A refining method of heavy aromatic hydrocarbon derivatives for processing automobile sealing rubber

Abstract

The application discloses a refining method of heavy aromatic hydrocarbon derivatives for automobile rubber sealing strips, and relates to the field of raw materials for automobile rubber sealing strips. The heavy aromatic hydrocarbon derivatives are prepared by separating aromatic hydrocarbon mixed oil through extraction cutting and separation processes. The diphenyl sulfone-based extractant in the method contains imidazole cations and bis-trifluoromethyl sulfonate anions through a butyl imidazole bis-trifluoromethyl sulfonimide salt ionic liquid. The acid groups (such as carboxyl groups and sulfonic acid groups) in the heavy aromatic hydrocarbon are ion exchanged with the diphenyl sulfone-based extractant to form stable salts, so that extraction is realized and the purity of the heavy aromatic hydrocarbon derivatives is improved. The heavy aromatic hydrocarbon derivatives are used as plasticizers to prepare automobile rubber sealing strips, and the tensile strength of the automobile rubber sealing strips is improved.

Description

TECHNICAL FIELD

[0001] The present application relates to the field of automobile rubber sealing strip raw materials, and particularly to a refining method of heavy aromatic hydrocarbon derivatives for automobile sealing rubber processing. BACKGROUND

[0002] The rapid development of China's automobile industry has driven the development of other related supporting industries, especially the rubber industry. In recent years, rubber products for automobiles have developed into a unique and specialized product industry. Automobile rubber products are an indispensable and important component element in automobile accessories. Among them, automobile rubber sealing strips are mainly used in automobile doors, windows, trunks, engine covers and other parts, and play the roles of sealing, windproof, rainproof, shock absorption and sound insulation.

[0003] Plasticizers are widely used in rubber products due to their good effects, small amount, fast absorption speed, good compatibility with rubber, and small volatility. Petroleum-based plasticizers are one of the most commonly used plasticizers in rubber processing. They have good plasticizing effect, abundant sources, and low cost. Petroleum-based plasticizers are obtained by atmospheric and vacuum distillation of appropriate crude oil. The main varieties include operating oil, three-line oil, transformer oil, machine oil, light and heavy oil, paraffin, vaseline, asphalt, and petroleum resin, etc.

[0004] A processing method for lightening heavy aromatic hydrocarbon oil (Chinese patent application number: CN202011189622.5) includes: distilling heavy aromatic hydrocarbon oil to obtain light fraction and heavy fraction, and separating the heavy fraction to obtain poor aromatic component and rich aromatic component; distilling the poor aromatic component to obtain pure poor aromatic component and pure rich aromatic component; and then performing hydrofining treatment on the pure rich aromatic component, the rich aromatic component, and the light fraction, and then performing hydrocracking treatment on the obtained hydrofining product and the pure poor aromatic component, thereby realizing the lightening of the heavy aromatic hydrocarbon oil. The heavy aromatic hydrocarbon oil hydrofining catalyst used in the hydrofining treatment includes a metal active component and a carrier supporting the metal active component.

[0005] A processing method for lightening heavy aromatic hydrocarbon and a heavy aromatic selective hydrogenation catalyst (Chinese patent application number: CN201910674110.9) The processing method for lightening heavy aromatic hydrocarbon includes: contacting a component containing heavy aromatic hydrocarbon with a heavy aromatic selective hydrogenation catalyst to perform hydrogenation saturation and cracking reaction of heavy aromatic hydrocarbon, and realize lightening of heavy aromatic hydrocarbon; wherein the heavy aromatic selective hydrogenation catalyst includes a metal active component, a carrier supporting the metal active component, and a molecular sieve as a lightening component, the carrier is mainly formed by mixing modified fullerene and aluminum hydroxide dry gel powder, and the metal active component includes metal oxide; the specific surface area of the heavy aromatic selective hydrogenation catalyst is 260-600 m 2 / g, and the pore volume is 0.20-0.40 ml / g.

