Coarse mineral fluidized bed separation equipment and method based on flotation process reinforcement

Abstract

The invention relates to a coarse-grain mineral fluidized bed separation device and method based on flotation process strengthening, belongs to the technical field of mineral processing and resource recovery, and solves the problems that in the prior art, coarse-grain mineral fluidized bed separation equipment is poor in separation efficiency and effect. The device comprises a fluidized bed column, a feeding stirring barrel and a hollow rotating shaft, the feeding stirring barrel is arranged at the lower part of the inner cavity of the fluidized bed column; the upper end of the hollow rotating shaft is positioned in the feeding stirring barrel; a plurality of layers of agent feeding blades are arranged on the inner wall of the feeding stirring barrel, a plurality of layers of ore pulp feeding blades are arranged at the upper end of the hollow rotating shaft, and the agent feeding blades and the ore pulp feeding blades are arranged in a staggered mode in the vertical direction. The built-in feeding stirring barrel effectively shortens the separation process and improves the separation efficiency, the ore pulp feeding blades and the agent feeding blades are arranged in a moving and stationary blade staggered mode, mineral particles can make full contact with a collecting agent in a high-turbulence-intensity shear flow field, effective modification on the surfaces of the mineral particles is effectively achieved, and the flotation effect is optimized.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of mineral processing and resource recovery, and particularly relates to a rough-grained mineral fluidized bed sorting equipment and method based on flotation process intensification. BACKGROUND

[0002] With the increasingly fierce global energy and resource competition, how to realize the efficient development and utilization of coal and mineral resources has become a key issue to guarantee national energy security and support the development of strategic emerging industries. At present, high-quality mineral resources are becoming increasingly depleted, and the proportion of low-grade and complex composition mineral resources is continuously rising, and the mineral selectivity is deteriorating. Traditional rough-grained sorting equipment has problems such as single structure and unreasonable flow field design, which further aggravates the sorting difficulty.

[0003] Under this background, the rough-grained fluidized bed column sorting technology is becoming a research hotspot due to its obvious energy saving and consumption reduction and tailing resource advantage. Compared with traditional photoelectric beneficiation and gravity separation and other large block ore processing technologies, the fluidization technology can form a dynamic sorting environment with stable bed and clear density stratification through accurate regulation of gas-liquid two-phase flow. Its continuous adjustable characteristics can adapt to the sorting needs of different particle size and density materials, providing a new idea for efficient sorting of millimeter-sized materials and opening up a new way for deep pre-concentration of low-grade mineral resources and recycling of waste resources.

[0004] Mineralization, as the core link of the flotation process, is significantly affected by the turbulence intensity. Moderate turbulence is conducive to promoting the collision and contact of bubbles and mineral particles, and accelerating the spreading of reagents on the particle surface. However, too high turbulence intensity will cause the detachment of gas flocs during transportation, reducing the mineral flotation recovery rate. In addition, the volatility of the upward flow will destroy the stability of the material bed layer in the fluidization sorting process, resulting in unclear density stratification of particles and decreased bed uniformity, and further deteriorating the fluidized bed sorting environment of rough-grained materials. SUMMARY

[0005] In view of the above analysis, the embodiments of the present application aim to provide a rough-grained mineral fluidized bed sorting equipment and method based on flotation process intensification, to solve the problems of poor sorting efficiency and effect of the existing rough-grained mineral fluidized bed sorting equipment.

[0006] In one aspect, the present application provides a rough-grained mineral fluidized bed sorting equipment based on flotation process intensification, comprising a fluidized bed column, a feed mixing drum and a hollow rotating shaft.

[0007] The feed mixing drum is arranged at the lower part of the inner cavity of the fluidized bed column, and the upper end of the hollow rotating shaft is located in the feed mixing drum.

[0008] The inner wall of the feeding stirring cylinder is provided with multiple layers of medicament feeding blades, and the upper end of the hollow rotating shaft is provided with multiple layers of ore pulp feeding blades.

[0009] Further, the ore pulp feeding blades and the medicament feeding blades are both provided with discharge holes.

[0010] Further, the ore pulp feeding blades and the medicament feeding blades are both provided with discharge holes.

[0011] Further, the ore pulp feeding blades and the medicament feeding blades are both provided with discharge holes.

[0012] Further, the medicament feeding unit comprises a first medicament pipe, an annular distributor and a second medicament pipe, the annular distributor is arranged outside the bottom of the fluidized bed column, one end of the first medicament pipe is connected with the annular distributor, and the other end is connected with the medicament feeding blades, one end of the second medicament pipe is connected with the annular distributor, and the other end is used for medicament feeding.

[0013] Further, multiple first medicament pipes are arranged around the feeding stirring cylinder, and the upper end of the first medicament pipe is provided with multiple branch pipes connected with the medicament feeding blades.

[0014] Further, the ore pulp feeding unit comprises an ore pulp feeding pipe and a slurry pump, one end of the ore pulp feeding pipe is connected with the lower end of the hollow rotating shaft, and the other end is connected with the slurry pump.

[0015] Further, a power transmission unit is further arranged to provide power for the hollow rotating shaft.

[0016] Further, a gas-water mixing unit is further arranged to supply fluidizing water into the fluidized bed column.

[0017] Further, an ultrasonic vibrator and a blocking inclined plate are arranged at the upper part of the inner cavity of the fluidized bed column, the ultrasonic vibrator and the blocking inclined plate are arranged alternately, and the blocking inclined plate is arranged between two ultrasonic vibrators.

