A polyolefin production system including: a first reactor configured to produce a first discharge slurry having a first polyolefin; a second reactor configured to produce a second discharge slurry having a second polyolefin; and a post-reactor treatment zone having at least a separation vessel configured to receive the second discharge slurry or both the first discharge slurry and the second discharge slurry.

A method includes at least two-stage process for the oligomerization of short-chain olefins in the presence of a catalyst, wherein the regeneration of the catalyst is stage-customized.

A method of producing p-xylene comprising the steps of separating the reformate feed in the reformate splitter to produce a benzene stream, a combined heavy stream, a xylene stream, and a toluene stream, converting the C9+ aromatic hydrocarbons in the presence of a dealkylation catalyst in the dealkylation reactor to produce a dealkylation effluent, separating the dealkylation effluent in the dealkylation splitter to produce a C9 stream and a C10+ stream, reacting the C9 stream, the toluene stream, the benzene stream, and the hydrogen stream in the presence of a transalkylation catalyst in the transalkylation reactor to produce a transalkylation effluent, separating the p-xylenes from the xylene stream in the p-xylene separation unit to produce a p-xylene product and a p-xylene depleted stream, converting the m-xylene and o-xylene in the p-xylene depleted stream in the isomerization unit to produce an isomerization effluent.

A process includes periodically or continuously introducing an olefin monomer and periodically or continuously introducing a catalyst system or catalyst system components into a reaction mixture within a reaction system, oligomerizing the olefin monomer within the reaction mixture to form an oligomer product, and periodically or continuously discharging a reaction system effluent comprising the oligomer product from the reaction system. The reaction system includes a total reaction mixture volume and a heat exchanged portion of the reaction system comprising a heat exchanged reaction mixture volume and a total heat exchanged surface area providing indirect contact between the reaction mixture and a heat exchange medium. A ratio of the total heat exchanged surface area to the total reaction mixture volume within the reaction system is in a range from 0.75 in.sup.1 to 5 in.sup.1, and an oligomer product discharge rate from the reaction system is between 1.0 (lb)(hr.sup.1)(gal.sup.1) to 6.0 (lb)(hr.sup.1)(gal.sup.1).

A mixture comprising liquid water, a gas and at least one organic compound are injected into a non-thermal gas-liquid plasma discharge reactor to generate a flowing liquid film region with a gas stream flowing alongside. A plasma discharge is propagated along the flowing liquid film region. Water is dissociated and reactive species such as hydroxyl radicals, hydrogen peroxide and nitrogen oxides are formed. The organic compound reacts with the reactive species such as hydroxyl radicals and hydrogen peroxide present in the flowing liquid film region and in the flowing gas stream to produce organic compound dissociation products. At least some organic compound dissociation products and nitrogen oxides are transferred to a bioreactor for further degradation of organic compounds. The nitrogen oxides are used as nutrients for bacteria in the bioreactor. Feedback control of the plasma reactor is based on conditions detected and determined in the biological reactor.

A gas-liquid reactor is provided. The gas-liquid reactor includes a reactor housing, where an outer side of the reactor housing is provided with a heat exchange jacket device, and the reactor housing is provided with a liquid phase inlet, a gas phase inlet and a gas-liquid phase outlet, and is internally provided with an electric dispersion gas distributor in communication with the gas phase inlet, and the electric dispersion gas distributor is provided with needle electrodes; and row tubes are arranged above the electric dispersion gas distributor, lower ends of the row tubes are grounded, and upper ends of the row tubes are located below the gas-liquid phase outlet. The gas-liquid reactor is configured to continuously produce gas-liquid reaction, and a gas-phase material is dispersed by utilizing the needle electrodes to form micrometer-scaled bubbles to be premixed with a liquid-phase material, and then stably flows through the row tubes.

A compact desktop continuous stirred tank reactor easily used on a magnetic stirrer is provided. A desktop continuous stirred tank reactor used on a magnetic stirrer includes a plurality of containers, each of the plurality of containers having a bottom and a shape capable of containing a stir bar, the plurality of containers being configured as a single unit member. The plurality of containers is arranged on the circumference of a circle of rotation of a pair of magnets of the magnetic stirrer or inside the circumference, and adjacent containers communicate through communication holes.

A method and device for producing high quality alcohol beverages, including liquor, cordial, tincture, whiskey, cognac, brandy, vodka, rum, gin, wine, cocktail, etc., is based on the action of hydrodynamic cavitation treatment of components of alcohol beverages. The fluid flow moves at a high rate through a multi-stage blending hydrodynamic device and multi-stage cavitation device to generate hydrodynamic cavitation features in the fluid flow. The cavitation features generate changes in the velocity, pressure, temperature, chemical composition and physical properties of the liquid. Hydrodynamic cavitation processing provides effective blending of components and homogenization of alcoholic beverage, improves its organoleptic qualities.

A compact desktop continuous stirred tank reactor easily used on a magnetic stirrer is provided. A desktop continuous stirred tank reactor used on a magnetic stirrer includes a plurality of containers, each of the plurality of containers having a bottom and a shape capable of containing a stir bar, the plurality of containers being configured as a single unit member. The plurality of containers is arranged on the circumference of a circle of rotation of a pair of magnets of the magnetic stirrer or inside the circumference, and adjacent containers communicate through communication holes.

A mixture comprising liquid water, a gas and at least one organic compound are injected into a non-thermal gas-liquid plasma discharge reactor to generate a flowing liquid film region with a gas stream flowing alongside. A plasma discharge is propagated along the flowing liquid film region. Water is dissociated and reactive species such as hydroxyl radicals, hydrogen peroxide and nitrogen oxides are formed. The organic compound reacts with the reactive species such as hydroxyl radicals and hydrogen peroxide present in the flowing liquid film region and in the flowing gas stream to produce organic compound dissociation products. At least some organic compound dissociation products and nitrogen oxides are transferred to a bioreactor for further degradation of organic compounds. The nitrogen oxides are used as nutrients for bacteria in the bioreactor. Feedback control of the plasma reactor is based on conditions detected and determined in the biological reactor.