Comprehensive recovery system for suspended ore phase transformation of polymetallic ore resources and its use method

Abstract

The present invention provides a comprehensive recovery system for suspended mineral phase transformation of polymetallic ore resources and a method for using the system. The system comprises a feed bin, a dryer, a first cyclone separator, a second cyclone separator, a suspended oxidation decomposer, a third cyclone separator, a first fluidized sealing valve, a fluidized mineral phase converter, a fourth cyclone separator, a second fluidized sealing valve, a first cyclone cooler, a second cyclone cooler, a ball mill, a weak magnetic separator, a rare earth flotation machine, a pickling agitator, a water washing tank, and a niobium flotation machine. The present invention adopts a suspended mineral phase transformation technology to achieve directional transformation of useful mineral components, expand the selectivity differences between minerals, and achieve centralized recovery of different mineral components in the ore, so as to improve the comprehensive recovery efficiency of complex polymetallic ore resources.

Description

Technical Field

[0001] The present invention relates to the field of mineral processing and smelting, and in particular to a comprehensive recovery system for suspended ore phase transformation of polymetallic ore resources and a method for using the system. Background Art

[0002] The Bayan Obo deposit is a rare super-large multimetallic co-existing deposit in the world, with huge reserves of iron, rare earth, niobium and other resources. The development and utilization of mineral resources in the region has made great contributions to my country's industrial development. With the continuous deepening of resource mining, the surface rich ore resources are gradually decreasing. In recent years, the country has attached more and more importance to the comprehensive utilization efficiency of resources. Therefore, the development and recovery of medium-poor ore resources and secondary resources in the Bayan Obo area has become increasingly important.

[0003] Due to the particularity of the ore resources in the Bayan Obo area, the traditional "weak magnetic-strong magnetic-flotation" process for recovering iron and rare earths can meet industrial production indicators, but it has shortcomings in the recovery of other associated minerals, especially in the recovery of niobium resources. As the largest niobium ore resource base in my country, the niobium resources in the Bayan Obo mining area account for 95% of my country's total reserves, but the ores in the area also have the characteristics of low niobium grade, fine embedded particle size, and high degree of niobium dispersion, resulting in the niobium resources have not been effectively utilized so far. Unutilized mineral resources flow into tailings, causing serious waste of resources. Therefore, it is particularly important to develop an effective conversion and recovery system for processing complex multi-metallic ore resources to meet the comprehensive utilization needs of mineral resources in Bayan Obo and similar areas. Summary of the invention

[0004] The system and method for using the suspended mineral phase transformation comprehensive recovery of polymetallic ore resources of the present invention are intended to overcome the defects of the prior art. In view of the difficulties of similar beneficiation properties of medium-lean ores and secondary resources in mines, a variety of co-existing minerals and fine distribution are encountered. The suspended mineral phase transformation technology is used to achieve directional transformation of useful mineral components, expand the selectivity differences between minerals, and realize centralized recovery of different mineral components in the ore, so as to improve the comprehensive recovery efficiency of complex polymetallic ore resources.

[0005] The technical solution adopted by the present invention to solve its technical problems is: a comprehensive recovery system for suspended mineral phase transformation of multi-metallic ore resources, including a feeding bin, the discharge port of the feeding bin is connected to the feed port of a dryer, the discharge port of the dryer is communicated with the feed port of a first cyclone separator, the discharge port of the first cyclone separator is communicated with the feed port of a second cyclone separator, the discharge port of the second cyclone separator is communicated with the feed port of a suspended oxidation decomposer, the discharge port of the suspended oxidation decomposer is communicated with a third cyclone separator through a pipeline, the discharge port of the third cyclone separator is communicated with the feed port of a fluidized mineral phase converter through a first fluidized sealing valve, the discharge port of the fluidized mineral phase converter is communicated with the feed port of a first cyclone cooler through a second fluidized sealing valve, the discharge port of the first cyclone cooler is communicated with the feed port of a second cyclone cooler, the material after cooling by the second cyclone cooler enters a collecting bin, and the material in the collecting bin The material is transported to the ball mill, the discharge port of the ball mill is connected with the feed port of the spiral classifier, the overflow port of the spiral classifier is connected with the feed port of the weak magnetic separator through a pipeline, the concentrate discharge port of the weak magnetic separator is connected with the iron concentrate collecting bin through a pipeline, the tailings discharge port of the weak magnetic separator is connected with the first stirring barrel through a pipeline, the first stirring barrel is connected with the rare earth flotation machine through a pipeline, the foam product of the rare earth flotation machine is sent to the rare earth concentrate collecting bin through a pipeline, the bottom discharge port of the rare earth flotation machine is connected with the pickling mixer through a pipeline, the pickling mixer discharge port is connected with the washing tank, the washing tank discharge port is connected with the concentrator, the concentrator discharge port is connected with the second stirring barrel through a pipeline, the second stirring barrel discharge port is connected with the niobium flotation machine through a pipeline, the foam product of the niobium flotation machine is passed into the niobium concentrate collecting bin through a pipeline, and the bottom discharge port of the niobium flotation machine is connected with the tailings collecting bin through a pipeline.

[0006] Furthermore, the polymetallic ore is Bayan Obo iron ore tailings or rare earth flotation tailings or medium-lean oxidized stockpiled ore, wherein the TFe grade is 15-40wt%, the REO grade is 2-11wt%, and the Nb2O5 grade is 0.1-4wt%.

[0007] Furthermore, the top discharge port of the first cyclone separator is connected to an electrostatic precipitator through a pipeline, the electrostatic precipitator is connected to a tail gas absorption station, and the tail gas absorption station is connected to a chimney through an induced draft fan.

[0008] Furthermore, the discharge port of the electrostatic precipitator is connected to the feed port of the air lift pump, and the discharge port of the air lift pump is connected to the third cyclone separator through a pipeline; the air lift pump is also connected to the ash return fan.

[0009] Furthermore, the top discharge port of the second cyclone cooler is connected to the first cyclone cooler through a pipeline, the top discharge port of the first cyclone cooler is connected to the third cyclone separator through a pipeline, the top discharge port of the third cyclone separator is connected to the second cyclone separator through a pipeline, and the top discharge port of the second cyclone separator is connected to the dryer through a pipeline.

