Efficient recovery system for valuable components of complex low-grade platinum-palladium-oxygen-sulfur mixed ore

Abstract

The utility model relates to an efficient recovery system for valuable components of complex low-grade platinum-palladium-oxygen-sulfur mixed ore, which comprises a coarse-grinding ball mill and a fine-grinding ball mill, discharge ports of the coarse-grinding ball mill and the fine-grinding ball mill are both connected to a feed port of an ore pulp pump pool, and a discharge port of the ore pulp pump pool is connected to a feed port of a classification cyclone through an ore pulp pump. A sand settling opening of the grading cyclone is connected to a feeding opening of the fine grinding ball mill; an overflow port of the grading cyclone is connected to a feeding port of the flotation system, a tailing discharging port of the flotation system is connected to a feeding port of the 1 # pulse high-gradient magnetic separator, and the flotation system and a concentrate discharging port of the 1 # pulse high-gradient magnetic separator are sequentially connected to the smelting furnace, the converting furnace, the cooling furnace, the fine grinding vertical mill and the 2 # pulse high-gradient magnetic separator. The device has a remarkable efficient recovery effect on the valuable components of the complex low-grade platinum-palladium-oxygen-sulfur mixed ore, the recovery rates of the valuable components such as platinum, palladium, gold, silver, copper and nickel are all more than 60%, and the recovery benefits are good.

Description

Technical Field

[0001] The utility model belongs to the technical field of precious metal metallurgy, and in particular relates to a system for efficiently recovering valuable components of a complex low-grade platinum-palladium oxygen-sulfur mixed ore. Background Art

[0002] These complex, low-grade platinum-palladium ores have a complex structure and composition. Gangue minerals, such as serpentine and pyroxene, are prone to mudification and good floatability, making separation difficult. Furthermore, these ores often undergo shallow alteration at various locations. Simultaneously with shallow alteration of the sulfide ore, the surrounding rock also undergoes alteration, leading to talcification, chloritization, and silicification of the gangue minerals and the precipitation of large amounts of water-soluble salts, further complicating process control. Currently, sulfide ores are being enriched using traditional flotation processes, followed by roasting and leaching using conventional or fully wet leaching systems. However, due to the high floatability and mudification of the gangue minerals, the resulting flotation product grade and recovery rate are low, resulting in large amounts of metallurgical slag, high production costs, and low overall recovery rates. Alternatively, oxide ores are directly leached using fully wet metallurgical systems, but this results in low overall recovery rates, high production costs, environmental pollution, and poor safety and controllability. Overall, these mines remain stagnant, hindering the effective development and utilization of resources.

[0003] In summary, current R&D process systems either focus on complex precious metal recovery while neglecting the recovery of lean copper and nickel, or simply recover lean copper and nickel while making recovery of the main precious metals difficult and resulting in high production costs. Traditional pyrometallurgical processes neglect precious metal recovery, resulting in ineffective resource recovery and significant waste. Therefore, finding a scientific and rational recovery process system has become a pressing technical challenge for the industry.

[0004] Based on the existing defects and deficiencies, the utility model provides a high-efficiency recovery system for valuable components of complex low-grade platinum-palladium ores with scientific and reasonable process, appropriate production cost and strong adaptability, which promotes the effective comprehensive utilization of resources and improves the economic and social benefits of the enterprise. Utility Model Content

[0005] In response to the above problems, the utility model provides an efficient recovery system for valuable components of complex low-grade platinum-palladium oxygen-sulfur mixed ores, which adopts a comprehensive resource recovery method of multi-stage quality improvement in the classification stage, efficient separation, separate refining, and closed-loop circulation treatment.

[0006] The specific technical solution is: a complex low-grade platinum palladium oxygen-sulfur mixed ore valuable component efficient recovery system, including a coarse grinding ball mill and a fine grinding ball mill, the coarse grinding ball mill and the fine grinding ball mill discharge port are connected to the slurry pump pool feed port, the slurry pump pool discharge port is connected to the classifying cyclone feed port through the slurry pump, the classifying cyclone sand settling port is connected to the fine grinding ball mill feed port; the classifying cyclone overflow port is connected to the flotation system feed port, the flotation system tailings discharge port is connected to the 1# pulse high gradient magnetic separator feed port, the flotation system and the 1# pulse high gradient magnetic separator concentrate discharge port are sequentially connected to the smelting furnace , blowing furnace, cooling furnace, fine grinding vertical mill and 2# pulse high gradient magnetic separator, the concentrate discharge port of the 2# pulse high gradient magnetic separator is connected to the feed port of the mixed gold acid leaching system, the leaching outlet of the mixed gold acid leaching system is connected to the feed port of the filter, the filtrate port of the filter is connected to the feed port of the crystallization system, the crystallization discharge port of the crystallization system is connected to the nickel refining system, the tailings discharge port of the 2# pulse high gradient magnetic separator is connected to the feed port of the copper sulfide priority flotation system, the concentrate discharge port of the copper sulfide priority flotation system is connected to the copper refining system, and the tailings discharge port of the copper sulfide priority flotation system is connected to the nickel refining system.

