The invention provides a pyrolysis reaction system, the system comprising: a pyrolysis chamber comprising a feed inlet, a gas inlet and a product outlet, wherein the pyrolysis chamber is configured i) to receive a pyrolysable organic feed and an inert gas via the feed inlet and gas inlet respectively, ii) to pyrolyse the organic feed at a pyrolysis temperature to produce a carbonaceous pyrolysis product and a pyrolysis gas, wherein the pyrolysis gas will combine with the inert gas to form a gas mixture having a pyrolysis chamber pressure in the pyrolysis chamber, and iii) to discharge the carbonaceous pyrolysis product via the product outlet; a gas reactor configured to react the pyrolysis gas by combustion and/or carbon deposition at a gas reaction temperature and a gas reactor pressure; and a first partition defining a boundary between the pyrolysis chamber and the gas reactor, the first partition comprising a plurality of first apertures to provide fluid communication between the pyrolysis chamber and the gas reactor, wherein the pyrolysis reaction system is operable with the gas reactor pressure less than the pyrolysis chamber pressure such that the gas mixture flows from the pyrolysis chamber to the gas reactor through the first apertures, thereby providing at least a portion of the pyrolysis gas for reaction in the gas reactor.

The invention provides a pyrolysis reaction system, the system comprising: a pyrolysis chamber comprising a feed inlet, a gas inlet and a product outlet, wherein the pyrolysis chamber is configured i) to receive a pyrolysable organic feed and an inert gas via the feed inlet and gas inlet respectively, ii) to pyrolyse the organic feed at a pyrolysis temperature to produce a carbonaceous pyrolysis product and a pyrolysis gas, wherein the pyrolysis gas will combine with the inert gas to form a gas mixture having a pyrolysis chamber pressure in the pyrolysis chamber, and iii) to discharge the carbonaceous pyrolysis product via the product outlet; a gas reactor configured to react the pyrolysis gas by combustion and/or carbon deposition at a gas reaction temperature and a gas reactor pressure; and a first partition defining a boundary between the pyrolysis chamber and the gas reactor, the first partition comprising a plurality of first apertures to provide fluid communication between the pyrolysis chamber and the gas reactor, wherein the pyrolysis reaction system is operable with the gas reactor pressure less than the pyrolysis chamber pressure such that the gas mixture flows from the pyrolysis chamber to the gas reactor through the first apertures, thereby providing at least a portion of the pyrolysis gas for reaction in the gas reactor.

A continuous bubbling fluid bed process converts biomass feedstocks into energy/heat, engineered biochar particles (including nanoparticles) and a vapor stream of organic compounds. The products have a multitude of applications determined by the specific conditions at which the process was operated, specifically controlling: temperature, catalysts, residence time, element and compound concentrations, and withdraw of products from various points in the system. The introduction of air, steam, and various gases into the vessel at selected locations and at controlled rates enables the economic, dependable and consistent production of these products.

A continuous bubbling fluid bed process converts biomass feedstocks into energy/heat, engineered biochar particles (including nanoparticles) and a vapor stream of organic compounds. The products have a multitude of applications determined by the specific conditions at which the process was operated, specifically controlling: temperature, catalysts, residence time, element and compound concentrations, and withdraw of products from various points in the system. The introduction of air, steam, and various gases into the vessel at selected locations and at controlled rates enables the economic, dependable and consistent production of these products.

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.

Processes for controlling afterburn in a reheater and loss of entrained solid particles in reheater flue gas are provided. Carbonaceous biomass feedstock is pyrolyzed using a heat transfer medium forming pyrolysis products and a spent heat transfer medium comprising combustible solid particles. The spent heat transfer medium is introduced into a fluidizing dense bed. The combustible solid particles of the spent heat transfer medium are combusted forming combustion product flue gas in a dilute phase above the fluidizing dense bed. The combustion product flue gas comprises flue gas and solid particles entrained therein. The solid particles are separated from the combustion product flue gas to form separated solid particles. At least a portion of the separated solid particles are returned to the fludizing dense bed.

Processes for controlling afterburn in a reheater and loss of entrained solid particles in reheater flue gas are provided. Carbonaceous biomass feedstock is pyrolyzed using a heat transfer medium forming pyrolysis products and a spent heat transfer medium comprising combustible solid particles. The spent heat transfer medium is introduced into a fluidizing dense bed. The combustible solid particles of the spent heat transfer medium are combusted forming combustion product flue gas in a dilute phase above the fluidizing dense bed. The combustion product flue gas comprises flue gas and solid particles entrained therein. The solid particles are separated from the combustion product flue gas to form separated solid particles. At least a portion of the separated solid particles are returned to the fludizing dense bed.