TECHNOLOGY FOCUS - CHEMICAL ENGINEERING - Preferred Conditions: The temperature of gaseous hydrocarbon is -2.3-83 degrees C. The distillation range of high-temperature condensate is 210-600 degrees C, and the distillation range of low-temperature condensate is 40-300 degrees C. The final boiling point of gaseous hydrocarbon is 40-80 degrees C, the initial boiling point of low-temperature condensate is 40-83 degrees C, the final boiling point of low-temperature condensate is 210-300 degrees C, and the initial boiling point of high-temperature condensate is 210-300 degrees C. The ratio of high-temperature condensate is 5-20 wt.%, the ratio of low-temperature condensate is 50-60 wt.%., and ratio of gaseous hydrocarbon is 20-40 wt.%. The residence time of gaseous hydrocarbon and high-temperature condensate in tube reactor (I) is 0-1 second, preferably 0-0.91 second, before contacting with catalyst. The mass ratio of catalyst and gaseous hydrocarbon is 7-39, preferably 10-30. The operating conditions of tube reactor (I) include reaction temperature of 490-600 degrees C, preferably 560-580 degrees C, high-temperature condensate reaction time of 0.5-10 seconds, preferably 2-6 seconds, material/oil ratio of 5-25, preferably 7-20, and reaction pressure of 0.15-0.3 MPa. The operating conditions of tube reactor (II) include solvent/oil ratio of 10-30, preferably 12-20, reaction time of 0.1-1.5 seconds, preferably 0.4-1.1 seconds, and reaction temperature of 490-600 degrees C, preferably 535-575 degrees C. The operating conditions of fluidized bed reactor include reaction temperature of 500-600 degrees C, preferably 525-565 degrees C, reaction pressure of 0.15-0.3 MPa, and hourly space velocity of 1-35 hour-1, preferably 3-15 hour-1. The catalyst has a carbon content of 0.2-0.9 wt.%. The catalyst introduced into tube reactor (II) is a mixture of regenerated catalyst from the regenerator and spent catalyst from stripper in a weight ratio of 0:100-100:1, preferably 20:80-80:20. The spent catalyst is heated by flue-gas heat during regeneration. The catalyst temperature in tube reactor (II) is 550-720 degrees C, preferably 580-690 degrees C. The product separator provides gasoline fraction. The cracked heavy oil obtained from the product separator is sent to tube reactor (II) or fluidized bed reactor. The high-temperature condensate is supplied to tube reactor (I) after metal-removal.