Wet-process phosphoric acid fluorine recovery reaction device

Abstract

The utility model provides a wet-process phosphoric acid fluorine recovery reaction device. The liquid outlet end of the hydrofluoric acid conveying pipeline is communicated with the liquid inlet end of the reaction slurry tank. The liquid inlet end of the flash evaporation reactor is communicated with the liquid outlet end of the reaction slurry tank, the liquid return end of the flash evaporation reactor is communicated with the liquid inlet end of the reaction slurry tank, and a backflow space is formed between the liquid return end of the flash evaporation reactor and the liquid inlet end of the reaction slurry tank. The liquid inlet end of the first temperature exchanger is communicated with the liquid outlet end of the hydrofluoric acid conveying pipeline, the gas outlet end of the first temperature exchanger is communicated with the gas inlet end of the flash evaporation reactor, and the gas inlet end of the second temperature exchanger is communicated with the gas outlet end of the flash evaporation reactor. And the first vacuumizing pump is arranged on a pipeline for communicating the flash evaporation reactor with the second temperature exchanger. And the liquid inlet end of the fluosilicic acid liquid storage tank is communicated with the liquid outlet end of the second temperature exchanger.

Description

Technical Field

[0001] The present invention relates to the field of production of lithium iron phosphate positive electrode raw materials, and in particular to a wet-process phosphoric acid fluoride recovery reaction device. Background Art

[0002] During the wet phosphoric acid reaction, about 50%-70% of the fluorine contained in the slurry flashes out in the flash cooler. The secondary steam coming out of the flash cooler contains SiF4 and HF. These fluorines are recovered in the form of H2SiF6 in two fluorine absorption towers connected in series. The absorption liquid is H2SiF6 solution. During the fluorine absorption process, SiF4 undergoes hydrolysis reaction with water in the H2SiF6 solution, and the formed SiO2 reacts with HF in the gas at the same time. The reaction formula is as follows:

[0003] 3SiF4+2H2O—2H2SiF6+SiO2(1)

[0004] 6HF+SiO2—H2SiF6+2H2O(2)

[0005] In reaction formula (1), SiO2 precipitated is in the form of white colloid or solid, and the precipitation of SiO2 depends on the molar ratio of HF and SiF4:

[0006] When n(HF) / n(SiF4)<2, SiO2 will precipitate;

[0007] When n(HF) / n(SiF4)≥2, no SiO2 precipitates;

[0008] However, in the actual production process, the HF content of the secondary steam is often insufficient to completely react SiO2, and SiO2 will scale and cause blockage on the equipment and pipelines, which will not only reduce the operating cycle of the reaction unit, but also reduce the fluorine absorption efficiency of the reaction unit.

[0009] Therefore, there is an urgent need for a reaction device that can prevent silica gel from clogging and improve fluorine absorption efficiency. Utility Model Content

[0010] The purpose of the present invention is to overcome the shortcomings of the prior art and provide a wet-process phosphoric acid fluoride recovery reaction device that can prevent silica gel clogging and improve fluorine absorption efficiency.

[0011] The purpose of this disclosure is achieved through the following technical solutions:

[0012] A wet process phosphoric acid fluoride recovery reaction device, comprising:

[0013] Reaction slurry tank;

[0014] A hydrofluoric acid delivery pipeline, wherein the liquid outlet end of the hydrofluoric acid delivery pipeline is connected to the liquid inlet end of the reaction slurry tank;

[0015] A flash reactor, wherein the liquid inlet end of the flash reactor is connected to the liquid outlet end of the reaction slurry tank, the liquid return end of the flash reactor is connected to the liquid inlet end of the reaction slurry tank, and a reflux gap is formed between the liquid return end of the flash reactor and the liquid inlet end of the reaction slurry tank;

[0016] A temperature exchange component, the temperature exchange component comprising a first temperature exchanger and a second temperature exchanger, the liquid inlet end of the first temperature exchanger is connected to the liquid outlet end of the hydrofluoric acid delivery pipeline, the gas outlet end of the first temperature exchanger is connected to the gas inlet end of the flash reactor, and the gas inlet end of the second temperature exchanger is connected to the gas outlet end of the flash reactor;

[0017] a first vacuum pump, wherein the first vacuum pump is disposed on a pipeline connecting the flash reactor and the second temperature exchanger;

[0018] A fluorosilicic acid storage tank, wherein a liquid inlet end of the fluorosilicic acid storage tank is connected to a liquid outlet end of the second temperature exchanger.

