Double reverse flotation water recovery method for high iron and aluminum type collophanite

Abstract

The present invention is a double reverse flotation water return method for high-iron-aluminum type collophosphate ore, belonging to the field of mineral processing. After the raw ore is crushed, ground and classified, it is reversely floated for de-ironization and de-aluminization. After the product in the tank is concentrated, it is fed into the reverse flotation de-magnesiumization operation. The concentrated overflow of the de-ironization and de-aluminization operation is fed to the return water sedimentation tank of the de-ironization and de-magnesiumization operation; the product in the tank of the reverse flotation and de-magnesiumization operation is dehydrated to become the final phosphate concentrate; the filtrate generated by the dehydration of the product in the tank is fed to the de-ironization and de-aluminization operation foam washing and thickening operation, and the excess water is fed to the return water sedimentation tank of the de-magnesiumization operation together with the filtrate generated by the dehydration of the foam product of the de-magnesiumization operation. The return water sedimentation tank is returned to the respective sections for use. The present invention greatly reduces the amount of foam and the viscosity of the foam by returning part of the filtrate of the de-magnesiumization operation to the de-ironization and de-aluminization operation, and well improves the fluidity of the flotation foam of the de-ironization and de-aluminization operation. It has the advantages of stable mineral processing process, good sorting effect, low iron and aluminum semi-oxide content in the concentrate product, and easy engineering.

Description

Technical Field

[0001] The invention belongs to the technical field of mineral processing, and in particular relates to a double reverse flotation water return method for high-iron-aluminum type collophanite. Background Art

[0002] In my country, phosphate resources are mainly concentrated in Yunnan, Guizhou, Sichuan, Hunan, Hubei and other places, mainly sedimentary phosphorite, among which medium and low-grade collophanite is the main one. Some low-grade collophanites contain aluminum and iron sesquioxides (R 2 O 3 ) is high. In the traditional wet process of phosphoric acid production, iron and aluminum elements can not only cause phosphoric acid to form sludge, but also greatly affect the growth of calcium sulfate crystals, ultimately causing P in the subsequent concentration process. 2 O 5 The loss is large. Therefore, in order to reduce the impact on the wet phosphoric acid and acid fertilizer production processes, it is necessary to reduce the content of iron and aluminum sesquioxides in the phosphate concentrate as much as possible.

[0003] The aluminum-containing minerals in collophanite are mainly clay minerals such as feldspar, mica, and kaolin, and the iron-containing minerals are mainly limonite, pyrite, and magnetite. At present, the main process flows for high-iron aluminum type collophanite are direct-reverse flotation process and double reverse flotation process. The direct-reverse flotation process has the disadvantages of fine grinding fineness, the need for heating, the difficulty of concentrate transportation and dehydration, the difficulty of direct flotation return water utilization, and the high cost of concentrate beneficiation. The double reverse flotation process has the disadvantages of large foam volume and high foam viscosity in the de-ironization and aluminum section, poor process, the de-ironization and aluminum flotation section is greatly affected by ore mud, and the selectivity of desiliconization reagents is poor. However, compared with the direct and reverse flotation process, it has the advantages of coarse grinding fineness, easy transportation and dehydration of concentrate products, and low beneficiation cost. Therefore, if the double reverse flotation process is to be realized in engineering, the key is to solve the problem of foam in the de-ironization and aluminum section, the problem of controlling the ore mud content in the flotation process, and the problem of reasonable return water reuse. Summary of the invention

[0004] The purpose of the present invention is to mainly focus on the deficiencies of the prior art and propose a process that is more reasonable and efficient for removing silicate, carbonate, iron-containing and aluminum-containing gangue minerals from collophanite.

[0005] The objective of the present invention is achieved through the following technical solutions:

[0006] A double reverse flotation water recovery method for high iron and aluminum type collophanite, the steps are as follows:

[0007] (1) After crushing, the raw ore is fed into the grinding and classification operation. The grinding fineness is controlled to be -200 mesh 45.00%~75.00%. After the pulp is adjusted to a pulp mass concentration of 20~40%, it is fed into the reverse flotation de-ironization and de-aluminization roughing operation. The roughing operation adopts a batch dosing method, and ether amine collectors are added. The overflow of the desludging operation is directly fed into the de-ironization and de-aluminization concentrate thickening operation;

[0008] (2) The slurry in the tank of the de-ironization and de-aluminization roughing operation is fed into the thickening operation. The thick bottom flow is fed into the reverse flotation and de-magnesium roughing operation after slurry adjustment. The thick overflow is returned to the de-ironization and de-aluminization return water sedimentation tank;

