In-situ leaching uranium mining large-flux leachate surface liquid phase solid removal device and method

Abstract

The invention provides an in-situ leaching uranium mining large-flux leachate earth surface liquid phase solid removal device and method, and relates to the technical field of in-situ leaching uranium mining, the in-situ leaching uranium mining large-flux leachate earth surface liquid phase solid removal device comprises a cyclone set, and the cyclone set is composed of a plurality of hydrocyclones; the fiber ball filter is composed of a hollow cylinder and two hemispherical seal heads, a liquid inlet pipe, a desorption pipe and a back-flushing tail liquid pipe are arranged on the fiber ball filter, and the back-flushing tail liquid pipe comprises a back-flushing inlet pipe and a back-flushing outlet pipe. According to the invention, a liquid collecting tank is replaced by the large-flux-small-diameter-parallel cyclone group, and efficient solid-liquid separation is realized while the leaching flux is ensured by coupling a'centrifugal-gravity 'effect; and after being subjected to primary solid removal in the cyclone group, the leachate flows to a fiber ball filter filled with a high polymer material from an overflow header pipe at the top of the cyclone group for deep filtration and enhanced solid removal, so that the solid-liquid separation efficiency of the leachate can be effectively improved, and the cost is reduced.

Description

Technical Field

[0001] The invention relates to the technical field of in-situ uranium leaching, and in particular to a surface liquid phase desolidification device and method for large-flux leaching solution of in-situ uranium leaching. Background Art

[0002] With the strengthening of the country's efforts in the exploration and development of sandstone uranium mines and the increase in the demand for natural uranium, the liquid phase solid removal method and technology of large flux leachate are in urgent need of breakthroughs. However, for a long time, the solid removal method has the following problems: (1) The liquid collecting tank is large in size. Its design volume is generally 0.5 times the flow rate of the leachate to be treated, which occupies a large area; at the same time, there is a scouring effect when the leachate pipeline enters the liquid collecting tank, which is very easy to roll up the settled solid phase and cause secondary mixing. (2) If the liquid collecting tank is connected to a sand filter tower, on the one hand, the sand filter tower equipment occupies a large area and has high investment, and on the other hand, it requires frequent backwashing operations, a large amount of wastewater treatment, and the quartz sand inside the tower needs to be replaced after a period of use. (3) If the liquid collecting tank is connected to a bag filter, the use of high-precision filter bags is efficient in intercepting particulate matter, but it requires frequent equipment switching and filter bag replacement, and the manual operation intensity and material cost remain high; if low-precision filter bags are used, although the flux can be guaranteed, the solid phase cannot be separated well. Summary of the invention

[0003] The purpose of the present invention is to provide a surface liquid phase solid removal device and method for high-flux leaching solution of uranium in situ leaching 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 surface liquid phase desolidification device for high-flux leaching solution of uranium in-situ leaching, comprising:

[0005] A cyclone group, the cyclone group is composed of a plurality of hydrocyclones, and the cyclone group includes an overflow main pipe;

[0006] A fiber ball filter, which consists of a hollow cylinder and two hemispherical heads. The fiber ball filter is provided with a liquid inlet pipe, a desorption pipe and a recoil tail liquid pipe. The recoil tail liquid pipe includes a recoil inlet pipe and a recoil outlet pipe. The liquid inlet pipe and the recoil outlet pipe are fixedly connected to the hemispherical head at the top, the desorption pipe and the recoil inlet pipe are fixedly connected to the hemispherical head at the bottom, and the liquid inlet pipe is connected to the overflow main pipe.

[0007] Furthermore, the device includes a common liquid bucket, and the common liquid bucket includes a liquid bucket inlet pipe, a liquid bucket solid waste pipe and a liquid bucket clear liquid pipe.

[0008] The liquid hopper inlet pipe is fixedly connected to the outlet main pipe, and an outlet pressure gauge is provided on the liquid hopper inlet pipe;

[0009] The liquid hopper clear liquid pipe is connected to the recoil main pipe, and a recoil pipeline pump and a recoil solenoid valve are sequentially arranged on the liquid hopper clear liquid pipe. The recoil solenoid valve is arranged at one end close to the recoil main pipe.

[0010] The liquid hopper solid waste pipe is sequentially provided with a liquid hopper pressure gauge, a liquid hopper solenoid valve, a post-processing pipeline pump and a post-pump solenoid valve.

[0011] Furthermore, the device includes a leaching liquid flow pipe, which is connected to the inlet main pipe. The leaching liquid flow pipe is sequentially provided with a liquid pump solenoid valve, a liquid pump, a liquid inlet solenoid valve, a total inlet flow meter and a total inlet pressure gauge, and the total inlet pressure gauge is arranged at one end close to the inlet main pipe.

