Heat exchange system of thickener

Abstract

The invention relates to a thickener heat exchange system, and belongs to the technical field of ore pulp treatment. Comprising a first heat exchange assembly and a second heat exchange assembly. The first heat exchange assembly and the second heat exchange assembly are both arranged in the thickener; the first heat exchange assembly and the second heat exchange assembly are internally provided with heat exchange media. The heat exchange medium is a reaction medium from a fission bin, and the heat exchange medium flows back to the fission bin after completing heat exchange in the thickener. The waste heat utilization of the fission bin and the ore pulp cooling process of the thickener are combined into a whole, so that not only is the equipment resource saved, but also the energy consumption of the system is obviously reduced. The viscosity of the ore pulp can be reduced by properly increasing the temperature of the ore pulp, the flowability of solid particles in the ore pulp is improved, the particles can settle to the bottom more quickly, and therefore the solid-liquid separation efficiency of the thickener is improved.

Description

Technical Field

[0001] The present invention belongs to the technical field of slurry processing, and relates to a technology for supplying heat energy from a fission chamber to a thickener, and in particular to a heat exchange system for a thickener. Background Art

[0002] In the slurry treatment process, the thickener is a key solid-liquid separation equipment, which is widely used in mining, chemical and other fields. The main function of the thickener is to separate the solid particles in the slurry by gravity sedimentation to form a high-concentration slurry and an upper clarified liquid. By using a stirring device, a flocculant and a tank structure design, the thickener can achieve a high sedimentation efficiency. However, since the temperature of the slurry has a significant impact on its fluidity and separation performance, in practical applications, reasonable temperature control becomes a key factor affecting the performance of the thickener.

[0003] In this context, fission chambers, as an auxiliary equipment in slurry processing, are widely used in links that require heating, cooling or specific temperature control. Fission chambers usually generate heat through fission reactions. However, there are major problems with heat management in traditional fission chamber systems. Generally, the high-temperature reaction medium generated by the fission chamber needs to be cooled with the help of an external heat exchanger to ensure the safety and stability of the system. This cooling method has the following problems:

[0004] After the high-temperature medium in the fission chamber is cooled by an external heat exchanger, the heat generated is not reasonably utilized, resulting in a large amount of energy being directly discharged, affecting the energy efficiency of the overall system.

[0005] The external heat exchanger needs to be equipped with cooling water or other cooling media, and the cooling pipe system is complicated, which not only increases the operation and maintenance costs, but also increases resource consumption, making it difficult to achieve energy conservation and environmental protection. Summary of the invention

[0006] In order to solve the above-mentioned problems in the prior art, the present invention provides a thickener heat exchange system.

[0007] In order to achieve the above object, the technical solution adopted by the present invention is:

[0008] A thickener heat exchange system is provided, comprising:

[0009] a first heat exchange component and a second heat exchange component;

[0010] The first heat exchange component and the second heat exchange component are both disposed in the thickener;

[0011] Wherein, the first heat exchange component and the second heat exchange component contain heat exchange medium;

[0012] Furthermore, the heat exchange medium is a reaction medium from the fission chamber, and after completing heat exchange in the thickener, the heat exchange medium flows back to the fission chamber;

[0013] Wherein, the first heat exchange component is arranged on the inner wall surface of the thickener;

[0014] Wherein, the second heat exchange component is arranged on the inner bottom surface of the thickener;

[0015] Furthermore, the first heat exchange component and the second heat exchange component form an annular convection area;

[0016] The ore slurry in the convection zone forms a convection flow.

[0017] Preferably, the first heat exchange component comprises:

[0018] a first heat exchange coil disposed along the inner wall surface of the thickener;

[0019] Wherein, in the first direction, the cross-sectional diameter D of the first heat exchange coil decreases successively;

[0020] The first direction is the direction from the bottom surface of the thickener to the opening of the thickener;

[0021] Furthermore, the heat exchange medium enters through the first heat exchange tube with the largest cross-sectional diameter D, and flows out through the first heat exchange tube with the smallest cross-sectional diameter D.

[0022] Preferably, the height of the first heat exchange assembly from the bottom surface of the thickener is H1, the overall height of the thickener is H2, and the following conditions are satisfied:

[0023] H1=K1*H2, the value range of K1 is 0.4 to 0.7.

[0024] Preferably, the first heat exchange component comprises:

[0025] Heat exchange chamber;

[0026] Wherein, the first heat exchange coil is arranged in the heat exchange chamber;

[0027] Wherein, the wall surface of the heat exchange chamber in contact with the slurry is provided with heat exchange fins;

[0028] Furthermore, the heat exchange fins and the wall surface of the heat exchange chamber form an angle a;

[0029] The angle a ranges from 30° to 45°.

[0030] Preferably, the second heat exchange component comprises:

[0031] A heat exchange cylinder is arranged at the center of the bottom surface of the thickener;

[0032] A second heat exchange coil is arranged inside the heat exchange tube;

[0033] Wherein, in the first direction, the diameters of the heat exchange tubes decrease successively.

