Water for injection production device and water for injection production method

Abstract

This application relates to the field of pharmaceutical technology, specifically to an apparatus and method for producing water for injection, comprising a condenser, a preheater, a multi-effect evaporation unit, and a degassing tank. The tube side of the condenser is used to receive raw water. The tube side of the condenser, the tube side of the preheater, the multi-effect evaporation unit, the shell side of the condenser, and the degassing tank are sequentially connected. The multi-effect evaporation unit includes a first evaporator, and atomizing nozzles and a first exhaust assembly, both installed at the top of the first evaporator for primary deoxygenation. The apparatus for producing water for injection further includes a second exhaust assembly installed in the degassing tank for secondary deoxygenation. The purpose of this application is to address at least one technical problem mentioned in the background art by providing an apparatus and method for producing water for injection.

Description

Technical Field

[0001] This application relates to the field of pharmaceutical technology, and more specifically, to an apparatus and method for producing water for injection. Background Technology

[0002] Water for injection is one of the most critical process waters in biopharmaceutical manufacturing, and its quality directly affects drug safety. While conventional multi-effect distillers and autoclave distillers can effectively remove endotoxins and most impurities, they cannot reduce the dissolved oxygen content in the product water to extremely low levels. For certain oxidation-sensitive biological agents (such as vaccines and antibody-drug conjugates), excessively high dissolved oxygen levels can lead to degradation of active ingredients and the formation of byproducts. Therefore, existing processes often require degassing membrane treatment of the raw water before distillation, or the addition of a vacuum degassing device after distillation. These additional treatment steps not only increase equipment investment and operating energy consumption but also require regular maintenance of consumables such as degassing membranes, significantly increasing production costs. Summary of the Invention

[0003] The purpose of this application is to provide an apparatus and method for producing water for injection, addressing at least one of the technical problems mentioned in the background art.

[0004] To achieve the above objectives, this application adopts the following technical solution: One aspect of this application provides an apparatus for producing water for injection, comprising a condenser, a preheater, a multi-effect evaporator, and a degassing tank. The tube side of the condenser is used to receive raw water, and the tube side of the condenser, the tube side of the preheater, the multi-effect evaporator, the shell side of the condenser, and the degassing tank are sequentially connected. The multi-effect evaporation unit includes a first evaporator, and atomizing nozzles and a first exhaust assembly, both installed on the top of the first evaporator for primary deoxygenation. The water-to-injection production apparatus further includes a second exhaust assembly, which is installed in the degassing tank for secondary deoxygenation.

[0005] Optionally, the water-to-injection production apparatus provided in this application further includes a cooler, and the degassing tank is connected to the shell side of the cooler.

[0006] The beneficial effects of this technical solution are as follows: The water for injection, after undergoing secondary deoxygenation in the degassing tank, directly enters the shell side of the cooler. Heat exchange occurs through cooling water connected to the tube side of the cooler, thereby reducing the temperature of the water for injection. This ensures that the high-temperature water for injection after degassing is cooled before output, meeting the requirements for use or storage of water for injection under normal or low-temperature conditions. Furthermore, the direct connection between the cooler and the degassing tank avoids intermediate buffering, helping to maintain the low dissolved oxygen state of the water for injection after deoxygenation and reducing the possibility of gas re-dissolution due to temperature changes. Simultaneously, the heat exchange design of the cooler's shell and tube sides allows for effective cooling using conventional cooling water, eliminating the need for additional cold source equipment.

[0007] Optionally, the first exhaust assembly includes a one-way valve and a first regulating valve connected in sequence. The inlet of the one-way valve is connected to the exhaust port at the top of the first evaporator, and the outlet of the first regulating valve is connected to the atmosphere.

[0008] The beneficial effects of this technical solution are as follows: the one-way valve can prevent external gas from flowing back into the first evaporator, and the first regulating valve continues to open after being adjusted to the set opening degree to maintain the continuous exhaust state at the top of the first evaporator, thereby ensuring the stable progress of the first-stage deoxygenation process and avoiding heat loss due to excessive exhaust.

[0009] Optionally, the second exhaust assembly includes a pneumatic switching valve and a second regulating valve, wherein the inlet of the pneumatic switching valve is connected to the exhaust port at the top of the degassing tank, and the outlet of the second regulating valve is connected to the atmosphere.