[0012] Further, the hydrocyclone includes an inlet pipe, an overflow pipe, a backwash pipe, an outlet pipe, an annular baffle, a separation cylinder and a separation cone, the inlet pipe is tangent to the separation cylinder, an inlet branch solenoid valve is arranged on the inlet pipe, a backwash branch solenoid valve is arranged on the backwash pipe, one end of the separation cylinder is fixedly connected to the circular bottom surface of the separation cone, an overflow pipe is arranged at the center position of the other end of the separation cylinder, an overflow screen is sleeved on one end of the overflow pipe close to the separation cylinder, an overflow branch solenoid valve is arranged on one end of the overflow pipe away from the separation cylinder, the annular baffle is arranged inside the separation cylinder, and the annular space between the annular baffle and the inner wall of the separation cylinder forms a cyclone chamber;

[0013] The cyclone group also includes an inlet main pipe, an outlet main pipe and a recoil main pipe. The inlet pipes of multiple hydrocyclones are connected in parallel to form the inlet main pipe, the overflow pipes of multiple hydrocyclones are connected in parallel to form the overflow main pipe, the outlet pipes of multiple hydrocyclones are connected in parallel to form the outlet main pipe, and the recoil pipes of multiple hydrocyclones are connected in parallel to form the recoil main pipe.

[0014] Furthermore, the fiber ball filter also includes a bypass pipe, on which a backflow pump and a backflow solenoid valve are arranged, one end of the bypass pipe is arranged on the desorption pipe, and the other end of the bypass pipe is arranged on the liquid inlet pipe.

[0015] The liquid inlet pipe is provided with a liquid inlet pressure gauge, and the desorption pipe is provided with a regulating solenoid valve; the recoil inlet pipe is provided with a first recoil solenoid valve, and the recoil outlet pipe is provided with a second recoil solenoid valve;

[0016] A height monitoring device is provided inside the fiber ball filter.

[0017] In a second aspect, the present application also provides a surface liquid phase desolidification method for high-flux leaching solution of uranium in leaching, comprising:

[0018] Setting some solenoid valves to a first setting state and starting the stock liquid pump, collecting the inlet pressure of the leaching stock liquid based on the total inlet pressure gauge to obtain a first pressure value, wherein the first setting state includes turning on the stock liquid pump solenoid valve, the liquid inlet solenoid valve, the inlet branch solenoid valve and the regulating solenoid valve, and closing the recoil branch solenoid valve, the recoil solenoid valve, the first recoil solenoid valve and the backflow solenoid valve;

[0019] Collect overflow pressure based on the liquid inlet pressure gauge to obtain a second pressure value;

[0020] Based on the first pressure value and the second pressure value, determining a cyclone to be flushed from a plurality of hydrocyclones;

[0021] Determine the first flushing pressure and the first flushing duration based on the size parameters of the overflow screen and the backflushing pipe;

[0022] The overflow screen of the cyclone to be flushed is periodically flushed based on the first flushing pressure and the first flushing time.

[0023] The beneficial effects of the present invention are:

[0024] The present invention replaces the liquid collecting tank with the large flux-small diameter-parallel cyclone group, and couples the "centrifugal-gravity" effect to ensure the leaching flux while achieving efficient solid-liquid separation; and after the leachate is initially desolidified in the cyclone group, it flows from the overflow main pipe at the top of the cyclone group to the fiber ball filter filled with a polymer material for deep filtration and enhanced desolidification, which can effectively improve the solid-liquid separation efficiency of the leachate and reduce costs.

[0025] 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

[0026] 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.

[0027] Figure 1 It is a schematic diagram of the structure of the surface liquid phase desolidification device for high-flux leaching solution of uranium in-situ leaching described in an embodiment of the present invention;

[0028] Figure 2Schematic diagram of the structure of the cyclone group described in an embodiment of the present invention;

[0029] Figure 3 Schematic diagram of the structure of the hydrocyclone described in an embodiment of the present invention;

[0030] Figure 4 The present invention is a schematic diagram of the process of surface liquid phase desolidification method of high-flux leaching solution for in situ uranium leaching described in an embodiment of the present invention.