[0007] Furthermore, preferably, the magnetic induction intensity of the 1# pulse high gradient magnetic separator is 900-1200 mT and the pulse intensity is 200-300 times / min.

[0008] Furthermore, preferably, the induction intensity of the 2# pulse high gradient magnetic separator is 200-300 mT and the pulse intensity is 200-300 times / min.

[0009] Beneficial effects of the utility model: The utility model has a significant effect on the efficient recovery of valuable components in complex low-grade platinum-palladium oxygen-sulfur mixed ores. The recovery rate of valuable components such as platinum, palladium, gold, silver, copper, and nickel is above 60%, with good recovery efficiency. The process system is stable and highly adaptable, and is of great significance for the comprehensive utilization of low-grade platinum-palladium mineral resources with poor copper and nickel. The beneficial effects of each process system are as follows:

[0010] (1) The utility model first adopts a low-concentration coarse grinding-classification-fine grinding closed-circuit circulation system to separate materials with relatively uniform particle size for a flotation, thereby avoiding the over-grinding of easy-to-grind and easy-to-float impurity ores that affects the flotation index; then, high-grade platinum palladium concentrate and low-grade platinum palladium iron concentrate are separated through low-concentration flotation-pulse high-gradient magnetic separation to ensure that the concentrate is fully recovered.

[0011] (2) The present invention uses a cooling furnace to cool the bottom matte liquid obtained from blowing in stages, thereby forming a mineral complex with a differentiated structure. For example, the sulfide single crystal has a large particle size and an appropriate yield of gold. This effectively avoids the formation of mixed crystals and creates favorable conditions for subsequent separation. The differentiated ore is then subjected to a fine grinding-pulse high gradient magnetic separation-preferential copper flotation separation system, effectively improving the separation effect and recovery rate of platinum, palladium, copper, and nickel.

[0012] (3) For the separated gold and silver-containing copper sulfide concentrates and nickel-cobalt sulfide concentrates, a large amount of waste is discarded according to their material properties by a combination of physical and chemical methods, so that the valuable components are efficiently enriched. Then, they are re-separated and refined separately using different refining systems, which greatly reduces the processing volume in the high-energy consumption stage and reduces the production cost. At the same time, a higher comprehensive recovery rate is obtained, so that the low-grade platinum and palladium mineral resources with poor copper and nickel are effectively and comprehensively utilized. BRIEF DESCRIPTION OF THE DRAWINGS

[0013] Figure 1 It is the equipment association diagram of the utility model;

[0014] In the figure: 1- coarse grinding ball mill, 2- fine grinding ball mill, 3- slurry pump pool, 4- slurry pump, 5- classifying cyclone, 6- flotation system, 7- 1# pulse high gradient magnetic separator, 8- smelting furnace, 9- blowing furnace, 10- cooling furnace, 11- fine grinding vertical mill, 12- 2# pulse high gradient magnetic separator, 13- copper sulfide preferential flotation system, 14- copper refining system, 15- alloy gold acid leaching system, 16- filter, 17- crystallization system, 18- nickel refining system. DETAILED DESCRIPTION

[0015] In order to make the technical problems and technical solutions solved by the present invention more clearly understood, the present invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are only used to explain the present invention and are not intended to limit the present invention.

[0016] In the description of the present invention, it should be understood that the terms "longitudinal", "transverse", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside", etc., indicating the orientation or position relationship, are based on the orientation or position relationship shown in the accompanying drawings, and are only for the convenience of describing the present invention, and do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation. Therefore, they should not be understood as limitations on the present invention.

[0017] It should also be noted that, in the description of this utility model, unless otherwise expressly specified or limited, the terms "disposed," "installed," and "connected" should be understood in a broad sense. For example, they may refer to fixed connections, detachable connections, or integral connections; mechanical connections, electrical connections; direct connections, indirect connections through an intermediate medium, and internal connections between two components. Those skilled in the art will understand the specific meanings of these terms in this utility model based on the specific circumstances.