[0009] (3) The foam from the roughing operation of de-ironization and de-aluminization is fed into the scavenging operation, and the foam from the scavenging operation is fed into the tailings to make it dense. The dense bottom flow of the tailings is filtered and then dry-piled, or directly transported to the tailings filling and tailings pond; the dense tailings overflow is returned to the return water sedimentation tank of the de-ironization and de-aluminization operation; the slurry in the tank of the de-ironization and de-aluminization scavenging operation is returned to the grinding operation through the slurry pump. The slurry concentration in the tank of the scavenging operation must be tested to ensure the appropriate grinding concentration;

[0010] (4) The de-magnesium roughing operation is carried out under acidic conditions, and sulfuric acid, phosphoric acid or a mixture of the two in any proportion is added as an inhibitor during pulping, and fatty acids are added as collectors;

[0011] The foam from the demagnesium removal roughing operation is fed into the re-selection operation, and the foam from the re-selection operation is fed into the demagnesium removal tailings thickening operation. The dense bottom flow of the tailings is filtered and then treated as a dry pile, or directly transported to tailings filling and tailings pond; the overflow returns to the demagnesium removal operation return water sedimentation tank; the slurry in the tank of the demagnesium removal roughing operation is fed into the concentration operation, and the foam from the concentration operation returns to the roughing operation. The product in the tank is fed into the concentrate thickening operation. The dense bottom flow of the concentrate is filtered and then treated as a dry pile, or directly transported to the downstream chemical plant, and the overflow of the thickener returns to the demagnesium removal operation return water sedimentation tank.

[0012] The above-mentioned double reverse flotation water recovery method for high iron and aluminum type collophanite, its further preferred technical solution is:

[0013] 1. The return water sedimentation tank of de-ironization and de-aluminization operation is divided into two parts. One part stores the dense overflow of coarse concentrate of de-ironization and de-aluminization operation; the other part stores the dense overflow of de-ironization and de-aluminization tailings and filtered filtrate.

[0014] 2. The return water sedimentation tank for demagnesiumization operation is divided into two parts, one part stores the dense overflow of demagnesiumization concentrate; the other part stores the dense overflow of demagnesiumization tailings and filtered filtrate.

[0015] 3. Part of the concentrated overflow (after clarification) of the concentrate in the return water sedimentation tank of the demagnesium operation is fed to the roughing operation of deironization and aluminum removal.

[0016] The foam flushing water from the sweeping operation and the defoaming water for thickening the iron-removing aluminum tailings are used as the process circulating water for the magnesium removal operation, and the sediment in the sedimentation tank is returned to the concentrate thickening operation.

[0017] 4. The thickened overflow of coarse concentrate in the return water sedimentation tank of de-ironization and de-aluminization operation (after clarification) is mainly used for grinding water of de-ironization and de-aluminization operation.

[0018] The roughing water is adjusted and the sediment in the sedimentation tank is returned to the magnesium removal roughing operation.

[0019] 5. The tailings thickening overflow and the supernatant of the filtered filtrate (after clarification) in the return water sedimentation tank of the de-ironization and de-aluminization operation are used as process water for the de-aluminization operation, and the unused part is used as foam flushing water for the de-magnesiumization operation and the sediment in the sedimentation tank is fed into the tailings thickening operation of the de-magnesiumization operation.

[0020] 6. The tailings thickening overflow and filtered filtrate (after clarification) in the return water sedimentation tank of the demagnesiumization operation are mainly used as the roughing foam flushing water of the demagnesiumization operation, and the sedimentation in the sedimentation tank is returned to the demagnesiumization tailings thickening operation.

[0021] 7. The roughing operation of de-ironization and aluminum removal adopts the batch dosing method. The reagents for the roughing operation are added in the slurry tank before the flotation tank and the flotation machine behind it.

[0022] 8. In step (3), the slurry concentration in the scavenging operation should be tested. The feed concentration of the preferred grinding operation is generally 96%, and the grinding concentration is about 60-70%. The amount of water to be added is determined based on the return volume of the slurry in the scavenging operation (generally 35%).

[0023] The above-mentioned double reverse flotation water recovery method for high iron and aluminum type collophanite, a further preferred technical solution is:

[0024] 1. The ore composition of the high-alumina siliceous collophanite in the above method is P 2 O 5 The grade is 16.1%~28.9%, the mass content of MgO is 1.5%~5.8%, and the mass content of SiO 2 The mass content is 11.1%~24.0%, Al 2 O 3 The mass content is 1.0%~6.8%, Fe 2 O 3 The mass content is 0.5%~3.9%;

[0025] 2. The cationic collector for de-ironization and de-aluminization operation is ether amine or mixed fatty amine cationic collector, and its dosage is 200 g / t ~800g / t of original ore.

[0026] 3. Before entering the de-iron and aluminum flotation operation, a desludging section is set up to feed the ground slurry to the desludging operation to remove fine particles. The classification particle size of the fine particles removed by the desludging section is -5~20μm; and the desludging section is set as a bypass process, and whether to perform the desludging operation is determined according to the content of fine particles in the slurry after grinding the original ore.

