Device for extracting cesium from lepidolite and preparing cesium formate through cesium formate preparation system

Abstract

The invention provides a device for extracting cesium from lepidolite and preparing cesium formate by a preparation system of cesium formate, which comprises: an extraction section, which comprises a plurality of first high-speed centrifugal extractors connected in series, and a first extraction inlet of the first high-speed centrifugal extractor of the last stage is introduced with a liquid to be extracted; the to-be-extracted liquid is leached frozen clear liquid of lepidolite, and the frozen clear liquid is alkaline and comprises cesium, rubidium, sodium, potassium and lithium ions; the t-BAMBP is diluted by adopting ESCAID 110 as an extraction agent, the concentration of the extraction agent is 0.4-0.6 mol / L of t-BAMBP, and the O / A ratio in the extraction section is 1: (1.8-2.0); the washing section comprises a plurality of second high-speed centrifugal extractors which are connected in series; the back extraction section comprises a third high-speed centrifugal extractor, and cesium bicarbonate back extraction post-liquid flows out of a first back extraction outlet of the third high-speed centrifugal extractor; the oil removal section is used for removing oil from the cesium bicarbonate back-extraction post-liquid; and the evaporation and concentration section is used for introducing formic acid for neutralization reaction to form a cesium formate solution after oil removal, and then evaporating and concentrating the cesium formate solution to obtain the final cesium formate solution.

Description

Technical Field

[0001] The present application relates to the field of cesium formate preparation, and in particular to a cesium formate preparation system for extracting cesium from lepidolite and preparing cesium formate. Background Art

[0002] Oil drilling operations, especially those exploring high-pressure oil and gas reservoirs, often require high-density drilling fluids to balance formation pressure and ensure wellbore stability. High-density drilling fluids are typically obtained by adding weighting agents. Traditionally, weighting agents are inert, water-insoluble solid materials such as barite powder, iron ore powder, limestone powder, and galena powder. These weighting agents often increase the solids content of the drilling fluid, leading to increased viscosity, reduced drilling speed, and reservoir pore blockage, thus damaging the formation. To minimize the damage caused by insoluble solids to the reservoir, water-soluble weighting agents are used in many drilling operations and in most completion fluid applications. Common water-soluble weighting agents include alkali metal inorganic salts (sodium chloride, potassium chloride, sodium bromide, etc.), divalent metal inorganic salts (calcium chloride, calcium bromide, zinc bromide, etc.), and alkali metal formates (sodium formate, potassium formate, cesium formate, etc.).

[0003] Currently, the most widely used weighting agent is alkali metal formates, particularly mixed solutions of cesium formate and potassium formate. This mixed solution is currently used extensively in clay-free, high-density drilling fluids both domestically and internationally, with annual consumption reaching 8,000 tons of cesium formate and 4,000 tons of potassium formate, and this consumption is growing at a rate of over 30% annually. However, its use in my country is limited by its relatively high cost.

[0004] Lepidolite, also known as "lepidolite," is typically a flake or scaly aggregate. It belongs to the mica family of minerals and is the most common lithium mineral. A basic aluminosilicate of potassium and lithium, it is a crucial mineral for lithium extraction. Furthermore, lepidolite often contains rare metals such as rubidium and cesium, making it a crucial raw material for their extraction. Therefore, developing a simple and efficient process for producing cesium formate solution could promote its widespread application in oil drilling, improve lepidolite resource utilization, reduce costs, and increase efficiency, possessing significant economic and social significance. Summary of the Invention

[0005] The purpose of the present invention is to solve the above problems and provide a system for preparing cesium formate, which is a device for extracting cesium from lepidolite and preparing cesium formate.

