A method for the continuous synthesis of isooctyl chloroformate

Abstract

The application discloses a method for continuously synthesizing isooctyl chloroformate, which comprises the following steps: preparing a continuous reaction device which comprises a photochemical tower, a transfer kettle and a chase light tower which are communicated with each other, feeding isooctanol and phosgene into the photochemical tower to perform a reaction, overflowing the obtained esterification liquid to the transfer kettle, performing gas-liquid separation on the obtained tail gas outside the tower, and feeding the liquid light into the tower; controlling the temperature of the transfer kettle at 30-40 DEG C, feeding the esterification liquid into the chase light tower after the transfer kettle collects a certain amount of esterification liquid, controlling the temperature of the chase light tower at 40-80 DEG C, feeding nitrogen into the chase light tower to perform chase light, and collecting high-purity isooctyl chloroformate in the chase light tower, wherein the content of the isooctyl chloroformate is greater than or equal to 99%, and the yield is greater than or equal to 97%. The method realizes continuous production under the premise of ensuring the quality and yield of the product, has small production land occupation, small liquid holdup of the reaction system, small risk, high production efficiency, easily controlled process conditions, little waste, accords with the green and environmental protection production concept, and is suitable for industrial production.

Description

Technical Field

[0001] This invention belongs to the field of organic compound synthesis and relates to a method for the continuous synthesis of isooctyl chloroformate, specifically a method for reacting 2-ethylhexanol (isooctanol) with phosgene to generate isooctyl chloroformate. Background Technology

[0002] Isooctyl chloroformate, also known as 2-ethylhexyl chloroformate, can be used to synthesize di(2-ethyl)hexyl peroxide dicarbonate (EHP). It is a colorless and transparent liquid. EHP is a highly active initiator. Compared with other peroxide dicarbonate initiators, it has better stability in transportation and storage. Because it is insoluble in water, it is not easy to produce aqueous polymers when initiating polymerization reactions. It has a small tendency to stick to the reactor and the polymerization reaction is exothermic and uniform, making it easy to obtain a uniform reaction rate.

[0003] Bibi, David, et al. (Neurochemical Research, 2017, No. 7) used triphosgene and isooctanol in a dichloromethane system with pyridine as a catalyst to react at 20°C for 2 hours to obtain isooctyl chloroformate. This method requires the depolymerization of pyridine into phosgene, which is then reacted with isooctanol in a dichloromethane system to obtain isooctyl chloroformate. The decomposition of triphosgene requires the addition of pyridine as a catalyst, which introduces impurities. Moreover, the reaction is carried out in a dichloromethane solvent, which makes the post-processing cumbersome and the yield low.

[0004] Wang Zhaohui and Yang Weiguo (Sichuan Chemical Industry, 2008, 03) used an intermittent method, which introduced phosgene into the isooctanol system and controlled the amount of phosgene introduced by raising the temperature in stages. After air replacement, water washing and drying, ≥95% isooctyl chloroformate was obtained. The isooctyl chloroformate content obtained by this method is not high, the reaction time is long, there are more impurities, and water washing reduces free chlorine, which is not environmentally friendly, has low production efficiency, and is not suitable for modern industrial production.

[0005] Chinese patent document CN114797735A discloses an apparatus for preparing isooctyl chloroformate from phosgene, employing a tower-type synthesis and tower-type photocatalysis. The synthesis section uses four-stage segmented temperature control, and the photocatalysis uses four-stage photocatalysis chambers. The document states that this scheme can yield higher purity isooctyl chloroformate, but it does not provide any supporting data. Furthermore, while segmented, stepwise temperature increases are beneficial for shifting the reaction equilibrium, the activity of impurity formation inevitably increases with rising temperature. These impurities cannot be removed by photocatalysis. Moreover, the operation of this apparatus is complex, requiring different chambers in the photocatalysis tower to achieve repeated photocatalysis. The difference and necessity of photocatalysis in the same tower are not explained, and the content and yield of the final product are not reported. Summary of the Invention

[0006] The technical problem to be solved by the present invention is to overcome the shortcomings of the prior art and provide a method for the continuous synthesis of isooctyl chloroformate that is easy to control, simple to operate, and environmentally friendly.

[0007] To solve the above-mentioned technical problems, the present invention adopts the following technical solution.

