CN111500853B - Bauxite suspension roasting dehydration dry method deironing system - Google Patents
Bauxite suspension roasting dehydration dry method deironing system Download PDFInfo
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- CN111500853B CN111500853B CN202010473118.1A CN202010473118A CN111500853B CN 111500853 B CN111500853 B CN 111500853B CN 202010473118 A CN202010473118 A CN 202010473118A CN 111500853 B CN111500853 B CN 111500853B
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Abstract
A bauxite suspension roasting dehydration dry method iron removing system, a feeding bin is opposite to a screw feeder, and the screw feeder is opposite to a feeding port of a Venturi dryer; the feeding holes of the Venturi dryer, the first cyclone preheater and the second cyclone preheater are communicated, the second cyclone preheater and the pre-oxidation suspension roasting furnace are communicated in series, the upper part of the pre-oxidation suspension roasting furnace is communicated with the thermal separation cyclone cylinder, the first flow seal valve, the top of the suspension reduction roasting furnace and the second flow seal valve are communicated in series, and the second flow seal valve, the first cooling cyclone cylinder, the second cooling cyclone cylinder and the third cooling cyclone cylinder are communicated with the collection bin in series; the collecting bin, the ore mill, the first pneumatic conveying pump, the wind power powder concentrator, the dust remover and the dry magnetic separator are matched in series. The device has strong adaptability to different types of bauxite and large processing capacity, and is suitable for large-scale industrial production.
Description
Technical Field
The invention belongs to the technical field of ore dressing, and particularly relates to a bauxite suspension roasting dehydration dry-method iron removal system.
Background
At present, the application of metal aluminum in national economic development of various countries in the world is second to steel, and with the development of modern high-technology industry, the metal aluminum is still an indispensable raw material. About 88 percent of the global bauxite reserves are laterite type bauxite which is characterized by medium aluminum, low silicon and high iron, wherein the main minerals of the bauxite comprise gibbsite, boehmite and diaspore, and the main minerals of the iron minerals comprise hematite, limonite and goethite; how to remove water and iron minerals in bauxite efficiently and realize the efficient and clean production of alumina has important significance.
Patent CN201610294513.7 discloses a method for separating iron and aluminum from high-iron bauxite, which proposes mixing high-iron bauxite powder with sodium hydroxide, limestone and water to make pellets, placing the high-iron bauxite pellets in a shaft furnace for direct reduction roasting after oxidation roasting, and obtaining aluminum enrichment and metallic iron through cooling, water grinding and wet magnetic separation; the iron-aluminum separation is realized, but the iron-aluminum separation needs to be carried out at the temperature of more than 1300 ℃ for oxidation roasting, and needs to be carried out at the temperature of more than 850 ℃ for direct reduction roasting for 3.5-4 hours, so that the defects of high energy consumption, low treatment capacity and the like exist, and the problem that the metal iron is easily oxidized again in the ore grinding and drying processes exists.
Patent CN201910374809.3 discloses a method for comprehensively utilizing iron and aluminum in high-iron bauxite, which proposes to use an acid solution to leach high-iron bauxite through stepwise oxidation, reduction and precipitation technologies to separate iron and aluminum, and recycle leachate.
Therefore, the most urgent problems at present are: develops equipment and a method capable of realizing the high-efficiency dehydration and iron removal of various types of bauxite and realizes large-scale industrial production.
Disclosure of Invention
The invention provides a bauxite suspension roasting dehydration dry method iron removal system, aiming at the technical problems of high energy consumption, low treatment capacity, large sewage production amount and the like in the existing bauxite dehydration iron removal technical process.
The bauxite suspension roasting dehydration dry-method iron removal system comprises a feeding bin 2, a Venturi dryer 5, a first cyclone preheater 6, a second cyclone preheater 7, a pre-oxidation suspension roasting furnace 8, a thermal separation cyclone 10, a suspension reduction roasting furnace 12, a collecting bin 18, an ore grinding machine 20, a first pneumatic conveying pump 21-1, a dust collector 28 and a dry-type magnetic separator 25; the outlet of the feeding bin 2 is opposite to the screw feeder 4, and the screw feeder 4 is opposite to the feeding port of the Venturi dryer 5; the discharge hole of the Venturi dryer 5 is communicated with the feed inlet of a first cyclone preheater 6, the discharge hole of the first cyclone preheater 6 is communicated with the feed inlet of a second cyclone preheater 7, the discharge hole of the second cyclone preheater 7 is communicated with the feed inlet below a pre-oxidation suspension roasting furnace 8, the bottom of the pre-oxidation suspension roasting furnace 8 is provided with a burner and an air inlet, the upper part of the pre-oxidation suspension roasting furnace 8 is communicated with the feed inlet of a thermal separation cyclone cylinder 10 through a pipeline, the discharge hole of the thermal separation cyclone cylinder 10 is communicated with the inlet of a first flow sealing valve 11, the outlet of the first flow sealing valve 11 is communicated with the feed inlet at the top of a suspension reduction roasting furnace 12, the bottom of the suspension reduction roasting furnace 12 is provided with a plurality of air inlets, the plurality of air inlets are communicated with a gas mixing tank, and the gas mixing tank is simultaneously communicated with a gas source and a nitrogen gas source; a discharge hole in the side part of the suspension reduction roasting furnace 12 is communicated with an inlet of a second flow seal valve 14, an outlet of the second flow seal valve 14 is communicated with a feed hole of a first cooling cyclone 15, a discharge hole of the first cooling cyclone 15 is communicated with a feed hole of a second cooling cyclone 16, a discharge hole of the second cooling cyclone 16 is communicated with a feed hole of a third cooling cyclone 17, and a discharge hole of the third cooling cyclone 17 is communicated with an inlet of a collection bin 18; the outlet of the collecting bin 18 is matched with the inlet of a grinding mill 20, and the outlet of the grinding mill 20 is opposite to the feeding hole of the first pneumatic conveying pump 21-1; the discharge hole of the first pneumatic conveying pump 21-1 is communicated with the feed inlet of the wind power powder concentrator 22, and the air inlet of the first pneumatic conveying pump 21-1 is communicated with the roots blower 30; the overflow port of the wind power powder concentrator 22 is communicated with the feed port of the dust remover 24; the discharge port of the dust remover 24 is opposite to the dry magnetic separator 25; the air outlet of the first cyclone preheater 6 is communicated with the air inlet of a dust collector 28, and the air outlet of the dust collector 26 is communicated with an induced draft fan 31.
