A process for reducing the environmental contaminants in a ISO 8217 compliant Feedstock Heavy Marine Fuel Oil, the process involving: mixing a quantity of the Feedstock Heavy Marine Fuel Oil with a quantity of Activating Gas mixture to give a feedstock mixture; contacting the feedstock mixture with one or more catalysts to form a Process Mixture from the feedstock mixture; separating the Product Heavy Marine Fuel Oil liquid components of the Process Mixture from the gaseous components and by-product hydrocarbon components of the Process Mixture and, discharging the Product Heavy Marine Fuel Oil. The Product Heavy Marine Fuel Oil is compliant 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% wt. to 0.5% wt. The Product Heavy Marine Fuel Oil can be used as or as a blending stock for an ISO 8217 compliant, IMO MARPOL Annex VI (revised) compliant low sulfur or ultralow sulfur heavy marine fuel oil. A device for conducting the process is also disclosed.

A process for the selective dimerization and etherification of isoolefins. The process including feeding a mixed C5 stream to a selective hydrogenation unit to convert dienes to olefins and isoolefins, producing a hydrogenated effluent stream. The hydrogenated effluent stream is fed to a first fixed bed reactor, producing a first reactor effluent. The first reactor effluent is fed to a catalytic distillation reactor system, producing a first overheads including unreacted olefins, isoolefins, oxygenate, and one or more C5 ethers and a first bottoms including dimers of the isoolefins, any produced trimers of the isoolefins, and heavy oxygenates. The first overheads is fed to a second fixed bed reactor, producing a second reactor effluent including dimers of the isoolefins, unreacted C5s, and unreacted oxygenates. The first bottoms stream and the second reactor effluent are combined and fed to a product splitter, producing a second overheads stream including unreacted C5 olefins, isoolefins, and oxygenates and a second bottoms stream including C10+ hydrocarbons.

Disclosed is a method for producing a catalyst, wherein the method comprises: a supplying step of supplying a dispersion containing a palladium-containing fine particle from a supplying part into a reaction container; a preparing step of preparing a copper-palladium-containing complex in which at least part of a surface of the palladium-containing fine particle is covered with copper, by passing the dispersion through a reacting part and bringing the palladium-containing fine particle in the dispersion into contact with a copper-containing member in the reacting part; and a substituting step of substituting the copper in the copper-palladium-containing complex emitted from an emitting part with platinum by bringing the complex into contact with a platinum-containing solution.

The present disclosure relates to reactor components and their use, e.g., in regenerative reactors. A process and apparatus for utilizing different wetted areas along the flow path of a fluid in a pyrolysis reactor, e.g., a thermally regenerating reactor, such as a regenerative, reverse-flow reactor, is described.

The present disclosure provides oxidative coupling of methane (OCM) systems for small scale and world scale production of olefins. An OCM system may comprise an OCM subsystem that generates a product stream comprising C.sub.2+ compounds and non-C.sub.2+ impurities from methane and an oxidizing agent. At least one separations subsystem downstream of, and fluidically coupled to, the OCM subsystem can be used to separate the non-C.sub.2+ impurities from the C.sub.2+ compounds. A methanation subsystem downstream and fluidically coupled to the OCM subsystem can be used to react H.sub.2 with CO and/or CO.sub.2 in the non-C.sub.2+ impurities to generate methane, which can be recycled to the OCM subsystem. The OCM system can be integrated in a non-OCM system, such as a natural gas liquids system or an existing ethylene cracker.

Systems and methods conducive to the formation of one or more alkene hydrocarbons using a methane source and an oxidant in an oxidative coupling of methane (OCM) reaction are provided. One or more vessels each containing one or more catalyst beds containing one or more catalysts each having similar or differing chemical composition or physical form may be used. The one or more catalyst beds may be operated under a variety of conditions. At least a portion of the catalyst beds may be operated under substantially adiabatic conditions. At least a portion of the catalyst beds may be operated under substantially isothermal conditions.

A method comprises receiving a carbon dioxide recycle stream having carbon dioxide and hydrocarbons. The carbon dioxide recycle stream is fed to a catalytic reactor. The hydrocarbons are converted to carbon dioxide in the catalytic reactor by a catalytic reaction without combustion to form a purified carbon dioxide recycle stream. Electrical energy is generated by using heat produced by the catalytic reactor in the conversion. Another method comprises receiving a recycle stream having carbon dioxide, C.sub.1-C.sub.2 hydrocarbons, and C.sub.3+ hydrocarbons. The C.sub.3+ hydrocarbons are separated from the carbon dioxide and the C.sub.1-C.sub.2 hydrocarbons. The carbon dioxide and the C.sub.1-C.sub.2 hydrocarbons are fed to a catalytic reactor at a pressure greater than about 300 pounds per square inch (psi), and the C.sub.1-C.sub.2 hydrocarbons are converted to carbon dioxide, water, and heat.

In a process for carrying out a chemical reaction gaseous reactants are supplied to a first reaction zone including a first catalyst having a first particle equivalent diameter. The first reaction zone is operated such that when the reactants are contacted with the first catalyst a portion of the reactants is converted to the desired product. An intermediate stream of unreacted reactants and the desired product is removed and passed to a second reaction zone including a tubular reactor. Tubes of the reactor are catalyst carriers containing a second catalyst having a second particle equivalent diameter smaller than the first particle equivalent diameter. The second reaction zone is operated such that when the unreacted reactants are contacted with the second catalyst, at least some of the unreacted reactants are converted to the desired product. A product stream is then recovered. Apparatus for carrying out the process is also described.

The present invention provides a method for producing -hydroxyisobutyric acid amide by hydration of acetone cyanohydrin under the presence of a catalyst composed mainly of manganese oxide using a reactor in which at least two reaction regions are connected in series, the method being characterized by comprising: a step (B) of cyclically supplying at least a portion of a reaction liquid withdrawn from at least one reaction region to a first reaction region (I) in the reactor; and a step (b1) of further cyclically supplying at least a portion of the reaction liquid withdrawn from at least one reaction region to at least one reaction region other than the first reaction region. The method is also characterized in that an oxidizing agent is supplied to at least one reaction region in the reactor.

Disclosed herein are an apparatus and method for continuously producing a cyclic carbonate. The apparatus includes an adiabatic reactor to be filled with a heterogeneous catalyst for reacting an epoxide with carbon dioxide, a circulation path for returning at least a portion of a fluid mixture in a liquid form flowed out through a reactor outlet into the reactor, a carbon dioxide supply means for continuously supplying carbon dioxide in a liquid form or a supercritical state into the circulation path, and an epoxide supply means for continuously supplying an epoxide in a liquid or solution form into the circulation path.