A preparation method of a heavy aromatic hydrocarbon derivative with low metal impurities

Abstract

The present invention discloses a preparation method of a heavy aromatic hydrocarbon derivative with low metal impurities, which relates to the field of petroleum processing. Specifically, after the raw material is heated and pressurized, it is transported to the first extraction, second extraction, third extraction, and bottom extraction heat exchange systems through a raw material flowmeter for heat exchange. After heat exchange, the raw material enters the reaction tower to remove the water contained in the raw material. The raw material at the bottom of the reaction tower is heated by a heating furnace and sent to a vacuum extraction tower for cutting. The injection of a solvent and an impurity adsorbent into the extraction tower is controlled by a flowmeter and a regulating valve. Finally, a mixed liquid of a solvent with a very low aromatic hydrocarbon content and light fuel oil is obtained at the top of the tower, and a mixed liquid of a solvent with a very high aromatic hydrocarbon content and aromatic hydrocarbons is obtained at the bottom of the tower, so as to separate aromatic hydrocarbons and non-aromatic hydrocarbons. The separation effect of the present invention is excellent, and metal impurities in heavy aromatic hydrocarbons can be significantly removed.

Description

Technical Field

[0001] The present invention relates to the field of petroleum processing, and in particular to a method for preparing heavy aromatic hydrocarbon derivatives with low metal impurities. Background Art

[0002] The rapid development of the world petrochemical industry has accelerated the development of aromatic hydrocarbon production technology. The separation and production technology of aromatic hydrocarbons is an indispensable step in aromatic hydrocarbon production. At present, the main raw materials for producing aromatic hydrocarbons are reformate and pyrolysis gasoline. The main methods for producing aromatic hydrocarbons can be divided into two categories according to the process route principle: aromatic hydrocarbon extraction and extractive distillation. Generally speaking, if the raw material fraction is narrow and the aromatic hydrocarbon content is high, the extractive distillation process is suitable; if the fraction is wide and the aromatic hydrocarbon content is low, the aromatic hydrocarbon extraction process is suitable.

[0003] Chinese Patent CN114437818B: A method for processing heavy aromatic hydrocarbon oil, including distilling heavy aromatic hydrocarbon oil into a light fraction and a heavy fraction, extracting the heavy fraction with a part of BTX benzene, toluene, and xylene and a light toluene fraction to obtain a poor aromatic component and a rich aromatic component, further distilling the rich aromatic component to separate out a light toluene fraction and a heavy toluene fraction, sending the heavy toluene fraction and the light fraction together for hydrofining, and sending the hydrogenation product and the poor aromatic component together into a hydrocracking reactor for further hydrocracking reaction. The cracked product is distilled to obtain C1-C4, BTX benzene, toluene, and xylene, a small amount of diesel products, and unconverted oil.

[0004] Chinese Patent CN111500316B: A method for preparing heavy aromatic hydrocarbons by extractive distillation, including the following steps: In the extractive distillation column, the light fuel oil and heavy aromatic hydrocarbons in the mixed material vaporize continuously from light to heavy according to the molecular weight. The light fuel oil and heavy aromatic hydrocarbon products in the mixed material start to separate and distill out. Then, the light fuel oil and heavy aromatic hydrocarbons are respectively sent to their respective product tanks by pumps. The light raw material flowing out from the top of the extractive distillation column is subjected to product separation and solvent recovery. After entering the product separation system, a vertical vacuum pump is started to evacuate; the distilled oil is cooled by a heat exchanger and a condenser and then flows into the light fuel oil product intermediate tank, the heavy aromatic hydrocarbon product intermediate tank, and the solvent intermediate tank. Then, the light fuel oil and heavy aromatic hydrocarbons are respectively sent to their respective product tanks by pumps, and the solvent is sent back to the solvent tank for repeated use. The heavy raw material is further heated by a heat exchanger with the side-line product and then transported to a heating furnace for heating and enters the extractive distillation column. The material is sent to each product tank.