[0006] A heavy oil catalytic cracking process for producing light and heavy aromatic hydrocarbon products (Chinese patent application number: CN201510493527.7) uses heavy oil (wax oil, residual oil and their mixture) as raw material to produce light and heavy aromatic hydrocarbon products. The heavy oil raw material is subjected to catalytic cracking reaction under the action of catalyst, and the aromatic hydrocarbon content in the light and heavy aromatic hydrocarbon products is more than 85%. The product can be obtained by subsequent selective hydrogenation and solvent extraction unit operation to obtain aromatic hydrocarbon raw material.

[0007] However, the heavy aromatic hydrocarbon derivative prepared by the prior art has high impurity content and poor separation effect, and when used as a plasticizer in automobile rubber sealing strips, it will be subject to certain application limitations. SUMMARY

[0008] The main purpose of the present application is to provide a refining method of heavy aromatic hydrocarbon derivative for automobile sealing rubber processing to overcome the shortcomings of the prior art.

[0009] To achieve the above-mentioned purpose of the application, the technical scheme adopted by the present application comprises:

[0010] The present application provides a refining method of heavy aromatic hydrocarbon derivative for automobile sealing rubber processing, and the operation steps are as follows:

[0011] Step 1: The raw material is sent to the bottom heat exchange system of extraction column 1, extraction column 2 and extraction column 3 through a flow meter for heat exchange, and then sent to the reaction column after heat exchange. The raw material at the bottom is heated to 360-400℃ by a heating furnace and then sent to a vacuum extraction column for cutting. According to the temperature gradient of the vacuum extraction column, the first extraction line fraction, the second extraction line fraction, the third extraction line fraction and the bottom oil are cut out respectively. The bottom oil and the raw material are cooled to 100-150℃ after heat exchange and then enter the product tank area;

[0012] Step 2: The first extraction line is cooled to 50-70℃, the second extraction line is heat exchanged to 100-150℃, and the third extraction line is heat exchanged to 100-150℃, and then respectively enters the corresponding extraction column for extraction. The heavy material at the bottom is condensed to 90-110℃ and then enters the product tank area. The solvent is injected into the extraction column through the flow meter and the regulating valve, and the solvent and the fuel oil mixed component are discharged from the top of the extraction column and then sent to the corresponding solvent separation column for warming and separation. The solvent at the top is condensed and then recovered to the recovery tank for recycling. The heavy aromatic hydrocarbon derivative at the bottom is cooled after being combined and then sent to the product tank area.

[0013] As a further supplement to the above technical scheme, the flow rate of the raw fuel oil is 45-55t / h, and the temperature after heat exchange is controlled at 220-280℃.

[0014] As a further supplement to the above technical scheme, the pressure in the vacuum extraction column is maintained at -92 to -99kPa.

[0015] As a further supplement of the above technical scheme, the flow of the first line is 1-5 t / h, and the solvent addition amount is 2-10 t / h; the flow of the second line is 5-20 t / h, and the solvent addition amount is 10-25 t / h; the flow of the third line is 2-10 t / h, and the solvent addition amount is 5-15 t / h.

[0016] As a further supplement of the above technical scheme, the tower top solvent is condensed to 50-70 DEG C.

[0017] As a further supplement of the above technical scheme, the heavy aromatic hydrocarbon derivative material is condensed to 70-100 DEG C after being combined.

[0018] As a further supplement of the above technical scheme, the solvent is a mixture of furfural, N-methyl pyrrolidone and diphenyl sulfone-based extractant, and the mass ratio of furfural, N-methyl pyrrolidone and diphenyl sulfone-based extractant is 1-4:9-11:0.005-0.03.

[0019] As a further supplement of the above technical scheme, a preparation method of the diphenyl sulfone-based extractant is provided.

