System for producing uranium tetrafluoride based on a reductive hydrofluorination reaction

Abstract

A uranium tetrafluoride preparation system based on a reducing hydrofluorination reaction includes a gas supply mechanism, a three-stage fluidized bed mechanism, and a tail gas treatment mechanism. The gas supply mechanism includes an ammonium fluoride heating tank and a gas separation tank. The gas separation tank has a mixed gas inlet, an ammonia outlet A, and a hydrogen fluoride outlet at its top. The mixed gas inlet of the gas separation tank is connected to the mixed gas outlet of the ammonium fluoride heating tank. The three-stage fluidized bed mechanism includes a fluidized bed A, an intermediate container X, a fluidized bed B, an intermediate container Y, and a fluidized bed C. The tail gas treatment mechanism includes a condenser, a crystallization tank, a plate filter, a microwave dryer, and a scrubbing tower. This invention uses a three-stage fluidized bed system to reduce and hydrofluorinate uranium oxide to prepare uranium tetrafluoride. Compared with the existing "uranium purification-uranium conversion" process, it enables continuous production control and significantly shortens the process flow.

Description

Technical Field

[0001] This invention relates to the field of natural uranium production technology, and in particular to a uranium tetrafluoride preparation system based on a reducing hydrofluorination reaction. Background Technology

[0002] In the production of natural uranium, uranium purification and uranium conversion are key steps. Uranium purification involves dissolving uranium oxides in nitric acid, followed by extraction and back-extraction, calcination for denitrification, and then oxidation-reduction to UO2. Uranium conversion involves passing UO2 through a two-stage countercurrent fluidized bed under conditions of excess hydrogen fluoride to produce the intermediate product UF4.

[0003] The above-mentioned "uranium purification-uranium conversion" process route has the following drawbacks in practical applications:

[0004] 1. The technical route is complex and the process flow is long;

[0005] 2. The extraction and back-extraction steps generate a large amount of wastewater;

[0006] 3. A large amount of hazardous chemical raw materials are required, and the transportation and storage of hazardous chemicals are fraught with risks.

[0007] In conclusion, developing new "uranium purification-uranium conversion" processes in the production of natural uranium is of great significance in order to shorten the process flow, reduce the generation of waste, and lower the demand for hazardous chemicals. Summary of the Invention

[0008] The purpose of this invention is to overcome the shortcomings of the prior art and provide a uranium tetrafluoride preparation system based on the reducing hydrofluorination reaction. It solves the problems of complex technical routes, large wastewater generation, and large amounts of hazardous chemical raw materials required in the existing "uranium purification-uranium conversion" process in the production of natural uranium.

[0009] The technical solution of the present invention is: a uranium tetrafluoride preparation system based on the reducing hydrofluorination reaction, comprising a gas supply mechanism, a three-stage fluidization mechanism and a tail gas treatment mechanism;

[0010] The gas supply mechanism includes an ammonium fluoride heating tank and a gas separator. The ammonium fluoride heating tank has an internal cavity for storing ammonium fluoride, a mixed gas outlet at its upper end, and a heating device A for heating its internal cavity. The gas separator has an internal cavity for holding potassium difluoride, a mixed gas inlet, an ammonia outlet A, and a hydrogen fluoride outlet at its top. The mixed gas inlet extends into the internal cavity of the gas separator to a greater depth than the ammonia outlet A and the hydrogen fluoride outlet extend into the internal cavity of the gas separator. A heating device B for heating its internal cavity is located on the outside of the gas separator. The mixed gas inlet of the gas separator is connected to the mixed gas outlet of the ammonium fluoride heating tank.

[0011] The three-stage fluidized bed system includes fluidized bed A, intermediate container X, fluidized bed B, intermediate container Y, and fluidized bed C. Fluidized bed A has an external air inlet A, an external exhaust outlet A, an external feed inlet A, and an external discharge outlet A. The air inlet A is connected to the ammonia outlet A of the gas separator. Intermediate container X has an external feed inlet X, an external discharge outlet X, and an external exhaust outlet X. The feed inlet X is connected to the discharge outlet A of fluidized bed A. Fluidized bed B has an external air inlet B, an external exhaust outlet B, and an external feed inlet B. Discharge port B and feed port B are connected to discharge port X of intermediate container X; the intermediate container Y is provided with feed port Y, discharge port Y and exhaust port Y on the outside, and feed port Y is connected to discharge port B of fluidized bed B; the fluidized bed C is provided with air inlet C, exhaust port C, feed port C and discharge port C on the outside, feed port C is connected to discharge port Y of intermediate container Y, exhaust port C is connected to air inlet B of fluidized bed B, and air inlet C is connected to hydrogen fluoride outlet of gas separator;

