A beneficiation method of tantalum-niobium-rubidium polymetallic lithium ore

Abstract

The application discloses a beneficiation method of tantalum, niobium and rubidium-containing polymetallic lithium ore, and comprises the following steps: (1) crushing and grinding and slurry conditioning of the lithium ore in sequence to obtain a slurry; (2) two-stage flotation is adopted for mineral flotation, one-stage roughing I is adopted for the first-stage flotation to float out easily-selected lithium rough concentrate I, two-stage roughing and two-stage cleaning and two-stage scavenging are adopted for the second-stage flotation to float out the lithium rough concentrate II of the difficult-to-select part, the lithium rough concentrate I and the lithium rough concentrate II are combined to obtain lithium rough concentrate III, and the last remaining part after the flotation is the flotation tailings; and (3) the lithium rough concentrate III of the step (2) is subjected to magnetic separation for iron removal by adopting the method of weak magnetic field first and high gradient strong magnetic field subsequently to obtain lithium concentrate. The two-stage flotation is adopted, the easily-floated lithium rough concentrate I is quickly floated out in the first-stage flotation, the product is directly produced in the one-stage roughing, the lithium rough concentrate II of the difficult-to-select part is floated out in the second-stage flotation, and the activation agent is added for strengthening capture, so that the middling circulation is reduced, and the lithium recovery rate is improved.

Description

Technical Field

[0001] This invention belongs to the field of mineral processing technology, specifically relating to a mineral processing method for tantalum-niobium-rubidium polymetallic lithium ore. Background Technology

[0002] my country's lithium ore resources are mainly composed of associated pegmatite deposits, with most ores containing multiple lithium-bearing minerals such as spodumene, lepidolite, and lepidolite, making them complex and difficult-to-process pegmatite lithium deposits. Currently, the gravity-magnetic-flotation process is commonly used for lithium ores containing associated polymetallic elements such as tantalum, niobium, and rubidium. This method can obtain high-grade tantalum, niobium, and rubidium concentrates, but the lithium recovery rate is poor, with a lithium concentrate grade of 4.73% and a recovery rate of 66.75%. Furthermore, due to the low tantalum, niobium, and rubidium content in the raw ore, multiple enrichment processes are required, and a large amount of processing equipment is needed, which is inconvenient for operation. Regarding beneficiation methods for tantalum, niobium, and rubidium polymetallic lithium ores, we found the following patent: 1. Application No.: 202111559430.3, Invention Title: A tailings-free beneficiation method for lithium ore recovery, the method comprising the following steps: lithium ore is sequentially crushed, ground, and slurry-treated, then pre-enriched with lepidolite using a preferential flotation process to obtain lepidolite rough concentrate; the lepidolite rough concentrate is subjected to blank cleaning to obtain flotation concentrate, which is lepidolite concentrate, and the flotation tailings are used as feed for feldspar and quartz separation; the tailings from the preferential flotation are ground and slurry-treated for flotation separation to obtain spodumene rough concentrate and feldspar and quartz separation feed respectively; the spodumene rough concentrate is subjected to weak magnetic separation to remove iron, followed by strong magnetic separation and spiral sluice gravity separation to obtain spodumene concentrate and niobium-tantalite minerals; feldspar and quartz are separated by flotation to obtain feldspar concentrate and quartz concentrate. This invention significantly improves the overall utilization rate of lithium ore by preferentially flotating lepidolite, removing iron from spodumene rough concentrate and enriching niobium and tantalum minerals, and separating quartz and feldspar. However, this invention uses a single-stage rough flotation for lithium ore recovery, which is not conducive to operation, and requires a large amount of depressant to suppress gangue and other impurities.

