EA040329B1 - FOAM FLOTATION CHAMBER - Google Patents

Description

The field of technology to which the invention belongs

The present invention relates to a froth flotation cell for processing mineral ore particles suspended in the pulp and for separating the pulp into bottom and top products, to a froth flotation line, to its use and to a froth flotation method.

The essence of the invention

The froth flotation chamber according to the present invention is characterized by that presented in claim 1.

The flotation line in accordance with the present invention is characterized by what is presented in paragraph 42.

The use of the froth flotation device according to the present invention is characterized by what is presented in claim 46.

The froth flotation process according to the present invention is characterized by that presented in claim 49.

The froth flotation chamber is designed to extract valuable metals containing ore particles from ore particles suspended in the slurry and to separate the slurry into bottom and top products. The froth flotation chamber comprises a tank with a center and a periphery, a gas source for introducing flotation gas into the pulp to form foam, a first froth collection channel surrounding the periphery of the tank so that an open surface of foam is formed inside the first froth collection channel, a second froth collection channel located between the center of the tank and the first channel for collecting foam and essentially concentric with the first channel for collecting foam, and the second chute for collecting foam contains the first edge for overflow of foam facing the center of the tank, and a radial chute for collecting foam containing a radial edge for foam overflow and extending from the first foam collection channel to the second foam collection channel and in fluid communication with the first foam collection channel. The pulp area, defined as the effective open surface area of the froth cell available for foam formation, measured in the froth cell at the height of the agitation area, defined as the portion or area of the flotation tank in the vertical direction where the slurry is agitated, is at least 15 ^m2 . The foam collected in the second foam collection channel is directed to the first foam collection channel. The froth flotation chamber is characterized in that it also contains a radial thickener containing a thickening side wall and extending from the second froth collection channel to the first froth collection channel.

The flotation line according to the present invention comprises a coarse flotation part with at least two coarse flotation cells connected in series and located in flow communication, and a test flotation part with at least two control flotation cells connected in series and located in flow communication. In the flotation line, the subsequent flotation cell is configured to receive underflow from the previous flotation cell. The flotation line is characterized in that at least one of the flotation cells is a froth flotation cell according to the present invention.

The use of a froth flotation line according to the present invention is for use in the recovery of mineral ore particles containing a valuable mineral.

A froth flotation process for treating mineral ore particles suspended in a slurry according to the present invention includes separating the slurry into an underproduct and an overhead product in a froth flotation chamber. The method is characterized in that the open surface of the foam of the flotation tank is divided into two open subsurfaces of the foam by a radial foam thickener located between the first radial overflow edge of the first radial froth collection trough and the second radial overflow edge of the second radial froth collection trough.

By using the invention described herein, the so-called brittle foam, i. a loosely textured froth layer containing generally larger flotation gas bubbles agglomerated with the mineral ore particles to be recovered to the froth overflow edge and into the froth collection chute. Brittle foam can be easily broken because the agglomerates of gas bubbles and ore particles are less stable and have reduced strength. Such a foam or foam layer cannot easily support the transport of ore particles, and especially larger particles, to the overflow edge of the froth for collection in the trough, resulting in the particles falling back into the pulp or slurry in the flotation cell or tank, and reduced recovery of the required material.

Brittle foam is usually associated with low salinity, ie. agglomerates of gas bubbles and ore particles with a limited number of ore particles containing the desired valuable mineral that were able to attach to the gas bubbles during the flotation process inside the flotation cell or tank. This problem is particularly pronounced in large size flotation cells or large volume and/or large diameter flotation tanks. Although froth collection may be difficult for large flotation cells or tanks, they nevertheless have the advantage of increasing delay and contact between gas and particles.

- 1 040329

Using the present invention, it is possible to thicken the foam and direct it to the foam overflow edges, reduce the foam transport distance (thereby reducing the risk of backfall), and at the same time maintain the same level or even reduce the length of the foam overflow edge.

In other words, handling and guiding the froth layer in the froth chamber or tank can become more efficient and simple.

It is also possible to improve froth recovery and thus the recovery of valuable mineral particles in large flotation cells or brittle froth tanks, especially in the later stages of the flotation line, for example in the coarse and/or control flotation stages of the flotation process.

In addition, with the invention described herein, the area of foam on the surface of the slurry inside the flotation cell or tank can be reduced in a reliable and simple mechanical way. At the same time, the overall length of the froth overflow edge in the froth chamber can be reduced. In this case, reliability should be understood as both structural simplicity and durability. By reducing the froth surface area of the flotation cell by thickening the froth or tapering side structure, instead of adding additional froth collection chutes, the froth cell as a whole can have a simpler structure. The thickener can simultaneously function both as a conduit for directing the collected overflow to other froth collection channels and as a flow connection between two froth collection channels, thereby also eliminating the need to add additional troughs to the flotation cell. It can also allow smaller, narrower, and simpler gutters to be made. Therefore, the use of a thickener can give a greater degree of freedom in designing froth collectors for flotation cells without having to change the volume of the flotation cells.

The amount of valuable material required that can be entrapped in the froth within the pulp can be very low, especially at the lower end of the flotation line. This phenomenon can be particularly pronounced in flotation processes designed to extract valuable material from low grade ores.

In order to collect valuable material containing ore particles from the foam layer into the foam collection chutes, the surface area of the foam must be reduced. By positioning the thickener in a froth cell in a movable manner, the exposed froth surfaces between the various froth overflow edges can be controlled. The thickener can be used to orient or direct upward flowing slurry within the flotation tank closer to the froth overflow edge of the froth chute or froth collection channel, thereby providing or facilitating froth formation very close to the froth overflow edge, which can increase the collection of valuable ore particles.

The thickener can also influence the complete convergence of the flotation gas bubbles and/or agglomerates of gas bubbles and ore particles into the froth layer. For example, if gas bubbles and/or agglomerates of gas bubbles and ore particles are directed towards the center of the flotation tank, then a thickener can be used to increase the area of the froth at or near any desired froth overflow edge.

With the invention described herein, it is possible to increase the recovery of the desired valuable ore particles during flotation. In other words, ore particles containing very small or even minimal amounts of the desired material can be recovered for further processing/treatment. This can be especially advantageous for low quality ores, i.e. ores with a very low content of valuable material at an early stage, such as from poor mineral deposits that may previously have been considered economically too insignificant to justify their use. For example, recovery of copper ore that foams easily can be greatly improved by the invention described herein.

It is possible to achieve high recovery for the entire pulp stream passing through the flotation line. In particular, at the lower end of the flotation line, the recovery of ore particles containing the desired mineral can be increased.

In addition, it is possible to improve the recovery of larger ore particles and the recovery of valuable mineral material in situations where the salinity of the flotation gas bubbles during the flotation process may not be ideal for some reason.

In this specification, the following definitions are used in relation to the invention.

By thickener herein is meant a foam blocker, a foam deflector, or a thickening plate, or a foam thickening device, or any other such structure or side structure, such as a side wall, inclined or vertical, having a thickening effect, i.e. thickening side wall.

Flotation includes phenomena related to the relative buoyancy of objects. Flotation is the process of separating hydrophobic materials from hydrophilic materials by adding a flotation gas such as air or any other suitable gas to the process. Flotation can be done based on natural differences in hydrophobic/hydrophilic properties or based on hydrophobic/hydrophilic differences resulting from the addition of a surfactant.

- 2 040329 or chemical collector. Gas can be added to the feedstock to be floated (slurry or slurry) in several different ways.

Basically, flotation is aimed at extracting a concentrate of ore particles containing the desired mineral. Typically, the required mineral is a valuable mineral. By concentrate in this document refers to the part of the pulp recovered in the top product or in the bottom product removed from the flotation cell. A valuable mineral is any mineral, metal or other material that has a commercial value.

Flotation includes phenomena related to the relative buoyancy of objects. The term flotation includes all flotation methods. The flotation may be, for example, froth flotation, dissolved air flotation (DAF) or induced gas flotation.

By flotation line, as used herein, is meant an assembly containing a number of flotation blocks or flotation cells that are fluidly connected to each other to allow slurry to flow between the flotation cells, either by gravity or by pumping, to form a flotation line. In a flotation line, several flotation cells are flow-through connected to each other so that the bottoms product of each previous flotation cell is sent to the next or subsequent flotation cell as feed, up to the last flotation cell of the flotation line, from which the bottoms product is sent outside the line in the form of streams. tailings or waste.

The flotation line is designed to process mineral ore particles suspended in the pulp by the flotation method. Thus, ore particles containing a valuable metal or mineral, or any desired mineral, are recovered from the ore particles suspended in the pulp. For example, the desired mineral may be a valuable metal contained in the ore particles. In other cases, the desired mineral may also be a non-valuable part of the pulp, such as silicate in iron backflotation.

The slurry is fed through the inlet to the first flotation cell of the flotation line to start the flotation process. The flotation line may be part of a larger flotation plant containing one or more flotation lines. Therefore, a number of different pre-treatment and post-treatment devices may be associated with the components of the flotation line, as will be known to those skilled in the art.

Under the flotation cell (or block) in this document refers to the part of the flotation line containing one or more flotation tanks. The flotation tank is typically cylindrical in shape, this shape being defined by the outer wall or outer walls. Flotation cells usually have a circular cross section. The flotation tanks may have a polygonal, eg rectangular, square, triangular, hexagonal or pentagonal, or other radially symmetrical cross section. The number of flotation cells may vary depending on the particular flotation line and/or ore type and/or grade processing operation, as known to those skilled in the art.

