High-purity indene rectification device and method with temperature self-adjusting function

Abstract

The invention discloses a high-purity indene rectification device and method with a temperature self-adjusting function, and relates to the technical field of rectification, the high-purity indene rectification device comprises a dissolving phase splitter, a drainage pump and an adsorption tower, an oil phase outlet of the dissolving phase splitter is communicated with the adsorption tower, and the rectification device comprises a preheater, a purification device and a condenser. The preheater is respectively communicated with the dissolving phase splitter and the condenser through pipelines, the adsorption tower is communicated with the purification device through a pipeline, the purification device is communicated with the condenser through a drainage pump through a pipeline, the purification device comprises a rectifying tower, a reboiler and a plurality of mass transfer assemblies, the rectifying tower is communicated with the reboiler through a pipeline, and the distance between the adjacent mass transfer assemblies is a mass transfer distance. And the mass transfer distance is gradually changed.

Description

Technical Field

[0001] This invention relates to the field of distillation technology, specifically to a high-purity indene distillation apparatus and method with self-regulating temperature function. Background Technology

[0002] Indene is an aromatic hydrocarbon with the molecular formula C9H8. It is a colorless, transparent, oily liquid at room temperature and has a boiling point of 182.6℃. Indene is a very important raw material in industry, mainly used to manufacture indene-coumarone resin and styrene-indene resin. High-purity indene is an excellent copolymer, widely used to modify the surface activity of molecules. In the biological and pharmaceutical fields, indene can be used as a pharmaceutical intermediate. Pharmaceutical indene requires very high purity. Currently, high-purity indene mainly comes from organic synthesis. Due to the cumbersome steps of organic synthesis, high-purity indene is very expensive. Industrial indene is mainly extracted from indene-containing fractions of coal tar. However, these fractions contain benzonitrile, phenol, cresol, xylenol, etc. Because indene is difficult to separate from benzonitrile, phenol, and cresol, industrial indene prepared from these fractions rarely achieves high purity.

[0003] Chinese patent CN202011264465.X discloses a method and apparatus for extracting high-purity indene from coal tar indene fraction. The method comprises the following steps: 1) The indene fraction first enters a pretreatment tower. Under operating conditions of absolute pressure 0.03–0.1 MPa and temperature 75–106°C, light components are collected from the top of the pretreatment tower through a connecting pipe, and the pretreated material is collected from the side stream and enters an extractive distillation tower. Heavy impurities are collected from the bottom of the tower; 2) Fresh extractant is mixed with extractant from the bottom of the extraction recovery tower and then enters the extractive distillation tower. The pretreated material and extractant react fully in the extractive distillation tower to extract... The distillation column operates at an absolute pressure of 0.05–0.15 MPa and an operating temperature of 89–117 °C. The vapor phase from the top of the extractive distillation column is used as a heat source for the pretreatment column, exchanging heat with the material at the bottom of the pretreatment column. One stream is then returned to the extractive distillation column as reflux, while the other stream yields indene product with a purity of 96%–99% or ≥99%. 3) The extraction recovery column (301) operates at an absolute pressure of 0.03–0.1 MPa and a temperature of 91–115 °C. One stream from the top of the extraction recovery column is returned to the extraction recovery column as reflux, while the other stream yields benzonitrile product. The extractant from the bottom of the column is returned to the extractive distillation column. This method uses a three-column process to purify indene and includes an extractant, making the process complex and energy-intensive.

[0004] Chinese patent CN201910336559.4 discloses a method for extracting and purifying indene products, as well as a purification device system based on this method. This method addresses the tendency of indene to undergo reactive polymerization during extraction and purification by employing a continuous three-stage negative pressure distillation process. Under negative pressure, the bubble point of heavy benzene or C9 aromatic hydrocarbons in the indene-containing material is lowered, thereby reducing the separation temperature and difficulty of indene and effectively avoiding its high-temperature polymerization characteristics. This method can yield indene products with a purity of up to 95%. However, due to the presence of benzonitrile in the indene fraction, this method is difficult to prepare high-purity indene products. Furthermore, this method requires a large reflux ratio to obtain indene products, resulting in excessive energy consumption.

