Method of three-stage technological parameters optimisation of centrifugal enrichment for recovery of precious metals in mineral form from ores, tailings from processing of embedded copper-nickel ores of norilsk deposits
SUBSTANCE: invention relates to the mining industry and can be used to increase the extraction of valuable elements from ores and products of their processing, in particular for the recovery of precious metals in mineral form and in part of sulphides of copper, nickel, iron from old tailings of the preserved tailing dump located in the Norilsk industrial district. The method of three-stage process optimisation of the parameters of the centrifugal enrichment for the recovery of precious metals in the mineral form from ores, tailings during processing of embedded copper-nickel ores of Norilsk deposits comprises selection of its own minerals of platinum group metals in the gravity concentrate before the flotation enrichment operation at a weight ratio of the amount of sulphides and magnetite and the amount of oxides of silicon and aluminium in the initial ore or tailings less than 1:2, the size of 30-65% class less than 74 microns. Isolation of own minerals of platinum metals is carried out at the value of the centrifugal Froude number of 11.75 and ratio of this value to the fluidising water pressure of 0.085 kPa. The method of optimising the parameters of centrifugal enrichment comprises the sequence of operations on the centrifugal separators, designed for continuous operation in industrial environments. At the first step an optimum accumulation time of the concentrate is determined. At the second step the optimum speed of jets of water or optimal water flow through the openings to the separator bowl inter-ripple space is selected. At the third stage the speed of jets of water or water flow through the openings to the separator bowl inter-ripple space is stepwise increased, starting with the optimal water flow, defined in the second step and the optimum time interval of accumulation of concentrate defined in the first step.
EFFECT: improving the efficiency of the recovery of precious metals from ores, tailings from the processing of ores of Norilsk deposits, as well as improving the efficiency of the optimisation parameters of centrifugal enrichment.
3 cl, 2 dwg, 4 tbl
Method three-stage process parameters optimization of centrifugal enrichment for the recovery of noble metals in mineral form of ores, tailings from processing of disseminated copper-Nickel ores of the Norilsk deposits.
The invention relates to the mining industry and can be used to increase the recovery of valuable elements from ores and products of their processing, in particular for the recovery of precious metals in mineral form and partially sulphides of copper, Nickel, iron from old tailings suspended tailings located in the Norilsk industrial district.
To achieve high performance when the centrifugal enrichment is necessary to consider the mineral composition of the original product, the deportment of precious and non-ferrous metals, their physical properties, as well as specific technical features of centrifugal separators. The invention also relates to the optimization of operating parameters of centrifugal separators, with the aim of increasing the content of precious metals in concentrate.
Tails suspended tailings (warehousing completed in 1975) have complex mineral composition, identical ore grades of industrial processed ore from Norilsk-1" from 1949 to the present. Metals lagorodnyi metals are in two forms: mineral and scattered. (Yushko-Zakharova O.E. Platinonosnost ore deposits. M., Nedra, 1975 table, 53, 57). The results of microprobe analysis in dump tails found more than 20 minerals of noble metals. The size of the mineral discharge of noble metals from 1-5 microns up to 150-200 microns, and more. Minerals of noble metals (BMP) with size more than 70 microns in beneficiation by flotation are not retrieved (Kovalenko, L.N., Blagodatin J.V., Golubeva SO, Lomteva L.L. deportment minerals of noble metals in the products of flotation enrichment of disseminated sulfide ores of the Norilsk group of fields. Obog. No. 1-2. 1993, p.18-25). Natural alloys of noble metals hard and ductile, magnetic and non-magnetic density 13-19 kg/DM3, sulfides and arsenides of noble metals, hard and brittle density 9-13 kg/DM3lost with final tailings in the form of free, large rasklapanje particles 100-400 microns and pereizluchennykh, oslavany particle size of less than 25 microns.
There is a method of enrichment material suspended tailings from the beneficiation of sulfide fine-disseminated ore from Norilsk-1". In these tails of BMP are mineral and dispersed forms.
In a known way the tails are subjected to two-stage screening for sizes 15 and 1.5 mm, to ensure the lamliang in the battery hydrocyclone diameter 250 mm size class of less than 20 microns. Drain hydrocyclone size less than 20 microns sent for storage in the tailings pond. Class larger than 20 µm (sand hydrocyclone) is directed to a centrifugal enrichment in the separators Knelson-48 for concentration of BMP larger than 70 μm. The tails of centrifugal separators is subjected to flotation with cleaning out concentrate to extract the BMP of size less than 70 μm, splices BMP with sulphides and free sulfides of copper, Nickel, iron. Concentrate centrifugal and flotation enrichment jointly referred to hydraulic copper or Nickel concentrate concentrator and later in pyrometallurgical processing (Blagodatin J.V., Yatsenko A.A., Zakharov B.A., Chegodaev E, Alekseeva LI involvement in the processing of new sources of raw materials of non-ferrous and noble metals. // Non-ferrous metals. 2003, No. 8-9. p.28-29).
The disadvantage of this method is the low content of noble metals in concentrate, and as a result, lower their removal. While in the secondary tails (after the ore enrichment and enrichment tailings from a tailings centrifugal separation and flotation) according to our research, in contrast to the known method, moving, noble metals, which are classes as larger than 50 μm and less than 50 μm (table 1).
A known design of separators, kotoryjraspolagaet fine-grained material in density occurs in a centrifugal field, which acts on particles of different density and particle size in the liquid phase in a rotating operating body. To prevent compaction of the particles, under the action of centrifugal forces, merrivale space water is pumped through a large number of holes of small diameter, under pressure, in the form of thin jets to create the liquefied layer, contributing to the mixing of particles and removal from the zone of separation of particles with low density. The most widely separators canadian firm "KNELSON" (Tsarkov, VA Foreign apparatus for centrifugal separation. Gorn. 1999, No. 3, p.76-79). The main disadvantage of the separator of this type is that under the concentration therein of fine-grained materials with intense penetration of heavy particles of a particular size through hole is pumped through the fluidizing water under pressure (Bogdanovich A.V. Intensification of gravity separation in centrifugal fields. Obog. 1999 №1-2. pp.33-35). Our experience is another disadvantage is piling holes large heavy particles of minerals, which leads to the cessation of liquefaction and compaction concentrate in marripalem space. Ultimately, the quality decreases concentrate on the content of noble metals and, as a consequence, SN is the quantitative retrieval. To clean the holes involves the removal of the bowl and mechanical cleaning approximately every 240 hours. The following significant disadvantage is the long time configuration of centrifugal separators for optimal operation modes - from several weeks to several months (Mitin L.A. ON some paradoxes in hydrogermylation the process of mineral processing. Kolyma. 2003 No. 1. p.26-30). This disadvantage is further confirmed by our experience.
Known construction and domestic centrifugal separators of this type. For example, patent RU 2278735 (or patent RU 2196004 where proposed separator with the changing angle of the rotor), which in contrast to the separator of the company "KNELSON" water in merrivale space is supplied through the diffuser having a cross-sectional shape of rectangles, the water supply in merriville the space provided in the form of a pulsating flow through the source of the pulsations. The disadvantage of this separator is the complexity of the design due to the additional mechanism of pulsation and the lack of data industrial tests of the advantages of this type of separator.
