In-situ leaching uranium mining leachate solid-liquid separation system and use method thereof

Abstract

The invention provides an in-situ leaching uranium mining leachate solid-liquid separation system and a use method thereof, and relates to the technical field of in-situ leaching uranium mining, the in-situ leaching uranium mining leachate solid-liquid separation system comprises a hydrocyclone group, the hydrocyclone group is composed of a plurality of hydrocyclones, and the plurality of hydrocyclones are arranged and distributed in a circle type or in-line type; the public liquid hopper comprises a liquid hopper main body, and a liquid hopper inlet pipe, a liquid hopper outlet pipe and a liquid hopper backflushing pipe which are arranged on the liquid hopper main body; and the bag type filter consists of a hollow cylinder and a hemispherical seal head. According to the invention, a large-flux parallel hydrocyclone group is utilized, an original liquid collecting tank is replaced, and efficient solid-liquid separation is realized while the leaching flux is ensured by coupling a'centrifugal-gravity 'effect; the public liquid hopper is arranged at the bottom of the hydrocyclone set, so that the hydrocyclone set serving as solid-liquid separation equipment has a buffering function, the robustness of a system can be improved, the use cost can be effectively reduced, and the solid-liquid separation efficiency of leachate is improved.

Description

Technical Field

[0001] The present invention relates to the technical field of in-situ uranium leaching, and in particular to a solid-liquid separation system for in-situ uranium leaching solution and a use method thereof. Background Art

[0002] With the country's increasing efforts in sandstone uranium exploration and development and the increase in demand for natural uranium, the liquid phase desolidification method and technology of the leachate are in urgent need of breakthroughs. However, for a long time, the existing methods have the following problems: (1) The volume of the liquid collecting tank is huge. Its design volume is generally 0.5 times the flow rate of the leachate to be treated (cubic meters / hour), and it occupies a large area; in addition, there is a scouring effect when the leachate pipeline enters the liquid collecting tank, which is very easy to roll up the already settled solid phase, causing secondary mixing. Practice shows that the liquid collecting tank plays a more "buffering" role, and the "separation" effect is very small. (2) After the leachate leaves the liquid collecting tank, it needs to be separated for the second time. Commonly used secondary separation equipment includes sand filter towers and bag filters. When the solid phase particle content of the leachate leaving the liquid collecting tank is high, not only does it require frequent switching of equipment and backwashing operations, increasing the amount of radioactive wastewater to be treated, but it also requires frequent replacement of filter materials, which leads to high manual operation intensity and material costs. Summary of the invention

[0003] The purpose of the present invention is to provide a solid-liquid separation system for in-situ leaching of uranium and a method for using the same to improve the above-mentioned problems. In order to achieve the above-mentioned purpose, the technical solution adopted by the present invention is as follows:

[0004] In a first aspect, the present application provides a solid-liquid separation system for in-situ leaching of uranium, comprising:

[0005] A hydrocyclone group, wherein the hydrocyclone group is composed of a plurality of hydrocyclones, wherein the hydrocyclones include a cyclone body, an inlet pipe, an overflow pipe, a backwash pipe and an outlet pipe arranged on the cyclone body, and the plurality of hydrocyclones are arranged in a circle or in a straight line;

[0006] A common liquid hopper, the common liquid hopper comprising a liquid hopper body, a liquid hopper inlet pipe, a liquid hopper outlet pipe and a liquid hopper backwash pipe arranged on the liquid hopper body, the liquid hopper inlet pipe is fixedly connected to the outlet pipes of the plurality of hydrocyclones, and the liquid hopper backwash pipe is fixedly connected to the backwash pipes of the plurality of hydrocyclones through a backwash main pipe;

[0007] A bag filter, the bag filter consists of a hollow cylinder and a hemispherical head, the bag filter is provided with a filter inlet pipe, a clear liquid outlet pipe and a solid waste outlet pipe, the filter inlet pipe is fixedly connected to the overflow pipes of the plurality of hydrocyclones through a total overflow pipe, and the liquid hopper outlet pipe is connected to the solid waste outlet pipe.

[0008] Furthermore, the cyclone body is composed of a separation cylinder and a separation cone, one end of the separation cylinder is fixedly connected to the circular bottom surface of the separation cone, the other end of the separation cylinder is provided with the overflow pipe, the overflow pipe is provided with an overflow pipe solenoid valve, the end of the overflow pipe close to the separation cylinder is sleeved with an inverted cone wire mesh, a cyclone chamber is provided inside the separation cylinder, the inlet pipe is tangent to the side of the separation cylinder, a branch pipe solenoid valve is provided on the inlet pipes of the multiple hydrocyclones, and a backwash branch pipe solenoid valve is provided on the backwash pipes of the multiple hydrocyclones.

[0009] Furthermore, the bag filter further comprises an internal circulation pipeline, the filter inlet pipe is provided with an inlet pipe pressure gauge, the clear liquid outlet pipe is provided with a clear liquid solid content detector and a clear liquid solenoid valve in sequence, and the clear liquid solid content detector is provided at one end close to the bag filter;

[0010] One end of the inner circulation pipeline is fixed between the clear liquid solid content detector and the clear liquid solenoid valve, the other end of the inner circulation pipeline is connected to the filter inlet pipe, and the inner circulation pipeline is provided with an inner circulation solenoid valve;

[0011] A solid waste solenoid valve and a solid waste pressure gauge are arranged on the solid waste outlet pipe, and the solid waste solenoid valve is arranged at one end of the solid waste outlet pipe close to the bag filter.

[0012] Furthermore, the inlet pipes of the multiple hydrocyclones are fixedly connected to the leaching liquid flow pipe, and the leaching liquid flow pipe is sequentially provided with a liquid pump solenoid valve, a liquid pump, an inlet pipe solenoid valve, an inlet pipe flow meter and an inlet pipe pressure gauge, and the inlet pipe flow meter is arranged at one end close to the inlet pipe.