[0012] The exhaust gas treatment system includes a condenser, a crystallization tank, a plate filter, a microwave dryer, and a scrubbing tower. The condenser has a gas inlet A and a condensate outlet on its exterior. Gas inlet A is connected to the exhaust port A of fluidized bed A, the exhaust port X of intermediate container X, the exhaust port B of fluidized bed B, and the exhaust port Y of intermediate container Y, respectively. The crystallization tank has an internal cavity for holding the condensate, and a third stirring device is installed within the cavity. The crystallization tank has a condensate inlet, a slurry outlet, an ammonia water replenishment port, and an ammonia outlet B on its exterior. The condensate inlet is connected to the condensate outlet of the condenser. The plate filter has a slurry inlet, a filtrate outlet, and a solids outlet on its exterior. The slurry inlet is connected to the slurry outlet of the crystallization tank, and the filtrate outlet is connected to the ammonia water replenishment port of the crystallization tank. The microwave dryer is used to dry the solids discharged from the solids outlet of the plate filter. The scrubbing tower has a gas inlet B and a scrubbing liquid outlet on its exterior. Gas inlet B is connected to the ammonia outlet B of the crystallization tank.

[0013] A further technical solution of the present invention is: a sampling port is provided on the side wall of the gas separator, and a valve A is provided on the sampling port.

[0014] A further technical solution of the present invention is: a valve B is provided on the mixed gas outlet of the ammonium fluoride heating tank, a valve C is provided on the ammonia outlet A of the gas separator, and a valve D is provided on the hydrogen fluoride outlet of the gas separator.

[0015] Compared with the prior art, the present invention has the following advantages:

[0016] 1. It adopts a three-stage fluidized bed structure to reduce and hydrofluorinate uranium oxides to prepare uranium tetrafluoride. Compared with the existing "uranium purification-uranium conversion" process, it can realize continuous production control and significantly shorten the process flow.

[0017] 2. The ammonia and hydrogen fluoride required for the reduction and hydrofluorination reactions, respectively, are obtained by the thermal decomposition of solid ammonium fluoride, avoiding the direct storage of hazardous chemicals (ammonia and hydrogen fluoride), meeting the actual needs of the process, and achieving an inherent safety improvement.

[0018] 3. The process flow does not generate any difficult-to-treat or toxic intermediate products, making it environmentally friendly. The exhaust gas from the three-stage fluidized bed is recovered to obtain ammonium fluoride and ammonia. Ammonium fluoride can be used for reduction and hydrofluorination reactions, while ammonia can be used to supplement the exhaust gas recovery step, achieving internal recycling within the process.

[0019] The present invention will be further described below with reference to the figures and embodiments. Attached Figure Description

[0020] Figure 1 This is a schematic diagram of the structure of the present invention;

[0021] Figure 2 This is a schematic diagram of the gas supply mechanism;

[0022] Figure 3 This is a process flow diagram of the present invention.

[0023] Legend: Ammonium fluoride heating tank 11; Mixed gas outlet 111; Gas separator 12; Mixed gas inlet 121; Ammonia outlet A122; Hydrogen fluoride outlet 123; Fluidized bed A21; Inlet A211; Exhaust port A212; Feed inlet A213; Discharge port A214; Intermediate container X22; Feed inlet X221; Discharge port X222; Exhaust port X223; Fluidized bed B23; Inlet B231; Exhaust port B232; Feed inlet B233; Discharge port B234; Fluidized bed C25; Air inlet C251; Exhaust outlet C252; Feed inlet C253; Discharge outlet C254; Condenser 31; Gas inlet A311; Condensate outlet 312; Crystallization tank 32; Condensate inlet 321; Slurry outlet 322; Ammonia water replenishment inlet 323; Ammonia outlet B324; Plate filter 33; Slurry inlet 331; Filtrate outlet 332; Solid outlet 333; Microwave dryer 34; Scrubber 35; Gas inlet B351. Detailed Implementation

[0024] Example 1:

[0025] like Figure 1-2 As shown, the uranium tetrafluoride preparation system based on the reducing hydrofluorination reaction includes a gas supply mechanism, a three-stage fluidization mechanism, and a tail gas treatment mechanism.

