WO2025086755A1 - Circulating fluidized bed flotation device and method suitable for recovery of coarse particles - Google Patents

Abstract

The present invention belongs to the technical field of mineral separation and processing. Disclosed is a circulating fluidized bed flotation device suitable for the recovery of coarse particles. The device comprises a first-stage fluidized bed flotation column (100), a second-stage fluidized bed flotation column (200) and a hydrocyclone (300), wherein the first-stage fluidized bed flotation column (100) is in communication with the second-stage fluidized bed flotation column (200) by means of the hydrocyclone (300). By means of the combined use of a high-speed ascending water flow and a low-speed ascending water flow and circulating fluidization flotation, the purposes of increasing the upper limit of flotation and broadening the size range of separation are achieved, and the recovery rate of coarse particles during flotation is improved on the basis of ensuring that both tailings and concentrates reach the standard. Also disclosed is a circulating fluidized bed flotation method suitable for the recovery of coarse particles.

Description

A circulating fluidized bed flotation device and method suitable for coarse particle recovery Technical Field

The present application relates to the technical field of mineral separation and processing, and in particular to a circulating fluidized bed flotation device and method suitable for recovering coarse particles.

Background Art

Flotation is one of the most effective means of mineral separation and recovery. It is an interfacial separation technology based on the difference in hydrophobicity of the particle surface. It uses bubbles as flotation carriers to selectively recover the target valuable mineral particles. To achieve selective recovery by flotation, it is necessary to ensure that the valuable components in the ore can be fully dissociated. However, since the target components often exist in the ore in the form of finer particles, the traditional flotation process can often only dissociate to a product particle size of tens of microns. This limitation leads to high energy consumption in the ore dissociation and grinding process, and too many fine gangue particles will cause the presence of fine mud in the flotation concentrate, thereby reducing the flotation efficiency.

Coarse particle fluidized flotation is an effective method to solve the problems of high energy consumption and low efficiency in traditional flotation process. This technology introduces rising water flow on the basis of traditional flotation, creates a low turbulence flow field environment suitable for processing coarse particles, effectively expands the upper limit of floatable particles, and becomes an effective means to achieve millimeter-level particle flotation recovery. However, the existing equipment has low coarse particle flotation recovery rate and poor sorting accuracy, which cannot meet the needs of mineral sorting and processing technology.

Summary of the invention

In view of the above analysis, the embodiments of the present application aim to provide a circulating fluidized bed flotation device and method suitable for coarse particle recovery, especially suitable for re-flotation coupling, to solve the problems of low coarse particle flotation recovery rate and poor sorting accuracy of existing equipment.

On the one hand, the present application provides a circulating fluidized bed flotation device suitable for coarse particle recovery, comprising a first-stage fluidized bed flotation column, a second-stage fluidized bed flotation column and a hydrocyclone, wherein the first-stage fluidized bed flotation column and the second-stage fluidized bed flotation column are connected via the hydrocyclone.

Furthermore, the one-stage fluidized bed flotation column comprises a first column and a first slurry distribution ring, wherein the first slurry distribution ring is sleeved on the upper part of the first column and communicated with the inner cavity of the first column.

Furthermore, the two-stage fluidized bed flotation column comprises a second column and a second slurry distribution ring, wherein the second slurry distribution ring is sleeved on the lower part of the second column and communicated with the inner cavity of the second column.

Furthermore, the hydrocyclone is connected to the upper end of the first column and the second slurry distribution ring.

Furthermore, it also includes a water storage tank, a first top water delivery pipeline and a second top water delivery pipeline.

Furthermore, one end of the first top water delivery pipeline is connected to the water storage tank, and the other end is connected to the first stage fluidized bed flotation column, and one end of the second top water delivery pipeline is connected to the water storage tank, and the other end is connected to the second stage fluidized bed flotation column.

Furthermore, it also includes a gas storage tank, a first gas delivery pipeline and a second gas delivery pipeline.

Furthermore, one end of the first gas delivery pipeline is connected to the gas storage tank, and the other end is connected to the first-stage fluidized bed flotation column; one end of the second gas delivery pipeline is connected to the gas storage tank, and the other end is connected to the second-stage fluidized bed flotation column.

Furthermore, the overflow port of the hydrocyclone is connected to the water storage tank through a pipeline.

On the other hand, the present application provides a circulating fluidized bed flotation method suitable for coarse particle recovery, which uses the above-mentioned circulating fluidized bed flotation device suitable for coarse particle recovery to perform flotation.