[0013] Furthermore, the liquid hopper inlet pipe is provided with an outlet pipe pressure gauge, and the liquid hopper outlet pipe is provided with a liquid hopper pressure gauge, a liquid hopper outlet solenoid valve, a post-processing pipeline pump and a post-pump solenoid valve in sequence, and the liquid hopper pressure gauge is provided at one end of the liquid hopper outlet pipe close to the common liquid hopper;

[0014] A backwash pipe pump and a backwash pipe solenoid valve are sequentially arranged on the backwash main pipe. The backwash pipe pump is arranged at one end of the backwash main pipe close to the common liquid bucket. A plurality of backwash branch pipes are arranged at one end of the backwash main pipe away from the backwash pipe pump. Each backwash branch pipe is fixedly connected to the backwash pipe of the hydrocyclone.

[0015] In a second aspect, the present application also provides a method for using a solid-liquid separation system for in-situ leaching of uranium, comprising:

[0016] Setting some solenoid valves to a first state and starting a stock liquid pump, collecting an inlet pressure of the leaching stock liquid based on an inlet pipe pressure gauge to obtain a first pressure value, wherein the first state includes opening a stock liquid pump solenoid valve, an inlet pipe solenoid valve, and a branch pipe solenoid valve, and closing a backwash main pipe solenoid valve and a backwash branch pipe solenoid valve;

[0017] Collect overflow pressure based on the inlet pipe pressure gauge to obtain a second pressure value;

[0018] Based on the first pressure value and the second pressure value, determining a cyclone to be flushed from a plurality of hydrocyclones;

[0019] Based on the size parameters of the inverted cone wire mesh and the overflow pipe, the flushing time and flushing pressure are determined;

[0020] Based on the flushing time and the flushing pressure, periodically flush the cyclone to be flushed and update the first pressure value after flushing;

[0021] The pressure of the common liquid bucket is collected based on the liquid bucket pressure gauge to obtain a third pressure value;

[0022] Calculating a difference between the third pressure value and the updated first pressure value to obtain a pressure difference;

[0023] When the pressure difference is greater than the initial threshold, some solenoid valves are set to a second state and a post-processing pipeline pump is turned on to discharge the solid waste in the common liquid hopper, wherein the second state includes turning on the liquid hopper outlet solenoid valve and the post-pump solenoid valve;

[0024] The solid content of the clear liquid in the clear liquid outlet pipe is detected based on the clear liquid solid content detector. When the solid content in the clear liquid exceeds the preset value and does not meet the requirements of the subsequent adsorption process, the clear liquid solenoid valve is closed and the internal circulation solenoid valve is opened to filter the clear liquid again.

[0025] The beneficial effects of the present invention are:

[0026] The present invention replaces the original liquid collecting tank by utilizing a large flux parallel hydrocyclone group, and achieves efficient solid-liquid separation while coupling the "centrifugal-gravity" effect to ensure the leaching flux; a common liquid hopper is arranged at the bottom of the hydrocyclone group, so that the hydrocyclone group as a solid-liquid separation device also has a buffer function, which can improve the robustness of the system, thereby effectively reducing the use cost and improving the solid-liquid separation efficiency of the leachate.

[0027] Other features and advantages of the present invention will be described in the following description, and partly become apparent from the description, or be understood by implementing the embodiments of the present invention. The purpose and other advantages of the present invention can be realized and obtained by the structures particularly pointed out in the written description, claims, and drawings. BRIEF DESCRIPTION OF THE DRAWINGS

[0028] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings required for use in the embodiments are briefly introduced below. It should be understood that the following drawings only show certain embodiments of the present invention and therefore should not be regarded as limiting the scope. For ordinary technicians in this field, other related drawings can be obtained based on these drawings without creative work.

[0029] Figure 1 It is a schematic diagram of a solid-liquid separation system for in-situ leaching of uranium according to an embodiment of the present invention;

[0030] Figure 2 It is a schematic diagram of the structure of the hydrocyclone group described in an embodiment of the present invention;

[0031] Figure 3 Schematic diagram of the structure of the hydrocyclone described in an embodiment of the present invention;

[0032] Figure 4 It is a schematic flow chart of a method for using the solid-liquid separation system for in-situ leaching of uranium leaching solution described in an embodiment of the present invention;

[0033] Figure 5 This is a curve diagram of the separation efficiency of a single hydrocyclone in a uranium mine in Inner Mongolia described in an embodiment of the present invention.

[0034] Markings in the figure:

[0035] 1. Inlet pipe; 2. Overflow pipe; 3. Backwash pipe; 4. Outlet pipe; 5. Separation cylinder; 6. Separation cone; 7. Conical wire mesh; 11. Leaching liquid inlet pipe; 12. Liquid pump solenoid valve; 13. Inlet pipe pressure gauge; 14. Inlet pipe flow meter; 15. Inlet pipe solenoid valve; 17. Liquid pump; 18. Branch pipe solenoid valve; 19. Hydrocyclone; 20. Liquid hopper inlet pipe; 21. Outlet pipe pressure gauge; 22. Public liquid hopper; 23. Liquid hopper backwash pipe; 24. Backwash pipeline pump; 25. Backwash main pipe solenoid valve; 26. Backwash branch pipe solenoid valve; 2 7. Backwash main pipe; 28. Backwash branch pipe; 29. ​​Main overflow pipe; 120. Liquid hopper outlet pipe; 121. Liquid hopper pressure gauge; 122. Liquid hopper outlet solenoid valve; 123. Post-processing pipeline pump; 124. Bag filter; 125. Inlet pipe pressure gauge; 126. Solid waste solenoid valve; 127. Solid waste pressure gauge; 128. Clear liquid solid content detector; 129. Clear liquid solenoid valve; 130. Circulation solenoid valve; 131. Solid waste outlet pipe; 132. Clear liquid outlet pipe; 133. Filter inlet pipe; 134. Internal circulation pipeline; 135. Pump rear solenoid valve. DETAILED DESCRIPTION

[0036] In order to make the purpose, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below in conjunction with the drawings in the embodiments of the present invention. Obviously, the described embodiments are part of the embodiments of the present invention, rather than all of the embodiments. The components of the embodiments of the present invention generally described and shown in the drawings here can be arranged and designed in various different configurations. Therefore, the following detailed description of the embodiments of the present invention provided in the drawings is not intended to limit the scope of the claimed invention, but merely represents selected embodiments of the present invention. Based on the embodiments in the present invention, all other embodiments obtained by ordinary technicians in this field without making creative work are within the scope of protection of the present invention.