[0020] According to weight parts, 40-80 parts of 1-allyl-3-butyl imidazole bis-trifluoromethanesulfonimide salt, 26-52 parts of 2,7-naphthyl dithiol, 2-6 parts of triethylamine, 200-300 parts of toluene are reacted for 30-60 minutes under stirring at 70-80 DEG C, then 0.5-3 parts of 3,4'-diamino diphenyl sulfone and 0.005-0.03 parts of 4`-amino diphenyl-18-crown-6 are added, and reacted for 30-60 minutes under stirring at 70-80 DEG C, and toluene is removed by distillation to obtain the diphenyl sulfone-based extractant.

[0021] In the production process, the tail gas is sent to a heating furnace for incineration treatment.

[0022] The reaction mechanism of the above diphenyl sulfone-based extractant is as follows:

[0023] 1-allyl-3-butyl imidazole bis-trifluoromethanesulfonimide salt and one end of 2,7-naphthyl dithiol perform allyl-mercapto addition reaction; 3,4'-diamino diphenyl sulfone and 4`-amino diphenyl-18-crown-6 perform amine-mercapto addition reaction with the excess mercapto group of 2,7-naphthyl dithiol to obtain diphenyl sulfone, naphthyl and crown ether; and the diphenyl sulfone-based extractant of bis-trifluoromethanesulfonimide salt is obviously effective in improving heavy aromatic hydrocarbon extraction effect.

[0024] Technical effect:

[0025] Compared with the prior art, the heavy aromatic hydrocarbon derivative refining method for processing automobile sealing rubber has the following remarkable effects:

[0026] 1. The butyl imidazole bis-trifluoromethyl sulfonimide salt ionic liquid contains imidazole cation and bis-trifluoromethyl sulfonimide anion, which exchanges ions with acidic groups (such as carboxyl, sulfonic acid group, etc.) in heavy aromatic hydrocarbons to form stable salts, thereby realizing extraction.

[0027] 2. The diphenyl sulfone contains benzene ring and sulfone group in its molecular structure, has high polarity and solubility, and helps to improve the extraction effect. The crown ether has a cavity formed by multiple oxygen atoms and nitrogen atoms, which can form a complex with metal ions, thereby possibly improving the extraction effect.

[0028] 3. The heavy aromatic hydrocarbon derivative can be used as a plasticizer for preparing automobile rubber sealing strips, and improves the tensile strength of the automobile rubber sealing strips. BRIEF DESCRIPTION OF DRAWINGS

[0029] Figure 1 A refining method flow chart of a heavy aromatic hydrocarbon derivative for processing automobile sealing rubber. DETAILED DESCRIPTION

[0030] In view of the deficiencies in the prior art, the present inventors have long studied and practiced to propose the technical solution of the present application, which will be further explained in the following with respect to the technical solution, its implementation process and principles.

[0031] Example 1

[0032] A refining method of a heavy aromatic hydrocarbon derivative for processing automobile sealing rubber, the operation steps of which are as follows:

[0033] Step 1: The raw material is sent to the bottom heat exchange system of extraction column 1, extraction column 2 and extraction column 3 through a flow meter for heat exchange, and then sent into a reaction column after heat exchange. The raw material at the bottom is heated to 360℃ by a heating furnace and then sent into a vacuum extraction column for cutting. According to the temperature gradient of the vacuum extraction column, the first extraction line fraction, the second extraction line fraction, the third extraction line fraction and the bottom oil are cut out. The bottom oil and the raw material are cooled to 100℃ after heat exchange and then enter the product tank area.

[0034] Step 2: The first extraction line is cooled to 50℃, the second extraction line is heat exchanged to 100℃, and the third extraction line is heat exchanged to 100℃, and then respectively enter the corresponding extraction column for extraction. The heavy material at the bottom is condensed to 90℃ and then enters the product tank area. The solvent is injected into the extraction column through a flow meter and a regulating valve, and the solvent and the fuel oil mixed components at the top of the extraction column are sent into the corresponding solvent separation column for warming and separation. The solvent at the top is condensed and then recovered to a recovery tank for recycling. The heavy aromatic hydrocarbon derivative at the bottom is cooled after being combined and then sent into the product tank area.