Also known a method for concentrating heavy minerals by creating mineral particles in sevashrama spiral flow pulsating radial components of motion due to the creation of the internal surface of the bowl of the concentration of the grooves with a variable radius from the center of rotation of the bowl, in this separator the water in merrivale space is not available to create loosening layer (patent RU 2423183), and heavy grain minerals held a rotational component of spiral flow force. The disadvantages of this design of the separator include the following: it is unclear how discharge the concentrate, difficulty making bowls with the changing radius of the concentration of the grooves on the inner surface of the bowl, and also the lack of data industrial tests of the advantages of this type of separator.
Common drawback in the above descriptions of the designs of centrifugal separators and methods of enrichment (split)- no methods of optimization of process parameters in an industrial environment, for expediting the configuration and the operation of the separators at optimal conditions.
Closest to the proposed method on some signs and the achieved result is a method of enrichment of sulphide copper-Nickel ores containing its own minerals of platinum metals and magnetite. Prototype (patent RU 2144429).
How to retrieve valuable items from copper-Nickel ores containing its own minerals of platinum metals and magnetite, including todopoderoso, ore grinding and hydraulic classification, selection, own the different minerals of the platinum metals centrifugal separation fluidized bed in a separate concentrate prior to the flotation. The result of platinochloride the gravity concentrate, sulfide flotation concentrates, final tailings containing waste rock and magnetite. In this way the optimal modes of centrifugal enrichment for the two ore types with different amount of sulphides and magnetite to the sum of the oxides of silicon and aluminum. If the value of this indicator is less than 1:2, the ore is crushed to a particle size of 30-65% class less than 74 microns, centrifugal enrichment is carried out at the maximum value Fruta 2-10 and the ratio of this value to the pressure of the fluidizing water 0,025-0,23 kPa-1. If the value of this index is equal to or more than 1:2, the ore must be milled to a particle size of from 60 to 95% class less than 74 microns and centrifugal enrichment may be carried out at the maximum value Fruta 0,5-1,75 and the ratio of this value to the pressure of the fluidizing water 0,0058 to 0.19 kPa-1.
A serious disadvantage of the prototype is that as one of the optimization criteria selected - water pressure, which depends on the state of the holes are clogged or loose), through which the water passes to create a fluidized bed. When hammered holes and the subsequent pressing of bed in the concentration grooves, the water pressure will be given to or higher than the mode, and the flow of water will decrease and will decrease showing the oil enrichment.
The next disadvantage of the prototype is the use when conducting experiments in a laboratory model of a centrifugal separator of the company "Knelson" (manual release) with the diameter of the bowl to 190.5 mm (7.5 inches). According to literature data (Bocharov, VA, Surikov AV, Surikov V.V. analysis of the processes of separation of gold products in the KNELSON concentrators and FALKON SB. Obog. 2002, No. 2, p.19) and our experience found that the indicators for the enrichment of fine mineral raw material received at the laboratory separator greatly exceed the industrial, and the resulting optimal modes are not modeled on industrial models separators.
The next disadvantage of the prototype is using as parameter the relationship of the amount of sulfides and magnetite to the sum of the oxides of silicon and aluminum in the source power when the enrichment of ore and industrial raw materials, which is almost impossible to quickly analyze because of the time consuming analysis and quickly change the mode of operation of centrifugal separators in the General enrichment of tails from these types of ores. This parameter, the ratio of the amount of sulfides and magnetite to the sum of the oxides of silicon and aluminum will change in the common stock tails when changing the volume of ore.
The problem solved by the invention is to optimize the parameters of centrifugal is Ogadenia for improving the recovery of precious metals from the tailings from the processing of ores of the Norilsk deposits reduce the time of conclusion of process parameters on the optimal modes.
The technical result achieved by the invention consists in obtaining a concentrate centrifugal enrichment, in which the high content of precious metals (increase extraction) is achieved by operation of centrifugal separators in optimal conditions.
The problem is solved in that in the proposed method, process parameters optimization of centrifugal enrichment, according to the invention purposefully selected optimal parameters in three stages in an industrial environment: the first stage is selected accumulation time of the concentrate at a second selected speed water jets (water flow) through the holes in merrivale space of the bowl of the separator to create originoo particle layer; a third step speed jets (water flow) in an optimal period of time the accumulation of concentrate, which is defined in the first stage, to obtain the release of blocked holes from particles with a size close to the diameter of the holes which served fluidizing water.
The efficiency of the separation of grains of different densities in a rotating flow of industrial centrifugal separator depends on a large number of factors acting on the particle is:
1. Centrale the strength of (bowl diameter and number of turns);
2. the vertical velocity of flow of the pulp (volumetric capacity);
3. the pulp density and particle size of the feeding of the separator.
4. accumulation time of the concentrate;
5. flow (velocity water jets) fluidizing water through the holes in merrivale space in the zone of enrichment.
All these parameters are changeable and the limits of regulation inherent in the design of the separator, except for the size and density of the minerals in the original power of the separators. Based on literature data we can conclude that when the enrichment of fine raw materials in centrifugal separators, the magnitude of the centrifugal force or the separation factor is not the determining criterion for performance evaluation (Mitin L.A. ON some paradoxes in hydrogermylation the process of mineral processing. Kolyma. 2003 No. 1. p.29), and the magnitude of the centrifugal force of 60 g is optimal (Tsarkov, VA Foreign apparatus for centrifugal separation. Gorn. 1999, No. 3, p.77). When testing, to determine the optimal parameters and to avoid distortion of the indicators of subsequent manufacturing operations, it is necessary to keep stable volumetric efficiency and power density in accordance with the technical characteristics of the separator and the requirement of technological tools is the enrichment for a given kind of raw material.
Thus, the problem of optimizing the parameters of centrifugal enrichment in industrial conditions for fine raw materials containing precious metals in mineral form, is reduced to the determination of the accumulation time of the concentrate and flow (velocity water jets) fluidizing water miritello space.
The goal to be solved at the first and second stages, is to get the concentrate on the total content of noble metals close to their contents in copper or Nickel concentrates produced in the ore cycle of enrichment and arriving at appropriate metallurgical plants, in terms of the optimal accumulation time of the concentrate and flow (speed jets) fluidizing water.
The purpose of the third stage further significant increase in the content of the amounts of noble metals in concentrate centrifugal enrichment: by increasing the speed of the jets in marripalem space and release of holes from large particles of minerals that are several times the maximum particle size (power falling into the material, perhaps because of the non-technological parameters), recovery, liquefaction and reduce compaction of the particles concentrate in marripalem space of the bowl of the separator. (Fedotov C.V. Theory and practice of processing of gold-bearing raw materials in Centro, the panorama of the hub. The dissertation on competition of a scientific degree of the doctor of technical Sciences. Irkutsk. The yoke. 2000, p.21).