[0018] like Figure 1 As shown, the present application provides a complex low-grade platinum palladium oxygen-sulfur mixed ore valuable component efficient recovery system, including a coarse grinding ball mill 1 and a fine grinding ball mill 2, the discharge ports of the coarse grinding ball mill 1 and the fine grinding ball mill 2 are both connected to the feed port of the slurry pump pool 3, the discharge port of the slurry pump pool 3 is connected to the feed port of the classifying cyclone 5 through the slurry pump 4, and the sand settling port of the classifying cyclone 5 is connected to the feed port of the fine grinding ball mill 2; the overflow port of the classifying cyclone 5 is connected to the feed port of the flotation system 6, the tailings discharge port of the flotation system 6 is connected to the feed port of the 1# pulse high gradient magnetic separator 7, and the concentrate discharge ports of the flotation system 6 and the 1# pulse high gradient magnetic separator 7 are sequentially connected to the smelting furnace 8, the blowing furnace 9, the reducing furnace 10, and the reducing furnace 11. The warm cooling furnace 10, the fine grinding vertical mill 11 and the 2# pulse high gradient magnetic separator 12, the concentrate discharge port of the 2# pulse high gradient magnetic separator 12 is connected to the feed port of the gold alloy acid leaching system 15, the leaching outlet of the gold alloy acid leaching system 15 is connected to the feed port of the filter 16, the filtrate port of the filter 16 is connected to the feed port of the crystallization system 17, the crystallization discharge port of the crystallization system 17 is connected to the nickel refining system 18, the tailings discharge port of the 2# pulse high gradient magnetic separator 12 is connected to the feed port of the copper sulfide priority flotation system 13, the concentrate discharge port of the copper sulfide priority flotation system 13 is connected to the copper refining system 14, and the tailings discharge port of the copper sulfide priority flotation system 13 is connected to the nickel refining system 18.

[0019] The magnetic induction intensity of the aforementioned #1 pulse high gradient magnetic separator 7 is 900-1200 mT, with a pulse intensity of 200-300 cycles / min; the magnetic induction intensity of the #2 pulse high gradient magnetic separator 12 is 200-300 mT, with a pulse intensity of 200-300 cycles / min. Furthermore, the aforementioned equipment is existing equipment, and this application only relates to the use of these existing equipment and does not involve improvements to these equipment.

[0020] Working principle: The complex low-grade platinum-palladium oxygen-sulfur mixed ore to be processed is added to the coarse grinding ball mill 1 for preliminary crushing. The crushed ore pulp enters the slurry pump pool 3 for slurry adjustment and is then transported by the slurry pump 4 to the classifying cyclone 5 for classification. Among them, the ore with a diameter of -0.074 mm is transferred from the overflow port of the classifying cyclone 5 to the flotation system 6 for flotation, and the ore with a diameter of +0.074 mm is returned from the sand settling port of the classifying cyclone 5 to the fine grinding ball mill 2 for re-crushing. After crushing, it circulates to the classifying cyclone 5 for classification again until the ore pulp with a diameter of -0.074 mm, which accounts for 80% to 90%, is separated and transferred to the flotation system 6.

[0021] The slurry entering the flotation system 6 is floated to obtain platinum palladium concentrate and flotation tailings, wherein the flotation tailings are transported to the 1# pulse high gradient magnetic separator 7 for magnetic separation, thereby magnetically separating the low-grade platinum palladium iron concentrate in the flotation tailings, and the magnetic tailings are transported to the tailings pond for storage.

[0022] The platinum-palladium concentrate obtained by flotation and the platinum-palladium-iron concentrate obtained by magnetic separation are then transported to the smelting furnace 8, mixed with additives (lime, coal powder) for slag smelting, and then transferred to the blowing furnace 9 for blowing after deslagging. Silica and lump coal additives are added during blowing. After blowing, matte liquid and iron silicate are obtained.

[0023] The precipitated matte liquid is then transported to a cooling furnace 10 for staged heat preservation and cooling to form differentiated structural sulfide ore. It is then transported to a fine grinding vertical mill 12 for fine grinding to -0.043mm, accounting for 75% to 80%, and then transported to a 2# pulse high gradient magnetic separator 12 for magnetic separation. The magnetically separated gold (platinum, palladium, gold, copper, nickel, and iron) is transferred to a gold acid leaching system 15 for acid leaching. After acid leaching, it is filtered through a filter 16 to obtain gold (platinum, palladium, gold, copper) and a filtrate. The filtrate is transported to a crystallization system 17 where nickel carbonate is first added to remove iron. After iron removal and filtration, the mother liquor is then subjected to nickel sulfate crystallization to obtain nickel sulfate crystals and nickel sulfate crystallization mother liquor (recycled).