In the device, a feeding belt 1 is arranged above the feeding bin 2 and used for conveying materials to the feeding bin 2.
In the device, a weightless feeder 3 is arranged between the feeding bin 2 and the screw feeder 4, and the weightless feeder 3 is respectively opposite to the outlet of the feeding bin 2 and the feeding end of the screw feeder 4.
In the device, a discharge hole of the dust collector 28 is opposite to an air chute 29, a discharge hole of the air chute 29 is opposite to a feed hole of a second pneumatic conveying pump 21-2, an air outlet of the second pneumatic conveying pump 21-2 is communicated with the feed hole of the thermal separation cyclone cylinder 10, and an air inlet of the second pneumatic conveying pump 21-2 is communicated with a roots blower 30; the air outlet of the thermal separation cyclone 10 is communicated with the feed inlet of the second cyclone preheater 7; the air outlet of the second cyclone preheater 7 is communicated with the air inlet at the bottom of the Venturi dryer 5 through a pipeline, a second auxiliary burner 9-3 and a third ash bucket valve 33-3 are arranged on the pipeline, and the second auxiliary burner 9-3 is communicated with a gas source.
In the device, an exhaust port arranged at the top of the suspension reduction roasting furnace 12 is communicated with a feed inlet at the bottom of the cyclone separator 13, an air outlet of the cyclone separator 13 is communicated with a feed inlet at the lower part of the pre-oxidation suspension roasting furnace 8, and a discharge port of the cyclone separator 13 is communicated with a second feed inlet at the top of the suspension reduction roasting furnace 12.
In the above device, the air outlet of the third cooling cyclone 17 is communicated with the feed inlet of the second cooling cyclone 16; the air outlet of the second cooling cyclone 16 is communicated with the feed inlet of the first cooling cyclone 15 through a pipeline, and a first ash bucket valve 33-1 is arranged on the pipeline; the air outlet of the first cooling cyclone 15 is communicated with the air inlet at the bottom of the pre-oxidation suspension roasting furnace 8 through a pipeline, and a second ash bucket valve 33-2 is arranged on the pipeline; the air inlet of the third cooling cyclone 17 is provided with an air duct 34-3 for letting in air.
In the device, a burner arranged at the bottom of the pre-oxidation suspension roasting furnace 8 consists of a main burner 9-1 and a first auxiliary burner 9-2, and the main burner 9-1 and the first auxiliary burner 9-2 are respectively communicated with a gas source.
In the device, the outlet of the induced draft fan 31 is communicated with the chimney 32.
In the above apparatus, the two outlets of the dry magnetic separator 25 are opposite to the aluminium concentrate collector 26 and the iron-containing tailings collector 27, respectively.
In the device, a sealing scraper conveyor 19 is arranged between a collecting bin 18 and a grinding mill 20, and the sealing scraper conveyor 19 is respectively matched with an outlet of the collecting bin 18 and an inlet of the grinding mill 20; the discharge port of the wind power powder concentrator 22 is matched with the inlet of the bucket elevator 23, and the outlet of the bucket elevator 23 is matched with the sealing scraper conveyor 19.
In the above apparatus, the pre-oxidation suspension roasting furnace 8, the suspension reduction roasting furnace 12, the dust collector 24 and the dust collector 27 are equipped with a couple temperature measuring device and a pressure sensor for detecting temperature and pressure.
In the above arrangement, the first cooling cyclone 15, the second cooling cyclone 16 and the third cooling cyclone 17 are equipped with galvanic temperature measuring devices and pressure sensors for detecting temperature and pressure.
The application method of the bauxite suspension roasting dehydration dry method iron removal system comprises the following steps:
1. crushing bauxite until the grain diameter is less than or equal to 15mm, then grinding until the part with the grain diameter of-0.074 mm accounts for more than or equal to 85 percent of the total mass, and obtaining fine ore; the bauxite contains Al according to the mass percentage2O3 30～55％，TFe 10～35％，SiO2 2～10％；
2. Placing the fine ore in a feeding bin 2, then conveying the fine ore to a screw feeder 4, and continuously conveying the fine ore into a Venturi dryer 5 through the screw feeder 4;
3. starting the induced draft fan 32 to generate negative pressure in the dust collector 27, the first cyclone preheater 6, the second cyclone preheater 7, the venturi dryer 5, the thermal separation cyclone 10 and the pre-oxidation suspension roasting furnace 8; introducing combustion flue gas into the Venturi dryer 5, mixing the combustion flue gas with the fine ore, and removing adsorption water of the fine ore; controlling the material temperature of a discharge port of the Venturi dryer 5 to be 130-150 ℃;
4. the combustion flue gas and the fine ore without adsorption water enter a first cyclone preheater 6 from a Venturi dryer 5, the solid material subjected to cyclone separation enters a second cyclone preheater 7, the solid material subjected to secondary cyclone separation is preheated to 450-600 ℃ in the second cyclone preheater 7, and then enters a pre-oxidation suspension roaster 8;
5. starting a burner to burn introduced gas to generate high-temperature flue gas, introducing the high-temperature flue gas into the pre-oxidation suspension roasting furnace 8, introducing air into the pre-oxidation suspension roasting furnace 8 through an air inlet, keeping the solid materials in the pre-oxidation suspension roasting furnace 8 in a suspension state under the action of air flow and negative pressure, and heating the solid materials to 700-750 ℃ to perform pre-oxidation roasting to remove adsorbed water; all materials after the pre-oxidation roasting are discharged from the upper part of the pre-oxidation suspension roasting furnace 8 along with air flow and enter a thermal separation cyclone 10; the solid material after cyclone separation is taken as oxidation slag powder, discharged from the thermal separation cyclone 10 and enters the suspension reduction roasting furnace 12 through the first flow seal valve 11;
6. introducing gas and nitrogen from the bottom of the suspension reduction roasting furnace 12, keeping the oxidized slag powder in a suspension state under the action of air flow and negative pressure, and carrying out reduction roasting at 600-650 ℃ to obtain weak-magnetic Fe2O3By reduction to ferromagnetic Fe3O4The solid material after reduction roasting is taken as reduction slag powder and is discharged from the side part of the suspension reduction roasting furnace 12;
7. reducing slag powder discharged from the suspension reduction roasting furnace 12 enters a second flow seal valve 14, then sequentially passes through a first cooling cyclone 15, a second cooling cyclone 16 and a third cooling cyclone 17, is cooled to be less than or equal to 100 ℃, and then enters a collection bin 18;
8. conveying the reduced slag powder in the collection bin 18 to a dry ore mill 20, performing dry ore milling until the part with the particle size of-0.074 mm accounts for more than or equal to 70% of the total mass, and then putting into a first pneumatic conveying pump 21-1; blowing air into the first pneumatic conveying pump 21-1 through the Roots blower 30, and conveying the materials in the first pneumatic conveying pump 21-1 to the wind power powder concentrator 22; wind power classification is carried out through a wind power powder concentrator 22, and overflow obtained by wind power classification is secondary powder ore with the grain diameter of-0.045 mm accounting for more than or equal to 70% of the total mass;
9. and conveying the secondary fine ore to a dust remover 24 for dust removal, and then conveying the secondary fine ore to a dry magnetic separator 25 for dry magnetic separation to obtain a non-magnetic product which is high-grade aluminum concentrate and a magnetic product which is iron-containing tailings.
