Exxon Research and Engineering Company

Other

Occidental Research Corporation

Frederic Leder

Guido Sartori

Cyrus A Irani

Robert P Cahn

George M Kramer

Stephen S Kasegrande

Daniel J McHugh

Christa G Kuehn

Herman J Solomon

Apparatus and method for the production of hydrogen peroxide in either a neutral, acidic or an alkaline solution utilizes a three compartment cell having an acid resistant anode, a gas-diffusion cathode, and both an anion and a cation membrane. Acid electrolyte is introduced between the anode and the cation membrane while a basic electrolyte is introduced between the cathode and the anion membrane. A neutral, acidic, or basic solution is introduced between the anion and cation membrane wherein hydrogen ions generated passing through the cation membrane and O.sub.2 H.sup.- ions passing through the anion membrane react to form hydrogen peroxide.

Three compartment electrolytic cell method for producing hydrogen

Acidic gases are substantially removed from a normally gaseous mixture by a process comprising contacting the normally gaseous mixture with an amine-solvent liquid absorbent comprising (i) an amine comprised of at least about 50 mol % of a sterically hindered amine, and (ii) a solvent for said amine mixture which is also a physical absorbent for said acidic gases. The liquid absorbent may also include up to about 35 weight percent water.

Process and amine-solvent absorbent for removing acidic gases from

Carbon dioxide containing acidic gases are removed from a normally gaseous mixture by a process comprising contacting the normally gaseous mixture with an aqueous solution comprising (a) a basic alkali metal salt or hydroxide and (b) an activator for said basic salt or alkali metal salt or hydroxide comprising at least one sterically hindered amine.

Process for removing carbon dioxide containing acidic gases from gaseous

Petroleum fractions may be separated into aromatic rich and paraffinic-rich hydrocarbon streams by the use of methanol/water mixtures having at least 10% water by volume. The paraffinic-rich stream is recovered as raffinate and the aromatic-rich as extract. After the extraction step additional water is added to the extract and raffinate streams where it acts as an anti-solvent to effect separation of the hydrocarbon from the solvent. The water and methanol are then separated for example by flash distillation or by using super critical CO.sub.2 as an extraction solvent.

Process for aromatics extraction from a 300.degree.-430.degree. F.

A method for producing sulfur from sulfur dioxide. In the broadest embodiment, sulfur is produced by reducing the sulfur dioxide with a reducing gas comprising one or more lower, monohydric alcohols. The reduction may be accomplished either thermally or catalytically and the principal products obtained will be elemental sulfur and/or hydrogen sulfide, depending principally upon the particular conditions and relative reactive concentrations actually employed and in some cases, at least, some carbon oxysulfide will be produced. In the broadest embodiment, the reduction, and hence, the sulfur production will be accomplished in a single stage. In the more preferred embodiments, however, the production will be accomplished in a plurality of stages and, in a most preferred embodiment, the sulfur dioxide is first contacted with methanol under conditions such that the molar ratio of the hydrogen sulfide and carbon oxysulfide actually produced to the unconverted sulfur dioxide is within the range from about 1.8:1 to about 2.2:1. The H.sub.2 S, COS and SO.sub.2 will then be further reacted in one or more catalytic converters so as to increase the sulfur yield. Conventional Claus plant equipment can be used to effect this further conversion.

Method of producing sulfur from sulfur dioxide

A forced convection heat exchanger for warming articles such as baby bottles is provided comprising a container having walls extending upwardly from a bottom end to define an open top end. A platform to receive and support the article to be warmed is mounted within the container spaced apart from the container bottom end. A plurality of spacers extend inwardly from the walls and upwardly from the platform. First drain openings are provided extending through the platform and second drain openings are provided within the walls below the platform adjacent the bottom end. The area of the platform relative to the total cross-sectional area of the first drain openings is dimensioned so as to provide a standing head of water under turbulent flow conditions within the container substantially up to the container open top end when the container receives an average flow of water from a tap.

Forced convection heat exchanger for warming articles

Carbon dioxide containing acidic gases are substantially removed from a normally gaseous mixture by a process comprising contacting the normally gaseous mixture with an aqueous amine solution, wherein at least one of the amines is a sterically hindered amine. The process is operated at a thermodynamic cyclic capacity (as determined from the vapor liquid equilibrium isotherm of the vapor-liquid system) which is greater than in an aqueous amine CO.sub.2 scrubbing process wherein monoethanolamine is the only amine utilized under similar conditions of gaseous feed composition, scrubbing solution composition, temperatures and pressures. A particularly preferred sterically hindered amine is 2-amino-2-methyl-1-propanol.

A hydrocarbon feed is isomerized in liquid phase in the presence of a metal halide catalyst, a hydrogen halide solvent and hydrogen at a temperature ranging from at least 50.degree.C and not greater than the critical temperature of the mixture of the hydrocarbon feed and the hydrogen halide. The partial pressure of the hydrocarbon feed-hydrogen halide mixture is maintained to be at least equal to the critical pressure of the hydrocarbon feed and not greater than the critical pressure of the mixture of the hydrocarbon feed and the hydrogen halide. The molar ratio of the hydrogen halide to the hydrocarbon feed is at least 1:1 and the molar ratio of hydrogen halide to metal halide catalyst ranges from about 10:1 to about 40:1. The preferred catalyst is aluminum chloride or aluminum bromide. The preferred solvent is hydrogen chloride or hydrogen bromide.

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Corona Del Mar, CA, United States of America

Frederic Leder