[0026] The gas supply mechanism includes an ammonium fluoride heating tank 11 and a gas separator 12. The ammonium fluoride heating tank 11 has an internal cavity for storing ammonium fluoride, and a mixed gas outlet 111 at its upper end. A heating device A (not shown in the figure) for heating its internal cavity is located outside the ammonium fluoride heating tank 11. The gas separator 12 has an internal cavity for holding potassium difluoride. A mixed gas inlet 121, an ammonia outlet A122, and a hydrogen fluoride outlet 123 are located at the top of the gas separator 12. The mixed gas inlet 121 extends into the internal cavity of the gas separator 12 to a greater depth than the ammonia outlet A122 and the hydrogen fluoride outlet 123 extend into the internal cavity of the gas separator 12. A heating device B (not shown in the figure) for heating its internal cavity is located outside the gas separator 12. The mixed gas inlet 121 of the gas separator 12 is connected to the mixed gas outlet 111 of the ammonium fluoride heating tank 11.

[0027] The three-stage fluidization system includes fluidized bed A21, intermediate container X22, fluidized bed B23, intermediate container Y24, and fluidized bed C25. Fluidized bed A21 has an external inlet A211, an external outlet A212, a feed inlet A213, and a discharge outlet A214. Feed inlet A213 is used to input uranium oxides, and inlet A211 is connected to the ammonia outlet A122 of gas separator 12. Intermediate container X22 has an external inlet X221, a discharge outlet X222, and an external outlet X223. Feed inlet X221 is connected to discharge outlet A213 of fluidized bed A21. Fluidized bed B23 has an external inlet B231, an external outlet B232, a feed inlet B233, and a discharge outlet B234. Feed inlet B233 is connected to discharge outlet X222 of intermediate container X22. The intermediate container Y24 is externally equipped with a feed inlet Y241, a discharge outlet Y242, and an exhaust outlet Y243. The feed inlet Y241 is connected to the discharge outlet B234 of the fluidized bed B23. The fluidized bed C25 is externally equipped with an air inlet C251, an exhaust outlet C252, a feed inlet C253, and a discharge outlet C254. The feed inlet C253 is connected to the discharge outlet Y242 of the intermediate container Y24, the exhaust outlet C252 is connected to the air inlet B231 of the fluidized bed B23, the discharge outlet C254 is used to discharge uranium tetrafluoride, and the air inlet C251 is connected to the hydrogen fluoride outlet 123 of the gas separator 12.

[0028] The exhaust gas treatment system includes a condenser 31, a crystallization tank 32, a plate filter 33, a microwave dryer 34, and a scrubbing tower 35. The condenser 31 has a gas inlet A311 and a condensate outlet 312 on its exterior. The gas inlet A311 is connected to the exhaust port A212 of the fluidized bed A21, the exhaust port X223 of the intermediate container X22, the exhaust port B232 of the fluidized bed B23, and the exhaust port Y243 of the intermediate container Y24. The crystallization tank 32 has an internal cavity for holding the condensate. A third stirring device (not shown in the figure) is installed in the internal cavity of the crystallization tank 32. The crystallization tank 32 has a condensate inlet 321, a slurry outlet 322, an ammonia water replenishment port 323, and an ammonia outlet B324 on its exterior. The condensate inlet 321 is connected to the condensate outlet 312 of the condenser 31. The plate filter 33 is externally equipped with a slurry inlet 331, a filtrate outlet 332, and a solids outlet 333. The slurry inlet 331 is connected to the slurry discharge port 322 of the crystallization tank 32, and the filtrate outlet 332 is connected to the ammonia water replenishment port 323 of the crystallization tank 32. A microwave dryer 34 is used to dry the solids discharged from the solids outlet 333 of the plate filter 33. The scrubbing tower 35 is externally equipped with a gas inlet B351 and a scrubbing liquid outlet. The gas inlet B351 is connected to the ammonia outlet B324 of the crystallization tank 32.

[0029] Preferably, a sampling port 124 is provided on the side wall of the gas separator 12, and a valve A is provided on the sampling port 124.

[0030] Preferably, valve B is provided on the mixed gas outlet 111 of the ammonium fluoride heating tank 11, valve C is provided on the ammonia outlet A122 of the gas separator 12, and valve D is provided on the hydrogen fluoride outlet 123 of the gas separator 12.