[0027] 4. The reverse flotation process for removing iron and aluminum consists of one roughing and one to three scavenging operations, and the reverse flotation process for removing magnesium consists of one roughing, 0 to 2 cleaning and 1 to 2 re-selection operations. In the scavenging operation for removing iron and aluminum and the re-selection operation for removing magnesium, the first flotation machine is preferably a strong stirring self-priming flotation machine to ensure that the roughing foam can flow into the flotation machine by itself.

[0028] The above-mentioned double reverse flotation water recovery method for high-iron aluminum type collophanite, further preferred technical scheme is: the reverse flotation operation depressant is selected from inorganic acid, the inorganic acid is sulfuric acid, phosphoric acid or a mixture of the two, the dosage is 5kg / t ~ 16kg / t of raw ore, the collector is selected from fatty acid soap organic matter, the dosage is 500 g / t ~ 1200g / t of raw ore;

[0029] The method of the present invention obtains P in the collophanite concentrate. 2 O 5 The grade is 30.5%~34.9%, the mass content of MgO is 0.6%~1.0%, and it contains aluminum and iron sesquioxides (R 2 O 3 ) mass content is 1.8%~3.0%.

[0030] Principle of the present invention: The mineral composition of high-iron aluminum type collophosphate ore is single, mainly low-carbon fluoroapatite, a small amount of carbon apatite and apatite, and the gangue minerals are mainly divided into three parts: carbonate minerals, silicate minerals, and iron-containing minerals. Carbonate minerals are mainly dolomite and calcite, silicate minerals are mainly quartz, aluminum silicate clay minerals, and iron-containing minerals are mainly pyrite and hematite. In order to obtain qualified phosphate concentrate, it is necessary to remove carbonates and silicates at the same time. Among them, the reverse flotation demagnesium process has been applied very maturely, and the return water quality has no adverse effect on the demagnesium process. The reverse flotation desiliconization process has a large amount of foam in roughing and scavenging, high foam viscosity, poor circulation, and difficult sedimentation of the tailings thickener. With multiple backwater reuse, the flotation ore mud content increases, the reagent selectivity deteriorates, and the dosage increases. Therefore, in order to successfully apply the reverse flotation desiliconization operation, the problem of post-foam must be solved first.

[0031] The problems of large amount of foam and high foam viscosity in the reverse flotation desiliconization process are mainly caused by the following reasons: (1) Commonly used cationic collectors such as fatty amines such as dodecylamine have the problem of rich foam and difficult defoaming; (2) As the number of backwater cycles increases, the amount of sludge increases, resulting in an increase in the dosage of dodecylamine and an increase in foam viscosity; (3) The tailings carry a large amount of foam, which causes the dense foam layer of the tailings to become thicker and tougher, and the thickening effect is poor.

[0032] The present invention is dedicated to solving the above problems by adopting the following method to improve the problems of large foam volume and high foam viscosity:

[0033] (1) The agent uses ether amines and mixed fatty amines as new cationic collectors, which greatly improves the foam volume and defoaming speed;

[0034] (2) Adding a desludging bypass before the de-ironization and de-aluminization operation reduces the sludge content entering the roughing operation and ensures the de-ironization.

[0035] The aluminum operation has a stable process;

[0036] (3) Return the concentrated overflow water (return water sedimentation tank) from the demagnesium operation to the desiliconization operation as a desiliconization

[0037] Foam flushing water for operations and thickening and defoaming water for tailings;

[0038] (4) The de-ironization and de-magnesiumization operations are divided into two separate return water sedimentation tanks, which effectively reduces the impact of the return water quality of the de-magnesiumization operation on the de-ironization and de-aluminization process;

[0039] (5) The de-ironization and de-aluminization return water sedimentation tanks are divided into two parts: concentrate and tailings.

[0040] Compared with the prior art, the method of the present invention has the following advantages:

[0041] (1) The amount of foam and foam viscosity in the dealilumination operation are greatly reduced;

[0042] (2) The -10μm particle size in the de-ironization and de-aluminization process is less than 1%;

[0043] (3) A portion of the concentrated overflow water (after settling in the sedimentation tank) from the magnesium removal operation is returned to the de-ironization and de-aluminization operation as foam flushing water for roughing and scavenging, which can greatly accelerate the defoaming speed and flow rate;

[0044] (4) A portion of the concentrate thickening overflow from the de-magnesiumization operation (after settling in the sedimentation tank) is returned to the tailings thickening operation of the de-ironization and de-aluminization operation as defoaming water, which can greatly reduce the defoaming amount of the overflow water. BRIEF DESCRIPTION OF THE DRAWINGS

[0045] Figure 1 It is the double reverse flotation process of collophanite;

[0046] Figure 2 It is the return water process of double reverse flotation of collophanite; DETAILED DESCRIPTION

[0047] The specific technical implementation scheme of the present invention is further described below in conjunction with implementation, but it does not constitute a limitation of the rights thereof.