[0037] It should be noted that similar reference numerals and letters represent similar items in the following drawings, so once an item is defined in one drawing, it does not need to be further defined and explained in the subsequent drawings. At the same time, in the description of the present invention, the terms "first", "second", etc. are only used to distinguish the description and cannot be understood as indicating or implying relative importance.

[0038] Embodiment 1:

[0039] This embodiment provides a solid-liquid separation system for in-situ leaching of uranium. Figure 1 .

[0040] A plurality of hydrocyclones 19, each of which comprises a hydrocyclone body, an inlet pipe 1, an overflow pipe 2, a backwash pipe 3 and an outlet pipe 4 arranged on the hydrocyclone body, and the plurality of hydrocyclones 19 are arranged in a circle or in a straight line;

[0041] A common liquid hopper 22, the common liquid hopper 22 comprises a liquid hopper body, a liquid hopper inlet pipe 20, a liquid hopper outlet pipe 120 and a liquid hopper backwash pipe 23 arranged on the liquid hopper body, the liquid hopper inlet pipe 20 is fixedly connected to the outlet pipes 4 of the plurality of hydrocyclones 19, and the liquid hopper backwash pipe 23 is fixedly connected to the backwash pipes 3 of the plurality of hydrocyclones 19 through a backwash main pipe 27;

[0042] The bag filter 124 is composed of a hollow cylinder and a hemispherical head. The bag filter 124 is provided with a filter inlet pipe 133, a clear liquid outlet pipe 132 and a solid waste outlet pipe 131. The filter inlet pipe 133 is fixedly connected to the overflow pipes 2 of the plurality of hydrocyclones 19 through the total overflow pipe 29. The liquid hopper outlet pipe 120 is connected to the solid waste outlet pipe 131.

[0043] In the present application embodiment, Figure 2As shown, the hydrocyclone group includes a plurality of hydrocyclones 19. The hydrocyclone 19 in the present application adopts a shear flow reversal type hydrocyclone. The structural type and size of the plurality of hydrocyclones 19 are consistent, and they are combined in a circumferential or in-line manner, occupying a small area.

[0044] The height of the common liquid hopper 22 is not higher than 0.5 times the length of the separation cone 6, and has both natural sedimentation and buffering functions. The common liquid hopper 22 has a trapezoidal longitudinal section and has a self-flowing effect. A liquid hopper outlet pipe 120 is designed at the lowest end.

[0045] like Figure 1 As shown, the leaching raw liquid enters the separation cylinder 5 tangentially from the horizontal inlet pipe 1, and is affected by the constraint force of the inner wall of the separation cylinder 5, generating centrifugal force inside the equipment. Under the dual effects of centrifugal force and gravity, the solid phase with heavier density is thrown to the side wall of the separation cylinder 5, and then flows downward and is discharged from the outlet pipe 4 to the common liquid bucket 22. The liquid phase with lighter density is in the center of the equipment, and flows upward while rotating, and flows out from the overflow pipe 2 to the bag filter 124, thereby realizing the effect of liquid phase desolidification. A small amount of clear liquid will inevitably be discharged from the outlet pipe 4. After natural sedimentation, the upper clear liquid of the common liquid bucket 22 is used as a backwash liquid. The clear liquid obtained after being filtered again by the bag filter 124 can be pumped to the hydrometallurgical process.

[0046] Within a certain inlet flow rate range, the separation efficiency of a single hydrocyclone 19 is proportional to the centrifugal force, that is, inversely proportional to the diameter of the separation cylinder 5, while the processing volume is proportional to the diameter of the separation cylinder 5. Therefore, in specific implementation, a small-diameter hydrocyclone 19 can be selected according to the physical properties of the solid phase particles in the leaching stock solution to achieve efficient liquid phase solid removal, and multiple units in parallel can meet large flux; if the flow rate decreases, in order to ensure efficient separation, the inlet pipe 1 of one or more hydrocyclones 19 can also be closed by a solenoid valve, so that the hydrocyclone 19 always maintains operation in a high-efficiency range, making the system highly robust.

[0047] The cyclone body is composed of a separation cylinder 5 and a separation cone 6. One end of the separation cylinder 5 is fixedly connected to the circular bottom surface of the separation cone 6. An overflow pipe 2 is provided at the other end of the separation cylinder 5. An overflow pipe solenoid valve 16 is provided on the overflow pipe 2. An inverted cone-shaped wire mesh 7 is sleeved on one end of the overflow pipe 2 close to the separation cylinder 5. A cyclone-making cavity is provided inside the separation cylinder 5. The inlet pipe 1 is tangent to the side of the separation cylinder 5. A branch pipe solenoid valve 18 is provided on the inlet pipe 1 of multiple hydrocyclones 19. A backwash branch pipe solenoid valve 26 is provided on the backwash pipe 3 of multiple hydrocyclones 19.

[0048] In the present application embodiment, Figure 3As shown, the structure of the hydrocyclone 19 is cylindrical and conical, and the joint of the cylinder and the cone can be processed as an integrated whole or connected using a flange structure; a horizontal inlet pipe 1 is connected to the upper end of the separation cylinder 5, which is tangent to the separation cylinder 5, the upper end of the separation cylinder 5 is concentrically connected to the overflow pipe 2, and the lower end of the separation cone 6 is concentrically connected to the outlet pipe 4; an inverted cone-shaped conical wire mesh 7 is provided at the connection between the separation cylinder 5 and the overflow pipe 2, and the mesh number of the conical wire mesh 7 ranges from 200 mesh to 400 mesh, and the length of the conical wire mesh is usually 0.15 times to 0.3 times the length of the separation cylinder 5.