[0005] Chinese Patent CN112295607B: A processing method for heavy aromatics lightening and a heavy aromatics selective hydrogenation catalyst. The processing method for heavy aromatics lightening includes: contacting a component containing heavy aromatics with a heavy aromatics selective hydrogenation catalyst to carry out hydrogenation saturation and cracking reactions of the heavy aromatics, so as to realize the lightening of the heavy aromatics; wherein, the heavy aromatics 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, the metal active component includes a metal oxide; the specific surface area of the heavy aromatics selective hydrogenation catalyst is 260-600m 2 / g, and the pore volume is 0.20-0.40 ml / g.

[0006] The above-mentioned patent and the prior art process flow are cumbersome, the operating conditions are harsh, the separation effect is not ideal, the energy consumption is high, the cost is relatively high, etc.; in addition, more importantly, the content of metal impurities in heavy aromatics is relatively high and difficult to remove, resulting in limited product applications. Summary of the Invention

[0007] The main object of the present invention is to provide a preparation method for heavy aromatics derivatives with low metal impurities to overcome the deficiencies in the prior art.

[0008] Another object of the present invention is also to provide an impurity adsorbent and a preparation method thereof.

[0009] To achieve the foregoing invention objects, the technical solutions adopted by the present invention include:

[0010] An embodiment of the present invention provides a preparation method for heavy aromatics derivatives with low metal impurities, which includes:

[0011] A preparation method for heavy aromatics derivatives with low metal impurities, and its operation steps are as follows:

[0012] A1: The raw fuel oil is transported to the bottom heat exchange systems of Extraction Tower 1, Extraction Tower 2, and Extraction Tower 3 through a raw material flowmeter for heat exchange, and after heat exchange, it is sent to a reaction tower to remove the moisture in the raw material. The raw material at the bottom of the reaction tower is heated by a heating furnace and then sent to a vacuum extraction tower for cutting. According to the temperature gradient of the vacuum extraction tower, extraction line 1 fraction, extraction line 2 fraction, extraction line 3 fraction, and bottom tower oil are cut out respectively;

[0013] A2: Extraction line 1 is cooled to 50-70 °C, extraction line 2 is heat exchanged to 100-150 °C, and extraction line 3 is heat exchanged to 100-150 °C and then enter the corresponding extraction towers for extraction respectively. The injection of solvent and impurity adsorbent into the extraction towers is controlled by a flowmeter and a regulating valve. After filtration, the heavy material at the bottom of the tower is heat exchanged with the raw material and then condensed to 90-110 °C and sent to the finished product tank area;

[0014] A3: The solvent and fuel oil mixed components discharged from the extraction tower top are respectively sent to the corresponding solvent separation towers for heating and separation. After the solvent at the tower top is condensed, it is recovered into the recovery tank and recycled. The heavy aromatic hydrocarbon derivative materials at the tower bottom are condensed and cooled after being merged and then sent to the finished product tank area;

[0015] A4: All the tail gases generated during the production process are sent to the heating furnace for incineration treatment.

[0016] Further, the flow rate of the raw material fuel oil is 50 - 60 t / h, and the temperature after heat exchange is controlled at 200 - 280 °C.

[0017] Further, the heating furnace is heated to 360 - 400 °C.

[0018] Further, the pressure inside the vacuum extraction tower is maintained at -95 to -99 kPa.

[0019] Further, the flow rate of the first extraction line is 2 - 5 t / h, and the solvent addition amount is 3 - 10 t / h; the flow rate of the second extraction line is 8 - 20 t / h, and the solvent addition amount is 10 - 25 t / h; the flow rate of the third extraction line is 3 - 10 t / h, and the solvent addition amount is 5 - 15 t / h.

[0020] Further, the solvent at the tower top is condensed to 50 - 70 °C.

[0021] Further, the heavy aromatic hydrocarbon derivative materials at the tower bottom are condensed and cooled to 70 - 100 °C after being merged.

[0022] Further, the solvent is a mixture of furfural and N-methylpyrrolidone, and the mass ratio is furfural:N-methylpyrrolidone = 1 - 9:9.