[0005] In addition, structured packings can hinder the exchange of light and heavy components during use, affecting the final exchange quality. Currently, most structured packings are arranged at equal intervals, which affects heat recovery efficiency under varying temperature conditions. Summary of the Invention

[0006] The purpose of this invention is to provide a high-purity indene distillation apparatus and method with temperature self-regulation function to solve the problems raised in the prior art.

[0007] To achieve the above objectives, the present invention provides the following technical solution: The distillation unit includes a dissolution phase separator, a priming pump, and an adsorption tower. The oil phase outlet of the dissolution phase separator is connected to the adsorption tower. The distillation unit also includes a preheater, a purification unit, and a condenser. The preheater is connected to the dissolution phase separator and the condenser via pipelines. The adsorption tower and the purification unit are connected via pipelines. The purification unit is connected to the condenser via a priming pump. The purification device includes a distillation column, a reboiler, and several mass transfer components. The distillation column and the reboiler are connected by pipes. The distance between adjacent mass transfer components is the mass transfer distance, which is set gradually.

[0008] After the raw material enters the preheater, the gaseous material flowing out of the distillation column also enters the preheater and exchanges heat with the raw material to preheat it. Simultaneously, the gaseous material is cooled, improving waste heat utilization efficiency. The cooled gaseous material enters the condenser to liquefy, forming high-purity indene. The preheated raw material then enters the dissolution phase separator, which has heating, dissolution, and phase separation functions. It can use steam to heat the process water, creating hot water, which is then introduced into the dissolution phase separator. Components such as benzonitrile dissolve in the hot water, while undissolved components such as indene enter the oil phase after phase separation. The dissolution phase separator can employ a liquid-liquid separator to separate the oil and water phases. The water phase is intermittently collected from the bottom, while the oil phase enters the adsorption tower through a pipeline. The adsorption tower can use activated carbon as the adsorbent to remove components such as phenol and cresol from the raw material. The adsorbed material from the adsorption tower enters the distillation column, where it is heated and vaporized in a reboiler. Distillation then proceeds through mass transfer components. A portion of the liquid phase formed in the condenser is collected as indene, while the remaining liquid phase is refluxed back into the distillation column. The liquid phase flows downwards, while the gaseous phase flows upwards. When the gaseous phase encounters the cooler reflux liquid, the heavier components with higher boiling points in the gaseous phase condense into liquid and mix with the reflux liquid, flowing downwards and increasing the purity of the rising gaseous phase. Meanwhile, the lighter components in the reflux liquid are re-vaporized and mixed with the rising gaseous phase, improving the purification efficiency. By setting several sets of mass transfer components for heat exchange between the liquid and gaseous phases, and by gradually varying the mass transfer gap to change the heat exchange time, the system can self-regulate according to temperature, further improving purification efficiency.

[0009] Furthermore, a liquid inlet is installed in the middle section of the distillation column.

[0010] The liquid adsorbed in the adsorption tower is introduced from the middle of the distillation tower, so that during the upward movement of the gas phase, heat exchange can be carried out simultaneously on the adsorbed liquid and the reflux liquid. At the same time, the liquid with increased heavy components will mix with the adsorbed liquid and flow downward, reducing the viscosity of the oil phase and improving its fluidity.

[0011] Furthermore, the mass transfer distance on both sides of the liquid inlet is set to increase progressively in the direction away from the liquid inlet.

[0012] By increasing the mass transfer distance at the bottom of the inlet, the downward flow velocity is increased, reducing gas flow resistance. When the reflux liquid at the top of the inlet flows downward, it transfers mass with the gas phase. By decreasing the downward distance, the downward flow velocity is slowed down, thereby increasing the mass transfer time. Meanwhile, the liquid flow velocity at the top is increased to prevent the light substance from carrying the heavy substance upward together due to excessive time or short distance, which would affect the final purification accuracy.

[0013] Furthermore, a liquid inlet is provided on one side of the lower end of the distillation column.

