CN111777087A - System and method for producing alumina from coal gangue - Google Patents
System and method for producing alumina from coal gangue Download PDFInfo
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- CN111777087A CN111777087A CN202010774087.3A CN202010774087A CN111777087A CN 111777087 A CN111777087 A CN 111777087A CN 202010774087 A CN202010774087 A CN 202010774087A CN 111777087 A CN111777087 A CN 111777087A
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- 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
- C01F7/30—Preparation of aluminium oxide or hydroxide by thermal decomposition or by hydrolysis or oxidation of aluminium compounds
- C01F7/308—Thermal decomposition of nitrates
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03B—SEPARATING SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS
- B03B7/00—Combinations of wet processes or apparatus with other processes or apparatus, e.g. for dressing ores or garbage
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03B—SEPARATING SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS
- B03B9/00—General arrangement of separating plant, e.g. flow sheets
- B03B9/005—General arrangement of separating plant, e.g. flow sheets specially adapted for coal
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- 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
- C01B21/40—Preparation by absorption of oxides of nitrogen
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B33/00—Silicon; Compounds thereof
- C01B33/113—Silicon oxides; Hydrates thereof
- C01B33/12—Silica; Hydrates thereof, e.g. lepidoic silicic acid
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- 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
- C01F7/66—Nitrates, with or without other cations besides aluminium
Abstract
The invention belongs to the technical field of coal gangue resource utilization and alumina extraction. The system comprises a first sorting system which is connected in sequence and is used for sorting tailings in the coal gangue into magnetic ores and non-magnetic ores; a second separation system for separating silica from non-magnetic ore; a third separation system for separating alumina product from the remaining material; and the liquid outlet of the third separation system is communicated with the nonmagnetic ore inlet of the second separation system through a pipeline to form a circulation. Through the layer-by-layer separation of the system, the utilization rate of the coal gangue is improved, the heat accumulator is used as a decomposition heat source of the aluminum nitrate, the yield and the quality of the aluminum oxide are greatly improved, the consumption of auxiliary materials in the production process is reduced, and the production cost is reduced.
Description
Technical Field
The invention belongs to the technical field of resource utilization of coal gangue and extraction of alumina, and particularly relates to a system and a method for producing alumina from coal gangue.
Background
The coal gangue is solid waste discharged in the coal mining process and the coal washing process, and is a black and gray rock which has lower carbon content and is harder than coal and is associated with a coal bed in the coal forming process. Comprises tunneling waste rocks in the tunneling process of a roadway, waste rocks extracted from a top plate, a bottom plate and an interlayer in the mining process, and washing waste rocks extracted in the coal washing process. The main component of which is Al2O3、SiO2And in addition, Fe in different quantities2O3、CaO、MgO、Na2O、K2O、P2O5、SO3And trace rare elements.
The coal associated waste rock generated in the whole coal mining process is one of mining solid wastes, and comprises a mixture of washed gangue in a coal washing plant, hand-selected gangue in coal production, coal and rock discharged in the tunneling of a half coal roadway and a rock roadway, white gangue out of a coal system stacked together with the coal gangue and the like. In particular a mixture of carbonaceous, argillaceous and sandy shale, having a low calorific value. Contains carbon 10-25 wt% and humic acid partially. In modern society, about 1000Mt of coal gangue is stored every year, and about 100Mt is continuously discharged every year, so that not only is the land occupied accumulated, but also spontaneous combustion can pollute air or cause fire. In the prior art, the coal gangue treatment mode comprises building materials such as gangue cement, lightweight aggregate of concrete, refractory bricks and the like, and can also be used for recovering coal, co-firing coal and gangue for power generation, preparing chemical products such as crystalline aluminum chloride, water glass and the like, extracting precious and rare metals and being used as fertilizers. However, in the above mode, the heat value of the coal gangue cannot be enriched to the maximum extent, the alumina produced by taking the coal gangue as a raw material has poor quality, the acid consumption is large, the concentration of the gas product for decomposing the aluminum salt is low, and the content of the acid recovered and converted is low; the preparation of chemical products such as crystalline aluminum chloride, water glass and the like has the defects of large consumption of raw and auxiliary materials, high equipment requirement, high production cost and the like.
Disclosure of Invention
The invention aims to overcome the defects of poor quality, high acid consumption, low concentration of gas products for decomposing aluminum salt, low content of recovered and converted acid, high production cost and the like of the aluminum oxide produced by using coal gangue as a raw material in the prior art, and provides a system and a method for producing the aluminum oxide by using the coal gangue.
In order to achieve the above purpose, the invention provides the following technical scheme:
a system for producing alumina by coal gangue comprises a first sorting system and a second sorting system, wherein the first sorting system is connected in sequence and is used for sorting tailings in the coal gangue into magnetic ores and non-magnetic ores; a second separation system for separating silica from non-magnetic ore; a third separation system for separating alumina product from the residual material after removing silica;
the nonmagnetic ore outlet of the first separation system is communicated with the inlet of the second separation system, the residual material outlet after removing the silicon dioxide in the second separation system is communicated with the inlet of the third separation system, and the liquid outlet of the third separation system is communicated with the inlet of the second separation system through a pipeline; and the third separation system is used for producing alumina by adopting a heat accumulator circulation heat storage decomposition aluminum nitrate method.
Through above-mentioned system, nitric acid need not to be used for the leaching of a large amount of iron, has the advantage that the acid consumption is low, through purifying the edulcoration to aluminium nitrate solution and handling, make aluminium nitrate solution purity improve, the aluminium oxide purity that evaporative crystallization obtained is high, leachate impurity content is low advantage of edulcoration with low costs, through adopting heat accumulator circulation heat accumulation's mode to carry out the decomposition of aluminium nitrate salt, overcome among the prior art and adopted a large amount of combustion gas and aluminium nitrate direct contact to make its thermal decomposition and the unable reasonable recycle's of gaseous product that leads to. The gas product subjected to pyrolysis has high concentration by adopting the heat accumulator for circulating heat storage, the recovery rate of regenerating nitric acid through further absorption is high, the nitric acid can be recycled, the equipment cost of the system is reduced, and the process is simpler.