[0018] Further, the gas-water mixing unit comprises a blocking distribution disc and a gas-water distribution ring, both of which are arranged inside the fluidized bed column, the blocking distribution disc is arranged above the feeding stirring cylinder, and the gas-water distribution ring is arranged outside the feeding stirring cylinder and at the middle-lower part of the feeding stirring cylinder.

[0019] Further, the retardation distribution disc is provided with water outlets facing the feeding stirring cylinder; the water outlets are arranged in an array along the circumference of the gas-water distribution ring, and three water outlets are arranged at equal intervals to form a group, and the water outlets face the retardation inclined plate.

[0020] In another aspect, the application provides a sorting method, which uses the above-mentioned coarse particle fluidized bed sorting equipment to perform sorting operation on coarse particles.

[0021] Compared with the prior art, the application can achieve at least one of the following beneficial effects:

[0022] (1) The application is provided with a stirring cylinder in the lower part of the inner cavity of the fluidized bed column, the inner wall of the feeding stirring cylinder is provided with multiple layers of medicament feeding blades, the hollow rotating shaft of the feeding stirring cylinder is provided with multiple layers of ore slurry feeding blades staggered with the medicament feeding blades, and a dynamic and static blade multi-layer feeding-restricted shear force coupling structure is formed in the space at the bottom of the fluidized bed column. On the one hand, the hollow rotating shaft drives the ore slurry feeding blades to rotate to excite the stirring shear flow field, which can fully mix the ore slurry fed through the hollow rotating shaft with the collector fed through the medicament feeding blades, optimize the contact effect of the collector molecules and the mineral particles, and the built-in feeding stirring cylinder can replace the slurry adjusting barrel to play a high-efficiency slurry adjusting role, effectively shorten the sorting process and improve the sorting efficiency. On the other hand, the ore slurry feeding blades and the medicament feeding blades are arranged in a dynamic and static blade staggered manner, which can make the mineral particles fully contact with the collector in a high-turbulence-intensity shear flow field, complete the adhesion process of the particles and the collector molecules, effectively modify the surface of the mineral particles, and optimize the flotation effect.

[0023] (2) The application forms an ultrasonic transducer disturbance-retardation inclined plate flow guide array coupling structure in the upper part of the inner cavity of the fluidized bed column. On the one hand, the use of low-power and medium-frequency ultrasonic waves can effectively disperse the rising ore slurry flow, effectively remove the gangue particles in the particle flow that are carried by the water flow and top up to the froth zone, and make them settle at the bottom of the fluidized bed as tailings. At the same time, the lower acoustic energy is input into the froth zone, which induces the tailings particles carried by the water flow to fall off from the froth layer, effectively improving the concentrate grade of the fluidized bed flotation; at the same time, without affecting the transportation of the concentrate, the effective dispersion of the bubbles and the particles is effectively promoted, and local particle accumulation is prevented to reduce the flotation rate. On the other hand, the introduction of the retardation inclined plate optimizes the flow path of the particles on the basis of the ultrasonic transducer, effectively prolongs the sorting time of the mineral particles by increasing the upward travel of the particles, and enlarges the terminal velocity difference of the particles, so that the concentrate particles rise while the gangue particles separate from the concentrate and sink under the action of the terminal velocity difference and the acoustic energy, further reducing the gangue particle entrainment and improving the concentrate grade.

[0024] (3) The present application is provided with a retardation distribution disc and a gas-water distribution ring in the fluidized bed column, the retardation distribution disc is arranged above the feeding stirring cylinder, and the gas-water distribution ring is arranged outside the feeding stirring cylinder, forming a structure of the retardation distribution disc reverse retardation primary mineralization-gas-water distribution ring array opening secondary mineralization, the retardation distribution disc retards the flow rate of the upward mineral slurry after the mixing, so that the feeding mineral slurry flows to the bottom of the fluidized bed in a relatively gentle manner, and the retardation distribution disc downwardly feeds the bubble flow, which realizes the bubble-particle reverse mineralization, effectively dissipates the turbulent energy of the mineral particles after being energized by the stirring shear flow field through the convection collision of the bubbles, effectively avoids the increase of the turbulent intensity in the fluidized bed column caused by the cyclone overflow feeding, from the energy dissipation angle of the flow field, a microgravity static environment suitable for the fluidized bed flotation is constructed, and the coarse mineral flotation recovery rate is effectively improved. On the other hand, the gas-water distribution ring is arranged outside the stirring cavity, the water containing the foaming agent is fed into the fluidized bed through the array opening of the gas-water distribution ring, which overcomes the uneven distribution of the bubbles caused by the traditional water distribution plate arrangement, and performs secondary mineralization on the mineral particles after being retarded and mineralized by the retardation distribution disc, optimizes the radial distribution of the bubbles in the fluidized bed column, and further improves the contact probability of the bubbles and the mineral particles in the static region, further promotes the bubble-particle collision, and optimizes the flotation effect.