[0014] By placing the inlet at the bottom, the gaseous substances are only resisted by the reflux liquid as they move upward, which increases the purification speed and improves the recovery quality of light components in the reflux liquid.

[0015] Furthermore, the mass transfer distance is set to increase from top to bottom.

[0016] The liquid material inlet is located on one side of the lower end of the distillation column, and it enters the reboiler directly through the distillation column for vaporization. During the ascent, the gaseous material only undergoes mass transfer with the reflux liquid. The overall mass transfer process is relatively long. When it reaches the top of the distillation column, the temperature of the gaseous material drops to its lowest point, but it cannot vaporize the heavy components in the reflux liquid. This ensures the purification accuracy and improves the purification efficiency.

[0017] Furthermore, the distillation column is equipped with a purification chamber, and a return port is provided on one side of the upper end of the purification chamber. The finished product outlet of the condenser is set with a dual outlet. One of the finished product outlets of the condenser is connected to the return port. A gas outlet is provided at the top of the purification chamber and is connected to the priming pump pipeline. The bottom outlet of the purification chamber is connected to the reboiler pipeline. A gas riser is provided on one side of the bottom of the purification chamber and is connected to the reboiler outlet and the gas riser pipeline.

[0018] The adsorbed liquid is fed into the purification chamber through the inlet for purification. The condenser cools the gaseous material and can be powered by an external circulating water system. Part of the resulting liquid is collected as indene, while the other part flows back into the purification chamber through the return inlet, where it undergoes mass transfer with the gaseous material. Through heat exchange, the light and heavy components in the two-phase fluids are exchanged, improving purification quality. A siphon pump, the main power source, creates a low-pressure zone at the top of the purification chamber and sends the purified gaseous material to the preheater for initial cooling, improving thermal efficiency. The outlet at the bottom of the purification chamber connects to a reboiler, where the gaseous material is reheated and re-enters the purification chamber through the riser for upward mass transfer.

[0019] Furthermore, the distillation column is provided with several transmission chambers. The mass transfer components include a support ring, a positioning motor, and a temperature sensor. The positioning motor is placed in the transmission chamber and is connected to the support ring via a transmission connection. The support ring is rotatably connected to the transmission chamber. The support ring is provided with structured packing. The temperature sensor is adapted to the structured packing and is located below the structured packing.

[0020] The positioning motor is installed through the transmission chamber. As the main power source, it drives the support ring to rotate. The transmission method can be gear meshing, with the gear located at the output end of the positioning motor and the tooth surface on the outside of the support. Temperature sensors are located below the structured packing or on the wall of the purification chamber. By using multiple temperature sensors, the temperature of the liquid flowing out of the structured packing is detected. When the detected temperature is high, the support ring is driven to rotate, causing the through-holes on the upper and lower layers of structured packing to misalign, thereby extending the mass transfer time and improving the recovery efficiency of light components in the reflux liquid.

[0021] Compared with the prior art, the beneficial effects of this invention are as follows: The increasing mass transfer distance at the bottom of the inlet increases the downward flow velocity and reduces gas flow resistance; when the reflux liquid at the top of the inlet flows downward, it undergoes mass transfer with the gaseous substance. The decreasing downward distance slows the downward flow velocity, thereby increasing the mass transfer time. Meanwhile, the increased liquid velocity at the top prevents the light substance from carrying away the heavy substance upwards due to excessive time or short distance, which would affect the final purification accuracy; during the upward process, the gaseous substance only undergoes mass transfer with the reflux liquid, resulting in a longer overall mass transfer process. When it reaches the top of the distillation column, the temperature of the gaseous substance drops to its lowest point, but it cannot vaporize the heavy components in the reflux liquid, thus ensuring purification accuracy and improving purification efficiency; by setting multiple temperature sensors to detect the temperature of the liquid flowing out of the structured packing, when the detected temperature is high, the support ring is driven to rotate, causing the through holes on the upper and lower layers of structured packing to misalign, thereby extending the mass transfer time and improving the recovery efficiency of light components in the reflux liquid. Attached Figure Description

[0022] Figure 1 This is a schematic diagram of the overall structure of the present invention; Figure 2 This is a schematic diagram of the feed section in the distillation column of the present invention; Figure 3 This is a schematic diagram of the liquid distributor structure of the present invention; Figure 4 This is a schematic diagram of the bottom feed of the distillation column of the present invention; Figure 5 This is a schematic diagram of the air inlet structure of the present invention; Figure 6 This is a schematic diagram of the mass transfer component structure of the present invention; Figure 7 This is a schematic diagram of the preheater structure of the present invention.