[0008] A method for the continuous synthesis of isooctyl chloroformate includes the following steps: preparing a continuous reaction apparatus, the continuous reaction apparatus comprising a photochemical tower, a transfer vessel, and a photochemical removal tower interconnected; controlling the temperature inside the photochemical tower at 0℃~20℃; introducing isooctyl alcohol and phosgene into the photochemical tower for reaction; overflowing the resulting esterified liquid into the transfer vessel; condensing and separating the tail gas outside the tower; and sending the resulting liquid phosgene to the middle of the photochemical tower for further reaction; controlling the temperature of the transfer vessel at 30℃~40℃; sending the esterified liquid collected in the transfer vessel to the photochemical removal tower; controlling the temperature inside the photochemical removal tower at 40℃~80℃; and introducing nitrogen gas into the photochemical removal tower for photochemical removal; finally, collecting high-purity isooctyl chloroformate in the photochemical removal tower, with a content ≥99% and a yield ≥97%.

[0009] In the above-described continuous synthesis method of isooctyl chloroformate, preferably, the molar ratio of phosgene to isooctyl alcohol is 1.02 to 4:1.

[0010] More preferably, in the above-described continuous synthesis method of isooctyl chloroformate, the molar ratio of phosgene to isooctyl alcohol is 1.05 to 1.1:1.

[0011] In the above-described method for the continuous synthesis of isooctyl chloroformate, preferably, the residence time of the material in the photochemical tower is 2h to 8h, and the residence time of the esterification liquid in the photochemical tower is 0.5h to 3h.

[0012] In the above-described method for the continuous synthesis of isooctyl chloroformate, preferably, the residence time of the material in the photochemical tower is 3h to 4h, and the residence time of the esterification liquid in the photochemical tower is 1h to 2h.

[0013] In the above-described method for the continuous synthesis of isooctyl chloroformate, preferably, the esterification liquid is sent to the photocatalytic tower when the volume of the esterification liquid collected in the transfer reactor is half of the volume of the transfer reactor.

[0014] In the above-described method for the continuous synthesis of isooctyl chloroformate, preferably, the temperature in the photochemical tower is 10°C to 20°C.

[0015] In the above-described method for the continuous synthesis of isooctyl chloroformate, preferably, the temperature in the light-reducing tower is 50°C to 60°C.

[0016] In the above-described method for the continuous synthesis of isooctyl chloroformate, preferably, the mass ratio of esterification liquid to nitrogen gas in the light-removing tower is 1:0.3 to 0.8.

[0017] In the above-described method for the continuous synthesis of isooctyl chloroformate, preferably, the mass ratio of esterification liquid to nitrogen gas in the light-removing tower is 1:0.4 to 0.6.

[0018] In the above-described method for the continuous synthesis of isooctyl chloroformate, preferably, the continuous reaction apparatus includes a photochemical tower, a transfer vessel, and a photochemical tower. The photochemical tower is provided with a first inlet, a second inlet, an overflow port, a tail gas outlet, and a tower inlet. The transfer vessel is provided with a third inlet and a discharge port. The overflow port is connected to the third inlet. The photochemical tower is provided with a fourth inlet, a nitrogen inlet, a discharge port, and a gas outlet. The discharge port is connected to the fourth inlet.

[0019] In the above-described method for the continuous synthesis of isooctyl chloroformate, preferably, the continuous reaction apparatus further includes a gas-liquid separator for condensing and separating phosgene in the tail gas of the photochemical tower, and a condenser connected to the gas outlet of the photochemical tower.

[0020] In the above-described method for the continuous synthesis of isooctyl chloroformate, preferably, the transfer vessel is provided with multiple layers of baffles and heating elements for guiding the flow.

[0021] In this invention, the rates of introduction of phosgene, isooctanol, esterification liquid, and nitrogen can be calculated from the material ratio and residence time of the reaction system in the corresponding tower.

[0022] This invention designs a process based on the reaction principle of isooctyl chloroformate. Isooctyl alcohol readily reacts with phosgene to form isooctyl chloroformate, requiring a large equivalent of phosgene to ensure the complete reaction of the small amount of isooctyl alcohol in the later stages. However, a large equivalent of phosgene implies significant phosgene loss and difficult post-processing. Therefore, the tail gas is condensed and separated into liquid and liquid phosgene before being introduced into the tower to increase the phosgene concentration in the later stages of the reaction, promoting complete reaction. The intermediate reactor is designed with baffles for flow guidance and heating, which promotes the shift of reaction equilibrium and, more importantly, preheats the esterification liquid, improving phosgene removal efficiency. This method significantly reduces phosgene loss, and high-content, high-yield isooctyl chloroformate can be obtained through phosgene removal.

