Mobil Oil Corporation

Mobile Oil Corporation

James H Beech, Jr

James A Stoos

Samuel A Tabak

Robert A Ware

Francis P Ragonese

Hartley Owen

Sergei Yurchak

Michael P Ramage

Albert H Wu

Douglas Miller

Jorge Luis Soto

Mohsen N Harandi

Stuart Damon Hellring

Terry Eugene Helton

Albin Huss, Jr

Stephen S Wong

Hye Kyung Timken

Weldon K Bell

Sadi Mizrahi

Roland Bernard Saeger

Charles M Sorensen

Altaf Husain

Norman J Rouleau

W Thomas Mo

Timothy Frederick Kinn

An improved process for production of diisopropyl ether by conversion of hydrocarbon feedstock containing propene, propane and C.sub.2 -- light gas components. The overall process steps include, (optionally) prefractionating fresh feedstock containing propene, propane and C.sub.2 -- light gas components to provide a reactor feedstream rich in propene; contacting the feedstock and water in a catalytic reactor with acidic catalyst under olefin hydration and etherification conditions; and recovering from the catalytic reactor a liquid reactor effluent stream containing diisopropyl ether, isopropanol, water, unreacted propene, propane, oligomer and C.sub.2 -- light gas components. DIPE product containing C.sub.6 + oligomer is recovered by separating the liquid effluent stream in a stripper column, and extracting the DIPE-rich liquid with water. An improved separation process is employed for removing water to provide DIPE liquid product substantially free of water.

Di-isopropyl ether synthesis and dry product recovery

A process for converting a heavy aromatics feed to lighter aromatic products, such as benzene and xylene, by reacting C.sub.9+ aromatic hydrocarbons and toluene or benzene under transalkylation reaction conditions, over a first catalyst composition including a zeolite having a constraint index ranging from 0.5 to 3 and a hydrogenation component and a second catalyst composition including an intermediate pore size zeolite having a constraint index ranging from 3 to 12 and a silica to alumina ratio of at least about 5, to produce a transalkylation reaction product containing benzene or toluene and xylene. The benzene or toluene from the reaction product can then be distilled to obtain a benzene or toluene product.

Process for converting C.sub.9 + aromatic hydrocarbons to lighter

A process is disclosed for alkylating an isoparaffin with an olefin comprising the steps of: (a) reacting an isoparaffin having from 4 to 8 carbon atoms with an olefin having from 2 to 12 carbon atoms in a first alkylation reaction stage at temperature from about -40.degree. C. to about 500.degree. C. and overall isoparaffin:olefin feed weight ratio of from about 1:1 to about 250:1 with a solid alkylation catalyst comprising a synthetic porous crystalline material characterized by an X-ray diffraction pattern including values substantially as set forth in Table I of the specification and having a composition comprising the molar relationship

Isoparaffin/olefin alkylation

An olefin hydration catalyst is regenerated with a non-oxidizing light gas, such as hydrogen. Light olefins, especially propylene, are converted to a mixture of alcohol(s), such as isopropanol (IPA) and ether(s), such as diisopropylether (DIPE) by contacting a feed containing the olefin with water and/or alcohol with the olefin hydration catalyst. Regeneration conditions include temperatures of from about 150.degree. C. to about 550.degree. C., pressures below about 1000 psig (6900 kPa). Lower pressures of regeneration unexpectedly demonstrated more effective catalyst regeneration through greater coke removal.

Olefin conversion catalyst regeneration

A method for conversion of linear C5 olefins in the presence of contaminant diolefins to corresponding iso-olefins of the same carbon number which comprises contacting a linear C5 olefin-containing organic feedstock with a catalyst comprising material having the structure of ZSM-35 under skeletal isomerization conditions, wherein said conversion is carried out at temperatures between about 100.degree. and 750.degree. C., weight hourly space velocities (WHSV) based on linear C5 olefins in said feedstock between 0.1 and 500 WHSV, C5 linear olefin partial pressures between 2 and 2000 kPa, and in the presence of hydrogen added in an amount sufficient to enhance linear C5 olefin conversion activity and extend the catalyst life of the catalyst relative to operation without any hydrogen added.

Skeletal isomerization of n-pentenes using ZSM-35 in the presence of

A process for production of diisopropyl ether by conversion of hydrocarbon feedstock containing propene, propane and C.sub.2 - light gas components, including the steps of: optionally, prefractionating fresh feedstock containing propene, propane and C.sub.2 - light gas components to provide a reactor feedstream rich in propene; contacting the feedstock and water in a catalytic reactor with acidic catalyst under olefin hydration and etherification conditions; and recovering from the catalytic reactor a liquid reactor effluent stream containing diisopropyl ether, isopropanol, water, unreacted propene, propane and C.sub.2 - light gas components. Improved operation is achieved by separating the liquid effluent stream in a vertical stripper column; recovering an overhead vapor stream containing propene, propane and C.sub.2 - light gas components from the stripper column; cooling the overhead vapor stream to provide a reflux stream rich in condensed propene and propane; removing the C.sub.2 - light gas components from condensed; recycling the reflux stream to an upper contact portion of the stripper column; and recovering a predominantly C3 recycle stream from the upper contact portion of the stripper column. Optionally, the C3 recycle stream may be passed to the to the prefractioning step for propene enrichment with fresh feedstock.

