Bubble column reactor assembly (100) is provided, the assembly comprising: a reactor vessel (104) comprising a bottom end and a top end; a pre- distributor plate (150) disposed above the bottom end of the reactor vessel (104) to distribute gas in a liquid, the plate comprising a bottom surface facing the bottom end of the reactor vessel (104) and a top surface opposite to the bottom surface. The pre-distributor plate (150) comprises a plurality of perforations (206), each perforation (206) comprising: a duct (170) projecting from the bottom surface of the pre-distributor plate; and a cap (180) enclosing the duct (170) and the perforation (206). The cap (180) comprises a plurality of openings (210). A gas distributor (110) is disposed below the pre-distributor plate (150) to receive gas and inject gas into the liquid prior to distribution of gas and the liquid by the pre- distributor plate (150).

Bubble column reactor assembly (100) is provided, the assembly comprising: a reactor vessel (104) comprising a bottom end and a top end; a pre- distributor plate (150) disposed above the bottom end of the reactor vessel (104) to distribute gas in a liquid, the plate comprising a bottom surface facing the bottom end of the reactor vessel (104) and a top surface opposite to the bottom surface. The pre-distributor plate (150) comprises a plurality of perforations (206), each perforation (206) comprising: a duct (170) projecting from the bottom surface of the pre-distributor plate; and a cap (180) enclosing the duct (170) and the perforation (206). The cap (180) comprises a plurality of openings (210). A gas distributor (110) is disposed below the pre-distributor plate (150) to receive gas and inject gas into the liquid prior to distribution of gas and the liquid by the pre- distributor plate (150).

The present invention discloses an external loop slurry reactor, comprising a gas-liquid integrated distributor, a riser, a degassing zone, a solid-liquid separation circulation unit, and a storage tank. When the reactor works, reactants are injected into the riser through the gas-liquid integrated distributor; the slurry mixes and flows upwards to the degassing zone at the top for gas removal, and a large number of bubbles are removed. The slurry with catalyst particles then enters a downcomer and flows downwards. The slurry flows into a first-stage hydrocyclone and a multi-stage hydrocyclone in sequence for solid-liquid separation. The diameter of the first-stage hydrocyclone is larger than that of the multi-stage hydrocyclone. The separated solid particles flow back into the riser to continue to participate in the reaction.

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 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).

Techniques for converting carbonate material to carbon monoxide include transferring heat and at least one feed stream that includes a carbonate material and at least one of hydrogen, oxygen, water, or a hydrocarbon, into an integrated calcination and syngas production system that includes a syngas generating calciner (SGC) reactor; calcining the carbonate material to produce a carbon dioxide product and a solid oxide product; initiating a syngas production reaction; producing, from the syngas production reaction, at least one syngas product that includes at least one of a carbon monoxide product, a water product or a hydrogen product; and transferring at least one of the solid oxide product or the at least one syngas product out of the SGC reactor.

A double fluidized bed reactor system including a staircase-type helical blade is proposed. The system includes a bubbling fluidized bed gasification furnace for receiving fuel (for example, combustible waste and biomass) and steam, forming a bubbling fluidized bed through a flow of flow medium therein, and gasifying the fuel, thereby generating a resultant gas, and a high-speed fluidized bed combustion furnace for receiving char of the resultant gas and the flow medium from the bubbling fluidized bed gasification furnace, additionally receiving air, combusting the char so as to heat the flow medium, and transferring the heated flow medium back to the bubbling fluidized bed gasification furnace.

Methods and apparatus for introducing a gas into the reaction zone of a reactor. Such methods and apparatus can more evenly distribute the gas throughout the reaction zone. Spargers for introducing a gas into the reaction zone of a reactor can be employed in systems and methods for carrying out the liquid-phase oxidation of an oxidizable compound, such as para-xylene.

Methods and apparatus for introducing a gas into the reaction zone of a reactor. Such methods and apparatus can more evenly distribute the gas throughout the reaction zone. Spargers for introducing a gas into the reaction zone of a reactor can be employed in systems and methods for carrying out the liquid-phase oxidation of an oxidizable compound, such as para-xylene.

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.