[0048] Example 1, reference Figure 1 and Figure 2 , double reverse flotation water return method for high iron and aluminum type collophanite:

[0049] (1) After crushing, the raw ore is fed into the grinding and classification operation. The first-stage grinding fineness is controlled to -200 mesh 70.00%. The ground slurry is fed into the desludging operation to remove the -10μm fine particle size. After that, water is added to adjust the slurry to 30% slurry concentration and then fed into the reverse flotation de-ironization and de-aluminization roughing operation. The roughing operation adopts the batch dosing method. The de-ironization and de-aluminization flotation reagent uses etheramine cationic collector, and the dosage is 600g / t raw ore. The overflow of the desludging operation is directly fed into the de-ironization and de-aluminization concentrate thickening operation.

[0050] (2) The slurry in the tank of the de-ironization and de-aluminization roughing operation is fed into the thickening operation. The thick bottom flow is fed into the reverse flotation and de-magnesium roughing operation after slurry adjustment. The thick overflow is returned to the de-ironization and de-aluminization return water sedimentation tank. The concentration of the thick bottom flow is controlled at 55%.

[0051] (3) The foam from the roughing operation of de-ironization and de-aluminization is fed into the scavenging operation, and the foam from the scavenging operation is fed into the tailings concentration. The dense tailings bottom flow is directly transported to the tailings filling, and the dense tailings overflow is returned to the de-ironization and de-aluminization operation return water sedimentation tank. The concentration of the dense tailings bottom flow is controlled at 50%.

[0052] (4) The slurry in the tank of the de-ironization and aluminumization operation is returned to the grinding operation through the slurry pump. The slurry concentration in the tank of the de-ironization and aluminumization operation must be tested to ensure that the grinding concentration is 70%.

[0053] (5) The demagnesium roughing operation is carried out under acidic conditions. During pulping, a mixture of sulfuric acid and phosphoric acid in a ratio of 1:1 is added as an inhibitor at a dosage of 8 kg / t of raw ore. Demagnesium fatty acids are added as collectors at a dosage of 800 g / t of raw ore.

[0054] (6) The foam from the de-magnesium roughing operation is fed into the re-selection operation, and the foam from the re-selection operation is fed into the de-magnesium tailings thickening operation. The thick underflow of the tailings is transported to the tailings filling operation, and the thick underflow is controlled to 60%; during the re-selection, a mixture of sulfuric acid and phosphoric acid in a ratio of 1:1 is added as an inhibitor, and the dosage is 2kg / t of raw ore.

[0055] (7) The slurry in the tank of the demagnesized roughing operation is fed into the concentrating operation, and the foam of the concentrating operation is returned to the roughing operation. The product in the tank is fed into the concentrate thickening operation. The concentrated underflow of the concentrate is directly transported to the downstream chemical plant. The concentration of the concentrated underflow is 60%. During the concentrating, a mixture of sulfuric acid and phosphoric acid in a ratio of 1:1 is added as an inhibitor at a dosage of 3 kg / t of raw ore. Demagnesized fatty acids are added as collectors at a dosage of 300 g / t of raw ore.

[0056] (8) The return water from the return water sedimentation tank for de-ironization and de-aluminization is mainly used in the de-ironization and de-aluminization section, and the return water from the return water sedimentation tank for de-magnesiumization is mainly used in the de-magnesiumization section.

[0057] The ore composition of the high-alumina siliceous collophanite in the above method is P 2 O 5 The grade is 24.3%, the mass content of MgO is 4.2%, and the mass content of SiO 2 The mass content is 13.8%, Al 2 O 3 The mass content is 4.0%, Fe 2 O 3 The mass content is 2.5%;

[0058] The above method obtains P in the collophanite concentrate. 2 O 5 The grade is 32.9%, the mass content of MgO is 0.67%, and it contains aluminum and iron sesquioxides (R 2 O 3 ) mass content is 2.88%.

[0059] Example 2, reference Figure 1 and Figure 2 , double reverse flotation water return method for high iron and aluminum type collophanite:

[0060] (1) After crushing, the raw ore is fed into the grinding and classification operation. The first-stage grinding fineness is controlled to -200 mesh 50.0%. The ground slurry is adjusted to 25% slurry concentration by adding water and then fed into the reverse flotation de-ironization and de-aluminization roughing operation. The roughing operation adopts the batch dosing method. The de-ironization and de-aluminization flotation agent is ether amine cationic collector, and the dosage is 400g / t raw ore.

[0061] (2) The slurry in the tank of the de-ironization and de-aluminization roughing operation is fed into the thickening operation. The thick bottom flow is fed into the reverse flotation and de-magnesium roughing operation after slurry adjustment. The thick overflow is returned to the de-ironization and de-aluminization return water sedimentation tank. The concentration of the thick bottom flow is controlled at 55%.

