Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B07—SEPARATING SOLIDS FROM SOLIDS; SORTING
  • B07B—SEPARATING SOLIDS FROM SOLIDS BY SIEVING, SCREENING, SIFTING OR BY USING GAS CURRENTS; SEPARATING BY OTHER DRY METHODS APPLICABLE TO BULK MATERIAL, e.g. LOOSE ARTICLES FIT TO BE HANDLED LIKE BULK MATERIAL
  • B07B4/00—Separating solids from solids by subjecting their mixture to gas currents
  • B07B4/08—Separating solids from solids by subjecting their mixture to gas currents while the mixtures are supported by sieves, screens, or like mechanical elements

Definitions

• the invention relates to the field of mineral processing and can be used to create mobile processing plants for processing and classification of raw materials into fractions in almost any weather conditions, including at ambient temperatures from -50 to +50 ° FROM.
• the technology for the enrichment of raw materials should be universal, easily tunable for processing various types of mineral raw materials, and at the same time be suitable for the enrichment of materials with different densities (coal, ore, industrial waste and non-metallic raw materials).
• the processing process should provide for the ability to quickly and smoothly change technological modes depending on the properties of the processed raw materials, requirements for the quality of processed products, etc., which will allow creating modular mill concentrates with a low level of capital costs for their delivery and installation.
• the technology for enrichment of raw materials must be highly efficient, ensuring high quality of the products obtained, and so that, when it is applied, only those wastes that are not suitable for further processing or direct use remain.
• the technology for the enrichment of raw materials should be all-weather and year-round so that the process does not take place seasonally with temporary attraction of labor resources, but proceeds constantly - with year-round employment of the local population.
• the technological cycle of enrichment of raw materials should include a range of ambient temperatures from -50 to +50 ° C and should allow the equipment to be placed outdoors or using light type shelters.
• the method allows year-round enrichment of raw materials under the open sky or using light type shelters.
• the main disadvantage of the known method of enrichment of raw materials is the low efficiency of the process of separation of products, a high degree of infection of heavy products with light fractions, because the process is carried out in the product layer located on the sieve.
• An increase in the layer thickness necessary for the formation of separate layers from products of different densities leads to its high resistance, and as a consequence of its low degree of loosening and low fraction separation efficiency.
• the known method of enrichment of raw materials does not allow for highly efficient separation of the raw materials into fractions due to the high influence of the moisture content of the raw material on the process.
• the known method allows the year-round enrichment of raw materials in the open air or using light type shelters, as well as the quick adjustment of the technological process for processing various types of mineral raw materials by changing the air flow rate.
• the main disadvantage of the known method is its insufficiently high productivity of the selection of particles of a given size, which is due to the following reasons.
• the basis of this invention is the task of increasing the productivity of the known method while maintaining the efficiency of the separation process.
• the specified task in the method of pneumatic enrichment of mineral raw materials comprising placing the enriched raw material on a breathable surface intersecting the separation chamber with an ascending air flow, lifting light fractions from a breathable surface, made in the form of a conveyor, passed below the lower base a separation chamber in which a volume pseudo-boiling layer of particles of a given density is formed by selecting the air flow velocity, into which particles of lower density are passed through it, and then they are transferred from the separation chamber to the gravitational deposition chamber by an ascending air flow, it is decided that the separation chamber is installed obliquely with respect to the conveyor plane, while its lower base is parallel to the conveyor plane, and the acute angle formed between the longitudinal walls of the separation chamber and its base is directed in the direction of movement of the conveyor.
• the indicated location of the separation chamber and its base relative to the surface of the conveyor can significantly reduce the compaction of the pseudo-boiling layer at the rear (along the conveyor movement) wall of the separation chamber with an increase in conveyor speed, due to its more uniform distribution over the entire cross-sectional area of the separation chamber .
• the separation chamber is divided inside by longitudinal parallel bulkheads into two or more successively and / or parallel sections, with the lower bases of the sections parallel to the plane of the conveyor, and the upper bases of the sections combined inside the separation chamber by a common air stream transporting particles into the gravitational deposition chamber.
• This is achieved due to the fact that in the separation chamber, designed to separate particles according to a given density boundary, it is possible to organize multi-stage selection of these particles by simultaneously exposing the particles to several successive vertical flows, each of which carries the particle into its section .
