Combined beneficiation method for mixed collophanite
Through the combination of photoelectric sorting and forward and reverse flotation, the problem of unstable flotation process of mixed rubber phosphate ore is solved, efficient and low-cost ore separation and recovery is achieved, and high-grade phosphorus concentrate is obtained, which is suitable for yellow phosphorus and wet phosphoric acid processes.
Patent Information
- Application Number
- CN202510721193.8
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- Filing Date
- 2025-05-30
- Publication Date
- 2025-08-01
AI Technical Summary
In the prior art, the flotation process of mixed rubber phosphate ores is unstable, with large amounts of floating ore, high cost and low recovery rate.
The ore dressing method is adopted that combines photoelectric sorting and forward-back flotation, including multi-stage crushing, screening, grinding, photoelectric sorting, positive flotation and anti-flotation. The dolomite ganglite is removed through photoelectric sorting, the dolomite ganglite is removed, the siliceous ganglite is removed, and the magnesium ganglite is removed, so as to achieve efficient separation and recovery.
It improves the stability of the ore dressing process, reduces the amount and cost of floating ore, improves the recovery rate, and obtains high-grade phosphorus concentrate, meeting the raw material requirements of yellow phosphorus and wet phosphoric acid processes.
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Abstract
Description
Technical Field
[0001] The present invention belongs to the technical field of mineral processing, and particularly relates to a combined beneficiation method for mixed collophanite ore. Background Art
[0002] In China, phosphate rock resources are mainly concentrated in Yunnan, Guizhou, Sichuan, Hunan, Hubei and other places, mainly sedimentary phosphorite, among which medium and low-grade collophanite ore is the main. Taking the phosphate rock in Yichang area as an example, the phosphate rock mainly includes dolomitic banded phosphorite, dense massive phosphate rock, striped phosphate rock and argillaceous banded phosphorite. Among them, the phosphate grades of dolomitic banded phosphorite and argillaceous banded phosphorite are relatively low. The contents of SiO2, Fe2O3 and Al2O3 are the highest in argillaceous banded phosphorite, and the content of MgO is the highest in dolomitic banded phosphorite. Among them, MgO, Fe2O3 and Al2O3 have a great influence on the phosphoric acid production process. For the thermal phosphoric acid process, MgO has a greater influence. And SiO2 is a beneficial mineral. The characteristic of dolomitic banded phosphorite is that the dissociation particle size of dolomite mineral is coarse, and there is an obvious color difference between dolomite and phosphate rock (dolomite is grayish white and phosphate rock is black).
[0003] The existing technology directly uses the conventional positive - reverse flotation process or double reverse flotation process for the flotation of mixed collophanite ore, which has defects such as unstable beneficiation process flow, large amount of ore fed into flotation, high cost and low recovery rate. Summary of the Invention
[0004] The purpose of the present invention is to address the deficiencies of the existing technology and propose a beneficiation method for mixed collophanite ore with a more reasonable and efficient process. This method has the advantages of stable process flow, small amount of ore fed into flotation, low cost and high recovery rate.
[0005] The present invention is a combined beneficiation method for mixed collophanite ore, which is characterized in that the steps are as follows: (1) The raw ore is subjected to multi-stage crushing to crush the raw ore to -60 mm; (2) The crushed ore is fed into a screening operation to obtain ore with a particle size of -8 mm and ore with a particle size of 8 - 60 mm; (3) The ore with a particle size of 8 - 60 mm is fed to an optoelectronic separation operation to obtain optoelectronic separation concentrate and optoelectronic separation tailings. The optoelectronic separation concentrate can be used as the final yellow phosphorus raw material concentrate, and the tailings of the optoelectronic separation are fed into a secondary crushing operation, and the secondary crushing adopts closed-circuit crushing and screening; (4) The tailings of the optoelectronic separation that are qualified after the secondary closed-circuit crushing and screening are mixed with the ore with a particle size of -8 mm and then fed into a grinding and classification operation; (5) The ground pulp is fed into a positive - reverse flotation operation. The concentrate of the positive - reverse flotation operation is fed into a downstream phosphoric acid device for use, and the tailings of the positive - reverse flotation are fed into a downstream filling operation; (6) The whole plant has three return water pools, which are used to store the return water from photoelectric separation operation, forward flotation operation and reverse flotation demagnesium operation respectively; The ore composition of the mixed collophosphate ore is as follows: P2O5 grade is 16.0%~22.0%, MgO mass content is 4%~9%, SiO2 mass content is 13.0%~22.0%, Al2O3 mass content is 1.2%~2.0%, and Fe2O3 mass content is 1.0%~1.5%.
