Extraction saponification cooling device and extraction saponification cooling method

Abstract

The application provides an extraction saponification cooling device and an extraction saponification cooling method. The extraction saponification cooling device comprises a saponification reaction tank, a clarification tank, a cooling tower and a cooling water transfer pump. The saponification reaction tank is used for saponification reaction of raw materials comprising empty-load organic matter, alkaline substances and water to obtain a saponification reaction system. The clarification tank is used for clarification separation of the saponification reaction system to obtain saponification organic matter and clarified saponification water. The cooling tower is used for cooling treatment of the clarified saponification water to obtain cooled saponification water. The cooling water transfer pump is used for returning the cooled saponification water to the saponification reaction tank. Thanks to the cooling tower arranged separately to cool and lower the temperature of the clarified saponification water, the application can avoid mutual interference of different cooling systems, reduce the probability of organic pollution of a cooling circulating water large system caused by leakage of a heat exchanger, and is convenient for operation and management and accurate in temperature control.

Description

Technical Field

[0001] This invention relates to the field of extraction saponification, and more specifically, to an extraction saponification cooling device and a extraction saponification cooling method. Background Technology

[0002] In hydrometallurgy, extraction technology is an important method for enrichment and purification. With declining ore grades and increasing complexity of minerals, extraction is becoming increasingly used in metal extraction. Depending on the characteristics of the extractant, metal extraction processes are divided into saponification extraction and non-saponification extraction. Typically, to minimize equipment investment and avoid introducing impurities into the extraction system due to corrosion, PVC is chosen as the material for extraction equipment. However, because saponification is an acid-base neutralization reaction, it releases a large amount of heat. When the temperature exceeds 55°C, PVC softens, affecting the structural strength and normal operation of the extraction equipment.

[0003] To address the issues of deformation and reduced structural strength of plastic extraction equipment caused by elevated temperatures during saponification, the most common treatment methods in China currently include:

[0004] 1. Built-in Coil Method: This method involves installing coils inside the mixing and clarification chambers of the extraction equipment, using circulating cooling water to cool the saponified organic matter. Because the contact area of ​​the coils is limited and the heat exchange process cannot be completed instantaneously, the saponification reaction tank generally requires CPVC material with better high-temperature resistance. However, CPVC material is more expensive than PVC, and the coils are relatively heavy. The placement of the coil support legs needs careful design to prevent the CPVC sheet at the support legs from cracking, thus increasing the complexity of the equipment design and costs.

[0005] 2. External Heat Exchanger Method: This method involves pumping the saponified organic matter to a heat exchanger, where it is indirectly cooled using circulating cooling water. The saponified organic matter is then sent to the next extraction stage. This method uses only a stirring tank, without a clarification tank, resulting in a smaller footprint, a larger heat exchange area, and more convenient and precise temperature control of the saponified organic matter. However, this method requires a pump to transfer a large amount of organic matter, leading to high energy consumption.

[0006] In summary, both the built-in coil method and the external heat exchanger method are indirect heat exchange methods. These not only have low heat exchange efficiency and high energy consumption, but also increase the investment and cost of heat exchange equipment. Furthermore, the oil-water mixture in the saponification reaction tank, where indirect heat exchange occurs, has a high temperature, leading to significant organic volatilization. If the cooling circulating water for the saponification process shares a cooling system with other systems, organic contamination of the circulating water system may occur due to heat exchanger leaks. Summary of the Invention

[0007] The main objective of this invention is to provide an extraction saponification cooling device and extraction saponification cooling method to solve the problems of high price of saponification extraction equipment, serious organic volatilization, low heat exchange efficiency of indirect heat exchange method and possible pollution of cooling circulating water system in the prior art.

[0008] To achieve the above objectives, according to one aspect of the present invention, an extraction saponification cooling device is provided. This device includes a saponification reaction tank, a clarification tank, a cooling tower, and a cooling water transfer pump. The inlet of the saponification reaction tank is connected to an unloaded organic source, an alkaline source, and a water source, respectively, for saponifying a raw material including unloaded organic matter, an alkaline substance, and water to obtain a saponification reaction system. The inlet of the clarification tank is connected to the outlet of the saponification reaction tank, for clarifying and separating the saponification reaction system to obtain saponified organic matter and clarified saponified water. The inlet of the cooling tower is connected to the outlet of the clarification tank, for cooling the clarified saponified water to obtain cooled saponified water. The inlet of the cooling water transfer pump is connected to the outlet of the cooling tower, for returning the cooled saponified water to the saponification reaction tank.