The flotation cell may be a froth cell, such as a mechanically agitated or reservoir cell, a column flotation cell, a Jameson cell, or a twin flotation cell. In a dual flotation cell, the cell contains at least two separate tanks, a first mechanically agitated pressure tank with an impeller and a flotation gas inlet, and a second tank with a tailings outlet and an overflow froth outlet configured to produce an agitated slurry from the first tank. The flotation cell may also be a fluidized bed flotation cell in which bubbles of air or other flotation gas that are dispersed by the fluidization system percolate through the difficult-to-set zone and attach to the hydrophobic component, changing its density and making it buoyant enough to float and be restored. In a fluidized bed in a flotation cell, axial mixing is not required. The flotation cell may also be of the type in which the mechanical flotation cell (ie, a flotation cell containing a mechanical agitator or impeller) contains a microbubble generator for generating microbubbles in the slurry within the flotation cell. The microbubble size distribution is smaller than conventional flotation gas bubbles introduced by an impeller or other gas supply system, which typically fall in the 0.8-2mm size range. The size range of microbubbles can be 1-1.2 mm. The microbubbles can be introduced by a microbubble generator containing a pulp recirculation system or a direct spray system.

Depending on the type, the flotation cell may contain a pulp agitator to keep it in suspension. Under the mixer in this document refers to any suitable means for mixing the pulp in the flotation cell. The mixer may be a mechanical mixer. The mechanical agitator may comprise a rotor-stator with a motor and a drive shaft, with the rotor-stator structure located at the bottom of the flotation cell. The chamber may have auxiliary agitators located higher in the vertical

- 3 040329 in the direction of the chamber to guarantee a sufficiently strong and continuous upward flow of pulp. The mixer may comprise, for example, a Wemco pump-type agitator that simultaneously acts as a source of gas supplied to the tank, drawing air from the surface of the slurry in the tank under the action of the rotational force of the pump and supplying this air to the slurry in the tank, or any similar device in self-priming or self-ventilated flotation cell or flotation tank.

Under the top product in this document means that part of the pulp, which is collected in the overflow trough of the flotation cell and, thus, leaves the flotation cell. The top product may contain foam, foam and pulp or, in some cases, all or most of the pulp. In some embodiments, the overhead product may be a product stream containing valuable material particles collected from the slurry. In other embodiments, the top product may be a waste stream. This is the case when the flotation process is used with reverse flotation.

Under the bottom product in this document refers to the fraction or part of the pulp, which does not float to the surface of the pulp during flotation. In some embodiments, the underflow may be a waste stream exiting the flotation cell through an outlet, which is typically located at the bottom of the flotation cell. Eventually, bottoms from the last flotation cell of a flotation line or flotation unit may leave the entire apparatus as a tailings stream or final waste.

In some embodiments, the bottom stream may be a received stream containing valuable mineral particles. This is the case when the flotation line and/or process is used in reverse flotation. For example, in iron (Fe) reverse flotation, silicates are floated and collected from the froth bed while the desired concentrate (Fe) is collected from the underflow or tailings stream. To achieve a silicate content of less than 1.5% by weight in the Fe concentrate, the last flotation cells or flotation stages of such a reverse flotation process can be difficult to optimally control due to low froth, brittle froth and/or low froth salinity. With the invention described herein, this problem can be solved.

By downstream direction in this document is meant the direction coinciding with the flow of the pulp (forward flow, indicated by arrows in the drawings), and by the direction upstream in this document is meant the direction opposite to the flow of the pulp or directed against it.

Slurry surface in this document means the effective open surface of the flotation cell or tank available for foam formation, measured in the flotation tank at the height of the mixing area, i.e. portions or areas of the flotation tank in the vertical direction where the slurry is agitated or otherwise caused to mix ore particles suspended in the slurry with bubbles of flotation gas. Depending on the type of flotation cell and/or flotation tank, the area of the mixing area may vary.

For example, in a flotation cell or flotation tank containing a rotor, the area of the mixing region is defined as the average cross-sectional area of the tank at the height of the rotor. For example, in a flotation cell in which gas is supplied to the slurry in a pre-treatment tank before the slurry is fed into the flotation tank, i. e. into a twin flotation tank, the mixing area is the cross-sectional area at the height of the pulp inlet. For example, in a flotation cell in which gas is supplied through bubblers (ie, a flotation cell column), the area of the mixing region is defined as the cross-sectional area of the reservoir at the height of the bubbler.

In one embodiment of the froth flotation chamber, the radial froth collection chute comprises a first radial froth overflow edge and a second radial froth overflow edge located opposite the first radial froth overflow edge.

In one embodiment of the froth flotation cell, at least one radial froth overflow edge is located so that it faces the thickening side wall of the radial thickener.

In one embodiment of the froth flotation chamber, the radial froth collection chute includes a side wall, which is a thickening side wall.

In one embodiment of the froth flotation chamber, the radial thickener comprises a thickening side wall and a froth collecting lip located opposite the thickening side wall, the froth collecting lip located so that it faces the thickening side wall of the radial froth collecting trough.

It is also envisaged that both the radial froth collection chute and the radial thickener have the same structure and shape in order to simplify the structure of the froth flotation chamber, and to make its manufacture and construction simpler and easier. Therefore, it can be foreseen that both the chute and thickening structures can act as collecting structures and/or as

- 4 040329 thickening structures. This is made possible by the arrangement of their side walls and edges. The thickening structure (thickening wall or side wall) extends high enough above the froth layer of the flotation cell to prevent froth overflow, while the lip of the trough or froth collecting lip is positioned to allow the overhead pulp and/or froth to move into the interior of the structure, to which she belongs. As a result, it is possible to reduce the open surface area of the froth relative to the length of the lip, thereby improving the recovery efficiency in the froth flotation chamber.

When the radial foam collection chute comprises a radial foam overflow edge and the radial thickener comprises a thickening side wall, or the radial foam collection chute comprises first and second overflow lips and the radial thickener comprises two thickening side walls, the exposed foam surfaces formed between the foam overflow edges and the thickening sidewalls are identical and the exposed foam surfaces are limited by these structures. In addition, by arranging at least some of the radial froth collecting troughs and the radial thickeners to include a thickening side wall or other thickening structure, the length of the edge of the froth flotation chamber can be effectively reduced while improving or maintaining extraction of particles of valuable mineral ore.

In one embodiment of the froth flotation chamber, the radial thickener comprises a first thickening side wall and a second thickening side wall.

In a design in which the radial foam collection trough comprises first and second radial foam overflow projections and the radial thickener comprises a first thickening side wall and a second thickening side wall, the radial foam collection troughs can be designed as lightweight structures that have minimal impact. on the volume of the froth cell or tank, or on the exposed surfaces of the froth of the cell or froth tank.

In one embodiment, the froth chamber comprises radial froth collection chutes and/or radial thickeners arranged such that the exposed froth surfaces formed between each radial froth collection trough and/or radial thickener are of equal area.

In one embodiment of the froth flotation cell, the first froth collection channel includes a first froth overflow edge facing the center of the tank.

In yet another embodiment of the froth flotation chamber, the first froth overflow edge is located at the top of the vertical side wall of the first froth collection channel.

In other words, the first foam collection channel may be positioned to function as a foam collection chute. By arranging a vertical side wall for the foam collecting channel, it is possible to ensure that the foam is efficiently guided into the foam collecting channel through the foam overflow edge of this channel. The vertical side wall can allow the froth to rise unobstructed along with the upward flow of the slurry in the flotation tank next to the froth collection channel until the froth reaches the froth overflow edge, thereby ensuring that as much of the valuable material containing ore particles as possible , is removed with foam overflow into the foam collection channel.

In yet another embodiment of the froth flotation cell, the first froth collection channel comprises a side structure facing the center of the tank, the side structure being designed to push froth away from the first froth collection channel. This makes it possible to reduce the length of the overflow lip and at the same time reduce the surface area of the foam.

In another embodiment of the froth flotation chamber, the side structure has an angle of inclination of 20-80° relative to the vertical of the tank.

This prevents the flotation gas bubbles from colliding and coalescing, while the foam area can be effectively reduced. This is particularly advantageous when the first foam collection channel has on its outer surface a lateral structure designed to push back the foam.

In other words, the first foam collection channel may be configured to act as a thickener, pushing foam on the exposed foam surfaces towards other foam overflow edges of the foam collection channels or troughs. To ensure sufficient thickening, the side structure may have an angle of inclination of 20-40° or even 20-80°, preferably approximately 30° relative to the vertical of the flotation tank.

In one embodiment of the froth flotation cell, the second froth collection channel also includes a second overflow lip facing the periphery of the tank.

In another embodiment of the froth flotation chamber, the second overflow edge is located at the top of the vertical side wall of the second froth collection channel.

In other words, the second foam collection channel may be configured to collect foam from exposed foam surfaces near both sides thereof. By arranging the vertical side wall for the foam collecting channel, it is possible to ensure that the foam is efficiently guided into the foam channel.

- 5 040329 foam collection through the overflow edge of the foam channel. This robust design is advantageous because the two overflow edges require only one collection pipe. In addition, brittle froth can be collected more efficiently and removed from the froth cell as an overhead product.

In yet another embodiment of the froth cell, the second froth collection channel also includes a side structure facing the periphery of the tank, the side structure being designed to push froth away from the second froth collection channel.

In another embodiment of the froth flotation chamber, the side structure has an angle of inclination of 20-80° relative to the vertical of the tank.

In other words, the second froth collecting passage may be configured to act as a thickener, thickening the froth on the exposed surfaces of the froth towards the other overflow edges of the froth collecting channels or troughs and towards the periphery of the tank. To ensure sufficient thickening, the side structure may have an angle of inclination of 20-40° or even 20-80°, preferably approximately 30° relative to the vertical of the flotation tank.

In one embodiment of the froth flotation chamber, the radial froth collection chute is configured to collect froth and direct the collected froth into the first froth collection channel.

In one embodiment of the froth flotation cell, the radial thickener is located in fluid communication with the first froth collection channel and the second froth collection channel, and is further configured to direct froth from the second froth collection channel to the first froth collection channel.

In this type of design, the material streams in the overhead can be efficiently collected and a thickener can be installed to direct and transport material from the second foam collection channel to the first foam collection channel. However, the radial troughs can be smaller (narrower and/or shallower) and therefore be light and simple in design.