[0006] A further preferred technical solution of the above-mentioned combined beneficiation method for mixed-type collophanite is that the mixed-type collophanite is dolomitic banded phosphate rock.
[0007] The above-mentioned combined beneficiation method for mixed collophosphate ore has a further preferred technical solution: a pre-screening operation is added to the crushing and screening operation before crushing, and an inspection screening operation is added after crushing to increase the proportion of 8~60mm particle size.
[0008] The above-mentioned combined beneficiation method for mixed collophanite has a further preferred technical solution: photoelectric sorting adopts one roughing and one concentrating operation, and the photoelectric sorting operation uses an X-ray optical sorter or a color sorter to mainly remove dolomite gangue in the collophanite, and dry photoelectric sorting or wet photoelectric sorting is selected according to the content of primary ore slime in the original ore.
[0009] The above-mentioned combined beneficiation method for mixed collophosphate ore has a further preferred technical solution: wet photoelectric sorting is to feed the crushed raw materials into a scrubbing machine, and after scrubbing, feed them into a wet screening operation to obtain 8~60mm ore and -8mm ore.
[0010] The above-mentioned combined beneficiation method for mixed collophosphate ore has a further preferred technical solution: -8mm ore and photoelectrically separated tailings are mixed in a mixed ore yard and then fed into a grinding and classification operation, and qualified slurry is fed into a direct flotation desiliconization operation. The direct flotation desiliconization operation consists of roughing, cleaning, and scavenging, wherein the first tank of each flotation operation is an XCF type slurry suction tank, and the rest are KYF type flotation tanks.
[0011] The above-mentioned combined beneficiation method for mixed collophosphate ore has a further preferred technical solution: there are two stirring tanks for the direct flotation desiliconization roughing operation, and the first stirring tank is added with the adjusting agent sodium carbonate and the inhibitor S711, and the collector 2# is added to the second stirring tank. The roughing operation is divided into two parts by an intermediate box, and the collector 2# is added in the intermediate box, the adjusting agent sodium carbonate and the inhibitor water glass are added in the roughing foam tank, and the adjusting agent sodium carbonate, the inhibitor S711, and the collector 2# are added in the scavenging feed box. The dosage of the reagents is controlled by a flow meter.
[0012] A combined ore dressing method for mixed collophanite as described above, a further preferred technical solution thereof is: the concentrate obtained by direct flotation flows by gravity to the rough separation operation of reverse flotation for magnesium removal. The reverse flotation operation for magnesium removal consists of rough separation, cleaning, and re-separation. The first cell of each stage of flotation operation is an XCF type pulp suction cell, and the rest are KYF type flotation cells.
[0013] A combined ore dressing method for mixed collophanite as described above, a further preferred technical solution thereof is: the medicament adding method for the rough separation operation of reverse flotation for magnesium removal is batch adding. The inhibitor sulfuric acid or mixed acid is respectively added to the agitation tank and the intermediate tank in the rough separation operation. The collector PA67 is added to the feed tank and the intermediate tank in the rough separation operation. The dosage of the medicament is controlled by a flowmeter.
[0014] A combined ore dressing method for mixed collophanite as described above, a further preferred technical solution thereof is: the recycled water from optoelectronic separation is used for optoelectronic separation. The recycled water from the direct flotation return water tank can be used for direct flotation. The recycled water from the reverse flotation return water tank is partially used for reverse flotation, and part of it is treated by a double-alkali process and then returned to the direct flotation process after being qualified.
[0015] The most preferred technical solution of the method of the present invention is as follows: (1) The original ore adopts a conventional crushing operation. For the conventional crushing, according to the feed particle size, if the feed particle size is more than 500 mm, three-stage crushing is adopted; if the feed particle size is less than 500 mm, two-stage crushing is adopted. The particle size after crushing is controlled to be more than -8 mm. The first stage of the conventional crushing adopts a jaw crusher, and the subsequent stage adopts a cone crusher. A pre-screening operation is added before the crushing and screening operation, and an inspection screening operation is added after the crushing to improve the proportion of the 8-60 mm particle size grade as much as possible.