[0062] (3) The foam from the roughing operation of de-ironization and de-aluminization is fed into the scavenging operation, and the foam from the scavenging operation is fed into the tailings thickening operation. The underflow of the tailings thickening is fed into the tailings filtration operation. The overflow of the tailings thickening and the filtered filtrate are returned to the return water sedimentation tank of the de-ironization and de-aluminization operation. The underflow concentration of the tailings thickening is controlled at 50%, and the water content of the filter cake after filtration is 18%.

[0063] (4) The slurry in the tank of the de-ironization and aluminumization operation is returned to the grinding operation through the slurry pump. The slurry concentration in the tank of the de-ironization and aluminumization operation must be tested to ensure that the grinding concentration is 70%.

[0064] (5) The demagnesium roughing operation is carried out under acidic conditions. Sulfuric acid is added as an inhibitor during slurry preparation at a dosage of 15 kg / t of raw ore; demagnesium fatty acids are added as collectors at a dosage of 900 g / t of raw ore.

[0065] (6) The foam from the de-magnesium roughing operation is fed into the re-selection operation, and the foam from the re-selection operation is fed into the de-magnesium tailings thickening operation. The thickened underflow of the tailings is transported to the tailings filtration operation. The thickened underflow is controlled at 50%, and the moisture content of the filter cake after filtration is 18%. Sulfuric acid is added as an inhibitor during the re-selection, and the dosage is 2kg / t of original ore.

[0066] (7) The slurry in the tank of the demagnesium roughing operation is fed to the concentration operation, the foam of the concentration operation is returned to the roughing operation, the product in the tank is fed to the concentrate thickening operation, and the concentrated underflow of the concentrate is fed to the concentrate filtration operation. The concentration of the thickened underflow is 50%, and the water content of the filter cake after filtration is 18%. Sulfuric acid is added as an inhibitor during the concentration, and the dosage is 4kg / t of the original ore. Demagnesium fatty acids are added as collectors, and the dosage is 300 g / t of the original ore.

[0067] (8) The return water from the return water sedimentation tank for de-ironization and de-aluminization is mainly used in the de-ironization and de-aluminization section, and the return water from the return water sedimentation tank for de-magnesiumization is mainly used in the de-magnesiumization section.

[0068] The ore composition of the high-alumina siliceous collophanite in the above method is P 2 O 5 The grade is 25.56%, the MgO content is 2.5%, and the SiO 2 The mass content is 14.2%, Al 2 O 3 The mass content is 3.5%, Fe 2 O 3 The mass content is 2.5%;

[0069] The above method obtains P in the collophanite concentrate. 2 O 5 The grade is 32.79%, the mass content of MgO is 0.65%, and it contains aluminum and iron sesquioxide (R 2 O 3 ) mass content is 2.75%.

[0070] Example 3, reference Figure 1 and Figure 2 , double reverse flotation water return method for high iron and aluminum type collophanite:

[0071] (1) After crushing, the raw ore is fed into the grinding and classification operation. The first-stage grinding fineness is controlled to be -200 mesh 65.00%. The ground slurry is fed into the desludging operation to remove the -10μm fine particle size. After that, water is added to adjust the slurry to 30% slurry concentration and then fed into the reverse flotation de-ironization and de-aluminization roughing operation. The roughing operation adopts the batch dosing method. The de-ironization and de-aluminization flotation reagent is etheramine cationic collector, and the dosage is 650g / t raw ore. The overflow of the desludging operation is directly fed into the de-ironization and de-aluminization concentrate thickening operation.

[0072] (2) The slurry in the tank of the de-ironization and de-aluminization roughing operation is fed to the thickening operation, the thick bottom flow is fed to the filtering operation, the filtrate is returned to the de-ironization and de-aluminization return water sedimentation tank, the filter cake is fed to the reverse flotation de-magnesium roughing operation after slurry adjustment, and the thick overflow is returned to the de-ironization and de-aluminization return water sedimentation tank. The concentration of the thick bottom flow is controlled at 55%, and the water content of the filter cake after filtration is 18%.

[0073] (3) The foam from the roughing operation of de-ironization and de-aluminization is fed into the scavenging operation, and the foam from the scavenging operation is fed into the tailings thickening operation. The dense underflow of the tailings is transported to the tailings filtration operation, and the dense overflow of the tailings is returned to the return water sedimentation tank of the de-ironization and de-aluminization operation. The concentration of the dense underflow of the tailings is controlled at 50%, and the water content of the filter cake after filtration is 18%.

[0074] (4) The slurry in the tank of the de-ironization and aluminumization operation is returned to the grinding operation through the slurry pump. The slurry concentration in the tank of the de-ironization and aluminumization operation must be tested to ensure that the grinding concentration is 70%.

