Evaporative crystallization system for extracting cesium chloride from lepidolite

Abstract

The utility model relates to the technical field of crystal preparation, and the utility model provides a kind of evaporative crystallization system of extracted cesium chloride in lepidolite, it is packed condensate preheater, condensate preheater leads to non-condensable gas preheater, non-condensable gas preheater leads to crystallization separator, crystallization separator has steam outlet, steam outlet leads to gas washing tower, gas washing tower leads to forced circulation evaporator, forced circulation evaporator has material outlet, non-condensable gas outlet, condensate outlet and steam inlet, material outlet leads to crystallization separator, non-condensable gas outlet leads to non-condensable gas preheater, condensate outlet leads to condensate preheater, gas washing tower leads to steam inlet.By repeated use of steam energy, the recovery of cesium in lepidolite is realized, so that resource recovery is more sufficient, and the technical problem of insufficient resource recovery in the process of extracting cesium from lepidolite in the prior art is solved.

Description

Technical Field

[0001] This utility model relates to the field of crystallization preparation technology, specifically to an evaporation crystallization system for cesium chloride extracted from lepidolite. Background Technology

[0002] The core technology of MVR (Mechanical Vapor Recompression) is "Mechanical Vapor Recompression Circulation Evaporation Technology," which is currently the most reliable and effective technical solution for treating high-salinity wastewater in the world. When using mechanical vapor recompression evaporation technology to treat wastewater, the heat energy required for evaporating the wastewater is mainly provided by the heat energy released or exchanged during steam condensation and the cooling of the condensate. During operation, there is no loss of latent heat; the only energy consumed is the electrical energy used to drive the pumps, steam compressor, condensate pumps, and control system within the evaporator.

[0003] Cesium is a typical rare element with properties very similar to potassium, and it often occurs in association with lithium and potassium minerals. Lepidolite is the main carrier mineral of cesium, with a CS₂O content as high as 1.2%, making it a scarce strategic mineral resource of critical cesium content. However, current development of lepidolite mines focuses only on lithium extraction, failing to effectively recover cesium resources, resulting in a serious waste of this key mineral resource. Utility Model Content

[0004] To overcome the above-mentioned defects, embodiments of this utility model provide an evaporation and crystallization system for extracting cesium chloride from lepidolite, which solves the technical problem of insufficient resource recovery in the prior art.

[0005] According to one aspect, at least one embodiment of the present invention provides an evaporation and crystallization system for extracting cesium chloride from lepidolite, comprising: Condensate preheater; Non-condensable gas preheater, wherein the condensate preheater is connected to the non-condensable gas preheater; A crystallization separator, wherein the non-condensable gas preheater leads to the crystallization separator, and the crystallization separator has a steam outlet; A gas scrubbing tower, wherein the steam outlet leads to the gas scrubbing tower; A forced circulation evaporator is provided, with a scrubbing tower connected to it. The forced circulation evaporator has a material outlet, a non-condensable gas outlet, a condensate outlet, and a steam inlet. The material outlet is connected to the crystallizer, the non-condensable gas outlet is connected to the non-condensable gas preheater, the condensate outlet is connected to the condensate preheater, and the scrubbing tower is connected to the steam inlet.

[0006] As a further technical solution, it also includes: Thickener, the crystallizer leads to the thickener; Centrifuge, the thickener leading to the centrifuge; The mother liquor tank is connected to the centrifuge, and the mother liquor tank is connected to the crystallizer.

[0007] As a further technical solution, it also includes: A feed pump, which leads to the condensate preheater, is used to supply material to the condensate preheater; A discharge pump is provided, and the crystallizer is connected to the thickener via the discharge pump. A forced circulation pump is provided, and the crystallizer is connected to the forced circulation evaporator via the forced circulation pump.

[0008] As a further technical solution, the cesium chloride evaporation and crystallization system extracted from lepidolite also includes: An air intake pipe, which leads to the steam inlet, is used to supply steam to the forced circulation evaporator; A vacuum pump, the non-condensable gas preheater being connected to the vacuum pump; An exhaust pipe, to which the vacuum pump is connected, is used to discharge non-condensable gases; A drain pipe is provided, and the condensate preheater is connected to the drain pipe, which is used to discharge condensate.

[0009] As a further technical solution, it also includes: The compressor is connected to the forced circulation evaporator via the gas scrubbing tower.

[0010] As a further technical solution, it also includes: The forced circulation evaporator is connected to the condensate preheater via the condensate tank. A water supply pipe leads to the condensate tank.