[0016] (2) The ore with a particle size of 8-60 mm is fed to the optoelectronic separation operation to obtain an optoelectronic separation concentrate and an optoelectronic separation tailing. The optoelectronic separation concentrate can be sold as the final yellow phosphorus raw material concentrate. The optoelectronic separation adopts one-stage rough separation and one-stage cleaning operation. The optoelectronic separation operation selects an X-ray-photoelectric separator or a color sorter, mainly to remove the dolomite gangue in the collophanite. According to the content of the primary ore sludge in the original ore, dry optoelectronic separation or wet optoelectronic separation is selected. The wet optoelectronic separation is to feed the crushed raw material into a scrubber, and after scrubbing, it is fed into a wet screening operation to obtain ore with a particle size of 8-60 mm and ore with a particle size of -8 mm.
[0017] (3) The tailings from optoelectronic separation are fed into the second-stage closed-circuit crushing and screening operation. The qualified tailings from optoelectronic separation after crushing are mixed with ores of -8 mm in the ore blending yard and then fed into the grinding and classification operation. The qualified pulp is fed into the positive flotation desilication operation. The positive flotation desilication operation consists of roughing, cleaning, and scavenging. The first cell of each stage of flotation operation is an XCF type pulp suction cell, and the rest are KYF type flotation cells. There are two agitation tanks in the roughing operation of positive flotation desilication. The first agitation tank is added with the regulator sodium carbonate and the inhibitor S711. The collector No. 2 drug is added to the second agitation tank. The roughing operation is divided into two parts through the intermediate box. The collector No. 2 drug is added in the intermediate box. The regulator sodium carbonate and the inhibitor sodium silicate are added in the roughing foam tank. The regulator sodium carbonate, the inhibitor S711, and the collector No. 2 drug are added in the scavenging feed box. The dosage of the drugs is controlled by a flow meter.
[0018] (4) The concentrate from positive flotation flows by gravity to the roughing operation of reverse flotation for magnesium removal. The reverse flotation for magnesium removal operation consists of roughing, cleaning, and re-selection. The first cell of each stage of flotation operation is an XCF type pulp suction cell, and the rest are KYF type flotation cells. The drug addition method for the roughing operation of reverse flotation for magnesium removal is batch addition. The inhibitor sulfuric acid or mixed acid is added to the agitation tank and the intermediate box of the roughing operation respectively. The collector PA67 is added to the feed box and the intermediate box of the roughing operation. The dosage of the drugs is controlled by a flow meter.
[0019] (5) The filtrate after the dehydration process of the optoelectronic separation scrubbing and de-sludging is fed to the optoelectronic separation return water sedimentation tank. The filtrate of the positive flotation tailings dehydration process is fed to the positive flotation return water sedimentation tank. The filtrate of the reverse flotation concentrate and tailings dehydration process is fed to the reverse flotation return water sedimentation tank.
[0020] (6) Three return water sedimentation tanks are set up separately to store the optoelectronic separation return water, the positive flotation return water, and the reverse flotation return water respectively. The return water of optoelectronic separation is used for optoelectronic separation. The return water of the positive flotation return water tank can be used for positive flotation. The return water of the reverse flotation return water tank is not used for reverse flotation, and the other part is treated by the double-alkali process and then returned to the positive flotation process after being qualified.
[0021] By using the method of the present invention, the P2O5 grade in the optoelectronic separation phosphorus concentrate can be 26% - 28%, the mass content of MgO is 2% - 4%, and the mass content of SiO2 is 15% - 24%. The P2O5 grade in the obtained flotation phosphorus ore concentrate is 28.00% - 31.50%, and the mass content of MgO is 0.7% - 1.5%.
[0022] The principle of the present invention is as follows: since this type of collophosphate ore is dolomite banded phosphorite and the dolomite dissociation particle size is coarse, photoelectric separation can be used to enrich the dolomite gangue of the original ore in the photoelectric separation tailings and the siliceous gangue in the photoelectric separation concentrate, thereby obtaining high-silicon, low-magnesium, high-grade phosphate ore and low-silicon, high-magnesium, low-grade phosphate ore. The high-silicon, low-magnesium, high-grade phosphate ore is used as the raw material for the yellow phosphorus process to fully utilize the phosphorus and silicon in the original ore, while the low-silicon, high-magnesium, low-grade phosphate ore can be used as the raw material for the downstream wet-process phosphoric acid process after the direct and reverse flotation process, thereby realizing the full utilization of the phosphate ore and squeezing it out completely.