[0034] Preferably, it also includes:

[0035] A flow-blocking component, disposed between the first heat exchange component and the second heat exchange component;

[0036] Wherein, the flow-blocking component at least forms an annular sedimentation channel;

[0037] Furthermore, the height of the sedimentation channel is smaller than the height of the first heat exchange coil.

[0038] Preferably, the flow blocking component comprises:

[0039] a first spoiler and a second spoiler;

[0040] The first baffle is disposed at a position close to the first heat exchange component;

[0041] The second baffle is disposed near the second heat exchange component;

[0042] Furthermore, the sedimentation channel is formed between the first spoiler and the second spoiler.

[0043] Preferably, the maximum width of the sedimentation channel is W1, and the minimum width is W2, wherein:

[0044] W2=K2*W1, the value range of K2 is 0.5 to 0.8.

[0045] Preferably, it includes:

[0046] Loop component;

[0047] wherein the circulation component forms at least a first port and a second port;

[0048] Wherein, the second port is arranged above the first heat exchange component;

[0049] Furthermore, the first port is communicated with the second port;

[0050] The first port is configured to guide a portion of the slurry in the liquid surface area to the second port;

[0051] The second port is configured to direct the slurry to the convection region.

[0052] Preferably, there are a plurality of the second ports, and the plurality of the second ports have a height difference;

[0053] The plurality of second ports with height differences are configured to adaptively guide the slurry following the change in the liquid level.

[0054] The present invention provides a thickener heat exchange system, and the beneficial effects of the present invention are embodied in:

[0055] Combining the waste heat utilization of the fission chamber with the thickener slurry cooling process not only saves equipment resources, but also significantly reduces the energy consumption of the system, which meets the urgent needs of modern industry for energy conservation and environmental protection.

[0056] On the other hand, during the heat exchange process, the temperature of the slurry in the thickener increases, thereby improving its sedimentation performance: an appropriate increase in the slurry temperature will reduce the slurry viscosity, improve the fluidity of the solid particles in the slurry, and enable the particles to settle to the bottom faster, thereby improving the solid-liquid separation efficiency of the thickener. BRIEF DESCRIPTION OF THE DRAWINGS

[0057] Figure 1 A three-dimensional diagram of the thickener heat exchange system proposed by the present invention;

[0058] Figure 2 It is a front view of the thickener heat exchange system proposed by the present invention;

[0059] Figure 3 A top view of the thickener heat exchange system proposed by the present invention;

[0060] Figure 4 A cross-sectional view of a thickener heat exchange system according to the present invention;

[0061] Figure 5 for Figure 4 A front view of the structure shown;

[0062] Figure 6 for Figure 5 A local enlarged schematic diagram at point A;

[0063] Figure 7 for Figure 5 A partial enlarged schematic diagram at point B.

[0064] Description of reference numerals:

[0065] 1. thickener; 2. first heat exchange component; 201. first heat exchange coil; 202. heat exchange chamber; 3. second heat exchange component; 301. heat exchange cylinder; 302. second heat exchange coil; 4. baffle component; 401. settling channel; 402. first baffle plate; 403. second baffle plate; 5. circulation component; 501. first port; 502. second port. DETAILED DESCRIPTION

[0066] The following will be combined with the drawings in the embodiments of the present invention to clearly and completely describe the technical solutions in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0067] See also Figures 1 to 7 As shown, the specific embodiments provided by the present invention are as follows:

[0068] like Figures 1 to 3 As shown, the first embodiment of the present invention provides a thickener heat exchange system, comprising:

[0069] A first heat exchange component 2 and a second heat exchange component 3;

[0070] The first heat exchange component 2 and the second heat exchange component 3 are both arranged in the thickener 1;

[0071] Wherein, the first heat exchange component 2 and the second heat exchange component 3 contain heat exchange medium;

[0072] Furthermore, the heat exchange medium is the reaction medium from the fission chamber;

[0073] Wherein, the first heat exchange component 2 is arranged on the inner wall surface of the thickener 1;

[0074] Wherein, the second heat exchange component 3 is arranged on the inner bottom surface of the thickener 1;

[0075] Furthermore, the first heat exchange component 2 and the second heat exchange component 3 form an annular convection area;

[0076] The ore slurry in the convection zone forms a convection flow.

[0077] In this embodiment, the thickener heat exchange system directly introduces the high-temperature reaction medium of the fission chamber into the thickener 1, thereby eliminating the need for an external heat exchanger originally required for the fission chamber and avoiding energy waste. The reaction medium is cooled by the slurry in the thickener 1, thereby directly recovering and utilizing the waste heat, thereby effectively improving the energy efficiency of the system.

[0078] Specifically, in a conventional fission chamber thermal management system, the cooling of the high-temperature reaction medium usually relies on an independent external heat exchanger. This type of heat exchange system has a complex structure, occupies a large space for the equipment, requires additional cooling water or cooling medium, has high energy consumption, and has a high maintenance frequency. However, this embodiment directly introduces the high-temperature reaction medium of the fission chamber into the thickener 1, uses the slurry itself as the cooling medium, eliminates the external heat exchanger and its supporting cooling system, reduces the demand for the cooling water system, and reduces the equipment complexity and installation cost.