[0023] Further, the addition amount of the impurity adsorbent is 1 - 4% of the total mass of the solvent, and its preparation method is as follows:

[0024] B1: Copolymerization

[0025] By weight, 100 - 130 parts of styrene, 5 - 10 parts of 4,4'-divinyl-2,2'-bipyridine, 0.05 - 0.5 part of 5,10,15,20-tetrakis(4-vinylphenyl)porphyrin, 2 - 4 parts of benzoyl peroxide, 6 - 10 parts of paraffin wax, and 1000 - 1300 parts of toluene are placed in a stirring kettle, and the gas is replaced by introducing nitrogen. The stirring reaction is carried out at 80 - 100 °C for 10 - 15 h. After the reaction is completed, filtration, washing, and drying are carried out to obtain the precursor;

[0026] B2: Wax extraction and pore formation

[0027] Place 100 - 130 parts of the precursor and 1000 - 1300 parts of solvent oil in a stirring kettle, and carry out a stirring reaction at 100 - 120 °C for 3 - 6 h. After the reaction, filter, wash, and dry to obtain a microporous impurity adsorbent.

[0028] The reaction mechanism of the adsorbent is as follows:

[0029] Styrene undergoes a cross - linking polymerization reaction with cross - linking agents 4,4'-divinyl - 2,2'-bipyridine and 5,10,15,20 - tetra(4 - vinylphenyl)porphyrin, and then the paraffin is dissolved out through pore formation to form a microporous structure, obtaining an impurity adsorbent.

[0030] Technical effects:

[0031] Both the bipyridine and phenylporphyrin groups of the impurity adsorbent have a large surface area and a special pore structure, which can effectively adsorb metal impurities in heavy aromatics, form coordination bonds with metal ions, and thus adsorb metal ions on the surface. In addition, these two adsorbents also have high chemical stability and thermal stability, can work under higher temperature and pressure conditions, thereby improving the adsorption effect. Description of the drawings

[0032] Figure 1 It is a flow chart of the preparation method of a low - metal - impurity heavy - aromatic hydrocarbon derivative of the present invention. Detailed implementation manners

[0033] In view of the deficiencies in the prior art, the inventor of this case has proposed the technical solution of the present invention through long - term research and a large number of practices. The following will further explain the technical solution, its implementation process, principles, etc.

[0034] In the embodiments of the present invention, the hydrocarbon component analysis method adopts SH / T0659 - 1998.

[0035] Example 1

[0036] A preparation method of a low - metal - impurity heavy - aromatic hydrocarbon derivative, and its operation steps are as follows:

[0037] A1: The raw fuel oil is transported through a raw material flowmeter to the bottom heat - exchange systems of Extraction Tower 1, Extraction Tower 2, and Extraction Tower 3 for heat exchange, and then sent to the reaction tower after heat exchange to remove the moisture in the raw material. The raw material at the bottom of the reaction tower is heated by a heating furnace and then sent to a vacuum extraction tower for cutting. According to the temperature gradient of the vacuum extraction tower, extraction line 1 fraction, extraction line 2 fraction, extraction line 3 fraction, and bottom tower oil are cut out respectively;

[0038] A2: The first extraction line is cooled to 50°C, the second extraction line is heat-exchanged to 100°C, and the third extraction line is heat-exchanged to 100°C and then enter the corresponding extraction towers for extraction respectively. The injection of solvent and impurity adsorbent into the extraction towers is controlled by flow meters and regulating valves. After filtration, the heavy materials at the bottom of the tower are heat-exchanged with the raw materials and then condensed to 90°C and enter the finished product tank area.

[0039] A3: The mixed components of solvent and fuel oil are taken out from the top of the extraction tower and sent to the corresponding solvent separation towers for heating and separation respectively. The solvent at the top of the tower is condensed and then recycled to the recovery tank for recycling use. The heavy aromatic hydrocarbon derivative materials at the bottom of the tower are merged and then condensed and cooled down and sent to the finished product tank area.

[0040] A4: All the tail gases generated during the production process are sent to the heating furnace for incineration treatment.

[0041] The flow rate of the raw material fuel oil is 50 t / h, and the temperature after heat exchange is controlled at 200°C.

[0042] The heating furnace is heated up to 360°C.

[0043] The pressure inside the vacuum extraction tower is maintained at -95 kPa.

[0044] The flow rate of the first extraction line is 2 t / h, and the solvent addition amount is 3 t / h; the flow rate of the second extraction line is 8 t / h, and the solvent addition amount is 10 t / h; the flow rate of the third extraction line is 3 t / h, and the solvent addition amount is 5 t / h.