[0019] In one embodiment, the surface interlayer of the first temperature exchanger is provided with a first cooling water inlet and a first cooling water outlet, and the surface interlayer of the second temperature exchanger is provided with a second cooling water inlet and a second cooling water outlet, the first cooling water inlet is connected to the second cooling water outlet, and the first cooling water outlet is connected to the second cooling water inlet.

[0020] In one embodiment, the temperature exchange component also includes a first water circulation pipe and a second water circulation pipe, wherein both ends of the first water circulation pipe are respectively connected to the first cooling water inlet and the second cooling water outlet, and both ends of the second water circulation pipe are respectively connected to the first cooling water outlet and the second cooling water inlet.

[0021] In one of the embodiments, the wet process phosphoric acid fluoride recovery reaction device further includes a liquid pumping and delivery pump, and the liquid pumping and delivery pump is arranged on a pipeline connecting the liquid outlet end of the reaction slurry tank and the liquid inlet end of the flash reactor.

[0022] In one embodiment, the wet process phosphoric acid fluoride recovery reaction device also includes a gas-liquid separation component, which includes a gas-liquid separator, an exhaust pipe and a second vacuum pump. The feed end of the gas-liquid separator is connected to the gas outlet end of the second temperature exchanger, the gas outlet end of the gas-liquid separator is connected to one end of the exhaust pipe, the liquid outlet end of the gas-liquid separator is connected to the liquid inlet end of the fluorosilicic acid storage tank, and the second vacuum pump is arranged on the exhaust pipe.

[0023] In one of the embodiments, the gas-liquid separation component further includes a first control switch valve, and the first control switch valve is arranged on a pipeline connecting the feed end of the gas-liquid separator and the gas outlet end of the second temperature exchanger.

[0024] In one embodiment, the temperature exchange component further includes a third temperature exchanger, wherein a feed end of the third temperature exchanger is connected to a gas outlet end of the second temperature exchanger, and a discharge end of the third temperature exchanger is connected to a feed end of the gas-liquid separator.

[0025] In one of the embodiments, the surface interlayer of the third temperature exchanger is provided with a chilled water inlet and a chilled water outlet, and the chilled water inlet and the chilled water outlet are both connected to the chilled water assembly.

[0026] In one of the embodiments, the temperature exchange component further includes a second control switch valve, and the second control switch valve is arranged on a pipeline connecting the gas outlet end of the second temperature exchanger and the feed end of the third temperature exchanger.

[0027] In one embodiment, the wet process phosphoric acid fluoride recovery reaction device further includes a hydrofluoric acid flow meter, and the hydrofluoric acid flow meter is arranged on the hydrofluoric acid delivery pipeline.

[0028] Compared with the prior art, the present invention has at least the following advantages:

[0029] 1. The slurry in the reaction slurry tank is transported to the flash reactor for flash vaporization to obtain steam, and then the vacuum degree in the flash reactor is adjusted by adjusting the size of the reflux spacing, that is, adjusting the height of the flash chamber, so as to ensure that the unevaporated liquid phase material in the flash reactor flows back to the reaction slurry tank to continue the reaction, so that the slurry in the reaction slurry tank can fully react with hydrofluoric acid, thereby improving the fluorine absorption efficiency of the wet-process phosphoric acid fluoride recovery reaction device.

[0030] 2. The hydrofluoric acid solution is transported to the first temperature exchanger through the hydrofluoric acid transport pipeline, and after being heated by the first temperature exchanger, atomized hydrofluoric acid is formed and transported to the flash reactor for mixing. The steam and atomized hydrofluoric acid in the flash reactor are then transported to the second temperature exchanger through the first vacuum pump for cooling and sufficient reaction. The fluorosilicic acid solution obtained by the reaction is transported to the fluorosilicic acid storage tank, which makes n(HF) / n(SiF4)≥6 in the flash reactor and the second temperature exchanger. This ensures that no silica gel is produced in the wet-process phosphoric acid fluoride recovery reaction device, avoids blockage caused by silica gel, and improves the operation cycle and fluorine absorption efficiency of the wet-process phosphoric acid fluoride recovery reaction device. BRIEF DESCRIPTION OF THE DRAWINGS

[0031] In order to more clearly illustrate the technical solutions of the embodiments of the present disclosure, the drawings required for use in the embodiments will be briefly introduced below. It should be understood that the following drawings only show certain embodiments of the present disclosure and therefore should not be regarded as limiting the scope. For ordinary technicians in this field, other related drawings can be obtained based on these drawings without paying creative work.

