Uop Lcc

David E Mackowiak

Christopher P Nicholas

Alakananda A Bhattacharyya

Tamotsu Imai

Gregory J Gajda

Paul T Barger

Edwin Paul Boldingh

Antoine Negiz

James E Rekoske

Dean E Rende

Jeffery C Bricker

Michael J McCall

Edwin H Homeier

Robert J Allen

Hayim Abrevaya

Vladislav Ivanov Kanazirev

Mark J O'Hara

Susie C Martins

Joel T Walenga

Catherine E Guzolek

A process for sulfuric acid catalyzed alkylation involving the use of surfactants which form bi-continuous micro-emulsions with the sulfuric acid and the hydrocarbon is described. The bi-continuous phase facilitates and improves the sulfuric acid catalyzed alkylation reactions. The concentration of the surfactant is selected based on the type of olefin feed. Easy to alkylate feeds, such as 2-butene, use lower concentrations of surfactant, while feeds which are harder to alkylate, such as propene or isobutene, use higher concentrations of the surfactant. In addition, increasing the concentration of sulfuric acid when a surfactant is included resulted in higher calculated RON. The use of a surfactant and a high concentration of sulfuric acid can provide a calculated RON over 100 and close to theoretical yields.

Sulfuric acid catalyzed alkylation process

One exemplary embodiment can be a process for increasing a mole ratio of methyl to phenyl of one or more aromatic compounds in a feed. The process can include reacting an effective amount of one or more aromatic compounds and an effective amount of one or more aromatic methylating agents to form a product having a mole ratio of methyl to phenyl of at least about 0.1:1 greater than the feed.

Process for increasing a mole ratio of methyl to phenyl

The process and apparatus converts ethylene in a dilute ethylene stream that may be derived from an FCC product to heavier hydrocarbons. The catalyst may be an amorphous silica-alumina base with a Group VIII and/or VIB metal. The catalyst is resistant to feed impurities such as hydrogen sulfide, carbon oxides, hydrogen and ammonia. At least 40 wt-% of the ethylene in the dilute ethylene stream can be converted to heavier hydrocarbons.

Process for oligomerizing dilute ethylene

One exemplary embodiment can be a process for increasing a mole ratio of methyl to phenyl of one or more aromatic compounds in a feed. The process can include reacting an effective amount of one or more aromatic compounds and an effective amount of one or more non-aromatic compounds to convert about 90%, by weight, of one or more C6non-aromatic compounds.

Process for increasing methyl to phenyl mole ratios and reducing benzene content in a motor fuel product

One exemplary embodiment can be a process using an aromatic methylating agent. Generally, the process includes reacting an effective amount of the aromatic methylating agent having at least one of an alkane, a cycloalkane, an alkane radical, and a cycloalkane radical with one or more aromatic compounds. As such, at least one of the one or more aromatic compounds may be converted to one or more higher methyl substituted aromatic compounds to provide a product having a greater mole ratio of methyl to phenyl than a feed.

Aromatic aklylating agent and an aromatic production apparatus

Apparatus for oligomerizing dilute ethylene

A method for preparing biomass for slurry processing. The method includes solubilizing the solid material into either a dissolved state or a suspended solid in a liquid phase, and processing the liquid phase to produce chemicals and fuels.

Enhancing conversion of lignocellulosic biomass

A method for preparing biomass for slurry processing. The method includes solubilizing the solid material into either a dissolved state or a suspended solid in a liquid phase, and treating the liquid phase to produce chemicals and fuels.

Conversion of lignocellulosic biomass to chemicals and fuels

The process of the invention comprises contacting a hydrocarbon stream, comprising light olefins plus impurities such as acetylenes, in the absence of hydrogen with a supported copper catalyst, preferably CuO/alumina. The acetylene component undergoes a coupling reaction producing a diacetylene which can be more readily removed. Thus, the methylacetylene (MA) contaminant in liquid propylene yields at about 80&#xb0; C. and 3792 kPa (550 psig) a significant amount dimethyl diacetylene (2,4-hexadiyne). Surprisingly, very little cyclization products are present. The process is useful for purification of olefin feeds. It can be used alone or in combination with known purification methods such as catalytic distillation or selective hydrogenation.

Method for removal of acetylenes from hydrocarbon streams

Dehydrogenatable hydrocarbons may be subjected to a dehydrogenation reaction in which the hydrocarbons are treated with a dehydrogenation catalyst comprising a modified iron catalyst in the presence of steam in a multicatalyst bed system. The reaction mixture containing unconverted hydrocarbons, dehydrogenated hydrocarbons, hydrogen and steam is then contacted with an oxidation catalyst whereby hydrogen is selectively oxidized. The selective oxidation catalyst which is used will comprise a noble metal of Group VIII of the Periodic Table, a metal of Group IVA and, if so desired, a metal of Group IA or IIA composited on a porous inorganic support. The inorganic support will comprise an alumina precursor which possesses and ABD less than about 0.6 g/cc, a pore volume greater than about 0.5 cc/g, and a pore distribution such that between 10% and 70% of the pore volume is present as pores whose diameters are greater than about 300 Angstroms. After peptizing and calcination at a temperature of about 900.degree. to about 1500.degree. C., the resulting alumina will possess an ABD in the range of from about 0.3 to about 1.1 g/cm, a pore volume greater than about 0.2 cc/g, a pore distribution such that more than 40% of the pore volume is present in pores greater than 1500 Angstroms, a piece density in the range of from about 0.3 to about 2.0 g/cc, and a particle size which possesses a diameter of at least 2 mm.

Dehydrogenation of dehydrogenatable hydrocarbons

Dehydrogenatable hydrocarbons may be subjected to a dehydrogenation reaction in which the hydrocarbons are treated with a dehydrogenation catalyst comprising a modified iron compound in the presence of steam in a multicatalyst bed system. The reaction mixture containing unconverted hydrocarbons, dehydrogenated hydrocarbons, hydrogen and steam is then contacted with an oxidation catalyst whereby hydrogen is selectively oxidized in preference to carbon dioxide and carbon monoxide or hydrocarbons. The selective oxidation of hydrogen will improve the combustion thereof and supply the necessary heat which is required for a subsequent dehydrogenation treatment. The selective oxidation catalyst which is used will comprise a noble metal of Group VIII of the Periodic Table and, if so desired, a metal of Group IA or IIA of the Periodic Table composited on a porous inorganic support. The inorganic support will have been calcined prior to impregnation thereof at a temperature in the range of from about 900.degree. to about 1500.degree. C. in the absense or presence of steam to provide a catalyst which possesses increased stability and activity when compared to prior catalysts.

Alcohols may be synthesized by treating an olefinic hydrocarbon with carbon monoxide and hydrogen in a hydroformylation zone using a rhodium complex catalyst and an amine modifier to effect the reaction. Following the formation of the alcohol, a catalyst may be extracted from said alcohol by treatment with an aqueous ammonium hydroxide solution. Following this, the aqueous ammonium solution containing the rhodium catalyst is subjected to an extraction process utilizing the amine modifier as the extractant and thereafter recycling the rhodium complex catalyst and amine modifier to the hydroformylation zone.

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Mount Prospect, IL, United States of America

David E Mackowiak