperature is 255 °C, and the leaching time is 1 h. After leaching, filtration and washing are carried out to obtain the post-leaching solution and the first leaching residue. The temperature of the post-leaching solution is 40 °C, which is fed into the second-stage nickel-cobalt-manganese slurry (nickel-cobalt-manganese slurry) for iron removal by oxidation to obtain an iron-removed oxidation slurry. The manganese-to-iron ratio (the molar ratio of manganese in the nickel-cobalt-manganese slurry to divalent iron in the post-first-stage iron and aluminum removal solution) is 5:1, the treatment time is 1 h, and the potential is 400 mV. Then, magnesium oxide is continuously used to pre-neutralize the iron-removed oxidation slurry, and the end-point pH is controlled at 2.0 for 5 h. After filtration, the post-neutralization residue is obtained, and the post-neutralization residue is washed with a sodium hydroxide solution at a temperature of 100 °C, the dosage coefficient of the sodium hydroxide solution is 3, and the time is 3 h to obtain a liquid phase and a second leaching residue. Magnesium oxide is added to the liquid phase for first-stage iron and aluminum removal, and the end-point pH is controlled at 4.0 for 5 h to obtain an open-circuit iron and aluminum slag and a first-stage iron and aluminum removal solution. Magnesium oxide is added to the first-stage iron and aluminum removal solution for second-stage iron and aluminum removal, and the end-point pH is controlled at 5.0 for 5 h to obtain a second-stage iron and aluminum slag and an iron and aluminum removal solution. The second-stage iron and aluminum slag is returned to the iron removal by oxidation step. Sodium hydroxide is used for first-stage nickel and cobalt precipitation in the iron and aluminum removal solution at a temperature of 65 °C for 3 h, and the end-point pH is controlled at 7.0 to obtain MHP products and a first-stage nickel and cobalt precipitation solution. Magnesium oxide is used to neutralize the first-stage nickel and cobalt precipitation solution. At the same time, compressed air is introduced for second-stage nickel and cobalt precipitation at a temperature of 65 °C for 3 h, and the end-point pH is controlled at 9.0. After precipitation, thickening is carried out to obtain a magnesium sulfate and manganese solution and a nickel-cobalt-manganese slurry, and the thickened underflow nickel-cobalt-manganese slurry is returned to the above iron removal by oxidation step.

[0102] Example 17

[0103] The difference from Example 4 is that limonite-type laterite nickel ore is used as the raw material, with a nickel content of 1.2%, a cobalt content of 0.12 wt%, an iron content of 45%, a magnesium content of 2%, a manganese content of 0.8 wt%, an aluminum content of 1.5%, and a scandium content of 40 ppm. After high-pressure sulfuric acid leaching, the acid-to-ore ratio is 250 kg / t of ore, the temperature is 255 °C, and the leaching time is 1 h. After leaching, filtration and washing are carried out to obtain the post-leaching solution and the first leaching residue. The post-leaching solution is subjected to cyclic leaching at a temperature of 90 °C to obtain a cyclic leaching pulp; magnesium oxide is continuously used to pre-neutralize the cyclic leaching pulp, the end-point pH is controlled at 1.5, and the time is 3 h. After filtration, the post-neutralization residue is obtained, and the post-neutralization residue is washed with sodium hydroxide solution at a temperature of 90 °C, the dosage coefficient of the sodium hydroxide solution is 3, and the time is 5 h to obtain a liquid phase and a second leaching residue. Magnesium oxide is added to carry out first-stage iron and aluminum removal on the liquid phase, the end-point pH is controlled at 4.0, and the time is 5 h to obtain an open-circuit iron and aluminum slag and a first-stage iron and aluminum removal post-liquid, which are fed into a second-stage nickel-cobalt-manganese pulp (nickel-cobalt-manganese slurry), the manganese-to-iron ratio is 1:1, the treatment time is 1 h, and the potential is 400 mV. The first-stage iron and aluminum removal post-liquid is subjected to second-stage iron and aluminum removal, the end-point pH is controlled at 5.0, and the time is 5 h to obtain a second-stage iron and aluminum slag and an iron and aluminum removal post-liquid. The second-stage iron and aluminum slag is returned to the step of oxidative iron removal. Sodium hydroxide is used to carry out first-stage nickel and cobalt precipitation on the iron and aluminum removal post-liquid at a temperature of 65 °C, the time is 3 h, the end-point pH is controlled at 7.0 to obtain an MHP product and a first-stage nickel and cobalt precipitation post-liquid. Magnesium oxide is used to neutralize the first-stage nickel and cobalt precipitation post-liquid. At the same time, compressed air is introduced to carry out second-stage nickel and cobalt precipitation at a temperature of 65 °C, the time is 3 h, and the end-point pH is controlled at 9.0. After precipitation, thickening is carried out to obtain a magnesium sulfate and manganese solution and a nickel-cobalt-manganese pulp, and the thickened underflow nickel-cobalt-manganese pulp is returned to the above oxidative iron removal step.