[0075] (5) The demagnesium roughing operation is carried out under acidic conditions. During pulping, a mixture of sulfuric acid and phosphoric acid in a ratio of 1:1 is added as an inhibitor at a dosage of 8 kg / t of raw ore; demagnesium fatty acids are added as collectors at a dosage of 1000 g / t of raw ore.

[0076] (6) The foam from the de-magnesium roughing operation is fed to the re-selection operation, and the foam from the re-selection operation is fed to the de-magnesium tailings thickening operation. The thickened underflow of the tailings is transported to the tailings filtration operation. The thickened underflow is controlled to 50%, and the moisture content of the filter cake after filtration is 18%. During the re-selection, a mixture of sulfuric acid and phosphoric acid in a ratio of 1:1 is added as an inhibitor, and the dosage is 2.0 kg / t of raw ore.

[0077] (7) The slurry in the tank of the demagnesium roughing operation is fed to the concentration operation, the foam of the concentration operation is returned to the roughing operation, the product in the tank is fed to the concentrate thickening operation, and the concentrated underflow of the concentrate is fed to the concentrate filtration operation. The concentration of the thickened underflow is 50%, and the water content of the filter cake after filtration is 18%. During the concentration, a mixture of sulfuric acid and phosphoric acid in a ratio of 1:1 is added as an inhibitor at a dosage of 3.0 kg / t of raw ore. Demagnesium fatty acids are added as collectors at a dosage of 200 g / t of raw ore.

[0078] (8) The return water from the return water sedimentation tank for de-ironization and de-aluminization is mainly used in the de-ironization and de-aluminization section, and the return water from the return water sedimentation tank for de-magnesiumization is mainly used in the de-magnesiumization section.

[0079] The ore composition of the high-alumina siliceous collophanite in the above method is P 2 O 5 The grade is 23.6%, the mass content of MgO is 4.8%, and the mass content of SiO 2 The mass content is 14.6%, Al 2 O 3 The mass content is 4.2%, Fe 2 O 3 The mass content is 2.1%;

[0080] The above method obtains P in the collophanite concentrate. 2 O 5 The grade is 31.0%, the mass content of MgO is 0.87%, and it contains aluminum and iron sesquioxides (R 2 O 3 ) mass content is 2.31%.

[0081] Example 4, reference Figure 1 and Figure 2 , double reverse flotation water return method for high iron and aluminum type collophanite:

[0082] (1) After crushing, the raw ore is fed into the grinding and classification operation. The first-stage grinding fineness is controlled to -200 mesh 60.00%. After adding water to adjust the pulp to 30% pulp concentration, it is fed into the reverse flotation de-ironization and de-aluminization roughing operation. The roughing operation adopts the batch dosing method. The de-ironization and de-aluminization flotation reagent uses ether amine cationic collector, and the dosage is 450g / t raw ore. The overflow of the desludging operation is directly fed into the de-ironization and de-aluminization concentrate thickening operation.

[0083] (2) The slurry in the tank of the de-ironization and de-aluminization roughing operation is fed into the thickening operation. The thick bottom flow is fed into the reverse flotation and de-magnesium roughing operation after slurry adjustment. The thick overflow is returned to the de-ironization and de-aluminization return water sedimentation tank. The concentration of the thick bottom flow is controlled at 55%.

[0084] (3) The foam from the roughing operation of de-ironization and de-aluminization is fed into the thickening section, and after thickening, the bottom flow is fed into the scavenging operation. The bottom flow concentration is controlled at 50%. The foam from the scavenging operation is fed into the tailings thickening section, and the bottom flow of the tailings thickening is directly transported to the tailings filling. The overflow of the tailings thickening is returned to the return water sedimentation tank of the de-ironization and de-aluminization operation. The bottom flow concentration of the tailings thickening is controlled at 50%.

[0085] (4) The slurry in the tank of the de-ironization and aluminumization operation is returned to the grinding operation through the slurry pump. The slurry concentration in the tank of the de-ironization and aluminumization operation must be tested to ensure that the grinding concentration is 70%.

[0086] (5) The demagnesium roughing operation is carried out under acidic conditions. Sulfuric acid is added as an inhibitor during slurry adjustment at a dosage of 16 kg / t of raw ore, and demagnesium fatty acids are added as collectors at a dosage of 1100 g / t of raw ore.

[0087] (6) The foam from the de-magnesium roughing operation is fed into the re-selection operation, and the foam from the re-selection operation is fed into the de-magnesium tailings thickening operation. The thick underflow of the tailings is transported to the tailings filling operation, and the thick underflow is controlled to 60%; sulfuric acid is added as an inhibitor during the re-selection, and the dosage is 3kg / t of original ore.

[0088] (7) The slurry in the tank of the demagnesized roughing operation is fed into the concentrating operation, and the foam of the concentrating operation is returned to the roughing operation. The product in the tank is fed into the concentrate thickening operation. The concentrated underflow of the concentrate is directly transported to the downstream chemical plant. The concentration of the concentrated underflow is 60%. Sulfuric acid is added as an inhibitor during the concentrating process, and the dosage is 4kg / t of raw ore. Demagnesized fatty acids are added as collectors, and the dosage is 200 g / t of raw ore.

