A vacuum device for concentrating byproducts in zirconium oxychloride production

Abstract

This utility model discloses a vacuum device for concentrating by-products in zirconium oxychloride production. The vacuum device comprises a reaction vessel, a heat exchanger, and a water-circulating vacuum unit. The exhaust port of the reaction vessel is connected to the heat medium inlet of the heat exchanger, and the heat medium outlet of the heat exchanger is connected to the water-circulating vacuum unit. This vacuum device for concentrating by-products in zirconium oxychloride production has the advantages of high waste heat utilization, rapid evaporation of water glass solution, reduced steam requirements, and cost savings in production.

Description

Technical Field

[0001] This application relates to the field of chemical equipment, and in particular to a vacuum device for concentrating byproducts in the production of zirconium oxychloride. Background Technology

[0002] In the production of zirconium oxychloride, waste residue and waste alkali (i.e., silicon slag and dilute alkaline solution) are generated. After concentration, the dilute alkaline solution reacts with the silicon slag to form water glass. The water glass solution can be evaporated, concentrated, and crystallized to form sodium metasilicate nonahydrate. The water glass solution is often concentrated by passing steam into the jacket of a jacketed reactor to heat and concentrate the water glass solution inside the reactor.

[0003] However, the presence of a large number of strongly interacting silicate ions in the water glass solution makes it difficult for water molecules to break free and turn into gas. When steam is introduced into the jacket layer to heat the vessel under normal atmospheric pressure, the water glass solution will have a long concentration time and require a large amount of heat energy during the heating process, i.e., a large amount of steam will be consumed. Utility Model Content

[0004] Based on this, the purpose of this utility model is to provide a vacuum device for concentrating by-products in the production of zirconium oxychloride, which has the advantages of high waste heat utilization rate, fast evaporation rate of water glass solution, reduced steam requirement, and saving production costs.

[0005] To achieve the above objectives, this utility model provides a vacuum device for concentrating by-products in zirconium oxychloride production, comprising:

[0006] The reactor comprises a reactor, a heat exchanger, and a water-circulating vacuum unit. The exhaust port of the reactor is connected to the heat medium inlet of the heat exchanger, and the heat medium outlet of the heat exchanger is connected to the water-circulating vacuum unit.

[0007] The vacuum device for concentrating by-products in zirconium oxychloride production described in this utility model utilizes a water-circulating vacuum system to create a negative pressure environment inside the reactor. Under negative pressure, the boiling point of the water glass solution decreases, resulting in faster and more efficient heating, evaporation, and concentration of the water glass solution inside the reactor. This reduces the amount of steam consumed in heating the reactor. Simultaneously, the water glass solution inside the reactor generates a large amount of water vapor during the evaporation and concentration process. This water vapor undergoes heat exchange in the heat exchanger, effectively utilizing the residual heat in the high-temperature water vapor.

[0008] In one embodiment, the water circulation vacuum unit includes a water circulation vacuum pump, a circulating water tank, and a first gas-liquid separator. The water circulation vacuum pump is connected to the circulating water tank via a pipeline. The suction port of the water circulation vacuum pump is connected to the exhaust port of the first gas-liquid separator. The inlet of the circulating water tank is connected to the drain port of the first gas-liquid separator. The heat medium outlet of the heat exchanger is connected to the gas-liquid inlet of the first gas-liquid separator. The water-circulating vacuum pump contains an impeller with multiple blades. Working water from the circulating water tank enters the pump, and the high-speed rotating impeller drives the water flow to form a water ring. A negative pressure cavity is formed between the water ring and the impeller. This cavity can draw in air and gas from the container to be vacuumed, thus creating a negative pressure environment within the container. At this time, the first gas-liquid separator removes liquid droplets from the gas drawn in by the pump, preventing them from entering the pump chamber and extending the pump's lifespan. During operation, the pump discharges a water vapor mixture containing a large number of air bubbles into the circulating water tank. The tank provides a large space, causing the water flow velocity to drop sharply, the bubbles to burst, and non-condensable gases to separate from the water and be released into the atmosphere. The separated water settles and can be recycled.

