Abstract: The invention relates to a process of the oxidative dehydrogenation of an alkane containing 2 to 6 carbon atoms and/or the oxidation of an alkene containing 2 to 6 carbon atoms, comprising contacting a first gas stream comprising oxygen and the alkane containing 2 to 6 carbon atoms and/or the alkene containing 2 to 6 carbon atoms with a mixed metal oxide catalyst containing molybdenum, vanadium, niobium and optionally tellurium; followed by contacting a second gas stream comprising methane, an inert gas or oxygen or any combination of two or more of these with the catalyst, wherein the second gas stream comprises 0 to 25 vol. % of the alkane containing 2 to 6 carbon atoms and/or alkene containing 2 to 6 carbon atoms.

Abstract: The invention relates to a process of the oxidative dehydrogenation of an alkane containing 2 to 6 carbon atoms and/or the oxidation of an alkene containing 2 to 6 carbon atoms, wherein a gas stream comprising oxygen and the alkane and/or alkene is contacted with a mixed metal oxide catalyst containing molybdenum, vanadium, niobium and optionally tellurium, and wherein the linear velocity of said gas stream is at least 10 cm/sec.

Abstract: The invention relates to a process of the oxidative dehydrogenation of an alkane containing 2 to 6 carbon atoms and/or the oxidation of an alkene containing 2 to 6 carbon atoms, wherein a gas stream comprising oxygen and the alkane and/or alkene is contacted with a mixed metal oxide catalyst containing molybdenum, vanadium, niobium and optionally tellurium, and wherein the weight hourly space velocity is of from 2.1 to 25.0 hr?1 and the temperature is of from 300 to 500° C.

Abstract: The present disclosure is directed to a process for hydroprocessing a hydrocarbon feedstock. The process utilizes a horizontal bubble reactor for slurry hydroprocessing of a heavy hydrocarbon feedstock having an API Gravity of less than 20, where the reactor is fitted with one or more vapor-only outlets to provide intrinsic separation of catalyst from product.

Abstract: Maintaining long residence times during hydrothermal digestion of cellulosic biomass solids may be complicated by a number of factors, including biomass compaction. Advantages in this regard may be realized by digesting cellulosic biomass solids in an inclined digestion unit. Such methods can comprise: introducing cellulosic biomass solids to a hydrothermal digestion unit comprising one or more inclined surfaces therein; introducing a fluid phase digestion medium containing a slurry catalyst to the hydrothermal digestion unit, the slurry catalyst being capable of activating molecular hydrogen; supplying an upwardly directed flow of molecular hydrogen from a source disposed along each inclined surface as the cellulosic biomass solids descend along each inclined surface; and heating the cellulosic biomass solids as they descend along each inclined surface in the presence of the slurry catalyst and the molecular hydrogen, thereby forming an alcoholic component derived from the cellulosic biomass solids.

Abstract: Biomass compaction during hydrothermal digestion of cellulosic biomass solids may become problematic, particularly as the vertical height of a cellulosic biomass charge increases. Compaction may be decreased in a horizontally configured hydrothermal digestion unit.

Abstract: The present invention pertains to a reactor tube comprising a fixed bed of Fischer-Tropsch catalyst particles, wherein the catalyst particles in 5% to 40% of the fixed bed volume at the upstream end have an average outer surface to volume ratio (S/V) in the range of between 3.0 to 4.5 mm?1, and the catalyst particles in the remaining fixed bed volume have an average outer surface to volume ratio (S/V) in the range of between 4.5 to 8.0 mm?1, and wherein the difference between the average S/V of the particles at the upstream end and the average S/V of the particles in the remaining fixed bed volume is at least 0.5 mm?1.

Abstract: Biomass compaction during hydrothermal digestion of cellulosic biomass solids may become problematic, particularly as the vertical height of a cellulosic biomass charge increases. Compaction may be decreased in a horizontally configured hydrothermal digestion unit.

Abstract: Maintaining long residence times during hydrothermal digestion of cellulosic biomass solids may be complicated by a number of factors, including biomass compaction. Advantages in this regard may be realized by digesting cellulosic biomass solids in an inclined digestion unit. Such methods can comprise: introducing cellulosic biomass solids to a hydrothermal digestion unit comprising one or more inclined surfaces therein; introducing a fluid phase digestion medium containing a slurry catalyst to the hydrothermal digestion unit, the slurry catalyst being capable of activating molecular hydrogen; supplying an upwardly directed flow of molecular hydrogen from a source disposed along each inclined surface as the cellulosic biomass solids descend along each inclined surface; and heating the cellulosic biomass solids as they descend along each inclined surface in the presence of the slurry catalyst and the molecular hydrogen, thereby forming an alcoholic component derived from the cellulosic biomass solids.

Abstract: A reactor system for the oxidation of ethylene to ethylene oxide. The reactor system includes a reactor tube that contains a packed bed of shaped support material that can include a catalytic component. The shaped support material has a hollow cylinder geometric configuration. The reactor system has specific combinations of reactor tube and catalyst system geometries.

