SU1738366A1 - Flotation machine - Google Patents

Abstract

Usage: in the enrichment of minerals, industrial and wastewater treatment. SUMMARY OF THE INVENTION: The chamber 1 of the machine is divided by partitions 2 into the flotation compartment 3 and two lateral flotation separation compartments 4 in which the deep-well jet aerators consisting of the chambers 5, the discharge piping 7, made in the form of eccentric and hermetically connected cylinders with common upper generatrix and diameters decreasing in the course of the working fluid flow and constant specific cross-sectional area, per each nozzle nozzle 8 which follow in the course of the flux movement. Lines of the pipeline 7 are connected to nozzles 8 by vertical pipes 9 with a length increasing along the flow direction, the specific cross-sectional area of the pipeline 7 is 2.5-6 times larger than the opening area of the nozzle 8 nozzles. fluids coming out of all nozzles 8. Supply of the latter with guide elements 10 in the form of grooves with sides and concave along the flow and flat in cross section of the bottom, divided by dividers 11 and 12 into an even number of channels 13, allows a round jet of liquid emerging from the nozzle-nozzle 8 to be converted into a system of flat jets falling on the gas-liquid interface in the chambers 5 of the aerators. 13 il. (L S XJ 00 00 with about Os V gshg

Description

The invention relates to flotation and can be used in mineral processing, industrial and wastewater treatment in the coal, metallurgical, chemical and other industries.

A known flotation machine, comprising a housing with a bottom, feed supply units and removal of enrichment products, a pressure pipe, an aerator consisting of a round or prismatic chamber, with the top base closed and open from the bottom of the machine and communicated with the air duct installed inside this chamber at an angle to its axis by nozzles-nozzles directed to the sides of the open part, an adjusting pipe with an air duct, which communicates with the atmosphere, and a fender plate, made in the form of a flat ring installed coaxially with the aerator chamber with a gap under its base.

The machine has a small area of aeration, which causes a small size of the chambers of the machine and low productivity. The initial power supply is not subjected to direct aeration under the influence of free-falling jets, which reduces the potential capabilities of the machine for the effective flotation of the thinnest classes.

The flow rate of the circulation load ejected into the aerator chamber through the hole in the fender plate is small and this load contains a small amount of solid. Therefore, the circulation load does not significantly affect the hydrodynamics and the intensification of the flotation process.

Closest to the offer is a flotation machine, which includes a chamber with a bottom, partitions, which divide the chamber into the central flotation compartment and two flotation and separation compartments with false bottoms, slurry pipes for receiving and distributing the original feed, aerators of the flotation and flotation separation compartments, consisting of chambers of aerators in the form of inverted troughs with open bases, gas-liquid level regulators, pressure slurry pipes with nozzles-nozzles, and air ducts uliruemymi gap height and visors, sedatives and adjustable lattice grate form dvuhr dnyh with actuators podelitel with pulsations of peaks, troughs, for selecting the circulation load connected via funnels to the circulation channels arranged between false and

the actual bottoms of the flotation-separation compartments, devices for the selection of the working fluid and enrichment chamber waste, made in the form

funnels with rectangular bases, connected to gutters with a stepped increase in cross-sectional area, high-angle gutters, foam foams, gutters for receiving a froth product, and pulp-release pockets with a slide gate device.

The known machine provides for the device of aerators of various sizes, including up to 6 m. The possibility of installing several aerators in one chamber of the machine without compromising its hydrodynamics; controlled separate deep aeration with freely falling jets in the aerators of the flotation compartment — the initial feed and in the aerators

0 flotation-separation compartments - circulation load transported through the chambers of these aerators in a thin layer at high speed: uniform distribution of the air-pulp mixture over

5 areas of aeration; supplying the foamed feed to a previously prepared and continuously maintained foam layer and the implementation in one machine of the flotation and foam separation processes with effective release of fine classes and granular minerals from the pulp flotation density into the foam product; uniform, depending on the technology requirements, selection of circulation load over the entire length of the flotation cell chambers; selection of a working fluid with a low solid content from the circulation flow.

0 The combination of these qualities provides for the creation of high-performance machines with a capacity of chambers of 12.25 and 40 m3, with a specific productivity 1.5-2 times higher than the highest world achievements.

However, pressure pipelines installed in the chambers of deep-seated aerators for supplying the working fluid to the nozzles-nozzles have a constant cross-sectional area along the entire length. Since nozzles-nozzles on pipelines are placed with a certain constant interval along their length, the speed of the working fluid in the areas between the nozzles along the flow in the pipelines is reduced in proportion to the volume flow rate of the fluid through the front nozzles. Due to the stepwise change in the velocity of the working fluid in each section of the pipeline between the nozzles, the

the pressure of the working fluid in the pipelines and, accordingly, the velocities of the jets of the working fluid exiting through the nozzle-nozzles into the chambers of the deep aerators change accordingly.

The exclusion of the possibility of stabilizing the velocities of the working fluid jets emitted by each nozzle within the optimum (for flat jets 14 m / s) causes a decrease in the ejection coefficient of free-falling jets to the gas-liquid interface and, accordingly, the need to increase the flow rate of the working fluid dispersed air in a flotation machine.

In proportion to the increase in the flow rate of the working fluid, the energy intensity of the flotation process increases, and when water is used as the working fluid, the flotation machine productivity also decreases by the amount of additional flow rate of the working fluid. In addition, when using part of the floated pulp as a working fluid, the use of fixed cross-section pipelines causes a decrease in the reliability of the flotation machine in operation, since a decrease in the flow rate along the length of the discharge pipe can lead to precipitation of solids in the sediment at the end of the pipeline and its subsequent clogging.

In flotation machines built on the principle of aeration of floated pulp by ejecting and dispersing air with free-flowing jets on the gas-liquid interface, slotted nozzles can be used to form free liquid jets of flat shape containing a hollow body and an outflow gap. When feeding pure liquid into these nozzles, they produce stable flat jets that have the shape of a fan and, as they expand, turn into thin films and then disintegrate.

The use of continuous flat jets does not sufficiently ensure uniform distribution of the ejected and dispersible air along the chambers of the aerators. In the area of the entrance of the flat jet to the surface of the aerated pulp, the concentration of dispersed air is excessively high (up to 10 m3 of air per 1 m of the working fluid consumption), and in the interval between the jets is 25% larger than the width of the jet at its entrance to the aerated pulp, air is not ejected. The use of thin films due to their low mass is not effective.

In addition, in the process of flotation and wastewater treatment, in many cases, the use of clean water as a working fluid is not effective, since the volumes of aerated pulp will increase by 1.5–2 times due to the influx of water in the form of a working fluid, which leads to a decrease in performance flotation machines, increasing energy intensity and cost of re-processing.

The use of a portion of floated pulp or chamber products for slotted nozzles as a working fluid is unacceptable due to the inevitable closure of mineral particles, fibrous remnants of shattered wood, etc.

Increasing the exhaust slots to dimensions that exclude their blocking is inefficient, as this will dramatically increase the cost of the working fluid, complicate the distribution of dispersed air over the aeration area, reduce the volume of ejected air per unit volume of the working fluid, which ultimately leads to a decrease in machine productivity and increase the energy intensity of the process.

Closest to the proposed nozzles are nozzles with round holes.

The disadvantages of these nozzles-nozzles L are the ejector and aerating ability of round jets issued by nozzles with round holes, all other conditions being equal, are 4-6 times lower than flat jets, nozzles-nozzles with round small holes (2 , 5-10 mm) can also be clogged up as slot nozzles.

Increasing the diameters of the round outlets to sizes that exclude their clogging is not effective, since it reduces the volume of ejected air per unit volume of the working fluid, reduces the uniformity of the distribution of dispersed air throughout the aeration area and increases energy costs.

The purpose of the invention is to reduce the energy intensity of the flotation process, increase the specific and overall performance of the flotation machine, as well as the reliability of its operation.

