The present invention relates to a non-spray-drying, dry-granulation process for making a ceramic particulate mixture comprising from 4 wt % to 9 wt % water, wherein at least 90 wt % of the particles have a particle size of from 80 m to 600 m, wherein the process comprises 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, wherein one air classification step removes at least a portion of the particles having a particle size of greater than 600 m from the crushed precursor material, and wherein the other air classification step removes at least a portion of the particles having a particle size of less than 80 m from the crushed precursor material.

A process comprising polymerizing olefin monomers and optionally comonomers in a first reactor vessel, thereby forming a raw product stream comprising polymerized solids, unreacted monomer and optionally comonomer, the polymerized solids comprising olefin polymer, volatile organic compounds (VOC) and catalyst system. Then the polymerized solids are contacted with a catalyst poison selected from carbon monoxide, carbon dioxide, oxygen, water, alcohols, amines, or mixtures thereof, thereby forming a passivated stream. The passivated stream is maintained in an agitated state within a second reactor. The passivated stream within the second reactor is then contacted with a circulating gas comprising unreacted monomer for a residence time, thereby reducing the concentration of VOC in the polymerized solids by at least 10 wt % compared to the level before entering the second reactor, thereby forming a purified olefin polymer solids stream.

An enclosure for separating and stripping an effluent containing particles includes a side wall defining an internal volume having a longitudinal axis and, inside the internal volume, a separating section and a stripping section for stripping particles downstream of the separating section relative to the circulation of the particles inside the enclosure. The enclosure includes, upstream of the stripping section or a zone of the stripping section provided with stripping elements extending through the internal cross-section of the enclosure, at least one grille extending transversely to the longitudinal axis, and the projection of a single grille or all the grilles onto a transverse plane perpendicular to the longitudinal axis covers 80 to 100% of the internal cross-section of the enclosure.

A hydrocarbon feed stream is exposed to heat in an absence of oxygen (pyrolysis) to convert the hydrocarbon feed stream into a solids stream and a gas stream. The solids stream includes carbon. The gas stream includes hydrogen. The gas stream is separated into an exhaust gas stream and a first hydrogen stream. The first hydrogen stream includes at least a portion of the hydrogen from the gas stream. The carbon is separated from the solids stream to produce a carbon stream. Electrolysis is performed on a water stream to produce an oxygen stream and a second hydrogen stream. At least a portion of the oxygen of the oxygen stream and at least a portion of the carbon of the carbon stream are combined to generate power and a carbon dioxide stream. At least a portion of the generated power is used to perform the electrolysis on the water stream.

A diffusiophoretic water filtration device includes a diffusiophoretic flow chamber having an inlet and an outlet, the flow chamber for receiving the colloidal suspension at the inlet from the inlet manifold, and passing the colloidal suspension between the inlet and at least one outlet in a flow direction; the flow chamber having a removable and reassemblable cover defining a boundary of the diffusiophoretic flow chamber.

A separation device, comprising: a third-stage cyclone housing, a separating unit, and a granule recycle and regeneration unit, wherein, the separating unit is disposed inside the third-stage cyclone housing and comprises: a cyclone separator and a moving bed coupled to each other; the granule recycle and regeneration unit comprises: a riser, a spouted bed regenerator, and a regeneration pipe connecting the spouted bed regenerator with the moving bed; the spouted bed regenerator has upper and lower ends opposing to each other, wherein, the upper end of the spouted bed regenerator is provided with a sleeve which opens downwardly, the sleeve divides an interior of the spouted bed regenerator into a fountain area and an annular gap area, and a regenerating gas outlet which is in communication with the annular gap area is provided on a side wall of the spouted bed regenerator. A centrifugal separation and intercepting filtration of the moving granular bed to fine particles can separate fine particles under low pressure drop, and can continuously separate the captured dust particles and the moving bed granules ensuring a sustainable recycling of the moving bed granules.

In an embodiment, a method of recovering phenol comprises heating a preheater inlet stream in a preheater to form a splitter inlet stream; separating the splitter inlet stream into a splitter top outlet stream and a splitter bottom outlet stream in a splitter column; separating the splitter bottom outlet stream into a crude top outlet stream and a crude bottom outlet stream in a crude phenol column; hydro-extracting the crude top outlet stream in a hydro-extractor column to form an extractor primary outlet stream; recovering a product phenol outlet stream from the extractor primary outlet stream in a finishing column; combining a bisphenol A plant phenol recovery stream from a bisphenol A reaction from a bisphenol A phenol purification system with the preheater inlet stream, the splitter inlet stream, the splitter bottom outlet stream, the crude top outlet stream, or a combination comprising at least one of the foregoing.

The present invention deals with an olefin polymerisation process. At least one olefin is polymerised in gas phase in a fluidised bed in the presence of an olefin polymerisation catalyst in a polymerisation reactor having a vertical body; a generally conical downwards tapering bottom zone; a generally cylindrical middle zone above and connected to said bottom zone; and a generally conical upwards tapering top zone above and connected to said middle zone. Fluidisation gas is introduced to the bottom zone of the reactor from where it passes upwards through the reactor, and withdrawn from the top zone of the reactor. The gas is then compressed, cooled and returned into the bottom zone of the reactor. A fluidised bed is thus formed within the reactor where the growing polymer particles are suspended in the upwards rising gas stream wherein the superficial velocity of the fluidisation gas is less than the transport velocity of the particles. There is no fluidisation grid in the reactor. The fluidisation gas is passed from an inlet chamber into the bottom zone and the gas flows from the upper part of the inlet chamber to the lower part thereof and the gas flows from the lower part of the inlet chamber to the bottom zone.

According to one or more embodiments disclosed herein, a system component of a fluid catalytic reactor system may include a catalyst separation section, a riser, and a reactor vessel. The catalyst separation section may include separation section walls defining an interior region of the catalyst separation section, a gas outlet port, a riser port, a separation device, and a catalyst outlet port. The riser may extend through the riser port of the catalyst separation section and include an external riser section and an internal riser section. The reactor vessel may include a reactor vessel inlet port, and a reactor vessel outlet port in fluid communication with the external riser section of the riser.

In an embodiment, a method of recovering phenol from a bisphenol A production facility comprises reacting phenol and acetone to produce a bisphenol A stream; separating the bisphenol A stream into a product bisphenol A stream and a purge stream; separating the purge stream into a primary top outlet stream and a primary bottom outlet stream; adding an acid catalyst to the primary bottom outlet stream to form a cracker inlet stream; separating the cracker inlet stream into a cracker top outlet stream and a cracker bottom outlet stream; separating the cracker top outlet stream and the cracker bottom outlet stream into a secondary top outlet stream and a secondary bottom outlet stream; forming a bisphenol A plant phenol recovery stream; combining the bisphenol A plant phenol recovery stream with a stream of a phenol purification plant.