[0025] In the present application, each of the above technical solutions can be combined with each other to realize more preferred combination schemes. Other features and advantages of the present application will be described in the subsequent specification, and some advantages will become apparent from the specification or be understood by implementing the present application. The purposes and other advantages of the present application can be realized and obtained from the contents specifically indicated in the specification and the drawings. BRIEF DESCRIPTION OF DRAWINGS

[0026] The accompanying drawings are included to provide a further understanding of the present application, and are incorporated herein and constitute a part of the detailed description. The drawings illustrate embodiments of the present application and, together with the description, serve to explain the principles of the present application. In the drawings:

[0027] Figure 1 The structure schematic diagram of the coarse mineral fluidized bed separation equipment of the specific embodiment;

[0028] Figure 2 The connection structure schematic diagram of the ultrasonic vibrator, the retardation inclined plate, the cross crossbar and the fluidized bed column of the specific embodiment;

[0029] Figure 3 The connection structure schematic diagram of the fluidized bed column, the feeding stirring cylinder, the hollow rotating shaft and the gas-water distribution ring of the specific embodiment;

[0030] Figure 4 The coarse mineral fluidized bed separation process schematic diagram of the specific embodiment.

[0031] Reference signs:

[0032] 1-fluidized bed column; 11-overflow weir; 111-concentrate discharge port; 12-tailings bin; 121-tailings discharge port; 122-emergency discharge port; 13-pressure sensor; 14-ultrasonic transducer; 15-retention chute; 16-crossing bar; 2-feed mixing drum; 21-agent feeding blade; 3-agent feeding unit; 31-first agent pipe; 32-annular distributor; 33-second agent pipe; 34-agent feeding device; 4-hollow rotating shaft; 41-ore pulp feeding blade; 5-ore pulp feeding unit; 51-ore pulp feeding pipe; 52-first electromagnetic control valve; 53-slurry pump; 6-power transmission unit; 7-air-water mixing unit; 71-water supplement tank; 72-water supply pipe; 73-bubble generator; 74-air pump; 75-air supply pipe; 76-liquid flow meter; 77-gas flow meter; 78-centrifugal pump; 79-first air-water distribution pipe; 70-second air-water distribution pipe; 701-retention distribution disc; 702-air-water distribution ring; 703-connection pipe. DETAILED DESCRIPTION

[0033] The preferred embodiments of the present application will be described in detail below with reference to the drawings, which form a part of this description, and together with the embodiments of the present application, illustrate the principles of the present application. It is to be noted, however, that the drawings are not to scale and in some instances dimensions of components are exaggerated for the sake of clarity.

[0034] Example 1

[0035] One specific embodiment of the present application discloses a rough particle mineral fluidized bed separation equipment based on flotation process intensification (hereinafter referred to as rough particle mineral fluidized bed separation equipment), which is used for rough particle separation and recovery of mineral resources such as coal and secondary resources. The equipment is particularly suitable for the combined process of rough particle mineral breaking and gangue removal and separation, and aims to realize efficient and deep flotation process for rough particle minerals, and improve the flotation efficiency and recovery rate.

[0036] As shown in Figure 1 , the rough particle mineral fluidized bed separation equipment comprises a fluidized bed column 1, a feed mixing drum 2, and a hollow rotating shaft 4. The feed mixing drum 2 is arranged at the lower part of the inner cavity of the fluidized bed column 1, the upper end of the hollow rotating shaft 4 is located in the feed mixing drum 2, the inner wall of the feed mixing drum 2 is provided with a plurality of agent feeding blades 21, the upper end of the hollow rotating shaft 4 is provided with a plurality of ore pulp feeding blades 41, and the agent feeding blades 21 and the ore pulp feeding blades 41 are arranged in a staggered manner in the vertical direction.

[0037] Further, as shown in Figure 1 , the rough particle mineral fluidized bed separation equipment further comprises an agent feeding unit 3 and an ore pulp feeding unit 5. The hollow rotating shaft 4 is connected with the ore pulp feeding unit 5, and the agent feeding unit 3 is connected with the agent feeding blades 21. The plurality of agent feeding blades 21 are arranged along the height direction of the inner wall of the feed mixing drum 2, and the plurality of ore pulp feeding blades 41 are arranged along the length direction of the hollow rotating shaft 4.

[0038] In implementation, the ore pulp is fed from the ore pulp supply unit 5 to the hollow rotating shaft 4, and then into the ore pulp feeding blades 41 of each layer, and is fed into the feed mixing drum 2 through the ore pulp feeding blades 41, and the reagent is fed from the reagent supply unit 3 to the reagent feeding blades 21, and is fed into the feed mixing drum 2 through the reagent feeding blades 21 of each layer.

[0039] Compared with the prior art, the coarse-grained mineral fluidized bed separation equipment provided by the embodiment is provided with the feed mixing drum 2 at the lower part of the inner cavity of the fluidized bed column 1, the inner wall of the feed mixing drum 2 is provided with the multiple layers of reagent feeding blades 21, the hollow rotating shaft 4 of the feed mixing drum 2 is partially provided with the multiple layers of ore pulp feeding blades 41 staggered with the reagent feeding blades 21, and a dynamic-stationary blade multi-layer feed-forced limited shear pulp conditioning coupling structure is formed in the space at the bottom of the fluidized bed column 1. On the one hand, based on the stirring shear flow field excited by the rotation of the ore pulp feeding blades 41 driven by the hollow rotating shaft 4, the ore pulp fed from the bottom of the fluidized bed column 1 into the feed mixing drum 2 through the hollow rotating shaft 4 can be fully mixed with the collecting agent fed through the reagent feeding blades 21, the contact effect of the reagent molecules and the mineral particles is optimized, the built-in feed mixing drum 2 can replace the pulp conditioning barrel to play a high-efficiency pulp conditioning role, and the separation process is effectively shortened and the separation efficiency is improved. On the other hand, the ore pulp feeding blades 41 and the reagent feeding blades 21 are arranged in a dynamic-stationary blade staggered manner, so that the mineral particles can be fully contacted with the collecting agent in a high-turbulence-intensity shear flow field, the particle and reagent molecule adhesion process is completed, the effective modification of the surface of the mineral particles is effectively realized, and the flotation effect is optimized.