It is known that when the centrifugal enrichment of fine raw materials increases the action antisegregation forces that change the looseness of the particles in marripalem space, and they are pressed. With the reduction of the share of particles the force of friction increases. When particle sizes in the tens of micrometer friction force more energy separation, which leads to reduction enrichment (Mitin L.A. ON some paradoxes in hydrogermylation the process of mineral processing. Kolyma. 2003 No. 1. P.29).
In our case, enriched raw material containing particles less 0,074 mm in 47%, which is also the reason for the lock holes for water supply in merrivale space. Increase the amount of water (speed jets) will reduce the number of compacted zones formed due to the friction of the particles in marripalem space, and will have a positive impact on technological parameters.
When the centrifugal enrichment at the entry point of the jet in merrivale space on the particle are the opposite forces: centrifugal (F) and the power pressure water jets (F). If the centrifugal force acting on the particle, the size of which is commensurate with the size of the holes for p is giving water to liquefaction in marripalem space, exceeds the pressure force of the water jet at the entry point in merrivale space, then there is a blockage of the holes, stops liquefaction, increase of the friction force and the seal of particles in marripalem space. The centrifugal force acting on the particle is calculated by the formula:
where: F centrifugal force (H);- angular velocity of rotation of the bowl, rad/sec; V - amount of particles, m3; (to simplify the calculation, the shape of particles adopted spherical); r is the radius of rotation of the particle, m (in the calculation is the average radius of the bowl of the separator); ρtis the particle density, kg/m3(quartz, pyrrhotite, tetraberlinia); ρW- the density of liquid, kg/m3(water).
In the calculation of the rotation speed of the particle is equal to the speed of rotation of the bowl of the separator (where:- the number of revolutions of the bowl of the separator 316 rpm; π - 3,14), because the near-wall layers of fluid with particles rotate at the same angular velocity as the wall miritello space of the bowl, the inner surface of the bowl circumferential displacement fluid is only a few percent value, which can be neglected. (Lopatin A.G. Centrifugal enrichment of ores and Sands. M., Nedra, 1987 C).
where: F - force jet at which asticou, H; ρW- the density of liquid, kg/m3(water); S is the cross-sectional area of the jet, m2; V is the stream velocity, m/s. (Chugaev P.P. Hydraulics. Energoizdat,1982, p.123).
The bowl of the separator has six cumulative channels (merrivale space to concentrate, which include 1780 holes with a diameter of 1.8 mm to supply water for liquefaction.
The coefficient of kinematic viscosity of water has very low value, in the hope he is not involved (Fedotov C.V., Romanchenko A.A., Senchenko AE calculation of the velocity of the hydrodynamic flow in a centrifugal concentrator. Gorn. 1998, No. 5, p.23).
Table 2 shows the calculations of the comparative values of the centrifugal force, the force of the water jet for liquefaction at the entry point of the jet in merrivale space of the centrifugal separator for particles of quartz, pyrrhotite and terferometry.
TMF is formed from the processing of ores of the Norilsk-1 Deposit. The concentration of mineralization is petricevich and Maximovich gabbro-dolerites (country rock) (A.D. Genkin, Distler, V.V., Gladyshev GD and other Sulfide copper-Nickel ores of the Norilsk deposits. M., Nauka, 1981, P.39). Hard milled minerals that are included in their composition, have a hardness of 6.5-7 and after grinding are in large classes, their composition is quartz, light and solid, it is also difficult for hogging the. In Norilsk ores group minerals pyrrhotite are the most common, platinum presents glandular forms, of which tetraterpene, paraplatin also the most common (A.D. Genkin, Distler V.V. Gladyshev GD and other Sulfide copper-Nickel ores of the Norilsk deposits. M. Science. 1981, p.63, 113).
Table 2 shows that the centrifugal force acting on the particles of quartz or the host rocks of the gabbro-dolerites sizes up to 1.8 mm, exceeds the force of the jet at the point of its entry into miritello space at the speed of jets 1,39; 1,52; 1.67 m/sec. When the speed of the jet is 1.81 m/s the force of the jet exceeds the centrifugal force and can prevent the penetration of particles into the holes or release already clogged.
Group minerals of pyrite or other sulphides, chalcopyrite, pentlandite, cubanite) calculations can also block the inlet for supplying fluidizing water. Sulfides fragile (Doroshenko M.V., Bashlykova T.V. Technological properties of minerals. M. Power. 2007, P.24, 75, 78, 115) compared to the host rocks and hit them neosmyslennymi size more than 1.5 mm is unlikely.
The platinum minerals (ferrous form) possess ductility and can, after grinding out rasklapanje in the form of plates, scales. The size of their Deposit up to 0.2 mm (A.D. Genkin, Distler V.V. Gladyshev GD and the R. Sulfide copper-Nickel ores of the Norilsk deposits. M. Science. 1981, str), so a very low probability of blocking these particles of holes for supplying fluidizing water.
Information about the three-stage process parameters optimization of centrifugal enrichment for fine raw materials containing precious metals, including the sequence of operations in an industrial environment: in the first stage determines the accumulation time concentrate on the second pick up speed water jets (water flow) through the holes in merrivale space of the bowl of the separator, at the third stage speed increase speed jets (water consumption), since the optimal volume of water defined in the second stage, and the optimal time of accumulation of the concentrate defined in the first stage, in the patent and scientific literature is not revealed. Not revealed details about the popularity of the distinctive features of the proposed method in the application of manual mode water flow (velocity jets) upwards, starting from the optimal and the optimal period of time the accumulation of concentrate, when used in industrial and research in laboratory conditions. Therefore, the claimed method meets the criterion of "Inventive level of the. The effectiveness of the proposed method is the resultant action of the three-stage process parameters optimization of centrifugal enrichment.
The method is as follows. Factory for the processing of tailings suspended tailings (Cheburashka YEAR, Geona NI analysis of the implementation of multipurpose industrial investment project to enrich shows of platinum-metal deposits. // Gold and technology. 2010, No. 2, p.39) works as follows. The tailings slurry from the career fields are classified according to the class of 1.8 mm on the vibrating screens. Underflow is directed to a desliming in two hydrocyclone battery 16 pcs. in each battery. The diameter of the hydrocyclone 250 mm Sand hydrocyclone test Peresecina sampler (PRO-6M), private clipped sample divider (GFC-4P) and dehydrated (OP-3M). Control the density of the sand hydrocyclone perform radioisotope densitometer (Berthold LB-444-01), the volume of sand is controlled by an electromagnetic flowmeter (ABB FSM4000/SE41F) and is pumped to the pressure fullpotential and next 4 centrifugal separator (KC-XD48), working within the given time to the program, excluding the moments of their simultaneous discharge of the concentrate. The concentrate also try Peresecina sampler control density radioisotope densitometer to measure the s volume of pulp electromagnetic flow meter. Tails centrifugal separators process collector (butyl xanthate), blowing agent (pine oil) and spend the bulk flotation followed by two cleanings. Concentrate centrifugal enrichment and concentrate the second peredishki unite and pumps is directed to the hydraulic system concentrates produced from raw ore. The main flotation tails together with plums hydrocyclones and the positive product of screens sent to the existing tailings pond.
