An apparatus for mineralization, a flotation system and a flotation method

Abstract

The present application relates to a kind of mineralization device, flotation system and flotation method, belong to mineral processing field, at least one of the problems such as mineralization efficiency insufficient in existing mineralization device, large reagent consumption, high energy consumption and maintenance cost is solved.One kind of mineralization device, including: spherical mixer, spherical mixer has spherical inner cavity, and mineral slurry inlet, flotation reagent adding port and mineral slurry discharge port are equipped on spherical mixer;Self-excited oscillation microbubble mineralization pipe, connected to the mineral slurry discharge port of spherical mixer, self-excited oscillation microbubble mineralization pipe includes organ pipe cavity, throat pipe and helmholtz cavity in turn along the direction of mineral slurry flow;Throat pipe is provided with compressed air suction pipe in side wall;Helmholtz cavity is connected with mineral slurry discharge pipe after mineralization in outlet.This application realizes the integration of fine generation and mineralization strengthening of microbubble, reduces reagent consumption, energy consumption and maintenance cost.

Description

Technical Field

[0001] This invention relates to the field of mineral processing technology, and in particular to a mineralization apparatus, flotation system and flotation method. Background Technology

[0002] Flotation is a core separation technology in the mineral processing field, and its separation effect largely depends on the mineralization process before flotation. With the increasing depletion of easily beneficiated rich ore resources, the development and utilization of fine-grained and complex ores has become a key focus of the industry, placing higher demands on the microbubble generation capacity and mineralization enhancement capacity of mineralization equipment.

[0003] Currently, the mineralization process before flotation mainly relies on mechanical stirring or jet-type mineralization devices. Mechanical stirring devices disperse air into bubbles through high-speed impeller rotation, but suffer from problems such as easy wear of mechanical transmission components, high maintenance costs, high energy consumption, and large, unevenly distributed bubble sizes. Jet-type mineralization devices utilize the negative pressure generated when a high-speed jet passes through a throat to aspirate and break up the gas into bubbles, but the average particle size of the generated microbubbles is still relatively large, and the particle size distribution is uneven. Furthermore, there is a lack of subsequent control over bubble size after generation, resulting in a low probability of particle-bubble collisions and unsatisfactory mineralization of fine-grained minerals. In addition, the mixing of slurry and reagents in existing mineralization devices often relies on a single flow field disturbance, leading to low mixing efficiency and high reagent consumption.

[0004] Therefore, it is necessary to optimize the existing mineralization equipment before flotation to solve the technical problems of insufficient mineralization efficiency, high reagent consumption, high energy consumption and high maintenance costs in the existing mineralization equipment. Summary of the Invention

[0005] In view of the above analysis, the present invention aims to provide a mineralization device, flotation system and flotation method to solve at least one of the problems of insufficient mineralization efficiency, large reagent consumption, high energy consumption and high maintenance cost in existing mineralization devices.

[0006] The objective of this invention is achieved through the following technical solution: This invention provides a mineralization apparatus, comprising: A spherical mixer having a spherical inner cavity, and the spherical mixer being provided with a slurry inlet, a flotation reagent addition inlet, and a slurry outlet; A self-excited oscillating microbubble mineralization tube is connected to the slurry outlet of the spherical mixer. The self-excited oscillating microbubble mineralization tube includes a pipe organ cavity, a throat, and a Helmholtz cavity that are connected sequentially along the slurry flow direction. The side wall of the throat is provided with a compressed air intake pipe, which is connected to an external air source. The outlet of the Helmholtz cavity is connected to a mineralized slurry discharge pipe.

[0007] Furthermore, the spherical mixer is provided with at least two slurry feed pipes, each of which is arranged toward the center of the spherical mixer, so as to allow the slurry streams to converge and counteract each other within the spherical mixer.

[0008] Furthermore, the spherical mixer is provided with at least two slurry feed pipes in the equatorial plane passing through the center of the sphere; the spherical mixer is provided with a flotation reagent addition pipe and a slurry outlet on an axis perpendicular to the equatorial plane and passing through the center of the sphere, and the self-excited oscillating microbubble mineralization pipe is connected to the slurry outlet.

[0009] Furthermore, the interior of the spherical mixer is provided with a perforated baffle, which is located in the quadrant region between the equatorial plane and the meridian plane of the spherical mixer. The meridian plane is a plane that passes through the center of the spherical mixer and is perpendicular to the equatorial plane.

[0010] Furthermore, each of the quadrant regions is provided with at least one of the perforated baffles.

[0011] Furthermore, each quadrant region is provided with a perforated baffle, and the perforated baffles have the same tilt angle relative to the equatorial plane; And / or, the perforated baffle faces the center of the spherical mixer but does not pass through the center of the spherical mixer.

[0012] Furthermore, the perforated baffle is tilted at an angle of 30° to 60° relative to the equatorial plane.

[0013] Furthermore, one side of the perforated baffle is conformally fitted and fixed to the inner wall of the spherical mixer, and the distance between the other side and the center of the spherical mixer is not less than 1 / 5 of the radius of the spherical mixer.

[0014] This invention provides a self-excited oscillation enhanced flotation system, comprising: A slurry pretreatment subsystem, which includes the aforementioned mineralization device; And at least one of the coarse selection subsystem, fine selection subsystem and sweeping selection subsystem; At least one of the coarse flotation subsystem, the fine flotation subsystem, and the sweeping flotation subsystem includes a non-drive flotation cell.

[0015] This invention provides a flotation method enhanced by self-excited oscillation, comprising the following steps: The slurry and flotation reagents are fed into the above-mentioned mineralization device for mixing and pre-mineralization to obtain a pre-mineralized slurry; The premineralized slurry is subjected to at least one of roughing, cleaning and scavenging processes; In this process, at least one of the roughing, cleaning, and sweeping processes is carried out using a non-drive flotation cell.

[0016] Compared with the prior art, the present invention can achieve at least one of the following beneficial effects: (1) In the mineralization device provided by the present invention, the spherical mixer has a spherical inner cavity. The slurry and flotation reagent are constrained and guided in an all-directional balance within the spherical space, which is conducive to forming a three-dimensional cross flow. This allows the slurry and reagent to fully contact, disperse and mix in the three-dimensional space, avoiding the mixing dead angle caused by the single flow cross section in traditional tubular or trough mixers. The self-excited oscillating microbubble mineralization tube is connected to the slurry outlet of the spherical mixer, allowing the mixed slurry to directly enter the pipe organ cavity, throat and Helmholtz cavity for step-by-step processing without intermediate conveying links, thus avoiding the re-separation of the mixed reagent or the premature merging of bubbles during the conveying process. The organ-shaped cavity initially rectifyes and accelerates the slurry, providing a stable high-speed jet for the subsequent throat. The throat, through cross-sectional contraction, dramatically increases the slurry velocity, creating negative pressure. Gas introduced through the compressed air intake pipe is sheared and broken into microbubbles by the high-speed jet, achieving self-absorption of gas and in-situ generation of microbubbles. After the microbubble-containing slurry jet enters the Helmholtz cavity, it generates self-excited oscillations and forms microvortices, further refining the microbubbles and increasing their dispersion uniformity. Simultaneously, the microvortices promote the collision and adhesion of fine mineral particles and microbubbles, significantly improving mineralization efficiency. The entire mineralization process requires no mechanical stirring, relying entirely on fluid kinetic energy. The reagents are uniformly dispersed in the spherical mixer, avoiding reagent waste caused by excessively high or low local concentrations, and significantly reducing reagent consumption.

[0017] (2) In the mineralization device provided by the present invention, the spherical mixer uses the spherical inner cavity to guide the slurry and reagent to mix naturally during the flow process. The accordion cavity, throat, and Helmholtz cavity of the self-excited oscillating microbubble mineralization tube successively utilize the fluid's own contraction acceleration, negative pressure air intake, jet shearing, and self-excited oscillation to complete bubble generation and mineralization enhancement. The entire mixing, foaming, and mineralization process is driven entirely by the fluid kinetic energy of the slurry itself, without the need for mechanical stirring components and external energy input. Compared with the existing mechanical stirring mineralization device, the mechanical transmission components such as motors, reducers, and impellers are eliminated, and there are no mechanical wear and sealing leakage problems, resulting in an extremely simple structure. At the same time, the self-excited oscillating microbubble mineralization tube is connected to the spherical mixer through the slurry outlet, and the Helmholtz cavity outlet is connected to the mineralized slurry discharge pipe. The overall structure is compact, without complex moving parts, the equipment failure rate is extremely low, the service life is long, and the maintenance cost is significantly reduced.

[0018] (3) In some preferred embodiments, by setting multiple slurry feed pipes facing the center of the sphere on the spherical mixer, multiple slurries converge and counteract each other in the spherical space to form a high-intensity three-dimensional cross turbulent field, which further improves the mixing efficiency and uniformity of slurry and flotation reagents, effectively avoids unnecessary consumption caused by local enrichment of reagents, and significantly reduces the amount of reagents used while ensuring the subsequent mineralization effect.

[0019] (4) In some preferred embodiments, by arranging the slurry feed pipe in the equatorial plane and setting the flotation reagent addition pipe and the slurry outlet opposite each other on the vertical axis, the slurry and reagent form a three-dimensional cross flow pattern of "horizontal counter-current + vertical shear", which further eliminates the mixing blind zone and takes into account the full mixing and consistency of each area in the whole space.

[0020] (5) In some preferred embodiments, by setting a perforated baffle inside the spherical mixer, the slurry forms a micro vortex behind the baffle after passing through it, which further eliminates the dead zone of the flow field, increases the kinetic energy of the fine particles, takes into account both the slurry passability and the turbulence intensity, and ensures the mixing effect while maintaining the smooth flow of the slurry.

[0021] (6) In some preferred embodiments, by setting perforated baffles in each quadrant area and making the inclination angle of each baffle consistent, the uniformity of turbulence and flow field symmetry in all directions of the circumference of the spherical mixer are further guaranteed, and the balance of the mixing effect in each area is taken into account, providing stable and uniform feed conditions for subsequent self-excited oscillation mineralization.

[0022] (7) In some preferred embodiments, by controlling the tilt angle of the perforated baffle within a suitable range, the balance between effective turbulence and flow resistance is further taken into account, avoiding the problems of insufficient turbulence or obstruction of slurry passage, and achieving a good comprehensive balance between mixing effect and flow efficiency.

[0023] (8) In some preferred embodiments, by conforming one side of the perforated baffle to the inner wall of the spherical mixer and keeping the other side at a predetermined distance from the center of the ball, the stability of the baffle installation and the full utilization of the counter-turbulence in the center of the ball are further taken into account, so that the high-intensity turbulent mixing at the center of the ball and the turbulent mixing of the outer micro vortex can work together to achieve efficient mixing in the entire space of the mixer.

[0024] In this invention, the above-described technical solutions can be combined with each other to achieve more preferred combinations. Other features and advantages of this invention will be set forth in the following description, and some advantages may become apparent from the description or be learned by practicing the invention. The objects and other advantages of this invention can be realized and obtained from what is particularly pointed out in the description and drawings. Attached Figure Description

[0025] The accompanying drawings are for illustrative purposes only and are not intended to limit the invention. Throughout the drawings, the same reference numerals denote the same parts.

[0026] Figure 1 This is a schematic diagram of the structure of the mineralization device provided in an embodiment of the present invention; Figure 2 A schematic diagram of the structure of the self-excited oscillating microbubble mineralization tube in the mineralization device provided in an embodiment of the present invention; Figure 3 A cross-sectional schematic diagram of the Helmholtz cavity in the mineralization device provided in an embodiment of the present invention; Figure 4 This is a schematic diagram of the structure of the transmissionless flotation cell provided in an embodiment of the present invention; Figure 5 A schematic diagram of the structure of the self-excited oscillation microbubble mineralization device in a non-drive flotation cell provided in an embodiment of the present invention; Figure 6 A schematic diagram of the spatial layout and structure of the self-excited oscillating microbubble mineralization device and the annular air pipe in the transmissionless flotation cell provided in an embodiment of the present invention. Figure 7 This is a schematic diagram of microbubbles, microvortices, and mineralization bubbles in a self-excited oscillating microbubble mineralization device in a non-drive flotation cell provided in an embodiment of the present invention. Figure 8 This is a schematic diagram of the spatial distribution and structure of the nozzles inside the driveless flotation cell provided in an embodiment of the present invention; Figure 9 This is a schematic diagram of the internal flow stabilizing plate of the non-drive flotation cell provided in an embodiment of the present invention; Figure 10 This is a cross-sectional schematic diagram of the self-excited oscillation chamber in a non-drive flotation cell provided in an embodiment of the present invention; Figure 11 A cross-sectional schematic diagram of a second self-excited oscillation cavity added between the extension tube and the throat tube in a driveless flotation cell provided in an embodiment of the present invention; Figure 12 A schematic flowchart of the flotation method provided in an embodiment of the present invention; Figure label: 110-Spherical mixer; 111-Pulp feed pipe; 112-Flotation reagent addition pipe; 113-Pulp outlet; 114-Perforated baffle; 115-Equatorial plane; 116-Meridian plane; 117-Quadrant region; 120-Self-excited oscillating microbubble mineralization pipe; 121-Bug organ cavity; 122-Throat of mineralization device; 123-Compressed air intake pipe; 124-Contraction section; 125-Throat; 130-Helmholtz cavity; 131-Inlet of Helmholtz cavity; 132-Helmholtz cavity; 133-Helmholtz outlet section; 134-Helmholtz cross-section abrupt step; 135-Helmholtz collision wall; 136-Expansion angle of Helmholtz cavity; 140-Mineralized slurry discharge pipe; 1-Flotation cell body; 11-Flotation chamber; 12-Collection chamber; 2-Self-excited oscillation microbubble mineralization device; 21-Expansion pipe; 22-Throat of the non-drive flotation cell; 221-Air inlet; 23-Self-excited oscillation chamber (first self-excited oscillation chamber); 231-Inlet of the self-excited oscillation chamber; 232-Self-excited oscillation chamber; 233-Self-excited oscillation outlet section; 234-Sudden change step of the self-excited oscillation cross section; 235-Self-excited oscillation collision wall; 236-Expansion angle of the self-excited oscillation chamber; 24-Annular air pipe; 25-Outlet guide pipe; 251-Nozzle; 26-Inlet flange; 27-Outlet end Flange; 3-Feeding system; 31-Feed pipe; 32-Slurry distributor; 33-Inlet guide pipe; 4-Discharge system; 41-Concentrate discharge system; 411-Concentrate overflow trough; 412-Concentrate collection port; 42-Tailings discharge system; 421-Tailings discharge port; 422-Mid-ore discharge port; 5-Flow stabilizer; 51-Through hole; 6-Spraying device; 61-Annular clear water pipe; 62-Sprayer head; 7-Float; 8-Support; 9-Frame; 81-Inlet pressure gauge; 82-Outlet pressure gauge; 201-Fine mineral particles; 202-Microbubbles; 203-Mineralized bubbles; 204-Micro vortex; 150 - Second self-excited oscillation cavity; 151 - Oscillation turbulence block; 152 - Wear-resistant ceramic containing micropores. Detailed Implementation

[0027] Preferred embodiments of the present invention will now be described in detail with reference to the accompanying drawings, which form part of this application and are used together with the embodiments of the present invention to illustrate the principles of the present invention, but are not intended to limit the scope of the present invention.

[0028] In view of the problems of insufficient mineralization efficiency, high reagent consumption, high energy consumption, and high maintenance costs in existing mineralization devices, this invention innovatively constructs an integrated mineralization device consisting of a "spherical mixer - organ cavity - throat - Helmholtz cavity" based on the coupling mechanism of self-excited oscillation effect and jet foaming. Through the sequential connection and coordinated matching of the above four functional sections, this invention achieves a complete functional chain of slurry premixing, jet acceleration, negative pressure foaming, and self-excited oscillation mineralization without the need for external energy input or mechanical stirring. This overcomes the shortcomings of existing mineralization devices, such as single function, separation of various links, high energy consumption, and high reagent consumption.

[0029] In a first aspect, the present invention provides a mineralization apparatus, comprising: a spherical mixer having a spherical inner cavity, and the spherical mixer being provided with a slurry inlet, a flotation reagent addition inlet, and a slurry outlet; A self-excited oscillating microbubble mineralization tube is connected to the slurry outlet of the spherical mixer. The self-excited oscillating microbubble mineralization tube includes a pipe organ cavity, a throat, and a Helmholtz cavity that are connected sequentially along the slurry flow direction. The side wall of the throat is provided with a compressed air intake pipe, which is connected to an external air source. The outlet of the Helmholtz cavity is connected to a mineralized slurry discharge pipe.

[0030] Specifically, the present invention provides a mineralization device with a self-excited oscillation function.

[0031] Compared with existing technologies, the integrated mineralization device constructed in this invention comprises a spherical mixer, a bellows chamber, a throat, and a Helmholtz chamber connected sequentially along the slurry flow direction. The spherical mixer utilizes the strong turbulence and micro-vortices generated by the convergence and collision of multiple slurry streams to rapidly and uniformly premix the flotation reagents and slurry without mechanical stirring, reducing reagent consumption. The bellows chamber rectifyes and accelerates the mixed slurry, storing pressure energy for subsequent negative pressure foaming. The throat uses a high-speed jet to generate negative pressure self-absorbed gas and shear and break it into microbubbles. The Helmholtz chamber generates periodic pressure pulsations and micro-vortices through self-excited oscillation, further refining the microbubbles and enhancing particle-bubble collision and adhesion. Through the sequential connection and synergistic matching of the above four functional segments, this invention achieves a complete functional chain of slurry premixing, jet acceleration, negative pressure foaming, and self-excited oscillation mineralization without the need for external energy input and mechanical stirring. It realizes the integration of fine microbubble generation and mineralization enhancement, reducing reagent consumption, energy consumption, and maintenance costs.