[0045] The solvent at the top of the tower is condensed to 50°C.

[0046] The heavy aromatic hydrocarbon derivative materials at the bottom of the tower are merged and then condensed and cooled down to 70°C.

[0047] The solvent is a mixture of furfural and N-methylpyrrolidone, and the mass ratio is furfural:N-methylpyrrolidone = 1:9.

[0048] The addition amount of the impurity adsorbent is 1% of the total mass of the solvent, and its preparation method is as follows:

[0049] B1: Copolymerization

[0050] 100 kg of styrene, 5 kg of 4,4'-divinyl-2,2'-bipyridine, 0.1 kg of 5,10,15,20-tetrakis(4-vinylphenyl)porphyrin, 2 kg of benzoyl peroxide, 6 kg of paraffin, and 1000 kg of toluene are placed in a stirring kettle, and the gas is replaced by introducing nitrogen. The stirring reaction is carried out at 80°C for 10 h. After the reaction is completed, filtration, washing, and drying are carried out to obtain the precursor.

[0051] B2: Wax extraction and pore formation

[0052] Place 100 kg of the precursor and 1000 kg of solvent oil in a stirring kettle, carry out a stirring reaction at 100 °C for 3 h, filter, wash, and dry after the reaction to obtain a microporous impurity adsorbent.

[0053] Example 2

[0054] A preparation method of a heavy aromatics derivative with low metal impurities, the operation steps are as follows:

[0055] A1: The raw fuel oil is transported to the bottom heat exchange systems of Extraction Tower 1, Extraction Tower 2, and Extraction Tower 3 through a raw material flowmeter for heat exchange, and then sent to a reaction tower after heat exchange to remove the moisture in the raw material. The raw material at the bottom of the reaction tower is heated by a heating furnace and then sent to a vacuum extraction tower for cutting. According to the temperature gradient of the vacuum extraction tower, the extraction first-line fraction, extraction second-line fraction, extraction third-line fraction, and bottom tower oil are cut out respectively;

[0056] A2: The extraction first-line is cooled to 60 °C, the extraction second-line is heat-exchanged to 125 °C, and the extraction third-line is heat-exchanged to 125 °C and then enter the corresponding extraction towers for extraction respectively. The injection of the solvent and the impurity adsorbent into the extraction towers is controlled through a flowmeter and a regulating valve. After filtration, the heavy material at the bottom of the tower is heat-exchanged with the raw material and then condensed to 100 °C and sent to the finished product tank area;

[0057] A3: The solvent and fuel oil mixed components discharged from the top of the extraction tower are sent to the corresponding solvent separation towers for heating and separation respectively. The solvent at the top of the tower is condensed and recycled to the recovery tank for recycling, and the heavy aromatics derivative material at the bottom of the tower is condensed and cooled after being merged and then sent to the finished product tank area;

[0058] A4: All the tail gases generated during the production process are sent to the heating furnace for incineration treatment.

[0059] The flow rate of the raw fuel oil is 55 t / h, and the temperature after heat exchange is controlled at 220 °C.

[0060] The heating furnace is heated to 380 °C.

[0061] The pressure inside the vacuum extraction tower is maintained at -96 kPa.

[0062] The flow rate of the extraction first-line is 3 t / h, and the solvent addition amount is 5 t / h; the flow rate of the extraction second-line is 12 t / h, and the solvent addition amount is 16 t / h; the flow rate of the extraction third-line is 5 t / h, and the solvent addition amount is 8 t / h.

[0063] The solvent at the top of the tower is condensed to 55 °C.

[0064] The heavy aromatics derivative material at the bottom of the tower is condensed and cooled to 80 °C after being merged.

[0065] The solvent is a mixture of furfural and N-methylpyrrolidone, and the mass ratio is furfural:N-methylpyrrolidone = 3:9.