[0003] 2. Application No.: 201310370568.8, Invention Title: A Comprehensive Recovery Process for Potassium Polymetallic Ores Associated with Fine-Grained Sawdust. This process includes steps such as coarse grinding of the raw ore, settling and desliming, flotation, agglomeration magnetic separation, and gravity separation. This invention's process method is particularly suitable for the comprehensive recovery of lithium polymetallic ores with high mud content, low-grade sawdust associated with the ore, and fine-grained disseminated particles in mining areas with consistently low temperatures. Furthermore, this technology is advanced, reliable, simple, reasonable, and highly targeted. It does not require high fineness in the raw ore grinding, requires less regrinding, has low operating costs, and achieves a high overall recovery rate. However, this invention uses a single-stage coarse flotation stage for lithium, which is inconvenient for operation and reduces the cost of flotation reagents. Summary of the Invention

[0004] The purpose of this invention is to solve the above-mentioned technical problems and provide a two-stage flotation lithium process that is easy to operate and saves reagent costs. This process can improve the recovery rate and grade of lithium concentrate and reduce the need for gravity separation equipment in the beneficiation of tantalum-niobium-rubidium polymetallic lithium ore.

[0005] To achieve the above objectives, the technical solution of the present invention is as follows: A beneficiation method for tantalum-niobium-rubidium polymetallic lithium ore includes the following steps: (1) The lithium ore is crushed, ground and slurryed in sequence to obtain slurry; (2) The slurry is subjected to mineral flotation operation in two stages. The first stage flotation uses one roughing I to float out the easily bleed lithium rough concentrate I, which includes lepidolite ore, etc. The second stage flotation uses one roughing II, two cleaning and two scavenging processes to float out the difficult-to-bleed lithium rough concentrate II, which includes spodumene, etc. The lithium rough concentrate I and lithium rough concentrate II are combined to obtain lithium rough concentrate III. The last residue after flotation is the flotation tailings. (3) The lithium crude concentrate III from step (2) was subjected to magnetic separation to remove iron by first weak magnetic separation and then high gradient strong magnetic separation to obtain lithium concentrate; the lithium concentrate contained 6.0% to 9.0% Li2O grade and the mineral analysis showed that it was a mixed concentrate containing spodumene and lepidolite. (4) The flotation tailings from step (2) are separated by weak magnetic separation to obtain magnetite and magnetic tailings; (5) After the magnetic separation tailings obtained in step (4) are subjected to roughing III and scavenging in sequence by spiral sluice, tantalum-niobium-rubidium rough concentrate and spiral sluice tailings are obtained. (6) The tantalum-niobium-rubidium rough concentrate from step (5) is classified and separated by a shaking table to obtain a tantalum-niobium-rubidium mixed concentrate.

[0006] As a further technical solution, the particle size of the above lithium ore raw ore after crushing and grinding is greater than 95% -0.2mm, of which -0.074mm accounts for 70% to 75%.

[0007] As a further technical solution, the above-mentioned slurry conditioning process involves adding NaOH and Na2CO3 as conditioning agents to the crushed and ground mineral particles, wherein the NaOH and Na2CO3 are added in a mass ratio of 1:1; the pH value of the slurry is 11-13, and the mass concentration of the slurry is 35%-40%. The mass concentration of the slurry refers to the content of solid mineral particles in the slurry.

[0008] As a further technical solution, the above-mentioned coarse selection I is carried out in the following order. In sequenceAdd reagents and stir: Add NaOH at 500g / t·feed to 800g / t·feed and stir for 5min to 10min; Add Na2CO3 at 500g / t·feed to 800g / t·feed and stir for 5min to 10min; Add calcium lignosulfonate at 500g / t·feed to 800g / t·feed and stir for 5min to 10min; Add saponified oleic acid, a collector, at 400g / t·feed to 500g / t·feed and stir for 3min to 5min. As a further technical solution, the above-mentioned coarse selection II is performed in the following order. In sequence Add reagents and stir: Add NaOH at 100g / t·feed to 200g / t·feed and stir for 5min to 10min; Add Na2CO3 at 100g / t·feed to 200g / t·feed and stir for 5min to 10min; Add calcium lignosulfonate at 100g / t·feed to 200g / t·feed and stir for 5min to 10min; Add NaClO at 200g / t·feed to 400g / t·feed and stir for 5min to 10min; Add saponified oleic acid and diesel oil, of which saponified oleic acid is 300g / t·feed to 400g / t·feed and diesel oil is 60g / t·feed to 100g / t·feed and stir for 3min to 5min.

[0009] As a further technical solution, the reagent added in the above-mentioned selection is NaClO, with an addition amount of 100g / t·feed to 200g / t·feed, and stirring for 3min to 5min.