[0032] To enhance the premixing effect of the slurry and flotation reagents, preferably, the spherical mixer is provided with at least two slurry feed pipes, each of which is arranged toward the center of the spherical mixer, so as to allow the slurry streams to converge and counteract each other within the spherical mixer.

[0033] In some embodiments, the spherical mixer has at least two slurry feed pipes within the equatorial plane passing through the center of the sphere; the spherical mixer has a flotation reagent addition pipe and a slurry outlet arranged opposite each other on an axis perpendicular to the equatorial plane and passing through the center of the sphere, and the self-excited oscillating microbubble mineralization pipe is connected to the slurry outlet. Thus, the slurry enters the spherical mixer from multiple directions within the equatorial plane, the reagents enter from the top, and after mixing, exit from the bottom, forming a three-dimensional cross-flow, promoting sufficient contact between the slurry and the reagents. The connection between the slurry feed pipe and the spherical mixer forms the slurry feed inlet. The connection between the flotation reagent addition pipe and the spherical mixer forms the flotation reagent addition outlet.

[0034] Preferably, each of the slurry feed pipes is symmetrically distributed around the center of the sphere, so that each stream of slurry converges and counteracts at the center of the sphere, achieving momentum balance and enhanced mixing.

[0035] In some embodiments, two slurry feed pipes are provided in the equatorial plane, which are symmetrically arranged with respect to the center of the sphere. The two slurries are injected into the spherical mixer in opposite directions and converge and counteract each other along the same straight line.

[0036] In some embodiments, three or four slurry feed pipes are provided in the equatorial plane, and each slurry feed pipe is evenly distributed around the center of the sphere, with each stream of slurry simultaneously directed toward the center of the sphere and converging against each other.

[0037] Preferably, the axes of each slurry feed pipe intersect at the center of the sphere to ensure that each stream of slurry collides head-on at the center of the sphere, forming a high-intensity turbulence zone, which is conducive to the rapid and uniform mixing of reagents and slurry.

[0038] In order to generate micro-vortices within the spherical mixer to enhance the mixing of the slurry and reagents, preferably, the spherical mixer is provided with perforated baffles inside.

[0039] Considering the flow path of the slurry within the spherical mixer and the turbulence coverage of the baffle, preferably, the perforated baffle is disposed in the quadrant region between the equatorial plane and the meridian plane of the spherical mixer, wherein the meridian plane is a plane passing through the center of the spherical mixer and perpendicular to the equatorial plane.

[0040] For example, at least one perforated baffle is provided in each of the quadrant regions. Thus, the perforated baffles effectively cover all four quadrant regions of the spherical mixer, ensuring that the slurry is turbulently acted upon by the baffles in all circumferential directions within the spherical mixer, avoiding localized undisturbed flow dead zones, and guaranteeing a uniform premixing effect between the slurry and the reagent within the spherical mixer.

[0041] In some embodiments, each of the quadrant regions is provided with a perforated baffle, and the perforated baffles have the same tilt angle relative to the equatorial plane, that is, the four perforated baffles are symmetrically distributed around the center of the sphere to ensure uniform turbulence of the slurry flow.

[0042] To achieve a balance between turbulence effect and flow resistance, the perforated baffle may optionally be tilted at an angle of 25° to 65° relative to the equatorial plane, preferably 30° to 60° (e.g., 35°, 40°, 45°, 50°, 55°, 60°). If the baffle tilt angle is too large, the turbulence effect is insufficient; if the tilt angle is too small, the flow resistance increases, potentially affecting the flow efficiency of the slurry. More preferably, the perforated baffle is tilted at an angle of 40° to 50° relative to the equatorial plane. Within this angle range, the baffle's turbulence effect on the slurry flow is more significant, and the flow resistance is moderate, which is beneficial for forming a stable and uniform micro-vortex field within the spherical mixer.

[0043] It is understandable that the perforated baffle has a porous structure. After the slurry flows through the perforated baffle, micro vortices are generated behind it, which helps to increase the kinetic energy of fine particles and eliminate dead zones in the flow field.

[0044] To balance slurry flowability and turbulence effect, the perforated baffle preferably has an opening ratio of 15% to 60% (e.g., 20%, 30%, 40%, 50%). If the opening ratio is too low, the slurry flow resistance is high, affecting flow efficiency; if the opening ratio is too high, the turbulence and dispersion effects are weakened, making it difficult to effectively generate micro-vortices. More preferably, the perforated baffle has an opening ratio of 25% to 45%. Within this range, it ensures smooth slurry flow through the baffle while generating sufficiently strong micro-vortices behind the baffle, achieving efficient mixing of the slurry and reagents. Even more preferably, the perforated baffle has an opening ratio of 30% to 40%, at which point the slurry flowability and turbulence effect achieve an optimal balance, making it particularly suitable for pre-treatment of fine-grained minerals before flotation.

[0045] To ensure that the perforated baffle can generate effective turbulence without obstructing the counter-mixing in the center region of the sphere, specifically, the surface of the perforated baffle faces the center of the spherical mixer but does not pass through the center of the sphere.

[0046] Preferably, one side of the perforated baffle is conformally fitted and fixed to the inner wall of the spherical mixer, and the shortest distance between the other side and the center of the spherical mixer is not less than 1 / 5 of the radius of the spherical mixer. More specifically, the shortest distance between the other side of the perforated baffle and the center of the spherical mixer is 1 / 5 to 1 / 3 of the radius of the spherical mixer, to ensure that the perforated baffle does not obstruct the center area, avoids the opposing mixing of slurry in the center area, and at the same time ensures effective turbulence.

[0047] Considering the impact of baffle area on flow disturbance and slurry flow capacity, preferably, the area of ​​each perforated baffle is 1 / 20 to 2 / 5 of the equatorial plane area of ​​the spherical mixer, more preferably 1 / 5 to 1 / 3. If the baffle area is too small, the flow disturbance effect is limited; if the area is too large, it will excessively obstruct the flow channels of the slurry and reagents. The total projected area of ​​the four baffles can reach a maximum of 160% of the equatorial plane area, with gaps still allowed between the baffles and in the central area.

[0048] For example, the ratio of the volume of the spherical inner cavity of the spherical mixer to the total cross-sectional area of ​​the slurry feed pipe is 5:1 to 100:1 (e.g., 20:1, 30:1, 40:1, 60:1, 80:1), and further to 10:1 to 50:1, to ensure that the slurry has sufficient residence time in the spherical mixer to achieve thorough mixing, while avoiding uneven reagent dispersion caused by excessive volume.

[0049] For example, the inner diameter of the slurry feed pipe is 1 / 10 to 1 / 5 of the radius of the spherical mixer to ensure that the slurry enters the spherical mixer at an appropriate jet velocity, and to ensure that the slurry flow rate meets the processing requirements while ensuring sufficient jet velocity.

[0050] Preferably, the outlet end of the flotation reagent addition pipe is equipped with a spray head or a dispersing screen. This allows the flotation reagent to be sprayed into the spherical mixer in the form of fine droplets or mist, effectively increasing the contact area between the reagent and the slurry. This avoids the problems of excessively high local concentrations and uneven dispersion that may occur when the reagent is added in a single stream, improving the uniformity of reagent dispersion in the slurry and reducing reagent consumption. This is particularly suitable for flotation of fine-grained minerals where high reagent dispersion is required.

[0051] For example, the thickness of the perforated baffle is 1 / 50 to 1 / 20 (e.g., 1 / 40, 1 / 30) of the radius of the spherical mixer to ensure that the baffle has sufficient structural strength while avoiding additional flow resistance caused by excessive baffle thickness.

[0052] For example, the perforated baffle has a circular, elliptical, or rectangular opening shape, preferably circular, with a diameter of 2mm to 10mm (e.g., 4mm, 6mm, 8mm). When the slurry passes through the circular opening, the flow resistance is small, which is beneficial for forming uniform micro-vortices behind the baffle.

[0053] To provide initial acceleration of the slurry and prepare for the subsequent Venturi effect at the throat, preferably, the pipe organ cavity is a variable-diameter straight pipe structure, with the inner diameter of the inlet end of the pipe organ cavity being larger than that of the outlet end along the slurry flow direction. Considering the influence of the degree of contraction of the pipe organ cavity on the slurry acceleration effect, optionally, the ratio of the inner diameter d1' of the inlet end to the inner diameter d2' of the outlet end of the pipe organ cavity is 1.1:1 to 3.5:1, preferably 1.2:1 to 3:1 (e.g., 1.8:1, 2.0:1, 2.2:1, 2.8:1). If the ratio is too small, the acceleration effect is not obvious; if the ratio is too large, the flow resistance increases, which may affect the slurry flow efficiency. More preferably, the ratio of the inner diameter d1' of the inlet end to the inner diameter d2' of the outlet end of the pipe organ cavity is 1.5:1 to 2.5:1. Within this ratio range, the acceleration effect and flow resistance of the slurry in the pipe organ cavity are optimally balanced, which can provide sufficient jet velocity for the Venturi effect at the subsequent throat, and will not affect the smooth flow of the slurry due to excessive contraction and excessive slurry flow resistance.

[0054] In some embodiments, for the mineralization apparatus, the inner diameter d2' of the outlet end of the organ cavity is equal to the inner diameter d3' of the inlet end of the throat. This allows for a smooth transition of the slurry from the organ cavity to the throat, avoiding additional flow resistance caused by abrupt changes in cross-section.

[0055] For the aforementioned mineralization device, in order to utilize the Venturi effect to generate negative pressure to draw in air and shear it to form microbubbles, preferably, the throat of the mineralization device is a Venturi tube structure. The throat consists of a contraction section and a throat section sequentially along the slurry flow direction. The inner diameter of the contraction section gradually decreases from the inlet end towards the throat, and the inner diameter of the throat is the minimum inner diameter d4' of the throat tube. The slurry accelerates in the contraction section and reaches its highest flow velocity in the throat, forming the lowest static pressure zone.

[0056] For the aforementioned mineralization device, considering the influence of the throat's contraction on the negative pressure and bubble breaking effect, the ratio of the minimum inner diameter d4' of the throat to the inner diameter d3' of the throat's inlet end is optionally 0.3:1 to 0.8:1, preferably 0.4:1 to 0.7:1. If the ratio is too small, the throat flow velocity is too high, and the flow resistance increases significantly; if the ratio is too large, the negative pressure is insufficient, and the air intake effect is weakened. More preferably, the ratio of the minimum inner diameter d4' of the throat to the inner diameter d3' of the throat's inlet end is 0.5:1 to 0.6:1. Within this ratio range, the throat can generate sufficient negative pressure to efficiently draw in air and achieve sufficient shearing and breaking of bubbles, while avoiding a significant increase in slurry flow resistance due to an excessively small throat cross-section, thus achieving a better balance between air intake effect and flow smoothness.

[0057] For the aforementioned mineralization device, in order to draw in air at the location with the strongest negative pressure, the compressed air intake pipe is located at the throat of the throat tube. Specifically, the compressed air intake pipe is located at 1 / 3 to 2 / 3 of the length of the throat from the inlet end along the slurry flow direction. At this point, the throat cross-section is at its smallest, the flow velocity is at its highest, and the static pressure is at its lowest, which is most conducive to air intake. More preferably, the compressed air intake pipe is located at 2 / 5 to 3 / 5 of the length of the throat from the inlet end along the slurry flow direction, that is, the middle 1 / 5 of the throat. Within this position range, the throat cross-section approaches its smallest, the flow velocity approaches its highest, and the static pressure approaches its lowest, thus achieving the best negative pressure air intake effect.

[0058] For the aforementioned mineralization device, considering the influence of compressed air intake on microbubble generation efficiency, the ratio of the inner diameter d5' of the compressed air intake pipe to the minimum inner diameter d4' of the throat pipe is optionally 0.05:1 to 0.4:1, preferably 0.1:1 to 0.3:1. If the ratio is too small, the intake volume is insufficient, resulting in low microbubble generation efficiency; if the ratio is too large, it may disrupt the negative pressure conditions in the throat, affecting the self-priming effect.

[0059] It is understandable that after air enters the throat through the compressed air intake pipe, it is broken into a large number of microbubbles under the shearing action of the high-speed jet. Microbubbles have a huge specific surface area, which can efficiently capture hydrophobic fine particles in the slurry, and further refine them under the resonance action of the subsequent Helmholtz chamber. At the same time, they are fully mixed with reagents to form stable mineralized bubbles, providing the preconditions for subsequent flotation separation.

[0060] To generate a high-frequency self-excited oscillating jet to achieve secondary refinement of microbubbles and enhanced turbulence of the slurry, preferably, the Helmholtz cavity includes a Helmholtz cavity body (i.e., the resonant cavity of the Helmholtz cavity) and a Helmholtz outlet section; the end of the throat outlet section of the mineralization device enters the inlet of the Helmholtz cavity body; the cross-sectional area of ​​the Helmholtz cavity body is larger than the cross-sectional area of ​​the end of the throat outlet section of the mineralization device, so that a Helmholtz cross-sectional abrupt step is formed at the inlet of the Helmholtz cavity body; The outlet of the Helmholtz cavity extends outward to form the Helmholtz outlet section, and the cross-sectional area of ​​the Helmholtz cavity is larger than the cross-sectional area of ​​the Helmholtz outlet section; The Helmholtz outlet section is coaxially arranged with the inlet of the Helmholtz cavity, and the outlet at the end of the Helmholtz outlet section is connected to the mineralized slurry discharge pipe. The inner wall surfaces of the Helmholtz cavity near the Helmholtz outlet section and located on both sides of the Helmholtz outlet section constitute Helmholtz collision walls, with the wall surfaces of the Helmholtz collision walls facing the inlet direction of the Helmholtz cavity.

[0061] It is understandable that after the slurry enters the Helmholtz cavity, longitudinal resonance and low-frequency pulsation are generated within the resonant cavity, forming a high-frequency self-excited oscillating jet. The collision wall reflects the jet to form a pressure feedback wave, which interacts with the continuously entering jet to maintain stable self-excited oscillation.

[0062] Preferably, the inner diameter d at the maximum cross-section of the Helmholtz cavity is... X1 The inner diameter d of the end of the throat outlet section of the mineralization device X3 The ratio is 1.5:1 to 10:1 (e.g., 3:1, 4:1, 5:1, 6:1, 7:1), and further 2:1 to 8:1. If the ratio is too small, the jet expansion is insufficient, resulting in inadequate oscillation intensity; if the ratio is too large, the cavity volume is too large, which may affect the stability of the resonant frequency. More preferably, the inner diameter d at the maximum cross-section of the Helmholtz cavity... X1 The inner diameter d of the end of the throat outlet section of the mineralization device X3 The ratio is 3:1 to 6:1. At this point, the jet expands and develops fully in the resonant cavity, and the oscillation intensity and the cavity volume reach a better balance.

[0063] Considering that the aspect ratio of the resonant cavity affects its resonant frequency and oscillation stability, the axial length d of the Helmholtz cavity (i.e., the resonant cavity of the Helmholtz cavity) is... X2 The inner diameter d at the maximum cross-section of the Helmholtz cavity (i.e., the resonant cavity of the Helmholtz cavity) X1 The ratio is 0.2:1 to 10:1, preferably 0.4:1 to 8:1 (e.g., 0.4:1, 0.8:1, 1.2:1, 1.5:1, 2.0:1, 3.0:1, 4.0:1, 6.0:1, 8.0:1).

[0064] To ensure sufficient jet velocity and impact force when the jet exits the resonant cavity through the outlet section, the inner diameter d of the Helmholtz outlet section is [specifically determined]. X4 The inner diameter d of the end of the throat outlet section of the mineralization device X3 The ratio is 0.2:1 to 1.2:1, preferably 0.4:1 to 1:1 (e.g., 0.6:1, 0.7:1, 0.8:1). When the ratio approaches 1, the jet velocity is relatively low, but the flow resistance is small; when the ratio approaches 0.4, the jet velocity is high and the impact force is strong, but the flow resistance increases accordingly. More preferably, the inner diameter d of the Helmholtz outlet section... X4 The inner diameter d of the end of the throat outlet section of the mineralization device X3 The ratio is 0.5:1 to 0.9:1. At this ratio, the jet velocity and flow resistance are more balanced, which is conducive to forming an oscillating jet with sufficient impact force, while ensuring the smooth flow of the slurry.

[0065] To ensure effective reflection of the jet by the collision wall and maintain stable pressure feedback oscillation, the angle α' between the wall surface of the Helmholtz collision wall (i.e., the collision wall of the Helmholtz cavity) and the axis of the Helmholtz cavity can optionally be 25° to 75°, preferably 30° to 70° (e.g., 40°, 50°, 60°). If the angle is too small, the jet reflection direction deviates from the axis, reducing the feedback efficiency; if the angle is too large, the energy loss of the jet at the collision wall increases, weakening the oscillation intensity. More preferably, the angle α' between the wall surface of the Helmholtz collision wall (i.e., the collision wall of the Helmholtz cavity) and the axis of the Helmholtz cavity is 35° to 65°. At this angle, the reflection efficiency of the collision wall on the jet is higher, the transmission path of the pressure feedback wave is better, and it is beneficial to maintain stable self-excited oscillation.