[0066] The addition amount of the impurity adsorbent is 2% of the total mass of the solvent, and its preparation method is as follows:

[0067] B1: Copolymerization

[0068] 110 kg of styrene, 7 kg of 4,4'-divinyl-2,2'-bipyridine, 0.25 kg of 5,10,15,20-tetrakis(4-vinylphenyl)porphyrin, 3 kg of benzoyl peroxide, 8 kg of paraffin wax, and 1100 kg of toluene are placed in a stirring kettle, and nitrogen is introduced to displace the gas. Stirring reaction is carried out at 90 °C for 12 h. After the reaction, filtration, washing, and drying are carried out to obtain a precursor;

[0069] B2: Wax extraction for pore formation

[0070] 110 kg of the precursor and 1100 kg of solvent oil are placed in a stirring kettle, and stirring reaction is carried out at 110 °C for 4 h. After the reaction, filtration, washing, and drying are carried out to obtain a microporous impurity adsorbent.

[0071] Example 3

[0072] A preparation method of a low-metal-impurity heavy aromatic hydrocarbon derivative, and its operation steps are as follows:

[0073] A1: The raw material fuel oil is transported to the bottom heat exchange systems of Extraction Tower 1, Extraction Tower 2, and Extraction Tower 3 through a raw material flowmeter for heat exchange, and then sent to a reaction tower after heat exchange to remove the moisture in the raw material. The raw material at the bottom of the reaction tower is heated by a heating furnace and then sent to a vacuum extraction tower for cutting. According to the temperature gradient of the vacuum extraction tower, extraction line 1 fraction, extraction line 2 fraction, extraction line 3 fraction, and bottom tower oil are cut out respectively;

[0074] A2: Extraction line 1 is cooled to 60 °C, extraction line 2 is heat-exchanged to 150 °C, and extraction line 3 is heat-exchanged to 150 °C and then enter the corresponding extraction towers for extraction respectively. The injection of the solvent and the impurity adsorbent into the extraction towers is controlled through a flowmeter and a regulating valve. After filtration, the heavy material at the bottom of the tower is heat-exchanged with the raw material and then condensed to 100 °C and sent to the finished product tank area;

[0075] A3: The solvent and fuel oil mixed components discharged from the top of the extraction tower are respectively sent to the corresponding solvent separation towers for heating and separation. The solvent at the top of the tower is condensed and then recycled to the recovery tank for recycling. The heavy aromatic hydrocarbon derivative material at the bottom of the tower is combined and then condensed and cooled and sent to the finished product tank area;

[0076] A4: All the tail gases generated during the production process are sent to the heating furnace for incineration treatment.

[0077] The flow rate of the raw material fuel oil is 55 t / h, and the temperature after heat exchange is controlled at 240 °C.

[0078] The heating furnace is heated to 380 °C.

[0079] The pressure inside the described vacuum extraction tower is maintained at -98 kPa.

[0080] The flow rate of the first extraction line is 4 t / h, and the solvent addition amount is 8 t / h; the flow rate of the second extraction line is 14 t / h, and the solvent addition amount is 20 t / h; the flow rate of the third extraction line is 8 t / h, and the solvent addition amount is 12 t / h.

[0081] The solvent at the top of the tower is condensed to 60 °C.

[0082] The heavy aromatic hydrocarbon derivatives at the bottom of the tower are condensed and cooled to 80 °C after being combined.

[0083] The described solvent is a mixture of furfural and N-methylpyrrolidone, and their mass ratio is furfural:N-methylpyrrolidone = 6:9.

[0084] The addition amount of the described impurity adsorbent is 3% of the total mass of the solvent, and its preparation method is as follows:

[0085] B1: Copolymerization

[0086] 120 kg of styrene, 8 kg of 4,4'-divinyl-2,2'-bipyridine, 0.4 kg of 5,10,15,20-tetrakis(4-vinylphenyl)porphyrin, 3 kg of benzoyl peroxide, 9 kg of paraffin, and 1200 kg of toluene are placed in a stirring kettle, and the gas is replaced by introducing nitrogen. The stirring reaction is carried out at 90 °C for 13 h. After the reaction is completed, filtration, washing, and drying are carried out to obtain the precursor.

[0087] B2: Wax extraction to form pores

[0088] 120 kg of the precursor and 1200 kg of solvent oil are placed in a stirring kettle, and the stirring reaction is carried out at 115 °C for 5 h. After the reaction is completed, filtration, washing, and drying are carried out to obtain the impurity adsorbent with micropores.