[0023] Compared with the prior art, the advantages of the present invention are as follows:

[0024] 1. This invention enables the continuous production of isooctyl chloroformate. The process is simple and reliable, with high production efficiency, low liquid holdup in the reaction system, and low reaction risk, which is more conducive to industrial production.

[0025] 2. By using a liquid phosgene tower after tail gas separation as the feed material, the present invention ensures the phosgene concentration in the later reaction and reduces phosgene loss. After comprehensive calculation, the phosgene content is ≤1.1 eq, which ensures the quality of isooctyl chloroformate. After photocatalysis, the product content is ≥99% and the yield is ≥97%.

[0026] 3. The present invention controls the temperature of the transfer vessel at 30℃~40℃, which on the one hand ensures that the extremely small amount of isooctyl alcohol reacts completely in the later stage, and on the other hand preheats the esterification liquid to improve the light-removing effect. Attached Figure Description

[0027] Figure 1 This is a schematic diagram of the continuous reaction apparatus used in Embodiments 1-4 of the present invention.

[0028] Legend:

[0029] 1. Photochemical tower; 2. Transfer vessel; 3. Photochemical tower; 4. First feed inlet; 5. Second feed inlet; 6. Overflow outlet; 7. Tail gas outlet; 8. Tower inlet; 9. Third feed inlet; 10. Discharge outlet; 11. Fourth feed inlet; 12. Nitrogen inlet; 13. Discharge outlet; 14. Gas outlet; 15. Gas-liquid separator; 16. Condenser. Detailed Implementation

[0030] The present invention will be further described below with reference to the accompanying drawings and specific preferred embodiments, but this does not limit the scope of protection of the present invention. All materials and instruments used in the following embodiments are commercially available. The density of isooctanol is 0.833 g / mL, and the density of the esterification solution is approximately 1.0 g / mL.

[0031] The continuous reaction apparatus used in Examples 1-4 below is as follows: Figure 1 As shown, the system includes a photochemical tower 1, a transfer vessel 2, and a phosgene extraction tower 3. The photochemical tower 1 has a first inlet 4, a second inlet 5, an overflow port 6, a tail gas outlet 7, and a tower inlet 8. The first inlet 4 serves as the isooctanol inlet, and the second inlet 5 serves as the phosgene inlet. The transfer vessel 2 has a third inlet 9 and a discharge port 10, with the overflow port 6 connected to the third inlet 9. The phosgene extraction tower 3 has a fourth inlet 11, a nitrogen inlet 12, a discharge port 13, and a gas outlet 14, with the discharge port 10 connected to the fourth inlet 11. Both the photochemical tower 1 and the phosgene extraction tower 3 are equipped with jackets.

[0032] The continuous reaction apparatus also includes a gas-liquid separator 15 and a condenser 16. The gas inlet of the gas-liquid separator 15 is connected to the tail gas outlet 7 of the photochemical tower 1, and the cold liquid outlet of the gas-liquid separator 15 is connected to the tower inlet 8 of the photochemical tower 1. The gas-liquid separator 15 is used to condense and separate the phosgene in the tail gas (containing phosgene and HCl gas) at the top of the photochemical tower 1. The condensed liquid phosgene is sent back to the photochemical tower 1 through the tower inlet 8, and the HCl gas is discharged. The gas inlet of the condenser 16 is connected to the gas outlet 14 of the photochemical tower 3, and is used to return a small amount of product that may be carried out with the gas in the photochemical tower 1 to the photochemical tower 3 after condensation by the condenser 16, thereby increasing the yield. Both the photochemical tower 1 and the photochemical tower 3 are filled with ceramic packing. The photochemical tower 1 operates at full capacity, and the transfer vessel 2 is equipped with multiple layers of baffles for flow guidance and heating elements.