In the above method, the fine ore is conveyed to the feed bin 2 through the feed belt 1.
In the method, the powder ore in the feeding bin 2 is continuously conveyed to the screw feeder 4 through the weightless feeder 3.
In the method, after the fine ore enters the first cyclone preheater 6, the separated gas is discharged from the first cyclone preheater 6 and then enters the dust collector 28, and the gas after dust removal enters the induced draft fan 31; after dust generated by dust removal is discharged, the dust enters the second pneumatic conveying pump 21-2 through an air chute 29; blowing air into the second pneumatic conveying pump 21-2 through the roots blower 30, and conveying dust in the second pneumatic conveying pump 21-2 to the thermal separation cyclone cylinder 10; the gas separated by the thermal separation cyclone 10 in the cyclone separation process is introduced into the second cyclone preheater 7; the gas separated by the second cyclone preheater 7 in the cyclone separation process is introduced into the venturi dryer 5 through a pipeline, the second auxiliary burner 9-3 arranged on the pipeline simultaneously introduces combustion flue gas into the venturi dryer 5, and a third ash bucket valve 33-3 arranged on the pipeline is used for cleaning ash.
In the method, gas generated in the reduction roasting process of the suspension reduction roasting furnace 12 is introduced into the cyclone separator 13 from an exhaust port at the top; the dust separated by the cyclone separator 13 returns to the suspension reduction roasting furnace 12 through a second feeding hole at the top of the suspension reduction roasting furnace 12, and the separated gas is introduced into a feeding hole at the lower part of the pre-oxidation suspension roasting furnace 8.
In the method, the gas separated by the third cooling cyclone 17 in the cyclone separation process is introduced into the feed inlet of the second cooling cyclone 16; the gas separated by the second cooling cyclone 16 in the cyclone separation process is introduced into the feed inlet of the first cooling cyclone 15 through a pipeline, and a first ash bucket valve 33-1 arranged on the pipeline is used for cleaning ash; the gas separated by the first cooling cyclone 15 in the cyclone separation process is introduced into the gas inlet at the bottom of the pre-oxidation suspension roasting furnace 8 through a pipeline, and a second ash bucket valve 33-2 arranged on the pipeline is used for removing ash; while the air duct 34-3 connected via the air inlet of the third cooling cyclone 17 is fed with air.
In the method, the burner arranged at the bottom of the pre-oxidation suspension roasting furnace 8 consists of a main burner 9-1 and a first auxiliary burner 9-2, and gas is respectively introduced through a gas pipeline 34-1.
In the method, gas and nitrogen are respectively introduced into a gas mixing tank communicated with a plurality of gas inlets of the suspension reduction roasting furnace 12 through a gas pipeline 34-1 and a nitrogen pipeline 34-2.
In the method, the gas exhausted by the induced draft fan 31 is exhausted through a chimney 32.
In the method, the reduced slag powder in the collection bin 18 is put into a sealed scraper conveyor 19 and then conveyed to a dry mill 20; the settled sand after wind classification is conveyed to a bucket elevator 23, and conveyed to a sealing scraper conveyor 19 through the bucket elevator 23.
In the method, the temperature and the pressure are detected by a galvanic couple temperature measuring device and a pressure sensor which are respectively assembled by the pre-oxidation suspension roasting furnace 8, the suspension reduction roasting furnace 12, the dust remover 24 and the dust collector 28.
In the above method, the temperature and pressure are detected by the even temperature measuring device and the pressure sensor assembled with the first cyclone 15, the second cooling cyclone 16 and the third cooling cyclone 17, respectively.
In the above method, the main reaction formula of the adsorption water for removing fine ore is:
2Al(OH)3＝Al2O3+3H2O、
2Al(OOH)＝Al2O3+H2o and
mFe2O3·nH2O＝mFe2O3+nH2O。
in the method, the retention time of the fine ore in the pre-oxidation suspension roasting furnace is 2-15 min.
In the method, the gas is introduced according to the amount of H in the gas2CO and Fe in fine ore2O31.1-1.3 times of the amount required by the complete reaction theory is introduced, and the reaction formula of the complete reaction is as follows:
Fe2O3+H2/CO＝Fe2O3+CO2/H2O。
in the method, the volume concentration of the coal gas in the reduction roasting furnace is 25-40%.
In the method, the retention time of the oxide slag powder in the reduction roasting furnace is 20-60 min.
In the method, the magnetic field intensity of the dry magnetic separation is 1100-1300 Oe.
The high-grade aluminum concentrate contains less than or equal to 6 percent of TFe and Al according to mass percent2O3 65～80％。
In the method, the recovery rate of the alumina is 80-85%.
Compared with the traditional dressing process and roasting process of the bauxite, the device and the method have the advantages of high heat and mass transfer efficiency, low energy consumption and the like, have strong adaptability to different types of bauxite, have large processing capacity and are suitable for large-scale industrial production.