In one embodiment of the froth cell, the radial froth collection chute is configured to be shaped to prevent flotation gas bubbles from colliding under the radial froth collection chute and pushing froth away from the radial froth collection chute.

In one embodiment of the froth cell, the radial froth collection chute is shaped to allow froth flow to flow into the radial froth collection chute.

In one embodiment of the froth cell, the cross section of the radial froth collection trough in the radial direction of the tank is substantially V-shaped, comprising a top directed towards the bottom of the tank, a first sloping side wall, and a second sloping side wall extending from the top so that between the first and second inclined side walls an angle α is formed at the top, and the first radial edge for foam overflow located on top of the first inclined side wall, and the second radial edge for foam overflow located on top of the second inclined side wall.

Thus, the volume of the froth flotation tank is minimally affected by the addition of one or more of these radial froth collection chutes, and therefore the flotation process conditions can be maintained despite the added structure.

In another embodiment of the froth flotation chamber, the radial froth collection chute comprises a vertically extending first side wall and a vertically extending second side wall opposite the first side wall, a first radial froth overflow edge located on top of the first side, and a second radial froth overflow edge , located on top of the second side, and an inclined bottom, essentially V-shaped with the apex directed towards the bottom of the tank and having an angle α at the apex, wherein the first and second side walls and the bottom form a channel for directing foam into the first channel for collecting foam .

In another embodiment of the froth flotation chamber, the length of the first and second side walls is at least 50 mm.

Due to the implementation of a radial chute for collecting foam of a certain shape, i.e. either a simpler V-shape with sloping sidewalls, or a shape with vertical sidewalls and a V-bottom, flotation gas bubbles can be prevented from colliding with each other under the radial froth collecting trough, which can lead to the breakdown of agglomerates of gas bubbles and particles ore and falling ore particles back to the bottom of the tank, thereby adversely affecting the efficiency of the flotation process; or prevent froth from moving from under the radial froth collection chute back to the froth overflow edges.

In addition, by means of the vertical side walls, it is possible to efficiently guide the foam into the radial foam collection chute through the radial froth overflow edges of the chute. In addition, by having a substantially V-shaped bottom, a sufficient width of the radial froth collection chute can be provided, thereby effectively guiding and transporting the collected froth and overhead within the channel defined by the side walls and the bottom.

In one embodiment of the froth flotation cell, the angle α at the top of the V-shaped bottom is 20-160°, preferably 20-80°.

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In one embodiment of the froth cell, the radial thickener is shaped to direct the froth towards the radial overflow edges of the radial froth collection troughs adjacent to the radial thickener.

In one embodiment of the froth cell, the cross section of the radial thickener in the radial direction of the tank has a functional V-shape, containing the top directed towards the bottom of the tank, and an inclined first side and an inclined second side extending from the top, so that between the first and second sides an angle β is formed; wherein the first side faces the first radial foam overflow edge of the adjacent first radial foam collection chute and the second side faces the second radial foam overflow edge of the adjacent second radial foam collection chute.

In another embodiment of the froth flotation chamber, the angle β is 20-80°.

By forming the radial thickener in the above manner, the foam load on each side of the radial thickener can be easily and simply balanced and controlled, and the direction and/or accumulation of foam, especially brittle foam, can be effectively influenced on both sides of the radial thickener.

By functional V-shape is meant herein that the radial thickener may have a cross-section that is substantially V-shaped. However, the outer edges of the radial thickener may not be completely flat or straight. Due to, for example, manufacturing factors, the shape may be more organic, the edges may be wavy, bumpy or otherwise uneven. This, however, does not affect the functionality of the radial thickener since its basic shape, as described herein, is a V-shape with two distinct sloped sides, a top and an open top opposite the top.

The functional V-shape and parts thereof, as described herein, are used herein to describe the basic shape of the radial thickener. A functional V shape can also be understood as an isosceles triangle standing on top and having a certain angle at the top.

Foam load as used herein refers to the amount of foam on an exposed surface over any given period of time.

This shape or design allows the radial thickener to be reliably used to separate, direct and balance the foam and slurry into two open foam areas or foam surfaces on either side of the radial thickener.

In one embodiment of the froth cell, the surface area of the radial thickener is greater than the surface area of the radial froth collection chute measured at the height of the froth surface. Preferably, the ratio of the surface area of the radial thickener to the surface area of the radial foam collection chute is at least 2, more preferably at least 3.

Due to the design of the radial thickener with such a surface area, which is the area formed between the sides of the radial thickener and the first and second channels for collecting foam, measured at the height of the surface of the foam (in relation to the bottom of the flotation tank) - more than that of a radial trough for collecting foam, reducing the effect that the radial thickener has on the exposed surface of the foam, may become more pronounced.

In one embodiment of the froth chamber, between the froth collecting channels and the radial froth collecting chutes, and within the second froth collecting trough, the reservoir comprises exposed froth surfaces.

In yet another embodiment of the froth cell, the exposed froth surface between any two radial froth collecting troughs may be divided into two open froth subsurfaces by a radial thickener, with one exposed froth surface located on the side of the first radial froth overflow edge of the first radial froth collecting trough. collecting foam, and one open subsurface of the foam is located on the side of the second radial edge for foam overflow of the second channel for collecting foam; so that the two exposed foam subsurfaces are completely separated by the radial thickener.

In one embodiment of the froth cell, the radial thickener is shaped to balance the froth load between the open froth surface on the first side of the functional V-shape and the open froth surface on the second side of the functional V-shape.

In one embodiment of the froth cell, the exposed froth surface area may be varied such that the ratio between the exposed froth subsurfaces between the two radial froth collection channels and the exposed froth surface within the first overflow edge of the second froth collection channel is changed.

In one embodiment of the froth cell, the ratio between the two open

- 7 040329 foam subsurfaces separated by a radial thickener can be changed by changing the vertical position of the radial thickener in relation to the height, measured from the bottom of the tank, of the radial edge for foam overflow near the radial thickener.

The relationship between said two open foam subsurfaces can be changed in such a way that it does not affect the balance of said two open foam subsurfaces, for example when they are already equalized. By moving only the radial thickener, a simple design can be maintained. If the radial foam collection chute or the foam collection channels were to move, the control of this movement would be extremely precise and precise, since the height of the foam layer would be affected. If the foam overflow edge becomes sloping or deviates from the horizontal, then there will be problems with collecting foam in the gutters. Obviously, the radial thickener must also be placed carefully, but even if the radial thickener is slightly off-horizontal, the height of the foam layer will not be as adversely affected.

The relative position of the lower part of the radial thickener, i.e. the top of the functional V-shape can affect the formation of foam, especially the amount of air or other flotation gas directed into the foam bed and thus the volume of the foam. In this way, the various exposed foam surfaces and subsurfaces can be balanced and the overflow of particles containing valuable material can be increased. In addition, thickening and/or guiding foam, especially brittle foam, can be more efficient and easier. In addition, by making the radial thickener movable, instead of moving the lip or lip to overflow the foam, the overall structure can become more reliable and easier to handle. The movement of the radial thickener is not as critical to the control of the flotation process as the movement of the froth overflow edge.

In one embodiment of the froth flotation cell, the gas source is located in the tank.

By locating the gas source directly in the flotation tank, no additional gasification tanks or systems are required within the flotation system, simplifying the overall design and simplifying operation and maintenance.

In one embodiment of the froth flotation chamber, the tank contains a mixing device.

In one embodiment of the froth flotation chamber, the mixing device contains a source of gas.

In one embodiment of the froth chamber, the pulp area is at least 40 m ² measured in the mixing area.

In one embodiment, the froth flotation cell has a volume of at least 150 m ² , or at least 250 m ² , or at least 400 m ² .

In one embodiment of the froth cell, the radial froth collection chute is configured to be supported by a second froth collection channel.

Thus, the radial foam collecting passage can be supported at both ends, facilitating the construction of the passage, which occupies a reduced spatial volume within the chamber. In addition, this allows the height of the radial froth collection channel to be reduced while maintaining the structural strength required for reliable operation of the froth cell.

In one embodiment, the froth flotation chamber comprises an equal number of radial froth collection channels and radial thickeners, for example four of each, arranged alternately around a circumference surrounding the second froth collection channel. The radial foam collection channels may be configured to be supported by a second foam collection channel.

As a result, the exposed foam surfaces on the two sides of each radial foam collection chute and/or radial thickener are automatically balanced.

In one embodiment of the froth cell, the radial froth collection chute comprises a straight radial froth overflow edge or a zigzag radial froth overflow edge.

Due to the fact that the overflow edge has a zigzag or wavy shape, the functional length of the gutter can be increased, while the physical length of the edge remains the same.

In one embodiment of the froth flotation cell, the radial froth collection chute includes a straight lip for froth overflow.

The straight shape of the overflow edge can be used to protect the edge from dirt and impurities.

In one embodiment of the froth flotation line, the control flotation portion comprises at least one froth flotation chamber.

In one embodiment of the froth flotation line, the coarse flotation portion comprises at least one froth flotation chamber. Large flotation cells improve froth flotation, especially for low copper grade ore. For this purpose, in the part of coarse flotation, it is preferable to use a large chamber. In particular, the design of the thickener according to the present invention allows the size of the froth flotation cell to be increased while improving mineral recovery. To this end, the froth flotation chamber may have a volume of at least 400 m ³ .

In one embodiment, the froth flotation line comprises at least two coarse or control flotation cells and/or at least two additional froth flotation cells made in accordance with the invention and designed to process the pulp before it can be process in a froth flotation cell according to the invention. Thus, the last flotation cell of the froth flotation line is a froth flotation cell according to the invention.

Under rough flotation, part of the rough flotation of the flotation line, rough flotation stage and/or rough flotation chambers in this document is meant the flotation stage, which gives a coarser (rougher) concentrate. The goal is to remove the maximum amount of valuable mineral with the largest possible particle size. For rougher flotation, full release is not required, only sufficient release to isolate enough gangue from the valuable mineral to obtain a high recovery. The main goal of the coarse flotation stage is to recover as many valuable minerals as possible with less emphasis on the quality of the concentrate produced.