[0010] The beneficial effects of this technical solution are as follows: the pneumatic switch valve can be opened intermittently according to the system operation needs to discharge the non-condensable gas generated by flash evaporation from the degassing tank; the second regulating valve is used to control the exhaust flow rate to maintain the normal pressure state in the degassing tank and reduce unnecessary entrainment of water vapor.

[0011] Optionally, the water-to-injection production apparatus provided in this application further includes an industrial steam regulating component, which includes a controller, a proportional regulating valve, and a temperature transmitter. Industrial steam is introduced into the shell side of the preheater through a steam inlet pipeline. The proportional regulating valve is installed in the steam inlet pipeline. The temperature transmitter is located on the pipeline between the tube-side outlet of the preheater and the tube-side inlet of the first evaporator. The proportional regulating valve and the temperature transmitter are interlocked and controlled by the controller to adjust the opening degree of the proportional regulating valve according to the temperature value detected by the temperature transmitter.

[0012] The beneficial effects of this technical solution are as follows: The input of industrial steam is automatically adjusted according to the actual temperature of the raw water before it enters the first evaporator. When the temperature deviates from the set range, the proportional regulating valve adjusts its opening accordingly, thereby controlling the temperature of the raw water entering the top of the first evaporator within the required range, providing stable temperature conditions for the release of non-condensable gases at the atomizing nozzle. Furthermore, the industrial steam regulating component reduces the frequency of manual adjustment, lowers the interference of temperature fluctuations on the primary deoxygenation effect and evaporation efficiency, and reduces steam consumption to a certain extent by supplying industrial steam on demand.

[0013] Optionally, industrial steam is connected to the top inlet end of the shell side of the first evaporator.

[0014] The beneficial effects of this technical solution are as follows: Industrial steam directly enters the shell side of the first evaporator and heats the raw water in the tube side as a heating medium. The industrial steam condenses and releases heat in the shell side, providing a heat source for the evaporation process in the first evaporator, causing the raw water to vaporize and generate pure steam, which in turn drives the operation of subsequent evaporators. This setting directly connects the external industrial steam with the first stage evaporator of the multi-effect evaporation unit, realizing the centralized input of heat energy, and using the secondary steam generated by the first evaporator as the heat source for subsequent stages, which helps to reduce the overall industrial steam consumption.

[0015] Optionally, the multi-effect evaporation unit further includes a second evaporator, wherein the lowest end outlet of the tube side of the first evaporator is connected to the top inlet of the tube side of the second evaporator, and the middle outlet of the tube side of the first evaporator is connected to the top inlet of the shell side of the second evaporator.

[0016] The beneficial effects of this technical solution are as follows: In this way, the lowest outlet of the tube side of the first evaporator is connected to the top inlet of the tube side of the second evaporator, allowing the unevaporated raw water in the first evaporator to enter the tube side of the second evaporator for continued heating and evaporation; at the same time, the middle outlet of the tube side of the first evaporator is connected to the top inlet of the shell side of the second evaporator, allowing the pure steam generated by the first evaporator to enter the shell side of the second evaporator as a heat source. This enables the injection water production device provided in this application to achieve the cascade utilization of heat within the multi-effect evaporation unit, that is, the secondary steam generated by the first evaporator consuming industrial steam is directly used to heat the raw water in the second evaporator, reducing the total demand for external steam.

[0017] Optionally, the multi-effect evaporation unit includes a plurality of second evaporators connected in sequence. The upstream second evaporator is connected to the first evaporator. In two adjacent second evaporators, the lowest end outlet of the tube side of the upstream second evaporator is connected to the top inlet of the tube side of the downstream second evaporator, the middle outlet of the tube side of the upstream second evaporator is connected to the top inlet of the shell side of the downstream second evaporator, and the downstream second evaporator is connected to the condenser.

[0018] The beneficial effects of this technical solution are as follows: In this way, the upstream second evaporator is connected to the first evaporator, so that the secondary steam generated by the first evaporator serves as the heat source for each stage of the second evaporator, forming a multi-stage heat utilization evaporation chain and reducing dependence on external industrial steam; at the same time, the downstream second evaporator is connected to the condenser, so that the pure steam and condensate generated by the last stage second evaporator enter the condenser and exchange heat with the raw water in the tube side, preheating the raw water while cooling itself, thereby realizing the multiple utilization of heat in the multi-effect evaporation unit, and recovering waste heat at the end through the condenser, which helps to reduce overall energy consumption and improve system thermal efficiency.