[0066] To control the diffusion angle of the jet as it exits the outlet section and achieve optimal mineralization, the included angle β' between the upper and lower inclined surfaces extending outward from the end of the Helmholtz outlet section (i.e., the expansion angle of the Helmholtz cavity) is 15° to 65°, preferably 20° to 60° (e.g., 30°, 40°, 50°). If the included angle is too small, the jet diffusion is insufficient, and the mineralization effect is limited; if the included angle is too large, the jet diffuses excessively, and the impact force decreases. More preferably, the included angle β' between the upper and lower inclined surfaces extending outward from the end of the Helmholtz outlet section is 25° to 55°. At this angle, the jet diffusion angle and impact force achieve a better balance, which is conducive to forming optimal particle-bubble collision conditions in the mineralization region.

[0067] It is understandable that Helmholtz chambers, when used alone in underwater operations such as ship cleaning and rock-breaking drilling, focus on generating high-impact pulsed jets to break up or remove target materials, with the chamber structure parameters primarily designed to maximize impact energy. However, directly applying traditional Helmholtz chambers to the flotation mineralization stage presents the following problems: First, the chamber size and internal structure of traditional Helmholtz chambers are designed primarily for high-impact jets, resulting in high resonant frequencies and short pulsation periods. This fails to provide sufficient residence time and space for collisions between fine particles and microbubbles, limiting the mineralization effect. Second, traditional Helmholtz chambers are typically used in conjunction with high-pressure gas sources or external excitation devices, leading to complex structures, high energy consumption, and the inability to be driven solely by the fluid kinetic energy of the slurry. Third, when used as independent devices, traditional Helmholtz chambers lack coordinated matching with upstream bubble generation structures, resulting in unstable initial states when the jet enters the chamber, making it difficult to maintain continuous self-excited oscillations, leading to insufficient bubble refinement and poor consistency in mineralization.

[0068] To address the aforementioned issues, this invention optimizes and controls the key structural parameters of the Helmholtz cavity, ensuring they are coordinated with the dimensional parameters of the upstream organ cavity and throat. This coordinated dimensional proportion ensures stable self-excited oscillation of the jet within the Helmholtz cavity, resulting in better microbubble refinement and mineralization. Parameters such as the diameter, length, outlet contraction, collision wall inclination angle, and outlet expansion angle of the resonant cavity collectively determine the resonant frequency, oscillation intensity, and jet characteristics of the Helmholtz cavity; these parameters are interconnected and mutually restrictive. After the microbubble-containing slurry jet enters the Helmholtz cavity, periodic pressure pulsations are generated under the cavity's resonance, creating microvortices within the cavity. These microvortices promote the collision and adsorption of fine particles with microbubbles and enhance the uniform mixing of the slurry and residual flotation reagents, further adsorbing the reagents onto the particle surface, thereby improving mineralization efficiency. Finally, the mineralized slurry is discharged through the mineralized slurry discharge pipe into the flotation equipment for subsequent flotation operations.

[0069] Secondly, the present invention provides a self-excited oscillation enhanced flotation system, comprising: Slurry pretreatment subsystem; the slurry pretreatment subsystem includes the aforementioned mineralization device; And at least one of the coarse selection subsystem, fine selection subsystem and sweeping selection subsystem; At least one of the coarse flotation subsystem, the fine flotation subsystem, and the scavenging subsystem includes a non-driven flotation cell. Preferably, at least one of the coarse flotation subsystem, the fine flotation subsystem, and the scavenging subsystem includes a non-driven flotation cell with self-excited oscillation function.

[0070] In some embodiments, the driveless flotation cell with self-excited oscillation function includes: The flotation cell body includes a flotation chamber and a collection chamber connected to the bottom of the flotation chamber; The self-excited oscillation microbubble mineralization device is located outside the main body of the flotation cell. The self-excited oscillation microbubble mineralization device includes an expansion pipe, a throat pipe and a self-excited oscillation chamber that are connected in sequence along the direction of slurry flow. An air inlet is provided on the side wall of the throat pipe and is connected to an external air source. The outlet of the self-excited oscillation chamber is connected to the inside of the flotation chamber. The feeding system is connected to the inlet of the self-excited oscillating microbubble mineralization device and is used to feed the slurry into the self-excited oscillating microbubble mineralization device. The discharge system is located on the upper part of the flotation chamber and the collection chamber, respectively, and is used to discharge concentrate, middlings and tailings.

[0071] Compared with existing technologies, the integrated device constructed in this invention comprises an expansion pipe, a throat, and a self-excited oscillation chamber connected sequentially along the slurry flow direction. These three components work in concert: the expansion pipe provides pressure energy storage for the throat, the throat introduces gas through an air inlet and utilizes jet shearing to form microbubbles, and the self-excited oscillation chamber further acts on the microbubbles and generates microvortices to enhance mineralization. These three components sequentially complete a functional chain of pressure energy storage, bubble generation, and mineralization enhancement along the slurry flow direction, achieving the integration of precise microbubble generation and efficient mineralization. The entire device requires no mechanical transmission components or external energy input, featuring a simple structure and convenient maintenance.

[0072] In some embodiments, the self-excited oscillation chamber includes a self-excited oscillation body (i.e., the resonant cavity of the self-excited oscillation chamber) and a self-excited oscillation outlet section; the throat outlet section of the non-drive flotation cell has an inlet at the end that enters the self-excited oscillation body. The cross-sectional area of ​​the self-excited oscillation cavity is larger than the cross-sectional area of ​​the throat outlet section of the non-drive flotation cell, so that a step-change in the self-excited oscillation cross section is formed at the inlet of the self-excited oscillation cavity. The outlet of the self-excited oscillation cavity extends outward to form the self-excited oscillation outlet section, and the cross-sectional area of ​​the self-excited oscillation cavity is larger than the cross-sectional area of ​​the self-excited oscillation outlet section; The self-excited oscillation outlet section is coaxially arranged with the inlet of the self-excited oscillation cavity, and the outlet at the end of the self-excited oscillation outlet section is connected to the interior of the flotation cavity; The inner wall surfaces of the self-excited oscillation cavity near the self-excited oscillation outlet section and located on both sides of the self-excited oscillation outlet section constitute a self-excited oscillation collision wall, and the wall surface of the self-excited oscillation collision wall faces the inlet direction of the self-excited oscillation cavity.

[0073] It is understandable that after the jet is ejected at high speed from the throat, it enters the self-excited oscillation cavity and suddenly expands at the abrupt change step in the cross-section, exciting the initial disturbance and vortex of the jet. When the jet propagates to the outlet end in the resonant cavity, it collides with the collision wall, which reflects the jet to form a pressure feedback wave that propagates in the opposite direction along the cavity axis. This pressure feedback wave interacts with the continuously entering jet to form periodic pressure pulsations and stable self-excited oscillation. During the oscillation, a strong micro-vortex field is generated in the resonant cavity. The micro-vortex field can significantly increase the collision probability of fine particles and microbubbles and promote the adhesion of fine particles and microbubbles. The self-excited oscillation outlet section is set coaxially with the inlet of the self-excited oscillation cavity, which ensures that the jet after oscillation is smoothly ejected in a straight line and reduces energy loss.

[0074] In some embodiments, the feeding system includes a feed pipe, a slurry distributor, and an inlet guide pipe. The feed pipe is connected to the inlet of the slurry distributor, and the outlet of the slurry distributor is connected to the inlet of the self-excited oscillating microbubble mineralization device through the inlet guide pipe.

[0075] It is understood that the slurry enters the slurry distributor through the feed pipe. Preferably, the slurry distributor evenly distributes the slurry to each of the self-excited oscillating microbubble mineralization devices to ensure that each device obtains the same flow rate and pressure of slurry, and avoids differences in mineralization effect caused by uneven flow distribution. The inlet guide pipe serves as the connection channel between the slurry distributor and the self-excited oscillating microbubble mineralization device, and smoothly guides the slurry into the expansion pipe.

[0076] In some embodiments, the inner diameter of the inlet end of the expansion tube is greater than the inner diameter of the outlet end of the inlet guide tube, the inner diameter of the inlet end of the throat tube is less than or equal to the inner diameter of the outlet end of the expansion tube, and the inner diameter of the inlet end of the self-excited oscillation chamber is greater than the inner diameter of the outlet end of the throat tube.

[0077] It should be noted that by controlling the dimensional relationship between the inner diameter of the inlet end and the inner diameter of the outlet end of each of the above sections, the slurry undergoes a series of cross-sectional changes of "expansion-contraction-expansion" as it flows through the self-excited oscillating microbubble mineralization device: First, the cross-section expands in the expansion tube, the flow velocity decreases and the static pressure increases, storing pressure energy for subsequent negative pressure air intake; then, the cross-section contracts in the throat tube, the flow velocity increases sharply and the static pressure decreases, forming a negative pressure zone to draw in external air and shear it into microbubbles; finally, when it enters the self-excited oscillation chamber, the cross-section expands again, the jet expands and generates self-excited oscillation in the resonant cavity, forming microvortices to promote the collision and adhesion of fine particles and microbubbles, thus achieving efficient mineralization of the slurry.

[0078] In some embodiments, the dimensional proportions of the key components in the self-excited oscillating microbubble mineralization device without a drive flotation cell are as follows: (a) Diameter ratio at the joints of each segment To ensure a smooth transition of the slurry between sections and to create fluid conditions conducive to self-excited oscillation, the inner diameter d at the inlet end of the expansion pipe is... e1 The inner diameter d of the outlet end of the inlet guide pipe is... g The slurry concentration is 0.9 to 5.0 times that of the expansion pipe, preferably 1.01 to 3.0 times (e.g., 1.1, 1.2, 1.3, 1.4, 1.5, 1.8, 2.0, 2.5 times), and further preferably 1.01 to 1.5 times (more preferably 1.05 to 1.15 times). This results in an increased cross-section, decreased flow velocity, and increased static pressure when the slurry enters the expansion pipe from the inlet end guide pipe, providing conditions for the subsequent Venturi negative pressure intake at the throat.

[0079] To ensure sufficient acceleration of the slurry as it enters the throat from the expansion pipe to create negative pressure for air intake, the inner diameter d at the inlet end of the throat is... h1 The inner diameter d of the outlet end of the expansion tube e2The ratio is 0.5 to 1.2 times, preferably 0.6 to 1.0 times, such as 0.7 times, 0.8 times, or 0.9 times, and more preferably 0.85 to 0.95 times. Therefore, the cross-section of the slurry at the throat inlet is appropriately reduced, increasing the flow velocity. According to Bernoulli's principle, the static pressure decreases, forming a negative pressure zone, which is beneficial for the intake of external air and shearing and crushing.

[0080] To ensure that the jet can fully expand and generate oscillation after entering the self-excited oscillation chamber, the inner diameter d of the resonant cavity of the self-excited oscillation chamber, i.e., the maximum cross-section of the self-excited oscillation chamber, is... Z1 The inner diameter d of the outlet end of the expansion tube e2 The ratio is 0.9 to 1.5 times (preferably 1 to 1.25 times). By controlling the ratio of the inner diameter of the expansion tube outlet end to the inner diameter of the resonant cavity at its maximum cross-section, and in conjunction with the accelerating effect of the throat contraction section, the slurry obtains a suitable velocity and expansion space when it enters the resonant cavity after being accelerated through the throat. If d Z1 / d e2 If the ratio is too small, the jet will not expand sufficiently after entering the resonant cavity, making it difficult to form vortices and pressure pulsations of a sufficiently large size within the cavity, thus hindering the effective establishment of self-excited oscillations. If the ratio is too large, the excessive expansion of the jet will cause its velocity to decay too quickly, resulting in insufficient energy to impact the walls and form a stable pressure feedback wave, making it difficult to maintain the oscillation. An appropriate ratio ensures that the jet expands sufficiently to excite oscillations while retaining enough impact energy to maintain continuous and stable self-excited oscillations, thereby achieving secondary refinement and mineralization enhancement of microbubbles.

[0081] (b) Expansion ratio of the expansion tube itself To control the deceleration and diffusion effect of the slurry within the expansion pipe, the inner diameter d at the outlet end of the expansion pipe is... e2 The inner diameter d of the inlet end of the expansion tube e1 The ratio is 1:1 to 1.6:1, and more preferably 1.1:1 to 1.5:1 (1.15:1 to 1.3:1). As a result, the expansion tube achieves a tapered gradual expansion, and the flow velocity of the slurry gradually decreases and the static pressure gradually increases within the expansion tube, providing sufficient pressure energy reserves for the negative pressure air intake at the subsequent throat.

[0082] (c) The proportion of spontaneous contraction of the larynx To achieve sufficient negative pressure at the throat to draw in air and shear it to form microbubbles, the inner diameter of the throat in the non-driven flotation cell gradually decreases from the inlet end to the middle, making the minimum inner diameter d of the throat... hmin Located in the middle of the throat; the minimum inner diameter d of the throat without a drive flotation cell. hmin The inner diameter d of the inlet end of the throat of the non-driven flotation cell h1The ratio is 0.3:1 to 0.85:1, further 0.4:1 to 0.8:1 (e.g., 0.45:1, 0.6:1, 0.65:1, 0.75:1), preferably 0.5:1 to 0.7:1. Thus, the slurry is accelerated to its highest velocity within the throat, forming a zone of lowest static pressure. External air is drawn into the throat under the pressure difference and broken into microbubbles under the shearing action of the high-speed jet. The throat of the non-driven flotation cell consists of a contraction section and a throat section along the slurry flow direction. The inner diameter of the contraction section gradually decreases from the inlet end towards the throat, and the inner diameter of the throat section is the minimum inner diameter d of the throat of the non-driven flotation cell. hmin The slurry accelerates in the contraction section, reaching its highest velocity at the throat, forming the lowest static pressure zone.

[0083] (d) The relationship between the axial length of each segment and the minimum inner diameter of the throat. To ensure that each section has sufficient length to achieve the corresponding hydrodynamic functions, the minimum inner diameter d of the throat of the non-driven flotation cell is used. hmin Based on: the axial length L of the throat of the flotation cell without transmission h The minimum inner diameter d of the throat of the non-drive flotation cell is hmin The axial length L of the expansion tube is 1.5 to 6.0 times (e.g., 2 times, 3 times, 4 times, 5 times), preferably 1.6 to 4.0 times. e The minimum inner diameter d of the throat of the non-drive flotation cell is hmin The axial length L of the self-excited oscillation chamber is 1 to 5 times (e.g., 2 times, 3 times, 4 times, 5 times), preferably 1.5 to 3.5 times. c The minimum inner diameter d of the throat of the non-drive flotation cell is hmin The axial length of each section is 2 to 10 times (e.g., 2 times, 3 times, 4 times, 5 times, 6 times, 8 times, 9 times), preferably 3 to 7 times. This coordinated ratio between the axial length of each section and the minimum inner diameter of the throat ensures that the slurry has sufficient space for flow development within each section, preventing insufficient length from causing the fluid to enter the next section before it has fully developed, while also avoiding unnecessary flow resistance losses due to excessive length.

[0084] (e) Internal dimensions of the self-excited oscillation chamber The self-excited oscillation chamber includes a self-excited oscillation cavity (i.e., the resonant cavity of the self-excited oscillation chamber) and a self-excited oscillation outlet section (i.e., the outlet section of the self-excited oscillation chamber). To ensure that the jet generates stable self-excited oscillation within the resonant cavity, the following coordinated proportional relationship exists between the internal dimensions: The inner diameter d at the maximum cross-section of the self-excited oscillation cavity Z1 The inner diameter d of the throat outlet section end of the non-drive flotation cell Z3The ratio is 1.5:1 to 10:1 (e.g., 3:1, 4:1, 5:1, 6:1, 7:1, 8:1), and further 2:1 to 10:1 (preferably 3:1 to 6:1). Thus, when the jet enters the self-excited oscillation cavity from the throat, the cross-section suddenly expands, forming strong vortices and pressure pulsations within the cavity, providing an initial disturbance source for the establishment of self-excited oscillation.

[0085] The axial length d of the self-excited oscillation cavity Z2 The inner diameter d at the maximum cross-section of the self-excited oscillation cavity Z1 The ratio is 0.2:1 to 8:1 (e.g., 0.4:1, 0.8:1, 1.2:1, 1.5:1, 2.0:1, 3.0:1, 4.0:1, 6.0:1, 8.0:1).

[0086] The inner diameter d of the self-excited oscillation outlet section Z4 The inner diameter d of the throat outlet section end of the non-drive flotation cell Z3 The ratio is 0.4:1 to 1:1 (e.g., 0.6:1, 0.7:1, 0.8:1), preferably 0.5:1 to 0.9:1. Thus, the outlet section of the self-excited oscillation cavity is in a contracted or constant-diameter state relative to the throat outlet section. The jet is accelerated as it exits the resonant cavity through the outlet section, forming an oscillating jet with sufficient impact force.

[0087] The angle α between the self-excited oscillation collision wall (i.e., the wall surface of the collision wall of the self-excited oscillation chamber) and the axial direction of the self-excited oscillation chamber is 20° to 80°, preferably 30° to 70° (e.g., 40°, 50°, 60°), and more preferably 35° to 65°. Thus, when the jet propagates within the resonant cavity to the outlet end, it impacts the collision wall, and the appropriate tilt angle forms an effective pressure feedback wave, maintaining stable self-excited oscillation.

