Disclosed herein are processes for producing neopentane. The processes generally relate to demethylating isooctane to produce neopentane. The isooctane may be provided by the alkylation of isobutane with butylenes.

Disclosed herein are processes for producing neopentane. The processes generally relate to demethylating isooctane to produce neopentane. The isooctane may be provided by the alkylation of isobutane with butylenes.

Processes for co-production of methyl tertiary-butyl ether (MTBE) and alkylate is disclosed. The process includes comprising passing a hydrocarbon feed stream comprising C.sub.4 hydrocarbons to a dehydrogenation unit to generate a dehydrogenation effluent comprising C.sub.4 olefins. The dehydrogenation effluent is passed to a MTBE unit to provide a mixed stream comprising C.sub.4 olefins and MTBE. The mixed stream is separated to provide an MTBE product stream and a fractionator overhead stream comprising olefins. The fractionator overhead stream is passed to an alkylation unit to produce an alkylation product stream comprising an alkylate.

Apparatuses and processes for converting an oxygenate feedstock, such as methanol and/or dimethyl ether, in a fluidized bed containing a catalyst to hydrocarbons, such as gasoline boiling components, olefins and aromatics are provided herein.

Apparatuses and processes for converting an oxygenate feedstock, such as methanol and/or dimethyl ether, in a fluidized bed containing a catalyst to hydrocarbons, such as gasoline boiling components, olefins and aromatics are provided herein.

The invention relates to a process for preparing 1,3-butadiene from n-butenes, comprising the steps of: A) providing an input gas stream a comprising butanes, 1-butene, 2-butene and isobutene, with or without 1,3-butadiene, from a fluid catalytic cracking plant; B) removing isobutene from the input gas stream a, giving a stream b comprising butanes, 1-butene and 2-butene, with or without 1,3-butadiene; C) feeding the stream b comprising butanes, 1-butene and 2-butene and optionally an, oxygenous gas and optionally water vapor into at least one dehydrogenating zone and dehydrogenating 1-butene and 2-butene to 1,3-butadiene, giving a product gas stream c comprising 1,3-butadiene, butanes, 2-butene and water vapor, with or without oxygen, with low-boiling hydrocarbons, with high-boiling secondary components, with or without carbon oxides and with or without inert gases; D) cooling and compressing the product gas stream c, giving at least one aqueous condensate stream d1 and a gas stream d2 comprising 1,3-butadiene, butanes, 2-butene and water vapor, with or without oxygen, with low-boiling hydrocarbons, with or without carbon oxides and with or without inert gases; Ea) removing uncondensable and low-boiling gas constituents comprising low-boiling hydrocarbons, with or without oxygen, with or without carbon oxides and with or without inert gases, as gas stream e2 from the gas stream d2 by absorbing the C.sub.4 hydrocarbons comprising 1,3-butadiene, butanes and 2-butene in an absorbent, giving an absorbent stream laden with C.sub.4 hydrocarbons and the gas stream e2, and Eb) subsequently desorbing the C.sub.4 hydrocarbons from the laden absorbent stream, giving a C.sub.4 hydrocarbon stream e1; F) separating the C.sub.4 hydrocarbon stream e1 by extractive distillation with a 1,3-butadiene-selective solvent into a stream f1 comprising 1,3-butadiene and the selective solvent and a stream f2 comprising butanes and 2-butene, wherein at least 90% of the 1-butene present in stream b is converted in step C) and a product stream f2 comprising butanes and 2-butene is obtained in step F.