[0104] The nickel content, cobalt content and scandium recovery rate in the MHP products of the above examples were tested, and the test data are listed in Table 1.

[0105] Table 1

[0106] Examples Nickel content (wt%) Cobalt content (wt%) Recovery rate of scandium (%) Example 1 40.1 4.0 80.2 Example 2 40.2 4.2 80.5 Example 3 40.3 4.1 40.1 Example 4 40.2 4.2 40.0 Example 5 40.1 4.1 80.2 Example 6 40.3 4.2 80.2 Example 7 40.2 4.2 75.2 Example 8 40.5 4.1 70.2 Example 9 40.2 4.3 80.3 Example 10 40.1 4.0 80.1 Example 11 40.4 4.0 88.0 Example 12 39.1 3.5 75.2 Example 13 40.1 4.0 80.0 Example 14 40.5 4.4 80.2 Example 15 40.3 4.5 80.2 Example 16 40.2 4.2 40.1 Example 17 40.0 4.1 40.3

[0107] It should be noted that the purities of the MHP product and the scandium slag in Example 6 are slightly reduced.

[0108] The purities of nickel and cobalt in Example 10 and Example 12 are slightly reduced.

[0109] The nickel and cobalt recovery rates in Example 11 are slightly reduced.

[0110] The aluminum content in the high-iron slag in Example 14 is slightly on the high side.

[0111] From the above description, it can be seen that the above embodiments of the present invention achieve the following technical effects:

[0112] In the traditional process, compressed air is used to oxidize ferrous iron, resulting in low efficiency and a utilization rate of less than 3%, leading to energy waste. This application uses a manganese-containing substance as an oxidant to oxidize ferrous iron to ferric iron, which not only solves the problems of slow oxidation rate of ferrous iron at low pH and waste of compressed air, improves the oxidation efficiency and the utilization rate of manganese, but also enables ferric iron to precipitate at a lower pH, thereby reducing the precipitation of aluminum and scandium, achieving the effective separation of iron from aluminum and scandium, and improving the recovery rate of scandium. In addition, there are a total of four specific implementation methods for oxidizing ferrous iron to ferric iron, which can be specifically referred to Figures 1 to 4 , and the process differences are reflected in step S2. It can be seen that the main effects of the above improved treatment method for laterite nickel ore are as follows: significantly improving the oxidation efficiency of ferrous iron and the utilization rate of manganese, reducing the use of compressed air or oxygen, reducing power consumption, and lowering production costs; by effectively recovering iron, reducing the slag rate, reducing the use of tailing ponds, and greatly reducing the potential safety hazards and pollution to the environment; achieving the effective separation of iron from aluminum and scandium, improving the recovery rates of scandium and aluminum, while also enhancing the recovery rates of nickel and cobalt and the product quality; the four process routes provided by this method enhance the adaptability and flexibility of the process.

[0113] The above are only the preferred embodiments of the present invention and are not intended to limit the present invention. For those skilled in the art, the present invention can have various modifications and changes. Any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present invention shall be included within the protection scope of the present invention.

