СПОСОБ И УСТРОЙСТВО ДЛЯ СНИЖЕНИЯ ЗАГРЯЗНИТЕЛЕЙ ОКРУЖАЮЩЕЙ СРЕДЫ В ТЯЖЕЛОМ СУДОВОМ ЖИДКОМ ТОПЛИВЕ

Изобретение относится к двум вариантам способа снижения загрязнителей окружающей среды в тяжелом судовом жидком топливе. Один из вариантов включает: смешивание некоторого количества сырья тяжелого судового жидкого топлива с некоторым количеством водородного газа в качестве активирующего газа с получением смеси исходного сырья; контактирование смеси сырья с катализаторами, в качестве которых используют по меньшей мере катализатор гидродеметаллирования и катализатор гидродесульфурации, с образованием технологической смеси из смеси сырья; получение указанной технологической смеси и отделение жидких компонентов продукта тяжелого судового жидкого топлива технологической смеси от газообразных компонентов и побочных углеводородных компонентов технологической смеси и выгрузку продукта тяжелого судового жидкого топлива, при этом осуществляют выборочное удаление загрязнений окружающей среды из исходного сырья тяжелого судового жидкого топлива с обеспечением контакта смеси сырья сначала со слоем катализатора ...

ПСЕВДОИЗОТЕРМИЧЕСКИЙ РЕАКТОР

КАТАЛИТИЧЕСКИЙ РЕАКТОР С НИСХОДЯЩИМ ПОТОКОМ

... 1. Каталитический реактор с нисходящим потоком, имеющий множество слоев катализатора, в которые проходит смесь газа и жидкости, причем область между последовательными слоями катализатора снабжена распределительной системой для распределения и смешивания газа и жидкости перед контактом со следующим слоем катализатора, и указанная область содержит (a) линию нагнетания газа, расположенную ниже поддона для поддержания катализатора, (b) собирающий поддон, приспособленный для приема газа и жидкости, (c) коллекторы слива, продолжающиеся выше уровня указанного собирающего поддона и снабженные выходными отверстиями для прохождения газа и жидкости, причем указанные выходные отверстия приспособлены для придания вихревого движения выходящим газу и жидкости, (d) камеру смешения, приспособленную для приема и поддержания вихревого движения газа и жидкости, спускающихся от указанных коллекторов слива, (e) отбойник ниже указанной камеры смешения, приспособленный для направления потока в радиальном направлении ...

СПОСОБ ОБРАБОТКИ СИСТЕМЫ КАТАЛИТИЧЕСКИХ РЕАКТОРОВПЕРЕД ПРОВЕДЕНИЕМ ТЕХНИЧЕСКОГО ОБСЛУЖИВАНИЯ РЕАКТОРОВ

... 1. Способ проведения технического обслуживания для системы каталитических реакторов, включающий уменьшение уровня содержания в системе каталитических реакторов, по меньшей мере, одного вредного вещества, включающего бензол, где активность содержащегося в системе катализатора после проведения технического обслуживания согласно измерению Т-экв. находится в пределах отклонения приблизительно на 11°С (20°F) от активности катализатора до проведения технического обслуживания. 2. Способ по п.1, где уменьшение уровня содержания, по меньшей мере, одного вредного вещества включает окисление, по меньшей мере, одного вредного вещества. 3. Способ по п.2, где окисление, по меньшей мере, одного вредного вещества происходит при температуре в диапазоне от приблизительно 177°С (350°F) до приблизительно 260°С (500°F). 4. Способ по п.1, где уменьшение уровня содержания, по меньшей мере, одного вредного вещества происходит до безопасного уровня воздействия. 5. Способ по п.2, дополнительно включающий отслеживание ...

NH3 Synthesekonfiguration für Großanlagen

Die Erfindung betrifft ein Verfahren und eine Vorrichtung zur Herstellung eines Produkts aus Synthesegas in zwei hintereinander geschalteten Reaktionsvorrichtungen mit jeweils wenigstens zwei Katalysatorbetten.

PROCEDURE AND DEVICE FOR THE PRODUCTION OF A STYRENE POLYMER IN A MECHANICALLY AGITATED REACTOR

Urea hydrolysis reactor for selective catalytic reduction

This disclosure features a urea conversion catalyst located within a urea decomposition reactor (e.g., a urea decomposition pipe) of a diesel exhaust aftertreatment system. The urea conversion catalyst includes a refractory metal oxide and a cationic 5 dopant. The urea conversion catalyst can decrease the temperature at which urea converts to ammonia, can increase the urea conversion yield, and can decrease the likelihood of incomplete urea conversion. PCCR56867_1 (GHMatters) P100936.AU || b |T ...