[0031] Markings in the figure:

[0032] 1. Inlet pipe; 2. Overflow pipe; 3. Backwash pipe; 4. Outlet pipe; 5. Separation cylinder; 6. Separation cone; 7. Annular baffle; 8. Inlet branch solenoid valve; 9. Overflow branch solenoid valve; 10. Backwash branch solenoid valve; 11. Leaching stock solution flow pipe; 12. Stock solution pump solenoid valve; 13. Total inlet pressure gauge; 14. Total inlet flow meter; 15. Liquid inlet solenoid valve; 16. Inlet main pipe; 17. Stock solution pump; 18. Outlet main pipe; 19. Overflow main pipe; 20. Liquid hopper inlet pipe; 21. Outlet pressure gauge; 22. Liquid hopper solid waste pipe; 23. Liquid hopper clear liquid pipe; 24. Backwash pipeline pump; 25. Recoil solenoid valve; 26. Liquid bucket pressure gauge; 27. Liquid bucket solenoid valve; 28. Post-processing pipeline pump; 29. ​​Pump rear solenoid valve; 30. Recoil main pipe; 31. Overflow screen; 120. Liquid inlet pipe; 121. Bypass pipe; 122. Backflow solenoid valve; 123. Backflow pump; 124. Liquid inlet pressure gauge; 125. Second recoil solenoid valve; 126. Recoil outlet pipe; 127. Fiber ball filter; 128. Adjustment solenoid valve; 129. Desorption tube; 130. First recoil solenoid valve; 131. Recoil inlet pipe; 132. Height monitoring device; 133. Fluid pressure gauge. DETAILED DESCRIPTION

[0033] 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 herein 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.

[0034] 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.

[0035] Embodiment 1:

[0036] See also Figure 1 This embodiment provides a surface liquid phase desolidification device for high-flux leaching solution of uranium in-situ leaching.

[0037] A cyclone group, the cyclone group is composed of a plurality of hydrocyclones, and the cyclone group includes an overflow main pipe 19;

[0038] The fiber ball filter 127 is composed of a hollow cylinder and two hemispherical heads. The fiber ball filter 127 is provided with a liquid inlet pipe 120, a desorption pipe 129 and a recoil tail liquid pipe. The recoil tail liquid pipe includes a recoil inlet pipe 131 and a recoil outlet pipe 126. The liquid inlet pipe 120 and the recoil outlet pipe 126 are fixedly connected to the hemispherical head at the top, the desorption pipe 129 and the recoil inlet pipe 131 are fixedly connected to the hemispherical head at the bottom, and the liquid inlet pipe 120 is connected to the overflow main pipe 19.

[0039] In the embodiment of the present application, the surface liquid phase desolidification device includes a pre-separation device and a fine filtration and enhanced separation device. The pre-separation device is a large flux-small diameter-parallel hydrocyclone group, and the fine filtration and enhanced separation device is a fiber ball filter 127.

[0040] like Figure 2 As shown, the large flux-small diameter-parallel hydrocyclone group is composed of multiple tangential flow reversing cyclones of the same structure and size. The multiple hydrocyclones are combined in parallel in a centrally symmetrical manner and occupy a small area.

[0041] The separation efficiency of the hydrocyclone is closely related to the cyclone intensity. When the inlet flow rate remains unchanged, the smaller the diameter of the hydrocyclone, the larger the centrifugal field and the greater the cyclone intensity, but the flow rate is limited. Therefore, in this application, multiple hydrocyclones are connected in parallel to achieve both "large flow" and "high efficiency".

[0042] The fiber ball filter 127 is a cylindrical device filled with fiber balls made of a polymer material. The fiber balls have been widely used in other water treatment industries, but have not yet been used in the field of in situ leaching of uranium. In this application, the fiber ball filter 127 is specifically improved as a fine filtration and enhanced separation device for the leachate, and the separation effect is remarkable.

[0043] The fiber ball filling volume occupies 1 / 2 to 2 / 3 of the fiber ball filter 127. A certain space is left at the upper end of the fiber ball filter 127 so that the fiber balls can roll up and down during the backwashing operation to enhance the backwashing effect.

[0044] The surface liquid phase desolidification device includes a common liquid hopper, which includes a liquid hopper inlet pipe 20, a liquid hopper solid waste pipe 22 and a liquid hopper clear liquid pipe 23. The liquid hopper inlet pipe 20 is fixedly connected to the outlet main pipe 18, and an outlet pressure gauge 21 is arranged on the liquid hopper inlet pipe 20; the liquid hopper clear liquid pipe 23 is connected to the recoil main pipe 30, and a recoil pipeline pump 24 and a recoil solenoid valve 25 are arranged on the liquid hopper clear liquid pipe 23 in sequence. The recoil solenoid valve 25 is arranged at one end close to the recoil main pipe 30, and a liquid hopper pressure gauge 26, a liquid hopper solenoid valve 27, a post-processing pipeline pump 28 and a post-pump solenoid valve 29 are arranged on the liquid hopper solid waste pipe 22 in sequence.

