Integrated treatment method for efficient multiphase flow separation and treatment of argillaceous sandstone uranium ore

Abstract

The present invention discloses an integrated treatment method for efficient multiphase flow grading and separation of muddy sandstone uranium ore, wherein the crushed mixed material of the muddy sandstone uranium ore is subjected to hydraulic washing and deagglomeration treatment, high-frequency linear vibration grading treatment, primary multiphase flow cyclone grading treatment, deep low-frequency high-efficiency ultrasonic scrubbing treatment, secondary multiphase flow cyclone grading treatment, jet mixing treatment, microcurrent activation treatment, tempering and concentration, and efficient squeezing solid-liquid separation treatment in sequence. The present invention realizes deep stripping of mud and sand of the crushed muddy sandstone uranium ore, fine grading and separation of materials, and at the same time, efficiently mixes and activates fine-grained muddy materials and dehydrates them deeply and efficiently. Four core materials are finally formed through continuous work, namely, coarse sand material, fine sand material, tailings dry slag and high-concentration uranium ore leaching solution, and finally realizes efficient multiphase flow grading, separation, concentration and purification treatment of muddy sandstone uranium ore, reduces the residual uranium element in the tailings, and improves the deep extraction rate of uranium ore resources.

Description

Technical Field

[0001] The present invention relates to the technical field of efficient uranium beneficiation and deep graded separation and disposal, and in particular to a method for integrated disposal of argillaceous sandstone uranium ore with efficient multiphase flow graded separation. Background Art

[0002] The efficient beneficiation and deep classification and separation of uranium resources have become the key industrial links that restrict the development of nuclear energy. At present, my country's uranium resources are generally low-grade uranium ores. With the crises of resource utilization and resource depletion, the demand for deep processing and purification technology of low-grade and low-quality uranium mining areas is becoming more and more urgent. However, the mud sandstone uranium deposits distributed in my country have loose surrounding rocks, severe mudification, complex structure, and tight combination of open-pit mining layers. In particular, fine clay particles are tightly attached to the surface of the ore particles, which seriously affects the chemical leaching of uranium ore. The leaching rate of uranium ore is low and the beneficiation cost remains high.

[0003] The existing conventional mineral processing mud and sand separation technology process mainly focuses on grinding and vibration screening classification. The process technology flow is single and extensive, and can only simply achieve large particle size classification, which is difficult to meet the needs of efficient and economic separation and uranium extraction of mud sandstone uranium ore in my country. For example, Chinese patent CN112774870A discloses a separation and pretreatment method for high-acid consumption mud sandstone uranium ore, which mainly grinds and floats the mudstone uranium ore for pretreatment and then classifies and selects it, which improves the utilization value of uranium ore to a certain extent. However, the overall grinding causes a high proportion of particle selection in the later analysis, and the process is complicated and the cost is high.

[0004] Therefore, the efficient mineral processing industry for low-grade mudstone sandstone uranium ore urgently needs to break through the technical bottlenecks of efficient stripping and separation of mud and sand, directional classification, efficient activation of particle interfaces, and uranium ore enrichment and purification, so as to improve the level of development and utilization of mudstone sandstone uranium ore. Summary of the invention

[0005] The technical problem to be solved by the present invention is to provide an integrated treatment method for efficient multiphase flow classification and separation of mud and sand in mud sandstone uranium ore, which can realize deep stripping of mud and sand in crushed mud sandstone ore, fine classification and separation of materials, efficient uniform mixing and activation of materials, and deep and efficient dehydration of fine-grained mud materials, thereby fully improving the selection efficiency of uranium ore resources.

[0006] The technical solution adopted by the present invention is:

[0007] A highly efficient multiphase flow graded separation integrated disposal method for argillaceous sandstone uranium ore comprises the following steps:

[0008] S1. The crushed argillaceous sandstone uranium ore mixture is subjected to hydraulic washing and deagglomeration treatment. The filtration particle size is designed to be N1. Particles above N1 are collected and crushed again after washing. The slurry smaller than N1 enters the next step;

[0009] S2, subjecting the slurry from S1 to high-frequency linear vibration classification treatment, the screening particle size is designed to be N2, N2<N1, and the sand material in the range of N2-N1 is collected and sent to the heap leaching process, and the mud material smaller than N2 enters the next step;

[0010] S3, the slurry material from S2 is subjected to a first-level multiphase cyclone classification treatment, and the median particle size of the classification is designed to be N3, N3<N2, and the materials in the range of N3-N2 form concentrated large-particle slurry materials and are diverted to the next step; the fine-particle light materials ≤N3 and a large amount of water overflow along the overflow port in the center of the cyclone field and are diverted to S7 for jet mixing treatment;

[0011] S4, subjecting the concentrated large-particle mud material produced in S3 to deep low-frequency and high-efficiency ultrasonic scrubbing treatment, applying low-frequency and high-amplitude ultrasonic waves to the mixed liquid, peeling off and breaking up the clay particles remaining on the surface of the sand particles, and providing high-speed stirring at the same time, finally achieving mud and sand separation to form a muddy particle mixed material;

[0012] S5, the muddy particle mixture produced by S4 is subjected to secondary multiphase flow cyclone classification treatment, and the median particle size of the classification is still designed to be N3. The clay particles ≤ N3 and a large amount of water materials stripped in the previous step overflow along the central overflow port of the cyclone field and are directed to S7 for jet mixing treatment; at the same time, the N3-N2 sand material formed by mud and sand classification enters the next step;

[0013] S6, subjecting the sand material produced in S5 to high-frequency linear vibration dehydration treatment, subjecting the material to solid-liquid separation, and collecting the material on the screen to form N3-N2 sand material with low water content, and subjecting it to centralized heap leaching process;

[0014] S7, subjecting the fine-grained mud-water mixture material of ≤N3 formed in steps S3 and S5 to jet mixing with an activator, and achieving efficient mixing of the mineral particles and the activator and chemical reaction by high-speed disturbance fluidization of a high-pressure air jet;

[0015] S8, subjecting the mixed materials in step S7 to micro-current activation treatment, accelerating the activation reaction by micro-current and finally dissolving the uranium element in the ore powder into the solution in the form of ions;

[0016] S9, further conditioning and thickening the mixed mud material after chemical leaching produced in step S8;

[0017] S10, subjecting the quenched and dense mixed slurry produced in step S9 to high-efficiency pressing for solid-liquid separation, and finally obtaining tailings dry slag with low water content and high-concentration uranium ore extract.

[0018] In the above scheme, in the secondary multiphase flow cyclone classification treatment process, an online monitoring device is set at the overflow port to monitor the material particle size information in real time. If coarse particles of N3-N2 appear in the overflow mud, it is considered unqualified, and the overflow mud is redirected to the primary multiphase flow cyclone classification for circulation treatment.

[0019] In the above scheme, a large amount of water generated in step S6 passes through the sieve plate into the water storage tank, and then flows back to the wastewater collection device for recycling after treatment.

[0020] In the above scheme, the hydraulic washing and agglomeration treatment adopts a horizontal hydraulic washing and agglomeration device, and the filtration particle size N1 is 1-4mm.

[0021] In the above scheme, the high-frequency linear vibration classification process adopts a high-frequency linear vibration classification device, the screen particle size N2 is 0.2-1mm, and the vibration frequency is 20-25Hz.

[0022] In the above scheme, the first-stage multiphase flow cyclone classification treatment and the second-stage multiphase flow cyclone classification treatment both use a cyclone, and the classification median particle size N3 of the cyclone is 40-74 μm.

[0023] In the above scheme, the deep low-frequency and high-efficiency ultrasonic scrubbing treatment adopts an energy-concentrating ultrasonic scrubbing device, which includes a scrubbing cylinder, a reverse stirring system, an energy-concentrating ultrasonic vibrator and a slurry storage tank; the scrubbing cylinder is provided with an inlet hopper and an overflow slag discharge pipe; the reverse stirring system is arranged inside the scrubbing cylinder, including a rotating shaft and at least four layers of reverse stirring blade structures arranged axially along the rotating shaft, each layer of the reverse stirring blade structure includes a plurality of blades arranged circumferentially along the rotating shaft, and the blades of the two adjacent layers of reverse stirring blade structures are inclined in opposite directions relative to the rotating shaft; the energy-concentrating ultrasonic vibrator includes an ultrasonic transducer device and an energy-concentrating vibration conduction rod, the ultrasonic transducer device is fixed to the outside of the scrubbing cylinder, and the energy-concentrating vibration conduction rod is connected to the ultrasonic transducer device and is located inside the scrubbing cylinder; the slurry storage tank is connected to the overflow slag discharge pipe, and the discharge port of the overflow slag discharge pipe is directly diverted to the slurry storage tank.

[0024] In the above solution, the angle between the blades of the reverse stirring blade structure and the rotating axis does not exceed 45°.

[0025] In the above solution, the energy-concentrating vibration conducting rod is provided with a plurality of spherical grooves at intervals along its axial direction.

[0026] In the above solution, the frequency of the energy-concentrating ultrasonic vibrator is 20-25KHz, and the amplitude is 80-100μm.

[0027] In the above scheme, the interior of the scrubbing cylinder is set to a single compartment or multiple compartments according to the production capacity requirements, and each compartment is provided with a set of the reverse stirring system and the energy-concentrating ultrasonic vibrator; when it is set to multiple compartments, an intermediate baffle is provided to divide the interior of the cylinder into multiple compartments, and a connecting channel is left at the bottom or top of the intermediate baffle to connect the compartments to each other, and the connecting channels are arranged alternately up and down to ensure that the material passes through the stirring area fully.