Di-isopropyl ether production

A method for starting up a fixed bed propylene hydration reactor containing shape selective metallosilicate catalyst particles for the production of isopropanol and/or diisopropyl ether is disclosed comprising the following sequential steps: contacting a feedstream comprising propane with catalyst particles in a hydration reactor; then introducing a feedstream comprising isopropanol into the reactor to displace propane. Next, a feedstream comprising propylene is introduced into the reactor under etherification conditions. Finally, a feedstream is introduced in the reactor comprising water under etherification and hydration reaction conditions whereby diisopropyl ether and isopropanol are produced.

Process for starting up an olefin hydration reactor

A process for production of dialkyl ether by hydration and etherification of olefinic feedstock containing at least one lower alkene by contacting the olefinic feedstock and water in a catalytic reaction zone with porous solid metallosilicate acidic catalyst under olefin hydration and etherification conditions. Improvement is achieved by recovering a first fluid effluent stream from the reaction zone; splitting the first fluid effluent stream into a liquid product recovery stream and a fluid recycle stream; and passing the fluid recycle stream consisting essentially of olefin, alcohol and ether in effluent stream proportions for feeding to the reaction zone along with fresh olefinic feedstock and fresh water, wherein the amount of fluid recycle stream is sufficient to maintain a homogeneous single fluid reaction phase in the reaction zone.

Catalytic olefin hydration for ether production

A process for production of ether by hydration and etherification of olefinic feedstock containing at least one lower alkene by contacting the olefinic feedstock and water in a plurality of catalytic reaction zones containing porous solid metal oxide acidic olefin hydration and etherification catalyst under olefin hydration and etherification conditions. Improved operation is achieved by recovering a first effluent stream from at least one fixed bed hydration zone, splitting the first effluent stream into a product recovery stream and a plurality of recycle streams, and passing at least a portion of cooled recycle streams comprising olefin, alcohol and ether in effluent stream component proportions for quenching at least one fixed bed reaction zone to control temperature of hot effluent from a preceding reaction zone.

Reactor quenching for catalytic olefin hydration in ether production

An oligomerization system is provided for upgrading lower olefins to distillate hydrocarbons, especially useful as high quality jet or diesel fuels. The olefinic feedstock is reacted over a shape selective acid zeolite, such as ZSM-5, to oligomerize feedstock olefins and further convert recycled hydrocarbons. Reactor effluent is fractionated to recover a light-middle distillate range product stream and to obtain gasoline and heavy hydrocarbon streams for recycle.

Production of middle distillate range hydrocarbons by light olefin

It is disclosed that in a fixed bed process for the conversion of C.sub.1 -C.sub.4 oxygenates in contact with acidic, medium pore, shape selective metallosilicate catalyst particles to produce gasoline boiling range hydrocarbons, including the step of reactivating spent catalyst at elevated temperature, the cycle time between regenerations can be substantially improved by reactivating the spent catalyst at reduced pressure and elevated temperature in contact with a stream of inert purge gas. Preferably, the reactivation is carried out at a reduced pressure from sub-atmospheric to 1400 kPa using nitrogen as a purge gas. Other purge gases include light paraffinic hydrocarbons, refinery fuel gas and Group VIII gases of the Periodic Table of the Elements.

Method for reactivating MTG process catalyst

A process for upgrading of unstable olefins, naphthas, and dienes, such as coker naphthas, is disclosed. The olefins in the unstable naphthas are oligomerized over a shape selective zeolite to gasoline and distillate products. The dienes are catalytically converted by the same zeolite. Preferably, hydrogen is added to increase catalyst life. Feed pretreatment, to remove basic nitrogen compounds also improves catalyst life. Water washing of coker naphtha is the preferred method of removing basic nitrogen compounds.

Process for upgrading unstable naphthas

A process for oligomerizing C2 to C10 olefins obtained by catalytic cracking of heavy crude oil is disclosed. The olefins are oligomerized in the presence of added hydrogen over a shape selective zeolite to gasoline and distillate products. Feed pretreatment, to remove basic nitrogen compounds present in light olefin stream in refinery, with water wash or a guard bed is practiced improves catalyst life.

Process for upgrading light olefinic streams

An oligomerization system is provided for upgrading lower olefins to distillate hydrocarbons, especially useful as high quality jet or diesel fuels. Thye olefinic feedstock is reacted over a shape selective acid zeolite, such as ZSM-5, to oligomerize feedstock olefins and further convert recycled hydrocarbons. Reactor effluent is fractionated to recover a light-middle distillate range product stream and to obtain gasoline and heavy hydrocarbon streams for recycle.

A technique for continuous conversion of diene-containing aliphatic hydrocarbon feedstock to heavier hydrocarbon products wherein the feedstock is contacted at elevated temperature under endothermic high severity reaction conditions with a fluidized bed of acidic zeolite fine catalyst particles, comprising methods and means for:

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Wilmington, DE, United States of America

James H Beech, Jr