As a preferable scheme of the invention, the first separation system comprises a body mill, a flotation machine and a magnetic separator which are sequentially connected through pipelines. The coal gangue raw material is firstly ground in a body mill and then pumped into a flotation machine for flotation, and carbon in the coal gangue is selected out and sold as clean coal. The gangue tailings enter a magnetic separator, and magnetic material iron ore concentrate containing a large amount of iron is separated by magnetic separation. And the nonmagnetic materials enter a second sorting system.
As a preferable scheme of the invention, the second separation system comprises a slurrying tank, a reaction kettle and a filter which are sequentially connected through pipelines, and the slurrying tank is also provided with a nitric acid liquid inlet pipe. The non-magnetic material enters a slurrying tank, is subjected to a slurrying reaction with a nitric acid solution, is transferred into a reaction kettle, and is treated by a nitric acid leaching process at a certain temperature and pressure, so that aluminum metal in the coal gangue exists in the leaching solution in the form of aluminum ions, and silicon dioxide exists in filter residues, wherein the silicon dioxide can be applied to the building material industry, the production of white carbon black, agricultural fertilizers and the like.
As a preferable embodiment of the present invention, the third sorting system includes a refined aluminum nitrate crystal system and an aluminum nitrate crystal decomposition system; the refined aluminum nitrate crystal system comprises a crude aluminum nitrate solution storage tank, a purification system, an extraction system, a refined aluminum nitrate storage tank and an evaporative crystallization system which are sequentially connected through pipelines, and an inlet of the third separation system is positioned in the crude aluminum nitrate solution storage tank;
filtering the filter residue by a filter in a second sorting system, keeping the filter residue in the filter, putting the leachate into a crude aluminum nitrate solution storage tank in a refined aluminum nitrate crystal system, adding hydrogen peroxide into the leachate under an acidic condition to oxidize ferrous iron, oxidizing the ferrous iron into ferric iron, and hydrolyzing the ferric iron to generate Fe (OH) when the pH value is lower3Precipitating, filtering, and extracting rare metals such as scandium, gallium, germanium and the like after the iron liquid is removed by an extraction process; the obtained pure aluminum nitrate solution is evaporated and concentrated by an evaporation crystallization system to form aluminum nitrate crystals, and the aluminum nitrate crystals enter an aluminum nitrate crystal decomposition system;
the aluminum nitrate crystal decomposition system comprises a gaseous decomposition furnace, a nitric acid absorption device and a nitric acid storage tank which are sequentially connected through pipelines; the evaporative crystallization system is connected with the gaseous decomposing furnace; and a nitric acid outlet pipe arranged on the nitric acid storage tank is connected with a nitric acid inlet pipe of the slurrying tank.
The pure aluminum nitrate crystals obtained in the aluminum nitrate crystal refining system can be calcined to obtain aluminum oxide, nitrogen oxide gas generated by calcination is absorbed by a nitric acid absorption device to generate high-concentration nitric acid, and the regenerated nitric acid is returned to leaching for recycling.
The system comprises an evaporation crystallization system, a gaseous decomposition furnace, an aluminum nitrate crystal storage tank, a gas phase decomposition furnace and a gas phase separation system, wherein the evaporation crystallization system is arranged in the gas phase separation furnace, the gas phase separation furnace is arranged in the evaporation crystallization system, and the gas phase separation furnace is arranged in the gas phase separation furnace.
The device comprises a gas state decomposing furnace, a gas state decomposing furnace and a gas state decomposing furnace, wherein the gas state decomposing furnace is used for supplying heat to the gas state decomposing furnace, a heat accumulator outlet and a heat accumulator inlet are arranged on the heat accumulator furnace, the gas state decomposing furnace is respectively connected with the heat accumulator outlet and the heat accumulator inlet through pipelines to form a heat accumulator circulation channel, and a gas discharge pipeline is further arranged on the gas state decomposing furnace and connected with a nitric acid absorption device.
The heat accumulator enters the gaseous decomposition furnace from the heat accumulator outlet after reaching a certain temperature through temperature rise and heat accumulation in the heat accumulator furnace, and exchanges heat with the aluminum nitrate crystals, so that the aluminum nitrate crystals are decomposed into aluminum oxide and nitrogen oxide gas under the high-temperature heat of the heat accumulator, and the nitrogen oxide gas enters the nitric acid absorption device from the gas discharge pipeline to generate high-concentration nitric acid for recycling.
A method for producing alumina by adopting the system for producing alumina by coal gangue comprises the following steps:
s1: magnetic ore and non-magnetic ore are separated, the magnetic ore is separated from coal gangue by using a first separation system, and the remaining non-magnetic ore material enters a slurrying tank obtained by a second separation system for standby;
s2: adding a nitric acid solution and a nonmagnetic mineral material into the slurrying tank, uniformly mixing, allowing the mixture to enter a reaction kettle for reaction for 1-3 hours, filtering out silicon dioxide slag, and allowing the obtained rough aluminum nitrate solution to enter a rough aluminum nitrate solution storage tank of a third separation system for later use;
s3: purifying, extracting and removing impurities from the crude aluminum nitrate solution to obtain a refined aluminum nitrate solution, and further evaporating and crystallizing to obtain aluminum nitrate crystals for later use;
s4: and calcining the obtained aluminum nitrate crystal in a decomposing furnace through heat accumulator circulation heat accumulation to obtain an aluminum oxide crystal, absorbing the generated nitrogen oxide gas by a nitric acid absorption device to generate a high-concentration nitric acid solution, and returning the regenerated nitric acid solution to the slurrying tank for recycling through the nitric acid liquid inlet pipe.