[0009] In one embodiment, the system further includes a feed tank and a feed circulation pump. The heat exchanger also includes a cold medium inlet and a cold medium outlet. The outlet of the feed tank is connected to the cold medium inlet of the heat exchanger. The feed circulation pump is located between the feed tank and the heat exchanger. The cold medium outlet of the heat exchanger is connected to the inlet of the feed tank via a first branch pipe, and a first control valve is installed on the first branch pipe. The feed circulation pump can transport the low-concentration water glass solution in the feed tank to the heat exchanger, where it enters the heat exchange tubes through the cold medium inlet. Inside the heat exchange tubes, it exchanges heat with the high-temperature medium through the tube walls, thus completing the preheating before the evaporation and concentration process. The preheated low-concentration water glass solution can be transported back to the feed tank through the first branch pipe and by opening the first control valve; this is the preheating circulation path for the low-concentration water glass solution.

[0010] In one embodiment, the reactor further includes a feed inlet, and the cold medium outlet of the heat exchanger is connected to the feed inlet of the reactor via a second branch pipe, on which a second control valve is installed. By using the second branch pipe and opening the second control valve, preheated low-concentration water glass solution can be conveyed into the reactor through the feed inlet, thus feeding the water glass solution into the reactor during the evaporation and concentration process.

[0011] In one embodiment, the reactor includes a vessel body and a steam jacket layer that surrounds and encloses the outside of the vessel body.

[0012] In one embodiment, the heat exchanger includes a tube side for conveying a low-concentration water glass solution and a shell side for conveying water vapor; the tube side includes multiple parallel heat exchange tubes, and the shell side includes an outer shell; the multiple heat exchange tubes are installed inside the outer shell of the heat exchanger. The heat exchanger can transfer heat from the water vapor generated by heating and concentrating the water glass solution in the reactor to the low-concentration water glass solution, preheating the low-concentration water glass solution before it enters the next process step.

[0013] In one embodiment, the system further includes a second gas-liquid separator and a condensate receiving tank. The second gas-liquid separator is disposed between the heat exchanger and the water circulation vacuum unit. The heat medium outlet of the heat exchanger is connected to the gas-liquid inlet of the second gas-liquid separator, the exhaust port of the second gas-liquid separator is connected to the gas-liquid inlet of the first gas-liquid separator, and the drain outlet of the second gas-liquid separator is connected to the inlet of the condensate receiving tank. Through the second gas-liquid separator and the condensate receiving tank, condensate after heat exchange with water vapor in the heat exchanger can be collected and applied to other production processes, achieving condensate recycling.

[0014] To better understand and implement this invention, the following detailed description is provided in conjunction with the accompanying drawings. Attached Figure Description

[0015] The accompanying drawings, which are included to provide a further understanding of the invention and form part of this invention, illustrate exemplary embodiments of the invention and are used to explain the invention, but do not constitute an undue limitation of the invention. In the drawings:

[0016] Figure 1 This is a schematic diagram of one embodiment of the vacuum device for concentrating by-products in the production of zirconium oxychloride according to this utility model.

[0017] Figure 2 This is a schematic diagram of another embodiment of the vacuum device for concentrating by-products in the production of zirconium oxychloride according to this utility model.

[0018] Figure 3 This is a schematic diagram of another embodiment of the vacuum device for concentrating by-products in the production of zirconium oxychloride according to this utility model.

[0019] The following components are marked in the diagram: reactor 1, heat exchanger 2, water circulation vacuum system 300, water circulation vacuum pump 301, circulating water tank 302, first gas-liquid separator 303, feed tank 4, feed circulation pump 5, first control valve 6, second control valve 7, second gas-liquid separator 8, and condensate receiving tank 9. Detailed Implementation

[0020] To make the objectives, technical solutions, and advantages of this utility model clearer, the technical solutions of this utility model will be clearly and completely described below in conjunction with specific embodiments and corresponding drawings. Obviously, the described embodiments are only a part of the embodiments of this invention, and not all of them. Based on the embodiments of this utility model, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of this utility model.

[0021] In the description of this utility model, it should be noted that the terms "vertical direction," "up," "down," and "horizontal," etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are used only for the convenience of describing this utility model and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this utility model. In addition, "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance.

[0022] In the description of this utility model, it should also be noted that, unless otherwise explicitly specified and limited, the terms "set," "install," "connect," and "link" should be interpreted broadly. For example, they can refer to thermally conductive connections, detachable connections, or integral connections; they can refer to mechanical connections or electrical connections; they can refer to direct connections or connections through an intermediate medium; and they can refer to the internal communication between two components. Those skilled in the art can understand the specific meaning of the above terms in this utility model according to the specific circumstances.

