The invention relates to a use of a fluorination gas, and the elemental fluorine (F.sub.2) is preferably present in a high concentration, for example, in a concentration of elemental fluorine (F.sub.2), especially of equal to much higher than 15% or even 20% by volume, and to a process for the manufacture of a fluorinated benzene derivative starting from benzoic acid derivative by direct fluorination employing a fluorination gas, wherein the elemental fluorine (F.sub.2) is preferably present in a high concentration, and subsequent decarboxylation of the benzoic acid hypofluorite derivative obtained by direct fluorination. The process of the invention is also directed to the manufacture of a benzoic acid hypofluorite derivative by direct fluorination of benzoic acid derivative. Especially the invention is of interest in the preparation of fluorinated benzene derivative, final products and as well intermediates, for usage in agro-, pharma-, electronics-, catalyst, solvent and other functional chemical applications.

Hydroprocessing reactor internals height reduction is achieved by placing a mixing chamber above the collection tray. The mixing chamber has spillways on the top (top spillways) and the side of the mixing chamber (side spillways) for fluid entry. The design of the spillways has a significant impact on pressure drop. The pressure drop is reduced by having wide shallow spillways rather than narrow and deep spillways without impacting mixing performance. With both side and top spillways, the height of the mixing chamber can be reduced significantly with minimal impact on fluid mixing and pressure drop.

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.

The present application provides a high-gravity device for generating nano/micron bubble and a reaction system. In the device, the liquid phase is continuous phase and the gas phase is dispersed phase. A gas enters the interior of the device from a hollow shaft, and the gas is subjected to primary shearing under a shearing effect of aerating micropores to form bubbles; then, the bubbles rapidly disengage from the surface of a rotating shaft under the effect of the rotating shaft rotating at a high speed, and are subjected to secondary shearing under the high-gravity environment with the strong shearing force formed by the rotating shaft to form nano/micron bubbles. The device has the advantages of fastness, stability, and small average particle size. The average particle size of the formed nano/micron bubbles is between 800 nanometers and 50 microns, and the average particle size of the bubbles can be regulated in a range by adjusting the rotating speed of the rotating shaft.

Systems and methods for hydrodearylation of a hydrocarbon feed stream comprising non-condensed alkyl-bridged multi-aromatic hydrocarbons, the method including supplying a hydrogen feed to the hydrocarbon feed stream comprising non-condensed alkyl-bridged multi-aromatic hydrocarbons; mixing the hydrogen feed with the hydrocarbon feed stream to saturate the hydrocarbon feed stream with hydrogen gas to create a hydrogen-enriched liquid hydrocarbon stream; passing the hydrogen-enriched liquid hydrocarbon stream to a hydrodearylation reactor without a separate gaseous phase of hydrogen; allowing the hydrogen-enriched liquid hydrocarbon stream to react in presence of a catalyst under specific reaction conditions to produce a product stream comprising a reduced concentration of di-aromatic compounds and an increased concentration of mono-aromatic compounds compared to the hydrocarbon feed stream comprising non-condensed alkyl-bridged multi-aromatic hydrocarbons; and recovering, from the hydrodearylation reactor, a product stream for a downstream process, wherein the non-condensed alkyl-bridged multi-aromatic hydrocarbons include at least two benzene rings connected by an alkyl bridge group having at least two carbons, wherein the benzene rings are connected to different carbons of the alkyl bridge group.

A process for shutting down a hydroprocessing reactor and for removing catalyst from the reactor, wherein the reactor includes a quench gas distribution system. The process comprises shutting off hydrocarbon feed to the reactor, stripping hydrocarbons from the catalyst, and cooling the reactor to a first threshold reactor temperature in the range of from 375-425° F. (190-218° C.). At least a portion of circulating gaseous medium flowing to the reactor is then routed through a temporary heat exchanger and cooling the gas to not less than 40° F. (4° C.). Once cooled, mixing the cooled gas with the circulating gaseous medium flowing to the reactor. Continuing steps routing and cooling until a second threshold temperature is reached wherein the reactor temperature is in a range between 120° F. and 250° F. (49° C.-121° C.). The reactor can then be purged with N.sub.2 gas, followed by introducing water into the reactor via the quench gas distribution system. The catalyst can then be safely removed from the reactor.

A method for enabling gas exchange and chemical reactions with one or more liquid streams contained in a reactive process vessel are provided. One or more exchange layers within the process vessel can be composed of both collector media and releaser media. The exchange layers allow elements to facilitate increased performance of vessel operations by promoting gas component mixing and diffusion. Improved rates of gas component exchange mean less coking and more gas components available for reaction.

A system and a process for co-producing dimethyl carbonate and ethylene glycol. The system comprises an interconnected ethylene carbonate preparation unit and an ethylene carbonate alcoholysis unit. The ethylene carbonate preparation unit comprises a fixed bed reactor and a light-component stripping column connected to each other. The fixed bed reactor is filled with a supported ionic liquid catalyst. The process comprises the steps of: reacting carbon dioxide and ethylene oxide as raw materials in the fixed bed reactor to produce ethylene carbonate, purifying the ethylene carbonate and then mixing it with an alcoholysis reaction catalyst, and reacting the mixture with methanol in a reactive distillation tower, producing dimethyl carbonate and ethylene glycol. The process increases the conversion rate of ethylene oxide and avoids the need for a process of separating conventional homogeneous catalysts from ethylene carbonate, thereby reducing process energy consumption and simplifying process procedures.

Hydroprocessing reactor internals height reduction is achieved by placing a mixing chamber above the collection tray. The mixing chamber has spillways on the top (top spillways) and the side of the mixing chamber (side spillways) for fluid entry. The design of the spillways has a significant impact on pressure drop. The pressure drop is reduced by having wide shallow spillways rather than narrow and deep spillways without impacting mixing performance. With both side and top spillways, the height of the mixing chamber can be reduced significantly with minimal impact on fluid mixing and pressure drop.

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.