RU2140327C1 - Method of enriching fine-fraction concentrates - Google Patents

Abstract

FIELD: mining industry. SUBSTANCE: method, in particular, can be used for enriching fine-fraction rock mass containing chemically unbound minerals or metals directly from mineral deposits and from man-caused rejects and concentration plant tails. Initial rock mass is subjected to calibration, mixing with working liquid, step-by-step size and density sorting in ascending current in vertical stepped column, and sieving concentration of each sorted fraction, after which concentrate is finely adjusted in the form of undersize. Finest fractions are sorted by precipitation in oblique canals of replaceable lamination units. Size and density of sorted fractions are controlled by varying intake and pressure of working liquid and choosing precipitation area, dimensions of canals and angle of inclination of canals in lamination units. EFFECT: increased isolation of minerals, preferably fine-class minerals. 17 cl, 5 dwg, 5 tbl

Description

 The invention relates to the field of enrichment of finely fractional mineral-bearing rock mass in order to extract minerals or metals, for example gold, in a free, chemically unbound state.

 The invention can be used to enrich and extract useful minerals or their concentrates, both directly from the fine fraction of the original rock mass extracted from the subsoil, and to work with the waste of its technological processing at mining enterprises.

 The invention can be used in deposits where the extraction of minerals is considered economically impractical due to the low recoverability and large technological losses on existing mining equipment, for example, placer deposits of fine and fine gold.

 The invention can be used to enrich and isolate useful minerals (or metals) from the original rock mass, provided that the particle density of the extracted mineral (or metal) exceeds the particle density of the host rock by two or more times.

 The invention can be used to isolate minerals or their concentrates from the original rock mass and waste from its industrial processing, both independently and as part of the technological lines of mining and processing enterprises, to create both laboratory and industrial plants.

 A device is known for hydraulic classification of a mineral-containing (or metal-containing) material into two fractions (a.s. N 388788, B 03 B 7/00, 1973), according to which the classification is carried out in a stepped column, in an upward flow of water with the last air supply to create a suspended layer of classified particles at the bottom.

 The disadvantages of the known device are the limited number of classification fractions, the possibility of carrying out small particles of the allocated mineral (or metal) by the water-air flow (flotation process), the complexity of setting up the device in order to obtain uniformity in the granulometric composition of the fine or large fractions of the allocated minerals (metals) or their concentrates in the process of classification, additional energy costs for compressor equipment in the case of using the device as an industrial installation edstvenno on-site field development.

 A known method of enrichment of fine-grained concentrates, including calibrating the initial rock mass, mixing it with a working fluid, stage-by-stage classification in a vertical stepwise working column according to particle size distribution and density, in an upward flow, subsequent enrichment of each classified fraction with a refinement, grinding of large fractions and their re-classification into working column (RF patent 2057594, B 03 B 9/00, 1994), which is the closest analogue to the proposed method and adopted as a pro totipa.

 The disadvantages of the prototype can also include a limited number of fractions of the classification due to the inability to control their size and density.

 The objective of the invention is to increase the extraction of useful minerals, mainly small classes.

 The specified technical result is achieved by the fact that in the method of enriching fine fraction concentrates, the classification of the smallest particles is carried out by deposition in the inclined channels of removable laminarization units located in the upper part of the working column, and the particle size distribution and density of the classified fractions are controlled by changing the flow rate and pressure of the working fluid supplied to the column bottom, and the choice of the deposition surface area, the channel size and the angle of the channels in the laminarization blocks, and after The eggs carry out the final refinement of the concentrate in the form of an undergrate product.

The specified technical result is also achieved by the fact that:
- laboratory determined particle size distribution and the content of the allocated mineral, which is in the original rock mass in a free finely dispersed form, as well as the particle size distribution of the host rock mineral,
- determines the coefficient of equidivision for the particles of the mineral and the host rock in the working fluid,
- the entire initial rock mass is calibrated to a size not exceeding the largest particle size of the allocated mineral,
- the calibrated rock mass is conventionally divided into several fractions, according to the particle size distribution, with the definition of the boundary grain in each fraction and the coefficient of equidivision in such a way that in each fraction the largest particle of the extracted mineral was equal to the smallest particle of the host rock,
- calibrated rock mass is mixed with water, maintaining the ratio T: W = (1: 5) - (1:10), to ensure fluidity of the slurry and gravity feed to the classification,
- particles classified in the column according to fractions are automatically removed from the classification sections by the blades of a rotor rotating inside the column, and the blades are present only in the cylindrical sections of the column,
- classified particles are removed from the classification column through windows in the working sections of the column,
- particles leaving the windows through inclined sealed working arms by gravity flow into concentrate collectors, which are sealed containers with shut-off valves at the inlet and outlet, and are also equipped with hydraulic locks,
- laminarization units are installed in the transitional conical sections of the working column,
- the concentrate from the collectors, corresponding in size to the selected fractions of the particle size distribution, is dispersed on the sieves, and the mesh size for the concentrate of each collector is equal in size to the smallest rock particle.

In addition, this result is achieved due to the fact that the calculation of the hydraulic and geometric parameters of the working column is based on the average final velocity of the constrained incidence of particles v _{st of a} certain fraction (boundary grains) according to the conditional division in accordance with the guest size distribution.

где v_o - конечная скорость свободного падения зерна, м/с,
θ - коэффициент разрыхления, зависящий от скорости восходящей струи,
п - показатель степени, зависящей от размера, плотности и формы частиц, п = 5-7.The value of v _article is determined by the formula Lyashchenko:

where v _o - the final speed of free fall of grain, m / s,
θ is the coefficient of loosening, depending on the speed of the rising jet,
n is an indicator of the degree, depending on the size, density and shape of the particles, n = 5-7.

где D_в - диаметр вышестоящей (по отношению к конической секции) цилиндрической секции, м,
D_н - диаметр нижестоящей цилиндрической секции, м,
У_к - угол конусности конической секции, градус.The internal diameters of the cylindrical chambers, which are the classification chambers, are determined from the following relationship:
(D _to - d _in ) • v _{senior average} • 3600 = Q,
where D _to - the inner diameter of the cylindrical classification chamber, m;
d _in - the diameter of the rotor shaft, m,
v _{senior average} - the value (average) of the speed of constrained incidence of particles of the host rock of a certain size, classified in the calculated section, m / s,
Q - the total volume of the working fluid (water) passing through the cross section of the column from bottom to top, m ³ / h,
3600 - conversion factor (number of seconds per hour),
H - the height of the cylindrical sections is determined by the formula

where D _in - the diameter of the superior (relative to the conical section) of the cylindrical section, m,
D _n - the diameter of the lower cylindrical section, m,
At _to - the cone angle of the conical section, degrees.