[0088] The angle β between the upper and lower inclined surfaces that expand outward from the end of the self-excited oscillation outlet section (i.e., the expansion angle of the self-excited oscillation chamber) is 20° to 60° (e.g., 30°, 40°, 50°), preferably 25° to 55°. Therefore, the jet exiting from the outlet section of the self-excited oscillation chamber has a suitable diffusion angle, which ensures effective diffusion of the jet within the flotation chamber to achieve uniform distribution of mineralized bubbles, while maintaining sufficient jet impact force.

[0089] It is understandable that Helmholtz chambers, when used alone in underwater operations such as ship cleaning and rock-breaking drilling, focus on generating high-impact pulsed jets to break up or remove target materials, with the chamber structure parameters primarily designed to maximize impact energy. However, directly applying traditional Helmholtz chambers to the flotation mineralization process presents the following problems: First, the chamber size and internal structure of traditional Helmholtz chambers are designed primarily for high-impact jets, resulting in high resonant frequencies and short pulsation periods. This fails to provide sufficient residence time and space for collisions between fine particles and microbubbles, limiting the mineralization effect. Second, traditional Helmholtz chambers are typically used in conjunction with high-pressure gas sources or external excitation devices, leading to complex structures, high energy consumption, and the inability to be driven solely by the fluid kinetic energy of the slurry. Third, when used as independent devices, traditional Helmholtz chambers lack coordinated matching with upstream bubble generation structures, resulting in unstable initial states when the jet enters the chamber, making it difficult to maintain continuous self-excited oscillations.

[0090] To address the aforementioned issues, this invention preferably controls parameters such as the inner diameter of the throat outlet section of the non-drive flotation cell, the inner diameter at the maximum cross-section of the self-excited oscillation chamber, the axial length of the self-excited oscillation chamber, the inner diameter of the self-excited oscillation outlet section, the inclination angle α of the self-excited oscillation collision wall, and the expansion angle β of the self-excited oscillation chamber. This ensures that these parameters are coordinated with the dimensional parameters of the upstream expansion pipe and the throat, enabling the microbubble-containing jet to generate stable self-excited oscillations without external energy input after entering the chamber, thereby achieving secondary refinement and mineralization enhancement of the microbubbles.

[0091] (f) Dimensional proportions of the air inlet and annular air pipe The air inlet is located in the middle of the throat tube, and at the point of minimum cross-section of the throat tube (e.g., the throat); the inner diameter d of the air inlet is... a The minimum inner diameter d of the throat. hmin The ratio is 0.05 to 0.5 times (e.g., 0.15, 0.2, 0.25, 0.35, 0.4, 0.45 times), preferably 0.1 to 0.3 times. Thus, the air inlet is positioned within the throat where the flow velocity is highest and the static pressure is lowest, ensuring that air is drawn in under maximum pressure differential and broken into microbubbles by high-speed jet shearing.

[0092] The air inlet is connected to an annular air pipe via a pipe. The annular air pipe is arranged around the outer periphery of the flotation chamber, and the inner diameter d of the annular air pipe is... r The inner diameter d of the air inlet a The diameter of the central ring of the annular air tube is 1.2 to 8 times, more preferably 1.2 to 3 times (preferably 1.5 to 2.5 times); r The outer diameter D of the flotation chamber tThe air volume is 1 to 1.5 times (preferably 1.1 to 1.3 times) that of the self-excited oscillating microbubble mineralization device. Therefore, the annular air pipe can simultaneously and uniformly supply air to multiple self-excited oscillating microbubble mineralization devices, ensuring consistent air intake for each device and avoiding differences in mineralization effects caused by uneven air supply.

[0093] In some embodiments, the outlet of the self-excited oscillating microbubble mineralization device is connected to the interior of the flotation chamber through an outlet end guide pipe. The outlet end guide pipe extends through the wall of the flotation chamber into the interior of the flotation chamber, and a nozzle is provided at the end of the outlet end guide pipe.

[0094] In some embodiments, a flow stabilizer is provided inside the flotation chamber. The flow stabilizer is located above the outlet guide pipe. The flow stabilizer is a horizontally arranged plate structure with through holes on its surface. The flow stabilizer is arranged at intervals along the axial direction of the flotation chamber.

[0095] In some embodiments, the outlet of the guide pipe extends into the flotation chamber at a position 1 / 8 to 1 / 3 of the height of the flotation chamber (preferably 1 / 5 to 1 / 4 of the height). Thus, the outlet of the guide pipe is located in the lower region of the flotation chamber, providing sufficient travel for the mineralized bubbles to rise, allowing them to fully mineralize and form a stable foam layer during their ascent, while also preventing the mineralized bubbles from being directly sucked into the tailings discharge outlet due to an excessively low outlet position.

[0096] In some embodiments, the distance between the outlet of the outlet guide pipe and the nearest stabilizing plate is not less than 1 / 10 of the total height of the flotation chamber; preferably, the distance between the outlet of the outlet guide pipe and the nearest stabilizing plate is 1 / 9 to 1 / 5 of the total height of the flotation chamber, and more preferably 1 / 8 to 1 / 7. Thus, sufficient distance is maintained between the outlet of the outlet guide pipe and the stabilizing plate, which avoids direct impact of the jet stream on the stabilizing plate causing flow field turbulence, and ensures that mineralized bubbles have sufficient space for preliminary separation before rising to the stabilizing plate.

[0097] In some embodiments, the distance between the outlet of the outlet guide pipe and the tailings discharge port at the bottom of the collecting chamber is not less than 1 / 8 of the total height of the flotation cell body; preferably, the distance between the outlet of the outlet guide pipe and the tailings discharge port at the bottom of the collecting chamber is 1 / 4 to 2 / 5 of the total height of the flotation cell body. Thus, a sufficient distance is maintained between the outlet of the outlet guide pipe and the tailings discharge port to prevent mineralized bubbles from being carried away by the tailings flow before completing their flotation separation, ensuring that the bubbles have sufficient time to rise to the froth layer.

[0098] In some embodiments, the number of flow stabilizers is 1 to 5 (e.g., 2, 4), and more specifically 1 to 3. Thus, an appropriate number of flow stabilizers can create a suitable flow field rectification effect within the flotation chamber; too few flow stabilizers will result in insufficient flow stabilization, while too many flow stabilizers will hinder the normal rise of mineralized bubbles.

[0099] For example, the spacing between adjacent flow stabilizers is not less than 1 / 10 of the total height of the flotation chamber (e.g., 1 / 9, 1 / 7, 1 / 6, 1 / 5, 1 / 4, 2 / 5). For instance, the spacing between adjacent flow stabilizers is 1 / 10 to 1 / 3 of the total height of the flotation chamber; preferably, the spacing between adjacent flow stabilizers is 1 / 8 to 1 / 4 of the total height of the flotation chamber. Thus, the flow stabilizers have a suitable spacing that ensures the gradual elimination of pulp pulsations without affecting the passage of mineralization bubbles due to excessively small spacing.

[0100] For example, the distance (vertical distance along the axial direction of the flotation chamber) between the uppermost flow stabilizer plate and the foam overflow end of the flotation chamber is not less than 1 / 10 of the total height of the flotation chamber (e.g., 1 / 9, 1 / 7, 1 / 6, 1 / 5, 1 / 4, 2 / 5). The distance between the uppermost flow stabilizer plate and the foam overflow end of the flotation chamber is 1 / 8 to 1 / 3 of the total height of the flotation chamber; preferably, the distance is 1 / 7 to 1 / 4 of the total height of the flotation chamber. Thus, sufficient space is left between the uppermost flow stabilizer plate and the foam overflow end, which is beneficial for forming a stable foam layer and avoids interference from the flow stabilizer plate on the formation and collection of the foam layer.

[0101] For example, the distance (vertical distance along the axial direction of the flotation chamber) between the lowest flow stabilizer plate and the tailings discharge port at the bottom of the collecting chamber is not less than 1 / 6 (e.g., 1 / 5, 1 / 3, 2 / 5, 1 / 2, 3 / 5) of the total height of the flotation cell body. The distance between the lowest flow stabilizer plate and the tailings discharge port at the bottom of the collecting chamber is 2 / 5 to 2 / 3 of the total height of the flotation cell body. Thus, a sufficient distance is maintained between the lowest flow stabilizer plate and the tailings discharge port to avoid interference with the settling and separation of the tailings area, while ensuring a relatively stable flow field in the tailings discharge port area, which is conducive to the smooth discharge of tailings.

[0102] In some embodiments, the opening ratio of the flow stabilizer plate is 30% to 90% (e.g., 40%, 50%, 60%, 70%, 80%); preferably, the opening ratio of the flow stabilizer plate is 50% to 85%. When the opening ratio is too low, the resistance of the slurry passing through the flow stabilizer plate is large, which will affect the circulation of the slurry and the rise of bubbles in the flotation chamber; when the opening ratio is too high, the flow stabilization effect is weakened, and it is difficult to effectively eliminate slurry pulsation.

[0103] For example, the through holes of the flow stabilizer plate are round or square. The diameter of the through holes (other shapes besides round holes are equivalent diameters) is 10mm to 50mm (e.g., 20mm, 30mm, 40mm), preferably 15mm to 45mm. Thus, the through hole size is moderate, ensuring smooth passage of slurry and bubbles, and also rectifying the slurry flow through the perforated plate structure, which is beneficial for forming a stable flow field.

[0104] For example, the holes of adjacent flow stabilizers are staggered on the horizontal projection plane, preferably with the projection point of the upper hole offset from the adjacent lower hole by 1 / 3 to 2 / 3 of the distance between adjacent holes. This staggered arrangement of holes in adjacent flow stabilizers prevents the slurry from flowing directly through the same vertical channel, increases the flow path of the slurry between the stabilizers, improves the flow stabilization effect, and further eliminates slurry pulsation, which is beneficial for the stable formation of the foam layer.

[0105] In some embodiments, the discharge system includes a concentrate discharge system and a tailings discharge system. The concentrate discharge system is located at the upper end of the flotation chamber, and the tailings discharge system is located on the collecting chamber. Thus, the concentrate and tailings are discharged at different heights within the flotation chamber; the concentrate overflows from the upper froth layer, and the tailings are discharged from the bottom collecting chamber, achieving efficient separation of light and heavy products.

[0106] In some embodiments, the concentrate discharge system includes a concentrate overflow trough and at least one concentrate collection port disposed at the bottom of the concentrate overflow trough; thereby, after the mineralized foam rises to the surface of the slurry, it naturally overflows into the concentrate overflow trough and is discharged through the concentrate collection port, achieving continuous and stable collection of concentrate. The tailings discharge system includes a tailings discharge port and a middlings discharge port; thereby, tailings and middlings are discharged from different outlets of the collecting chamber, facilitating subsequent classification or middlings recycling.

[0107] In some embodiments, the non-driven flotation cell further includes a spraying device positioned above the concentrate overflow tank. The spraying device is connected to an annular water pipe that surrounds the outer periphery of the flotation chamber. The spraying device comprises multiple nozzles evenly distributed circumferentially around the flotation chamber. Thus, the spraying device uniformly washes the mineralized froth layer from above, effectively removing gangue and fine mud entrained in the froth, achieving secondary enrichment of the mineralized froth layer, and improving the concentrate grade. The even circumferential distribution of multiple nozzles ensures uniform coverage of the froth layer surface with sprayed water, avoiding over- or under-washing in certain areas.

[0108] In some embodiments, the number of self-excited oscillating microbubble mineralization devices is two or more (e.g., three, five, six, or seven), such as four to eight, evenly distributed along the circumference of the flotation chamber. Each self-excited oscillating microbubble mineralization device is connected to the slurry distributor via an independent inlet guide pipe. Thus, the circumferentially uniform arrangement of multiple self-excited oscillating microbubble mineralization devices can form a uniform mineralized slurry supply around the circumference of the flotation chamber, avoiding excessively high or low local concentrations and ensuring the symmetry and stability of the slurry flow field within the flotation chamber. Each mineralization device, connected to the slurry distributor via an independent inlet guide pipe, allows for independent adjustment of the feed rate according to the operating status of each device, improving the flexibility and reliability of the system operation.

[0109] In some embodiments, the self-excited oscillating microbubble mineralization device is detachably connected to the inlet guide pipe via an inlet flange and to the outlet guide pipe via an outlet flange. This allows for detachable connections between the self-excited oscillating microbubble mineralization device and the upstream and downstream pipelines, facilitating installation, disassembly, and maintenance. When a self-excited oscillating microbubble mineralization device experiences wear or malfunction, it can be disassembled and replaced independently without affecting the operation of other devices, significantly reducing maintenance costs and downtime.

[0110] In some embodiments, a float is installed inside the flotation chamber to adjust and indicate the liquid level. The float moves up and down with the slurry level, directly reflecting changes in the liquid level within the flotation chamber. This, combined with a liquid level control system, enables automatic adjustment of the liquid level, ensuring a stable froth layer thickness and consequently, stable concentrate grade and recovery rate.

[0111] In some embodiments, an inlet pressure gauge is installed on the inlet pipe (such as the inlet guide pipe 33) of the self-excited oscillating microbubble mineralization device, and an outlet pressure gauge is installed on the outlet pipe. Thus, the slurry pressure at the inlet and outlet of the self-excited oscillating microbubble mineralization device can be monitored in real time using the inlet and outlet pressure gauges. The pressure difference can be used to determine whether there are any abnormalities such as blockages or wear inside the device, facilitating timely maintenance and repair.

[0112] In some embodiments, the flotation cell body is mounted on a frame via a bracket, and the slurry distributor and the self-excited oscillating microbubble mineralization device are both mounted on the frame and located outside the flotation chamber. Thus, the slurry distributor and the self-excited oscillating microbubble mineralization device are fixed to the frame and located outside the flotation chamber, ensuring the installation stability of each device and achieving an external layout for the self-excited oscillating microbubble mineralization device. This external layout allows for maintenance and replacement of the device without shutting down the system, reducing maintenance costs and downtime, while also avoiding sealing and corrosion problems caused by immersing the device in the slurry.

[0113] In some embodiments, the self-excited oscillating microbubble mineralization device without a drive flotation cell further includes a second self-excited oscillation chamber disposed between the expansion tube and the throat. The self-excited oscillation chamber downstream of the throat is the first self-excited oscillation chamber, and the second self-excited oscillation chamber is disposed between the expansion tube and the first self-excited oscillation chamber. The second self-excited oscillation chamber is provided with oscillation disturbance blocks, which are used to induce periodic oscillations and disturbances in the slurry as it flows between the expansion tube and the throat. The number of oscillation disturbance blocks is two or more (e.g., three, four, or five), for example, two to six, arranged at intervals along the slurry flow direction on the inner wall of the second self-excited oscillation chamber. The oscillation disturbance blocks are adjustable, and the jet oscillation intensity and the main oscillation frequency can be adjusted by changing at least one of the number, spacing, or tilt angle of the oscillation disturbance blocks.

[0114] In some embodiments, the inner wall of the throat is provided with microporous wear-resistant ceramic. Thus, the microporous wear-resistant ceramic layer can resist the erosion and wear of the throat's inner wall by solid particles in the slurry, extending the throat's service life; and its microporous structure can provide numerous nucleation sites for dissolved gas precipitation in the negative pressure zone of the throat, promoting the generation of microbubbles and improving the collision and adhesion efficiency between bubbles and mineral particles in subsequent flotation processes.

[0115] In some embodiments, the inner wall of the self-excited oscillating microbubble mineralization device that comes into contact with the slurry is made of wear-resistant ceramic, polyurethane, silicon carbide, alumina ceramic, or wear-resistant alloy material.

[0116] In some embodiments, the oscillating turbulence block is wedge-shaped, with its upstream face being an inclined plane and its downstream face being a steep slope or a vertical plane. It is fixed to the inner wall of the second self-excited oscillation cavity. Exemplarily, the thin end of the oscillating turbulence block faces the expansion pipe, and its upstream face faces the inner wall of the second self-excited oscillation cavity. The oscillating turbulence blocks are distributed circumferentially and arranged axially at intervals along the second self-excited oscillation cavity. The angle between the upstream inclined plane of the oscillating turbulence block and the axial direction of the second self-excited oscillation cavity is 30° to 60°.

[0117] Thirdly, the present invention provides a flotation method enhanced by self-excited oscillation, comprising the following steps: S1. The slurry and flotation reagents are fed into the mineralization device with self-excited oscillation function for mixing and pre-mineralization to obtain a pre-mineralized slurry. S2. The premineralized slurry is subjected to at least one of roughing, cleaning and scavenging processes; In this process, at least one of the roughing, cleaning, and sweeping processes is carried out using a non-drive flotation cell; preferably, the aforementioned non-drive flotation cell with self-excited oscillation function is used.

[0118] In some embodiments, the flotation method is used to process bauxite.

[0119] In some embodiments, prior to step S1, the flotation method further includes a pulp preparation step; the pulp preparation includes: crushing, grinding and classifying the raw bauxite ore and then adjusting the pulp to obtain a pulp.

[0120] Preferably, in the preparation of the slurry, the mass concentration of the slurry is 25-45% (e.g., 30%, 35%, 40%). The slurry temperature is 15-45℃ (e.g., 20℃, 25℃, 30℃, 35℃, 40℃). The particle size of the slurry is controlled to be -0.074mm, accounting for 70-90%.

