A powdered catalyst material on a titanium oxide basis. The powdered catalyst material includes a combined content of at least 90 wt.-% of a hydrated titanium oxide having the general formula TiO.sub.(2-x)(OH).sub.2x, with 0<x?1, (calculated as TiO.sub.2), and a silicon dioxide and hydrated precursors of the silicon dioxide (calculated as SiO.sub.2). A weight ratio of TiO.sub.2/SiO.sub.2, determined for TiO.sub.2 and SiO.sub.2 respectively, is at least 3 and less than 30. The wt.-% is based on a total weight of the catalyst material after the catalyst material has been dried at 105? C. for at least 2 hours. The powdered catalyst material has a specific surface area of >300 m.sup.2/g and an isoelectric point of from 4.0 to 7.0.

A catalyst containing molybdenum, bismuth, and iron, in which R1 represented by the following equation (1) is 0.45 or more and 5.00 or less is provided, and use of the catalyst achieves a high yield, in the case of the use in a gas phase oxidation reaction, particularly in the case of the use in producing an unsaturated aldehyde compound or an unsaturated carboxylic acid compound by a partial oxidation reaction,

[00001]$\begin{array}{cc}R1=\left(\mathrm{maximum}\mathrm{value}\mathrm{of}\mathrm{peak}\mathrm{at}886{\mathrm{cm}}^{-1}?5{\mathrm{cm}}^{-1}\right)?\left(\mathrm{maximum}\mathrm{value}\mathrm{of}\mathrm{peak}\mathrm{at}354{\mathrm{cm}}^{-1}?5{\mathrm{cm}}^{-1}\right)\mathrm{as}\mathrm{measured}\mathrm{by}\mathrm{Raman}\mathrm{spectroscopy}.& \left(1\right)\end{array}$

A catalyst containing molybdenum, bismuth, and iron, in which R1 represented by the following equation (1) is 0.45 or more and 5.00 or less is provided, and use of the catalyst achieves a high yield, in the case of the use in a gas phase oxidation reaction, particularly in the case of the use in producing an unsaturated aldehyde compound or an unsaturated carboxylic acid compound by a partial oxidation reaction,

[00001]$\begin{array}{cc}R1=\left(\mathrm{maximum}\mathrm{value}\mathrm{of}\mathrm{peak}\mathrm{at}886{\mathrm{cm}}^{-1}?5{\mathrm{cm}}^{-1}\right)?\left(\mathrm{maximum}\mathrm{value}\mathrm{of}\mathrm{peak}\mathrm{at}354{\mathrm{cm}}^{-1}?5{\mathrm{cm}}^{-1}\right)\mathrm{as}\mathrm{measured}\mathrm{by}\mathrm{Raman}\mathrm{spectroscopy}.& \left(1\right)\end{array}$

A feed stream including ethane is flowed to a purification unit that includes a first oxidative dehydrogenation catalyst. The feed stream is contacted with the first oxidative dehydrogenation catalyst at a first temperature to reduce a concentration of impurities in the feed stream to produce a purified feed stream. The purified feed stream is flowed to an oxidative dehydrogenation unit that includes a second oxidative dehydrogenation catalyst. The purified feed stream is contacted with the second oxidative dehydrogenation catalyst in the presence of oxygen at a second temperature greater than the first temperature to dehydrogenate ethane to produce a product stream that includes ethylene.

A method provides for valorization of naturally abundant organic solid biomass under a specified gas atmosphere with the existence of a catalyst structure. The method effectively converts the organic solid feedstock while producing valuable liquid hydrocarbon products, as well as utilizing methane rich resources, providing an economical and environmental benefit in the oil and gas industry.

A method provides for valorization of naturally abundant organic solid biomass under a specified gas atmosphere with the existence of a catalyst structure. The method effectively converts the organic solid feedstock while producing valuable liquid hydrocarbon products, as well as utilizing methane rich resources, providing an economical and environmental benefit in the oil and gas industry.

A method for producing a target compound includes distributing a feed mixture containing ethane to multiple reaction tubes of a shell-and-tube reactor arranged in parallel, and subjecting to an oxidative catalytic conversion of the ethane in the reaction tubes. The catalytic reaction is carried out by means of catalysis zones with different activity arranged in series in the reaction tubes. One or more catalytically active materials and one or more catalytically inactive materials are provided in each of the catalysis zones. The different activity of the catalysis zones is effected by providing the one or more catalytically active materials having identical or essentially identical basic formulation, wherein the one or more catalytically active materials is or are prepared using different calcination intensities.

A method for producing a target compound includes distributing a feed mixture containing ethane to multiple reaction tubes of a shell-and-tube reactor arranged in parallel, and subjecting to an oxidative catalytic conversion of the ethane in the reaction tubes. The catalytic reaction is carried out by means of catalysis zones with different activity arranged in series in the reaction tubes. One or more catalytically active materials and one or more catalytically inactive materials are provided in each of the catalysis zones. The different activity of the catalysis zones is effected by providing the one or more catalytically active materials having identical or essentially identical basic formulation, wherein the one or more catalytically active materials is or are prepared using different calcination intensities.

The present disclosure relates to an additive and a catalyst composition for a catalytic cracking process of vacuum gas oil for preparing cracked run naphtha having reduced liquid olefin content, and increased propylene and butylene yields in the LPG fraction. The process makes use of a catalyst composition which is a mixture of an FCC equilibrated catalyst and an additive comprising a zeolite, phosphorus and a combination of metal promoters. The process is successful in achieving high propylene and butylene yields in the LPG fraction along with a lower liquid olefin content and increased aromatic content with increase in RON unit in the resultant cracked run naphtha, as compared to that achieved using an FCC equilibrated catalyst alone.

The present disclosure relates to an additive and a catalyst composition for a catalytic cracking process of vacuum gas oil for preparing cracked run naphtha having reduced liquid olefin content, and increased propylene and butylene yields in the LPG fraction. The process makes use of a catalyst composition which is a mixture of an FCC equilibrated catalyst and an additive comprising a zeolite, phosphorus and a combination of metal promoters. The process is successful in achieving high propylene and butylene yields in the LPG fraction along with a lower liquid olefin content and increased aromatic content with increase in RON unit in the resultant cracked run naphtha, as compared to that achieved using an FCC equilibrated catalyst alone.