Drawings
FIG. 1 is a schematic structural diagram of a bauxite suspension roasting dehydration dry-process iron removal system of the present invention;
in the figure, 1, a feeding belt, 2, a feeding bin, 3, a weight loss feeder, 4, a screw feeder, 5, a Venturi dryer, 6, a first cyclone preheater, 7, a second cyclone preheater, 8, a pre-oxidation suspension roasting furnace, 9-1, a main burner, 9-2, a first auxiliary burner, 9-3, a second auxiliary burner, 10, a thermal separation cyclone cylinder, 11, a first flow sealing valve, 12, a suspension reduction roasting furnace, 13, a cyclone separator, 14, a second flow sealing valve, 15, a first cooling cyclone cylinder, 16, a second cooling cyclone cylinder, 17, a third cooling cyclone cylinder, 18, a collecting bin, 19, a sealing scraper conveyor, 20, a dry-type ore grinding machine, 21-1, a first air conveying pump, 21-2, a second air conveying pump, 22, a wind power selector, 23 and a bucket elevator, 24. the device comprises a dust collector, 25 parts of a dry magnetic separator, 26 parts of an aluminum concentrate collector, 27 parts of an iron-containing tailing collector, 28 parts of a dust collector, 29 parts of an air chute, 30 parts of a Roots blower, 31 parts of a draught fan, 32 parts of a chimney, 33-1 parts of a first ash bucket valve, 32-3 parts of a second ash bucket valve, 33-3 parts of a third ash bucket valve, 34-1 parts of a gas pipeline, 34-2 parts of a nitrogen pipeline, 34-3 parts of an air pipeline;
fig. 2 is a schematic diagram of the flow seal valve structure of the present invention.
Detailed Description
The bauxite adopted in the embodiment of the invention contains Al according to the mass percentage2O3 30～55％，TFe 10～35％，SiO2 2～10％。
The feeding belt, the weight loss feeder, the screw feeder and the venturi dryer adopted in the embodiment of the invention are commercially available products.
The first cooling cyclone, the second cooling cyclone, the third cooling cyclone, the first cyclone preheater and the second cyclone preheater adopted in the embodiment of the invention are all commercially available cyclone separators.
The sealing scraper conveyor, the ash bucket valve, the air chute, the pneumatic conveying pump, the dry ore mill, the dry magnetic separator, the bucket elevator and the wind power powder concentrator adopted in the embodiment of the invention are commercially available products.
The dust collector adopted in the embodiment of the invention is a commercially available electric dust collector.
The dust remover adopted in the embodiment of the invention is a commercially available bag-type dust remover.
The structural principle of the flow seal valve adopted in the embodiment of the invention is shown in fig. 2, a baffle plate is arranged in the flow seal valve to divide the interior of the flow seal valve into a feeding chamber and a discharging chamber, the top edge and the side edge of the baffle plate are fixedly connected with the interior of the flow seal valve, and a gap is formed between the bottom edge of the baffle plate and the bottom of the flow seal valve to serve as a horizontal channel; a feeding hole is formed in the side wall of the feeding chamber, a discharging hole is formed in the side wall of the discharging chamber, the feeding hole and the discharging hole are both positioned above the bottom edge of the baffle, and the feeding hole is higher than the discharging hole; the bottom plate of the feeding chamber is provided with a loosening air inlet communicated with the air inlet pipeline 1, and the bottom plate of the discharging chamber is provided with a fluidizing air inlet communicated with the air inlet pipeline 2; the air inlet pipeline 1 and the air inlet pipeline 2 are respectively communicated with an air source.
The working method of the flow seal valve in the embodiment of the invention comprises the following steps: solid materials entering from the feeding hole are gradually accumulated, when the horizontal channel is closed by the solid materials, gas is introduced into the feeding chamber through the gas inlet pipeline 1 to serve as loosening wind, and gas is introduced into the discharging chamber through the gas inlet pipeline 2 to serve as fluidized wind, so that the solid materials in the feeding chamber move towards the discharging chamber under the action of gas flow; along with the solid materials are gradually accumulated in the feeding chamber and the discharging chamber, when the top surface of the solid materials in the discharging chamber is lifted to the position of the discharging port, the solid materials in the discharging chamber are discharged from the discharging port under the action of air flow.
In the embodiment of the invention, the air pipeline 1 and the air inlet pipeline 2 are respectively communicated with a nitrogen source, and nitrogen is used as loosening air and fluidizing air.
In the embodiment of the present invention, the pre-oxidation suspension roasting furnace 8, the suspension reduction roasting furnace 12, the dust collector 24, and the dust collector 27 are equipped with a couple temperature measuring device and a pressure sensor for detecting temperature and pressure.
In an embodiment of the invention, the first cooling cyclone 15, the second cooling cyclone 16 and the third cooling cyclone 17 are equipped with galvanic temperature measuring devices and pressure sensors for detecting temperature and pressure.
In the embodiment of the invention, the temperature and the pressure are detected by a galvanic couple temperature measuring device and a pressure sensor which are respectively assembled by the pre-oxidation suspension roasting furnace 8, the suspension reduction roasting furnace 12, the dust remover 24 and the dust collector 28.
In the embodiment of the present invention, the temperature and the pressure are detected by the dual temperature measuring device and the pressure sensor assembled with the first cyclone 15, the second cooling cyclone 16 and the third cooling cyclone 17, respectively.
The present invention will be described in further detail with reference to the accompanying drawings and specific embodiments.