[0089] Example 4

[0090] A preparation method of low-metal-impurity heavy aromatic hydrocarbon derivatives, and its operation steps are as follows:

[0091] A1: The raw fuel oil is transported to the bottom heat exchange systems of Extraction Tower 1, Extraction Tower 2, and Extraction Tower 3 through a raw material flowmeter for heat exchange, and then sent to a reaction tower after heat exchange to remove the moisture in the raw material. The raw material at the bottom of the reaction tower is heated by a heating furnace and then sent to a vacuum extraction tower for cutting. According to the temperature gradient of the vacuum extraction tower, the first extraction line fraction, the second extraction line fraction, the third extraction line fraction, and the bottom tower oil are cut out respectively.

[0092] A2: The first extraction line is cooled to 70°C, the second extraction line is heat-exchanged to 150°C, and the third extraction line is heat-exchanged to 150°C and then enter the corresponding extraction towers for extraction respectively. The injection of solvent and impurity adsorbent into the extraction towers is controlled by flow meters and regulating valves. After filtration, the heavy materials at the bottom of the tower are heat-exchanged with the raw materials and then condensed to 110°C and enter the finished product tank area;

[0093] A3: The mixed components of solvent and fuel oil are taken out from the top of the extraction tower and sent to the corresponding solvent separation towers for heating and separation respectively. The solvent at the top of the tower is condensed and then recycled to the recovery tank for recycling. The heavy aromatic hydrocarbon derivative materials at the bottom of the tower are merged and then condensed and cooled down and sent to the finished product tank area;

[0094] A4: All the tail gases generated during the production process are sent to the heating furnace for incineration treatment.

[0095] The flow rate of the raw material fuel oil is 60 t / h, and the temperature after heat exchange is controlled at 280°C.

[0096] The heating furnace is heated up to 400°C.

[0097] The pressure inside the vacuum extraction tower is maintained at -99 kPa.

[0098] The flow rate of the first extraction line is 5 t / h, and the solvent addition amount is 10 t / h; the flow rate of the second extraction line is 20 t / h, and the solvent addition amount is 25 t / h; the flow rate of the third extraction line is 10 t / h, and the solvent addition amount is 15 t / h.

[0099] The solvent at the top of the tower is condensed to 70°C.

[0100] The heavy aromatic hydrocarbon derivative materials at the bottom of the tower are merged and then condensed and cooled down to 100°C.

[0101] The solvent is a mixture of furfural and N-methylpyrrolidone, and the mass ratio is furfural:N-methylpyrrolidone = 9:9.

[0102] The addition amount of the impurity adsorbent is 4% of the total mass of the solvent, and its preparation method is:

[0103] B1: Copolymerization

[0104] 130 kg of styrene, 10 kg of 4,4'-divinyl-2,2'-bipyridine, 0.5 kg of 5,10,15,20-tetrakis(4-vinylphenyl)porphyrin, 4 kg of benzoyl peroxide, 10 kg of paraffin, and 1300 kg of toluene are placed in a stirring kettle, and the gas is replaced by introducing nitrogen. The stirring reaction is carried out at 100°C for 15 h. After the reaction is completed, filtration, washing, and drying are carried out to obtain the precursor;

[0105] B2: Wax extraction and pore formation

[0106] Place 130 kg of the precursor and 1300 kg of solvent oil in a stirring kettle, and carry out a stirring reaction at 120 °C for 6 h. After the reaction is completed, filter, wash, and dry to obtain a microporous impurity adsorbent.

[0107] Comparative Example 1

[0108] In this example, no impurity adsorbent is added, and the others are the same as in Example 1.

[0109] The test results of the above examples are as follows:

[0110]

[0111]

[0112] It should be understood that the above examples are only for illustrating the technical concept and characteristics of the present invention, and the purpose is to enable those skilled in the art to understand the content of the present invention and implement it accordingly. It is not intended to limit the protection scope of the present invention. Any equivalent changes or modifications made according to the spirit and essence of the present invention should be covered within the protection scope of the present invention.