[0045] In the embodiment of the present application, the height of the common liquid hopper is not higher than 0.5 times the length of the hydrocyclone separation cone 6, and has both natural sedimentation and buffering functions; the common liquid hopper has a trapezoidal longitudinal section and has a self-flowing effect, and a liquid hopper solid waste pipe 22 is designed at the lowest end for discharging solid waste.

[0046] The surface liquid phase desolidification device comprises a leaching liquid inlet pipe 11, which is connected to an inlet main pipe 16. A liquid pump solenoid valve 121, a liquid pump 17, a liquid inlet solenoid valve 15, a total inlet flow meter 14 and a total inlet pressure gauge 13 are sequentially arranged on the leaching liquid inlet pipe 11. The total inlet pressure gauge 13 is arranged at one end close to the inlet main pipe 16.

[0047] The hydrocyclone comprises an inlet pipe 1, an overflow pipe 2, a backwash pipe 3, an outlet pipe 4, an annular baffle 7, a separation cylinder 5 and a separation cone 6. The inlet pipe 1 is tangent to the separation cylinder 5. An inlet branch electromagnetic valve 8 is arranged on the inlet pipe 1. A backwash branch electromagnetic valve 10 is arranged on the backwash pipe 3. 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 arranged at the center of the other end of the separation cylinder 5. An overflow screen 31 is sleeved on one end of the overflow pipe 2 close to the separation cylinder 5. An overflow branch electromagnetic valve 9 is arranged on one end of the overflow pipe 2 away from the separation cylinder 5. The annular baffle 7 is arranged inside the separation cylinder 5. The annular space between the annular baffle 7 and the inner wall of the separation cylinder 5 forms a cyclone chamber.

[0048] In the present application embodiment, Figure 3As shown, the structure of the hydrocyclone is in the shape of a cylinder cone, and the joint of the cylinder and cone can be processed as an integrated whole or connected using a flange structure. The upper end of the separation cylinder 5 is connected to a horizontal inlet pipe 1, which is tangent to the separation cylinder 5, and an inlet branch electromagnetic valve 8 is provided on the inlet pipe 1; the upper end of the separation cylinder 5 is concentrically connected to the overflow pipe 2, and an overflow branch electromagnetic valve 9 is provided on the overflow pipe 2; the lower end of the separation cone 6 is concentrically connected to the outlet pipe 4. Inside the separation cylinder 5 of the hydrocyclone, at the connection with the overflow pipe 2, an inverted cone overflow screen 31 is designed, the mesh number of the overflow screen 31 ranges from 200 mesh to 400 mesh, and the length of the overflow screen 31 is about 0.15 times to 0.3 times the length of the separation cylinder 5.

[0049] The working principle of the hydrocyclone is as follows: after the liquid-solid two-phase leachate enters the separation cylinder 5 tangentially from the horizontal inlet pipe 1, it is affected by the wall constraint force and generates centrifugal force inside the equipment. Under the dual effects of centrifugal force and gravity, the heavier solid phase is thrown to the side wall, then flows downward and flows out from the outlet pipe 4, while the lighter liquid phase is in the center of the equipment, rotating and flowing upward, and flows out from the overflow pipe 2, thereby realizing the liquid phase solid removal function.

[0050] Within a certain flow rate range of the inlet pipe 1, the separation efficiency of a single hydrocyclone is proportional to the centrifugal force, that is, inversely proportional to the diameter of the separation cylinder 5, and the processing volume is proportional to the diameter of the separation cylinder 5. Therefore, by connecting multiple small-diameter hydrocyclones in parallel, efficient liquid-phase solid removal can be achieved and large flux can be met; if the flow rate decreases, in order to ensure efficient separation, one or more hydrocyclones can be controlled to close to deal with it, making the device very robust.

[0051] The hydrocyclone group further includes an inlet manifold 16, an outlet manifold 18 and a recoil manifold 30, wherein the inlet pipes 1 of the multiple hydrocyclones are connected in parallel to form the inlet manifold 16, the overflow pipes 2 of the multiple hydrocyclones are connected in parallel to form the overflow manifold 19, the outlet pipes 4 of the multiple hydrocyclones are connected in parallel to form the outlet manifold 18, and the recoil pipes 3 of the multiple hydrocyclones are connected in parallel to form the recoil manifold 30;

[0052] In the embodiment of the present application, a plurality of hydrocyclones are integrated in parallel to form a hydrocyclone group, and a common liquid bucket is additionally provided around the outlet pipe 4. The leachate first flows into the inlet main pipe 16, and then is divided into each hydrocyclone. After the liquid phase desolidification is completed, the clear liquid flows out from the overflow pipe 2 of each device into the overflow main pipe 19, and then flows from the overflow main pipe 19 into the subsequent filtering equipment; the turbid liquid flows out from the outlet pipe 4 of the hydrocyclone, and enters the common liquid bucket through the outlet main pipe 18.

