The invention provides a use of metal ferrite oxygen carrier for converting carbon dioxide to carbon monoxide or synthesis gas via three processes: catalytic dry reforming of methane, chemical looping dry reforming of fuel and promoting coal gasification with CO.sub.2. The metal ferrite oxygen carrier comprises M.sub.zFe.sub.xO.sub.y, where M.sub.zFe.sub.xO.sub.y is a chemical composition with 0<x4, z>0 and 0<y6 and M is one of Ca, Ba, and/or combinations thereof. For example, M.sub.zFe.sub.xO.sub.y may be one of CaFe.sub.2O.sub.4, BaFe.sub.2O.sub.4, MgFe.sub.2O.sub.4, SrFe.sub.2O.sub.4 and/or combinations thereof. In catalytic dry reforming, methane and carbon dioxide react in the presence of metal ferrites generating a product stream comprising at least 50 vol. % CO and H.sub.2. In another embodiment, chemical looping dry reforming process where metal ferrite is reduced with a fuel and then oxidized with carbon dioxide is used for production of CO from carbon dioxide. In another embodiment, the metal ferrite is used as a promoter to produce CO continuously from coal gasification with CO.sub.2.

A lift engager for providing a stream of fluidized catalyst particles with an adjustable conduit and process using the lift engager. The lift engager includes a vessel with an inlet configured to receive catalyst from a reaction zone. A first conduit, within the vessel, is configured to supply lift gas into the lift engager. The first conduit includes a fixed member and a movable member secured to the fixed member and is configured to adjust a length of the first conduit within the vessel. A second conduit inside the first conduit and configured to provide fluidized catalyst to a regeneration zone.

A process for producing a carbon dioxide depleted synthesis gas product by steam reforming is provided. The process includes cooling crude synthesis gas stream produced in a main reforming stage in a first cooling device and reacting in a carbon dioxide absorption column, reacting a carbon dioxide loaded absorbent stream from the carbon dioxide absorption column in an absorbent regeneration column, cooling the carbon dioxide enriched hot vapor stream from the absorbent regeneration column in a second cooling device and cooling a carbon dioxide depleted hot absorbent stream from the absorbent regeneration column in a third cooling device. Preheated air streams from the cooling devices are fed as oxidant to the main reforming stage.

A process for producing a carbon dioxide depleted synthesis gas product by steam reforming is provided. The process includes cooling crude synthesis gas stream produced in a main reforming stage in a first cooling device and reacting in a carbon dioxide absorption column, reacting a carbon dioxide loaded absorbent stream from the carbon dioxide absorption column in an absorbent regeneration column, cooling the carbon dioxide enriched hot vapor stream from the absorbent regeneration column in a second cooling device and cooling a carbon dioxide depleted hot absorbent stream from the absorbent regeneration column in a third cooling device. Preheated air streams from the cooling devices are fed as oxidant to the main reforming stage.

The invention provides a use of metal ferrite oxygen carrier for converting carbon dioxide to carbon monoxide or synthesis gas via three processes: catalytic dry reforming of methane, chemical looping dry reforming of fuel and promoting coal gasification with CO.sub.2. The metal ferrite oxygen carrier comprises M.sub.zFe.sub.xO.sub.y, where M.sub.zFe.sub.xO.sub.y is a chemical composition with 0<x4, z>0 and 0<y6 and M is one of Ca, Ba, and/or combinations thereof. For example, M.sub.zFe.sub.xO.sub.y may be one of CaFe.sub.2O.sub.4, BaFe.sub.2O.sub.4, MgFe.sub.2O.sub.4, SrFe.sub.2O.sub.4 and/or combinations thereof. In catalytic dry reforming, methane and carbon dioxide react in the presence of metal ferrites generating a product stream comprising at least 50 vol. % CO and H.sub.2. In another embodiment, chemical looping dry reforming process where metal ferrite is reduced with a fuel and then oxidized with carbon dioxide is used for production of CO from carbon dioxide. In another embodiment, the metal ferrite is used as a promoter to produce CO continuously from coal gasification with CO.sub.2.

The present invention relates generally to processes for hydromethanating a carbonaceous feedstock in a hydromethanation reactor to a methane-enriched raw product stream, and more specifically to processing of solid char by-product removed from the hydromethanation reactor to improve the carbon utilization and thermal efficiency of the overall process and thereby lower the net costs of the end-product pipeline quality substitute natural gas.

A lift engager for providing a stream of fluidized catalyst particles with an adjustable conduit and process using the lift engager. The lift engager includes a vessel with an inlet configured to receive catalyst from a reaction zone. A first conduit, within the vessel, is configured to supply lift gas into the lift engager. The first conduit includes a fixed member and a movable member secured to the fixed member and is configured to adjust a length of the first conduit within the vessel. A second conduit inside the first conduit and configured to provide fluidized catalyst to a regeneration zone.

The disclosed technology provides processes for producing hydrogen that is renewable, has negative carbon intensity, and is associated with net water production. The hydrogen is economically, environmentally, and socially superior to conventional hydrogen via steam reforming of natural gas or electrolysis of water. Some variations provide a process for manufacturing carbon-negative hydrogen and optionally activated carbon, comprising: feeding biomass into a first heated vessel or zone to generate dried biomass and a first recovered water stream; feeding the dried biomass into a second heated vessel or zone to pyrolyze the dried biomass, generating a biocatalyst and a biogas; feeding the biocatalyst, the first recovered water stream, and biogas to a third heated vessel or zone for biocatalytic conversion, thereby generating H.sub.2, CO, and optionally activated carbon; and recovering the hydrogen. The H.sub.2 is carbon-negative hydrogen characterized by a carbon intensity less than 0 kg CO.sub.2e per metric ton H.sub.2.

The disclosed technology provides processes for producing hydrogen that is renewable, has negative carbon intensity, and is associated with net water production. The hydrogen is economically, environmentally, and socially superior to conventional hydrogen via steam reforming of natural gas or electrolysis of water. Some variations provide a process for manufacturing carbon-negative hydrogen and optionally activated carbon, comprising: feeding biomass into a first heated vessel or zone to generate dried biomass and a first recovered water stream; feeding the dried biomass into a second heated vessel or zone to pyrolyze the dried biomass, generating a biocatalyst and a biogas; feeding the biocatalyst, the first recovered water stream, and biogas to a third heated vessel or zone for biocatalytic conversion, thereby generating H.sub.2, CO, and optionally activated carbon; and recovering the hydrogen. The H.sub.2 is carbon-negative hydrogen characterized by a carbon intensity less than 0 kg CO.sub.2e per metric ton H.sub.2.

A reactor configuration is proposed for selectively converting gaseous, liquid or solid fuels to a syngas specification which is flexible in terms of H.sub.2/CO ratio. This reactor and system configuration can be used with a specific oxygen carrier to hydro-carbon fuel molar ratio, a specific range of operating temperatures and pressures, and a co-current downward moving bed system. The concept of a CO.sub.2 stream injected in-conjunction with the specified operating parameters for a moving bed reducer is claimed, wherein the injection location in the reactor system is flexible for both steam and CO.sub.2 such that, carbon efficiency of the system is maximized.