Coarse flotation is often followed by a control flotation, which is used for coarse tailings. By control flotation, part of the control flotation of a flotation line, a control flotation stage and/or a control flotation cell is meant a flotation stage, the purpose of which is to recover any valuable mineral material that was not recovered in the initial rougher flotation stage. This can be achieved by changing the flotation conditions to be harsher than the original rough treatment, or, in some embodiments of the invention, by introducing microbubbles into the pulp. The concentrate from the cell or control flotation stage can be returned to the rough feed for reflotation or sent to the regrinding stage and then to the control cleaner flotation line.

Any type of flotation cell or flotation tank can be used as the coarse or control flotation cell, and this type can be selected according to the specific needs established by the type of material to be processed in the flotation line. It is possible that the froth cell or cells according to the invention can be incorporated into existing flotation lines as upgraded flotation line assemblies in order to increase the variability of use as well as the collection efficiency of the desired valuable material. Typically, at the downstream end of the flotation line, the amount of ore particles containing valuable material is small, since most of the floating material is captured and collected already in the upstream part of the flotation line. By adding one or more froth cells according to the invention to the downstream end of such a flotation line, even the small amount still remaining in the slurry can be efficiently collected by the froth cells described herein, and, thus, the efficiency of the flotation line as a whole is improved. This can be especially useful in operations where the foam or foam layer is brittle and/or mineralization is low.

In one embodiment of a froth flotation line according to the invention, the flotation line is configured to recover mineral ore particles containing a desired mineral from a low grade ore.

In yet another embodiment of the froth flotation line according to the invention, the flotation line is configured to recover Cu containing mineral ore particles from low copper ore.

For example, when extracting copper from low-grade ores obtained from poor mineral ore deposits, the amount of copper can be as low as 0.1% by weight of the raw material, i.e. pulp feed to the flotation line. A froth flotation line according to the invention can be very practical for recovering copper, since copper is a so-called easily floatable mineral. By using the flotation line according to the present invention, it is possible to effectively increase the recovery of such small amounts of a valuable mineral such as copper, and even exploit poor deposits at minimal cost. As known rich deposits become more and more depleted, there is a need to process even less favorable deposits, which may previously have been left undeveloped due to the lack of suitable technology and processes to extract valuable material in very small quantities in the ore.

In one embodiment of the froth flotation process, the two exposed froth subsurfaces are completely separated by a radial thickener.

In one embodiment of the froth flotation process, the open surface area of the froth is changed such that the ratio between the area of open froth subsurfaces between the two radial froth collection channels and the open surface area of the froth within the first overflow edge of the second froth collection channel is changed.

In one embodiment of the froth flotation process, the ratio between the areas of the two exposed froth subsurfaces separated by the radial thickener is changed by changing the vertical position of the radial thickener relative to the height of the radial froth overflow edge next to the radial thickener.

- 9 040329

Brief description of the drawings

The accompanying drawings, which are included to provide a further understanding of the present invention and form part of this specification, illustrate embodiments of the invention and, together with the description, help to explain the principles of the invention.

On the drawings:

fig. 1a-c show a schematic cross-section of a froth flotation cell according to an exemplary embodiment of the invention, FIG. 1d is a cross section along line D-D in FIG. 1a of a froth flotation cell according to an exemplary embodiment of the invention, FIG. 1e is a cross section along line E-E in FIG. 1c of a froth flotation cell in accordance with an exemplary embodiment of the invention, FIG. 1f is a cross section along line F-F in FIG. 1a of a froth flotation cell according to an exemplary embodiment of the invention, FIG. 1g is a cross section along line G-G in FIG. 1c of a froth flotation cell in accordance with an exemplary embodiment of the invention, FIG. 1h is a cross-sectional view of another exemplary embodiment of a froth flotation cell according to the invention, FIG. 1i is a cross section along the line I-I in FIG. 1h of a froth flotation cell in accordance with an exemplary embodiment of the invention, FIG. 1j is a cross-sectional view of another exemplary embodiment of a froth flotation cell according to the invention, FIG. 2a-c are schematic radial sections showing details of embodiments of a froth flotation cell according to the invention, FIG. 3a-d are schematic 3D views of exemplary embodiments of a froth flotation cell in accordance with the invention, FIGS. 4 is a schematic illustration of an exemplary embodiment of a froth flotation cell according to the invention, FIG. 5 is a schematic representation of another exemplary embodiment of a camera in accordance with the invention, FIG. 6a-b are a schematic illustration of another exemplary embodiment of a camera according to the invention, FIG. 7a-b illustrate block diagrams of embodiments of a flotation line in accordance with the invention.

Detailed description of the invention

Embodiments of the invention are described in detail below, examples of which are illustrated in the accompanying drawings.

The following description discloses some embodiments in such detail that a person skilled in the art can use the froth cell, line, application and method based on the description. Not all steps of the embodiments are described in detail, as many of the steps will be apparent to those skilled in the art based on this description. The drawings are not shown in proportion, with many components of the froth chamber 10 and froth line 1 omitted for clarity. The direct direction of the flow of pulp 1 is shown in the drawings by arrows.

For simplicity, in the case of repeating components in subsequent illustrative embodiments, the position numbers will be retained.

In FIG. 1a-j and 3a-6b, the tank 11 of the froth flotation chamber 10 receives the pulp flow, i. a pulp stream 100 containing ore particles, water, and flotation chemicals such as chemical collectors and non-collecting flotation chemicals. The chemical collector molecules are attached to surface areas on the ore particles containing the desired mineral to be floated through an adsorption process. The desired mineral acts as an adsorbent and the chemical collector acts as an adsorbate. The chemical collector molecules form a film on the areas of the desired mineral on the surface of the floated ore particle. Typically, the desired mineral is the valuable mineral contained in the ore particle. In reverse flotation, the mineral may be the valueless portion of the pulp thus collected from the concentrate of valuable material. For example, in the reverse flotation of Fe, particles of silicate-containing ore float, while valuable particles of Fe-containing ore are collected from the underflow or tailings.

The chemical collector molecules have a non-polar part and a polar part. The polar parts of the collector molecules are adsorbed on the surface areas of ore particles containing valuable minerals. The non-polar parts are hydrophobic and therefore repel water. The repulsion causes the hydrophobic tails of the collector molecules to stick to the flotation gas bubbles. An example of a flotation gas is atmospheric air introduced, for example, by blowing, compressing or pumping into the froth flotation chamber 10 or into the reservoir 11 of the flotation chamber 10. A sufficient amount of adsorbed collector molecules on sufficiently large surface areas of valuable minerals on an ore particle can cause the ore particle to attach to the flotation gas bubble. This phenomenon can be called mineralization. At low salinity, less than the optimum amount of ore particles attaches to the flotation gas bubbles, resulting in brittle foam and problems in extracting the required ore particles from the foam bed to the froth overflow edge and to the froth collection chute.

Ore particles attach or adhere to gas bubbles to form agglomerates of ore particles and gas bubbles. These agglomerates rise to the surface 113 of the flotation tank 11 in the uppermost part of the tank 11 due to the buoyancy of the gas bubbles, and also due to the continuous upward flow of pulp caused by mechanical agitation and/or feeding of the pulp 100 into the tank 11. The gas bubbles form a layer of foam 3, while foam 3 collected on the pulp surface in chamber 10 and containing agglomerates of gas bubbles and ore particles flows out of chamber 10 as top product 50 through foam overflow edges 121a, 122a-b, 123a-b into foam collection channels 21, 22 or into the radial chute 23 to collect the foam.

Any or all of the foam overflow edges, including the first foam overflow edge 121a of the first foam collection channel 21, the first foam overflow edge 122a of the second foam collection channel 22, the second foam overflow edge 122b of the second foam collection channel 22, the first edge 123a for overflow of the foam of the radial trough 23 for collecting foam, the second edge 123a for overflow of the froth of the radial trough 23 for collecting foam and/or the edge 123a, 123b for overflow of the foam of the radial design can be straight or sinuous, for example zigzag or wavy edges. Although zigzag edges can be used, the length of the edge is preferably reduced by using radial thickeners 31 or radial structures having at least one sidewall instead, configured as a thickener.

The collected pulp overhead 50 may be sent for further processing or collected as a final product, depending on the location in the flotation line 1 in which the product 50 is collected. Further processing may include any necessary process steps to improve product quality, such as regrinding and/or cleaning. The tailings can be made to flow as underflow 1a through the outlet into the subsequent flotation cell and finally exit the process as gangue or final residue.

The slurry 100 is first introduced into a froth flotation chamber 10 in which the slurry 100 is treated by introducing flotation gas into it by means of a gas source 12 (see FIGS. 5, 6b), which may be any conventional gas supply means. For example, gas can be fed into the tank through the agitator 14 (FIGS. 4, 5) or into the tank without agitation through the gas inlets (FIG. 6b), as in the case of a columned flotation cell. Flotation gas may be introduced into tank 11. Before pulp 100 is supplied to flotation tank 11b, flotation gas may be introduced into the pulp in a separate pre-treatment or conditioning tank 11a, as in the case of a dual flotation cell (FIG. 6a).

The slurry can be mechanically agitated by means of the agitator 14, i. e. tank 11 contains a mixing device 14, which can be, for example, a rotary-stator type agitator located in a flotation tank 11 (FIG. 4), or by means of a pump 14, 12 in a so-called self-priming tank, as shown in FIG. 5 (the pump acts as both agitator 14 and gas source 12), or using any other type of mechanical agitation known in the art. One or more auxiliary agitators can also be used, located in the flotation tank 11 in its vertical direction.

In one embodiment of the froth chamber 10, as shown in FIG. 1a-c, 1h, 3a-d and 4, it comprises a reservoir 11 having a center 111 and a periphery 110, as well as a first foam collection channel 21 surrounding the periphery 111 of the reservoir 11 so that an open space is formed inside the first foam collection channel 21. Af foam surface.