[0053] The fiber ball filter 127 further includes a bypass pipe 121, on which a backflow pump 123 and a backflow solenoid valve 122 are arranged, one end of the bypass pipe 121 is arranged on a desorption pipe 129, and the other end of the bypass pipe 121 is arranged on a liquid inlet pipe 120, on which a liquid inlet pressure gauge 124 is arranged, and on which a regulating solenoid valve 128 is arranged; a first backwash solenoid valve 130 is arranged on a backwash inlet pipe 131, and a second backwash solenoid valve 125 is arranged on a backwash outlet pipe 126; a height monitoring device 132 is arranged in the fiber ball filter 127;

[0054] In the embodiment of the present application, the reflux pump 123 and the reflux solenoid valve 122 on the bypass pipe 121 are used to reflux part of the clear liquid flowing out of the desorption tube 129 back into the liquid inlet pipe 120 when the filtered clear liquid output by the fiber ball filter 127 does not meet the conditions, and perform the filtering operation again based on the fiber ball filter 127.

[0055] Embodiment 2:

[0056] This embodiment provides a surface liquid phase desolidification method for high-flux leaching solution of uranium in-situ leaching.

[0057] like Figure 4 As shown in the figure, the method includes step S10, step S20, step S30, step S40 and step S50:

[0058] Step S10. Set some solenoid valves to the first setting state and start the stock liquid pump 17, collect the inlet pressure of the leaching stock solution based on the total inlet pressure gauge 13, and obtain a first pressure value. The first setting state includes opening the stock liquid pump solenoid valve 121, the liquid inlet solenoid valve 15, the inlet branch solenoid valve 8 and the regulating solenoid valve 128, and closing the recoil branch solenoid valve 10, the recoil solenoid valve 25, the first recoil solenoid valve 130 and the backflow solenoid valve 122;

[0059] Step S20. Collect the overflow pressure based on the liquid inlet pressure gauge 124 to obtain a second pressure value;

[0060] Step S30. Based on the first pressure value and the second pressure value, determining a cyclone to be flushed from a plurality of hydrocyclones;

[0061] Specifically, during the actual operation of the cyclone group, the blockage conditions of the overflow screens 31 of different hydrocyclones may be different. Considering that only the hydrocyclone group with more serious blockage needs to be flushed, the present application determines the cyclone to be flushed that needs to be backwashed through the ratio of the first pressure value to the second pressure value.

[0062] Specifically, step S30 specifically includes step S31, step S32 and step S33:

[0063] Step S31. By controlling the switch state of each overflow branch solenoid valve 9, the overflow pressure of each hydrocyclone is obtained, and multiple overflow pressures are obtained;

[0064] Step S32. Calculate the ratio of the first pressure value to the multiple overflow pressure values ​​to obtain multiple pressure ratios;

[0065] Step S33. Compare the multiple pressure ratios with the preset ratio range to determine the cyclone to be flushed, and the pressure ratio of the cyclone to be flushed does not belong to the preset ratio range;

[0066] Specifically, under normal circumstances, the fluctuation range of the first pressure value is small, and the second pressure value of each hydrocyclone will change according to the fluctuation of the first pressure value and gradually increase as the working time increases. When the pressure ratio of the first pressure value to the second pressure value does not meet the preset ratio range, the corresponding hydrocyclone is obviously blocked and needs to be backwashed.

[0067] Step S40. Determine the first flushing pressure and the first flushing duration based on the size parameters of the overflow screen 31 and the backflushing tube 3;

[0068] Specifically, step S40 specifically includes step S41, step S42, step S43, step S44, step S45, step S46, step S47, step S48, step S49, step S410 and step S411:

[0069] Step S41. Obtain the current ambient temperature, and determine the surface tension of the overflow screen 31 based on the current ambient temperature;

[0070] Step S42. Obtaining the pore diameter, porosity, operation time and filtration flow rate of the overflow screen 31;

[0071] Step S43. Determine the thickness of the adhesion on the overflow screen 31 based on the operation time and the filtration flow rate;

[0072] Step S44. Based on the surface tension, the pore diameter and the porosity, a first pressure is calculated, and the first pressure is used to characterize the pore resistance that the liquid needs to overcome to pass through the overflow screen 31;

[0073] Step S45. Based on the pore diameter, the thickness of the adhered matter and the preset particle adhesion coefficient, a second pressure is calculated, and the second pressure is used to characterize the adhesion force that the particles attached to the overflow screen 31 need to overcome;

[0074] Step S46. Calculate the sum of the first pressure and the second pressure to obtain a first flushing pressure;

[0075] Specifically, based on the filtration theory, after the overflow screen 31 is clogged, the flushing pressure can be estimated by balancing the adhesion force of the adhered matter and the flushing force of the backwashing fluid.