[0024] However, the tailings magnetically separated by the 2# pulse high gradient magnetic separator 12 enter the copper sulfide preferential flotation system 13, and flotation is performed to obtain silver-containing copper sulfide concentrate and nickel-cobalt sulfide concentrate.

[0025] Finally, the silver-containing copper sulfide concentrate obtained by flotation is transported to the copper refining system 14, and is smelted in an electric furnace, blown in a Kaldo furnace, and refined in an anode furnace to obtain copper anode plates, which are then sent to the copper electrolysis process for electrolysis to obtain copper cathode plates and silver-containing anode mud. The nickel-cobalt sulfide concentrate obtained by flotation is quenched with high-temperature water, dissolved with concentrated hydrochloric acid, filtered, and crystallized to obtain nickel chloride crystals and crystallization mother liquor. The nickel chloride crystals and the nickel sulfate crystals obtained by crystallization are then transported to the nickel refining system 18, and cathode nickel, anode mud and cobalt slag products are obtained after electrolysis.

[0026] Additionally, the sulfur dioxide flue gas generated by each stage of the system can be removed through an electrostatic precipitator (ESP) and then mixed and proportioned to produce a mixed flue gas with a sulfur dioxide concentration of at least 8.0%. This mixed gas can then be transported to the acid plant for recycling in the production of sulfuric acid. Intermediate products from each stage of the system, if they contain a high concentration of mineral elements, can be returned to the smelting furnace for recycling. The small amount of elemental copper in the gold (platinum, palladium, gold, and copper) produced by the system can be separated and recovered through traditional precious metal smelting processes.

[0027] Application Example 1

[0028] Raw material 1#: A complex, low-grade platinum-palladium oxygen-sulfur mixed ore, with a 1:1 ratio of sulfide ore to oxide ore. The main elements and contents of the sulfide ore are: 1.00g / t platinum, 1.71g / t palladium, 0.02g / t gold, 0.12% copper, 0.16% nickel, 0.018% cobalt, 4g / t silver, and 8.19% iron. The main elements and contents of the oxide ore are: 0.61g / t platinum, 0.86g / t palladium, 0.01g / t gold, 0.06% copper, 0.14% nickel, 0.016% cobalt, 5g / t silver, and 10.42% iron.

[0029] The recovery system described in the utility model is used to recover the complex low-grade platinum-palladium oxygen-sulfur mixed ore. The specific treatment process is as follows:

[0030] (1) Pretreatment: Raw material 1# is transported to coarse grinding ball mill 1, classification cyclone 2, and fine grinding ball mill 3 for low-concentration cyclic crushing and classification until the classified particles of -0.074mm account for 80% to 90%. During this process, 1000g / t of sodium carbonate and 150g / t of sodium hexametaphosphate need to be added to coarse grinding ball mill 1. The grinding concentration of the two ball mills is controlled at 50% to 55%, and the classification concentration is 30% to 35%.

[0031] (2) Primary enrichment of useful components: The slurry after classification in step (1) is transported to the flotation system 6 for flotation. During the flotation process, 300 g / t of sodium hexametaphosphate inhibitor, 100 g / t of butyl xanthate + butyl ammonium black medicine collector, and 40 g / t of POC foaming agent are added to the flotation system to obtain platinum palladium concentrate and flotation tailings by flotation. The flotation tailings are then transported to the 1# pulse high gradient magnetic separator 7 for magnetic separation. The magnetic induction intensity of the magnetic separator is 900~1200 mT and the pulse intensity is 200~300 times / min. Low-grade platinum palladium iron concentrate and magnetic separation tailings are obtained by magnetic separation.

[0032] (3) Fire secondary enrichment: The platinum-palladium concentrate and low-grade platinum-palladium-iron concentrate obtained in step (2) are dried, mixed with lime and coal powder in a ratio of 4:1-5:1, and transferred to a smelting furnace 8 for slag smelting. After removing the scum, the product is transferred to a blowing furnace 9, and silicon dioxide and lump coal are added for blowing. After completion, a bottom matte liquid (iron content controlled to be 3.2%-3.4%, sulfur content to be 20%-25%) and iron silicate are obtained. In this process, the smelting temperature is 1300-1350°C, the blowing temperature is 1180-1300°C, the amount of smelting lime used is 20%-25% of the platinum-palladium concentrate, and the amount of blowing silicon dioxide used is 25%-30% of the smelting product.