Compared with the prior art, the present invention can achieve at least one of the following beneficial effects:

(1) The flotation column of the present application is a circulating fluidized flotation coupled with refloatation under the action of rising water flow, through the coordinated use of high-speed rising water flow and low-speed rising water flow and circulating fluidized flotation, The purpose of increasing the upper limit of flotation and expanding the range of separation particle size is achieved, and the recovery rate of coarse particle flotation is improved on the basis of ensuring that both tailings and concentrates meet the standards.

(2) The distribution plates in the flotation column of the present application are arranged in multiple layers in an interlaced manner. The number of distribution plates can be freely adjusted to achieve fluidized concentration and sweeping times to match the flotation of minerals with different particle sizes and densities. It is suitable for the flotation of minerals with different particle size ranges and different types of ores, and has the advantage of one machine for multiple uses.

(3) The present application adopts a hydrocyclone to concentrate the slurry in the circulating fluidized bed flotation device, thereby ensuring a stable and appropriate slurry concentration in the flotation system, reducing reagent consumption and improving selectivity.

(4) The slurry of the present application is fed into the flotation column through a distribution ring. The confined space structure composed of the distribution ring and the column wall redirects the slurry multiple times. The slurry dissipates a lot of energy and is fed into the flotation column along the inner wall of the flotation column at a relatively low speed, thereby reducing the disturbance of the flow field in the flotation column caused by the feed.

(5) A water distribution plate and an air distribution plate (i.e., a bubble generating plate) are arranged under the flotation column of the present application, thereby realizing the construction of a flotation environment with small fluid disturbance and sufficient microbubble content suitable for coarse particle flotation; back-mixing is avoided by high-speed rising water flow to ensure the quality of waste; low-speed rising water flow achieves the quality of coarse particle concentrate; circulating middlings for reselection improves the flotation "coarse run" phenomenon and increases the recovery rate of coarse particles.

In the present application, the above-mentioned technical solutions can also be combined with each other to achieve more preferred combination solutions. Other features and advantages of the present application will be described in the subsequent description, and some advantages can become obvious from the description, or can be understood by practicing the present application. The purpose and other advantages of the present application can be realized and obtained through the contents particularly pointed out in the description and the drawings.

BRIEF DESCRIPTION OF THE DRAWINGS

The accompanying drawings are only for the purpose of illustrating specific embodiments and are not to be considered as limiting the present application. The same reference symbols denote the same components throughout the accompanying drawings.

FIG1 is a schematic structural diagram of a circulating fluidized bed flotation device according to a specific embodiment;

FIG2 is a schematic diagram of the material flow in a circulating fluidized bed flotation device according to a specific embodiment;

FIG3 is a schematic diagram of the flow of gas-water mixture in a circulating fluidized bed flotation device according to a specific embodiment;

FIG4 is a schematic structural diagram of a first slurry distribution ring according to a specific embodiment;

5 is a schematic structural diagram of a first water distribution plate and a first bubble generating plate in a specific embodiment;

FIG6 is a schematic structural diagram of a second slurry distribution ring in a specific embodiment;

FIG. 7 is a schematic structural diagram of a second water distribution plate and a second bubble generating plate in a specific embodiment.

Reference numerals:
100-a fluidized bed flotation column; 101-a first column; 102-a first pulp distribution ring; 103-
First distribution plate; 104-first overflow pipe; 105-first sorting chamber; 106-first scavenging chamber; 107-second scavenging chamber; 108-third scavenging chamber; 109-fourth scavenging chamber; 110-first water distribution plate; 111-first bubble generating plate; 112-first tailings outlet; 113-first annular distribution chamber; 114-first annular baffle; 115-first opening; 116-first feed inlet; 117-first water inlet; 118-first air inlet;
200-second stage fluidized bed flotation column; 201-second column; 202-second slurry distribution ring; 203-
Second distribution plate; 204-second overflow pipe; 205-second sorting chamber; 206-first concentration chamber; 207-second concentration chamber; 208-second water distribution plate; 209-second bubble generating plate; 210-second tailings outlet; 211-second annular distribution chamber; 212-second annular baffle; 213-second opening; 214-second feed inlet; 215-second water inlet; 216-second air inlet; 217-concentrate collecting tank; 218-concentrate outlet;
300- hydrocyclone; 301- overflow port; 302- bottom flow port; 303- slurry conveying pipe; 400-
Water storage tank; 401-fifth solenoid valve; 402-water pump; 500-gas storage tank; 501-sixth solenoid valve;
600-first top water delivery pipeline; 601-first solenoid valve; 602-first liquid flow meter; 603-
First flow regulating valve; 700-second top water delivery pipeline; 701-second solenoid valve; 702-second liquid flow meter; 703-second flow regulating valve; 800-first gas delivery pipeline; 801-third solenoid valve; 802-third liquid flow meter; 803-third flow regulating valve; 900-second gas delivery pipeline; 901-fourth solenoid valve; 902-fourth liquid flow meter; 903-fourth flow regulating valve.