[0023] In the diagram: 1. Preheater; 11. Shell; 12. Heat exchange tube; 2. Dissolution phase separator; 3. Adsorption tower; 4. Purification unit; 41. Distillation tower; 411. Purification chamber; 412. Liquid inlet; 413. Liquid return port; 414. Gas riser; 415. Gas outlet; 416. Transmission chamber; 42. Liquid distributor; 43. Mass transfer assembly; 431. Support ring; 432. Structured packing; 433. Positioning motor; 434. Temperature sensor; 44. Reboiler; 5. Diversion pump; 6. Condenser. Detailed Implementation

[0024] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0025] Example 1: As Figures 1-3 , Figures 6-7 As shown, the present invention provides a high-purity indene distillation apparatus and method with temperature self-regulation function.

[0026] The distillation unit includes a dissolution phase separator 2, a priming pump 5, and an adsorption tower 3. The oil phase outlet of the dissolution phase separator 2 is connected to the adsorption tower 3. The distillation unit includes a preheater 1, a purification unit 4, and a condenser 6. The preheater 1 is connected to the dissolution phase separator 2 and the condenser 6 respectively. The adsorption tower 3 is connected to the purification unit 4. The purification unit 4 is connected to the condenser 6 through the priming pump 5. The purification device 4 includes a distillation column 41, a reboiler 44 and several mass transfer components 43. The distillation column 41 and the reboiler 44 are connected by pipes. The distance between adjacent mass transfer components 43 is the mass transfer distance, which is set gradually.

[0027] After the raw material enters preheater 1, the gaseous material flowing out of distillation column 41 also enters preheater 1 and exchanges heat with the raw material to preheat it. Simultaneously, the gaseous material is cooled to improve waste heat utilization efficiency. The cooled gaseous material enters condenser 6 to liquefy, forming high-purity indene. The preheated raw material enters dissolution phase separator 2, which has heating, dissolution, and phase separation functions. It can use steam to heat process water to form hot water, which is then introduced into the dissolution phase separator. Components such as benzonitrile dissolve in the hot water, while undissolved components such as indene enter the oil phase after phase separation. Dissolution phase separator 2 can employ a liquid-liquid separator to separate the oil and water phases. The water phase is intermittently collected from the bottom, and the oil phase enters adsorption tower 3 through a pipeline. Adsorption tower 3 can use activated carbon as the adsorbent to remove components such as phenol and cresol from the raw material. The activated carbon micropore diameter is selected to be 20-25 nm, and the activated carbon consumption is 6 g adsorbent / 1 L of raw material. The adsorbed material from adsorption tower 3 enters distillation tower 41 and is heated and vaporized by reboiler. It then undergoes distillation via mass transfer assembly 43. A portion of the liquid phase formed in condenser 6 is collected as indene product, while the remaining liquid phase is refluxed back into distillation tower 41. The liquid phase flows from top to bottom, while the gaseous phase flows from bottom to top. When encountering the cooler reflux liquid, the heavier components with higher boiling points in the gaseous phase are condensed into liquid and mixed into the reflux liquid, flowing downwards and increasing the purity of the rising gaseous phase. Meanwhile, the lighter components in the reflux liquid are re-vaporized and mixed into the rising gaseous phase, improving the purification efficiency. By setting several sets of mass transfer assemblies for heat exchange between the liquid and gaseous phases, and by gradually varying the mass transfer gap to change the heat exchange time, self-regulation based on temperature can be achieved, improving purification efficiency. Preheater 1 includes a shell 11 and heat exchange tubes 12. The inner cavity of the shell is used to connect to the raw material, and the heat exchange tubes 12 are used to connect to the gaseous material output from distillation tower 41.