[0023] Compared with the prior art, the present invention has the following beneficial effects: The method of the present invention adopts photoelectric separation to select a portion of high-silicon, low-magnesium phosphate concentrate for direct sale, thereby reducing the amount of ore required for subsequent grinding and flotation. Compared with directly adopting a conventional direct-reverse flotation process or a double reverse flotation process, the method has the advantages of stable mineral processing technology, small amount of flotation ore, low cost, high recovery rate, etc. DETAILED DESCRIPTION
[0024] Example 1: A combined beneficiation method for mixed collophosphate ore: (1) The raw ore is crushed by conventional operation. Conventional crushing is based on the feed particle size. The feed particle size is below 350mm. Two-stage crushing is adopted. Cone crusher is used for both. Pre-screening operation is added before coarse crushing. Inspection screening operation is added after crushing. The screening operation uses a double-layer screen to screen out 8-60mm raw materials. +60mm is returned to the first stage of crushing, and -8mm is fed to the powder silo.
[0025] (2) The 8~60mm ore is fed to the photoelectric sorting operation to obtain photoelectric concentrate and photoelectric tailings. The photoelectric concentrate can be exported as the final yellow phosphorus raw material concentrate. The photoelectric sorting adopts one roughing and one finishing operation. The photoelectric sorting operation uses an X-ray-optical sorter.
[0026] (3) The tailings from the photoelectric separation are fed into the second-stage closed-circuit crushing and screening operation. After crushing, the qualified photoelectric separation tailings are mixed with -8mm ore in the mixing yard and then fed into the grinding and classification operation. The qualified slurry is fed into the direct flotation desiliconization operation. The direct flotation desiliconization operation consists of roughing, cleaning, and scavenging. The first tank of each flotation operation is an XCF type slurry suction tank, and the rest are KYF type flotation tanks. There are two stirring tanks for the direct flotation desiliconization roughing operation. The first stirring tank is added with the adjusting agent sodium carbonate and the inhibitor S711, and the collector 2# is added to the second stirring tank. The roughing operation is divided into two parts by the intermediate box. The collector 2# is added in the intermediate box, the adjusting agent sodium carbonate and the inhibitor water glass are added in the roughing foam tank, and the adjusting agent sodium carbonate, the inhibitor S711, and the collector 2# are added in the scavenging feed box. The dosage of the reagents is controlled by a flow meter.
[0027] (4) The concentrate of direct flotation flows by gravity to the rough separation operation of reverse flotation for magnesium removal. The reverse flotation operation for magnesium removal consists of rough separation, cleaning, and re-separation. In each stage of the flotation operation, the first cell is an XCF type pulp suction cell, and the rest are KYF type flotation cells. The medicine addition method for the rough separation operation of reverse flotation for magnesium removal is batch addition. The inhibitor sulfuric acid or mixed acid is respectively added to the agitation tank and the intermediate tank of the rough separation operation. The collector PA67 is added to the feed tank and the intermediate tank of the rough separation operation. The dosage of the medicine is controlled by a flowmeter.
[0028] (5) The filtrate of the dewatering process of the tailings of direct flotation is fed to the backwater sedimentation tank of direct flotation, and the filtrate of the dewatering process of the fine tailings of reverse flotation is fed to the backwater sedimentation tank of reverse flotation.
[0029] (6) Two backwater sedimentation tanks are separately set up to store the backwater of direct flotation and the backwater of reverse flotation respectively. The backwater of the direct flotation backwater tank can be used for direct flotation. The backwater of the reverse flotation backwater tank is not only used for reverse flotation, and the other part is treated by the double-alkali process and then returned to the direct flotation process after being qualified.
[0030] In the above method, the ore composition of the mixed-type collophanite is that the grade of P2O5 is 22.0%, the mass content of MgO is 5%, the mass content of SiO2 is 14%, the mass content of Al2O3 is 1.2%, and the mass content of Fe2O3 is 1.1%; In the above method, the grade of P2O5 in the obtained optoelectronic separation phosphorus concentrate is 28.0%, the mass content of MgO is 1.8%, and the mass content of SiO2 is 20%.
[0031] In the above method, the grade of P2O5 in the obtained flotation phosphorus concentrate is 30.5%, and the mass content of MgO is 1.0%.
[0032] Example 2: A combined ore dressing method for mixed-type collophanite: (1) The original ore adopts a conventional crushing operation. The feeding particle size is more than 1000 mm. Three-stage crushing is adopted. The first stage uses a jaw crusher, and the subsequent stages use cone crushers. The first-stage crushing is an open-circuit crushing. The raw materials after the first-stage crushing are fed into a dry screening operation to separate out +60 mm, 8 - 60 mm, and -8 mm raw ore. The +60 mm is returned to the first-stage crushing, and the -8 mm is fed to the fine ore bin. The 8 - 60 mm raw ore is fed into a cylindrical scrubber. After scrubbing, it is fed into a wet screening operation to remove slime and obtain 8 - 60 mm raw ore. The slime is fed into a slime thickener. The overflow of the thickener is returned to the optoelectronic separation backwater sedimentation tank, and the underflow of the thickener is fed to the grinding operation.