[0010] In this invention, NaOH and Na2CO3 from roughing I and roughing II are used as modifiers, calcium lignosulfonate is used as a gangue inhibitor, NaClO is used as an activator, and saponified oleic acid and diesel oil are used as collectors.

[0011] As a further technical solution, the two scavenging processes mentioned above include scavenging I and scavenging II; in scavenging I, first add 100g / t·feed to 200g / t·feed of NaClO and 100g / t·feed to 200g / t·feed of saponified oleic acid, and then stir for 3min to 5min; then add 15g / t·feed to 30g / t·feed of diesel oil and stir for 2min to 3min; As a further technical solution, in the above-mentioned scavenging process II, first add 100g / t·feed to 200g / t·feed and stir for 3min to 5min; then add 50g / t·feed to 100g / t·feed of saponified oleic acid and stir for 2min to 3min; then add 15g / t·feed to 30g / t·feed of diesel oil and stir for 2min to 3min.

[0012] As a further technical solution, the magnetic field strength of the weak magnet mentioned above is 0.35T, and the magnetic field strength of the high gradient strong magnet is 0.9~1.2T.

[0013] As a further technical solution, in step (5) above, both roughing III and scavenging in the spiral chute are carried out under the conditions of feed concentration of 20% to 25%, feed rate of 200 kg / h to 300 kg / h, and water supply of 1500 kg / h to 1600 kg / h.

[0014] As a further technical solution, the shaking table classification and separation described above is divided into three particle sizes: +0.15mm, 0.15 to +0.074mm, and -0.074mm; the shaking table stroke is 8 to 14 mm, the number of strokes is 300 to 400 r / min, the transverse slope of the table surface is 1°30″ to 3°30″, the feed concentration is 15% to 25%, and the washing water volume is 15 t / unit·d to 30 t / unit·d.

[0015] In this invention, the feed refers to the ore particles being transported in this operation.

[0016] Compared with the prior art, the beneficial effects of the present invention are as follows: 1. In this invention, the lithium ore is a co-existing pegmatite mineral containing various lithium-bearing minerals such as spodumene, lepidolite, and lepidolite. In the slurry preparation process, NaOH and Na₂CO₃ are added to adjust the pH of the slurry to alkaline. This serves two purposes: firstly, it can neutralize the Fe₂O₃ produced during grinding of the lithium ore. 3+ Firstly, it allows impurity ions to precipitate, reducing their inhibitory effect on the floatability of spodumene, which has poor floatability, during flotation. Secondly, it effectively cleans the sludge adsorbed on the surface of spodumene during grinding, reducing the amount of sludge competing with reagents for floatation during flotation, thereby improving the flotation efficiency of spodumene and ultimately increasing the lithium recovery rate.

[0017] 2. Because existing technologies only use a single flotation process, the middlings from the beneficiation process significantly interfere with the flotation. Middlings refer to the intermediate products obtained during the beneficiation process, and the useful content of middlings is generally between that of concentrate and tailings. Therefore, this invention employs a two-stage flotation process. The first stage of flotation quickly floats out the easily floatable lithium rough concentrate I, and the first roughing stage directly produces the product. The second stage of flotation floats out the difficult-to-benefit lithium rough concentrate II, and an activator is added to enhance the collection, thereby reducing middlings recycling and improving the lithium recovery rate.

[0018] 3. This invention adds a combined collector of saponified oleic acid and diesel oil to the flotation process. Because both saponified oleic acid and diesel oil contain mixed acids such as resin acids and higher fatty acids, they undergo hydrolysis reactions in alkaline pulp containing NaOH to generate a series of fatty acid sodium salts with good collection effects on lithium minerals. Different alkyl fatty acid sodium salts act on the surface of different types of lithium minerals, thereby achieving effective flotation recovery of mixed lithium minerals and improving the lithium recovery rate.

[0019] 4. The lithium rough concentrate III produced by the flotation combination of the present invention adopts a combined magnetic separation process of first weak magnetic separation followed by high gradient strong magnetic separation, which can not only reduce the iron content in the concentrate, but also improve the grade of lithium concentrate, and its recovery rate is maintained at over 98%.