[0028] Furthermore, a liquid inlet 412 is provided in the middle section of the distillation column 41.

[0029] The liquid adsorbed in adsorption tower 3 is introduced into the middle of distillation tower 41, so that during the upward movement of the gas phase, heat exchange can be carried out simultaneously on the adsorbed liquid and the reflux liquid. At the same time, the liquid with increased heavy components will mix with the adsorbed liquid and flow downward, reducing the viscosity of the oil phase and improving its fluidity.

[0030] Furthermore, the mass transfer distance on both sides of the liquid inlet 412 is set to increase gradually in the direction away from the liquid inlet 412.

[0031] By increasing the mass transfer distance at the bottom of the inlet 412, the downward flow velocity is increased, reducing gas flow resistance. When the reflux liquid at the top of the inlet 412 flows downward, it transfers mass with the gas phase. By decreasing the downward distance, the downward flow velocity is slowed down, thereby increasing the mass transfer time. Meanwhile, the liquid flow velocity at the top is increased to prevent the light substance from carrying the heavy substance upward together due to excessive time or short distance, which would affect the final purification accuracy.

[0032] Furthermore, the distillation column 41 is provided with a purification chamber 411, and a return port 413 is provided on one side of the upper end of the purification chamber 411. The finished product outlet of the condenser 6 is set with a dual outlet. One of the finished product outlets of the condenser 6 is connected to the return port 413. The top of the purification chamber 411 is provided with a gas outlet 415, which is connected to the priming pump 5. The bottom outlet of the purification chamber 411 is connected to the reboiler 44. A riser port 414 is provided on one side of the bottom of the purification chamber 411, and the outlet of the reboiler 44 is connected to the riser port 414.

[0033] The adsorbed liquid is fed into the purification chamber 411 through the liquid inlet 412 for purification. The condenser 6 is used to condense and cool the gaseous material, which can be cooled by external circulating water. Part of the resulting liquid phase is collected as indene product, and the other part flows back into the purification chamber 411 through the liquid return port 413 to exchange mass with the gaseous material. Through heat exchange, the light and heavy components in the two-phase fluid are exchanged, improving the purification quality. The siphon pump 5 serves as the main power source, used to generate a low-pressure zone at the top of the purification chamber 411 and send the purified gaseous material into the preheater 1 for preliminary cooling, improving the thermal energy utilization rate. The outlet at the bottom of the purification chamber 411 is connected to the reboiler 44, which reheats the gaseous material to generate gaseous material, which then re-enters the purification chamber 411 through the gas riser 414 for upward mass transfer.

[0034] Furthermore, the distillation column 41 is provided with several transmission chambers 416, and the mass transfer assembly 43 includes a support ring 431, a positioning motor 433 and a temperature sensor 434. The positioning motor 433 is placed in the transmission chamber 416 and is connected to the support ring 431 in a transmission connection. The support ring 431 is rotatably connected to the transmission chamber 416. The support ring 431 is provided with structured packing 432, and the temperature sensor 434 is adapted to the structured packing 432. The temperature sensor 434 is located below the structured packing 432.

[0035] The positioning motor 433 is installed through the transmission cavity 416. As the main power source, the positioning motor 433 drives the support ring 431 to rotate. The transmission method can be gear meshing, with the gear located at the output end of the positioning motor 433 and the support ring 431 having a toothed surface on its exterior. Temperature sensors 434 are located below the structured packing 432 or can be installed on the wall of the purification cavity 411. By setting multiple temperature sensors 434, the temperature of the liquid flowing out of the structured packing 432 is monitored. When the detected temperature is high, the support ring 431 is driven to rotate, causing the through holes on the upper and lower layers of structured packing 432 to misalign, thereby extending the mass transfer time and improving the recovery efficiency of light components in the reflux liquid. Example

[0036] like Figures 4-5 As shown, compared with Example 1, the difference lies in the arrangement position of the liquid inlet and the gradual direction of the mass transfer distance.