[0011] As a further technical solution, a wire mesh filter is installed at the steam outlet of the gas scrubbing tower.

[0012] As a further technical solution, both the condensate preheater and the non-condensable gas preheater are plate heat exchangers.

[0013] As a further technical solution, the level gauge on the crystallizer is a dual-flange differential pressure transmitter, and the flange on the dual-flange differential pressure transmitter is a wall-mounted flange.

[0014] As a further technical solution, the discharge pump is a low-speed, open-impeller pump.

[0015] The beneficial effects of this utility model are as follows: In this invention, a cascade preheating system is constructed by connecting a condensate preheater and a non-condensable gas preheater in series, tapping into the system's waste heat potential. The material first passes through the condensate preheater, utilizing the waste heat from the condensate in the forced circulation evaporator to raise its temperature by 35°C-40°C. Then, it passes through the non-condensable gas preheater, absorbing the waste heat from the non-condensable gas to further raise its temperature by 5°C. This two-step preheating can raise the initial temperature of the material by 40°C-45°C, reducing the heat load requirement of the forced circulation evaporator and minimizing energy consumption in the core heating stage. The closed-loop steam cycle formed by the crystallizer, the gas scrubbing tower, and the forced circulation evaporator achieves efficient internal energy circulation. The secondary steam generated by the crystallizer is purified by the gas scrubbing tower and then fed into the forced circulation evaporator. The non-condensable gas from the forced circulation evaporator flows back to the non-condensable gas preheater through the non-condensable gas outlet, and the condensate flows back to the condensate preheater through the condensate outlet. The system's thermal utilization rate is improved compared to traditional single-stage preheating systems. This closed-loop structure ensures continuous concentration of cesium chloride solution between the crystallizer and the forced circulation evaporator. It also achieves synergy of "low energy consumption and high concentration" through the cascade utilization of thermal energy, solving the problems of high energy consumption and insufficient resource recovery in the process of cesium extraction from lepidolite, and improving the primary recovery rate of cesium resources. Attached Figure Description

[0016] To more clearly illustrate the technical solutions in the embodiments of this utility model, the accompanying drawings used in the description of the embodiments of this utility model will be briefly introduced below. Obviously, the drawings described below are merely some exemplary embodiments of this utility model. For those skilled in the art, other drawings can be obtained based on the content of the exemplary embodiments of this utility model and these drawings without any creative effort.

[0017] Figure 1 This is a schematic diagram illustrating the circulation principle of one embodiment of the present invention; Figure 2 for Figure 1 A simplified schematic diagram of the connected structure in the embodiment.

[0018] In the diagram: condensate preheater-1, non-condensable gas preheater-2, crystallizer-3, steam outlet-301, gas scrubbing tower-4, forced circulation evaporator-5, material outlet-501, non-condensable gas outlet-502, condensate outlet-503, steam inlet-504, thickener-6, centrifuge-7, mother liquor tank-8, feed pump-9, discharge pump-10, forced circulation pump-11, air inlet pipe-12, vacuum pump-13, exhaust pipe-14, liquid drain pipe-15, compressor-16, condensate tank-17, water replenishment pipe-18. Detailed Implementation

[0019] The present invention will now be described in further detail with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the present invention and not intended to limit its scope.

[0020] To keep the drawings concise, only the parts relevant to the utility model are shown schematically in each drawing; these do not represent the actual structure of the product. Furthermore, for ease of understanding, in some drawings, only one of the components with the same structure or function is schematically shown, or only one is labeled. In this document, "a" not only means "only one," but can also mean "more than one," and "several" includes "two" and "more than two."

[0021] In this document, it should be noted that, unless otherwise explicitly specified and limited, the terms "installation," "connection," and "linking" should be interpreted broadly. For example, they can refer to fixed connections, detachable connections, or integral connections; they can refer to mechanical connections or electrical connections; they can refer to direct connections or indirect connections through an intermediate medium; and they can refer to the internal connection between two components. Those skilled in the art can understand the specific meaning of the above terms in this utility model based on the specific circumstances.

[0022] In this invention, unless otherwise explicitly specified and limited, "above" or "below" the second feature can include direct contact between the first and second features, or contact between the first and second features through another feature between them. Furthermore, "above," "over," and "on top" of the second feature includes the first feature directly above or diagonally above the second feature, or simply indicates that the first feature is at a higher horizontal level than the second feature. "Below," "below," and "under" the second feature includes the first feature directly below or diagonally below the second feature, or simply indicates that the first feature is at a lower horizontal level than the second feature.