Example 1
The structure of the bauxite suspension roasting dehydration dry-method iron removal system is shown in figure 1, and comprises a feeding bin 2, a venturi dryer 5, a first cyclone preheater 6, a second cyclone preheater 7, a pre-oxidation suspension roasting furnace 8, a thermal separation cyclone cylinder 10, a suspension reduction roasting furnace 12, a collecting bin 18, an ore mill 20, a first pneumatic conveying pump 21-1, a dust collector 28 and a dry-type magnetic separator 25;
a feeding belt 1 is arranged above the feeding bin 2 and used for conveying materials to the feeding bin 2; a weightless feeder 3 is arranged between the feeding bin 2 and the screw feeder 4, the weightless feeder 3 is respectively opposite to the outlet of the feeding bin 2 and the feeding end of the screw feeder 4, and the screw feeder 4 is opposite to the feeding port of the venturi dryer 5;
the discharge hole of the Venturi dryer 5 is communicated with the feed inlet of a first cyclone preheater 6, the discharge hole of the first cyclone preheater 6 is communicated with the feed inlet of a second cyclone preheater 7, the discharge hole of the second cyclone preheater 7 is communicated with the feed inlet below a pre-oxidation suspension roasting furnace 8, the bottom of the pre-oxidation suspension roasting furnace 8 is provided with a burner and an air inlet, the upper part of the pre-oxidation suspension roasting furnace 8 is communicated with the feed inlet of a thermal separation cyclone cylinder 10 through a pipeline, the discharge hole of the thermal separation cyclone cylinder 10 is communicated with the inlet of a first flow sealing valve 11, the outlet of the first flow sealing valve 11 is communicated with the feed inlet at the top of a suspension reduction roasting furnace 12, the bottom of the suspension reduction roasting furnace 12 is provided with a plurality of air inlets, the plurality of air inlets are communicated with a gas mixing tank, and the gas mixing tank is simultaneously communicated with a gas source and a nitrogen gas source;
a discharge hole in the side part of the suspension reduction roasting furnace 12 is communicated with an inlet of a second flow seal valve 14, an outlet of the second flow seal valve 14 is communicated with a feed hole of a first cooling cyclone 15, a discharge hole of the first cooling cyclone 15 is communicated with a feed hole of a second cooling cyclone 16, a discharge hole of the second cooling cyclone 16 is communicated with a feed hole of a third cooling cyclone 17, and a discharge hole of the third cooling cyclone 17 is communicated with an inlet of a collection bin 18;
a sealing scraper conveyor 19 is arranged between the collecting bin 18 and the ore mill 20, and the sealing scraper conveyor 19 is respectively matched with an outlet of the collecting bin 18 and an inlet of the ore mill 20; the discharge port of the wind power powder concentrator 22 is matched with the inlet of the bucket elevator 23, and the outlet of the bucket elevator 23 is matched with the sealing scraper conveyor 19;
the outlet of the mill 20 is opposite to the feed inlet of the first pneumatic conveying pump 21-1; the discharge hole of the first pneumatic conveying pump 21-1 is communicated with the feed inlet of the wind power powder concentrator 22, and the air inlet of the first pneumatic conveying pump 21-1 is communicated with the roots blower 30; the overflow port of the wind power powder concentrator 22 is communicated with the feed port of the dust remover 24; the discharge port of the dust remover 24 is opposite to the dry magnetic separator 25; an air outlet of the first cyclone preheater 6 is communicated with an air inlet of a dust collector 28, and an air outlet of the dust collector 26 is communicated with an induced draft fan 31;
the discharge hole of the dust collector 28 is opposite to the air chute 29, the discharge hole of the air chute 29 is opposite to the feed hole of the second pneumatic conveying pump 21-2, the air outlet of the second pneumatic conveying pump 21-2 is communicated with the feed hole of the thermal separation cyclone cylinder 10, and the air inlet of the second pneumatic conveying pump 21-2 is communicated with the roots blower 30; the air outlet of the thermal separation cyclone 10 is communicated with the feed inlet of the second cyclone preheater 7; an air outlet of the second cyclone preheater 7 is communicated with an air inlet at the bottom of the Venturi dryer 5 through a pipeline, a second auxiliary burner 9-3 and a third ash bucket valve 33-3 are arranged on the pipeline, and the second auxiliary burner 9-3 is communicated with a gas source;
an exhaust port arranged at the top of the suspension reduction roasting furnace 12 is communicated with a feed inlet at the bottom of the cyclone separator 13, an air outlet of the cyclone separator 13 is communicated with a feed inlet at the lower part of the pre-oxidation suspension roasting furnace 8, and a discharge port of the cyclone separator 13 is communicated with a second feed inlet at the top of the suspension reduction roasting furnace 12;
the air outlet of the third cooling cyclone 17 is communicated with the feed inlet of the second cooling cyclone 16; the air outlet of the second cooling cyclone 16 is communicated with the feed inlet of the first cooling cyclone 15 through a pipeline, and a first ash bucket valve 33-1 is arranged on the pipeline; the air outlet of the first cooling cyclone 15 is communicated with the air inlet at the bottom of the pre-oxidation suspension roasting furnace 8 through a pipeline, and a second ash bucket valve 33-2 is arranged on the pipeline; the air inlet of the third cooling cyclone 17 is provided with an air pipeline 34-3 for introducing air;
the burner arranged at the bottom of the pre-oxidation suspension roasting furnace 8 consists of a main burner 9-1 and a first auxiliary burner 9-2, and the main burner 9-1 and the first auxiliary burner 9-2 are respectively communicated with a gas source;
the outlet of the induced draft fan 31 is communicated with a chimney 32;
two outlets of the dry magnetic separator 25 are respectively opposite to the aluminum concentrate collector 26 and the iron-containing tailings collector 27;
the adopted bauxite contains Al according to the mass percentage2O3 50.96％，TFe 18.93％，SiO22.67%, the method is:
crushing bauxite until the grain diameter is less than or equal to 15mm, then grinding until the part with the grain diameter of-0.074 mm accounts for 85 percent of the total mass, and obtaining fine ore;
the powder ore is conveyed to a feeding bin 2 through a feeding belt 1, the powder ore in the feeding bin 2 is continuously conveyed to a screw feeder 4 through a weightless feeder 3, and is continuously conveyed into a Venturi dryer 5 through the screw feeder 4;
starting the induced draft fan 32 to generate negative pressure in the dust collector 27, the first cyclone preheater 6, the second cyclone preheater 7, the venturi dryer 5, the thermal separation cyclone 10 and the pre-oxidation suspension roasting furnace 8; introducing combustion flue gas into the Venturi dryer 5, mixing the combustion flue gas with the fine ore, and removing adsorption water of the fine ore; controlling the material temperature at the discharge port of the Venturi dryer 5 to be 130 ℃;