[0035] The flow rate of the raw fuel oil is 45t / h, and the temperature after heat exchange is controlled at 220℃.

[0036] The pressure in the tower is kept at -92 kPa

[0037] The flow rate of the first line is 1 t / h, and the solvent is added at a rate of 2 t / h; the flow rate of the second line is 5 t / h, and the solvent is added at a rate of 10 t / h; and the flow rate of the third line is 2 t / h, and the solvent is added at a rate of 5 t / h.

[0038] The solvent at the top of the tower is condensed to 50°C.

[0039] The heavy aromatic hydrocarbon derivative at the bottom of the tower is condensed to 70°C after being combined.

[0040] The solvent is a mixture of furfural, N-methylpyrrolidone, and diphenyl sulfone-based extractant, with a mass ratio of furfural:N-methylpyrrolidone:diphenyl sulfone-based extractant = 1:9:0.005.

[0041] A preparation method of a diphenyl sulfone-based extractant:

[0042] 40 kg of 1-allyl-3-butylimidazole bistrifluoromethanesulfonimide salt, 26 kg of 2,7-naphthyl dithiol, 2 kg of triethylamine, 200 kg of toluene, are stirred at 70°C for 30 minutes, then 0.5 kg of 3,4'-diaminodiphenyl sulfone and 0.005 kg of 4`-aminodibenzo-18-crown-6 are added, and stirred at 70°C for 30 minutes. The toluene is removed by distillation to obtain the diphenyl sulfone-based extractant.

[0043] Example 2

[0044] A refining method of heavy aromatic hydrocarbon derivatives for processing of automobile sealing rubber, the operation steps of which are as follows:

[0045] Step 1: The raw material is sent to the heat exchange system at the bottom of the extraction tower 1, extraction tower 2, and extraction tower 3 through a flow meter for heat exchange, and then sent to the reaction tower. The raw material at the bottom is heated to 380°C by a heating furnace and sent to the vacuum extraction tower for cutting. According to the temperature gradient of the vacuum extraction tower, the first line fraction, the second line fraction, the third line fraction, and the bottom oil are cut out. The bottom oil and the raw material are cooled to 120°C after heat exchange and then sent to the product tank area.

[0046] Step 2: The first line is cooled to 60°C, the second line is heat exchanged to 120°C, and the third line is heat exchanged to 120°C, respectively, and then sent to the corresponding extraction tower for extraction. The heavy material at the bottom is cooled to 100°C and then sent to the product tank area. The solvent is injected into the extraction tower through a flow meter and a regulating valve. The solvent at the top of the extraction tower is mixed with the fuel oil component and sent to the corresponding solvent separation tower for warming and separation. The solvent at the top is condensed and then recovered to the recovery tank for recycling. The heavy aromatic hydrocarbon derivative at the bottom is cooled after being combined and then sent to the product tank area.

[0047] The flow rate of the raw fuel oil is 50 t / h, and the temperature after heat exchange is controlled at 240℃.

[0048] The pressure in the vacuum extraction column is kept at -94 kPa

[0049] The flow rate of the first extraction line is 2 t / h, and the solvent addition amount is 4 t / h; the flow rate of the second extraction line is 10 t / h, and the solvent addition amount is 15 t / h; the flow rate of the third extraction line is 5 t / h, and the solvent addition amount is 10 t / h.

[0050] The overhead solvent is condensed to 60℃.

[0051] The heavy aromatic hydrocarbon derivative at the bottom of the column is condensed to 80℃ after being combined.

[0052] The solvent is a mixture of furfural, N-methylpyrrolidone, and diphenyl sulfone-based extractant, with a mass ratio of furfural:N-methylpyrrolidone:diphenyl sulfone-based extractant = 2:10:0.01.