[0023] In the description of this embodiment, terms such as "upper," "lower," "left," and "right" are based on the orientation or positional relationship shown in the accompanying drawings. They are used only for the convenience of description and simplification of operation, and are not intended to indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this utility model.

[0024] Furthermore, in the description of this application, the terms "first," "second," etc., are used only to distinguish descriptions and should not be construed as indicating or implying relative importance.

[0025] like Figures 1-2The diagram illustrates an evaporation and crystallization system for extracting cesium chloride from lepidolite according to an embodiment of the present invention. The system includes a condensate preheater 1, which connects to a non-condensable gas preheater 2. The non-condensable gas preheater 2 connects to a crystallization separator 3. The crystallization separator 3 has a steam outlet 301, which connects to a gas scrubbing tower 4. The gas scrubbing tower 4 connects to a forced circulation evaporator 5. The forced circulation evaporator 5 has a material outlet 501, a non-condensable gas outlet 502, a condensate outlet 503, and a steam inlet 504. The material outlet 501 connects to the crystallization separator 3, the non-condensable gas outlet 502 connects to the non-condensable gas preheater 2, the condensate outlet 503 connects to the condensate preheater 1, and the gas scrubbing tower 4 connects to the steam inlet 504.

[0026] In some examples, the series connection of condensate preheater 1 and non-condensable gas preheater 2 constructs a tiered preheating system, tapping into the system's waste heat potential. The material first passes through condensate preheater 1, utilizing the waste heat from the condensate in the forced circulation evaporator 5 to raise its temperature by 35℃-40℃. Then, it passes through non-condensable gas preheater 2, absorbing the waste heat from the non-condensable gas to further raise its temperature by 5℃. This two-step preheating can increase the initial temperature of the material by 40℃-45℃, reducing the heat load requirement of the forced circulation evaporator 5 and decreasing energy consumption in the core heating stage. A closed-loop steam cycle is formed by steam outlet 301 leading to gas scrubbing tower 4, gas scrubbing tower 4 leading to steam inlet 504, and non-condensable gas outlet 502 leading to non-condensable gas preheater 2, achieving efficient internal energy circulation. The secondary steam generated by the crystallizer separator 3 is purified by the scrubbing tower 4 and then fed into the forced circulation evaporator 5. The non-condensable gas from the forced circulation evaporator 5 is returned to the non-condensable gas preheater 2 through the non-condensable gas outlet 502, and the condensate is returned to the condensate preheater 1 through the condensate outlet 503. The system's thermal utilization rate is improved compared to the traditional single-stage preheating system. This closed-loop structure ensures continuous concentration of the cesium chloride solution between the crystallizer separator 3 and the forced circulation evaporator 5. It also achieves a synergistic effect of "low energy consumption - high concentration" through the cascade utilization of thermal energy, solving the problems of high energy consumption and insufficient resource recovery in the process of cesium extraction from lepidolite, and improving the primary recovery rate of cesium resources.

[0027] Lithium sulfate solution is fed into condensate preheater 1 via feed pump 9 for preheating. The preheated material then undergoes heat exchange in non-condensable gas preheater 2. After being preheated to the required temperature by these two preheaters, the material is then fed into crystallizer 3. After being concentrated through circulation between crystallizer 3, forced circulation evaporator 5, and forced circulation pump 11, the material is fed into thickener 6 via discharge pump 10 for crystal precipitation and growth. Finally, it enters centrifuge 7 for solid-liquid separation. The steam generated by the crystallizer enters forced circulation evaporator 5 via scrubbing tower 4. The presence of scrubbing tower 4 reduces the entrainment of secondary steam mist, thus ensuring the system's service life and normal operation.

[0028] Furthermore, it also includes a thickener 6, a crystallizer 3 leading to the thickener 6, a centrifuge 7 leading to the centrifuge 7, a mother liquor tank 8 leading to the mother liquor tank 8, and a crystallizer 3 leading to the crystallizer 3.