[0028] In the above scheme, the high-frequency linear vibration dehydration treatment adopts a high-frequency linear vibration dehydration device, the screen particle size is 0.075-0.1mm, and the vibration frequency is designed to be 30-35Hz.

[0029] In the above scheme, the jet mixing treatment adopts a pneumatic kinetic energy mixed phase flow mixing device, and the pneumatic kinetic energy mixed phase flow mixing device includes a mixing reactor cylinder, a mixed phase flow mixing injection device and a high-pressure air supply device; the mixed phase flow mixing injection device includes a fixed bracket, a mixed phase flow mixing nozzle and a pneumatic kinetic energy distributor, the fixed bracket is fixedly installed at the bottom of the mixing reactor cylinder, the mixed phase flow mixing nozzle and the pneumatic kinetic energy distributor are respectively installed on the fixed bracket, the air inlet of the pneumatic kinetic energy distributor is connected to the high-pressure air supply device, and the air outlet of the pneumatic kinetic energy distributor is connected to the high-pressure air supply device. The mixed-phase flow homogenizing nozzle is connected, and the high-pressure gas generated by the high-pressure gas supply device enters the mixed-phase flow homogenizing nozzle through the pneumatic kinetic energy distributor. In the mixed-phase flow homogenizing nozzle, the pneumatic kinetic energy is provided by the high-pressure gas jet, and the mixed slurry is contacted and mixed in the limited space in the pipeline to form a relatively low-density mixed-phase flow material, which is quickly transmitted under the action of continuous pneumatic thrust and buoyancy, and is ejected and diffused at high speed from the pipeline outlet, driving the slurry particles to form high-speed turbulence and mixed flow, so that the slurry particles and the activator are quickly mixed, completing the mutual conversion of pneumatic kinetic energy and mechanical kinetic energy of the mixed phase to realize shaftless stirring and homogenizing.

[0030] In the above scheme, the mixed-phase flow homogenizing nozzle includes a mixed-phase flow nozzle, an axial sleeve and a slurry inlet pipe which are coaxially arranged and interconnected; the upper end of the axial sleeve is fixedly connected to the mixed-phase flow nozzle, and a gap is left between the inner wall of the lower end of the mixed-phase flow nozzle and the outer wall of the upper end of the axial sleeve to form a high-pressure air chamber, and the high-pressure air chamber is provided with an air inlet joint for connecting the air outlet of the pneumatic energy distributor; the area where the mixed-phase flow nozzle is located on the upper part of the axial sleeve is, from bottom to top, a mixed flow negative pressure zone, a multiphase flow mixed flow lifting zone and a diffusion flow outlet, wherein the mixed flow negative pressure zone is connected to the high-pressure air chamber by a gap channel; the lower end of the axial sleeve is fixedly connected to the slurry inlet pipe, and a slurry inlet channel is formed inside the slurry inlet pipe and the axial sleeve.

[0031] In the above scheme, the slurry inlet pipe is a trumpet structure with a thick bottom and a thin top. The diameter D of the upper end of the slurry inlet pipe is equal to the inner diameter of the shaft sleeve. The diameter D of the upper end of the slurry inlet pipe needs to satisfy formula (1):

[0032] D≤ (1)

[0033] In the formula, Q m is the slurry design flow rate, is the advance design value; V is the lift flow rate, and the lift flow rate V is calculated according to formula (2):

[0034] V>4ω max (2)

[0035] In the formula, ω max is the maximum value of the slurry particle settling velocity ω, and the slurry particle settling velocity ω is calculated according to formula (5):

[0036] (5)

[0037] In the formula, , Re is the Reynolds coefficient, , ρ s is the density of mud and sand particles, ρ is the fluid density, d is the spherical diameter of mud and sand particles, is the kinematic viscosity coefficient of the liquid.

[0038] In the above scheme, the inner diameter of the mixed flow negative pressure zone of the mixed-phase flow nozzle gradually decreases from bottom to top, the inner diameter of the multiphase flow mixed flow lifting zone remains unchanged from bottom to top, and the inner diameter of the diffusion flow outlet gradually increases from bottom to top.

[0039] In the above scheme, the microcurrent activation treatment adopts a microelectrolysis activation device, which includes a plate-type microelectrolysis electrode, a microelectrolysis activation reaction cell and a constant current power supply; the plate-type microelectrolysis electrode is fixed at both ends of the inner side of the microelectrolysis activation reaction cell by insulating materials, and the constant current power supply is arranged on the outer side of the microelectrolysis activation reaction cell and connected to the plate-type microelectrolysis electrode through a wire.

[0040] In the above scheme, the tempering and thickening device is used for the tempering and thickening, and the pulp inlet pressure is controlled at 1.2-1.8MPa to complete the first-level pulp dehydration.

[0041] In the above scheme, the high-efficiency squeezing solid-liquid separation treatment adopts a high-pressure diaphragm filter press, and the diaphragm squeezing pressure is controlled at 1.0-1.2MPa for secondary squeezing and dehydration.

[0042] The beneficial effects produced by the present invention are:

[0043] 1. The method of the present invention adopts the idea of ​​less crushing and no grinding. The ore material is crushed to 3mm only by initial high-efficiency crushing, which reduces the ball milling process of the ore and avoids the crushing of some ore particles (74μm-3mm) that are beneficial to heap leaching to increase the amount of ore powder (-74μm). Instead, the physical stripping method is used for extreme desludging, thereby reducing the workload of chemical activation leaching and mineral processing in the later stage, thereby improving efficiency and reducing costs.

[0044] 2. The method of the present invention firstly adopts hydraulic washing and deagglomeration treatment to break up the mud clumps wrapped together by clay particles, and peels out some clay particles, which reduces the workload of subsequent ultrasonic scrubbing and improves efficiency; adopts two-stage multiphase flow cyclone classification treatment, which greatly increases the classification capacity and effect, and greatly reduces the mud content in the sand particles, and the mud content is less than 3%, which is far lower than the existing level in the domestic and foreign industries; adopts deep low-frequency and high-efficiency ultrasonic scrubbing treatment to efficiently peel off and break up the clay particles remaining wrapped on the surface of the sand particles, solving the technical problems in the mud-sand separation industry , reduce the mud content of particles, and provide high-quality sand ore for heap leaching; use jet mixing treatment to achieve efficient mixing of mineral particles and activation agents, and accelerate the activation reaction through a micro-current electric field, resolve metal minerals in a free ionic state, and quickly improve the leaching efficiency of metal minerals; finally, the mixed mud material after chemical leaching is subjected to physical and chemical conditioning and concentration, and then high-pressure plate and frame pressing and dehydration are adopted to achieve efficient solid-liquid separation, and the moisture content of the mud cake is less than 35%, which greatly reduces the volume of dry tailings, realizes dry tailings discharge, and reduces the cost of tailings disposal. The method of the present invention finally forms four core materials, namely coarse sand material, fine sand material, dry tailings and high-concentration uranium ore leachate, among which coarse sand material and fine sand material are respectively collected and entered into the heap leaching process, and the composite treatment of in-situ leaching and chemical activation leaching is adopted to classify and treat materials of different particle sizes to improve the efficiency and accuracy of uranium resource selection, reduce the residual uranium element in the tailings, and improve the deep extraction rate of uranium ore resources. The key problems of high mud content in muddy sandstone uranium ore, inability to classify and leach, low leaching rate, high residual uranium content in tailings and low utilization rate of uranium ore resources have been solved.

[0045] 3. The method of the present invention adopts an energy-concentrating ultrasonic scrubbing device. On the one hand, the desludging effect is improved through a multi-layer reverse stirring blade structure. Specifically, the slurry is gathered and compressed through the trumpet-shaped channel formed by the two adjacent layers of reverse stirring blade structures to form a compressed multiphase flow channel, thereby increasing the mutual friction power between the mineral particles and achieving strong scrubbing, thereby crushing and breaking up small-sized clay particles and destroying the fine-grained clay layer wrapped on the surface of the sand particles; at the same time, the closing structure formed between the two adjacent trumpet-shaped channels reduces the pressure at the center of the rear end flow field when rotating and stirring clockwise, increasing the slurry turbulence and continuing to increase the collision friction between the particles, thereby achieving efficient desludging of muddy sandstone particles. On the other hand, the ultrasonic kinetic energy and cavitation explosion kinetic energy provided by low-frequency and high-energy ultrasonic vibration are far greater than the interfacial adhesion force, destroying the sand particle interface and separating the clay particles. Deep separation of mud and sand is achieved under the combined action of high-pressure scrubbing in the multiphase flow channel and low-frequency and high-energy ultrasonic vibration. The energy-concentrating vibration conduction rod is designed as an energy-concentrating structure, that is, a number of spherical grooves are arranged at intervals along its axial direction. When the end face of the energy-concentrating vibration conduction rod generates high-intensity axial vibration, the spherical structure of the spherical groove contacts the mud medium to form a large number of cavitation nuclei with the center of the sphere as the center, generating a large cavitation intensity and energy, and diffuses divergently to finally achieve high-energy vibration similar to the lateral direction, which increases the vibration dimension and density, causes greater destructive force on the particle surface, peels off the clay particles, and further reduces the mud content of the uranium ore.