Process for the ammonia production

Process and plant for the synthesis of ammonia from a hydrocarbon feedstock, comprising: primary reforming with steam and air-fired secondary reforming wherein primary reforming is performed at a temperature and pressure of at least 790 °C and 50 bar, and secondary reforming is carried out substantially in absence of excess air, the so obtained make-up synthesis gas having a H ...

IMPROVED DISTRIBUTOR SYSTEM FOR DOWNFLOW REACTORS

Downflow catalytic reactor having a plurality of catalyst beds in which a mixture of gas and liquid are passed, the region in between subsequent catalyst beds being provided with a distributor system for the distribution and mixing of gas and liquid prior to contact with a subsequent catalyst bed, said region comprising: (a) gas injection line arranged below a catalyst support tray, (b) collector tray adapted to receive gas and liquid, (c) spillway collectors extending above the level of said collecting tray, (d) mixing chamber adapted to receive the gas and liquid descending from said spillway collectors, (e) impingement plate below said mixing chamber, (f) first distributor tray arranged below said impingement plate having a number of apertures throughout and a number chimneys, and (g) second distributor tray arranged below said first distributor tray for the redistribution of gas and liquid prior to contact with the subsequent catalyst bed, wherein the at least one chimney is provided ...

PROCESS AND DEVICE FOR REDUCING ENVIRONMENTAL CONTAMINATES IN HEAVY MARINE FUEL OIL

A process and device for reducing the environmental contaminants in a ISO 8217 compliant Feedstock Heavy Marine Fuel Oil, the process involving: mixing a quantity of the Feedstock Heavy Marine Fuel Oil with a quantity of Activating Gas mixture to give a feedstock mixture; contacting the feedstock mixture with one or more catalysts to form a Process Mixture from the feedstock mixture; separating the Product Heavy Marine Fuel Oil liquid components of the Process Mixture from the gaseous components and by-product hydrocarbon components of the Process Mixture and, discharging the Product Heavy Marine Fuel Oil. The Product Heavy Marine Fuel Oil is compliant with ISO 821 7 for residual marine fuel oils and has a sulfur level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05 % wt. to 0.5 % wt.. The Product Heavy Marine Fuel Oil can be used as or as a blending stock for an ISO 8217 compliant, IMO MARPOL Annex VI (revised) compliant low sulfur or ultralow sulfur heavy ...

APPARATUS AND METHOD

An apparatus for use in heterogeneous catalytic reactions comprising a column reactor comprising a plurality of trays mounted one above another, each adapted to hold a predetermined liquid volume and a charge of particles of a solid catalyst thereon; means for introducing a liquid phase reactant above the uppermost tray; means for introducing a vapour phase reactant below the lowermost tray; means for removing a liquid phase post-reaction stream from below the lowermost tray; means for removing a vapour phase post-reaction stream from above the uppermost tray; vapour upcomer means associated with each tray adapted to allow vapour to enter that tray from below; underflow means associated with each tray adapted to remove liquid from that tray and the column reactor before being introduced into the column reactor at a lower tray; means for temporarily directing said liquid removed from a tray to bypass at least one lower tray and be reintroduced to the column reactor at a tray located below ...

PROCESS FOR THE AMMONIA PRODUCTION

METHODS FOR CONVERSION OF METHANE IN SYNTHESIS GAS-

Temperature-variable isothermal methanol synthesis reactor

PROCESS AND EQUIPMENT TO MANUFACTURE A POLYMER OF STYRENE IN UNREACTEUR AGITATE MECHANICALLY

La présente invention concerne un appareillage et un procédé de polymérisation du styrène par mise en oeuvre d'un milieu liquide réactionnel de polymérisation dans un réacteur de forme cylindrique, d'axe (A) vertical et muni d'un dispositif d'agitation mécanique comprenant un arbre central mis en rotation dans un sens (S) par un moteur, au moins un mobile d'agitation fixé à l'arbre et au moins une chicane. Plus particulièrement, la chicane est décollée de la paroi latérale du réacteur et a la forme d'un cylindre d'axe vertical et de section transversale choisie parmi l'une des trois formes suivantes : (i) une première forme comprenant un losange ayant une petite (d) et une grande (D) diagonale de rapport (d/D) allant de 0,1/1 à 0,9/1, la petite diagonale étant orientée selon une direction radiale par rapport à l'axe (A) ou selon une direction faisant un angle supérieur à 0° et inférieur ou égal à 45° par rapport à ladite direction radiale, (ii) une seconde forme identique à la première, ...