[0033] (2) Feed the ore sized 8 - 60 mm after scrubbing and desliming to the optoelectronic separation operation to obtain optoelectronic separation concentrate and optoelectronic separation tailings. The optoelectronic separation concentrate can be sold as the final yellow phosphorus raw material concentrate. The optoelectronic separation adopts one roughing operation, one cleaning operation and one scavenging operation. A color sorter is selected for the optoelectronic separation operation. The tailings of the optoelectronic separation are fed into the second-stage closed-circuit crushing and screening operation. The qualified tailings of the optoelectronic separation after crushing are mixed with the ore sized -8 mm and then fed into the fine ore bin before grinding.
[0034] (3) Feed the raw ore in the fine ore bin and the underflow of the ore slime thickener into the grinding and classification operation. The qualified pulp is fed into the positive flotation desilication operation. The positive flotation desilication operation consists of roughing, cleaning and scavenging. The first cell of each stage of the flotation operation is an XCF type pulp suction cell, and the rest are KYF type flotation cells. There are two agitation tanks in the roughing operation of the positive flotation desilication. Sodium carbonate as the regulator and inhibitor S711 are added to the first agitation tank, and collector No. 2 is added to the second agitation tank. The roughing operation is divided into two parts through an intermediate box. Collector No. 2 is added in the intermediate box, sodium carbonate as the regulator and water glass as the inhibitor are added in the roughing foam tank, and sodium carbonate as the regulator, inhibitor S711 and collector No. 2 are added in the scavenging feed box. The dosage of the reagents is controlled by a flow meter.
[0035] (4) The concentrate of the positive flotation flows by gravity to the roughing operation of the reverse flotation for magnesia removal. The reverse flotation for magnesia removal operation consists of roughing, cleaning and re-selection. The first cell of each stage of the flotation operation is an XCF type pulp suction cell, and the rest are KYF type flotation cells. The reagent addition method for the roughing operation of the reverse flotation for magnesia removal is batch addition. Sulfuric acid or mixed acid as the inhibitor is added to the agitation tank and the intermediate box of the roughing operation respectively, and collector PA67 is added to the feed box and the intermediate box of the roughing operation. The dosage of the reagents is controlled by a flow meter.
[0036] (5) The filtrate of the positive flotation tailings dehydration process is fed to the positive flotation return water sedimentation tank, and the filtrate of the reverse flotation concentrate and tailings dehydration process is fed to the reverse flotation return water sedimentation tank.
[0037] (6) Three return water sedimentation tanks are set up separately to store the return water of the optoelectronic separation, the return water of the positive flotation and the return water of the reverse flotation respectively. The return water of the optoelectronic separation is used for the optoelectronic separation, the return water of the positive flotation pool can be used for the positive flotation, the return water of the reverse flotation pool can be used for the reverse flotation except for a part, and the other part is treated by the double-alkali process and then returned to the positive flotation process after being qualified.
[0038] In the above method, the ore composition of the mixed-type collophanite is that the grade of P2O5 is 18.0%, the mass content of MgO is 7.5%, and the mass content of SiO2 is 14%; In the above method, the grade of P2O5 in the obtained optoelectronic separation phosphorus concentrate is 26.5%, the mass content of MgO is 2.2%, and the mass content of SiO2 is 18%.
[0039] The flotation phosphate concentrate obtained by the above method has a P2O5 grade of 28.5% and a MgO mass content of 1.0%.
[0040] Example 3: A combined beneficiation method for mixed collophosphate ore, (1) The raw ore is crushed in a conventional manner with a feed size of 500 mm or more. Two-stage crushing is used, both using cone crushers. The first stage is open-circuit crushing. The raw materials after the first stage crushing are fed into a dry screening operation to separate +60 mm, 12-60 mm, and -12 mm raw ore. The +60 mm ore is returned to the first stage crushing, and the -12 mm ore is fed to the fine ore bin. The 12-60 mm raw ore is fed into a drum scrubber. After scrubbing, it is fed into a wet screening operation to remove the ore slime and obtain the 12-60 mm raw ore. The ore slime is fed into a sludge thickener. The overflow of the thickener is returned to the photoelectric separation return water sedimentation tank, and the underflow of the thickener is fed into the grinding operation.