[0076] Assuming that the pore diameter of the overflow screen 31 is d, the thickness of the adherend is h, and the porosity of the filter medium is ε, the first flushing pressure calculation formula is:

[0077]

[0078] Wherein, P is the first flushing pressure; γ is the surface tension, which is 7.2 mN / m at 25°C; ε ​​is the porosity; h is the thickness of the adherend; d is the pore diameter; and k is a constant related to the particle adhesion force.

[0079] The first term of the above formula represents the pore resistance that the liquid needs to overcome when passing through the filter cloth; the second term of the formula is the adhesion force that needs to be overcome to attach the adherend, which is proportional to the thickness h of the adherend.

[0080] Step S47. Calculate the mass of the adhesion based on the thickness of the adhesion and the preset density of the adhesion;

[0081] Step S48. Determine the filtration area based on the size parameters of the overflow screen 31;

[0082] Step S49. Determine the backwash flow rate based on the first flushing pressure and the size parameters of the backwash tube 3;

[0083] Step S410. Calculate the product of the adhesion density, the filtration area and the backwash flow rate to obtain the product result;

[0084] Step S411. Calculate the ratio of the mass of the adhered matter to the product result to obtain the first flushing time;

[0085] Specifically, the first flushing time is mainly determined by the backwashing flow rate and the geometric characteristics of the overflow screen 31. Assuming that a certain proportion of adhesions are removed by backwashing, the backwashing time can be calculated by the following formula:

[0086]

[0087] Wherein, m is the mass of the adhered matter; ρ is the density of the adhered matter; S is the filtration area of ​​the overflow screen 31; v is the backwashing flow rate; and t is the first flushing time.

[0088] Step S50: periodically flushing the overflow screen 31 of the cyclone to be flushed based on the first flushing pressure and the first flushing time;

[0089] Step S60. Obtain the volume and flow rate of the filtered fluid of the fiber ball filter 127, and collect the fiber ball height value in real time based on the height monitoring device 132;

[0090] Step S70. Calculate the flow ratio based on the volume of the filtered fluid and the fiber ball height value, the flow ratio is used to characterize the operating load and cumulative processing capacity of the fiber ball filter 127;

[0091] Step S80. When the flow ratio is greater than the set threshold, the pressure value is collected based on the liquid inlet pressure gauge 124 to obtain a third pressure value;

[0092] Step S90. Determine a second flushing pressure and a second flushing duration of the fiber ball filter 127 based on the third pressure value and the second pressure value;

[0093] Step S100. Periodically flush the fiber balls in the fiber ball filter 127 based on the second flushing pressure and the second flushing duration;

[0094] Specifically, after the cyclone group is backwashed, when the difference between the pressure value collected by the liquid hopper pressure gauge 26 on the common liquid hopper and the first pressure value exceeds the set threshold, the common liquid hopper solid waste discharge procedure is executed, that is, the post-processing pipeline pump 28 is opened to transport the solid waste slurry to the post-processing process.

[0095] The liquid phase separated by the cyclone group enters the fiber ball filter 127 for secondary separation by deep filtration. The fiber ball filter 127 is equipped with a flow meter and a liquid inlet pressure gauge 124 to monitor the flow ratio and the equipment pressure of the fiber ball filter 127.

[0096] When the flow ratio exceeds the set threshold and the difference between the equipment pressure of the fiber ball filter 127 and the first pressure value is greater than a certain threshold, the flushing process of the fiber ball filter 127 is executed. It is necessary to close the liquid inlet pipe 120 and the desorption pipe 129 of the fiber ball filter 127, and open the bypass pipe 121, the backwash inlet pipe 131 and the backwash outlet pipe 126 until the equipment pressure of the fiber ball filter 127 is within the normal range.

[0097] The clear liquid output from the fiber ball filter 127 will be tested in real time. If the clear liquid fails the test, the desorption tube 129 will be closed and the clear liquid will be pumped to the liquid inlet pipe 120 of the fiber ball filter 127 for re-filtration until the clear liquid passes the test and is pumped to the subsequent water metallurgical process.

[0098] 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.