[0079] The waste heat from the fission chamber is introduced into the thickener 1, so that the heat energy that would have been directly discharged by the cooling system can be utilized, forming an internal heat energy cycle. The external heat exchanger is easily affected by sediments during long-term operation, which increases the maintenance burden of the equipment. However, by using the natural convection cooling medium of the slurry, this design avoids the failure and wear of external equipment, reduces maintenance costs, and effectively extends the service life of the equipment.

[0080] This design combines the waste heat utilization of the fission chamber with the slurry cooling process of the thickener 1, which not only saves equipment resources, but also significantly reduces the energy consumption of the system, meeting the urgent needs of modern industry for energy conservation and environmental protection.

[0081] On the other hand, during the heat exchange process, the temperature of the slurry in the thickener 1 increases, thereby improving its sedimentation performance: an appropriate increase in the slurry temperature will reduce the slurry viscosity, improve the fluidity of the solid particles in the slurry, and enable the particles to settle to the bottom faster, thereby improving the solid-liquid separation efficiency of the thickener 1.

[0082] Moreover, by heating the slurry to improve the settling efficiency, the residence time of the slurry in the thickener 1 can be reduced, rapid separation can be achieved, and the processing capacity can be increased. This design effectively compensates for the problem of unstable settling speed caused by temperature fluctuations in traditional cooling methods.

[0083] By directly utilizing the waste heat of the fission chamber, this embodiment not only achieves the purpose of temperature control, but also realizes a significant improvement in the slurry settling performance.

[0084] On the other hand, the layout of the first heat exchange assembly 2 and the second heat exchange assembly 3 forms an annular convection area. This design produces a unique flow pattern in the clear liquid area of ​​the thickener 1, specifically:

[0085] The convection flow causes the originally fine particles in the clear liquid layer to contact and collide with each other, gradually agglomerating into larger particles. This agglomeration phenomenon improves the sedimentation of the particles, allowing the fine particles to settle to the bottom, thereby further improving the solid-liquid separation effect of the thickener 1.

[0086] Small particles in the conventional thickener 1 are often difficult to effectively settle and remain in the clear liquid, affecting the quality of the clear liquid. However, in this embodiment, the small particles in the clear liquid are accelerated to agglomerate through convection circulation, which greatly improves the clarity of the clear liquid and provides a higher quality separation medium for the downstream process.

[0087] The design of the annular convection area enables spontaneous convection to form inside the thickener 1, without the need for additional stirring equipment or fluid guiding structures, thereby simplifying the system design and improving operational stability. This automated flow pattern improves the particle settling efficiency in the clear liquid layer and maintains the clarification effect of the clear liquid layer.

[0088] The design of the annular convection area innovatively combines the convection of the slurry and the agglomeration process of small particles in the clear liquid, achieving a double separation effect. This not only simplifies the system structure, but also effectively solves the problem that the clear liquid in the traditional thickener 1 is difficult to completely clarify.

[0089] like Figures 4 to 5 As shown, the second embodiment of the present invention provides a thickener heat exchange system, and based on the first embodiment, the first heat exchange component 2 includes:

[0090] The first heat exchange coil 201 is arranged along the inner wall surface of the thickener 1;

[0091] Wherein, in the first direction, the cross-sectional diameter D of the first heat exchange coil 201 decreases successively;

[0092] The first direction is the direction from the bottom surface of the thickener 1 to the opening of the thickener 1;

[0093] Furthermore, the heat exchange medium enters through the first heat exchange tube with the largest cross-sectional diameter D, and flows out through the first heat exchange tube with the smallest cross-sectional diameter D.

[0094] In this embodiment, by further optimizing the structure of the first heat exchange assembly 2, a first heat exchange coil 201 structure with a gradually decreasing cross-sectional diameter is adopted. The first heat exchange coil 201 is arranged along the inner wall surface of the thickener 1, and the cross-sectional diameter D is gradually reduced in the direction from the bottom surface of the thickener 1 to the opening (i.e., the first direction).

[0095] The heat exchange medium enters from the part with the largest cross-sectional diameter D and gradually flows to the part with the smallest cross-sectional diameter D. As the diameter of the first heat exchange coil 201 gradually decreases, the flow rate of the medium in the tube gradually increases, and the turbulent effect of the fluid is enhanced, thereby improving the heat transfer efficiency. Specifically, in laminar flow, the fluid flows in layers, and the heat exchange between the inner layer and the tube wall is slow. In turbulent flow, the fluid is constantly mixed and disturbed, and the high-temperature or low-temperature fluid in the inner layer is more easily brought to the vicinity of the tube wall and exchanges heat with the tube wall. This turbulent flow characteristic significantly improves the heat transfer efficiency. Therefore, as the diameter of the first heat exchange coil 201 gradually decreases, the flow rate increases, the turbulence is enhanced, and the heat transfer efficiency is improved. This gradually shrinking cross-sectional design makes full use of the principles of fluid mechanics, so that the heat exchange medium is evenly cooled or heated throughout the path of the first heat exchange coil 201, ensuring the uniformity of the temperature distribution in the inner wall area of ​​the thickener 1, which is conducive to improving the overall sedimentation efficiency of the slurry.