[0037] Furthermore, a liquid inlet 412 is provided on one side of the lower end of the distillation column 41.

[0038] By setting the inlet 412 at the bottom, the gaseous material is only resisted by the reflux liquid as it moves upward, which improves the purification speed and the recovery quality of light components in the reflux liquid.

[0039] Furthermore, the mass transfer distance is set to increase from top to bottom.

[0040] The liquid material inlet is located on one side of the lower end of the distillation column 41. It enters the reboiler 44 directly through the distillation column 41 for vaporization. During the ascent, the gaseous material only transfers mass with the reflux liquid. The overall mass transfer process is relatively long. When it reaches the top of the distillation column 41, the temperature of the gaseous material drops to the lowest point, but it cannot vaporize the heavy components in the reflux liquid. This ensures the purification accuracy and improves the purification efficiency.

[0041] The distillation method includes the following steps; S1. The raw material first enters the preheater 1 and exchanges heat with the gaseous material output from the top of the distillation column 41 to effectively utilize the waste heat. S2. The preheated raw material enters the dissolution phase separator 2. By inputting process water, the components such as benzonitrile are dissolved to form an aqueous phase, which is intermittently extracted from the bottom, while the oil phase flows out. S3. Oil phase substances enter the adsorption tower 3 and are removed by the internal adsorbent, such as phenol and cresol. Activated carbon adsorbent with a micropore diameter of 10~15nm can be used, and the consumption is 7g adsorbent / 1L raw material. S4. The adsorbed material enters the distillation column 41, is heated and vaporized by the reboiler 44 at the bottom, rises and exchanges components with the reflux liquid, thereby separating the light component indene from other heavy components. Finally, it enters the condenser 6 as a gas phase, and forms a liquid phase through condensation. Part of it is collected as indene product, and the other part flows into the distillation column 41 as reflux liquid.

[0042] In S4, distillation column 41 operates under negative pressure, with an operating pressure of 5-10 kPa and a reflux ratio of 3-6. The mass transfer distance within distillation column 41 is gradually varied. By setting a negative pressure, the gaseous substances within distillation column 41 flow upwards, facilitating the exchange of light and heavy components for purification. The gradually varied mass transfer distance alters the flow rate and adjusts the mass transfer time.

[0043] The working principle of this invention is as follows: The mass transfer distance at the lower part of the inlet 412 is progressively increased, increasing the downward flow velocity and reducing gas flow resistance. When the reflux liquid at the upper part of the inlet 412 flows downward, it undergoes mass transfer with the gaseous substance. The progressively decreasing downward distance slows the downward flow velocity, thereby increasing the mass transfer time. Meanwhile, the increased liquid velocity at the top prevents the light substance from carrying away the heavy substance and flowing upward together, which would affect the final purification accuracy, due to excessively long time or short distance. During the upward process, the gaseous substance only interacts with the reflux liquid. Mass transfer is carried out, and the overall mass transfer process is relatively long. When it reaches the top of the distillation column 41, the temperature of the gaseous substance drops to the lowest point, but it cannot vaporize the heavy components in the reflux liquid, thus ensuring the purification accuracy and improving the purification efficiency. By setting multiple temperature sensors 434, the temperature of the liquid flowing out of the structured packing 432 is monitored. When the detected temperature is high, the support ring 431 is driven to rotate, causing the through holes on the upper and lower layers of structured packing 432 to be misaligned, thereby extending the mass transfer time and improving the recovery efficiency of light components in the reflux liquid.

[0044] It will be apparent to those skilled in the art that the present invention is not limited to the details of the exemplary embodiments described above, and that the invention can be implemented in other specific forms without departing from its spirit or essential characteristics. Therefore, the embodiments should be considered in all respects as exemplary and non-limiting, and the scope of the invention is defined by the appended claims rather than the foregoing description. Thus, all variations falling within the meaning and scope of equivalents of the claims are intended to be included within the present invention. No reference numerals in the claims should be construed as limiting the scope of the claims.