The goal is achieved by the fact that a flotation machine, which includes a chamber with a bottom, partitions, divides the chamber into flotation and flotation-separation compartments with false bottoms, slurry pipes for receiving and distributing the initial feed, deep-well jet aerators of flotation and flotation-separating compartments consisting of chambers of aerators in the form of inverted gutters with open

bases, gas-liquid level regulators, horizontally installed pressure pipelines with nozzles in the form of hollow pipes and air ducts, a puller with canopies, guiding peaks with adjustable height and size of the installation gap, dampers-distributors of an air-and-air mixture across the area aeration in the form of double-grate grates with lifting mechanisms for adjusting the gaps between rows of grates, chutes for collecting the circulation load, circulation channels placed between the false and the actual bottoms of the flotation separation compartments communicated with the grooves, devices for collecting the working fluid and devices for collecting chamber waste along the entire length of the machine chamber, consisting of funnels and grooves with a stepwise increasing cross-sectional area along the stream, pecogons, gutter for receiving the froth product and pulp outlet with a sliding device, equipped with nozzles that connect the nozzle-nozzles with pressure pipes that supply the working fluid through the nozzles to the nozzles Adherents of aerators made in the form of eccentrically and hermetically connected cylinders with a decreasing diameter and a constant specific cross-sectional area, a nozzle-nozzle mounted on each front pipe installed along the flow of the working fluid and a cross-sectional area exceeding the cross-sectional area 2.5-6 times, with the pressure pipelines at the upper point having a common cylinder line, and at the base, at the end of each cylinder, upstream of the cylinder are located vertically l connecting nozzles with increasing length along the flow of the working fluid by the amount of decreasing the diameter of the cylinders forming the pressure pipe.

Nozzles intended for supplying the working fluid to one side of each chamber of the flotation cell aerator are made with one on each nozzle a guiding element shaped like a groove with gently diverging flanges at an angle of 15-30 ° to its axis with a concave along flow and a flat cross-section bottom, divided by wedge-shaped dissectors into an even number of equal width channels and adjacent narrowed concave part to the perimeter of the nozzle-nozzle outlet,

the bending of the bottom of the guide element is made not less than before the complete intersection of the projection of the cross section of the nozzle-nozzle outlet to the bend of the bottom, and the continuation of the bottom beyond the bend is performed with a straight line angle of 45-60 ° to the nozzle-nozzle axis fixed in the socket for connecting the nozzles to the pressure pipe and is directed to the bottom of the gap between the base of the wall of the flotation cell (which is also the side of the aerator chamber) and the horizontal bottom of the flotation cell at an angle of 30-45 °.

5 A central wedge-shaped divider is located along the axis of the bottom of the guide element directly behind the outlet nozzle of the nozzle and divides the bottom along the entire length, and the side wedge-shaped dividers are placed beyond the edge of the bottom bend on its straight extension, while the opposite walls of the wedge-shaped dividers, as well as beads of the guiding element and

5 the walls of the wedge-shaped dividers opposite them are located at an angle of 1-2 °, forming expanding channels to the flow of the working fluid, and the wedge-shaped dividers have a height at the end

0 of the straight section of the bottom of the guide element is not less than the magnitude of the quotient obtained from dividing the area of the outlet of the nozzle-nozzle by the total width of the channels formed on the bottom

5 guiding element.

Nozzles-nozzles designed to supply the working fluid to the two sides of the chambers of the aerators of the flotation-separation compartments are made with two

0 guiding elements having the form of grooves with smoothly diverging sides at an angle of 15-30 ° to the axis of the grooves, with concave along the flow and flat in cross section of the heads, divided by wedge-shaped dissectors 5 along the length into an even number of channels equal in width and adjacent constricted curved parts of the bottoms to each other at an angle of 180 ° and jointly to the end of the nozzle,

0 division of the nozzle outlet nozzle on the axis parallel to the longitudinal axis of the aerator chamber. Moreover, the bending of the heads of the guide elements is made not less than before the complete intersection of the projection of the half of the cross section of the outlet of the nozzle-nozzle onto the bending of the bottom, and the extension of the bottoms beyond the bend is made linear at an angle of 45-60 ° to the nozzle-nozzle axis, vertically fixed in the nozzle for connecting nozzles to the pressure pipe and are directed to the bottom of the gaps between the bases of the beams in the chambers of the aerator and the horizontally installed bottoms of the flotation-separating compartments of the flotation machine and 5 to the surface of the aerated pulp in the chambers of the aerators at an angle of 30-45 °.

The central wedge-shaped dividers are located on the axes of the bottoms of the guiding elements 10 directly behind the nozzle-nozzle outlet and divide the bottoms along the entire length, and the lateral dividers are placed beyond the edge of the bottoms on their straight lines, with the opposite walls of the wedge-shaped dividers and also the sides of the guiding elements and the walls of wedge-shaped dividers opposite them are located at an angle of 1-2 ° to form widened channels along the flow of the working fluid, the wedge-shaped dividers have m height at the bottom end of the straight portion of rectilinear guide member of at least the private value obtained by dividing the 25 half cross-sectional area of the nozzle outlet, the nozzle on the total width of the channels formed on the bottom of the guide member.

The use of the proposed machine 30 makes it possible to stabilize the speed and pressure of the working fluid along the entire length of the discharge pipe, thereby ensuring the release of the working fluid through all nozzles mounted on the pipeline at the optimum speed, and accordingly increase the coefficient ejection, as well as reduce the consumption of the working fluid and energy consumption for its supply to the chambers of the aerators (this prevents the solid from falling into the sediment and skimming the discharge pipeline when used as a working fluid). those parts of the pulp being floated); convert large-sized round jets into a series of flat 45 fan-like diverging jets, eliminating clogging of nozzles-nozzles with sludge of floated pulp used as working fluid, and ensuring uniform distribution of 50 freely flowing jets of working fluid along the length of aerators chambers, as well as jet delivery on the surface of the aerated pulp at an angle close to optimum.

Figure 1 shows the camera of the machine, 55 is a side view; figure 2 is the same cross section; on fig.Z - pressure pipe, side view with a schematic installation of nozzles-nozzles; figure 4 is the same, front view; Fig. 5 shows the nozzles with one guide element, a front view and a section along the axis of the pressure pipeline; on fig.b - the same, side view; 7 - pressure pipeline, side view; Fig. 8 is the same front view with the installation of nozzles with two guiding elements; Fig. 9 shows a nozzle with two guiding elements, front view; in fig. 10 - the same, side view; figure 11 - machine cross section; in fig. 12 - car camera, side view; in fig. 13 - the same cross section.

Depending on the technical requirements for the enrichment products and the component content of the minerals being floated in the pulp, the machine consists of one or several chambers arranged in a cascade.

Each chamber of the machine consists of a bath 1, divided by walls 2 into the flotation compartment 3 and two lateral flotation-separation compartments 4. On the longitudinal sides of the base of compartment 3 there are jet depth aerators consisting of chambers 5, made in the form of open channels, displaced to the axis of the machine, having in cross-section the shape of an irregular polygon formed by the bases of the walls 2, partitions b and the bottoms of the flotation-separation compartments 4 closed on top.

In addition, each chamber consists of pressure piping 7 supplying the working fluid to the nozzles 8 of the aerators of the flotation compartment 3, designed as eccentrically and hermetically connected cylinders with decreasing diameter and constant specific cross-sectional area a nozzle 8 along the flow of the working fluid and a larger cross-sectional area of the outlet of the nozzle-nozzle 8 2.5-6 times, and the pressure pipes 7 are installed horizontally and vertically The circumferential points have a common cylinder line, and at the base, at the end of each cylinder, vertical pipes 9 are installed vertically along the working fluid flow for connecting nozzles 8, which have increasing length by decreasing the diameter of the cylinders forming the pressure pipe 7. The pressure pipe characteristics and nozzles-nozzles can be expressed as:

Si For Zs Si n n-1 n -2 p- (| -1) Itching - const,

where Si; 82; 83 ..- Si are the cross-sectional areas of the cylinders forming the pressure pipe with number along the flow of the working fluid;

p - the number of nozzles-nozzles installed on the pipeline;

The itch is the specific cross-sectional area of the discharge pipeline, coming from each nozzle-nozzle installed on the pipeline, fed by the working fluid, passing through the cylinders forming the discharge pipeline and having cross-sectional areas of Si; 82; Sa ... Si. For each cylinder and discharge pipe as a whole, Pruritus Itch.