[0023] like Figure 1 As shown, this embodiment provides a vacuum device for concentrating by-products in zirconium oxychloride production, including a reactor 1, a heat exchanger 2 connected to the exhaust port of the reactor, and a water circulation vacuum system 300 connected to the heat medium outlet of the heat exchanger 2. This water circulation vacuum system 300 continuously draws air from the reactor 1 and water vapor generated during the evaporation and concentration of the water glass solution, thereby creating the required negative pressure environment inside the reactor and achieving the effect of lowering the boiling point of the water glass solution.

[0024] Reactor 1 is used to heat a low-concentration water glass solution, causing it to evaporate and concentrate. In this embodiment, reactor 1 is a jacketed reactor, including a vessel body, a jacket layer, and a pressure gauge. The jacket layer wraps around the outside of the vessel body to form a cavity. The pressure gauge is located on the top of the reactor to monitor the gas pressure inside the vessel in real time. In this embodiment, steam is introduced into the cavity formed by the jacket layer wrapping the vessel body. The steam exchanges heat with the low-concentration water glass solution inside the vessel through the vessel wall, achieving the effect of evaporating and concentrating the low-concentration water glass solution. Of course, in other alternative embodiments, heat transfer oil can also be introduced into the cavity. If heat transfer oil is introduced, the vacuum device for concentrating by-products in the zirconium oxychloride production can save the heat energy required to heat the heat transfer oil. In addition, reactor 1 can also be a coil-type heating reactor, with a spiral coil installed inside the reactor. Steam can be introduced into the coil to achieve heating and concentration of the low-concentration water glass solution inside the vessel.

[0025] Heat exchanger 2 is used to exchange heat between the high-temperature water vapor generated during the evaporation and concentration of the water glass solution in reactor 1 and the low-concentration water glass solution from feed tank 7. During the heat exchange, the low-concentration water glass solution is heated, and part of the high-temperature water vapor condenses into water. In this embodiment, heat exchanger 2 is a shell-and-tube heat exchanger, including a shell side and a tube side. The shell side includes an outer shell, and the tube side includes multiple heat exchange tubes installed in parallel inside the outer shell. The multiple heat exchange tubes are installed inside the outer shell of the heat exchanger. The high-temperature water vapor generated during the evaporation and concentration of the low-concentration water glass solution in reactor 1 flows in the shell side, and the low-concentration water glass solution from feed tank 4 flows in the tube side. The high-temperature water vapor and the low-temperature low-concentration water glass solution exchange heat through heat conduction through the tube walls. Of course, in other alternative embodiments, heat exchanger 2 can also be other types of heat exchangers, as long as they can achieve the function of heat exchange between the low-concentration water glass solution and the high-temperature water vapor.

[0026] The water circulation vacuum system 300 is used to create a vacuum environment inside the reactor 1. The water circulation vacuum system 300 continuously draws in air and high-temperature water vapor generated during the evaporation and concentration of the water glass solution inside the reactor 1, thereby creating the required negative pressure environment inside the reactor and achieving the effect of lowering the boiling point of the water glass solution.

[0027] Please see Figure 3 In another embodiment, the water circulation vacuum system 300 includes a water circulation vacuum pump 301, a circulating water tank 302 connected to the water circulation vacuum pump 301 via a pipeline, and a first gas-liquid separator 303 connected to the suction port of the water circulation vacuum pump 301. In this case, the gas-liquid inlet of the first gas-liquid separator 303 is connected to the exhaust port of the second gas-liquid separator 8.

[0028] The suction port of the water circulation jet vacuum pump 301 is connected to the exhaust port of the first gas-liquid separator 303. The water circulation jet vacuum pump 301 is used to generate a vacuum environment to lower the boiling point of the water glass solution in the reactor 1 and improve the evaporation efficiency. It is also used to draw non-condensable gases from the first gas-liquid separator 303 to maintain the vacuum environment inside the reactor.

[0029] The circulating water tank 302 is connected to the water circulation vacuum pump 301 through a pipeline. The circulating water tank 302 is used to provide the working water source for the water circulation vacuum pump 301 and to receive the liquid phase from the first gas-liquid separator 303. The non-condensable gas pumped by the water circulation vacuum pump 301 is discharged into the circulating water tank 302 and discharged from the circulating water tank 302 into the atmospheric environment.

[0030] The gas-liquid inlet of the first gas-liquid separator 303 is connected to the exhaust port of the second gas-liquid separator 8. The first gas-liquid separator 303 is used to further separate the gas phase from the second gas-liquid separator 8 into two phases. The separated gas phase is a non-condensable gas. At this time, the gas phase will be drawn from the exhaust port of the first gas-liquid separator 303 through the suction port of the water circulation vacuum pump 301 and the liquid phase will be discharged from the drain port of the first gas-liquid separator 303 to the circulating water tank 302.