[0046] 4. The method of the present invention adopts a pneumatic energy mixed phase flow homogenizing device, uses a compressed high-pressure air jet to provide pneumatic energy, mixes with the mixed slurry in the limited space in the pipeline, forms a relatively low-density mixed phase flow material, and is quickly transmitted under the action of continuous pneumatic thrust and buoyancy, and is ejected and diffused at high speed from the pipeline outlet, driving the slurry particles to form high-speed turbulence and mixed flow, so that the slurry particles and the activator are quickly mixed, and the pneumatic kinetic energy and the mechanical kinetic energy of the mixed phase are converted to each other to achieve shaftless stirring and homogenizing. The high-pressure air flow is mixed with the slurry to form a mixed phase flow material, and the air and the slurry mixture exchange kinetic energy. The air is mixed in the mixed phase flow with tiny compressed bubbles. With the pneumatic support energy, the multiphase mixed flow slurry is ejected at high speed from the pipeline outlet of the pneumatic kinetic energy mixed phase flow device, and the turbulence and eddy current disturbance with large stroke in the stirring barrel fully mix the material. At the same time, the tiny compressed bubbles grow rapidly and break up to release energy to break up the adhered and agglomerated particle clusters, increase the contact area of ​​the particles, and thus achieve efficient homogenizing of the mineral particles and the activating agent. The shaftless mixing method makes the overall structure simple, without mechanical transmission and high-speed rotating structure. The mixing structure has strong corrosion resistance, which greatly reduces the failure rate when working in extreme acid and alkali and strong redox environments, improves the overall service life, and reduces the operation and maintenance costs of system equipment. BRIEF DESCRIPTION OF THE DRAWINGS

[0047] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the following briefly introduces the drawings required for use in the embodiments or the description of the prior art. Obviously, the drawings described below are some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative work.

[0048] Figure 1 This is a flow chart of the high-efficiency multiphase flow graded separation integrated disposal method for argillaceous sandstone uranium ore of the present invention;

[0049] Figure 2 It is a schematic diagram of the structure of the disposal system adopted by the disposal method of the present invention;

[0050] Figure 3 It is a structural schematic diagram of an energy-focusing ultrasonic scrubbing device;

[0051] Figure 4 yes Figure 3 A schematic structural diagram of a reverse stirring system of an energy-concentrating ultrasonic scrubbing device is shown;

[0052] Figure 5 yes Figure 3 A schematic structural diagram of an energy-concentrating ultrasonic vibrator of the energy-concentrating ultrasonic scrubbing device shown;

[0053] Figure 6 yes Figure 5 The structural principle diagram of the energy-concentrating ultrasonic vibrator at position B is shown;

[0054] Figure 7 It is a structural schematic diagram of a high-efficiency homogeneous mixing activation system;

[0055] Figure 8 yes Figure 7 A schematic diagram of the structure of a pneumatic kinetic energy mixed phase flow homogenizing device of a high-efficiency homogenizing activation system;

[0056] Fig. 9 yes Figure 8 A schematic structural diagram of a mixed-phase flow homogenizing injection device of a pneumatic kinetic energy mixed-phase flow homogenizing device;

[0057] Fig.10 yes Figure 8 A top view of a mixed-phase flow homogenizing injection device of the pneumatic kinetic energy mixed-phase flow homogenizing device;

[0058] Fig.11 yes Fig.10 A schematic diagram of the structure of a mixed-phase flow homogenizing nozzle of a mixed-phase flow homogenizing injection device shown;

[0059] Fig.12 yes Fig.11 The structural exploded view of the mixed phase flow homogenizing nozzle shown;

[0060] Fig.13 yes Fig.11 The structural cross-sectional view of the mixed-phase flow homogenizing nozzle is shown.

[0061] In the figure: 1. Horizontal hydraulic washing and deagglomeration device; 11. Large material discharge port; 12. Slurry mixture discharge port;

[0062] 2. High frequency linear vibration classifier;

[0063] 3. Primary multiphase flow cyclone classification device;

[0064] 4. Energy-concentrating ultrasonic scrubbing device; 41. Scrubbing cylinder; 411. Feeding hopper; 412. Overflow discharge pipe; 42. Reverse stirring system; 421. Rotating shaft; 422. First layer of blades; 423. Second layer of blades; 424. Third layer of blades; 425. Fourth layer of blades; 43. Power reducer; 44. Energy-concentrating ultrasonic vibrator; 441. Ultrasonic transducer; 442. Fixed flange; 443. Energy-concentrating vibration conduction rod; 4431. Spherical groove; 4432. End face; 45. Energy-concentrating ultrasonic power supply; 46. Slurry storage tank; 461. Clean water pipe; 462. Mud mixing device; 47. Cleaning discharge port; 48. High-pressure centrifugal slurry pump;

[0065] 5. Secondary multiphase flow cyclone classification device;

[0066] 6. High-frequency linear vibration dehydration device;

[0067] 7. High-efficiency homogenous mixing activation system; 71. Pneumatic energy mixed-phase flow homogenous mixing device; 711. Homogenous mixing reactor cylinder; 712. Mixed-phase flow homogenous mixing injection device; 7121. Fixed bracket; 7122. Mixed-phase flow homogenous mixing nozzle; 71221. Mixed-phase flow nozzle; 71222. Axis sleeve; 71223. Slurry inlet pipe; 71224. Air inlet joint; 71225. High-pressure air chamber; 71226. Mixed flow negative pressure zone; 71227. Multiphase flow mixed flow lifting zone; 71228. Diffusion flow outlet; 71229. Slurry inlet channel; 7123, directional locking hinge; 7124, pneumatic energy distributor; 7125, pipe clamp device; 7126, high-pressure airway hose; 7127, air inlet; 713, slurry discharge pipeline; 714, electromagnetic control valve; 715, air inlet pipeline; 716, high-pressure air supply device; 72, micro-electrolysis activation device; 721, plate-type micro-electrolysis electrode; 722, micro-electrolysis activation reaction cell; 723, constant current power supply; 724, wire; 725, activated slurry outlet; 73, activator dosing device;

[0068] 8. Tempering and squeezing dehydration system; 81. Tempering and thickening device; 82. High-pressure plunger grouting device; 83. High-pressure diaphragm filter press; 84. High-concentration uranium ore leachate collection device;

[0069] 91. Wastewater collection device; 92. Centrifugal slurry pump; 93. Coarse sand material; 94. Fine sand material; 95. Dry tailings. DETAILED DESCRIPTION

[0070] In order to make the purpose, technical solution and advantages of the present invention more clearly understood, the present invention is further described in detail below in conjunction with the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are only used to explain the present invention and are not used to limit the present invention.

[0071] It should be noted that the illustrations provided in the embodiments of the present invention are only used to illustrate the basic concept of the present invention in a schematic manner. Therefore, the drawings only show components related to the present invention rather than being drawn according to the number, shape and size of components in actual implementation. In actual implementation, the type, quantity and proportion of each component may be changed arbitrarily, and the component layout type may also be more complicated.

[0072] In the present invention, it is also necessary to explain that, if the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc. appear, the orientation or position relationship indicated is based on the orientation or position relationship shown in the drawings, which is only for the convenience of describing the present application and simplifying the description, and does not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as a limitation on the present application. In addition, if the terms "first" and "second" appear, they are only used for description and distinction purposes, and cannot be understood as indicating or implying relative importance.

[0073] like Figure 1 As shown, an efficient multiphase flow graded separation integrated disposal method for argillaceous sandstone uranium ore proposed in an embodiment of the present invention comprises the following steps:

[0074] S1. The crushed argillaceous sandstone uranium ore mixed material is subjected to hydraulic washing and deagglomeration treatment. The large aggregated mixed minerals are fully dispersed by hydraulic washing. Most of the discrete particles and clay particles are separated after preliminary washing. The filter particle size is designed to be N1. In this embodiment, N1=3mm. Particles larger than 3mm are collected and crushed again after washing, and the slurry smaller than 3mm enters the next step of high-frequency vibration classification.

[0075] S2, the material from S1 is subjected to high-frequency vibration classification treatment, and the mud material is graded and separated by particle size to provide a mixed material with a smaller particle size for the next step. The screening particle size is designed to be N2. In this embodiment, N2=1mm, and the material on the screen is a sand material in the range of 1mm-3mm, which is collected and entered into the heap leaching process; the material under the screen is a mud material of less than 1mm, which enters the next step of primary multiphase flow cyclone classification.

[0076] S3, the slurry material from S2 is subjected to a first-level multiphase flow cyclone classification treatment, and the slurry pump provides high-speed tangential power to enter the cyclone, and the slurry material is graded and separated according to different particle sizes under the action of centrifugal multiphase flow cyclone. The median particle size of the classification is designed to be N3. In this embodiment, N3=74μm, and the material in the range of (+74μm-1mm) moves downward along the inner wall and is discharged from the lower end outlet, forming a concentrated large-particle slurry material that is diverted through the pipeline into the next step of deep low-frequency and high-efficiency ultrasonic scrubbing; while the fine-particle light material ≤74μm and a large amount of water overflow along the overflow port in the center of the cyclone field and are diverted to S7 for jet mixing treatment.

[0077] S4, deep low-frequency high-efficiency ultrasonic scrubbing treatment is performed on the concentrated large-particle mud material (+74μm-1mm) produced by S3. There are many clay particles attached to the surface of the muddy sandstone uranium ore particles, which are difficult to separate by water washing and stirring. The present invention uses low-frequency and high-amplitude ultrasonic waves to act on the mixed liquid to peel off and break up the clay particles remaining on the surface of the sand particles; at the same time, high-speed stirring is provided to form strong collisions and mutual frictions between the particles, and finally achieve mud and sand separation to form a muddy particle mixture.

[0078] S5, subject the muddy particle mixture produced by S4 to secondary multiphase flow cyclone classification treatment, further achieve particle size classification separation, and deep mud removal. The classification median particle size is still designed to be N3. In this embodiment, N3=74μm. The clay particles ≤74μm and a large amount of water materials stripped in the previous step overflow along the central overflow port of the cyclone field and are directed to S7 for jet mixing treatment; at the same time, the (+74μm-1mm) sand material formed by mud and sand classification enters the next step of high-frequency linear vibration dehydration.