[0029] In some examples, the solid-liquid separation and recovery system consisting of thickener 6, centrifuge 7, and mother liquor tank 8 achieves precise conversion of cesium chloride crystals from concentrate to pure product. Thickener 6 provides a stable crystal growth environment for the concentrated cesium chloride solution, promoting the aggregation of fine crystals and the full growth of large crystals by controlling temperature and residence time, laying the foundation for subsequent separation. Centrifuge 7 achieves efficient separation of crystals and mother liquor through high-speed centrifugation, solving the problems of incomplete separation and excessive mother liquor entrainment in crystals caused by traditional filtration methods. Mother liquor tank 8 temporarily stores the mother liquor after centrifugation and then sends it back to crystallizer 3 through a return pipeline to participate in the recycling and concentration, enabling the secondary recovery of cesium resources that were originally lost with the mother liquor. The overall system recovery rate is increased from 85% in single-stage separation to over 95%, reducing the waste of scarce cesium resources and improving economic efficiency.

[0030] Furthermore, it also includes a feed pump 9, which is connected to the condensate preheater 1 and is used to supply material to the condensate preheater 1. The crystallizer 3 is connected to the thickener 6 through the discharge pump 10, and the crystallizer 3 is connected to the forced circulation evaporator 5 through the forced circulation pump 11.

[0031] In some examples, the feed pump 9, discharge pump 10, and forced circulation pump 11 ensure the stability and efficiency of material flow. The feed pump 9 uses frequency conversion control, which can dynamically adjust the feed rate according to the load of the condensate preheater 1, ensuring that the material is heated evenly in the preheater and avoiding changes in solution composition caused by local overheating, thus improving preheating uniformity. The discharge pump 10 is connected to the crystallizer 3 and the thickener 6, and is adjusted in real time through a flow sensor to ensure a stable concentration of material entering the thickener 6, providing stable initial conditions for the crystal growth process and reducing crystal quality differences caused by concentration fluctuations. The forced circulation pump 11 is the key power source for circulation concentration. Its output pressure can ensure that the flow velocity of the material in the heat exchange tubes of the forced circulation evaporator 5 is maintained stably at 2.0-2.2 m / s. The high flow velocity not only enhances the degree of turbulence and improves the heat transfer coefficient (compared to conventional flow velocities), but also effectively flushes the heat exchange tube walls, reduces scale deposition, extends the continuous operation cycle of the evaporator, reduces the frequency of shutdown for cleaning, and improves production efficiency.

[0032] Furthermore, the cesium chloride evaporation and crystallization system extracted from lepidolite also includes an inlet pipe 12, which leads to a steam inlet 504 for introducing steam into the forced circulation evaporator 5; a non-condensable gas preheater 2 leads to a vacuum pump 13, which leads to an exhaust pipe 14 for discharging non-condensable gas; and a condensate preheater 1 leads to a drain pipe 15 for discharging condensate.

[0033] In some examples, the inlet pipe 12, vacuum pump 13, exhaust pipe 14, and drain pipe 15 form a system auxiliary control network. The inlet pipe 12 can supplement external steam to the steam inlet 504 of the forced circulation evaporator 5 during the initial system startup or when steam is insufficient, quickly raising the evaporator temperature to the operating range (60-80℃), shortening the system startup time, and reducing energy waste during the startup phase. The vacuum pump 13, in conjunction with the exhaust pipe 14, continuously removes accumulated non-condensable gases (such as air and trace amounts of inert gases) from the system, maintaining the system vacuum and preventing the formation of a gas film on the heat exchange surface that would reduce heat transfer efficiency, thus ensuring a stable evaporation rate. The drain pipe 15 promptly discharges the condensate that has completed heat exchange in the condensate preheater 1, preventing condensate accumulation in the preheater and affecting the heat exchange area, ensuring a stable material temperature at the preheater outlet, and providing a reliable initial temperature for subsequent concentration processes. The compressor 16 is a centrifugal steam compressor.

[0034] Furthermore, it also includes a compressor 16, and the gas scrubbing tower 4 is connected to the forced circulation evaporator 5 through the compressor 16.

[0035] In some examples, compressor 16, as a device in MVR technology, enables the energy upgrading and recycling of secondary steam. The secondary steam purified by scrubbing tower 4 (temperature approximately 70℃, pressure approximately 0.02MPa) is compressed by compressor 16, raising its temperature to 85-90℃ and pressure to 0.06-0.08MPa, significantly improving its heat quality. This allows it to be directly fed into forced circulation evaporator 5 as a heating source, replacing traditional external fresh steam. During this process, the latent heat of the steam is fully recovered, reducing the system's demand for external steam by more than 10%, consuming only the power required to drive the compressor. Simultaneously, steam recycling reduces condensate discharge and lowers wastewater treatment costs, achieving both energy-saving and environmental benefits.