Claims

1. An improved treatment method for laterite nickel ore, wherein the laterite nickel ore is a mixed ore of limonite-type laterite nickel ore and residual-type laterite nickel ore in any proportion, and is characterized in that, The improved treatment method includes: Step S1: Acid-leach the laterite nickel ore and then filter and wash it to obtain a post-leaching solution and a first leaching residue; Step S2: Step S2 is selected from any one of Step S2-1, Step S2-2, and Step S2-3; In Step S2-1: Use a manganese-containing substance to oxidize and remove iron from the post-leaching solution to obtain an iron-oxidized removal ore pulp; Use an iron-removing neutralizing agent to sequentially perform neutralizing iron removal and liquid-solid separation on the iron-oxidized removal ore pulp to obtain an iron-removing residue, use an aluminum-washing alkaline solution to perform aluminum-washing treatment on the iron-removing residue to obtain a liquid phase and a high-iron slag product; Use a scandium-aluminum-precipitating neutralizing agent to perform scandium-aluminum precipitation on the liquid phase to obtain a scandium-rich aluminum slag and a post-aluminum-scandium-removal solution; In Step S2-2: Use a manganese-containing substance to oxidize and remove iron from the post-leaching solution to obtain an iron-oxidized removal ore pulp; Use a pre-neutralizing agent to sequentially perform pre-neutralization and liquid-solid separation on the iron-oxidized removal ore pulp to obtain a post-neutralization residue, wash the post-neutralization residue to obtain a liquid phase and a second leaching residue; Use a first-stage iron-aluminum-removing neutralizing agent to perform first-stage iron-aluminum removal on the liquid phase to obtain an open-circuit iron-aluminum slag and a first-stage post-iron-aluminum-removal solution, use a second-stage iron-aluminum-removing neutralizing agent to perform second-stage iron-aluminum removal on the first-stage post-iron-aluminum-removal solution to obtain a second-stage iron-aluminum slag and a post-iron-aluminum-removal solution; Return the second-stage iron-aluminum slag to the step of iron oxidation removal; In Step S2-3: Perform cyclic leaching on the post-leaching solution to obtain a cyclic leaching ore pulp; Use a pre-neutralizing agent to sequentially perform pre-neutralization and liquid-solid separation on the cyclic leaching ore pulp to obtain a post-neutralization residue, wash the post-neutralization residue to obtain a liquid phase and a second leaching residue; Use a first-stage iron-aluminum-removing neutralizing agent to perform first-stage iron-aluminum removal on the liquid phase to obtain an open-circuit iron-aluminum slag and a first-stage post-iron-aluminum-removal solution, use a manganese-containing substance to perform second-stage iron-aluminum removal on the first-stage post-iron-aluminum-removal solution to obtain a second-stage iron-aluminum slag and a post-iron-aluminum-removal solution; Return the second-stage iron-aluminum slag to the step of cyclic leaching; Step S3: Use a precipitating agent to perform first-stage nickel-cobalt precipitation and thickening filtration on the post-aluminum-scandium-removal solution or the post-iron-aluminum-removal solution to obtain a first-stage post-nickel-cobalt-precipitation solution and a nickel-cobalt hydroxide product; Step S4: Use a nickel-cobalt-precipitating neutralizing agent and an oxidizing agent to perform second-stage nickel-cobalt precipitation on the first-stage post-nickel-cobalt-precipitation solution to obtain a magnesium sulfate manganese solution and a nickel-cobalt-manganese pulp.

2. The improved processing method according to claim 1, wherein The manganese-containing substance is selected from any one or more of the nickel-cobalt-manganese pulp, manganese dioxide, potassium permanganate, sodium permanganate, pyrolusite, manganese sesquioxide, and manganese tetroxide.

3. The improved processing method according to claim 1, wherein In Step S2-1, the molar ratio of manganese in the manganese-containing substance to divalent iron in the post-leaching solution is 0.1-10:1; And / or, the temperature of the iron oxidation removal is 25°C-100°C, and the time of the iron oxidation removal is 0.1 h-5 h.