[0019] Another aspect of this application provides a method for producing water for injection, implemented using the water for injection production apparatus provided in this application, the method comprising: The raw water is preheated in the tube side of the condenser and then heated in the tube side of the preheater. The heated raw water, which is atomized by the atomizing nozzle, is fed into the first evaporator from the top of the first evaporator to release non-condensable gases in the raw water, and the first exhaust assembly is controlled to discharge the non-condensable gases to achieve primary deoxygenation. The pure steam and condensate from the multi-effect evaporation unit are fed into the shell side of the condenser. The superheated condensate flowing out of the shell side of the condenser is sent to the degassing tank for flash evaporation, and the remaining non-condensable gases are discharged through the second exhaust assembly, thereby achieving secondary deoxygenation.

[0020] Optionally, the water-to-injection production apparatus further includes an industrial steam regulating component, which includes a controller, a proportional regulating valve, and a temperature transmitter. Industrial steam is introduced into the shell side of the preheater through a steam inlet pipe. The proportional regulating valve is installed in the steam inlet pipe. The temperature transmitter is located on the pipe between the tube-side outlet of the preheater and the tube-side inlet of the first evaporator. The proportional regulating valve and the temperature transmitter are interlocked through the controller. The method further includes: The temperature transmitter detects the actual temperature of the raw water at the tube outlet of the preheater and transmits the temperature signal to the controller. The controller compares the actual temperature with the preset temperature and outputs a control signal to the proportional regulating valve based on the comparison result. Then, the controller adjusts the opening of the proportional regulating valve according to the control signal to adjust the industrial steam flow rate entering the shell side of the preheater.

[0021] The beneficial effects of this technical solution are as follows: In this way, the water for injection production method provided in this application forms a closed-loop control mode, which maintains the temperature of the raw water entering the top of the first evaporator within the required range, providing relatively stable temperature conditions for the release of non-condensable gases at the atomizing nozzle; at the same time, the proportional regulating valve automatically adjusts the industrial steam input according to the actual temperature change, reducing the frequency of manual intervention and reducing the consumption of industrial steam, which to a certain extent helps to reduce operating energy consumption.

[0022] The technical solution provided in this application can achieve at least one of the following beneficial effects: The water-to-injection production apparatus and method provided in this application reduce the dissolved oxygen content in water-to-injection through a combination of two-stage deoxygenation structures without adding an external degassing membrane or vacuum degassing device. Since no additional degassing membrane or other consumables are required, the investment in related equipment, operating energy consumption, and maintenance costs are reduced. At the same time, the direct connection between the condenser shell side and the degassing tank utilizes the waste heat of the water-to-injection production apparatus itself for flash deoxygenation, which helps to reduce overall energy consumption.

[0023] The additional technical features and advantages of this application will become more apparent from the following description or from practical application. Attached Figure Description

[0024] To more clearly illustrate the technical solutions of the specific embodiments of this application, the accompanying drawings used in the description of the specific embodiments will be briefly introduced below. Obviously, the accompanying drawings described below are some embodiments of this application. For those skilled in the art, other drawings can be obtained from these drawings without creative effort.

[0025] Figure 1 A schematic diagram of one embodiment of the water-for-injection production apparatus provided in this application; Figure 2 This is a schematic flowchart of one embodiment of the water for injection production method provided in this application.

[0026] Figure label: 01. Condenser; 02. Second evaporator; 03. Preheater; 04. Temperature transmitter; 05. First regulating valve; 06. Check valve; 07. Proportional regulating valve; 08. Atomizing nozzle; 9. First evaporator; 10. Steam trap; 11. Cooler; 12. Degassing tank; 13. Pneumatic switching valve; 14. Second regulating valve. Detailed Implementation

[0027] The technical solutions of this application will now be clearly and completely described with reference to the accompanying drawings. Obviously, the described embodiments are only some, not all, of the embodiments of this application. Based on the embodiments of this application, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of this application.

[0028] In the description of this application, it should be noted that the terms "center," "upper," "lower," "left," "right," "vertical," "horizontal," "inner," and "outer," 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 application 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 application. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and should not be construed as indicating or implying relative importance.

[0029] In the description of this application, it should be noted that, unless otherwise expressly specified and limited, the terms "installation," "connection," and "linking" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal connection between two components. Those skilled in the art can understand the specific meaning of the above terms in this application based on the specific circumstances.