[0006] The technical solution of this application is achieved as follows: The present invention provides a cesium formate preparation system for extracting cesium from lepidolite and preparing cesium formate, comprising: An extraction section includes a plurality of first high-speed centrifugal extractors connected in series, each of the first high-speed centrifugal extractors including a first extraction inlet and a second extraction inlet at one end, and a first extraction outlet and a second extraction outlet at the other end. The first extraction inlet is connected to the first extraction outlet, and the second extraction inlet is connected to the second extraction outlet. Between two adjacent first high-speed centrifugal extractors, the second extraction outlet of the first high-speed centrifugal extractor in the upper stage is connected to the second extraction inlet of the first high-speed centrifugal extractor in the lower stage via a pipeline, and the first extraction inlet of the first high-speed centrifugal extractor in the upper stage is connected to the first extraction outlet of the first high-speed centrifugal extractor in the lower stage via a pipeline. An extractant is introduced into the second extraction inlet of the first high-speed centrifugal extractor in the first stage via a pipeline, while an extractant is introduced into the first extraction inlet of the first high-speed centrifugal extractor in the last stage. The extractant is a frozen supernatant of lepidolite leaching, which is alkaline and contains cesium, rubidium, sodium, potassium, and lithium ions. The extractant is ESCAID 110 diluted with t-BAMBP, and the O / A ratio in the extraction section is 1:1.8-2.0. A washing section includes a plurality of second high-speed centrifugal extractors connected in series, each second high-speed centrifugal extractor including a first washing inlet and a second washing inlet at one end, and a first washing outlet and a second washing outlet at the other end, wherein the first washing inlet is connected to the first washing outlet, and the second washing inlet is connected to the second washing outlet; between two adjacent second high-speed centrifugal extractors, the second washing outlet of the second high-speed centrifugal extractor of the upper stage is connected to the second washing inlet of the second high-speed centrifugal extractor of the lower stage via a pipeline, and the first washing inlet of the second high-speed centrifugal extractor of the upper stage is connected to the first washing outlet of the second high-speed centrifugal extractor of the lower stage via a pipeline; the second washing inlet of the second high-speed centrifugal extractor of the first stage is connected to the second extraction outlet of the first high-speed centrifugal extractor of the last stage via a pipeline, and the first washing sulfuric acid is introduced into the first washing inlet of the second high-speed centrifugal extractor of the last stage, and the first washed liquid flows out of the first washing outlet of the second high-speed centrifugal extractor of the first stage; a stripping section comprising a third high-speed centrifugal extractor, wherein the third high-speed centrifugal extractor comprises a first stripping inlet and a second stripping inlet provided at one end, and a first stripping outlet and a second stripping outlet provided at the other end, wherein the first stripping inlet is connected to the first stripping outlet, and the second stripping inlet is connected to the second stripping outlet; the second stripping inlet of the third high-speed centrifugal extractor is connected to the second washing outlet of the second high-speed centrifugal extractor of the last stage via a pipeline, and a mixed solution of carbon dioxide and water is introduced into the first stripping inlet of the third high-speed centrifugal extractor, and a cesium bicarbonate stripping liquid flows out of the first stripping outlet of the third high-speed centrifugal extractor; An oil removal section, used for removing oil from the cesium bicarbonate stripping liquid; The evaporation and concentration section is used to introduce formic acid into the oil after degreasing to carry out a neutralization reaction to form a cesium formate solution, and then evaporate and concentrate the cesium formate solution to obtain the final cesium formate solution.

[0007] The advantages or beneficial effects of the above technical solution include at least: The cesium formate preparation system provided by the present invention extracts cesium from lepidolite and prepares cesium formate. By diluting t-BAMBP with ESCAID 110 and combining it with a high-speed centrifugal extractor, the system significantly reduces the number of extraction, washing, and stripping stages, thereby lowering costs and reaction time. Furthermore, by reducing the number of extraction stages, the present invention significantly reduces equipment investment and operating costs, while also reducing chemical consumption and waste liquid generation, thereby lowering overall production costs. Furthermore, by precisely controlling the extractant concentration, O / A ratio, and process parameters of each stage, the present invention effectively improves the cesium extraction rate and purity, reduces impurity co-extraction, and ensures the high purity of the final product. Furthermore, the use of ESCAID 110 as a diluent is less toxic, safer, and more environmentally friendly than traditional solvents such as sulfonated kerosene. Furthermore, by optimizing the process flow, waste liquid generation is reduced, minimizing environmental pollution. Finally, the present invention creatively adopts carbon dioxide for stripping, then performs formic acid acidification, performs evaporation concentration, and adjusts the pH to an appropriate range. This not only saves the amount of formic acid, but also avoids the introduction of other impurity ions, and can obtain a cesium formate solution with higher purity. BRIEF DESCRIPTION OF THE DRAWINGS

