TECHNOLOGY FOCUS - INSTRUMENTATION AND TESTING - Preferred Method: The fluidized-bed reactor is maintained at a partial pressure of hydrogen of 200-600 psig. The temperature of the fluidized bed reactor is 343-593 degrees C. The feedstock is prepared in such a way that solid residues, remaining after hydropyrolysis of the feedstock, are substantially smaller, in their largest dimension, than the solid catalyst particles that form the fluidized bed. The feedstock is introduced to the reactor as a stream comprising solid particles entrained in a rapidly-moving transport gas stream, where the transport of feedstock into the fluidized bed is accomplished primarily via the action of the transport gas on solid particles of feedstock. The method further comprises separating metallic catalyst fines from char, where the separation is effected: with a barrier filter that incorporates a remotely energized and de-energized magnetic field to retain magnetic catalyst particles until they can be discharged by backpulsing when the magnetic field is de-energized, where the char can be separated from the product stream and removed by backpulsing while the magnetic field remains energized and magnetic material is retained on the filtering surface; or by a virtual impactor that diverts a stream of heavier catalyst fines to a downstream collection stage, where the downstream collection stage is a barrier filter that can be cleaned by periodic backpulsing and incorporates a remotely energized magnetic field to retain magnetic catalyst particles the until they can be discharged when the magnetic field is de-energized and the filter is cleaned by backpulsing. The slugging in the fluidized bed is controlled via the use of equipment incorporating lateral obstructions, obstacles, or constrictions, an axis or centerline of the equipment intersecting a centerline of the fluidized bed reactor. The modifications that control slugging in the fluidized bed reactor incorporate internal heat-exchanging flow pathways connected to external piping that is isolated from the internal environment of the reactor through which liquids and gases can be passed to extract heat from the reactor. In the method, all required process heat is supplied from the deoxygenation reactions occurring during hydropyrolysis of the feedstock. Preferred Components: The recovered stream of condensed liquid contains less than 4 mass% of oxygen. The relationship between a volumetric feed rate of solid feedstock particles and a volume of the fluidized bed reactor is the volume hourly space velocity (VHSV) of the reactor is 1-40. The density of particles of catalyst is 0.5-2 kg/l. The feedstock contains no water and is only partly dewatered, and contains some water. The feedstock comprises: particles of solid biomass; solid particles of an oxygenated polymer e.g. polyethylene terephthalate; a wholly or partially dewatered biomass feedstock that is high in lipid content e.g. high-lipid algae; organic material of an aquatic origin e.g. fish, fish parts and wastes from fish processing; materials manufactured or otherwise obtained from biomass e.g. paper products and residues rejected as waste streams by paper mills; organic material of animal origin e.g. offal, fats, greases and tissues; waste organic material of animal origin e.g. manure or sewage sludge; a slurry of solid particles, suspended in a carrier liquid that evaporates when it is introduced into the reactor; and an oxygenated organic liquid, which undergoes hydropyrolysis in the hydropyrolysis process. The superficial velocity of fluidizing gas passing through the fluidized bed reactor is sufficient or no higher than the minimum needed to create a state consistent with that of a bubbling fluidized bed. The solid particles of catalyst: are spherical, attrition-resistant or porous and include a large internal surface area within the outer surface of the particle; and have properties consistent with those of a highly active hydrotreating catalyst. The solid particles of catalyst comprise: an alumina-based substrate, impregnated with a sulfided nickel-molybdenum catalyst or sulfided cobalt-molybdenum catalyst or a metal e.g. nickel, cobalt, iron or other metals that can be used as catalysts in hydrotreating; an aluminosilicate-based substrate or glass-ceramic-based substrate, impregnated with the metal; or at least two catalysts which differ by at least one of density, aerodynamic size or aerodynamic diameter but are otherwise physically similar, and are disposed throughout the fluidized bubbling bed and by virtue of having different properties tend to segregate and stratify, becoming vertically ordered by property so as to create regions within the bed that differ in catalytic activity. The mean diameter of catalyst particles is greater than 3.2 mm. The cross-sectional area of the obstructions, obstacles, or constrictions, when seen from a top of the fluidized-bed reactor, is equal to 40% of the cross-sectional area of the fluidized bed reactor. The obstructions, obstacles, or constrictions, are: equipped with at least one of temperature-sensing means and means by which heat may be removed from or added to the fluidized bed, in such a manner that the temperature of the fluidized bed around the obstructions, obstacles, or constrictions can be monitored and/or regulated; and installed at vertical locations along the fluidized bed reactor that are separated from one another by one to two reactor diameters. The orientations of the obstructions, obstacles, or constrictions, are varied, when seen from a top of the reactor, so that a single, open passage, running the length of the reactor for a distance of more than two reactor diameters, is not present. The upper surfaces of the obstructions, obstacles, or constrictions, are: at least one of rounded, peaked or sloped in order to prevent bed material from coming to rest on the surface; porous and constructed so that gas can pass through the upper part of the obstruction in order to prevent bed material from coming to rest on the surface; or uniformly porous and constructed of a highly abrasion-resistant sintered glass ceramic material so that gas can pass through the exterior of the obstruction in order to prevent bed material from coming to rest on the surface. The equipment is: highly-abrasion resistant; at least partially constructed of an extremely hard ceramic or glass-ceramic material; or at least partially coated with one of a highly abrasion-resistant coating and an extremely hard ceramic or glass-ceramic material. The surfaces of the equipment are catalytically active, and facilitate hydropyrolysis reactions. The equipment comprises an insert (130) with: a centrally located support, running along the central axis of the fluidized bed reactor, to which the obstructions, obstacles, or constrictions, are attached; a circumferential support, disposed around the circumference of the fluidized bed reactor, to which the obstructions, obstacles, or constrictions, are attached; or a circumferential support, disposed around the circumference of the fluidized-bed reactor, with gas paths available to connect with locations to where porous obstructions, obstacles, or constrictions are attached. The equipment comprises; obstructions, obstacles, or constrictions that are directly attached to, supported by, and in communication with the wall of the fluidized bed reactor; and obstructions, obstacles, or constrictions that molded or cast into a molded or cast refractory lining of the fluidized bed reactor. EXAMPLE - No suitable example given.