[0030] like Figure 1 As shown, one aspect of this application provides a water-to-injection production apparatus, including a condenser 01, a preheater 03, a multi-effect evaporation unit, and a degassing tank 12. The tube side of the condenser 01 is used to receive raw water. The tube side of the condenser 01, the tube side of the preheater 03, the multi-effect evaporation unit, the shell side of the condenser 01, and the degassing tank 12 are connected in sequence. The multi-effect evaporation unit includes a first evaporator 09, and atomizing nozzles 08 and a first exhaust assembly, both installed on the top of the first evaporator 09 for primary deoxygenation. The water for injection production apparatus also includes a second exhaust assembly, which is installed in the degassing tank 12 for secondary deoxygenation.

[0031] The water-to-injection production apparatus provided in this application, compared with conventional multi-effect distillation machines or hot-press distillation machines, is equipped with a first exhaust assembly installed at the top of the first evaporator 09 and a second exhaust assembly installed in the deaeration tank 12, in addition to the condenser 01, preheater 03 and multi-effect evaporation unit. The raw water flows sequentially through the tube side of the condenser 01 and the tube side of the preheater 03 before entering the multi-effect evaporation unit. At the top of the first evaporator 09, it is atomized by the atomizing nozzle 08. Dissolved oxygen is discharged with the non-condensable gas through the first exhaust assembly, achieving primary deoxygenation. Subsequently, the steam and condensate generated by the multi-effect evaporation unit enter the shell side of the condenser 01 and then flow into the deaeration tank 12. The residual dissolved oxygen in the deaeration tank 12 is discharged through the second exhaust assembly during the flash evaporation process, achieving secondary deoxygenation.

[0032] The water-to-injection production apparatus provided in this application reduces the dissolved oxygen content in water-to-injection through a combination of two-stage deoxygenation structures without adding an external degassing membrane or vacuum degassing device. Since no additional degassing membrane or other consumables are required, the investment in related equipment, operating energy consumption, and maintenance costs are reduced. At the same time, the direct connection between the shell side of the condenser 01 and the degassing tank 12 utilizes the waste heat of the water-to-injection production apparatus itself for flash deoxygenation, which helps to reduce overall energy consumption.

[0033] Optionally, the water for injection production apparatus provided in this application further includes a cooler 11, and the degassing tank 12 is connected to the shell side of the cooler 11.

[0034] In this way, the water for injection, after undergoing secondary deoxygenation in the degassing tank 12, directly enters the shell side of the cooler 11. Cooling water is then connected to the tube side of the cooler 11 for heat exchange, thereby reducing the temperature of the water for injection. This ensures that the high-temperature water for injection after degassing is cooled before output, meeting the requirements for use or storage of water for injection under normal or low-temperature conditions. Furthermore, the direct connection between the cooler 11 and the degassing tank 12 avoids intermediate buffering, helping to maintain the low dissolved oxygen state of the water for injection after deoxygenation and reducing the possibility of gas re-dissolution due to temperature changes. Simultaneously, the heat exchange design of the shell and tube sides of the cooler 11 allows for effective cooling using conventional cooling water, eliminating the need for additional cold source equipment. Preferably, the diameter of the lower outlet pipe and subsequent pipe of the degassing tank 12 is larger than the diameter of the middle inlet pipe of the degassing tank 12, so that the liquid level in the degassing tank 12 is always lower than the position of the middle inlet. The degassing tank 12 discharges water for injection by gravity flow. This structure avoids the retention of residual liquid in the tank and achieves continuous and stable discharge without additional liquid level control.

[0035] Optionally, the first exhaust assembly includes a one-way valve 06 and a first regulating valve 05 connected in sequence. The inlet of the one-way valve 06 is connected to the exhaust port at the top of the first evaporator 09, and the outlet of the first regulating valve 05 is connected to the atmosphere. The one-way valve 06 prevents external gas from flowing back into the first evaporator 09. The first regulating valve 05 remains open after being adjusted to a set opening degree to maintain continuous exhaust at the top of the first evaporator 09, thereby ensuring the stable operation of the first-stage deoxygenation process and avoiding heat loss due to excessive exhaust. Specifically, during equipment commissioning, after the operator adjusts the opening degree of the first regulating valve 05 to the position where the dissolved oxygen content of the water for injection reaches the minimum value, the first regulating valve 05 remains open at this opening degree without intermittent or interlocking adjustments.

