A method for manufacturing solketal ((2,2-Dimethyl-1,3-dioxolan-4-yl)methanol) includes: (1) milling starting reagents, including at least: glycerol, a catalyst selected from a hard Lewis acid including at least one transition metal, and acetone, the molar ratio (glycerol):(acetone) being less than or equal to 0.8; preferably less than or equal to 0.7, at an ambient temperature greater than or equal to 50° C., preferably greater than or equal to 56° C., in a three-dimensional microbead mill in a liquid phase for a residence time less than or equal to 15 minutes, preferably less than or equal to 10 minutes, and in particular less than or equal to 5 minutes; (2) recovering, as output from the mill, a final composition including solketal and, where appropriate, one or more sub-products corresponding to the starting reagents that have not reacted and/or to 1,3-O-isopropylidene-glycerol, and (3) optionally, separating the solketal from the one or more sub-products.

The present disclosure includes a system for producing low carbon olefins and/or aromatics from raw material comprising naphtha. The system can include a reaction unit that includes a fast fluidized bed reactor, a stripping unit that includes a stripper, and a regeneration unit. The reactor unit is adapted to allow the catalytic cracking of naphtha and to output reaction unit effluent material (spent catalyst and product gas) into the stripping unit, which is adapted to output product gas. The stripping unit is connected to and in fluid communication with the regeneration unit such that the stripping unit supplies the spent catalyst from the reaction unit to regeneration unit. The regeneration unit is adapted to regenerate the spent catalyst to form regenerated catalyst. The regeneration unit is connected to and in fluid communication with the fast fluidized bed reactor such that, in operation, regenerated catalyst can be sent to the fast fluidized bed reactor of the reaction unit.

A coupling reaction apparatus for heavy oil cracking-gasification, including a cracking section and a gasification section communicated with each other, and the cracking section is located above the gasification section; the cracking section is provided with a heavy oil raw material inlet and a fluidizing gas inlet, and an upper part of the cracking section is provided with an oil-gas outlet; and the gasification section is provided with a gasification agent inlet.

A downflow reactor, e.g. a downer reactor or system, includes an outer wall defining an interior reactor space. An elongated plug is within the outer wall having a first end and a second end, defining a longitudinal axis between the first and second ends. A distribution baffle positioned at a vertical position between the first end and the second end of the elongated plug configured and adapted to direct hot down flowing catalyst towards a feedstock spray.

The invention provides an improved system for separation technology intended to reduce unwanted catalyst/thermal reactions by minimizing contact of the hydrocarbons and the catalyst within the reactor.

The invention relates to processes for preparing alkanolamines and ethyleneamines in the liquid phase, by reacting ethylene glycol and/or monoethanolamine with ammonia in the presence of an amination catalyst comprising one or more active metals selected from Sn and the elements of groups 8, 9, 10 and 11 of the Periodic Table of the Elements, wherein the amination catalyst is obtained by reductive calcination of a catalyst precursor. The catalyst precursor here is preferably prepared by contacting a conventional or catalytic support material with one or more soluble compounds of the active metals and optionally one or more soluble compounds of added catalyst elements. The present invention further relates to a process for preparing an amination catalyst comprising one or more active metals selected from Sn and the elements of groups 8, 9, 10 and 11 of the Periodic Table of the Elements, the amination catalyst being obtained by reductive calcination of a catalyst precursor, wherein the reactor in which the catalyst precursor is reductively calcined is connected to a denox plant, and to the use of a denox plant in the preparation of amination catalysts.

In the hydrochlorination reaction, silicon tetrachloride (STC), metallurgical silicon, and hydrogen are converted to trichlorosilane (TCS) at about 540° C. Previously, a pilot-scale reactor was used to study the yield of TCS produced by the hydrochlorination reaction. The yield observed by experimentation compared favorably with a scalable mathematical model developed to predict the rate of TCS conversion. The model predicted that 90% of the final amount of TCS produced was achieved after the reactant gas traveled a quarter of the vertical distance in the reaction section of the reactor. The pilot-scale reactor was shortened to verify the model predictions. In addition, some catalytic effects on the reaction were studied.

A system for removing particle agglomerates from a particulate product stream. The system including a product stream inlet configured for receiving the particulate product stream, a diverter system configured for permitting a particulate product having a size less than or equal to a desired size to pass through the diverter system, a carrying fluid source connected to the diverter system configured to feed a carrying fluid into the diverter system to carry the particle agglomerate out of the diverter system during a discharge operation, a collector vessel connected to the diverter system, the collector vessel configured for receiving the particle agglomerate carried out by the carrying fluid from the diverter system during the discharge operation, and a particulate product outlet connected to the diverter system, the particulate product outlet configured for conveying the particulate product to a downstream process.

A turbulent fluidized bed reactor, device and method for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene, resolving or improving the competition problem between an MTO reaction and an alkylation reaction during the process of producing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene, and achieving a synergistic effect between the MTO reaction and the alkylation reaction. By controlling the mass transfer and reaction, competition between the MTO reaction and the alkylation reaction is coordinated and optimized to facilitate a synergistic effect of the two reactions, so that the conversion rate of benzene, the yield of para-xylene, and the selectivity of light olefins are increased. The turbulent fluidized bed reactor includes a first reactor feed distributor and a number of second reactor feed distributors; the first reactor feed distributor and the plurality of second reactor feed distributions are sequentially arranged.

A universal chemical processor (UCP) including a reactor vessel having a central longitudinal axis and main chamber comprises a first inlet port for a main feedstock, a second inlet port for a fluidizing medium and a third inlet port for one or more reactants. The UCP also includes a reactive radioactive chemical processor (R.sup.2CP) that contains a radioactive element positioned extending along the longitudinal axis in the main chamber. In operation, a fluidized bed can be supported in the main chamber when a fluidizing medium and feedstock are supplied to the main chamber through the first and second inlet ports and the radioactive element of the R.sup.2CP emits ionizing radiation that is capable of ionizing feedstock and reactants, inducing chemical reactions, and sterilizing and decomposing any organic materials within a radiation zone.