 The taper angle of the conical section is selected depending on the mode of movement of the working fluid (water) from the bottom up to the working column.

где Re - критерий Рейнольдса,
v_{ст.средн.} - среднее значение конечной скорости стесненного падения зерна (частицы) в сечении нижестоящей секции рабочей колонны,
d - диаметр канала, в нашем случае d=D_к, м,
μ - кинематический коэффициент вязкости, см²/с,
условно μ примем равной 0,0131 см²/с (для воды).The nature of the pressure movement of the fluid in the closed channels is determined by the criterion (or number) of Reynolds, which is determined by the formula

where Re is the Reynolds criterion,
v _{senior average} - the average value of the final speed of the constrained fall of grain (particles) in the section of the lower section of the working column,
d is the diameter of the channel, in our case, d = D _k , m,
μ is the kinematic coefficient of viscosity, cm ² / s,
conditionally, we take μ equal to 0.0131 cm ² / s (for water).

With the laminar nature of the movement of the slurry during the transition from the cylindrical (lower) section to the conical section, the taper angle of the conical section should not exceed 12 ^o to avoid separation of the flow from the walls of the transition conical section, i.e. Y / 2 = 6.

 In this case, the parameters in the lamination units are determined by the following dependencies.

где F - площадь поверхности осаждения, м²,
V_о - количество жидкой фазы в гидросмеси, м³/ч,
v_{ст.средн.} - средняя скорость стесненного падения частиц, м/с,
X₂ - концентрация осадка в 1 кг сухого вещества на 1 кг жидкой фазы в осадке,
X₁ - концентрация суспензии до отстаивания в 1 кг сухого осадка на 1 кг жидкой фазы.The deposition surface F is determined by the Burdakov formula:

where F is the surface area of the deposition, m ² ,
V _about - the amount of liquid phase in the slurry, m ³ / h,
v _{senior average} - the average speed of constrained particle fall, m / s,
X ₂ - sediment concentration in 1 kg of dry matter per 1 kg of the liquid phase in the precipitate,
X ₁ - suspension concentration before settling in 1 kg of dry sediment per 1 kg of the liquid phase.

Knowing the value of F, one can find the number of channels N by the formula
N = F / f,
where F is the area of the sump, m ² ,
f is the surface area of the deposition of one channel, m ² .

где H₁ - высота цилиндрической секции (камеры) до блока ламиниразации, м,
D_к - внутренний диаметр цилиндрической секции, м,
d_в - диаметр вала ротора, м.The height of the cylindrical chamber to the laminarization unit installed in the transition conical section is determined by the formula

where H ₁ - the height of the cylindrical section (chamber) to the lamination unit, m,
D _to - the inner diameter of the cylindrical section, m,
d _in - the diameter of the rotor shaft, m

где L - длина канала, м,
h - высота канала,
v_{ст.средн.} - средняя скорость стесненного падения частицы, м/с,
K₂ - коэффициент, учитывающий сужение полости канала,
v₁ - скорость восходящего потока пульпы, м/с,
β - угол наклона канала к горизонтальной плоскости.The length of the channels of the laminarization unit (see Fig. 4) is determined by the formula

where L is the length of the channel, m,
h is the height of the channel,
v _{senior average} - the average speed of the constrained fall of a particle, m / s,
K ₂ - coefficient taking into account the narrowing of the cavity of the channel,
v ₁ - the velocity of the upward flow of the pulp, m / s,
β is the angle of inclination of the channel to the horizontal plane.

где Q - расход гидросмеси через сечение цилиндрической секции рабочей колонны, м³/ч,
D_к - внутренний диаметр цилиндрической секции, м,
d_в - диаметр вала ротора, м,
Кроме того, восходящий поток рабочей жидкости, поступающий снизу в классификационную колонну, для выравнивания величин скорости по сечению потока дезинтегрируется устройством в виде решетки и сетки, размещенным в нижней части колонны, а лопасти ротора имеют торцевые уплотнители для устранения эффекта перетекания гидросмеси в межлопастные пространства в процессе вращения ротора.The speed of the upstream v ₁ is determined by the formula

where Q is the flow rate of the slurry through the cross section of the cylindrical section of the working column, m ³ / h,
D _to - the inner diameter of the cylindrical section, m,
d _in - the diameter of the rotor shaft, m,
In addition, the upward flow of the working fluid coming from below into the classification column is disintegrated by a device in the form of a grating and a grid located at the bottom of the column to equalize the velocity values along the flow cross section, and the rotor blades have end seals to eliminate the effect of the flow of the hydraulic mixture into the interlobe spaces in the process of rotation of the rotor.

 The set of essential features of the proposed method exhibits new properties, consisting in the fact that the proposed combination and the sequence of the proposed operations with the rock mass create the necessary conditions and ensure high-quality separation of particles into a mineral (metal) and rock, and also allow to separate mineral particles from the rock mass (or metals) in free form or in the form of rich concentrates that cannot be isolated directly at the field by existing industrial plants, and particles minerals (or metals) of such sizes (less than 0.25 millimeters) are not shown in the characteristics of the studied samples of deposits during geological exploration for industrial development of deposits (for example, deposits of fine and fine gold).

 The proposed method of enrichment and separation of a mineral (metal) or minerals (metals) from the initial rock mass is carried out as follows and in the following sequence.

 In FIG. 1 shows a diagram of a device for implementing the proposed method.

 The device comprises a receiving hopper 1 with a slide device 2 mounted on the output pipe connecting the receiving hopper with a mixing chamber 3 having a water supply pipe 4 with a valve 5 and an output pipe with a sliding device 6.

 The outlet pipe of the mixing chamber 3 is connected by a transition sleeve 7 with the inlet pipe 8 of the working column 9.

 The working column 9 consists of a set of cylindrical and conical sections and is a sealed (with respect to water) container, closed on top by a lid 10.

 The working column 9 is the main unit of the proposed device and is a vertical hydraulic classifier, a complete calculation of its technological and structural parameters is given as an example of calculation in this patent application.

 The classification of the initial mass in the working column is carried out according to the "bottom-up" principle - the classified material enters the working column from above, and the working fluid (water) is supplied from below. The diameters of the cylindrical classifying sections of the working column increase as the flow moves from bottom to top, while the speed of the flow as the sections of the working column pass gradually decrease. With this distribution of speeds, large particles will be classified and allocated in the lower sections, and small particles, as lighter, will be carried up and classified and allocated in the upper sections of the working column. This classification scheme is called “small to large”.

