Hydrocarbon conversion system

Claim 1

A METHOD OF CONVERTING A LIGHT HYDROCARBON OIL INTO A HIGH ANTI-KNOCK MOTOR FUEL BY HYDROCFORMING WHICH COMPRISES PASSING LIGHT HYDROCARBON OIL REACTANT VAPORS AND SEPARATELY INTRODUCING NOT HYDROGEEN-CONTAINING REACTANT GAS THROUGH A DENSE FLUIDIZED BED OF FINELY DIVIDED HYDROFORMING CATALYST IN A REACTION ZONE AT A TEMPERATURE OF ABOUT 825* TO ABOUT 1025*F., AT A PRESSURE OF ABOUT 25 TO ABOUT 750 P.S.I., AND A CATALYST TO OIL RATIO BY WEIGHT OF FFROM 0.03 TO 0.5, WITHDRAWING A STREAM OF REACTION PRODUCTS CONTAINING SMALL AMOUNTS OF REESIDUAL ENTRAINED CATALYST OVERHEAD FROM THE REACTION ZONE, WITHDRAWING A STREAM OF CATALYST PARTTICLES DIRECTLY FROM THE DENSE FLUID IZED BED IN SAID REACTION ZONE, STRIPPING ADSORBED HYDROCARBON MATERIAL FROM THE STREAM OF CATALYST, REGENERATING THE STRIPPED CATALYST PARTICLES BY BURNING OFF CARBONACEOUS DEPOSITS IN A DENSE FLUIDIZED BED IN A REGENERATION ZONE CONTROLLING THE TEMPERATURE OF THE CATLAYST UNDERGOING REGENERATION TO BELOW ABOUT 1200*F., WITHDRAWING CATALYST PARTICLES FROM THE REGENERATION ZONE AND RECYCLING THE SAME TO THE REACTION ZONE, SEPARATING CATALYST MATERIAL ENTRAINED WITH THE STREAM OF REACTION PRODUCTS PASSING AT LEAST ONE OF THE REACTANT MATERIALS IN INDIRECT HEAT EXCHANGE RELATION ONE OF THE STREAM OF REACTION PRODUCTS THEREBY REMOVING SOME OF THE HEAT THEREFROM, HEATING THE LIGHT HYDROCARBON OIL REACTANT TO A TEMPERATURE OF ABOUT 750* TO ABOUT 1050*F. PREPARATORY TO INTRODUCING THE SAME INTO THE REACTION ZONE, COOLING THE STREAM OF REACTION PRODUCTS TO CONDENSE HYDROFORMATE, SEPARATING HYDROFORMATE FROM GASEOUS CONSTITUENTS OF THE REATIOIN PRODUCT STREAM, HEATING THE GASEOUS CONSTITUENTS TO A TEMPERATURE WHICH IS GREATER THAN THE TEMPERATURE OF THEE LIGHT HYDROCARBON OIL REACTANT PRIOR TO BEING INTRODUCED INTO THE REACTION ZONE BUT NOT HIGHER THAN ABOUT 1150*F. AND RECYCLING THE SAME TO THE REACTION ZONE.

Claim 2

A METHOD OF CONVERTING A LIGHT HYDROCARBON OIL INTO A HIGH ANTI-KNOCK MOTOR FUEL BY HYDROCFORMING WHICH COMPRISES PASSING LIGHT HYDROCARBON OIL REACTANT VAPORS AND SEPARATELY INTRODUCING NOT HYDROGEEN-CONTAINING REACTANT GAS THROUGH A DENSE FLUIDIZED BED OF FINELY DIVIDED HYDROFORMING CATALYST IN A REACTION ZONE AT A TEMPERATURE OF ABOUT 825* TO ABOUT 1025*F., AT A PRESSURE OF ABOUT 25 TO ABOUT 750 P.S.I., AND A CATALYST TO OIL RATIO BY WEIGHT OF FFROM 0.03 TO 0.5, WITHDRAWING A STREAM OF REACTION PRODUCTS CONTAINING SMALL AMOUNTS OF REESIDUAL ENTRAINED CATALYST OVERHEAD FROM THE REACTION ZONE, WITHDRAWING A STREAM OF CATALYST PARTTICLES DIRECTLY FROM THE DENSE FLUID IZED BED IN SAID REACTION ZONE, STRIPPING ADSORBED HYDROCARBON MATERIAL FROM THE STREAM OF CATALYST, REGENERATING THE STRIPPED CATALYST PARTICLES BY BURNING OFF CARBONACEOUS DEPOSITS IN A DENSE FLUIDIZED BED IN A REGENERATION ZONE CONTROLLING THE TEMPERATURE OF THE CATLAYST UNDERGOING REGENERATION TO BELOW ABOUT 1200*F., WITHDRAWING CATALYST PARTICLES FROM THE REGENERATION ZONE AND RECYCLING THE SAME TO THE REACTION ZONE, SEPARATING CATALYST MATERIAL ENTRAINED WITH THE STREAM OF REACTION PRODUCTS PASSING AT LEAST ONE OF THE REACTANT MATERIALS IN INDIRECT HEAT EXCHANGE RELATION ONE OF THE STREAM OF REACTION PRODUCTS THEREBY REMOVING SOME OF THE HEAT THEREFROM, HEATING THE LIGHT HYDROCARBON OIL REACTANT TO A TEMPERATURE OF ABOUT 750* TO ABOUT 1050*F. PREPARATORY TO INTRODUCING THE SAME INTO THE REACTION ZONE, COOLING THE STREAM OF REACTION PRODUCTS TO CONDENSE HYDROFORMATE, SEPARATING HYDROFORMATE FROM GASEOUS CONSTITUENTS OF THE REATIOIN PRODUCT STREAM, HEATING THE GASEOUS CONSTITUENTS TO A TEMPERATURE WHICH IS GREATER THAN THE TEMPERATURE OF THEE LIGHT HYDROCARBON OIL REACTANT PRIOR TO BEING INTRODUCED INTO THE REACTION ZONE BUT NOT HIGHER THAN ABOUT 1150*F. AND RECYCLING THE SAME TO THE REACTION ZONE.