Described is a process for producing 1-(4-isobutylphenyl)ethanol by reacting 1-(4-isobutyl-phenyl)ethanone with hydrogen in the presence of a catalyst composition comprising cop-per and one or more metals other than copper, and a use of a respective composition and/or of a pre-composition, the pre-composition comprising a mixture of oxides of copper and oxides of one or more metals other than copper, in a catalytic hydrogenation process for producing 1-(4-isobutylphenyl)ethanol from 1-(4-isobutylphenyl)ethanone.

A mixing device mounted between two catalyst beds in a multi-bed catalytic reactor with a cylindrical shape. The mixing device has a circular outer rim which corresponds to the inner wall of the reactor, and includes a collecting section for collecting fluid from an up-stream catalytic bed, a mixing section for mixing the collected fluid, and a discharging section for discharging the mixed fluid to a down-stream catalytic bed. The collecting section, the mixing section and the discharging section are disposed outside the center of the circular cross-section of the reactor.

The selective dimerization of isoolefins, such as isobutene or isopentane, or mixtures thereof, may be conducted in a system including a series of fixed bed reactors and a catalytic distillation reactor. The system may provide for conveyance of the fixed bed reactor effluents, without componential separation, to a downstream reactor. It has been found that a high selectivity to the dimer may be achieved even though intermediate separation of the desired product from unreacted components between reactors is not performed. Further, embodiments provide for use of a divided wall column for recovery of a high purity dimer product, reducing unit piece count and plot size.

Methods, reactor tubes, reactors, and systems for catalysis are disclosed. A reactor tube includes an outer shell defining a catalyst bed, a catalyst within the catalyst bed, and an inner tube extending through the catalyst bed. An interior of the inner tube is isolated from the catalyst within the catalyst bed. Methods of activating a catalyst are also disclosed herein.

The hydroprocessing reactor quench zone internals comprise a collection tray, a mixing chamber, a ring quench distributer, a rough liquid distribution tray, and a vapor-liquid distribution tray. The rough liquid distribution tray has a central pan for receiving vapor and liquid out of the mixing chamber and multiple fluid distribution troughs attached to the central pan that extended radially outwards with the outer end close to the reactor shell. The fluid distribution troughs can include at least one longitudinal baffle, or at least one cross baffle, or both, and optionally an end baffle. The baffles improve the liquid and/or vapor flow in the rough liquid distribution tray.

A process for the selective dimerization and etherification of isoolefins, including feeding a mixed C4 stream and an oxygenate stream to a first fixed bed reactor containing a first catalyst, producing a first reactor effluent comprising dimers of the isoolefin, unreacted C4s, and unreacted oxygenates. Feeding the first reactor effluent directly to a second fixed bed reactor containing a second catalyst, producing a second reactor effluent containing dimers of the isoolefin, unreacted C4s, and unreacted oxygenates. Feeding the second reactor effluent to a catalytic distillation reactor system containing a third catalyst. Concurrently in the catalyst distillation reactor system reacting unreacted C4s in the presence of the third catalyst to form additional dimers of the isoolefin and/or ethers, and separating the dimers of the isoolefins from unreacted oxygenates and unreacted C4s.

A process for the selective dimerization and etherification of isoolefins, including feeding a mixed C4 stream and an oxygenate stream to a first fixed bed reactor containing a first catalyst, producing a first reactor effluent comprising dimers of the isoolefin, unreacted C4s, and unreacted oxygenates. Feeding the first reactor effluent directly to a second fixed bed reactor containing a second catalyst, producing a second reactor effluent containing dimers of the isoolefin, unreacted C4s, and unreacted oxygenates. Feeding the second reactor effluent to a catalytic distillation reactor system containing a third catalyst. Concurrently in the catalyst distillation reactor system reacting unreacted C4s in the presence of the third catalyst to form additional dimers of the isoolefin and/or ethers, and separating the dimers of the isoolefins from unreacted oxygenates and unreacted C4s.

A multi-stage process for reducing the environmental contaminants in an ISO8217 compliant Feedstock Heavy Marine Fuel Oil involving a core desulfurizing process and a ultrasound treatment process as either a pre-treating step or post-treating step to the core process. The Product Heavy Marine Fuel Oil complies with ISO 8217 for residual marine fuel oils and has a sulfur level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05 mass % to 1.0 mass. A process plant for conducting the process is also disclosed.

Producing C5 olefins from steam cracker C5 feeds may include reacting a mixed hydrocarbon stream comprising cyclopentadiene, C5 olefins, and C6+ hydrocarbons in a dimerization reactor where cyclopentadiene is dimerized to dicyclopentadiene. The dimerization reactor effluent may be separated into a fraction comprising the C6+ hydrocarbons and dicyclopentadiene and a second fraction comprising C5 olefins and C5 dienes. The second fraction, a saturated hydrocarbon diluent stream, and hydrogen may be fed to a catalytic distillation reactor system for concurrently separating linear C5 olefins from saturated hydrocarbon diluent, cyclic C5 olefins, and C5 dienes contained in the second fraction and selectively hydrogenating C5 dienes. An overhead distillate including the linear C5 olefins and a bottoms product including cyclic C5 olefins are recovered from the catalytic distillation reactor system. Other aspects of the C5 olefin systems and processes, including catalyst configurations and control schemes, are also described.

A plant for the co-production of methanol and ammonia from a hydrocarbon feed without venting to the atmosphere carbon dioxide captured from the methanol or ammonia synthesis gas and without using expensive air separation units and water gas shift.