The internal diameters of the cylindrical chambers (see Fig. 2), which are classification chambers, are determined from the following relationship:
(D _to - d _in ) • v _{senior average} • 3600 = Q,
where D _to - the inner diameter of the cylindrical classification chamber, m,
d _in - the diameter of the rotor shaft, m,
v _{page average} - the value (average) of the speed of constrained incidence of particles of the host rock of a certain size, classified in the calculated section, m / s,
Q - the total volume of the working fluid (water) passing through the cross-section of the column from the bottom up, m ³ / h,
3600 - conversion factor (number of seconds per hour).

Calculation of hydraulic and structural (geometric) workstring parameters are constrained by the final velocity v _st particles fall certain fraction (grain boundary) according to the conditional division in accordance with a granulometry gostirovannym next.

где v_о - конечная скорость свободного падения зерна, м/с,
θ - коэффициент разрыхления, зависящий от скорости восходящей струи,
п - показатель степени, зависящий от размера, плотности и формы частиц, п = 5-7, пример п=6.The value of v _article is determined by the formula Lyashchenko:

where v _about - the final speed of free fall of grain, m / s,
θ is the coefficient of loosening, depending on the speed of the rising jet,
n is an exponent, depending on the size, density and shape of the particles, n = 5-7, example n = 6.

 The working fluid (aqueous medium) in which the classification takes place has resistance to the particles falling in it, and the rate of drop depends on the size of the particles, their shape and density.

 When particles (grains) fall, two types of medium resistance arise: dynamic and static (viscous).

 When large grains fall at high speed, dynamic resistance prevails, which is characteristic of the turbulent flow of water around the grain, which leads to the formation of vortices and low pressure zones behind the grain.

 The fall of small particles at a low speed is due to the predominance of the viscous resistance characteristic of laminar flow of grain over water. With increasing viscosity of the medium, the resistance to the fall of small particles increases much faster than for large grains.

 At the initial moment, under the action of the gravitational force, all grains fall in the medium (water) with acceleration, but with an increase in the speed of movement, the resistance of the medium increases and quickly reaches the magnitude of the gravitational force moving the grain down. From this moment, the grain begins to move at a constant speed, called the final rate of incidence of these grains.

формула Ратингера для зерен крупнее 1 мм,

формула Аллена для зерен размером от 1 мм до 0,1 мм,
v_о=S•d²(b-1000) -
формула Стокса для зерен размерами меньше 0,1 мм,
где v_о - конечная скорость свободного падения зерен, м/с,
d - диаметр шарообразного зерна, м,
b - плотность зерна, кг/м³,
эмпирические коэффициенты для водной среды: R = 0,16; A = 1,146; S = 545.Having taken the falling grains as particles of regular spherical shape, the final free fall rates of grains v _{о are} determined by the following theoretical formulas for different grain sizes (particles):

Ratinger formula for grains larger than 1 mm,

Allen's formula for grains ranging in size from 1 mm to 0.1 mm,
v _о = S • d ² (b-1000) -
Stokes formula for grains smaller than 0.1 mm,
where v _about - the final speed of free fall of grains, m / s,
d is the diameter of the spherical grain, m,
b - grain density, kg / m ³ ,
empirical coefficients for the aquatic environment: R = 0.16; A = 1.146; S = 545.

 The final falling velocities calculated using these theoretical formulas do not coincide with the actual velocity values, since due to their shape, physical particles (as a result of mechanical grinding or in their natural forms) have a fall rate less than the theoretical value.

In addition, a consideration of the laws governing the fall of an isolated grain under free (theoretical) conditions cannot fully characterize the hydraulic classification process, in which grain movement occurs in the confined spaces of the hydroclassifier chambers (in cylindrical sections). In such a process, each grain undergoes the dynamic action of other grains upon distribution in the vertical and horizontal plane of the volume (the process of concentration diffusion), as well as the entire mass of grains as a whole. The fall of grain (particles) under such conditions is called cramped fall, the final fall velocity v _{st of} grains (particles) in such conditions are determined by the reduced empirical formula Lyashchenko:
Conditionally accepting n = 6 and putting this value in Lyashchenko’s formula, we get:
v _article = v _o × θ ³ , m / s.
Calculated by this formula, the values of the speeds v _Art. the constrained particle incidence coincides with their practical incidence rates for grains (particles) of size less than 0.1 mm.

For grains (particles) with a particle size of 0.1 mm or more, the following formula applies:
v _article = v _o × θ ² , m / s.
The value of the loosening coefficient θ varies from 0.8 to 0.95. Varying the value of θ and determining the final free fall velocity v _о for the boundary grains of a certain fraction, we find the value of v _st.red. . By analyzing the numerical values of v _st at various values from max to min values and comparing them with the value of v _st. , we can conclude that they differ by no more than 30% from both the minimum and maximum values of the constrained particle fall rates for a given fraction.

Having a value of v _senior for grains (particles) of the calculated section of the cylindrical section of the working column, we determine the diameter of the section of the cylindrical section. The calculation is repeated for each section in accordance with v _avg. and grain sizes (particles) for each section of the cylindrical sections of the working column (hydroclassifier).

где D_в - диаметр вышестоящей (по отношению к конической секции) цилиндрической секции, м,
D_н - диаметр нижестоящей цилиндрической секции, м,
У_к - угол конусности конической секции, градус.The cylindrical sections are structurally assembled (for example, by welding) with conical sections of the working column (see Fig. 2). The height of the conical section is determined by the formula:

where D _in - the diameter of the superior (relative to the conical section) of the cylindrical section, m,
D _n - the diameter of the lower cylindrical section, m,
At _to - the cone angle of the conical section, degrees.

где Re - критерий Рейнольдса.The taper angle of the conical section is selected depending on the mode of movement of the working fluid (water) from the bottom up to the working column. The nature of the pressure movement of the fluid in the closed channels is determined by the criterion (or number) of Reynolds, which is determined by the formula:

where Re is the Reynolds criterion.

 At Re <2300, the laminar motion mode; at Re> 2300, the turbulent motion mode.

v _{senior average} - the average value of the final speed of the constrained fall of grain (particles) in the section of the lower section of the working column,
d is the diameter of the channel in our case, d = D _to , m,
μ is the kinematic coefficient of viscosity, cm ² / s.

We conventionally accept the viscosity of a slurry (pulp) moving from bottom to top along the working column, due to the large value of the T: W ratio, equal to the viscosity of the working fluid (water) at a temperature of +10 ^o C, i.e. the value is assumed to be 0.0131 cm ² / s.

With the laminar nature of the movement of the slurry during the transition from the cylindrical (lower) section to the conical section, the taper angle of the conical section should not exceed 12 ^o to avoid separation of the flow from the walls of the transition conical section, i.e. Y / 2 = 6 ^o .