[0032] Figure 1 This is a schematic structural diagram of a wet-process phosphoric acid fluoride recovery reaction device in one embodiment;

[0033] Figure 2 for Figure 1 A partial structural schematic diagram of a wet-process phosphoric acid fluoride recovery reaction device is shown;

[0034] Figure 3 for Figure 1 A partial structural schematic diagram of a wet-process phosphoric acid fluoride recovery reaction device is shown;

[0035] Figure numerals: wet-process phosphoric acid fluoride recovery reaction device 10; reaction slurry tank 100; hydrofluoric acid delivery pipeline 200; flash reactor 300; temperature exchange component 400; first temperature exchanger 410; first cooling water inlet 412; first cooling water outlet 414; second temperature exchanger 420; second cooling water inlet 422; second cooling water outlet 424; first water circulation pipeline 430; second water circulation pipeline 440; third temperature exchanger 450; chilled water inlet 452; chilled water outlet 454; second control switch valve 460; first vacuum pump 500; fluorosilicic acid storage tank 600; liquid delivery pump 700; gas-liquid separation component 800; gas-liquid separator 810; exhaust pipeline 820; second vacuum pump 830; first control switch valve 840; hydrofluoric acid flow meter 900. DETAILED DESCRIPTION

[0036] In order to facilitate the understanding of the present disclosure, the present disclosure will be described more fully below with reference to the relevant drawings. The preferred embodiments of the present disclosure are given in the drawings. However, the present disclosure can be implemented in many different forms and is not limited to the embodiments described herein. On the contrary, the purpose of providing these embodiments is to make the disclosure of the present disclosure more thoroughly and comprehensively understood.

[0037] It should be noted that when an element is referred to as being "fixed to" another element, it may be directly on the other element or there may be a central element. When an element is considered to be "connected to" another element, it may be directly connected to the other element or there may be a central element at the same time. The terms "vertical", "horizontal", "left", "right" and similar expressions used herein are for illustrative purposes only and do not represent the only implementation method.

[0038] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as those commonly understood by those skilled in the art of the present disclosure. The terms used herein in the specification of the present disclosure are only for the purpose of describing specific embodiments and are not intended to limit the present disclosure. The term "and / or" used herein includes any and all combinations of one or more related listed items.

[0039] See also Figures 1 to 3 In order to better understand the wet process phosphoric acid fluoride recovery reaction device 10 disclosed in the present invention, the wet process phosphoric acid fluoride recovery reaction device 10 is further explained as follows:

[0040] A wet process phosphoric acid fluoride recovery reaction device 10 of one embodiment includes a reaction slurry tank 100, a hydrofluoric acid delivery pipeline 200, a flash reactor 300, a temperature exchange component 400, a first vacuum pump 500 and a fluorosilicic acid storage tank 600. The liquid outlet end of the hydrofluoric acid delivery pipeline 200 is connected to the liquid inlet end of the reaction slurry tank 100. The liquid inlet end of the flash reactor 300 is connected to the liquid outlet end of the reaction slurry tank 100, and the liquid return end of the flash reactor 300 is connected to the liquid inlet end of the reaction slurry tank 100, and a reflux gap is formed between the liquid return end of the flash reactor 300 and the liquid inlet end of the reaction slurry tank 100. The temperature exchange assembly 400 includes a first temperature exchanger 410 and a second temperature exchanger 420. The liquid inlet end of the first temperature exchanger 410 is connected to the liquid outlet end of the hydrofluoric acid delivery pipeline 200, the gas outlet end of the first temperature exchanger 410 is connected to the gas inlet end of the flash reactor 300, and the gas inlet end of the second temperature exchanger 420 is connected to the gas outlet end of the flash reactor 300. The first vacuum pump 500 is disposed on the pipeline connecting the flash reactor 300 and the second temperature exchanger 420. The liquid inlet end of the fluorosilicic acid storage tank 600 is connected to the liquid outlet end of the second temperature exchanger 420.

