A method for facilitating the distribution of the flow of one or more streams within a bed vessel is provided. Disposed within the bed vessel are internal materials and structures including multiple operating zones. One type of operating zone can be a processing zone composed of one or more beds of solid processing material. Another type of operating zone can be a treating zone. Treating zones can facilitate the distribution of the one or more streams fed to processing zones. The distribution can facilitate contact between the feed streams and the processing materials contained in the processing zones.

A process (and a related system) for collecting samples of a polymerization catalyst or of a catalyst-containing polymer from an operation unit, having an upper end and a lower end, of a polymerization plant, including the steps of: a) extracting a prefixed amount of product from the lower end of the operation unit through a discharge valve; b) directing the product towards a filtering unit through an inlet valve; c) flushing an inert gas through the filtering unit; d) outgassing the filtering unit, through the outlet valve; and e) displacing the filtering unit, for collecting the sample.

An exhaust gas purification catalyst device including a substrate and an SCR catalyst layer on the substrate, the substrate containing catalyst precious metal particles directly supported on the substrate, the catalyst precious metal particles containing Pt, and the catalyst precious metal particles having an average particle diameter of 30 to 120 nm inclusive.

A method for fluid catalytic cracking (FCC) of petroleum oil feedstock includes reacting the petroleum oil feedstock with a catalyst mixture in a reaction zone of an FCC unit to obtain a product stream including desulfurized hydrocarbon product, unreacted petroleum oil feedstock, and spent catalyst. During the reacting a process control system develops a process model based on data collected during the reacting, the process model characterizing a relationship among the feed rate of the base cracking catalyst, the feed rate of the FCC additive, the operating conditions, the composition of the product stream, and emissions from the reaction; and one or more of (i) a target feed rate of the base cracking catalyst, (ii) a target feed rate of the FCC additive, and (iii) one or more target operating conditions of the reaction in the reaction zone to reduce the emissions from the FCC unit and to increase a yield of the desulfurized hydrocarbon product in the product stream are determined.

The present specification discloses a membrane reactor comprising a reaction region; a permeate region; and a composite membrane disposed at a boundary of the reaction region and the permeate region, wherein the reaction region comprises a bed filled with a catalyst for dehydrogenation reaction, wherein the composite membrane comprises a support layer including a metal with a body-centered-cubic (BCC) crystal structure, and a catalyst layer including a palladium (Pd) or a palladium alloy formed onto the support layer, wherein ammonia (NH.sub.3) is supplied to the reaction region, the ammonia is converted into hydrogen (H.sub.2) by the dehydrogenation reaction in the presence of the catalyst for dehydrogenation reaction, and the hydrogen permeates the composite membrane and is emitted from the membrane reactor through the permeate region.

A multi-bed catalytic converter comprising: a plurality of catalytic beds which are traversed in series by a process gas, sequentially from a first catalytic bed to a last catalytic bed of said plurality, and at least one inter-bed heat exchanger (7) positioned between a first catalytic bed and a second catalytic bed of said plurality, wherein at least the last catalytic bed of said plurality is adiabatic and is made of fine catalyst with a particle size not greater than 2 mm.

A tube reactor for heterogeneous catalysed gas phase reactions having a thermal tube with a catalyst material around which a fluid heat transfer medium, a temperature-sensitive optical waveguide surrounded by a capillary tube that extends into the catalyst material and has measuring points having a predetermined spacing between adjacent measurement points, and can be connected to a source for optical signals and to an evaluation unit (31) for optical signals reflected by the optical waveguide. The optical waveguide has measuring points having a spacing between adjacent measuring points in the axial direction of the thermal tube which is 0.8 to 5 times the shortest edge length of all imaginary cuboids which, having a minimum volume in the cases in which nominal external dimensions are associated with particles of the catalyst material.

A method of improving the operation of polysilicon fluidized bed reactors is disclosed. The present disclosure is directed to the optimization of axial temperature gradients in gas-solid fluidized bed systems. Varying the width of the particle size distribution in the reactor alters the temperature gradient within the reactor, thereby providing a means of a better control of internal temperature profiles and hence better reactor performance.

A classifying fluid bed granulation unit includes a perforated bed floor; a fluid bed section; a solid feed inlet or internal crushing device; a fluidization air inlet; a liquid solution or melt feed inlet and nozzles; an air outlet; and a product outlet; wherein the fluid bed section comprises at least one particle classification element comprising one or more vertically inclined channels having top and bottom end feed openings, and wherein the one or more vertically inclined channels have upper and lower side slots. In operation of the above fluid bed granulation unit, each channel of the element is separating particles into large particle and small particle fractions and transporting the large particle fraction upwards and the small particle fraction downwards in each channel, and the large particle and small particle fractions are transported out of the upper and lower side slots, respectively.

A method for disposing a bed comprising particles in a burner through which a gas can flow, more particularly in a burner basket of an ammonia oxidation burner, where the particles are disposed such that the bed has a greater flow resistance in an edge region of the burner than in an inner region of the burner. Further, a burner basket for a burner may have a bed comprising particles, wherein the particles are disposed such that the bed has a greater flow resistance in an edge region of the burner basket than in an inner region of the burner basket.