[0033] In the continuous reaction apparatus, isooctanol and phosgene are simultaneously fed into the photochemical tower 1 through the first inlet 4 and the second inlet 5, respectively, for reaction. The resulting esterified liquid is sent to the transfer vessel 2 through the overflow port 6. The tail gas from the top of the tower is sent to the gas-liquid separator 15 through the tail gas outlet 7 for gas-liquid separation of the condensed liquid phosgene and HCl gas. The separated liquid phosgene is sent back to the photochemical tower 1 for further reaction to increase the phosgene concentration in the later stages of the reaction. After the transfer vessel 2 collects a certain amount of esterified liquid, it is sent to the photochemical tower 3 through the fourth inlet 11. Nitrogen gas is introduced into the photochemical tower 3 through the nitrogen inlet 12 for photochemical removal. Products that may be carried out with the gas in the photochemical tower 3 are condensed by the condenser 16 and returned to the reaction system to increase the yield.

[0034] Example 1:

[0035] A method for the continuous synthesis of isooctyl chloroformate according to the present invention includes the following steps:

[0036] The photochemical reaction tower 1 (Φ50mm, H1000mm) is filled with ceramic packing. The jacket temperature of the photochemical reaction tower 1 is controlled at 10-15℃. Isooctanol is pumped into the photochemical reaction tower 1 at a rate of 4.0mL / min through the first inlet 4 at the bottom of the tower. Phosgene is introduced into the photochemical reaction tower 1 at a rate of 2.78g / min (1.1eq) through the second inlet 5 at the bottom of the tower. The residence time of the reactants is controlled at 4h, i.e., the molar ratio of phosgene to isooctanol is 1.1:1. The esterification liquid overflowing from the top of the photochemical reaction tower 1 is sent to the transfer vessel 2, which is controlled at 30℃. The tail gas from the top of the photochemical reaction tower 1 is sent to the gas-liquid separator 15 for phosgene condensation and gas-liquid separation. The separated liquid phosgene is sent back into the photochemical reaction tower 1 through the inlet 8 to continue the reaction. After the intermediate reactor 2 collected half of its volume of esterified liquid, the photocatalytic pump was turned on and pumped into the top of the photocatalytic tower 3 (Φ50mm, H1000mm) at a rate of 4.0mL / min. The tower was filled with ceramic packing, and the jacket temperature in the photocatalytic tower 3 was 50℃. Nitrogen gas was introduced into the photocatalytic tower 3 from the bottom at a rate of 1.6g / min for photocatalytic operation. The residence time of the esterified liquid was controlled at 1h by the discharge rate from the feed port, i.e., the mass ratio of esterified liquid to nitrogen gas in the photocatalytic tower 3 was 1:0.4. After the reaction stabilized, multiple time intervals (in 1h units) were randomly selected for yield calculation, and the average was taken. The average yield of isooctyl chloroformate was 97.5%, the content was 99.2%, free chlorine ≤0.1%, and phosgene ≤0.1%.

[0037] Example 2:

[0038] A method for the continuous synthesis of isooctyl chloroformate according to the present invention includes the following steps:

[0039] The photochemical reaction tower 1 (Φ50mm, H1000mm) is filled with ceramic packing. The jacket temperature of the photochemical reaction tower 1 is controlled at 15-20℃. Isooctanol is pumped into the tower 1 at a rate of 5.0mL / min through the first inlet 4 at the bottom. Simultaneously, phosgene is introduced into the tower 1 at a rate of 3.48g / min (1.1eq) through the second inlet at the bottom. The residence time of the reaction liquid is controlled at approximately 3.0h, i.e., the molar ratio of phosgene to isooctanol is 1.1:1. The esterification liquid overflowing from the top of the photochemical reaction tower 1 is transferred to the transfer vessel 2, which is maintained at a temperature of 35℃. The tail gas from the top of the photochemical reaction tower 1 enters the gas-liquid separator 15. The condensed and separated liquid phosgene is then introduced into the photochemical reaction tower 1 through the inlet 8 to continue the reaction. After the intermediate reactor 2 collected half of its volume of esterified liquid, the photocatalytic pump was turned on and pumped into the top of the photocatalytic tower 3 (Φ50mm, H1000mm) at a rate of 5.0 mL / min. The tower was filled with ceramic packing, and the jacket temperature in the photocatalytic tower 3 was 55℃. Nitrogen gas was introduced into the photocatalytic tower 3 from the bottom at a rate of 2.5 g / min for photocatalytic operation. The residence time of the esterified liquid was controlled at 1 h by the discharge rate from the feed port, i.e., the mass ratio of esterified liquid to nitrogen gas in the photocatalytic tower 3 was 1:0.5. After the reaction stabilized, multiple time intervals (in 1-hour increments) were randomly selected for yield calculation, and the average was taken. The average yield of isooctyl chloroformate was 97.7%, the content was 99.1%, free chlorine ≤0.1%, and phosgene ≤0.1%.