[0041] In this embodiment, the slurry in the reaction slurry tank 100 is transported to the flash reactor 300 for flash vaporization to obtain steam, and then the vacuum degree in the flash reactor 300 is adjusted by adjusting the size of the reflux spacing, that is, the height of the flash chamber is adjusted. This ensures that the unevaporated liquid material in the flash reactor 300 flows back to the reaction slurry tank 100 to continue the reaction, so that the slurry in the reaction slurry tank 100 can fully react with hydrofluoric acid, thereby improving the fluorine absorption efficiency of the wet-process phosphoric acid fluorine recovery reaction device 10.

[0042] Furthermore, the hydrofluoric acid solution is transported to the first temperature exchanger 410 through the hydrofluoric acid delivery pipeline 200, and after being heated by the first temperature exchanger 410, it is formed into atomized hydrofluoric acid and transported to the flash reactor 300 for mixing, and then the steam and atomized hydrofluoric acid in the flash reactor 300 are transported to the second temperature exchanger 420 through the first vacuum pump 500 for cooling and sufficient reaction. The fluorosilicic acid solution obtained by the reaction is transported to the fluorosilicic acid storage tank 600, which makes n(HF) / n(SiF4)≥6 in the flash reactor 300 and the second temperature exchanger 420, thereby ensuring that no silica gel is produced in the wet phosphoric acid fluoride recovery reaction device 10, avoiding the blockage caused by silica gel, and improving the operation cycle and fluorine absorption efficiency of the wet phosphoric acid fluoride recovery reaction device 10.

[0043] It should be noted that the hydrofluoric acid solution is transported to the reaction slurry tank 100 through the hydrofluoric acid delivery pipeline 200 for reaction, and the slurry components transported from the reaction slurry tank 100 to the flash reactor 300 mainly include H2SiF6 and SiF4, that is, the steam components are mainly H2SiF6, SiF4, HF and H2O, and the steam and atomized hydrofluoric acid are transported to the second temperature exchanger 420 through the first vacuum pump 500 for cooling and sufficient contact reaction. During this period, n(HF) / n(SiF4)≥6, and no SiO2 is precipitated.

[0044] In one embodiment, the height of the reflow spacing is set to H, and the minimum value of the height H satisfies the following formula:

[0045]

[0046] Wherein P1 is the pressure in the reaction slurry tank 100, P2 is the pressure in the flash reactor 300, ρ is the slurry density, and g is the gravitational acceleration. It can be understood that by adjusting the height of the flash reactor 300, the vacuum degree in the flash reactor 300 is increased while ensuring that the slurry can overcome the suction of the first vacuum pump 500 to flow back into the reaction slurry tank 100.

[0047] like Figure 2As shown, in one embodiment, the surface interlayer of the first temperature exchanger 410 is provided with a first cooling water inlet 412 and a first cooling water outlet 414, and the surface interlayer of the second temperature exchanger 420 is provided with a second cooling water inlet 422 and a second cooling water outlet 424, the first cooling water inlet 412 is communicated with the second cooling water outlet 424, and the first cooling water outlet 414 is communicated with the second cooling water inlet 422. It can be understood that the function of the first temperature exchanger 410 is heating, that is, the first cooling water inlet 412 inputs hot water, which forms cooling water after indirect contact and is discharged from the first cooling water outlet 414. Similarly, the function of the second temperature exchanger 420 is cooling, that is, the second cooling water inlet 422 inputs cold water, which forms hot water after indirect contact and is discharged from the second cooling water outlet 424.