[0010] Furthermore, a burner is provided at the bottom of the suspended oxidizer, and the burner is connected to a reducing gas source and an air source through a pipeline.

[0011] Furthermore, the dryer is connected to a drying heat generator through a pipeline, a first ash hopper is also provided on the pipeline, and a second ash hopper is provided on a discharge pipeline between the first cyclone cooler and the second cyclone cooler; the drying heat generator is connected to a reducing gas source.

[0012] Furthermore, the first fluidized sealing valve and the second fluidized sealing valve are both provided with air inlets at the bottom and are connected to a nitrogen gas source pipeline.

[0013] Furthermore, an air inlet is provided at the bottom of the fluidized mineral phase converter and is connected to the reducing gas source pipeline, and a ventilation port is provided at the top of the fluidized mineral phase converter and is connected to the fourth cyclone separator; the top discharge port of the fourth cyclone separator is connected to the suspended oxidation decomposer.

[0014] Furthermore, the flotation machine is provided with a pH online monitoring device, a temperature control device and a pulp concentration detection device.

[0015] Furthermore, the suspended oxidation decomposer, fluidized mineral phase converter and electrostatic precipitator are all equipped with temperature measuring devices and pressure sensing devices for monitoring the operating temperature and pressure.

[0016] The method for using the above-mentioned multi-metallic ore resource suspended ore phase conversion comprehensive recovery system comprises the following steps:

[0017] S1. Start the induced draft fan to generate negative pressure in the tail gas absorption station, the first cyclone separator of the electrostatic precipitator, the second cyclone separator, the suspended oxidation decomposer, and the third cyclone separator;

[0018] S2. Introduce combustion flue gas into the dryer to remove water and preheat the material. The material temperature at the dryer outlet is 150-200°C;

[0019] S3, the mineral powder in the feed bin is sent to the dryer, and after drying and dehydration, the mineral powder is sent to the first cyclone separator, and the bottom material after cyclone separation is sent to the suspended oxidation decomposer through the second cyclone separator;

[0020] S4, the flue gas is introduced through the air inlet at the bottom of the suspended oxidation decomposer, so that the material in the suspended oxidation decomposer is oxidized and decomposed and is in a suspended state, and the material temperature is controlled at 450-700°C, and the residence time is 1-10 minutes;

[0021] S5. The material after oxidation and decomposition enters the third cyclone separator. After cyclone separation, the material at the bottom enters the first fluidized sealing valve to isolate air and oxygen. Then the material is passed into the fluidized mineral phase converter. Reducing gas is passed into the fluidized mineral phase converter. The material is kept in a suspended state and converted under the action of the reducing gas. The material temperature is controlled at 400-600°C and the residence time is 20-90 minutes.

[0022] S6. After the material is converted, the reducing gas is isolated and discharged through the second fluidized sealing valve, and then cooled to below 200°C through heat exchange in the first cyclone cooler and the second cyclone cooler before being discharged into the collection bin;

[0023] S7, the materials in the collection bin are sent to the ball mill, the materials are ground in the ball mill and then discharged into the spiral classifier, the material particle size is controlled to be -0.038mm and the content is 85-95wt%, and then discharged into the weak magnetic separator for magnetic separation; the magnetic field strength is 500-2500Oe, and the magnetic iron concentrate and magnetic tailings are obtained;

[0024] S8, the magnetically separated iron concentrate is discharged into the iron concentrate collection bin, and the magnetically separated tailings are discharged into the first stirring barrel, where a flotation agent is added and the slurry is stirred and adjusted, and then the slurry is passed into the rare earth flotation machine for rare earth flotation;

[0025] S9, the rare earth flotation temperature is controlled at 30-80°C, the pulp concentration is controlled at 25-60wt%, the concentrate (foam product) is passed into the rare earth concentrate collection bin, and the rare earth flotation tailings (bottom material) is passed into the pickling mixer;

[0026] S10, the acid used for pickling of rare earth flotation tailings is sulfuric acid with a concentration of 5-12 mol / L and a solid-liquid ratio of 1:7-1:12. The stirring time is controlled to be 5-30 min. After the pickling is completed, the tailings are passed into a water washing tank. After washing in the water washing tank until the pH value reaches 5-7, the tailings are passed into a concentrator to concentrate the pulp to 20-40 wt%;

[0027] S11, the concentrated slurry is passed into a second stirring barrel, a flotation agent is added, and the slurry is stirred and slurried, and then discharged into a niobium flotation machine for niobium flotation; the flotation temperature is room temperature, and the slurry concentration is controlled at 20-40wt%;

[0028] S12. The niobium flotation concentrate (foam product) is passed into a niobium concentrate collecting bin, and the niobium flotation tailings (bottom material) is passed into a tailings collecting bin for storage.

[0029] Furthermore, after the material passes into the first cyclone separator, the separated dust is discharged into the electrostatic precipitator, and the flue gas after dust removal is passed into the exhaust gas absorption station for purification and then discharged from the chimney; the dust collected by the electrostatic precipitator is returned to the third cyclone separator through the pneumatic lift pump under the action of the ash return fan.

[0030] Furthermore, the flue gas generated during the operation of the suspended oxidation decomposer is returned to the dryer through a pipeline via the third cyclone separator and the second cyclone separator to realize waste heat utilization.

[0031] Furthermore, the flue gas separated by the second cyclone cooler is returned to the first cyclone cooler; the flue gas separated by the first cyclone cooler is returned to the third cyclone separator; the flue gas separated by the third cyclone separator is returned to the second cyclone separator; the flue gas separated by the second cyclone separator is returned to the dryer, so that the fine particles in the flue gas are returned to participate in the cycle for recovery, and the hot gas is used as an auxiliary heat source for the dryer.

[0032] Furthermore, the spiral classifier classifies the ground material and returns the sand to the ball mill for further grinding.

[0033] Furthermore, the reducing gas introduced into the fluidized mineral phase converter is one of the reducing gases such as H2, CO, methane, natural gas and coal gas (preferably H2), or a mixed reducing gas composed of several of them. If the mixed reducing gas contains H2, the volume ratio of H2 in the mixed reducing gas is not less than 55%.

