Method for maximizing the reaction volume in a slurry phase reactor by determining the ratio (f) between the height of the foams (H.sub.f) and the height of the reactor (H.sub.R) through an algorithm defining the gas hold-up in three zones, a first lower zone in which a bubble regime is established, a second intermediate zone where there can be the presence of foams, a third zone situated in the upper hemispherical part in which the multiphase mixture is accelerated until it reaches outlet conditions, the average gas hold-up being given by the weighted average of each of the three gas hold-ups of the three zones, characterized in that it uses nuclear densimeters positioned inside the reactor at different heights and comprises: measuring, for each nuclear densimeter used, gas density values, relating to different gas and/or slurry velocities, which correspond through said algorithm to calculated gas hold-up values, revealing, with a calculated gas hold-up of less than 40%, the absence of foams at least up to the height at which the densimeter is positioned, whose density measured corresponds to said gas hold-up, with a calculated gas hold-up higher than 70%, the presence of foams starting at least from the height of the reactor in which the densimeter is positioned, whose density measured corresponds to said gas hold-up, finally, determining through said algorithm, the ratio f and the extension in height of the possible presence of foams, calculating the consequent height H.sub.f.

Herein disclosed is a method of producing value-added product from light gases, the method comprising: (a) providing light gases comprising at least one compound selected from the group consisting of C1-C6 compounds and combinations thereof; (b) intimately mixing the light gases with a liquid carrier in a high shear device to form a dispersion of gas in the liquid carrier, wherein the dispersion is supersaturated with the light gases and comprises gas bubbles at least some of which have a mean diameter of less than or equal to about 5 micron(s); (c) allowing the value-added product to form and utilizing vacuum to extract unreacted light gases from the liquid carrier; (d) extracting the value-added product; wherein the value-added product comprises at least one component selected from the group consisting of higher hydrocarbons, hydrogen, olefins, alcohols, aldehydes, and ketones. A system for producing value-added product from light gases is also disclosed.

An apparatus may include a mud pot and a reflectometer to monitor a level of an interface between liquid diluent and catalyst slurry in the mud pot using reflectometry. The apparatus may include a mixing tank and a conduit to transfer catalyst slurry from the mud pot to the mixing tank. The apparatus may include a polymerization reactor and a conduit to provide catalyst slurry from the mixing tank to the polymerization reactor.

The present invention concerns a device for limiting the entrainment of solid particles placed inside a three-phase fluidized reactor, said device being constituted by an assembly of flat or truncated cone-shaped plates ranked vertically in one or more rows, and the maximum section of the device being in the range 1 to 10 times the section of the outlet pipework for the effluents. It also concerns a three-phase process employing said device.

The present invention concerns a device for limiting the entrainment of solid particles placed inside a three-phase fluidized reactor, said device being constituted by an assembly of flat or truncated cone-shaped plates ranked vertically in one or more rows, and the maximum section of the device being in the range 1 to 10 times the section of the outlet pipework for the effluents. It also concerns a three-phase process employing said device.

The invention provides a built-in micro-interface oxidation system for preparing terephthalic acid from p-xylene. The oxidation system includes a first reactor, a rectifying tower and a second reactor which are sequentially connected. A first outlet is disposed on a side wall of the first reactor; a first inlet is disposed on a side wall of the second reactor; a material inlet is disposed on a side wall of the rectifying tower; and a material outlet is disposed at a bottom of the rectifying tower. The first outlet is connected with the material inlet of the rectifying tower; the first inlet is connected with the material outlet of the rectifying tower. Micro-interface units are arranged in the first reactor and the second reactor for dispersing and crushing air into bubbles. Through disposing micro-interface units in reactors, problems of high energy consumption, high raw material consumption and low reaction efficiency are solved.

A apparatus comprising: a vessel component comprising a flow-through interior chamber having an interior sidewall and an exterior sidewall; at least two inlets for introducing chemical components into the flow-through interior chamber; at least one outlet for removing product from the flow-through interior chamber; and an off center rotation component which is operatively connected to the vessel component. During operation of the apparatus, the off center rotation component generates vortical movement of at least two chemical components through the flow-through interior chamber of the vessel, and converts at least a portion of the at least two chemical components to at least one reaction product or product mixture. A method of using the apparatus to produce reaction products or product mixtures. The apparatus and method are useful for producing specialty chemicals such as fragrance and flavor compounds, insect pheromones, petrochemicals, pharmaceutical compounds, agrichemical compounds, and the like.

A catalytic cracking system in which liquid hydrocarbon and bio-oil are directed into a reactor riser of a fluid catalytic cracking unit by separate feed spray nozzle assemblies. To protect liquid bio-oil directed through the liquid bio-oil feed nozzle assembly from high temperature degradation, an insulating layer is provided between a central bio-oil feed tube in a concentrically surrounding atomizing gas passageway. Cooling channels also may be provided in the spray tip of the bio-oil feed nozzle assembly.

A catalytic cracking system in which liquid hydrocarbon and bio-oil are directed into a reactor riser of a fluid catalytic cracking unit by separate feed spray nozzle assemblies. To protect liquid bio-oil directed through the liquid bio-oil feed nozzle assembly from high temperature degradation, an insulating layer is provided between a central bio-oil feed tube in a concentrically surrounding atomizing gas passageway. Cooling channels also may be provided in the spray tip of the bio-oil feed nozzle assembly.

Provided is an oxidation reactor capable of oxidizing hydrocarbons with both reaction efficiency and energy efficiency. The oxidation reactor according to the present invention includes a liquid inlet channel, a gas inlet channel, a gas-liquid mixing unit, and a flow reactor. Through the liquid inlet channel, a liquid containing a reaction substrate hydrocarbon is introduced. Through the gas inlet channel, a gas containing oxygen and ozone is introduced. The gas-liquid mixing unit mixes the liquid introduced from the liquid inlet channel with the gas introduced from the gas inlet channel. In the flow reactor, an oxidation catalyst is immobilized or packed. The gas-liquid mixing unit houses, in its channel, a mobile particle which is capable of rotating and/or moving to mix the liquid with the gas to thereby form a gas-liquid slug flow. The gas-liquid slug flow is introduced into the flow reactor.