[0031] exist Figure 1 , Figure 2 and Figure 3 In the three embodiments shown, the outlet of the liquid tank 4 is connected to the cold medium inlet of the heat exchanger 2, and the liquid circulation pump 5 is set between the outlet of the liquid tank 4 and the cold medium inlet of the heat exchanger 2; the cold medium outlet of the heat exchanger 2 is connected to the inlet of the liquid tank 4 through a first branch pipe, and a first control valve 6 is set on the first branch pipe.

[0032] The feed tank 4 is used to store low-concentration water glass solution, and the feed circulation pump 5 is used to transport the low-concentration water glass solution in the feed tank 4 to the heat exchange tube of the heat exchanger 2. The low-concentration water glass solution exchanges heat with high-temperature water vapor in the heat exchanger 2, effectively utilizing the residual heat in the high-temperature water vapor to achieve the effect of preheating the low-concentration water glass solution, thus preparing it for the next evaporation and concentration process.

[0033] The first branch pipe is used to connect the inlet of the liquid tank 4 and the cold medium outlet of the heat exchanger 2. The first control valve 6 is installed on the first branch pipe. When the first control valve 6 is opened, the low-concentration water glass solution after heat exchange in the heat exchanger 2 can flow back to the liquid tank, realizing the circulation of liquid preheating.

[0034] The reactor 1 also includes a feed inlet. The cold medium outlet of the heat exchanger 2 is connected to the feed inlet of the reactor 1 through a second branch pipe. A second control valve 7 is installed on the second branch pipe.

[0035] The second branch pipe is used to connect the feed inlet of reactor 1 and the cold medium outlet of heat exchanger 2. The second control valve 7 is installed on the second branch pipe. When the second control valve 7 is opened, the low-concentration water glass solution after heat exchange in heat exchanger 2 can flow to reactor 1, thereby realizing the feeding of reactor 1.

[0036] Please see Figure 3 In one embodiment, the vacuum device for concentrating by-products in zirconium oxychloride production further includes a second gas-liquid separator 8 and a condensate receiving tank 9. The second gas-liquid separator 8 is disposed between the heat exchanger 2 and the water circulation vacuum unit 300. The heat medium outlet of the heat exchanger 2 is connected to the gas-liquid inlet of the second gas-liquid separator 8, the exhaust port of the second gas-liquid separator 8 is connected to the gas-liquid inlet of the first gas-liquid separator 303, and the drain port of the second gas-liquid separator 8 is connected to the water inlet of the condensate receiving tank 9.

[0037] The second gas-liquid separator 8 is used to perform the first gas-liquid separation on the water vapor after heat exchange in the heat exchanger 2, and the condensate receiving tank 9 is used to recycle the condensate separated in the second gas-liquid separator 8. The gas-liquid inlet of the second gas-liquid separator 8 is connected to the heat medium outlet of the heat exchanger 2 through a pipe, and the water inlet of the condensate receiving tank 9 is connected to the drain outlet of the second gas-liquid separator 8. After the second gas-liquid separator 8 separates the condensate and uncondensed water vapor formed after heat exchange into a gas-liquid two-phase system, the gas phase is discharged through the exhaust port located at the top of the second gas-liquid separator 8 to the first gas-liquid separator 303 in the water circulation vacuum system 300, and the liquid phase is discharged through the drain outlet located at the bottom of the second gas-liquid separator 8 and recycled back to the condensate receiving tank 8 through the water inlet of the condensate receiving tank 8.

[0038] Of course, in other alternative embodiments, since the function of the second gas-liquid separator 8 and the condensate receiving tank 9 is to perform preliminary gas-liquid two-phase separation of condensate and uncondensed water vapor formed after heat exchange of high-temperature water vapor through the heat exchanger and to recycle the condensate, and the first gas-liquid separator 303 can also achieve the function of gas-liquid separation, the second gas-liquid separator 8 and the condensate receiving tank 9 may not be included in the by-product concentration vacuum device in this zirconium oxychloride production. In this case, the heat medium outlet of the heat exchanger 2 is connected to the gas-liquid inlet of the first gas-liquid separator 303. The gas-liquid two-phase separation of condensate and uncondensed water vapor discharged from the heat medium outlet of the heat exchanger 2 is completed in the first gas-liquid separator 303. The gas phase is drawn by the water circulation vacuum pump 301, and the liquid phase is discharged into the circulating water tank 302 through the drain outlet of the first gas-liquid separator 303. For the specific structure, please refer to [link to specific structure]. Figure 2 .