Since the absolute value of 5uf should satisfy the conditions for ensuring the weighting velocity of the working fluid, i.e. precluding solid precipitating and sintering of the pipeline, and the magnitude of the weighting rate, depending on the size and density of the material being floated, can vary considerably, then the corresponding significant fluctuations

 2.5-6, 5s.f.

where Ff is the cross-sectional area of the outlet of the nozzle-nozzle with one guide element.

The discharge pipe 7 through a system of pipes with valves and fittings is connected to a pump that supplies the working fluid.

The machine contains nozzles designed to supply the working fluid to one side of the chamber 5 of the aerator, made in the form of hollow nozzles (nozzles) 8 with one guiding element 10 on each nozzle, having the form of a groove with smoothly diverging sides at an angle a 15- 30 ° to the groove axis, with a bottom concave along the flow and flat in cross section, divided along the length by a central wedge-shaped divider 11 and two or four lateral wedge-shaped dissectors 12 into an even number of widening channels 13 equal in width and extending the narrowed concave part to the perimeter of the nozzle outlet nozzle 8. In this case, the bottom of the guide element 10 is bent not less than until the projection of the nozzle 8 of the nozzle 8 to the bottom bend is completely intersected, and the bottom is extended beyond the bend. linear at an angle of / 5 45-60 ° to the axis of the nozzle-nozzle 8, vertically fixed in the nozzle 9 for connecting nozzles-nozzles

to the pressure pipeline 7 and is directed to the bottom of the slit 14 between the wall 2 and the horizontal bottom of the flotation compartment 3 at an angle y - 30-45 ° to the bottom of the compartment 3 and

respectively, to the surface of the aerated pulp in the chambers of the aerators 5. A central wedge-shaped divider 11 is located along the axis of the bottom of the groove 10 directly behind the outlet of the nozzle-nozzle 8,

and the side dividers 12 are located beyond the bend of the bottom of the groove in its straight extension. At the same time, the opposite walls of the wedge-shaped dividers, as well as the sides of the groove and the opposite walls of the dividers are located at an angle r of 1-2 °, forming expanding channels along the flow of the working fluid.

Nozzles with one guide

the element is connected to a pressure pipe consisting of eight cylinders of decreasing diameter, i.e. designed to install eight nozzles. The machine consists of ducts 15, having a slot in the form of a narrow slot along its entire length, connected through a duct system with a blower, regulators 16 of the gas-liquid level in the chambers of the aerators 5, made in the form

sealed box structures installed on the end wall of the machine chamber and communicated through the outlet tube to the atmosphere. Along the sides of the chambers of the aerators 5, there are slurry tubes 17c with nozzles 18 for connecting the cells of the photomachine to the sources of the initial power supply. The pulp conductors 17 communicate through the slots 19 with the aerator chambers, and the cameras 5 through the slots 14 communicate with the base

flotation compartment along its entire length. Aerator chambers 5 are also communicated via slots 20 to gas-liquid level 16 regulators in chambers 5 of aerators. The upper edges of the slots 20 in the end walls at the base of the bath, 1 are located above the bases of the walls 2, i.e. the upper edges of the slits 14, and the upper edges of the slits 14 above the upper edges of the slits 19, bounded by partitions 6.

In the upper part of the compartment 3, the pulpodel 21 with visors is installed along its axis, and on the outer side of the walls 2 forming the compartment 3, there are installed peaks 22 with adjustable height and gaps 23 between the walls 2 and the visors 22.

Under the base of the gaps 23 are installed fairings 24, having a height equal to the maximum size of the gaps 23 at their base. Gutters 25 are installed along the sides of the bath 1 for collecting circulation load in the non-aeration zones and communicating with circulation channels 26 formed between the bottoms of the bath 1 in the compartments 4 and false bottoms 27 installed with gaps above the real bottoms. Circulation channels 26 communicate through slots 28 with the bases of the chambers of aerators 29 of flotation-separation compartments A, installed with gaps above the bottoms of bath 1 and false bottoms 27 forming outlet slots 30 of the chambers 29 of the aerators along their entire length.

In the upper corners of the triangular prisms of the chambers of the aerators 29, pressure pipelines 31 are placed, supplying the working fluid to the nozzles-nozzles 32 of the aerators of flotation-separation compartments 4, as well as pressure pipes 7, made in the form of eccentric and hermetically connected cylinders with decreasing diameter and a constant specific cross-sectional area, a nozzle-nozzle mounted on each front pipe installed along the flow of the working fluid and exceeding an outlet cross-sectional area and nozzle nozzles 32 2.5-6 times.

Pressure pipelines 31 are also installed horizontally, at the upper point of the circumference they have a common cylinder forming, and at the base, at the end of each cylinder, in the course of the working fluid flow, pipes 33 are installed vertically on the pipeline to connect nozzle nozzles 32, having increasing length by reducing the diameter of the cylinders, forming a pressure pipe 31.

The dependence of the characteristics of the discharge pipe and nozzles-nozzles can be expressed as follows: Sci SC2 h SC3 Sci

n n -1 n -2 n - (I -1)

 Sy.c - const,

 2.5-6,

oc.c

where is sci; Sc2; SC3 ... SCi are the cross-sectional areas of the cylinders forming the discharge pipe of the flotation-separation compartments 4 with the order numbers along the flow of the working fluid;

n is the number of nozzles mounted on the pipeline;

Sy.c is the specific cross-sectional area of the pressure pipeline 31, which comes from to each nozzle-nozzle 32 installed on the pipeline, satisfying the conditions for ensuring

the weighting velocity of the working fluid (pulp);

Sc.c is the cross-sectional area of the outlet of the nozzle-nozzle 32.

Since the nozzles-nozzles 32 are designed to supply the working fluid to the two sides of the chambers 29 of the aerators, respectively, the increase in the flow rate of the working fluid Sy.c and Sc.c are twice as large

value in comparison with the corresponding parameters of the pressure pipe 7 and the nozzle-nozzle 8.

The nozzles intended for supplying the working fluid to the two sides of the chamber 29 of the aerator are made in the form of hollow nozzles 32 with two guide elements 34 on each nozzle, having the form of grooves with gently diverging beads at an angle of 15-30 ° to the axis grooves with concave along the flow and flat in cross section of the heads, divided along the length of the central wedge-shaped dividers 35 and two or four lateral wedge-shaped dividers 36 into an even number of equal widths of channels 37 and adjacent narrowed curved The bottom parts to each other at an angle of 180 ° and jointly to the end of the nozzle-nozzle, produce a division of the outlet of the nozzle-nozzle 31 along an axis parallel to the longitudinal axis of the aerator chamber 29. Moreover, the bending of the bottoms of the guide elements 34 is made not less than before the full intersection of the projection of the half cross section of the outlet of the nozzle-nozzle 32 to the bending of the bottom, and the extension of the bottoms beyond the bend is made straight at an angle of 45 to 60 ° to the nozzle-nozzle axis 32, vertically mounted in a pipe 33 for connecting nozzles to the pressure pipe 31, and directed to the bottom of the discharge slots 30 between the bases of the chambers 29 of the aerators and the bottoms of the compartments 4 under

angle of 30-45 ° to horizontal bottoms and respectively to the surface of aerated pulp in chambers 29 of aerators and flotation-separation compartments 4.

The central wedge-shaped dividers 35 are located on the axes of the bottom of the guide elements 34 directly behind the outlet of the nozzle-nozzle 32 and divide the bottom along the entire length, and the side dividers 36 are placed beyond the bend

bottoms on their linear extensions. In this case, the opposite walls of the dividers, as well as the sides of the guide elements and the opposite walls of the wedge-shaped dividers are located

at an angle T of 1-2 ° along the flow of the working fluid and have a height at the gathering of flat jets from the bottom of each guide element not less than the size of the quotient obtained from dividing half of the cross-sectional area of the nozzle-nozzle outlet 32 by the total width of the ca-. 37 formed on the bottom of the guide element 34.

The pressure pipelines 31c with shut-off and control valves are connected through a piping system to the pump, which supplies the working fluid to the chambers 29 of the aerators. In the middle part of the chambers 29 of the aerators, air ducts 38 are located, which have narrow slots for uniform air release into the chambers of the aerators along their entire length. Air ducts 38 are connected through a piping system with shut-off and control valves to the blower.