[0034] Furthermore, the main reactions occurring in the suspended oxidation decomposer are:

[0035] Fe2O3·nH2O→α-Fe2O3+nH2O

[0036] 4FeCO3+O2→2α-Fe2O3+4CO2

[0037] 4Fe3O4+O2→6α-Fe2O3

[0038] CeCO3F→CeOF+CO2

[0039] Furthermore, the main reactions occurring in the fluidized mineral phase converter are:

[0040] 3Fe2O3+CO→2Fe3O4+CO2

[0041] 3Fe2O3+H2→2Fe3O4+H2O

[0042] 2CeOF+H2O→Ce2O3+2HF

[0043] Furthermore, the main reactions occurring in the first cyclone cooler and the second cyclone cooler are:

[0044] 4Fe3O4+O2→6γ-Fe2O3

[0045] 14 / 3Ce2O3+O2→4 / 3Ce7O 12

[0046] Furthermore, rare earth flotation adopts a "one coarse and three fine" closed-circuit direct flotation operation.

[0047] Furthermore, niobium flotation adopts a "one rough and three fine" closed-circuit direct flotation operation.

[0048] Furthermore, the depressant used in rare earth flotation is water glass, with a total dosage of 0.5-7 kg / t, the collector is a hydroxamic acid collector, with a total dosage of 0.2-8 kg / t, and the frother is 2# oil, with a total dosage of 0.01-1 kg / t; the depressant used in niobium flotation is a combined depressant, specifically a compound of sulfuric acid, water glass and CMC, with a total dosage of 0.5-4 kg / t, the activator used is lead nitrate, with a total dosage of 0.3-2.5 kg / t, and the collector used is C 5～9 Hydroxamic acid, total dosage is 0.8~8kg / t.

[0049] Compared with the prior art, the present invention has the following beneficial effects:

[0050] The system of the present invention utilizes the suspended mineral phase transformation technology to transform weakly magnetic iron minerals into strongly magnetic magnetite with stronger magnetism, which is beneficial to the separation of iron from rare earth and niobium components, and improves the comprehensive utilization efficiency of each component; compared with the traditional carbon-based magnetization roasting technology, the suspended mineral phase transformation can achieve low-temperature, low-carbon and high-efficiency transformation, better heat and mass transfer efficiency, lower required reaction time and reaction temperature, and less carbon emissions. In addition, the suspended mineral phase transformation can also avoid the influence caused by insufficient carbon combustion on the surface of mineral particles, reducing the flotation recovery effect; after the ore particles are treated with the suspended mineral phase transformation technology, cracks can be generated inside the particles, which is beneficial to fine grinding operations, can achieve better monomer dissociation and achieve energy saving and consumption reduction effects to a certain extent. BRIEF DESCRIPTION OF THE DRAWINGS

[0051] Figure 1 This is a schematic diagram of the structure of the comprehensive recovery system for the transformation of the suspended ore phase of polymetallic ore resources of the present invention;

[0052] Figure 2 It is a schematic structural diagram of a fluidized ore phase converter of the multi-metal ore resource suspended ore phase conversion comprehensive recovery system of the present invention;

[0053] Figure 3 It is a schematic diagram of the structure of the fluidized sealing valve of the comprehensive recovery system for the suspended ore phase transformation of multi-metallic ore resources of the present invention;

[0054] In the figure: 1. Feeding bin, 2. First feeding belt, 3. Venturi dryer, 4. First cyclone separator, 5. Second cyclone separator, 6. Suspended oxidation decomposer, 7. Burner, 8. Third cyclone separator, 9. First fluidized sealing valve, 10. Fluidized mineral phase converter, 11. Fourth cyclone separator, 12. Second fluidized sealing valve, 13. First cyclone cooler, 14. Second cyclone cooler, 15. Collection bin, 16. Second feeding belt, 17. Ball mill, 18. Spiral classifier, 19. Weak magnetic separator, 20. Iron concentrate collection bin, 21. First mixing barrel, 22. Rare earth flotation machine, 23. Rare earth concentrate collection bin, 24. Pickling mixer, 25. Washing tank, 26. Concentrator, 27. Second mixing barrel, 28. Niobium flotation machine, 29. Niobium concentrate collection bin, 30. Tailings collection bin, 31. Electrostatic precipitator, 32. Tail gas absorption station, 33. Induced draft fan, 34. Chimney, 35. Air lift pump, 36. Ash return fan, 37. Second ash hopper, 38. First ash hopper, 39. Dry heat generator;

[0055] 10-1. Mineral phase conversion feed port, 10-2. Feed port stop valve, 10-3. Mineral phase conversion discharge port, 10-4. Reduction chamber, 10-5. Mineral phase conversion air distribution plate, 10-6. Baffle, 10-7. Separator, 10-8. Mineral phase conversion air inlet, 10-9. Air inlet stop valve;

[0056] 12-1. Feed inlet, 12-2. Discharge outlet, 12-3. Top fluidization sealing baffle, 12-4. Fluidization chamber, 12-5. Fluidization sealing air distribution plate, 12-6. Bottom fluidization sealing baffle, 12-7. Nitrogen stop valve, 12-8. Nitrogen inlet. DETAILED DESCRIPTION

[0057] The present invention is further described below in conjunction with the accompanying drawings and examples. The equipment, reagents and materials described in the following examples, unless otherwise specified, can all be obtained from commercial channels; the test methods described, unless otherwise specified, are all conventional methods.

[0058] Example 1

[0059] The structure of the comprehensive recovery system for the transformation of suspended mineral phase of polymetallic ore resources is as follows: Figure 1 As shown, it includes a feed bin 1, a venturi dryer 3, a first cyclone separator 4, a second cyclone separator 5, a suspended oxidation decomposer 6, a third cyclone separator 8, a first fluidized sealing valve 9, a fluidized mineral phase converter 10, a fourth cyclone separator 11, a second fluidized sealing valve 12, a first cyclone cooler 13, a second cyclone cooler 14, a ball mill 17, a weak magnetic separator 19, a rare earth flotation machine 22, a pickling mixer 24, a water washing tank 25, and a niobium flotation machine 28;

