Saudi Basic Industries Corporation

Sd Lizenzverwertungsgesellschaft Mbh & Co Kg

Sabic Global Technolgoies B.v.

Shpp Global Technologies B.v.

Scientific Design Company, Inc.

Xiankuan Zhang

Jaap Willem Van Hal

Shahid N Shaikh

Clark David Rea

John S Ledford

James Kauffman

Aghaddin Mamedov

William Crudge

Ray Montez

Xin Li

Alla Konstantin Khanmamedova

Jorge Jimenez

Paulette N Hazin

Gary Mell Bates

Aghaddin Kh Mammadov

Patricia Ann Hooks

Douglas Henry Lenz

Christelle Verrier

Balamurali Krishna R Nair

Kenchaiah Lohith

Aghaddin Mammadov

Mike Huckman

Vivek Chandra Gyani

Omoyemen E Ofoegbu

Reggie Tennyson

Robin Woodbury

A conditioning process that is employed with a high selectivity catalyst (HSC) during an initial phase (i.e., start-up) of the epoxidation process is provided. The HSC conditioning process of the present disclosure ensures that the heat release from a catalyst bed containing an HSC during a start-up operation is less than 2000 kJ/Kgcat·hr. The HSC containing catalyst bed that has been conditioned by the process of the present disclosure exhibits improved performance (i.e., EO selectivity) and reduced hot spots.

Ethylene oxide high selectivity catalyst conditioning process

A phenol alkylation catalyst exhibiting a desirable combination of activity, selectivity, and regenerability is prepared from a catalyst precursor that includes specific amounts of magnesium oxide, copper oxide or a copper oxide precursor, a hydrous magnesium aluminosilicate-containing binder, a pore-former, a lubricant, and water. Methods of forming and regenerating the catalyst, as well as a phenol alkylation method, are described.

Phenol alkylation catalyst precursor and catalyst, method of forming catalyst, method of regenerating catalyst, and method of alkylating phenol

Methods for producing butadiene by the oxidative dehydrogenation of butene are provided. Methods for producing butadiene from a feed stream including oxygen and butene in a molar ratio of oxygen to butene (O/CH) from about 0.9 to about 1.5 can include introducing the feed stream to a catalyst in the presence of steam. The molar ratio of steam to butene (HO/CH) can be from about 10 to about 20. Methods can further include reacting the butene to generate a product stream therefrom comprising butadiene and water. Methods can further include separating water from the product stream to generate a butadiene stream including greater than about 85 wt-% butadiene.

Methods for the oxidative dehydrogenation of butene to produce butadiene

In one embodiment, a process for the purification of COfrom chlorinated and non-chlorinated hydrocarbons, comprising: contacting a COstream with a metal oxide catalyst, wherein the stream comprises the COand impurities comprising the non-chlorinated hydrocarbons and the chlorinated hydrocarbons; interacting the impurities with the catalyst to form additional COand metal chloride; and regenerating the catalyst by contacting the metal chloride with an oxygen containing gas stream. In another embodiment, a process for the purification of COfrom chlorinated hydrocarbons and non-chlorinated hydrocarbons, comprising: contacting a COstream with a metal oxide catalyst, wherein the COstream comprises the COand impurities comprising the non-chlorinated hydrocarbons and the chlorinated hydrocarbons; oxidizing the impurities with catalyst oxygen to form additional COand converting the chlorine to metal chloride; and regenerating the catalyst by contacting the metal chloride with an oxygen containing gas stream.

Purification of carbon dioxide streams

A dehydrogenation catalyst is formed by forming a mixture comprising a bayerite aluminum hydroxide (Al(OH)), a lanthanum (La) source, a cerium (Ce) source, a barium (Ba) source, a zirconium (Zr) source, and water into a shaped body. The shaped body is calcined at a temperature of at least 750&#xb0; C. to form a catalyst support. The catalyst support is treated with a dehydrogenation catalyst component to form a treated catalyst support containing the dehydrogenation catalyst component. The treated catalyst support is then calcined. The resulting catalyst composition may be used by contacting a paraffin hydrocarbon feed with a catalyst within a reactor in the presence of steam under dehydrogenation reaction conditions suitable to form dehydrogenated hydrocarbon products.