[0009] Furthermore, the above-mentioned extraction saponification cooling device also includes a saponification water cooling pump, which is installed on the pipeline connecting the clarification tank and the cooling tower, and is used to transport the clarified saponified water into the cooling tower.

[0010] Furthermore, the above-mentioned extraction saponification cooling device also includes a saponification water discharge pump. The inlet of the saponification water discharge pump is connected to the outlet of the clarification tank and is used to discharge a portion of the saponification water from the extraction saponification cooling device. The portion of the total saponification water content in the extraction saponification cooling device that exceeds the initial amount of water added to the saponification reaction tank is the discharged saponification water.

[0011] According to another aspect of the present invention, an extraction saponification cooling method is provided, the extraction saponification cooling method comprising step S1, subjecting a raw material including an empty organic compound, an alkaline substance and water to a saponification reaction system; step S2, clarifying and separating the saponification reaction system to obtain saponified organic compound and clarified saponified water; step S3, cooling the clarified saponified water to obtain cooled saponified water; and step S4, returning the cooled saponified water to step S1 as water; and repeating steps S1 to S4.

[0012] Furthermore, in step S3 above, the temperature of the saponified water after cooling is 20–32°C.

[0013] Furthermore, the temperature range for converting the above-mentioned unloaded organic matter into saponified organic matter is -8 to 24°C; preferably, the temperature of the saponified organic matter is ≤55°C.

[0014] Furthermore, the volumetric flow ratio of the water to the empty organic matter is 0.3 to 2:1, preferably 0.5 to 2:1, more preferably 1 to 2:1, the water temperature is preferably 20 to 32°C, and the empty organic matter temperature is preferably 30 to 50°C.

[0015] Furthermore, the extraction equivalent of the saponified organic matter is 0.1–0.6 N.

[0016] Furthermore, the volume ratio of the alkaline substance to the empty organic matter is 0.01 to 0.07:1. Preferably, the alkaline substance is ammonia water and / or liquid alkali, and preferably, the empty organic matter is an acidic extractant. Preferably, the acidic extractant is selected from any one or more of P204, P507, and C272.

[0017] Furthermore, if the total saponified water content in the above-mentioned extraction saponification cooling device is greater than the initial amount of water added in step S1, the excess saponified water will be discharged from the extraction saponification cooling device.

[0018] By applying the technical solution of this application, this invention utilizes the characteristics of water having a high specific heat capacity and organic matter having a low specific heat capacity. The cooled saponified water is returned to the saponification reaction tank for direct heat exchange during the saponification process, saving investment in indirect heat exchangers. Specifically, a large flow of saponified water absorbs the heat released during saponification, significantly reducing the temperature rise of the saponified organic matter. The saponification equipment can be made of ordinary PVC material, resulting in low cost. The saponified reaction system is clarified and separated, and the obtained saponified organic matter is sent to the next extraction process. The clarified saponified water is then sent to a cooling tower for cooling, and the cooled saponified water is returned to the saponification reaction process for continued use. Finally, thanks to the separate cooling tower for cooling the clarified saponified water, this invention not only avoids interference between different cooling systems and reduces the likelihood of organic contamination of the large cooling water system due to heat exchanger leaks, but also provides convenient operation and management and precise temperature control. Attached Figure Description

[0019] The accompanying drawings, which form part of this application, are used to provide a further understanding of the invention. The illustrative embodiments of the invention and their descriptions are used to explain the invention and do not constitute an undue limitation of the invention. In the drawings:

[0020] Figure 1 A schematic diagram of an extraction saponification cooling device according to Embodiment 1 of the present invention is shown.

[0021] The above figures include the following reference numerals:

[0022] 1. Saponification reaction tank; 2. Clarification tank; 3. Cooling tower; 4. Cooling water transfer pump; 5. Saponification water cooling pump; 6. Saponification water discharge pump. Detailed Implementation

[0023] It should be noted that, unless otherwise specified, the embodiments and features described in this application can be combined with each other. The present invention will now be described in detail with reference to the accompanying drawings and embodiments.