[0060] The discharge port of the feeding bin 1 is opposite to the first feeding belt 2, the discharge end of the first feeding belt 2 is opposite to the feed port of the venturi dryer 3, the discharge port of the venturi dryer 3 is connected to the feed port of the first cyclone separator 4, the discharge port of the first cyclone separator 4 is connected to the feed port of the second cyclone separator 5, the discharge port of the second cyclone separator 5 is connected to the feed port of the suspended oxidation decomposer 6, the discharge port of the suspended oxidation decomposer 6 is connected to the third cyclone separator 8 through a pipeline, and the discharge port of the third cyclone separator 8 is connected to the first fluidized bed The feed port of the sealing valve 9 is opposite to each other, the discharge port of the first fluidized sealing valve 9 is matched with the feed port of the fluidized mineral phase converter 10, the discharge port of the fluidized mineral phase converter 10 is matched with the feed port of the second fluidized sealing valve 12, the discharge port of the second fluidized sealing valve 12 is connected with the feed port of the first cyclone cooler 13 through a pipeline, the discharge port of the first cyclone cooler 13 is connected with the feed port of the second cyclone cooler 14, the discharge port of the second cyclone cooler 14 is opposite to the collecting bin 15, and the discharge port of the collecting bin 15 is opposite to the second feeding belt 16 The discharge end of the second feeding belt 16 is opposite to the ball mill 17, the discharge port of the ball mill 17 is connected to the feed port of the spiral classifier 18, the overflow port of the spiral classifier 18 is connected to the feed port of the weak magnetic separator 19 through a pipeline, the concentrate discharge port of the weak magnetic separator 19 is connected to the iron concentrate collection bin 20 through a pipeline, the tailings discharge port of the weak magnetic separator 19 is connected to the first stirring barrel 21 through a pipeline, the first stirring barrel 21 is connected to the rare earth flotation machine 22 through a pipeline, and the foam product of the rare earth flotation machine 22 is fed into the rare earth concentrate through a pipeline The collecting bin 23, the bottom discharge port of the rare earth flotation machine 22 is connected with the pickling mixer 24 through a pipeline, the discharge port of the pickling mixer 24 is connected with the water washing tank 25, the discharge port of the water washing tank 25 is connected with the concentrator 26, the discharge port of the concentrator 26 is connected with the second stirring barrel 27 through a pipeline, the discharge port of the second stirring barrel 27 is connected with the niobium flotation machine 28 through a pipeline, the foam product of the niobium flotation machine 28 is passed into the niobium concentrate collecting bin 29 through a pipeline, and the bottom discharge port of the niobium flotation machine 28 is connected with the tailings collecting bin 30 through a pipeline.

[0061] Among them, the top discharge port of the first cyclone separator 4 is connected to the electrostatic precipitator 31 through a pipeline, the electrostatic precipitator 31 is connected to the exhaust gas absorption station 32, the exhaust gas absorption station 32 and the induced draft fan 33 cooperate, and the induced draft fan 33 is connected to the chimney 34 through a pipeline; the discharge port of the electrostatic precipitator 31 is connected to the feed port of the air lift pump 35, and the discharge port of the air lift pump 35 is connected to the third cyclone separator 8 through a pipeline, and the air lift pump 35 is also connected to the ash return fan 36.

[0062] The top discharge port of the second cyclone cooler 14 is connected to the first cyclone cooler 13 through a pipeline, the top discharge port of the first cyclone cooler 13 is connected to the third cyclone separator 8 through a pipeline, the top discharge port of the third cyclone separator 8 is connected to the second cyclone separator 5 through a pipeline, and the top discharge port of the second cyclone separator 5 is connected to the venturi dryer 3 through a pipeline. The flue gas separated by the second cyclone cooler 14 returns to the first cyclone cooler 13; the flue gas separated by the first cyclone cooler 13 returns to the third cyclone separator 8; the flue gas separated by the third cyclone separator 8 returns to the second cyclone separator 5; the flue gas separated by the second cyclone separator 5 returns to the dryer 3. The fine-grained materials in the flue gas are returned to participate in the cycle for recovery, and the hot gas is used as an auxiliary heat source for the dryer.

[0063] Wherein, a burner 7 is provided at the bottom of the suspended oxidizer 6, and the burner 7 is connected to the H2 / CO gas source and the air gas source through a pipeline.

[0064] The venturi dryer 3 is connected to a drying heat generator 39 through a pipeline, and a first ash hopper 38 is also provided on the pipeline. The second ash hopper 37 is provided on the discharge pipeline between the first cyclone cooler 13 and the second cyclone cooler 14; the drying heat generator 39 is connected to the H2 / CO gas source.

[0065] The first fluidized sealing valve 9 and the second fluidized sealing valve 12 are both provided with air inlets at the bottom and are connected to the nitrogen gas source pipeline.

[0066] Among them, the fluidized mineral phase converter 10 is provided with an air inlet at the bottom and is connected to the reducing gas source pipeline, and the fluidized mineral phase converter 10 is provided with a ventilation port at the top and is connected to the fourth cyclone separator 11; the top discharge port of the fourth cyclone separator 11 is connected to the suspended oxidation decomposer 6.

[0067] Wherein, the flotation machine is equipped with a pH online monitoring device, a temperature control device and a pulp concentration detection device;

[0068] The suspended oxidation decomposer 6, the fluidized mineral phase converter 10 and the electrostatic precipitator 31 are all provided with a temperature measuring device and a pressure sensing device for monitoring the operating temperature and pressure.

[0069] The structure of the fluidized mineral phase converter is as follows: Figure 2 As shown, it includes a mineral phase conversion feed port 10-1, a feed port stop valve 10-2, a mineral phase conversion discharge port 10-3, a reduction chamber 10-4, a mineral phase conversion air distribution plate 10-5, a baffle 10-6, a partition plate 10-7, a mineral phase conversion air inlet 10-8, and an air inlet stop valve 10-9.