The first foam collection channel 21 may comprise a first foam overflow edge 121a facing the center 111 of the reservoir 11, i. the first foam collection channel may function as a foam collection chute (see FIGS. 1a-b and 3a-b). In this case, the first foam collection channel 21 may comprise a vertical side wall 210 also facing the center 111 of the reservoir 11. The side wall 210 ends with a first foam overflow edge 121a, i. the first edge 121a is located at the top of the side wall 210.

Alternatively, the first foam collection channel 21 may comprise a side structure 212 facing the center 111 of the tank 11 (see FIGS. 3c-d). The side structure 212 is configured to push the foam 3 away from the first channel 21 for collecting foam to the center 111 of the tank 11. The side structure 212 is inclined so that relative to the vertical p of the tank 11, the side structure 212 has an angle of inclination of 20-40° or even 20-80° . The angle of inclination may be, for example, 24, 28.5, 30, 35 or 37.5°.

The froth flotation chamber 10 also includes a second froth collection passage 22 located between the center 111 of the tank 11 and the first froth collection passage 21. The second foam collection channel 22 has a first foam overflow edge 122a facing the center 111 of the tank 11.

The froth flotation chamber 10 may also include a central thickener 32 located within the second froth collection channel 22, as shown in FIG. 1a-c and 3a-d. The central thickener 32 may be located at the center 111 of the reservoir 11, for example, axially along the central axis of the reservoir 11. The central thickener 32 may be in the form of a cone or truncated cone, and its narrow end is directed towards the bottom 112 of the reservoir 11. The central thickener 32 can be adjusted to control of the open surface of the foam formed inside the second channel 22 for collecting foam. For this purpose, the vertical position of the central thickener can be changed depending on the height measured from the bottom of the tank, the first edge 122a for overflow of foam of the second channel 22 for collecting foam.

The second foam collection channel 22 may also include a second overflow edge 122b facing the periphery 110 of the reservoir 11. In this case, similar to the first foam collection channel 21, the second foam collection channel 22 may also include a vertical side wall 220 facing the center 111 of the tank 11. The side wall 220 ends with a second foam overflow edge 122b, i. e. the second edge 122b for collecting foam is located on top of the side wall 220.

Alternatively, the second foam collection channel 22 may also include a side structure 222 facing the periphery 110 of the tank 11. The side structure 222 is configured to push the foam 3 away from the second foam collection channel 22 towards the periphery 110 of the tank 11. The side structure 222 is inclined so that relative to the vertical p of the tank 11, the side structure 222 has an angle of inclination of 20-40° or even 20-80°. The angle of inclination may be, for example, 24, 28.5, 30, 35 or 37.5°.

The foam 3 collected in the second foam collection channel 22 is directed to the first foam collection channel 21 . This can be realized, for example, with a separate connecting pipe or pipes or other pipelines (not shown in the drawings).

The froth flotation chamber 10 also includes a radial froth collection chute 23 extending from the first froth collection channel 21 towards the second froth collection channel 22.

The radial foam collecting chute 23 includes at least one radial foam overflow edge 123a. In one embodiment, it may comprise a first radial foam overflow edge 123a and a second radial foam overflow edge 123b opposite the first edge (see FIG. 2a), i. both sides of the radial foam collection chute function as collecting structures to allow the collection of foam and/or pulp overflow into the radial foam collection chute 23. At least one radial foam overflow edge 123a is located facing the thickening side wall 310 of the radial thickener 31, which allows the thickening effect due to the presence of the foam thickener to effectively push and guide the material in the foam layer 3 towards the radial foam collection chute 23. Both the first and second radial foam overflow edges 123a, 123b can be positioned facing the side wall 310, 320 of the radial thickeners 31, between which is located a radial foam collection chute (see, for example, Fig. 3c).

The radial foam collection chute 23 may also include a side wall 230a which is a thickening side wall, i.e. one side of the radial trough 23 does not collect foam, but provides a thickening effect (see Fig. 2b). This thickening side wall is positioned to face the foam collecting edge 302 of the adjacent radial thickener 31 to push and direct the flow of foam and/or pulp towards this collecting structure.

The radial foam collection chute 23 is in fluid communication with the first foam collection channel 21 . In the froth flotation chamber 10, at least one radial trough 23 can be installed to collect the froth. In one embodiment, the froth flotation chamber 10 may comprise four such radial froth collection chutes 23, as shown, for example, in FIG. 1a, 1c, 3a and 3c. In another embodiment, the froth flotation chamber 10 may comprise eight such radial froth collection troughs 23, as shown, for example, in FIG. 1b, 1h, 3b and 3d. The number of radial froth collecting troughs 23 can easily be selected according to the size (tank diameter, tank volume, slurry area Ap) of the froth flotation chamber and/or according to any other actual parameter of the flotation process. The froth collection troughs 23 may be arranged symmetrically with respect to each other and/or the center 111 of the reservoir 11. For example, they may be located substantially 30°, 60 or 90° apart from each other with respect to the central longitudinal axis of the reservoir 11.

The radial foam collection chute 23 may be configured to collect the foam 3 from the surface 113 of the tank 11 and to direct the collected foam 3 into the first foam collection channel 21 . The radial chute 23 for collecting foam is located in fluid communication with the first channel 21 for collecting foam. Any or all of the radial foam collection channels 23 may be located separately from the second foam collection channel 22 (see FIGS. 1a-c and 3a-d) so that they do not have flow communication, at least direct flow communication with the second channel 22 for collecting foam. Any or all of the radial troughs 23 may therefore be shorter than the radial distance between the first foam collection channel 21 and the second foam collection channel 22.

Alternatively or additionally, any or all of the radial froth collection chutes 23

- 12 040329 can be positioned so that they are supported by the second channel 22 for collecting foam (see Fig. 1hj). This can be implemented as a structural connection, such as a direct structural connection 124 between the radial trough 23 and the second channel 22. Therefore, the radial troughs 23 may have a length at least equal to the radial distance between the first channel 21 for collecting foam and the second channel 22 for foam collection. Depending on the length of the radial foam collection troughs 23, any or all of them may be positioned so as to separate the exposed foam surfaces Af into separate subsurfaces, but they may also be positioned so as not to separate the exposed foam surfaces Af into separate subsurfaces. , i.e. they facilitate the direct connection of subsurfaces.

The radial froth collecting chute 23 may have a shape that prevents the flotation gas bubbles from colliding under the radial froth collecting chute 23 and a shape that also prevents the froth 3 from moving away from the radial froth collecting chute 23. In addition, the froth collecting chute 23 can be configured as in such a way that it has a shape which directs the flow of foam 3 into the radial foam collection trough.

This shape is achieved due to the fact that the radial chute 23 has at least one radial foam overflow edge 123a, 123b for collecting the foam.

For example, the chute 23 may have a shape in which its cross-section in the radial direction of the tank 11 is essentially V-shaped (see Fig. 2a), containing the top 123c directed towards the bottom 112 of the tank 11, the first inclined side a wall c and a second inclined side wall d extending from the apex 123 c so that an angle α is formed between the first and second inclined side walls c, d at the apex, and a first radial foam overflow edge 123a located on top of the first inclined side wall c, and a second radial foam overflow edge 123b located on top of the second inclined side wall d.

The radial trough 23 in the radial direction of the tank 11 may also have a functional V-shape cross-section (see FIG. 2a where this alternative shape can be seen inside the radial froth collection trough 23). The functional V-shape has a vertex directed towards the bottom 112 of the tank 11 and an inclined first side wall and an inclined second side wall extending from the apex so that an apex angle α is formed between the first and second sides. Angle α at the top can even be 20-160°. Said at least one foam overflow edge 123a, 123b for collecting foam is formed over the functional V shape. The low profile of the radial foam trough 23, for example with an apex angle α of 120-160°, is an advantage for reducing the space volume that the trough 23 occupies in the tank 11. Said at least one foam overflow edge 123a, 123b may then be formed directly on the edge and/or edges of the functional V-shape or on the top of the side wall extending only a short distance from it. In particular, the invention makes it possible to reduce the length of the overflow edge 123a, 123b while improving the recovery of foam 3.

The side wall 230b, c, configured as a thickening side wall, can be tilted to increase the thickening effect, as shown in FIG. 2b.

Alternatively, the chute 23 may include a vertically extending first side wall 230a and a vertically extending second side wall 230b opposite the first side wall 230a. The first and second side walls 230a, 230b may be at least 5 mm long to ensure that the radial trough 23 extends deep enough into the foam layer 3 on the surface of the tank 11, and the vertical side wall can effectively guide the foam 3 to flow through the radial edges 123a, 123b for foam overflow of the radial trough 23.

The first radial foam overflow edge 123a may be positioned on top of the first side wall 230a, and the second radial foam overflow edge 123b may be positioned on top of the second side wall 230b, i. both ends of the first and second side walls 230a, 230b in their upper parts (parts extending closer to the surface 113 of the tank 11) extend into the radial edges 123a, 123b for foam overflow. The first and second side walls 230a, 230b are connected by their lower parts (parts extending closer to the bottom 112 of the tank 11) by an inclined bottom 230c, essentially V-shaped with the top 123c directed towards the bottom 112 of the tank 11. The first and second side walls 230a, 230b and bottom 230c together form a channel 231 for directing the foam 3 into the first channel 21 for collecting foam. The bottom 230c may include an inclined first sidewall and an inclined second sidewall extending from the top 123c so that a top angle α is formed between the first and second sides. The angle α can be an arbitrarily chosen value between 20° and 80°.

The radial trough 23 may have a substantially rectangular cross-section in the horizontal direction of the tank 11, i. e. the first and second side walls are straight. In one embodiment, such as shown in FIG. 1a-c and 3a-d, the first and second side walls can be inclined in such a way that the radial chute 23 becomes larger or wider closer to the first channel 21 for collecting foam and closer to the second channel 22 for collecting foam, those. channel 231 can expand in the direction of the flow of foam 3 into the first channel 21.