[0099] 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 surface liquid phase desolidification device for high-flux leaching solution of uranium in situ leaching, characterized in that: include: A cyclone group, the cyclone group is composed of a plurality of hydrocyclones, and the cyclone group includes an overflow main pipe (19); A fiber ball filter (127), the fiber ball filter (127) is composed of a hollow cylinder and two hemispherical heads, the fiber ball filter (127) is provided with a liquid inlet pipe (120), a desorption pipe (129) and a recoil tail liquid pipe, the recoil tail liquid pipe includes a recoil inlet pipe (131) and a recoil outlet pipe (126), the liquid inlet pipe (120) and the recoil outlet pipe (126) are fixedly connected to the hemispherical head at the top, the desorption pipe (129) and the recoil inlet pipe (131) are fixedly connected to the hemispherical head at the bottom, and the liquid inlet pipe (120) is connected to the overflow main pipe (19).

2. The surface liquid phase desolidification device for high-flux leaching solution of in-situ uranium leaching according to claim 1 is characterized in that The device comprises a common liquid bucket, wherein the common liquid bucket comprises a liquid bucket inlet pipe (20), a liquid bucket solid waste pipe (22) and a liquid bucket clear liquid pipe (23). The liquid hopper inlet pipe (20) is fixedly connected to the outlet main pipe (18), and an outlet pressure gauge (21) is provided on the liquid hopper inlet pipe (20); The liquid hopper clear liquid pipe (23) is in communication with the recoil main pipe (30), and a recoil pipeline pump (24) and a recoil solenoid valve (25) are sequentially arranged on the liquid hopper clear liquid pipe (23), and the recoil solenoid valve (25) is arranged at one end close to the recoil main pipe (30). The liquid hopper solid waste pipe (22) is provided with a liquid hopper pressure gauge (26), a liquid hopper electromagnetic valve (27), a post-processing pipeline pump (28) and a post-pump electromagnetic valve (29) in sequence.

3. The surface liquid phase desolidification device for high-flux leaching solution of in-situ uranium leaching according to claim 1 is characterized in that The device comprises a leachable liquid inlet pipe (11), the leachable liquid inlet pipe (11) is connected to the inlet main pipe (16), and the leachable liquid inlet pipe (11) is provided with a liquid pump solenoid valve (121), a liquid pump (17), a liquid inlet solenoid valve (15), a total inlet flow meter (14) and a total inlet pressure gauge (13) in sequence, and the total inlet pressure gauge (13) is arranged at one end close to the inlet main pipe (16).

4. The surface liquid phase desolidification device for high-flux leaching solution of uranium in situ leaching according to claim 1 is characterized in that The hydrocyclone comprises an inlet pipe (1), an overflow pipe (2), a backwash pipe (3), an outlet pipe (4), an annular baffle (7), a separation cylinder (5) and a separation cone (6); the inlet pipe (1) is tangent to the separation cylinder (5); an inlet branch electromagnetic valve (8) is provided on the inlet pipe (1); a backwash pipe (3) is provided with a backwash branch electromagnetic valve (10); one end of the separation cylinder (5) is fixed to the circular bottom surface of the separation cone (6); The separation cylinder (5) is connected to the separator, an overflow pipe (2) is arranged at the center of the other end of the separation cylinder (5), an overflow screen (31) is sleeved on one end of the overflow pipe (2) close to the separation cylinder (5), an overflow branch electromagnetic valve (9) is arranged on one end of the overflow pipe (2) away from the separation cylinder (5), the annular baffle (7) is arranged inside the separation cylinder (5), and the annular space between the annular baffle (7) and the inner wall of the separation cylinder (5) forms a vortex chamber; The hydrocyclone group further comprises an inlet manifold (16), an outlet manifold (18) and a recoil manifold (30); a plurality of inlet pipes (1) of the hydrocyclones are connected in parallel to form the inlet manifold (16); a plurality of overflow pipes (2) of the hydrocyclones are connected in parallel to form the overflow manifold (19); a plurality of outlet pipes (4) of the hydrocyclones are connected in parallel to form the outlet manifold (18); and a plurality of recoil pipes (3) of the hydrocyclones are connected in parallel to form the recoil manifold (30).

5. The surface liquid phase desolidification device for high-flux leaching solution of in-situ uranium leaching according to claim 1 is characterized in that The fiber ball filter (127) further comprises a bypass pipe (121), on which a backflow pump (123) and a backflow solenoid valve (122) are arranged, one end of the bypass pipe (121) is arranged on the desorption pipe (129), and the other end of the bypass pipe (121) is arranged on the liquid inlet pipe (120), The liquid inlet pipe (120) is provided with a liquid inlet pressure gauge (124), and the desorption pipe (129) is provided with a regulating electromagnetic valve (128); the recoil inlet pipe (131) is provided with a first recoil electromagnetic valve (130), and the recoil outlet pipe (126) is provided with a second recoil electromagnetic valve (125); A height monitoring device (132) is arranged inside the fiber ball filter (127).