Dehydrogenation catalyst, its use and method of preparation

The invention relates to a catalyst and process for making syngas mixtures including hydrogen, carbon monoxide and carbon dioxide. The process comprises contacting a gaseous feed mixture containing carbon dioxide and hydrogen with the catalyst, where the catalyst comprises Mn oxide and an auxiliary metal oxide selected from the group consisting of La, Ca, K, W, Cu, Al and mixtures or combinations thereof. The process enables hydrogenation of carbon dioxide into carbon monoxide with high selectivity, and good catalyst stability over time and under variations in processing conditions. The process can be applied separately, but can also be integrated with other processes, both up-stream and/or down-stream including methane reforming or other synthesis processes for making products like alkanes, aldehydes, or alcohols.

Mixed oxide based catalyst for the conversion of carbon dioxide to syngas and method of preparation and use

Dialkyl carbonate and diol products are prepared in an integrated process performed by reacting an alkylene oxide with carbon dioxide in the presence of a non-halide-containing homogeneous carbonation catalyst in a first reaction zone to form a crude cyclic carbonate product. The crude cyclic carbonate product is introduced along with an aliphatic monohydric alcohol to a second reaction zone containing a transesterification catalyst. The transesterification catalyst is comprised of a strongly basic Type I ion exchange resin in gel having a particular form. The cyclic carbonate product and monohydric alcohol are reacted to form the dialkyl carbonate and diol products. In another aspect, dialkyl carbonate and diol products are prepared in an integrated process wherein a halide-containing homogeneous carbonation catalyst is used to form a crude cyclic carbonate product that is then used in a transesterification reaction. The transesterification catalyst is regenerated to accommodate the effects of the halide-containing catalyst.

Process for preparing dialkyl carbonate and diol products

A method of forming a cyclic carbonate product is carried out by reacting an alkylene oxide, such as ethylene oxide, with carbon dioxide in the presence of a metal organic framework (MOF) catalyst with less than 0.5 mol % of any potassium or quaternary ammonium salts present based on moles of alkylene oxide feed in a reaction zone under reaction conditions to form a cyclic carbonate product. The cyclic carbonate product may be optionally fed as a crude carbonate product that does not undergo any purification or separation, other than the optional removal of any portion of unreacted alkylene oxide, carbon dioxide, and light hydrocarbon gases, to a second reaction zone containing a transesterification catalyst along with an aliphatic monohydric alcohol. The cyclic carbonate product and monohydric alcohol are allowed to react under reaction conditions to form the dialkyl carbonate and diol products.

Process for preparing carbonate and diol products

A method for making a syngas mixture is accomplished by introducing a gaseous feed mixture containing carbon dioxide and hydrogen into a reactor containing a non-zinc catalyst. The catalyst contacts the gaseous feed mixture to form syngas mixture reaction products. The reaction takes place in the presence of nickel-containing and/or iron-containing materials. The gaseous feed mixture is introduced into the reactor at a reactor inlet temperature of from 700&#xb0; C. to 800&#xb0; C., with the reaction being carried out at substantially adiabatic conditions or wherein the syngas mixture reaction products are removed from the reactor at a reactor outlet temperature of from 500&#xb0; C. to 600&#xb0; C.