[0079] In the secondary multiphase flow cyclone classification process, an online monitoring device is set at the overflow port to monitor the material particle size information in real time. If coarse particles N3-N2 appear in the overflow mud, it is considered unqualified and the overflow mud is redirected to the primary multiphase flow cyclone classification for circulation treatment.

[0080] S6, the (+74μm-1mm) sand material produced in S5 is subjected to high-frequency linear vibration dehydration treatment, the material is subjected to solid-liquid separation, the material on the screen is collected and concentrated to form a (+74μm-1mm) sand material with a low moisture content, and a centralized heap leaching process is performed. The material under the screen has a large amount of water, which passes through the screen plate into the water storage tank, and then is diverted to the wastewater collection device for recycling after treatment, such as the water used in step S1.

[0081] S7, subjecting the fine-grained mud-water mixture material of ≤74 μm formed in steps S3 and S5 to jet mixing with an activator, and achieving efficient mixing of the mineral particles and the activator and chemical reaction through high-speed disturbance fluidization of a high-pressure air jet.

[0082] S8, subjecting the mixed materials in step S7 to micro-current activation treatment, accelerating the activation reaction by micro-current and finally dissolving the uranium element in the ore powder into the solution in the form of ions.

[0083] S9, further conditioning and concentrating the mixed mud material after chemical leaching produced in step S8, changing the agglomeration effect of the material, and increasing the dewatering performance of the mixed slurry.

[0084] S10, subjecting the quenched and concentrated mixed slurry produced in step S9 to a high-efficiency pressing solid-liquid separation process, separating the uranium-containing chemical leaching solution and the solid particles through high-pressure plate and frame pressing, achieving high-efficiency solid-liquid separation, and finally obtaining tailings dry slag with low water content and high-concentration uranium ore extract.

[0085] The above-mentioned disposal method of the present invention realizes deep stripping of mud and sand of crushed muddy sandstone uranium ore, fine graded separation of materials, jet mixing of fine-grained muddy materials, efficient activation of microcurrent, and deep and efficient dehydration after conditioning and concentration. Through the present invention, four core materials are formed in the disposal of muddy sandstone uranium ore, which are classified and disposed. The oversize materials produced in step S2 are coarse sand material (1mm-3mm) and the fine sand material with low water content (+74μm-1mm) produced in step 6 are subjected to centralized heap leaching process; the tailings dry residue produced in step 10 is safely landfilled and sealed for disposal; the high-concentration uranium ore extract produced in step 10 is further subjected to deep uranium element extraction to obtain uranium metal. Finally, efficient multiphase flow graded separation, concentration and purification disposal of muddy sandstone uranium ore is realized, and the selection efficiency of uranium ore resources is fully improved.

[0086] like Figure 2 As shown, it is a processing system used in an embodiment of the present invention to implement the above method, including a horizontal hydraulic washing and deagglomerating device 1, a high-frequency linear vibration classification device 2, a primary multiphase flow cyclone classification device 3, an energy-concentrating ultrasonic scrubbing device 4, a secondary multiphase flow cyclone classification device 5, a high-frequency linear vibration dehydration device 6, a high-efficiency mixing and activation system 7 and a tempering and pressing dehydration system 8.

[0087] The hydraulic washing and deagglomeration treatment adopts a horizontal hydraulic washing and deagglomeration device 1. The crushed mixed mineral material enters the horizontal hydraulic washing and deagglomeration device 1, and clean water is injected for mixing and slurrying. The horizontal hydraulic washing and deagglomeration device 1 rolls evenly to drive the material to flip and toss. The large aggregated mixed minerals are fully broken up by the hydraulic washing action, and most of the discrete particles and clay particles are separated after preliminary washing. The filter particle size of the horizontal hydraulic washing and deagglomeration device 1 is designed to be N1. In this embodiment, N1=3mm. After washing, the particles above 3mm are collected and crushed again at the tail end from the large material slag outlet 11. The slurry smaller than 3mm is transported to the high-frequency linear vibration classification device 2 through the ore pulp mixture outlet 12.

[0088] The high-frequency linear vibration grading treatment adopts a high-frequency linear vibration grading device 2. The function of the high-frequency linear vibration grading device 2 is to grade and separate the slurry material by high-frequency linear vibration screening to provide a mixed material with a smaller particle size for the next step. Slurry smaller than N1 falls directly onto the surface of the screen plate of the high-frequency linear vibration grading device 2, and as the screen plate performs high-frequency linear vibration, rapid material grading is achieved. The screening particle size of the high-frequency linear vibration grading device 2 is designed to be N2. In this embodiment, N2=1mm, and the vibration frequency is designed to be 20-25Hz, which can efficiently achieve material grading, wherein sand particles ≥1mm are retained on the surface of the screen plate, and mud-water mixtures smaller than 1mm are collected through the sieve holes into the slurry storage tank under the screen. After being processed by the high-frequency linear vibration classifying device 2, two kinds of materials are formed, among which the material on the screen is a coarse sand material 93 in the range of 1mm-3mm, which has high permeability and large specific surface area, and meets the heap leaching beneficiation process. Therefore, the particle size in this range is collected and enters the heap leaching process separately; the material under the screen is a mud material with a size of less than 1mm, which is transported into the first-stage multiphase flow cyclone classifying device 3 through the centrifugal slurry pump 92 arranged at the lower end of the slurry storage tank, and provides tangential power for the slurry to enter.

[0089] The first-stage multiphase flow cyclone classification treatment device 3 adopts a cyclone. The function of the first-stage multiphase flow cyclone classification device 3 is to rely on the high-speed tangential power of the slurry to classify and separate the mud material particles under the action of the centrifugal multiphase flow cyclone. Mud materials with a size of less than 1 mm enter at high speed from the slurry inlet of the first-stage multiphase flow cyclone classification device 3 and form a larger centrifugal cyclone field; the classification median particle size of the first-stage multiphase flow cyclone classification device 3 is designed to be N3. In this embodiment, N3=74μm. In the multiphase flow centrifugal cyclone field, larger particle materials (74μm-1mm) move downward along the inner wall to form concentrated large-particle mud materials, which are discharged from the bottom flow outlet at the lower end of the first-stage multiphase flow cyclone classification device 3. This part belongs to the high-mud bottom flow mixed material, and the material A large number of small-sized clay particles are attached to the surface of the material, and even sandstone uranium ore particles are wrapped inside. Further stripping and mud removal is required, and the material is diverted through a pipeline into the energy-focusing ultrasonic scrubbing device 4 for deep mud removal; while fine-grained light materials ≤74μm and a large amount of water overflow along the overflow port in the center of the cyclone field. This part of the material is mainly clay and fine ore powder materials with large specific surface area and poor permeability, which are suitable for chemical leaching. This part of the material overflows through a pipeline to the high-efficiency homogeneous mixing activation system 7 for activation and chemical leaching processes.

[0090] The deep low-frequency and high-efficiency ultrasonic scrubbing treatment adopts an energy-focusing ultrasonic scrubbing device 4. The muddy bottom flow mixed material generated by the bottom flow at the lower end of the first-stage multiphase flow cyclone classification device 3 enters the energy-focusing ultrasonic scrubbing device 4. The clay particles remaining on the surface of the sand particles are efficiently peeled off and broken up through low-frequency and high-energy ultrasonic vibration and strong stirring to achieve a mixed slurry with relatively independent separation of mud and sand. The mixed slurry overflows to the slurry storage tank 46 below and is pumped into the second-stage multiphase flow cyclone classification device 5 through the centrifugal slurry pump 92.

[0091] The secondary multiphase flow cyclone classification treatment device 5 adopts a cyclone to further realize particle size classification and separation. The classification median particle size of the secondary multiphase flow cyclone classification device 5 is still designed to be N3. In this embodiment, N3=74μm. The clay particles ≤74μm and a large amount of water materials stripped off by the energy-focusing ultrasonic scrubbing device 4 are guided along the overflow port at the center of the cyclone field to the high-efficiency uniform mixing activation system 7; at the same time, the bottom flow material of the cyclone field has a particle size of 74μm-1mm, the surface of this part of the ore sand material is clean, the mud content is greatly reduced, and the mud content is less than 3%, which meets the requirements of the heap leaching process. This part of the sand material is guided to the high-frequency linear vibration dehydration device 6.

[0092] The high-frequency linear vibration dehydration treatment adopts a high-frequency linear vibration dehydration device 6, which is designed as a high-frequency linear vibration screening method. In this embodiment, the sieve plate mesh is designed to be 0.075-0.1mm, and the vibration frequency is designed to be 30-35Hz, so as to achieve solid-liquid separation and form a fine sand material 94 with a low moisture content (moisture content less than 30%) for centralized heap leaching. A large amount of water is collected through the screen to the water storage tank, and then diverted to the wastewater collection device 91 for recycling after treatment.

[0093] The high-efficiency homogenizing and activating system 7 includes a pneumatic energy mixed phase flow homogenizing device 71 and a micro-electrolysis activation device 72. The jet homogenizing treatment uses the pneumatic energy mixed phase flow homogenizing device 71, and the micro-current activation treatment uses the micro-electrolysis activation device 72. The overflow ports of the primary multiphase flow cyclone classification device 3 and the secondary multiphase flow cyclone classification device 5 are both connected to the pneumatic energy mixed phase flow homogenizing device 71, the discharge port of the pneumatic energy mixed phase flow homogenizing device 71 is connected to the micro-electrolysis activation device 72, and the discharge port of the micro-electrolysis activation device 72 is connected to the conditioning, squeezing and dehydration system 8. When the material enters the high-efficiency mixing and activation system 7, it first passes through the pneumatic energy mixed-phase flow mixing device 71, and at the same time, the activator dosing device adds the chemical activator according to the design parameters, and the material and the chemical activator are efficiently mixed and fully contacted through the mixed-phase flow mixing injection device 712. After mixing, the mixed material flows by itself to the micro-electrolysis activation device 72. Under the joint action of microcurrent and activator, efficient activation is achieved, and the uranium metal elements in the fine ore particles are fully dissolved and leached.