[0070] The reduction chamber 10-4 is provided with a mineral phase conversion feed port 10-1 and a mineral phase conversion discharge port 10-3, and the mineral phase conversion feed port 10-1 is provided with a feed port stop valve 10-2; the reduction chamber is provided with a plurality of baffles 10-6 staggered and vertically fixed at the top and bottom of the reduction chamber; a partition plate fixed at the bottom of the reduction chamber 10-4 and on the same vertical plane as the baffle plate arranged at the top of the reduction chamber 10-4 is also provided; the baffle plate 10-6 and the partition plate 10-7 are arranged at the same vertical plane as the baffle plate 10-6; Both side edges are fixed on the inner wall of the reduction chamber, and the gap between the baffle and the partition plate arranged at the top of the reduction chamber 10-4 and the gap between the baffle and the top of the reduction chamber arranged at the bottom of the reduction chamber 10-4 form a serpentine material channel connecting the mineral phase conversion feed port 10-1 and the mineral phase conversion discharge port 10-3; a mineral phase conversion air inlet 10-8 is provided at the bottom of the reduction chamber at the end of each vertical channel in the serpentine material channel, and an air inlet stop valve 10-9 is provided on the mineral phase conversion air inlet 10-8.

[0071] The top of the partition plate 10-7 is provided with a horizontally arranged mineral phase conversion air distribution plate 10-5 fixed on the inner wall of the reduction chamber, and the tops of all the partition plates 10-7 are on the same horizontal plane.

[0072] The mineral phase conversion feed port 10-1 is arranged at the top of the reduction chamber, and the mineral phase conversion discharge port 10-3 is arranged at the upper part of the side wall of the reduction chamber.

[0073] Wherein, the fluidized sealing valve structure is as follows Figure 3 As shown, it includes a feed port 12-1, a discharge port 12-2, a top fluidizing sealing baffle 12-3, a fluidizing chamber 12-4, a fluidizing sealing air distribution plate 12-5, a bottom fluidizing sealing baffle 12-6, a nitrogen shut-off valve 12-7, and a nitrogen inlet 12-8.

[0074] The fluidizing chamber 12-4 is provided with a feed inlet 12-1 and a discharge outlet 12-2. The fluidizing chamber 12-4 is provided with a top fluidizing sealing baffle 12-3 fixed at the top of the fluidizing chamber 12-4 and a bottom fluidizing sealing baffle 12-6 fixed at the bottom of the fluidizing chamber 12-4. The top fluidizing sealing baffle 12-3 and the bottom fluidizing sealing baffle 12-6 are located on the same vertical plane. The top of the bottom fluidizing sealing baffle 12-6 is provided with a horizontally arranged fluidizing sealing baffle fixed on the inner wall of the fluidizing chamber. Sealing air distribution plate 12-5; both sides of the top fluidizing sealing baffle 12-3 and the bottom fluidizing sealing baffle 12-6 are fixed on the inner wall of the reduction chamber, and the gap between the top fluidizing sealing baffle 12-3 and the bottom fluidizing sealing baffle 12-6 and the feed port 12-1 and the discharge port 12-2 form a U-shaped material channel; a nitrogen inlet 12-8 is provided at the bottom of the fluidizing chamber at the end of each vertical channel in the U-shaped material channel, and a nitrogen shut-off valve 12-7 is provided on the nitrogen inlet 12-8.

[0075] The feed port 12-1 is arranged at the top of the fluidizing chamber, and the discharge port 12-2 is arranged at the upper part of the side wall of the fluidizing chamber.

[0076] The raw ore is taken from the ore sample of the medium-poor oxide ore pile in the Bayan Obo area of ​​Inner Mongolia. After crushing and screening, the particle size of the ore sample is below 3-5mm. The TFe grade in the ore sample is 29wt%, the REO grade is 5.1wt%, and the Nb2O5 grade is 0.13wt%. The method of using the above system is carried out according to the following steps:

[0077] S1, start the induced draft fan 33 to generate negative pressure in the tail gas absorption station 32, the first cyclone separator 4 of the electrostatic precipitator 31, the second cyclone separator 5, the suspended oxidation decomposer 6, and the third cyclone separator 8;

[0078] S2, introducing combustion flue gas into the venturi dryer 3 to remove the adsorbed water of the mineral powder and preheat the material, and the material temperature at the discharge port is 150°C;

[0079] S3, the mineral powder in the feed bin 1 is fed into the venturi dryer 3 through the first feeding belt 2, and after drying and dehydration, the mineral powder is fed into the first cyclone separator 4, and the bottom material after cyclone separation is fed into the suspended oxidation decomposer 6 through the second cyclone separator 5;

[0080] S4, the burner 7 generates flue gas by burning the air and H2 / CO mixed gas, and the flue gas is introduced through the air inlet at the bottom of the suspended oxidation decomposer 6, so that the material in the suspended oxidation decomposer 6 is oxidized and decomposed and is in a suspended state, and the material temperature is controlled at 600°C and the residence time is 10 minutes;

[0081] S5. The material after oxidation and decomposition enters the third cyclone separator 8. After cyclone separation, the bottom material enters the first fluidized sealing valve 9 to isolate air and oxygen. Then the material is passed into the fluidized mineral phase converter 10. The mixed reducing gas is passed into the fluidized mineral phase converter 10. The material is kept in a suspended state and converted under the action of the mixed gas. The material temperature is controlled at 450°C and the residence time is 30 minutes. The mixed reducing gas refers to a mixed gas of H2 and CO, and the volume ratio H2:CO=2:1.

[0082] S6, after the material is converted, the reducing gas is isolated through the second fluidized sealing valve 12 and the conversion product is discharged. The conversion product is cooled to 150° C. through heat exchange in the first cyclone cooler 13 and the second cyclone cooler 14 and then discharged into the collection bin 15;

[0083] S7, the ore powder in the collecting bin 15 is fed into the ball mill 17 through the second feeding belt 16, the material is ground in the ball mill 17 and then discharged into the spiral classifier 18, the material particle size is controlled to be -0.038mm and the content is 90wt%, and then discharged into the weak magnetic separator 19 for magnetic separation; the magnetic field strength is 1800Oe, and the magnetic iron concentrate and magnetic tailings with TFe 59wt% and recovery rate 82% are obtained respectively;

[0084] S8, the magnetically separated iron concentrate is discharged into the iron concentrate collection bin, and the magnetically separated tailings are discharged into the first stirring barrel 21, where a flotation agent is added and the slurry is stirred and slurried, and then passed into the rare earth flotation machine for rare earth flotation;

