A separation membrane module a tubular housing, a monolith type membrane structure housed in the housing, and a first flow regulation portion housed in the housing. The housing has an inner circumferential surface and a first opening formed in the inner circumferential surface and configured to allow a sweep gas to flow therethrough. The membrane structure has an outer circumferential surface and a first slit formed in the outer circumferential surface and configured to allow the sweep gas to flow therethrough. The first flow regulation portion has a first flow regulation surface configured to regulate a flow of the sweep gas between the first opening and the first slit.

In a process for the epoxidation of an olefin by continuously reacting the olefin with hydrogen peroxide in a methanol solvent on a fixed bed epoxidation catalyst comprising a titanium zeolite, the hydrogen peroxide is used as an aqueous hydrogen peroxide solution made by an anthraquinone process, the aqueous hydrogen peroxide solution is mixed with methanol to give a feed mixture and this feed mixture is filtered before being contacted with the fixed bed epoxidation catalyst.

Methods and systems or devices for synthesis of dimethyl ether (DME) from carbon dioxide and hydrogen are provided. A high surface area hollow fiber catalytic membrane reactor such as with hollow fibers coated with a water permeable membrane material is used. The reactor also contains a bi-functional methanol synthesis component and dehydration catalyst component such that the two-step reaction takes place on the catalyst surface. Produced water permeates through the membrane, exiting the reactor immediately after it is formed. Unreacted reactants and products flow to the reactor exit.

The present invention relates to a process for the continuous preparation of core-shell nanoparticles, comprising a core of a core material, preferably of a semiconductor material, and a shell of a shell material, preferably of a semiconductor material, wherein selected starting materials for the shell material are mixed with a dispersion of nanoparticles of the core material and are passed continuously through a reaction zone of a tubular reactor, and other starting materials for the shell material are fed to the reaction zone of the tubular reactor at two or more locations, preferably via a tubular membrane, and the starting materials for the shell material react in the reaction zone to form a shell around the nanoparticles of the core material. The invention also relates to the tubular reactor with the membrane and its use for the continuous synthesis of core-shell nanoparticles. The invention also relates to core-shell nanoparticles comprising a core of a core material, preferably of a first semiconductor material, and an outer shell of a shell material, characterized in that, between core and shell, there is only a layer of a transition zone, in which the proportion of the core material gradually decreases toward the shell, while the proportion of the shell material gradually increases.

In one aspect, catalytic membranes are described herein. In some embodiments, a catalytic membrane comprises a surface functionalized with a polymer, the polymer comprising cellulose solubilization functionalities and acid functionalities for the catalytic hydrolysis of cellulose and/or hemicellulose.

An apparatus for generating a desired gas is provided. The apparatus includes an effusion tube comprising a first zone and a second zone. The first zone includes walls of micro-porous metal tube, and a closed end. The second zone includes non-porous metal tube, and an open end. The two-zone effusion tube is fixtured inside of a larger cylindrical metal jacket with gas entry and exit ports at opposite ends of the jacket, which allows gas to flow over the exterior of the effusion tube. The effusion tube is configured to contain a matrix comprising media containing a parent compound and an inert media. A heating means for heating the effusion tube, thereby producing a desired gas which exits the open end of the metal jacket.

The invention relates to a method particularly for reacting phosgene with compounds that contain hydroxyl, thiol, amino and/or formamide groups, comprising the steps of: (I) providing a reactor which has a first reaction chamber (300, 310, 320, 330, 340, 350) and a second reaction chamber (200, 210, 220, 230, 240, 250, 260), the first and the second reaction chambers being separated from one another by means of a porous carbon membrane (100, 110, 120, 130, 140, 150); (II) providing carbon monoxide and chlorine in the first reaction chamber; and simultaneously (III) providing a compound containing hydroxyl, thiol, amino and/or formamide groups in the second reaction chamber. The porous carbon membrane is configured to catalyze the reaction of carbon monoxide and chlorine to obtain phosgene, and to allow this formed phosgene to pass into the second reaction chamber. The invention also relates to a reactor that is suitable for carrying out the claimed method.

Non-oxidative direct methane conversion (NDMC) to value-added products, such as H.sub.2, C.sub.2 hydrocarbons, and aromatics, occurs within a reactor heated to an elevated temperature. The reactor can have a first volume, where a feed gas including methane is provided, separated from a second volume, where a sweep gas is provided, by a dense thin film membrane supported on a porous wall. The thin film membrane is a mixed ionic-electronic permeable membrane that allows H2 generated in the first volume to be transported to the second volume for removal by (or reaction with) the sweep gas. A catalyst can be provided in or adjacent to the first volume. For example, the catalyst can be a metal doped quartz material (e.g., Fe(c)SiO.sub.2) or a metal/zeolite material (e.g., Mo/ZSM5). Methane conversion and/or product selectivity in the reactor can be manipulated by control of gas flow rates, reaction temperatures, and/or feed and sweep gas compositions.

A process for producing xylenes, in particular para-xylene that is less energy intensive than conventional processes is provided. In an embodiment the process comprises contacting a feed mixture in an isomerization zone with a catalyst at isomerization conditions and producing an isomerized product comprising a higher proportion of p-xylene than in the feed mixture, wherein the catalyst comprises an acidic sulfonated catalytic membrane. Xylene isomerization can also be coupled with a p-xylene extraction process, where the raffinate (p-xylene deprived stream) from the extraction process is fed to an isomerization reactor to produce p-xylene. In an embodiment, the process can comprise: a) providing a feed stream comprising a mixture of xylene isomers including p-xylene; b) extracting p-xylene from the feed stream using a separator to separate the feed stream into a p-xylene rich stream and a p-xylene deprived stream; and c) delivering the p-xylene deprived stream to an isomerization unit, the isomerization unit including an acidic sulfonated catalytic membrane, and using the isomerization unit to produce an isomerized product comprising a higher proportion of p-xylene than in the p-xylene deprived stream delivered to the isomerization unit. In any one or more aspects, the isomerization unit can be operated at a temperature in the range of less than 350, for example about 20 C. to about 200 C.

An apparatus includes a conduit with two process fluid inlets at one end of the conduit, one process fluid outlet at an opposing end, a heat exchange medium inlet, and a heat exchange medium outlet. One of the fluid inlets includes a tube extending into the conduit and a perforated node at the end of the tube, and the other of the fluid inlets is arranged up stream of the perforated node. The apparatus further includes hollow tubes positioned longitudinally within the conduit between the two process fluid inlets, the process fluid outlet, the heat exchange medium inlet and the heat exchange medium outlet. In addition, the apparatus includes a collection vessel positioned proximate the fluid outlet and fibers extending through each of the hollow tubes, wherein one end of the fibers is secured to the perforated node and the other end of the fibers extends into the collection vessel.