[0020] 5. In the gravity separation recovery of magnetic separation tailings, the present invention adopts a spiral chute for pre-enrichment of tantalum-niobium-rubidium rough concentrate, and then combines it with shaking table for classification separation, which effectively reduces the number of shaking tables used. Attached Figure Description

[0021] Figure 1 This is a complete flow diagram of a mineral processing method for a polymetallic lithium ore containing tantalum, niobium, and rubidium according to the present invention. Detailed Implementation

[0022] The present invention will be further described in detail below with reference to the embodiments, but the implementation of the present invention is not limited to the scope shown in the embodiments. Example 1:

[0023] This embodiment uses a domestic pegmatite lithium deposit containing 2.52% Li2O, 219 g / t Ta2O5, 53 g / t Nb2O5, and 0.44% Rb. The main lithium-bearing minerals are spodumene, lepidolite, and lepidolite, while the main tantalum and niobium minerals are columbite and tantalite. Rubidium does not exist as a standalone mineral but is mainly found in lepidolite and lepidolite. The main gangue minerals are quartz, potassium feldspar, and sodium feldspar.

[0024] like Figure 1 As shown, a beneficiation method for a tantalum-niobium-rubidium polymetallic lithium ore includes the following steps: (1) Crushing and grinding: The lithium ore is first crushed and ground to a content of 97% for -0.2mm, of which -0.074mm accounts for 70.01%; (2) Slurry preparation: Add NaOH and Na2CO3 as adjusters to the crushed and ground ore particles at a rate of 741 g / t of raw ore, adjust the slurry to pH 12 and mechanically stir for 10 min, and the slurry mass concentration is 35%; (3) First stage flotation: The slurry after conditioning is added to the flotation machine, and the easy-to-select lithium crude concentrate I is floated out by first roughing I. That is, NaOH 741g / t·feed is added to the slurry in sequence and stirred for 10min; Na2CO3 741g / t·feed is stirred for 10min; calcium lignosulfonate 740g / t·feed is stirred for 5min; saponified oleic acid 463g / t·feed is stirred for 3min; the foam that is enriched and floated is the lithium crude concentrate I. (4) Two-stage flotation, including: ① Roughing II: Add NaOH 185g / t·feed to the remaining slurry after the first flotation stage, stirring for 5 min; Na2CO3 185g / t·feed, stirring for 5 min; calcium lignosulfonate 185g / t·feed, stirring for 5 min; NaClO 400g / t·feed, stirring for 5 min; saponified oleic acid 370g / t·feed; diesel oil 71g / t·feed, stirring for 3 min; enrich the resulting foam; ② Fine Selection I: Add 110g / t NaClO to the remaining slurry after roughing II, stir for 3min; enrich the resulting foam; ③Selection II: Add 110g / t NaClO to the remaining slurry after Selection I and stir for 3 minutes; enrich the resulting foam; ④ Scavenging I: Add NaClO 110g / t·feed to the remaining slurry after cleaning II, and stir for 3 min; saponified oleic acid 140g / t·feed, and stir for 2 min; diesel oil 27g / t·feed, and stir for 2 min; enrich the resulting foam; ⑤ Scavenging II: Add NaClO 185g / t·feed to the remaining slurry after scavenging I, and stir for 3 min; saponified oleic acid 93g / t·feed, and stir for 2 min; diesel oil 18g / t·feed, and stir for 2 min; enrich the resulting foam, and the remainder is the flotation tailings; The foams enriched in ①~⑤ are combined to obtain lithium crude concentrate II; (5) Combine lithium crude concentrate I and lithium crude concentrate II to obtain lithium crude concentrate III; (6) The lithium crude concentrate III was added to the magnetic separator. First, a weak magnetic separation of 0.35T was used, followed by a high gradient strong magnetic separation of 1.2T. After separation, lithium concentrate was obtained. The lithium concentrate contained 8.09% Li2O and the recovery rate was 69.73%. (7) Add the flotation tailings into a magnetic separator and use a weak magnetic separation of 0.35T to obtain magnetite and magnetic tailings; (8) The magnetic separation tailings are added to a φ900 spiral sluice for roughing III, with a feed concentration of 25%, a feed rate of 300 kg / h, and a water feed rate of 1490 kg / h, to obtain roughing concentrate and roughing tailings; the roughing tailings are then further scavenged using a spiral sluice, with a feed concentration of 25%, a feed rate of 300 kg / h, and a water feed rate of 1490 kg / h, to obtain scavenging concentrate and spiral sluice tailings; the roughing concentrate and scavenging concentrate are then combined to obtain tantalum-niobium-rubidium rough concentrate; (9) The tantalum, niobium and rubidium rough concentrates were divided into three particle sizes: +0.15 mm, 0.15 to +0.074 mm and -0.074 mm. The three sizes were separated by shaking table separation. Finally, the tantalum concentrate contained 5615.72 g / t of tantalum, the niobium concentrate contained 1519.06 g / t of niobium and the rubidium concentrate contained 3.56% of rubidium. Example 2:

[0025] This embodiment uses a domestic pegmatite lithium deposit containing 0.52% Li2O, 91 g / t Ta2O5, 12 g / t Nb2O5, and 0.13% Rb. The main lithium-bearing minerals are spodumene, lepidolite, and lepidolite, while the tantalum and niobium minerals are mainly columbite and tantalite. Rubidium does not exist as a standalone mineral but is mainly found in lepidolite and lepidolite. The main gangue minerals are quartz, potassium feldspar, and sodium feldspar.

[0026] like Figure 1 As shown, a beneficiation method for a tantalum-niobium-rubidium polymetallic lithium ore includes the following steps: (1) Crushing and grinding: The lithium ore is first crushed and ground to a content of 95% for -0.2mm, of which -0.074mm accounts for 72%; (2) Slurry preparation: Add NaOH and Na2CO3 as adjusters to the crushed and ground ore particles at a rate of 540 g / t of raw ore, adjust the slurry to pH 12 and mechanically stir for 10 min, and the slurry mass concentration is 35%; (3) First stage flotation: The slurry after conditioning is added to the flotation machine, and the easy-to-select lithium rough concentrate I is floated out by first roughing I. That is, NaOH 540g / t·feed is added to the slurry in sequence and stirred for 10min; Na2CO3 540g / t·feed is stirred for 10min; calcium lignosulfonate 650g / t·feed is stirred for 5min; saponified oleic acid 400g / t·feed is stirred for 5min; the enriched and floated foam is the lithium rough concentrate I. (4) Two-stage flotation, including: ① Roughing II: Add NaOH 185g / t·feed to the remaining slurry after the first stage of flotation, stirring for 5 min; Na2CO3 185g / t·feed, stirring for 5 min; calcium lignosulfonate 120g / t·feed, stirring for 5 min; NaClO 300g / t·feed, stirring for 5 min; saponified oleic acid 370g / t·feed; diesel oil 60g / t·feed, stirring for 3 min; enrich the resulting froth; ② Fine Selection I: Add 100g / t NaClO to the remaining slurry after roughing II and stir for 3 minutes; enrich the resulting foam; ③Selection II: Add 100g / t NaClO to the remaining slurry after Selection I and stir for 3 minutes; enrich the resulting foam; ④ Scavenging I: Add NaClO 110g / t·feed to the remaining slurry after cleaning II, and stir for 3 min; saponified oleic acid 140g / t·feed, and stir for 2 min; diesel oil 27g / t·feed, and stir for 2 min; enrich the resulting foam; ⑤ Scavenging II: Add NaClO 185g / t·feed to the remaining slurry after scavenging I, and stir for 3 min; saponified oleic acid 93g / t·feed, and stir for 2 min; diesel oil 18g / t·feed, and stir for 2 min; enrich the resulting foam, and the remainder is the flotation tailings; The foams enriched in ①~⑤ are combined to obtain lithium crude concentrate II; (5) Combine lithium crude concentrate I and lithium crude concentrate II to obtain lithium crude concentrate III; (6) The lithium crude concentrate III was added to the magnetic separator. First, a weak magnetic separation of 0.35T was used, followed by a high gradient strong magnetic separation of 0.9T. After separation, lithium concentrate was obtained. The lithium concentrate contained 6.65% Li2O and the recovery rate was 69.55%. (7) Add the flotation tailings into a magnetic separator and use a weak magnetic separation of 0.35T to obtain magnetite and magnetic tailings; (8) The magnetic separation tailings are added to a φ900 spiral sluice for roughing III, with a feed concentration of 25%, a feed rate of 300 kg / h, and a water feed rate of 1490 kg / h, to obtain roughing concentrate and roughing tailings; the roughing tailings are then further scavenged using a spiral sluice, with a feed concentration of 25%, a feed rate of 300 kg / h, and a water feed rate of 1490 kg / h, to obtain scavenging concentrate and spiral sluice tailings; the roughing concentrate and scavenging concentrate are then combined to obtain tantalum-niobium-rubidium rough concentrate; (9) The tantalum, niobium and rubidium rough concentrates were divided into three particle sizes: +0.15 mm, 0.15 to +0.074 mm and -0.074 mm. The three sizes were separated by shaking table separation. Finally, the tantalum concentrate contained 3615.49 g / t of tantalum, the niobium concentrate contained 1019.06 g / t of niobium and the rubidium concentrate contained 1.27% of rubidium. Example 3:

[0027] This embodiment uses a domestic pegmatite lithium deposit containing 1.52% Li2O, 119 g / t Ta2O5, 23 g / t Nb2O5, and 0.23% Rb. The main lithium-bearing minerals are spodumene, lepidolite, and lepidolite, while the main tantalum and niobium minerals are columbite and tantalite. Rubidium does not exist as a standalone mineral but is mainly found in lepidolite and lepidolite. The main gangue minerals are quartz, potassium feldspar, and sodium feldspar.

[0028] like Figure 1 As shown, a beneficiation method for a tantalum-niobium-rubidium polymetallic lithium ore includes the following steps: (1) Crushing and grinding: The lithium ore is first crushed and ground to a content of 95% for -0.2mm, of which -0.074mm accounts for 72%; (2) Slurry preparation: Add NaOH and Na2CO3 as adjusters to the crushed and ground ore particles at a rate of 540 g / t of raw ore, adjust the slurry to pH 12 and mechanically stir for 10 min, and the slurry mass concentration is 35%; (3) First stage flotation: The slurry after conditioning is added to the flotation machine, and the easy-to-select lithium rough concentrate I is floated out by first roughing I. That is, NaOH 540g / t·feed is added to the slurry in sequence and stirred for 10min; Na2CO3 540g / t·feed is stirred for 10min; calcium lignosulfonate 500g / t·feed is stirred for 5min; saponified oleic acid 400g / t·feed is stirred for 5min; the enriched and floated foam is the lithium rough concentrate I. (4) Two-stage flotation, including: ① Roughing II: Add NaOH 185g / t·feed to the remaining slurry after the first flotation stage, stirring for 5 min; Na2CO3 185g / t·feed, stirring for 5 min; calcium lignosulfonate 120g / t·feed, stirring for 5 min; NaClO 200g / t·feed, stirring for 5 min; saponified oleic acid 370g / t·feed; diesel oil 60g / t·feed, stirring for 3 min; enrich the resulting froth; ② Fine Selection I: Add 100g / t NaClO to the remaining slurry after roughing II and stir for 3 minutes; enrich the resulting foam; ③Selection II: Add 100g / t NaClO to the remaining slurry after Selection I and stir for 3 minutes; enrich the resulting foam; ④ Scavenging I: Add NaClO 110g / t·feed to the remaining slurry after cleaning II, and stir for 3 min; saponified oleic acid 140g / t·feed, and stir for 2 min; diesel oil 27g / t·feed, and stir for 2 min; enrich the resulting foam; ⑤ Scavenging II: Add NaClO 185g / t·feed to the remaining slurry after scavenging I, and stir for 3 min; saponified oleic acid 93g / t·feed, and stir for 2 min; diesel oil 15g / t·feed, and stir for 2 min; enrich the resulting foam, and the remainder is the flotation tailings; The foams enriched in ①~⑤ are combined to obtain lithium crude concentrate II; (5) Combine lithium crude concentrate I and lithium crude concentrate II to obtain lithium crude concentrate III; (6) The lithium crude concentrate III was added to the magnetic separator. First, a weak magnetic separation of 0.35T was used, followed by a high gradient strong magnetic separation of 0.9T. After separation, lithium concentrate was obtained. The lithium concentrate contained 6.68% Li2O and the recovery rate was 68.55%. (7) Add the flotation tailings into a magnetic separator and use a weak magnetic separation of 0.35T to obtain magnetite and magnetic tailings; (8) The magnetic separation tailings are added to a φ900 spiral sluice for roughing III, with a feed concentration of 25%, a feed rate of 300 kg / h, and a water feed rate of 1490 kg / h, to obtain roughing concentrate and roughing tailings; the roughing tailings are then further scavenged using a spiral sluice, with a feed concentration of 25%, a feed rate of 300 kg / h, and a water feed rate of 1490 kg / h, to obtain scavenging concentrate and spiral sluice tailings; the roughing concentrate and scavenging concentrate are then combined to obtain tantalum-niobium-rubidium rough concentrate; (9) The tantalum, niobium and rubidium rough concentrates were divided into three particle sizes: +0.15 mm, 0.15 to +0.074 mm and -0.074 mm. The three sizes were separated by shaking table separation. Finally, the tantalum concentrate contained 3615.49 g / t of tantalum, the niobium concentrate contained 1019.06 g / t of niobium and the rubidium concentrate contained 1.27% of rubidium.