[0053] A preparation method of a diphenyl sulfone-based extractant is provided:

[0054] 55 kg of 1-allyl-3-butylimidazole bistrifluoromethanesulfonimide salt, 34 kg of 2,7-naphthyl dithiol, 3 kg of triethylamine, 225 kg of toluene, are stirred at 75℃ for 40 minutes, then 1.5 kg of 3,4'-diaminodiphenyl sulfone and 0.02 kg of 4`-aminodibenzo-18-crown-6 are added, and stirred at 75℃ for 40 minutes. Toluene is removed by distillation to obtain a diphenyl sulfone-based extractant.

[0055] Example 3

[0056] A refining method of heavy aromatic hydrocarbon derivatives for processing of automobile sealing rubber, the operation steps are:

[0057] Step 1: The raw material is sent to the bottom heat exchange system of extraction column 1, extraction column 2, and extraction column 3 through a flow meter for heat exchange, and then sent to the reaction column. The raw material at the bottom is heated to 380℃ by a heating furnace and sent to the vacuum extraction column for cutting. According to the temperature gradient of the vacuum extraction column, the first extraction line fraction, the second extraction line fraction, the third extraction line fraction, and the bottom oil are cut out. The bottom oil and the raw material after heat exchange are condensed to 140℃ and then enter the product tank area.

[0058] Step 2: The first line is extracted and cooled to 60℃, the second line is extracted and heat exchanged to 140℃, and the third line is extracted and heat exchanged to 140℃, respectively, into the corresponding extraction tower for extraction. The heavy material at the bottom of the tower is condensed to 100℃ and then enters the product tank area. The solvent is injected into the extraction tower through the flow meter and adjusting valve, and the solvent and fuel oil mixed components at the top of the extraction tower are sent into the corresponding solvent separation tower for warming and separation. The solvent at the top is condensed and recovered to the recovery tank for recycling. The heavy aromatic hydrocarbon derivative at the bottom of the tower is condensed and cooled after being combined, and then sent into the product tank area.

[0059] The flow rate of the raw fuel oil is 55t / h, and the temperature after heat exchange is controlled at 280℃.

[0060] The pressure in the vacuum extraction tower is maintained at -97kPa.

[0061] The flow rate of the first line is 4t / h, and the solvent addition amount is 8t / h. The flow rate of the second line is 15t / h, and the solvent addition amount is 20t / h. The flow rate of the third line is 8t / h, and the solvent addition amount is 10t / h.

[0062] The solvent at the top is condensed to 60℃.

[0063] The heavy aromatic hydrocarbon derivative at the bottom of the tower is condensed and cooled to 90℃ after being combined.

[0064] The solvent is a mixture of furfural, N-methyl pyrrolidone, and diphenyl sulfone-based extractant, with a mass ratio of furfural:N-methyl pyrrolidone:diphenyl sulfone-based extractant = 3:10:0.02.

[0065] A preparation method of a diphenyl sulfone-based extractant is provided:

[0066] 80kg of 1-allyl-3-butylimidazole bistrifluoromethanesulfonylimide salt, 44kg of 2,7-naphthyl dithiol, 5kg of triethylamine, 275kg of toluene, are stirred at 75℃ for 50 minutes, then 2kg of 3,4'-diaminodiphenyl sulfone and 0.02kg of 4`-aminodibenzo-18-crown-6 are added, and stirred at 75℃ for 50 minutes. Distill off the toluene to obtain the diphenyl sulfone-based extractant.

[0067] Example 4

[0068] A refining method of heavy aromatic hydrocarbon derivatives for processing of automobile sealing rubber, the operation steps of which are as follows:

[0069] Step 1: The raw material is sent to the bottom heat exchange system of extraction column 1, extraction column 2 and extraction column 3 through a flow meter for heat exchange, and then sent to the reaction column. The raw material at the bottom is heated to 400℃ by a heating furnace and then sent to the vacuum extraction column for cutting. According to the temperature gradient of the vacuum extraction column, the first extraction line fraction, the second extraction line fraction, the third extraction line fraction and the bottom oil are cut off respectively. The bottom oil and the raw material are heat exchanged and then condensed to 150℃ and sent to the product tank area.