[0089] (8) The return water from the return water sedimentation tank for de-ironization and de-aluminization is mainly used in the de-ironization and de-aluminization section, and the return water from the return water sedimentation tank for de-magnesiumization is mainly used in the de-magnesiumization section.

[0090] The ore composition of the high-alumina siliceous collophanite in the above method is P 2 O 5 The grade is 23.8%, the mass content of MgO is 3.9%, and the mass content of SiO 2 The mass content is 15.7%, Al 2 O 3 The mass content is 2.8%, Fe 2 O 3 The mass content is 1.7%;

[0091] The above method obtains P in the collophanite concentrate. 2 O 5 The grade is 30.5%, the mass content of MgO is 0.7%, and it contains aluminum and iron sesquioxide (R 2 O 3 ) mass content is 2.16%.

[0092] In the above examples, refer to Figure 2 , the return water circulation adopts the following method:

[0093] (1) The demagnesiumization operation return water sedimentation tank is divided into two parts, one part stores the demagnesiumization operation concentrate thickening overflow, and the other part stores the demagnesiumization tailings thickening overflow and filtered filtrate. A part of the concentrate thickening overflow (after clarification) in the demagnesiumization operation return water sedimentation tank is provided to the demagnesiumization roughing operation and scavenging operation foam washing water, demagnesiumization tailings thickening defoaming water, and the rest is used for demagnesiumization operation process circulating water. The sedimentation tank sedimentation is returned to the concentrate thickening operation. The tailings thickening overflow and filtered filtrate (after clarification) in the demagnesiumization operation return water sedimentation tank are mainly used for demagnesiumization roughing foam washing water,

[0094] The sedimentation tank sediment is returned to the de-magnesium tailings thickening operation.

[0095] (2) The return water sedimentation tank of the de-ironization operation is divided into two parts. One part stores the thickened overflow of the coarse concentrate of the de-ironization operation; the other part stores the thickened overflow of the tailings of the de-ironization operation and the filtrate. The thickened overflow of the coarse concentrate (after clarification) in the return water sedimentation tank of the de-ironization operation is mainly used as grinding water and roughing slurry water for the de-ironization operation. The sedimentation tank is returned to the roughing operation of the de-magnesiumization operation. The supernatant of the thickened overflow of the tailings and the filtrate (after clarification) in the return water sedimentation tank of the de-ironization operation is used as process water for the de-aluminization operation, and the unused part is used as foam flushing water for the re-selection operation of the de-magnesiumization operation. The sediment in the sedimentation tank is fed to the thickening operation of the tailings of the de-magnesiumization operation.

[0096] In the above examples, the reverse flotation de-ironization and de-aluminization process consists of one roughing and one to three scavenging operations, and the reverse flotation de-magnesiumization flotation consists of one roughing, 0 to 2 secondary cleaning and 1 to 2 re-selection operations. The first flotation machine in the de-ironization and de-aluminumization scavenging operation and de-magnesium re-selection operation uses a strong stirring self-priming flotation machine to ensure that the roughing foam can flow to the flotation machine by itself.

Claims

1. A double reverse flotation water recovery method for high iron and aluminum type collophanite, characterized in that: The steps of this method are as follows: (1) After crushing, the raw ore is fed into the grinding and classification process. The grinding fineness is controlled to be -200 mesh 45.00%~75.00%. After the pulp is adjusted to a pulp mass concentration of 20~40%, it is fed into the reverse flotation de-ironization and de-aluminization roughing process. Ether amine collectors are added, and the overflow of the desludging process is directly fed into the de-ironization and de-aluminization concentrate thickening process; (2) The slurry in the tank of the de-ironization and de-aluminization roughing operation is fed to the thickening operation. The thick bottom flow is fed to the reverse flotation and de-magnesium roughing operation after slurry adjustment, and the thick overflow is returned to the de-ironization and de-aluminization return water sedimentation tank; (3) The foam from the roughing operation of de-ironization and de-aluminization is fed into the scavenging operation. The foam from the scavenging operation is fed into the tailings to make it dense. The dense bottom flow of the tailings is filtered and then dry-piled, or directly transported to the tailings filling and tailings pond; the dense overflow of the tailings is returned to the return water sedimentation tank of the de-ironization and de-aluminization operation; the slurry in the tank of the de-ironization and de-aluminization scavenging operation is returned to the grinding operation through the slurry pump. The slurry concentration in the tank of the scavenging operation must be tested to ensure the appropriate grinding concentration; (4) The ore pulp in the trough of the iron and aluminum roughing operation is subjected to the demagnesium roughing operation. The demagnesium roughing operation is carried out under acidic conditions. During the slurry preparation, sulfuric acid, phosphoric acid or a mixture of the two in any proportion is added as an inhibitor, and fatty acids are added as collectors; The foam from the demagnesium removal roughing operation is fed into the re-selection operation, and the foam from the re-selection operation is fed into the demagnesium removal tailings thickening operation. The dense bottom flow of the tailings is filtered and then treated as a dry pile, or directly transported to tailings filling and tailings pond; the overflow returns to the demagnesium removal operation return water sedimentation tank; the slurry in the tank of the demagnesium removal roughing operation is fed into the concentration operation, and the foam from the concentration operation returns to the roughing operation. The product in the tank is fed into the concentrate thickening operation. The dense bottom flow of the concentrate is filtered and then treated as a dry pile, or directly transported to the downstream chemical plant, and the overflow of the thickener returns to the demagnesium removal operation return water sedimentation tank.