[0036] Optionally, the second exhaust assembly includes a pneumatic switching valve 13 and a second regulating valve 14. The inlet of the pneumatic switching valve 13 is connected to the exhaust port at the top of the degassing tank 12, and the outlet of the second regulating valve 14 is connected to the atmosphere. The pneumatic switching valve 13 can be opened intermittently as needed for system operation to discharge the non-condensable gases (containing oxygen) generated by flash evaporation from the degassing tank 12. The second regulating valve 14 is used to control the exhaust flow rate to maintain the atmospheric pressure state inside the degassing tank 12 while reducing unnecessary water vapor entrainment.

[0037] Optionally, the water-to-injection production apparatus provided in this application further includes an industrial steam regulating component, which includes a controller, a proportional regulating valve 07, and a temperature transmitter 04. Industrial steam is introduced into the shell side of the preheater 03 through a steam inlet pipe. The proportional regulating valve 07 is installed in the steam inlet pipe. The temperature transmitter 04 is located in the pipe between the tube-side outlet of the preheater 03 and the tube-side inlet of the first evaporator 09. The proportional regulating valve 07 and the temperature transmitter 04 are interlocked and controlled by the controller to adjust the opening degree of the proportional regulating valve 07 according to the temperature value detected by the temperature transmitter 04. In this way, the input of saturated industrial steam is automatically adjusted according to the actual temperature of the raw water before it enters the first evaporator 09. When the temperature deviates from the set range, the proportional regulating valve 07 adjusts its opening accordingly, thereby controlling the temperature of the raw water entering the top of the first evaporator 09 within the required range, providing stable temperature conditions for the release of non-condensable gases at the atomizing nozzle 08. Moreover, the industrial steam regulating component reduces the frequency of manual adjustment and reduces the interference of temperature fluctuations on the first-stage deoxygenation effect and evaporation efficiency. By supplying industrial steam on demand, steam consumption can be reduced to a certain extent. Preferably, the pressure range of the industrial steam is 3 bar to 5 bar (gauge pressure); the set value of the raw water temperature at the tube outlet of the preheater 03 is lower than the evaporation temperature of the first evaporator 09, the evaporation temperature range of the first evaporator 09 is 135°C to 148°C, and the evaporation temperature of the first evaporator 09 is 8°C to 10°C lower than the temperature of the industrial steam entering its shell side; in the multi-effect evaporation unit, starting from the first evaporator 09, the evaporation temperature of each subsequent evaporator is 6°C to 10°C lower than the previous stage. Industrial steam flows through the shell side of preheater 03 to form industrial steam condensate, which is then discharged through steam trap 10.

[0038] Optionally, the top inlet of the shell side of the first evaporator 09 is connected to industrial steam. This allows industrial steam to directly enter the shell side of the first evaporator 09, serving as a heating medium to heat the raw water in the tube side. The industrial steam condenses and releases heat in the shell side, providing a heat source for the evaporation process in the first evaporator 09, causing the raw water to vaporize and generate pure steam, which in turn drives the operation of subsequent evaporators. This configuration directly connects external industrial steam to the first stage evaporator of the multi-effect evaporation unit, achieving centralized input of heat energy, and utilizing the secondary steam generated by the first evaporator 09 as a heat source for subsequent stages, which helps to reduce the overall industrial steam consumption.

[0039] Optionally, the multi-effect evaporation unit further includes a second evaporator 02. The lowest outlet of the tube side of the first evaporator 09 is connected to the top inlet of the tube side of the second evaporator 02, and the middle outlet of the tube side of the first evaporator 09 is connected to the top inlet of the shell side of the second evaporator 02. In this way, the connection between the lowest outlet of the tube side of the first evaporator 09 and the top inlet of the tube side of the second evaporator 02 allows unevaporated raw water in the first evaporator 09 to enter the tube side of the second evaporator 02 for continued heating and evaporation. Simultaneously, the connection between the middle outlet of the tube side of the first evaporator 09 and the top inlet of the shell side of the second evaporator 02 allows pure steam generated by the first evaporator 09 to enter the shell side of the second evaporator 02 as a heat source. This enables the injection water production apparatus provided in this application to achieve cascaded utilization of heat within the multi-effect evaporation unit, i.e., the secondary steam generated by the first evaporator 09 consuming industrial steam is directly used to heat the raw water in the second evaporator 02, reducing the total external steam demand.