4. The improved processing method according to claim 1, wherein In Step S2-1, the end-point pH of the neutralizing iron removal is 2.8-3.5, the temperature of the neutralizing iron removal is 25°C-100°C, and the time of the neutralizing iron removal is 0.5 h-8 h; The iron-removing neutralizing agent is selected from any one or more of sodium carbonate, sodium bicarbonate, potassium carbonate, potassium bicarbonate, magnesium carbonate, magnesium bicarbonate, ammonium carbonate, ammonium bicarbonate, calcium oxide, magnesium oxide, sodium hydroxide, potassium hydroxide, ammonia water, calcium hydroxide, magnesium hydroxide, calcium carbonate, calcium bicarbonate, limestone, bitter earth powder, magnesite, dolomite and marble.

5. The improved processing method according to claim 1, characterized in that, In the step S2-1, the mass concentration of the aluminum-scrubbing lye is 0.1 wt% to 40 wt%, and the dosage of the aluminum-scrubbing lye is 0.8 to 8 times the stoichiometric ratio of aluminum element in the iron slag. and / or the temperature of the aluminum-scrubbing treatment is 25°C to 100°C, and the time of the aluminum-scrubbing treatment is 0.5 h to 8 h; and / or, returning the manganese sulfate solution to the step S2-1 as the aluminum-scrubbing lye.

6. The improved processing method according to claim 1, wherein, In the step S2-1, the end point pH of the aluminum and scandium precipitation treatment is 4.5 to 5.2, the temperature of the aluminum and scandium precipitation treatment is 25°C to 100°C, and the time of the aluminum and scandium precipitation treatment is 0.5 h to 8 h; and / or, the aluminum and scandium precipitation neutralizing agent is selected from any one or more of sodium carbonate, sodium bicarbonate, potassium carbonate, potassium bicarbonate, magnesium carbonate, magnesium bicarbonate, ammonium carbonate, ammonium bicarbonate, calcium oxide, magnesium oxide, sodium hydroxide, potassium hydroxide, ammonia water, calcium hydroxide, magnesium hydroxide, calcium carbonate, calcium bicarbonate, limestone, bitter earth powder, magnesite, dolomite and marble.

7. The improved processing method according to claim 1, characterized in that The step S2-1 further includes: successively drying and roasting the iron slag obtained by the aluminum-scrubbing treatment to obtain the high-iron slag product; wherein, the temperature of the roasting treatment is 500°C to 1200°C, the time of the roasting treatment is 1 min to 5 h, and the iron content in the high-iron slag product is 55% to 65%.

8. The improved processing method according to claim 1, characterized in that, In the step S2-2, the temperature of the iron oxidation removal is 25°C to 100°C, and the time of the iron oxidation removal is 0.1 h to 5 h.

9. The improved processing method according to claim 1, wherein, In the step S2-2, the pre-neutralizing agent, the first-stage iron and aluminum removal neutralizing agent and the second-stage iron and aluminum removal neutralizing agent are each independently selected from any one or more of sodium carbonate, sodium bicarbonate, potassium carbonate, potassium bicarbonate, magnesium carbonate, magnesium bicarbonate, ammonium carbonate, ammonium bicarbonate, calcium oxide, magnesium oxide, sodium hydroxide, potassium hydroxide, ammonia water, calcium hydroxide, magnesium hydroxide, calcium carbonate, calcium bicarbonate, limestone, bitter earth powder, magnesite, dolomite and marble; and / or, the end point pH of the pre-neutralization is 1 to 2, the temperature of the pre-neutralization is 25°C to 100°C, and the time of the pre-neutralization is 0.5 h to 8 h; and / or, the end point pH of the first-stage iron and aluminum removal is 3 to 4, the temperature of the first-stage iron and aluminum removal is 25°C to 100°C, and the time of the first-stage iron and aluminum removal is 0.5 h to 8 h; and / or, the end point pH of the second-stage iron and aluminum removal is 4 to 5, the temperature of the second-stage iron and aluminum removal is 25°C to 100°C, and the time of the second-stage iron and aluminum removal is 0.5 h to 8 h.