[0096] Moreover, by allowing the heat exchange medium to enter from the heat exchange tube with a larger diameter and gradually flow to the area with a smaller diameter, a relatively smooth temperature gradient can be established during the heat exchange process. This temperature gradient optimizes the heat distribution at various heights on the inner wall surface of the thickener 1, so that the slurry forms a more uniform heat transfer in the side wall area, which helps to maintain the convection flow of the slurry in the thickener 1, thereby improving the sedimentation effect of solid particles.

[0097] On the other hand, the gradually shrinking structural design of the first heat exchange coil 201 helps to evenly distribute the fluid pressure between different diameter areas, reducing the resistance generated when the heat exchange medium flows in the tube. In this way, the system energy consumption can be reduced while ensuring a good heat exchange effect, making the operation of the entire thickener 1 system more economical and efficient.

[0098] The heat exchange coils in this embodiment are arranged along the inner wall and gradually shrink as the height changes, creating a temperature gradient along the side wall, so that the temperature of the slurry near the clear liquid layer is relatively high, which is conducive to the small particles in the clear liquid layer being affected by the temperature difference and further agglomerating. The small particles in the clear liquid layer area of ​​the thickener 1 aggregate into larger particles under the action of convection and eventually settle to the bottom, thereby improving the clarity and separation effect of the slurry.

[0099] The third embodiment of the present invention provides a thickener heat exchange system, and based on the previous embodiment, the height of the first heat exchange component 2 from the bottom surface of the thickener 1 is H1, the overall height of the thickener 1 is H2, and the following conditions are satisfied:

[0100] H1=K1*H2, the value range of K1 is 0.4 to 0.7.

[0101] In this embodiment, the installation height of the first heat exchange assembly 2 relative to the bottom surface of the thickener 1 is further optimized, and the first heat exchange assembly 2 is arranged at a position H1 from the bottom surface, which ensures that the temperature gradient in the thickener 1 is optimally distributed within a height range of 0.4 to 0.7. The reasonable distribution of the temperature gradient forms a natural annular convection flow, which helps the slurry to form a stable convection cycle in the thickener 1, thereby effectively improving the sedimentation speed and separation efficiency of the slurry.

[0102] By optimizing the installation height of the first heat exchange component 2 so that it acts on the middle area of ​​the slurry, the problem of uneven temperature caused by the heat exchange component being too high or too low is effectively avoided. A more uniform temperature distribution can improve the fluidity of the slurry, especially in the middle area. The slurry with a moderate temperature is more conducive to the sedimentation of solid particles, avoiding the accumulation of particles at the bottom and affecting the separation effect.

[0103] When the first heat exchange component 2 is located at an appropriate height, the temperature at this height can guide the small particles in the clear liquid layer to agglomerate more fully. Specifically, through convection, these small particles contact and aggregate under the drive of temperature difference, thereby forming larger particles, which eventually settle to the bottom. In this way, the small particles in the clear liquid layer are effectively removed, significantly improving the clarity of the clear liquid.

[0104] Placing the first heat exchange component 2 within an appropriate height range (i.e., 0.4 to 0.7 times the height) can reduce unnecessary heating areas and avoid energy waste. At the same time, this position relationship helps to improve heat exchange efficiency, reduce the flow resistance of the heat exchange medium, and enable the entire system to achieve energy saving and consumption reduction while maintaining efficient heat exchange.

[0105] The fourth embodiment of the present invention provides a thickener heat exchange system, and based on the previous embodiment, the first heat exchange component 2 includes:

[0106] Heat exchange chamber 202;

[0107] Wherein, the first heat exchange coil 201 is disposed in the heat exchange chamber 202;

[0108] Wherein, the wall surface of the heat exchange chamber 202 in contact with the slurry has heat exchange fins;

[0109] Furthermore, the heat exchange fins and the wall surface of the heat exchange chamber 202 form an angle a;

[0110] The angle a ranges from 30° to 45°.

[0111] In this embodiment, the heat exchange chamber 202 structure is introduced into the first heat exchange assembly 2, and heat exchange fins are arranged on the wall surface of the heat exchange chamber 202 in contact with the slurry, thereby further improving the heat exchange efficiency and the fluidity of the slurry. Specifically:

[0112] The heat exchange chamber 202, as an independent heat exchange space, accommodates the first heat exchange coil 201, so that the heat of the heat exchange medium is transferred to the slurry through the heat exchange chamber 202. Through the design of the independent area of ​​the heat exchange chamber 202, the heat exchange process can be carried out more concentratedly and efficiently, avoiding the ineffective loss of heat and improving the overall heat exchange efficiency of the system. Heat exchange fins are arranged on the wall of the heat exchange chamber 202, which greatly improves the heat exchange effect by increasing the surface area of ​​the wall. The fins form an angle of 30° to 45° with the wall of the heat exchange chamber 202. This angle design has an optimized heat conduction effect: within the angle range of 30° to 45°, the heat exchange fins can effectively guide the slurry to flow through the fins, promote the slurry to fully contact with the fins, and increase the heat transfer area. At the same time, this angle enables the fins to maintain good fluid contact during the heat conduction process and avoid excessive fluid disturbance that may be caused by too large an angle. The design of the fins allows the heat of the heat exchange chamber 202 to be transferred to the slurry more evenly, thereby forming a stable temperature distribution near the heat exchange chamber 202 and promoting the settling and flow of the slurry.