Claims

1. A preparation method of a heavy aromatic hydrocarbon derivative with low metal impurities, the operation steps of which are as follows: A1: The raw fuel oil is transported to the bottom heat exchange systems of Extraction Tower 1, Extraction Tower 2, and Extraction Tower 3 through a raw material flowmeter for heat exchange, and after heat exchange, it is sent to a reaction tower to remove the moisture in the raw material. The raw material at the bottom of the reaction tower is heated by a heating furnace and then sent to a vacuum extraction tower for cutting. According to the temperature gradient of the vacuum extraction tower, extraction line 1 fraction, extraction line 2 fraction, extraction line 3 fraction, and bottom tower oil are cut out respectively; A2: Extraction line 1 is cooled to 50 - 70 °C, extraction line 2 is heat-exchanged to 100 - 150 °C, and extraction line 3 is heat-exchanged to 100 - 150 °C and then enter the corresponding extraction towers for extraction. The injection of solvent and impurity adsorbent into the extraction towers is controlled by a flowmeter and a regulating valve. After filtration, the heavy material at the bottom of the tower is heat-exchanged with the raw material and then condensed to 90 - 110 °C and sent to the finished product tank area; A3: The mixed component of solvent and fuel oil is taken out from the top of the extraction tower and sent to the corresponding solvent separation tower for heating and separation. The solvent at the top of the tower is condensed and recycled to the recovery tank for recycling, and the heavy aromatic hydrocarbon derivative material at the bottom of the tower is condensed and cooled after being combined and then sent to the finished product tank area; A4: All the tail gas generated during the production process is sent to the heating furnace for incineration treatment; The addition amount of the impurity adsorbent is 1 - 4% of the total mass of the solvent, and its preparation method is as follows: B1: Copolymerization By weight, 100 - 130 parts of styrene, 5 - 10 parts of 4,4'-divinyl-2,2'-bipyridine, 0.05 - 0.5 parts of 5,10,15,20-tetrakis(4-vinylphenyl)porphyrin, 2 - 4 parts of benzoyl peroxide, 6 - 10 parts of paraffin, and 1000 - 1300 parts of toluene are placed in a stirring kettle, and the gas is replaced by introducing nitrogen. Stirring reaction is carried out at 80 - 100 °C for 10 - 15 h. After the reaction, filtration, washing, and drying are carried out to obtain a precursor; B2: Wax extraction for pore formation 100 - 130 parts of the precursor and 1000 - 1300 parts of solvent oil are placed in a stirring kettle, and stirring reaction is carried out at 100 - 120 °C for 3 - 6 h. After the reaction, filtration, washing, and drying are carried out to obtain an impurity adsorbent with micropores.

2. The preparation method of a heavy aromatic hydrocarbon derivative with low metal impurities according to claim 1, characterized in that: The flow rate of the raw material fuel oil is 50 - 60 t / h, and the temperature after heat exchange is controlled at 200 - 280 °C.

3. The preparation method of a low-metal impurity heavy aromatic hydrocarbon derivative according to claim 1, wherein: The heating furnace is heated to 360 - 400 °C.

4. The preparation method of a heavy aromatic hydrocarbon derivative with low metal impurities according to claim 1, characterized in that: The pressure inside the vacuum extraction tower is maintained at -95 to -99 kPa.

5. The preparation method of a low-metal impurity heavy aromatic hydrocarbon derivative according to claim 1, characterized in that: The flow rate of extraction line 1 is 2 - 5 t / h, and the solvent addition amount is 3 - 10 t / h; the flow rate of extraction line 2 is 8 - 20 t / h, and the solvent addition amount is 10 - 25 t / h; the flow rate of extraction line 3 is 3 - 10 t / h, and the solvent addition amount is 5 - 15 t / h.

6. The preparation method of a heavy aromatic hydrocarbon derivative with low metal impurities according to claim 1, characterized in that: The solvent at the top of the tower is condensed to 50 - 70 °C.

7. The preparation method of a heavy aromatic hydrocarbon derivative with low metal impurities according to claim 1, characterized in that: The heavy aromatic hydrocarbon derivative material at the bottom of the tower is condensed and cooled to 70 - 100 °C after being combined.

8. The preparation method of a heavy aromatic hydrocarbon derivative with low metal impurities according to claim 1, characterized in that: The solvent is a mixture of furfural and N-methylpyrrolidone, and the mass ratio is furfural:N-methylpyrrolidone = 1 - 9:9.

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