According to the scheme, the carbon concentrate is separated from the coal gangue raw material through layer-by-layer separation, the carbon concentrate is separated from the coal gangue raw material through a flotation process in a first separation system and is used for producing refined carbon powder, and the iron concentrate is further separated through magnetic separation of tailings of the coal gangue; the non-magnetic mineral materials are mixed with nitric acid in the second sorting system and react in the reaction kettle to generate aluminum nitrate solution and silicon dioxide, wherein the silicon dioxide can be used for producing white carbon black, building materials, agricultural fertilizers and the like, the aluminum nitrate solution is purified, extracted and concentrated in the third sorting system to obtain aluminum nitrate crystals, the aluminum nitrate crystals are further combusted to produce aluminum oxide, the raw material utilization rate in the whole process is high, the consumption of auxiliary materials is low, and finally the combusted byproducts are regenerated into the nitric acid for recycling through a nitric acid absorption device, so that the production cost is reduced, the environmental pollution is reduced, and the theme of green and energy conservation is better met.
Preferably, in S1, water is added into the coal gangue for bulk grinding in a bulk mill, then the slurry is pumped into a flotation machine, carbon in the coal gangue is separated by flotation, the remaining tailings are magnetically separated under the field intensity of 3000-12000 gauss, and are filtered, and the iron-containing filter residue is separated from the non-magnetic ore material.
Preferably, in the S2, water is added into a slurrying tank according to the liquid-solid ratio of 2-5:1 for stirring and slurrying, and then nitric acid with the concentration of 20% -60% is added according to 1.1-1.8 times of the theoretical molar weight of aluminum consumption acid in the nonmagnetic mineral material for reaction, and the reaction temperature is 120-190 ℃.
Preferably, the molar quantity of the added nitric acid is 1.3-1.6 times of the molar quantity of the aluminum in the nonmagnetic mineral material, the aluminum element in the nonmagnetic mineral material can be fully reacted by enabling the nitric acid to be excessive, the phenomenon that the reaction of the aluminum element is insufficient due to the consumption of a small quantity of metal elements except the aluminum in the nonmagnetic mineral material on the nitric acid is avoided, on the other hand, the excessive nitric acid can enable the leachate to maintain a certain acidity to enable the reaction to be carried out, and the phenomenon that the yield of the aluminum nitrate is reduced due to the insufficient amount of the nitric acid, and further the final yield of the aluminum oxide is influenced is avoided.
Preferably, in S3, the purification reaction is carried out by adding an aqueous hydrogen peroxide solution to the crude aluminum nitrate solution and adjusting the pH to a range of 2.5 to 3.5, followed by filtration and extraction to obtain a purified aluminum nitrate solution.
Preferably, when the pH is adjusted to 2.5 to 3.0, al (oh) easily occurs due to an excessively high solution pH3Precipitating, fully reacting the precipitate with a rough aluminum nitrate solution through hydrogen peroxide, filtering to finally obtain an aluminum nitrate solution and iron slag after impurity removal, and carrying out extraction reaction on the aluminum nitrate solution to obtain a purified aluminum nitrate solution and rare metal slag such as scandium, gallium, germanium and the like.
Preferably, the temperature of the refined aluminum nitrate solution in the evaporation concentration process is 60-150 ℃.
Preferably, in the S4, the decomposition temperature range of the decomposition furnace is 800-1100 ℃.
Compared with the prior art, the invention has the beneficial effects that: .
1. By the process method, the heat value of the coal gangue is enriched by layer separation, the utilization rate of the coal gangue is improved, standard coal, iron ore concentrate, white carbon black, alumina and other products are separated from the coal gangue and can be reused, the heat value of the coal gangue is enriched to the maximum extent, the comprehensive utilization rate of the coal gangue is improved, no waste slag is generated, and waste liquid is recycled.
2. In the third separation system, the heat accumulator is used as a decomposition heat source of the aluminum nitrate, so that the yield and quality of the aluminum oxide are greatly improved, and the recovery rate of the nitric acid is more than 98%.
3. According to the invention, by further optimizing the leaching process, the leaching rate of the alumina reaches more than 90%, and the leachate can be further utilized through circulation, so that the consumption of auxiliary materials in the production process is greatly reduced, and the production cost is reduced.
Description of the drawings:
FIG. 1 is a process flow diagram of the present invention;
FIG. 2 is a schematic diagram of the system of the present invention;
the labels in the figure are: the method comprises the following steps of 1-body grinding machine, 2-flotation tank, 3-magnetic separator, 4-slurrying tank, 5-reaction kettle, 6-filter, 7-crude aluminum nitrate solution storage tank, 8-purification system, 9-extraction system, 10-refined aluminum nitrate storage tank, 11-evaporative crystallization system, 12-aluminum nitrate crystal storage tank, 13-gaseous decomposition furnace, 14-heat accumulator furnace, 15-nitric acid absorption device and 16-nitric acid storage tank.
Detailed Description
The present invention will be described in further detail with reference to test examples and specific embodiments. It should be understood that the scope of the above-described subject matter is not limited to the following examples, and any techniques implemented based on the disclosure of the present invention are within the scope of the present invention.
Example 1
A system for producing alumina by coal gangue comprises a first sorting system and a second sorting system, wherein the first sorting system is connected in sequence and is used for sorting tailings in the coal gangue into magnetic ores and non-magnetic ores; a second separation system for separating silica from non-magnetic ore; a third separation system for separating alumina product from the residual material after removing silica; the nonmagnetic ore outlet of the first separation system is communicated with the inlet of the second separation system, the residual material outlet after removing the silicon dioxide in the second separation system is communicated with the inlet of the third separation system, and the liquid outlet of the third separation system is communicated with the inlet of the second separation system through a pipeline; the process of producing the alumina by the third separation system comprises the step of preparing the alumina by decomposing the aluminum nitrate by adopting the heat accumulator for circulating heat storage.