In the first stage, in industrial conditions, we can determine the optimal accumulation time concentrate at 10, 16, 20, 24, 30, 44, 60, 120 minutes. During a predetermined period of accumulation are all four of the separator, except for the accumulation time at 10 and 16 minutes, where at this time there are two separator in order to avoid simultaneous unloading. When determining the optimal accumulation time flow of fluidizing water (speed jets) is the same for all time regimes and equal 22,71 m3/h (1,39 m/sec). Consider the procedure for accumulation time 24 minutes In all four of the separator KC-XD48. On the control panel interface of each separator is set accumulation time concentrate 24 minutes Running all four are made every 5 min to eliminate simultaneous unloading. The sampler is brought is not the reading operation. Recorded readings of density meters, flow meters installed on the Sands of hydrocyclones (power separators KC-XD48) and concentrate centrifugal enrichment. When the centrifugal enrichment of fine raw material parameter in determining the recovery of precious metals is contained in the concentrate, the weight of the concentrate varies slightly. During the experiments, the reliability of the obtained results it is necessary that each separator has produced three unloading. After the experience of the newly recorded readings of density meters, flow meters. Removed sample source power and concentrate from the dehydrator, they are drying, weighing, cutting, division for sieve and chemical analyses on non-ferrous and precious metals. Similarly perform actions when different accumulation time of the concentrate. According to the results of measurements of the contents of noble metals graph that determines the optimal accumulation time of the concentrate.
In the second stage, also in an industrial environment, determines the optimum water flow rate (speed jets) for liquefaction in marripalem space at the optimum accumulation time determined in the first stage. Procedure during the second stage optimization is similar to the first. In all modes there are four separator. N is the control panel interface is set to the desired flow rate of fluidizing water for all four separators. Water consumption (speed jets) varies according to the experiments, m3per hour (m/sec): 22,71 (1,39); 24,98 (1,52); 27,25 (1,67); 29, 52 (1,81); 31,79 (1,94); 36,34 (2,07). According to the results of measurements of the contents of noble metals graph that determines the optimum water flow rate (speed jets).
At the third stage, also in an industrial environment, to obtain reliable results, spend four experience.
The first experience standard, with a duration of 240 hours is optimal parameters obtained in the first and second stages of the optimization with a constant flow of fluidizing water, the procedure is similar to the first stage of optimization, only constantly all four of the separator. The samplers are transferred to the carrying mode sampling interval cutoff increment 6 minutes of the Second experience, also 240 hours. The procedure is similar to the first experience. Time accumulation concentrate 24 min, speed the flow of fluidizing water 24,98 m3per hour (jet speed of 1.52 m/sec) for 10 min, following 10 min of the flow rate of fluidizing water 27,52 m3per hour (the speed of a jet 1.67 m/s) and 4 min water flow 29,52 m3per hour (the speed of a jet is 1.81 m/s)at which the force of the jet exceeds the centrifugal. The third experiment 240 hours. The procedure is similar to the second experience. Time accumulation concentrate 20 min, speed the flow of fluidizing water 24,98 m3/h (SC is the speed of the jet of 1.52 m/sec) for 10 min, the following 6 min of the flow rate of fluidizing water 27,52 m3per hour (the speed of a jet 1.67 m/s) and 4 min water flow 29,52 m3per hour (the speed of a jet is 1.81 m/s). Fourth, the experience of 240 hours. The procedure is similar to the second experience. Time accumulation concentrate 18 min, speed the flow of fluidizing water 24,98 m3per hour (jet speed of 1.52 m/sec) for 10 min, following 6 min of the flow rate of fluidizing water 27,52 m3per hour (the speed of a jet 1.67 m/s) and 2 min water flow 29,52 m3per hour (the speed of a jet is 1.81 m/s).
A specific example of using the proposed method in an industrial environment below in the text, figures and tables.
1. The first stage of optimization. The proposed method. Determination of the optimal accumulation time at a constant flow rate of fluidizing water (stream velocity). The flow of fluidizing water 22,71 m3/h (1,39 m/sec). The time of the experiments the accumulation of concentrate 10, 16, 20, 24, 30, 44, 60, 120 minutes based On test results, we plot the dependence of the substance amount of noble metals (platinum, palladium, gold) in concentrate centrifugal enrichment (Figure 1).
On the graph you can see that the optimal accumulation time of the concentrate is in the range of 20-24 min with the total content of noble metals on the level of 25.7-of 26.1 g/so
2. The second stage of optimization. The proposed method. Determination of the optimal flow of fluidizing water (speed jets) is miritello space at the optimum accumulation time, defined in the first stage. Water consumption (speed jets) varies according to the experiments, m3per hour (m/sec): 22,71 (1,39); 24,98 (1,52); 27,25 (1,67); 29, 52 (1,81); 31,79 (1,94); 36,34 (2,07). According to the results of measurements of the contents of noble metals is plotted according to the content amount of noble metals (platinum, palladium, gold) in concentrate centrifugal enrichment, which is determined by the optimal flow rate (speed jets) fluidizing water (Fig.2). From the graph it is seen that the optimum water flow rate is within 22,7-27,25 m3/h (1,39-1.67 m/sec). The concentrate has the total content of noble metals within 26,34-26,85 g/so
3. The third stage of optimization. The proposed method. Conducted four experience in an industrial environment for 240 hours each, to improve the reliability of the results (table 3).
The first experience of the standard, when the accumulation time concentrate 24 min with a constant flow of water 24,98 m3per hour (jet speed of 1.52 m/sec), which is defined as optimal on the first and second stages of the optimization. This experience can be attributed to the prototype. The mineral composition of Sands of hydrocyclones (source powered centrifugal enrichment) for all four experiments: pentlandite - 0,3%; chalcopyrite - 0,2%; pyrrhotite - 4%; magnetite - 5%; SiO2- 40%; Al2O3- 10%. The content of particles less than 74 μm is 50%. The ratio of the sum Sul who feeds and magnetite to the sum of the oxides of silicon and aluminum is equal to 0.19; criterion froda (calculation according to patent No. 2144429, prototype) for industrial separator KC-XD48 equal 11,75. The criteria fruda to the pressure of the fluidizing water before discharge of concentrate (in the experiments, the final pressure fluidizing water before discharge of concentrate of 116.7-137,4 kPa) is 0,0855 kPa pressure 137,4 kPa.
Technological parameters of the first experiment is shown in colour and the platinum metals in table 3. The total content of platinum and palladium in concentrate 17.1 g/t, the degree of enrichment of 14.5 (content amount of the platinum metals in the food separator to their contents in the concentrate), the extraction amount of 1.94%. Low, despite the fact that the parameters of the centrifugal enrichment is close to or within the claims of the patent prototype for the original power centrifugal enrichment with respect to the amount of sulfides and magnetite to the sum of the oxides of silicon and aluminum is less than 1:2.
