Methods for separating gaseous components, such as unreacted hydrocarbon monomer and/or solvent, from polyolefin solids are provided. The methods include contacting a first stream including polyolefin solids and gaseous unreacted hydrocarbon monomer and/or solvent with a first purge gas in a gas-solid separation vessel to separate the gaseous unreacted hydrocarbon monomer and/or solvent from the polyolefin solids to produce a second stream including polyolefin solids substantially free of gaseous unreacted hydrocarbon monomer and/or solvent and a third stream including the gaseous unreacted hydrocarbon monomer and/or solvent. The first purge gas includes hydrocarbon monomer and/or solvent and has a temperature of at least about 70° C. when entering the gas-solid separation vessel. Systems for carrying out such methods are also provided.

An equal flow scale catcher device, or EFSC, is designed based on a unique scale catching technology for a reactor. With multiple scale catching modules, the EFSC offers equal flows to a catalyst bed or distribution tray of the reactor, independent of each module's degree of saturation with particles of an incoming fluid during operation. Thus, the innovative EFSC system achieves substantial uniformity of fluid delivery across the distribution tray of the reactor and the static pressure field above the liquid level on the distribution tray. Further, the EFSC effectively captures solid particles in the incoming fluid to the reactor and solid particles that form at the top head of the reactor. The EFSC employs a modular structure that allows optimal configuration of the scale catching modules and scale catching units inside each scale catching module, thus efficiently facilitating simple and efficient installation, maintenance, and/or replacement of the EFSC.

The present invention relates generally to an apparatus for housing a chemical looping process comprising of at least one fluidized-bed combustor reactor, at least one entrained riser, at least one particle separator, optionally at least one particle holding reactor, at least one moving-bed reactor, at least one standpipe, at least one L-valve system for solid flow control and interconnecting sections.

In the present invention, only low-growth carbon nanotubes are selectively separated among solid particles discharged during a reaction and then re-input to a reactor, so that it is possible to improve the quality of a carbon nanotube product to be produced and the productivity of a carbon nanotube production process.

A method for processing a chemical stream includes contacting a feed stream with a catalyst in a reactor portion of a reactor system causing a reaction which forms a product stream. The method includes separating the product stream from the catalyst, passing the catalyst to a catalyst processing portion of the reactor system, processing the catalyst in the catalyst processing portion, and passing a portion of the catalyst from the catalyst processing portion of the reactor system into a catalyst withdrawal system that includes a catalyst withdrawal vessel and a transfer line coupling the catalyst withdrawal vessel to the catalyst processing portion. Each of the catalyst withdrawal vessel and the transfer line include an outer metallic shell and an inner refractory lining. The method further includes cooling the catalyst in the catalyst withdrawal vessel from greater than or equal to 680° C. to less than or equal to 350° C.

Apparatus and processes herein provide for converting hydrocarbon feeds to light olefins and other hydrocarbons. The processes and apparatus include a conventional riser reactor in combination with a mixed flow (e.g., including both counter-current and co-current catalyst flows) fluidized bed reactor designed for maximizing light olefins production. The effluents from the riser reactor and mixed flow reactor are processed in a catalyst disengagement vessel, and the catalysts used in each reactor may be regenerated in a common catalyst regeneration vessel. Further, integration of the two-reactor scheme with a catalyst cooler provides a refinery the flexibility of switching the operation between the two-reactor flow scheme, a catalyst cooler only flow scheme, or using both simultaneously.

Systems and methods are provided for oligomerization of olefins to distillate boiling range products while also recycling naphtha boiling range olefins as part of the feed. By performing the olefin oligomerization while also recycling naphtha boiling range olefins, it has been discovered that the resulting distillate boiling range products can have an unexpected improvement in diesel combustion quality, such as an unexpected improvement in cetane rating. In order to manage coke formation and maintain consistent activity profile for the oligomerization catalyst, the reaction can be performed in a moving bed reactor. Additional temperature control can be maintained by the recycling of the naphtha boiling range portions of the oligomerization product back to the reactor.

A coke control reactor, and a device and method for preparing low-carbon olefins from an oxygen-containing compound are provided. The coke control reactor includes a coke control reactor shell, a reaction zone I, and a coke controlled catalyst settling zone; a cross-sectional area at any position of the reaction zone I is less than that of the coke controlled catalyst settling zone; n baffles are arranged in a vertical direction in the reaction zone I; the n baffles divide the reaction zone I into m reaction zone I subzones; and a catalyst circulation hole is formed in each of the baffles, such that a catalyst flows in the reaction zone I in a preset manner. A catalyst charge in the present coke control reactor can be automatically adjusted, and an average residence time of a catalyst in the coke control reactor can be controlled by changing process operating conditions.

A non-spray-drying, dry-granulation process for making a ceramic particulate mixture including from 4 wt % to 9 wt % water. At least 90 wt % of the particles have a particle size of from 80 μm to 600 μm. The process includes the steps of: (a) forming a precursor material; (b) subjecting the precursor material to a compaction step to form a compacted precursor material; (c) subjecting the compacted precursor material to a crushing step to form a crushed precursor material; and (d) subjecting the crushed precursor material to at least two air classification steps. One air classification step removes at least a portion of the particles having a particle size of greater than 600 μm from the crushed precursor material, and the other air classification step removes at least a portion of the particles having a particle size of less than 80 μm from the crushed precursor material.

An apparatus and method for the dry separation of bulk particulate material, especially coarse particles, is provided. The apparatus comprises a chamber, a screen adjacent the chamber and a fluidising device fluidly connected to the chamber. The screen has a screen surface, a plurality of apertures and an opening larger in size than the aperture. A mixture of the coarse particles and a fine particulate medium is fed into the chamber. The fluidising device directs a fluidising fluid to fluidise a fine particulate medium and create a fluidised bed directed towards the screen. The fine particulate medium and the coarse particles pass from the chamber through the openings. The fine particulate medium passes back through the apertures to the chamber. Relatively high density coarse particles also pass back through the openings to the chamber. Relatively low density coarse particles are retained on the screen surface. Vibrations may also be used.