TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Method: The method involves: feeding first reactant comprising the solid hydrocarbonaceous material to a fluidized bed reactor comprising a distributor (28) by injection of the solid material in a gas jet or gas jets through a port or ports, where the carrier gas in the gas jet is at a temperature of less than 200 degrees C, to form a gas mixture comprising suspended solid particles in a lower section of the reactor that has a normalized temperature of 100-600 degrees C; and pyrolyzing within an upper section of the reactor at least a portion of the gas mixture comprising suspended solid particles in a catalyzed reaction at a temperature of at least 500 degrees C to produce pyrolysis products. The method further involves feeding fluidizing gas into the lower section. The fluidizing gas passes through distributor prior to entering the lower section. The lower section does not contain any catalyst trays and the upper section comprises at least one catalyst tray. The lower section contains less than 10 wt.% of the total catalyst in the reactor and the upper section comprises at least 50 wt.% of the total catalyst in the reactor. The upper section has a temperature of 500-800 degrees C. The linear velocity of the carrier fluid in the feed port is 25-10000 cm/sec. The ratio of gas flow rate injected with the solid hydrocarbonaceous material to the gas flow rate introduced through the fluidization port is less than 10. The space velocity of the biomass in comparison to the catalyst contained in the reactor is at least 0.1. The fluidization gas residence time in contact with the catalyst bed is at least 1.0 seconds. The solid hydrocarbonaceous material is fed into the reactor through a feed port, where the feed port has an angle that is at least 15 degrees from the horizontal at the point at which it enters the reactor. The maximum angle of the feed port is about 90 degrees . A gas for the gas jet is carried through a carrier flow tube that carries the gas into the feed, and where the angle that the carrier flow tube makes with the horizontal is greater than the angle at which the biomass feed tube enters the pyrolysis reactor, both are positive values. The ratio of gas flow rate injected with the solid hydrocarbonaceous material biomass to the gas flow rate introduced through the fluidization port is 0.01-5. The solid hydrocarbonaceous material is fed in discontinuous pulses in the gas feed. The solid hydrocarbonaceous material is introduced by the injection in a flowing gas stream into reactor comprising fluidized bed, where, prior to introduction to the fluidized bed, the hydrocarbonaceous material is maintained at a temperature of less than 300 degrees C. Preferred System: The upper section is above the lower section with respect to gravity. The lower section comprises a volume that includes an inner diameter of the fluidized bed reactor and a height that is at least 2% of the total reactor height. The upper section comprises a volume that includes an inner diameter of the fluidized bed reactor and a height that is at least 5% of the total reactor height. The lower and upper sections are both above the distributor. The lower section is disposed immediately above a distributor. The lower section comprises a gas injector inlet through which a gas carrying biomass is introduced and where a fluidizing gas that does not contain biomass passes through the distributor and forms a mixture with the gas carrying the biomass that flows into the reactor through the gas injector. Preferred Apparatus: The angle alpha of the feed port is at least 25 degrees from the horizontal. The apparatus comprises a carrier flow tube that is adapted to carry the gas into the feed. The angle that the carrier flow tube makes with the horizontal is greater than the angle at which the biomass feed tube enters the pyrolysis reactor, both are positive values. EXAMPLE - No suitable example given.