[0024] As analyzed in the background section of this application, the prior art has problems such as high cost of saponification extraction equipment, serious organic volatilization, low heat exchange efficiency of indirect heat exchange method and possible pollution of cooling circulating water system. In order to solve this problem, this application provides an extraction saponification cooling device and extraction saponification cooling method.

[0025] In a typical embodiment of this application, an extraction saponification cooling device is provided, such as... Figure 1 As shown, the extraction saponification cooling device includes a saponification reaction tank 1, a clarification tank 2, a cooling tower 3, and a cooling water transfer pump 4. The inlet of the saponification reaction tank 1 is connected to an empty organic source, an alkaline source, and a water source, respectively. The saponification reaction tank 1 is used to saponify the raw materials including empty organic matter, alkaline substances, and water to obtain a saponification reaction system. The inlet of the clarification tank 2 is connected to the outlet of the saponification reaction tank 1. The clarification tank 2 is used to clarify and separate the saponification reaction system to obtain saponified organic matter and clarified saponified water. The inlet of the cooling tower 3 is connected to the outlet of the clarification tank 2. The cooling tower 3 is used to cool the clarified saponified water to obtain cooled saponified water. The inlet of the cooling water transfer pump 4 is connected to the outlet of the cooling tower 3. The cooling water transfer pump 4 is used to return the cooled saponified water to the saponification reaction tank 1.

[0026] This invention utilizes the high specific heat capacity of water and the low specific heat capacity of organic matter to directly exchange heat during the saponification reaction in saponification tank 1 after cooling. This saves on the investment in indirect heat exchangers. Specifically, a large flow of saponified water absorbs the heat released during saponification, significantly reducing the temperature rise of the saponified organic matter. The saponification equipment can be made of ordinary PVC material, resulting in low cost. The saponified reaction system is then clarified and separated. The obtained saponified organic matter is sent to the next extraction process, while the clarified saponified water is sent to cooling tower 3 for cooling. The cooled saponified water is then returned to the saponification reaction process for continued use. Finally, thanks to the separate cooling tower 3 for cooling the clarified saponified water, this invention not only avoids interference between different cooling systems and reduces the likelihood of organic contamination of the cooling water circulation system due to heat exchanger leaks, but also provides convenient operation and management and precise temperature control.

[0027] In one embodiment of this application, the above-mentioned extraction saponification cooling device further includes a saponification water cooling pump 5, which is installed on the pipeline connecting the clarification tank 2 and the cooling tower 3, and is used to transport the clarified saponified water into the cooling tower 3.

[0028] The saponified saponified water, which has a higher temperature than that obtained in the clarification tank 2, can be continuously transported to the cooling tower 3 by the saponified water cooling pump, so that the clarified saponified water can be cooled in the cooling tower 3 to obtain cooled saponified water.

[0029] In one embodiment of this application, the above-mentioned extraction saponification cooling device further includes a saponification water discharge pump 6. The inlet of the saponification water discharge pump 6 is connected to the outlet of the clarification tank 2, and is used to discharge a portion of the saponification water from the extraction saponification cooling device. The portion of the total saponification water content in the extraction saponification cooling device that exceeds the initial amount of water added to the saponification reaction tank 1 is the discharged saponification water.

[0030] Based on the water balance, a portion of the saponification water is periodically discharged to maintain a constant water volume in the entire extraction saponification cooling device, thereby better maintaining a relatively stable temperature rise in the saponification reaction within the device.

[0031] In another typical embodiment of this application, an extraction saponification cooling method is provided, which includes: step S1, subjecting a raw material comprising an empty organic compound, an alkaline substance, and water to a saponification reaction to obtain a saponification reaction system; step S2, clarifying and separating the saponification reaction system to obtain saponified organic compound and clarified saponified water; step S3, cooling the clarified saponified water to obtain cooled saponified water; and step S4, returning the cooled saponified water to step S1 as water; and repeating steps S1 to S4.

[0032] This invention utilizes the high specific heat capacity of water and the low specific heat capacity of organic matter to directly exchange heat in the saponification reaction process by returning the cooled saponified water to step S1, saving the investment in indirect heat exchangers. Specifically, a large flow of saponified water absorbs the heat released during saponification, thus significantly reducing the temperature rise of the saponified organic matter. The saponification equipment can be made of ordinary PVC material, resulting in low cost. The saponified reaction system is clarified and separated, and the obtained saponified organic matter is sent to the next stage of extraction. The clarified saponified water is then cooled and returned to the saponification reaction process for continued use. Finally, thanks to the separate cooling measures for the clarified saponified water in this invention, not only can interference between different cooling steps be avoided, reducing the probability of organic contamination of the large cooling water system due to heat exchanger leaks, but operation and management are also convenient and temperature control is precise.