The aerator chambers 29 through the slots 30 in the end walls of the machine chamber communicate with the regulators 40 at the gas-liquid level section in the chambers of the aerators, and the level regulators communicate with the atmosphere by means of discharge tubes. The upper edges of the slots 39 are located above the upper edges of the slots 30 between the bottoms of the side compartments and the bases of the sides of the chambers 29 of the aerators.

In the complex, chambers 29 of aerators, pressure pipelines with nozzles-nozzles 31, air ducts 38 and gas-liquid level regulators 40 in chambers 29 of aerators comprise aerators of flotation-separation compartments 4.

In addition, the circulation load through chutes 25, circulation channels 26 and slots 28 into the chambers 29 of the aerators has a significant effect on increasing the efficiency of the aerators.

Underneath the base of the side compartments 4 are devices 41 for collecting the working fluid, made in the form of grooves with a stepwise increasing cross-sectional area and funnels connected to the circulation channels 26 through the windows in the bottoms of the compartments 4. The devices 41 for collecting the working fluid from the circulating flow The load of the load passing through the channels 26 is also connected to the inlets of the pumps supplying the working fluid to the chambers 29 of the aerators through pipelines 31.

Above the chambers of the aerators 29 horizontally mounted soothing-distribution grilles, made in the form of two-row fixed and mobile rows of grates, are installed horizontally. A fixed range of grates 42 is formed

rod elements having a V-shaped cross-sectional shape, secured by electric welding M-shaped kerchiefs on the support plates 43, rigidly connected to the base of the compartment 4.

The movable row of grates 44 is also made of rod elements mounted on perforated carriers.

0 plates 45 connected with t g, having at the upper end threads with threaded bushings gear-worm lifting mechanism 46 installed above the camera flotation machines and providing

5 lifting the mobile grate 44 to a height of at least a V-shaped element measured from the upper edges of the support plates 43. In this case, in double-grate bars 42 and 44, the V-shaped elements have a slope of 15-45 ° to the vertical plane or an angle at the base 30-90 °; rod-shaped V-shaped elements are located in the grate with an interval of 10-20% more than the width of the cross-section of the V-shaped

5 elements in checkerboard order relative to row; rod V-shaped elements are installed in the grate perpendicular to the plane, passing along the axis of the chambers of the aerators or parallel

0 slits 30 between the bases of the chambers 29 of the aerators and the bottoms of the compartments 4; the supporting perforated plates 45 are arranged perpendicular to the rod-shaped V-shaped elements of the grate bars 42 and 44.

5 Along the sides of the base of the compartments 4 there are devices for the uniform collection of chamber waste along the entire length of the chambers, made in the form of funnels 47 with an angle of inclination of the walls greater than the angle of the natural

0 slopes of the transported material, connected by outlets to the collecting chutes 48 with stepwise increasing height and cross section along the flow of waste connected to

5 by the pulp tapping pocket 49 by means of the grooves 50. In this case, the upper plane of the fixed grates 42 and the upper bases of the funnels 47 are located at the same level. Over the gutters 25

0 non-aerating zones, pecogons 51 are installed. Chutes 52 are placed along the sides of the chambers to collect the frothy product.

The machine works as follows. The chambers of the aerators 5 supply air from a blower under air pressure 15, surpassing the hydrostatic pressure of the pulp filling the flotation compartment 3. Under the influence of compressed air, excess pulp is displaced from the chambers 5 and a gas-liquid section is created at a given level. After the gas-liquid section is formed, the aerator chambers 5 through the pressure pipelines 7 with nozzles 8 connected to the nozzles 9 supply the working fluid under pressure ensuring the velocity of freely falling jets in the range of 12-20 m / s.

As the working fluid can be used in the flotation of salts of the mother liquor; in flotation of dense slurries (requiring dilution), the filtrate, clarified or technical water; during flotation of liquid slurries, for example, to aerate the initial feed, discharge the hydrocyclone used to divide the liquid pulp into a working fluid with a low solids content of the thinnest classes and the condensed portion entering the machine as the initial feed of the flotation compartment 3 of the first chamber; in the process of its control flotation in the side compartments of the first chamber, as well as for the working fluid of all the aerators of the second and subsequent chambers, the circulation load released in the upper regions St x non-aeration zones of the compartment 4 of each chamber with a low solid content, represented by the thinnest classes.

In the pressure pipe 7, the working fluid flow rate is constant throughout the entire length, since the cylinders forming the pressure pipe have a constant specific cross-sectional area, coming in each nozzle nozzle 8 installed in the pipeline along the working fluid flow. It also stabilizes the pressure in the pressure pipe 7, which causes the release of the working fluid from all nozzles 8 at a constant speed close to the optimum of 14-17 m / s.

Since the calculation of the pressure pipeline 7 is carried out taking into account the provision of the weighing flow rate of the working fluid, eliminating solid precipitation, when the flow rate stabilizes in all cylinders forming the pressure pipeline 7, it is not heated over the entire length.

The working fluid discharging the free jet from the outlet of the nozzle nozzle 8 tangentially to the concave bottom of the guide element 10 is converted into a flat jet across the entire width of the bottom of the guide element 10 under the action of centrifugal force and is divided into equal parts by a central wedge-shaped divider. 11, located on the bottom axis. On the concave part of the bottom

the guide element 10, the flat jets separated by a central wedge-shaped divider 11, acquire a predetermined thickness. Beyond the bend, on the straight extension of the bottom of the guide element 10, lateral wedge-shaped dividers 12 are installed, which together with the central wedge-shaped divider 11 and the sides of the guide

element 10 is four or six (depending on the number of lateral wedge-shaped dividers 12), channels 13 having an equal width increasing along the flow of the working fluid due to

the location of the opposite walls of the wedge-shaped dividers 11 and 12, as well as the sides of the guide elements 10 and the opposite walls of the lateral wedge-shaped dividers 12 at an angle of 1-2 °.

The expansion of the channels 13 at an angle of 1-2 ° causes the expansion of flat jets at this angle in order to counteract their coagulation under the influence of the surface tension of the liquid.

Since the straight extension of the bottom of the guide element 10 is located at an angle of f 60-45 ° to the vertical axis of the nozzle-nozzle 8, the freely falling jets of working fluid,

leaving the channels 13 are directed to the gas-liquid interface in the chamber of the aerator 5 at an angle of 30-45 ° to the bottom of the slit 14.

Due to the arrangement of the flanks of the guide element 10 relative to its axis at an angle of 15-30 °, a fan-shaped distribution of freely falling jets occurs at the gas-liquid interface along slit 14 at an optimum drop height (400 m) for respectively 290-580 m.

Under the conditions of the horizontal arrangement of the pressure pipe 7 and the decreasing diameter of the cylinders,

forming, the optimum installation height of the nozzle nozzles 8 is achieved by increasing the length of the nozzles 9 for connecting the nozzles nozzles to the pressure pipe by the amount of decreasing the diameter of the cylinders along the flow of the pulp.

The nozzles-nozzles 8 having a diameter of the outlet 10 times and more than the maximum maximum size of the floatable material make it possible to use part of the pulp and chamber products as a working fluid, which creates preconditions for the flotation of liquid pulps (for example, coal). flotation machines 2 times.

The guiding elements 10 provide for the conversion of circular jets into a series of flat ones with a given characteristic in width and thickness, as well as the distribution of these jets along the length of the outlet slots 14 of the chambers 5 aerators.

The flat liquid jets formed in the nozzles, falling at an angle of 30-45 ° to an artificially created gas-liquid section, eject the air in chambers 5 in a ratio of up to 8-10 m3 of air per 1 m3 of working fluid, which is dispersed into flooded jets and when they hit the bottom under the chambers 5. form torches 100-150 mm wide and providing a high uniformity of pulp aeration.

