Processes for treating effluent streams in alkylation processes are described. One or more process streams rom HF alkylation processes, H.sub.2SO.sub.4 alkylation processes, or ionic liquid alkylation processes can be thermally oxidized in a thermal oxidation system. The thermal oxidation system can replace at least one of the caustic wash unit, the neutralization unit, and the acid gas treatment unit.

An HF olefin/isoparaffin alkylation process is carried out in an alkylation unit with a settling vessel in which the alkylate product is separated from the HF acid catalyst containing water and acid soluble oil (ASO). The density of the liquids in the settling vessel is measured at different levels by means of a nuclear density profile analyzer. The acid strength of the acid phase is determined from the density measurement and an optional temperature measurement. The proportion of water in the acid phase may also be measured separately by measurement of its electrical conductivity to determine the respective contributions of the water and the ASO to the density of the HF acid phase.

Processes for treating effluent streams in alkylation processes are described. One or more process streams rom HF alkylation processes, H.sub.2SO.sub.4 alkylation processes, or ionic liquid alkylation processes can be thermally oxidized in a thermal oxidation system. The thermal oxidation system can replace at least one of the caustic wash unit, the neutralization unit, and the acid gas treatment unit.

A process for acid catalyzed alkylation involving the use of surfactants which form bi-continuous micro-emulsions with the liquid acid and the hydrocarbon is described. The bicontinuous phase formed between the hydrocarbon and liquid acid phases at surfactant addition facilitates and improves the liquid acid catalyzed alkylation reactions including motor-fuel alkylation reaction.

A process is provided for producing linear alkylbenzenes with an improved yield from paraffin feed due to the use of a new catalyst that has a reduced selectivity to produce undesired aromatic compounds. In some embodiments, it is now possible to operate the process without including a unit to remove such aromatic compounds which allows for an operator of a plant to make modifications to the process to increase product yield.

The present invention relates to the integration of an alkylation unit for use in a hydrocarbon conversion process. More specifically, the present invention relates to the integration of a dehydrogenation unit and an alkylation unit and the placement of different isomerization units located off the deisobutanizer and the debutanizer.

A process for acid catalyzed alkylation involving the use of surfactants which form bi-continuous micro-emulsions with the liquid acid and the hydrocarbon is described. The bicontinuous phase formed between the hydrocarbon and liquid acid phases at surfactant addition facilitates and improves the liquid acid catalyzed alkylation reactions including motor-fuel alkylation reaction.

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 the integration of an alkylation unit for use in a hydrocarbon conversion process. More specifically, the present invention relates to the integration of a dehydrogenation unit and an alkylation unit and the placement of different isomerization units located off the deisobutanizer and the debutanizer.

The present invention relates to the integration of an alkylation unit for use in a hydrocarbon conversion process. More specifically, the present invention relates to the integration of a dehydrogenation unit and an alkylation unit and the placement of different isomerization units located off the deisobutanizer and the debutanizer.