[0040] Optionally, the multi-effect evaporation unit includes a plurality of second evaporators 02 connected in sequence. The uppermost second evaporator 02 is connected to the first evaporator 09. Among two adjacent second evaporators 02, the lowest end outlet of the tube side of the uppermost second evaporator 02 is connected to the top inlet of the tube side of the lowermost second evaporator 02, and the middle outlet of the tube side of the uppermost second evaporator 02 is connected to the top inlet of the shell side of the lowermost second evaporator 02. The lowermost second evaporator 02 is connected to the condenser 01. In this way, the upstream second evaporator 02 is connected to the first evaporator 09, so that the secondary steam generated by the first evaporator 09 serves as the heat source for each stage of the second evaporator 02, forming a multi-stage heat utilization evaporation chain and reducing dependence on external industrial steam. At the same time, the downstream second evaporator 02 is connected to the condenser 01, so that the pure steam and condensate generated by the last stage second evaporator 02 enter the condenser 01 and exchange heat with the raw water in the tube side, preheating the raw water while cooling itself, thereby realizing the multiple utilization of heat in the multi-effect evaporation unit, and recovering waste heat at the end through the condenser 01, which helps to reduce overall energy consumption and improve system thermal efficiency. In this embodiment of the application, the first evaporator 09 can also be called a single-effect evaporator, and each second evaporator 02 can be called a double-effect evaporator, a triple-effect evaporator, or an N-effect evaporator from upstream to downstream, where N is a natural number and the value of N ranges from 4 to 10. Under the condition of fixed industrial steam consumption, increasing the value of N can increase the production of water for injection. The lowest outlet of the tube side of the most downstream second evaporator 02 is connected to the concentrated water discharge pipe.

[0041] like Figure 2As shown, another aspect of this application provides a method for producing water for injection, implemented using the water for injection production apparatus provided in this application, the method comprising: S100: After the raw water is preheated by passing it through the tube side of the condenser 01, it is then sent to the tube side of the preheater 03 for heating. S200: The heated raw water, which is atomized by the atomizing nozzle 08, is sent from the top of the first evaporator 09 into the first evaporator 09 to release the non-condensable gas in the raw water, and the first exhaust assembly is controlled to discharge the non-condensable gas to achieve primary deoxygenation. S300: The pure steam and condensate from the multi-effect evaporation unit are fed into the shell side of the condenser 01; S400: The superheated condensate flowing out of the shell side of the condenser 01 is sent into the degassing tank 12 for flash evaporation in the degassing tank 12, and the remaining non-condensable gas is discharged through the second exhaust assembly, thereby achieving secondary deoxygenation.

[0042] The water-to-injection production method provided in this application is implemented using the water-to-injection production apparatus provided in this application. By combining two-stage deoxygenation structures, the dissolved oxygen content in the water-to-injection is reduced without adding an external degassing membrane or vacuum degassing device. Since no additional degassing membrane or other consumables are required, the investment in related equipment, operating energy consumption, and maintenance costs are reduced. At the same time, the direct connection between the shell side of the condenser 01 and the degassing tank 12 utilizes the waste heat of the water-to-injection production apparatus itself for flash deoxygenation, which helps to reduce overall energy consumption.

[0043] Optionally, the water-to-injection production apparatus further includes an industrial steam regulating component, which includes a controller, a proportional regulating valve 07, and a temperature transmitter 04. Industrial steam is introduced into the shell side of the preheater 03 through a steam inlet pipe. The proportional regulating valve 07 is installed in the steam inlet pipe. The temperature transmitter 04 is located on the pipe between the tube-side outlet of the preheater 03 and the tube-side inlet of the first evaporator 09. The proportional regulating valve 07 and the temperature transmitter 04 are interlocked by the controller. The method further includes: The temperature transmitter 04 detects the actual temperature of the raw water at the tube outlet of the preheater 03 and transmits the temperature signal to the controller. The controller compares the actual temperature with the preset temperature and outputs a control signal to the proportional regulating valve 07 based on the comparison result. Then, the controller adjusts the opening of the proportional regulating valve 07 according to the control signal to adjust the industrial steam flow rate entering the shell side of the preheater 03.