[0040] Preferably, the reagent feeding blades 21 are provided with 3-5 layers, preferably 4 layers, along the height direction of the feed mixing drum 2, and the ore pulp feeding blades 41 are provided with 3-5 layers, preferably 4 layers, along the height direction of the hollow rotating shaft 4.

[0041] The horizontal center line of the ore pulp feeding blades 41 is consistent with the spacing center line of the reagent feeding blades 21, that is, the ore pulp feeding blades 41 are arranged between two reagent feeding blades 21 and have equal spacing with the two reagent feeding blades 21; and the reagent feeding blades 21 are arranged between two ore pulp feeding blades 41 and have equal spacing with the two ore pulp feeding blades 41.

[0042] Exemplarily, the inner diameter of the feeding stirring barrel 2 is generally 200-300 mm, preferably 250 mm. The spacing of the medicament feeding blades 21 is generally 50-150 mm, preferably 100 mm. The spacing of the ore pulp feeding blades 41 is generally 50-150 mm, preferably 100 mm. The height of the feeding stirring barrel 2 is generally 400-600 mm, preferably 500 mm. The upper part of the feeding stirring barrel 2 is a cylindrical section, and the height of the cylindrical section is generally 400-500 mm, preferably 450 mm. The lower part of the feeding stirring barrel 2 is a circular truncated cone section, and the height of the circular truncated cone section is 50 mm, and the bottom diameter is generally 100-200 mm, preferably 150 mm.

[0043] Considering that the ore pulp and the medicament are fed into the feeding stirring barrel 2 through the ore pulp feeding blades 41 and the medicament feeding blades 21 respectively, the ore pulp feeding blades 41 and the medicament feeding blades 21 are both provided with openings (i.e. discharge holes), the ore pulp is fed from the openings of the rotating ore pulp feeding blades 41, and the capturing agent is fed from the openings of the medicament feeding blades 21. Understandably, the inner cavity of the medicament feeding blades 21 is in communication with the medicament adding unit 3, and the inner cavity of the ore pulp feeding blades 41 is in communication with the hollow rotating shaft 4.

[0044] Further, as shown in Figure 3 Each layer of ore pulp feeding blades 41 and medicament feeding blades 21 is arranged in a circumferential array. Specifically, each layer of ore pulp feeding blades 41 is provided with a plurality of ore pulp feeding blades 41 which are circumferentially distributed around the hollow rotating shaft 4, and each layer of medicament feeding blades 21 is provided with a plurality of medicament feeding blades 21 which are circumferentially distributed along the inner wall of the feeding stirring barrel 2. Preferably, each layer of ore pulp feeding blades 41 and each layer of medicament feeding blades 21 are provided with four.

[0045] Unlike the traditional one-way ore pulp feeding mode, the ore pulp is fed through the openings of the ore pulp feeding blades in the present embodiment, and the ore pulp particles perform centrifugal motion as soon as they enter the feeding stirring barrel 2 and are thrown out. Compared with the traditional one-way particle energizing, this feeding mode makes the particles move more chaotically in space, i.e. the energy input makes the particles move more fully in space. Combined with the multi-layer staggered blade array arrangement, the ore pulp is accelerated to enter through the openings of the ore pulp feeding blades 41 at different heights, which can fully optimize the initial spatial distribution of mineral particles, greatly saving the time required for particle dispersion and improving the flotation efficiency. The local structure of the built-in feeding stirring barrel 2 effectively introduces the ore pulp preparation into the separation process, and at the same time, the plant realizes flexible separation and flotation process cost reduction and efficiency increase, providing a technical reference.

[0046] Considering the collection of the concentrate and the tailings, as shown in Figure 1As shown, the top of the fluidized bed column 1 is provided with an overflow weir 11, and the overflow weir 11 is provided with a concentrate discharge port 111. The bottom of the fluidized bed column 1 is a tailings bin 12, and the bottom of the tailings bin 12 is provided with a tailings discharge port 121 and an emergency discharge port 122. In order to control the opening and closing of the tailings discharge port 121 and the emergency discharge port 122, an electromagnetic valve is arranged on each of the tailings discharge port 121 and the emergency discharge port 122. The number of tailings discharge ports 121 is generally 6-10, preferably 8.

[0047] Preferably, the fluidized bed column 1 is a cylindrical structure, and the tailings bin 12 is a circular truncated cone structure. The inner diameter of the fluidized bed column 1 is generally 0.4-1.0 m, preferably 0.7 m. Considering the arrangement of the working conditions in combination with the separation rate and efficiency, the height of the fluidized bed column 1 is generally 1.5-2.5 times the inner diameter, i.e. 0.6-2.5 m, preferably 1.5 m. The inclination angle of the tailings bin 12 is generally 10-30°, preferably 15°, and the height of the tailings bin 12 is generally 0.2 m. The upper part of the top overflow weir 11 is arranged to be higher than the upper part of the fluidized bed column 1 by 0.1 m, and the inclination angle is generally set to 15-35°. Considering the increase of the roughing discharge speed and the suppression of the plugging phenomenon, the inclination angle is preferably 25°.