[0008] The accompanying drawings illustrate exemplary implementations of the present application of embodiments of the present invention and, together with the description, are used to explain the principles of the present application. These drawings are included to provide a further understanding of the present application, and the drawings are included in and constitute a part of this specification.

[0009] Figure 1 A schematic diagram of a device for extracting cesium from lepidolite and preparing cesium formate in a system for preparing cesium formate provided by an embodiment of the present invention is shown. DETAILED DESCRIPTION

[0010] The following describes embodiments of the present application in more detail with reference to the accompanying drawings. Although certain embodiments of the present application are shown in the accompanying drawings, it should be understood that the present application can be implemented in various forms and should not be construed as limited to the embodiments described herein. Instead, these embodiments are provided to provide a more thorough and complete understanding of the present application. It should be understood that the drawings and embodiments of the present application are for illustrative purposes only and are not intended to limit the scope of protection of the present application.

[0011] It should be noted that, in the absence of conflict, the embodiments and features of the embodiments in this application can be combined with each other. The present application will be described in detail below with reference to the accompanying drawings and in combination with the embodiments.

[0012] The names of the messages or information exchanged between multiple devices in the embodiments of the present application are only used for illustrative purposes and are not used to limit the scope of these messages or information.

[0013] Reference Figure 1 The embodiment of the present invention provides a system for preparing cesium formate, which is a device for extracting cesium from lepidolite and preparing cesium formate, comprising: The extraction section 10 includes a plurality of first high-speed centrifugal extractors 11 connected in series, wherein each first high-speed centrifugal extractor 11 includes a first extraction inlet 110 and a second extraction inlet 112 at one end, and a first extraction outlet 111 and a second extraction outlet 113 at the other end, and the first extraction inlet 110 is connected to the first extraction outlet 111, and the second extraction inlet 112 is connected to the second extraction outlet 113; between two adjacent first high-speed centrifugal extractors 11, the second extraction outlet 113 of the first high-speed centrifugal extractor 11 of the upper stage is connected to the second extraction outlet 113 of the first high-speed centrifugal extractor 11 of the lower stage. The second extraction inlet 112 of the first high-speed centrifugal extractor 11 is connected via a pipeline, and the first extraction inlet 110 of the first high-speed centrifugal extractor 11 of the previous stage is connected to the first extraction outlet 111 of the first high-speed centrifugal extractor 11 of the next stage via a pipeline; and the extractant is introduced into the second extraction inlet 112 of the first high-speed centrifugal extractor 11 of the first stage via a pipeline, while the liquid to be extracted 12 is introduced into the first extraction inlet 110 of the first high-speed centrifugal extractor 11 of the last stage, and the aqueous raffinate 13 flows out of the first extraction outlet 111 of the first stage.

[0014] The washing section 20 includes a plurality of second high-speed centrifugal extractors 21 connected in series, wherein each second high-speed centrifugal extractor 21 includes a first washing inlet 210 and a second washing inlet 212 at one end, and a first washing outlet 211 and a second washing outlet 213 at the other end, and the first washing inlet 210 is connected to the first washing outlet 211, and the second washing inlet 212 is connected to the second washing outlet 213; between two adjacent second high-speed centrifugal extractors 21, the second washing outlet 213 of the second high-speed centrifugal extractor 21 of the upper stage is connected to the second washing outlet 213 of the second high-speed centrifugal extractor 21 of the lower stage. The washing inlet 212 is connected through a pipeline, and the first washing inlet 210 of the second high-speed centrifugal extractor 21 of the previous stage is connected to the first washing outlet 211 of the second high-speed centrifugal extractor 21 of the next stage is connected through a pipeline; and the second washing inlet 212 of the second high-speed centrifugal extractor 21 of the first stage is connected to the second extraction outlet 113 of the first high-speed centrifugal extractor 11 of the last stage through a pipeline, and the first washing sulfuric acid 22 is introduced into the first washing inlet 210 of the second high-speed centrifugal extractor 21 of the last stage, and the first washed liquid 23 flows out of the first washing outlet 211 of the second high-speed centrifugal extractor 21 of the first stage.