The flow of air ejected by freely falling jets is compensated for by its continuous inflow into the chambers of the aerators 5 through the air ducts 15. The specified gas-liquid partition level in the chambers 5 is maintained using gas-liquid interface level adjusters 16 as follows. Since the level controllers 16 communicate with the chambers of the aerators 5 through the slots 20, the upper edge of which is at the lower limit of the gas-liquid interface and above the level of the slots 14 under the base of the partitions 2 intended to release the aerated pulp from the chambers 5 to the flotation compartment 3, then, when an overpressure is created in the chambers 5, which exceeds the permissible limit and the corresponding decrease in the level of the pulp in the bases of the chambers 5 to the upper edges of the slits 20, the excess air through these slits enters the level regulator 16 and Cutting its air vent tube ejects it into the atmosphere. In this case, the pressure in chambers 5 is reduced, the published gas-liquid level is restored, and the release of non-dispersed air through the slots 14 into the flotation compartment 3 is eliminated.

Simultaneously with supplying the working fluid to the chambers of the aerators 5, the pulpups 17 through the nozzles 18 are fed by gravity to the initial power, pretreated with reagents with a pressure exceeding the hydrostatic pressure of the pulp column that fills the flotation compartment 3 and provides the necessary flow rate corresponding to the specified machine capacity.

 From the slurry pipe 17 through the slits 19, the initial power supply with a thin layer evenly enters the chambers of the aerators 5 along the entire length of the machine chamber. The volumetric flow rate of the feed supplied to the chambers of the aerators 5 from the slurry lines 17 is 3-6 times higher than the volumetric flow rate of the working fluid supplied to these chambers through pressure pipes with nozzles 8. In the chambers of the aerators 5, as well as at the outlet to the base of the compartment 3, a thin layer of the initial feed is uniformly saturated with dispersed air under conditions of intensive mixing of the pulp and air mixture due to the high rate of the initial feed from the slurry feeds 17 through the slots 19 and the high energy of freely falling jets and the gas-liquid interface.

The pulp and air mixture from the chambers of the aerators 5 through the slots 14 under the base of the partitions 2 enters the base of the compartment 3 at high speed. A large total consumption of the original power supply and working fluid, which exceeds the flow of the working fluid 4-7 times, and as a result, the speed of transportation of the air-to-air mixture through chambers 5 of aerators and slits 14, exceeding the speed of free ascent of air bubbles of flotation size 5-10 times, causes a high coefficient of removal of the ejected and dispersed air free the bottom of the dropping jets in the chambers of the aerators 5 to the bottom of the flotation compartment 3.

Horizontal flows of the pulp and air mixture leaving through the slots 14 of the opposite aerators are mixed and converted into ascending vertical flows. Intensive mixing of the opposite flows of the pulp and air mixture contributes to the installation of nozzles 8 on the pressure pipelines 7 of the opposite aerators in a checkerboard pattern, as well as a small base width. compartment 3 and the speed of oncoming flows. Above the upper face of the sharp narrowing of the base of compartment 3 a homogeneous pulp air mixture is created, the upward flow is stabilized, and its speed decreases in proportion to the increase in the cross-sectional area of the flotation compartment 3.

At the same time, at the base of the compartment 3, in the area of increased speeds and intensive mixing of the pulp and air mixture, favorable conditions are created for processing float complexes containing the thinnest classes. Then, over the area of sharp narrowing of the flotation compartment 3 under conditions of stabilized upstream, having a dense packing of mineral particles and air bubbles with low relative displacement rates, the necessary conditions are created for creating flotation complexes, including mainly granular minerals, as by the method of frothy flotation in a boiling both in suspended layers and by adhesion.

In the upper part of compartment 3, the upward flow of the pulp and air mixture is divided by a puller with guide peaks 21 into two streams. Above the upper edges of the partitions 2 between the peaks 22, the speed of the ascending flows decreases in proportion to the increase in the width and area of the flows and they are converted from ascending to horizontal. This also involves partial separation of the pulp and air mixture with a concentration in the upper layers of floatable minerals, mainly in the form of aeroflocs, forming a foam layer with a low fluid content and non-floated minerals in comparison with the pulp and air mixture that fills compartment 3 and the lower layer respectively, with a high content of liquid phase and waste.

The top layer in the foam state is poured over the edges of the visors.

22 and is smoothly applied to the surface of the previously created and continuously maintained foam layer in the lateral flotation-separation compartments A by aeration of the chamber products filling these compartments.

Smooth feeding of foamed feed to the foam layer is provided by adjusting the height of the peaks 22, taking into account the thickness of the previously created and maintained foam layer in compartments 4, depending on the characteristics of the materials being processed, the content of floatable components, the density of the pulp, the reagents used and the specific load on the machine .

Since the specific weight of the foamed initial feed and the specific weight of the foam layer in compartments 4 are either equal or close in magnitude, regardless of the load on the machine and the density of the initial feed, the foam layer created in compartments 4 will not collapse. Lower layer with a high content of liquid and non-floating minerals through the gaps

23 between the baffles 2, the peaks 22 and the skins 24 is brought into the internal volume of the pulp filling the flotation separation compartments 4 to the control flotation.

The magnitude of the adjustable gaps 23 is preset by q taking into account the characteristics of the processed pulp, which determine the mode of operation of the machine and the volumetric flow of the original feed residues transported through the gaps 23. The unloaded residues of proflotted pulp in the flotation compartment 3 through the gaps 23 can be carried out in the automatic control mode depending on different hydrostatic the pressures of the pulp and air mixture pillars filling the gaps 23 and compartments 4 at the junction with the visors 22 from the outside, at a height from the curb lei to the surface, gas foam in this section. Therefore, in the first chamber, with a high density of the initial feed and a high content of floated minerals, such as coal and intensive aeration of the pulp (in the ratio of pulle: dispersed air 1: 1.5-2), a 100% yield of the initial feed in a foamed state is possible. it on the foam layer in the compartments 4.

In the flotation-separation compartments 4, the level of the mirror of the pulp (without taking into account the thickness of the foam layer) is maintained at an elevation of 20-50 mm above the side walls of the bath 1, but not above the upper cut edge of the partitions 2, using a gate in the pulp discharge pocket 49, which causes continuous overflow of pulp into chutes 25 and eliminates the likelihood of the chamber product returning from compartments 4 to compartment 3.

Due to the continuous inflow of foamed feed and pulp residues from compartment 3 and pulp overflow from compartments 4 to troughs 25 in the upper zone of flotation-separation compartments 4, directed flows from partitions 2 to the sides of the bath 1 are created. Directed flows transport the foam layer created on its surface in compartments 4, and the initial feed of the machine chamber fed in the foamed state to the foam layer. During the transportation of the combined foam layer, it is intensively stratified, releasing a foamy product with high density and low content of non-floated minerals and waste adhesive and foam flotation and separation all the way from the edges of the peaks 22 to the sides of the bath 1 at the end of the path. Foamy product is discharged from each the machine chambers using foams 51 in the chutes 52 for receiving the flotation concentrate.

The aerators of the side flotation-separation compartments 4 have a similar principle of operation with the aerators of the flotation compartment 3 and are activated simultaneously with them. In the chambers 29 of the aerators of the side flotation-separation compartments 4, through the air ducts 38, air is blown from the blower under pressure exceeding the hydrostatic pressure of the pulp,

the filling compartment 4. Under the influence of compressed air, excess pulp is displaced from the chambers of the aerators 29 and a gas-liquid partition is created at a given level. After the gas-liquid section is formed, the chambers of the aerators 29 through the pressure pipelines 31 with nozzles connected to the pump supply the working fluid under pressure to ensure the speed of freely falling jets within 12–20 m / s.

The working fluid is withdrawn for the aerator chambers 29 due to the circulation load with low solid content of the thinnest classes through the channels 25, circulation channels 26 and communicating with the channels 41 of the device, connected by pipelines to the inlets of the pumps supplying the working fluid to the pressure pipelines 31 nozzles 32.

In the pressure pipe 31, the working fluid flow rate and pressure remain constant, since the cylinders forming the pressure pipe 31 have a constant specific cross-sectional area, coming in each nozzle nozzle 32 installed in the pipeline along the working fluid flow.

Stabilizing the speed and pressure of the working fluid in the pressure pipe

31conditions the release of working fluid from all nozzles 32 installed on the pipeline with a speed close to the optimum of 14-17 m / s, and eliminates the likelihood of pipeline flaming, since the cross-sectional area of each cylinder meets the conditions for ensuring the weighting speed.