[0048] In order to monitor the pressure distribution in the column during the separation process to determine whether the tailings need to be discharged or the equipment parameters need to be adjusted, such as Figure 1 As shown, a plurality of pressure sensors 13 are arranged in the fluidized bed column 1 from top to bottom. The number of pressure sensors 13 is generally 3-8, preferably 4.

[0049] In combination with Figure 1 and Figure 2 As shown, an ultrasonic vibrator 14 and a retardation inclined plate 15 are arranged at the upper part of the inner cavity of the fluidized bed column 1. Considering the installation of the ultrasonic vibrator 14 and the retardation inclined plate 15, a cross bar 16 is arranged at the upper part of the inner cavity of the fluidized bed column 1, and the end of the cross bar 16 is connected to the inner wall of the fluidized bed column 1. The ultrasonic vibrator 14 is provided with a plurality of ultrasonic vibrators 14 arranged on the cross bar 16. The retardation inclined plate 15 is also provided with a plurality of retardation inclined plates 15 arranged on the cross bar 16. The number of single-axis installations of the ultrasonic vibrator 14 on the cross bar 16 is generally 4-6, preferably 5. The retardation inclined plate 15 is located between the ultrasonic vibrators 14, and the inclination angle of the retardation inclined plate 15 is generally 60-80°, preferably 70°.

[0050] Exemplarily, 5 ultrasonic transducers 14 are mounted on the single shaft of the cross beam 16, and correspondingly, 4 blocking inclined plates 15 are arranged on the single shaft, forming inner zone blocking inclined plates 15 and outer zone blocking inclined plates 15. The inner zone blocking inclined plates 15 refer to the blocking inclined plates 15 close to the center of the inner cavity of the fluidized bed column 1. The length of the blocking inclined plates 15 in the inner zone and the outer zone is generally 100-200 mm, and preferably 150 mm. The width of the inner zone blocking inclined plates 15 is generally 50-100 mm, and preferably 75 mm. The width of the outer zone blocking inclined plates 15 is generally 100-200 mm, and preferably 150 mm.

[0051] In the embodiment, the cross beam 16 is arranged at the upper part of the inner cavity of the fluidized bed column 1, and the ultrasonic transducers 14 and the blocking inclined plates 15 are arranged alternately on the cross beam 16, forming a structure of ultrasonic transducer 14 disturbance-blocking inclined plate 15 flow guide array coupling. On the one hand, by arranging the cross beam 16 at the upper part of the fluidized bed column 1 and arraying the ultrasonic transducers 14, the rising slurry flow is effectively dispersed by using low-power and medium-frequency ultrasonic waves, the gangue particles in the particle flow that are carried by the water flow and top up to the froth zone are effectively removed, and they are settled to the bottom of the fluidized bed as tailings and discharged. At the same time, the lower acoustic energy is input into the froth zone, which induces the tailings particles carried by the water flow to fall off from the froth layer, effectively improving the concentrate grade of the fluidized bed flotation. At the same time, without affecting the concentrate transportation, the effective dispersion of bubbles and particles is effectively promoted, and local particle accumulation is prevented to reduce the flotation rate. On the other hand, the introduction of the blocking inclined plate 15 optimizes the flow path of the particles on the basis of the ultrasonic transducer 14, effectively prolongs the mineral particle separation time by increasing the particle rising path, and amplifies the terminal velocity difference of the particles. The concentrate particles rise, while the gangue particles separate from the concentrate and sink under the action of the terminal velocity difference and the acoustic energy, further reducing the gangue particle entrainment and improving the concentrate grade. This provides certain technical reference for the plant to realize efficient separation of coarse particles and equipment technology development from the perspective of separation process in the froth zone.

[0052] Considering that the medicament feeding blades 21 are uniformly distributed along the inner wall circumference of the charging barrel, in order to adapt and connect the medicament feeding unit 3 with the arrayed medicament feeding blades 21, as shown in Figure 1 , the medicament feeding unit 3 includes a first medicament pipe 31, an annular distributor 32, and a second medicament pipe 33. The annular distributor 32 is arranged outside the bottom of the fluidized bed column 1. One end of the first medicament pipe 31 is connected with the annular distributor 32, and the other end is connected with the medicament feeding blades 21. One end of the second medicament pipe 33 is connected with the annular distributor 32, and the other end is connected with a medicament feeding device 34. Understandably, the first medicament pipe 31 is arranged around the charging barrel 2, and the upper end of the first medicament pipe 31 is provided with a plurality of branch pipes corresponding to the multiple layers of medicament feeding blades 21.

[0053] As shown in Figure 1As shown, the slurry supply unit 5 includes a slurry inlet pipe 51, a first electromagnetic control valve 52 and a slurry pump 53. One end of the slurry inlet pipe 51 is connected to the lower end of the hollow rotating shaft 4, and the other end is connected to the slurry pump 53. The slurry pump 53 is connected to another slurry inlet pipe 51. The first electromagnetic control valve 52 is arranged on the slurry inlet pipe 51. It should be noted that since the hollow rotating shaft 4 rotates and the slurry inlet pipe 51 is stationary, a dynamic sealing structure is used at the connection between the hollow rotating shaft 4 and the slurry inlet pipe 51. The structure of the dynamic sealing structure is a prior art and will not be described here.