APPARATUS AND METHOD

Ozone/water contactor

An gas/fluid contactor is provided for reacting water and other fluids with an ozone-containing gas. The contactor comprises an elongate tubular reaction chamber having a gas/fluid combining chamber adjacent the inlet to draw an ozone-containing gas into the device and to provide an initial mixing between the gas and the fluid. One or more mixing chambers are positioned within the reaction chamber, each being filled with a material that provides a matrix of solid elements with interstices of between 0.1 and 2.0 mm. in diameter between the solid elements.

Multi-Stage Device for Reducing Environmental Contaminates in Heavy Marine Fuel Oil

A multi-stage device for reducing the environmental contaminants in an ISO8217 compliant Feedstock Heavy Marine Fuel Oil involving a core desulfurizing process and an ionic liquid extraction desulfurizing process as either a pre-treating step or post-treating step to the core process. The Product Heavy Marine Fuel Oil is compliant with ISO 8217 for residual marine fuel oils and has a sulfur level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05% wt. to 0.5% wt. 1. A device for reducing the environmental contaminants in a Feedstock Heavy Marine Fuel Oil , the device comprising: means for contacting a Feedstock Heavy Marine Fuel Oil with an ionic liquid under extractive desulfurizing conditions to give a pre-treated Feedstock Heavy Marine Fuel Oil; means for mixing a quantity of the pre-treated Feedstock Heavy Marine Fuel Oil with a quantity of Activating Gas mixture to give a Feedstock Mixture; means for contacting the Feedstock Mixture with one or more catalysts under desulfurizing conditions to form a Process Mixture from said Feedstock Mixture; means for receiving said Process Mixture and separating liquid components of the Process Mixture from any gaseous components and any by-product hydrocarbon components of the Process Mixture to form a Product Heavy Marine Fuel Oil and , means for discharging the Product Heavy Marine Fuel Oil.2. The device of claim 1 , wherein the means for contacting a Feedstock Heavy Marine Fuel Oil with a ionic liquid under extractive desulfurizing conditions to give a pre-treated Feedstock Heavy Marine Fuel Oil comprises of a contacting vessel having a first feed inlet pipe through which the Feedstock Heavy Marine Fuel Oil is introduced into the contacting vessel and a second feed inlet pipe through which a sulfur lean ionic liquid is introduced into the contacting vessel; one or more contacting devices or mixing devices in the contacting vessel for forming an emulsion like mixture of the Feedstock Heavy ...

СПОСОБ И УСТАНОВКА ДЛЯ ПОЛУЧЕНИЯ ПОЛИМЕРА СТИРОЛА В РЕАКТОРЕ С МЕХАНИЧЕСКОЙ МЕШАЛКОЙ

Изобретение может быть использовано при осуществлении процесса (со)полимеризации стирола в массе или в растворе. Реактор представляет собой аппарат с боковой стенкой 1 в форме цилиндра вращения относительно вертикальной оси А, нижним 2 и верхним 3 днищами, присоединенными к боковой стенке 1. Механическое устройство для перемешивания включает центральный вращающийся вал 4 с вертикальной осью, совпадающей с осью А, и соединенный с системой привода, включающей двигатель 5 для вращения центрального вала, перемешивающий элемент 7, прикрепленный к центральному валу 4 и направляющую перегородку 14, прикрепленную к аппарату. Направляющая перегородка 14 имеет колонновидную форму с вертикальной осью А'. Изобретение позволяет создать устройство для перемешивания, которое во время полимеризации стирола в водной суспензии обеспечит сохранение устойчивости жидкой смеси для полимеризации, 2 н. и 17 з.п. ф-лы, 9 ил.