[0033] Preferably, in step S3 above, the temperature of the saponified water after cooling is 20-32°C (e.g., 20°C, 25°C, 28°C or 32°C), which helps to improve the cooling effect of the saponified water returning to step S1 on the heat released by the saponification reaction.

[0034] Preferably, the temperature range for converting the above-mentioned unloaded organic matter into saponified organic matter is -8 to 24℃, such as -8℃, -7.8℃, -5℃, -1.3℃, -0.5℃, -0.3℃, 0℃, 2.8℃, 6.5℃, 8.5℃, 11℃, 11.4℃, 13℃, 15℃, 18.8℃, 20℃, 23.3℃, ​​or 24℃; preferably, the temperature of the saponified organic matter is ≤55℃, such as 28.7℃, 32.8℃, 30℃, 36.5℃, 38.5℃, 39.5℃, 41.0℃, 41.4℃, 42.2℃, 43℃, 45℃, 48.8℃, 49.7℃, 50℃, 53.3℃, ​​or 55℃. By controlling the temperature range and temperature of the saponified organic matter, the saponification equipment can be made of ordinary PVC material to reduce costs.

[0035] In one embodiment of this application, the volumetric flow ratio of water to empty organic matter is 0.3 to 2:1, preferably 0.5 to 2:1, preferably 1 to 2:1, the water temperature is preferably 20 to 32°C, and the empty organic matter temperature is preferably 30 to 50°C.

[0036] Controlling the volumetric flow ratio of water to unloaded organic matter, the water temperature (e.g., 20°C, 25°C, 28°C, or 32°C), and the temperature of unloaded organic matter (e.g., 30°C, 40°C, or 50°C) within the above ranges helps to more accurately control the temperature rise of the saponification reaction within a lower range, and the temperature rise range is more stable.

[0037] Preferably, the extraction equivalent of the saponified organic matter is 0.1 to 0.6N, such as 0.1N, 0.2N, 0.3N, 0.4N, 0.5N or 0.6N, which helps to improve the extraction efficiency and effect of the saponified organic matter.

[0038] In one embodiment of this application, the volume ratio of the alkaline substance to the empty organic matter is 0.01 to 0.07:1 (e.g., 0.01:1, 0.02:1, 0.03:1, 0.04:1, 0.05:1, 0.06:1 or 0.07:1). Preferably, the alkaline substance is ammonia water and / or liquid alkali, and preferably, the empty organic matter is an acidic extractant. Preferably, the acidic extractant is selected from any one or more of P204, P507, and C272.

[0039] The preferred volume ratio of the alkaline substance to the unloaded organic matter helps control the degree of saponification reaction, thereby controlling the heat released and improving the heat absorption effect of the saponification water after cooling. The preferred liquid alkaline substance helps improve its contact with the unloaded organic matter, increasing the efficiency of the saponification reaction. There are no limitations on the alkaline substance and the unloaded organic matter; those skilled in the art can choose other types of corresponding substances, which will not be elaborated here.

[0040] When the total saponified water content in the extraction saponification cooling device is greater than the initial amount of water added in step S1, the excess saponified water is discharged from the extraction saponification cooling device, which helps to maintain a relatively stable saponification reaction temperature rise in the extraction saponification cooling device.

[0041] The beneficial effects of this application will be further illustrated below with reference to embodiments and comparative examples.

[0042] Example 1

[0043] according to Figure 1 The schematic diagram of the extraction saponification cooling device shown illustrates the extraction saponification cooling process:

[0044] Step S1: Empty organic matter P204, alkaline substance ammonia water and water are introduced into saponification reaction tank 1 to carry out saponification reaction to obtain saponification reaction system; wherein, the volume flow ratio of water to empty organic matter P204 is 2:1, the temperature of water is 32℃, the temperature of empty organic matter P204 is 30℃, and the volume ratio of alkaline substance ammonia water to empty organic matter is 0.07:1.

[0045] Step S2: The saponification reaction system is clarified and separated in clarification tank 2 to obtain saponified organic matter and clarified saponified water; wherein, the extraction equivalent of saponified organic matter is 0.6N.