[0048] like Figure 2 As shown, in one embodiment, the temperature exchange component 400 further includes a first water circulation pipeline 430 and a second water circulation pipeline 440, the two ends of the first water circulation pipeline 430 are respectively connected to the first cooling water inlet 412 and the second cooling water outlet 424, and the two ends of the second water circulation pipeline 440 are respectively connected to the first cooling water outlet 414 and the second cooling water inlet 422. It can be understood that firstly, the surface interlayer in the first temperature exchanger 410 is filled with hot water, which becomes cooling water after indirect contact, and the cooling water is discharged from the first cooling water outlet 414 to the second water circulation pipeline 440, that is, the cooling water is transported to the surface interlayer of the second temperature exchanger 420, and becomes hot water again after indirect contact, and the hot water is discharged from the second cooling water outlet 424 to the first water circulation pipeline 430, that is, the hot water is transported to the surface interlayer of the first temperature exchanger 410, so that the recycling of cooling water can be realized, the utilization rate of thermal energy is improved, and the production cost of the wet-process phosphoric acid fluoride recovery reaction device 10 is effectively reduced.

[0049] like Figure 1 and Figure 2 As shown, in one embodiment, the wet process phosphoric acid fluoride recovery reaction device 10 further includes a liquid pumping and delivery pump 700, and the liquid pumping and delivery pump 700 is arranged on a pipeline connecting the liquid outlet end of the reaction slurry tank 100 and the liquid inlet end of the flash reactor 300. It can be understood that the slurry of the reaction slurry tank 100 can be pumped into the flash reactor 300 by the liquid pumping and delivery pump 700, that is, pumped from the liquid outlet end at the bottom of the reaction slurry tank 100 to the liquid inlet end in the middle of the flash reactor 300.

[0050] like Figures 1 to 3As shown, in one embodiment, the wet process phosphoric acid fluoride recovery reaction device 10 also includes a gas-liquid separation component 800, and the gas-liquid separation component 800 includes a gas-liquid separator 810, an exhaust pipe 820 and a second vacuum pump 830, the feed end of the gas-liquid separator 810 is connected to the gas outlet end of the second temperature exchanger 420, the gas outlet end of the gas-liquid separator 810 is connected to one end of the exhaust pipe 820, the liquid outlet end of the gas-liquid separator 810 is connected to the liquid inlet end of the fluorosilicic acid storage tank 600, and the second vacuum pump 830 is arranged on the exhaust pipe 820. It can be understood that the air discharged from the second temperature exchanger 420 is mixed with part of the fluorosilicic acid solution, and then the air discharged from the second temperature exchanger 420 is discharged into the gas-liquid separator 810 for gas-liquid separation operation. This part of the fluorosilicic acid solution is transported from the liquid outlet end of the gas-liquid separator 810 to the fluorosilicic acid storage tank 600 for recovery, while the air is extracted by the second vacuum pump 830 to the exhaust pipe 820 for discharge.

[0051] like Figure 3 As shown, in one embodiment, the gas-liquid separation component 800 further includes a first control switch valve 840, and the first control switch valve 840 is disposed on a pipeline connecting the feed end of the gas-liquid separator 810 and the gas outlet end of the second temperature exchanger 420. It can be understood that the air discharge of the second temperature exchanger 420 is controlled by the first control switch valve 840, so as to control the air discharge in the second temperature exchanger 420.

[0052] like Figures 1 to 3 As shown, in one embodiment, the temperature exchange component 400 further includes a third temperature exchanger 450, the feed end of the third temperature exchanger 450 is connected to the gas outlet end of the second temperature exchanger 420, and the discharge end of the third temperature exchanger 450 is connected to the feed end of the gas-liquid separator 810. It can be understood that the third temperature exchanger 450 has a cooling effect. In summer, the temperature of the cooling water is high, and the second temperature exchanger 420 is not enough to cool and liquefy the steam. At this time, the steam and atomized hydrofluoric acid are transferred from the second temperature exchanger 420 to the third temperature exchanger 450 for cooling and liquefaction, and the obtained fluorosilicic acid solution and air are transported by the third temperature exchanger 450 to the gas-liquid separator 810 for gas-liquid separation operation, so that the wet-process phosphoric acid fluoride recovery reaction device 10 can adapt to different use environments.

[0053] like Figure 3As shown, in one embodiment, the surface interlayer of the third temperature exchanger 450 is provided with a chilled water inlet 452 and a chilled water outlet 454, and the chilled water inlet 452 and the chilled water outlet 454 are both connected to the chilled water assembly. It can be understood that chilled water is introduced into the surface interlayer of the third temperature exchanger 450 to ensure the cooling effect of the third temperature exchanger 450, thereby ensuring that the steam and the atomized hydrofluoric acid can be completely liquefied and fully contacted to react, thereby effectively improving the fluorine absorption efficiency of the wet-process phosphoric acid fluorine recovery reaction device 10.

