The invention generally relates to processes for reducing fouling in amine systems and to equipment useful in such processes. Such amine systems are useful for removing one or more acidic gases such as CO.sub.2 or H.sub.2S from olefin containing hydrocarbon streams. The invention generally relates to minimizing residence time of foulant and foulant precursors at the relatively high temperature found in the amine regenerator and/or to purging the foulant and foulant precursors from the regenerator system. This is accomplished by operating the regenerator column as a stripper (no reflux) and re-routing reflux liquid containing foulant or foulant precursors to a processing location that is less prone to fouling or, optionally, by replacing the reflux liquid with fresh make-up amine or water.

This invention is directed to methods for recovery of C3-C6 alcohols. The recovery process advantageously utilizes the immiscible properties of a first phase liquid and a second phase liquid to separate the liquids prior to processing C3-C6 alcohols to recovery. The invention is also directed to C3-C6 alcohol-containing compositions.

A method for preparing a purified styrene composition is provided. The method includes providing a crude composition and subjecting the crude composition to at least one crystallization step. The crude composition contains 70% by weight or more styrene based on the total weight of the crude composition. The at least one crystallization step comprises at least one of a static crystallization stage and a dynamic crystallization stage. The crude composition contains at least one impurity selected from the group consisting of: color inducing species, oxygenates, sulfur species, alpha-methylstyrene, and mixtures thereof.

Processes for converting methane and/or other hydrocarbons to synthesis gas (i.e., a gaseous mixture comprising H.sub.2 and CO) are disclosed, in which at least a portion of the hydrocarbon(s) is reacted with CO.sub.2. At least a second portion of the methane may be reacted with H.sub.2O (steam), thereby improving overall thermodynamics of the process, in terms of reducing endothermicity (ΔH) and the required energy input, compared to “pure” dry reforming in which no H.sub.2O is present. Such dry reforming (reaction with CO.sub.2 only) or CO.sub.2-steam reforming (reaction with both CO.sub.2 and steam) processes are advantageously integrated with Fischer-Tropsch synthesis to yield liquid hydrocarbon fuels. Further integration may involve the use of a downstream finishing stage involving hydroisomerization to remove FT wax. Yet other integration options involve the use of combined CO.sub.2-steam reforming and FT synthesis stages (optionally with finishing) for producing liquid fuels from gas streams generated in a number of possible processes, including the hydropyrolysis of biomass.

PROBLEM To provide a composition comprising highly enriched PUFA or its alkyl esters while containing fatty acid esters of 3-MCPD at adequately low concentrations and to provide an efficient method for producing the composition. MEANS FOR SOLVING A composition that contains fatty acids or fatty acid alkyl esters as its major component, the composition containing highly unsaturated fatty acid or alkyl ester thereof, wherein the proportion of the highly unsaturated fatty acid in the constituent fatty acids of the composition is 50 area % or more and wherein the concentration of 3-MCPD as found upon analyzing the composition by American Oil Chemists' Society official method Cd 29b-13 assay A is less than 1.80 ppm.

The invention provides a built-in micro-interface oxidation system for preparing terephthalic acid from p-xylene. The oxidation system includes a first reactor, a rectifying tower and a second reactor which are sequentially connected. A first outlet is disposed on a side wall of the first reactor; a first inlet is disposed on a side wall of the second reactor; a material inlet is disposed on a side wall of the rectifying tower; and a material outlet is disposed at a bottom of the rectifying tower. The first outlet is connected with the material inlet of the rectifying tower; the first inlet is connected with the material outlet of the rectifying tower. Micro-interface units are arranged in the first reactor and the second reactor for dispersing and crushing air into bubbles. Through disposing micro-interface units in reactors, problems of high energy consumption, high raw material consumption and low reaction efficiency are solved.

Improved systems and methods for producing propylene from olefins including isobutylene is disclosed. The improvements combine streams containing co-produced 1-butene, 2-butene, butadiene, and heavy olefins (C5+) exiting both a metathesis reactor and a skeletal isomerization reactor in a gasoline fractionation tower to remove the heavy olefins. The C4-containing distillate from the gasoline fractionation tower is then fed to a hydroisomerization unit to form mono-olefins and 2-butene. The resulting 2-butene rich stream can then be utilized in metathesis reactions to increase the production of propylene while increasing the lifetime of the metathesis catalyst.

Method and Apparatus for separating at least one CO isotope compound, especially isotope compound 13C16O, from natural CO, comprising: a rectification column system (110) comprising a plurality of rectification sections (112,114,116,118,120) arranged adjacent to one another in a chain-like manner, including an upper rectification section (112) and a plurality of lower rectification sections (114,116,118,120), each rectification section comprising a heating means (112a,114a,116a,118a,120a) to maintain evaporation of liquid present therein, provided that the heating means (112a) of the at least one of the plurality of rectification sections (112) is provided to comprise a heat pump cycle (112b).

A process for recovering an ethylene oxide (EO) enriched product stream from fat absorbent (FA) comprising water, EO, and acetaldehyde. The process comprises passing a feed of FA from a loopgas EO absorber to a multi-stage countercurrent distillation zone, the feed of FA having a concentration of EO in the range of from about 1 to about 15 wt % upon entering the distillation zone; and obtaining from the distillation zone an acetaldehyde enriched stream, a lean absorbent (LA) stream, a vapour stream enriched in light ends, a glycol enriched bottoms stream and an EO enriched product stream. Suitable apparatus is also disclosed.

Separation of chlorosilane mixtures containing boron, arsenic, and/or phosphorus impurities is facilitated by a distillative separation using at least one divided column, with recycle streams to a first column being passed through an external absorbent for the impurities.