[0094] The conditioning and squeezing dehydration system 8 includes a conditioning and thickening device 81, a high-pressure plunger grouting device 82, a high-pressure diaphragm filter press 83 and a high-concentration uranium ore leachate collection device 84. The conditioning and thickening device 81 is used for conditioning and thickening, and the slurry inlet pressure is controlled at 1.2-1.8MPa to complete the first-level slurry inlet dehydration; the high-efficiency squeezing solid-liquid separation treatment uses a high-pressure diaphragm filter press 83, and the diaphragm squeezing pressure is controlled at 1.0-1.2MPa for secondary squeezing dehydration; to improve the slurry dehydration efficiency, ensure the dehydration quality, and make the moisture content less than 35%. After chemical leaching, the mixed mud material is pumped to the conditioning and squeezing dehydration system 8 by a centrifugal slurry pump 92 for solid-liquid separation. The mixed mud material is first subjected to physical and chemical conditioning by the conditioning and thickening device 81 to change the dehydration performance and achieve efficient thickening to increase the feed concentration; the thickened slurry is pumped by the high-pressure plunger grouting device 82 to the high-pressure diaphragm filter press 83 for high-pressure mechanical dehydration to form a mud cake with a low moisture content (mud cake moisture content <35%), namely, tailings dry residue 95; the liquid separated by the plate and frame filter press is a uranium-containing leaching liquid, which is collected in the high-concentration uranium ore leaching liquid collection device 84 for storage and enters the uranium ore extraction process. The high-pressure diaphragm filter press 83 is provided with a clean water backwashing link, which greatly reduces the residual ionic uranium metal in the mud cake, thereby achieving full extraction of mud sandstone uranium ore and improving the utilization rate of uranium ore resources.

[0095] like Figure 3-6 As shown, the energy-concentrating ultrasonic scrubbing device 4 includes a scrubbing cylinder 41, a reverse stirring system 42, an energy-concentrating ultrasonic vibrator 44 and a slurry storage tank 46. Among them, a feed hopper 411 is provided on one end wall of the scrubbing cylinder 41, and an overflow slag discharge pipe 412 is provided on the other end wall, thereby forming a complete channel for feeding, filling and overflow drainage. The reverse stirring system 42 is arranged inside the scrubbing cylinder 41, and the reverse stirring system 42 includes a rotating shaft 421 and at least four layers of reverse stirring blade structures arranged axially along the rotating shaft 421, wherein the rotating shaft 421 is connected to a power reducer 43 arranged above the scrubbing cylinder 41 through a transmission shaft, and can rotate at high speed under the drive of the power reducer 43. Each layer of the reverse stirring blade structure includes a plurality of blades arranged circumferentially along the rotating shaft 421, and the blades of the two adjacent layers of the reverse stirring blade structure are inclined in opposite directions relative to the rotating shaft 421. The energy-concentrating ultrasonic vibrator 44 includes an ultrasonic transducer 441 and an energy-concentrating vibration conduction rod 443. The ultrasonic transducer 441 is fixed to the outside of the scrubbing cylinder 41 through a fixing flange 442. The energy-concentrating vibration conduction rod 443 is connected to the ultrasonic transducer 441 and is located inside the scrubbing cylinder 41. The slurry storage tank 46 is arranged below the scrubbing cylinder 41 as a load-bearing platform of the energy-concentrating ultrasonic scrubbing device 4. The slurry storage tank 46 is connected to the overflow slag discharge pipe 412, and the discharge port of the overflow slag discharge pipe 412 is directly guided to the slurry storage tank 46.

[0096] The energy-concentrating ultrasonic scrubbing device 4 of the present invention realizes compression of the multiphase flow channel through at least four layers of reverse stirring blade structures, increases the mutual friction power between the mineral particles, realizes strong scrubbing, breaks up the small-size clay particles, and destroys the fine-grained clay layer wrapped on the surface of the sand particles; at the same time, the ultrasonic kinetic energy and cavitation explosion kinetic energy provided by the low-frequency high-energy ultrasonic vibration are far greater than the interfacial adhesion force, destroys the clay interface on the surface of the sand particles, and the clay particles are separated; under the combined action of high-pressure scrubbing in the multiphase flow channel and low-frequency high-energy ultrasonic vibration, deep separation of mud and sand is achieved.

[0097] In this embodiment, the reverse stirring system 42 includes a four-layer reverse stirring blade structure uniformly arranged along the axial direction of the rotating shaft 421, and each layer of the reverse stirring blade structure includes six blades uniformly arranged circumferentially along the rotating shaft 421, and the two adjacent layers of blades from top to bottom are designed as reverse structures. The reverse stirring system 42 rotates clockwise when working, and each layer of blades forms a certain angle A with the axis, such as the first layer of blades 422 tilts to the left in the direction of the upstream water flow, and the second layer of blades 423 tilts to the right, and they are arranged in sequence. Finally, the first layer of blades 422 and the second layer of blades 423, the third layer of blades 424 and the fourth layer of blades 425 respectively form two bell-mouth channels. When the reverse stirring system 42 rotates clockwise, the bell-mouth channel gathers and compresses the slurry to form a compressed multiphase flow channel, increases the mutual friction power between the mineral particles, and realizes strong scrubbing, thereby breaking up the small-sized clay particles and destroying the fine-grained clay layer wrapped on the surface of the sand particles. At the same time, a closing structure is formed between the second blade 423 and the third blade 424. When the stirring is rotated clockwise, the pressure of the rear flow field is reduced, the turbulence of the slurry is increased, and the collision friction between the particles is further increased, thereby achieving efficient desludging of muddy sandstone particles. The stirring blades of conventional scrubbing machines only achieve disturbance to form turbulence, and the particles only collide with each other in a disordered manner, and the friction strength is limited.

[0098] Further optimization, in order to ensure the convergence and compression effect and disturbance capacity of the slurry, the angle A between the blades of the reverse stirring blade structure and the rotating shaft 421 is designed to be no more than 45°.

[0099] Further optimized, the power reducer 43 is composed of a variable frequency motor and a reducer, which is used to provide power for the rotating shaft 421, with a maximum torque of 1000 N·m and a rotation speed of 200-300 rpm.

[0100] Further optimization, the energy-gathering ultrasonic scrubbing device 4 also includes an energy-gathering ultrasonic power supply 45 installed on the scrubbing cylinder 41, and the energy-gathering ultrasonic power supply 45 is electrically connected to the ultrasonic transducer 441. Power is provided by the energy-gathering ultrasonic power supply 45, and the electrical energy is converted into ultrasonic mechanical kinetic energy through the ultrasonic transducer 441. The energy-gathering vibration conduction rod 443 conducts low-frequency high-energy vibration to form a cavitation effect in the mud medium. The low-frequency high-energy ultrasonic vibration provides ultrasonic kinetic energy and cavitation explosion kinetic energy that is far greater than the interfacial adhesion force, destroying the sand interface and separating the clay particles. Conventional ultrasonic cleaning machines mostly use a plate structure, that is, multiple small transducers are arranged into a vibration plate to drive the ultrasonic vibration of the side wall of the container. It usually shows insufficient vibration intensity at the same power and low effective kinetic energy. At the same time, although the vibration surface of the ordinary cylindrical vibrating rod can generate high-intensity energy, it only relies on the diameter end face to do work, and the impact range is limited.

[0101] In this embodiment, the energy-concentrating vibration conduction rod 443 is designed as an energy-concentrating structure, that is, a plurality of spherical grooves 4431 are arranged at intervals along its axial direction. When the end face 4432 of the energy-concentrating vibration conduction rod 443 generates high-intensity axial vibration, the spherical structure of the spherical grooves 4431 contacts the mud medium to form a large number of cavitation nuclei with the center of the sphere as the center, thereby generating a large cavitation intensity and energy, and diffuses divergently to finally realize high-energy vibration similar to the lateral direction, thereby increasing the vibration dimension and density, causing greater destructive force on the particle surface, and peeling off the clay particles.

[0102] Further optimization, in this embodiment, the energy-focusing ultrasonic power supply 45 and the energy-focusing ultrasonic vibrator 44 select industrial-grade low-frequency and high-energy parameters. The frequency of the energy-focusing ultrasonic vibrator 44 is 20-25KHz, the amplitude is 80-100μm, the transmission capacity is high, the cavitation intensity is large, and the efficient vibration effect can affect a three-dimensional space of 300-400mm.

[0103] For further optimization, in this embodiment, a cleaning discharge port 47 is provided at the bottom of the scrubbing cylinder 41 as a shutdown unloading and cleaning sewage discharge channel, and a gate valve is provided in a normally closed state.

[0104] Further optimization, in this embodiment, a clean water pipe 461 is provided on the slurry storage tank 46 for adding clean water; a mud mixing device 462 is also provided inside the slurry storage tank 46. When the mud concentration is too high, clean water needs to be added through the clean water pipe 461 fixed on the frame of the slurry storage tank 46, and the mud mixing device 462 performs uniform mixing. A slurry discharge port and a high-pressure centrifugal slurry pump 48 are provided at the bottom of the slurry storage tank 46, and the high-pressure centrifugal slurry pump 48 is used to lift and discharge the mud material into the next process.