[0029] In the mineral processing industry, roughing refers to the process of separating clay, impurities, gangue, etc., from the raw ore through a single beneficiation process, resulting in a concentrate product with a higher grade than the original ore, called rough concentrate. This concentrate usually does not yet meet the required fines grade; this process is called roughing operation. Scavenging refers to the process where the tailings from roughing are not yet considered final waste tailings and generally require further processing; this process is called scavenging operation. Cleaning refers to the secondary beneficiation of the concentrate from roughing to obtain a qualified fines product; this process is called mineral processing cleaning operation. Sometimes, the rough concentrate needs to undergo multiple cleaning operations to obtain a qualified fines product; these operations are successively called primary cleaning, secondary cleaning, tertiary cleaning, etc., until the required fines grade is achieved. After the ore has undergone beneficiation, most of the gangue and impurities have been removed, resulting in a concentration of valuable minerals; the product is called concentrate. Concentrate is the final product of a mineral processing plant and is generally used as a raw material for smelting. The final concentrate must meet national standards for its main components and impurity content to be considered a qualified concentrate. After the raw ore undergoes beneficiation, its main components are concentrated in the concentrate. In some cases, after comprehensive processing, minor components or other associated metals are also recovered. Therefore, the remaining product contains very low levels of useful components; this portion is called tailings, or final tailings. It should be noted that tailings still contain useful components that are difficult to extract due to current technological limitations, but may potentially become reused raw materials in the future. Therefore, tailings are generally stored in tailings ponds. The intermediate product obtained during the beneficiation process is called middlings; the useful component content of middlings generally falls between that of the concentrate and the tailings.

[0030] The above embodiments are merely specific examples to further illustrate the purpose, technical solution, and beneficial effects of the present invention, and the present invention is not limited thereto. Any modifications, equivalent substitutions, improvements, etc., made within the scope of the disclosure of the present invention are included within the protection scope of the present invention.