The second experience. Time accumulation concentrate 24 min. water Flow rate (speed jets) for liquefaction in marripalem space - step. Within 10 min water flow rate (speed jets) 24,98 m3/min (1.52 m/sec), following 10 min 27,52 m3/min (1.67 m/s) and 4 min flow rate 29,52 m3/min (1,81 m/sec). The total content of platinum and palladium 62 g/t, the degree of enrichment 46,6, removing the amount 6,53%. From literature data it is known that platinum this is ichnogenus field is composed of mineral forms and 87% of it is in classes of size -0,14+0.05 mm, palladium presents mineral forms and 74.8% of it is in the same size class. (Dodin D.A. Izoitko VA Superlarge man-made deposits of platinum metals. Obog. 2006, No. 6, p.20).
Thus, it can be stated that in the second experiment with speed water flow should result in an increase of this productive platinum metals size class.
Granulometric composition of concentrates centrifugal enrichment with constant speed and water flow (experiments 1 and 2) are shown in table 4, where it is shown that in the second experiment there was an increase of the content of the productive class size on the platinum metals on to 5.55%, due to the use of speed of water flow (velocity jets) and the release of blocked holes from particles of minerals with a size close to the diameter of the holes which served fluidizing water, reducing the number of compacted zones formed due to the friction of the particles in marripalem space that had a positive effect on technological parameters. In the proposed method, three-stage process optimization obtained real best modes of centrifugal separators in an industrial environment, ready to use, in a short period of time, without prior laboratory studies with unrealistic targets.<> The third experiment. Time accumulation concentrate 20 min. water Flow rate (speed jets) for liquefaction in marripalem space - step. Within 10 min water flow rate (speed jets) 24,98 m3/min (1.52 m/sec), the following 6 min 27,52 m3/min (1.67 m/s) and 4 min flow rate 29,52 m3/min (1,81 m/sec). The total content of platinum and palladium and 49.2 g/t, the degree of enrichment 42,4, removing the amount of 6.4%. The total content of platinum and palladium in concentrate somewhat smaller compared to the experience of the two, by reducing the accumulation time of the concentrate, but removing the remained at the same level.
The fourth experience. Time accumulation concentrate 18 min. water Flow rate (speed jets) for liquefaction in marripalem space - step. Within 10 min water flow rate (speed jets) 24,98 m3/min (1.52 m/sec), the following 6 min 27,52 m3/min (1.67 m/s) and 2 min flow 29,52 m3/min (1,81 m/sec). The total content of platinum and palladium 31 g/t, the degree of enrichment 29,2, removing the amount 4.09 to%. The total content of platinum and palladium in concentrate is less in comparison with the second and third experiments, by reducing the total accumulation time of the concentrate, reduce operating time when the speed of the jet is 1.81 m/s, when there is a release of blocked holes for liquefaction miritello space of the separator and increase the number of compacted zones formed due to C the friction of the particles in marripalem space.
|The distribution of metals by class size in the tails after the ore enrichment and enrichment tailings from a tailings centrifugal separation and flotation.|
|№ p/p||Class size (mm)||Output %||Content, %, g/t||Distribution %|
|3||-0,14+0,09||21,05||0,08||0,05||0,71||0,49||1,2||13,42||16,79||19,65||13,90||the value of 16,81|
|5||-0,071+0,05||12,58||0,11||0,05||0,64||0,71||1,35||11,05||there is a 10.03||of 10.58||12,04||11,30|
|7||The original product||100||0,12||0,063||0,76||0,74||1,5||100||100||100||100||100|
|Estimated comparative values for particles of quartz, pyrrhotite, terferometry centrifugal force and the force of the water jet for liquefaction at the entry point of the jet in merrivale space of the centrifugal separator KC-XD48*|
|№ p/p||Particle size (mm)||VST=1,3 9 m/s (22,71 m3/h)||VST=1.52 m/sec (24,98 m3/h)||VST=1.67 m/s (27,25 m3/h)||VST=1,81 m/s (29,52 m3/h)|
|Quartz, density 2.7 g/cm3the hardness is 7.|
|1||1,8||6,21||4,91||1,26||6,21||by 5.87||1,06||6,21||7,1||1,14||6,21||8,33||of 1.34|
|3||1,0||1,06||4,91||4,63||1,06||by 5.87||5,54||1,06||7,1||to 2.06|
|4||0,5||0,13||0,13||by 5.87||45,15||of 0.133||7,1||4,11|
|Pyrrhotite, with a density of 4.7 g/cm3the hardness is 4.|
|Titrate aroplatin, density of 15 g/cm3, malleable.|
|4||0,5||1,1||4,91||4,46||1,1||by 5.87||5,34||1,1||7,1||6,45||1,1||8,33||EUR 7.57|
|*Notation: VST - speed sigalda jet of water at the entrance to the annular channel (merrivale space) separator;|
F centrifugal force acting on the particle;
Fc - power jet sigalda water acting on a particle of spherical shape;
|Industrial comparative performance of four centrifugal separators KC-XD48, at a constant speed and the flow rate (speed jet) fluidizing water through the holes in merriville the working space of the cone. Optimal and constant conditions of each experience: time of 240 hours, the speed of rotation of the bowl 316 rpm (acceleration-60g), the solid content in the source power 34-36%.|
|no experience||Name of product||Output %||Content, %, g/t||Extract, %||Conditions of experiments|
|Tails||99,866||99,69||99,79||94,78||99,56||98,06||1. quantity of water (W) for 24 min - 24,98 m3/hour.|
|2. The performance of a single separator (Q). - 68,3 t/h|
|3. Speed water jets (V) through hole - 1.52 m/sec|
|Tails||99,86||99,6td align="center"> 99,4||86,0||97,56||93,47||1.W within 10 min - 24,98 m3per hour, 10 min - 27,52 m3per hour, 4 min - 29,52 m3per hour|
|2. Q. - 68,0 t/h|
|3.V - 10 min - 1.52 m/sec|
|V - 10 min - 1.67 m/s|
|V - 4 min - 1,81 m/s|
|Tails||99,849||99,56||99,37||84,91||98,72||93,60||1. W for 10 minutes - 24,98 m3per hour, 6 min - 27,52 m3per hour, 4 min - 29,52 m3per hour|
|2. Q. - 64,7,0 t/h|
|3.V - 10 min - 1.52 m/sec|
|V - 6 min - 1.67 m/s|
|V - 4 min - 1,81 m/s|
|Tails||99,86||99,52||99,3||89,58||98,78||to 95.91||1. W for 10 minutes - 24,98 m3/hour 6 minutes - 27,52 m3per hour, 2 minutes - 29,52 m3per hour|
|2. Q. - 66,7,0 t/h|
|3. V - 10 min - 1.52 m/sec|
|V - 6 min - 1.67 m/s|
|V - 2 min - 1,81 m/s|
|Granulometric composition of concentrates centrifugal enrichment (experiments 1 and 2)|
|the number of experience||Name of product||Classes size, mm %|
|1||Concentrate centrifugal enrichment (standard)||26,87||53,77||19,36|
|2||Concentrate centrifugal enrichment||25,11||59,32||15,57|
1. Method three-stage process optimization PA is amerov centrifugal enrichment for the recovery of precious metals in mineral form of ores, tails in the processing of disseminated copper-Nickel ores of the Norilsk deposits and including the selection of proper minerals of the platinum metals in the gravity concentrate to the operation of flotation enrichment when the mass ratio of the amount of sulfides and magnetite and the amount of oxides of silicon and aluminum in the original ore or tailings is less than 1:2, size 30-65% class less than 74 microns, characterized in that the selection of proper minerals of the platinum metals is carried out at a value of centrifugal criterion Fruta 11,75 and the ratio of this value to the pressure of the fluidizing water 0,085 kPa, as well as three-stage process parameters optimization of centrifugal enrichment for fine raw materials containing precious metals in mineral the form, which includes the sequence of operations in centrifugal separators, designed for continuous operation in industrial conditions: in the first stage determines the optimal accumulation time concentrate on the second pick the optimum speed water jets or the optimum water flow rate through the holes in merrivale space of the bowl of the separator, at the third stage speed increase the speed of the jets or water flow through the holes in merrivale space of the bowl of the separator, since the optimal volume of water specified on the WTO the stage and the optimal period of time the accumulation of concentrate, defined in the first stage.