• the separation chamber selects particles with a density lower than a given density, for example, 1, 4 g / cm 3 . Since the separated material may contain a large number of particles with a density less than the separation density, the separation of the separation chamber into sections having equal or different cross-sectional areas and, accordingly, the same or different flow rates in them, will allow for the gradual separation of particles with density less than the specified, thereby reducing the load on the last chamber and increase the efficiency of separation of particles with a density of up to 1.4 g / cm 3 .
• different sections of the separation chamber can have the same or different height of the base of the sections above the conveyor, thereby ensuring the creation of a pseudo-boiling layer of the same or different density in each section of the separation chamber, which will allow in the first sections of the separation cameras to provide preliminary separation of particles with a density significantly lower than the specified, and in the last sections to conduct a more accurate and efficient separation of particles according to lotnosti.
• the separation of the separation chamber into sections located along the direction of movement of the conveyor allows you to eliminate the unevenness of the air velocity field in the separation chamber in cross section (along the conveyor), and the separation of the chamber into sections located across the direction of movement of the conveyor allows you to eliminate the unevenness of the air velocity field in separation chamber, both in the transverse and in the longitudinal section (perpendicular to the conveyor), as well as to prevent the transverse and longitudinal flows of pseudo particles fluidized bed and ensure its uniformity over the entire cross section of the chamber.
• the separation chamber installed obliquely with respect to the plane of the conveyor, and the plane of its base is parallel to the plane of the conveyor can significantly (2 times or more) increase the productivity of the proposed method compared to the prototype, while maintaining or even increasing the high selectivity of the pneumatic method of mineral processing, which has no analogues among the known methods currently used in pneumatic separation plants, which means that meets the criterion of "inventive step".
• FIG. 1 shows a block diagram of a plant for pneumatic enrichment of mineral raw materials, on which the separation chamber is vertical, as in the prototype, and arrows show the trajectories of particles of enriched mineral raw materials that are sucked from the breathable conveyor and their interaction with the air stream and particles of a pseudo-boiling layer.
• FIG. 2a and 26 are views A showing the distribution of particles in a pseudo-boiling layer at low and high conveyor speeds: at a high speed of the conveyor, the pseudo-boiling layer is shifted to the rear (in the direction of conveyor movement) wall of the separation chamber.
• FIG. Figure 3 shows a fragment of the inlet part of a pneumatic separation unit, on which the separation chamber is made oblique, and arrows show the trajectories of the enriched mineral raw materials particles sucked from the air-permeable conveyor and their interaction with the air flow and particles of the pseudo-boiling layer.
• the uniform distribution of the layer itself in the plane of the base of the chamber is also shown, where: 12–126 are the walls of the separation chamber; 13 - direction of movement of the suction air flow in the separation chamber; 14 - an air-permeable conveyor with particles of enriched mineral raw materials 15; 16 - plane of the lower base of the separation chamber; 17- 176 - directions of motion of particles of enriched mineral raw materials inside the chamber.
• FIG. Figure 4 shows a fragment of the inlet of the installation for pneumatic separation, on which the separation chamber is made inclined and consists of three successively installed sections located along the conveyor, the lower bases of the sections being at the same height relative to the conveyor, where: 18 are the walls separation chamber; 19a – 19c — directions of motion of the suction air flows in sections of the separation chamber; 20a-20c are the planes of the lower bases of the sections of the separation chamber; 21 - breathable conveyor with particles of enriched mineral raw materials 22; 23-35 - the direction of motion of the particles of the enriched mineral raw materials near the lower bases of the sections of the separation chamber and in the pseudo-boiling layer.
• FIG. Figure 5 shows a fragment of the inlet of a pneumatic separation unit, on which the separation chamber is made inclined and consists of three successively installed sections located along conveyor, and the lower bases of the sections are at different heights relative to the conveyor, where: 36 - walls of the separation chamber; 37a - 37c — directions of motion of the suction air flows in sections of the separation chamber; 38a-38c are the planes of the lower bases of the sections of the separation chamber, installed at different heights relative to the conveyor 39 with particles of enriched mineral raw materials 40.