Claims

1. A beneficiation method for a polymetallic lithium ore containing tantalum, niobium, and rubidium, characterized in that, Includes the following steps: (1) The lithium ore is crushed, ground and slurry-treated sequentially to obtain a slurry; the slurry-treatment involves adding NaOH and Na2CO3 as adjusters to the crushed and ground ore particles, wherein the NaOH and Na2CO3 are added in a mass ratio of 1:1; the pH value of the slurry is 11-13 and the mass concentration of the slurry is 35%-40%; (2) The slurry is subjected to mineral flotation operation in two stages. The first stage flotation uses one roughing I to float out the easily soluble lithium crude concentrate I. The second stage flotation uses one roughing II, two cleaning and two scavenging processes to float out the difficult-to-dissolve lithium crude concentrate II. The lithium crude concentrate I and lithium crude concentrate II are combined to obtain lithium crude concentrate III. The last residue after flotation is the flotation tailings. The roughing process (I) involves adding reagents in the following order and stirring: NaOH 500g / t·feed to 800g / t·feed, stirring for 5min to 10min; Na2CO3 500g / t·feed to 800g / t·feed, stirring for 5min to 10min; calcium lignosulfonate 500g / t·feed to 800g / t·feed, stirring for 5min to 10min; saponified oleic acid 400g / t·feed to 500g / t·feed, stirring for 3min to 5min. The roughing process II involves adding reagents in the following order and stirring: NaOH 100g / t·feed to 200g / t·feed, stirring for 5min to 10min; Na2CO3 100g / t·feed to 200g / t·feed, stirring for 5min to 10min; calcium lignosulfonate 100g / t·feed to 200g / t·feed, stirring for 5min to 10min; NaClO 200g / t·feed to 400g / t·feed, stirring for 5min to 10min; saponified oleic acid and diesel oil, wherein saponified oleic acid 300g / t·feed to 400g / t·feed and diesel oil 60g / t·feed to 100g / t·feed, stirring for 3min to 5min; The two selections include Selection I and Selection II: The reagent added in the refined section I is NaClO, and the addition amount is 100g / t·feed to 200g / t·feed, and the mixture is stirred for 3min to 5min. The reagent added in the refined II section is NaClO, with an addition amount of 100g / t·feed to 200g / t·feed, and stirring for 3min to 5min; The two scanning processes include Scan I and Scan II: In the first scavenging process, first add 100g / t·feed to 200g / t·feed of NaClO and 100g / t·feed to 200g / t·feed of saponified oleic acid, and then stir for 3min to 5min; then add 15g / t·feed to 30g / t·feed of diesel oil and stir for 2min to 3min. In the second scavenging process, first add 100g / t·feed to 200g / t·feed and stir for 3min to 5min; then add 50g / t·feed to 100g / t·feed of saponified oleic acid and stir for 2min to 3min; then add 15g / t·feed to 30g / t·feed of diesel oil and stir for 2min to 3min. (3) The lithium crude concentrate III from step (2) is subjected to magnetic separation to remove iron by first weak magnetic separation and then high gradient strong magnetic separation to obtain lithium concentrate; (4) The flotation tailings from step (2) are separated by weak magnetic separation to obtain magnetite and magnetic tailings; (5) After the magnetic separation tailings obtained in step (4) are subjected to roughing III and scavenging in sequence by spiral sluice, tantalum-niobium-rubidium rough concentrate and spiral sluice tailings are obtained. (6) The tantalum-niobium-rubidium rough concentrate from step (5) is classified and separated by a shaking table to obtain a tantalum-niobium-rubidium mixed concentrate.

2. The beneficiation method for a tantalum-niobium-rubidium polymetallic lithium ore according to claim 1, characterized in that: The lithium ore is crushed and ground to a particle size of -0.2mm with a content greater than 95%, of which -0.074mm accounts for 70% to 75%.

3. The beneficiation method for a tantalum-niobium-rubidium polymetallic lithium ore according to claim 1, characterized in that: The magnetic field strength of the weak magnet is 0.35T, and the magnetic field strength of the high gradient strong magnet is 0.9 to 1.2T.

4. The beneficiation method for a tantalum-niobium-rubidium polymetallic lithium ore according to claim 1, characterized in that: In step (5), both roughing and scavenging in the spiral chute are carried out under the conditions of a feed concentration of 20% to 25%, a feed rate of 200 kg / h to 300 kg / h, and a water supply of 1500 kg / h to 1600 kg / h.

5. The beneficiation method for a tantalum-niobium-rubidium polymetallic lithium ore according to claim 1, characterized in that: The shaking table is used for grading and separating particles into three sizes: +0.15mm, 0.15 to +0.074mm, and -0.074mm. The shaking table stroke is 8 to 14 mm, the number of strokes is 300 to 400 r / min, the transverse slope of the table surface is 1°30″ to 3°30″, the feed concentration is 15% to 25%, and the washing water volume is 15 t / table·d to 30 t / table·d.

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