[0039] Utilize Figure 3 The process for concentrating water glass solution using the apparatus shown is as follows:

[0040] In the initial state of the apparatus, reactor 1 and feed tank 7 contain sufficient low-concentration water glass solution, and circulating water tank 302 contains sufficient clean water. At this time, the first control valve 6 is open, the second control valve 7 is closed, and the feed circulation pump 5 is in the off state. The water circulation vacuum pump 301 draws clean water from the circulating water tank 302 to form a water ring, and at the same time begins to continuously draw air from reactor 1, causing the pressure inside the reactor to continuously decrease, thereby establishing the required negative pressure environment. The pressure gauge at the top of the jacketed reactor 1 is used to determine whether the required negative pressure environment of 0.02 to 0.06 MPa has been formed.

[0041] After the required negative pressure environment is formed, steam is introduced into the jacket layer of reactor 1 to heat the reactor body. The low-concentration water glass solution inside the reactor is heated. Under the negative pressure environment, the boiling point of the low-concentration water glass solution decreases, the heat required for evaporation and concentration is reduced, and the amount of steam consumed is reduced. During the evaporation and concentration process, the low-concentration water glass solution will generate a large amount of high-temperature water vapor. The water vapor contains abundant residual heat. The water vapor enters the shell side of heat exchanger 2 through the exhaust port of reactor 1 and the heat medium inlet of heat exchanger 2.

[0042] When steam is introduced into reactor 1, the feed circulation pump 5 starts operating. The feed circulation pump 5 is used to transport the low-concentration water glass solution in feed tank 4. The low-concentration water glass solution enters the heat exchange tube through the cold medium inlet of heat exchanger 2 and exchanges heat with the high-temperature water vapor in the shell side. The low-concentration water glass solution is heated, achieving the preheating effect before the evaporation and concentration process. This makes full use of the residual heat in the high-temperature water vapor generated by the evaporation and concentration of the water glass solution in reactor 1, and also saves the amount of steam required for the subsequent evaporation and concentration process. Since the first control valve 6 is in the open state and the second control valve 7 is in the closed state at this time, the heated low-concentration water glass solution enters the first branch pipe through the cold medium outlet of heat exchanger 2. The low-concentration water glass solution is recovered to feed tank 4 through the feed inlet, thus completing the preheating circulation path. As long as the water glass solution in reactor 1 is still in the evaporation and concentration process, the preheating circulation of the low-concentration water glass solution will not stop, and the first control valve 6 will always be in the open state.

[0043] In heat exchanger 2, a low-concentration water glass solution in the tube side and high-temperature water vapor in the shell side exchange heat. The low-concentration water glass solution is heated, and the water vapor condenses. Some of the water vapor condenses into water. The condensate and uncondensed water vapor enter the second gas-liquid separator 8 sequentially through the heat medium outlet of heat exchanger 2 and the gas-liquid inlet of the second gas-liquid separator 8. In the second gas-liquid separator 8, the condensate flows out from its drain outlet and is recovered into the condensate receiving tank 9 through the water inlet. The recovered condensate can be reused in subsequent production systems. Some uncondensed water vapor enters the first gas-liquid separator 303 through the exhaust outlet of the second gas-liquid separator 8 and the gas-liquid inlet of the first gas-liquid separator 303. In the first gas-liquid separator 303, the gas and liquid phases are further separated. Non-condensable gases and a very small amount of uncondensed water vapor are drawn in by the water circulation vacuum pump 301 through the exhaust outlet of the first gas-liquid separator 303. The condensate is recovered into the circulating water tank 302 through the drain outlet of the first gas-liquid separator 303.

[0044] The water circulation vacuum pump 301 draws in non-condensable gases and a very small amount of uncondensed water vapor. During operation, it discharges a water vapor mixture containing a large number of air bubbles into the circulating water tank 302. The circulating water tank 302 provides a large space, which causes the water flow rate to drop sharply, the air bubbles to burst, and the non-condensable gases to be separated from the water and discharged into the atmosphere. The separated water settles down and can be recycled.