[0070] Step 2: The first extraction line is cooled to 70℃, the second extraction line is heat exchanged to 150℃, and the third extraction line is heat exchanged to 150℃, and then respectively sent to the corresponding extraction column for extraction. The heavy material at the bottom is condensed to 110℃ and then sent to the product tank area. The solvent is injected into the extraction column through the flow meter and the regulating valve. The solvent at the top of the extraction column is mixed with the fuel oil mixture and then sent to the corresponding solvent separation column for warming and separation. The solvent at the top is condensed and then recovered to the recovery tank for recycling. The heavy aromatic hydrocarbon derivative at the bottom is cooled after being combined and then sent to the product tank area.

[0071] The flow rate of the raw material fuel oil is 55t / h, and the temperature after heat exchange is controlled at 280℃.

[0072] The pressure in the vacuum extraction column is maintained at -99kPa.

[0073] The flow rate of the first extraction line is 5t / h, and the solvent is added at a rate of 10t / h. The flow rate of the second extraction line is 20t / h, and the solvent is added at a rate of 25t / h. The flow rate of the third extraction line is 10t / h, and the solvent is added at a rate of 15t / h.

[0074] The solvent at the top is condensed to 70℃.

[0075] The heavy aromatic hydrocarbon derivative at the bottom is cooled after being combined to 100℃.

[0076] The solvent is a mixture of furfural, N-methyl pyrrolidone and diphenyl sulfone-based extractant, and the mass ratio is furfural:N-methyl pyrrolidone:diphenyl sulfone-based extractant=4:11:0.03.

[0077] A preparation method of a diphenyl sulfone-based extractant is provided.

[0078] 80kg of 1-allyl-3-butylimidazole bistrifluoromethanesulfonylimide salt, 52kg of 2,7-naphthyl dithiol, 6kg of triethylamine, 300kg of toluene, are stirred at 80℃ for 60 minutes, then 3kg of 3,4'-diaminodiphenyl sulfone and 0.03kg of 4`-aminodibenzo-18-crown-6 are added, and stirred at 80℃ for 60 minutes. Distill off the toluene to obtain the diphenyl sulfone-based extractant.

[0079] Example 5

[0080] The automobile rubber sealing strip formula prepared by using examples 1-4 is as follows:

[0081] The EPDM raw rubber (4770) 6kg, EPDM raw rubber (4570) 3kg, N-550 carbon black 18kg, calcium carbonate 10kg, paraffin oil 8kg, heavy aromatic hydrocarbon derivative 4kg, zinc oxide 0.4kg, stearic acid 0.1kg, polyethylene glycol 0.2kg, the pressure is 0.4MPa, the temperature is raised to 80℃, the pressure is reduced to 0.1MPa, then the calcium oxide 1.2kg, sulfur 0.12kg, accelerator M 0.03kg, accelerator ETU 0.09kg, accelerator ZDBC 0.3kg, anti-scorching agent E-800.07kg are put in, mixed and milled for 5min, the temperature is raised to 110℃, the system is automatically discharged, the reaction is carried out for 100 seconds at 70℃ in the mixer, and the required product is obtained.

[0082] The hydrocarbon component before and after extraction in example 1 of the present application is analyzed, the analysis method is SH / T0659-1998, and the results are shown in the table.

[0083]

[0084]

[0085] The detection data of the automobile rubber sealing strip prepared by using examples 1-4 are as follows

[0086] Tensile strength MPa Tear elongation % Compression set % Example 1 10.54 325 20.5 Example 2 12.34 340 16.4 Example 3 11.98 333 17.3 Example 4 12.55 342 15.8

[0087] As can be seen from the above implementation method, the rubber prepared by using the heavy aromatic hydrocarbon prepared by the method has excellent mechanical properties and compression permanent deformation, and can be applied to automobile rubber sealing strips.