[0015] The stripping section 30 includes a third high-speed centrifugal extractor 31. The third high-speed centrifugal extractor 31 includes a first stripping inlet 310 and a second stripping inlet 312 at one end, and a first stripping outlet 311 and a second stripping outlet 313 at the other end. The first stripping inlet 310 is connected to the first stripping outlet 311, and the second stripping inlet 312 is connected to the second stripping outlet 313. The second stripping inlet 312 of the third high-speed centrifugal extractor 31 is connected to the second washing outlet 213 of the second high-speed centrifugal extractor 21 of the last stage via a pipeline. A mixed solution 32 of carbon dioxide and water is introduced into the first stripping inlet 310 of the third high-speed centrifugal extractor 31, and a cesium bicarbonate stripping solution 33 is discharged from the first stripping outlet 311 of the third high-speed centrifugal extractor 31. The second stripping outlet 313 of the third high-speed centrifugal extractor 31 is connected to the second extraction inlet 112 of the first high-speed centrifugal extractor 11 of the first stage, thereby forming a circulation of the extract.

[0016] The oil removal section 40 is used to remove oil from the cesium bicarbonate stripping liquid 33 .

[0017] The evaporation and concentration section 50 is used to introduce formic acid into the evaporation chamber after oil removal for neutralization reaction to form a cesium formate solution, and then evaporate and concentrate the cesium formate solution to obtain a final cesium formate solution.

[0018] In one embodiment, the liquid to be extracted 12 is a frozen clear liquid extracted from lepidolite, and the main element contents thereof are shown in Table 1: Table 1 Elemental composition of frozen supernatant (g / L)

[0019] In one embodiment, the extractant used is ESCAID 110 to dilute t-BAMBP, with a concentration of 0.4 to 0.6 mol / L. The present invention's innovative use of ESCAID 110 to dilute t-BAMBP significantly reduces the number of extraction, washing, and stripping stages, thereby improving extraction efficiency.

[0020] Under alkaline conditions, the H on the phenolic hydroxyl group of t-BAMBP in the extractant is easily replaced by metal ions to form phenolates. The extraction order of this system is cesium > rubidium > potassium > sodium. - In this case, the saturated loading of cesium can reach 5.5 g / L, and the saturated loading of rubidium can reach 3.3 g / L. Therefore, in this embodiment, preferably, the extraction solution 12 includes 0.4 mol / L of OH - .

[0021] Preferably, the extraction section 10 includes 3 to 5 first high-speed centrifugal extractors 11 connected in series. In one embodiment, the extraction section 10 includes 4 first high-speed centrifugal extractors 11 connected in series. Therefore, the extractant is introduced into the second extraction inlet 112 of the first high-speed centrifugal extractor 11 of the first stage through a pipeline, while the liquid to be extracted 12 is introduced into the first extraction inlet 110 of the first high-speed centrifugal extractor 11 of the fourth stage. An aqueous raffinate 13 flows out of the first extraction outlet 111 of the first stage, and the cesium-loaded organic phase flows out of the second extraction outlet 113 of the first high-speed centrifugal extractor 11 of the fourth stage and enters the washing section 20.

[0022] More preferably, to achieve the best extraction effect, the ratio of the extractant to the liquid to be extracted 12 needs to be strictly controlled. The effects of O / A ratios of 1:1, 1:1.2, 1:1.5, 1:1.8, and 1:2 in the extraction section 10 on the Cs extraction effect are shown in Table 2.