[0041] (2) After scrubbing and desludging, the 12~60mm ore is sent to the photoelectric sorting operation to obtain photoelectric concentrate and photoelectric tailings. The photoelectric concentrate can be exported as the final yellow phosphorus raw material concentrate. The photoelectric sorting adopts one roughing and one fine selection operation. The photoelectric sorting operation uses an X-ray-optical sorter. The photoelectric tailings are fed into the second-stage closed-circuit crushing and screening operation. After crushing, the qualified photoelectric tailings are mixed with the -12mm ore and then fed into the powder ore bin before grinding.
[0042] (3) The raw ore in the powder ore bin and the bottom flow of the ore thickener are fed into the grinding and classification operation. The qualified slurry is fed into the direct flotation desiliconization operation. The direct flotation desiliconization operation consists of roughing, cleaning, and scavenging. The first tank of each flotation operation is an XCF type slurry suction tank, and the rest are KYF type flotation tanks. There are two stirring tanks for the direct flotation desiliconization roughing operation. The first stirring tank is added with the adjusting agent sodium carbonate and the inhibitor S711, and the collector 2# is added to the second stirring tank. The roughing operation is divided into two parts by the intermediate box. The collector 2# is added in the intermediate box, the adjusting agent sodium carbonate and the inhibitor water glass are added in the roughing foam tank, and the adjusting agent sodium carbonate, the inhibitor S711, and the collector 2# are added in the scavenging feed box. The dosage of the reagents is controlled by a flow meter.
[0043] (4) The direct flotation concentrate flows by gravity to the reverse flotation demagnesium roughing operation. The reverse flotation demagnesium operation consists of roughing, fine selection and reselection. The first tank of each flotation operation is an XCF type slurry suction tank, and the rest are KYF type flotation tanks. The dosing method of the reverse flotation demagnesium roughing operation is batch dosing. The inhibitor sulfuric acid or mixed acid is added to the stirring tank and the roughing operation intermediate box respectively, and the collector PA67 is added to the roughing operation feed box and the intermediate box. The dosage of the reagent is controlled by a flow meter.
[0044] (5)The filtrate from the positive flotation tailings dewatering process is fed to the positive flotation return water sedimentation tank, and the filtrate from the reverse flotation concentrate tailings dewatering process is fed to the reverse flotation return water sedimentation tank.
[0045] (6)Three return water sedimentation tanks are separately set up to store the return water from optoelectronic separation, positive flotation, and reverse flotation respectively. The return water from optoelectronic separation is used for optoelectronic separation, the return water from the positive flotation pond can be used for positive flotation, and the return water from the reverse flotation pond is not only used for reverse flotation, and the other part is treated by the double-alkali process and then returned to the positive flotation process after being qualified.
[0046] In the above method, the ore composition of the mixed collophanite is that the grade of P2O5 is 24.0%, the mass content of MgO is 2.5%, the mass content of SiO2 is 18%, the mass content of Al2O3 is 1.1%, and the mass content of Fe2O3 is 1.0%; In the above method, the grade of P2O5 in the optoelectronic separation phosphorus concentrate obtained is 28.5%, the mass content of MgO is 1.2%, and the mass content of SiO2 is 18%.
[0047] In the above method, the grade of P2O5 in the flotation phosphorus concentrate obtained is 30.5%, and the mass content of MgO is 0.8%.
[0048] Example 4. The following are the comparative experimental examples done by the inventor: Comparative experiment 1: Positive-reverse flotation process; Comparative experiment 2: Double reverse flotation process; Experimental example: The process of the present invention; The dewatering processes of the positive-reverse flotation process, the double reverse flotation process, and the present invention are the same. The main differences are in the crushing, grinding, and separation processes. The crushing processes of the positive-reverse flotation process and the double reverse flotation process are the same. The following are the specific implementation methods: (1)Crushing and screening: The feed particle size of the original ore is -350 mm. Conventional crushing adopts two-stage one-closed-circuit crushing. The first-stage crushing uses a jaw crusher, and the second-stage crushing uses a cone crusher to crush the material to -12 mm.
[0049] (2)Grinding process: The grinding processes of the double reverse flotation and the process of the present invention are the same, both adopting one-stage grinding and classification process, while the positive-reverse flotation adopts two-stage grinding process.