СПОСОБ И УСТРОЙСТВО ДЛЯ УМЕНЬШЕНИЯ ГАЗОВЫДЕЛЕНИЯ ТРИТИЙСОДЕРЖАЩИМИ ОТХОДАМИ, ВЫДЕЛЯЕМЫМИ АТОМНОЙ ПРОМЫШЛЕННОСТЬЮ

... 1. Способ уменьшения количества тритиевого водорода (Tили HT) и/или тритиевой воды (HTO или TO), создаваемого по меньшей мере одним контейнером, содержащим по меньшей мере один блок тритийсодержащих отходов (5), создаваемых атомной промышленностью, причем способ отличается тем, что он включает в себя следующие этапы, на которых:приводят контейнер во взаимодействие со смесью (2), содержащей диоксид марганца (MnO), смешанный с соединением, содержащим серебро;приводят контейнер во взаимодействие по меньшей мере с цеолитом (1).2. Способ по п. 1, в котором серебро содержится в смеси (2) в форме по меньшей мере одного из соединений: оксида серебра, соли серебра или комплексного соединения серебра.3. Способ по п. 1, в котором серебро находится в форме оксида серебра в смеси (2), причем массовая концентрация диоксида марганца в смеси (2) составляет от 80 до 99%, а массовая концентрация оксида серебра в смеси (2) составляет от 20 до 1%.4. Способ по п. 3, в котором массовые концентрации в смеси ( ...

СПОСОБ УМЕНЬШЕНИЯ ЗАГРЯЗНЕНИЯ ОКРУЖАЮЩЕЙ СРЕДЫ ИСХОДНЫМ СЫРЬЕМ ТЯЖЕЛОГО СУДОВОГО ЖИДКОГО ТОПЛИВА И УСТРОЙСТВО ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ

Brennstoffzellensystem mit kombinierten passiven und aktiven Sorptionsmittelbetten

Ein Brennstoffzellensystem, das umfasst: einen Kohlenwasserstoffbrennstoffstrom, der eine Schwefelverbindung enthält; ein passives Sorptionsmittelbett, dass ein selektives Schwefel-Sorptionsmittel aufweist, das konfiguriert ist, um die Schwefelverbindung aus dem Kohlenwasserstoffbrennstoffstrom zu entfernen; einen SCSO-Reaktor und ein aktives Sorptionsmittelbett, das ein Schwefeloxid-Sorptionsmittel aufweist, wobei das aktive Sorptionsmittelbett konfiguriert ist, um einen Ablaufstrom von dem SCSO-Reaktor zu empfangen und wenigstens einen Teil der Schwefeloxide über das Schwefeloxid-Sorptionsmittel zu entfernen. Während des Hochfahrens des Brennstoffzellensystems kann der Kohlenwasserstoffbrennstoffstrom während einer ersten Zeitspanne entlang eines ersten Strömungswegs durch das passive Sorptionsmittelbett geleitet werden, um die Schwefelverbindung aus dem Brennstoffstrom zu entfernen, und dann während einer zweiten Zeitspanne z.B. wenn der SCSO-Reaktor/das aktive Sorptionsmittelbett einmal ...

Apparatus and method

Apparatus and method

REACTOR SYSTEM FOR DANGEROUS WASTES.

HAZARDOUS WASTE REACTOR SYSTEM

HAZARDOUS WASTE REACTOR SYSTEM A method and reactor system are described for decomposing organic compounds. A gaseous mixture of organic compounds and water, equal to or in excess of stoichiometry, is passed into a first reaction zone having a temperature range between about 200.degree.C and 1400.degree.C. The first reaction zone has a labyrinthine path which presents organically adsorbent surfaces to the gaseous mixture to provide a residence time in the first reaction zone sufficient to react substantially all of the gaseous organic compounds and the water at high rate. The effluent from the first reaction zone, still with water equal to or in excess of stoichiometry, is then passed to a second reaction zone having a temperature range between about 750.degree.C and 1820.degree.C to decompose the organic compounds remaining in the effluent. The first reaction zone is an annulus which is coaxial with and surrounds the second reaction zone. The labyrinthine path is formed by particulate ...

CATALYTICALLY HEATED FUEL PROCESSOR WITH REPLACEABLE STRUCTURED SUPPORTS BEARING CATALYST FOR FUEL CELL

A highly compact heat integrated fuel processor, which can be used for the production of hydrogen from a fuel source, suitable to feed a fuel cell, is described. The fuel processor assembly comprises a catalytic reforming zone and a catalytic combustion zone, separated by a wall. Catalyst able to induce the reforming reactions is placed in the reforming zone and catalyst able to induce the combustion reaction is placed in the combustion zone, both in the form of coating on a suitable structured substrate, in the form of a metal monolith. Fe¨Cr¨Al¨Y steel foils, in corrugated form so as to enhance the available area for reaction, can be used as suitable substrates. The reforming and the combustion zones can be either in rectangular shape, forming a stack with alternating combustion/reforming zones or in cylindrical shape forming annular sections with alternating combustion/reforming zones, in close contact to each other. The close placement of the combustion and reforming catalyst facilitate ...