[0105] Further optimization, the interior of the scrubbing cylinder 41 is set to a single bin or multiple bins according to the production capacity requirements, and each bin is provided with a reverse stirring system 42 and an energy-concentrating ultrasonic vibrator 44; when it is set to multiple bins, an intermediate baffle is provided to divide the interior of the cylinder into multiple bins, and a connecting channel is left at the bottom or top of the intermediate baffle so that the bins are interconnected, and the connecting channels are arranged alternately up and down to ensure that the material fully passes through the stirring area, and is uniformly fed from the first bin and discharged from the tail bin. Dividing the interior of the scrubbing cylinder 41 into multiple bins can, on the one hand, increase the scrubbing intensity of the slurry in a single bin, and on the other hand, the interconnection of the bin bottoms increases the flow path and scrubbing time of the mixed slurry material, thereby improving the scrubbing quality. In this embodiment, the interior of the scrubbing cylinder 41 is divided into double bins, which are connected at the bottom.

[0106] like Figure 8 As shown, the high-efficiency homogenous mixing and activation system 7 includes a pneumatic energy mixed-phase flow homogenous mixing device 71 , a micro-electrolysis activation device 72 and an activator dosing device 73 .

[0107] like Figure 9-13 As shown, the pneumatic kinetic energy mixed phase flow homogenizing device 71 comprises a homogenizing reactor cylinder 711, a mixed phase flow homogenizing injection device 712 and a high pressure gas supply device 716. The mixed phase flow homogenizing injection device 712 comprises a fixed bracket 7121, a mixed phase flow homogenizing nozzle 7122 and a pneumatic kinetic energy distributor 7124, wherein the fixed bracket 7121 is fixedly mounted on the bottom of the homogenizing reactor cylinder 711, the mixed phase flow homogenizing nozzle 7122 and the pneumatic kinetic energy distributor 7124 are respectively mounted on the fixed bracket 7121, the air inlet 7127 of the pneumatic kinetic energy distributor 7124 is connected to the high pressure gas supply device 716 via an air inlet pipeline 715, and the air outlet of the pneumatic kinetic energy distributor 7124 is connected to the mixed phase flow homogenizing nozzle 7122 via a high pressure gas hose 7126. The high-pressure air generated by the high-pressure air supply device 716 enters the pneumatic energy distributor 7124 through the air inlet pipeline 715, and then enters the mixed-phase flow homogenizing nozzle 7122. In the mixed-phase flow homogenizing nozzle 7122, the pneumatic energy is provided by the compressed high-pressure air jet, and the mixed slurry is contacted and mixed in the limited space in the pipeline to form a relatively low-density mixed-phase flow material, which is quickly transmitted under the action of continuous pneumatic thrust and buoyancy, and is ejected and diffused at high speed from the pipeline outlet, driving the slurry particles to form high-speed turbulence and mixed flow, so that the slurry particles and the activator are quickly mixed, and the pneumatic kinetic energy and the mechanical kinetic energy of the mixed phase are converted to each other to achieve shaftless stirring and homogenizing. The discharge port at the bottom of the homogenizing reactor cylinder 711 is connected to the slurry discharge pipeline 713, and the slurry discharge pipeline 713 is provided with an electromagnetic control valve 714.

[0108] The mixed-phase flow homogenizing nozzle 7122 is installed on the fixed bracket 7121 through a directional locking hinge 7123, and the directional locking hinge 7123 can adjust the angle of the mixed-phase flow homogenizing nozzle 7122 and has a locking function. In this embodiment, three mixed-phase flow homogenizing nozzles 7122 are evenly arranged along the circumference of the fixed bracket 7121. The pneumatic energy distributor 7124 is fixed by a pipe clamp device 7125 provided on the fixed bracket 7121; three air supply ports are provided on the pneumatic energy distributor 7124, which are respectively connected to the three mixed-phase flow homogenizing nozzles 7122 through high-pressure airway hoses 7126. The fixed bracket 7121 is fixed to the bottom of the homogenizing reactor cylinder 711 by anti-corrosion bolts or welding.

[0109] The mixed-phase flow homogenizing nozzle 7122 is the core component of the pneumatic energy mixed-phase flow homogenizing device 71, which includes a coaxially arranged and mutually connected mixed-phase flow nozzle 71221, an axis sleeve 71222 and a slurry inlet pipe 71223. The upper end of the axis sleeve 71222 is fixedly connected to the mixed-phase flow nozzle 71221 through an external thread, and a gap is left between the lower end inner wall of the mixed-phase flow nozzle 71221 and the upper end outer wall of the axis sleeve 71222 to form a high-pressure air chamber 71225. The high-pressure air chamber 71225 is provided with an air inlet joint 71224 for connecting the air outlet of the pneumatic energy distributor 7124. The mixed-phase flow nozzle 71221 is located on the upper part of the shaft sleeve 71222, and the areas from bottom to top are mixed flow negative pressure area 71226, multiphase mixed flow lifting area 71227 and diffuser outlet 71228, wherein the mixed flow negative pressure area 71226 is connected to the high-pressure air chamber 71225 by a gap channel. The lower end of the shaft sleeve 71222 is fixedly connected to the slurry inlet pipe 71223 through an internal thread, and the slurry inlet pipe 71223 and the shaft sleeve 71222 form a slurry inlet channel 71229.

[0110] Further optimization is carried out, the inner diameter of the mixed flow negative pressure zone 71226 of the mixed-phase flow nozzle 71221 gradually decreases from bottom to top, which has a better compression effect on the high flow rate medium, so that the pressure in the transition zone from the mixed flow negative pressure zone 71226 to the multiphase flow mixed flow lifting zone 71227 is increased, which is conducive to the mixing of high-pressure air and slurry to form a high-speed gas-liquid-solid multiphase mixed flow material; the inner diameter of the multiphase flow mixed flow lifting zone 71227 remains unchanged from bottom to top, increasing the uniform mixing time and path of the multiphase mixed flow material, and the inner diameter of the diffusion flow outlet 71228 gradually expands from bottom to top, which is conducive to the high-speed injection and diffusion of the multiphase mixed flow material.

[0111] Further optimization, the slurry inlet pipe 71223 is a trumpet structure that is thick at the bottom and thin at the top, which is conducive to the collection and feeding of mud. The diameter D of the upper end of the slurry inlet pipe 71223 is equal to the inner diameter of the shaft sleeve 71222.

[0112] The working principle of the mixed phase flow homogenizing nozzle 7122 is:

[0113] High-pressure air enters the high-pressure air chamber 71225 from the air inlet joint 71224. The high-pressure air chamber 71225 and the mixed flow negative pressure zone 71226 are connected by a gap channel A with a smaller cross-section. The high-pressure air enters the mixed flow negative pressure zone 71226 through the gap channel A at a high speed jet flow, mixes with the slurry in the chamber to form a gas-liquid-solid multiphase mixed flow; the compressed air initially mixes with the slurry in the form of larger bubbles, and continues to enter the multiphase flow mixed flow lifting zone 71227. At this time, the inner diameter of the tube decreases, the local pressure increases, the air and the slurry mixture exchange kinetic energy, the diameter of the compressed air bubbles decreases and mixes in the mixed phase flow with tiny compressed bubbles, the multiphase mixed flow density decreases, and the newly formed multiphase mixed flow generates an upward lifting and squeezing force, and a higher flow rate is formed under the composite action of the pneumatic lifting kinetic energy as the main force, and then continues to enter the diffusion flow outlet 71228 and is sprayed at a high speed to diffuse into the external slurry.

[0114] At the same time, when the high-pressure air enters the mixed flow negative pressure zone 71226 through the gap channel A at a high speed, a certain negative pressure is formed in the transition zone B at the intersection with the upper end of the slurry inlet channel 71229. Under the action of the internal and external pressure difference, the slurry in the slurry inlet channel 71229 is continuously lifted to participate in the mixed flow and uniform mixing, and then a large amount of mixed slurry is sucked into the circulation through the slurry inlet pipe 71223. When the inlet slurry flow rate is large enough, a large amount of solid particles will be entrained for mixed flow circulation. With the pneumatic support energy, the multiphase mixed flow slurry is ejected at high speed from the outlet of the mixed phase flow uniform mixing nozzle 7122, forming a large turbulent and eddy disturbance in the uniform mixing reactor cylinder 711, and the materials are fully mixed.

[0115] In order to ensure the suction, lifting and mixing flow capacity and efficiency of the mixed phase flow homogenizing nozzle 7122, it is necessary to ensure a sufficient slurry inlet flow rate. When the kinetic energy of the compressed air is fixed, the diameter of the slurry inlet channel 71229 and the slurry inlet pipe 71223 is the core of the entire structure, which affects the overall equipment structure size on the one hand, and the overall mixed flow flow rate and production capacity of the equipment on the other hand. Therefore, when the total mixed flow volume is determined, the diameter D of the slurry inlet pipe 71223 will directly affect the production capacity and the size of the entire equipment components.

[0116] The diameter D parameter design of the slurry inlet pipe 71223 of the present invention is calculated using formula (1), which is:

[0117] D≤ (1)

[0118] In the formula, Q m is the design flow rate of the slurry, which is a pre-designed value and is generally a value measured through actual working condition tests; V is the lift flow rate.