[0054] like Figures 1 to 3 As shown, in one embodiment, the temperature exchange component 400 further includes a second control switch valve 460, and the second control switch valve 460 is disposed on a pipeline connecting the gas outlet end of the second temperature exchanger 420 and the feed end of the third temperature exchanger 450. It can be understood that the second control switch valve 460 is used to switch the second temperature exchanger 420 and the third temperature exchanger 450 back and forth in the wet-process phosphoric acid fluoride recovery reaction device 10, so as to improve the convenience of use of the wet-process phosphoric acid fluoride recovery reaction device 10.

[0055] like Figure 1 and Figure 2 As shown, in one embodiment, the wet-process phosphoric acid fluoride recovery reaction device 10 further includes a hydrofluoric acid flow meter 900, and the hydrofluoric acid flow meter 900 is disposed on the hydrofluoric acid delivery pipeline 200. It is understandable that the input amount of hydrofluoric acid is controlled by the hydrofluoric acid flow meter 900 to ensure that n(HF) / n(SiF4)≥6, so that no silica gel is generated in the wet-process phosphoric acid fluoride recovery reaction device 10, and the situation that the silica gel causes the device to be blocked occurs, thereby improving the operation cycle of the wet-process phosphoric acid fluoride recovery reaction device 10 and the fluorine absorption efficiency.

[0056] Compared with the prior art, the present invention has at least the following advantages:

[0057] 1. The slurry in the reaction slurry tank is transported to the flash reactor for flash vaporization to obtain steam, and then the vacuum degree in the flash reactor is adjusted by adjusting the size of the reflux spacing, that is, adjusting the height of the flash chamber, so as to ensure that the unevaporated liquid phase material in the flash reactor flows back to the reaction slurry tank to continue the reaction, so that the slurry in the reaction slurry tank can fully react with hydrofluoric acid, thereby improving the fluorine absorption efficiency of the wet-process phosphoric acid fluoride recovery reaction device.

[0058] 2. The hydrofluoric acid solution is transported to the first temperature exchanger through the hydrofluoric acid transport pipeline, and after being heated by the first temperature exchanger, atomized hydrofluoric acid is formed and transported to the flash reactor for mixing. The steam and atomized hydrofluoric acid in the flash reactor are then transported to the second temperature exchanger through the first vacuum pump for cooling and sufficient reaction. The fluorosilicic acid solution obtained by the reaction is transported to the fluorosilicic acid storage tank, which makes n(HF) / n(SiF4)≥6 in the flash reactor and the second temperature exchanger. This ensures that no silica gel is produced in the wet-process phosphoric acid fluoride recovery reaction device, avoids blockage caused by silica gel, and improves the operation cycle and fluorine absorption efficiency of the wet-process phosphoric acid fluoride recovery reaction device.

[0059] The above-mentioned embodiments only express several implementation methods of the present disclosure, and the descriptions thereof are relatively specific and detailed, but they cannot be understood as limiting the scope of the disclosed patent. It should be pointed out that, for a person of ordinary skill in the art, several variations and improvements can be made without departing from the concept of the present disclosure, and these all belong to the protection scope of the present disclosure. Therefore, the protection scope of the disclosed patent shall be subject to the attached claims.

Claims

1. A wet process phosphoric acid fluoride recovery reaction device (10), characterized in that: include: Reaction slurry tank (100); A hydrofluoric acid delivery pipeline (200), wherein the liquid outlet end of the hydrofluoric acid delivery pipeline (200) is connected to the liquid inlet end of the reaction slurry tank (100); A flash reactor (300), wherein the liquid inlet end of the flash reactor (300) is connected to the liquid outlet end of the reaction slurry tank (100), the liquid return end of the flash reactor (300) is connected to the liquid inlet end of the reaction slurry tank (100), and a reflux gap is formed between the liquid return end of the flash reactor (300) and the liquid inlet end of the reaction slurry tank (100); A temperature exchange component (400), the temperature exchange component (400) comprising a first temperature exchanger (410) and a second temperature exchanger (420), the liquid inlet end of the first temperature exchanger (410) being in communication with the liquid outlet end of the hydrofluoric acid delivery pipeline (200), the gas outlet end of the first temperature exchanger (410) being in communication with the gas inlet end of the flash reactor (300), and the gas inlet end of the second temperature exchanger (420) being in communication with the gas outlet end of the flash reactor (300); a first vacuum pump (500), the first vacuum pump (500) being arranged on a pipeline connecting the flash reactor (300) and the second temperature exchanger (420); A fluorosilicic acid storage tank (600), wherein the liquid inlet end of the fluorosilicic acid storage tank (600) is connected to the liquid outlet end of the second temperature exchanger (420).