[0033] (4) Differentiation ore production: The precipitated matte liquid obtained in step (3) is promptly transported to the cooling furnace 10 for staged heat preservation and cooling to obtain a differentiated structure matte ore; wherein, the specific operation of the heat preservation and cooling stage is to cool the temperature from 1180°C to 580°C for 2 to 3 days, to cool the temperature from 580°C to 520°C for 6 to 7 days, and to cool the temperature from 520°C to 370°C for 2 to 3 days.

[0034] (5) Separation of differentiated ores: The differentiated structure matte ore obtained in step (4) is transported to the fine grinding vertical mill 11 for fine grinding until it is -0.043 mm, accounting for 75% to 80%, and is further transported to the 2# pulse high gradient magnetic separator for magnetic separation. The magnetic separation obtains the gold (containing 15% to 20% copper, 50% to 55% nickel, and 1400 to 1500 g / t of palladium, platinum and gold) and magnetic tailings. The magnetic tailings are transferred to the copper sulfide preferential flotation system 13 for low-concentration separation to obtain silver-containing copper sulfide concentrate (containing copper ≥ 70%, nickel ≤ 5%, and silver ≥ 500 g / t) and nickel-cobalt sulfide concentrate (containing nickel ≥ 70%, and copper ≤ 0.5%). During this process, the magnetic induction intensity of the pulse high gradient magnetic separation is 200~300mT and the pulse intensity is 200~300 times / min; the copper sulfide preferential flotation system 13 adds lime to adjust the slurry pH to 12.2~12.6, and adds 50g / t of high-selectivity collector short-chain dithiosulfate and 30g / t of foaming agent isobutyl methanol.

[0035] (6) Separation of gold alloy: The gold alloy obtained in step (5) is subjected to acid leaching at normal pressure, filtration, precipitation, filtration, and crystallization. The gold alloy is first transported to the gold alloy acid leaching system 15 for acid leaching. After acid leaching, it is filtered through the filter 16 to obtain platinum-palladium gold alloy and filtrate. The filtrate is transported to the crystallization system 17, where nickel carbonate is first added to remove iron. After iron removal and filtration, the mother liquor is then crystallized with nickel sulfate to obtain nickel sulfate crystals and nickel sulfate crystallization mother liquor (recycled). In this process, the leaching conditions are controlled as follows: leaching pH is 1-2, leaching temperature is 75-85°C, liquid-solid ratio is 2:1-4:1, and leaching time is 2-3 hours; nickel carbonate is used to adjust the pH to 2.7-3.5 during iron removal.

[0036] (7) The by-products copper and nickel are refined separately: the silver-containing copper sulfide concentrate obtained in step (5) is transported to the copper refining system 14, smelted in an electric furnace, blown in a Kaldo furnace, and refined in an anode furnace to obtain a copper anode plate, which is then sent to the copper electrolysis process for electrolysis to obtain a copper cathode plate and a silver-containing anode mud; the nickel-cobalt sulfide concentrate obtained in step (5) is quenched with high-temperature water, dissolved with concentrated hydrochloric acid, filtered, and crystallized to obtain nickel chloride crystals and crystallization mother liquor, and then the nickel chloride crystals and the nickel sulfate crystals obtained in step (6) are transported to the nickel refining system 18, and cathode nickel, anode mud and cobalt slag products are obtained after electrolysis.

[0037] The above treatment process was applied to raw material 1#, and the test results were: platinum recovery rate was 80.87%, palladium recovery rate was 82.52%, gold recovery rate was 66.54%, silver recovery rate was 64.85%, copper recovery rate was 77.44%, and nickel recovery rate was 70.72%.

[0038] Application Example 2

[0039] Raw material 2#: A complex, low-grade platinum-palladium oxygen-sulfur mixed ore, with a sulfide ore to oxide ore ratio of 1.5:1. The main elements and contents of the sulfide ore are: 1.00g / t platinum, 1.71g / t palladium, 0.02g / t gold, 0.12% copper, 0.16% nickel, 0.018% cobalt, 4g / t silver, and 8.19% iron. The main elements and contents of the oxide ore are: 0.61g / t platinum, 0.86g / t palladium, 0.01g / t gold, 0.06% copper, 0.14% nickel, 0.016% cobalt, 5g / t silver, and 10.42% iron.