CATALYTIC FIXED BED REACTOR FOR PRODUCING ETHYLENE OXIDE BY PARTIAL OXIDATION OF ETHYLENE

A method and a reaction vessel for producing gaseous ethylene oxide from partial oxidation of hydrocarbon using a heterogeneous catalyst fixed bed comprising: - introducing gaseous ethylene, oxygen, ballast gas, and catalyst promoter into a reaction vessel having a catalyst bed with a length such that an outflow area and an inflow area over said catalyst bed length in between the reactor outflow and inflow has an absolute ratio difference less than or equal to 1.3 m; said catalyst having a selectivity greater than 80%; - circulating a heat transfer fluid through at least one coolant heat exchanger in said shell interior; said heat exchanger having a coolant flow cross sectional area ratio to cooling surface area less than 1; - flowing said gaseous ethylene, oxygen, ballast gas and catalyst promoter over said catalyst and through an outlet zone in said reactor vessel, said zone configured with an average residence time of less than or equal to 4 seconds from the catalyst bed to the heat ...

CATALYTICALLY HEATED FUEL PROCESSOR WITH REPLACEABLE STRUCTURED SUPPORTS BEARING CATALYST FOR FUEL CELL

A highly compact heat integrated fuel processor, which can be used for the production of hydrogen from a fuel source, suitable to feed a fuel cell, is described. The fuel processor assembly comprises a catalytic reforming zone (29) and a catalytic combustion zone (28), separated by a wall (27). Catalyst able to induce the reforming reactions is placed in the reforming zone and catalyst able to induce the combustion reaction is placed in the combustion zone, both in the form of coating on a suitable structured substrate, in the form of a metal monolith. Fe-Cr-AI-Y steel foils, in corrugated form so as to enhance the available area for reaction, can be used as suitable substrates The reforming and the combustion zones can be either in rectangular shape, forming a stack with alternating combustion / reforming zones or in cylindrical shape forming annular sections with alternating combustion / reforming zones, in close contact to each other. The close placement of the combustion and reforming ...

DEVICE AND METHOD

APPARATUS AND PROCESS FOR CARRYING OUT HETEROGENEOUS CATALYTIC REACTIONS

Apparatus and method

reator e método de formação, de reação, de montagem ou desmontagem, e de reabastecimento de catalisador

Method for revamping a secondary reformer

A method for revamping a secondary reformer (1), the reformer comprising an internal gas riser pipe (8) for routing a process gas from a bottom gas inlet to a combustion chamber (5) located above a catalytic zone (6), and a distributor (9) for introduction of an oxidation agent such as process air into the combustion chamber. The original distributor of the oxidation agent is discontinued, the gas riser pipe is shortened (8′) and the outlet end of the shortened gas riser pipe is arranged to deliver a gas flow directed upwards. A new burner (20) is installed on top of the reformer, the new burner being arranged to deliver an oxidation agent such as process air with a downward flow, thus obtaining a counterflow mixing zone (23) and formation of a diffusion flame above the outlet end of the gas riser pipe.

System and method for on stream catalyst replacement

A system of reforming reactors comprises a plurality of reactors coupled by flow lines, a feed header coupled to the plurality of reactors by a plurality of feed lines, an effluent header coupled to the plurality of reactors by a plurality of effluent lines, and a plurality of valves disposed in the flow lines, the feed lines, and the effluent lines. Each reactor comprises a reforming catalyst, and the plurality of valves is configured to dynamically connect the plurality of reactors to create a first serial flow path and reconnect the plurality of reactors to create a second serial flow path through the plurality of reactors. A first reactor of the plurality of reactors is adjacent to a second reactor of the plurality of reactors in the first serial flow path, and the first reactor is not adjacent to the second reactor in the second serial flow path.

СПОСОБ ПОЛУЧЕНИЯ АММИАКА

Изобретение относится к способу получения аммиака каталитической реакцией подпиточного синтез-газа, получаемого риформингом углеводородного сырья, и к установке для его осуществления. Способ включает: первичный риформинг углеводородного сырья с водяным паром, с получением первого риформинг-газа, вторичный риформинг первого риформинг-газа с огневым подогревом воздуха, с получением сырого синтез-газа, очистку сырого синтез-газа, с получением подпиточного синтез-газа, конверсию подпиточного синтез-газа в аммиак в контуре синтеза. При этом первичный риформинг проводят при температуре, равной по меньшей мере 790°С, и давлении, равном по меньшей мере 50 бар, а вторичный риформинг проводят в основном без избытка воздуха, по сравнению с его стехиометрическим количеством. Подпиточный синтез-газ имеет молярное отношение Нк N, равное 2,5 или более, но менее 3. Затем осуществляют отбор из контура синтеза продувочного потока, отделение от него потока, содержащего водород, и добавление этого содержащего ...

