Impure gaseous hydrogen chloride from organochlorosilane hydrolysis is freed of impurities by first scrubbing with an organochlorosilane, which may be the same or different from the organochlorosilane(s) hydrolyzed, and then further scrubbing with chloromethane. The purified gaseous hydrogen chloride is preferably used in chlorosilane synthesis.

The invention relates to a process for the treatment of a gas stream comprising hydrochloric acid, hydrofluoric acid and fluorinated/oxygenated compounds, in which the gas stream is successively subjected to: a stage of catalytic hydrolysis; a stage of washing with an acid solution; a stage of adsorption of impurities by active charcoal; a stage of adiabatic or isothermal absorption of the hydrochloric acid in an aqueous solution, making it possible to collect hydrochloric acid solution.

The invention relates to a process for the treatment of a gas stream comprising hydrochloric acid, hydrofluoric acid and fluorinated/oxygenated compounds, in which the gas stream is successively subjected to: a stage of catalytic hydrolysis; a stage of washing with an acid solution; a stage of adsorption of impurities by active charcoal; a stage of adiabatic or isothermal absorption of the hydrochloric acid in an aqueous solution, making it possible to collect hydrochloric acid solution.

Process for producing epichlorohydrin comprising subjecting to a dehydrochlorination operation, dichloropropanol produced from glycerol comprising aldehydes.

Disclosed is process for the production of (E) 1-chloro-3,3,3-trifluoropropene (HCFO-1233zd(E)) by conducting a continuous reaction without the use of a catalyst. Also disclosed is an integrated system for producing hydrofluoro olefins, particularly 1233zd(E). The manufacturing process includes six major unit operations: (1) a fluorination reaction of HCC-240fa (in continuous or semi-batch mode) using HF with simultaneous removal of by-product HCl and the product 1233zd(E); (2) recycle of unreacted HCC-240fa and HF together with under-fluorinated by-products back to (1); (3) separation and purification of by-product HCl; (4) separation of excess HF back to (1); (5) purification of final product, 1233zd(E); and (6) isomerization of by-product 1233zd(Z) to 1233zd(E) to maximize the process yield.

A process for the production of chlorine by thermo-catalytic gas phase oxidation of hydrogen chloride and oxygen is described, the process comprising at least (1) a cerium oxide catalyst and (2) an adiabatic reaction cascade, containing at least two adiabatic stages connected in series with intermediate cooling, wherein the molar O.sub.2/HCl-ratio is equal or above 0.75 in any part of the cerium oxide catalyst beds.

A sugar mixture comprising: monosaccharides; oligosaccharides in a ratio 0.06 to total saccharides; disaccharides in a ratio to total saccharides 0.05; pentose in a ratio to total saccharides 0.05; at least one alpha-bonded di-glucose; and at least one beta-bonded di-glucose. Also disclosed are methods to make and/or use such mixtures.

A process according to the invention is a process to separate an initial fluid stream comprising phosgene and hydrogen chloride in at least a first and a second fluid stream, said first fluid stream being a hydrogen chloride enriched and phosgene depleted gaseous stream, said second fluid stream being a hydrogen chloride depleted and phosgene enriched stream. The separation is performed by feeding said initial fluid stream to a membrane separation unit, said membrane separation unit separating said initial fluid stream in a first and a second fluid stream.

A method for producing a high-purity hydrogen chloride gas comprises performing a purification process that includes the steps 1) to 3) below on a byproduct hydrogen chloride gas: 1) a crude hydrochloric acid generation step of allowing water to absorb the byproduct hydrogen chloride gas; 2) a volatile organic impurity-removed hydrochloric acid generation step of bringing the crude hydrochloric acid obtained in the step 1) into contact with an inert gas at a liquid temperature of 20 to 45 C. to dissipate volatile organic impurities; and 3) a high-purity hydrogen chloride gas generation step of supplying the volatile organic impurity-removed hydrochloric acid obtained in the step 2) to a distillation column and performing distillation under conditions of a column bottom temperature of higher than 60 C. and 108 C. or lower and a column top temperature of 60 C. or lower to distill out a high-purity hydrogen chloride gas.

The apparatus includes one or more cylindrical housings connected to one another, a jacket on an outer side of a housing, an inner cylinder disposed at least in an interior of a first cylindrical housing, a heat insulation gasket, inner members, a corrosive high temperature gas inlet disposed on the heat insulation gasket, a gas and liquid phase outlet disposed at a bottom of the housing or a bottom of a last housing and a coolant inlet and outlet connected to an interior of the jacket. The heat insulation gasket seals the first cylindrical housing and a top of the inner cylinder in the interior of the first cylindrical housing. The inner members are distributed along a wall of the housing, communicate an interior of the jacket with an interior of the housing, and distribute a liquid in the interior of the jacket to the interior of the housing.