[0049] The bag filter 124 further includes an internal circulation pipeline 134, an inlet pipe pressure gauge 125 is provided on the filter inlet pipe 133, and a clear liquid solid content detector 128 and a clear liquid solenoid valve 129 are provided on the clear liquid outlet pipe 132 in sequence, and the clear liquid solid content detector 128 is provided at one end close to the bag filter 124;

[0050] One end of the inner circulation pipeline 134 is fixed between the clear liquid solid content detector 128 and the clear liquid electromagnetic valve 129, and the other end of the inner circulation pipeline 134 is connected to the filter inlet pipe 133. The inner circulation electromagnetic valve 130 is arranged on the inner circulation pipeline 134;

[0051] A solid waste solenoid valve 126 and a solid waste pressure gauge 127 are disposed on the solid waste outlet pipe 131. The solid waste solenoid valve 126 is disposed at one end of the solid waste outlet pipe 131 close to the bag filter 124.

[0052] In the embodiment of the present application, the internal circulation pipe 134 is used to transport the clear liquid that does not meet the conditions back to the bag filter 124 for filtration again until the conditions are met.

[0053] The solid waste solenoid valve 126 is usually in a closed state and will only be opened when the pressure value collected on the solid waste pressure gauge 127 meets certain conditions.

[0054] The inlet pipes 1 of the multiple hydrocyclones 19 are fixedly connected to the leaching stock solution flow pipe 11, and the leaching stock solution flow pipe 11 is sequentially provided with a stock solution pump solenoid valve 12, a stock solution pump 17, an inlet pipe solenoid valve 15, an inlet pipe flow meter 14 and an inlet pipe pressure gauge 13, and the inlet pipe flow meter 14 is arranged at one end close to the inlet pipe 1;

[0055] The liquid hopper inlet pipe 20 is provided with an outlet pipe pressure gauge 21, and the liquid hopper outlet pipe 120 is provided with a liquid hopper pressure gauge 121, a liquid hopper outlet solenoid valve 122, a post-processing pipeline pump 123 and a post-pump solenoid valve 135 in sequence, and the liquid hopper pressure gauge 121 is provided at one end of the liquid hopper outlet pipe 120 close to the common liquid hopper 22;

[0056] A backwashing pipeline pump 24 and a backwashing pipeline solenoid valve 25 are sequentially arranged on the backwashing main pipe 27. The backwashing pipeline pump 24 is arranged at one end of the backwashing main pipe 27 close to the common liquid bucket 22. A plurality of backwashing branch pipes 28 are arranged at one end of the backwashing main pipe 27 away from the backwashing pipeline pump 24. Each backwashing branch pipe 28 is fixedly connected to the backwashing pipe 3 of the hydrocyclone 19.

[0057] In the embodiment of the present application, for multiple hydrocyclones 19, when the pressure in the total overflow pipe 29 increases, it is possible to determine the hydrocyclone 19 in which the conical wire mesh 7 is more severely clogged, so that only the backwash branch pipe 28 of the severely clogged hydrocyclone 19 is backwashed, which can effectively save backwashing resources.

[0058] Embodiment 2:

[0059] This embodiment provides a method for using a solid-liquid separation system for in-situ leaching of uranium.

[0060] like Figure 4 As shown in the figure, the method includes step S10, step S20, step S30, step S40, step S50, step S60, step S70, step S80 and step S90:

[0061] Step S10. Set some solenoid valves to the first state and start the stock liquid pump 17, collect the inlet pressure of the leaching stock liquid based on the inlet pipe pressure gauge 13, and obtain a first pressure value. The first state includes opening the stock liquid pump solenoid valve 12, the inlet pipe solenoid valve 15 and the branch pipe solenoid valve 18, and closing the backwash main pipe solenoid valve 25 and the backwash branch pipe solenoid valve 26;

[0062] Step S20. Collecting overflow pressure based on the inlet pipe pressure gauge 125 to obtain a second pressure value;

[0063] Step S30. Based on the first pressure value and the second pressure value, determining the cyclone to be flushed from the plurality of hydrocyclones 19;

[0064] Specifically, considering that the degree of blockage of each hydrocyclone 19 may vary during actual use, uniform backwashing may waste backwashing resources. In this application, the overflow pressure value of each hydrocyclone 19 is used to determine the hydrocyclone 19 that needs to be backwashed.

[0065] Specifically, step S30 specifically includes step S31, step S32, step S33, step S34, step S35, step S36, step S37 and step S38:

[0066] Step S31. By controlling the switch state of each branch pipe solenoid valve 18, the overflow pressure of each hydrocyclone 19 is obtained, and multiple overflow pressures are obtained;

[0067] Step S32. Obtaining a normal range of overflow pressure, the normal range of overflow pressure including a preset upper limit value of overflow pressure and a preset lower limit value of overflow pressure;

[0068] Step S33. When the overflow pressure of the hydrocyclone 19 is within the normal range of the overflow pressure, the overflow degree coefficient corresponding to the hydrocyclone 19 is set to a first set threshold value;

[0069] Step S34. When the pressure value of the hydrocyclone 19 is not within the normal range of the overflow pressure, the difference between the overflow pressure and the preset lower limit of the overflow pressure is calculated to obtain a first value;

[0070] Step S35. Calculate the difference between the preset upper limit value of the overflow pressure and the preset lower limit value of the overflow pressure to obtain a second value;

[0071] Step S36. Calculate the ratio of the first value to the second value to obtain the overflow degree coefficient corresponding to the hydrocyclone 19;

[0072] Specifically, in the present application, the overflow degree value of each hydrocyclone is determined by comparing whether the overflow pressure of the hydrocyclone 19 meets the preset normal range of overflow pressure. When the overflow pressure does not meet the normal range of overflow pressure, the calculation formula of the overflow degree value is:

[0073]

[0074] Among them, k i is the overflow value of the i-th hydrocyclone; P Yi is the overflow pressure of the i-th hydrocyclone; P u The upper limit value of the overflow pressure is preset; P d Preset lower limit value for relief pressure.