[0023] Table 2 Effect of different O / A on Cs extraction

[0024] The data shows that during the cesium extraction stage, the extraction rates of Cs and Rb decrease as the aqueous phase flow rate increases. When the aqueous phase flow rate ratio is above 1.8, the co-extraction rate of Rb can be controlled within 5%, which is beneficial for the washing stage to completely elute Rb. Comparing the data of O / A of 1:1 and 1:1.5, it is recommended to select an extraction O / A of 1:1.8 to 2.0 to reduce the amount of organic extractant. At the same time, the Cs extraction rate can be improved by increasing the number of extraction stages. That is, preferably, the O / A ratio in the extraction section 10 is 1:1.8 to 2.0. In one embodiment, the O / A ratio in the extraction section 10 is about 1:1.8, that is, the volume ratio of the extractant to the liquid to be extracted 12 is about 1:1.8.

[0025] In one embodiment, after testing and analysis, the element content of the aqueous raffinate 13 is shown in Table 3: Table 3 Elemental composition of cesium extraction residue (g / L)

[0026] It can be seen from Table 3 that the cesium ions in the aqueous raffinate 13 are significantly reduced, while other metals have no significant changes.

[0027] Preferably, the washing section 20 includes 4 to 7 second high-speed centrifugal extractors 21 connected in series. In one embodiment, the washing section 20 includes 5 second high-speed centrifugal extractors 21 connected in series. Therefore, the second washing inlet 212 of the first-stage second high-speed centrifugal extractor 21 is connected to the second extraction outlet 113 of the fourth-stage first high-speed centrifugal extractor 11 via a pipeline, while the first washing sulfuric acid 22 is introduced into the first washing inlet 210 of the fifth-stage second high-speed centrifugal extractor 21, and the first post-wash liquid 23 flows out of the first washing outlet 211 of the first-stage second high-speed centrifugal extractor 21.

[0028] In order to obtain the best extraction effect, preferably, in the washing section 20, the ratio of the first washing sulfuric acid 22 to the cesium-loaded organic phase needs to be strictly controlled. Preferably, the O / A ratio in the washing section 20 is 2 to 3: 1. In one embodiment, the O / A ratio in the washing section 20 is about 2.5: 1, that is, the volume ratio of the cesium-loaded organic phase to the first washing sulfuric acid 22 is about 2.5: 1, so that the impurity ions can be fully washed away. Further, the first washing sulfuric acid 22 also needs to be strictly controlled. Preferably, the concentration of the first washing sulfuric acid 22 is 0.02 mol / L to 0.03 mol / L. In one embodiment, the concentration of the first washing sulfuric acid 22 is about 0.025 mol / L.

[0029] In order to obtain the best stripping effect, preferably, in the stripping section 30, the ratio of the mixed solution 32 of carbon dioxide and water to the cesium-loaded organic phase after washing needs to be strictly controlled. Preferably, the O / A ratio in the stripping section 30 is 5.5~6.5:1. In one embodiment, the O / A ratio in the stripping section 30 is about 6:1, that is, the volume ratio of the cesium-loaded organic phase after washing to the mixed solution 32 of carbon dioxide and water is about 6:1, so that sufficient stripping can be achieved. Further, the mixed solution 32 of carbon dioxide and water also needs to be strictly controlled. Preferably, the concentration of the mixed solution 32 of carbon dioxide and water is 0.15~0.2mol / L. In one embodiment, the Cs concentration in the loaded organic phase after washing is approximately 3 g / L, or 0.0223 mol / L, based on experimental data. With an oil-to-water ratio of 5.5 to 6.5:1 in the stripping stage, the Cs concentration in the stripping solution is enriched to 0.123 to 0.145 mol / L. Carbon dioxide, water, and cesium ions react in an equimolar manner, so the theoretical required carbon dioxide concentration should be 0.123 to 0.145 mol / L. Considering system fluctuations and excess carbon dioxide, the concentration is preferably 0.15 to 0.2 mol / L. In one embodiment, the concentration of the carbon dioxide and water mixed solution 32 is 0.16 mol / L. In one embodiment, the pH of the cesium bicarbonate stripping solution 33 is 7.5, and the solution is essentially in the form of bicarbonate (when the pH is < 8, there is essentially no carbonate).

