▎ 摘　　要

NOVELTY - Maximizing production of chemicals involves introducing raw material oil into the raw material orientation modifying unit, under the action of directional modified catalyst, the reaction temperature is 350-650degrees Celsius, the pressure is 0.1-1.0 megaPascal, the steam/oil mass ratio is 0.1:1-10:1 under the condition of performing directional decarburization, demetallization and heavy component cracking modification reaction to obtain hydrogen, rich alkene gas, modified alkene-rich fraction oil, coke to obtain the modified olefin-rich fraction oil into the selective hydrorefining unit, under the action of the selective hydrorefining catalyst, the reaction temperature is 60-180degrees Celsius, the pressure is 2.0-4.0 megaPascal, the mass space velocity is 0.5-3.0 per hour, the volume ratio of hydrogen to oil is 400:1-800:1, removed the colloid, dialkene, alkaline nitrogen impurity, obtained fuel gas and refined fraction oil. USE - Method for maximizing production of chemicals such as low carbon olefin, aromatic hydrocarbon and needle coke used for producing high-quality gasoline and diesel. ADVANTAGE - The process has strong raw material adaptability, high chemical yield, low hydrogen consumption, mild operation condition and can be used for industrial production. The process maximally converts the oil into low-carbon olefin, aromatic hydrocarbon and high-quality needle coke. DETAILED DESCRIPTION - Maximizing production of chemicals involves introducing raw material oil into the raw material orientation modifying unit, under the action of directional modified catalyst, the reaction temperature is 350-650degrees Celsius, the pressure is 0.1-1.0 megaPascal, the steam/oil mass ratio is 0.1:1-10:1 under the condition of performing directional decarburization, demetallization and heavy component cracking modification reaction to obtain hydrogen, rich alkene gas, modified alkene-rich fraction oil, coke to obtain the modified olefin-rich fraction oil into the selective hydrorefining unit, under the action of the selective hydrorefining catalyst, the reaction temperature is 60-180degrees Celsius, the pressure is 2.0-4.0 megaPascal, the mass space velocity is 0.5-3.0 per hour, the volume ratio of hydrogen to oil is 400:1-800:1, removed the colloid, dialkene, alkaline nitrogen impurity, obtained fuel gas and refined fraction oil, the refined fraction oil obtained enters the refined fraction oil cutting unit to obtain the gasoline and diesel fraction rich in olefin at 350degrees Celsius and heavy distillate oil rich in polycyclic aromatic hydrocarbon to 350degrees Celsius, the gasoline and diesel fraction obtained enters the gasoline and diesel adsorption separation unit, under the action of the adsorbent, the adsorption temperature is 60-120degrees Celsius, the pressure is 0.2-0.6 megaPascal, the mass space velocity is 1.0-2.0 per hour, separated the gasoline and diesel aromatic hydrocarbon component and non-aromatic hydrocarbon component, obtained the adsorbed aromatic hydrocarbon component, absorbed the olefin-rich non-aromatic hydrocarbon component, the heavy fraction oil obtained into the needle coke yield increasing unit, the delayed coking, high temperature calcined process to obtain needle coke, coked gasoline and diesel oil, rich alkene gas to obtain the adsorbed graphene- rich non-aromatic hydrocarbon component, obtained coked gasoline and diesel oil enter into olefin production unit, under the action of olefin yield catalyst, the reaction temperature is 500-650degrees Celsius, the pressure is 0.1-0.5 megaPascal, agent oil ratio of 5:1-20:1, steam/oil mass ratio of 0.1:1-1.5:1, carried out directional catalytic cracking reaction to obtain the alkene-rich gas, cracking aromatic gasoline and diesel oil, coke, absorbed aromatic hydrocarbon component obtained and cracked rich aromatic steam diesel oil into aromatic hydrocarbon production unit, under the action of aromatic hydrocarbon production increasing catalyst, the reaction temperature is 360-500degrees Celsius, the pressure is 3.0-6.0 megaPascal, the volume space velocity is 0.5-2.0 per hour, the volume ratio of hydrogen to oil is 800:1-1500:1, performed selective cracking reaction to obtain fuel gas, saturated liquefied gas, light aromatic hydrocarbon, 9/10C aromatic hydrocarbon, the raw material orientation modifying unit, the heavy oil macromolecule in the raw oil is directionally modified reaction, the conversion rate of the heavy oil is 70 wt.%, the olefin content in the converted gasoline product is 40-60 wt.%, the content of the aromatic hydrocarbon is 20-40 wt.%, and the content of the polycyclic aromatic hydrocarbon in the heavy oil is 60-80 wt.%.