2. The wet process phosphoric acid fluoride recovery reaction device (10) according to claim 1, characterized in that: The surface interlayer of the first temperature exchanger (410) is provided with a first cooling water inlet (412) and a first cooling water outlet (414), and the surface interlayer of the second temperature exchanger (420) is provided with a second cooling water inlet (422) and a second cooling water outlet (424), the first cooling water inlet (412) is connected to the second cooling water outlet (424), and the first cooling water outlet (414) is connected to the second cooling water inlet (422).

3. The wet process phosphoric acid fluoride recovery reaction device (10) according to claim 2, characterized in that: The temperature exchange component (400) further includes a first water circulation pipe (430) and a second water circulation pipe (440), wherein both ends of the first water circulation pipe (430) are respectively connected to the first cooling water inlet (412) and the second cooling water outlet (424), and both ends of the second water circulation pipe (440) are respectively connected to the first cooling water outlet (414) and the second cooling water inlet (422).

4. The wet process phosphoric acid fluoride recovery reaction device (10) according to claim 1, characterized in that: It also includes a liquid pumping and delivery pump (700), which is arranged on a pipeline connecting the liquid outlet end of the reaction slurry tank (100) and the liquid inlet end of the flash reactor (300).

5. The wet process phosphoric acid fluoride recovery reaction device (10) according to claim 1, characterized in that: The invention also includes a gas-liquid separation component (800), wherein the gas-liquid separation component (800) includes a gas-liquid separator (810), an exhaust pipe (820) and a second vacuum pump (830), wherein the feed end of the gas-liquid separator (810) is connected to the gas outlet end of the second temperature exchanger (420), the gas outlet end of the gas-liquid separator (810) is connected to one end of the exhaust pipe (820), the liquid outlet end of the gas-liquid separator (810) is connected to the liquid inlet end of the fluorosilicic acid storage tank (600), and the second vacuum pump (830) is arranged on the exhaust pipe (820).

6. The wet process phosphoric acid fluoride recovery reaction device (10) according to claim 5, characterized in that: The gas-liquid separation component (800) further comprises a first control switch valve (840), wherein the first control switch valve (840) is arranged on a pipeline connecting the feed end of the gas-liquid separator (810) and the gas outlet end of the second temperature exchanger (420).

7. The wet process phosphoric acid fluoride recovery reaction device (10) according to claim 5, characterized in that: The temperature exchange component (400) further comprises a third temperature exchanger (450), the feed end of the third temperature exchanger (450) being connected to the gas outlet end of the second temperature exchanger (420), and the discharge end of the third temperature exchanger (450) being connected to the feed end of the gas-liquid separator (810).

8. The wet process phosphoric acid fluoride recovery reaction device (10) according to claim 7, characterized in that: The surface interlayer of the third temperature exchanger (450) is provided with a chilled water inlet (452) and a chilled water outlet (454), and both the chilled water inlet (452) and the chilled water outlet (454) are connected to the chilled water component.

9. The wet process phosphoric acid fluoride recovery reaction device (10) according to claim 7, characterized in that: The temperature exchange component (400) further comprises a second control switch valve (460), and the second control switch valve (460) is arranged on a pipeline connecting the gas outlet end of the second temperature exchanger (420) and the feed end of the third temperature exchanger (450).

10. The wet process phosphoric acid fluoride recovery reaction device (10) according to claim 1, characterized in that: It also includes a hydrofluoric acid flow meter (900), and the hydrofluoric acid flow meter (900) is arranged on the hydrofluoric acid delivery pipeline (200).

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