[0036] Furthermore, it also includes a condensate tank 17, through which the forced circulation evaporator 5 is connected to the condensate preheater 1, and the water supply pipe 18 leads to the condensate tank 17.

[0037] In some examples, the condensate tank 17 and the water supply line 18 ensure the heat recovery efficiency of the preheating process. The condensate tank 17 temporarily stores the condensate produced by the forced circulation evaporator 5 and stabilizes the output flow rate through an internal liquid level control system. This prevents flow fluctuations caused by direct condensate delivery from affecting the heat exchange effect of the condensate preheater 1, ensuring that the material preheating temperature difference remains stable within the design range. The water supply line 18 is equipped with a float level switch. When the liquid level in the condensate tank 17 is lower than the set value, it automatically activates the water supply to replenish the condensate lost due to system leakage or evaporation. This ensures that the condensate preheater 1 always has a sufficient heat source medium, preventing a decrease in preheating efficiency due to insufficient condensate, ensuring the continuity and stability of the entire preheating process, and reducing production interruptions caused by water shortage.

[0038] Furthermore, a wire mesh filter is installed at the steam outlet 301 of the gas scrubbing tower 4.

[0039] In some examples, the wire mesh filter installed at the steam outlet 301 of the scrubbing tower 4 is a key design feature for protecting downstream equipment and improving system reliability. Made of stainless steel, the filter effectively intercepts mist entrained in the steam, preventing mist containing tiny cesium chloride crystals from entering the compressor 16. This design reduces the erosion and wear of the compressor impeller by crystal particles at the source, while also preventing dynamic imbalance caused by scale buildup on the impeller surface, thus reducing compressor downtime. Furthermore, the filtered clean steam entering the evaporator reduces the risk of scale buildup on the inner walls of the heat exchange tubes, extends the evaporator cleaning cycle, and lowers system maintenance costs.

[0040] Furthermore, both the condensate preheater 1 and the non-condensable gas preheater 2 are plate heat exchangers.

[0041] In some examples, condensate preheater 1 and non-condensable gas preheater 2 employ plate heat exchangers, which are well-suited to the characteristics of cesium chloride solution and improve heat exchange efficiency. The corrugated plate design of the plate heat exchanger increases the heat exchange area compared to a tube heat exchanger of the same volume, and the cold side (material) and hot side (condensate / non-condensable gas) media flow counter-currently, resulting in a large temperature difference and high heat exchange efficiency. Considering the absence of crystalline particles in the cesium chloride solution, a single-pass design ensures uniform material flow between the plates, avoiding temperature unevenness caused by localized stagnation and guaranteeing stable initial concentration in subsequent concentration processes. Furthermore, the plate heat exchanger has a compact structure, facilitating installation and maintenance; the plates can be individually disassembled for cleaning, reducing equipment maintenance time and improving equipment utilization.

[0042] Furthermore, the level gauge on the crystallizer 3 is a dual-flange differential pressure transmitter, and the flange on the dual-flange differential pressure transmitter is a wall-mounted flange.

[0043] In some examples, the crystallizer separator 3 uses a dual-flange differential pressure transmitter (wall-mounted flange) as a level gauge, effectively solving the problems of scaling and level detection in crystallization equipment. Traditional flange level gauges have gaps between the flange and the separator wall, which can easily become dead zones for crystal deposition, leading to level detection drift. The wall-mounted flange design ensures the flange face is completely flush with the inner wall of the separator, eliminating gap accumulation points and reducing the scaling rate. The dual-flange differential pressure transmitter calculates the level by measuring the pressure difference between the upper and lower ends of the separator, unaffected by fluctuations in solution density, and can accurately control the level height within the crystallizer separator 3. A stable level ensures a constant vapor space volume and stable secondary steam generation, avoiding increased mist entrainment due to excessively high levels or insufficient heat transfer area due to excessively low levels, thus ensuring stable cesium chloride crystal production.

[0044] Furthermore, the discharge pump 10 is an impeller pump with a low speed and an open impeller.

[0045] In some examples, the discharge pump 10 employs a low-speed (800-1000 r / min) open impeller design to meet the conveying requirements of cesium chloride crystals. Low-speed operation significantly reduces the shear force exerted by the impeller on the crystals, lowering the crystal breakage rate and ensuring uniform crystal particle size, meeting the particle size requirements of optical-grade cesium chloride. The open impeller features a large-channel design with a large gap between the blades and the pump casing, allowing larger particles to pass through and effectively preventing crystal accumulation and blockage at the impeller. Furthermore, the low-speed design reduces pump vibration and noise, extends the lifespan of bearings and other wear parts, reduces equipment maintenance costs and downtime, and improves the system's continuous operation capability.

