A process can be used to prepare alkenes by catalytic conversion of synthesis gas to a first mixture comprising alkenes and alcohols. The alcohols present in the first mixture are converted to the corresponding alkenes by dehydration in a subsequent step. At least one alkene having two to four carbon atoms is obtained as isolated product from a product mixture by processing thereof and/or separation steps. In the catalytic conversion, a catalyst is preferably used that comprises grains of non-graphitic carbon having cobalt nanoparticles dispersed therein. The cobalt nanoparticles have an average diameter d.sub.p of 1-20 nm. An average distance D between individual cobalt nanoparticles in the grains is 2-150 nm. A combined total mass fraction ω of metal in the grains is from 30%-70% by weight of a total mass of the grains such that 4.5 dp/ω>D≥0.25 dp/ω.

A process can be used to prepare alkenes by catalytic conversion of synthesis gas to a first mixture comprising alkenes and alcohols. The alcohols present in the first mixture are converted to the corresponding alkenes by dehydration in a subsequent step. At least one alkene having two to four carbon atoms is obtained as isolated product from a product mixture by processing thereof and/or separation steps. In the catalytic conversion, a catalyst is preferably used that comprises grains of non-graphitic carbon having cobalt nanoparticles dispersed therein. The cobalt nanoparticles have an average diameter d.sub.p of 1-20 nm. An average distance D between individual cobalt nanoparticles in the grains is 2-150 nm. A combined total mass fraction ω of metal in the grains is from 30%-70% by weight of a total mass of the grains such that 4.5 dp/ω>D≥0.25 dp/ω.

A process for preparing C.sub.2 to C.sub.5 paraffins includes introducing a feed stream comprising hydrogen gas and a carbon-containing gas into a reaction zone of a reactor, and converting the feed stream into a product stream comprising C.sub.2 to C.sub.5 paraffins in the reaction zone in the presence of a hybrid catalyst. The hybrid catalyst includes a metal oxide catalyst component and a microporous catalyst component. The metal oxide catalyst component satisfies: an atomic ratio of Cu/Zn from 0.01 to 3.00; an atomic ratio of Cr/Zn from 0.01 to 1.50; and percentage of (Al+Cr) from greater than 0.0 at % to 50.0 at % based on a total amount of metal in the metal oxide catalyst component.

A process for preparing C.sub.2 to C.sub.5 paraffins includes introducing a feed stream comprising hydrogen gas and a carbon-containing gas into a reaction zone of a reactor, and converting the feed stream into a product stream comprising C.sub.2 to C.sub.5 paraffins in the reaction zone in the presence of a hybrid catalyst. The hybrid catalyst includes a metal oxide catalyst component and a microporous catalyst component. The metal oxide catalyst component satisfies: an atomic ratio of Cu/Zn from 0.01 to 3.00; an atomic ratio of Cr/Zn from 0.01 to 1.50; and percentage of (Al+Cr) from greater than 0.0 at % to 50.0 at % based on a total amount of metal in the metal oxide catalyst component.

A process for preparing C.sub.2 to C.sub.5 paraffins includes introducing a feed stream comprising hydrogen gas and a carbon-containing gas into a reaction zone of a reactor, and converting the feed stream into a product stream comprising C.sub.2 to C.sub.5 paraffins in the reaction zone in the presence of a hybrid catalyst. The hybrid catalyst includes a metal oxide catalyst component and a microporous catalyst component. The metal oxide catalyst component satisfies: an atomic ratio of Cu/Zn from 0.01 to 3.00; an atomic ratio of Cr/Zn from 0.01 to 1.50; and percentage of (Al+Cr) from greater than 0.0 at % to 50.0 at % based on a total amount of metal in the metal oxide catalyst component.

A process for preparing C.sub.2 to C.sub.5 paraffins includes introducing a feed stream comprising hydrogen gas and a carbon-containing gas into a reaction zone of a reactor, and converting the feed stream into a product stream comprising C.sub.2 to C.sub.5 paraffins in the reaction zone in the presence of a hybrid catalyst. The hybrid catalyst includes a metal oxide catalyst component and a microporous catalyst component. The metal oxide catalyst component satisfies: an atomic ratio of Cu/Zn from 0.01 to 3.00; an atomic ratio of Cr/Zn from 0.01 to 1.50; and percentage of (Al+Cr) from greater than 0.0 at % to 50.0 at % based on a total amount of metal in the metal oxide catalyst component.

Systems and methods are provided for conversion of oxygenate-containing feeds to a hydrocarbon effluent that includes a naphtha boiling range portion with an increased research octane number and/or increased octane rating. The conditions for converting the oxygenate-containing feed can correspond to conversion conditions for fluidized bed operation and/or moving bed operation, with a low acidity catalyst that also includes phosphorus to improve the hydrogen transfer rate relative to the expected hydrogen transfer rate for a low acidity catalyst. In addition to providing a naphtha fraction with an improved research octane number and/or octane rating, the amount of durene in the naphtha fraction can be reduced or minimized.

Systems and methods are provided for conversion of oxygenate-containing feeds to a hydrocarbon effluent that includes a naphtha boiling range portion with an increased research octane number and/or increased octane rating. The conditions for converting the oxygenate-containing feed can correspond to conversion conditions for fluidized bed operation and/or moving bed operation, with a low acidity catalyst that also includes phosphorus to improve the hydrogen transfer rate relative to the expected hydrogen transfer rate for a low acidity catalyst. In addition to providing a naphtha fraction with an improved research octane number and/or octane rating, the amount of durene in the naphtha fraction can be reduced or minimized.

Disclosed are a fluidized bed gas distributor and a fluidized bed reactor, the fluidized bed reactor comprising a first distributor (1) and a second distributor (2), wherein the first distributor (1) is located at the bottom of a fluidized bed, and second distributor (2) is located downstream of a gas from the first distributor (1). Also disclosed is a method for producing a para-xylene and co-producing light olefins, the method comprising the following steps: material stream A enters a reaction zone (3) of a fluidized bed reactor from a first gas distributor (1); material stream B enters the reaction zone (3) of the fluidized bed reactor from a second gas distributor (2); and the reactants are brought into contact with a catalyst in the reaction zone (3) to generate a gas phase stream comprising para-xylene and light olefins.

A process for preparing C.sub.2 to C.sub.5 paraffins includes introducing a feed stream comprising hydrogen gas and a carbon-containing gas into a reaction zone of a reactor, and converting the feed stream into a product stream comprising C.sub.2 to C.sub.5 paraffins in the reaction zone in the presence of a hybrid catalyst. The hybrid catalyst includes a metal oxide catalyst component and a microporous catalyst component. The metal oxide catalyst component satisfies: an atomic ratio of Cu/Zn from 0.01 to 3.00; an atomic ratio of Cr/Zn from 0.01 to 1.50; and percentage of (Al+Cr) from greater than 0.0 at % to 50.0 at % based on a total amount of metal in the metal oxide catalyst component.