A fluidized catalyst stripping unit for displacing entrained gas from catalyst particles comprising: a vessel housing a two stage cyclonic separation section which comprises one or more primary cyclonic separation devices and one or more secondary cyclones; a stripping section which comprises internals; and an inlet in fluid communication with a catalytic reactor to feed a particulate-fluid suspension to the two stage cyclonic separation section; wherein each primary cyclonic separation device comprises an internal cylindrical surface to separate a major fraction of the particulates from the suspension and form a vortex of reduced particulate content; a particulate discharge outlet from each secondary cyclone to the stripping section; wherein the particulate discharge outlet of the secondary cyclone is submerged in a catalyst bed located above the stripper internals, and wherein the stripping section comprises one or more bubble breaking grids within the catalyst bed and above the stripping internals is provided.

A fluidized catalyst stripping unit for displacing entrained gas from catalyst particles comprising: a vessel housing a two stage cyclonic separation section which comprises one or more primary cyclonic separation devices and one or more secondary cyclones; a stripping section which comprises internals; and an inlet in fluid communication with a catalytic reactor to feed a particulate-fluid suspension to the two stage cyclonic separation section; wherein each primary cyclonic separation device comprises an internal cylindrical surface to separate a major fraction of the particulates from the suspension and form a vortex of reduced particulate content; a particulate discharge outlet from each secondary cyclone to the stripping section; wherein the particulate discharge outlet of the secondary cyclone is submerged in a catalyst bed located above the stripper internals, and wherein the stripping section comprises one or more bubble breaking grids within the catalyst bed and above the stripping internals is provided.

A system for converting carbonaceous fuels is provided. The system includes a gaseous fuel conversion reactor, a solid fuel conversion reactor, and a fuel pretreatment fluidized bed reactor disposed between the gaseous fuel conversion reactor and the solid fuel conversion reactor. The fuel pretreatment fluidized bed reactor devolatilizes a solid fuel using heat to produce an off-gas and a devolatilized solid fuel. The gaseous fuel conversion reactor converts the off-gas from the fuel pretreatment fluidized bed reactor to a product gas stream comprising carbon dioxide and water. The solid fuel conversion reactor receives a mixture of oxygen carrier solids and devolatilized solid fuel from the pretreatment reactor discharge and reduces the devolatilized solid fuel with the oxygen carrier solids to convert the devolatilized solid fuel to an intermediate gas.

A process for producing lower olefins from oxygenates includes the steps of contacting a feedstock comprising oxygenates with molecular sieve catalyst in fluidized bed reaction zone under effective conditions, to produce product including ethylene and/or propylene; the effective conditions include that in the fluidized bed reaction zone, the weights of catalysts having various carbon deposition amounts are controlled, calculated as the weight of the molecular sieve in the catalysts, to have the following proportions based on the total weight of the catalysts in the fluidized bed reaction zone: the proportion of the weight of the catalyst having a coke deposition amount of less than 3 wt % is 1-20 wt %; the catalyst having a coke deposition amount of from 3 wt % to less than 5 wt % represents 10 to 70 wt %; and the catalyst having a coke deposition amount from 5 wt % to 10 wt % represents 10 to 88 wt %.

Methods for distributing catalyst in a counter-current reactor may include passing the catalyst from a catalyst hopper to a perforated plate distributor; distributing the catalyst into a reaction zone of the counter-current reactor by passing the catalyst from a catalyst discharge zone, through the perforations of the perforated plate distributor, into the reaction zone, wherein the catalyst enters the perforations of the perforated plate distributor at a superficial velocity from 0.01 m/s to 10 m/s, and the superficial velocity is in a substantially downward direction; and passing a hydrocarbon feed stream into the reaction zone, wherein the catalyst moves in a substantially downward direction through the reaction zone, the hydrocarbon feed stream moves in a substantially upward direction through the reaction zone, and wherein contacting the catalyst with the hydrocarbon feed stream cracks one or more components of the hydrocarbon feed stream and forms a hydrocarbon product stream.

The present disclosure generally relates to a liquid-solid radial moving bed reaction apparatus comprising a radial moving bed reactor, a spent catalyst receiver, a catalyst regenerator, and a regenerated catalyst receiver that are successively connected. Also disclosed is a solid acid alkylation process using the liquid-solid radial moving bed reaction apparatus.

A reactor for carrying out an endothermic reaction, in particular a high-temperature reaction, in which a product gas is obtained from a feed gas, wherein: the reactor surrounds a reactor interior; the reactor is configured to provide a reactor bed in a reaction zone of the reactor interior, which reactor bed comprises a large number of solid material particles; the reactor is also configured to guide the feed gas into the reaction zone; in order to heat the feed gas, the reactor is designed to heat the solid material particles in the reaction zone such that, by transferring heat from the solid material particles to the feed gas, the feed gas in the reaction zone can be heated to a reaction temperature in order to participate as a starting product in the endothermic reaction for producing the product gas.

Methods for distributing catalyst in a counter-current reactor may include passing the catalyst from a catalyst hopper to a perforated plate distributor; distributing the catalyst into a reaction zone of the counter-current reactor by passing the catalyst from a catalyst discharge zone, through the perforations of the perforated plate distributor, into the reaction zone, wherein the catalyst enters the perforations of the perforated plate distributor at a superficial velocity from 0.01 m/s to 10 m/s, and the superficial velocity is in a substantially downward direction; and passing a hydrocarbon feed stream into the reaction zone, wherein the catalyst moves in a substantially downward direction through the reaction zone, the hydrocarbon feed stream moves in a substantially upward direction through the reaction zone, and wherein contacting the catalyst with the hydrocarbon feed stream cracks one or more components of the hydrocarbon feed stream and forms a hydrocarbon product stream.