[0088] It should be understood that the above examples are only for illustrating the technical concept and characteristics of the present application, the purpose is to enable those skilled in the art to understand the content of the present application and to implement it, and it cannot limit the protection scope of the present application. Any equivalent changes or modifications made according to the spirit and essence of the present application should be covered within the protection scope of the present application.

Claims

1. A method for refining heavy aromatic hydrocarbon derivatives for processing automobile sealing rubber, comprising the following steps: Step 1: the raw material is sent to the bottom heat exchange system of extraction column 1, extraction column 2 and extraction column 3 through a flow meter, and then sent to a reaction column after heat exchange, the bottom material is heated to 360-400℃ by a heating furnace, and then sent to a vacuum extraction column for cutting, and according to the temperature gradient of the vacuum extraction column, extraction 1, extraction 2, extraction 3 and bottom oil are cut out, respectively, the bottom oil and the raw material are cooled to 100-150℃ after heat exchange, and then sent to a product tank area; Step 2: extraction 1 is cooled to 50-70℃, extraction 2 is heat exchanged to 100-150℃, and extraction 3 is heat exchanged to 100-150℃, and then sent to the corresponding extraction column for extraction, the bottom heavy material is cooled to 90-110℃, and then sent to the product tank area, the solvent is injected into the extraction column through a flow meter and a regulating valve, the solvent at the top of the extraction column is mixed with fuel oil components, and then sent to the corresponding solvent separation column for warming and separation, the solvent at the top is cooled and recovered to a recovery tank, and then recycled, and the heavy aromatic hydrocarbon derivative at the bottom is cooled after being combined, and then sent to the product tank area. The solvent is a mixture of furfural, N-methyl pyrrolidone and diphenyl sulfone-based extractant, and the mass ratio of furfural, N-methyl pyrrolidone and diphenyl sulfone-based extractant is 1-4:9-11:0.005-0.

03. The preparation method of the diphenyl sulfone-based extractant comprises the following steps: 40-80 parts of 1-allyl-3-butyl imidazole bis-trifluoromethanesulfonylimide salt, 26-52 parts of 2,7-naphthyl dithiol, 2-6 parts of triethylamine, 200-300 parts of toluene are stirred at 70-80℃ for 30-60 minutes, 0.5-3 parts of 3,4'-diamino diphenyl sulfone and 0.005-0.03 parts of 4'-amino biphenyl-18-crown-6 are added, and then stirred at 70-80℃ for 30-60 minutes, and toluene is removed by distillation to obtain the diphenyl sulfone-based extractant. The flow rate of the raw fuel oil is 45-55t / h, and the temperature after heat exchange is controlled at 220-280℃. The pressure in the tower of the vacuum extraction column is kept at -92 to -99kPa. The flow rate of extraction 1 is 1-5t / h, and the amount of solvent added is 2-10t / h; the flow rate of extraction 2 is 5-20t / h, and the amount of solvent added is 10-25t / h; the flow rate of extraction 3 is 2-10t / h, and the amount of solvent added is 5-15t / h.

2. The method for refining heavy aromatic hydrocarbon derivatives for processing of automobile sealing rubber according to claim 1, characterized in that: The solvent at the top is cooled to 50-70℃.

3. The refining method for heavy aromatic hydrocarbon derivatives used in automotive sealing rubber processing according to claim 1, characterized in that: The heavy aromatic hydrocarbon derivative at the bottom is cooled to 70-100℃ after being combined.

4. The method of claim 1, wherein the heavy aromatic hydrocarbon derivative is refined by the process of claim 1. The tail gas generated in the production process is sent to a heating furnace for incineration.

5. The refining method for heavy aromatic hydrocarbon derivatives used in automotive sealing rubber processing according to claim 1, characterized in that: ​ 6. The method of claim 1, wherein the heavy aromatic hydrocarbon derivative is a heavy aromatic hydrocarbon derivative of a car sealant rubber processing. ​ 7. The method of claim 1, wherein the heavy aromatic hydrocarbon derivative is a heavy aromatic hydrocarbon derivative of a car sealant rubber processing. ​

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