[0119] According to the data model design, in order to ensure that the particles in the mud can be efficiently lifted through the suction port, the negative pressure suction power must be greater than the particle sedimentation, that is, the lifting flow rate V in the pipeline must be greater than the slurry particle sedimentation velocity ω; in order to ensure that the mineral particles within a certain particle range are smoothly lifted and mixed, the lifting flow rate V must be greater than the maximum value of the slurry particle sedimentation velocity ω max , calculated according to formula (2):

[0120] V>4ω max (2)

[0121] Based on experience and related basic research theories, it is assumed that the slurry particles are spherical. During the particle descent process, when the resistance of the particles is balanced with gravity, they are in a constant descent. The value of the slurry particle settling velocity ω can be calculated according to formula (3):

[0122] (3)

[0123] Where Cd is the sedimentation resistance coefficient of mud and sand particles, ρ s is the density of mud and sand particles, ρ is the fluid density; d is the spherical diameter of mud and sand particles, is the acceleration due to gravity.

[0124] However, in actual working conditions, the shape of slurry particles is not a standard sphere, so it is necessary to introduce further parameters for revision. Combining a large amount of experimental data and empirical parameters, the sedimentation resistance coefficient Cd of mud and sand particles is expressed as formula (4):

[0125] (4)

[0126] Where Re is the Reynolds coefficient.

[0127] Therefore, formula (4) is substituted into formula (3), and formula (5) is obtained through empirical parameter optimization:

[0128] (5)

[0129] In the formula, , , is the kinematic viscosity coefficient of the liquid. Based on the data experience summary, the parameter design values ​​in this embodiment are C1=13.95, C2=1.09; μ can be determined based on experience.

[0130] According to the prototype experiment verification, by comparing with the stirring effect of the stirring blade, the overall effective cycle mixing time of the pneumatic kinetic energy mixed-phase flow mixing device 71 of the present invention is reduced by 50%, thereby effectively improving the mixed-phase flow mixing quality and efficiency.

[0131] Continue to see Figure 8The micro-electrolysis activation device 72 includes a plate-type micro-electrolysis electrode 721, a micro-electrolysis activation reaction pool 722 and 724. The plate-type micro-electrolysis electrode 721 is fixed to the inner ends of the micro-electrolysis activation reaction pool 722 by insulating materials, and the constant current power supply 723 is arranged on the outer side of the micro-electrolysis activation reaction pool 722 and connected to the plate-type micro-electrolysis electrode 721 by a wire to form a stable electric field. According to the working condition experimental verification summary, it is more appropriate to set the micro-electric field voltage to 36V. An activated slurry outlet 725 is provided at the bottom of the micro-electrolysis activation reaction pool 722, and the bottom end of the plate-type micro-electrolysis electrode 721 is spaced a certain distance from the bottom of the micro-electrolysis activation reaction pool 722 to ensure the normal flow and discharge of the slurry material.

[0132] The working principle of the high-efficiency homogeneous mixing activation system 7 is:

[0133] The crushed and ground homogenized ore slurry and activating agent are added into the feed port at the upper end of the mixing reactor cylinder 711 of the pneumatic kinetic energy mixed-phase flow mixing device 71 respectively by pipeline transportation, until the liquid level of the mixed slurry reaches one-third of the total volume. After the slurry fully submerges the mixed-phase flow mixing injection device 712, the automatic control system 73 starts the high-pressure gas supply device 716 to supply gas.

[0134] The mixed-phase flow homogenizing injection device 712 uses a compressed high-pressure air jet to provide pneumatic energy, which contacts and mixes with the mixed slurry in the limited space in the pipeline to form a relatively low-density mixed-phase flow material, which is quickly transmitted under the action of continuous pneumatic thrust and buoyancy, and is ejected and diffused at high speed from the pipeline outlet, driving the slurry particles to form high-speed turbulence and mixed flow, so that the slurry particles and the activator are quickly mixed, and shaftless stirring and homogenizing are achieved. At the same time, a certain negative pressure is formed at the intersection of the high-pressure air injection port and the lower end feed pipe. Under the action of the internal and external pressure difference, the slurry in the pipe is continuously lifted to participate in the mixed flow and homogenizing. When the high-pressure air flow mixes with the slurry to form a mixed-phase flow material, the air and the slurry mixture exchange kinetic energy, and the air is mixed in the mixed-phase flow as tiny compressed bubbles. With the pneumatic support energy, the multiphase flow mixed flow slurry is ejected at high speed from the pneumatic kinetic energy mixed-phase flow device pipeline outlet, forming a large turbulence and eddy disturbance in the homogenizing reactor cylinder 711, and the material is fully homogenized. At the same time, tiny compressed bubbles grow and break up quickly, releasing energy to break up the agglomerated particles, increasing the contact area of ​​the particles, thereby achieving efficient and uniform mixing of mineral particles and activating agents. When the flow rate in the pipe is large enough, the slurry at the inlet will carry particles and heavier mud and sand into the mixed flow circulation, avoiding solid particles from settling and clogging due to excessively fast sedimentation.

[0135] After the ore pulp and the activation agent are evenly mixed, they need to be aged for a certain period of time to allow the activator to fully react with the mineral particles and resolve the metal minerals in a free ionic state. The present invention adds a micro-electrolysis activation device 72 to accelerate the activation reaction through a micro-current electric field, thereby rapidly improving the leaching efficiency of metal minerals. After the ore pulp mixture is evenly mixed in the gas kinetic energy mixed phase flow evenly mixing device 71, the electromagnetic control valve 714 is started, the valve is opened, and the ore pulp mixture enters the micro-electrolysis activation device 72 through the slurry discharge pipe 713. When the evenly mixed ore pulp material fills the micro-electrolysis activation reaction tank 722, the activation reaction is accelerated under the micro-current electric field, the leaching efficiency of metal minerals is rapidly improved, and the metal minerals are resolved in a free ionic state. Finally, the activated mixture is discharged through the activated ore pulp discharge port into the next process flow, ultimately achieving high-value metal high-precision extreme beneficiation.

[0136] The high-efficiency homogeneous mixing activation system 7 of the present invention improves the turbulence and mixed flow power between the ore pulp and the activation agent, strengthens the turbulence and eddy disturbance of the mixed slurry, increases the micro-electrolysis efficiency of the activation reaction, and improves the efficiency of homogeneous mixing activation and chemical leaching. It is an integrated system with high-efficiency homogeneous mixing activation function of ore pulp under extreme environments.

[0137] It should be pointed out that, according to the needs of implementation, the various steps / components described in this application can be split into more steps / components, and two or more steps / components or partial operations of steps / components can be combined into new steps / components to achieve the purpose of the present invention.

[0138] The order of execution of each step in the above embodiment does not mean the order of execution. The order of execution of each process should be determined by its function and internal logic, and should not constitute any limitation on the implementation process of the embodiment of the present application.

[0139] It should be understood that those skilled in the art can make improvements or changes based on the above description, and all these improvements and changes should fall within the scope of protection of the appended claims of the present invention.

Claims

1. A highly efficient multiphase flow graded separation integrated treatment method for argillaceous sandstone uranium ore, characterized in that: The following steps are involved: S1. The crushed argillaceous sandstone uranium ore mixture is subjected to hydraulic washing and deagglomeration treatment. The filtration particle size is designed to be N1. Particles above N1 are collected and crushed again after washing. The slurry smaller than N1 enters the next step; S2, subjecting the slurry from S1 to high-frequency linear vibration classification treatment, the screening particle size is designed to be N2, N2<N1, and the sand material in the range of N2-N1 is collected and sent to the heap leaching process, and the mud material smaller than N2 enters the next step; S3, the slurry material from S2 is subjected to a first-level multiphase cyclone classification treatment, and the median particle size of the classification is designed to be N3, N3<N2, and the materials in the range of N3-N2 form concentrated large-particle slurry materials and are diverted to the next step; the fine-particle light materials ≤N3 and a large amount of water overflow along the overflow port in the center of the cyclone field and are diverted to S7 for jet mixing treatment; S4, subjecting the concentrated large-particle mud material produced in S3 to deep low-frequency and high-efficiency ultrasonic scrubbing treatment, applying low-frequency and high-amplitude ultrasonic waves to the mixed liquid, peeling off and breaking up the clay particles remaining on the surface of the sand particles, and providing high-speed stirring at the same time, finally achieving mud and sand separation to form a muddy particle mixed material; S5, the muddy particle mixture produced by S4 is subjected to secondary multiphase flow cyclone classification treatment, and the median particle size of the classification is still designed to be N3. The clay particles ≤ N3 and a large amount of water materials stripped in the previous step overflow along the central overflow port of the cyclone field and are directed to S7 for jet mixing treatment; at the same time, the N3-N2 sand material formed by mud and sand classification enters the next step; S6, subjecting the sand material produced in S5 to high-frequency linear vibration dehydration treatment, subjecting the material to solid-liquid separation, and collecting the material on the screen to form N3-N2 sand material with low water content, and subjecting it to centralized heap leaching process; S7, subjecting the fine-grained mud-water mixture material of ≤N3 formed in steps S3 and S5 to jet mixing with an activator, and achieving efficient mixing of the mineral particles and the activator and chemical reaction by high-speed disturbance fluidization of a high-pressure air jet; S8, subjecting the mixed materials in step S7 to micro-current activation treatment, accelerating the activation reaction by micro-current and finally dissolving the uranium element in the ore powder into the solution in the form of ions; S9, further conditioning and thickening the mixed mud material after chemical leaching produced in step S8; S10, subjecting the quenched and dense mixed slurry produced in step S9 to high-efficiency pressing for solid-liquid separation, and finally obtaining tailings dry slag with low water content and high-concentration uranium ore extract.