2. A double reverse flotation water recovery method for high iron and aluminum type collophanite according to claim 1, characterized in that: The return water from the return water sedimentation tank for de-ironization and de-aluminization is mainly used in the de-ironization and de-aluminization section; the return water from the return water sedimentation tank for de-magnesiumization is mainly used in the de-magnesiumization section.

3. A double reverse flotation water recovery method for high iron and aluminum type collophanite according to claim 1 or 2, characterized in that: The return water sedimentation tank for demagnesing operation is divided into two parts, one part stores the dense overflow of demagnesing operation concentrate, and the other part stores the dense overflow of demagnesing tailings and filtered filtrate; a part of the dense overflow of concentrate in the return water sedimentation tank for demagnesing operation is provided to the foam washing water of deironization and aluminum roughing and scavenging operation, and the dense defoaming water of deironization and aluminum tailings after clarification, and the rest is used as the circulating water of demagnesing operation process, and the sediment in the sedimentation tank is returned to the concentrate thickening operation; the dense overflow of tailings and filtered filtrate in the return water sedimentation tank for magnesium operation are mainly used as the roughing foam washing water of demagnesing operation after clarification, and the sediment in the return water sedimentation tank is returned to the thickening operation of demagnesing tailings.

4. A double reverse flotation water recovery method for high iron and aluminum type collophanite according to claim 1, characterized in that: The de-ironization and de-aluminization operation return water sedimentation tank is divided into two parts, one part stores the concentrated overflow of the de-ironization and de-aluminization operation concentrate, and the other part stores the concentrated overflow of the de-ironization and de-aluminization tailings and the filtrate; the concentrated overflow of the coarse concentrate in the de-ironization and de-aluminization operation return water sedimentation tank is mainly used as de-ironization and de-aluminization operation grinding water and roughing slurry water after clarification, and the sedimentation in the sedimentation tank is returned to the de-magnesium roughing operation; The tailings thickening overflow and filtered filtrate in the return water sedimentation tank of the de-ironization and de-aluminization operation are clarified, and the supernatant is used as process water for the de-aluminization operation, and the unused part is used as foam flushing water for the de-magnesization operation and the sediment in the sedimentation tank is fed into the tailings thickening operation of the de-magnesium operation.

5. The method according to claim 1, characterized in that: The de-ironization and de-aluminization flotation reagents are ether amine or mixed fatty amine cationic collectors, with a dosage of 200 g / t ~800g / t of raw ore.

6. The method according to claim 1, characterized in that: The magnesium removal flotation reagent fatty acid soap organic matter is used in an amount of 500 g / t ~1500g / t of raw ore, and the inhibitor is an inorganic acid, which is sulfuric acid, phosphoric acid or a mixture of the two, and the dosage is 5 kg / t ~18kg / t of raw ore.

7. The method according to claim 1, characterized in that: Before entering the de-iron and aluminum flotation operation, a desludging section is set up to feed the ground slurry to the desludging operation to remove fine particles.

8. The method according to claim 7, characterized in that: The desludging section removes fine particles with a grading size of -5~20μm; and the desludging section is set as a bypass process, and whether to perform desludging operation is determined based on the content of fine particles in the slurry after grinding of the original ore.

9. The method according to claim 1, characterized in that: The ore composition of high-alumina siliceous collophosphate is: P2O5 grade is 16.1%~28.9%, MgO mass content is 1.5%~5.8%, SiO2 mass content is 11.1%~24.0%, Al2O3 mass content is 1.0%~6.8%, and Fe2O3 mass content is 0.5%~3.9%.

10. The method according to claim 1, characterized in that: The reverse flotation process for removing iron and aluminum consists of one roughing and one to three scavenging operations, and the reverse flotation process for removing magnesium consists of one roughing, 0 to 2 cleaning and 1 to 2 re-selection operations. In the scavenging operation for removing iron and aluminum and the re-selection operation for removing magnesium, the first flotation machine uses a strong stirring self-priming flotation machine to ensure that the roughing foam can flow into the flotation machine by itself.

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