 This calculation procedure is repeated when calculating all conical transition sections of the working column.

Applying this technique to the calculation of the cross sections of cylindrical and conical sections of the working column, it can be noted that the values of the internal diameters D _{to the} cylindrical classification chambers increase sharply when calculating the classification chambers for small and very small classified particles of both the released mineral (metal) and the host rock . The design dimensions of the sections reach a diameter of 5-10 m, which makes the structure non-technological and difficult to transport (due to the large size) on any type of transport when using the structure as a mobile field installation.

To classify and isolate small and very small grains and reduce the dimensions of the inner diameters D _{to the} cylindrical sections of the working column, in the conical (transitional) sections, laminarization units of the hydraulic mixture flow are installed, which are narrow, isolated from each other, inclined rectilinear channels made of corrosion-resistant relative to the working fluid (water) of the material that is not subject to adhesion from the particles of the released mineral (metal) and the host rock (for example, titanium, stainless steel, eraser, etc.).

 The channels are installed at angles of inclination to the horizontal plane, exceeding the angles of repose of the grains (particles) of the material of the mineral (metal) and the rock including it, structurally these values are selected within 40-80 degrees (see Fig. 3).

 In each of the inclined channels, two oncoming flows, the laminar flow of the suspension moves upward, from which suspended particles intensively settle to the bottom of the channel. Settling to the bottom, these particles form a dense layer, which, under the action of gravitational force, falls down along the plane of the channel in the form of thin jets. Due to the laminar regime of the moving stream moving upward, the bottom sliding layer of solid particles is not stirred up, since the speed of the oncoming stream in the bottom layer is close to zero.

 The use of laminarization blocks accelerates the process of deposition and separation of small and very small particles hundreds and thousands of times, making it possible to structurally sharply reduce the dimensions of the working (classification) column.

 The calculation of the area and size of laminarization blocks is carried out in the following order and according to the following formulas.

 The hydraulic mixture moving from bottom to top along the working column is a heterogeneous liquid system with solid particles (grains) of the dispersed phase (rock and mineral or metal) and dispersion medium (working fluid). The density of the dispersed phase is higher than the density of the dispersion medium and the suspended particles settle down under the action of gravity of solid particles in suspension in a liquid medium. This deposition (or sedimentation) is called thickening or sedimentation. In practice, this method of sedimentation is used mainly for the separation of coarse suspensions, which include the hydraulic mixture, which is classified in the working column of the proposed device.

 The laminarization blocks in this regard are a compact sedimentation tank, the productivity of which depends on the deposition rate and the free surface of the sedimentation tank, with a highly developed free deposition surface F and a minimum height (channel height).

где F - площадь поверхности осаждения, м²,
V_о - количество жидкой воды в гидросмеси, м³/ч,
v_{ст.средн.} - средняя скорость стесненного падения частиц, м/с,
X₂ - концентрация осадка в 1 кг сухого вещества на 1 кг жидкой фазы в осадке,
X₁ - концентрация суспензии до отстаивания в 1 кг сухого осадка на 1 кг жидкой фазы.The deposition surface F is determined by the Burdakov formula:

where F is the surface area of the deposition, m ² ,
V _about - the amount of liquid water in the hydraulic mixture, m ³ / h,
v _{senior average} - the average speed of constrained particle fall, m / s,
X ₂ - sediment concentration in 1 kg of dry matter per 1 kg of the liquid phase in the precipitate,
X ₁ - suspension concentration before settling in 1 kg of dry sediment per 1 kg of the liquid phase.

 This formula is applicable provided that the slurry is continuously supplied to the sump and the clarified liquid is continuously discharged, the sediment can be removed continuously or periodically, as it accumulates.

Knowing the value of F, you can find the number of channels N by the formula:
N = F / f,
where F is the area of the sump, m ² ,
f is the surface area of the deposition of one channel, m ² .

 The installation of laminarization blocks can dramatically reduce the difference in the diameters of the cylindrical sections connected by one transition conical section, which will eliminate unfavorable conditions for the transition from one flow rate to another by eliminating the accumulation zones of "difficult grains", as well as increase the accuracy of separation and reduce the geometric height of the conical transition chambers of the working column.

где H₁ - высота цилиндрической секции (камеры) до блока, м,
D_к - внутренний диаметр цилиндрической секции, м,
d_в - диаметр вала ротора, м.The height of the cylindrical chamber to the laminarization unit installed in the transition conical section is determined by the formula:

where H ₁ - the height of the cylindrical section (chamber) to the block, m,
D _to - the inner diameter of the cylindrical section, m,
d _in - the diameter of the rotor shaft, m

где L - длина ламинарного канала, м,
h - высота ламинарного канала, м,
v_{ст.средн.} - средняя скорость стесненного падения частицы, м/с,
K₂ - коэффициент, учитывающий сужение полости каналами,
v₁ - скорость восходящего потока пульпы, м/с,

угол наклона каналов к горизонтальной плоскости.The length of the channels of the laminarization blocks (see Fig. 4) is determined by the formula:

where L is the length of the laminar channel, m,
h is the height of the laminar channel, m,
v _{senior average} - the average speed of the constrained fall of a particle, m / s,
K ₂ - coefficient taking into account the narrowing of the cavity by channels,
v ₁ - the velocity of the upward flow of the pulp, m / s,

the angle of inclination of the channels to the horizontal plane.

где Q - расход гидросмеси через сечение цилиндрической секции рабочей колонны, м³/ч.The speed of the upstream v ₁ is determined by the formula:

where Q is the flow rate of the slurry through the cross section of the cylindrical section of the working column, m ³ / h

D _to - the inner diameter of the cylindrical section, m,
d _in - the diameter of the rotor shaft, m

 Inside the working column 9 (see Fig. 4) there is a shaft 11, driven by a drive 12. The blades 13 are mounted on the shaft 11 with seals 14, and the blades are located in the cylindrical sections of the working column. The shaft rotation speed is selected within the range of 1-1.5 revolutions per minute.

 In the upper conical sections of the working column, as mentioned above, removable laminarization blocks 21 are placed, which are sets of rectilinear inclined channels 22 isolated from each other by hermetic filling 23, and from below the working column 9 is closed by a flange connection with a conical bottom 18, in the upper part of which a water flow disintegration device is located, consisting of a grid 19 and a grid 20.

 The lower part of the conical bottom 18 is connected via a pipe fitting with a flow meter 17 and a pressure regulator 16. The presence of a pressure regulator and a flow meter in the system for supplying working fluid from below to the working column allows you to adjust the pressure and flow rate of the fluid flow, and at the same time, the hydraulic mixture flow through which classification process.