[0054] In order to realize the rotation of the hollow rotating shaft 4, as shown in Figure 1 The coarse-grained mineral fluidized bed separation device also includes a power transmission unit 6, which provides rotating power for the hollow rotating shaft 4. Exemplarily, the power transmission unit 6 includes a motor, a first pulley, a second pulley and a belt. The first pulley is connected to the lower end of the hollow rotating shaft 4, the second pulley is connected to the output shaft of the motor, and the belt connects the first pulley and the second pulley.

[0055] As shown in Figure 1 The coarse-grained mineral fluidized bed separation device also includes a gas-water mixing unit 7, which includes a make-up water tank 71, a water inlet pipe 72, a bubble generator 73, a gas pump 74 and a gas inlet pipe 75. One end of the water inlet pipe 72 is connected to the make-up water tank 71, and the other end is connected to the bubble generator 73. One end of the gas inlet pipe 75 is connected to the gas pump 74, and the other end is connected to the bubble generator 73.

[0056] As shown in Figure 1 The gas-water mixing unit 7 also includes a liquid flow meter 76, a gas flow meter 77 and a centrifugal pump 78. The liquid flow meter 76 and the centrifugal pump 78 are both arranged on the water inlet pipe 72. Exemplarily, one water inlet pipe 72 communicates the make-up water tank 71 and the centrifugal pump 78, and the other water inlet pipe 72 communicates the centrifugal pump 78 and the bubble generator 73. The gas flow meter 77 is arranged on the gas inlet pipe 75.

[0057] As shown in Figure 1 The gas-water mixing unit 7 also includes a first gas-water distribution pipe 79 and a second gas-water distribution pipe 70. One end of the first gas-water distribution pipe 79 is connected to the bubble generator 73, and the other end is located in the fluidized bed column 1. One end of the second gas-water distribution pipe 70 is connected to the bubble generator 73, and the other end is annularly located outside the lower part of the fluidized bed column 1.

[0058] In combination with Figure 1 and Figure 3As shown, the gas-water mixing unit 7 further comprises a retardation distribution disc 701 and a gas-water distribution ring 702, both of which are arranged inside the fluidized bed column 1. The retardation distribution disc 701 is located above the feeding stirring cylinder 2, and the gas-water distribution ring 702 is arranged around the feeding stirring cylinder 2 and located at the middle and lower part of the feeding stirring cylinder 2. The retardation distribution disc 701 is provided with downward water outlet holes; the gas-water distribution ring 702 is provided with upward water outlet holes in the form of holes arrayed in the circumferential direction. Three holes form a group and are arranged at equal intervals, and the interval between each group is 15°. The retardation distribution disc 701, the fluidized bed column 1 and the feeding stirring cylinder 2 are concentrically arranged.

[0059] Exemplarily, the diameter of the retardation distribution disc 701 is generally 500-700 mm, and preferably 600 mm. The interval between the retardation distribution disc 701 and the feeding stirring cylinder 2 is generally 100-200 mm, and preferably 150 mm. The inner diameter of the gas-water distribution ring 702 is generally 450-550 mm, and preferably 500 mm; and the outer diameter is generally 550-650 mm, and preferably 600 mm.

[0060] In order to realize the connection between the gas-water distribution ring 702 and the external second gas-water distribution pipe 70, the gas-water distribution ring 702 is provided with a connecting pipe 703. Figure 1 As shown, the gas-water mixing unit 7 further comprises a connecting pipe 703, the lower end of which is connected with the second gas-water distribution pipe 70, and the upper end of which is located inside the fluidized bed column 1 and connected with the gas-water distribution ring 702.

[0061] In this embodiment, the fluidized bed column 1 is provided with a retardation distribution plate 701 and a gas-water distribution ring 702. The retardation distribution plate 701 is arranged above the material feeding stirring barrel 2, and the gas-water distribution ring 702 is arranged outside the material feeding stirring barrel 2, forming a structure in which the retardation distribution plate 701 reversely retards the primary mineralization and the gas-water distribution ring 702 array opening secondary mineralization. The retardation distribution plate 701 is arranged above the stirring cavity at the bottom of the fluidized bed, and the upward mineral slurry flow after thickening is subjected to flow rate retardation, so that the material feeding mineral slurry flows to the bottom of the fluidized bed in a relatively gentle manner after retardation, and the retardation distribution plate 701 downwardly feeds the bubble flow, which realizes the reverse mineralization of the bubbles and particles, and effectively dissipates the turbulent kinetic energy of the mineral particles after being energized by the stirring shear flow field through the convection collision of the bubbles, effectively avoids the increase of the turbulent intensity in the fluidized bed column caused by the cyclone overflow of the material feeding, and from the perspective of flow field energy dissipation, constructs a microgravity static environment suitable for the fluidized bed flotation, and effectively improves the flotation recovery rate of coarse mineral particles. On the other hand, the gas-water distribution ring 702 is arranged outside the stirring cavity, the water containing a foaming agent is fed into the fluidized bed through the array opening of the gas-water distribution ring 702, which overcomes the disadvantage of uneven distribution of bubbles caused by the bottom arrangement of the traditional water distribution plate, and performs secondary mineralization on the mineral particles after retardation and mineralization by the retardation distribution plate 701, optimizes the radial distribution of bubbles in the fluidized bed column 1, and further improves the contact probability of bubbles and mineral particles in the static region, further promotes the bubble-particle collision, and optimizes the flotation effect. At the same time, the design of the peripheral gas-water distribution ring 702 effectively constructs a microgravity environment suitable for particle fluidization, overcomes the interference settlement of the particles along the density stratification in the whole column which cannot be realized by the bottom water feeding method, and promotes the strengthening of the gravity separation process in the fluidized bed "flotation-gravity coupling" separation.