[0113] Due to the angle design of the fins in the heat exchange chamber 202, the temperature difference generated during the slurry flow drives the convection flow near the heat exchange chamber 202, forming a local thermal cycle. This convection effect helps the aggregation and sedimentation of particles in the slurry, accelerating the separation efficiency of the slurry. In addition, the higher temperature gradient can also cause small particles to collide and aggregate with each other, thereby forming large particles and quickly settling, improving the clarity of the clear liquid.

[0114] By concentrating the heat exchange area and optimizing the fin angle and the number of fins, this embodiment improves the heat exchange efficiency while reducing the laying area of ​​the heat exchange coil, thereby reducing the energy consumption of the overall system. In addition, the fin design avoids direct contact between the heat exchange coil and the slurry, reduces the accumulation of attachments on the pipe surface, extends the system cleaning cycle, and reduces maintenance costs.

[0115] like Figures 4 to 5 As shown, the fifth embodiment of the present invention proposes a thickener heat exchange system, and based on the previous embodiment, the second heat exchange component 3 includes:

[0116] The heat exchange cylinder 301 is arranged at the center of the bottom surface of the thickener 1;

[0117] The second heat exchange coil 302 is arranged inside the heat exchange tube 301;

[0118] Wherein, in the first direction, the diameter of the heat exchange tube 301 decreases successively.

[0119] In this embodiment, a heat exchange tube 301 structure is introduced into the second heat exchange assembly 3, and a second heat exchange coil 302 is arranged in the heat exchange tube 301 to further improve the heat exchange effect of the bottom area. The heat exchange tube 301 is arranged at the center of the bottom surface of the thickener 1, and its diameter gradually decreases in the first direction (i.e., from the bottom to the top). The design of the heat exchange tube 301 gradually decreasing in diameter in the first direction helps to guide the slurry to form natural convection driven by temperature difference along the tube wall. As the diameter of the heat exchange tube 301 decreases, the flow rate of the slurry around the heat exchange tube 301 gradually increases, so that the heat exchange efficiency is improved.

[0120] The heat exchange tube 301 is located at the center of the bottom, so that the heat convection generated by the slurry after heating can quickly spread to the surrounding area, forming a natural upward flow. At the same time, the rising slurry forms a convection cycle with the surrounding cooled slurry, which helps small particles in the clear liquid to sink and gather, thereby improving the clarity of the clear liquid. The second heat exchange coil 302 is arranged inside the heat exchange tube 301, so that the coil does not directly contact the slurry, effectively avoiding the risk of wear and blockage caused by the attachment of solid particles in the slurry. This protective arrangement extends the service life of the coil, reduces the need for frequent cleaning, and reduces the maintenance cost of the equipment.

[0121] like Figure 7 As shown, the sixth embodiment of the present invention provides a thickener heat exchange system, and based on the previous embodiment, further includes:

[0122] A flow-blocking component 4 is disposed between the first heat exchange component 2 and the second heat exchange component 3;

[0123] Wherein, the flow blocking component 4 at least forms an annular sedimentation channel 401;

[0124] Furthermore, the height of the settling channel 401 is smaller than the height of the first heat exchange coil 201 .

[0125] In this embodiment, by adding a flow-blocking component 4 between the first heat exchange component 2 and the second heat exchange component 3, the effects of slurry sedimentation and convection flow are further optimized.

[0126] The flow-blocking component 4 establishes an annular settling channel 401 between the first heat exchange component 2 and the second heat exchange component 3, which is specifically used to guide the settling of solid particles. Since the height of the settling channel 401 is lower than the height of the first heat exchange coil 201, the solid particles can naturally settle into the channel, avoiding direct contact between the particles and the heat exchange coil, and reducing the accumulation of particles around the heat exchange components. This design helps to enhance the settling efficiency of particles without interfering with heat exchange.

[0127] The flow-blocking component 4 not only guides the path of the settling particles, but also effectively optimizes the convection path of the slurry. By introducing the flow-blocking structure between the first and second heat exchange components 3, the slurry is moderately hindered when flowing in the annular settling channel 401, forming a stable local convection. This convection enhances the overall fluidity of the slurry, making the small particles in the slurry more evenly distributed and gradually settled, and improving the clarity of the clear liquid layer.