[0121] For example, in the preparation of the slurry, the conditioning time is 3-12 min (e.g., 5 min, 8 min, 10 min), and the stirring speed is 500-1500 r / min (e.g., 800 r / min, 1000 r / min, 1200 r / min). The solvent used for conditioning is water.

[0122] In some embodiments, in step S1, the flotation reagent includes one or more of a pH adjuster, a depressant, a collector, and a frother. The pH adjuster includes sodium carbonate to adjust the pulp pH to 8.5-10.5; the depressant includes water glass and sodium hexametaphosphate; and the collector includes sodium oleate.

[0123] Specifically, in step S1, the feed pressure of the slurry entering the mineralization device is 0.1~0.6MPa (e.g., 0.2MPa, 0.25MPa, 0.3MPa, 0.35MPa, 0.4MPa, 0.5MPa). The feed flow rate of the slurry entering the mineralization device is 10~60m³. 3 / h (e.g., 20m) 3 / h, 30m 3 / h, 40m 3 / h, 50m 3 / h). The temperature of the slurry entering the mineralization device is 15~45℃ (e.g., 20℃, 25℃, 30℃, 35℃, 40℃).

[0124] In some embodiments, in step S1, the slurry is introduced into the spherical space of the mineralization device via the slurry feed pipe, specifically a spherical mixer. In some embodiments, in step S1, the feed pressure of the slurry entering the spherical mixer of the mineralization device is 0.1~0.6 MPa, preferably 0.15~0.40 MPa. The feed flow rate of the slurry entering the spherical mixer of the mineralization device is 10~60 m³ / s. 3 / h, preferably 20~50m 3 / h. The temperature of the slurry entering the spherical mixer of the mineralization device is 15~45℃, preferably 20~40℃.

[0125] Specifically, in step S1, the flow rate of the flotation reagent entering the mineralization device is 0.05~5.0 L / min (e.g., 0.1 L / min, 0.5 L / min, 1.0 L / min, 2.0 L / min, 3.0 L / min, 4.0 L / min). The reagent inlet temperature of the flotation reagent entering the mineralization device is 15~45℃ (e.g., 20℃, 25℃, 30℃, 35℃, 40℃).

[0126] In some embodiments, in step S1, the flotation reagent is added to the spherical space of the mineralization device via the flotation reagent addition pipe of the mineralization device, specifically a spherical mixer.

[0127] In some embodiments, in step S1, the flow rate of the flotation reagent entering the spherical mixer of the mineralization device is 0.05~5.0 L / min, preferably 0.5~3.0 L / min. The reagent inlet temperature of the flotation reagent entering the spherical mixer of the mineralization device is 15~45℃, preferably 20~40℃.

[0128] In some embodiments, the addition pressure of the flotation reagent into the mineralization device (specifically, into the spherical mixer of the mineralization device) is 0.1~1.0 MPa (e.g., 0.2 MPa, 0.4 MPa, 0.5 MPa, 0.8 MPa), preferably 0.15~0.60 MPa.

[0129] Specifically, in step S1, the air inlet pressure into the mineralization device is 0.1~0.5MPa (e.g., 0.2MPa, 0.3MPa, 0.4MPa). The air inlet flow rate into the mineralization device is 0.2~25m³. 3 / h (e.g., 1m) 3 / h、5m 3 / h, 10m 3 / h, 15m 3 / h, 20m 3 / h). The air entering the mineralization device is at a temperature of 15~30℃ (e.g., 20℃, 25℃).

[0130] In some embodiments, in step S1, the air is introduced into the mineralization device via an external air source and drawn into the throat of the mineralization device. The inlet pressure of the air into the throat of the mineralization device is 0.1~0.5 MPa, preferably 0.1~0.4 MPa. The inlet flow rate of the air into the throat of the mineralization device is 0.2~25 m³ / s.3 / h, preferably 5~20 m 3 / h. The inlet temperature of the air entering the throat of the mineralization device is 15~30℃, preferably 20~25℃.

[0131] In some embodiments, in step S1, the residence time of the slurry in the mineralization device is 5-20 s (e.g., 10 s, 12 s, 14 s, 16 s, 18 s); preferably 8-15 s. The residence time of the slurry in the mineralization device is controlled by adjusting the feed flow rate of the slurry and / or the effective cavity volume of the mineralization device.

[0132] Specifically, in step S2, the feed pressure of the slurry entering the non-driven flotation cell is 0.1~0.6MPa (e.g., 0.2MPa, 0.25MPa, 0.3MPa, 0.35MPa, 0.4MPa, 0.5MPa). The feed flow rate of the slurry entering the non-driven flotation cell is 10~60m³. 3 / h (e.g., 20m) 3 / h, 30m 3 / h, 40m 3 / h, 50m 3 / h). The temperature of the slurry entering the non-drive flotation cell is 15~45℃ (e.g., 20℃, 25℃, 30℃, 35℃, 40℃).

[0133] In some embodiments, in step S2, the slurry is added to the self-excited oscillating microbubble mineralization device via the feed system of the non-drive flotation cell. Specifically, the slurry is fed into the expansion pipe of the self-excited oscillating microbubble mineralization device via the feed pipe of the non-drive flotation cell and distributed by the slurry distributor, and then added to the expansion pipe of the self-excited oscillating microbubble mineralization device through the inlet end guide pipe.

[0134] In some embodiments, in step S2, the feed pressure of the slurry entering the self-excited oscillating microbubble mineralization device of the non-drive flotation cell is 0.1~0.6MPa, preferably 0.15~0.40MPa. The feed flow rate of the slurry entering the self-excited oscillating microbubble mineralization device of the non-drive flotation cell is 10~60m³. 3 / h, preferably 20~50m 3 / h. The feed temperature of the slurry entering the self-excited oscillating microbubble mineralization device of the non-drive flotation cell is 15~45℃, preferably 20~40℃.

[0135] Specifically, in step S2, the air inlet pressure into the non-driven flotation cell is 0.1~0.5MPa (e.g., 0.2MPa, 0.3MPa, 0.4MPa). The air inlet flow rate into the non-driven flotation cell is 0.2~25m³. 3 / h (e.g., 1m)3 / h、5m 3 / h, 10m 3 / h, 15m 3 / h, 20m 3 / h). The air entering the non-drive flotation cell is at a temperature of 15~30℃ (e.g., 20℃, 25℃).

[0136] In some embodiments, in step S2, the air is drawn into the throat through an air inlet located in the middle of the throat of the self-excited oscillating microbubble mineralization device without transmission; preferably, the air is drawn into the throat through an air inlet located at the smallest cross-section in the middle of the throat.

[0137] In some embodiments, in step S2, the air inlet pressure into the self-excited oscillating microbubble mineralization device of the non-driven flotation cell is 0.1~0.5MPa, preferably 0.15~0.35MPa; the inlet flow rate is 0.2~25 m³ / s. 3 / h, preferably 5~20 m 3 / h. The air temperature entering the self-excited oscillating microbubble mineralization device of the non-drive flotation cell is 15~30℃, preferably 20~25℃.

[0138] In some embodiments, in step S2, the residence time of the slurry in the self-excited oscillating microbubble mineralization device of the non-drive flotation cell is 5-20 s (e.g., 10 s, 12 s, 14 s, 16 s, 18 s), preferably 8-15 s. The residence time of the slurry in the self-excited oscillating microbubble mineralization device of the non-drive flotation cell is controlled by adjusting the feed flow rate of the slurry and / or the effective cavity volume of the self-excited oscillating microbubble mineralization device.

[0139] In some embodiments, in step S2, the liquid level in the flotation cell body is 0.6×H~0.9×H; preferably 0.65×H~0.85×H; where H represents the total height of the flotation cell body (flotation chamber + collection chamber).

[0140] In some embodiments, in step S2, the thickness of the foam layer in the flotation chamber is 0.01×H to 0.35×H; preferably, the thickness of the foam layer is 0.02×H to 0.25×H.

[0141] In some embodiments, the flotation time in step S2 is 2 to 12 minutes (e.g., 4 minutes, 6 minutes, 8 minutes); preferably 3 to 10 minutes.

[0142] In some embodiments, in step S2, the pH value of the slurry is controlled at 8.5~10.5; preferably 9.0~10.0.

[0143] In some embodiments, in step S2, the concentrate scraper speed is 10~50 r / min (e.g., 20 r / min, 30 r / min, 40 r / min); preferably 15~40 r / min.

[0144] It is understood that the flotation time in the flotation operation can be controlled by adjusting the feed flow rate of the slurry and / or the liquid level in the flotation chamber. The pH value of the slurry can be controlled by installing an online pH monitor and pH adjuster addition device on the feed pipeline of the non-drive flotation cell, or by controlling the amount of pH adjuster added during the slurry conditioning operation.

[0145] It is understood that in step S2, the mineralized slurry (the gas-solid-liquid three-phase slurry after being treated by the self-excited oscillating microbubble mineralization device) is injected into the body of the flotation cell through the pipeline at the outlet end of the self-excited oscillating microbubble mineralization device of the non-drive flotation cell and the nozzle at the end of the pipeline at the outlet end; during the process of mineralizing bubbles carrying hydrophobic mineral particles floating up inside the body of the flotation cell, the mineralizing bubbles pass through the flow stabilizers arranged at intervals along the axial direction of the body of the flotation cell, and after being rectified by the flow stabilizers, they float up to the foam layer. The hydrophobic mineral particles are enriched in the foam layer and overflow to become concentrate, while the unmineralized mineral particles (hydrophilic mineral particles not captured by the bubbles) settle into the collection cavity at the bottom of the body of the flotation cell and are discharged through the tailings discharge port and the middlings discharge port, respectively. It is understandable that the flow stabilizer effectively rectifyes the slurry flow field, eliminating the pulsations and large-scale eddies brought in by the jet, and forming a stable upward flow field in the flotation chamber. This is conducive to the smooth floating of mineralized bubbles to the foam layer, avoiding the damage to the stability of the foam layer caused by flow field turbulence, and reducing the mechanical entrainment of gangue minerals. Thus, while ensuring the recovery rate, the concentrate grade is improved.

[0146] In some embodiments, the roughing is carried out using the driveless flotation cell with self-excited oscillation function; based on the aforementioned parameter range, by finely controlling the process parameters of the roughing process section, it is beneficial to balance the concentrate grade and recovery rate in the roughing operation.

[0147] For example, in the roughing stage, the feed flow rate of the slurry into the self-excited oscillating microbubble mineralization device of the non-drive flotation cell is 10~60 m³ / s. 3 / h, preferably 20~50m 3 / h. The residence time of the slurry in the self-excited oscillating microbubble mineralization device without a drive flotation cell is 5~20s, preferably 8~15s. In addition, the range of slurry feed pressure, slurry feed temperature and slurry pH value is as described above.

[0148] For example, in the roughing process, the air flow rate into the self-excited oscillating microbubble mineralization device of the non-driven flotation cell is 0.2~25m³. 3 / h, preferably 5~18m 3 / h. Furthermore, the ranges for air inlet pressure and inlet temperature are as described above.

[0149] For example, in the coarse flotation, the liquid level in the main body of the flotation cell is (0.7~0.9)×H, preferably (0.75~0.85)×H. The thickness of the foam layer is (0.03~0.25)×H, preferably (0.05~0.15)×H. The flotation time is 3~10 min, preferably 4~8 min.

[0150] For example, in the roughing process, the concentrate scraper speed is 25~50 r / min, preferably 30~40 r / min.

[0151] For example, after the slurry is mineralized by the self-excited oscillating microbubble mineralization device, it enters the flotation chamber for roughing. The roughing froth product is rough concentrate, and the product in the tank includes at least one of roughing concentrate and roughing tailings. The rough concentrate enters the cleaning operation for further enrichment, and the roughing concentrate and / or roughing tailings enter the scavenging operation for further recovery.

[0152] In some embodiments, the refining is carried out using the non-drive flotation cell with self-excited oscillation function; based on the aforementioned parameter range, by finely controlling the process parameters of the refining process section, it is beneficial to balance the concentrate grade and recovery rate in the refining operation.

[0153] For example, in the fine-grained process, the feed flow rate of the slurry into the self-excited oscillating microbubble mineralization device of the non-drive flotation cell is 10~60 m³ / s. 3 / h, preferably 20~50 m 3 / h. The residence time of the slurry in the self-excited oscillating microbubble mineralization device without a drive flotation cell is 5~15s, preferably 6~12s. In addition, the range of slurry feed pressure, slurry feed temperature and slurry pH value are as described above.

[0154] For example, in the fine selection process, the air flow rate into the self-excited oscillating microbubble mineralization device of the non-driven flotation cell is 0.2~25m³. 3 / h, preferably 3~12m 3 / h. Furthermore, the ranges for air inlet pressure and inlet temperature are as described above.

[0155] For example, in the fine selection process, the liquid level in the main body of the flotation cell is (0.7~0.9)×H, preferably (0.75~0.85)×H. The thickness of the foam layer is (0.10~0.35)×H, preferably (0.15~0.25)×H. The flotation time is 2~8 min, preferably 3~6 min.

[0156] For example, in the fine-graining process, the concentrate scraper speed is 10~40 r / min, preferably 15~30 r / min.

[0157] For example, after the slurry is mineralized by the self-excited oscillating microbubble mineralization device, it enters the flotation chamber for fine selection. The fined froth product is the final concentrate, and the product in the tank includes at least one of fined middlings and fined tailings. The fined middlings and / or fined tailings are returned to the roughing operation.

[0158] In some embodiments, the scavenging is carried out using a non-drive flotation cell with self-excited oscillation function; based on the aforementioned parameter range, by finely controlling the process parameters of the scavenging process section, it is beneficial to improve the total recovery rate of the target mineral in the scavenging operation.

[0159] For example, during the scavenging process, the feed flow rate of the slurry into the self-excited oscillating microbubble mineralization device of the non-drive flotation cell is 10~40 m³. 3 / h, preferably 15~30m 3 / h. The residence time of the slurry in the self-excited oscillating microbubble mineralization device without a drive flotation cell is 5~20s, preferably 8~15s. In addition, the ranges of slurry feed pressure, slurry feed temperature and slurry pH value are as described above.

[0160] For example, during the scavenging process, the air flow rate into the self-excited oscillating microbubble mineralization device of the non-driven flotation cell is 0.2~20m³. 3 / h, preferably 3~12m 3 / h. Furthermore, the ranges for air inlet pressure and inlet temperature are as described above.

[0161] For example, during the sweeping process, the liquid level in the main body of the flotation cell is (0.6~0.85)×H, preferably (0.65~0.80)×H. The thickness of the foam layer is (0.01~0.20)×H, preferably (0.02~0.10)×H. The flotation time is 4~12 min, preferably 5~10 min.

[0162] For example, during the scavenging process, the speed of the concentrate scraper is 10~40 r / min, preferably 15~30 r / min.

[0163] For example, after the slurry is mineralized by the self-excited oscillating microbubble mineralization device, it enters the flotation chamber for scavenging. The scavenging froth product is scavenging concentrate, and the product in the tank includes at least one of scavenging concentrate and scavenging tailings (final tailings). The scavenging concentrate and / or scavenging concentrate are returned to the roughing operation, and the scavenging tailings are discharged.

[0164] In some embodiments, the flotation method further includes middlings recycling: the middlings and / or tailings produced by the cleaning operation, and the scavenging concentrate and / or middlings produced by the scavenging operation are returned to the roughing operation inlet, combined with the pre-mineralized slurry, and then enter the non-drive flotation cell of the roughing operation for further roughing; or returned to the inlet of the mineralization device, combined with the slurry after conditioning, and then enter the mineralization device for further pre-mineralization, and after mineralization, enter the roughing operation for further roughing.

[0165] In some embodiments, the middlings return flow rate in the middlings circulation is 0.5~25m³. 3 / h (e.g., 1m) 3 / h、5m 3 / h, 10m 3 / h, 15m 3 / h, 20m 3 ( / h), preferably 5~15m 3 / h; the middlings return temperature is 15~45℃ (e.g., 20℃, 25℃, 30℃, 35℃, 40℃), preferably 20~40℃. When the middlings return to the inlet of the mineralization unit, the middlings mix with the slurry after conditioning to jointly constitute the feed flow rate and feed temperature entering the mineralization unit; when the middlings return to the roughing operation inlet, the middlings mix with the pre-mineralized slurry to jointly constitute the feed flow rate and feed temperature entering the non-driven flotation cell of the roughing operation.

[0166] In some embodiments, the flotation method further includes concentrate dewatering and tailings treatment: the final concentrate obtained from the fine selection is fed into a thickener for concentration, and the concentrate underflow is filtered by a filter to obtain the final concentrate product; the overflow water from the thickener is returned to the slurry preparation operation for recycling; the final tailings produced by the scavenging operation are discharged. Exemplarily, the filter is a ceramic filter or a plate and frame filter press. The moisture content of the filtered aluminum concentrate filter cake is 8-18% (e.g., 10%, 12%, 14%, 16%).

[0167] In some embodiments, the flotation is direct flotation, reverse flotation, or a combination of both. When direct flotation is used, the collector is a fatty acid, a hydroxamic acid, or a mixture thereof, and the collector dosage is 200-1200 g / t (e.g., 400 g / t, 600 g / t, 1000 g / t), preferably 300-800 g / t; when reverse flotation is used, the collector is an amine, a quaternary ammonium salt, or a mixture thereof, and the collector dosage is 50-500 g / t (e.g., 200 g / t, 300 g / t), preferably 100-400 g / t. The foaming agent is methyl isobutyl methanol, pine oil, or polyethylene glycol ether, and the amount of foaming agent used is 50~150g / t (e.g., 70g / t, 80g / t, 90g / t, 120g / t), preferably 60~100g / t.