[0030] The deoiling section 40 is used to deoil the cesium bicarbonate stripping liquid 33. Specifically, there are many ways to remove oil, which can be carried out using an adsorption column or an adsorption tank. Specifically, the adsorption column is a vertical cylindrical container with an adsorbent inside. The material enters from the top of the adsorption column and flows downward through the adsorbent layer. The oil is adsorbed by the adsorbent, and the purified material flows out from the bottom of the adsorption column. The evaporation method can also be used. The material is heated in a distillation kettle. After the oil evaporates, it enters the condenser, is cooled into a liquid in the condenser, and finally flows into a receiver for collection. The centrifugal method can also be used to separate the oil from the liquid or solid material using centrifugal force. When the material is in a high-speed rotating centrifuge, due to the different densities of the oil and the material, the oil will be thrown to the outer wall of the centrifuge, thereby separating from the material. There is no limitation here, and those skilled in the art can make a choice according to actual needs.

[0031] After oil removal, the evaporation and concentration section 50 is used to introduce formic acid for a neutralization reaction to form a cesium formate solution, which is then evaporated and concentrated to obtain the final cesium formate solution. The evaporation and concentration section 50 can be performed in an evaporation tank or other container, without limitation. In one embodiment, the final cesium formate solution has test data as shown in Table 4.

[0032] Table 4 Cesium formate solution test data

[0033] The data show that the above synthesis route can be used to synthesize a cesium formate solution product that meets the requirements. The stripping liquid obtained by extraction-washing-CO2 stripping of the frozen clear liquid, i.e., the raw material of the cesium bicarbonate solution, is neutralized with formic acid aqueous solution, and then evaporated and concentrated, and the pH is adjusted to finally obtain an 80% mass fraction of cesium formate aqueous solution. The density of this solution is 2.5g / cm 3 The pH value is 10, and the obtained solution sample is a colorless, transparent liquid with no visible precipitate. Its impurity ion requirements meet the requirements of Y / ST 1144-2016.

[0034] The present invention creatively adopts carbon dioxide for stripping, then performs formic acid acidification, performs evaporation concentration, and adjusts the pH to an appropriate range, thereby saving formic acid usage and avoiding the introduction of other impurity ions, thereby obtaining a cesium formate solution with higher purity.

[0035] Those skilled in the art will appreciate that the above embodiments are merely for the purpose of illustrating the present application and are not intended to limit the scope of the present application. Those skilled in the art may make other changes or modifications based on the above disclosure, and such changes or modifications are still within the scope of the present application.