[0046] It should be noted that the above embodiments are only used to illustrate the technical solution of this utility model and are not intended to limit it. Although this utility model has been described in detail with reference to preferred embodiments, those skilled in the art should understand that modifications or equivalent substitutions can be made to the technical solution of this utility model without departing from the spirit and scope of the technical solution of this utility model, and all such modifications or substitutions should be covered within the scope of the claims of this utility model.

Claims

1. A system for evaporating and crystallizing cesium chloride extracted from lepidolite, characterized in that, include: Condensate preheater (1); Non-condensable gas preheater (2), the condensate preheater (1) is connected to the non-condensable gas preheater (2); Crystallization separator (3), the non-condensable gas preheater (2) leads to the crystallization separator (3), the crystallization separator (3) has a steam outlet (301); The gas scrubbing tower (4) has a steam outlet (301) leading to it. A forced circulation evaporator (5) is provided, and a gas scrubbing tower (4) is connected to the forced circulation evaporator (5). The forced circulation evaporator (5) has a material outlet (501), a non-condensable gas outlet (502), a condensate outlet (503), and a steam inlet (504). The material outlet (501) is connected to the crystallizer (3), the non-condensable gas outlet (502) is connected to the non-condensable gas preheater (2), the condensate outlet (503) is connected to the condensate preheater (1), and the gas scrubbing tower (4) is connected to the steam inlet (504).

2. The evaporation and crystallization system for extracting cesium chloride from lepidolite according to claim 1, characterized in that, Also includes: Thickener (6), the crystallizer (3) leads to the thickener (6); Centrifuge (7), the thickener (6) leads to the centrifuge (7); Mother liquor tank (8), centrifuge (7) leads to mother liquor tank (8), mother liquor tank (8) leads to crystallizer (3).

3. The evaporation and crystallization system for extracting cesium chloride from lepidolite according to claim 2, characterized in that, Also includes: Feed pump (9), which is connected to the condensate preheater (1) and is used to feed the condensate preheater (1); The discharge pump (10) is connected to the thickener (6) through the crystallizer (3); Forced circulation pump (11), the crystallizer (3) is connected to the forced circulation evaporator (5) through the forced circulation pump (11).

4. The evaporation and crystallization system for extracting cesium chloride from lepidolite according to claim 1, characterized in that, The cesium chloride evaporation and crystallization system extracted from lepidolite also includes: An air intake pipe (12) leads to the steam inlet (504) for supplying steam to the forced circulation evaporator (5); Vacuum pump (13), the non-condensable gas preheater (2) is connected to the vacuum pump (13); An exhaust pipe (14) is provided, through which the vacuum pump (13) is connected, and the exhaust pipe (14) is used to discharge non-condensable gases. Drainage pipe (15), the condensate preheater (1) is connected to the drainage pipe (15), the drainage pipe (15) is used to discharge condensate.

5. The evaporation and crystallization system for extracting cesium chloride from lepidolite according to claim 1, characterized in that, Also includes: The compressor (16) is connected to the forced circulation evaporator (5) via the gas scrubbing tower (4).

6. The evaporation and crystallization system for extracting cesium chloride from lepidolite according to claim 1, characterized in that, Also includes: Condensate tank (17), the forced circulation evaporator (5) is connected to the condensate preheater (1) through the condensate tank (17); Water supply pipe (18) leads to the condensate tank (17).

7. The evaporation and crystallization system for extracting cesium chloride from lepidolite according to claim 1, characterized in that, A wire mesh filter is installed at the steam outlet (301) of the gas scrubbing tower (4).

8. The evaporation and crystallization system for extracting cesium chloride from lepidolite according to claim 1, characterized in that, The condensate preheater (1) and the non-condensable gas preheater (2) are both plate heat exchangers.

9. The evaporation and crystallization system for extracting cesium chloride from lepidolite according to claim 1, characterized in that, The level gauge on the crystallizer (3) is a dual-flange differential pressure transmitter, and the flange on the dual-flange differential pressure transmitter is a wall-mounted flange.

10. The evaporation and crystallization system for extracting cesium chloride from lepidolite according to claim 3, characterized in that, The discharge pump (10) is a low-speed, open-type impeller pump.

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