TECHNOLOGY FOCUS - INORGANIC CHEMISTRY - Preferred Components: The catalyst comprises one or more of a zeolite catalyst, a non-zeolite catalyst, a metal catalyst and/or a metal oxide catalyst. The catalyst comprises a zeolite catalyst, preferably ZSM-5. The catalyst comprises silica to alumina ratio of 30:1-150:1. The zeolite catalyst comprises pores having a pore size of 5-100 Angstroms, preferably 5.9-6.3 Angstroms or 7-8 Angstroms. The zeolite catalyst has a bimodal distribution of pore sizes. The catalyst comprises many pores, where: at least 95% of the pores of the one or more catalysts have smallest crosssectional diameters that lie within a first size distribution or a second size distribution, at least 5% of the pores of the one or more catalysts have smallest crosssectional diameters that lie within the first size distribution, at least 5% of the pores of the one or more catalysts have smallest crosssectional diameters that lie within the second size distribution, and the first and second size distributions do not overlap; or at least 95% of the pores of the one or more catalysts have smallest crosssectional diameters that lie within a first distribution and a second distribution, which first distribution is 5.9-6.3 Angstroms and second distribution is different from and does not overlap with the first distribution, at least about 5% of the pores of the one or more catalysts have smallest crosssectional diameters of 5.9-6.3 Angstroms, and at least 5% of the pores of the one or more catalysts have smallest crosssectional diameters that lie within the second distribution; or at least 95% of the pores of the catalysts have smallest crosssectional diameters of 5.9-6.3 Angstroms or 7-200 Angstroms, at least 5% of the pores of the one or more catalysts have smallest crosssectional diameters of 5.9-6.3 Angstroms, and at least 5% of the pores of the one or more zeolite catalysts have smallest cross-sectional diameters of 7-200 Angstroms. The catalyst has one or more metals incorporated in it. The catalyst comprises a gallium. The catalyst comprises a galloaluminosilicate mordenite framework inverted zeolite. The galloaluminosilicate mordenite framework inverted zeolite is in the hydrogen form. The ratio of moles of silicon (Si) in the galloaluminosilicate zeolite catalyst to the sum of the moles of gallium (Ga) and aluminum (Al) in the galloaluminosilicate zeolite catalyst is at least 15:1. The ratio of moles of Si in the galloaluminosilicate zeolite catalyst to the moles of Ga in the galloaluminosilicate zeolite catalyst is at least 30:1. The ratio of moles of Si in the galloaluminosilicate zeolite catalyst to the moles of Al in the galloaluminosilicate zeolite catalyst is at least 10:1.    TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Process: The catalytic reaction is catalyzed via many catalyst particles, and at least about 50% of the sum of the total volume of catalyst is occupied by particles having maximum cross-sectional dimensions of less than 1 micron. The hydrocarbonaceous material is fed to a fluidized bed reactor, preferably a circulating fluidized bed reactor or a turbulent fluidized bed reactor. The hydrocarbonaceous material is fed to the reactor at a mass-normalized space velocity of 0.01-10 hour-1. The process further comprises varying the mass-normalized space velocity of the hydrocarbonaceous material to selectively produce different fluid hydrocarbon products. The process further comprises: separating the hydrocarbon products from the catalyst by passing the catalyst and the hydrocarbon products through a solids separator at a solids separator residence time of at least 1 second and at a solids separator temperature of greater than 500 degrees C; and introducing a fluidization fluid into the fluidized bed reactor, where the fluidization fluid has an average fluidization fluid residence time of at least 1 second in the reactor. The pyrolyzing step occurs at a temperature of 500-1000 degrees C. The catalytic reaction step occurs at a temperature of 500-1000 degrees C. The pyrolyzing step and the catalytic reaction step occur in the same or different reactor. In the process, the reactor, in which the catalytic reaction occurs, has a volume of at least 1 liter. The hydrocarbonaceous material and catalyst are fed in one or more feed streams to the reactor such that the mass ratio of the catalyst to the hydrocarbonaceous material in the one or more feed streams is 0.5:1-20:1. The residence time of the hydrocarbonaceous material in the reactor is 2-480 seconds. The contents of the reactor in which the pyrolyzing step occurs are heated at a heating rate of greater than 50 degrees C/second. In the process, the contents of the reactor in which the catalytic reaction step occurs are heated at a heating rate of greater than 50 degrees C/second. Preferred Components: The ratio of the mass of carbon within the hydrocarbonaceous material to the mass of carbon in the olefins in the recycle stream is 2:1-20:1, preferably 3:1-10:1 or 4:1-5:1. The fluid hydrocarbon products contain more aromatic compounds than olefinic compounds. The hydrocarbonaceous material comprises a solid or a biomass material, preferably: plastic waste, recycled plastics, agricultural and municipal solid waste, food waste, animal waste, carbohydrates, and/or lignocellulosic materials; xylitol, glucose, cellobiose, hemi-cellulose, and/or lignin; and sugar cane bagasse, glucose, wood, and/or corn stover. The fluid hydrocarbon product comprises an amount of aromatic compounds that is 35-40 wt.%, preferably at least 15 wt.%, at least 35 wt.% or at least 39 wt.% of the total amount of the hydrocarbonaceous material used in forming the pyrolysis products and which is calculated as the weight of the aromatic compounds present in the fluid hydrocarbon product divided by the weight of the hydrocarbonaceous material used in forming the pyrolysis products. The hydrocarbonaceous material comprises a first component and a second component, where the first and second components are different, and the process further comprises: providing first and second catalysts in the reactor, where the first catalyst is selective for catalytically reacting the first component or its derivative to produce a fluid hydrocarbon product, and the second catalyst is selective for catalytically reacting the second component or its derivative to produce a fluid hydrocarbon product. The fluid hydrocarbon products are produced from the pyrolysis products by dehydration, decarbonylation, decarboxylation, isomerization, oligomerization and/or dehydrogenation catalytic reactions. EXAMPLE - Mixture of Glucose and catalyst containing zeolite (ZSM-5) with a mass ratio of 19 were fed into a reactor. The mixture was pyrolyzed within the reactor at a heating rate of 1000 degrees C/second and reaction time of 240 seconds. The mixture was catalytically reacted to produce fluid hydrocarbon products comprising olefins and aromatics compounds with a yield of 31.4%.