[0062] The embodiment innovatively proposes a "turbulent shear mixing-static transport separation" coupling mechanism. By designing a local structure suitable for the flotation process of coarse mineral particles, and introducing a strong shear flow field based on the mineralization mechanism to strengthen the collision and adhesion effect, and setting an energy dissipation zone in the subsequent flow field space to inhibit the detachment behavior. From the perspective of flow field characteristics and separation process optimization, through the innovative design of the turbulent mineralization-static transport function module, the quality and efficiency of the coarse mineral particle fluidization column flotation process are improved.

[0063] The coarse mineral fluidized bed separation equipment of the embodiment effectively shortens the separation process and reduces the consumption of water and reagents in the separation process, and coordinates the flow field characteristics and the separation process, which provides a more systematic and objective reference and guidance for the research on the coarse mineral fluidized bed column separation process, the selectability of coarse mineral particles and the process parameter regulation.

[0064] Embodiment 2

[0065] Another specific embodiment of the application is as follows: Figure 4As shown, a coarse-grained mineral fluidized bed separation method is disclosed, using the coarse-grained mineral fluidized bed separation equipment of Example 1, comprising the following steps:

[0066] Step S1: Pre-checking of the fluidized bed column separation equipment

[0067] First, confirm that the electric control valves at the accident discharge port 122 and the tailings discharge port 121 are in the closed state to prevent accidental leakage of the mineral particles to be separated. Check the waterproofing of the bottom motor and the wear of the traction belt to prevent power unit failure from affecting the separation process.

[0068] Step S2: Pre-fluidization with water and frother

[0069] Open the pipeline valve of the water supplement tank 71 and the air pump 74. The clean water is pressurized by the centrifugal pump 78, and its speed is adjusted by the liquid flow meter 76. The water is then sequentially passed through the water delivery pipe 72 and the bubble generator 73. The gas is delivered to the bubble generator 73 through the gas delivery pipe 75. After the gas and water are mixed in the bubble generator 73, they are used as part of the fluidizing medium and enter the interior of the fluidized bed column 1 through the first gas-water distribution pipe 79 and are given from the holdback distribution disc 701. The other part is given to the gas-water distribution ring 702 inside the fluidized bed column 1 through the second gas-water distribution pipe 70.

[0070] It should be noted that the gas delivery speed of the air pump 74 can be set at 0.2-0.6 m / s, adjusted according to the separation test conditions. The speed of the clean water can be set at 2.0-8.0 m / s, adjusted according to the range of feed particle size. The frother (generally set at 5-15 mg / L, adjusted according to the dispersion of bubbles) is added dropwise in the water supplement tank 71 and enters the interior of the fluidized bed column 1 together with the clean water. The frother generally includes pine oil (No. 2 oil), methyl isobutyl carbinol (MIBC), and diethyl phthalate, with pine oil (No. 2 oil) being preferred.

[0071] The pressure sensor 13 monitors the pressure change in the column. When the pressure difference is stable (i.e., there is no significant fluctuation in the pressure sensor 13 reading), the fluidization state is stable, and the clean water valve is closed, and the first gas-water distribution pipe 79 is also closed at this time, and only the gas-water distribution ring 702 supplies gas. Understandably, the water delivery pipe 72 and the first gas-water distribution pipe 79 are each provided with an electromagnetic control valve.

[0072] Step 3: Slurry adjustment in the stirring chamber, twice mineralization

[0073] The collector (usually set at 200-800 mg / L, adjusted according to the specific separation) is fed into the feed mixing drum 2 from the medicament feeding device 34 through the second medicament pipe 33 and the arrayed first medicament pipe 31. The collector is usually sodium ethyl xanthate, sodium isopropyl xanthate, sodium butyl xanthate, sodium (potassium) isobutyl xanthate, etc., and sodium ethyl xanthate is preferred. The medicament concentration in the ore pulp is controlled by adjusting the mass of the fed medicament; at the same time, the ore pulp is pumped from the ore pulp inlet through the slurry pump 53 and fed out from the ore pulp feeding pipe 51 at the ore pulp feeding blade 41 of the hollow rotating shaft 4. The ore pulp concentration is set at 30-40% (adjusted according to the specific test conditions and the properties of the minerals).

[0074] In this step, the hollow rotating shaft 4 drives the ore pulp feeding blade 41 to rotate to excite the stirring shear flow field, so that the mineral particles can be fully contacted with the collector in the high-turbulence shear flow field, the particle and medicament molecular adhesion process is completed, the effective modification of the surface of the mineral particles is effectively realized, the contact effect of the medicament molecules and the mineral particles is optimized, and the separation process is shortened and the separation efficiency is improved.

[0075] After the ore pulp is stirred in the stirring chamber for 1 min, the electromagnetic control valves on the water feeding pipe 72 and the first air-water distribution pipe 79 are opened, so that the retardation distribution disc 701 and the air-water distribution ring 702 again transport the fluidized water to form the reverse retardation of the retardation distribution disc 701 on the first mineralization-air-water distribution ring 702.