2. The method for efficient multiphase flow graded separation and integrated disposal of argillaceous sandstone uranium ore according to claim 1 is characterized in that: In the secondary multiphase flow cyclone classification process, an online monitoring device is set at the overflow port to monitor the material particle size information in real time. If coarse particles N3-N2 appear in the overflow mud, it is considered unqualified and the overflow mud is redirected to the primary multiphase flow cyclone classification for circulation treatment.

3. The method for efficient multiphase flow graded separation and integrated disposal of argillaceous sandstone uranium ore according to claim 1 is characterized in that: A large amount of water generated in step S6 passes through the sieve plate into the water storage tank, and then flows back to the wastewater collection device for recycling after treatment.

4. The method for efficient multiphase flow graded separation and integrated disposal of argillaceous sandstone uranium ore according to claim 1, characterized in that: The hydraulic washing and agglomeration treatment adopts a horizontal hydraulic washing and agglomeration device, and the filter particle size N1 is 1-4mm.

5. The method for efficient multiphase flow graded separation and integrated disposal of argillaceous sandstone uranium ore according to claim 1, characterized in that: The high-frequency linear vibration classification process adopts a high-frequency linear vibration classification device, the screen particle size N2 is 0.2-1mm, and the vibration frequency is 20-25Hz.

6. The method for efficient multiphase flow graded separation and integrated disposal of argillaceous sandstone uranium ore according to claim 1, characterized in that: The first-stage multiphase flow cyclone classification treatment and the second-stage multiphase flow cyclone classification treatment both use a cyclone, and the classification median particle size N3 of the cyclone is 40-74 μm.

7. The method for efficient multiphase flow graded separation and integrated disposal of argillaceous sandstone uranium ore according to claim 1, characterized in that: The deep low-frequency and high-efficiency ultrasonic scrubbing treatment adopts an energy-concentrating ultrasonic scrubbing device, which includes a scrubbing cylinder, a reverse stirring system, an energy-concentrating ultrasonic vibrator and a slurry storage tank; the scrubbing cylinder is provided with an inlet hopper and an overflow slag discharge pipe; the reverse stirring system is arranged inside the scrubbing cylinder, including a rotating shaft and at least four layers of reverse stirring blade structures arranged axially along the rotating shaft, each layer of the reverse stirring blade structure includes a plurality of blades arranged circumferentially along the rotating shaft, and the blades of the two adjacent layers of reverse stirring blade structures are inclined in opposite directions relative to the rotating shaft; the energy-concentrating ultrasonic vibrator includes an ultrasonic transducer device and an energy-concentrating vibration conduction rod, the ultrasonic transducer device is fixed to the outside of the scrubbing cylinder, the energy-concentrating vibration conduction rod is connected to the ultrasonic transducer device and is located inside the scrubbing cylinder; the slurry storage tank is connected to the overflow slag discharge pipe, and the discharge port of the overflow slag discharge pipe is directly diverted to the slurry storage tank.

8. The method for efficient multiphase flow graded separation and integrated disposal of argillaceous sandstone uranium ore according to claim 7, characterized in that: The angle between the blades of the reverse stirring blade structure and the rotation axis does not exceed 45°.

9. The method for efficient multiphase flow graded separation and integrated disposal of argillaceous sandstone uranium ore according to claim 7, characterized in that: The energy-concentrating vibration conducting rod is provided with a plurality of spherical grooves at intervals along the axial direction thereof.

10. The method for efficient multiphase flow graded separation and integrated disposal of argillaceous sandstone uranium ore according to claim 7, characterized in that: The frequency of the energy-concentrating ultrasonic vibrator is 20-25 KHz, and the amplitude is 80-100 μm.

11. The method for efficient multiphase flow graded separation and integrated disposal of argillaceous sandstone uranium ore according to claim 7, characterized in that: The interior of the scrubbing cylinder is set to a single compartment or multiple compartments according to production capacity requirements, and each compartment is provided with a set of the reverse stirring system and the energy-concentrating ultrasonic vibrator; when it is set to multiple compartments, an intermediate baffle is provided to divide the interior of the cylinder into multiple compartments, and a connecting channel is left at the bottom or top of the intermediate baffle to connect the compartments to each other, and the connecting channels are arranged alternately up and down to ensure that the material passes through the stirring area fully.

12. The method for efficient multiphase flow graded separation and integrated disposal of argillaceous sandstone uranium ore according to claim 1, characterized in that: The high-frequency linear vibration dehydration treatment adopts a high-frequency linear vibration dehydration device, the screen particle size is 0.075-0.1mm, and the vibration frequency is designed to be 30-35Hz.

13. The method for efficient multiphase flow graded separation and integrated disposal of argillaceous sandstone uranium ore according to claim 1, characterized in that: The jet mixing treatment adopts a pneumatic kinetic energy mixed-phase flow mixing device, which includes a mixing reactor cylinder, a mixed-phase flow mixing injection device and a high-pressure air supply device; the mixed-phase flow mixing injection device includes a fixed bracket, a mixed-phase flow mixing nozzle and a pneumatic kinetic energy distributor, the fixed bracket is fixedly installed at the bottom of the mixing reactor cylinder, the mixed-phase flow mixing nozzle and the pneumatic kinetic energy distributor are respectively installed on the fixed bracket, the air inlet of the pneumatic kinetic energy distributor is connected to the high-pressure air supply device, and the air outlet of the pneumatic kinetic energy distributor is connected to the mixed-phase flow The high-pressure gas generated by the high-pressure gas supply device enters the mixed-phase flow mixing nozzle through the pneumatic kinetic energy distributor. In the mixed-phase flow mixing nozzle, the high-pressure gas jet provides pneumatic kinetic energy, which contacts and mixes with the mixed slurry in the limited space in the pipeline to form a relatively low-density mixed-phase flow material, which is quickly transmitted under the action of continuous pneumatic thrust and buoyancy, and is ejected and diffused at high speed from the pipeline outlet, driving the slurry particles to form high-speed turbulence and mixed flow, so that the slurry particles and the activator are quickly mixed, completing the mutual conversion of pneumatic kinetic energy and mechanical kinetic energy of the mixed phase to achieve shaftless stirring and mixing.

14. The method for efficient multiphase flow graded separation and integrated disposal of argillaceous sandstone uranium ore according to claim 13, characterized in that: The mixed-phase flow homogenizing nozzle comprises a mixed-phase flow nozzle, an axial sleeve and a slurry inlet pipe which are coaxially arranged and interconnected; the upper end of the axial sleeve is fixedly connected to the mixed-phase flow nozzle, and a gap is left between the inner wall of the lower end of the mixed-phase flow nozzle and the outer wall of the upper end of the axial sleeve to form a high-pressure air chamber, and the high-pressure air chamber is provided with an air inlet joint for connecting the air outlet of the pneumatic energy distributor; the area where the mixed-phase flow nozzle is located on the upper part of the axial sleeve is, from bottom to top, a mixed flow negative pressure zone, a multiphase flow mixed flow lifting zone and a diffusion flow outlet, wherein the mixed flow negative pressure zone is connected to the high-pressure air chamber by a gap channel; the lower end of the axial sleeve is fixedly connected to the slurry inlet pipe, and a slurry inlet channel is formed inside the slurry inlet pipe and the axial sleeve.

15. The method for efficient multiphase flow graded separation and integrated disposal of argillaceous sandstone uranium ore according to claim 14, characterized in that: The slurry inlet pipe is a trumpet structure with a thick bottom and a thin top. The diameter D of the upper end of the slurry inlet pipe is equal to the inner diameter of the shaft sleeve. The diameter D of the upper end of the slurry inlet pipe needs to satisfy formula (1): D≤ （1） In the formula, Q m is the slurry design flow rate, is the advance design value; V is the lift flow rate, and the lift flow rate V is calculated according to formula (2): V>4ω max (2) In the formula, ω max is the maximum value of the slurry particle settling velocity ω, and the slurry particle settling velocity ω is calculated according to formula (5): （5） In the formula, , Re is the Reynolds coefficient, , ρ s is the density of mud and sand particles, ρ is the fluid density, d is the spherical diameter of mud and sand particles, is the kinematic viscosity coefficient of the liquid.

16. The method for efficient multiphase flow graded separation and integrated disposal of argillaceous sandstone uranium ore according to claim 14, characterized in that: The inner diameter of the mixed flow negative pressure zone of the mixed-phase flow nozzle gradually decreases from bottom to top, the inner diameter of the multiphase flow mixed flow lifting zone remains unchanged from bottom to top, and the inner diameter of the diffusion flow outlet gradually increases from bottom to top.

17. The method for efficient multiphase flow graded separation and integrated disposal of argillaceous sandstone uranium ore according to claim 1, characterized in that: The microcurrent activation treatment adopts a microelectrolysis activation device, which includes a plate-type microelectrolysis electrode, a microelectrolysis activation reaction cell and a constant current power supply; the plate-type microelectrolysis electrode is fixed at both ends of the inner side of the microelectrolysis activation reaction cell by insulating materials, and the constant current power supply is arranged on the outer side of the microelectrolysis activation reaction cell and connected to the plate-type microelectrolysis electrode through a wire.

18. The method for efficient multiphase flow graded separation and integrated disposal of argillaceous sandstone uranium ore according to claim 1, characterized in that: The conditioning and thickening process adopts a conditioning and thickening device, and the pulp inlet pressure is controlled at 1.2-1.8 MPa to complete the first-level pulp dehydration.

19. The method for efficient multiphase flow graded separation and integrated disposal of argillaceous sandstone uranium ore according to claim 1, characterized in that: The high-efficiency squeezing solid-liquid separation process adopts a high-pressure diaphragm filter press, and the diaphragm squeezing pressure is controlled at 1.0-1.2 MPa for secondary squeezing and dehydration.

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