Specifically, the first separation system comprises a body mill 1, a flotation machine 2 and a magnetic separator 3 which are sequentially connected through pipelines. The coal gangue raw material is firstly ground by a body mill 1 and then pumped into a flotation machine 2 for flotation, and carbon in the coal gangue is selected out to be sold as clean coal. The gangue tailings enter a magnetic separator 3, magnetic material iron ore concentrate containing a large amount of iron is separated through magnetic separation, and nonmagnetic materials enter a second separation system.
Specifically, the second separation system comprises a slurrying tank 4, a reaction kettle 5 and a filter 6 which are sequentially connected through a pipeline, and the slurrying tank 4 is further provided with a nitric acid liquid inlet pipe. The nonmagnetic material enters a slurrying tank 4, is subjected to a slurrying reaction with a nitric acid solution, is transferred into a reaction kettle 5, and is treated by a nitric acid leaching process at a certain temperature and under a certain pressure, so that aluminum metal in the coal gangue exists in a leaching solution in the form of aluminum ions, and silicon dioxide exists in filter residues, wherein the silicon dioxide can be applied to the building material industry, the production of white carbon black, agricultural fertilizers and the like.
Specifically, the third separation system comprises a refined aluminum nitrate crystal system and an aluminum nitrate crystal decomposition system; the refined aluminum nitrate crystal system comprises a crude aluminum nitrate solution storage tank 7, a purification system 8, an extraction system 9, a refined aluminum nitrate storage tank 10 and an evaporative crystallization system 11 which are sequentially connected through pipelines, and an inlet of the third separation system is positioned in the crude aluminum nitrate solution storage tank 7; filtering with a filter 6 in the second separation system to retain the filter residue in the filter 6, and introducing the leachate into refined nitric acidIn a crude aluminum nitrate solution storage tank 7 in the aluminum crystal system, hydrogen peroxide is added into the leaching solution under the acidic condition to oxidize ferrous iron, so that the ferrous iron is oxidized into ferric iron, and the hydrolysis of the ferric iron generates Fe (OH) when the pH value is lower3Precipitating, filtering, and extracting rare metals such as scandium, gallium, germanium and the like after the iron liquid is removed by an extraction process; the obtained pure aluminum nitrate solution is evaporated and concentrated by an evaporative crystallization system 11 to form aluminum nitrate crystals, and the aluminum nitrate crystals enter an aluminum nitrate crystal decomposition system;
the aluminum nitrate crystal decomposition system comprises a gaseous decomposition furnace 13, a nitric acid absorption device 15 and a nitric acid storage tank 16 which are sequentially connected through pipelines; the evaporative crystallization system 11 is connected with the gaseous decomposing furnace 13; and a nitric acid outlet pipe arranged on the nitric acid storage tank 16 is connected with a nitric acid inlet pipe of the slurrying tank 4. Further, the system comprises an aluminum nitrate crystal storage tank 12, wherein the aluminum nitrate crystal storage tank 12 is arranged between the evaporative crystallization system 11 and the gaseous decomposition furnace 13, and the aluminum nitrate crystal storage tank 12 is used for receiving the aluminum nitrate crystal obtained by crystallization of the evaporative crystallization system 11.
The pure aluminum nitrate crystals obtained in the aluminum nitrate crystal refining system can be calcined to obtain aluminum oxide, nitrogen oxide gas generated by calcination is absorbed by a nitric acid absorption device to generate high-concentration nitric acid, and the regenerated nitric acid is returned to leaching for recycling. Further, the refined aluminum nitrate crystal system further comprises a heat accumulator furnace 14, wherein the heat accumulator furnace 14 is used for providing a heat source for the gaseous decomposing furnace 13, a heat accumulator outlet and a heat accumulator inlet are arranged on the heat accumulator furnace 14, the gaseous decomposing furnace 13 is respectively connected with the heat accumulator outlet and the heat accumulator inlet through pipelines to form a heat accumulator circulation channel, and a gas discharge pipeline is further arranged on the gaseous decomposing furnace 13 and connected with the nitric acid absorbing device 15. The heat accumulator enters the gaseous decomposition furnace 13 from the outlet of the heat accumulator after reaching a certain temperature through temperature rise and heat accumulation in the heat accumulator furnace, and exchanges heat with the aluminum nitrate crystals, so that the aluminum nitrate crystals are decomposed into alumina and nitrogen oxide gas under the high-temperature heat of the heat accumulator, and the nitrogen oxide gas enters the nitric acid absorption device 15 from the gas discharge pipeline to generate high-concentration nitric acid for recycling.
Example 2
Embodiment 2 is a method for producing alumina by using the system for producing alumina by using coal gangue, which refers to the process flow of fig. 1:
the method specifically comprises the following steps:
s1: magnetic ore and non-magnetic ore are separated, the magnetic ore is separated from coal gangue by using a first separation system, and the remaining non-magnetic ore material enters a slurrying tank obtained by a second separation system for standby; specifically, water is added into the coal gangue, the coal gangue is subjected to body grinding in a body grinder to enable the particle size of the coal gangue to be smaller than 100 meshes, then an ore pulp pump is conveyed to a flotation machine, carbon in the coal gangue is separated out through flotation, the remaining tailings are subjected to magnetic separation under the field intensity of 8000 Gauss, filtering is carried out, and iron-containing filter residues are separated out from the nonmagnetic ore materials.