 The combination of the possibility of changing the parameters of the working fluid flow inside the classification column (working column) with a set of interchangeable laminarization units, the various technological parameters of which (deposition surface area, channel size and angle of inclination to the horizontal plane) allows the classification of various materials in one working column, as according to their particle size distribution and their density, making the proposed device design universal and mobile in terms of applicability ology classification.

 The use of removable laminarization units with large areas of deposition surface (with compact design) and low-height laminarization channels allows the proposed classification method to be used to create mobile, mobile field installations for classifying and isolating small and very small particles of minerals (or metals, for example, fine and fine gold from alluvial deposits or from industrial dumps of their industrial mining), which cannot be allocated by existing technologies for their industrial mining chi. This is especially important for working with materials that are not amenable to enrichment by flotation.

где D_к - внутренний диаметр цилиндрической секции рабочей колонны, м,
n - число лопастей ротора.In the cylindrical sections (see Fig. 5) of the working column 9, unloading windows are made, connected to unloading sleeves 25, which are connected to concentrate collectors 26 through adapter pipes with hose valves 28. The height of the unloading windows is selected within 80-90% of the height of the cylindrical sections of the working column, and the width (length along the arc C) is determined by the formula:

where D _to - the inner diameter of the cylindrical section of the working column, m,
n is the number of rotor blades.

 The rotor 11 rotates in the casing 9 of the working column with a very low angular speed (of the order of 1-1.5 revolutions per minute), this is due to minimizing the mechanical impact of the surfaces of the moving blades on the process of concentration diffusion of particles in the inter-blade space in the cylindrical sections of the working column.

 At the ends of the blades facing the walls of the cylindrical sections of the working column, seals are installed that overlap the structural gap between the ends of the blades and the walls of the cylindrical sections and prevent the flow of the hydraulic mixture between the inter-blade spaces. Pads are made of elastic and corrosion-resistant (with respect to the working fluid) material and are attached to the blades by means of bolted joints.

 Concentrate collectors 26 are sealed cylindrical containers with conical upper and lower bottoms. In the cylindrical parts of the collectors there are inspection windows 27, as well as water supply pipes with valves 29 and water locks 30.

 The entrance and exits in the concentrate collectors are blocked by hose valves 28. When loading the concentrate collector (operating mode), the upper hose valve is open and the lower one is closed. In the mode of concentrate unloading from the collector, the upper shutter closes and the lower one opens, while water is supplied to the internal cavity of the collector from the main through an open valve 29. Water is supplied to facilitate unloading of the concentrate in the collector in the form of a dense layer of solid particles. The upper level of the concentrate in the collectors 26 is controlled through the inspection windows 27 in the bodies of the concentrate collectors.

 To prevent breakthrough of the slurry flow moving from bottom to top along the working column and to ensure the required technological classification mode, the sealed (relative to the working fluid) containers of the concentrate collectors are connected to hydraulic lock pipes made of pipes, the upper section of which is raised to the level of the hydraulic mixture runoff in top of the working column. This design provides a smooth exit of solid particles (grains) from the zones of concentration diffusion in the inter-blade space inside the cylindrical sections of the working column and the transition to the discharge sleeves 25 through the discharge windows. Under the influence of gravitational force, the particles settle on the inclined bottoms of the discharge hoses, the angle of inclination of which to the horizontal plane is 10-15 degrees greater than the angle of repose for the particles (grains) of the deposited material and gradually fall into the containers of the concentrate collectors 26.

 Concentrate collectors 26 are tied in a technological chain with serial calibrating devices 31 (such as hydraulic screens or wet screens), the under-sieve product of which is finally brought to the finishing equipment 32, for example, rich gold concentrate (after drying) is brought to magnetic gravity separators.

 Rich concentrate (or pure mineral, metal) is collected in collectors 33, and waste rock is discharged into dumps 34.

 In the process of processing fine-grained concentrates in the working column 9, in its lower cylindrical sections (one or two, depending on the particle size distribution of the initial mass and technological tasks), a large concentrate is formed, which is rock particles with particles of a mineral (or metal) embedded in it and coming through unloading sleeves 25 to collectors 26. Such a concentrate is supplied for grinding to serial devices 35 (such as ball mills, hydro-cavitation mills, etc.) and serves as a grinding product back into the receiving hopper 1.

 The supply of process water to all units is carried out by a pump 15 from a reservoir or from a water supply network.

 Technological effluents from the working column 9 and the water traps 30 of the concentrate collectors 26 are discharged to the sump 24, where the natural clarification of water occurs, which is again supplied to the device apparatuses by the pump 15.

 The method is as follows.

 The initial rock mass, previously calibrated (for example, on sieves or roar) to the size of the largest particles of the allocated mineral (or metal), the dimensions of which are determined by preliminary analyzes and laboratory processing of the original rock mass, which is in a free, chemically unbound state in its containing rock mass is fed (for example, a stacker) into the receiving hopper 1.

 At the same time, water enters the receiving hopper through the inlet pipe 4 with the control valve 5. In the receiving hopper 1, the initial mass is mixed with water (sparged) in the ratio T: W = (1: 3) - (1: 5), to ensure fluidity of the hydraulic mixture, and dosed into the mixing chamber 3. Dosing is carried out by means of a hose valve 2.

 The initial slurry flows by gravity through a hose valve 2 into the spiral labyrinth of the mixing chamber 3, in which it is additionally mixed (sparged) with water supplied from the line 4 through the control valve 5, the flow of which moves the pulp obtained during repeated bubbling to the outlet of the mixing chamber 3.

 From the outlet of the mixing chamber 3, located in the center of the conical bottom, the slurry enters the outlet pipe having an outlet hose shutter 6 connected by a transition sleeve 7 with an inlet pipe 8 mounted in a conical transition section of the working chamber 9 (second or third, counting from the bottom) .

 The working column 9 consists of a set of cylindrical and conical sections, interconnected by welding in a single structure or in separate sections, assembled into a single column on flanged joints and is a hydraulic type vertical classifier.

 The initial mass in the working column is classified according to the “bottom-up” principle - the classified material enters the working column from above, and the working fluid (water) is supplied from below by adjustable parameters. The diameters of the cylindrical classification sections of the working column increase as the flow moves from bottom to top, while the speed of the flow as the sections of the working column pass, gradually decreases. With this distribution of speeds, large particles are classified and released in the lower sections, and small particles, as lighter, are carried up and classified and allocated in the upper sections of the working column.