[0050] Comparative experiment 1: Positive-reverse process: The material at the bottom of the powder ore bin is quantitatively fed to the grinding and classification operation by a disk feeder. Two-stage grinding is selected for grinding. The disk feeder adopts variable frequency speed regulation. The first-stage grinding operation uses a lattice type ball mill, and the second-stage grinding uses an overflow type ball mill. The classification particle size is controlled at 74 μm, and the grinding fineness is controlled at 85%. The qualified particle size of the classification operation is fed into the flotation operation buffer tank; Comparative Experiment 2: Double Reverse Flotation Process: For grinding, single-stage grinding is selected. For classification, primary controlled classification is adopted. The disc feeder uses variable frequency speed regulation. The rod mill is used for the grinding operation. The hydrocyclone is used for the primary controlled classification operation, and the classification particle size is controlled at 74 μm. The grinding fineness of the material before gravity separation is controlled at 65%. The qualified particle size of the classification operation is fed into the buffer tank of the reverse flotation magnesium removal operation; (3)Separation Process: For the positive and reverse flotation process, the sequence is first positive flotation for magnesium removal and then reverse flotation for silicon removal. For the double reverse flotation process, first pre-sludge removal is carried out, and the sludged pulp is then sequentially subjected to reverse flotation for magnesium removal and silicon removal step by step.
[0051] Comparative Experiment 1: Positive and Reverse Flotation Process: The ground pulp is fed into the positive flotation process. The flotation environment is a weakly alkaline environment. Sodium carbonate is selected as the pH regulator. Sodium silicate is used as the inhibitor. The No. 2 reagent is used as the collector for positive flotation. The collector is added in batches. The positive flotation operation includes one roughing, one scavenging, and one cleaning. The foam of the positive flotation is fed into the reverse flotation magnesium removal operation. The flotation environment is a weakly acidic environment. Phosphoric acid is selected as the pH regulator. PA-67 is selected as the collector for magnesium removal. The collector is added in batches. The reverse flotation operation includes one roughing, two scavengings, and one cleaning. The tailings of the positive flotation, the tailings of the reverse flotation, and the concentrate of the reverse flotation are fed into the subsequent dehydration operation; Comparative Experiment 2: Double Reverse Flotation Process: The ground pulp is fed into the sludge removal operation. Hydrocyclone is used for sludge removal, removing the -38μm slime. The sludged pulp after sludge removal is fed into the reverse flotation magnesium removal process. The flotation environment is a weakly acidic environment. Phosphoric acid is selected as the pH regulator. PA-67 is selected as the collector for magnesium removal. The collector is added in batches. The reverse flotation operation includes one roughing, two scavengings, and one cleaning. The in-tank product of the reverse flotation magnesium removal is fed into the reverse flotation silicon removal operation. The flotation environment is a weakly alkaline environment. Sodium carbonate is selected as the pH regulator. MAC is used as the collector for reverse flotation. The collector is added in batches. The positive flotation operation includes one roughing, one scavenging, and one cleaning. The tailings of the reverse flotation magnesium removal, the tailings of the reverse flotation silicon removal, the concentrate of the reverse flotation silicon removal, and the slime are fed into the subsequent dehydration operation; (4)Thickening and Filtration: The dehydration operations for the concentrate and tailings both adopt two dehydration processes of thickening and filtration. The overflow and filtrate of the dehydration operation are respectively returned to their own water tanks.
[0052] In the above method, the ore composition of the mixed collophanite is that the P2O5 grade is 24.0%, the mass content of MgO is 2.5%, the mass content of SiO2 is 18%, the mass content of Al2O3 is 1.1%, and the mass content of Fe2O3 is 1.0%.
[0053] The P2O5 grade in the collophanite concentrate obtained by positive and reverse flotation is 31.00%, the mass content of MgO is 0.95%, and the recovery rate is about 80%. The phosphorus concentrate can be used for the subsequent wet-process phosphoric acid process.
[0054] The P2O5 grade of the collophanite concentrate obtained by double reverse flotation is 30.50%, the mass content of MgO is 0.85%, and the recovery rate is about 65%. The phosphorus concentrate can be used for the subsequent wet-process phosphoric acid process.
[0055] The process of the present invention adopts the technical solution described in Example 3.
[0056] The following table shows the cost comparison between the process of the present invention and the conventional direct and reverse flotation processes and double reverse flotation processes:
[0057] It can be seen from the above comparative experiments that the present invention can obtain two finished concentrates. One is the electro-optical separation concentrate: the P2O5 grade is 28.5%, and the recovery rate is 42%; the other is the flotation concentrate: the P2O5 grade is 30.5%, and the recovery rate is 50%. The recovery rate is greatly improved and the cost is reduced.
