A method is described for treating a hydrocarbon oil feedstream to a delayed coking unit to maximize the ratio of the yield of liquids-to-gases, and to minimize the formation of coke which includes: a. mixing an oil-soluble catalyst with the hydrocarbon oil feedstream to produce a uniform mixture; b. contacting the catalyst-containing hydrocarbon oil feedstream with an excess of hydrogen under predetermined conditions that are favorable to maximizing the solubility of the hydrogen in the feedstream in a hydrogen distribution zone that is upstream of the coking unit; c. introducing the feedstream containing the solubilized catalyst and dissolved hydrogen, and the excess hydrogen gas into a flashing zone; d. recovering from the flashing zone a hydrogen gas stream and a single-phase hydrocarbon oil feedstream containing dissolved hydrogen and catalyst; e. maintaining the hydrocarbon oil feedstream containing dissolved hydrogen and catalyst under single-phase conditions to promote the reaction of the dissolved hydrogen with free radicals formed in the feedstream and to promote the catalyzed hydrodesulfurization of any sulfur-containing compounds present in the feedstream; f. introducing the catalyst-containing feedstream into a coking furnace upstream of the coking unit to heat the feedstream to a predetermined coking temperature; g. introducing the hot feedstream into the coking unit; and h. recovering a coking unit product stream that is free of catalyst and forming a coke product that contains the catalyst.

Examples of a flexible pyrolysis system are provided that include at least one reaction chamber capable of pyrolyzing a combination of coal in a supercritical carbon dioxide (CO.sub.2) atmosphere. The system includes a recuperating and condensing circuit that removes dissolved pyrolysis products from the supercritical CO.sub.2 atmosphere and then recovers CO.sub.2 for reuse in the reaction chamber. The recuperating and condensing circuit includes multiple stages of recuperators and collectors that can be independently controlled in order to selectively fractionate the pyrolysis products. In addition, the pyrolysis reaction may be controlled to alter the pyrolysis products generated.

Examples of a flexible pyrolysis system are provided that include at least one reaction chamber capable of pyrolyzing a combination of coal in a supercritical carbon dioxide (CO.sub.2) atmosphere. The system includes a recuperating and condensing circuit that removes dissolved pyrolysis products from the supercritical CO.sub.2 atmosphere and then recovers CO.sub.2 for reuse in the reaction chamber. The recuperating and condensing circuit includes multiple stages of recuperators and collectors that can be independently controlled in order to selectively fractionate the pyrolysis products. In addition, the pyrolysis reaction may be controlled to alter the pyrolysis products generated.

Systems and methods are provided for using an oxygen-containing gas as at least part of the stripping gas for the stripping zone or section in a fluidized coker. By using an oxygen-containing gas as the stripping gas, heat can be added to the stripping zone selectively based on combustion of coke and/or hydrocarbons with the oxygen in the stripping gas. This can allow the temperature of the stripping zone to be increased relative to the temperature of the coking zone of a fluidized coking system. The flow of oxygen can be controlled to achieve a desirable temperature in the stripper while the reactor temperature is independently set by preheating of the feed and/or hot coke circulation to the reaction zone.

Systems and methods are provided for using an oxygen-containing gas as at least part of the stripping gas for the stripping zone or section in a fluidized coker. By using an oxygen-containing gas as the stripping gas, heat can be added to the stripping zone selectively based on combustion of coke and/or hydrocarbons with the oxygen in the stripping gas. This can allow the temperature of the stripping zone to be increased relative to the temperature of the coking zone of a fluidized coking system. The flow of oxygen can be controlled to achieve a desirable temperature in the stripper while the reactor temperature is independently set by preheating of the feed and/or hot coke circulation to the reaction zone.

Systems and methods are provided for using an oxygen-containing gas as at least part of the stripping gas for the stripping zone or section in a fluidized coker. By using an oxygen-containing gas as the stripping gas, heat can be added to the stripping zone selectively based on combustion of coke and/or hydrocarbons with the oxygen in the stripping gas. This can allow the temperature of the stripping zone to be increased relative to the temperature of the coking zone of a fluidized coking system. The flow of oxygen can be controlled to achieve a desirable temperature in the stripper while the reactor temperature is independently set by preheating of the feed and/or hot coke circulation to the reaction zone.

Systems and methods are provided for using an oxygen-containing gas as at least part of the stripping gas for the stripping zone or section in a fluidized coker. By using an oxygen-containing gas as the stripping gas, heat can be added to the stripping zone selectively based on combustion of coke and/or hydrocarbons with the oxygen in the stripping gas. This can allow the temperature of the stripping zone to be increased relative to the temperature of the coking zone of a fluidized coking system. The flow of oxygen can be controlled to achieve a desirable temperature in the stripper while the reactor temperature is independently set by preheating of the feed and/or hot coke circulation to the reaction zone.

A material heating device comprises a rotary kiln, a plurality of heat exchange tubes, a hot air hood, a high-temperature gas input mechanism, an exhaust-gas collecting chamber, and an exhaust-gas output pipeline. The rotary kiln is provided with a material feed end and a material discharge end. The heat exchange tubes are in the rotary kiln. The hot air hood is outside the rotary kiln. The air inlet ends of the heat exchange tubes communicate with the hot air hood, and the air outlet ends of the heat exchange tubes communicate with the exhaust-gas collecting chamber. The exhaust-gas collecting chamber communicates with the exhaust-gas output pipeline. The hot air hood communicates with the high-temperature gas input mechanism, and the cavity between the heat exchange tubes and the heat insulation layer of the rotary kiln is a material channel. The heat exchange tubes are directly in contact with the material.

A material heating device comprises a rotary kiln, a plurality of heat exchange tubes, a hot air hood, a high-temperature gas input mechanism, an exhaust-gas collecting chamber, and an exhaust-gas output pipeline. The rotary kiln is provided with a material feed end and a material discharge end. The heat exchange tubes are in the rotary kiln. The hot air hood is outside the rotary kiln. The air inlet ends of the heat exchange tubes communicate with the hot air hood, and the air outlet ends of the heat exchange tubes communicate with the exhaust-gas collecting chamber. The exhaust-gas collecting chamber communicates with the exhaust-gas output pipeline. The hot air hood communicates with the high-temperature gas input mechanism, and the cavity between the heat exchange tubes and the heat insulation layer of the rotary kiln is a material channel. The heat exchange tubes are directly in contact with the material.

A system and method for torrefying a combination of biomass and biochar colloidal dispersion is provided.