S2: adding a nitric acid solution and a nonmagnetic mineral material into the slurrying tank, uniformly mixing, allowing the mixture to enter a reaction kettle for reaction for 1-3 hours, filtering out silicon dioxide slag, and allowing the obtained rough aluminum nitrate solution to enter a rough aluminum nitrate solution storage tank of a third separation system for later use; in the S2, water is added into a slurrying tank according to the liquid-solid ratio of 5:1 for stirring and slurrying, and then nitric acid with the concentration of 50% is added according to 1.5 times of the theoretical amount of aluminum consumed in the nonmagnetic mineral material for reaction, wherein the reaction temperature is 150 ℃.
S3: purifying, extracting and removing impurities from the crude aluminum nitrate solution to obtain a refined aluminum nitrate solution, and further evaporating and crystallizing to obtain aluminum nitrate crystals for later use; in the step S3, an aqueous hydrogen peroxide solution is added to the crude aluminum nitrate solution, the pH value is adjusted to 2.8, a purification reaction is performed, then, the aluminum nitrate solution and the iron slag are obtained after impurity removal by filtration, and the aluminum nitrate solution is subjected to an extraction reaction to obtain the purified aluminum nitrate solution and rare metals such as scandium, gallium, germanium, and the like. The temperature of the evaporative crystallization was 120 ℃.
S4: and calcining the obtained aluminum nitrate crystal through a heat storage decomposition furnace to obtain an aluminum oxide crystal, dissolving and pumping the aluminum nitrate crystal into a heat storage body circulation heat storage type gaseous decomposition furnace at 150 ℃, contacting with a circulation nitrogen oxide gas at 1100 ℃, decomposing for 2min, absorbing the generated nitrogen oxide gas through a nitric acid absorption device to generate a high-concentration nitric acid solution, and returning the regenerated nitric acid solution to the slurrying tank for recycling through the nitric acid liquid inlet pipe.
In order to improve the yield of the alumina and simultaneously control the production cost to be the lowest, the concentration of nitric acid as an auxiliary material, the reaction temperature and the reaction time have certain comprehensive influence on the yield of the alumina in the process of producing the alumina from the coal gangue. In order to reduce the production cost and improve the yield, a large number of experimental optimization process flows are carried out. First, the following experiment was designed: under the condition that other parameters are fixed, the yield and the production cost of the alumina are compared by adjusting different nitric acid concentrations:
example 3
Example 3-1
A method for producing alumina by coal gangue comprises the following steps:
adding water into 1kg of coal gangue, carrying out bulk grinding in a bulk grinder to ensure that the particle size of the coal gangue is less than 100 meshes, then pumping the ore pulp into a flotation machine, selecting carbon in the coal gangue through flotation, carrying out magnetic separation on the remaining tailings under the field intensity of 3000-12000 gauss, filtering, and separating iron-containing filter residues from the non-magnetic ore materials.
Adding a nitric acid solution and a nonmagnetic mineral material into the slurrying tank, uniformly mixing, allowing the mixture to enter a reaction kettle for reaction for 1 hour, filtering out silicon dioxide slag, and allowing the obtained rough aluminum nitrate solution to enter a rough aluminum nitrate solution storage tank of a third separation system for later use; adding water into a slurrying tank according to the liquid-solid ratio of 2:1, stirring and slurrying, then adding 20% nitric acid according to 1.5 times of the theoretical amount of aluminum consumption in the nonmagnetic mineral material, and controlling the reaction temperature to be about 125 ℃.
Purifying, extracting and removing impurities from the crude aluminum nitrate solution to obtain a refined aluminum nitrate solution, and further evaporating and crystallizing to obtain aluminum nitrate crystals for later use; adding hydrogen peroxide solution into the rough aluminum nitrate solution, adjusting the pH value to about 3, carrying out purification reaction, filtering to obtain impurity-removed aluminum nitrate solution and iron slag, and carrying out extraction reaction on the aluminum nitrate solution to obtain purified aluminum nitrate solution and rare metals such as scandium, gallium, germanium and the like. The temperature of evaporative crystallization was 85 ℃.
And storing heat of the obtained aluminum nitrate crystal by a heat storage body, calcining the aluminum nitrate crystal in a gaseous decomposition furnace to obtain aluminum oxide, dissolving and pumping the aluminum nitrate crystal into a heat storage type circulating gaseous decomposition furnace at 100 ℃, contacting with 950 ℃ circulating nitrogen oxide gas, decomposing for 1-3min, absorbing the generated nitrogen oxide gas by a nitric acid absorption device to generate dilute nitric acid with the concentration of 55%, and returning the regenerated nitric acid to a slurrying tank for recycling through a nitric acid liquid inlet pipe.
Examples 3 to 2
The concentration of nitric acid is 30 percent, and the rest steps are the same as the example 3-1;
examples 3 to 3
The concentration of nitric acid is 40 percent, and the rest steps are the same as the example 3-1;
examples 3 to 4
The concentration of nitric acid is 50 percent, and the rest steps are the same as the example 3-1;
examples 3 to 5
The concentration of nitric acid is 60 percent, and the rest steps are the same as the example 3-1;
the results of each experiment in example 3 are summarized in table 1 as follows:
table 1 is a summary of the data for different nitric acid concentrations
| Example 3-1 | Examples 3 to 2 | Examples 3 to 3 | Examples 3 to 4 | Examples 3 to 5 | |
| HNO3/％ | 20 | 30 | 40 | 50 | 60 |
| Temperature/. degree.C | 125 | 125 | 125 | 125 | 125 |
| Time/h | 1 | 1 | 1 | 1 | 1 |
| Alumina/g | 372 | 395 | 440 | 445 | 448 |
From the experimental data in the summary table, it can be seen that when only the concentration of nitric acid is changed, 1kg of coal gangue is treated, the yield of alumina is increased when the concentration of nitric acid is increased, and when the concentration of nitric acid is 40-50%, the aluminum nitrate is generated most in the same time, and the concentration is increased continuously, and the growth is slower.