[0076] In this step, the retardation distribution disc 701 retards the flow rate of the rising ore pulp after stirring, so that the feed ore pulp flows to the bottom of the fluidized bed in a relatively gentle manner after retardation, and the retardation distribution disc 701 downwardly feeds the bubble flow, which realizes the reverse mineralization of the bubbles and particles, and effectively dissipates the turbulent kinetic energy of the mineral particles after being energized by the stirring shear flow field, thereby effectively avoiding the increase of the turbulent intensity in the fluidized bed column caused by the introduction of the cyclone overflow feed. The water containing the foaming agent is fed into the fluidized bed through the arrayed holes on the air-water distribution ring 702, the bubbles are uniformly distributed, and the mineral particles after retardation and mineralization by the retardation distribution disc 701 are secondarily mineralized, which optimizes the radial distribution of the bubbles in the fluidized bed column 1, further improves the contact probability of the bubbles and the mineral particles in the static region, further promotes the collision of the bubbles and the particles, and optimizes the flotation effect.

[0077] Step S4: vibration and retardation

[0078] The arrayed retardation inclined plate 15 and the ultrasonic vibrator 14 are operated, the ultrasonic vibrator 14 is started after the ore pulp is stirred for 1 min, and the ultrasonic vibrator 14 is set at a low power (25 W) and a medium frequency (50 kHz).

[0079] In this step, the ultrasonic transducer 14 disturbs and blocks the inclined plate 15 guide array coupling, the low-power, medium-frequency ultrasonic waves effectively disperse the rising slurry flow, effectively remove the gangue particles in the particle flow carried by the water flow and the large particles that top to the froth zone, and make them settle at the bottom of the fluidized bed as tailings. At the same time, the lower acoustic energy input into the froth zone induces the tailings particles carried by the water flow to fall off from the froth layer, effectively improving the concentrate grade of the fluidized bed flotation; at the same time, without affecting the concentrate transportation, effectively promoting the effective dispersion of bubbles and particles, preventing local particle accumulation and reducing the flotation rate. The blocking inclined plate 15 optimizes the flow path of the particles, effectively extends the mineral particle separation time by increasing the particle rising path, and amplifies the terminal velocity difference of the particles, so that the concentrate particles rise, and the gangue particles separate from the concentrate under the action of the terminal velocity difference and the acoustic energy and sink, further reducing the gangue particle entrainment and improving the concentrate grade.

[0080] Step S5: concentrate collection and tailings discharge

[0081] The separated concentrate particles float upwards and are collected by the overflow weir 11 to the concentrate discharge port 111 for discharge, and the tailings particles sink to the bottom of the fluidized bed, and the pressure sensor 13 is used to monitor the tailings accumulation state in real time. When the pressure reaches the preset upper limit, the tailings discharge port 121 valve is automatically opened to discharge the tailings; when the pressure drops to the preset lower limit, the valve is closed to prevent excessive discharge of the tailings from causing a sudden change in the pressure of the fluidized bed, thereby ensuring the stability of the fluidized bed layer.

[0082] In this embodiment, the efficient and feasible coarse particle mineral separation is realized from the perspective of strengthening the separation process, and the safety, flexibility and economy of the operation are also considered, thereby providing advanced and systematic technical reference and guidance for the selection plant in the aspects of coarse particle fluidized bed column separation process and coarse particle ore selectability research.

[0083] The above describes only the preferred specific embodiments of the present application, but the protection scope of the present application is not limited thereto, and any person skilled in the art can easily think of changes or replacements within the technical range disclosed by the present application, which should be covered within the protection scope of the present application.

Claims

1. A rough particle mineral fluidized bed separation apparatus based on flotation process intensification, characterized in that, The fluidized bed column (1), the feeding stirring cylinder (2) and the hollow rotating shaft (4); The feeding stirring cylinder (2) is arranged at the lower part of the inner cavity of the fluidized bed column (1), and the upper end of the hollow rotating shaft (4) is located in the feeding stirring cylinder (2); The inner wall of the feeding stirring cylinder (2) is provided with multiple layers of medicament feeding blades (21), the upper end of the hollow rotating shaft (4) is provided with multiple layers of ore pulp feeding blades (41), and the medicament feeding blades (21) and the ore pulp feeding blades (41) are arranged in a staggered manner in the vertical direction.

2. The flotation process intensified fluidized bed of coarse particles separation apparatus according to claim 1, characterized in that, The ore pulp feeding blades (41) and the medicament feeding blades (21) are both provided with discharge holes.

3. The flotation process intensified fluidized bed of coarse particles separation apparatus according to claim 1, characterized in that, Each layer of the ore pulp feeding blades (41) and each layer of the medicament feeding blades (21) are arranged in a circumferential array.

4. The flotation process intensified fluidized bed of coarse particles separation apparatus according to any one of claims 1 to 3, characterized in that, The power transmission unit (6) is further arranged to provide power for the hollow rotating shaft (4).

5. The flotation process intensified fluidized bed of coarse particles separation apparatus according to claim 4, characterized in that, The gas-water mixing unit (7) is further arranged to supply fluidizing water into the fluidized bed column (1).

6. The flotation process intensified fluidized bed of coarse particles separation apparatus according to claim 5, characterized in that, 10. A sorting method, which uses the coarse-grained fluidized bed sorting equipment according to any one of claims 1-9 to perform a sorting operation on coarse-grained minerals.

7. The flotation process intensified fluidized bed of coarse particles separation apparatus according to claim 4, characterized in that, ​ 8. The flotation process intensified fluidized bed of coarse particles separation apparatus according to any of claims 1-3, 5-7, characterized in that, ​ 9. The flotation process intensified fluidized bed of coarse particles separation apparatus according to any of claims 1-3, 5-7, characterized in that, ​ ​

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