6. A method for removing solids from the surface liquid phase of a large-flux leaching solution of uranium in situ leaching, characterized in that: include: Setting some solenoid valves to a first setting state and starting a stock liquid pump (17), collecting the inlet pressure of the leaching stock liquid based on a total inlet pressure gauge (13), and obtaining a first pressure value, wherein the first setting state includes starting a stock liquid pump solenoid valve (121), a liquid inlet solenoid valve (15), an inlet branch solenoid valve (8), and a regulating solenoid valve (128), and closing a recoil branch solenoid valve (10), a recoil solenoid valve (25), a first recoil solenoid valve (130), and a backflow solenoid valve (122); Collecting overflow pressure based on a liquid inlet pressure gauge (124) 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; Determining a first flushing pressure and a first flushing duration based on the size parameters of the overflow screen (31) and the backflushing pipe (3); The overflow screen (31) of the cyclone to be flushed is periodically flushed based on the first flushing pressure and the first flushing time.

7. The method for surface liquid phase solid removal of high-flux leaching solution for in-situ uranium leaching according to claim 6, characterized in that: Based on the first pressure value and the second pressure value, determining a cyclone to be flushed from a plurality of hydrocyclones, comprising: By controlling the on / off state of each overflow branch electromagnetic valve (9), the overflow pressure of each hydrocyclone is obtained, thereby obtaining a plurality of overflow pressures; Calculating ratios of the first pressure value to a plurality of overflow pressure values ​​to obtain a plurality of pressure ratios; A plurality of pressure ratios are compared with a preset ratio range to determine a cyclone to be flushed, wherein the pressure ratio of the cyclone to be flushed does not belong to the preset ratio range.

8. The method for surface liquid phase solid removal of high-flux leaching solution for in-situ uranium leaching according to claim 6, characterized in that: Based on the size parameters of the overflow screen (31) and the backwash pipe (3), determining the first flushing pressure and the first flushing duration includes: Acquiring the current ambient temperature, and determining the surface tension of the overflow screen (31) based on the current ambient temperature; Obtaining the pore diameter, porosity, operation time and filtration flow rate of the overflow screen (31); Determining the thickness of the adhered matter on the overflow screen (31) based on the operation time and the filtration flow rate; Based on the surface tension, the pore diameter and the porosity, a first pressure is calculated, wherein the first pressure is used to characterize the pore resistance that the liquid needs to overcome to pass through the overflow screen (31); Based on the pore diameter, the thickness of the adhered matter and a preset particle adhesion coefficient, a second pressure is calculated, and the second pressure is used to characterize the adhesion force that the particles attached to the overflow screen (31) need to overcome; The first flushing pressure is obtained by calculating the sum of the first pressure and the second pressure.

9. The method for surface liquid phase solid removal of high-flux leaching solution for in-situ uranium leaching according to claim 8, characterized in that: Based on the size parameters of the overflow screen (31) and the backwash pipe (3), determining the first flushing pressure and the first flushing duration includes: Calculating the mass of the adhesion material based on the adhesion material thickness and a preset adhesion material density; Determining a filtration area based on the size parameters of the overflow screen (31); Determining a backwash flow rate based on the first flushing pressure and the size parameters of the backwash tube (3); Calculating the product of the adhesion density, the filtration area and the backwash flow rate to obtain a product result; The ratio of the mass of the adhered matter to the multiplication result is calculated to obtain the first flushing time.

10. The method for surface liquid phase solid removal of high-flux leaching solution for in-situ uranium leaching according to claim 6, characterized in that: After periodically flushing the overflow screen (31) of the cyclone to be flushed based on the first flushing pressure and the first flushing time, the method comprises: Obtaining the volume and flow rate of filtered fluid of the fiber ball filter (127), and collecting the fiber ball height value in real time based on the height monitoring device (132); Calculating a flow ratio based on the filtered fluid volume and the fiber ball height value, wherein the flow ratio is used to characterize the operating load and cumulative processing capacity of the fiber ball filter (127); When the flow ratio is greater than a set threshold, a pressure value is collected based on a liquid inlet pressure gauge (124) to obtain a third pressure value; Determining a second flushing pressure and a second flushing duration of the fiber ball filter (127) based on the third pressure value and the second pressure value; The fiber balls in the fiber ball filter (127) are periodically flushed based on the second flushing pressure and the second flushing time.

Images