2. The method according to claim 1, characterized in that when the enrichment of fine raw materials containing precious metals in mineral form, in centrifugal separators stepped increase the flow of fluidizing water or the speed of the jets in marripalem space separator at time intervals: within 10 min and subsequent 10 min and 4 min, for 10 min and subsequent 6 min and 4 min, for 10 min and subsequent 6 min and 2 min at the optimum accumulation time.
3. The method according to claim 1, characterized in that when the enrichment of fine raw materials containing precious metals in mineral form, in centrifugal separators stepped increase the flow of fluidizing water or increase the speed of the jets in marripalem space of the separator bowl, starting with the lowest optimal and ending water flow or stream velocity at which the force of the jet exceeds the centrifugal force to the particles of the host rocks, commensurate with the diameter of holes for supplying fluidizing water.
SUBSTANCE: method includes enrichment of sludge by hydrocycloning, filtration of an obtained pre-concentrate, which represents a mixture of large fractions of a sedimentary and a part of a floated material, dehydration, drying, granulation, drying. To hydrocycloning supplied is sludge with a ratio of S:L=1:2. Hydrocycloning is carried out in 4 stages. Discharges of each stage of hydrocycloning are combined in the pre-concentrate. An initial pulp is supplied to the first hydrocyclone at a temperature of 50÷70°C and under pressure of 2.5÷4 atm. A ratio of sand muzzle to the draining one in all the hydrocyclones constitutes 0.5÷0.66:1. Drying of granules is realised at a temperature up to 150°C to avoid loss of noble metals in sublimates.
EFFECT: maximal extraction of noble metals from the obtained concentrate.
4 cl, 5 tbl
SUBSTANCE: method of determining gold mineralisation of rock formation comprises multistage crushing of raw material to fractions of the size not greater than 0.5 mm, the subsequent classification of the resulting material and its processing with bromoform. Classification is carried out by sedimentation with the separation of the material class of -0.05+0.02 mm of water discharges, followed by drying and sieving the remaining material with the separation of the fraction -0.5 +0.1 mm and -0.1+0.05 mm, treating each of the resulting classes with 10-30% alcohol solution of bromoform. Sedimentation is carried out once with the accumulation of sediment for 15-20 min and repeatedly for 3-5 minutes, followed by the integration of the water discharges obtained during it.
EFFECT: increase in reliability of determining of gold areas and determining areas of gold mineralisation.
2 cl, 1 ex
SUBSTANCE: proposed process comprises ore screening, magnetic separation to obtain magnetic and nonmagnetic fractions, grinding, hydraulic classification, thickening and drying. Martite ore is first subjected to screening with separation to three size classes, i.e. coarse, intermediate and fine. Coarse class is directed to sensory separation to obtain tails and concentrate to be additionally ground and screened to intermediate and fine classes. Intermediate class is conveyed to metallurgical processing while fine class is subjected to pelletising. Hydrohematite ore is first subjected to screening with separation to three size classes, i.e. coarse, intermediate and fine. Coarse class is directed to sensory separation to obtain tails and concentrate to be additionally ground and screened to intermediate and fine classes. Intermediate class is conveyed to metallurgical processing. Portion of fine class is directed for pelletising while another portion is directed to magnetic separation, its magnetic fraction is fed for pelletising. Nonmagnetic fraction is ground with mixing by grinding medium and directed to hydraulic classification of the first stage. Classification sands are returned to the mill. Sink is fed to second stage of classification, its sink being used as 3rd grade pigment after thickening and drying. Sands of second classification are fed to second stage of grinding with mixing by grinding medium. Product ground at second stage is subjected to 3rd stage hydraulic classification, its sands being dried and used as 2nd grade pigment. Thereafter, sink is thickened, dried and used as 1st grade pigment.
EFFECT: simultaneous production of several grades of iron oxide pigment and finished stock for metallurgy.
2 cl, 1 dwg, 1 tbl
SUBSTANCE: invention relates to the field of dressing of hard minerals, namely, to methods for enrichment of rare-metal ores. The method of dressing of eudialyte ores includes application of electromagnetic separation in intense field with separation of nepheline-feldspar concentrate into non-magnetic fraction and subsequent electric separation of magnet fractions with production of aegirine and eudialyte concentrates. In the head of the process they perform separation of ore with total secondary characteristic radiation Kα1-series of elements of strontium, yttrium, zirconium and niobium in the energy range of 13.0-17.5 keV.
EFFECT: increased efficiency of extraction of eudialyte concentrate, reduced costs for grinding and crushing of ore, and also reduced quantity of cleaning operations.
1 dwg, 1 tbl, 1 ex
SUBSTANCE: invention relates to concentration of minerals and can be used to increase the yield of valuable products, particularly, zinc and lead, by flotation. Proposed method comprises flotation, processing of pulp-bearing solution by pulse discharges and precipitation of solid phase. Processing of pulp-bearing solution is carried out by pulsed high-voltage discharges of specific energy of 8.6-11.2 kJ/dm3 fed directly into pipeline communicating flotation machine with settle-thickener. Action of pulsed high-voltage discharges is brought about provided that: R/Ro=10.4 where: R is the radius of efficient wave effects; Ro is the spacing between electrodes and R.
EFFECT: higher intensity and rate of deposition of disperse particles from foam after flotation.
2 cl, 3 dwg, 1 tbl
SUBSTANCE: method includes treatment of coal extracted from coal deposits for opening of its splices with rock. At the same time the coal is placed in layers at the intermediate storage, arranged on the southern slope of a knoll (mountain, hill) or a pit heap, the site of which has an angle of inclination 10-25°, exposed in spring-autumn periods to solar radiation with the number of "thawing-freezing" cycles with transition of temperature via 0°C equal to at least 7. Besides, the thickness of the coal layers is taken on the basis of the calculation sufficient for daily heating-cooling, and after thermal processing the coal is shipped from the warehouse for subsequent demineralisation.
EFFECT: increased opening of coal splices with rock.
FIELD: machine building.