DETAILED DESCRIPTION

The preferred embodiments of the present application are described in detail below in conjunction with the accompanying drawings, wherein the accompanying drawings constitute a part of the present application and are used together with the embodiments of the present application to illustrate the principles of the present application, and are not used to limit the scope of the present application.

Example 1

A specific embodiment of the present application, as shown in FIG1 , discloses a circulating fluidized bed flotation device suitable for coarse particle recovery (hereinafter referred to as the circulating fluidized bed flotation device), as shown in FIGS. 1 , 2 and 3 , comprising a first-stage fluidized bed flotation column 100, a second-stage fluidized bed flotation column 200 and a hydrocyclone 300, wherein the first-stage fluidized bed flotation column 100 and the second-stage fluidized bed flotation column 200 are connected via the hydrocyclone 300.

As shown in FIG1 , a fluidized bed flotation column 100 includes a first column 101 and a first slurry distribution ring 102. The first slurry distribution ring 102 is sleeved on the first column 101 and communicates with the inner cavity of the first column 101. The first slurry distribution ring 102 is disposed at the upper portion of the first column 101.

A first distribution plate 103 is horizontally arranged in the first column 101. The first distribution plate 103 is a plate with holes. The hole diameter of the first distribution plate 103 is 1-3 mm. There are 2-5 first distribution plates 103, preferably 4. The edge of the first distribution plate 103 is provided with a first through hole. The first through hole is tangent to the edge of the first distribution plate 103. A first overflow pipe 104 is arranged in the first through hole. The upper end of the first overflow pipe 104 is higher than the top of the first distribution plate 103, and the lower end of the first overflow pipe 104 is lower than the bottom of the first distribution plate 103.

In this embodiment, a plurality of first distribution plates 103 are provided in the first column 101, and a first overflow pipe 104 is provided at the edge of the first distribution plate 103. Both ends of the first overflow pipe 104 exceed the two sides of the first distribution plate 103, forming a barrel-shaped structure with the distribution layer, buffering the slurry and forming a sorting bed layer, thereby increasing the sorting time of the slurry and improving the sorting efficiency.

Two adjacent first overflow pipes 104 are respectively located on both sides of the inner cavity of the first column 101. From the longitudinal section of the first column 101, the first distribution plates 103 are staggered in the first column 101, and the first overflow pipe 104 is disposed between the first distribution plate 103 and the inner wall of the first column 101. It should be noted that the longitudinal section of the first column 101 refers to a section along the axis passing through the first column 101 and passing through the diameter of the first distribution plate 103 and the first through hole.

In this embodiment, the first overflow pipes 104 are staggered on both sides of the inner cavity of the first column 101, forcing the slurry from top to bottom to be sorted at each layer, thereby preventing the slurry from directly entering the first tailings outlet 112 without being sorted, causing a slurry short circuit.

The four first distribution plates 103 divide the inner cavity of the first column 101 from top to bottom into a first sorting chamber 105, a first scavenging chamber 106, a second scavenging chamber 107, a third scavenging chamber 108 and a fourth scavenging chamber 109. The multi-layer first distribution plates 103 divide the inner cavity of the first column 101 into multi-layer fluidized beds, and adjacent fluidized beds are connected through the first overflow pipe 104.

As shown in Fig. 1 and Fig. 4, a first water distribution plate 110 and a first bubble generating plate 111 are provided at the lower end of the interior of the first column 101, and the first water distribution plate 110 and the first bubble generating plate 111 are arranged concentrically with the first column 101. The first water distribution plate 110 is arranged obliquely in the inner cavity of the first column 101, that is, the first water distribution plate 110 is arranged in an inverted cone shape at the bottom of the inner cavity of the first column 101. The inclination angle of the first water distribution plate 110 is 5 to 35°, preferably 15°.

The first bubble generating plate 111 is disposed below the first water distribution plate 110. The first bubble generating plate 111 is a circular ring structure. The middle of the first bubble generating plate 111 passes through the first tailings outlet 112. The upper end of the first tailings outlet 112 is connected to the bottom of the first water distribution plate 110. The lower end of the first tailings outlet 112 passes through the lower end of the first column 101. The first bubble generating plate 111 is a microporous ceramic plate, and the pore size of the microporous ceramic plate is 5 to 10 μm, preferably 5 μm.