[0128] The presence of the flow-blocking component 4 causes small particles to aggregate, collide and gradually form larger particles in the annular sedimentation channel 401. This agglomeration effect significantly improves the sedimentation performance of the particles, enables small particles to gradually aggregate into large particles, and further improves the quality of the clear liquid. As the convection cycle continues, the small particles in the clear liquid layer are fully separated to obtain a higher degree of clarity, meeting the strict industrial requirements for the quality of the clear liquid. The establishment of the flow-blocking component 4 effectively protects the first and second heat exchange components 3, so that the settled solid particles do not directly accumulate on the heat exchange components, avoiding wear and blockage caused by particle contact. This not only improves the heat exchange efficiency, but also extends the service life of the heat exchange components and reduces the frequency and cost of system maintenance.

[0129] By setting the height of the settling channel 401 lower than the height of the first heat exchange coil 201, it is ensured that the settling channel 401 is dedicated to particle settling, while the heat exchange area is used for fluid convection and heat exchange. Such a partition design reduces unnecessary energy consumption, concentrates heat transfer in the most needed area, and conforms to the design concept of energy saving and high efficiency.

[0130] The seventh embodiment of the present invention provides a thickener heat exchange system, and based on the previous embodiment, the baffle assembly 4 includes:

[0131] A first spoiler 402 and a second spoiler 403;

[0132] The first baffle plate 402 is disposed near the first heat exchange component 2;

[0133] The second baffle plate 403 is disposed close to the second heat exchange component 3;

[0134] Furthermore, the sedimentation channel 401 is formed between the first spoiler 402 and the second spoiler 403 .

[0135] In this embodiment, by further introducing the structure of the first baffle 402 and the second baffle 403 into the baffle assembly 4, the sedimentation efficiency of the slurry and the clarity of the clear liquid are significantly improved. Specifically, the layout of the first baffle 402 and the second baffle 403 enables the sedimentation channel 401 to form a clear sedimentation area in the thickener 1, ensuring that the solid particles naturally settle along the specified path. This structural design limits the sedimentation particles in the slurry to the channel, effectively avoiding the attachment and accumulation of particles on the first and second heat exchange components 3, thereby ensuring smooth flow around the heat exchange components and further improving the heat exchange efficiency of the system. The baffle is set to reasonably guide the convection path of the slurry while optimizing the sedimentation path. The sedimentation channel 401 between the first baffle 402 and the second baffle 403 forms a low-speed area during the slurry convection process, so that small particles can have enough time to settle in this area. This design makes the convection flow in the slurry more uniform, while avoiding the particle resuspension phenomenon caused by excessive flow rate, and improving the overall separation effect of the slurry. The setting of the sedimentation channel 401 provides a relatively stable sedimentation environment for small particles, so that small particles in the clear liquid layer can contact and collide with each other in the channel and gradually agglomerate to form larger particles. This agglomeration effect significantly improves the sedimentation performance of the particles, helps to quickly separate small particles from the clear liquid, thereby obtaining a clear liquid with higher clarity, and providing a purer liquid medium for downstream processes.

[0136] The first and second baffles 403 structures concentrate the settled particles in the channel, preventing solid particles from directly accumulating on the heat exchange components, and reducing the risk of wear and blockage of the heat exchange coils due to particle attachment. By extending the service life of the heat exchange components and reducing the need for cleaning and maintenance, the operating cost of the equipment is significantly reduced.

[0137] In this embodiment, the width of the sedimentation channel 401 between the first baffle 402 and the second baffle 403 can be flexibly adjusted according to specific working conditions to adapt to the changing requirements of different slurry concentrations and particle sizes. Width adjustment can optimize the sedimentation effect, making the system more adaptable to a wider range of applications and meeting the separation requirements under various industrial conditions.

[0138] In summary, this embodiment forms a clear sedimentation channel 401 by adding a first baffle plate 402 and a second baffle plate 403 in the baffle assembly 4, thereby successfully achieving precise control of the slurry sedimentation path, optimization of convection flow, and improvement of clear liquid quality.

[0139] The eighth embodiment of the present invention provides a thickener heat exchange system, and based on the previous embodiment, the maximum width of the settling channel 401 is W1, and the minimum width is W2, wherein:

[0140] W2=K2*W1, the value range of K2 is 0.5 to 0.8.

[0141] In this embodiment, by further optimizing the width of the sedimentation channel 401, the proportional relationship between the maximum width W1 and the minimum width W2 of the sedimentation channel 401 is clarified, and the width of the sedimentation channel 401 gradually transitions from the maximum value W1 to the minimum value W2, forming a conical or gradual channel structure. This width change guides the particle sedimentation path, so that the particles gradually approach the bottom when flowing in the channel, and finally settle to the bottom of the thickener 1. This gradual design reduces the resuspension of small particles during the sedimentation process and improves the sedimentation efficiency of the particles. And the design of the sedimentation channel 401 with gradually narrowed width slows down the slurry flow rate at the width change, thereby providing a more stable environment for the sedimentation of small particles. The gradual width of the channel controls the flow rate of the slurry, avoids the phenomenon of resuspension of small particles caused by too fast flow rate, makes the sedimentation process more stable, and effectively improves the clarity of the clear liquid. The gradual design of the channel width brings about a local fluid compression effect, which makes the small particles in the clear liquid more likely to gather together when flowing through the narrowing part of the channel. The gradient width not only makes the particles settle smoothly, but also promotes small particles to form larger aggregates in the channel by controlling the flow rate difference, thereby accelerating the clarification process of the clear liquid layer and providing high-quality separation effect.