Since the nozzles 32 are designed to supply the working fluid to the two sides of the chamber of the aerator 29, then, all other things being equal, the cross-sectional area of the outlet of the nozzle-nozzles

32 should be two times larger in comparison with the area of the outlet of the nozzle-nozzle 7. Accordingly, the specific area of the cylinders forming the pressure pipe 31, which each head ahead, the nozzle-nozzle 32 is installed in the pipeline along the flow of the working fluid twice a larger value in comparison with the specific area of the pipeline 7 falling on the nozzle-nozzle 8.

The working fluid, which is discharged with a free stream from the outlet of the nozzle-nozzle 32, is divided by narrowed portions of the bottoms of the guide elements 34 adjacent to the outlet.

nozzles-nozzles 32 along its axis into two jets entering the concave bottoms of the guide elements 34. On the concave bottoms, under the action of centrifugal forces, the semicircular jets are transformed into planar and their simultaneous division by central wedge-shaped dissecting 35 into two jets on each guide element 34.

Beyond the edge of the bends on the straight extension of the bottoms of the guide elements 34, the formation of flat jets in the channels 37 located between the central wedge-shaped divider 35, lateral wedge-shaped dividers 36 and the sides of the guide elements 34 is completed.

This creates four or six flat expanding jets of working fluid at an angle g of 1-2 ° according to the number of side dividers 36 installed on the bottoms and the angles between the opposite walls of the dividers 35 and 36 and the sides of the guide elements 34.

The expansion of freely falling jets, formed in the channels 37 at an angle of 1–2 °, prevents their coagulation under the influence of the surface tension of the liquid. Since the rectilinear extensions of the bottoms of the guide elements 34 are at an angle (60-45 ° to the vertical axis of the nozzle-nozzle 31), the freely falling jets of working fluid emerging from the channels 37 are directed to the gas-liquid interface in the aerator chamber 29 under at an angle of 30-45 ° to the bottom of the outlet slots 30 between the bases of the chamber 29 of the aerator and the bottoms of the flotation separation compartments 4.

The jets of working fluid coming from each guide element 34 form a fan with equal intervals between the jets, ensuring the distribution of the working fluid along the outlet slots 30 when the jets fall from an optimum height of 400 mm over 300-600 mm, which due to the location of the flanges of the guide elements 34 relative to the axis of the bottoms, respectively, at an angle of 15-30 ° and an equal width of the wedge-shaped dividers 35 and 36, delimiting flat jets at their exit from the channels 37.

When horizontal installation of the pressure pipeline 31 and reducing the diameter of the cylinders forming the pressure pipeline along the flow of the working fluid, the optimum height of installation of the nozzles 32 with the guide elements 34 is achieved by increasing the length of the nozzles 33 to fasten the nozzles 32 on the pipeline 31 by the amount of diameter reduction corresponding cylinders.

The nozzles-nozzles 32 have an outlet orifice diameter 15 times the maximum size of floated particles, which makes it possible to use the chamber product as a working fluid and thereby increase the productivity of the flotation machine during the flotation of liquid slurries, such as coal, by 2 times. This prevents the nozzles from being flushed by the floatable material.

The liquid streams formed in the nozzles-nozzles, falling at an angle of 30-45 ° to the artificially created gas-liquid section, eject the air in the chambers 29 in a ratio of up to 8-10 m3 of air per 1 m3 of working fluid. The ejected air is dispersed in submerged jets, as well as on impacting the bottom, forming torches of intensely aerated pulp up to 150 mm wide each jet. The flow of air ejected by free-flowing jets and dispersed into the machine chamber is compensated for by continuous inflow into the chambers 29 of the aerators through the air ducts 38. The gas-liquid section in the chambers 29 is maintained by releasing excess air from the chambers 29 through slots 39 controllers 40 with air outlets communicating with the atmosphere.

At the same time, the air pressure in the chambers 29 decreases and the level of the liquid filling the base of the chamber 29 accordingly increases.

Since the upper edges of the slits 39 of the regulators 40 are above the level of the upper edges of the outlet slits 30, by which the chambers 29 of the aerators are connected to the bases of the flotation and separation compartments 4, this prevents the release of undispersed air from the chambers 29 to the compartments 4. Since the level of aerated pulp in the flotation-separation compartments 4 is maintained by means of a gate in the pulp discharge pocket 49 above the sides of the bath 1, after the side compartments 4 are activated, a hydrostatic differential occurs. pulp column pressures of non-aerated, filling chute 25 and aerated filling zone aeration zone 4. Under the influence of the hydrostatic pressure differential, the circulation load with a small solid content of the thinnest classes passes through chutes 25, circular channels 27 and slots 28 in false heads 27 into bases of chambers 29 of aerators along the entire length of the machine chamber.

The flow rate of the circulation load entering through the slots 28 into the chambers 29 of the aerators is 2-3 times greater than the volumetric flow rate of the working fluid supplied to these chambers. In the aerator chambers 29, the circulation load passing with a thin layer through the bases of the chambers, as well as at the exit to the base of the compartments 4, is uniformly saturated with dispersed air under conditions of intensive mixing of the air mixture.

The pulp and air mixture from the chambers 29 of the aerators through the slots 30 between the bottoms and sides of the chambers 29 enters the bases of the flotation and separation compartments 4, limited in height by the distributors of the pulp air mixture adjusted for a given optimal flow rate of circulation by changing the area of the living cross section of gaps between V- shaped fixed grates 42 mounted on support plates 43 and movable V-shaped grates 44 mounted on bearing plates 45. due to the vertical movement of moving olosnikov 44 with the lifting mechanism 46 up or down. At the same time, regardless of the flow rate of the circulation load, to which the pulpoa distributors and the position of the moving row of grates relative to the stationary row were previously tuned, they do not come in contact with each other, which prevents them from being skimmed off and the likelihood of difficulties occurring during reconfiguration of the pulverized mixture distributors to another mode of operation.

The high flow rate of the circulation load passing in a thin layer through the chambers 29, exceeding the rate of float of the air bubble of flotation size, causes a high output of dispersed air from the chambers 29 of the aerators to the base of the compartment 4. At the bases of the compartments 4 there is a pulpous air see, exit, exit through the slots 30, it is reflected from the sides of the base of the compartments 4, and when several aerators are installed in each compartment 4, they also rise vertically from the demarcation walls. A portion of the pulp and air mixture passes through the gaps between the grate bars 42 and 44 directly above the outlet slots 30.

The bulk of the pulp and air mixture moves under the grate in the direction of least deceleration.

flow, mainly along V-shaped core elements and gaps between them, to the axes of chambers 29 of aerators and sides of compartments A, and partially in the plane, perpendicular to the core elements of grates 42 and 44 and gaps between them, replacing unaired ) or weakly aerated pulp forming downward flows over inclined planes of prisms — the outer sides of chambers 29 of aerators and sides of compartment 4, as well as in the intervals between the bases of the flares of aerated pulp exiting through slots 30 created by ejectors air dispersion by surface fan-shaped dispersed flat streams of working fluid issued by nozzles 32 and covering an inlet to the aerated pulp, approximately equal to the distance between the axes of the adjacent nozzles installing or aeration area aerated by each nozzles nozzles.

The vortex-like flows of the pulp-air mixture at the base of the compartments 4 under the distributors of the pulp-air mixture ensure uniform distribution of dispersed air over the aeration area of the flotation-operating compartments.

Since the pulp and air distributors create constrained conditions for the output of the pulp and air mixture to the nickle space of compartments 4, and under the influence of the hydrostatic pressure difference between the pulp poles, non-aerated, in the grooves 25 and aerated in the compartments 4 to the base of the compartments 4, a continuous flow of circular load is provided the pulp and air mixture, an overpressure is created under the grates 42 and 44, which prevents the pulp from flowing out of the above-grate chambers of the machine into the refined volume.

The pulp and air mixture with multiple jets passes through the gaps between the grate bars 42 and 44 into the above-grate volume of compartments 4 over the entire area of aeration. Since the grate bars consist of V-shaped elements, stagnant zones may form below them with accumulation of air bubbles causing their subsequent coalition, since air bubbles located at the junction with inclined planes of V-shaped elements forming the grate bars will move upwards with greater speed compared to the flow of the liquid phase due to their lifting force, as well as

less friction and braking forces on the plane of the grate.