The invention relates to a process for preparing 1,3-butadiene from n-butenes, comprising the steps of: A) providing an input gas stream a comprising butanes, 1-butene, 2-butene and isobutene, with or without 1,3-butadiene, from a fluid catalytic cracking plant; B) removing isobutene from the input gas stream a, giving a stream b comprising butanes, 1-butene and 2-butene, with or without 1,3-butadiene; C) feeding the stream b comprising butanes, 1-butene and 2-butene and optionally an, oxygenous gas and optionally water vapor into at least one dehydrogenating zone and dehydrogenating 1-butene and 2-butene to 1,3-butadiene, giving a product gas stream c comprising 1,3-butadiene, butanes, 2-butene and water vapor, with or without oxygen, with low-boiling hydrocarbons, with high-boiling secondary components, with or without carbon oxides and with or without inert gases; D) cooling and compressing the product gas stream c, giving at least one aqueous condensate stream d1 and a gas stream d2 comprising 1,3-butadiene, butanes, 2-butene and water vapor, with or without oxygen, with low-boiling hydrocarbons, with or without carbon oxides and with or without inert gases; Ea) removing uncondensable and low-boiling gas constituents comprising low-boiling hydrocarbons, with or without oxygen, with or without carbon oxides and with or without inert gases, as gas stream e2 from the gas stream d2 by absorbing the C.sub.4 hydrocarbons comprising 1,3-butadiene, butanes and 2-butene in an absorbent, giving an absorbent stream laden with C.sub.4 hydrocarbons and the gas stream e2, and Eb) subsequently desorbing the C.sub.4 hydrocarbons from the laden absorbent stream, giving a C.sub.4 hydrocarbon stream e1; F) separating the C.sub.4 hydrocarbon stream e1 by extractive distillation with a 1,3-butadiene-selective solvent into a stream f1 comprising 1,3-butadiene and the selective solvent and a stream f2 comprising butanes and 2-butene, wherein at least 90% of the 1-butene present in stream b is converted in step C) and a product stream f2 comprising butanes and 2-butene is obtained in step F.

The present invention relates to free radical reaction methods in which low molecular weight, C2 to C6, unsaturated organic compounds such as ethylene and/or propylene are reacted with low molecular weight, C1 to C15, preferably C1 to C10 saturated organic compounds to form low molecular weight, linear or branched C3 to C24, preferably C3 to C12 organic compounds. The present invention is based at least in part upon the concept of carrying out the free radical reaction in the presence of a typically low concentrations of the unsaturated reactant(s) in the reaction zone(s). By doing this, chain transfer mechanisms are more favored while chain extension mechanisms are less favored. In some embodiments, principles of the present invention are helpful to create conditions under which chain transfer to form more stable, secondary or tertiary branched radicals is favored over olefin addition via chain extension.

The present invention relates to free radical reaction methods in which low molecular weight, C2 to C6, unsaturated organic compounds such as ethylene and/or propylene are reacted with low molecular weight, C1 to C15, preferably C1 to C10 saturated organic compounds to form low molecular weight, linear or branched C3 to C24, preferably C3 to C12 organic compounds. The present invention is based at least in part upon the concept of carrying out the free radical reaction in the presence of a typically low concentrations of the unsaturated reactant(s) in the reaction zone(s). By doing this, chain transfer mechanisms are more favored while chain extension mechanisms are less favored. In some embodiments, principles of the present invention are helpful to create conditions under which chain transfer to form more stable, secondary or tertiary branched radicals is favored over olefin addition via chain extension.

A process, comprising: providing an olefin feed comprising pentenes, butenes, and isopentane; and alkylating the olefin feed with isobutane using an acidic ionic liquid catalyst; wherein less than 5 mol % of C5 olefins in the olefin feed are converted to isopentane, and the alkylate gasoline has defined final boiling points and high RONs. A process comprising: alkylating an olefin feed comprising pentenes and isopentane, with isobutane using an acidic ionic liquid catalyst; wherein less than 5 mol % of C5 olefins in the olefin feed are converted to isopentane; and wherein an n-pentane product yield is low. An alkylate gasoline, comprising less than 0.1 wt % olefins and aromatics, less than 1.8 wt % C12+hydrocarbons, and greater than 60 wt % combined C8 and C9 hydrocarbons, wherein the trimethylpentane in the C8 hydrocarbons and the trimethylhexane in the C9 hydrocarbons are defined.