Abstract: The present invention pertains to a reactor tube comprising a fixed bed of Fischer-Tropsch catalyst particles, wherein the catalyst particles in 5% to 40% of the fixed bed volume at the upstream end have an average outer surface to volume ratio (S/V) in the range of between 3.0 to 4.5 mm?1, and the catalyst particles in the remaining fixed bed volume have an average outer surface to volume ratio (S/V) in the range of between 4.5 to 8.0 mm?1, and wherein the difference between the average S/V of the particles at the upstream end and the average S/V of the particles in the remaining fixed bed volume is at least 0.5 mm?1.

Abstract: A process for selecting shaped particles for use in a tube which is capable of being packed with shaped particles to form a packed bed in the tube. A desired value of one or more properties of the packed bed is defined. The dimensions of the shaped particles are calculated such that a packed bed in the tube of the shaped particles having the calculated dimensions meets or substantially meets the desired value(s), and shaped particles are selected in accordance with the calculated dimensions. The properties of the packed bed may be the volume fraction which is occupied by shaped particles, the packing density, and the resistivity for a gas flowing through the packed bed.

Abstract: The present invention pertains to a reverse-flow reactor comprising at least one catalyst bed which is preceded and followed by at least one bed containing selectively adsorbing material, and its application for in a process for the removal of contaminants from a process stream.

Abstract: The invention provides a process for the mixing of an oxidant having explosive potential with a hydrocarbon material, which comprises conveying a first stream comprising the hydrocarbon material and a second stream comprising the oxidant into a microchannel apparatus, allowing mixing to occur, and withdrawing the mixture. The process is useful for the preparation of ethylene oxide.

Abstract: A reactor system for the epoxidation of ethylene, which reactor system comprises an elongated tube having an internal tube diameter of more than 40 mm, wherein contained is a catalyst bed of catalyst particles comprising silver and a promoter component deposited on a carrier, which promoter component comprises an element selected from rhenium, tungsten, molybdenum and chromium; a process for the epoxidation of ethylene comprising reacting ethylene with oxygen in the presence of the catalyst bed contained in the reactor system; and a method of preparing ethylene glycol, an ethylene glycol ether or an ethanol amine comprising obtaining ethylene oxide by the process for the epoxidation of ethylene, and converting the ethylene oxide into ethylene glycol, the ethylene glycol ether, or the ethanol amine. Preferably, the internal tube diameter is at least 45 mm.

Abstract: The invention relates to a process for the preparation of styrene and/or a substituted styrene from a feed containing 1-phenylethanol and 2-phenylethanol and/or a substituted 1-phenylethanol and a substituted 2-phenylethanol, comprising a gas phase dehydration of the feed at elevated temperature in the presence of a catalyst comprising particles of alumina having a multimodal pore size distribution.

Abstract: A high activity and high selectivity silver catalyst comprising silver and, optionally, one or more promoters supported on a suitable support material having the form of a shaped agglomerate. The structure of the shaped agglomerate is that of a hollow cylinder having a relatively small inside (bore) diameter. The catalyst is made by providing the shaped material of a particular geometry and incorporating the catalytic components therein. The catalyst is useful in the epoxidation of ethylene.

Abstract: The present invention pertains to a reverse-flow reactor comprising at least one catalyst bed which is preceded and followed by at least one bed containing selectively adsorbing material, and its application for in a process for the removal of contaminants from a process stream.

Abstract: The present invention relates to an improved epoxidation process and an improved epoxidation reactor. The present invention makes use of a reactor which comprises a plurality of microchannels. Such process microchannels may be adapted such that the epoxidation and optionally other processes can take place in the microchannels and that they are in a heat exchange relation with channels adapted to contain a heat exchange fluid. A reactor comprising such process microchannels is referred to as a “microchannel reactor”. The invention also provides a method of installing an epoxidation catalyst in a microchannel reactor. The invention also provides a method of preparing an epoxidation catalyst. The invention also provides an epoxidation catalyst. The invention also provides a certain process for the epoxidation of an olefin and a process for the preparation of a chemical derivable from an olefin oxide. The invention also provides a microchannel reactor.

Abstract: The present invention relates to an improved epoxidation process and an improved epoxidation reactor. The present invention makes use of a reactor which comprises a plurality of microchannels. Such process microchannels may be adapted such that the epoxidation and optionally other processes can take place in the microchannels and that they are in a heat exchange relation with channels adapted to contain a heat exchange fluid. A reactor comprising such process microchannels is referred to as a “microchannel reactor”. The invention also provides a method of installing an epoxidation catalyst in a microchannel reactor. The invention also provides a method of preparing an epoxidation catalyst. The invention also provides an epoxidation catalyst. The invention also provides a certain process for the epoxidation of an olefin and a process for the preparation of a chemical derivable from an olefin oxide. The invention also provides a microchannel reactor.