[0040] The treatment process described in Application Example 1 was applied to raw material 2#, and the test results were: platinum recovery rate was 81.35%, palladium recovery rate was 82.98%, gold recovery rate was 66.92%, silver recovery rate was 65.63%, copper recovery rate was 78.57%, and nickel recovery rate was 71.09%.

[0041] Application Example 3

[0042] Raw material 3#: A complex, low-grade platinum-palladium oxygen-sulfur mixed ore, with a sulfide ore to oxide ore ratio of 2:1. The main elements and contents of the sulfide ore are: 1.00g / t platinum, 1.71g / t palladium, 0.02g / t gold, 0.12% copper, 0.16% nickel, 0.018% cobalt, 4g / t silver, and 8.19% iron; the main elements and contents of the oxide ore are: 0.61g / t platinum, 0.86g / t palladium, 0.01g / t gold, 0.06% copper, 0.14% nickel, 0.016% cobalt, 5g / t silver, and 10.42% iron.

[0043] The treatment process described in Application Example 1 was applied to raw material 3#, and the test results were: platinum recovery rate was 79.59%, palladium recovery rate was 80.88%, gold recovery rate was 63.94%, silver recovery rate was 63.55%, copper recovery rate was 76.86%, and nickel recovery rate was 69.76%.

[0044] In summary, the utility model is used to treat complex low-grade platinum-palladium oxygen-sulfur mixed ores, and can effectively recover valuable metals in such ores, with a platinum recovery rate of about 80%, a palladium recovery rate of about 81%, a gold recovery rate of about 64%, a silver recovery rate of about 65%, a copper recovery rate of about 77%, and a nickel recovery rate of about 70%. The recovery efficiency is good, the process system is stable and has strong adaptability, and it is of great significance to the comprehensive utilization of copper-nickel-poor low-grade platinum-palladium mineral resources.

[0045] The present invention is described in detail above through specific and preferred embodiments, but those skilled in the art should understand that the present invention is not limited to the embodiments described above. Any modifications, equivalent substitutions, etc. made within the spirit and principles of the present invention should be included in the scope of protection of the present invention.

Claims

1. A system for efficiently recovering valuable components from complex low-grade platinum-palladium oxygen-sulfur mixed ores, characterized in that: The invention comprises a coarse grinding ball mill (1) and a fine grinding ball mill (2), wherein the discharge ports of the coarse grinding ball mill (1) and the fine grinding ball mill (2) are both connected to the feed port of a slurry pump pool (3), the discharge port of the slurry pump pool (3) is connected to the feed port of a grading cyclone (5) through a slurry pump (4), and the sand settling port of the grading cyclone (5) is connected to the feed port of the fine grinding ball mill (2); the overflow port of the grading cyclone (5) is connected to the feed port of a flotation system (6), the tailings discharge port of the flotation system (6) is connected to the feed port of a 1# pulse high gradient magnetic separator (7), and the concentrate discharge ports of the flotation system (6) and the 1# pulse high gradient magnetic separator (7) are both connected in sequence to a smelting furnace (8), a blowing furnace (9), a cooling furnace (10), a fine grinding vertical mill (11), and a smelting furnace (8). ) and a 2# pulse high gradient magnetic separator (12), the concentrate discharge port of the 2# pulse high gradient magnetic separator (12) is connected to the feed port of the gold-rich acid leaching system (15), the leaching outlet of the gold-rich acid leaching system (15) is connected to the feed port of the filter (16), the filtrate port of the filter (16) is connected to the feed port of the crystallization system (17), the crystallization discharge port of the crystallization system (17) is connected to the nickel refining system (18), the tailings discharge port of the 2# pulse high gradient magnetic separator (12) is connected to the feed port of the copper sulfide preferential flotation system (13), the concentrate discharge port of the copper sulfide preferential flotation system (13) is connected to the copper refining system (14), and the tailings discharge port of the copper sulfide preferential flotation system (13) is connected to the nickel refining system (18).

2. The system for efficiently recovering valuable components from a complex low-grade platinum-palladium oxygen-sulfur mixed ore according to claim 1, characterized in that: The magnetic induction intensity of the 1# pulse high gradient magnetic separator (7) is 900-1200 mT, and the pulse intensity is 200-300 times / min.

3. The system for efficiently recovering valuable components from complex low-grade platinum-palladium oxygen-sulfur mixed ore according to claim 1, characterized in that: The induction intensity of the 2# pulse high gradient magnetic separator (12) is 200-300 mT, and the pulse intensity is 200-300 times / min.

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