[0168] In some embodiments, the dominant oscillation frequency f of the microbubble-containing slurry jet within the resonant cavity is 20~2000Hz (e.g., 50Hz, 80Hz, 100Hz, 200Hz, 500Hz, 800Hz, 1000Hz, 1200Hz, 1400Hz, 1600Hz, 1800Hz), preferably 80~800Hz. The dominant oscillation frequency is adjusted by changing the structure and / or operating parameters of the mineralization device and / or the self-excited oscillating microbubble mineralization device of the non-drive flotation cell. Exemplarily, the dominant oscillation frequency f of the microbubble-containing slurry jet within the resonant cavity is f, and the dominant oscillation frequency f is adjusted by changing at least one of the following: the inlet pressure of the slurry entering the resonant cavity, the ratio of the axial length to the diameter of the resonant cavity, and the ratio of the outlet diameter of the resonant cavity to the diameter of the flotation cavity after discharge.

[0169] In some embodiments, for the mineralization apparatus, the resonant cavity refers to the Helmholtz cavity included in the mineralization apparatus; for the non-drive flotation cell, the resonant cavity refers to the self-excited oscillation chamber included in the non-drive flotation cell.

[0170] (1) When a low-frequency oscillation of 80Hz≤f≤200Hz is required, the ratio of the axial length of the Helmholtz cavity and / or the self-excited oscillation chamber to the inner diameter of the cavity is controlled to be 3.0~8.0, the inlet pressure of the slurry entering the Helmholtz cavity and / or the self-excited oscillation chamber is controlled to be 0.1~0.2 MPa, and the ratio of the outlet diameter of the Helmholtz cavity and / or the self-excited oscillation chamber to the diameter of the flotation chamber after discharge is controlled to be 0.2~0.35; (2) When a medium-frequency oscillation of 200Hz < f ≤ 800Hz is required, the ratio of the axial length of the Helmholtz cavity and / or the self-excited oscillation chamber to the inner diameter of the cavity is controlled to be 1.5~4.0, the inlet pressure of the slurry entering the Helmholtz cavity and / or the self-excited oscillation chamber is controlled to be 0.2~0.35MPa, and the ratio of the outlet diameter of the Helmholtz cavity and / or the self-excited oscillation chamber to the diameter of the flotation chamber after discharge is controlled to be 0.15~0.30; (3) When a higher frequency oscillation of 800Hz < f ≤ 1400Hz is required, the ratio of the axial length of the Helmholtz cavity and / or the self-excited oscillation chamber to the inner diameter of the cavity is controlled to be 0.8~2.0, the inlet pressure of the slurry entering the Helmholtz cavity and / or the self-excited oscillation chamber is controlled to be 0.35~0.50MPa, and the ratio of the outlet diameter of the Helmholtz cavity and / or the self-excited oscillation chamber to the diameter of the flotation chamber after discharge is controlled to be 0.1~0.25; (4) When a high-frequency oscillation of 1400Hz < f ≤ 2000Hz is required, the ratio of the axial length of the Helmholtz cavity and / or the self-excited oscillation chamber to the inner diameter of the cavity is controlled to be 0.4~1.2, the inlet pressure of the slurry entering the Helmholtz cavity and / or the self-excited oscillation chamber is controlled to be 0.45~0.6MPa, and the ratio of the outlet diameter of the Helmholtz cavity and / or the self-excited oscillation chamber to the diameter of the flotation chamber after discharge is controlled to be 0.05~0.2.

[0171] It is understood that, for the aforementioned mineralization device, the ratio of the outlet diameter to the diameter of the flotation chamber after discharge refers to the ratio of the inner diameter of the end of the outlet section of the Helmholtz chamber (i.e., the discharge pipe of the mineralized slurry) to the diameter of the flotation chamber after the mineralized slurry is discharged. For the self-excited oscillating microbubble mineralization device without a drive flotation cell, the ratio of the outlet diameter to the diameter of the flotation chamber after discharge specifically refers to the ratio of the inner diameter of the end of the outlet guide pipe connected to the self-excited oscillation chamber (if there is a nozzle, it refers to the minimum inner diameter of the nozzle) to the diameter of the flotation chamber after the outlet guide pipe is discharged.

[0172] In some embodiments, the flotation method is suitable for desilication of medium- and low-grade bauxite. The raw bauxite ore has an Al2O3 grade of 55-62% and an Aluminum-to-Silica ratio of 4.0-5.5. After one roughing stage, the Al2O3 grade of the rough concentrate is 65-69%, the Al2O3 recovery rate is 82-90%, and the Aluminum-to-Silica ratio of the concentrate after roughing is 8-12. Compared with conventional flotation methods, the Al2O3 recovery rate is increased by at least 2-6% after one roughing stage, and the collector dosage is reduced by 5-15%.

[0173] The technical solution of the present invention will be further described in detail below with reference to specific embodiments and comparative examples.

[0174] Example 1: This embodiment provides a mineralization device with a self-excited oscillation function. The mineralization device includes: a spherical mixer 110, a self-excited oscillating microbubble mineralization tube 120, and a mineralized slurry discharge pipe 140. The spherical mixer has a spherical inner cavity. The spherical mixer is provided with two slurry feed pipes 111, a flotation reagent addition pipe 112, and a slurry outlet 113. The slurry feed pipes 111 are used to feed slurry into the spherical mixer 110, and the flotation reagent addition pipe 112 is used to add flotation reagents into the spherical mixer 110.

[0175] The spherical mixer 110 has two slurry feed pipes 111 located within the equatorial plane 115 passing through the center of the sphere. The two slurry feed pipes 111 are symmetrically arranged with respect to the center of the sphere, and the axes of the two slurry feed pipes 111 intersect at the center of the sphere, so as to allow the two slurries to converge and counteract at the center of the spherical mixer 110. The flotation reagent addition pipe 112 and the slurry outlet 113 are arranged opposite each other on an axis perpendicular to the equatorial plane 115 and passing through the center of the sphere in the spherical mixer 110.

[0176] The spherical mixer 110 is internally provided with four perforated baffles 114. The four perforated baffles 114 are respectively disposed in four quadrant regions 117 between the equatorial plane 115 and the meridian plane 116 of the spherical mixer 110. Each quadrant region 117 contains one perforated baffle 114, and the inclination angle of the four perforated baffles 114 relative to the equatorial plane 115 is 30°. The perforation rate of the perforated baffles 114 is 15%. One side of the perforated baffle 114 is conformally fitted and fixed to the inner wall surface of the spherical mixer 110 (the shape of one side of the perforated baffle corresponds to the shape of the inner wall surface of the spherical mixer), and the shortest distance between the other side of the perforated baffle 114 (e.g., a straight line) and the center of the spherical mixer 110 is 1 / 5 of the radius of the spherical mixer.

[0177] The self-excited oscillating microbubble mineralization tube 120 is connected to the slurry outlet 113 of the spherical mixer 110. The self-excited oscillating microbubble mineralization tube 120 includes a pipe organ cavity 121, a throat 122, and a Helmholtz cavity 130 connected sequentially along the slurry flow direction.

[0178] The organ cavity 121 is a variable-diameter straight pipe structure, with its inlet inner diameter d1' being larger than its outlet inner diameter d2'. The ratio of the inlet inner diameter d1' to the outlet inner diameter d2' of the organ cavity 121 is 1.2:1. The outlet inner diameter d2' of the organ cavity 121 is equal to the inlet inner diameter d3' of the throat 122.

[0179] The throat 122 has a Venturi tube structure, consisting of a contraction section 124 and a throat 125 along the slurry flow direction. The inner diameter of the contraction section 124 gradually decreases from the inlet end towards the throat 125, and the inner diameter of the throat 125 is the minimum inner diameter d4' of the throat 122. The ratio of the minimum inner diameter d4' of the throat 125 to the inner diameter d3' of the inlet end of the throat 122 is 0.4:1.

[0180] A compressed air intake pipe 123 is provided on the side wall of the throat 122. The compressed air intake pipe 123 is located at the throat 125 of the throat 122, specifically at a point one-third of the length of the throat 125 along the slurry flow direction from the inlet end of the throat 125. The compressed air intake pipe 123 is connected to an external air source. The ratio of the inner diameter d5' of the compressed air intake pipe 123 to the minimum inner diameter d4' of the throat 122 is 0.1:1.

[0181] The inlet of the Helmholtz cavity 130 is connected to the outlet of the throat 122. The Helmholtz cavity 130 includes a Helmholtz cavity body 132 and a Helmholtz outlet section 133; the end of the outlet section of the throat 122 of the mineralization device enters the inlet 131 of the Helmholtz cavity body. The cross-sectional area of ​​the Helmholtz cavity 132 is larger than the cross-sectional area of ​​the end of the outlet section of the throat 122 of the mineralization device, so that a Helmholtz cross-sectional abrupt step 134 is formed at the inlet 131 of the Helmholtz cavity. The outlet of the Helmholtz cavity 132 extends outward to form the Helmholtz outlet section 133, and the cross-sectional area of ​​the Helmholtz cavity 132 is larger than the cross-sectional area of ​​the Helmholtz outlet section 133. The Helmholtz outlet section 133 is coaxially arranged with the inlet 131 of the Helmholtz cavity, and the outlet at the end of the Helmholtz outlet section 133 is connected to the mineralized slurry discharge pipe 140. The inner wall surfaces of the Helmholtz cavity 132, located near the Helmholtz outlet section 133 and on both sides of the Helmholtz outlet section 133, form Helmholtz collision walls 135, with the wall surfaces of the Helmholtz collision walls 135 facing the inlet 131 of the Helmholtz cavity.

[0182] The angle α' between the wall surface of the Helmholtz collision wall and the axial direction of the Helmholtz cavity is 30°.

[0183] The inner diameter d at the maximum cross-section of the Helmholtz cavity X1 The inner diameter d of the throat outlet section of the mineralization device X3 The ratio is 2:1. The axial length d of the Helmholtz cavity... X2The inner diameter d at the maximum cross-section of the Helmholtz cavity X1 The ratio is 0.4:1. The inner diameter d of the Helmholtz outlet section... X4 The inner diameter d of the end of the throat outlet section of the mineralization device X3 The ratio is 0.4:1. The included angle between the upper and lower inclined surfaces of the outward expansion at the end of the Helmholtz outlet section (i.e., the expansion angle 136° of the Helmholtz cavity) β' is 20°. The end of the Helmholtz outlet section is connected to the mineralized slurry discharge pipe 140.

[0184] Example 2 This embodiment provides a mineralization device with a self-excited oscillation function. The mineralization device includes: a spherical mixer 110, a self-excited oscillating microbubble mineralization tube 120, and a mineralized slurry discharge pipe 140. The spherical mixer has a spherical inner cavity. The spherical mixer is provided with two slurry feed pipes 111, a flotation reagent addition pipe 112, and a slurry outlet 113. The slurry feed pipes 111 are used to feed slurry into the spherical mixer 110, and the flotation reagent addition pipe 112 is used to add flotation reagents into the spherical mixer 110.

[0185] The spherical mixer 110 has two slurry feed pipes 111 located within the equatorial plane 115 passing through the center of the sphere. The two slurry feed pipes 111 are symmetrically arranged with respect to the center of the sphere, and the axes of the two slurry feed pipes 111 intersect at the center of the sphere, so as to allow the two slurries to converge and counteract at the center of the spherical mixer 110. The flotation reagent addition pipe 112 and the slurry outlet 113 are arranged opposite each other on an axis perpendicular to the equatorial plane 115 and passing through the center of the sphere in the spherical mixer 110.

[0186] A spray head is provided at the outlet end of the flotation reagent addition pipe 112.

[0187] The spherical mixer 110 is internally provided with four perforated baffles 114. The four perforated baffles 114 are respectively disposed in four quadrant regions 117 between the equatorial plane 115 and the meridian plane 116 of the spherical mixer 110. Each quadrant region 117 contains one perforated baffle 114, and the inclination angle of the four perforated baffles 114 relative to the equatorial plane 115 is 45°. The perforation rate of the perforated baffles 114 is 35%. One side of the perforated baffle 114 is conformally fitted and fixed to the inner wall surface of the spherical mixer 110 (the shape of one side of the perforated baffle corresponds to the shape of the inner wall surface of the spherical mixer), and the shortest distance between the other side of the perforated baffle 114 (e.g., arc-shaped) and the center of the spherical mixer 110 is 1 / 4 of the radius of the spherical mixer. The holes in the perforated baffle are round and have a diameter of 6 mm.

[0188] The self-excited oscillating microbubble mineralization tube 120 is connected to the slurry outlet 113 of the spherical mixer 110. The self-excited oscillating microbubble mineralization tube 120 includes a pipe organ cavity 121, a throat 122, and a Helmholtz cavity 130 connected sequentially along the slurry flow direction.

[0189] The organ cavity 121 is a variable-diameter straight pipe structure, with its inlet inner diameter d1' being larger than its outlet inner diameter d2'. The ratio of the inlet inner diameter d1' to the outlet inner diameter d2' of the organ cavity 121 is 2.0:1. The outlet inner diameter d2' of the organ cavity 121 is equal to the inlet inner diameter d3' of the throat 122.

[0190] The throat 122 has a Venturi tube structure, consisting of a contraction section 124 and a throat 125 along the slurry flow direction. The inner diameter of the contraction section 124 gradually decreases from the inlet end towards the throat 125, and the inner diameter of the throat 125 is the minimum inner diameter d4' of the throat 122. The ratio of the minimum inner diameter d4' of the throat 125 to the inner diameter d3' of the inlet end of the throat 122 is 0.55:1. A compressed air intake pipe 123 is provided on the side wall of the throat 122. The compressed air intake pipe 123 is located at the throat 125 of the throat 122, specifically at a distance of 1 / 2 the length from the inlet end of the throat 125 along the slurry flow direction. The compressed air intake pipe 123 is connected to an external air source. The ratio of the inner diameter d5' of the compressed air intake pipe 123 to the minimum inner diameter d4' of the throat 122 is 0.2:1.

[0191] The inlet of the Helmholtz cavity 130 is connected to the outlet of the throat 122. The Helmholtz cavity 130 includes a Helmholtz cavity body 132 and a Helmholtz outlet section 133; the end of the outlet section of the throat 122 of the mineralization device enters the inlet 131 of the Helmholtz cavity body. The cross-sectional area of ​​the Helmholtz cavity 132 is larger than the cross-sectional area of ​​the end of the outlet section of the throat 122 of the mineralization device, so that a Helmholtz cross-sectional abrupt step 134 is formed at the inlet 131 of the Helmholtz cavity. The outlet of the Helmholtz cavity 132 extends outward to form the Helmholtz outlet section 133, and the cross-sectional area of ​​the Helmholtz cavity 132 is larger than the cross-sectional area of ​​the Helmholtz outlet section 133. The Helmholtz outlet section 133 is coaxially arranged with the inlet 131 of the Helmholtz cavity, and the outlet at the end of the Helmholtz outlet section 133 is connected to the mineralized slurry discharge pipe 140. The inner wall surfaces of the Helmholtz cavity 132, located near the Helmholtz outlet section 133 and on both sides of the Helmholtz outlet section 133, form Helmholtz collision walls 135, with the wall surfaces of the Helmholtz collision walls 135 facing the inlet 131 of the Helmholtz cavity.

[0192] The angle α' between the wall surface of the Helmholtz collision wall and the axial direction of the Helmholtz cavity is 50°.

[0193] The inner diameter d at the maximum cross-section of the Helmholtz cavity X1 The inner diameter d of the throat outlet section of the mineralization device X3 The ratio is 4.5:1. The axial length d of the Helmholtz cavity... X2 The inner diameter d at the maximum cross-section of the Helmholtz cavity X1 The ratio is 8:1. The inner diameter d of the Helmholtz outlet section... X4 The inner diameter d of the throat outlet section of the mineralization device X3 The ratio is 0.7:1. The included angle between the upper and lower inclined surfaces that expand outward at the end of the Helmholtz outlet section (i.e., the expansion angle 136° of the Helmholtz cavity) β' is 40°. The end of the Helmholtz outlet section is connected to the mineralized slurry discharge pipe 140.

[0194] Example 3 This embodiment provides a mineralization device with self-excited oscillation function, which has the same structure as that in embodiment 1, except that the spherical mixer does not have a perforated baffle inside.

[0195] Example 4 This embodiment provides a mineralization device with self-excited oscillation function, whose structure is basically the same as that of Embodiment 1, except that: (1) The angle of inclination of the perforated baffle relative to the equatorial plane is 65°; (2) The ratio of the inner diameter d1' at the inlet end to the inner diameter d2' at the outlet end of the organ cavity is 3.2:1; (3) The ratio of the minimum inner diameter d4' of the throat to the inner diameter d3' of the inlet end of the larynx is 0.35:1; (4) The ratio of the inner diameter d5' of the compressed air intake pipe to the minimum inner diameter d4' of the throat pipe is 0.35:1; (5) The angle α' between the wall surface of the Helmholtz collision wall and the axis of the Helmholtz cavity is 75°; (6) The inner diameter d at the maximum cross-section of the Helmholtz cavity X1 The inner diameter d of the end of the throat outlet section of the mineralization device X3 The ratio is 8.5:1; (7) The axial length d of the Helmholtz cavity X2 The inner diameter d at the maximum cross-section of the Helmholtz cavity X1 The ratio is 0.3:1; (8) The inner diameter d of the Helmholtz outlet section X4 The inner diameter d of the end of the throat outlet section of the mineralization device X3 The ratio is 1.1:1; (9) The included angle β' between the upper and lower inclined surfaces that expand outward at the end of the Helmholtz outlet section is 65°.