 Classifications and the allocation of the smallest particles ranging in size from 5 to 40 microns occur in the inclined rectilinear channels of the laminarization units of the slurry flow installed in the transitional conical sections of the working column in its upper part.

 In each of the inclined channels, two oncoming flows — the laminar flow of the suspension moves upward, from which suspended particles intensively settle to the bottom of the channel. Settling to the bottom, these particles form a dense layer, which, under the action of gravitational force, falls down along the plane of the channel in the form of thin jets. Due to the laminar regime of a moving flow moving upward, the bottom sliding layer of solid particles is not agitated, since the oncoming flow velocity is close to zero.

 In the lower cylindrical sections of the working column, where the heaviest particles “hang”, particles of the mineral (or metal, for example, gold in quartz) embedded in the rock can also be concentrated. Such particles after separation and removal from the working column are sent for further technological processing (for example, in ball or hydrocavitation mills, etc.), for grinding to a grain size disseminated mineral (or metal).

 A multi-vane rotor slowly rotates inside the working column, the blades of which push the particles “suspended” in the fluidized bed of the particle, due to the concentration diffusion process, to the discharge windows made in cylindrical sections of the working column through which the particles fall into inclined discharge sleeves connected to the collectors.

 The inlet and outlet in the concentrate collectors are blocked by hose valves 28. In operating mode, the upper hose valve is open and the lower one is closed. In the mode of concentrate unloading, after filling it, the upper shutter closes and the lower one opens, while water is supplied to the internal cavity of the collector from the main through an open valve 29. Water is supplied to facilitate unloading of the concentrate in the collector in the form of a dense layer of solid particles. The degree of filling of the collectors 26 with concentrate is controlled through the inspection windows 27 in the housings of the concentrate collectors.

 To prevent breakthrough of the slurry flow, moving up and down the working column, and to ensure the required technological classification mode, the containers of concentrate collectors are connected to hydraulic lock pipes, the upper cut of which is raised to the level of the slurry drain in the upper part of the working column. In a normal technological process, the concentrate enters the collectors from the water trap pipes and the fluid constantly expires.

 This design provides a smooth exit of solid particles (grains) from the zones of concentration diffusion in the inter-blade space inside the cylindrical sections of the working column and the transition to the discharge sleeves 25 between the discharge windows.

 Concentrate collectors 26 are tied in a technological chain with serial calibrating devices 31 (such as hydraulic screens or wet screens), which have calibrating openings for screens or grids equal in size to the largest size of the released mineral (or metal), which allows simple separation to separate free particles (grains) mineral (or metal) from the waste rock enclosing them.

 The waste rock, the particles of which are larger than the particles of the allocated mineral (or metal) by the equidistant coefficient, is transported to the dump 34.

 Particles of a mineral (or metal) in the form of an under-sieve product are final refined on special technological equipment (for example, rich gold concentrate), after drying they are brought on magnetic-gravity separators.

 Technological effluents from the working column 9 and the water traps 30 of the concentrate collectors 36 are discharged to the sump 26 for natural clarification and pump 15 to the system (reverse water supply).

 Calculation example.

 1. The source data.

1.1. The initial rock mass is the material of the tailings (technological waste) of the processing plant, the density of which is 1.02 - 1.2 t / m ³ (gravity enrichment for gold) with an average gold grade of 12.07 g / t, theoretical density of gold (chemically pure metal) is equal to 19.3 t / m ³ .

 1.2. The mineralogical composition of the tails is given in table. 1.

 1.3. The particle size distribution of the tails is shown in table. 2.

Для промежуточных частиц

где К_р - коэффициент равнопадаемости,
q_з - плотность золота, кг/м³,
q_к - плотность кварца, кг/м³,
q_в - плотность воды, кг/м³.1.4. Analyzing the data table. 1 and tab. 2, we will calculate the classifier according to two groups of particles - quartz and gold, assuming the density of gold in its natural state equal to 18000 kg / m ³ , while conditionally we will divide the particle size distribution into the following fractions (by gold particles):
+ 0.45 - - 0.063 + 0.025
- 0.45 + 0.16 - - 0.025 + 0.010
- 0.16 + 0.063 - - 0.010 + 0.003
1.5. According to the table. 1, gold particles predominate in the tails, which belong to the category of small, i.e. sizes less than 0.1 mm and particles of intermediate size - from 0.1 mm to 1 mm. Equivalence coefficient for small particles of gold and quartz (in water) according to the following formulas:
For small particles

For intermediate particles

where K _p - coefficient of equidivision,
q _s - the density of gold, kg / m ³ ,
q _to - the density of quartz, kg / m ³ ,
q _in - the density of water, kg / m ³ .

 The equidistant coefficient shows how many times in each fraction the particle (grain) of a light mineral (quartz) is larger in particle size (grain) of a heavy mineral (gold), having the same rate of fall in the working fluid (water). The mineralogical composition of the tails is dominated by particles of quartz, from which gold particles must be isolated.

формула Ратингера для зерен крупнее 1 мм,

формула Аллена для зерен размером от 1 мм до 0,1 мм,
v_o = S • d²(b - 1000)
формула Стокса для зерен размерами меньше 0,1 мм,
где v₀ - конечная скорость свободного падения зерен, м/с,
d - диаметр шарообразного зерна, м,
b - плотность зерна, кг/м³,
эмпирические коэффициенты для водной среды:
R = 0,16; A = 1,146; S = 545.1.6. Using the values of the equidistant coefficients, we take for the calculated value cr = 3.2, and using the particle size distribution data for fractions of a part of gold given in Section 1.4, we determine the sizes of quartz particles by fractions in accordance with the fractions of gold particles:
+ 1.44 - - 0.2016 + 0.08
- 1.44 + 0.512 - - 0.08 + 0.032
- 0,512 + 0,2016 - - 0,032 + 0,0096
1.7. We define the final (theoretical) particle free fall velocities by fractions, taking the falling grains as particles of regular spherical shape according to the following formulas:

Ratinger formula for grains larger than 1 mm,

Allen's formula for grains ranging in size from 1 mm to 0.1 mm,
v _o = S • d ² (b - 1000)
Stokes formula for grains smaller than 0.1 mm,
where v ₀ - the final speed of free fall of grains, m / s,
d is the diameter of the spherical grain, m,
b - grain density, kg / m ³ ,
empirical coefficients for the aquatic environment:
R = 0.16; A = 1.146; S = 545.

 The final falling velocities calculated using these theoretical formulas do not coincide with the actual values of the velocities; moreover, consideration of the laws of incidence of isolated grains cannot fully characterize the hydraulic classification process in which grains move in confined spaces of hydroclassification chambers.