Alternatively or additionally, the height of peak 123c may be substantially aligned with the bottom 112 of tank 11 along the entire length of the radial chute 23. In one embodiment, the height of peak 123c may decrease in length from the second foam collection channel 22 in to the first channel 21 for collecting foam, so that the channel 231 deepens in the direction of the flow of foam 3 to the first channel 21.

By shaping the radial trough 23 in the above manner, a substantially constant transport distance d between the radial thickener and the radial foam overflow edge 123a, 123b of the radial trough 23 can be maintained. 1a-c and 1h) can improve the collection of froth from the corner regions where the radial froth collection chute 23 meets the first froth collection channel 21 or the second froth collection chute 22.

The radial trough 23 has a surface area A _L measured at the height H of the surface of the foam 3 (from the bottom 112), i.e. the area formed between the first and second side walls 230a, 230b, c, d and at least the first foam collection channel 21 from which the radial trough 23 emerges (see FIG. 1d). By using a radial froth collection chute in the froth flotation chamber 10, this surface area corresponds to a reduction in the open area Af of the froth surface.

The froth flotation chamber 10 also includes a radial thickener 31 extending from the second froth collection passage 22 to the first froth collection passage 22.

The radial thickener 31 includes a thickening sidewall 310 (see FIGS. 2a-c). In one embodiment, the radial thickener 31 comprises a thickening sidewall 310, 320 and a foam collecting edge 302 (i.e., the top edge 302 of the sidewall 310a may function as a foam collecting edge 302) opposite the thickening sidewall, with the foam collecting edge 302 the foam collector is located facing the thickening side wall 230a of the radial trough 23. Therefore, the radial thickener 31 of this design can function as a collecting structure where foam and/or slurry from exposed surfaces Af can flow over the foam collecting edge 302. In one embodiment, the foam collecting edge 302 of the radial thickener 31 may be positioned to face the radial foam overflow edge 123a of the radial chute 23 (see FIG. 2c). This type of construction makes it possible to effectively extract particles of valuable mineral ore in the chamber 10. If the radial thickener 31 is configured to function as a collecting structure, then the side wall a can have a vertical part (see Fig. 2b, 2c), which effectively directs the flow pulp and/or foam through the top edge 302 of the side wall a, acting as a foam overflow edge 302 . In other words, on the side of the froth overflow edge 302, the radial thickener may have a shape similar to that of the radial froth collection chute as described above.

In one embodiment, the radial thickener 31 may include a first thickening sidewall 310 and a second thickening sidewall 320, i. e. the radial thickener 31 is configured to function as a conventional thickener.

The radial thickener 31 may be located in flow communication with the first channel 21 for collecting foam and the second channel 22 for collecting foam. In addition, the radial thickener 31 can be configured to direct the foam from the second foam collection channel 21 to the first foam collection channel, so that the transport of the collected foam overflow can be greatly increased in volume and efficiency. The radial thickener 31 may be configured to separate the exposed foam surfaces Af into separate subsurfaces, but it may also be positioned so as not to separate the exposed foam surfaces Af into separate subsurfaces, i. facilitating direct connection between subsurfaces. The use of the radial thickener 31 together with the second froth collection channel 22 makes it possible to significantly simplify and lighten the design of the froth flotation chamber 10. The second foam collection channel 22 allows for a marked improvement in volume and weight to cover the area between the periphery 110 and the center 111.

At least one radial thickener 31 may be installed in the froth flotation chamber 10. In one embodiment, the chamber 10 may contain four such radial thickeners 31. The number of radial thickeners 31 can, similarly to the number of froth collection channels 23, be easily selected according to the size (tank diameter, tank volume, slurry area Ap) of the froth flotation cell and/or according to any other parameter of the flotation process. In one embodiment, chamber 10 comprises an equal number of radial froth collection chutes 23 and radial thickeners 31 arranged in an alternating manner (see FIGS. 1a and 1c). The angular distance between adjacent radial troughs 23 and/or radial foam thickeners 31 may be constant.

The chamber 10 may contain the same number of radial chutes 23 and radial thickeners 31 arranged alternately, i.e. so that when moving in a circle in the area between the first channel 21 and the second channel 22 for collecting foam, behind each radial chute for collecting foam

- 14 040329 follows the radial thickener and vice versa. Any or all of the radial troughs 23 may be configured to be supported by a second foam collection channel 22 as described above (see FIG. 1j).

The radial thickener 31 may be shaped to direct the foam 3 towards the radial edges.

123a, 123b for overflow of the foam of the radial froth collection chutes 23a, 23b next to the radial thickener 31. The shape contributes to preventing the collection of foam 3 by the thickener 31.

This shape may be realized by a radial thickener 31 having sidewalls configured to prevent foam 3 from passing over them. the shape 300 includes a top 301 directed towards the bottom 112 of the tank 11 and an inclined first side wall a, 310 and an inclined second side wall b, 320 extending from the top 301 so that an angle β is formed between the first and second sides a, b. The angle β is 20-80°. The angle β may, for example, be 24, 28.5, 31, 35 or 37.5°. Preferably, the angle β is about 30°. The structure may comprise one or more additional side walls extending from the functional V-shape, for example vertically or obliquely.

The first side 1 faces the first radial foam overflow edge 123a of the adjacent first radial foam collecting chute 23a, and the second side b faces the second radial foam overflow edge 123b of the adjacent second radial foam collecting chute 23b. A radial thickener 31 is located between two radial froth collection chutes 23 (see FIGS. 2a-c).

In one embodiment, the radial chute 23 includes a first froth overflow edge 123a and a second froth overflow edge 123b, and the radial thickener 31 includes a thickening sidewall 310 and a second thickening sidewall 320. In yet another embodiment, the froth flotation cell is configured with the same number such radial foam collection troughs 23 and radial thickeners 31 arranged alternately and symmetrically (at equal distances from each other) along the periphery 110 of the tank 11. Designs of this type provide a light construction of the radial foam collection troughs 23, which occupy only a small space, those. do not significantly reduce the volume of the reservoir 11 or the area of exposed surfaces of the foam.

In addition, the radial froth collecting troughs 23 and/or the radial thickeners 31 within the froth flotation chamber 10 can be arranged such that the exposed froth surfaces Af formed between each radial froth collecting trough and/or the radial thickener have the same surface area.

Similar to the radial froth collection trough 23, the radial thickener 31 may have a substantially rectangular cross-section in the horizontal direction of the tank 11, i. e. the first and second sides a, b are straight. In one embodiment, the first and second sides a, b can be inclined so that the radial thickener 31 becomes larger or wider closer to the first froth collection channel 21 and closer to the second froth collection channel 22, i. e. the channel formed by the functional V-shape can expand in the direction of the flow of the foam 3 into the first channel 21 to collect the foam. The height of the top 301 may be substantially aligned with the bottom 112 of the tank 11 along the length of the radial foam collector 31 . In one embodiment, the height of peak 301 may decrease as it extends from the second froth collection channel 22 to the first froth collection channel 21 so that the channel formed by the functional V-shape deepens in the direction of foam 3 flow towards the first froth collection channel 21. foam collection, i.e. the lower part of the radial thickener 31 may be inclined or sloped towards the first foam collecting passage 21 so that the radial cross section of the radial thickener 31 expands towards the periphery 110 of the tank. Thus, the conveying distance d between the radial thickener 31 and the adjacent radial foam overflow edge 123a can be kept constant over the entire radial length that the radial thickener 31 and the radial foam collection chute 23 extend from the second foam collection channel 22 to the first channel 21 to collect foam.

The radial thickener has a surface area A _C measured at the height H of the foam surface 3 (from the bottom 112), i. e. the area formed between the first and second side walls 310, 320, a, b and the first and second foam collecting channels 21, 22, from which a radial foam collecting trough 23 extends (see FIG. 1d). This surface area corresponds to the reduction in the open surface area Af of the froth caused by the radial thickener 31 in the froth flotation chamber 10 . Preferably, the surface area A _C of the radial thickener 31 is larger than the surface area A _L of the radial froth collection chute 23. In one embodiment, the AC/AL ratio is at least 2. In one embodiment, the A _C /A _L ratio is at least 3.

This type of structure is particularly suitable when the radial foam collection chute 23 comprises a first foam overflow edge 123a and a second foam overflow edge 123b, and the radial thickener 31 comprises a first thickening sidewall 310 and a second thickening sidewall 320. Alternatively or additionally , the above arrangement can be even more advantageous when the froth cell has the same number of such radial troughs

- 15 040329 for collecting foam and radial thickeners 31, located alternately and symmetrically (at equal distances from each other) along the periphery 110 of the tank 11.

The reservoir 11 may include open foam surfaces Af between the foam collecting channels 21, 22 and the radial foam collecting channels 23, as well as within the second foam collecting channel 22. The open surface Af between any two radial foam collecting troughs 23a, 23b can be divided by the radial thickener 31 into two open foam subsurfaces Afa, Afb so that one open foam subsurface Afa is formed on the side of the first radial foam overflow edge 123a of the first radial trough 23a and one open foam subsurface Afb was formed on the side of the second radial foam overflow edge 123b of the second radial foam collecting passage 23b. The two open subsurfaces Afa, Afb of the foam are completely separated by the radial thickener 31 (see Fig. 2).

The exposed foam surfaces Af between the foam collecting channels 21, 22 can be automatically balanced with each other since they are circumferentially spaced at a constant radial distance from the central axis of the tank 11. However, the foam surfaces Af between the foam collecting channels 21, 22 can be unbalanced. with respect to any or all of the foam surfaces A _fc within the second foam collection channel 22 . The exposed foam surfaces A _f between the foam collecting channels 21, 22 can be balanced or positioned to be balanced with respect to the open foam surfaces A _fc in the second foam collecting channel 22 by moving any or all of the radial thickeners 31 vertically up or down . In particular, all of the radial thickeners 31 can be positioned vertically at the same height. Alternatively or additionally, the foam surfaces Af between the foam collecting channels 21, 22 can be balanced or positioned to be balanced with respect to the open foam surfaces Afc within the second foam collecting channel 22 by moving the central thickener 32 vertically upward or down.

