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

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

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

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

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

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 thermochemical treatment system for plastic and/or elastomeric waste is described, having three Reaction Units (1), (2) and (3) connected in series, being performed in each Reaction Unit, under positive pressure and low temperature (between 200 C. and 660 C.), one step of the thermochemical treatment process of the plastic and/or elastomeric waste without pretreatment (grinding, washing and drying), through the indirect heating by molten salt coils (5), with the generation of a solid fraction which is continuously drained by an outlet (104); a gas fraction which is treated in a Gas Scrubbing Unit (10) for release into the atmosphere, and a liquid fraction (molten plastic) which is subjected to an endothermic reaction under positive pressure (between 2 and 10 bar) and at temperature above 300 C., which generates a gas fraction that is fed into a Heat Exchanger (13), wherein the condensable gases are converted into fractionated combustible liquids of carbon chains from 5 to 35, and the non-condensable combustible gases are reused for heating the system modules, with the excess heat constituting a thermal battery.

Pressure vessels containing a charge are preheated at pressure of 2 to 5 kPa with liquid heat carrier to maximally 120 C. They are afterheated in another place to maximally 550 C. The pressure vessels are continually added and/or replaced and generated gasses are continuously drawn off, cooled to maximally 60 C. and separated oily condensate. Residual gasses and solid residues are burned after treatment in a cogeneration unit.

Pressure vessels containing a charge are preheated at pressure of 2 to 5 kPa with liquid heat carrier to maximally 120 C. They are afterheated in another place to maximally 550 C. The pressure vessels are continually added and/or replaced and generated gasses are continuously drawn off, cooled to maximally 60 C. and separated oily condensate. Residual gasses and solid residues are burned after treatment in a cogeneration unit.

A reactor apparatus for a continuous depolymerization of polymers, in particular polyolefins from polymer wastes, includes a primary reactor, further includes a heating unit for a heating and a melting and for an at least partial depolymerization of the polymers within the primary reactor, and includes at least one primary circulation unit for a circulation of molten polymers in the primary reactor, wherein the reactor apparatus comprises a secondary reactor, which is connected downstream of the primary reactor and forms a reactor cascade with the primary reactor.