Example 4
Further, setting the concentration of nitric acid as an auxiliary material to be 45%, changing the reaction temperature on the basis, observing the influence of different reaction temperatures on alumina in the same reaction time, and setting 5 groups of gradient experiments as shown in table 2, wherein the specific experimental steps are shown in reference example 3;
table 2 is a summary of the data for different reaction temperatures
| Example 3-1 | Examples 3 to 2 | Examples 3 to 3 | Examples 3 to 4 | Examples 3 to 5 | |
| HNO3/％ | 45 | 45 | 45 | 45 | 45 |
| Temperature/. degree.C | 125 | 140 | 155 | 170 | 185 |
| Time/h | 2 | 2 | 2 | 2 | 2 |
| Alumina/g | 448 | 455 | 468 | 472 | 475 |
The data in table 2 show that increasing the temperature can effectively increase the alumina yield in the same reaction time, and at 170 ℃, the alumina yield is the best, the energy consumption is relatively low, the alumina yield tends to be stable when the temperature is continuously increased, and the energy consumption is high. Therefore, when the temperature is kept at about 170 ℃, the yield of the alumina can be ensured, and the consumption of the whole equipment is minimized.
Example 4
Further, in order to make the energy consumption of the whole process last, a comparative experiment was further performed on the reaction time, as shown in table 3;
table 3 is a summary of the data for different reaction times
| Example 3-1 | Examples 3 to 2 | Examples 3 to 3 | Examples 3 to 4 | Examples 3 to 5 | |
| HNO3/％ | 45 | 45 | 45 | 45 | 45 |
| Temperature/. degree.C | 175 | 175 | 175 | 175 | 175 |
| Time/h | 1 | 1.5 | 2 | 2.5 | 3 |
| Alumina/g | 451 | 459 | 473 | 475 | 474 |
As seen from the above table, when the reaction time is controlled to be 2-2.5h, the efficiency of the alumina can be further improved, and the corresponding energy consumption is increased to a certain extent. In the process for producing the alumina by the coal gangue, the coal gangue is treated by the first separation system, the nitric acid reacts with the separated nonmagnetic mineral materials to generate the aluminum nitrate, the leaching rate of the finally obtained alumina is obviously improved by further treatment, and meanwhile, the nitric acid is prevented from being consumed by leaching iron elements by the nitric acid, the using amount of the nitric acid is saved, and the production cost is reduced. The final decomposed gas can regenerate nitric acid solution for aluminum nitrate production through absorption, thereby greatly saving the consumption of auxiliary materials.
Example 5
In the above embodiment, through different optimization experiments, the selected optimal experimental parameters for producing alumina are processed by using coal gangue of different qualities and batches, and the experimental steps are as follows:
adding water into the coal gangue, carrying out bulk grinding in a bulk grinder to ensure that the particle size of the coal gangue is less than 100 meshes, then pumping the ore pulp into a flotation machine, selecting carbon in the coal gangue through flotation, carrying out magnetic separation on the remaining tailings under the field intensity of 3000-12000 gausses, filtering, and separating iron-containing filter residues from the nonmagnetic ore materials.
Adding a nitric acid solution and a nonmagnetic mineral material into the slurrying tank, uniformly mixing, allowing the mixture to enter a reaction kettle for reaction for 2.5 hours, filtering out silicon dioxide slag, and allowing the obtained rough aluminum nitrate solution to enter a rough aluminum nitrate solution storage tank of a third separation system for later use; adding water into a slurrying tank according to the liquid-solid ratio of 2:1, stirring and slurrying, then adding 45% nitric acid according to 1.5 times of the theoretical amount of aluminum consumption in the nonmagnetic mineral material, and reacting at the reaction temperature of about 175 ℃.
Purifying, extracting and removing impurities from the crude aluminum nitrate solution to obtain a refined aluminum nitrate solution, and further evaporating and crystallizing to obtain aluminum nitrate crystals for later use; adding hydrogen peroxide solution into the crude aluminum nitrate solution, adjusting the pH value to about 2.5, carrying out purification reaction, filtering to obtain impurity-removed aluminum nitrate solution and iron slag, and carrying out extraction reaction on the aluminum nitrate solution to obtain purified aluminum nitrate solution and rare metals such as scandium, gallium, germanium and the like. The temperature of the evaporative crystallization was 105 ℃.
And calcining the obtained aluminum nitrate crystals by a heat storage decomposition furnace to obtain aluminum oxide, dissolving and pumping the aluminum nitrate crystals into the heat storage type circulating gaseous decomposition furnace at 100 ℃, contacting with circulating nitric oxide gas at 950 ℃, decomposing for 3min, absorbing the generated nitric oxide gas by a nitric acid absorption device to generate dilute nitric acid with the concentration of 55%, and returning the regenerated nitric acid to the slurrying tank for recycling through the nitric acid liquid inlet pipe.
The experimental data are summarized in table 4:
table 4: statistical table of coal gangue processing data in example 5
| Example 5-1 | Examples 5 and 2 | Examples 5 to 3 | Examples 5 to 4 | |
| Coal gangue | 1kg | 1.5kg | 2kg | 2.5kg |
| Standard coal/kg | 0.15 | 0.22 | 0.32 | 0.35 |
| Quality of standard coal | 6500 big card | 6800 big card | 6700 big card | 6800 big card |
| HNO3Recovery rate | 98％ | 98.5％ | 99％ | 98.5％ |
| Leaching rate of alumina | 90％ | 92％ | 92％ | 92.5％ |
| Alumina content | 98％ | 98.3％ | 98.4％ | 98.5％ |
Comparative example
Reference is made to examples 5 to 4, which differ only in that: a direct-fired calcination decomposition device, such as a rotary kiln, a vertical decomposition furnace, a horizontal decomposition furnace and the like, is used as an aluminum nitrate crystal pyrolysis device, and combustion tail gas and gas products are mixed and enter an acid absorption device in the decomposition process, so that the volume of the existing nitric acid absorption device is about 20 times of that of the nitric acid absorption device.