[0085] S9. Rare earth flotation adopts the "one rough and three fine" positive flotation process. The flotation temperature is controlled at 60℃, the pulp concentration is controlled at 50wt%, the inhibitor used in the roughing of rare earth flotation is water glass, the dosage is 2kg / t, the collector is a hydroxamic acid collector, the dosage is 4kg / t, and the frother is 2# oil, the dosage is 0.08kg / t; the dosing steps of the fine selection are the same as the roughing selection, and the dosage of the reagent is 1kg / t of water glass for the fine selection, 1.5kg / t of the hydroxamic acid collector, and 1.5kg / t of the frother. kg / t, 2# oil 0.02kg / t, selected II water glass 0.7kg / t, hydroxamic acid collector 0.5kg / t, selected III water glass 0.25kg / t, hydroxamic acid collector 0.3kg / t; after flotation, a rare earth flotation concentrate with a REO grade of 59wt% and a recovery rate of 48% is obtained, the flotation concentrate (foam product) is introduced into a rare earth concentrate collecting bin 23, and the rare earth flotation tailings (bottom material) is introduced into a pickling mixer 24;

[0086] S10, the acid used for pickling of rare earth flotation tailings is sulfuric acid with a concentration of 7.5 mol / L, a solid-liquid ratio of 1:10, and a stirring time of 15 min. After pickling, the tailings are passed into a water washing tank 25, and after washing in the water washing tank 25 until the pH value reaches 5, the tailings are passed into a concentrator 26 to concentrate the pulp to 30 wt%;

[0087] S11, the concentrated pulp is introduced into the second stirring barrel 27, a flotation agent is added, and the pulp is stirred and slurried, and then discharged into the niobium flotation machine 28 for niobium flotation; the niobium flotation adopts the "one roughing and three fines" closed-circuit positive flotation process, the flotation temperature is room temperature, the pulp concentration is controlled at 30wt%, the inhibitor used in the roughing of niobium flotation is a combined inhibitor, specifically a compound of sulfuric acid, water glass and CMC, the dosage is 1.2kg / t, the activator used is lead nitrate, the dosage is 0.8kg / t, the collector used is C 5～9 Hydroxamic acid, dosage is 2kg / t; the dosing steps of the concentrate are the same as those of the rough concentrate, the dosage of the reagent is 0.8kg / t for the concentrate I combined inhibitor, 0.4kg / t for lead nitrate, and 0.6kg / t for C 5～9The dosage of hydroxamic acid is 1kg / t, the dosage of the selected II combined inhibitor is 0.2kg / t, C 5～9 The dosage of hydroxamic acid is 0.8kg / t, the dosage of the selected III combination inhibitor is 0.2kg / t, C 5～9 The dosage of hydroxamic acid is 0.2kg / t;

[0088] After flotation, a niobium concentrate with a Nb2O5 grade of 2.5wt% and a recovery rate of 40% can be obtained. The niobium flotation concentrate (foam product) is passed into a niobium concentrate collecting bin 29, and the niobium flotation tailings (bottom material) is passed into a tailings collecting bin 30 for storage.

[0089] Example 2

[0090] The raw ore was taken from the rare earth flotation tailings sample in the Bayan Obo area of ​​Inner Mongolia. The sample particle size was -0.074mm, accounting for 85wt%. The TFe grade in the ore sample was 26wt%, the REO grade was 4.2wt%, and the Nb2O5 grade was 0.24wt%.

[0091] The system structure is the same as that of Example 1;

[0092] The method is the same as in Example 1, except that:

[0093] S4, the material temperature in the suspended oxidation decomposer 6 is controlled at 550°C, and the residence time is 8 minutes;

[0094] S5, the material temperature in the fluidized phase converter 10 is controlled at 500°C, and the residence time is 50 min; the volume flow ratio of H2 and CO introduced into the fluidized phase converter 10 is 3:1;

[0095] S7, the mineral phase conversion product is ground to -0.038mm and the content is 95wt%; the magnetic field strength of weak magnetic separation is 2000Oe;

[0096] S9. In the rare earth flotation operation, the flotation temperature is 55°C, the roughing pulp concentration is 45wt%, the water glass dosage is 3kg / t, the hydroxamic acid collector dosage is 4kg / t, and the 2# oil dosage is 0.08kg / t; the selected I water glass is 2kg / t, the hydroxamic acid collector is 2kg / t, and the 2# oil is 0.02kg / t; the selected II water glass is 0.8kg / t, and the hydroxamic acid collector is 1kg / t; the selected III water glass is 0.5kg / t, and the hydroxamic acid collector is 0.5kg / t;

[0097] S10, in the pickling and stirring operation, the sulfuric acid concentration is 5 mol / L, the pickling solid-liquid ratio is 1:12, and the stirring time is 20 min;

[0098] S11. In niobium flotation operation, the concentration of roughing pulp is 30wt%, the dosage of roughing combined depressant is 2kg / t, the dosage of lead nitrate is 1kg / t, C5～9 The dosage of hydroxamic acid is 2kg / t; the dosage of the selected I combined inhibitor is 1kg / t, the dosage of lead nitrate is 0.5kg / t, and the dosage of C 5～9 The dosage of hydroxamic acid is 1kg / t, the dosage of the selected II combined inhibitor is 0.3kg / t, C 5～9 The dosage of hydroxamic acid is 0.5kg / t, the dosage of the selected III combination inhibitor is 0.2kg / t, C 5～9 The dosage of hydroxamic acid is 0.2kg / t;

[0099] The TFe grade in the obtained iron concentrate is 56wt%, and the TFe recovery rate is 73%; the REO grade in the rare earth flotation concentrate is 45wt%, and the REO recovery rate is 63%; the Nb2O5 grade in the niobium concentrate is 4.7wt%, and the recovery rate is 49%.

[0100] Example 3

[0101] The raw ore was taken from the iron tailings sample in the Bayan Obo area of ​​Inner Mongolia. The sample particle size was -0.074mm, accounting for 80wt%. The TFe grade in the ore sample was 30wt%, the REO grade was 10.2wt%, and the Nb2O5 grade was 0.16wt%.