[0040] Example 3:

[0041] A method for the continuous synthesis of isooctyl chloroformate according to the present invention includes the following steps:

[0042] The photochemical reaction tower 1 (Φ50mm, H1000mm) is filled with ceramic packing. The jacket temperature inside the photochemical reaction tower 1 is controlled at 10-15℃. Isooctanol is pumped into the tower 1 at a rate of 5.0mL / min through the first inlet 4 at the bottom of the tower 1, while phosgene is introduced at a rate of 3.32g / min (1.05eq) through the second inlet 5 at the bottom of the tower 1. The residence time of the reaction liquid is controlled at about 3.0h, i.e., the molar ratio of phosgene to isooctanol is 1.05:1. The esterification liquid overflowing from the top of the photochemical reaction tower 1 is transferred to the transfer vessel 2, which is controlled at 35℃. The tail gas from the top of the tower 1 enters the gas-liquid separator 15, where it is condensed and separated. The resulting liquid phosgene enters the tower 1 for reaction through inlet 8. After the intermediate reactor 2 collected half of its volume of esterified liquid, the photocatalytic pump was turned on and pumped into the top of the photocatalytic tower 3 (Φ50mm, H1000mm) at a rate of 5.0 mL / min. The tower was filled with ceramic packing, and the jacket temperature of the photocatalytic tower 3 was 50℃. Nitrogen gas was introduced into the photocatalytic tower 3 from the bottom at a rate of 2.5 g / min for photocatalytic operation. The residence time of the esterified liquid was controlled at 1 hour by the discharge rate from the feed port, i.e., the mass ratio of esterified liquid to nitrogen gas in the photocatalytic tower 3 was 1:0.5. After the reaction stabilized, multiple time intervals (in 1-hour increments) were randomly selected for yield calculation, and the average was taken. The average yield of isooctyl chloroformate was 97.4%, the content was 99.1%, free chlorine ≤0.1%, and phosgene ≤0.1%.

[0043] Example 4:

[0044] A method for the continuous synthesis of isooctyl chloroformate according to the present invention includes the following steps:

[0045] The photochemical reaction tower 1 (Φ50mm, H1000mm) is filled with ceramic packing. The jacket temperature of the photochemical reaction tower 1 is controlled at 10-15℃. Isooctanol is pumped into the photochemical reaction tower 1 at a rate of 4.0mL / min through the first inlet 4 at the bottom of the tower. Phosgene is introduced into the photochemical reaction tower 1 at a rate of 2.66g / min (1.05eq) through the second inlet 5 at the bottom of the tower. The residence time of the reaction liquid is controlled at about 4 hours, i.e., the molar ratio of phosgene to isooctanol is 1.05:1. The overflow esterification liquid from the top of the photochemical reaction tower 1 is sent to the transfer vessel 2, which is controlled at 35℃. The tail gas from the top of the photochemical reaction tower 1 enters the gas-liquid separator 15. The condensed and separated liquid phosgene is introduced into the photochemical reaction tower 1 through the inlet 8. After the intermediate reactor 2 collected half of its volume of esterified liquid, the photocatalytic pump was turned on and pumped into the top of the photocatalytic tower 3 (Φ50mm, H1000mm) at a rate of 4.0 mL / min. The tower was filled with ceramic packing, and the jacket temperature in the photocatalytic tower 3 was 50℃. Nitrogen gas was introduced into the photocatalytic tower 3 from the bottom at a rate of 2.4 g / min for photocatalytic operation. The residence time of the esterified liquid was controlled at 1 h by the discharge rate from the feed port, i.e., the mass ratio of esterified liquid to nitrogen gas in the photocatalytic tower 3 was 1:0.6. After the reaction stabilized, multiple time intervals (in 1-hour increments) were randomly selected for yield calculation, and the average was taken. The average yield of isooctyl chloroformate was 97.5%, the content was 99.2%, free chlorine ≤0.1%, and phosgene ≤0.1%.

