TECHNOLOGY FOCUS - BIOLOGY - Preferred Component: The solid product comprises torrefied biomass feedstock.    TECHNOLOGY FOCUS - INORGANIC CHEMISTRY - Preferred Component: The carrier gas stream is selected from nitrogen, helium, carbon dioxide and argon. The solid acid catalyst is ZSM-5. The solid base catalyst is hydrotalcite. The silica catalyst is diatomite. The silica-alumina catalyst is kaolin. The group B metal oxide catalyst is ammonium molybdate. The gaseous product comprises (vol.%): carbon dioxide (0-85, preferably 5-50), carbon monoxide (0-40, preferably 0-30); water (0-95, preferably 30-80), and total amount of hydrogen, 1C/2C/3C hydrocarbons, acetic acid, formic acid and other light organic compounds (0-75, preferably 0-50).    TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Process: In the process, the step a) or step b) are carried out in the presence of a carrier gas stream, where the object (O1) further comprises the carrier gas stream. The step c) is carried out in the presence of a heat carrier, where the heat carrier is selected from solid catalysts, solid particles, steam and flue gas. The step c) is carried out in fluidized bed or fast transport bed in the presence of catalysts or solid particles such that heated catalysts and heat solid particles may obtained, where the heated catalysts or the heated particles are fed to an object (O1). The torrefaction reaction condition includes a temperature of 180-350 (preferably 220-240) degrees C, a pressure of atmospheric to 500 psig (preferably -3 psig to atmospheric pressure of 15 psig), and a residence time of 1 minute to 24 hours (preferably 5-20 minutes), where the pyrolysis reaction condition includes a temperature of 375-700 (preferably 425-525) degrees C, a pressure of vacuum condition to 1000 psig (preferably atmospheric pressure to 300 psi), and residence time of 0.01-200 (preferably 0.5-2) seconds, where the combustion reaction condition includes a temperature of 100-3000 (preferably 400-1200) degrees C, a pressure of near atmospheric pressure to 300 psi (preferably atmospheric pressure), with a residence time of 0.01 millisecond to 30 minutes (preferably 0.1 millisecond to 30 seconds), where the pyrolysis oil product has a total acid number (TAN) 80-200 (preferably 20-50). The torrefaction reaction is carried out in reactor A selected from augers reactors, ablative reactors, rotating cones, fluidized-bed reactors, circulating fluidized bed reactors, entrained-flow reactors, vacuum moving-bed reactors, transported-bed reactors, and fixed-bed reactors. The torrefaction reaction is carried out in the presence of a catalytic material selected from solid acid catalysts, solid base catalysts, silica catalysts, silica-alumina catalysts, group B metal oxide catalysts, and/or pyrolytic char. The torrefaction reaction is carried out in the absence of diatomic oxygen in an inert gas atmosphere selected from nitrogen, argon, steam, and carbon oxides. The torrefaction reaction is carried out in a reducing gas atmosphere. The torrefaction reaction is carried out in a gas atmosphere comprising carbon monoxide. The torrefaction reaction is carried out with a reactant selected from hydrogen and ammonia. The pyrolysis reaction is carried out in reactor B selected from auger reactors, ablative reactors, a bubbling fluidized bed reactor, circulating fluidized beds/transport reactor, rotating cone pyrolyzer, and vacuum pyrolyzer. The combustion reaction is carried out in reactor C selected from furnace, combustion fluid beds, combustion fixed beds, gas turbines, kilns, gas burners, and boilers. The process further involves steps of i) generating a process steam from the heat after step c); and ii) feeding the process steam to an object (O1). EXAMPLE - No suitable example given.