As shown in Fig. 4, the first slurry distribution ring 102 includes a first annular distribution chamber 113 and a first annular baffle 114, which are respectively located on the outer and inner sides of the first column 101. The longitudinal section of the first annular distribution chamber 113 is a "凵"-shaped structure, and the two symmetrical side walls of the first annular distribution chamber 113 are connected to the side walls of the first column 101. A first opening 115 is provided between two symmetrical side walls of the first annular distribution chamber 113 on the first column 101 , so that the first annular distribution chamber 113 is in communication with the inner cavity of the first column 101 .

The longitudinal section of the first annular baffle 114 is L-shaped. The short side end of the first annular baffle 114 is connected to the inner wall of the first column 101, and the connection position is located no higher than the first opening 115. The long side end of the first annular baffle 114 extends upward from the short side end and blocks the first opening 115 in front of the first column 101.

In this embodiment, a first annular baffle 114 is provided on the inner side of the first column 101. The first annular baffle 114 blocks the front of the first opening 115, so that the slurry in the first annular distribution chamber 113 does not flow directly into the first column 101 from the first opening 115, but flows upward after passing through the first opening 115, and flows into the first column 101 from the gap between the long side end of the first annular baffle 114 and the inner wall of the first column 101. The first annular baffle 114 is used to consume part of the energy of the slurry, so as to avoid the slurry in the first annular distribution chamber 113 directly flowing into the first column 101 to disturb the steady-state sorting environment in the first column 101, thereby affecting the sorting effect.

As shown in Fig. 1, Fig. 4 and Fig. 5, the first slurry distribution ring 102 is also provided with a first feed port 116, which is in communication with the first annular distribution chamber 113. A first water inlet 117 and a first air inlet 118 are also provided at the lower part of the first column 101, the first water inlet 117 is in communication with the space between the first water distribution plate 110 and the first bubble generating plate 111, and the first air inlet 118 is provided below the first bubble generating plate 111. The number of the first water inlet 117 and the first air inlet 118 are both 4 to 8, preferably 4, and the 4 first water inlets 117 and the 4 first air inlets 118 are evenly distributed along the outer periphery of the first column 101.

As shown in FIG1 , the two-stage fluidized bed flotation column 200 includes a second column 201 and a second slurry distribution ring 202. The second slurry distribution ring 202 is sleeved on the second column 201 and communicates with the inner cavity of the second column 201. The second slurry distribution ring 202 is disposed at the lower part of the second column 201.

The second column 201 is provided with a second distribution plate 203 horizontally, and the second distribution plate 203 is a plate with holes, and the hole diameter of the second distribution plate 203 is 1-3mm. There are 2-5 second distribution plates 203, preferably Select 2, a second through hole is opened on the edge of the second distribution plate 203, the second through hole is tangent to the edge of the second distribution plate 203, a second overflow pipe 204 is arranged in the second through hole, the upper end of the second overflow pipe 204 is higher than the top of the second distribution plate 203, and the lower end of the second overflow pipe 204 is lower than the bottom of the second distribution plate 203.

In this embodiment, a plurality of layers of second distribution plates 203 are provided in the second column 201, and a second overflow pipe 204 is provided at the edge of the second distribution plate 203. Both ends of the second overflow pipe 204 exceed the two sides of the second distribution plate 203, forming a barrel-shaped structure with the distribution layer, buffering the slurry and forming a sorting bed layer, thereby increasing the sorting time of the slurry and improving the sorting efficiency.

Two adjacent second overflow pipes 204 are respectively located on both sides of the inner cavity of the second column 201. From the longitudinal section of the second column 201, the second distribution plates 203 are staggered in the second column 201, and the second overflow pipe 204 is arranged between the second distribution plate 203 and the inner wall of the second column 201. It should be noted that the longitudinal section of the second column 201 refers to a section along the axis passing through the second column 201 and passing through the diameter of the second distribution plate 203 and the through hole at the same time.

In this embodiment, the second overflow pipes 204 are staggered on both sides of the inner cavity of the second column 201, forcing the slurry from top to bottom to be sorted at each layer, thereby preventing the slurry from directly entering the second tailings outlet 210 without being sorted, causing a slurry short circuit.

The two second distribution plates 203 divide the inner cavity of the second column 201 from bottom to top into a second sorting chamber 205, a first concentration chamber 206 and a second concentration chamber 207. The multi-layer second distribution plates 203 divide the inner cavity of the second column 201 into multi-layer fluidized beds, and the adjacent fluidized beds are connected through the second overflow pipe 204.