The fall of grains (particles) under such conditions is called cramped fall, the final rate of fall v v _. grains (particles) in such conditions are determined by the empirical formula Lyashchenko.

Conditionally accepting n = 6, substituting this value in Lyashchenko’s formula, we obtain:
v _article = v _o × θ ³ , m / s.
Calculated by this formula velocity value v _v constrained particles fall coincide with their practical speeds fall to grain (particle) size of less than 0.1 mm.

For grains (particles) with a particle size of 0.1 mm to 12.5 mm, the following formula is used:
v _article = v _o × θ ² , m / s.
The value of the loosening coefficient θ varies from 0.8 to 0.95. Varying the value of θ and determining the final free fall velocity v ₀ for the boundary grains of a certain fraction, we find the value of v _st.red .

 The calculation results are summarized in table 3.

Analyzing the data of table 3, we can make sure that the values of v _st.max differ from the value of v _st.sredn by no more than 24.5%, which allows you to adjust v _st due to changes in the supply volume.

1.8. We define the internal diameters of the cylindrical classification chambers, are determined from the following relationship:
(D _to - d _in ) • v _{senior average} • 3600 = Q,
where D _to - the inner diameter of the cylindrical classification chamber, m,
d _in - the diameter of the rotor shaft, m, d _in = 0.05 m,
v _{senior environment} - the value (average) of the speed of constrained incidence of particles of the host rock of a certain size, classified in the calculated section, m / s,
Q - the total volume of the working fluid (water) passing through the cross-section of the column from the bottom up, m ³ / h,
3600 - conversion factor (number of seconds per hour).

где Re - критерий Рейнольдса.1.9. The nature of the fluid movement during the passage of the cylindrical sections of the working column (pressure fluid movement in closed channels) is determined by the Reynolds criterion according to the formula:

where Re is the Reynolds criterion.

At Re <2300 - the laminar motion mode, at Re> 2300 - the turbulent motion mode,
v _senior average - the average value of the final speed of the constrained fall of grain (particles) in the section of the lower section of the working column,
d is the diameter of the channel in our case, d = D _to , m,
μ is the kinematic coefficient of viscosity, cm ² / s.

We conventionally accept the viscosity of the slurry (pulp) moving from bottom to top along the working column, due to the large value of the T: W ratio, equal to the viscosity of the working fluid (water) at a temperature of + 10 ^o C, i.e. the value is assumed to be 0.0131 cm ² / s.

где D_в - диаметр вышестоящей (по отношению к конической секции) цилиндрической секции, м,
D_н - диаметр нижестоящей цилиндрической секции, м,
У_к - угол конусности конической секции, градус.1.10. The height of the conical section is determined by the formula:

where D _in - the diameter of the superior (relative to the conical section) of the cylindrical section, m,
D _n - the diameter of the lower cylindrical section, m,
At _to - the cone angle of the conical section, degrees.

1.11. The taper angle of the conical section is selected depending on the mode of movement of the working fluid (water) from the bottom up to the working column. The nature of the pressure movement of fluid in closed channels is determined by the Reynolds criterion. With the laminar nature of the movement of the slurry during the transition from the cylindrical (lower) section to the conical section, the taper angle of the conical section should not exceed 12 ^o to avoid separation of the flow from the walls of the transition conical section, i.e. Y / 2 = 6 ^o .

 This calculation procedure is repeated when calculating all conical transition sections of the working column.

 1.12. The results of calculations according to p. 1.8. - 1.11 are summarized in table 4.

1.13. Analyzing the numerical data of the table. 4, we conclude that the difference in the diameters of the cylindrical sections 5 and 6 is very large and this is due to the structurally and technologically unacceptable dimensions of the adapter (2.4524 m) and the diameter D _to section 6, equal to 3.0755 m, it is necessary to insert the laminar block into transition conical section.

 1.14. Define the geometric parameters of the laminarization unit.

где Q - расход гидросмеси через сечение цилиндрической секции рабочей колонны, м³/ч, = 0,5 м³/ч,
D_к - внутренний диаметр пятой цилиндрической секции, м,
D_к = 0,92318 м,
d_в - диаметр вала ротора, м, = 0,05 м.The speed of the upstream v _s is determined by the formula:

where Q is the flow rate of the slurry through the cross section of the cylindrical section of the working column, m ³ / h, = 0.5 m ³ / h,
D _to - the inner diameter of the fifth cylindrical section, m,
D _to = 0.92318 m,
d _in - the diameter of the rotor shaft, m, = 0.05 m

где L - длина канала, м,
h - высота канала равна 0,025 м,
v_{ст.средн} - средняя скорость стесненного падения частицы, м/с,
K₂ - коэффициент, учитывающий сужение полости каналами,
v₁ - скорость восходящего потока пульпы, м/с,
β - угол наклона каналов, равный 45^o.The length of the channels is determined by the formula:

where L is the length of the channel, m,
h - the height of the channel is equal to 0.025 m,
v _st.sredn - the average speed of constrained incidence of a particle, m / s,
K ₂ - coefficient taking into account the narrowing of the cavity by channels,
v ₁ - the velocity of the upward flow of the pulp, m / s,
β is the angle of the channels equal to 45 ^o .

где F - площадь поверхности осаждения, м²,
V₀ - количество жидкой воды в гидросмеси, м³/ч, = 0,5 м³,
v_{ст.средн} - средняя скорость стесненного падения частиц, м/с,
v_{ст.средн} = 0,000056148 м/с,
X₂ - концентрация осадка в кг сухого вещества на 1 кг жидкой фазы в осадке.The deposition surface F is determined by the Burdakov formula:

where F is the surface area of the deposition, m ² ,
V ₀ - the amount of liquid water in the hydraulic mixture, m ³ / h, = 0.5 m ³ ,
v _st.sredn - the average speed of constrained particle fall, m / s,
v _{senior average} = 0.000056148 m / s,
X ₂ - sediment concentration in kg of dry matter per 1 kg of the liquid phase in the sediment.

X ₁ - suspension concentration before settling in kg of dry sediment per 1 kg of the liquid phase.

To determine the values of X ₁ and X _{2 we} will calculate the values of the volumes of the rock mass classified in each cylindrical section, the initial data is taken from the table. 1 and p. 1.6. Calculations are summarized in table. 5, given that the rock mass of 0.2 m ³ is fed into the third (bottom) conical section mixed with water (in the form of pulp) in a volume of 0.1 m ³ , and we assume the diameter of the cylindrical section 6 to be 0.56 m.

 Analyzing the numerical data of the table. 5, you can increase the performance of the classifier "solid" up to 40 liters per hour by performing a series of tests, with laboratory processing of samples in commissioning mode.