SUBSTANCE: proposed machine comprises cylindrical housing, initial material feed pipe, material discharge pipe and rotor drive. Initial material distributor composed of fixed cone is arranged directly above the rotor. Circular flanges are arranged at housing sidewall while fine dusty fraction discharge pipe is arranged at housing top section. Rotor fitted on the shaft in said housing is shaped to cylinder in height equal to rub-off zone and equipped with radial blades. It includes industrial blower is communicated with pipe discharging the fine dusty fraction along with airflow. Initial material feed pipe is arranged directly above initial material distributor. Finished product discharge pipe is arranged at housing bottom section.
EFFECT: higher efficiency of rubbing-off and separation.
FIELD: process engineering.
SUBSTANCE: invention relates to combined methods of separation of solid materials, particularly, to processing of radio electronic scrap. Proposed method comprises primarily two-step separation of solid materials by hammer crushers to required size, magnetic and screen separation of ground scrap with subsequent pneumatic classification by bulk density of oversize and undersize products of screen classification. Note here that ground scrap fraction of boundary size obtained at pneumatic classification is subjected to additional grinding at ball mill to size of nonmetallic component of not over 1 mm. To isolate metallic component of processed scrap aforesaid ground fraction is subjected to pneumatic classification by bulk density.
EFFECT: higher efficiency of processing.
FIELD: process engineering.
SUBSTANCE: invention relates to mining and can be used for extraction of valuable components and products of their processing, particular, for extraction of copper, nickel and iron sulphides and noble metals from aged tailings of suspended tailing pit of in cryolite zone of Norilsk deposits. Dressing module comprises open-pit field, two or three dredges, beach pump station consisting of stationary and vibratory screens, sunk basin with overflow pocket communicated by gravity feed hydraulic transport with open-pit field. Besides, it comprises two pump, pressure five-jet pulp separators communicated with vibratory screens, sunk basins and pump communicated with batteries of desliming 250 mm-dia hydraulic cyclones with their sand outlets connected via sunken basins and controlled-delivery pumps with said pressure five-jet pulp separators and, further, with rotary separators. Tailings from the latter are communicate by gravity feed hydraulic transport via appropriate sunk basin and controlled-delivery pump with mechanical camber flotation machine consisting of 130 m3-chambers. Concentrate outlet is communicated with appropriate sunk basin and controlled-delivery pump and, further, with pneumomechanical camber flotation machine consisting of four first-cleaner 17 m3-chambers. Concentrate outlet is communicated with appropriate sunk basin and controlled-delivery pump and, further, with pneumomechanical camber flotation machine consisting of four second-cleaner 8 m3-chambers. Module includes one or two giant jets installed in open-pit field lane, distribution box to direct portion of warm desliming drains by gravity feed hydraulic transport to open-pit field to accelerate tailing thaw and wash-off at two or more point of the pit and further direction to pit lane, screens mounted at beach pump stations, said screens feature 12-16 mm square meshes. Main flotation chamber has three chambers. Desliming hydraulic cyclones feature two cones with 20-10 deg-taper angle. Beach pump station sunk basin overflow pocket is additionally communicated by gravity feed hydraulic transport with two or three points of open-pit working board to return excess pulp into lane and to accelerate tailing thaw and wash-off.
EFFECT: higher yield and quality of flotation, decreased losses of valuable elements.
FIELD: process engineering.
SUBSTANCE: set of invention relates to concentration of minerals and can be used at coal dressing plants. In compliance with first version, proposed plant comprises pulp feed line connected with inlet of first hydraulic cyclone for slurry classification with its sand outlet connected to first stage helical separator inlet. Said plant is equipped with second hydraulic cyclone for thickening of fine concentrate and helical separator of second stage. First stage helical separator outlet for concentrate is connected with arched screen inlet with its undersize outlet connected with fine concentrate sump. Sump fine concentrate outlet is connected with second hydraulic cyclone with its sand outlet connected with second stage helical separator inlet. Second stage separator fine concentrate outlet is connected with centrifuge inlet. Oversize screen outlet is connected with the same inlet of centrifuge. Centrate outlet of centrifuge filtration section is connected with fine concentrate sump. Centrate outlet of centrifuge precipitation section is connected with high-ash sludge sump. Note here that outlets of both cyclones and outlet of second stage separator are connected wit appropriate lines of feeding drainage into thickener. In compliance with second version, proposed plant incorporates no second stage helical separator while peck outlet of second cyclone is directly connected with centrifuge inlet.
EFFECT: extraction of coal particles sized to 0,04-1 (2) mm in one process step.
4 cl, 2 dwg
SUBSTANCE: centrifugal-segregation concentrator comprises a housing consisting of a conical part, the means for loosening the material, the means for tangential supplying water through openings, the means for loading the enriched products and unloading of products of dividing, in which the concentrating rings with slotted openings are mounted, adjacent to the inner surface of the cylindrical part of the housing, between which the means for loosening the boundary layer of the material is located, and a conical part which is connected to the cylindrical part of the housing. The conical part of the housing is provided with a device for concentrating solid particles, made with the ability to move in the axial (vertical) direction in the form of a perforated inner cone. The device for concentrating solid particles is connected to the device for unloading the concentrate. The device for concentrating solid particles is formed from a set of rigidly interconnected rings forming the perforated cone abutting against the inner surface of the conical housing.
EFFECT: increased recovery of heavy minerals, increase in productivity by improving the conditions of segregation of particles to improve the efficiency of the enrichment process.
2 cl, 5 dwg
FIELD: process engineering.
SUBSTANCE: invention relates to loose material size, shape and density separation and can be used to classification of abrasive grains in production of abrasive tools. Proposed device consists of the rotor fitted on shaft and engaged with motor shaft via clutch, intake chutes, tray coupled via pipeline with pump. Besides, classifier comprises suspension mixer communicated by pipeline with pump to optimise suspension state prior to feeding to rotor and composed by mixing device, motor and valve. Tray-type intake chutes with baffle plates are arranged one above the other on bed its height being adjusted by pins. Rotor represents a composite surface in the form of flat disc nearby rotational axis and hemisphere with locating conical hole for fitting o the shaft. Rotor shaft runs in rolling bearings inserted via sleeve in bearing barrel secured with cover and motor at said bed mounted with the help of posts on the plate.
EFFECT: higher efficiency of classification to size and shape and process efficiency.
6 cl, 2 dwg
FIELD: process engineering.
SUBSTANCE: dressing device comprises pulp feeder, rotary actuator, at least, two coaxial cylindrical shells, one being partially fitted inside the other with clearance and device bottom section being open toward annular trough furnished with discharge pipes. Pulp feeder is composed of intake conical funnel aligned with said shells. Funnel outlet diameter corresponds to section diameter of larger shell. Rotary actuator is composed of tangential pipes arranged tangentially to intake funnel case and directed in direction of earth rotation forces acting on pulp, and vaned swirler with vanes secured to shell inner surfaces to swirl said pump in the same direction. One of the walls of annular flute is composed by smaller shell wall section locked in chamber of overlying shell. Every annular flute is communicated with separate vibration concentrator by separate distribution bin shaped to prism with section shaped to a symmetric triangle with its vertex directed downward, separated by inner web into equal-volume compartments. Slot is arranged between bin outer inclined wall bottom edges and its inner web, slot width making, at least, three maximum sizes of fractions fed from annular flute. Bin inner web is secured to swing at horizontal shaft arranged across the vibration concentrator flute through angle not exceeding that between said inner web and outer inclined wall. Annular flute discharge pipe outlets are located above bin intake with their lengthwise axis belonging to vertical plane crossing bin swinging horizontal axis.