[0075] Step S37. Calculate the sum of the overflow degree coefficients corresponding to all the hydrocyclones 19 to obtain the overflow degree value;

[0076] Step S38. Determine the cyclone to be backwashed based on the overflow degree value;

[0077] Specifically, step S38 specifically includes step S381, step S382 and step S383:

[0078] Step S381. When the overflow degree value is greater than the second set threshold, each overflow degree coefficient is compared with the third set threshold to obtain a comparison result, which includes the hydrocyclone 19 corresponding to the overflow degree coefficient less than the third set threshold;

[0079] Step S382. The hydrocyclone 19 included in the comparison result is used as the hydrocyclone to be flushed;

[0080] Step S383. When the overflow degree value is not greater than the second set threshold value, all hydrocyclones 19 are used as cyclones to be flushed;

[0081] Specifically, the sum of the overflow degree values ​​of all the hydrocyclones 19 in the hydrocyclone group is calculated to obtain the overflow degree value of the hydrocyclone group. When the overflow degree value of the hydrocyclone group is greater than the set condition, all the hydrocyclones 19 in the hydrocyclone group need to be backwashed. If the overflow degree value is not greater than the set condition, it is necessary to determine some of the hydrocyclones 19 that need to be backwashed from the hydrocyclone group.

[0082] Step S40. Based on the size parameters of the inverted tapered screen 7 and the overflow pipe 2, determine the flushing time and flushing pressure;

[0083] Specifically, the direct manifestation of the blockage of the conical screen 7 is: the overflow pressure increases and the flow rate of the overflow pipe 2 decreases. The side area S of the conical screen 7 structure is: S = π * r * l, where r is the radius of the circular cross section of the conical screen 7, and l is the conical generatrix; because many meshes are arranged on the inverted cone structure, when there is no blockage, the actual flow area S1 is: S1 = (0.75 ~ 0.90) * S, where S1 is the flow area when there is no blockage, and S is the side area of ​​the conical screen 7 structure. When the flow rate of the overflow pipe 2 is Q1, the flow velocity V1 of the overflow pipe 2 is: Among them, S1 is the flow area when not blocked, and Q1 is the flow rate when not blocked. When blockage occurs, the overflow flow rate will inevitably decrease. Assuming it becomes Q2, the actual flow area S2 of the overflow screen 7 is: S2 = (0.50 ~ 0.75) * S, then the flow rate V2 is: Among them, S2 is the flow area when blocked, and Q2 is the flow rate when blocked.

[0084] Specifically, step S40 specifically includes step S41, step S42, step S43, step S44, step S45, step S46, step S47, step S48, step S49 and step S410:

[0085] Step S41. Obtaining the cross-sectional area of ​​the overflow pipe 2 of the cyclone to be flushed;

[0086] Step S42. Obtain the top circular cross-section radius and cone height of the inverted tapered screen 7;

[0087] Step S43. Calculate the volume of the majority of inverted tapered screens 7 based on the radius of the top circular cross section and the cone height;

[0088] Step S44. Based on the cross-sectional area of ​​the overflow pipe 2 and the overflow pressure, the overflow flow rate of the cyclone to be flushed is calculated;

[0089] Step S45. Calculate the ratio of overflow flow rate to volume to obtain the initial duration;

[0090] Step S46. Calculate the product of the initial duration and the preset multiple to obtain the flushing duration;

[0091] Specifically, the volume of the conical wire mesh 7 is:

[0092]

[0093] Wherein, V is the volume of the conical wire mesh 7; r is the radius of the circular cross section of the conical wire mesh 7; and H is the height of the conical wire mesh 7.

[0094] When the overflow screen 7 is blocked and the overflow flow is Q2, the time required to fill the unit volume of the overflow screen 7 is:

[0095]

[0096] Wherein, t is the time required to fill the unit volume of overflow screen 7; V is the volume of conical screen 7; Q2 is the flow rate when blocked.

[0097] In this application, it is specified that at least 3 volumes of fluid per unit overflow screen 7 are used for backwashing, so the flushing time is:

[0098] T≥3*n*t

[0099] Wherein, T is the flushing time; n is the number of cyclones to be flushed; and t is the time required to fill the unit volume of the overflow screen 7.

[0100] Step S47. Obtain the fluid density of the liquid output from the overflow pipe 2 and the initial flow area of ​​the inverted cone screen 7;

[0101] Step S48. Determine the actual flow area of ​​the cyclone to be flushed based on the random function;

[0102] Step S49. Calculate the square of the ratio of the overflow flow rate to the actual flow area to obtain a third value;

[0103] Step S410. Calculate the product of the third value, the fluid density and the fourth set threshold value to obtain the flushing pressure;

[0104] Specifically, according to fluid mechanics theory, the fluid dynamic pressure after the overflow screen 7 is blocked is:

[0105]

[0106] Among them, P2 is the fluid dynamic pressure; ρ is the fluid density; S2 is the flow area when blocked, and Q2 is the flow rate when blocked.

[0107] When cleaning the overflow screen 7, the backwash water flow rate Q should be greater than the flow rate Q2 when blocked, and the backwash pressure P must be greater than the fluid dynamic pressure P2.

[0108] Step S50. Based on the flushing time and flushing pressure, the cyclone to be flushed is periodically flushed and the first pressure value after flushing is updated;

[0109] Step S60. Based on the liquid hopper pressure gauge 121, the pressure of the public liquid hopper 22 is collected to obtain a third pressure value;

[0110] Step S70. Calculate the difference between the third pressure value and the updated first pressure value to obtain a pressure difference;

[0111] Step S80. When the pressure difference is greater than the initial threshold, some solenoid valves are set to the second state and the post-processing pipeline pump 123 is turned on to discharge the solid waste in the common liquid hopper 22. The second state includes opening the liquid hopper outlet solenoid valve 122 and the post-pump solenoid valve 135;

[0112] Specifically, when the difference between the third pressure value and the first pressure value exceeds the threshold, the solid waste discharge procedure of the common liquid bucket 22 is executed, that is, the post-processing pipeline pump 123 is turned on to transport the solid waste-containing slurry to the post-processing process, which is usually performed for 3 to 5 minutes.