As shown in Fig. 1 and Fig. 7, a second water distribution plate 208 and a second bubble generating plate 209 are provided at the inner lower end of the second column 201, and the second water distribution plate 208 and the second bubble generating plate 209 are arranged concentrically with the second column 201. The second water distribution plate 208 is arranged obliquely in the inner cavity of the second column 201, that is, the second water distribution plate 208 is arranged in an inverted cone shape at the bottom of the inner cavity of the second column 201. The inclination angle of the second water distribution plate 208 is 5 to 35°, preferably 15°.

The second bubble generating plate 209 is disposed below the second water distribution plate 208. The second bubble generating plate 209 is a circular ring structure. The middle of the second bubble generating plate 209 passes through the second tailings outlet 210. The upper end of the second tailings outlet 210 is connected to the bottom of the second water distribution plate 208. The lower end of the second tailings outlet 210 passes through the lower end of the second column 201. The second bubble generating plate 209 is a microporous ceramic plate, and the pore size of the microporous ceramic plate is 5 to 10 μm, preferably 5 μm.

As shown in Fig. 6, the second slurry distribution ring 202 includes a second annular distribution chamber 211 and a second annular baffle 212, which are respectively located on the outer and inner sides of the second column 201. The longitudinal section of the second annular distribution chamber 211 is a "凵"-shaped structure, and the two symmetrical side walls of the second annular distribution chamber 211 are connected to the side walls of the second column 201. A second opening 213 is provided on the second column 201 between the two symmetrical side walls of the second annular distribution chamber 211, so that the second annular distribution chamber 211 is connected to the inner cavity of the second column 201.

The longitudinal section of the second annular baffle 212 is L-shaped. The short side end of the second annular baffle 212 is connected to the inner wall of the second column 201, and the connection position is located no higher than the second opening 213. The long side end of the second annular baffle 212 extends upward from the short side end and blocks the second opening 213 in the second column 201.

In this embodiment, a second annular baffle 212 is provided on the inner side of the second column 201. The second annular baffle 212 blocks the front of the second opening 213, so that the slurry in the second annular distribution chamber 211 will not flow directly into the second column 201 from the second opening 213, but will flow upward after passing through the second opening 213, and flow into the second column 201 from the gap between the long side end of the second annular baffle 212 and the inner wall of the second column 201. The second annular baffle 212 is used to consume part of the energy of the slurry, so as to avoid the slurry in the second annular distribution chamber 211 directly flowing into the second column 201 to disturb the steady-state sorting environment in the second column 201, thereby affecting the sorting effect.

As shown in Figures 6 and 7, the second slurry distribution ring 202 is further provided with a second feed inlet 214, which is communicated with the second annular distribution chamber 211. A second water inlet 215 and a second air inlet 216 are further provided at the lower part of the second column 201, and the second water inlet 215 is communicated with the second water distribution plate 214. 208 is connected to the space between the second bubble generating plate 209, and the second air inlet 216 is opened below the second bubble generating plate 209. The number of the second water inlet 215 and the second air inlet 216 are both 4 to 8, preferably 4, and the four second water inlets 215 and the four second air inlets 216 are evenly distributed along the outer periphery of the second column 201.

As shown in Fig. 1, the upper end of the second column 201 is connected to a concentrate collecting tank 217, which surrounds the second column 201 and has a concentrate opening 218. A water spraying device is also provided on the top of the second column 201.

As shown in Figure 1, the hydrocyclone 300 is provided with an overflow port 301 at the top and an underflow port 302 at the bottom. The upper end of the first column 101 is tangentially connected to the hydrocyclone 300 through a pipeline. The underflow port 302 of the hydrocyclone 300 is connected to the second slurry distribution ring 202 through a slurry conveying pipe 303. The slurry conveying pipe 303 is specifically connected to the second feed port 214.

As shown in Fig. 1, the circulating fluidized bed flotation device further includes a water storage tank 400, a gas storage tank 500, a first top water delivery pipeline 600, a second top water delivery pipeline 700, a first gas delivery pipeline 800, and a second gas delivery pipeline 900. One end of the first top water delivery pipeline 600 is in communication with the water storage tank 400, and the other end is in communication with the first water inlet 117, one end of the second top water delivery pipeline 700 is in communication with the water storage tank 400, and the other end is in communication with the second water inlet 215, one end of the first gas delivery pipeline 800 is in communication with the gas storage tank 500, and the other end is in communication with the first gas inlet 118, and one end of the second gas delivery pipeline 900 is in communication with the gas storage tank 500, and the other end is in communication with the second gas inlet 216.