The final calculated nitric acid recovery rate is only 81% due to the decrease in the concentration of acid gases in the absorption gas caused by the mixing of nitrogen oxides produced by the decomposition with the combustion off-gas.
In the system and the process of producing the alumina by using the system, the separation of various useful components in the coal gangue is realized through the cooperation of the first separation system, the second separation system and the third separation system in the system, the leaching rate of the alumina is improved through optimizing and controlling the concentration of nitric acid, the reaction temperature and the reaction time in the separation process, and the alumina content in the alumina powder accounts for more than 98 percent and basically does not contain impurities. In the process of decomposing aluminum nitrate, a heat source is provided for aluminum nitrate crystals by adopting a heat accumulator circulation heat storage mode, a large amount of combustion gas, oil and other heat sources are adopted to be in direct contact with inorganic salt to be decomposed in the traditional mode, and the process for heating and decomposing the inorganic salt is compared. In addition, the aluminum nitrate crystal prepared by dissolving the nitric acid is extremely high in purity, high in decomposition efficiency in the decomposition process of the heat accumulator, high in quality of decomposition products, recyclable in system, and capable of continuously and stably running without faults in a device system.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents and improvements made within the spirit and principle of the present invention are intended to be included within the scope of the present invention.
Claims (10)
1. A system for producing alumina by coal gangue is characterized by comprising a first separation system, a second separation system and a third separation system which are connected in sequence,
the first separation system is used for separating tailings in the coal gangue into magnetic ores and non-magnetic ores;
a second separation system for separating silica from the non-magnetic ore;
the third separation system is used for separating alumina from the residual material after the silicon dioxide is removed;
the nonmagnetic ore outlet of the first separation system is communicated with the inlet of the second separation system, the residual material outlet after removing the silicon dioxide in the second separation system is communicated with the inlet of the third separation system, and the liquid outlet of the third separation system is communicated with the inlet of the second separation system through a pipeline; the process of sorting the alumina by the third sorting system comprises the step of preparing the alumina by decomposing the aluminum nitrate by adopting the heat accumulator for circulating heat storage.
2. The system for producing the alumina by using the coal gangue as the claim 1, wherein the first separation system comprises a body mill (1), a flotation machine (2) and a magnetic separator (3) which are sequentially connected and arranged through pipelines.
3. The system for producing the alumina by using the coal gangue as recited in claim 1, wherein the second separation system comprises a slurrying tank (4), a reaction kettle (5) and a filter (6) which are sequentially connected through a pipeline, and the slurrying tank (4) is further provided with a nitric acid inlet pipe.
4. The system for producing aluminum oxide from coal gangue according to claim 3, wherein the third separation system comprises a refined aluminum nitrate crystal system and an aluminum nitrate crystal decomposition system;
the refined aluminum nitrate crystal system comprises a crude aluminum nitrate solution storage tank (7), a purification system (8), an extraction system (9), a refined aluminum nitrate storage tank (10) and an evaporative crystallization system (11) which are sequentially connected through pipelines, and an inlet of the third separation system is positioned in the crude aluminum nitrate solution storage tank;
the aluminum nitrate crystal decomposition system comprises an aluminum nitrate crystal storage tank (12), a gaseous decomposition furnace (13), a heat accumulator furnace (14), a nitric acid absorption device (15) and a nitric acid storage tank (16) which are sequentially connected through pipelines; the evaporative crystallization system (11) is connected with the aluminum nitrate crystal storage tank (12) through a pipeline; a nitric acid outlet pipe is arranged on the nitric acid storage tank (16) and is connected with a nitric acid inlet pipe of the slurrying tank (4);
the aluminum nitrate crystal storage tank (12) is used for receiving aluminum nitrate crystals obtained by crystallization of the evaporative crystallization system (11).
5. The method for producing the alumina by using the coal gangue is characterized by comprising the following steps of:
s1: magnetic ore and non-magnetic ore are separated, the magnetic ore is separated from coal gangue by using a first separation system, and the remaining non-magnetic ore material enters a slurrying tank of a second separation system for standby;
s2: adding a nitric acid solution and a nonmagnetic mineral material into the slurrying tank, uniformly mixing, conveying the mixture into a reaction kettle, reacting for 1-3 hours, and filtering out silicon dioxide slag to obtain a rough aluminum nitrate solution;
s3: purifying, extracting and removing impurities from the crude aluminum nitrate solution obtained in the step S2 to obtain a refined aluminum nitrate solution, and further evaporating and crystallizing to obtain aluminum nitrate crystals;
s4: and (4) performing cyclic heat storage on the aluminum nitrate crystal obtained in the step (S3) through a heat accumulator, calcining the aluminum nitrate crystal in the gaseous decomposing furnace to obtain an aluminum oxide crystal, absorbing nitrogen oxide gas generated by calcination by a nitric acid absorption device to generate a nitric acid solution, and returning the nitric acid solution to the slurrying tank for recycling.
6. The method as set forth in claim 5, wherein in S1, water is added into the coal gangue for bulk grinding, the obtained slurry is pumped to a flotation machine for flotation to separate carbon from the coal gangue, the remaining tailings are magnetically separated at field strength of 3000-12000 Gauss, and then filtered to separate the iron-containing filter residue from the non-magnetic mineral materials.
7. The method for producing alumina from coal gangue as claimed in claim 5, wherein in the S2, water is added into a slurrying tank according to the liquid-solid ratio of 2-5:1 for stirring and slurrying, and then nitric acid with the mass concentration of 20-60% is added according to 1.1-1.8 times of the theoretical molar quantity of the aluminum consumption acid in the nonmagnetic mineral material, and the reaction is carried out at the temperature of 120 ℃ and 190 ℃.
