Described herein are methods for the continuous preparation of 1,2-di(furan-2-yl)ethane-1,2-diol from furan-2-carbaldehyde. The methods can proceed chemically or electrochemically. In certain examples, the methods further comprise the application of a static mixer. The present methods produce 1,2-di(furan-2-yl)ethane-1,2-diol in greater yield, purity, chemoselectivity, and stereoselectivity than traditional batch methods.

Provided herein is a method for producing methyl pentenone (MPO) in high yield in a continuous mode in a fixed bed reactor having a plurality of sidewall injecting ports by reacting excess methyl ethyl ketone (MEK) with acetaldehyde in presence of a cation exchange resin catalyst, wherein the acetaldehyde is injected from the plurality of sidewall injecting ports of the reactor. The method is also effective in reducing the complete consumption of the catalyst during the course of the reaction.

A reactor having a shell comprising one or more reactor tubes located within the shell, said reactor tube or tubes comprising a plurality of catalyst receptacles containing catalyst; means for providing a heat transfer fluid to the reactor shell such that the heat transfer fluid contacts the tube or tubes; an inlet for providing reactants to the reactor tubes; and an outlet for recovering products from the reactor tubes; wherein the plurality of catalyst receptacles containing catalyst within a tube comprises catalyst receptacles containing catalyst of at least two configurations.

The present disclosure relates to a low temperature method for the production of pure hydrogen using a methane rich stream as raw material, and to perform in-situ catalyst regeneration. The process involves the decomposition of methane into COx-free hydrogen in an electrochemical/chemical membrane/chemical reactor or chemical fluidised reactor. As the methane decomposition reaction progresses, carbon structures (whiskers) are accumulated at the catalyst surface leading eventually to its deactivation. The catalyst regeneration is achieved using a small fraction of the produced hydrogen to react with carbon formed at the catalyst surface provoking the carbon detachment, thus regenerating the catalyst. This is achieved either by chemical/electrochemical methanation of carbon at the catalyst interface with hydrogen/protons or by rising the temperature of the catalyst, ideally keeping the reactor temperature constant. A single compact device is described, enabling the hydrogen production, hydrogen purification and catalyst regeneration.

A multi-phase combination reaction system has at least one fixed bed hydrogenation reactor. The fixed bed hydrogenation reactor has, arranged from top to bottom, a first hydrogenation reaction area, a gas-liquid separation area, a second hydrogenation reaction area and a third hydrogenation reaction area. The gas-liquid separation area is provided with a raw oil inlet. A hydrogen inlet is provided between the second hydrogenation reaction area and the third hydrogenation reaction area. The system is capable of simultaneously obtaining two fractions in one hydrogenation reactor.

The invention relates to a device (D) for distributing a fluid, which is able to be arranged in a fixed catalytic bed (C.sub.1, C.sub.2) of a reactor (R), said device comprising conveying means for conveying said fluid, comprising a plurality of pipes each directly receiving a distinct share of said fluid, distribution means for distributing said fluid, means for generating a local pressure drop in said fluid, such that: the device comprises manifold means (2a) for collecting said fluid together, and providing the fluidic connection between the pipes of said fluid conveying means and said fluid distribution means, said means for generating a local pressure drop are added on to said conveying or distribution or manifold (2a) means.

A process of polymerizing olefins comprising combining propylene with a polymerization catalyst, hydrogen, and at least one external electron donor, such as at least one amino-silane donor, to form polypropylene in a first polymerization medium under solution or slurry conditions at or below the bubble point; removing hydrogen from the first polymerization medium and providing a first olefin/polyolefin separation step to form a second polymerization medium; transferring the second polymerization medium to a gas phase reactor and further combining with ethylene; obtaining a propylene-based impact copolymer. The propylene-based impact copolymer desirably has a melt flow rate of at least 60 g/10 min and is useful in automotive components.

The present invention relates to a process for producing 2,3,3,3-tetrafluoropropene, comprising the steps: i) providing a stream A comprising at least one starting compound selected from the group consisting of 2-chloro-3,3,3-trifluoropropene and 2,3-dichloro-1,1,1-trifluoropropane; and ii) in an adiabatic reactor comprising a fixed bed composed of an inlet and an outlet, bringing said stream A into contact, in the presence or absence of a catalyst, with HF in order to produce a stream B comprising 2,3,3,3-tetrafluoropropene, characterized in that the temperature at the inlet of the fixed bed of said adiabatic reactor is between 300° C. and 400° C. and the longitudinal temperature difference between the inlet of the fixed bed and the outlet of the fixed bed of said reactor is less than 20° C.

Incorporating into a fixed bed reactor for an exothermal reaction having a catalyst supported on a support having a thermal conductivity typically less than 30 W/mk within the reaction temperature control limits heat dissipative particles having a thermal conductivity of at least 50 W/mk less than 30 W/mk within the reaction temperature control limits helps control the temperature of the reactor bed.

The present invention relates to a process for producing 2-chloro-3,3,3-trifluoropropene, comprising the steps: i) providing a stream A comprising at least one chlorinated compound selected from the group consisting of 2,3-dichloro-1,1,1-trifluoropropane, 1,1,1,2,3-pentachloropropane, 1,1,2,3-tetrachloropropene and 2,3,3,3-tetrachloropropene; and ii) in an adiabatic reactor comprising a fixed bed composed of an inlet and an outlet, bringing said stream A into contact, in the presence or absence of a catalyst, with HF in order to produce a stream B comprising 2-chloro-3,3,3-trifluoropropene, characterized in that the temperature at the inlet of the fixed bed of said adiabatic reactor is between 300° C. and 400° C. and the longitudinal temperature difference between the inlet of the fixed bed and the outlet of the fixed bed of said reactor is less than 20° C.