Claims

1. A rectification device for high-purity indene with temperature self-adjusting function, comprising a dissolving phase separator (2), a flow guide pump (5) and an adsorption tower (3), wherein the oil phase outlet of the dissolving phase separator (2) is communicated with the adsorption tower (3), and characterized in that: The rectification device comprises a preheater (1), a purification device (4) and a condenser (6), the preheater (1) is in pipeline communication with a dissolving phase separator (2) and the condenser (6) respectively, the adsorption tower (3) and the purification device (4) are in pipeline communication, and the purification device (4) is in pipeline communication with the condenser (6) through a flow pump (5). ​ The purification device (4) comprises a rectification tower (41), a reboiler (44) and a plurality of mass transfer assemblies (43), the rectification tower (41) and the reboiler (44) are in pipeline communication, the distance between adjacent mass transfer assemblies (43) is a mass transfer distance, and the mass transfer distance is gradually changed.

2. The rectification device for high-purity indene with temperature self-adjusting function according to claim 1, characterized in that: A liquid inlet (412) is arranged in the middle section of the rectification tower (41).

3. The rectification device for high-purity indene with temperature self-adjusting function according to claim 2, characterized in that: The mass transfer distance on both sides of the liquid inlet (412) is gradually increased in the direction away from the liquid inlet (412).

4. The rectification device for high purity indene with temperature self-adjusting function according to claim 1, characterized in that: One side of the lower end of the rectification tower (41) is provided with a liquid inlet (412).

5. The rectification device for high-purity indene with temperature self-adjusting function according to claim 4, characterized in that: The mass transfer distance is gradually increased from top to bottom.

6. The rectification device for high-purity indene with temperature self-adjusting function according to any one of claims 1-5, characterized in that: The rectification tower (41) is provided with a purification cavity (411), one side of the upper end of the purification cavity (411) is provided with a liquid return port (413), the product outlet of the condenser (6) is provided with double outlets, one of the product outlets of the condenser (6) is communicated with the liquid return port (413), the liquid return port (413) is provided with a liquid distributor (42) at the tail end, the top end of the purification cavity (411) is provided with a gas outlet (415), the gas outlet (415) is in pipeline communication with the flow pump (5), the bottom end outlet of the purification cavity (411) is in pipeline communication with the reboiler (44), one side of the bottom end of the purification cavity (411) is provided with a gas lifting port (414), and the outlet of the reboiler (44) is in pipeline communication with the gas lifting port (414).

7. The rectification device for high-purity indene with temperature self-adjusting function according to claim 6, characterized in that: The rectification tower (41) is provided with a plurality of transmission cavities (416), the mass transfer assembly (43) comprises a supporting ring (431), a position adjusting motor (433) and a temperature sensor (434), the position adjusting motor (433) is arranged in the transmission cavity (416), the position adjusting motor (433) and the supporting ring (431) are in transmission connection, the supporting ring (431) and the transmission cavity (416) are in rotation connection, the supporting ring (431) is provided with structured packing (432), the temperature sensor (434) is matched with the structured packing (432), and the temperature sensor (434) is located below the structured packing (432).

8. The rectification method of the rectification device for high-purity indene with temperature self-adjusting function according to any one of claims 1-5, characterized in that: The rectification method comprises the following steps: S1, preheating of raw materials, utilizing the waste heat of the top gas of the rectification tower (41); S2, dissolving and separating phases, making the undissolved indene enter the oil phase after phase separation; S3, adsorption, removing phenol and cresol; S4, negative pressure rectification, the extracted material is gasified through the reboiler (44), the light component indene is separated from other heavy components in the rectification tower (41), and becomes a liquid phase after condensation.

9. The rectification method of high purity indene with temperature self-adjusting function according to claim 8, characterized in that: In S4, the rectification tower (41) is operated under negative pressure, the operating pressure is 5-10 kPa, the reflux ratio is 3-6, and the mass transfer distance in the rectification tower (41) is gradually changed.

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