[0113] Step S90. The solid content of the clear liquid in the clear liquid outlet pipe 132 is detected based on the clear liquid solid content detector 128. When the solid content in the clear liquid exceeds a preset value and does not meet the requirements of the subsequent adsorption process, the clear liquid solenoid valve 129 is closed and the internal circulation solenoid valve 130 is opened to filter the clear liquid again;

[0114] Specifically, the clear liquid outlet pipe 132 after the bag filter 124 is equipped with a clear liquid solid content detector 128. If the clear liquid test fails, the clear liquid solenoid valve 129 is closed, and the circulation solenoid valve 130 is opened to pump the unqualified clear liquid to the filter inlet pipe 133 again. This step is repeated until the clear liquid test passes, and then it is pumped to the water metallurgical process.

[0115] Embodiment 3:

[0116] The solid-liquid separation system for in-situ leaching of uranium in this application was installed and tested in a uranium mine in Inner Mongolia. The effect of improving efficiency and reducing costs was obvious, and the cost of filter material replacement was reduced by 57%, as shown in Table 1:

[0117] Table 1 Process data of a uranium mine in Inner Mongolia (leaching solution flow rate: 22m 3 / h)

[0118]

[0119] The system replaces six filter bags in the bag filter 124 each time, and the cost of each filter bag is 30 yuan.

[0120] Embodiment 4:

[0121] The embodiments of the present application provide a theoretical analysis of the stability of a hydrocyclone group system.

[0122] Assume that the hydrocyclone group is composed of n hydrocyclones 19 connected in parallel in a circle, and the vortex generated by each hydrocyclone 19 can be regarded as a point vortex on a two-dimensional plane, and its coordinates are represented by z i =(x i ,y i ), where i = 1, 2...n, and the vortex strength of each point vortex is W i If the system is a viscous incompressible fluid, then according to Hamiltonian mechanics theory, the sum of the interaction energy between each point vortex is:

[0123]

[0124] Where H is the sum of the interaction energy between each vortex; z i and z j are the coordinates of the i-th and j-th vortices respectively; |z i -z j | is the Euclidean distance between the i-th and j-th vortices; W i and W j are the vortex strengths of the i-th and j-th point vortices respectively.

[0125] The total center of mass of the hydrocyclone group is Z c , the moment of inertia is I:

[0126]

[0127] Where n is the number of hydrocyclones; Z c is the total center of mass position of the hydrocyclone group; z j is the coordinate of the jth point vortex;

[0128]

[0129] Where I is the moment of inertia; z j is the coordinate of the jth point vortex; W j is the vortex intensity of the jth point vortex; n is the number of hydrocyclones.

[0130] Further, when the hydrocyclone group is disturbed (for example, the position or flow rate of a single hydrocyclone 19 changes due to changes in upstream flow or solid particle concentration, or the inlet pipe solenoid valve 15 of a hydrocyclone 19 is closed), the displacement Δz of the center of mass of the i-th hydrocyclone 19 is i After the disturbance, the coordinates of the point vortex of the i-th hydrocyclone 19 are z' i =z i +Δz i At this time, the changes in the center of mass position and moment of inertia of the system are:

[0131]

[0132] Among them, ΔZ c is the change in the center of mass position; Δz i is the mass center offset of the i-th hydrocyclone 19; n is the number of hydrocyclones;

[0133]

[0134] Where, ΔI is the change in moment of inertia; W j is the vortex strength of the i-th point vortex; n is the number of hydrocyclones; Δz i is the mass center offset of the i-th hydrocyclone 19; R is the real part function; is Δz i The complex conjugate of .

[0135] The change in the center of mass position ΔZ c With the disturbance Δz i The proportional coefficient is 1 / n, and n is usually a large number (i.e., there are multiple hydrocyclones 19 in parallel in the system), so the center of mass position Z c It has a strong ability to resist disturbances. At the same time, the change in the moment of inertia ΔI is a second-order quantity caused by disturbances, which can be ignored under small disturbances, and the change in the moment of inertia is also very small.

[0136] In addition, for the regular polygon structure of the hydrocyclone group, according to the translation invariance and rotation invariance of the solution of the Hamilton equation, in determining the point vortex coordinate z i and vortex strength W i After that, the system's center of mass moment G and moment of inertia M are conserved, that is:

[0137]

[0138] Where G is the centroid moment; z i is the coordinate of the i-th point vortex; W i is the vortex intensity of the i-th point vortex; n is the number of hydrocyclones.

[0139]

[0140] Where M is the moment of inertia; z i is the coordinate of the i-th point vortex; W i is the vortex intensity of the i-th point vortex; n is the number of hydrocyclones.

[0141] When the i-th hydrocyclone 19 is disturbed, the point vortex coordinate offset is Δz i , the positions of other hydrocyclones 19 will be adjusted spontaneously to satisfy the conservation of center of mass moment and moment of inertia.

[0142] Specifically, another hydrocyclone 19 (assuming it is the jth hydrocyclone) in the hydrocyclone group and located in the opposite direction should also be displaced and adjusted to maintain balance. Then before the disturbance:

[0143] z i +z j =0

[0144] Among them, z i is the coordinate of the i-th point vortex; z j is the coordinate of the jth point vortex.

[0145] z i 2 +z j 2 =C

[0146] Among them, z i is the coordinate of the i-th point vortex; z j is the coordinate of the jth point vortex; C is a constant.