the combustion flue gas and the fine ore without adsorption water enter a first cyclone preheater 6 from a Venturi dryer 5, the solid material after cyclone separation enters a second cyclone preheater 7, the solid material after secondary cyclone separation is preheated to 450 ℃ in the second cyclone preheater 7, and then enters a pre-oxidation suspension roaster 8;
after the fine ore enters the first cyclone preheater 6, the separated gas is discharged from the first cyclone preheater 6 and then enters the dust collector 28, and the gas after dust removal enters the induced draft fan 31; the gas exhausted from the induced draft fan 31 is exhausted through a chimney 32;
after dust generated by dust removal is discharged, the dust enters the second pneumatic conveying pump 21-2 through an air chute 29; blowing air into the second pneumatic conveying pump 21-2 through the roots blower 30, and conveying dust in the second pneumatic conveying pump 21-2 to the thermal separation cyclone cylinder 10; the gas separated by the thermal separation cyclone 10 in the cyclone separation process is introduced into the second cyclone preheater 7; the gas separated by the second cyclone preheater 7 in the cyclone separation process is introduced into the venturi dryer 5 through a pipeline, a second auxiliary burner 9-3 arranged on the pipeline simultaneously introduces combustion flue gas into the venturi dryer 5, and a third ash bucket valve 33-3 arranged on the pipeline is used for cleaning ash;
the burner arranged at the bottom of the pre-oxidation suspension roasting furnace 8 consists of a main burner 9-1 and a first auxiliary burner 9-2, and gas is respectively introduced through a gas pipeline 34-1;
starting a burner to burn the introduced gas to generate high-temperature flue gas, introducing the high-temperature flue gas into the pre-oxidation suspension roasting furnace 8, introducing air into the pre-oxidation suspension roasting furnace 8 through an air inlet, keeping the solid materials in the pre-oxidation suspension roasting furnace 8 in a suspension state under the action of air flow and negative pressure, and heating the solid materials to 700 ℃ for pre-oxidation roasting to remove adsorbed water; all materials after the pre-oxidation roasting are discharged from the upper part of the pre-oxidation suspension roasting furnace 8 along with air flow and enter a thermal separation cyclone 10; the solid material after cyclone separation is taken as oxidation slag powder, discharged from the thermal separation cyclone 10 and enters the suspension reduction roasting furnace 12 through the first flow seal valve 11; the retention time of the fine ore in the pre-oxidation suspension roasting furnace is 15 min;
a gas mixing tank communicated with a plurality of gas inlets of the suspension reduction roasting furnace 12 is respectively filled with gas and nitrogen through a gas pipeline 34-1 and a nitrogen pipeline 34-2;
introducing gas and nitrogen from the bottom of the suspension reduction roasting furnace 12, keeping the oxidized slag powder in a suspension state under the action of air flow and negative pressure, and carrying out reduction roasting at 600 ℃ to obtain weak-magnetic Fe2O3By reduction to ferromagnetic Fe3O4The solid material after reduction roasting is taken as reduction slag powder and is discharged from the side part of the suspension reduction roasting furnace 12; the input of the coal gas is according to H in the coal gas2CO and Fe in fine ore2O31.1 times of the amount theoretically required for complete reaction; the volume concentration of the coal gas in the reduction roasting furnace is 40 percent; the retention time of the oxidized slag powder in the reduction roasting furnace is 60 min;
the suspension reduction roasting furnace 12 generates gas in the reduction roasting process and the gas is introduced into the cyclone separator 13 from a gas outlet at the top; the dust separated by the cyclone separator 13 returns to the suspension reduction roasting furnace 12 through a second feeding hole at the top of the suspension reduction roasting furnace 12, and the separated gas is introduced into a feeding hole at the lower part of the pre-oxidation suspension roasting furnace 8;
reducing slag powder discharged from the suspension reduction roasting furnace 12 enters a second flow seal valve 14, then sequentially passes through a first cooling cyclone 15, a second cooling cyclone 16 and a third cooling cyclone 17, is cooled to be less than or equal to 100 ℃, and then enters a collection bin 18;
the gas separated by the third cooling cyclone 17 in the cyclone separation process is introduced into the feed inlet of the second cooling cyclone 16; the gas separated by the second cooling cyclone 16 in the cyclone separation process is introduced into the feed inlet of the first cooling cyclone 15 through a pipeline, and a first ash bucket valve 33-1 arranged on the pipeline is used for cleaning ash; the gas separated by the first cooling cyclone 15 in the cyclone separation process is introduced into the gas inlet at the bottom of the pre-oxidation suspension roasting furnace 8 through a pipeline, and a second ash bucket valve 33-2 arranged on the pipeline is used for removing ash; meanwhile, air is introduced through an air pipeline 34-3 connected with the air inlet of the third cooling cyclone 17;
the reduced slag powder in the collection bin 18 is put into a sealed scraper conveyor 19 and then conveyed to a dry ore mill 20, the part of the reduced slag powder with the particle size of-0.074 mm accounts for 70 percent of the total mass after dry ore milling, and then the reduced slag powder is put into a first pneumatic conveying pump 21-1; blowing air into the first pneumatic conveying pump 21-1 through the Roots blower 30, and conveying the materials in the first pneumatic conveying pump 21-1 to the wind power powder concentrator 22; wind power classification is carried out through a wind power powder concentrator 22, and overflow obtained by wind power classification is secondary powder ore with the particle size of-0.045 mm accounting for 70% of the total mass; the settled sand after wind classification is conveyed to a bucket elevator 23 and is conveyed to a sealing scraper conveyor 19 through the bucket elevator 23;
conveying the secondary fine ore to a dust remover 24 for dust removal, and then conveying the secondary fine ore to a dry magnetic separator 25 for dry magnetic separation, wherein the magnetic field intensity of the dry magnetic separation is 1100Oe, the obtained nonmagnetic product is high-grade aluminum concentrate, and the magnetic product is iron-containing tailings; the high-grade aluminum concentrate contains 5.78 percent of TFe and Al according to the mass percentage2O377.14 percent; the recovery rate of alumina is 81.02%.