The first top water delivery pipeline 600 is provided with a first solenoid valve 601, a first liquid flow meter 602 and a first flow regulating valve 603, which are arranged in sequence from the water storage tank 400 to the first water inlet 117. The second top water delivery pipeline 700 is provided with a second solenoid valve 701, a second liquid flow meter 702 and a second flow regulating valve 703, which are arranged in sequence from the water storage tank 400 to the second water inlet 215.

In this embodiment, by using the first top water delivery pipeline 600 and the second top water delivery pipeline 700 A solenoid valve, a liquid flow meter and a flow regulating valve are provided to control the delivery amount, delivery speed and whether to deliver the top water to meet the top water demand of the first-stage fluidized bed flotation column 100 and the second-stage fluidized bed flotation column 200.

The first gas delivery pipeline 800 is provided with a third solenoid valve 801, a third liquid flow meter 802 and a third flow regulating valve 803, and the third solenoid valve 801, the third liquid flow meter 802 and the third flow regulating valve 803 are arranged in sequence from the gas storage tank 500 to the first air inlet 118. The second gas delivery pipeline 900 is provided with a fourth solenoid valve 901, a fourth liquid flow meter 902 and a fourth flow regulating valve 903, and the fourth solenoid valve 901, the fourth liquid flow meter 902 and the fourth flow regulating valve 903 are arranged in sequence from the gas storage tank 500 to the second air inlet 216.

In this embodiment, by providing a solenoid valve, a liquid flow meter and a flow regulating valve on the first gas delivery pipeline 800 and the second gas delivery pipeline 900, the gas delivery amount, delivery speed and whether to deliver the gas can be controlled to meet the gas demand of the first-stage fluidized bed flotation column 100 and the second-stage fluidized bed flotation column 200.

In order to facilitate simultaneous control of the opening and closing of the first top water delivery pipeline 600 and the second top water delivery pipeline 700, the first top water delivery pipeline 600 and the second top water delivery pipeline 700 are simultaneously passed through the fifth solenoid valve 401 before being connected to the water storage tank 400. In order to facilitate simultaneous control of the opening and closing of the first gas delivery pipeline 800 and the second gas delivery pipeline 900, the first gas delivery pipeline 800 and the second gas delivery pipeline 900 are simultaneously passed through the sixth solenoid valve 501 before being connected to the gas storage tank 500.

As shown in Figure 1, the overflow port 301 of the hydrocyclone 300 is connected to the water storage tank 400 through a pipeline, and a water pump 402 is provided in the pipeline. The second tailings outlet 210 is connected to the first feed port 116 through a pipeline (not shown in the figure).

Example 2

Another specific embodiment of the present application, as shown in FIG. 1 to FIG. 7 , discloses a circulating fluidized bed flotation method suitable for coarse particle recovery, using the circulating fluidized bed flotation device suitable for coarse particle recovery of Example 1, comprising the following steps:

Step 1: The water storage tank 400 injects top water containing a frother into the air-water mixing chamber of a first-stage fluidized bed flotation column 100 at a relatively high water velocity (3-6 cm/s), and at the same time, the air storage tank 500 injects air into the high-pressure air chamber of a first-stage fluidized bed flotation column 100 at a relatively high air velocity (0.3-0.5 L/min).

Specifically, the top water in the water storage tank 400 enters the gas-water mixing chamber at the bottom of the column of the first fluidized bed flotation column 100 through the first top water delivery pipeline 600 and the first water inlet 117, and the air in the gas storage tank 500 enters the high-pressure gas chamber at the bottom of the column of the first fluidized bed flotation column 100 through the first gas delivery pipeline 800 and the first gas inlet 118. The speed and flow of the top water and the speed and flow of the gas are regulated by the first flow regulating valve 603 and the second flow regulating valve 703.

It should be noted that the gas-water mixing chamber of a fluidized bed flotation column 100 refers to the space between the first water distribution plate 110, the first bubble generating plate 111 and the inner wall of the first column 101, and the high-pressure gas chamber of a fluidized bed flotation column 100 refers to the space between the first bubble generating plate 111, the first tailings outlet 112 and the inner wall of the first column 101.

Step 2: After a section of the fluidized bed flotation column 100 is filled with the gas-water mixture, the gas-water mixture is fed into the hydrocyclone 300 along the tangential direction and forms a cyclone in the hydrocyclone 300 .

In this embodiment, a hydrocyclone is used to concentrate the pulp in the circulating fluidized bed flotation device, which ensures that the pulp concentration in the flotation system is stable and appropriate, reduces reagent consumption, and improves selectivity.