10. The improved processing method according to claim 1, wherein, In the step S2-3, the molar ratio of manganese in the manganese-containing substance to ferrous iron in the solution after the first-stage iron and aluminum removal is 0.1 to 10:

1.

11. The improved processing method according to claim 1, wherein In the step S2-3, the pre-neutralizing agent and the first-stage iron and aluminum removing neutralizing agent are each independently selected from any one or more of sodium carbonate, sodium bicarbonate, potassium carbonate, potassium bicarbonate, magnesium carbonate, magnesium bicarbonate, ammonium carbonate, ammonium bicarbonate, calcium oxide, magnesium oxide, sodium hydroxide, potassium hydroxide, ammonia water, calcium hydroxide, magnesium hydroxide, calcium carbonate, calcium bicarbonate, limestone, bitter earth powder, magnesite, dolomite and marble; and / or, the end pH of the pre-neutralization is 1-2, the temperature of the pre-neutralization is 25°C-100°C, and the time of the pre-neutralization is 0.5 h-8 h; and / or, the end pH of the first-stage iron and aluminum removal is 3-4, the temperature of the first-stage iron and aluminum removal is 25°C-100°C, and the time of the first-stage iron and aluminum removal is 0.5 h-8 h; and / or, the end pH of the second-stage iron and aluminum removal is 4-5, the temperature of the second-stage iron and aluminum removal is 25°C-100°C, and the time of the second-stage iron and aluminum removal is 0.1 h-5 h.

12. The improved processing method according to claim 1, wherein In the step S3, the end pH of the first-stage nickel and cobalt precipitation is 7.0-8.0, the temperature of the first-stage nickel and cobalt precipitation is 25°C-100°C, and the time of the first-stage nickel and cobalt precipitation is 0.5 h-8 h; The precipitating agent is selected from any one or more of magnesium oxide, sodium hydroxide and calcium hydroxide.

13. The improved processing method according to claim 1, characterized in that, In the step S4, the end pH of the second-stage nickel and cobalt precipitation is 8.0-9.0, the temperature of the second-stage nickel and cobalt precipitation is 25°C-100°C, and the time of the second-stage nickel and cobalt precipitation is 0.5 h-8 h; and / or, the nickel and cobalt precipitation neutralizing agent is selected from any one or more of sodium carbonate, sodium bicarbonate, potassium carbonate, potassium bicarbonate, magnesium carbonate, magnesium bicarbonate, ammonium carbonate, ammonium bicarbonate, calcium oxide, magnesium oxide, sodium hydroxide, potassium hydroxide, ammonia water, calcium hydroxide, magnesium hydroxide, calcium carbonate and calcium bicarbonate; and / or, the oxidizing agent is selected from any one or more of a mixture of sulfur dioxide and oxygen, oxygen, compressed air, oxygen enrichment, hydrogen peroxide, sodium persulfate, potassium persulfate and potassium permanganate.

14. The improved processing method according to claim 1, characterized in that, In the step S1, the temperature of the acid leaching is 80°C-280°C, the time of the acid leaching is 0.1-10 h, and the acid-to-ore ratio of the acid leaching is 200-400 kg / t ore.

15. The improved processing method according to claim 1, wherein The improved treatment method further includes: performing aluminum leaching treatment on the scandium-rich aluminum slag with an aluminum leaching alkali solution to obtain a scandium-rich slag product and a post-aluminum leaching solution; wherein, the mass concentration of the aluminum leaching alkali solution is 0.1 wt%-40 wt%, and the dosage of the aluminum leaching alkali solution is 0.8-8 times the stoichiometric ratio of the aluminum element in the scandium-rich aluminum slag; and / or, the temperature of the aluminum leaching treatment is 25°C-100°C, and the time of the aluminum leaching treatment is 0.5 h-8 h; and / or, the post-aluminum leaching solution is recycled and used as the aluminum leaching alkali solution.

Images