Example 2
The system structure is the same as that of embodiment 1;
the adopted bauxite contains Al according to the mass percentage2O3 39.75％，TFe 21.86％，SiO22.25%, the method is the same as example 1, except that:
(1) the part which is ground to the particle size of-0.074 mm accounts for 90 percent of the total mass;
(2) controlling the material temperature at the discharge port of the Venturi dryer 5 to be 140 ℃; preheated to 500 ℃ in the second cyclone preheater 7;
(3) the pre-oxidation roasting temperature is 720 ℃; the retention time of the fine ore in the pre-oxidation suspension roasting furnace is 8 min;
(4) the reduction roasting temperature is 630 ℃; the input of the coal gas is according to H in the coal gas2CO and Fe in fine ore2O31.2 times of the amount required by the complete reaction theory is introduced; the volume concentration of the coal gas in the reduction roasting furnace is 30 percent; the retention time of the oxidized slag powder in the reduction roasting furnace is 40 min;
(5) the part of dry grinding ore with the particle size of-0.074 mm accounts for 75 percent of the total mass; the overflow obtained by wind classification is secondary fine ore with the grain diameter of-0.045 mm accounting for 75% of the total mass;
(6) the magnetic field intensity of the dry magnetic separation is 1200Oe, the high-grade aluminum concentrate contains 5.23 percent of TFe and Al according to the mass percentage2O368.58 percent; the recovery rate of alumina is 82.39%.
Example 3
The system structure is the same as that of embodiment 1;
the adopted bauxite contains Al according to the mass percentage2O3 47.83％，TFe 30.65％，SiO24.53%, the method is the same as example 1, except that:
(1) the part which is ground to the particle size of-0.074 mm accounts for 95 percent of the total mass;
(2) controlling the material temperature at the discharge port of the Venturi dryer 5 to be 150 ℃; preheated to 600 ℃ in the second cyclone preheater 7;
(3) the pre-oxidation roasting temperature is 750 ℃; the retention time of the fine ore in the pre-oxidation suspension roasting furnace is 2 min;
(4) the reduction roasting temperature is 650 ℃; the input of the coal gas is according to H in the coal gas2CO and Fe in fine ore2O31.3 times of the amount theoretically required for complete reaction; the volume concentration of the coal gas in the reduction roasting furnace is 25 percent; the retention time of the oxidized slag powder in the reduction roasting furnace is 20 min;
(5) the part of dry grinding ore with the particle size of-0.074 mm accounts for 80 percent of the total mass; the overflow obtained by wind classification is secondary fine ore with the grain diameter of-0.045 mm accounting for 80 percent of the total mass;
(6) the magnetic field intensity of the dry magnetic separation is 1300Oe, the high-grade aluminum concentrate contains 3.12 percent of TFe and Al according to the mass percentage2O373.26 percent; the recovery rate of alumina is 84.55%.
Claims (7)
1. A bauxite suspension roasting dehydration dry method iron removal system is characterized by comprising a feeding bin, a Venturi dryer, a first cyclone preheater, a second cyclone preheater, a pre-oxidation suspension roasting furnace, a thermal separation cyclone, a suspension reduction roasting furnace, a collecting bin, an ore grinding machine, a first pneumatic conveying pump, a dust collector and a dry magnetic separator; the outlet of the feeding bin is opposite to the screw feeder, and the screw feeder is opposite to the feeding port of the Venturi dryer; the discharge port of the Venturi dryer is communicated with the feed port of the first cyclone preheater, the discharge port of the first cyclone preheater is communicated with the feed port of the second cyclone preheater, the discharge port of the second cyclone preheater is communicated with the feed port below the pre-oxidation suspension roasting furnace, the bottom of the pre-oxidation suspension roasting furnace is provided with a burner and a gas inlet, the upper part of the pre-oxidation suspension roasting furnace is communicated with the feed port of the thermal separation cyclone cylinder through a pipeline, the discharge port of the thermal separation cyclone cylinder is communicated with the inlet of the first flow seal valve, the outlet of the first flow seal valve is communicated with the feed port at the top of the suspension reduction roasting furnace, the bottom of the suspension reduction roasting furnace is provided with a plurality of gas inlets, the plurality of gas inlets are communicated with a gas mixing tank, and the gas mixing tank is simultaneously communicated with a gas source and a nitrogen source; a discharge hole in the side part of the suspension reduction roasting furnace is communicated with an inlet of a second flow seal valve, an outlet of the second flow seal valve is communicated with a feed hole of a first cooling cyclone, a discharge hole of the first cooling cyclone is communicated with a feed hole of a second cooling cyclone, a discharge hole of the second cooling cyclone is communicated with a feed hole of a third cooling cyclone, and a discharge hole of the third cooling cyclone is communicated with an inlet of a collection bin; the outlet of the collecting bin is matched with the inlet of the ore mill, and the outlet of the ore mill is opposite to the feeding hole of the first pneumatic conveying pump; the discharge hole of the first pneumatic conveying pump is communicated with the feed inlet of the wind power powder concentrator, and the air inlet of the first pneumatic conveying pump is communicated with the roots blower; the overflow port of the wind power powder concentrator is communicated with the feed port of the dust remover; the discharge hole of the dust remover is opposite to the dry magnetic separator; the air outlet of the first cyclone preheater is communicated with the air inlet of the dust collector, and the air outlet of the dust collector is communicated with the induced draft fan; the air outlet of the third cooling cyclone is communicated with the feed inlet of the second cooling cyclone; the air outlet of the second cooling cyclone is communicated with the feed inlet of the first cooling cyclone through a pipeline, and a first ash bucket valve is arranged on the pipeline; the air outlet of the first cooling cyclone is communicated with the air inlet at the bottom of the pre-oxidation suspension roasting furnace through a pipeline, and a second ash hopper valve is arranged on the pipeline; an air inlet of the third cooling cyclone is provided with an air pipeline for introducing air.
2. The system of claim 1, wherein a weight loss feeder is disposed between the feeding bin and the screw feeder, and the weight loss feeder is respectively opposite to the outlet of the feeding bin and the feeding end of the screw feeder.
3. The system for removing iron from bauxite by the dry method through suspension roasting and dehydration process according to claim 1, wherein a discharge port of the dust collector is opposite to an air chute, a discharge port of the air chute is opposite to a feed port of a second pneumatic conveying pump, an air outlet of the second pneumatic conveying pump is communicated with a feed port of a thermal separation cyclone, and an air inlet of the second pneumatic conveying pump is communicated with a roots blower; the air outlet of the thermal separation cyclone is communicated with the feed inlet of the second cyclone preheater; the gas outlet of the second cyclone preheater is communicated with the gas inlet at the bottom of the Venturi dryer through a pipeline, a second auxiliary burner and a third ash bucket valve are arranged on the pipeline, and the second auxiliary burner is communicated with a gas source.