[0044] Thus, the water for injection production method provided in this application forms a closed-loop control mode, which maintains the temperature of the raw water entering the top of the first evaporator 09 within the required range, providing relatively stable temperature conditions for the release of non-condensable gases at the atomizing nozzle 08; at the same time, the proportional regulating valve 07 automatically adjusts the industrial steam input according to the actual temperature change, reducing the frequency of manual intervention and reducing the consumption of industrial steam, which to some extent helps to reduce operating energy consumption.

[0045] To better illustrate the water-for-injection production apparatus and method provided in this application, this application also provides an application example of the water-for-injection production apparatus and method, as follows: In this application example, the water-to-injection production apparatus includes a condenser 01, a preheater 03, a multi-effect evaporation unit, a degassing tank 12, and a cooler 11. The multi-effect evaporation unit includes a first evaporator 09 and three sequentially connected second evaporators 02, referred to as the first-stage second evaporator 02, the second-stage second evaporator 02, and the third-stage second evaporator 02 (i.e., first-effect, second-effect, third-effect, and fourth-effect evaporators). The designed production capacity of this embodiment is 500 L / h of water for injection.

[0046] The feed rate of raw water is 550 L / h, and the industrial steam pressure is 4 bar. The raw water first enters the tube side of the condenser 01, where it is preheated to approximately 102°C by the injection water flowing out of the shell side of the third-stage second evaporator 02 and the pure steam generated by its tube side. It then enters the tube side of the preheater 03, where it is heated to 125°C to 130°C by industrial steam (this temperature must be lower than the evaporation temperature of the first evaporator 09; the specific setting is adjusted based on the industrial steam pressure and the evaporation temperature of the first evaporator 09). The heated raw water enters the top of the first evaporator 09, where it is atomized by the atomizing nozzle 08 installed at the top of the first evaporator 09, releasing non-condensable gases. These gases are then continuously discharged through the first exhaust assembly (including a one-way valve 06 and a first regulating valve 05), completing the first stage of deoxygenation.

[0047] The shell side of the first evaporator 09 is supplied with 4 bar industrial steam, and its evaporation temperature ranges from 135°C to 138°C (8°C to 10°C lower than the industrial steam temperature). Unevaporated raw water in the tube side of the first evaporator 09 enters the tube side of the first-stage second evaporator 02, and the pure steam generated by the first evaporator 09 enters the shell side of the first-stage second evaporator 02, whose evaporation temperature ranges from 125°C to 128°C; and so on, with the second-stage second evaporator 02 having an evaporation temperature range of 115°C to 118°C, and the third-stage second evaporator 02 having an evaporation temperature range of 105°C to 108°C.

[0048] The water for injection collected at the bottom of the shell side of the third-stage second evaporator 02 (i.e., the most downstream second evaporator 02) and the pure steam generated by its tube side enter the shell side of the condenser 01. After heat exchange with the raw water in the tube side, superheated water for injection with a temperature greater than 100°C is obtained. This superheated water for injection enters the degassing tank 12 and flashes under atmospheric pressure. Residual oxygen is intermittently discharged with the flash steam through the second exhaust assembly (including a pneumatic switch valve 13 and a second regulating valve 14) installed at the top of the degassing tank 12, completing the secondary deoxygenation. The "atmospheric pressure" mentioned in this application refers to the pressure in a state of communication with the atmosphere, i.e., an absolute pressure of 101.325 kPa ± 5 kPa (gauge pressure of 0 bar ± 0.05 bar). The water for injection flowing out of the degassing tank 12 enters the shell side of the cooler 11, where it is cooled by the cooling water in the tube side, producing 500 L / h of water for injection. Testing shows that the dissolved oxygen content of the resulting water for injection is below 10 ppb. In this embodiment, the industrial steam consumption is approximately 220 kg / h, and the cooling water consumption is approximately 400 L / h. In this application example, the degassing tank 12 does not have any distributors, packing, or level control devices inside. The diameter of its lower outlet pipe and subsequent pipes is larger than the diameter of its middle inlet pipe. The degassing tank 12 discharges the water for injection by gravity, and the liquid level inside the tank is always lower than the middle inlet position.

[0049] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of this application, and are not intended to limit them. Although this application has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some or all of the technical features therein. Such modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of this application.