During the intensive mixing of the pulp-air mixture and high flow rates at the base of the compartments 4 and at the exit from the gaps between the V-shaped elements of the grates 42 and 44, favorable conditions are created for the formation of flotation complexes, including the thinnest particles of floated minerals.

In the oversize volume of the flotation-separation compartments 4, an upward flow of an air-pulp mixture is created over the entire area of aeration. At the same time, immediately above the distributors of the pulp and air mixture, fluidized bed conditions are created, and in the internal volume of the pulp compartments 4 above the distributors at a height of more than 100-150 mm, suspended layer conditions favorable for flotation of granular minerals. Perforated carrier plates 45, located perpendicular to the horizontal flow of floated pulp transported over the grate in the direction of discharge, significantly reduce the flow rate at the height of the plates 45. At the same time, the flotation time of the upper grades in the fluidized bed above the grate 42 and 44 and their output to the froth product accordingly increases. At the same time, a weak horizontal flow above the grates ensures the transportation of waste of the upper size classes to unloading and contributes to an even distribution of the pulp and air mixture over the aeration area.

Using aerators of flotation-separation compartments 4 on the surface of the pulp mirror in the compartments, a foam layer is created due to the flotation of the remnants of floatable minerals from the internal volume of the pulp. Over the entire area of aeration, a submerged layer is also created and continuously maintained, consisting largely of free air bubbles. At the same time, due to the weak inclination of the partition 2 to the axis of the compartments 4, the partitions 2 have an increased concentration of dispersed air, which provides intensive aeration of residues of professional pulp in compartments 3, discharged through the slots 23 above the fairings 24 to compartments 4, as well as intensive formation of a foam layer of greater height under the edges of the peaks 22, which increases the reliability and efficiency of the foam separation of the initial feed, which was fed in a foamy form to the previously prepared and continuously support second foam layer.

In the area of non-aerating zones above the sloping walls of the sides of the bath 1, downflows are created containing non-flooded minerals entering through the niches under the sloping walls of the bath into waste disposal devices consisting of funnels 47 connected to the chutes 48 with stepwise increasing height and cross-sectional area along the waste stream, into the connecting chutes 50 and discharged as chamber waste or final flotation waste, using a pulp outlet pocket with a gate 49.

The flotation machine, having one flotation-separation compartment in the chamber (Fig. 11), works in a similar way. At the same time, the ability to install a pressure pipe for supplying working fluid and an air duct from both ends of the machine chamber, as well as the location of the pulp-receiving pipe 18 in the middle of the slurry line 17, allows you to create a machine with a chamber length twice as large as compared to the variant shown in FIG. .1 and 2.

The flotation machine (Figs. 12 and 13) with the identity of the aerator device, the presence of pulsation-air flow controllers, gas-liquid level regulators, false bottoms, grooves for collecting the circulation load and circulation channels and devices for collecting the working fluid from the circulating flow. This load has a different layout solution, which determines the characteristics of its hydrodynamics. The units and parts of this machine, having an identical device, the principle of operation and purpose, are denoted by the same numbers as used to designate the units and parts of the machine shown in Figures 1 and 2.

The difference in the layout solution is mainly that the pulp lines 17, chambers 5 and 29 of the aerators are installed perpendicular to the axis of the machine chamber. According to the arrangement of the slurry lines and aerators, the initial power supply to the chambers of the aerators through the slots 19 and the circulation load through the slots 28 is carried out the entire width of the base of the camera of the machine. Moreover, each aerator chamber 29 is in communication with a separate circulation channel 26. The machine does not divide the chamber into flotation and flotation and separation compartments, which causes the flotation process to take place only from the internal volume of the slurry transported in the aerated

the volume of the chambers from entering the feed to the pocket for discharging waste along the axis of the machine.

Since each aerator chamber 29 is in communication with a separate circulation channel 26, the channels 25, designed to take the circulation load from the machine chamber in the area of each aerator bounded by partitions 2 or the end wall of the bath 1 and part 2, have a length equal to action aerator. At the same time, the troughs 25, installed in the area of action of the aerators with chambers 5 and having one outlet funnel each, are connected to the circulation channels 26 of the nearest aerator with the chamber 29. Troughs 25, installed in the area of operation of the aerators with chambers 29 and having two exhaust ports the funnels are connected by the first funnel to the circulation channel 26 of the aerators, in the area of which chutes 25 are installed, and the second funnels are connected to the channel 26, which communicates with the next chamber 29 of the aerator along the pulp flow.

The circulation channels 26, which communicate with the aerator chamber 29, installed at the end of the machine chamber in front of the pulp outlet pocket 49, are connected via one funnel of the grooves 25 installed in the area of operation of the preceding aerator along the flow of the pulp and two funnels of the grooves 25, located in the area of action of the final aerator. In the end wall of the bath 1, above the grates of the distributors of the pulp and air mixture 42 and 44, windows 53 were cut out symmetrically to the axis of the machine chamber to release the chamber waste into the pulp discharge pocket 49.

The peculiarities of the operation of this machine are that the pulp treated with reagents is fed through the nozzle 18 into the pulpway 17, and then is produced in a thin layer through the slit 19 into the chamber 5 of the aerator operating according to the described principle. From the chamber 5 of the aerator, aerated pulp through the slit 14 enters the base of the chamber of the machine across its entire width. The aerated initial power supplied through the slit 14 into the base of the machine chamber, limited in height by the grate bars 42 and 44 of the air-to-air mixture distributor with an adjustable gap area between the grate bars and the chamber 2, creates an upward flow of air-pulp mixture uniformly distributed over the aeration area between the end of the sloping wall of the base of the bath 1 and the partition 2 under the influence of eddy flows generated due to the difference in hydrostatic pressures of the pillars of intensively aerated ulps on joining to the partition 2 and weakly aerating above the inclination of the end wall of the base of the bath 1. Under the grate bars 42 and 44, adjusted to the given performance, under the influence of a continuous inflow of the pulverized mixture through the slot 14 and the constrained conditions of passage through the gap between the grate bars create an overpressure in comparison with the hydrostatic pressure at the base of the aerated pulp column above the grate bars, which excludes the flow of pulp from the oversize chamber volume to the sublattice one.

The aerated feed source with a plurality of jets passes through the gaps between the grate bars 42 and 44 at high speed. Above the grate, the upstream flow rate decreases in proportion to the increase in the area occupied by the aerated initial power supply due to the increase in chamber area in height, due to the increased distance between the longitudinal inclined sides of the bath 1, and also due to the partial movement of this flow along the longitudinal axis.

In the upstream of the feed from the base to the pulp mirror, continuous mineralization of air bubbles occurs, including a number of fluorescent complexes, including the thinnest classes, directly above the grate 42 and 44 in the fluidized bed into the flotation complexes, under the conditions of intensive mixing. includes both finely dispersed minerals and a granular part of the minerals being floated, and in the internal volume of the pulp above the grate at an altitude of 100-150 mm or more in the suspended layer, ayuts aeroflokuly due average particle size and granular minerals.

Using the gate in the pulp discharge pocket 49, the level of the pulp mirror is higher than the sides of the bath 1 by 20-50 mm, which causes the chamber product to overflow into the grooves 25 communicating with the circulation channels 26 communicated through the slots 28 with the bases of the chambers 29 of the aerators.

Since the sides of the bath 1 have a slope causing the formation of non-aeration zones, in the near-wall layer under the influence of the hydrostatic pressure difference of the aerated pulp column above the grate 42 and 44 and of the aerated over the inclined sides of the bath 1, downward flows occur, accumulating the bulk of the mineral particles included in the flotation complexes and re-entering the aeration zone above the soothing grate. Therefore, the overflow of the chamber product entering the chutes 25 and constituting the circulation load contains the minimum amount of solid and only the thinnest classes. The pulp consumption for the formation of a downward flow over the inclined longitudinal sides of the bath 1 and the circulation load taken through the chutes 25 is compensated for by the horizontal flows of the upper layers under the pulp mirror from the machine axis to its sides. In this case, the froth layer is transported by gravity to unloading and is discharged by means of foam boilers 51 into the troughs 52 to receive the frothy product.