Claims

1. A system for preparing cesium formate, which is a device for extracting cesium from lepidolite and preparing cesium formate, characterized in that: include: An extraction section includes a plurality of first high-speed centrifugal extractors connected in series, each of the first high-speed centrifugal extractors including a first extraction inlet and a second extraction inlet at one end, and a first extraction outlet and a second extraction outlet at the other end; the first extraction inlet is connected to the first extraction outlet, and the second extraction inlet is connected to the second extraction outlet; between two adjacent first high-speed centrifugal extractors, the second extraction outlet of the first high-speed centrifugal extractor in the upper stage is connected to the second extraction inlet of the first high-speed centrifugal extractor in the lower stage via a pipeline, and the first extraction inlet of the first high-speed centrifugal extractor in the upper stage is connected to the first extraction outlet of the first high-speed centrifugal extractor in the lower stage via a pipeline; the second extraction inlet of the first high-speed centrifugal extractor in the first stage is supplied with an extractant via a pipeline, while the first extraction inlet of the first high-speed centrifugal extractor in the last stage is supplied with a liquid to be extracted; The extraction liquid is a frozen supernatant of lepidolite leaching, the frozen supernatant is alkaline and contains cesium, rubidium, sodium, potassium and lithium ions; the extraction agent is ESCAID 110 to dilute t-BAMBP, the concentration of the extraction agent is 0.4-0.6 mol / L t-BAMBP, and the O / A ratio in the extraction section is 1:1.8-2.0; A washing section includes a plurality of second high-speed centrifugal extractors connected in series, each second high-speed centrifugal extractor including a first washing inlet and a second washing inlet at one end, and a first washing outlet and a second washing outlet at the other end, wherein the first washing inlet is connected to the first washing outlet, and the second washing inlet is connected to the second washing outlet; between two adjacent second high-speed centrifugal extractors, the second washing outlet of the second high-speed centrifugal extractor of the upper stage is connected to the second washing inlet of the second high-speed centrifugal extractor of the lower stage via a pipeline, and the first washing inlet of the second high-speed centrifugal extractor of the upper stage is connected to the first washing outlet of the second high-speed centrifugal extractor of the lower stage via a pipeline; the second washing inlet of the second high-speed centrifugal extractor of the first stage is connected to the second extraction outlet of the first high-speed centrifugal extractor of the last stage via a pipeline, and the first washing sulfuric acid is introduced into the first washing inlet of the second high-speed centrifugal extractor of the last stage, and the first washed liquid flows out of the first washing outlet of the second high-speed centrifugal extractor of the first stage; a stripping section comprising a third high-speed centrifugal extractor, wherein the third high-speed centrifugal extractor comprises a first stripping inlet and a second stripping inlet provided at one end, and a first stripping outlet and a second stripping outlet provided at the other end, wherein the first stripping inlet is connected to the first stripping outlet, and the second stripping inlet is connected to the second stripping outlet; the second stripping inlet of the third high-speed centrifugal extractor is connected to the second washing outlet of the second high-speed centrifugal extractor of the last stage via a pipeline, and a mixed solution of carbon dioxide and water is introduced into the first stripping inlet of the third high-speed centrifugal extractor, and a cesium bicarbonate stripping liquid flows out of the first stripping outlet of the third high-speed centrifugal extractor; An oil removal section, used for removing oil from the cesium bicarbonate stripping liquid; The evaporation and concentration section is used to introduce formic acid into the oil after degreasing to carry out a neutralization reaction to form a cesium formate solution, and then evaporate and concentrate the cesium formate solution to obtain the final cesium formate solution.

2. The cesium formate preparation system according to claim 1 is a device for extracting cesium from lepidolite and preparing cesium formate, characterized in that: The extraction solution includes 0.4 mol / L OH - .

3. The cesium formate preparation system according to claim 2, wherein the device for extracting cesium from lepidolite and preparing cesium formate is characterized in that: The extraction section includes 3 to 5 first high-speed centrifugal extractors connected in series; the washing section includes 4 to 6 second high-speed centrifugal extractors connected in series; and the stripping section includes 2 to 4 third high-speed centrifugal extractors connected in series.

4. The cesium formate preparation system according to claim 3, wherein the device for extracting cesium from lepidolite and preparing cesium formate is characterized in that: The extraction section includes four first high-speed centrifugal extractors connected in series; the washing section includes five second high-speed centrifugal extractors connected in series; and the stripping section includes three third high-speed centrifugal extractors connected in series.

5. The cesium formate preparation system according to claim 1, wherein the device for extracting cesium from lepidolite and preparing cesium formate is characterized in that: The concentration of the first washing sulfuric acid is 0.02 mol / L to 0.03 mol / L.

6. The cesium formate preparation system according to claim 1, wherein the device for extracting cesium from lepidolite and preparing cesium formate is characterized in that: The O / A ratio in the washing section is 2-3:

1.

7. The cesium formate preparation system according to claim 1, wherein the device for extracting cesium from lepidolite and preparing cesium formate is characterized in that: The concentration of carbon dioxide in a mixed solution of carbon dioxide and water is 0.15~0.2mol / L.

8. The cesium formate preparation system according to claim 1, wherein the device for extracting cesium from lepidolite and preparing cesium formate is characterized in that: The O / A ratio in the stripping section is 5.5-6.5:

1.

9. The cesium formate preparation system according to claim 1, wherein the device for extracting cesium from lepidolite and preparing cesium formate is characterized in that: The reaction temperature in the stripping section is 38-42°C.

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