In one embodiment, the radial thickener 31 may be shaped to balance the foam load between the open foam subsurface A _fa on the first side a of the functional V-shape 300 and the open foam subsurface Afb on the second side b of the functional V-shape 300.

In one embodiment, the area of the open surface A _f of the foam can be changed so as to change the ratio between the open subsurfaces A _fa , Afb of the foam between the two radial troughs 23a, 23b for collecting foam and the open surface Afb of the foam inside the first overflow edge 122a of the second channel 22 for foam collection.

In one embodiment, the ratio between the two open subsurfaces A _fa , Afb, separated by the radial thickener 31, can be changed by changing the vertical position of the radial thickener 31 relative to the height H, measured from the bottom 112 of the tank 11, the radial edge 123a, 123a for foam overflow near the radial thickener 31.

The angle formed between the radial thickener 31 and the radial froth collection chute 23 may not be too steep to avoid collisions between the gas bubbles, which may cause the bubbles to coalesce. Therefore, the area of exposed surfaces or subsurfaces must be affected not by moving the radial thickener 31 closer to or further from the radial froth collection chute 23, but by changing the vertical position of the radial thickener 31. By moving the radial thickener 31 lower in the vertical direction of the tank 11, the open subsurface foam can be reduced and the foam thickens towards the radial edge 123a, 123b to overflow the foam. By moving the radial thickener 31 higher, the thickening effect is reduced, but at the same time it can also be ensured that the foam 3 does not flow into the radial thickener 31. By moving the radial thickener 31, the difference in height between the top 301 of the radial thickener 31 and the top 123 from the radial chute 23 to foam collection can vary significantly (see Fig. 2).

The radial thickener 31 may be movable by any suitable drive or control device known in the art, driven by, for example, an electric motor or hydraulic or pneumatic transmission equipment.

The froth flotation chamber 10 may have a slurry area Ap of at least 15 m ² measured in the mixing region 140 (see FIGS. 4, 5, 6a-b). In one embodiment, the froth flotation chamber 10 may have a slurry area Ap of at least 40 m ² . The area Ap of the pulp can be understood as the effective surface area of the foam, i.e. the maximum possible area of the tank 11 on which foam can form, measured as the area of the pulp at the height of the mixing area 140, which is in principle available for the formation of the foam layer 3.

The mixing area 140 depends on the type of flotation cell. In the flotation cell 10 containing the rotor 14, the mixing area 140 is defined as the average cross-sectional area of the tank at the height of the rotor (FIG. 4). In the self-priming flotation cell 10 (FIG. 5), the area 140 of the mixing area is defined as the average cross-sectional area of the reservoir 10 at the height of the pump 14, 12. In the flotation cell 10, in which the gas 12

- 16 040329 is carried out in the pre-treatment tank 11a before the pulp is fed into the flotation tank 11b, i.e. in a dual flotation tank (FIG. 6a), the mixing area 140 is the cross-sectional area at the height of the pulp inlet 100. In the flotation tank 10 in which gas 2 is supplied through gas supply bubblers 12a (not shown in detail), i.e. columned flotation cell (FIG. 6b), the area 140 of the mixing region is defined as the cross-sectional area of the reservoir 10 at the height of the bubbler 12a of the gas supply.

Chamber 10 may have a volume of at least 150 m ³ . In one embodiment, chamber 10 may have a volume of at least 250 m ³ . In one embodiment, chamber 10 may have a volume of at least 400 m ³ . Under the volume of the chamber 10 can be understood as the volume of the tank 11, 11b.

The froth flotation cell 10 described above may be part of a froth flotation line 1 (see FIGS. 7a-b). The flotation line 1 is a slurry treatment device 100 for the purpose of separating valuable metal-containing ore particles from ore particles suspended in the slurry in a plurality of fluidly connected chambers 10 and in flotation chambers 15a, 15b, which may be of any known type for specialist in this field of technology.

In accordance with one aspect of the invention, the flotation line 1 comprises a coarse flotation part 1a with at least two coarse flotation cells 15a connected in series and located in flow communication, and a control flotation part 1b with at least two control flotation chambers 15b connected sequentially and arranged in flow communication. The subsequent flotation cell is designed to receive the bottom product 40 from the previous flotation cell. The top product 50 from each flotation cell 15a, 15b is withdrawn from the flotation line 1 for further processing, such as regrinding, cleaning, conditioning or further flotation, in accordance with a process well known in the art.

At least one of the flotation cells in the flotation line 1 may be a froth flotation cell 10 according to the invention. Preferably, said at least one froth flotation chamber 10 is located at the downstream end of the flotation line 1. In one embodiment, the control flotation part 1b comprises at least one froth flotation chamber 10 made in accordance with this invention. Alternatively or additionally, the coarse flotation part 1a of the flotation line 1 may comprise at least one froth flotation chamber 10 .

According to one embodiment, the flotation line 1 may comprise at least two coarse or control flotation chambers 15a, 15b and/or at least two additional froth flotation chambers 10a, 10b for treating the pulp 1 before it is sent to the froth chamber 10 flotation (see Fig. 7b).

A froth flotation line 1 comprising at least one froth flotation cell 10 according to the present invention can be used to recover mineral ore particles containing a valuable mineral, especially, but not necessarily, from low grade ore. More specifically, froth flotation line 1 can be used to recover copper (Cu) containing mineral ore particles from low copper ore. The amount of Cu can be as low as 0.1% by weight of the raw material, i.e. feed 100 to the flotation line.

In a froth flotation process for treating mineral ore particles suspended in pulp, pulp 100 is separated into bottom product 40 and top product 50 in a froth flotation chamber 10 in accordance with the present disclosure. The open surface Af of the foam of the flotation tank 11 is divided into two open subsurfaces Afa, A _fb of the foam by means of a radial thickener 31 located between the first radial overflow edge 123a of the first radial froth collection trough 23a and the second radial overflow edge 123a of the second radial froth collection trough 23 .

In one embodiment, the two open foam subsurfaces A _fa , A _fb are completely separated by the radial thickener 31. According to another embodiment, the open surface area Af of the foam is changed so that the ratio between the open foam subsurfaces A _fa , Afb between the two radial troughs 23a is changed. , 23b for collecting foam and an open subsurface (A _fc ) of foam within the first overflow edge 122a of the second channel 22 for collecting foam. In accordance with one embodiment, the ratio between the two open foam subsurfaces A _fa , Afb separated by the radial thickener 31 is changed by changing the vertical position of the radial thickener 31 relative to the height H of the radial foam overflow edge 123a, 123b next to the radial thickener 31.

For a person skilled in the art it is obvious that with the development of technology the main idea of the invention can be implemented in various ways. Thus, the invention and its embodiments are not limited to the examples described above, instead they may vary within the scope of the claims.

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Claims (43)