[0031] Briefly describe the working principle of this invention:

[0032] A method for preparing uranium tetrafluoride based on a reducing hydrofluorination reaction is provided, applied to the aforementioned uranium tetrafluoride preparation system based on a reducing hydrofluorination reaction. The following preparatory work is performed before preparing uranium tetrafluoride:

[0033] 1. Solid ammonium fluoride is placed inside the ammonium fluoride heating tank 11;

[0034] 2. Fill the inner cavity of the gas separator 2 with solid potassium difluorocyanide, ensuring that the lower port of the mixed gas inlet 21 is inserted into the potassium difluorocyanide, and the upper ports of the ammonia outlet 22 and the hydrogen fluoride outlet 23 are both located above the potassium difluorocyanide.

[0035] The steps are as follows:

[0036] S01, thermal decomposition of ammonium fluoride:

[0037] Open valve B on ammonium fluoride heating tank 11; start heating device A to control the temperature in the inner cavity of ammonium fluoride heating tank 11 at 160-180℃, so that the solid ammonium fluoride in the inner cavity of ammonium fluoride heating tank 11 thermally decomposes to produce ammonia and hydrogen fluoride. The mixed gas of ammonia and hydrogen fluoride is discharged through the mixed gas outlet 111 of ammonium fluoride heating tank 11.

[0038] In this step, the following reaction occurs: NH4F → NH3 + HF.

[0039] SO2, alternately separating ammonia and hydrogen fluoride in the mixed gas:

[0040] A. Start the heating device B to control the temperature in the inner cavity of the gas separator 12 at 90-110℃. Open valve B on the ammonium fluoride heating tank 11, open valve C on the gas separator 12, and close valve D on the gas separator 12. The mixed gas generated in the ammonium fluoride heating tank 11 is then introduced into the inner cavity of the gas separator 2 through the mixed gas inlet 21. Hydrogen fluoride in the mixed gas reacts with potassium difluoride to form potassium fluoride complex salt. The potassium fluoride complex salt is molten at 90-110℃ (the melting point of the potassium fluoride complex salt is lower than that of potassium difluoride). Ammonia in the mixed gas is insoluble in the molten potassium fluoride complex salt and is discharged from the ammonia outlet 22. During this process, the potassium fluoride complex salt is periodically sampled through the sampling port 124 to detect the hydrogen fluoride content. When the mass percentage of hydrogen fluoride in the potassium fluoride complex salt reaches 50%-55%, it indicates that the absorption of hydrogen fluoride by potassium difluoride is close to saturation, and the process proceeds to step B.

[0041] B. Using heating device B, control the temperature in the inner cavity of gas separator 12 at 110-200℃. Close valve B on ammonium fluoride heating tank 11, close valve C on gas separator 12, and open valve D on gas separator 12. Stop the flow of the mixed gas generated in ammonium fluoride heating tank 11 into the inner cavity of gas separator 12. Hydrogen fluoride in potassium fluoride composite salt overflows at 110-200℃, turning back into free hydrogen fluoride gas, and is discharged from hydrogen fluoride outlet 123. During this process, periodically sample potassium fluoride composite salt through sampling port 124 to detect the hydrogen fluoride content in potassium fluoride composite salt. When the mass percentage of hydrogen fluoride in potassium fluoride composite salt drops to 30%-35%, it indicates that the hydrogen fluoride in potassium fluoride composite salt has been almost completely released. Repeat step A.

[0042] In this step, ammonia and hydrogen fluoride in the mixed gas are separated alternately by performing sub-steps A and B alternately.

[0043] In this step, the following reaction occurs in sub-step A: F2HK + nHF → KF·(n+1)HF.

[0044] In this step, the following reaction occurs in substep B: KF·(n+1)HF→F2HK+nHF.

[0045] In this step, the ammonia gas separated in step A contains a small amount of hydrogen fluoride, and the purity of the ammonia gas is greater than 80%. The hydrogen fluoride gas separated in step B contains a small amount of ammonia, and the purity of the hydrogen fluoride gas is greater than 95%.

[0046] SO3, the reducing hydrofluorination reaction of uranium oxide:

[0047] A. On the one hand, uranium oxide is fed into the fluidized bed A21 through the feed inlet A213. On the other hand, ammonia gas separated from the gas separator 12 is fed into the fluidized bed A21 through the gas inlet A211. The temperature of the fluidized bed A21 is controlled between 500-650℃ to reduce the uranium oxide. The final solid produced includes a mixture of uranium dioxide (large amount) and uranium tetrafluoride (small amount). The final residual tail gas includes water vapor, nitrogen and excess ammonia.