[0196] Example 5 This embodiment provides a driveless flotation cell with self-excited oscillation function. The driveless flotation cell includes: a flotation cell body 1, a self-excited oscillation microbubble mineralization device 2, a feeding system 3, and a discharging system 4. The flotation cell body 1 includes a flotation chamber 11 and a collecting chamber 12 connected to the bottom of the flotation chamber 11.

[0197] The self-excited oscillating microbubble mineralization device 2 is disposed outside the main body 1 of the flotation cell, and there are four of them, evenly distributed along the circumference of the flotation chamber 11. The self-excited oscillating microbubble mineralization device 2 includes an expansion pipe 21, a throat pipe 22, and a self-excited oscillation chamber 23 connected sequentially along the direction of slurry flow. An inlet guide pipe 33 is connected to the inlet end of the expansion pipe 21. The inner diameter d of the inlet end of the expansion pipe 21 is... e1 The inner diameter d of the outlet end of the inlet guide pipe 33 is... g 1.01 times. The inner diameter d of the inlet end of the throat tube 22. h1 The inner diameter d of the outlet end of the expansion tube 21 e2 0.6 times. An air inlet 221 is provided on the side wall of the throat tube 22, and the air inlet 221 is connected to an external air source. The inner diameter d at the maximum cross-section of the resonant cavity of the self-excited oscillation chamber, i.e., the self-excited oscillation cavity 232, is... Z1 The inner diameter d of the outlet end of the expansion tube 21 e2 0.9 times. The inner diameter d at the outlet end of the expansion tube 21 e2 The inner diameter d of the inlet end of the expansion tube 21 e1 The ratio is 1.1:1. The minimum inner diameter d of the throat 22 hmin The inner diameter d of the inlet end of the throat tube 22 h1 The ratio is 0.4:1. The inner diameter d at the maximum cross-section of the self-excited oscillation cavity 232 is... Z1 The inner diameter d of the throat outlet section end of the non-drive flotation cell Z3 The ratio is 2:1.

[0198] The self-excited oscillation chamber 23 includes a self-excited oscillation body 232 and a self-excited oscillation outlet section 233; the end of the outlet section of the throat tube 22 of the non-drive flotation cell enters the inlet 231 of the self-excited oscillation body. The cross-sectional area of ​​the self-excited oscillation cavity 232 is larger than the cross-sectional area of ​​the outlet section of the throat 22 of the non-drive flotation cell, so that a step 234 of abrupt change in the cross-section of the self-excited oscillation cavity is formed at the inlet 231 of the self-excited oscillation cavity. The outlet of the self-excited oscillation cavity 232 extends outward to form the self-excited oscillation outlet section 233, and the cross-sectional area of ​​the self-excited oscillation cavity 232 is larger than the cross-sectional area of ​​the self-excited oscillation outlet section 233. The self-excited oscillation outlet section 233 is coaxially arranged with the inlet 231 of the self-excited oscillation cavity, and the outlet at the end of the self-excited oscillation outlet section 233 is connected to the interior of the flotation cavity 11. The inner wall surface of the self-excited oscillation cavity 232, located near the self-excited oscillation outlet section 233 and on both sides of the self-excited oscillation outlet section 233, constitutes a self-excited oscillation collision wall 235, and the wall surface of the self-excited oscillation collision wall 235 faces the inlet 231 of the self-excited oscillation cavity.

[0199] The angle α between the wall surface of the self-excited oscillation collision wall 235 and the axial direction of the self-excited oscillation cavity 232 is 30°. The angle β between the upper and lower inclined surfaces that expand outward at the end of the self-excited oscillation outlet section 233 (i.e., the expansion angle 236 of the self-excited oscillation chamber) is 20°.

[0200] The air inlet 221 is connected to an annular air pipe 24 via a pipe, and the annular air pipe 24 is arranged around the outer periphery of the flotation chamber 11. The inner diameter d of the annular air pipe 24 is... r The inner diameter d of the air inlet 221 a 1.2 times. The central ring diameter D of the annular air tube 24 r The outer diameter D of the flotation chamber 11 t 1.1 times.

[0201] The outlet of the self-excited oscillating microbubble mineralization device 2 is connected to the interior of the flotation chamber 11 through the outlet end guide pipe 25. The outlet end guide pipe 25 extends through the wall of the flotation chamber 11 and into the interior of the flotation chamber 11, and a nozzle 251 is provided at the end of the outlet end guide pipe 25.

[0202] A flow stabilizing plate 5 is provided inside the flotation chamber 11, and the flow stabilizing plate 5 is positioned above the outlet guide pipe 25. The flow stabilizing plate 5 is a horizontally arranged plate structure with through holes 51 on its surface. There is one flow stabilizing plate 5.

[0203] The feeding system 3 includes a feed pipe 31, a slurry distributor 32, and an inlet guide pipe 33. The feed pipe 31 is connected to the inlet of the slurry distributor 32, and the outlet of the slurry distributor 32 is connected to the inlet of the self-excited oscillating microbubble mineralization device 2 through the inlet guide pipe 33.

[0204] The discharge system 4 includes a concentrate discharge system 41 and a tailings discharge system 42. The concentrate discharge system 41 is located at the upper end of the flotation chamber 11 and includes a concentrate overflow trough 411 and a concentrate collection port 412 located at the bottom of the concentrate overflow trough 411. The tailings discharge system 42 is located on the collecting chamber 12 and includes a tailings discharge port 421 and a middlings discharge port 422.

[0205] Example 6 This embodiment provides a driveless flotation cell with self-excited oscillation function. The driveless flotation cell includes: a flotation cell body 1, a self-excited oscillation microbubble mineralization device 2, a feeding system 3, and a discharging system 4. The flotation cell body 1 includes a flotation chamber 11 and a collecting chamber 12 connected to the bottom of the flotation chamber 11.

[0206] The self-excited oscillating microbubble mineralization device 2 is disposed outside the main body 1 of the flotation cell, and there are four of them, evenly distributed along the circumference of the flotation chamber 11. The self-excited oscillating microbubble mineralization device 2 includes an expansion pipe 21, a throat pipe 22, and a self-excited oscillation chamber 23 connected sequentially along the direction of slurry flow. An inlet guide pipe 33 is connected to the inlet end of the expansion pipe 21. The inner diameter d of the inlet end of the expansion pipe 21 is... e1 The inner diameter d of the outlet end of the inlet guide pipe 33 is... g 1.10 times. The inner diameter d at the inlet end of the throat 22. h1 The inner diameter d of the outlet end of the expansion tube 21 e2 0.90 times. An air inlet 221 is provided on the side wall of the throat tube 22, and the air inlet 221 is connected to an external air source. The resonant cavity of the self-excited oscillation chamber 23, i.e., the inner diameter d at the maximum cross-section of the self-excited oscillation chamber 232. Z1 The inner diameter d of the outlet end of the expansion tube 21 e2 1.2 times. The inner diameter d at the outlet end of the expansion tube 21 e2 The inner diameter d of the inlet end of the expansion tube 21 e1 The ratio is 1.2:1. The inner diameter of the throat 22 gradually decreases from the inlet end to the middle, and the minimum inner diameter d of the throat 22 is... hmin Located in the middle of the throat 22, the minimum inner diameter d of the throat 22 hmin The inner diameter d of the inlet end of the throat tube 22 h1 The ratio is 0.6:1. The axial length L of the throat 22 hThe minimum inner diameter d of the throat 22 hmin 3.0 times. The axial length L of the expansion tube 21 e The minimum inner diameter d of the throat 22 hmin 2.5 times. The axial length L of the self-excited oscillation chamber 23 c The minimum inner diameter d of the throat 22 hmin 5.0 times.

[0207] The self-excited oscillation chamber 23 includes a self-excited oscillation body 232 and a self-excited oscillation outlet section 233; the end of the outlet section of the throat tube 22 of the non-drive flotation cell enters the inlet 231 of the self-excited oscillation body. The cross-sectional area of ​​the self-excited oscillation cavity 232 is larger than the cross-sectional area of ​​the outlet section of the throat 22 of the non-drive flotation cell, so that a step 234 of abrupt change in the cross-section of the self-excited oscillation cavity is formed at the inlet 231 of the self-excited oscillation cavity. The outlet of the self-excited oscillation cavity 232 extends outward to form the self-excited oscillation outlet section 233, and the cross-sectional area of ​​the self-excited oscillation cavity 232 is larger than the cross-sectional area of ​​the self-excited oscillation outlet section 233. The self-excited oscillation outlet section 233 is coaxially arranged with the inlet 231 of the self-excited oscillation cavity, and the outlet at the end of the self-excited oscillation outlet section 233 is connected to the interior of the flotation cavity 11. The inner wall surface of the self-excited oscillation cavity 232, located near the self-excited oscillation outlet section 233 and on both sides of the self-excited oscillation outlet section 233, constitutes a self-excited oscillation collision wall 235, and the wall surface of the self-excited oscillation collision wall 235 faces the inlet 231 of the self-excited oscillation cavity.

[0208] The angle α between the wall surface of the self-excited oscillation collision wall 235 and the axial direction of the self-excited oscillation cavity 232 is 50°. The angle β between the upper and lower inclined surfaces that expand outward at the end of the self-excited oscillation outlet section 233 (i.e., the expansion angle 236 of the self-excited oscillation chamber) is 40°. The inner diameter d at the maximum cross-section of the self-excited oscillation cavity 232 is... Z1 The inner diameter d of the throat outlet section end of the non-drive flotation cell Z3 The ratio is 4.5:1. The axial length d of the self-excited oscillation cavity 232 is... Z2 The inner diameter d at the maximum cross-section of the self-excited oscillation cavity 232 Z1 The ratio is 8:1. The inner diameter d of the self-excited oscillation outlet section 233... Z4 The inner diameter d of the throat outlet section end of the non-drive flotation cell Z3 The ratio is 0.7:1.

[0209] The air inlet 221 is located in the middle of the throat 22, at the point of minimum cross-section of the throat 22. The inner diameter d of the air inlet 221 is... a The minimum inner diameter d of the throat 22 hmin 0.20 times. The air inlet 221 is connected to the annular air pipe 24 via a pipe, and the annular air pipe 24 is arranged around the outer periphery of the flotation chamber 11. The inner diameter d of the annular air pipe 24 is... r The inner diameter d of the air inlet 221 a 2.0 times. The central ring diameter D of the annular air tube 24 r The outer diameter D of the flotation chamber 11 t 1.2 times that.

[0210] The outlet of the self-excited oscillating microbubble mineralization device 2 is connected to the interior of the flotation chamber 11 via an outlet end guide pipe 25. The outlet end guide pipe 25 extends through the wall of the flotation chamber 11 and into its interior, with a nozzle 251 at its end. The outlet of the outlet end guide pipe 25 extends into the flotation chamber 11 at a position corresponding to the lower 1 / 4 height of the chamber. The distance between the outlet of the outlet end guide pipe 25 and the nearest flow stabilizer plate 5 is 1 / 8 of the total height of the flotation chamber 11. The distance between the outlet of the outlet end guide pipe 25 and the tailings discharge port 421 at the bottom of the collecting chamber 12 is 1 / 3 of the total height of the flotation cell body.

[0211] A flow stabilizing plate 5 is installed inside the flotation chamber 11, and the flow stabilizing plate 5 is positioned above the outlet guide pipe 25. The flow stabilizing plate 5 is a horizontally arranged plate structure with through holes 51 on its surface. The flow stabilizing plates 5 are spaced apart along the axial direction of the flotation chamber 11. There are two flow stabilizing plates 5. The distance between adjacent flow stabilizing plates 5 is 1 / 6 of the total height of the flotation chamber 11. The distance between the uppermost flow stabilizing plate 5 and the upper foam overflow end of the flotation chamber 11 is 1 / 6 of the total height of the flotation chamber 11. The distance between the lowermost flow stabilizing plate 5 and the tailings discharge port 421 at the bottom of the collecting chamber 12 is 1 / 2 of the total height of the flotation cell body. The opening ratio of the flow stabilizing plate 5 is 70%. The through holes 51 of the flow stabilizing plate 5 are circular holes with a diameter of 30 mm. The holes of the two adjacent flow stabilizers 5 are staggered on the horizontal projection plane, and the offset of the projection point of the upper hole relative to the adjacent lower hole is 1 / 2 of the distance between the adjacent holes.

[0212] The feeding system 3 includes a feed pipe 31, a slurry distributor 32, and an inlet guide pipe 33. The feed pipe 31 is connected to the inlet of the slurry distributor 32, and the outlet of the slurry distributor 32 is connected to the inlet of the self-excited oscillating microbubble mineralization device 2 through the inlet guide pipe 33.

[0213] The discharge system 4 includes a concentrate discharge system 41 and a tailings discharge system 42. The concentrate discharge system 41 is located at the upper end of the flotation chamber 11 and includes a concentrate overflow trough 411 and a concentrate collection port 412 located at the bottom of the concentrate overflow trough 411. The tailings discharge system 42 is located on the collecting chamber 12 and includes a tailings discharge port 421 and a middlings discharge port 422.

[0214] The non-drive flotation cell also includes a spraying device 6, which is located above the concentrate overflow tank 411. The spraying device 6 is connected to an annular clear water pipe 61, which is arranged around the outer periphery of the flotation chamber 11. The spraying device 6 includes multiple nozzles 62, which are evenly distributed along the circumference of the flotation chamber 11.

[0215] The self-excited oscillating microbubble mineralization device 2 is detachably connected to the inlet guide pipe 33 via the inlet flange 26 and detachably connected to the outlet guide pipe 25 via the outlet flange 27.

[0216] A float ball 7 is installed inside the flotation chamber 11. An inlet pressure gauge 81 is installed on the inlet pipe of the self-excited oscillating microbubble mineralization device 2, and an outlet pressure gauge 82 is installed on the outlet pipe. The flotation cell body 1 is mounted on the frame 9 via a bracket 8. The slurry distributor 32 and the self-excited oscillating microbubble mineralization device 2 are both mounted on the frame 9 and located outside the flotation chamber 11.

[0217] Example 7 This embodiment provides a non-drive flotation cell with self-excited oscillation function. Its structure is basically the same as that of embodiment 5, except that the flotation chamber 11 does not have a flow stabilizer 5 inside.

[0218] Example 8 This embodiment provides a driveless flotation cell with self-excited oscillation function, whose structure is basically the same as that of embodiment 5, except that: (1) The inner diameter d of the inlet end of the expansion tube 21 e1 The inner diameter d of the outlet end of the inlet guide pipe 33 is... g 0.9 times; (2) The inner diameter d of the inlet end of the throat tube 22 h1 The inner diameter d of the outlet end of the expansion tube 21 e2 0.5 times; (3) The inner diameter d at the maximum cross-section of the self-excited oscillation cavity 232 Z1 The inner diameter d of the outlet end of the expansion tube 21 e2 1.4 times; (4) The inner diameter d of the outlet end of the expansion tube 21 e2 The inner diameter d of the inlet end of the expansion tube 21 e1 The ratio is 1.6:1; (5) The minimum inner diameter d of the throat 22 hmin The inner diameter d of the inlet end of the throat tube 22 h1 The ratio is 0.35:1; (6) The inner diameter d at the maximum cross-section of the self-excited oscillation cavity 232 Z1 The inner diameter d of the throat outlet section end of the non-drive flotation cell Z3 The ratio is 10:1; (7) The angle α between the wall surface of the self-excited oscillation collision wall 235 and the axis of the self-excited oscillation cavity 232 is 75°; (8) The included angle β between the upper and lower inclined surfaces that expand outward at the end of the self-excited oscillation outlet section 233 is 20°.

[0219] Example 9 This embodiment provides a flotation method enhanced by self-excited oscillation. In this embodiment, the pulp pretreatment adopts the mineralization device described in Example 1, and the roughing, cleaning, and scavenging all adopt the non-drive flotation cell and its supporting existing flotation technology described in Comparative Example 2.

[0220] The flotation method includes the following steps: feeding the slurry and flotation reagents into a mineralization device for mixing and pre-mineralization to obtain a pre-mineralized slurry; and subjecting the pre-mineralized slurry to roughing, cleaning, and scavenging processes sequentially. The feed pressure of the slurry entering the mineralization device is 0.1 MPa, and the feed flow rate is 10 m³ / s. 3 The flotation reagent is added to the mineralization device at a flow rate of 0.05 L / min and a pressure of 0.1 MPa at 15°C. The air entering the mineralization device is introduced at a pressure of 0.1 MPa and a flow rate of 0.2 m³ / min. 3 / h, the inlet temperature is 15℃; the residence time of the slurry in the mineralization device is 5s.

[0221] Example 10 This embodiment provides a flotation method enhanced by self-excited oscillation. In this embodiment, the pulp pretreatment adopts the mineralization device described in Comparative Example 1, the roughing adopts the non-drive flotation cell described in Example 5, but the cleaning and scavenging still adopt the non-drive flotation cell and its supporting existing flotation technology described in Comparative Example 2.