The circulatory load taken into the channels 25 in the area of the aerator with the chamber 5 is completely transferred to the circulation channel 26, which is connected through the slot 28 with the nearest chamber 29 of the aerator. The principle of operation of aerators with chambers 29 and devices 41 for collecting the working fluid from circulation channels 26 is similar to that described. The circulatory load selected in the chutes 25 in the area of aerators is divided into two halves with chambers 29, from which the first is fed into the circulation channel of the aerator, in the field of which it was selected, and the second enters the circulation channel communicating with the following aerator along the flow of the pulp.

Transferring from the area of operation of the first aerator, issuing to the internal volume of the machine chamber an intensively aerated feed stream, the total volume of the circulation load to the circulation channel of the next chamber and transferring 50% of the circulation load to the subsequent aerators selected in the area of the previous aerator with chamber 29 , intensifies the transportation of a significant part of the pulp with a low content of solid and floatable minerals along the axis of the machine in the direction of unloading waste.

At the same time, the residence time in the aerated volume of the pulp machine chamber with a high content of solid and floatable minerals, especially their granular part, increases accordingly.

The area of operation of the final aerator in the chamber of the machine adjacent to the discharge pocket 49 receives “50% of the circulation load taken in the area of the previous aerator and its entire volume flow taken from the final aerator.

The increased flow rate of the circulating load at the end of the machine chamber intensifies the upward flow from the underbody tree to the torsion volume of the machine chamber and mixing of the pulp air mixture over the grates 42 and 44, which improves the discharge of flotation waste, including their granular part, and stabilizes the operation of the machine into the area of the final aerator by compensating for the increased circulation load of the flotation waste consumption through the window 53 for discharging flotation waste into the pulp discharge pocket 49.

The machine maintains a high flow rate of the circulation load that enters the aerators with chambers 29, which is close in magnitude to the flow rate of the initial power supply to the chamber 5 of the aerator. Since the circulation load after mixing it with the working fluid that ejects the air is the carrier of the dispersed air, the higher the flow rate of the circulation load is, the lower the coalescence of air bubbles and the higher the output of the dispersed air from the aerator chamber to the machine chamber under equal conditions .

The high flow rate of the circulation load through chutes 25 in combination with the formation of downward flows over the sloping sides of bath 1 under the influence of the hydrostatic pressure difference of non-aerated pulp pillars in chutes 25 and non-aeration zones over the sloping sides of bath 1 and aerated pulp columns located in the aeration zone causes : creation of intensive upward flows of a pulp-air mixture from the podolosnikovy to the head of the chamber and maintaining the suspended particles of mineral particles into the airspace the volume of pulp above the grates 42 and 44 of the distributors of the pulp and air mixture; the creation of intense horizontal flows above the pulp mirror directed from the longitudinal axis of the machine chamber to its sides, ensuring the formation of descending flows in the non-aeration zones above the inclined sides of the bath 1, accumulating minerals not included in the flotation complexes, separating the circulation load with low solids and only the thinnest classes entering chutes 25 (horizontal streams transport the foam layer on its surface for unloading); creation of pulp flows over distributors of the pulp and air mixture formed due to descending flows in the area of non-aeration zones above the inclined sides of the bath 1 directed from the sides of the chamber to its longitudinal axis and providing input to the aeration zone of minerals not included in the flotation complexes, as well as transportation waste at the end of the chamber to the window 53 to unload.

The interaction of the continuous feed flow and the flows generated by the circulating load and downward flows over the inclined sides of the bath 1 causes the spiral circulation of the pulp from the load to the pulp discharge pocket along the pulp flow along the right side of the machine chamber from bottom to top and to the side of the bath from the pulp dividers 21 and the axis of the chamber, and on the left side of the axis of the chamber in the opposite direction. In this case, the bulk of the solid, with the exception of some of the thinnest classes contained in the circulation load, is continuously in the aerated chamber volume above the grate 42 and 44.

The proposed machine makes it possible to stabilize the velocity and pressure of the working fluid flow in the pressure pipelines and thereby optimize the speed of freely falling jets on the gas-liquid interface produced by each nozzle-nozzle and, as a consequence, increase the air ejection ratio by jets by 15-20% and accordingly reduce the flow rate of the working fluid and the energy intensity of the flotation process; use part of the pulp floated and chamber products as the working fluid; to increase the reliability of the flotation machine operation by repeatedly reducing the likelihood of backfilling of the pressure pipe and nozzle nozzles, including when using a part of floated pulp as the working fluid; improve the uniform distribution of dispersed air along the chambers of the aerators of the photomachine and, accordingly, over the aeration area, as well as increase the specific and overall performance of the photomachine (by increasing the air ejection coefficient by free-flowing jets, using part of the floated pulp and chamber products as working fluid, increasing the uniformity of distribution dispersed air by area of aeration and reduction of downtime due to the backfilling of pressure pipelines and nozzles) in environments it is 20-25%.

On the basis of the proposed technical solution, it is possible to create a parametric row of a photomachine with a chamber capacity of 6.3, 12, 25 and 40 m3.

Claims (1)

Claims of the invention A flotation machine comprising a chamber with a bottom and partitions dividing the chamber into flotation and flotation separating compartments, slurry pipes for receiving and distributing the initial feed along the length of the flotation compartment, depth jet aerators of the flotation compartment and flotation separating compartments consisting of chambers of aerators, gas-liquid level regulators, horizontal pressure pipelines with nozzles in the form of hollow nozzles, and air ducts, a splitter with canopies, guides to Adjustable height and size of the installation gap, dampers - pulp-bed mixture distributors over the aeration area in the form of double-grate grates with adjustable gaps between rows of grates, circulation channels for collecting circulation load, circulation channels formed between the bottom of the chamber and the false bottom separation compartments, devices for the selection of working fluid and chamber waste, made of funnels and grooves with increasing cross-sectional area during the movement of products nogons, gutters for receiving a froth product and a pulp outflow pocket with a gate, characterized in that, in order to reduce the energy intensity of the flotation process, to increase the specific and overall performance and reliability of the flotation machine, it is equipped with nozzles that connect the nozzles-nozzles with pressure piping made in the form of eccentrically and hermetically connected cylinders with a common upper generator and diameters decreasing in the course of the working fluid flow and a constant specific cross-sectional area The nozzle-nozzle arriving at each subsequent flow of the working fluid flow, while the specific cross-sectional area of the discharge pipeline is 2.5-6 times larger than the cross-sectional area the nozzle outlet nozzles and nozzles are located vertically at the base at the end of each cylinder along the flow of the working fluid and are made with a length increasing along the flow by the amount of decreasing cylinder diameter; the nozzles are nozzles made with guide elements in the shape of a groove the sides diverging along the flow at an angle of 15-30 ° to its axis with a concave along the flow and flat in cross section of the bottom, divided by wedge-shaped dividers along an even number of equal widths e expanding channels adjoining the narrowed concave part to the perimeter of the nozzle outlet nozzle, part of the bottom of the guide element located after the concave part, is made straight, inclined at an angle of 45-60 ° to the nozzle axis and directed to the slit between the aerator chambers and the bottom of the compartments at an angle of 30-45 ° to the horizontal plane, the central divider is located on the axis of the guide element directly behind the outlet nozzle of the nozzle and divides its bottom along the entire length, and the lateral dividers The opposite sides of the dividers, as well as the sides of the guide element and the opposite walls of the dividers are at an angle of 1-2 ° to each other, and the height of the dividers at the end of the straight part of the bottom of the guide element is greater than or equal to the magnitude of the quotient from dividing the cross-sectional area of the outlet of the nozzle-nozzle by the total width of the channels at this point of the bottom, and the concave part of the bottom of the guide element is made not less than the projection of the outlet Versions of the nozzle-nozzle on the concave bottom in the aerators of the flotation compartment and at least half of the projection of the outlet of the nozzle-nozzle in the aerators of the f / utation-separation compartments, the nozzle-nozzles in the latter are made with two guiding elements adjacent narrowed concave parts one to another, at an angle of 180 ° and jointly to the outlet of the nozzle-nozzle along an axis parallel to the longitudinal axis of the aerator chamber.  7 8 10 FIG. five FIG. 7 Fig.8 31 37 J7 ShigE 19ypy is pr Ё7 41 / th FIG C6 /four Phage. AND § "OS 26 FIG. 13