[0046] In summary, the design of the photochemical tower 1 in the method of this invention first ensures the phosgene concentration in the later stage of the reaction, greatly reducing phosgene loss. The baffle guiding design of the transfer vessel 2 ensures complete reaction and preheats the esterification liquid, improving photocatalytic efficiency. Therefore, this method achieves continuous production while ensuring product quality and yield. It has a small production footprint, low liquid holdup in the reaction system, low risk, high production efficiency, easy-to-control process conditions, and minimal waste, conforming to the concept of green and environmentally friendly production and suitable for industrial production.

[0047] The above description is merely a preferred embodiment of the present invention and is not intended to limit the present invention in any way. Although the present invention has been disclosed above with reference to preferred embodiments, it is not intended to limit the present invention. Any person skilled in the art can make many possible variations and modifications to the technical solutions of the present invention using the methods and techniques disclosed above, or modify them into equivalent embodiments with equivalent changes, without departing from the spirit and technical essence of the present invention. Therefore, any simple modifications, equivalent substitutions, equivalent changes, and modifications made to the above embodiments based on the technical essence of the present invention without departing from the content of the technical solutions of the present invention shall still fall within the protection scope of the technical solutions of the present invention.

Claims

1. A method for the continuous synthesis of isooctyl chloroformate, characterized in that, The process includes the following steps: preparing a continuous reaction apparatus, which includes a photochemical tower (1), a transfer vessel (2), and a photochemical tower (3) connected to each other. The temperature inside the photochemical tower (1) is controlled at 0℃~20℃. Isooctanol and phosgene are introduced into the photochemical tower (1) for reaction. The resulting esterified liquid overflows into the transfer vessel (2). The resulting tail gas is condensed outside the tower and separated into gas and liquid. The resulting liquid phosgene is then sent to the middle of the photochemical tower (1) to continue the reaction. The temperature of the transfer vessel (2) is controlled at 30℃~40℃. The esterified liquid collected in the transfer vessel (2) is sent to the photochemical tower (3). The temperature in the photochemical tower (3) is controlled at 40℃~80℃. Nitrogen gas is introduced into the photochemical tower (3) for photochemical removal. Finally, high-purity isooctyl chloroformate is collected in the photochemical tower (3), with a content ≥99% and a yield ≥97%. The molar ratio of phosgene to isooctanol is 1.05 to 1.1:1; The material residence time in the photochemical tower (1) is 2h to 4h, and the esterification liquid residence time in the photochemical tower (3) is 0.5h to 1h. When the volume of the esterified liquid collected in the intermediate transfer vessel (2) is half the volume of the intermediate transfer vessel (2), the esterified liquid is sent to the light-removing tower (3); The mass ratio of esterified liquid to nitrogen in the light-removing tower (3) is 1:0.3 to 0.

8.

2. The method for continuous synthesis of isooctyl chloroformate according to claim 1, characterized in that, The temperature in the photochemical tower (1) is 10℃~20℃; the temperature in the photochemical tower (3) is 50℃~60℃.

3. The method for continuous synthesis of isooctyl chloroformate according to claim 1, characterized in that, The mass ratio of esterified liquid to nitrogen in the light-removing tower (3) is 1:0.4 to 0.

6.

4. The method for continuous synthesis of isooctyl chloroformate according to claim 1, characterized in that, The continuous reaction device includes a photochemical tower (1), a transfer vessel (2), and a photochemical tower (3). The photochemical tower (1) is provided with a first feed inlet (4), a second feed inlet (5), an overflow outlet (6), a tail gas outlet (7), and a tower inlet (8). The transfer vessel (2) is provided with a third feed inlet (9) and a discharge outlet (10). The overflow outlet (6) is connected to the third feed inlet (9). The photochemical tower (3) is provided with a fourth feed inlet (11), a nitrogen inlet (12), a discharge outlet (13), and a gas outlet (14). The discharge outlet (10) is connected to the fourth feed inlet (11). The continuous reaction apparatus also includes a gas-liquid separator (15) for condensing and separating the phosgene in the tail gas of the photochemical tower (1) and a condenser (16) connected to the gas outlet (14) of the photochemical tower (3). The transfer vessel (2) is equipped with multiple layers of baffles and heating elements for guiding the flow.

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