[0046] In step S3, the clarified saponified water is transported to the cooling tower 3 by the saponified water cooling pump 5 for cooling treatment, and the cooled saponified water has a temperature of 38.5℃ before and 32℃ after cooling.

[0047] In step S4, the cooled saponified water is returned to the saponification reaction tank 1 as water by the cooling water transfer pump 4; according to the water balance, a portion of the saponified water is periodically discharged by the saponified water discharge pump 6.

[0048] Example 2

[0049] The difference from Example 1 is that the volumetric flow rate ratio of water to empty organic matter P204 is 1:1, and saponified organic matter P204 is finally obtained.

[0050] Example 3

[0051] The difference from Example 1 is that the volumetric flow rate ratio of water to unloaded organic matter P204 is 0.5:1, ultimately yielding saponified organic matter P204.

[0052] Example 4

[0053] The difference from Example 1 is that the volumetric flow rate ratio of water to unloaded organic matter P204 is 0.3:1, ultimately yielding saponified organic matter P204.

[0054] Example 5

[0055] The difference from Example 1 is that the temperature of the empty organic compound P204 is 50°C, and the final product is saponified organic compound P204.

[0056] Example 6

[0057] The difference from Example 1 is that the volume ratio of the alkaline substance ammonia water to the empty organic matter is 0.05:1, and the final product is saponified organic matter P204.

[0058] Example 7

[0059] The difference from Example 1 is that the volume ratio of the alkaline substance ammonia water to the empty organic matter is 0.1:1, and the final product is saponified organic matter P204.

[0060] Example 8

[0061] The difference from Example 1 is that the temperature of the saponified water after cooling is 20°C, and the final saponified organic compound P204 is obtained.

[0062] Example 9

[0063] The difference from Example 1 is that the temperature of the saponified water after cooling is 25°C, and the final saponified organic compound P204 is obtained.

[0064] Example 10

[0065] The difference from Example 1 is that the temperature of the saponified water after cooling is 35°C, and the final saponified organic compound P204 is obtained.

[0066] Example 11

[0067] The difference from Example 1 is that the empty organic compound is P507, the temperature is 40°C, the alkaline substance is sodium hydroxide solution, the extraction equivalent of the saponified organic compound is 0.4N, the volume flow ratio of water to empty organic compound P507 is 1:1, and the temperature of the saponified water after cooling is 28°C, finally obtaining saponified organic compound P507.

[0068] Example 12

[0069] The difference from Example 1 is that the empty organic compound is C272, the temperature is 50°C, the alkaline substance is sodium hydroxide solution, the extraction equivalent of the saponified organic compound is 0.1N, the volume flow ratio of water to empty organic compound C272 is 0.1:1, and the temperature of the saponified water after cooling is 20°C, finally obtaining saponified organic compound C272.

[0070] Comparative Example 1

[0071] Step S1: Empty organic matter P204 and alkaline substance ammonia water are introduced into saponification reaction tank 1 to carry out saponification reaction to obtain saponification reaction system; wherein, the temperature of empty organic matter P204 is 40℃, and the volume ratio of alkaline substance ammonia water to empty organic matter is 0.076:1.

[0072] Step S2: The saponification reaction system is clarified and separated in clarification tank 2 to obtain saponified organic matter and clarified saponified water; wherein, the extraction equivalent of saponified organic matter is 0.65N.

[0073] Table 1 lists the temperature of the saponified water after cooling, the temperature of the unloaded organic matter, the temperature of the saponified organic matter, and the temperature rise of the organic matter before and after saponification in Examples 1 to 12 and Comparative Example 1.

[0074] Table 1

[0075]

[0076] As can be seen from the above description, the embodiments of the present invention achieve the following technical effects:

[0077] This invention utilizes the high specific heat capacity of water and the low specific heat capacity of organic matter to directly exchange heat between the cooled saponified water and the saponification reaction tank, saving the investment in indirect heat exchangers. Specifically, a large flow of saponified water absorbs the heat released during saponification, significantly reducing the temperature rise of the saponified organic matter. The saponification equipment can be made of ordinary PVC material, resulting in low cost. The saponified reaction system is then clarified and separated. The obtained saponified organic matter is sent to the next extraction process, while the clarified saponified water is cooled in a cooling tower and then returned to the saponification reaction for reuse. Finally, thanks to the separate cooling tower for cooling the clarified saponified water, this invention not only avoids interference between different cooling systems and reduces the likelihood of organic contamination of the cooling water system due to heat exchanger leaks, but also offers convenient operation and management and precise temperature control.