CLAIM 1. A froth flotation chamber (10) for processing mineral ore particles suspended in the slurry (100) and for separating the slurry into an underproduct (40) and an overhead product (50), the froth flotation chamber comprising: tank (11) with center (111) and periphery (110), gas source (12) for supplying flotation gas (2) into the pulp with foam formation (3), first channel (21) for collecting foam, surrounding periphery (110) tank (11), so that inside the first channel (21) for collecting foam, an open surface (Af) of foam is formed, the second channel (22) for collecting foam, located between the center (111) of the tank (11) and the first channel (21) for and substantially concentric with the first foam collection channel (21), the second foam collection chute comprising a first foam overflow edge (122a) facing the center (111) of the tank (11) and a first radial chute ( 23) for collecting foam, containing the first radial overflow edge (123a), made with the possibility of overflowing pulp (100) and / or foam (3) into the first radial chute (23a) for collecting foam, and the first radial chute (23a) for collecting foam passes from the first channel (21) for collecting foam towards the second channel (22) for collecting foam and proto directly communicates with the first channel (21) for collecting foam, the second radial chute (23b) for collecting foam, containing the second radial overflow edge (123b) made with the possibility of overflowing pulp (100) and/or foam (3) into the second radial chute (23b) for collecting foam, wherein the second radial chute (23b) for collecting foam extends from the first channel (21) for collecting foam towards the second channel (22) for collecting foam and is in fluid communication with the first channel (21) for collecting foam , wherein the froth cell has a slurry surface area (Ap), defined as the effective open surface area of the froth cell available for foam formation, of at least 15 m ² and measured at the height of the mixing area (140), defined as part or area flotation tank (11) in the vertical direction, where the pulp is mixed, and the foam (3) collected in the second channel (22) for collecting foam is sent to the first channel (21) for collecting foam, characterized in that the froth flotation chamber (10) also contains a radial thickener (31) containing a thickening side wall (310) located so that it passes over the foam (3), ensuring that the foam (3) overflow is prevented, and the radial foam thickener (31) passes from the second channel (22) for collecting foam to the first channel (21) for collecting foam, while the radial foam thickener (31) is located between the first radial overflow edge (123a) of the first radial chute (23a) for collecting foam and the second radial overflow edge (123a) of the second radial trough (23) for collecting foam, while the open surface (Af) of the foam of the flotation tank (11) is divided into two open subsurfaces (Afa, A _fb ) of the foam by the radial thickener (31) of the foam, and these two open the subsurfaces (A _fa , Afb) of the foam are completely separated by the radial foam thickener (31). 2. The chamber (10) according to claim 1, characterized in that the radial chute for collecting foam contains a first radial edge (123a) for overflowing foam and a second radial edge (123b) for overflowing foam, located opposite the first radial edge for overflowing foam. 3. Chamber (10) according to claim 1 or 2, characterized in that at least one radial foam overflow edge (123a, 123b) faces the radial thickening side wall (310) of the radial foam thickener (31). 4. The chamber (10) according to claim 1, characterized in that the radial chute (23) for collecting foam contains a side wall (230a), which is a thickening side wall. 5. The chamber (10) according to claim 4, characterized in that the radial thickener (31) contains a thickening side wall (310, 320) and a foam collecting edge (302) located opposite the thickening side wall, while the foam collecting edge faces the thickening side wall (230a) of the radial trough (23) for collecting foam. 6. Chamber (10) according to any one of claims 1 to 4, characterized in that the radial thickener (31) comprises a first thickening side wall (310) and a second thickening side wall (320). 7. The chamber (10) according to any one of claims 1 to 6, characterized in that it contains radial troughs (23) for collecting foam and/or radial foam thickeners (31) located in such a way that the open surfaces (Af) of the foam formed between each respective radial foam collection troughs and/or radial foam thickeners have the same area. 8. Chamber (10) according to any one of claims 1 to 7, characterized in that the first foam collection channel (21) has a first foam overflow edge (121a) facing the center (111) of the reservoir (11). 9. The chamber (10) according to claim 8, characterized in that the first edge (121a) for overflow of foam is located at the top of the vertical side wall (210) of the first channel (21) for collecting foam. 10. The chamber (10) according to claims 1 to 7, characterized in that the first channel (21) for collecting foam contains side - 18 040329 the first structure (212) facing the center (111) of the tank (11), and the side structure (212) is configured to push the foam (3) away from the first channel (21) to collect the foam. 11. Camera (10) according to claim 10, characterized in that the side structure (212) is inclined at an angle from 20 to 80° relative to the vertical (n) of the tank (11). 12. A chamber (10) according to any one of claims 1 to 11, characterized in that the second foam collection channel (22) also comprises a second overflow edge (122b) facing the periphery (110) of the reservoir (11). 13. The chamber (10) according to claim 12, characterized in that the second overflow edge (122b) is located on top of the vertical side wall (220) of the second channel (22) for collecting foam. 14. The chamber (10) according to any one of claims 1 to 11, characterized in that the second channel (22) for collecting foam also contains a side structure (222) facing the periphery (110) of the tank (11), and the side structure ( 222b) is configured to push the foam (3) away from the second foam collection channel (22). 15. Chamber (10) according to claim 14, characterized in that the side structure (222) is inclined at an angle of 20 to 80° relative to the vertical (n) of the tank (11). 16. Chamber (10) according to any one of claims 1 to 15, characterized in that the radial chute (23) for collecting foam is configured to collect foam (3) and direct the collected foam (3) to the first channel (21) for collecting foam. 17. The chamber (10) according to any one of claims 1 to 16, characterized in that the radial foam thickener (31) is located in fluid communication with the first channel (21) for collecting foam and the second channel (22) for collecting foam and is made with the possibility of directing foam from the second channel (22) for collecting foam to the first channel (21) for collecting foam. 18. Chamber (10) according to any one of claims 1 to 17, characterized in that the radial froth collection chute (23) is shaped to prevent collision of flotation gas bubbles under the radial froth collection chute (23) and to prevent froth from moving away from the radial troughs (23) for collecting foam. 19. Chamber (10) according to any one of claims 1 to 18, characterized in that the radial foam collection chute (23) is shaped to direct the flow of foam (3) into the radial foam collection chute (23). 20. The chamber (10) according to any one of claims 1 to 19, characterized in that the cross section of the radial chute (23) for collecting foam in the radial direction of the tank (11) is essentially V-shaped, containing: top (123c) directed towards the bottom (112) of the tank (11), the first inclined side wall (c) and the second inclined side wall (d) extending from the top (123c) so that between the first and second inclined side walls (c , d) an angle α is formed at the top, and the first radial edge (123a) for foam overflow, located on top of the first inclined side wall (c), and the second radial edge (123b) for foam overflow, located on top of the second inclined side wall (d) . 21. Chamber (10) according to any one of claims 1 to 19, characterized in that the radial chute (23) for collecting foam contains: a vertically extending first side wall (230a) and a vertically extending second side wall (230b) located opposite the first side wall (230a), a first radial edge (123a) for foam overflow located on top of the first side wall (230a), and a second radial edge (123b) for foam overflow, located on top of the second side wall (230b), and essentially a V-shaped sloping bottom (230c) with a top (123c) directed towards the bottom (112) of the tank (11) and having an angle α, moreover, the first and second side walls (230a, 230b) and the bottom (230c) define a channel (231) for directing foam into the first channel (21) for collecting foam. 22. Chamber (10) according to claim 21, characterized in that the length of the first side wall (230a) and the second side wall (230b) is at least 50 mm. 23. Chamber (10) according to any one of claims 19 to 22, characterized in that the angle α is between 20 and 160°, preferably between 20 and 80°. 24. Chamber (10) according to any one of claims 1 to 23, characterized in that the radial thickener (31) is shaped to direct the foam (3) towards the radial overflow edges (123a, 123b) of the radial troughs (23a, 23b) for collecting foam next to the radial foam thickener (31). 25. The chamber (10) according to any one of claims 1 to 24, characterized in that the cross section of the radial foam thickener (31) in the radial direction of the tank (11) has a functional V-shape (300) containing the top (301), directed towards the bottom (112) of the tank (11), and an inclined first side (a) and an inclined second side (b) extending from the top (301) so that an angle β is formed between said first and second sides (a, b), wherein the first side (a) faces the first radial edge (123a) for foam overflow of the adjacent first radial chute (23a) for collecting foam, and - 19 040329 the second side (b) faces the second radial foam overflow edge (123b) of the adjacent second radial foam collecting chute (23b). 26. Chamber (10) according to claim 25, characterized in that the angle β is between 20 and 80°. 27. Chamber (10) according to any one of claims 1 to 26, characterized in that the surface area (AC) of the radial foam thickener (31) is greater than the surface area (AL) of the radial trough (23) for collecting foam, measured at height (H) the surface of the foam (3), preferably the ratio A _C /A _L is at least 2, more preferably at least 3. 28. Chamber (10) according to any one of claims 1 to 27, characterized in that between the channels (21, 22) for collecting foam and the radial troughs (23) for collecting foam, as well as in the second channel (22) for collecting foam the reservoir (11) contains open surfaces (Af) of the foam. 29. The chamber (10) according to claim 28, characterized in that the open surface (Af) of the foam between any two radial troughs (23a, 23b) for collecting foam can be divided into two open subsurfaces (Afa, Afb) of the foam by means of a radial thickener (31) foam: one open foam subsurface (Afa) on the side of the first radial edge (123a) for the overflow of the foam of the first radial trough (23a) for collecting the foam and one open subsurface (Afb) of the foam on the side of the second radial edge (123b) for the overflow foam of the second channel (23b) for collecting foam, so that the two open subsurfaces (Afa, Afb) of the foam are completely separated by the radial thickener (31). 30. Chamber (10) according to claim 28 or 29, characterized in that the radial thickener (31) is shaped to balance the foam load between the open subsurface (Afa) of the foam on the first side (a) of the functional V-shape (300) and an open subsurface (Afb) of foam on the second side (b) of the functional V-shape (300). 31. A chamber (10) according to any one of claims 28-30, characterized in that the open surface area (Af) of the foam can be changed to change the ratio between the areas of open subsurfaces (Afa, Afb) of the foam between the two radial troughs (23a, 23b ) for collecting foam and the open subsurface area (A _fc ) of foam inside the first overflow edge (122a) of the second channel (22) for collecting foam. 32. The chamber (10) according to any one of claims 28-31, characterized in that the ratio between the areas of the two open subsurfaces (A _fa , Afb) of the foam separated by the radial foam thickener (31) can be changed by changing the vertical position of the radial thickener ( 31) foam relative to the height (H) of the radial edge (123a, 123a) for foam overflow next to the radial foam thickener (31), measured from the bottom (112) of the tank (11). 33. A chamber (10) according to any one of claims 1 to 32, characterized in that the gas source (12) is located in the reservoir (11). 34. Chamber (10) according to any one of claims 1 to 33, characterized in that the reservoir (11) contains a mixing device (14). 35. The chamber (10) according to claim 34, characterized in that the mixing device (14) contains a gas source (12). 36. Chamber (10) according to any one of claims 1 to 35, characterized in that the pulp area (Ap) measured in the mixing area (140) is at least 40 m ² . 37. Chamber (10) according to any one of claims 1 to 36, characterized in that its volume is at least 150 m ³ , or at least 250 m ³ , or at least 400 m ³ . 38. A chamber (10) according to any one of claims 1 to 37, characterized in that the radial foam collecting chute (23) is supported by a second foam collecting channel (22). 39. Chamber (10) according to any one of claims 1 to 38, characterized in that it contains the same number of radial chutes (23) for collecting foam and radial foam thickeners (31) arranged alternately around the circumference surrounding the second channel (22) for collecting foam, while the radial troughs (22) for collecting foam are made with the possibility of being supported by a second channel (22) for collecting foam. 40. The chamber (10) according to any one of claims 1 to 39, characterized in that the radial chute (23) for collecting foam contains a straight radial edge (123a, 123b) for overflowing foam or a zigzag radial edge (123a, 123b) for overflowing foam. 41. Chamber (10) according to any one of claims 1 to 39, characterized in that the radial chute (23) for collecting foam has a straight radial edge (123a, 123b) for overflowing foam. 42. Line (1) flotation containing part (1a) rough flotation with at least two chambers (15a) rough flotation connected in series and located in flow communication, and part (1b) control flotation with at least two chambers (15b ) control flotation connected in series and located in flow communication, while in the flotation line (1) any subsequent flotation chamber is configured to receive the bottom product (40) from the previous flotation chamber, characterized in that at least one of the flotation chambers ( 15a, 15b) is a froth flotation chamber (10) according to any one of claims 141. 43. Line (1) according to claim 42, characterized in that the control flotation part (1b) comprises at least one froth flotation chamber (10). -