• FIG. 6 is a fragment of the inlet part of the pneumatic separation unit, on which the separation chamber is inclined and multi-sectional, consisting of three successively mounted sections located along the conveyor and three successively installed sections located across the conveyor, with lower bases all sections are at the same height relative to the conveyor, where: 41 is a multi-section inclined separation chamber, consisting of three rows of sections 43 '- 45', located along the direction the movement of the breathable conveyor 42 and three rows of sections 43 "- 43" "located across the direction of its movement, and Fig. 7 is a drawing explaining the distribution of particles of enrichable mineral raw materials within sections 43" - 43 "".
• the distribution of particles in the pseudo-boiling layer corresponds to the figure in figa, and with increasing speed of the conveyor 3, the distribution of particles takes the form shown in the figure in fig. .2b, i.e. the pseudo-boiling layer is shifted to the rear (in the direction of conveyor movement) wall of the vertical chamber. This decreases the efficiency of the separation process in a vertical chamber. This is explained by the fact that during the movement of particles 4 in a pseudo-boiling layer, there arise both streams providing separation of particles by density, and stray flows.
• a light particle moving along the 6d trajectory can interact with a high-density particle moving along the 6d trajectory, and taking into account the presence of the horizontal velocity of the 6d particle and its higher density, there is a possibility that this particle will carry with it a particle moving along the trajectory 6g and remove it from the space of the separation chamber.
• the separation chamber be inclined, as shown in FIG. Due to the fact that the area of the absorbed base 16 is larger than the area of the base 5 of the vertical separation chamber (FIG. 1), and the wall of the separation chamber 12a is inclined towards the movement of the conveyor 14, the movement of particles in the pseudo-boiling layer is formed by two flows: ascending directed along the inclined wall 12a and vertical descending towards the inclined wall 126, which leads to an organized circulation of particles.
• the pseudo-boiling layer under the influence of the particle flow 17a, it is shifted to the front (in the direction of conveyor movement) wall 126 and, thereby, the pseudo-boiling layer is aligned with the entire area of the base 16 of the separation chamber.
• FIG. 6 shows another embodiment of the inventive method, in which an inclined separation multi-sectional chamber is presented, consisting of three successively mounted sections 43 '- 45' located along the conveyor 42 and three successively installed sections 43 "- 43"", located across the conveyor, and the lower bases of all sections are at the same height relative to the conveyor 42.
• This arrangement of sections inside the separation chamber allows at the same time to ensure uniform the pseudo-boiling layer, both in the longitudinal and in the cross section of the vertical chamber.
• 7 shows the distribution of particles of enriched mineral raw materials inside sections 43 "- 43""located across the conveyor 42.
• a pilot plant for the separation of slag from ferrochromic production was manufactured with the aim of further producing ferrochrome.
• the process of pneumatic enrichment was carried out on a separation inclined chamber, which consisted of 3 consecutive sections (Fig. 4), and the angle of inclination to the conveyor plane was 55 °.
• slags Prior to the start of pneumatic processing, slags were previously crushed to a particle size of 0–6 mm and fed to a conveyor belt, with a web made of mesh with a 1 mm mesh, 600 mm wide, and a speed of 0.5–1.5 m / s.
• the inclined separation chamber was made with a rectangular cross-section of 600x150 mm and a height of 900 mm and was divided into 3 equal section sections inside the partitions.
• the chamber is connected by air ducts to gravity deposition chambers with a diameter of 1200 mm and a height of 2500 mm.
• the air flow in the separation chamber was selected so that a product was released in the chamber that did not contain ferrochrome grains and had a density of less than 2.9-3.5 t / mZ, and metal ferrochrome with insignificant inclusions of slag remained on the conveyor after passing through the chamber, which was a commodity concentration Tom.
• the indicated design of the separation chamber made it possible to evenly distribute the pseudo-boiling layer and increase the productivity of the installation 2.2 times as compared to a single rectangular vertical separation chamber with a cross section of 600x150 mm and a height of 900 mm.

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• Engineering & Computer Science (AREA)
• Mechanical Engineering (AREA)
• Combined Means For Separation Of Solids (AREA)
• Preparation Of Fruits And Vegetables (AREA)
• Separation Using Semi-Permeable Membranes (AREA)
• General Preparation And Processing Of Foods (AREA)

Priority Applications (5)

Applications Claiming Priority (1)

Publications (1)

Family

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Family Applications (1)

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Citations (6)

Family Cites Families (6)

• 2016
  • 2016-12-27 EA EA201800423A patent/EA036686B1/ru not_active IP Right Cessation
  • 2016-12-27 EP EP16925969.4A patent/EP3563939B1/de active Active
  • 2016-12-27 WO PCT/RU2016/000937 patent/WO2018124910A1/ru active Application Filing
  • 2016-12-27 CN CN201680091198.6A patent/CN110022994B/zh active Active
• 2019
  • 2019-02-11 ZA ZA2019/00871A patent/ZA201900871B/en unknown

Patent Citations (6)

Non-Patent Citations (3)

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