Claims (17)

 1. A method for enriching fine fraction concentrates, including calibrating the initial rock mass, mixing it with a working fluid, phased classification in a vertical stepwise working column according to particle size distribution and density in an upward flow, subsequent enrichment of each classified fraction with a refinement, grinding of large fractions and their re-classification into working column, characterized in that the classification of the smallest particles is carried out by deposition in inclined channels of interchangeable blocks lam irrigation, located in the upper part of the working column, and the particle size distribution and density of the classified fractions are regulated by changing the flow rate and pressure of the working fluid supplied to the column from below, and by choosing the deposition surface area, channel size and their angle in the laminarization units, and after settling, the final refinement of the concentrate in the form of an under-sieve product.  2. The method according to claim 1, characterized in that the particle size distribution and the content of the allocated mineral, which is in the original rock mass in free finely dispersed form, as well as the particle size distribution of the host mineral, are determined by laboratory methods.  3. The method according to claim 1, characterized in that the coefficient of equidivision for the particles of the mineral and the host rock in the working fluid is determined.  4. The method according to claim 1, characterized in that the entire initial rock mass is calibrated to a size not exceeding the largest particle size of the allocated mineral.  5. The method according to claim 1, characterized in that the calibrated rock mass is conventionally divided into several fractions according to the particle size distribution with the definition of the boundary grain in each fraction and the coefficient of equidocity so that in each fraction the largest particle of the recovered mineral is equal to the smallest particle the host breed.  6. The method according to p. 1, characterized in that the calibrated rock mass is mixed with water, maintaining the ratio T: W = 1: 5-1: 10 (to ensure fluidity of the slurry) and gravity fed to the classification.  7. The method according to claim 1, characterized in that the particles classified in the column according to fractions are automatically removed from the classification sections by the blades of a rotor rotating inside the column, and the blades are only in the cylindrical sections of the column.  8. The method according to claim 1, characterized in that the classified particles are removed from the classification column through windows in the working sections of the column.  9. The method according to claim 1, characterized in that the particles leaving the windows through inclined sealed working arms by gravity flow into concentrate collectors, which are sealed containers with shut-off valves at the inlet and outlet, and are also equipped with hydraulic locks.  10. The method according to claim 1, characterized in that the laminarization units are installed in the transitional conical sections of the working column.  11. The method according to claim 1, characterized in that the large particles classified in the working column are further crushed, and then fed to a receiving hopper for re-classification. 12. The method according to claim 1, characterized in that the calculation of the hydraulic and geometric parameters of the working column is carried out according to the average final velocity of the constrained incidence of particles v _{st of a} certain fraction (boundary grains) according to conditional division in accordance with the guest size distribution, the value of v _st is determined by Lyashchenko’s formula

where v _about - the final speed of free fall of grain, m / s;
θ is the coefficient of loosening, depending on the speed of the ascending stream;
P - exponent, depending on the size, density and shape of the particles, P = 5-7. 13. The method according to claim 1, characterized in that the inner diameters of the cylindrical sections, which are the classification chambers, are determined from the following relationship:
(D _to - d _in ) x v _{senior average} x 3600 = Q,
where D _to - the inner diameter of the cylindrical classification chamber, m; d _in - the diameter of the rotor shaft, m;
v _st.sredn - the value (average) of the speed of constrained incidence of particles of the host rock of a certain size, classified in the calculated section, m / s;
Q - the total volume of the working fluid (water) passing through the cross-section of the column from the bottom up, m ³ / h;
3600 - conversion factor (number of seconds per hour). 14. The method according to claim 1, characterized in that the height of the cylindrical sections is determined by the formula

where D _in - the diameter of the superior (relative to the conical section) of the cylindrical section, m;
D _n - the diameter of the lower cylindrical section, m;
At _to - the cone angle of the conical section in degrees;
the taper angle of the conical section is selected depending on the mode of movement of the working fluid (water) from bottom to top along the working column, the nature of the pressure flow of the fluid in the closed channels is determined by the criterion (or number) of Reynolds, which is determined by the formula

where Re is the Reynolds criterion;
v _senior average - the average value of the final speed of the constrained fall of grain (particles) in the section of the lower section of the working column;
d is the diameter of the channel, in our case, d = D _k , m;
μ is the kinematic coefficient of viscosity, sq.cm / s, conditionally μ is assumed to be 0.0131 cm ² / s (for water)
with the laminar nature of the movement of the slurry during the transition from the cylindrical (lower) section to the conical section, the taper angle of the conical section should not exceed 12 to avoid separation of the flow from the walls of the transition conical section, i.e. Y / 2 = 6. 15. The method according to claim 1, characterized in that the classification of very small particles is carried out in laminarization units, the parameters of which are determined by the following relationships: the deposition surface F is determined by the Burdakov formula

where F is the surface area of the deposition, m ² ;
V _about - the amount of liquid phase in the slurry, m ³ / h;
v _{senior mean} - the average speed of constrained particle fall, m / s;
X ₂ - sediment concentration in 1 kg of dry matter per 1 kg of the liquid phase in the precipitate;
X ₁ - suspension concentration before settling in 1 kg of dry sediment per 1 kg of the liquid phase,
knowing the value of F, one can find the number of channels N by the formula
N = F / f,
where F is the area of the sump, m ² ,
f is the surface area of the deposition of one channel, m ² ,
the height of the cylindrical chamber to the laminarization unit installed in the transition conical section is determined by the formula

where H ₁ - the height of the cylindrical section (chamber) to the laminarization unit, m;
D _to - the inner diameter of the cylindrical section, m;
d _in - the diameter of the rotor shaft, m;
the length of the channels of the laminarization blocks is determined by the formula

where L is the length of the channel, m;
h - channel height, m;
v _st.sredn - the average speed of constrained incidence of a particle, m / s;
K ₂ - coefficient taking into account the narrowing of the cavity by channels;
v ₁ - the velocity of the upward flow of the pulp, m / s;
β is the angle of inclination of the channels to the horizontal plane,
upward flow velocity v ₁ is determined by the formula

where Q is the flow rate of the slurry through the cross section of the cylindrical section of the working column, m ³ / h;
D _to - the inner diameter of the cylindrical section, m;
d _in - the diameter of the rotor shaft, m  16. The method according to claim 1, characterized in that the upward flow of the working fluid coming from below into the classified column is disintegrated by a device in the form of a grating and mesh located in the lower part of the column to equalize the velocity values along the flow cross section.  17. The method according to claim 1, characterized in that the rotor blades have end seals to eliminate the effect of the flow of the hydraulic mixture into the inter-blade spaces during the rotation of the rotor.

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