Claims

1. A water-for-injection production apparatus, characterized in that, The system includes a condenser, a preheater, a multi-effect evaporator, and a degassing tank. The tube side of the condenser is used to receive raw water. The tube side of the condenser, the tube side of the preheater, the multi-effect evaporator, the shell side of the condenser, and the degassing tank are connected in sequence. The multi-effect evaporation unit includes a first evaporator, and atomizing nozzles and a first exhaust assembly, both installed on the top of the first evaporator for primary deoxygenation. The water-to-injection production apparatus further includes a second exhaust assembly, which is installed in the degassing tank for secondary deoxygenation.

2. The water-for-injection production apparatus according to claim 1, characterized in that, It also includes a cooler, with the degassing tank connected to the shell side of the cooler.

3. The water-for-injection production apparatus according to claim 1, characterized in that, The first exhaust assembly includes a one-way valve and a first regulating valve connected in sequence. The inlet of the one-way valve is connected to the exhaust port at the top of the first evaporator, and the outlet of the first regulating valve is connected to the atmosphere.

4. The water-for-injection production apparatus according to claim 1, characterized in that, The second exhaust assembly includes a pneumatic switching valve and a second regulating valve. The inlet of the pneumatic switching valve is connected to the exhaust port at the top of the degassing tank, and the outlet of the second regulating valve is connected to the atmosphere.

5. The water-for-injection production apparatus according to claim 1, characterized in that, It also includes an industrial steam regulating assembly, which includes a controller, a proportional regulating valve, and a temperature transmitter. Industrial steam is introduced into the shell side of the preheater through a steam inlet pipe. The proportional regulating valve is installed in the steam inlet pipe. The temperature transmitter is located on the pipe between the tube-side outlet of the preheater and the tube-side inlet of the first evaporator. The proportional regulating valve and the temperature transmitter are interlocked and controlled by the controller to adjust the opening degree of the proportional regulating valve according to the temperature value detected by the temperature transmitter.

6. The water-for-injection production apparatus according to any one of claims 1 to 5, characterized in that, The top inlet end of the shell side of the first evaporator is connected to industrial steam.

7. The water-for-injection production apparatus according to claim 6, characterized in that, The multi-effect evaporation unit further includes a second evaporator, wherein the lowest end outlet of the tube side of the first evaporator is connected to the top inlet of the tube side of the second evaporator, and the middle outlet of the tube side of the first evaporator is connected to the top inlet of the shell side of the second evaporator.

8. The water-for-injection production apparatus according to claim 7, characterized in that, The multi-effect evaporation unit includes multiple second evaporators connected in sequence. The upstream second evaporator is connected to the first evaporator. Among two adjacent second evaporators, the lowest end outlet of the tube side of the upstream second evaporator is connected to the top inlet of the tube side of the downstream second evaporator, and the middle outlet of the tube side of the upstream second evaporator is connected to the top inlet of the shell side of the downstream second evaporator. The downstream second evaporator is connected to the condenser.

9. A method for producing water for injection, characterized in that, The method is implemented using the water-for-injection production apparatus as described in any one of claims 1 to 8, and includes: The raw water is preheated in the tube side of the condenser and then heated in the tube side of the preheater. The heated raw water, which is atomized by the atomizing nozzle, is fed into the first evaporator from the top of the first evaporator to release non-condensable gases in the raw water, and the first exhaust assembly is controlled to discharge the non-condensable gases to achieve primary deoxygenation. The pure steam and condensate from the multi-effect evaporation unit are fed into the shell side of the condenser. The superheated condensate flowing out of the shell side of the condenser is sent into the degassing tank for flash evaporation, and the remaining non-condensable gases are discharged through the second exhaust assembly, thereby achieving secondary deoxygenation.

10. The method for producing water for injection according to claim 9, characterized in that, The water-to-injection production apparatus further includes an industrial steam conditioning component, which includes a controller, a proportional control valve, and a temperature transmitter. Industrial steam is introduced into the shell side of the preheater through a steam inlet pipeline. The proportional control valve is installed in the steam inlet pipeline. The temperature transmitter is located on the pipeline between the tube-side outlet of the preheater and the tube-side inlet of the first evaporator. The proportional control valve and the temperature transmitter are interlocked by the controller. The method further includes: The temperature transmitter detects the actual temperature of the raw water at the tube outlet of the preheater and transmits the temperature signal to the controller. The controller compares the actual temperature with the preset temperature and outputs a control signal to the proportional regulating valve based on the comparison result. Then, the controller adjusts the opening of the proportional regulating valve according to the control signal to adjust the industrial steam flow rate entering the shell side of the preheater.

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