Claims
1. A combined ore dressing method for mixed collophanite, characterized in that: The steps are as follows: (1) Multi-stage crushing of the raw ore to -60mm; (2) The crushed ore is fed into the screening operation to obtain ore with a particle size of -8mm and ore with a particle size of 8~60mm; (3) Feed the 8~60mm ore to the photoelectric separation operation to obtain photoelectric concentrate and photoelectric tailings. The photoelectric concentrate can be used as the final yellow phosphorus raw material concentrate, and the photoelectric tailings are fed to the second stage crushing operation. The second stage crushing adopts closed circuit crushing and screening; (4) The qualified tailings from photoelectric separation after the second stage closed circuit crushing and screening are mixed with -8mm ore and then fed into the grinding and classification operation; (5) The ground slurry is fed into the forward and reverse flotation operation, the concentrate from the forward and reverse flotation operation is fed into the downstream phosphoric acid unit for use, and the tailings from the forward and reverse flotation operation is fed into the downstream filling operation; (6) The whole plant has three return water pools, which are used to store the return water from photoelectric separation operation, forward flotation operation and reverse flotation demagnesium operation respectively; The ore composition of the mixed collophosphate ore is as follows: P2O5 grade is 16.0%~22.0%, MgO mass content is 4%~9%, SiO2 mass content is 13.0%~22.0%, Al2O3 mass content is 1.2%~2.0%, and Fe2O3 mass content is 1.0%~1.5%.
2. The combined ore dressing method for mixed collophanite according to claim 1, characterized in that: The mixed type collophosphate is dolomitic banded phosphorite.
3. The combined ore dressing method for mixed collophanite according to claim 1, wherein: The crushing and screening operations include adding pre-screening operations before crushing and adding inspection screening operations after crushing to increase the proportion of 8~60mm particle size.
4. A combined ore dressing method for hybrid collophanite according to claim 1, characterized in that: Photoelectric sorting adopts one roughing and one cleaning operation. Photoelectric sorting uses X-ray optical sorter or color sorter, which is mainly used to remove dolomite gangue in collophosphate ore. Dry photoelectric sorting or wet photoelectric sorting is selected according to the content of primary ore slime in the original ore.
5. A combined beneficiation method for mixed collophanite according to claim 4, characterized in that: Wet photoelectric sorting is to feed the crushed raw materials into a scrubbing machine, and then feed them into a wet screening operation after scrubbing to obtain 8~60mm ores and -8mm ores.
6. The combined ore dressing method for mixed collophanite according to claim 1, characterized in that: -8mm ore and tailings from photoelectric separation are mixed evenly in the mixed ore yard and then fed into the grinding and classification operation. The qualified ore pulp is fed into the direct flotation desiliconization operation. The direct flotation desiliconization operation consists of roughing, cleaning and scavenging. The first tank of each flotation operation is an XCF type slurry suction tank, and the rest are KYF type flotation tanks.
7. A combined beneficiation method for mixed collophanite according to claim 6, characterized in that: There are two stirring tanks for the direct flotation desiliconization roughing operation. The first stirring tank is added with adjusting agent sodium carbonate and inhibitor S711, and the collector 2# is added to the second stirring tank. The roughing operation is divided into two parts by the middle box. Collector 2# is added in the middle box, adjusting agent sodium carbonate and inhibitor water glass are added in the roughing foam tank, and adjusting agent sodium carbonate, inhibitor S711 and collector 2# are added in the scavenging feed box. The dosage of the reagents is controlled by a flow meter.
8. A combined beneficiation method for mixed collophanite according to claim 1, characterized in that: The direct flotation concentrate flows by gravity to the reverse flotation de-magnesium roughing operation. The reverse flotation de-magnesium operation consists of roughing, concentrating and re-selection. The first tank of each flotation operation is an XCF type slurry suction tank, and the rest are KYF type flotation tanks.
9. A combined beneficiation method for mixed collophanite according to claim 8, characterized in that: The reagent addition method for the rough separation operation of reverse flotation to remove magnesium is batch addition. The inhibitor sulfuric acid or mixed acid is respectively added into the agitation tank and the intermediate tank of the rough separation operation, and the collector PA67 is added into the feed tank and the intermediate tank of the rough separation operation. The dosage of the reagent is controlled by a flowmeter.
10. A combined ore dressing method for mixed collophanite according to claim 1, characterized in that: The recycled water from the optoelectronic separation is used for optoelectronic separation. The recycled water from the positive flotation return water tank can be used for positive flotation. Part of the recycled water from the reverse flotation return water tank is used for reverse flotation, and part is treated by the double-alkali process and then returned to the positive flotation process after being qualified.