4. The system of claim 1, wherein the top of the suspension reduction roaster is provided with an exhaust port communicated with a feed inlet at the bottom of the cyclone separator, an air outlet of the cyclone separator is communicated with a feed inlet at the lower part of the pre-oxidation suspension roaster, and a discharge outlet of the cyclone separator is communicated with a second feed inlet at the top of the suspension reduction roaster.
5. The system of claim 1, wherein the burner disposed at the bottom of the pre-oxidation suspension roaster comprises a main burner and a first auxiliary burner, and the main burner and the first auxiliary burner are respectively communicated with a gas source.
6. The system of claim 1, wherein a sealing scraper conveyor is arranged between the collection bin and the ore mill, and the sealing scraper conveyor is respectively matched with the outlet of the collection bin and the inlet of the ore mill; the discharge port of the wind power powder concentrator is matched with the inlet of the bucket elevator, and the outlet of the bucket elevator is matched with the sealing scraper conveyor.
7. The use method of the bauxite suspension roasting dehydration dry method iron removal system in the claim 1 is characterized by comprising the following steps:
(1) crushing bauxite until the grain diameter is less than or equal to 15mm, then grinding until the part with the grain diameter of-0.074 mm accounts for more than or equal to 85 percent of the total mass, and obtaining fine ore; the bauxite contains Al according to the mass percentage2O3 30~55%，TFe 10~35%，SiO2 2~10%；
(2) Placing the fine ore in a feeding bin, then conveying the fine ore to a screw feeder, and continuously conveying the fine ore into a Venturi dryer through the screw feeder;
(3) starting a draught fan to generate negative pressure in the dust collector, the first cyclone preheater, the second cyclone preheater, the venturi dryer, the thermal separation cyclone and the pre-oxidation suspension roasting furnace; introducing combustion flue gas into the Venturi dryer, mixing the combustion flue gas with the fine ore, and removing adsorption water of the fine ore; controlling the material temperature of a discharge port of the Venturi dryer to be 130-150 ℃;
(4) the method comprises the following steps that (1) burning flue gas and fine ore with adsorbed water removed enter a first cyclone preheater from a Venturi dryer, solid materials subjected to cyclone separation enter a second cyclone preheater, the solid materials subjected to secondary cyclone separation are preheated to 450-600 ℃ in the second cyclone preheater, and then enter a pre-oxidation suspension roasting furnace;
(5) starting a burner to burn introduced gas to generate high-temperature flue gas, introducing the high-temperature flue gas into a pre-oxidation suspension roasting furnace, introducing air into the pre-oxidation suspension roasting furnace through an air inlet, keeping solid materials in the pre-oxidation suspension roasting furnace in a suspension state under the action of air flow and negative pressure, and heating the solid materials to 700-750 ℃ for pre-oxidation roasting to remove adsorbed water; discharging all the materials subjected to pre-oxidation roasting from the upper part of the pre-oxidation suspension roasting furnace along with air flow, and feeding the materials into a thermal separation cyclone cylinder; the solid material after cyclone separation is taken as oxidation slag powder, discharged from the thermal separation cyclone cylinder and enters the suspension reduction roasting furnace through the first flow seal valve;
(6) introducing gas and nitrogen from the bottom of the suspension reduction roasting furnace, keeping the oxidized slag powder in a suspension state under the action of air flow and negative pressure, and carrying out reduction roasting at 600-650 ℃ to obtain weak-magnetic Fe2O3By reduction to ferromagnetic Fe3O4The solid material after reduction roasting is taken as reduction slag powder and is discharged from the side part of the suspension reduction roasting furnace;
(7) reducing slag powder discharged from the suspension reduction roasting furnace enters a second flow seal valve, then sequentially passes through a first cooling cyclone cylinder, a second cooling cyclone cylinder and a third cooling cyclone cylinder, is cooled to be less than or equal to 100 ℃, and then enters a collection bin;
(8) conveying the reduced slag powder in the collection bin to a dry ore mill, performing dry ore milling until the part with the particle size of-0.074 mm accounts for more than or equal to 70% of the total mass, and then putting the reduced slag powder into a first pneumatic conveying pump; blowing air into the first pneumatic conveying pump through the Roots blower, and conveying the materials in the first pneumatic conveying pump to the wind power powder concentrator; wind power classification is carried out through a wind power powder concentrator, and overflow obtained by wind power classification is secondary powder ore with the grain diameter of-0.045 mm accounting for more than or equal to 70% of the total mass;
(9) and conveying the secondary fine ore to a dust remover for dust removal, and then conveying the secondary fine ore to a dry magnetic separator for dry magnetic separation to obtain a non-magnetic product which is high-grade aluminum concentrate and a magnetic product which is iron-containing tailings.
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| US3297429A (en) * | 1963-10-28 | 1967-01-10 | Allis Chalmers Mfg Co | Controlled atomsphere magetic roasting of iron ore |
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| CN101618887B (en) * | 2009-07-31 | 2011-05-18 | 刘鹤群 | Aluminium hydroxide suspension roasting furnace and layout in production plant |
| CN101921137A (en) * | 2010-05-27 | 2010-12-22 | 中国科学院地球化学研究所 | Method for selecting and preparing raw materials of 550kN-grade suspension-type porcelain insulator glaze |
| CN101870492B (en) * | 2010-07-14 | 2012-01-11 | 河南东大泰隆冶金科技有限公司 | New technology for gas suspension calcination of aluminium hydroxide |
| CN203451234U (en) * | 2013-08-30 | 2014-02-26 | 鞠复勇 | Aluminum oxide gas state suspension roaster |
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| CN104692435A (en) * | 2015-03-31 | 2015-06-10 | 沈阳鑫博工业技术股份有限公司 | Suspension roasting device and technology for producing multiform aluminum oxide |
| CN105000582B (en) * | 2015-08-28 | 2016-08-24 | 沈阳鑫博工业技术股份有限公司 | A kind of system and method for roasting aluminium hydroxide recycle-water steam |
| CN107460307B (en) * | 2017-07-19 | 2019-02-05 | 东北大学 | A kind of high-iron bauxite suspension roasting utilization system and method |
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