[0045] After the water glass solution evaporated and concentrated in reactor 1 reaches a certain concentration, the evaporation and concentration process is completed. The concentrated water glass solution is discharged from the outlet of reactor 1 to the next process. At this time, the first control valve 6 is closed and the second control valve 7 is opened. Sufficient low-concentration water glass solution, preheated by heat exchanger 2, enters the reactor from the inlet of reactor 1 through the second branch pipe, completing the feeding of low-concentration water glass solution. After feeding is completed, the second control valve 7 is closed and the first control valve 6 is opened. At this time, the second water glass solution evaporation and concentration process and the preheating circulation of low-concentration water glass solution begin. When the low-concentration water glass solution in the feed tank 4 is insufficient, the feed circulation pump 8 is turned off, and sufficient low-concentration water glass solution is added to the feed tank 4.

[0046] In summary, the water-circulating vacuum system of this invention provides a negative pressure environment for the evaporation and concentration process of the water glass solution in the reactor, lowering the boiling point of the water glass solution and thus reducing the amount of steam required to heat the reactor, achieving steam conservation. Simultaneously, the heat exchanger utilizes the high-temperature steam generated during the evaporation and concentration process to preheat the low-concentration water glass solution, fully utilizing the waste heat in the steam. The preheated low-concentration water glass solution requires less heat for evaporation and concentration, also achieving steam conservation. Therefore, this invention achieves high waste heat utilization, rapid evaporation of the water glass solution, reduced steam requirements, and cost savings by creating a negative pressure environment during the evaporation and concentration process and by implementing a preheating cycle before evaporation and concentration.

[0047] The embodiments described above are merely examples of several implementations of this utility model, and while the descriptions are relatively specific and detailed, they should not be construed as limiting the scope of the utility model patent. It should be noted that those skilled in the art can make various modifications and improvements without departing from the concept of this utility model, and this utility model also intends to include these modifications and variations.

Claims

1. A vacuum device for concentrating by-products in the production of zirconium oxychloride, characterized in that, include: The reactor comprises a reactor, a heat exchanger, and a water-circulating vacuum unit. The exhaust port of the reactor is connected to the heat medium inlet of the heat exchanger, and the heat medium outlet of the heat exchanger is connected to the water-circulating vacuum unit.

2. The vacuum device for concentrating by-products in zirconium oxychloride production according to claim 1, characterized in that: The water circulation vacuum unit includes a water circulation vacuum pump, a circulating water tank, and a first gas-liquid separator. The water circulation vacuum pump is connected to the circulating water tank via a pipeline. The suction port of the water circulation vacuum pump is connected to the exhaust port of the first gas-liquid separator. The inlet of the circulating water tank is connected to the outlet of the first gas-liquid separator. The heat medium outlet of the heat exchanger is connected to the gas-liquid inlet of the first gas-liquid separator.

3. The vacuum device for concentrating by-products in zirconium oxychloride production according to claim 1, characterized in that: It also includes a liquid tank and a liquid circulation pump; the heat exchanger also includes a cold medium inlet and a cold medium outlet, the outlet of the liquid tank is connected to the cold medium inlet of the heat exchanger, and the liquid circulation pump is located between the liquid tank and the heat exchanger; the cold medium outlet of the heat exchanger is connected to the inlet of the liquid tank through a first branch pipe, and a first control valve is provided on the first branch pipe.

4. The vacuum device for concentrating by-products in zirconium oxychloride production according to claim 1, characterized in that: The reactor also includes a feed inlet, and the cold medium outlet of the heat exchanger is connected to the feed inlet of the reactor through a second branch pipe, on which a second control valve is provided.

5. A vacuum device for concentrating by-products in zirconium oxychloride production according to claim 1, characterized in that: The reactor includes a vessel body and a steam jacket layer, which surrounds and encloses the outside of the vessel body.

6. The vacuum device for concentrating by-products in zirconium oxychloride production according to claim 1, characterized in that: The heat exchanger includes a tube side for conveying a low-concentration water glass solution and a shell side for conveying water vapor; the tube side includes multiple parallel heat exchange tubes, and the shell side includes an outer shell; the multiple heat exchange tubes are installed inside the outer shell of the heat exchanger.

7. A vacuum device for concentrating by-products in zirconium oxychloride production according to claim 2, characterized in that: It also includes a second gas-liquid separator and a condensate receiving tank. The second gas-liquid separator is disposed between the heat exchanger and the water circulation vacuum unit. The heat medium outlet of the heat exchanger is connected to the gas-liquid inlet of the second gas-liquid separator, the exhaust port of the second gas-liquid separator is connected to the gas-liquid inlet of the first gas-liquid separator, and the drain port of the second gas-liquid separator is connected to the water inlet of the condensate receiving tank.

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