[0102] The system structure is the same as that of Example 1;

[0103] The method is the same as in Example 1, except that:

[0104] S4, the material temperature in the suspended oxidation decomposer 6 is controlled at 600°C, and the residence time is 7 minutes;

[0105] S5, the material temperature in the fluidized phase converter 10 is controlled at 450°C, and the residence time is 40 minutes; the volume flow ratio of H2 and CO gas introduced into the fluidized phase converter 10 is 5:1;

[0106] S7, the mineral phase conversion product is ground to -0.038mm and the content is 92wt%; the magnetic field strength of weak magnetic separation is 2300Oe;

[0107] S9. In the rare earth flotation operation, the flotation temperature is 55°C, the roughing pulp concentration is 50wt%, the water glass dosage is 2.2kg / t, the hydroxamic acid collector dosage is 2.8kg / t, and the 2# oil dosage is 0.08kg / t; the selected I water glass is 1.1kg / t, the hydroxamic acid collector is 1.4kg / t, and the 2# oil is 0.02kg / t; the selected II water glass is 0.8kg / t, and the hydroxamic acid collector is 0.6kg / t; the selected III water glass is 0.3kg / t, and the hydroxamic acid collector is 0.3kg / t;

[0108] S10, in the pickling and stirring operation, the sulfuric acid concentration is 6 mol / L, the pickling solid-liquid ratio is 1:9, and the stirring time is 40 min;

[0109] S11. In niobium flotation operation, the concentration of roughing pulp is 30wt%, the dosage of roughing combined depressant is 2.2kg / t, the dosage of lead nitrate is 1.1kg / t, and C 5～9 The dosage of hydroxamic acid is 1.8kg / t; the dosage of the selected I combined inhibitor is 1kg / t, the dosage of lead nitrate is 0.5kg / t, and the dosage of C 5～9 The dosage of hydroxamic acid is 0.8kg / t, the dosage of the selected II combined inhibitor is 0.3kg / t, C 5～9 The dosage of hydroxamic acid is 0.5kg / t, the dosage of the selected III combination inhibitor is 0.2kg / t, C 5～9 The dosage of hydroxamic acid is 0.2kg / t;

[0110] The TFe grade in the obtained iron concentrate is 56wt%, and the TFe recovery rate is 67%; the REO grade in the rare earth flotation concentrate is 56wt%, and the REO recovery rate is 57%; the Nb2O5 grade in the niobium concentrate is 3.6wt%, and the recovery rate is 53%.

[0111] The above technical scheme explains the technical idea of ​​the present invention, which cannot be used to limit the protection scope of the present invention. Any changes and modifications made to the above technical scheme based on the technical essence of the present invention without departing from the content of the technical scheme of the present invention shall fall within the protection scope of the technical scheme of the present invention.

Claims

1. A comprehensive recovery system for the conversion of suspended mineral phases of polymetallic ore resources, characterized by: The invention comprises a feeding bin, wherein the discharge port of the feeding bin is connected to the feed port of the dryer, the discharge port of the dryer is communicated with the feed port of the first cyclone separator, the discharge port of the first cyclone separator is communicated with the feed port of the second cyclone separator, the discharge port of the second cyclone separator is communicated with the feed port of the suspended oxidation decomposer, the discharge port of the suspended oxidation decomposer is communicated with the third cyclone separator through a pipeline, the discharge port of the third cyclone separator is communicated with the feed port of the fluidized mineral phase converter through a first fluidized sealing valve, the discharge port of the fluidized mineral phase converter is communicated with the feed port of the first cyclone cooler through a second fluidized sealing valve, the discharge port of the first cyclone cooler is communicated with the feed port of the second cyclone cooler, the material cooled by the second cyclone cooler enters the collecting bin, the material in the collecting bin is transported to the ball mill, the discharge port of the ball mill is connected to the spiral separator The feed port of the spiral classifier is connected, the overflow port of the spiral classifier is connected with the feed port of the weak magnetic separator through a pipeline, the concentrate discharge port of the weak magnetic separator is connected with the iron concentrate collection bin through a pipeline, the tailings discharge port of the weak magnetic separator is connected with the first stirring barrel through a pipeline, the first stirring barrel is connected with the rare earth flotation machine through a pipeline, the foam product of the rare earth flotation machine is sent to the rare earth concentrate collection bin through a pipeline, the bottom discharge port of the rare earth flotation machine is connected with the pickling mixer through a pipeline, the pickling mixer discharge port is connected with the water washing tank, the water washing tank discharge port is connected with the concentrator, the concentrator discharge port is connected with the second stirring barrel through a pipeline, the second stirring barrel discharge port is connected with the niobium flotation machine through a pipeline, the foam product of the niobium flotation machine is passed into the niobium concentrate collection bin through a pipeline, and the bottom discharge port of the niobium flotation machine is connected with the tailings collection bin through a pipeline; The fluidized mineral phase converter comprises a mineral phase conversion feed port, a feed port stop valve, a mineral phase conversion discharge port, a reduction chamber, a mineral phase conversion air distribution plate, a baffle, a partition plate, a mineral phase conversion air inlet, and an air inlet stop valve. The reduction chamber is provided with a mineral phase conversion feed port and a mineral phase conversion discharge port. The mineral phase conversion feed port is provided with a feed port stop valve. The reduction chamber is provided with a plurality of baffles vertically fixed at the top and bottom of the reduction chamber in an interlaced manner. A baffle fixed at the reduction chamber is also provided below the baffle at the top of the reduction chamber. The baffle plate is located at the bottom of the chamber and is on the same vertical plane as the baffle plate. Both sides of the baffle plate and the baffle plate are fixed on the inner wall of the reduction chamber. The gap between the baffle plate and the baffle plate at the top of the reduction chamber and the gap between the baffle plate and the top of the reduction chamber form a serpentine material channel connecting the mineral phase conversion feed port and the mineral phase conversion discharge port. The mineral phase conversion air inlet is provided at the bottom of the reduction chamber at the end of each vertical channel in the serpentine material channel, and the mineral phase conversion air inlet is provided with an air inlet stop valve; Reducing gas is introduced into the fluidized mineral phase converter, and the material is kept in a suspended state and converted under the action of the reducing gas. The material temperature is controlled at 400-600° C. and the residence time is 20-90 minutes.

2. The multi-metal ore resource suspended mineral phase conversion comprehensive recovery system according to claim 1 is characterized by: The top discharge port of the first cyclone separator is connected to an electrostatic precipitator through a pipeline, the electrostatic precipitator is connected to a tail gas absorption station, and the tail gas absorption station is connected to a chimney through an induced draft fan.