[0222] The flotation method includes the following steps: feeding the slurry and flotation reagents into the mineralization device described in Comparative Example 1 for mixing and pre-mineralization to obtain a pre-mineralized slurry. For specific steps, please refer to CN 122032763 A.

[0223] In the roughing process, the feed pressure of the slurry entering the non-drive flotation cell described in Example 5 is 0.1 MPa, and the feed flow rate is 10 m³ / s. 3 The air flow rate is 0.1 MPa at 15°C per hour and 0.2 m³ / h at 15°C. 3 The flotation time is 2 minutes, the inlet temperature is 15℃, the liquid level in the main body of the flotation cell is 0.9×H, the foam layer thickness is 0.01×H, the flotation time is 2 minutes, the pH value of the slurry is controlled at 8.3±0.1, and the concentrate scraper speed is 10 r / min.

[0224] Example 11 This embodiment provides a flotation method enhanced by self-excited oscillation. In this embodiment, the pulp pretreatment adopts the mineralization device described in Example 1, the roughing adopts the non-drive flotation cell described in Example 5, but the cleaning and scavenging still adopt the non-drive flotation cell and its supporting existing flotation technology described in Comparative Example 2.

[0225] The flotation method includes the following steps: feeding the slurry and flotation reagents into the mineralization device described in Example 1 for mixing and pre-mineralization to obtain a pre-mineralized slurry; and subjecting the pre-mineralized slurry to roughing, cleaning, and scavenging in sequence. The feed pressure of the slurry entering the mineralization device is 0.1 MPa, and the feed flow rate is 10 m³ / s. 3 The flotation reagent is added to the mineralization device at a flow rate of 0.05 L / min and a pressure of 0.1 MPa at 15°C. The air entering the mineralization device is introduced at a pressure of 0.1 MPa and a flow rate of 0.2 m³ / min. 3 / h, the inlet temperature is 15℃; the residence time of the slurry in the mineralization device is 5s.

[0226] In the roughing process, the feed pressure of the slurry entering the non-drive flotation cell described in Example 5 is 0.1 MPa, and the feed flow rate is 10 m³ / s. 3 The air flow rate is 0.1 MPa at 15°C per hour and 0.2 m³ / h at 15°C. 3 The flotation time is 2 minutes, the inlet temperature is 15℃, the liquid level in the main body of the flotation cell is 0.9×H, the foam layer thickness is 0.01×H, the flotation time is 2 minutes, the pH value of the slurry is controlled at 8.3±0.1, and the concentrate scraper speed is 10 r / min.

[0227] Example 12 This embodiment provides a flotation method enhanced by self-excited oscillation, the steps of which are basically the same as those in Embodiment 11, the difference being the specific values ​​of the process parameters. In this embodiment, the pulp pretreatment adopts the mineralization device described in Embodiment 1, the roughing adopts the non-drive flotation cell described in Embodiment 5, but the cleaning and scavenging still adopt the non-drive flotation cell and its supporting existing flotation technology described in Comparative Example 2.

[0228] The flotation method includes the following steps: feeding the slurry and flotation reagents into the mineralization device described in Example 1 for mixing and pre-mineralization to obtain a pre-mineralized slurry; and subjecting the pre-mineralized slurry to roughing, cleaning, and scavenging in sequence. The feed pressure of the slurry entering the mineralization device is 0.25 MPa, and the feed flow rate is 35 m³ / s. 3 The flotation reagent is added to the mineralization device at a flow rate of 1.5 L / min and a pressure of 0.35 MPa at a temperature of 30°C. The air entering the mineralization device is introduced at a pressure of 0.3 MPa and a flow rate of 12 m³ / min. 3 / h, the inlet temperature is 25℃; the residence time of the slurry in the mineralization device is 12s.

[0229] In the roughing process, the feed pressure of the slurry entering the non-drive flotation cell described in Example 5 is 0.25 MPa, and the feed flow rate is 35 m³ / s. 3 The air flow rate is 12 m³ / h, and the temperature is 30°C. The air pressure entering the non-driven flotation cell is 0.3 MPa, and the flow rate is 12 m³ / h. 3 The flotation time is 6 minutes, the inlet temperature is 25℃, the liquid level in the main body of the flotation cell is 0.75×H, the foam layer thickness is 0.10×H, the flotation time is 6 minutes, the pH value of the slurry is controlled at 9.5±0.1, and the concentrate scraper speed is 35 r / min.

[0230] Example 13 This embodiment provides a flotation method enhanced by self-excited oscillation. The steps are basically the same as in Embodiment 12, except that the cleaning and scavenging processes also employ the non-drive flotation cell described in Embodiment 5. In this embodiment, the pulp pretreatment uses the mineralization device described in Embodiment 1, and the roughing, cleaning, and scavenging processes all employ the non-drive flotation cell described in Embodiment 5.

[0231] The flotation method includes the following steps: feeding the slurry and flotation reagents into the mineralization device described in Example 1 for mixing and pre-mineralization to obtain a pre-mineralized slurry; and subjecting the pre-mineralized slurry to roughing, cleaning, and scavenging in sequence. The feed pressure of the slurry entering the mineralization device is 0.25 MPa, and the feed flow rate is 35 m³ / s. 3The flotation reagent is added to the mineralization device at a flow rate of 1.5 L / min and a pressure of 0.35 MPa at a temperature of 30°C. The air entering the mineralization device is introduced at a pressure of 0.3 MPa and a flow rate of 12 m³ / min. 3 / h, the inlet temperature is 25℃; the residence time of the slurry in the mineralization device is 12s.

[0232] In the roughing stage, the feed pressure of the slurry entering the non-drive flotation cell described in Example 5 is 0.25 MPa, and the feed flow rate is 35 m³ / s. 3 / h, temperature is 30℃; the air entering the non-driven flotation cell has an inlet pressure of 0.3MPa and an inlet flow rate of 12m³ / h. 3 The flotation time is 6 minutes, the inlet temperature is 25℃, the liquid level in the main body of the flotation cell is 0.75×H, the foam layer thickness is 0.10×H, the flotation time is 6 minutes, the pH value of the slurry is controlled at 9.5±0.1, and the concentrate scraper speed is 35 r / min.

[0233] In the fine selection process, the feed pressure of the slurry entering the non-drive flotation cell described in Example 5 is 0.25 MPa, and the feed flow rate is 35 m³ / s. 3 / h, temperature is 30℃; the air entering the non-driven flotation cell has an inlet pressure of 0.3MPa and an inlet flow rate of 8m³ / h. 3 The flotation time is 4 min, the inlet temperature is 25℃, the liquid level in the main body of the flotation cell is 0.80×H, the foam layer thickness is 0.20×H, the flotation time is 4 min, the pH value of the slurry is controlled at 9.5±0.1, and the concentrate scraper speed is 20 r / min.

[0234] During the sweep process, the feed pressure of the slurry entering the non-drive flotation cell described in Example 5 is 0.25 MPa, and the feed flow rate is 20 m³ / s. 3 / h, temperature is 30℃; the air entering the non-driven flotation cell has an inlet pressure of 0.3MPa and an inlet flow rate of 8m³ / h. 3 The flotation time is 8 minutes, the inlet temperature is 25℃, the liquid level in the main body of the flotation cell is 0.70×H, the foam layer thickness is 0.05×H, the flotation time is 8 minutes, the pH value of the slurry is controlled at 9.5±0.1, and the concentrate scraper speed is 20 r / min.

[0235] Example 14 This embodiment provides a flotation method enhanced by self-excited oscillation, the steps of which are basically the same as those in Embodiment 13, except that the slurry pretreatment adopts the mineralization device described in Embodiment 2.

[0236] Example 15 This embodiment provides a flotation method enhanced by self-excited oscillation, the steps of which are basically the same as those in Embodiment 13, except that the pulp pretreatment adopts the mineralization device described in Embodiment 3.

[0237] Example 16 This embodiment provides a flotation method enhanced by self-excited oscillation, the steps of which are basically the same as those in Embodiment 13, except that the pulp pretreatment adopts the mineralization device described in Embodiment 4.

[0238] Example 17 This embodiment provides a flotation method enhanced by self-excited oscillation, the steps of which are basically the same as those in Embodiment 13, except that: the roughing, cleaning and scavenging all adopt the non-drive flotation cell described in Embodiment 6.

[0239] Example 18 This embodiment provides a flotation method enhanced by self-excited oscillation, the steps of which are basically the same as those in Embodiment 13, except that: the roughing, cleaning and scavenging all adopt the non-drive flotation cell described in Embodiment 7.

[0240] Example 19 This embodiment provides a flotation method enhanced by self-excited oscillation, the steps of which are basically the same as those in Embodiment 13, except that: the roughing, cleaning and scavenging all adopt the non-drive flotation cell described in Embodiment 8.

[0241] Comparative Example 1 This comparative example provides an existing mineralization apparatus, which is a fluid-enhanced flotation treatment device that combines self-excited oscillation with acoustic vortex rings. The apparatus includes a feeding mechanism, a feeding conveying pipe, a volute pre-swirl mechanism and a stepped ultrasonic enhancement mechanism sequentially arranged along the feeding direction on the feeding conveying pipe, a Helmholtz cavity pulsating amplifier arranged on the volute pre-swirl mechanism, and a main flotation mechanism connected to the end of the feeding conveying pipe. The volute pre-swirl mechanism includes a volute, a volute inlet pipe communicating with the volute and arranged along the circumferential tangent of the volute, a spiral guide plate disposed inside the volute, a spiral flow channel formed by the spiral guide plate and the volute, a volute tongue located at the inlet of the spiral flow channel, and a volute outlet located in the middle of the side plane of the volute. The Helmholtz cavity pulsating amplifier includes a teardrop-shaped housing, a tapered neck communicating with the amplifier inlet at the upper part of the teardrop-shaped housing, an auxiliary self-priming air intake assembly disposed on the outer periphery of the throat section of the tapered neck, a flow stabilizing assembly disposed inside the teardrop-shaped housing, and a pressure sensor disposed on the teardrop-shaped housing. For example, CN 122032763 A.

[0242] Comparative Example 2 This comparative example provides an existing non-drive flotation cell with the following core structure: It includes a cell body and a slurry distributor. A feed pipe is installed above the slurry distributor, and at least one Venturi tube (two or more can be connected in parallel, each Venturi tube equipped with a valve) is installed below it. This Venturi tube connects to a mineralization pipe, which in turn connects to a slurry mixer. At least one steel pipe is installed at the bottom of the slurry mixer, and a slurry injection device (spherical, cylindrical, or irregularly shaped) is installed at the bottom of the steel pipe. The injection device is equipped with several nozzles (3-12, evenly arranged, with the injection direction at a 30-75° angle to the horizontal plane). The steel pipe is installed within the cell body. A foam collection tank is located at the top of the cell body, and a foam outlet pipe is installed at the bottom of the foam collection tank. The bottom of the cell body is conical, and an underflow discharge valve is installed. The cell body is connected to a middlings tank via a pipe, and a middlings regulating gate is installed at the top of the middlings tank. For example, CN101439315B, CN201592140U, CN221656854U.

[0243] Comparative Example 3 This comparative example provides a flotation method, and the object of processing (raw ore) is the same batch of bauxite samples from a certain area in Henan Province as in Examples 9-19. In this comparative example, the pulp pretreatment adopts the mineralization device described in Comparative Example 1, and the primary roughing, primary cleaning, and primary scavenging all adopt the non-drive flotation cell and its supporting existing flotation technology described in Comparative Example 2.

[0244] The results shown in Tables 1 and 2 are obtained after the slurry and flotation reagents are fed into the mineralization unit for mixing and pre-mineralization to obtain a pre-mineralized slurry, and then the pre-mineralized slurry is subjected to one roughing, one cleaning, and one scavenging process.

[0245] The flotation targets in Examples 9-19 of Table 1 were all bauxite samples from the same batch in a certain area of ​​Henan Province. The main aluminum-bearing mineral was gibbsite, and the main silica-bearing gangues were illite, kaolinite, and quartz. The feed conditions were kept consistent in each example. In each experiment, the Al2O3 and SiO2 grades of the final concentrate obtained after one roughing, one cleaning, and one scavenging were analyzed to calculate the Al2O3 recovery rate and the aluminum-silicon ratio (A / S) of the final concentrate.

[0246] The differences in indicators for Examples 9-19 in Table 1 have a clear correspondence with whether each example uses the mineralization device with self-excited oscillation function and / or the non-drive flotation cell of the present invention, the changes in the structural parameters of each device, and the changes in the flotation process parameters. Example 11 is superior to Examples 9 and 10: Although Example 9 uses the mineralization device of the present invention, the first roughing, first cleaning, and first scavenging are all existing flotation cells and their associated existing processes; although Example 10 uses the non-drive flotation cell of the present invention, the mineralization pretreatment is an existing mineralization device and its existing process; while in Example 11, both the mineralization pretreatment and the first roughing adopt the scheme of the present invention, and its concentrate Al2O3 grade, recovery rate, and aluminum-silicon ratio are all superior to those of Examples 9 and 10. This indicates that the mineralization device and the non-drive flotation cell of the present invention have good synergistic compatibility in upstream and downstream processes. The combined use of the two can produce a cumulative gain superior to that of a single application, proving the synergistic compatibility of the mineralization device and the non-drive flotation cell of the present invention in upstream and downstream processes.

[0247] Building upon Example 11, Example 12 further improved the grade, recovery rate, and aluminum-silicon ratio of the concentrate by optimizing the mineralization and roughing process parameters. Based on Example 12, Example 13 employed the non-driven flotation cell and flotation process provided in this invention for its first roughing, first cleaning, and first scavenging stages. Ultimately, the grade, recovery rate, and aluminum-silicon ratio of the concentrate were further improved compared to Example 12, verifying the cumulative advantages of the non-driven flotation cell in multi-stage separation described in this invention.

[0248] Table 1: Flotation operation indicators and results of the examples

[0249] Table 2: Flotation operation indicators and results of the comparative example

[0250] The above description is only a preferred embodiment of the present invention, but the scope of protection of the present invention is not limited thereto. Any changes or substitutions that can be easily conceived by those skilled in the art within the scope of the technology disclosed in the present invention should be included within the scope of protection of the present invention.

Claims

1. A mineralization device, characterized in that, include: A spherical mixer having a spherical inner cavity, and the spherical mixer being provided with a slurry inlet, a flotation reagent addition inlet, and a slurry outlet; A self-excited oscillating microbubble mineralization tube is connected to the slurry outlet of the spherical mixer. The self-excited oscillating microbubble mineralization tube includes a pipe organ cavity, a throat, and a Helmholtz cavity that are connected sequentially along the slurry flow direction. The side wall of the throat is provided with a compressed air intake pipe, which is connected to an external air source. The outlet of the Helmholtz cavity is connected to a mineralized slurry discharge pipe.

2. The mineralization apparatus according to claim 1, characterized in that, The spherical mixer is provided with at least two slurry feed pipes, each of which is arranged toward the center of the spherical mixer to allow the slurry streams to converge and counteract each other within the spherical mixer.

3. The mineralization apparatus according to claim 1, characterized in that, The spherical mixer is provided with at least two slurry feed pipes in the equatorial plane passing through the center of the sphere; the spherical mixer is provided with a flotation reagent addition pipe and a slurry outlet on an axis perpendicular to the equatorial plane and passing through the center of the sphere, and the self-excited oscillating microbubble mineralization pipe is connected to the slurry outlet.

4. The mineralization apparatus according to claim 1, characterized in that, The spherical mixer is provided with a perforated baffle inside. The perforated baffle is located in the quadrant region between the equatorial plane and the meridian plane of the spherical mixer. The meridian plane is a plane that passes through the center of the spherical mixer and is perpendicular to the equatorial plane.

5. The mineralization apparatus according to claim 4, characterized in that, At least one perforated baffle is provided in each of the quadrant regions.

6. The mineralization apparatus according to claim 5, characterized in that, Each of the quadrant regions is provided with a perforated baffle, and the perforated baffles have the same tilt angle relative to the equatorial plane; And / or, the perforated baffle faces the center of the spherical mixer but does not pass through the center of the spherical mixer.

7. The mineralization apparatus according to claim 4, characterized in that, The perforated baffle is tilted at an angle of 30° to 60° relative to the equatorial plane.

8. The mineralization apparatus according to claim 4, characterized in that, One side of the perforated baffle is conformally fitted and fixed to the inner wall of the spherical mixer, and the distance between the other side and the center of the spherical mixer is not less than 1 / 5 of the radius of the spherical mixer.

9. A self-excited oscillation enhanced flotation system, characterized in that, include: A slurry pretreatment subsystem, the slurry pretreatment subsystem comprising a mineralization device as described in any one of claims 1 to 8; And at least one of the coarse selection subsystem, fine selection subsystem and sweeping selection subsystem; At least one of the coarse flotation subsystem, the fine flotation subsystem, and the sweeping flotation subsystem includes a non-drive flotation cell.

10. A flotation method enhanced by self-excited oscillation, characterized in that, Includes the following steps: The slurry and flotation reagents are fed into the mineralization device as described in any one of claims 1 to 8 for mixing and pre-mineralization to obtain a pre-mineralized slurry; The premineralized slurry is subjected to at least one of roughing, cleaning and scavenging processes; In this process, at least one of the roughing, cleaning, and sweeping processes is carried out using a non-drive flotation cell.

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