EFFECT: higher quality of dressing.
FIELD: process engineering.
SUBSTANCE: invention relates to powder metallurgy, particularly, to sizing of polydisperse materials. Proposed method comprises feeding polydisperse materials in fluid flow in sizing zone at volumetric flow rate, creating outlet flow in said zone to flow counter action of centrifugal field forces at speed approximating to that material presser size particles. Besides it comprises discharging first outlet flow counter action of centrifugal field forces from said zone and discharging material particles therefrom, their size exceeding preset pone, in direction of centrifugal field forces. Note here that fluid without material is fed at preset volumetric flow rate in sizing zone at section located behind the polydisperse material entry along centrifugal filed forces. Proposed method is implemented using the device including hollow rotor with axle made up of cylindrical vessel, means to feed polydisperse materials in fluid flow, sizing assembly arranged in said rotor to make chamber in said rotor along its rotational axis. It includes also, at least, one sizing channel perpendicular to rotor rotational axis that has first outlet open to said rotor chamber, and second outlet. Note here that second outlet flow area is smaller than that of first outlet to create hydraulic resistance to fluid flow at second outlet. It has first inlet for feed of polydisperse materials in fluid flow arranged between said outlets and communicated with means to feed polydisperse materials in fluid flow to rotor. Note here that sizing channel has second inlet to feed clean fluid therein arranged behind first inlet in direction from rotor rotational axis to communicate with means to feed polydisperse materials in fluid flow to rotor.
EFFECT: higher efficiency.
16 cl, 4 dwg, 3 ex
FIELD: process engineering.
SUBSTANCE: invention relates to mining, particularly, to concentration of minerals and may be used for density separation of solids at polymetallic, tin, and gold-mining factories. Concentrator comprises rotor made up of inside truncated taper with bottom on smaller base and outer shell arranged concentrically and having annular slot between said shell and taper larger base edge. Outer shell has annular flanges on sides of inside taper larger base and inside tape smaller base. Inside taper and outer shell are rigidly interconnected.
EFFECT: simplified design, higher reliability and quality.
3 cl, 1 dwg
FIELD: process engineering.
SUBSTANCE: invention relates to extraction of gold and platinum-containing sands and may be used in ponds cleaning systems, construction, etc. Proposed separator comprises cylindrical case with deflectors, mineral suspension discharge branch pipe, flaps with drives arranged at cylindrical case bottom base and in mineral suspension discharge branch pipe. Metal inclusion detector made from non-conducting material is arranged on case outer surface and connected to delay line. It comprises also means to discharge light and heavy fractions. Heavy fraction discharge means represents taper section with screw groove on inner surface communicated with annular collector of valuable components and filled with fluid mot mixing with mineral suspension. Heavy fraction discharge means is made from bimetal while screw groove cavity features dovetail shape. Aforesaid drives represent drive motors with flap displacement speed regulator. The latter is connected with flow rate regulator connected to flow rate pickup. Flap displacement speed regulator is connected with delay regulator output with detector connected thereto. Flow rate and delay regulators comprise interconnected comparison and setting units. Comparison unit is connected with input of electronic amplifier equipped with unit of nonlinear feedback circuit. Electronic amplifier output is connected with magnetic amplifier input. Magnetic amplifier incorporates rectifier with its output connected to speed regulator made up of powder electromagnetic couplings of flap drive mechanisms.
EFFECT: higher and invariable efficiency of centrifugal separator.
FIELD: process engineering.
SUBSTANCE: invention relates to concentration of minerals to density by flushing granulated, powder and lumpy materials exploiting centrifugal force and may be used for production of gravity concentrate containing heavy minerals, particularly, noble metals and their compounds, with continuous yield of preset amount of enriched product. Proposed concentrator comprises coaxial rotors with different angular rotation speed and auger fitted on inner rotor outer surface. Rotors are driven by independent drive motors with smooth rpm adjustment. Rotors are made up of cylindrical drums. Inner rotor inner surface represents a cone made from polyurethane. Aforesaid auger has two coils.
EFFECT: higher yield of heavy minerals and process efficiency.
FIELD: process engineering.
SUBSTANCE: invention relates to mining, in particular, to devices intended for extraction of heavy noble metals. Proposed device comprises frame accommodating working member made up of bowl, squeezer rolls arranged on platform rotating about vertical axis, and drive consisting of two motors. To increase effects of squeezer rolls on pulp via working member wall, said member is made up of paraboloid of revolution while every roll is divided into separate disks fitted on axle.
EFFECT: higher efficiency of extraction.
3 cl, 2 dwg
FIELD: process engineering.
SUBSTANCE: invention relates to dressing of mineral resources and may be used for concentration of ores and sands containing heavy fine-grain minerals. Proposed concentrator comprises support frame, stationary housing with flange joint, tailings discharge flute, taper settling chamber with permeable side surface, inserted screen cone and pressure taper mask fitted on hollow shaft, hydraulic seal between stationary housing and rotary settling chamber, tripping water feed device, moving cone with concentrate discharge communicated with stationary housing via rubber diaphragm. Tripping water feed device tangentially feed water into housing hydraulic seal zone at least six points along housing perimetre. Housing hydraulic seal is made up of one revolving lower and one stationary rings. Revolving ring outer surface incorporates radial vanes arranged along perimetre.
EFFECT: higher efficiency of dressing, simplified design.
2 cl, 4 dwg
FIELD: process engineering.
SUBSTANCE: invention relates to dressing of minerals containing fine gold. Centrifugal concentrator comprises receiving bin, working member made up of rotary perforated encased cup, central bearing tube, discharge flute to discharge tails, device to discharge dressed concentrate, and drive. It comprises also bearing frame, clarified water radial deflector provided with safety replaceable coarse screen arranged inside perforated cup to flow over clarified water in to said central bearing tube, centrifugal vaned pump to feed clarified loosening water. Pump drive shaft is coupled with perforated cup running in bearings of central bearing tube. Tube bottom is provided with openings for centrifugal pump. Receiving bin is equipped with distribution pipes that allow uniform feed of initial liquefied material in working zone, and arranged above radial deflector. Concentrate discharger is arranged inside central bearing tube.
EFFECT: higher efficiency of dressing.
FIELD: equipment for concentration of ore and sand comprising free heavy metals and minerals.
SUBSTANCE: centrifugal concentrator has working tool rotated by drive mechanism with flexible coupling therebetween. Working tool is made in the form of rotating ellipsoid and is equipped with device for oscillating of working tool relative to axis of rotational drive. Oscillating device is formed as lever for connecting working tool with stem performing reciprocating motions provided by electric engine and crankshaft.
EFFECT: increased efficiency in enrichment and concentration of metal.