[0048] B. The mixture produced by fluidized bed A21 is discharged through discharge port A214 and then sent to intermediate container X22 for temporary storage through feed port X221. Intermediate container X22 serves to adjust the reaction process, reduce the difficulty of control, and prevent cross-contamination between fluidized bed A21 and fluidized bed B23.

[0049] C. On the one hand, the material temporarily stored in the intermediate container X22 is discharged through the discharge port X222 and then enters the inner cavity of the fluidized bed B23 through the feed port B233. On the other hand, the tail gas discharged from the fluidized bed C25 is input into the inner cavity of the fluidized bed B23 through the air inlet B231. The temperature of the fluidized bed B23 is controlled at 260-320℃ to perform preliminary hydrofluorination of uranium dioxide. The final solid produced includes uranium tetrafluoride, and the final remaining tail gas includes water vapor, nitrogen and excess hydrogen fluoride.

[0050] D. The material produced by fluidized bed B23 is discharged through discharge port B234 and then sent to intermediate container Y24 for temporary storage through feed port Y241. Intermediate container Y24 serves to adjust the reaction process, reduce control difficulty, and prevent cross-contamination between fluidized bed B23 and fluidized bed C25.

[0051] E. On the one hand, the mixture temporarily stored in the intermediate container Y24 is discharged through the discharge port Y242 and then enters the inner cavity of the fluidized bed C25 through the feed port C253. On the other hand, the hydrogen fluoride separated by the gas separator 12 is sent into the inner cavity of the fluidized bed C25 through the air inlet C251. The temperature of the fluidized bed C25 is controlled at 380-420℃ to perform deep hydrofluorination of uranium dioxide. The final solid produced includes uranium tetrafluoride. The final residual tail gas includes water vapor, nitrogen and excess hydrogen fluoride. The tail gas is discharged through the exhaust port C252 and then sent into the inner cavity of the fluidized bed B23 through the air inlet B231.

[0052] In this step, ammonia gas is added in excess in sub-step A to ensure that uranium oxide is fully reduced.

[0053] In this step, hydrogen fluoride in sub-step E is added in excess to ensure that uranium dioxide is fully hydrofluorinated.

[0054] In this step, the following reactions mainly occur in sub-step A: 4NH3 + 3U3O8 → 9UO2 + 2N2 + 6H2O; U3O8 + 8HF → 2UO2F2 + UF4 + 4H2O; 6UO2F2 + 4NH3 → 3UO2 + 3UF4 + 2N2 + 6H2O.

[0055] In this step, the following reaction mainly occurs in sub-steps C and E: UO2 + 4HF → UF4 + H2O.

[0056] In this step, the input gas in sub-step C contains water vapor. On the one hand, water vapor can mitigate the initial intense reaction between uranium dioxide and hydrogen fluoride, which is beneficial for protecting the reaction. On the other hand, water vapor has a high thermal conductivity, which allows the heat generated by the reaction in fluidized bed B23 to be conducted away more quickly.

[0057] S04, exhaust gas recovery and utilization:

[0058] A. The exhaust gas produced by the three-stage fluidization mechanism is discharged through exhaust port A212, exhaust port X223, exhaust port B232, exhaust port Y243 and exhaust port C252 respectively. All exhaust gas enters the inner cavity of condenser 31 through gas inlet A311 and is condensed into acidic wastewater containing hydrogen fluoride and ammonium ions in the inner cavity of condenser 31.

[0059] B. After the acidic wastewater is discharged from the condensate outlet 312 of the condenser 31, silica gel balls are used to adsorb uranium ions in the acidic wastewater.

[0060] C. The acidic wastewater after uranium removal is fed into the inner cavity of the crystallization tank 32 through the condensate inlet 321. The filtrate in the crystallization tank 32 is heated and evaporated until ammonium fluoride crystals precipitate, resulting in a saturated ammonium fluoride solution. The saturated ammonium fluoride solution is cooled to room temperature to reduce the solubility of ammonium fluoride, allowing more ammonium fluoride crystals to precipitate. During the heating and evaporation of the filtrate, ammonia gas is volatilized and discharged through the ammonia outlet B324. The ammonia gas then enters the scrubbing tower 35 through the gas inlet B351, where it is scrubbed to recover ammonia water. During the precipitation of ammonium fluoride crystals, the third stirring device is continuously started to ensure that the ammonium fluoride crystals are evenly dispersed in the saturated ammonium fluoride solution, forming a slurry. The slurry is discharged through the slurry outlet 322.