Step 3: The water storage tank 400 injects top water containing a frother into the air-water mixing chamber of the second-stage fluidized bed flotation column 200 at a relatively low water velocity (1-3 cm/s), and at the same time, the air storage tank 500 injects air into the high-pressure air chamber of the second-stage fluidized bed flotation column 200 at a relatively low air velocity (0.1-0.3 L/min).

Specifically, the top water in the water storage tank 400 enters the gas-water mixing chamber at the bottom of the column body of the second-stage fluidized bed flotation column 200 through the second top water delivery pipeline 700 and the second water inlet 215, and the air in the gas storage tank 500 enters the high-pressure gas chamber at the bottom of the column body of the second-stage fluidized bed flotation column 200 through the second gas delivery pipeline 900 and the second gas inlet 216. The speed and flow of the top water and the speed and flow of the gas are regulated by the third flow regulating valve 803 and the fourth flow regulating valve 903.

It should be noted that the air-water mixing chamber of the second-stage fluidized bed flotation column 200 refers to the second water distribution chamber. The space between the plate 208 , the second bubble generating plate 209 and the inner wall of the second column 201 , and the high-pressure air chamber of the second-stage fluidized bed flotation column 200 refers to the space between the second bubble generating plate 209 , the second tailings outlet 210 and the inner wall of the second column 201 .

Step 4: When the gas-water mixture fills 2/3 of the second-stage fluidized flotation column 200, the slurry is fed into the first-stage fluidized bed flotation column 100 for circulating fluidized separation.

Specifically, water and air are introduced through the first water distribution plate 110 and the first bubble generating plate 111 to form a flotation flow field environment with small fluid disturbance and sufficient microbubble content in the first column 101 .

Coarse-grained minerals and water are mixed into a uniform slurry which is pumped into the first slurry distribution ring 102 through a material pump. The slurry has a large energy dissipation after multiple redirections in the confined space structure formed by the first slurry distribution ring 102 and the wall of the first column 101. The slurry is fed into the first column 101 along the inner wall of the first column 101 at a relatively low speed, thereby reducing the disturbance of the flow field in the first column 101 caused by the feed.

Step 5: The slurry is scavenged multiple times in a fluidized flotation column 100 to form a coarse concentrate, which is then discarded.

Specifically, in a fluidized flotation column 100, coarse particles in the slurry in the first separation chamber 105 collide with the rising bubbles, and the hydrophobic particles adhere to the bubbles to form particle-bubble aggregates. Under the dual effects of the buoyancy of the bubbles and the rising water flow, the particle-bubble aggregates float up, and some hydrophilic minerals also float up under the action of the rising water flow to become coarse concentrate; under the action of gravity, the unmineralized hydrophilic particles and some hydrophobic minerals sink from top to bottom through the pores of the first distribution plate 103 and the first overflow pipe 104 to the first scavenging chamber 106 for the second sorting, and the hydrophobic particles adhere to the bubbles to form particle-bubble aggregates again. Under the dual effects of the buoyancy of the bubbles and the rising water flow, the particle-bubble aggregates float up through the first distribution plate 103 into the first separation chamber 105, and finally form coarse concentrate; the material that has not been mineralized at this time sinks again to the lower second scavenging chamber 107 for the third sorting. By analogy, after multiple sweeps, the high-density hydrophilic particles settle to the bottom of the first column 101 and are discharged from the first tailings outlet 112, thereby achieving the pre-disposal of high-density gangue.

Step 6: The coarse concentrate is fed into the hydrocyclone 300 for concentration, and the concentrated coarse concentrate is fed into the second-stage fluidized bed flotation column 200.

Specifically, after the coarse concentrate produced by a fluidized bed flotation column 100 enters the pipeline, the cross-section of the pipeline decreases relative to the cross-section of the first column 101, the speed increases, and it is fed into the hydrocyclone 300 along the tangent of the cylindrical section of the hydrocyclone 300 to form a vortex; under the action of gravity and centrifugal force, the coarse concentrate particles rotate and sink along the wall, and the gas-water mixture rotates and rises, thereby achieving the concentration of the coarse concentrate.

The rising gas-water mixture is discharged from the overflow port 301 of the hydrocyclone and pumped into the water storage tank 400 for recycling through the water pump 402; the sinking concentrated coarse concentrate is fed into the second slurry distribution ring 202 through the slurry conveying pipe 303. Similarly, the sinking concentrated coarse concentrate is fed into the second column 201 along the inner wall of the second column 201 at a lower speed after multiple redirections.

Step 7: The coarse concentrate is concentrated and sorted multiple times in the second-stage fluidized flotation column 200 to form a concentrate.

