213results about "Effluent separation" patented technology

The invention relates to an installation and a process for the production of liquid fuels starting from a solid feedstock that contains the organic material in which:a) the solid feedstock is subjected to a gasification stage so as to convert said feedstock into synthesis gas,b) the synthesis gas is subjected to a purification treatment,c) the purified synthesis gas is subjected to a conversion stage that comprises the implementation of a Fischer-Tropsch-type synthesis so as to convert said synthesis gas into a liquid effluent and a gaseous effluent,d) the liquid effluent is fractionated so as to obtain a gaseous fraction, a naphtha fraction, a kerosene fraction and a gas oil fraction, ande) at least a portion of the naphtha fraction is recycled in gasification stage a).

A method for utilizing natural gas condensate as a feedstock for an olefin production plant wherein the feedstock is subjected to vaporization and separation conditions that remove light hydrocarbons from the condensate for thermal cracking in the plant, and leave liquid distillate for separate recovery.

The invention concerns a process for treating a hydrocarbon feed comprising a series of a first upstream process for hydrocarbon hydroconversion comprising at least one reaction chamber, the reaction or reactions occurring inside said chambers and employing at least one solid phase, at least one liquid phase and at least one gas phase, and a second downstream steam reforming process comprising at least one reaction chamber, characterized in that the said upstream process is carried out in a “slurry” and / or an ebullated bed mode and in that the downstream process comprises a first step for at least partial conversion of hydrocarbons heavier than methane into methane, termed the pre-reforming step, and in that the reaction or reactions occurring inside the chambers of the downstream stream reforming process enables the production of a reagent, namely hydrogen, which is necessary for the reactions in the first upstream process.

A method for utilizing a feed comprising condensate and crude oil for an olefin production plant is disclosed. The feed is subjected to vaporization and separated into vaporous hydrocarbons and liquid hydrocarbons. The vaporous hydrocarbons stream is thermally cracked in the plant. The liquid hydrocarbons are recovered.

Disclosed is a combined process for hydrotreating and catalytic cracking of residue, wherein the residue, catalytic cracking heavy cycle oil with acidic solid impurity being removed, optional distillate oil and adistillate of catalytic cracking slurry oil from which the acidic solid impurity is removed are fed into residue hydrotreating unit, the hydrogenated residue obtained and optional vacuum gas oil are fed into catalytic cracking unit to obtain various products; the catalytic cracking heavy cycle oil from which the acidic solid impurity is removed is circulated to the residue hydrotreating unit; the catalytic cracking slurry oil is separated by distilling, the distillate of the catalytic cracking slurry oil after removing off the acidic solid impurity is circulated to the residue hydrotreating unit. This process makes the residue hydrotreating and catalytic cracking being combined together more effectively such that it is not only able to improve product quality of the residue hydrotreating, elongate operation cycle of the residue hydrotreating unit, but also increases the yield of the hydrogenated diesel oil and catalytic cracking light oil, and decreases coking quantity of the catalytic cracking.

A process for selectively producing C3 olefins from a catalytically cracked or thermally cracked naphtha stream is disclosed herein. The naphtha stream is introduced into a process unit comprised of a reaction zone, a stripping zone containing a dense phase, a catalyst regeneration zone, and a fractionation zone. The naphtha feedstream is contacted in the reaction zone with a catalyst containing from about 10 to about 50 wt. % of a crystalline zeolite having an average pore diameter less than about 0.7 nanometers at reaction conditions. Vapor products are collected overhead and the catalyst particles are passed through the stripping zone on the way to the catalyst regeneration zone. Volatiles are stripped with steam in the stripping zone and the catalyst particles are sent to the catalyst regeneration zone where coke is burned from the catalyst, and are then recycled to the reaction zone. Overhead products from the reaction zone are passed to a fractionation zone where a stream of C3 products is recovered and a stream rich in C4 olefins is recycled to a dilute phase reaction zone in the stripping zone separate from the dense phase of the stripping zone. The olefins can be further processed and polymerized to form a variety of polymer materials.