[0061] D. After the slurry is discharged from the slurry outlet 322, it enters the plate filter 33 through the slurry inlet 331 for solid-liquid separation. The separated solid is ammonium fluoride crystals, which are discharged from the solid outlet 333 and then sent to the microwave dryer 34 for drying to obtain solid ammonium fluoride. The separated liquid is a solution containing ammonium ions, which is discharged from the filtrate outlet 332 and then returned to the crystallization tank 32 through the ammonia water replenishment port 323. It is heated and evaporated again to volatilize ammonia gas. The ammonia gas is discharged through the ammonia gas outlet B324 and then enters the scrubbing tower 35 through the gas inlet B351. After scrubbing, ammonia water is obtained.

[0062] In this step, the following reaction occurs in sub-steps C and D: NH3·H2O→NH3+H2O.

Claims

1. A system for preparing uranium tetrafluoride based on a reducing hydrofluorination reaction, characterized by: It includes a gas supply system, a three-stage fluidization system, and an exhaust gas treatment system; The gas supply mechanism includes an ammonium fluoride heating tank and a gas separator. The ammonium fluoride heating tank has an internal cavity for storing ammonium fluoride, a mixed gas outlet at its upper end, and a heating device A for heating its internal cavity. The gas separator has an internal cavity for holding potassium difluoride, a mixed gas inlet, an ammonia outlet A, and a hydrogen fluoride outlet at its top. The mixed gas inlet extends into the internal cavity of the gas separator to a greater depth than the ammonia outlet A and the hydrogen fluoride outlet extend into the internal cavity of the gas separator. A heating device B for heating its internal cavity is located on the outside of the gas separator. The mixed gas inlet of the gas separator is connected to the mixed gas outlet of the ammonium fluoride heating tank. The three-stage fluidized bed system includes fluidized bed A, intermediate container X, fluidized bed B, intermediate container Y, and fluidized bed C. Fluidized bed A has an external air inlet A, an external exhaust outlet A, an external feed inlet A, and an external discharge outlet A. The air inlet A is connected to the ammonia outlet A of the gas separator. Intermediate container X has an external feed inlet X, an external discharge outlet X, and an external exhaust outlet X. The feed inlet X is connected to the discharge outlet A of fluidized bed A. Fluidized bed B has an external air inlet B, an external exhaust outlet B, and an external feed inlet B. Discharge port B and feed port B are connected to discharge port X of intermediate container X; the intermediate container Y is provided with feed port Y, discharge port Y and exhaust port Y on the outside, and feed port Y is connected to discharge port B of fluidized bed B; the fluidized bed C is provided with air inlet C, exhaust port C, feed port C and discharge port C on the outside, feed port C is connected to discharge port Y of intermediate container Y, exhaust port C is connected to air inlet B of fluidized bed B, and air inlet C is connected to hydrogen fluoride outlet of gas separator; The exhaust gas treatment system includes a condenser, a crystallization tank, a plate filter, a microwave dryer, and a scrubbing tower. The condenser has a gas inlet A and a condensate outlet on its exterior. Gas inlet A is connected to the exhaust port A of fluidized bed A, the exhaust port X of intermediate container X, the exhaust port B of fluidized bed B, and the exhaust port Y of intermediate container Y, respectively. The crystallization tank has an internal cavity for holding the condensate, and a third stirring device is installed within the cavity. The crystallization tank has a condensate inlet, a slurry outlet, an ammonia water replenishment port, and an ammonia outlet B on its exterior. The condensate inlet is connected to the condensate outlet of the condenser. The plate filter has a slurry inlet, a filtrate outlet, and a solids outlet on its exterior. The slurry inlet is connected to the slurry outlet of the crystallization tank, and the filtrate outlet is connected to the ammonia water replenishment port of the crystallization tank. The microwave dryer is used to dry the solids discharged from the solids outlet of the plate filter. The scrubbing tower has a gas inlet B and a scrubbing liquid outlet on its exterior. Gas inlet B is connected to the ammonia outlet B of the crystallization tank.

2. The uranium tetrafluoride preparation system based on the reducing hydrofluorination reaction as described in claim 1, characterized in that: A sampling port is provided on the side wall of the gas separator, and valve A is provided on the sampling port.

3. The uranium tetrafluoride preparation system based on the reducing hydrofluorination reaction as described in claim 2, characterized in that: The ammonium fluoride heating tank has a valve B at the mixed gas outlet, the ammonia outlet A of the gas separator has a valve C, and the hydrogen fluoride outlet of the gas separator has a valve D.

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