[0142] By setting the K2 value within a reasonable range (0.5 to 0.8), the channel width ratio can be flexibly adjusted according to the particle size and concentration requirements of the solid particles in the slurry. This width adjustability ensures that the system can adapt to different slurry characteristics and enhances the adaptability of the thickener 1 under different working conditions.

[0143] like Figure 6 As shown, the ninth embodiment of the present invention provides a thickener heat exchange system, and based on the previous embodiment, includes:

[0144] Circulation component 5;

[0145] Wherein, the circulation component 5 at least forms a first port 501 and a second port 502;

[0146] Wherein, the second port 502 is arranged above the first heat exchange component 2;

[0147] Furthermore, the first port 501 is in communication with the second port 502;

[0148] The first port 501 is configured to guide part of the slurry in the liquid surface area to the second port 502;

[0149] The second port 502 is configured to direct the slurry to the convection region.

[0150] In this embodiment, the flow path and heat exchange effect of the slurry in the thickener 1 are further optimized by introducing the circulation component 5. The circulation component 5 includes a first port 501 and a second port 502. The first port 501 is located in the liquid surface area, and the second port 502 is located above the first heat exchange component 2, and the two are connected. The design of the circulation component 5 achieves the following innovative effects:

[0151] The slurry in the liquid surface area is guided to the second port 502 through the first port 501, so that the slurry flows into the convection area, forming an internal circulation flow. The circulating flow continuously guides new slurry into the convection area during the heat exchange process, so that the entire slurry system maintains a uniform temperature distribution near the heat exchange component, significantly improving the heat exchange efficiency. Compared with the static sedimentation mode, this design uses the circulating flow to drive the heat transfer of the slurry, so that the slurry is heated evenly, and the overall heat exchange effect is improved. The introduction of the circulation component 5 breaks the temperature and concentration stratification of the liquid surface area in the thickener 1, so that the slurry close to the liquid surface can flow into the convection area and fully mix with the slurry below. By homogenizing the temperature and concentration distribution, the problem of uneven settling speed of solid particles in the slurry is effectively prevented, thereby enhancing the overall settling effect of the slurry in the thickener 1.

[0152] The circulating flow drives the small particles back to the convection area. These small particles frequently contact and collide with other particles during the circulation process, gradually forming larger aggregates, effectively improving the clarity of the clear liquid. The design of the circulation component 5 allows the small particles to be fully agglomerated in the slurry system, ensuring a lower particle content in the clear liquid, thereby providing a higher quality clear liquid.

[0153] The tenth embodiment of the present invention provides a thickener heat exchange system, and based on the previous embodiment, there are multiple second ports 502, and the multiple second ports 502 have a height difference;

[0154] The plurality of second ports 502 with height differences are configured to adaptively guide the slurry following the change in the liquid level.

[0155] In this embodiment, by introducing a plurality of second ports 502 with height differences in the circulation component 5, the adaptability of the thickener 1 system to changes in the liquid level is further improved. Specifically, these second ports 502 are distributed at different heights and can adaptively guide the slurry according to the dynamic changes in the liquid level. Since the liquid level may fluctuate due to changes in the amount of slurry in and out during the operation of the thickener 1, providing a plurality of second ports 502 with height differences can enable the system to automatically adapt to such changes. When the liquid level rises or falls, the second ports 502 at different heights will be enabled accordingly, thereby ensuring that the slurry in the liquid surface area can always be effectively guided to the convection area. This design improves the flexibility of the thickener 1 system under different working conditions, allowing the system to maintain efficient operation when processing slurries of different magnitudes.

[0156] The setting of the height difference port enables the circulation component 5 to automatically select the appropriate port according to the change of the liquid level, and guide the slurry in the liquid area to the convection area, avoiding convection interruption or unevenness caused by liquid level fluctuations. By maintaining continuous and stable convection flow, this design further optimizes the circulation efficiency of the slurry, so that the temperature and concentration of the slurry are always uniform, which helps to improve the heat exchange effect and sedimentation performance.

[0157] As the liquid level changes, the appropriate second port 502 is automatically selected to return the small particle slurry to the convection area, so that the particles continue to agglomerate and settle during the slurry circulation. This can effectively reduce the suspension of small particles in the clear liquid layer, thereby improving the clarity of the clear liquid and ensuring a more stable separation effect. The improvement of the clear liquid quality has a significant positive impact on the downstream process and improves the overall performance of the system.