3. The multi-metal ore resource suspended mineral phase conversion comprehensive recovery system according to claim 1 is characterized by: The discharge port of the electrostatic precipitator is connected with the feed port of the air lift pump, and the discharge port of the air lift pump is connected with the third cyclone separator through a pipeline; the air lift pump is also connected with the ash return fan.

4. The multi-metal ore resource suspended mineral phase conversion comprehensive recovery system according to claim 1 is characterized by: The top discharge port of the second cyclone cooler is connected to the first cyclone cooler through a pipeline, the top discharge port of the first cyclone cooler is connected to the third cyclone separator through a pipeline, the top discharge port of the third cyclone separator is connected to the second cyclone separator through a pipeline, and the top discharge port of the second cyclone separator is connected to the dryer through a pipeline.

5. The multi-metal ore resource suspended ore phase conversion comprehensive recovery system according to claim 1 is characterized by: The fluidized mineral phase converter is provided with an air inlet at the bottom and is connected to the reducing gas source pipeline, and the fluidized mineral phase converter is provided with a ventilation port at the top and is connected to the fourth cyclone separator; the top discharge port of the fourth cyclone separator is connected to the suspended oxidation decomposer.

6. The method for using the multi-metallic ore resource suspended ore phase conversion comprehensive recovery system according to claim 2, characterized in that: The following steps are involved: S1. Start the induced draft fan to generate negative pressure in the tail gas absorption station, the electrostatic precipitator, the first cyclone separator, the second cyclone separator, the suspended oxidation decomposer, and the third cyclone separator; S2. Introduce combustion flue gas into the dryer to remove water and preheat the material. The material temperature at the dryer outlet is 150~200℃; S3, the mineral powder in the feed bin is sent to the dryer, and after drying and dehydration, the mineral powder is sent to the first cyclone separator, and the bottom material after cyclone separation is sent to the suspended oxidation decomposer through the second cyclone separator; S4, the flue gas is introduced through the air inlet at the bottom of the suspended oxidation decomposer, so that the material in the suspended oxidation decomposer is oxidized and decomposed and is in a suspended state, and the material temperature is controlled at 450~700℃, and the residence time is 1~10min; S5. The material after oxidation and decomposition enters the third cyclone separator. After cyclone separation, the material at the bottom enters the first fluidized sealing valve to isolate air and oxygen. Then the material is passed into the fluidized mineral phase converter. Reducing gas is passed into the fluidized mineral phase converter. The material is kept in a suspended state and converted under the action of the reducing gas. The material temperature is controlled at 400-600°C and the residence time is 20-90 minutes. S6. After the material is converted, the reducing gas is isolated and discharged through the second fluidized sealing valve, and then cooled to below 200°C through heat exchange in the first cyclone cooler and the second cyclone cooler before being discharged into the collection bin; S7, the materials in the collection bin are sent to the ball mill, the materials are ground in the ball mill and then discharged into the spiral classifier, the material particle size is controlled to be -0.038mm and the content is 85~95wt%, and then discharged into the weak magnetic separator for magnetic separation; the magnetic field strength is 500~2500Oe, and magnetic iron concentrate and magnetic tailings are obtained; S8, the magnetically separated iron concentrate is discharged into the iron concentrate collection bin, and the magnetically separated tailings are discharged into the first stirring barrel, where a flotation agent is added and the slurry is stirred and adjusted, and then the slurry is passed into the rare earth flotation machine for rare earth flotation; S9, the rare earth flotation temperature is controlled at 30~80℃, the pulp concentration is controlled at 25~60wt%, the concentrate is passed into the rare earth concentrate collection bin, and the rare earth flotation tailings are passed into the pickling mixer; S10, rare earth flotation tailings acid washing acid is sulfuric acid, the concentration is 5-12 mol / L, the solid-liquid ratio is 1:7-1:12, the stirring time is controlled to be 5-30min, after the acid washing is completed, it is passed into the washing tank, washed in the washing tank until the pH value reaches 5-7, and then passed into the concentrator to concentrate the pulp to 20-40wt%; S11, the concentrated pulp is passed into the second stirring barrel, a flotation agent is added, and the pulp is stirred and slurried, and then discharged into the niobium flotation machine for niobium flotation; the flotation temperature is room temperature, and the pulp concentration is controlled at 20-40wt%; S12. The niobium flotation concentrate is passed into a niobium concentrate collecting bin, and the niobium flotation tailings are passed into a tailings collecting bin for storage.

7. The method for using the multi-metallic ore resource suspended ore phase conversion comprehensive recovery system according to claim 6 is characterized by: After the material passes into the first cyclone separator, the separated dust is discharged into the electrostatic precipitator, and the flue gas after dust removal is passed into the exhaust gas absorption station for purification and then discharged from the chimney; the dust collected by the electrostatic precipitator is returned to the third cyclone separator through the pneumatic lift pump under the action of the ash return fan; the flue gas generated during the operation of the suspended oxidation decomposer is returned to the dryer through the pipeline via the third cyclone separator and the second cyclone separator to realize the waste heat utilization.

8. The method for using the multi-metallic ore resource suspended ore phase conversion comprehensive recovery system according to claim 6, characterized in that: The reducing gas introduced into the fluidized mineral phase converter is one of H2, CO, methane, natural gas and coal gas, or a mixed reducing gas composed of several of them. If the mixed reducing gas contains H2, the volume ratio of H2 in the mixed reducing gas is not less than 55%.

9. The method for using the multi-metallic ore resource suspended ore phase conversion comprehensive recovery system according to claim 6, characterized in that: Rare earth flotation and niobium flotation adopt "one coarse and three fine" closed-circuit direct flotation operation.

10. The method for using the multi-metallic ore resource suspended ore phase conversion comprehensive recovery system according to claim 9, characterized in that: The depressant used in rare earth flotation is water glass, with a total dosage of 0.5~7kg / t, the collector is a hydroxamic acid collector, with a total dosage of 0.2~8kg / t, and the frother is 2# oil, with a total dosage of 0.01~1kg / t; the depressant used in niobium flotation is a combined depressant, specifically a compound of sulfuric acid, water glass and CMC, with a total dosage of 0.5~4kg / t, the activator used is lead nitrate, with a total dosage of 0.3~2.5kg / t, and the collector used is C 5~9 Hydroxamic acid, total dosage is 0.8~8kg / t.

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