[0078] The above are merely preferred embodiments of the present invention and are not intended to limit the present invention. Various modifications and variations can be made to the present invention by those skilled in the art. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present invention should be included within the scope of protection of the present invention.

Claims

1. An extraction saponification cooling device, characterized in that, The extraction saponification cooling device includes: The saponification reaction tank (1) has its inlet connected to an empty organic source, an alkaline source and a water source, respectively, and is used to saponify raw materials including empty organic matter, alkaline substances and water to obtain a saponification reaction system. Clarification tank (2), whose inlet is connected to the outlet of the saponification reaction tank (1), is used to clarify and separate the saponification reaction system to obtain saponified organic matter and clarified saponified water; Cooling tower (3), whose inlet is connected to the outlet of the clarification tank (2), is used to cool the clarified saponified water to obtain cooled saponified water; and A cooling water transfer pump (4) has its inlet connected to the outlet of the cooling tower (3) and is used to return the cooled saponified water to the saponification reaction tank (1).

2. The extraction saponification cooling device according to claim 1, characterized in that, The extraction saponification cooling device also includes: A saponified water cooling pump (5) is installed on the pipeline connecting the clarification tank (2) and the cooling tower (3) to transport the clarified saponified water into the cooling tower (3).

3. The extraction saponification cooling device according to claim 1 or 2, characterized in that, The extraction saponification cooling device also includes: The saponification water discharge pump (6) has its inlet connected to the outlet of the clarification tank (2) and is used to discharge part of the saponification water from the extraction saponification cooling device. The portion of the total saponification water content in the extraction saponification cooling device that is greater than the initial amount of water added to the saponification reaction tank (1) is the discharged saponification water.

4. A method for extraction saponification cooling using the extraction saponification cooling device according to any one of claims 1 to 3, characterized in that, The extraction, saponification, and cooling method includes: Step S1 involves subjecting the raw materials, including unloaded organic matter, alkaline substances, and water, to a saponification reaction to obtain a saponification reaction system. In step S2, the saponification reaction system is clarified and separated to obtain saponified organic matter and clarified saponified water; Step S3: Cool the clarified saponified water to obtain cooled saponified water; and Step S4: Return the cooled saponified water to step S1 as the water. Repeat steps S1 to S4; In step S3, the temperature of the saponified water after cooling is 20~32℃; The volumetric flow rate ratio of the water to the empty organic matter is 0.3~2:

1.

5. The extraction, saponification, and cooling method according to claim 4, characterized in that, The temperature range for converting the empty organic matter into the saponified organic matter is -8 to 24°C.

6. The extraction, saponification, and cooling method according to claim 4, characterized in that, The temperature of the saponified organic matter is ≤55℃.

7. The extraction, saponification, and cooling method according to any one of claims 4 to 6, characterized in that, The volumetric flow ratio of the water to the empty organic matter is 0.5~2:1, the temperature of the water is 20~32℃, and the temperature of the empty organic matter is 30~50℃.

8. The extraction, saponification, and cooling method according to claim 7, characterized in that, The volumetric flow rate ratio of the water to the empty organic matter is 1~2:

1.

9. The extraction, saponification, and cooling method according to any one of claims 4 to 6, characterized in that, The extraction equivalent of the saponified organic matter is 0.1~0.6N.

10. The extraction, saponification, and cooling method according to any one of claims 4 to 6, characterized in that, The volume ratio of the alkaline substance to the empty organic matter is 0.01~0.07:

1.

11. The extraction, saponification, and cooling method according to any one of claims 4 to 6, characterized in that, The alkaline substance is ammonia water and / or liquid alkali.

12. The extraction, saponification, and cooling method according to any one of claims 4 to 6, characterized in that, The empty organic compound is an acidic extractant.

13. The extraction, saponification, and cooling method according to claim 12, characterized in that, The acidic extractant is selected from any one or more of P204, P507, and C272.

14. The extraction, saponification, and cooling method according to any one of claims 4 to 6, characterized in that, When the total saponified water content in the extraction saponification cooling device exceeds the initial amount of water added in step S1, the excess saponified water is discharged from the extraction saponification cooling device.

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