TECHNOLOGY FOCUS - INORGANIC CHEMISTRY - Preferred Catalyst: The catalyst is in a particulate form. The catalyst has an average particle size of 20-150 mu m, preferably 25-125 mu m, especially 30-80 mu m; acid site loading, as measured by ammonia adsorption, of 3-10 ml of NH3 per gram of catalyst, preferably 3-8 ml of NH3 per gram of catalyst; has a tap bulk density of 0.5-2.2 g/cc; has Brunauer, Emmett and Teller (BET) surface area of 20-150 m2/g. The catalyst comprises porosity providing a pore volume of 0.2-1.0 cc of pore volume per gram of catalyst; Attrition index of 2-25; non-zeolitic support; zirconia support. The catalyst further comprises a catalytic promoter. The catalyst comprises a zirconia support and tungsten oxide on the zirconia support at a tungsten oxide loading of 10-20 wt.%, based on total weight of zirconia and tungsten oxide, where the catalyst being of particulate form with an average particle size of 20-150 mu m, with an acid site loading, as measured by ammonia adsorption, of 3-10 ml of NH3 per gram of catalyst, and where Lewis acid and Bronsted acid sites are present on the catalyst at a Lewis to Bronsted infrared band height ratio (cm-1/cm-1) of 0.1-50. Preferred Components: The Lewis acid and Bronsted acid sites are present on the catalyst at a Lewis to Bronsted infrared band height ratio (cm-1/cm-1) of 0.1-50, preferably 0.5-20, especially 0.75-5. The metal oxide has a loading on the matrix material of 10-20 wt.%, preferably 12-18 wt.%, especially 15-17 wt.%. The metal oxide comprises tungsten oxide. The matrix material comprises a support comprising material selected from titania, alumina, silica, ceria, zirconia, zeolites, and/or their compatible mixtures or alloys; binder. The zirconia comprises tetragonal phase zirconia. The binder comprises material selected from macroreticulate polymers, alumina, kieselguhr, kaolin, bentonite and/or clays. The catalytic promoter comprises a metal selected from platinum, palladium, ruthenium, cobalt, nickel, molybdenum, hafnium, copper, iron, tin, manganese, magnesium, chromium and/or lanthanum. The catalytic promoter is present in the catalyst at concentration of 1-15 wt.%. The reactor comprises a transport reactor, fluidized bed reactor, circulating fluid bed reactor. The catalyst is fluidized in the reactor. The dilute air or steam comprises a diluent selected from argon, helium, nitrogen, or carbon dioxide. The bio-oil has an oxygen content of 1-25% of oxygen by weight, based on weight of the bio-oil.    TECHNOLOGY FOCUS - POLYMERS - Preferred Components: The biomass starting material comprises a lignocellulosic material; particularized biomass having an average particle size of 0.1-10 mm; particularized biomass having an average particle size of 0.1-8 mm. Preferred Method: The pyrolysis reaction is carried out at a weight ratio of catalyst to biomass starting material that is of 1:1-100:1. The pyrolysis reaction is carried out in a reactor. The residence time of the biomass starting material in the reactor is 0.25-5 seconds. The pyrolysis conditions comprises temperature of 200-700 degrees C, preferably 200-550 degrees C; pressure of 1-25 bar or ambient pressure. The pyrolysis reaction and regeneration of the catalyst are carried out continuously with one another. The regeneration of the catalyst is carried out at 400-1000 degrees C, preferably 400-850 degrees C, especially 500-700 degrees C. The regeneration of the catalyst is carried out in the presence of oxygen or an oxygen-containing gas; or air or dilute air; steam and air, dilute air or oxygen; dilute steam and air, dilute air or oxygen. The method (M1) further involves: recovering tail gas from regeneration of the catalyst, and recycling the tail gas to the pyrolysis reaction; recovering a bio-oil from the pyrolysis product. The recovering the bio-oil from the pyrolysis product involves: separating the pyrolysis product to recover vapor and gas fraction, and solids fraction comprising pyrolysis product solids, including biomass char, unreacted biomass, and biomass ash, and the catalyst; cooling the vapor and gas fraction to recover a bio-crude liquid; and removing water from the bio-crude liquid to yield the bio-oil. The catalyst from the solids fraction is regenerated and then is recycled to the pyrolysis reaction. The method (M1) involves carbon conversion efficiency of 20-65 wt.%. EXAMPLE - No suitable example given.