8. The method for producing aluminum oxide from coal gangue as claimed in claim 5, wherein in the step S3, the purification is performed by adding an aqueous solution of hydrogen peroxide into the crude aluminum nitrate solution, adjusting the pH value to be in the range of 2.5-3.5, and filtering and extracting after the purification is completed to obtain the refined aluminum nitrate solution.
9. The method for producing aluminum oxide from coal gangue as claimed in claim 8, wherein the temperature during the evaporation concentration of the refined aluminum nitrate solution is 60-150 ℃.
10. The method for producing alumina from coal gangue as recited in claim 5, wherein in the S4, the decomposition temperature is in the range of 800-1100 ℃.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113336252A (en) * | 2021-06-24 | 2021-09-03 | 四川顺应动力电池材料有限公司 | Method for removing calcium from pickle liquor of coal-based solid waste |
| CN113430377A (en) * | 2021-05-13 | 2021-09-24 | 北京科技大学 | Method for comprehensively extracting valuable components from coal gangue |
Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR521029A (en) * | 1919-09-19 | 1921-07-05 | Norske Elektrokemisk Ind As | Process for the production of alumina starting from solutions of aluminum nitrate |
| CN101450811A (en) * | 2008-10-23 | 2009-06-10 | 长春市超威新材料科技有限公司 | Method for extracting alumina from coal gangue |
| CN101913632A (en) * | 2010-08-30 | 2010-12-15 | 昆明理工大学 | Method for extracting aluminum oxide, monox and ferric oxide from gangue combustion ashes |
| RU2012134287A (en) * | 2012-08-10 | 2014-02-20 | Федеральное государственное бюджетное учреждение науки Объединенный институт высоких температур РАН (ОИВТ РАН) | METHOD FOR PROCESSING ASH AND SLAG MATERIALS OF COAL POWER PLANTS |
| CN106032286A (en) * | 2015-03-13 | 2016-10-19 | 中国石油化工股份有限公司 | Production method of alumina |
| CN107626712A (en) * | 2017-08-29 | 2018-01-26 | 陕西三秦能源长宏铝业有限公司 | A kind of aluminium electroloysis danger solid waste integrated conduct method and recycling |
| CN109721038A (en) * | 2019-02-19 | 2019-05-07 | 眉山顺应动力电池材料有限公司 | A kind of nitrate pyrolysis recycling method of nitric acid and apparatus system |
| CN110342479A (en) * | 2019-07-10 | 2019-10-18 | 辽宁东大粉体工程技术有限公司 | The system and method for carrying out magnesium nitrate atomization pyrolysis is heated using regenerative cycles |
| CN110963515A (en) * | 2019-12-27 | 2020-04-07 | 眉山顺应动力电池材料有限公司 | Method for recovering alumina from fly ash |
| CN211004576U (en) * | 2019-09-27 | 2020-07-14 | 眉山顺应动力电池材料有限公司 | Device system for preparing nitric acid by thermal decomposition of metal nitrate |
| CN212532311U (en) * | 2020-08-04 | 2021-02-12 | 四川顺应动力电池材料有限公司 | System for gangue production aluminium oxide |
-
2020
- 2020-08-04 CN CN202010774087.3A patent/CN111777087A/en active Pending
Patent Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR521029A (en) * | 1919-09-19 | 1921-07-05 | Norske Elektrokemisk Ind As | Process for the production of alumina starting from solutions of aluminum nitrate |
| CN101450811A (en) * | 2008-10-23 | 2009-06-10 | 长春市超威新材料科技有限公司 | Method for extracting alumina from coal gangue |
| CN101913632A (en) * | 2010-08-30 | 2010-12-15 | 昆明理工大学 | Method for extracting aluminum oxide, monox and ferric oxide from gangue combustion ashes |
| RU2012134287A (en) * | 2012-08-10 | 2014-02-20 | Федеральное государственное бюджетное учреждение науки Объединенный институт высоких температур РАН (ОИВТ РАН) | METHOD FOR PROCESSING ASH AND SLAG MATERIALS OF COAL POWER PLANTS |
| CN106032286A (en) * | 2015-03-13 | 2016-10-19 | 中国石油化工股份有限公司 | Production method of alumina |
| CN107626712A (en) * | 2017-08-29 | 2018-01-26 | 陕西三秦能源长宏铝业有限公司 | A kind of aluminium electroloysis danger solid waste integrated conduct method and recycling |
| CN109721038A (en) * | 2019-02-19 | 2019-05-07 | 眉山顺应动力电池材料有限公司 | A kind of nitrate pyrolysis recycling method of nitric acid and apparatus system |
| CN110342479A (en) * | 2019-07-10 | 2019-10-18 | 辽宁东大粉体工程技术有限公司 | The system and method for carrying out magnesium nitrate atomization pyrolysis is heated using regenerative cycles |
| CN211004576U (en) * | 2019-09-27 | 2020-07-14 | 眉山顺应动力电池材料有限公司 | Device system for preparing nitric acid by thermal decomposition of metal nitrate |
| CN110963515A (en) * | 2019-12-27 | 2020-04-07 | 眉山顺应动力电池材料有限公司 | Method for recovering alumina from fly ash |
| CN212532311U (en) * | 2020-08-04 | 2021-02-12 | 四川顺应动力电池材料有限公司 | System for gangue production aluminium oxide |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113430377A (en) * | 2021-05-13 | 2021-09-24 | 北京科技大学 | Method for comprehensively extracting valuable components from coal gangue |
| CN113336252A (en) * | 2021-06-24 | 2021-09-03 | 四川顺应动力电池材料有限公司 | Method for removing calcium from pickle liquor of coal-based solid waste |
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