[0147] After the disturbance, if the hydrocyclone point vortex coordinate z i If moving forward, z j Move in the negative direction. According to the law of conservation of inertia, if z i 2 becomes larger, then z j 2 It should be reduced so that the total change is 0. This means that when the point vortex of one hydrocyclone 19 is displaced, the point vortex coordinate adjustment of other hydrocyclones 19 will maintain the overall balance of the system. It can be seen that when the hydrocyclone group is disturbed, the center of mass position and moment of inertia of the system remain stable and can automatically return to a balanced state without human intervention, so the system has strong robustness.

[0148] Embodiment 5:

[0149] The embodiment of the present application discloses the separation efficiency of a single hydrocyclone 19 .

[0150] like Figure 5As shown, the separation efficiency is measured using glass beads of different particle sizes, and the density of the glass beads is ρ p =1840kg / m 3 , cyclone inlet velocity V in =3~6m / s. The measurement results show that the separation efficiency of a single hydrocyclone 19 first increases and then decreases with the inlet velocity, and the performance curve is a typical "hump shape". The hydrocyclone group is equipped with a flow control system. When the flow of the leaching stock solution inlet pipe 11 of the parallel hydrocyclone group fluctuates, the branch pipe solenoid valves 18 of some hydrocyclones 19 are opened and closed to increase or decrease the inlet velocity of the remaining hydrocyclones 19, ensuring that each hydrocyclone operates at a high separation efficiency.

[0151] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. For those skilled in the art, the present invention may have various modifications and variations. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention shall be included in the protection scope of the present invention.

[0152] The above is only a specific embodiment of the present invention, but the protection scope of the present invention is not limited thereto. Any person skilled in the art can easily think of changes or substitutions within the technical scope disclosed by the present invention, which should be included in the protection scope of the present invention. Therefore, the protection scope of the present invention should be based on the protection scope of the claims.

Claims

1. A solid-liquid separation system for in-situ leaching of uranium, characterized in that: include: A hydrocyclone group, the hydrocyclone group comprising a plurality of hydrocyclones (19), the hydrocyclone (19) comprising a cyclone body, an inlet pipe (1), an overflow pipe (2), a backwash pipe (3) and an outlet pipe (4) arranged on the cyclone body, the plurality of hydrocyclones (19) being arranged in a circle or in a straight line; A common liquid hopper (22), the common liquid hopper (22) comprising a liquid hopper body, a liquid hopper inlet pipe (20), a liquid hopper outlet pipe (120) and a liquid hopper backwash pipe (23) arranged on the liquid hopper body, the liquid hopper inlet pipe (20) being fixedly connected to the outlet pipes (4) of the plurality of hydrocyclones (19), and the liquid hopper backwash pipe (23) being fixedly connected to the backwash pipes (3) of the plurality of hydrocyclones (19) via a backwash main pipe (27); A bag filter (124), the bag filter (124) consisting of a hollow cylinder and a hemispherical head, the bag filter (124) being provided with a filter inlet pipe (133), a clear liquid outlet pipe (132) and a solid waste outlet pipe (131), the filter inlet pipe (133) being fixedly connected to the overflow pipes (2) of the plurality of hydrocyclones (19) via a total overflow pipe (29), and the liquid hopper outlet pipe (120) being in communication with the solid waste outlet pipe (131).

2. The solid-liquid separation system for in-situ leaching of uranium according to claim 1, characterized in that The cyclone body is composed of a separation cylinder (5) and a separation cone (6). One end of the separation cylinder (5) is fixedly connected to the circular bottom surface of the separation cone (6). The other end of the separation cylinder (5) is provided with the overflow pipe (2). The overflow pipe (2) is provided with an overflow pipe electromagnetic valve (16). An end of the overflow pipe (2) close to the separation cylinder (5) is sleeved with an inverted cone-shaped wire mesh (7). A cyclone-making chamber is provided inside the separation cylinder (5). The inlet pipe (1) is tangent to the side of the separation cylinder (5). A branch pipe electromagnetic valve (18) is provided on the inlet pipe (1) of the plurality of hydrocyclones (19). A backwash branch pipe electromagnetic valve (26) is provided on the backwash pipe (3) of the plurality of hydrocyclones (19).

3. The solid-liquid separation system for in-situ leaching of uranium according to claim 1, characterized in that The bag filter (124) further comprises an internal circulation pipeline (134), the filter inlet pipe (133) is provided with an inlet pipe pressure gauge (125), the clear liquid outlet pipe (132) is provided with a clear liquid solid content detector (128) and a clear liquid solenoid valve (129) in sequence, and the clear liquid solid content detector (128) is provided at one end close to the bag filter (124); One end of the inner circulation pipeline (134) is fixed between the clear liquid solid content detector (128) and the clear liquid electromagnetic valve (129), the other end of the inner circulation pipeline (134) is connected to the filter inlet pipe (133), and the inner circulation electromagnetic valve (130) is provided on the inner circulation pipeline (134); The solid waste outlet pipe (131) is provided with a solid waste solenoid valve (126) and a solid waste pressure gauge (127), and the solid waste solenoid valve (126) is provided at one end of the solid waste outlet pipe (131) close to the bag filter (124).

4. The solid-liquid separation system for in-situ leaching of uranium according to claim 1, characterized in that The inlet pipes (1) of the plurality of hydrocyclones (19) are fixedly connected to the leaching stock solution flow pipe (11), and the leaching stock solution flow pipe (11) is provided with a stock solution pump solenoid valve (12), a stock solution pump (17), an inlet pipe solenoid valve (15), an inlet pipe flow meter (14) and an inlet pipe pressure gauge (13) in sequence, and the inlet pipe flow meter (14) is arranged at one end close to the inlet pipe (1).