[0158] By automatically adapting to the change in liquid level and continuously guiding the slurry to flow into the convection area, the heat loss of the high-temperature slurry in the liquid surface area is avoided. As the liquid level fluctuates, the second port 502 at different heights guides the hot slurry back to the convection area, so that the heat is fully utilized inside the thickener 1, thereby reducing unnecessary heat loss and further improving the energy efficiency of the system.

[0159] In the description of the embodiments of the present invention, it needs to be understood that terms such as “up”, “down”, “front”, “back”, “left”, “right”, “vertical”, “horizontal”, “center”, “top”, “bottom”, “top”, “bottom”, “inside”, “outside”, “inside”, and “outside” indicate orientation or positional relationships.

[0160] In the description of the embodiments of the present invention, it should be understood that "-" and "~" represent a range between two values, and the range includes the endpoints. For example: "AB" represents a range greater than or equal to A, and less than or equal to B. "A~B" represents a range greater than or equal to A, and less than or equal to B.

[0161] In the description of the embodiments of the present invention, the term "and / or" herein is merely a description of the association relationship of associated objects, indicating that three relationships may exist. For example, A and / or B may represent: A exists alone, A and B exist at the same time, and B exists alone. In addition, the character " / " herein generally indicates that the associated objects before and after are in an "or" relationship.

[0162] Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that various changes, modifications, substitutions and variations may be made to the embodiments without departing from the principles and spirit of the present invention, and that the scope of the present invention is defined by the appended claims and their equivalents.

Claims

1. A thickener heat exchange system, characterized in that: include: a first heat exchange component and a second heat exchange component; The first heat exchange component and the second heat exchange component are both disposed in the thickener; Wherein, the first heat exchange component and the second heat exchange component contain heat exchange medium; Furthermore, the heat exchange medium is a reaction medium from the fission chamber, and after completing heat exchange in the thickener, the heat exchange medium flows back to the fission chamber; Wherein, the first heat exchange component is arranged on the inner wall surface of the thickener; Wherein, the second heat exchange component is arranged on the inner bottom surface of the thickener; Furthermore, the first heat exchange component and the second heat exchange component form an annular convection area; The ore slurry in the convection zone forms a convection flow.

2. The thickener heat exchange system according to claim 1, characterized in that: The first heat exchange component comprises: a first heat exchange coil disposed along the inner wall surface of the thickener; Wherein, in the first direction, the cross-sectional diameter D of the first heat exchange coil decreases successively; The first direction is the direction from the bottom surface of the thickener to the opening of the thickener; Furthermore, the heat exchange medium enters through the first heat exchange tube with the largest cross-sectional diameter D, and flows out through the first heat exchange tube with the smallest cross-sectional diameter D.

3. The thickener heat exchange system according to claim 2, characterized in that: The height of the first heat exchange assembly from the bottom surface of the thickener is H1, the overall height of the thickener is H2, and the following conditions are satisfied: H1=K1*H2, the value range of K1 is 0.4 to 0.

7.

4. The thickener heat exchange system according to claim 3, characterized in that: The first heat exchange component comprises: Heat exchange chamber; Wherein, the first heat exchange coil is arranged in the heat exchange chamber; Wherein, the wall surface of the heat exchange chamber in contact with the slurry is provided with heat exchange fins; Furthermore, the heat exchange fins and the wall surface of the heat exchange chamber form an angle a; The angle a ranges from 30° to 45°.

5. The thickener heat exchange system according to claim 2, characterized in that: The second heat exchange component comprises: A heat exchange cylinder is arranged at the center of the bottom surface of the thickener; A second heat exchange coil is arranged inside the heat exchange tube; Wherein, in the first direction, the diameters of the heat exchange tubes decrease successively.

6. The thickener heat exchange system according to claim 5, characterized in that: Also includes: A flow-blocking component, disposed between the first heat exchange component and the second heat exchange component; Wherein, the flow-blocking component at least forms an annular sedimentation channel; Furthermore, the height of the sedimentation channel is smaller than the height of the first heat exchange coil.

7. The thickener heat exchange system according to claim 6, characterized in that: The flow blocking component comprises: a first spoiler and a second spoiler; The first baffle is disposed at a position close to the first heat exchange component; The second baffle is disposed near the second heat exchange component; Furthermore, the sedimentation channel is formed between the first spoiler and the second spoiler.

8. The thickener heat exchange system according to claim 7, characterized in that: The maximum width of the sedimentation channel is W1, and the minimum width is W2, wherein: W2=K2*W1, the value range of K2 is 0.5 to 0.

8.

9. The thickener heat exchange system according to claim 1, characterized in that: include: Loop component; wherein the circulation component forms at least a first port and a second port; Wherein, the second port is arranged above the first heat exchange component; Furthermore, the first port is communicated with the second port; The first port is configured to guide a portion of the slurry in the liquid surface area to the second port; The second port is configured to direct the slurry to the convection region.

10. The thickener heat exchange system according to claim 9, characterized in that: There are a plurality of second ports, and the plurality of second ports have a height difference; The plurality of second ports with height differences are configured to adaptively guide the slurry following the change in the liquid level.

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