TECHNOLOGY FOCUS - INSTRUMENTATION AND TESTING - Preferred Components: The reactor system further comprises at least one wash nozzle disposed within the conveyor housing between the opening and screen section; an air lock chamber disposed above the reaction chamber for controlling entrance of material into the reaction chamber, the air lock chamber having an exit in sealed communication with an inlet to the reaction chamber; and an air lock controlling exit of material from the second vessel; a feedstock conveyor communicating with an inlet of the air lock chamber; and an inserting system communicating with the air lock chamber remove combustible gases from it before opening to the reaction chamber. The length of the conveyor housing is sufficient to provide a residence time for solids moving through the conveyor of at least 30 minutes. The reaction chamber and conveyor housing are sealed together around the open bottom; the first vessel is in sealed communication with the screen section of the conveyor housing; and the second vessel is sealed around the conveyor exit. The biased closed cover is disposed within the second vessel.    TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Process: The slurry is subjected to temperature of 125-400 degrees C and pressure of 20-800 psig during step (b). The step (d) comprises: further separating water from the liquid product; and a second reaction comprising coking at 400-600 degrees C and pressures of 15-75 psig, where the second reaction comprises subjecting the liquid product to processes of coking, vis-breaking, and/or hydrotreating. The step (b) comprises decomposing and hydrolyzing the slurry, where the decomposing occurs at 125-400 degrees C and 20-600 psig pressure and the hydrolyzing occurs at 200-350 degrees C and 210-800 psig pressure. The process further comprises an initial separating between the depolymerizing and hydrolyzing to remove solids and gases from the liquid product before the hydrolyzing. The separation of water from the liquid product in the converting step produces a liquid hydrocarbon fuel. The decomposing occurs for 15-120 or 60-180 minutes and the hydrolyzing occurs for 30-60 minutes. When the feedstock comprises animal processing waste, then the slurry is subjected to 125-260 degrees C and 20-600 psig pressure during the step (b); the decomposing occurs at 125-190 degrees C and 20-600 psig pressure for 15-120 minutes; and the hydrolyzing occurs at 200-260 degrees C and 210-600 psig pressure for 30-60 minutes. When the feedstock comprises municipal sewage sludge, then the slurry is subjected to 170-270 degrees C and 100-600 psig pressure during the step (b); the decomposing occurs at 170-200 degrees C and 100-600 psig pressure for 15-120 minutes; and the hydrolyzing occurs at 200-270 degrees C and 210-800 psig pressure for 30-60 minutes. When the feedstock comprises municipal solid waste, then the slurry is subjected to 150-350 degrees C and 55-800 psig pressure during the step (b); the decomposing occurs at 150-350 degrees C and 55-250 psig pressure for 60-180 minutes; and the hydrolyzing occurs at 200-350 degrees C and 210-800 psig pressure for 30-60 minutes. When the feedstock comprises shredder residue, then the slurry is subjected to 250-400 degrees C and 55-800 psig pressure during the step (b); the decomposing occurs at 250-400 degrees C and 55-250 psig pressure for 60-180 minutes; and the hydrolyzing occurs at 200-350 degrees C and 210-800 psig pressure for 30-60 minutes. When the feedstock comprises a grass feedstock, then the slurry is subjected to 120-270 degrees C and 20-800 psig pressure during the step (b); the decomposing occurs at 150-200 degrees C and 20-600 psig pressure for 15-120 minutes; and the hydrolyzing occurs at 200-270 degrees C and 210-800 psig pressure for 30-60 minutes. The process for generating useful materials, further comprises slurrying the feedstock prior to the decomposing. The decomposing step comprises heating the slurried feedstock to a temperature sufficient to reduce viscosity and break down feedstock components into constituent parts while at least substantially avoiding formation of char or ash. The decomposing step comprises heating the feedstock to 125-400 degrees C for 15-180 minutes; and the decomposing occurs in at least two stages. The hydrolyzing step comprises at least one of