In the two-stage fluidized flotation column 200, in the second sorting chamber 205, the hydrophobic particle bubble aggregates and the mixed hydrophilic particles in the concentrated coarse concentrate float from bottom to top through the pores of the second distribution plate 203 to the first selection chamber 206 for secondary sorting under the action of the rising water flow and buoyancy; the mixed hydrophilic particles and some hydrophobic particles detached from the bubbles settle and are discharged from the second tailings outlet 210, and are sent to the first fluidized bed flotation column 100 through the pipeline for further sorting. The hydrophobic particles in the material entering the first selection chamber 206 adhere to the bubbles and form particle bubble aggregates again. Under the dual action of the bubble buoyancy and the rising water flow, the particle bubble aggregates float through the second distribution plate 203 and enter the second selection chamber 207 for the third sorting, and finally form a concentrate that floats into the foam area to form a foam product, i.e., a concentrate, and finally is discharged from the concentrate outlet 218 at the top of the second column 201. At this time, the medium hydrophobic particles that have not been mineralized yet, under the action of gravity, sink from top to bottom through the pores of the second distribution plate 203 and the second overflow pipe 204 to the second separation chamber 205, and then are discharged from the second tailings outlet 210 and transported to a fluidized bed flotation column through a pipeline. 100 is sorted continuously to ensure the number and quality of coarse particles.

In this embodiment, high-speed rising water flow is used to avoid back mixing and ensure the quality of waste disposal; low-speed rising water flow achieves the quality of coarse particle concentrate; and the recycling of middlings for reselection improves the flotation "coarse" phenomenon and increases the recovery rate of coarse particles.

The above is only a preferred specific implementation of the present application, but the protection scope of the present application is not limited thereto. Any changes or substitutions that can be easily conceived by any technician familiar with the technical field within the technical scope disclosed in the present application should be covered within the protection scope of the present application.

Claims (10)

A circulating fluidized bed flotation device suitable for recovering coarse particles, characterized in that it comprises a first-stage fluidized bed flotation column (100), a second-stage fluidized bed flotation column (200) and a hydrocyclone (300), wherein the first-stage fluidized bed flotation column (100) and the second-stage fluidized bed flotation column (200) are connected via the hydrocyclone (300). According to claim 1, the circulating fluidized bed flotation device suitable for coarse particle recovery is characterized in that the one-stage fluidized bed flotation column (100) includes a first column (101) and a first slurry distribution ring (102), and the first slurry distribution ring (102) is sleeved on the upper part of the first column (101) and communicated with the inner cavity of the first column (101). According to claim 2, the circulating fluidized bed flotation device suitable for coarse particle recovery is characterized in that the two-stage fluidized bed flotation column (200) includes a second column (201) and a second slurry distribution ring (202), and the second slurry distribution ring (202) is sleeved on the lower part of the second column (201) and is connected to the inner cavity of the second column (201). The circulating fluidized bed flotation device suitable for coarse particle recovery according to claim 3 is characterized in that the hydrocyclone (300) is connected to the upper end of the first column (101) and the second slurry distribution ring (202). The circulating fluidized bed flotation device suitable for coarse particle recovery according to any one of claims 1 to 4 is characterized in that it also includes a water storage tank (400), a first top water delivery pipeline (600) and a second top water delivery pipeline (700). According to claim 5, the circulating fluidized bed flotation device suitable for coarse particle recovery is characterized in that one end of the first top water delivery pipeline (600) is connected to the water storage tank (400), and the other end is connected to the first-stage fluidized bed flotation column (100), and one end of the second top water delivery pipeline (700) is connected to the water storage tank (400), and the other end is connected to the second-stage fluidized bed flotation column (200). A circulating fluidized bed suitable for coarse particle recovery according to any one of claims 1 to 4 and 6 The bed flotation device is characterized by further comprising a gas storage tank (500), a first gas delivery pipeline (800) and a second gas delivery pipeline (900). According to claim 7, the circulating fluidized bed flotation device suitable for coarse particle recovery is characterized in that one end of the first gas delivery pipeline (800) is connected to the gas storage tank (500), and the other end is connected to the first-stage fluidized bed flotation column (100), and one end of the second gas delivery pipeline (900) is connected to the gas storage tank (500), and the other end is connected to the second-stage fluidized bed flotation column (200). The circulating fluidized bed flotation device suitable for coarse particle recovery according to claim 5 is characterized in that the overflow port (301) of the hydrocyclone (300) is connected to the water storage tank (400) through a pipeline. A circulating fluidized bed flotation method suitable for coarse particle recovery, characterized in that flotation is performed using the circulating fluidized bed flotation device suitable for coarse particle recovery described in any one of claims 1 to 9.