Method of forming a syngas mixture

A catalyst for oxidative dehydrogenation of organic compounds is provided by forming a solution of catalyst precursor components comprised of Feand Zncations and at least one other modifier element cation in water to form an aqueous solution of the catalyst precursor components. The modifier element cation has a standard reduction potential of from greater than about &#x2212;2.87 E&#xb0; (V) to less than about &#x2212;0.036 E&#xb0; (V) with a valence of +2. A base is separately and simultaneously added to the aqueous solution in amounts to maintain the pH of the aqueous solution at a pH of from about 8.5 to about 9.5 as the catalyst precursor components. The catalyst precursor components are allowed to react and precipitate out of solution as a precipitate. The resulting precipitate is calcined to form a modified zinc ferrite catalyst compound.

Modified zinc ferrite catalyst and method of preparation and use

A solid (i.e., heterogeneous) catalyst useful for preparing an alkylene glycol from the corresponding alkylene oxide as well as a process for the catalytic hydration of an alkylene oxide to an alkylene glycol utilizing such a catalyst are provided. The catalyst of the present invention is based on an ion exchange resin including polystyrene crosslinked with from about 2 to about 10 weight (wt.) % divinyl benzene. The ion exchange resin further includes quaternary ammonium groups or quaternary phosphonium groups. The process includes reacting water and an alkylene oxide in at least one reactor under conditions to form an alkylene glycol, wherein the at least one reactor includes a catalyst based on an ion exchange resin that includes polystyrene crosslinked with from about 2 to about 10 weight (wt.) % divinyl benzene.

Solid catalyst useful for converting an alkylene oxide to an alkylene glycol

A catalytic process for preparing a monoalkylene glycol from a corresponding alkylene oxide utilizing an ion exchange resin and a reactor in which an upflow process is used is provided. In particular, the process includes reacting water and an alkylene oxide in at least one reactor under conditions to form an alkylene glycol, wherein the at least one reactor includes an ion exchange resin and the reactor is operating in an upflow direction.

Process for preparing an alkylene glycol

The present invention if for a catalyst for epoxidation of an alkene, such as ethylene, to an alkene oxide, such as ethylene oxide, on which silver has been deposited on alumina as a support which has been modified with certain weak base compounds, such as oxides of a Group 1A, Group 2A, Group 3A or the first transition series of the Periodic Table of Elements, and with a high temperature heat treatment. Optional promoters selected from the group consisting of compounds of Group 1A, Group 2A, Group 7A and Group 8 may be contacted with the alpha-alumina support in solution with a silver compound, with the catalyst precursor before calcination or with the catalyst after calcination. The catalyst is brought into contact with alkene and oxygen under reaction conditions to selectively convert the alkene to an alkene oxide.

Catalyst for epoxidation of an alkene to an alkene oxide, method of making and method of using thereof

Disclosed is a process for the preparation of alkylene glycols from the corresponding alkylene oxide, such as ethylene glycol from ethylene oxide, in the presence of water, a catalyst and, optionally, carbon dioxide. The catalyst is a SALEN-type compound which contains an amino group and an oxy or hydroxy group connected by a hydrocarbon, such as an alkyl or an alkylaryl. The SALEN-type compounds may be Schiff bases, i.e., a condensate product of a primary amine with an aldehyde, ketone or an alcohol. The SALEN-type compound may be a mono or bis compound and may be complexed with a Group 4-14 metal, such as aluminum, tin, vanadium, chromium, manganese, iron, cobalt or platinum.

Process for the preparation of alkylene glycols

Disclosed is a process for the preparation of alkylene glycols from the corresponding alkylene oxide, such as ethylene glycol from ethylene oxide, in the presence of water, a catalyst and, optionally, carbon dioxide. The catalyst contains an amphoteric compound, such as such as (ethylenedinitrilo) tetraacetic acid (EDTA). These befunctional compounds have both acid and base moieties. Preferably, a compound useful in the present invention forms a buffered solution in water, i.e., the acid and base moieties do not completely disassociate. The pH of the buffered solution should be 2-10, preferably 5-10, more preferably 4-9. A compound useful in the present invention is preferably organic with the base moiety and the acid moiety being separated by one to four carbon atoms.

Growing community of inventors

Houston, TX, United States of America

Xiankuan Zhang