breaking peptide linkages in proteins to yield individual amino acid residues, fat degradation into triglycerides, fatty acids and glycerol, deamination and decarboxylation of amino acids, degradation of lignin and cellulose, breaking of halogen or metal salt bonds and breaking of sulfur bonds. The hydrolyzing step separates contaminants (comprising arsenic, barium, cadmium, chlorine (preferred), chromium, copper, lead, mercury, and zinc) from the liquid mixture into a water phase. The hydrolyzing comprises heating the liquid mixture to 200-350 degrees C and at 210-800 psig pressure for 30-60 minutes. The separating step of solids, gases and vapors, and water includes flashing the hydrolyzed liquid mixture to a lower temperature and pressure. The separating step further includes centrifuging the liquid mixture to remove solids and water. The conditioning comprises oil polishing comprising removing water from the hydrocarbon liquid. The step of removing water comprises gravity decanting. The oil polishing further comprises filtering particulate from the hydrocarbon liquid. The conditioning further comprises treatment of the hydrocarbon liquid with a thermal-chemical platform, which is vis-breaking, hydrotreating, coking, gasifying or pyrolyzing. When the feedstock comprises animal by-products, then the decomposing occurs at 125-190 degrees C and 20-600 psig pressure; and the hydrolyzing occurs at 200-260 degrees C and 210-800 psig pressure. When the feed stock comprises lignocellulosic material, then the decomposing occurs at 125-200 degrees C and 20-600 psig pressure; and the hydrolyzing occurs at 200-270 degrees C and 210-800 psig pressure. In the process of conversion of shredder residue into at least carbons solids and a liquid hydrocarbon fuel, the decomposing comprises reacting the shredder residue at 250-400 degrees C, under a pressure of 55-250 psig for a time sufficient to decompose non-metallic solids to produce a liquid mixture of hydrocarbons and solids. The process of conversion of shredder residue into at least carbons solids and a liquid hydrocarbon fuel comprises adding a solvent to the shredder residue in connection with the reacting. The hydrolyzing comprises reacting the heavier hydrocarbon fractions in the presence of water at 200-350 degrees C under a pressure of 210-800 psig for a time sufficient to produce a medium weight hydrocarbon liquid and water mixture; determining a contaminant content for the lighter fractions; and directing the lower molecular weight fractions to the hydrolyzing when contaminant content exceeds a predetermined threshold. The process for conversion of shredder residue into at least carbons solids and a liquid hydrocarbon fuel, further comprises flashing the hydrocarbon liquid and water mixture to a reduced pressure and temperature after the hydrolyzing; and controlling the reacting of the shredder residue and decomposable liquid to at least substantially avoid the formation of char or ash. The separating solids comprise washing solids with a solvent. Preferred Components: The feedstock comprises a lignocellulosic material (preferably a grass feedstock comprising C3 grasses, which is a mixed grass feedstock), and switch grass, Indian grass, big bluestem, little bluestem, Canada wildrye, Virginia wildrye, and/or goldenrod wildflowers. The fractions comprise fractionally distilling the liquid mixture to produce at least a low molecular weight hydrocarbon fraction, a medium molecular weight hydrocarbon fraction and a high molecular weight fraction. The solvent is a hydrocarbon liquid produced in a later step of the process. EXAMPLE - In a pilot run, a mixed grass feedstock (225 g) was size-reduced to small pieces for input into a Parr reactor fitted with a mechanical stirrer to implement. Components of the mixed grass feedstock included switch grass, Indian grass, big bluestem, little bluestem, Canada wildrye, Virginia wildrye, and goldenrod wildflowers. The raw feed first underwent first stage depolymerization at 150 degrees C, 29 psig for 0.5 hour followed by first stage hydrolysis at 250 degrees C, 609 psig for 0.5 hour. This run produced first stage solids (182.1 g), flashed water (5.3 g), and gases (37.6 g). The Parr reactor residuals, e.g. produced water, organic liquid, and mineral matrix, were separated using a separation technique e.g. hot centrifugation.