A process for producing hydrogen and pyrolytic carbon from hydrocarbons may involve converting hydrocarbons into hydrogen and carbon in a reactor at temperatures of 1000 C. or more. The reactor may include two electrodes spaced apart from one another in a flow direction of the hydrocarbons. In a region of the reactor between the electrodes an inert gas component is supplied over an entire reactor cross section. The reactor contains carbon particles in the region between the two electrodes. By introducing an inert gas component over the entire reactor cross section, deposition of carbon in this region of the reactor inner wall is prevented, thus effectively inhibiting the formation of conductivity bridges on the reactor inner wall.

Processes and systems for the production of heavy isoparaffinic hydrocarbons include feeding hydrogen and a mixed isoolefin stream, including C8-C12 olefins, isoolefins, and oligomers, and C8-C12+ hydrogenated hydrocarbons to a trickle-bed reactor system. The hydrogen and mixed isoolefin are reacted over a hydrogenation catalyst, producing a liquid effluent comprising hydrogenated hydrocarbons and unreacted olefins and oligomers, and a vapor effluent comprising hydrogenated hydrocarbons, hydrogen and unreacted olefins and oligomers. The liquid effluent is fed to a first heat exchanger, producing a cooled liquid effluent stream, which is combined with the vapor effluent, producing a mixed phase effluent. The mixed phase effluent is cooled in a second heat exchanger, producing a partially condensed effluent, which is fed to a drum, producing a vent stream, a hydrogenated product stream having greater than 95 wt % C8-C12 saturated hydrocarbons, and a hydrogenated recycle stream. The hydrogenated product stream may be provided to downstream blending systems.

The invention discloses partial conversion of a hydrocarbon fuel to CO and H.sub.2 within a heat exchanger reformer, prior to injection of the fuel into fuel reactor of a chemical looping combustion system, including reforming portion of the fuel used for the chemical looping combustion system in the heat exchange reformer through reaction with steam and/or other suitable gas, or reforming portion of the fuel used for the chemical looping combustion system in the heat exchange reformer through reaction with recycled flue gas. The invention further discloses the use of recycled flue gas, without the use of a heat exchange reformer prior to injection of the fuel into the fuel reactor of a chemical looping combustion system.

System for mixing a catalyst precursor into heavy oil using a high boiling hydrocarbon diluent to form a diluted precursor mixture, which is mixed with the heavy oil to form a conditioned feedstock, which is heated to decompose the precursor and form dispersed metal sulfide catalyst particles in situ. The high boiling hydrocarbon diluent is at a temperature above the decomposition temperature of the catalyst precursor and is first fed through a cooler and/or mixed with a cooler diluent to reduce its temperature and avoid premature decomposition of the catalyst precursor. The high boiling hydrocarbon diluent may include a portion of the heavy oil feedstock, a portion of the conditioned feedstock, a vacuum tower bottoms product, or other high boiling hydrocarbon material having a boiling point higher than 524 C. A portion of the diluent may optionally include a medium boiling hydrocarbon material having a boiling point less than 524 C.

Disclosed is a combined reformer including two or more catalyst tubes reacting at different temperatures, having different reforming reactions continuously performed as a combustion gas sequentially supplies heat to two or more catalyst tubes, and capable of easily replacing a catalyst, and a catalyst replacement method thereof.

The present disclosure relates to the aromatization of hydrocarbons with an aromatization catalyst, including methods of aromatization comprising the use of a continuous catalyst regeneration type reformer.

A system including an absorption column configured to receive an acetylene-rich gas stream flowing upwards and a cooled acetylene-lean solvent stream flowing downwards to generate an acetylene-lean gas effluent and an acetylene-rich solvent effluent, one or more heat exchangers for receiving the acetylene-rich solvent effluent, the one or more heat exchangers being configured to transfer heat to the acetylene-rich solvent effluent to generate a heated acetylene-rich solvent stream, and one or more hydrogenation reactors each having one or more catalyst beds, wherein at least a first one of the one or more hydrogenation reactors is configured to convert at least a portion of acetylene in the heated acetylene-rich solvent stream to ethylene in the presence of a first hydrogenation catalyst and hydrogen under first hydrogenation reaction conditions to generate a first hydrogenation effluent including ethylene and a first acetylene-lean solvent effluent.

An electrically heated reactor is a tube surrounded by electrical heating means having radiative sheeting placed coaxially with regard to the reactor tube. The surface area of the sheeting facing the outer surface area of the reactor tube defines an inner surface area covering at least 60% of the reactor tube outer surface area. The distance between the reactor tube and the heating means is selected such that the ratio between the inner surface area of the electrical heating means to the reactor tube outer surface area is in the range of 0.7 to 3.0. The reactor is useful in many industrial scale high temperature gas conversion and heating technologies.