5. The solid-liquid separation system for in-situ leaching of uranium according to claim 1, characterized in that The liquid hopper inlet pipe (20) is provided with an outlet pipe pressure gauge (21), and the liquid hopper outlet pipe (120) is provided with a liquid hopper pressure gauge (121), a liquid hopper outlet solenoid valve (122), a post-processing pipeline pump (123) and a post-pump solenoid valve (135) in sequence, and the liquid hopper pressure gauge (121) is provided at one end of the liquid hopper outlet pipe (120) close to the common liquid hopper (22); A backwashing pipeline pump (24) and a backwashing pipeline solenoid valve (25) are sequentially arranged on the backwashing main pipe (27); the backwashing pipeline pump (24) is arranged at one end of the backwashing main pipe (27) close to the common liquid hopper (22); and a plurality of backwashing branch pipes (28) are arranged at one end of the backwashing main pipe (27) away from the backwashing pipeline pump (24); each backwashing branch pipe (28) is fixedly connected to the backwashing pipe (3) of the hydrocyclone (19).

6. A method for using a solid-liquid separation system for in-situ leaching of uranium, characterized in that: include: Setting some solenoid valves to a first state and starting a stock liquid pump (17), collecting the inlet pressure of the leaching stock liquid based on the inlet pipe pressure gauge (13), and obtaining a first pressure value, wherein the first state includes opening the stock liquid pump solenoid valve (12), the inlet pipe solenoid valve (15) and the branch pipe solenoid valve (18), and closing the backwash main pipe solenoid valve (25) and the backwash branch pipe solenoid valve (26); Collecting overflow pressure based on the inlet pipe pressure gauge (125) to obtain a second pressure value; Based on the first pressure value and the second pressure value, determining a cyclone to be flushed from a plurality of hydrocyclones (19); Based on the size parameters of the inverted cone-shaped wire mesh (7) and the overflow pipe (2), the flushing time and flushing pressure are determined; Based on the flushing time and the flushing pressure, periodically flush the cyclone to be flushed and update the first pressure value after flushing; collecting the pressure of the common liquid bucket (22) based on the liquid bucket pressure gauge (121) to obtain a third pressure value; Calculating a difference between the third pressure value and the updated first pressure value to obtain a pressure difference; When the pressure difference is greater than the initial threshold, some of the solenoid valves are set to a second state and the post-processing pipeline pump (123) is turned on to discharge the solid waste in the common liquid bucket (22), wherein the second state includes turning on the liquid bucket outlet solenoid valve (122) and the post-pump solenoid valve (135); The solid content of the clear liquid in the clear liquid outlet pipe (132) is detected based on the clear liquid solid content detector (128). When the solid content in the clear liquid exceeds a preset value and does not meet the requirements of the subsequent adsorption process, the clear liquid solenoid valve (129) is closed and the internal circulation solenoid valve (130) is opened to filter the clear liquid again.

7. The method for using the solid-liquid separation system for in-situ leaching of uranium according to claim 6, characterized in that: Based on the first pressure value and the second pressure value, a cyclone to be flushed is determined from a plurality of hydrocyclones (19), including By controlling the switch state of each branch pipe solenoid valve (18), the overflow pressure of each hydrocyclone (19) is obtained, thereby obtaining a plurality of overflow pressures; Acquiring a normal range of overflow pressure, wherein the normal range of overflow pressure includes a preset upper limit value of overflow pressure and a preset lower limit value of overflow pressure; When the overflow pressure of the hydrocyclone (19) is within the normal range of the overflow pressure, the overflow degree coefficient corresponding to the hydrocyclone (19) is set to a first set threshold value; When the pressure value of the hydrocyclone (19) does not fall within the normal range of the overflow pressure, the difference between the overflow pressure and the preset lower limit of the overflow pressure is calculated to obtain a first value; Calculating the difference between the preset upper limit value of the overflow pressure and the preset lower limit value of the overflow pressure to obtain a second value; Calculating the ratio of the first value to the second value to obtain an overflow degree coefficient corresponding to the hydrocyclone (19); Calculating the sum of the overflow degree coefficients corresponding to all the hydrocyclones (19) to obtain an overflow degree value; The cyclone to be flushed that needs to be backflushed is determined based on the overflow degree value.

8. The method for using the solid-liquid separation system for in-situ leaching of uranium according to claim 7, characterized in that: Determining the cyclone to be flushed that needs to be backwashed based on the overflow degree value includes: When the overflow degree value is greater than the second set threshold, each overflow degree coefficient is compared with a third set threshold to obtain a comparison result, wherein the comparison result includes a hydrocyclone (19) corresponding to an overflow degree coefficient less than the third set threshold; The hydrocyclone (19) included in the comparison result is used as the hydrocyclone to be flushed; When the overflow degree value is not greater than a second set threshold value, all hydrocyclones (19) are used as the hydrocyclones to be flushed.

9. The method for using the solid-liquid separation system for in-situ leaching of uranium according to claim 7, characterized in that: Based on the size parameters of the inverted cone-shaped wire mesh (7) and the overflow pipe (2), the flushing time and flushing pressure are determined, including: Obtaining the cross-sectional area of ​​the overflow pipe (2) of the cyclone to be flushed; Obtaining the top circular cross-section radius and cone height of the inverted cone-shaped wire mesh (7); The volume of the plurality of inverted cone-shaped screens (7) is calculated based on the radius of the top circular cross section and the cone height; Based on the cross-sectional area of ​​the overflow pipe (2) and the overflow pressure, the overflow flow rate of the cyclone to be flushed is calculated; Calculating the ratio of the overflow flow rate to the volume to obtain an initial duration; The product of the initial duration and the preset multiple is calculated to obtain the flushing duration.

10. The method for using the solid-liquid separation system for in-situ leaching of uranium according to claim 9, characterized in that: Based on the size parameters of the inverted cone-shaped wire mesh (7) and the overflow pipe (2), the flushing time and flushing pressure are determined, including: Obtaining the fluid density of the liquid output from the overflow pipe (2) and the initial flow area of ​​the inverted cone screen (7); Determining the actual flow area of ​​the cyclone to be flushed based on a random function; Calculate the square of the ratio of the overflow flow rate to the actual flow area to obtain a third value; The product of the third value, the fluid density and a fourth set threshold is calculated to obtain the flushing pressure.

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