СМЕСИТЕЛЬНОЕ И РАСПРЕДЕЛИТЕЛЬНОЕ УСТРОЙСТВО, СОДЕРЖАЩЕЕ РАСПРЕДЕЛИТЕЛЬНУЮ ТАРЕЛКУ С ПЕРИФЕРИЙНЫМИ ОТВЕРСТИЯМИ

СПОСОБ МОДЕРНИЗАЦИИ ВТОРИЧНОГО РИФОРМЕРА

... 1. Способ модернизации вторичного риформера (1), включающего:вертикальный корпус (2) для работы под давлением;нижний впускной канал (7) для технологического газа;камеру сгорания (5) и каталитическую зону (6), расположенную ниже камеры сгорания;трубу (8) внутреннего газового стояка, присоединенную к нижнему впускному каналу для технологического газа;средства (9) распределения для введения окислителя, такого как технологический воздух, в камеру сгорания,причем труба (8) газового стояка имеет выпускной конец для газа, расположенный над камерой сгорания, и содержит средства (11) для направления технологического газа вниз так, чтобы он пересекал камеру сгорания и далее каталитическую зону, протекая сверху вниз,отличающийся тем, что в нем, по меньшей мере:удаляют имеющиеся средства (9) распределения окислителя;укорачивают (8′) трубу газового стояка так, чтобы выпускной конец для газа трубы газового стояка опустился ниже по высоте в корпусе высокого давления и ближе к каталитической зоне, по сравнению ...

DISTRIBUTOR DEVICE FOR DOWNWARDFLOWING REACTORS WITH A MINDESTEN SUBDIVIDED CHIMNEY CHAMBER

PROCESS AND DEVICE FOR REDUCING ENVIRONMENTAL CONTAMINATES IN HEAVY MARINE FUEL OIL

Method of treating a catalytic reactor system prior to reactor servicing

distribution and mixing device comprising a cup distribution with peripheral openings

PROCESS AND DEVICE FOR REDUCING ENVIRONMENTAL CONTAMINATES IN HEAVY MARINE FUEL OIL

A process and device for reducing the environmental contaminants in a ISO 8217 compliant Feedstock Heavy Marine Fuel Oil, the process involving: mixing a quantity of the Feedstock Heavy Marine Fuel Oil with a quantity of Activating Gas mixture to give a feedstock mixture; contacting the feedstock mixture with one or more catalysts to form a Process Mixture from the feedstock mixture; separating the Product Heavy Marine Fuel Oil liquid components of the Process Mixture from the gaseous components and by-product hydrocarbon components of the Process Mixture and, discharging the Product Heavy Marine Fuel Oil. The Product Heavy Marine Fuel Oil is compliant with ISO 821 7 for residual marine fuel oils and has a sulfur level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05% wt. to 0.5% wt. The Product Heavy Marine Fuel Oil can be used as or as a blending stock for an ISO 8217 compliant, IMO MARPOL Annex VI (revised) compliant low sulfur or ultralow sulfur heavy marine ...

SYSTEMS AND PROCESSES FOR CONVERSION OF ETHYLENE FEEDSTOCKS TO HYDROCARBON FUELS

Systems, processes, and catalysts are disclosed for obtaining fuel and fuel blends containing selected ratios of open-chain and closed-chain fuel-range hydrocarbons suitable for production of alternate fuels including gasolines, jet fuels, and diesel fuels. Fuel-range hydrocarbons may be derived from ethylene-containing feedstocks and ethanol-containing feedstocks.

Oxygen storage and catalytic alkane conversion

The inventing relates to hydrocarbon conversion, and more particularly to catalytically converting alkane in the presence of oxygen released from an oxygen storage material. Conversion products include C2 hydrocarbon, such as C2+ olefin. The hydrocarbon conversion process can be an oxidative coupling reaction, which refers to the catalytic conversion of methane in the presence of oxidant to produce the olefin product. Flow-through reactors can be used to carry out oxygen storage and the oxidative coupling reaction. Reverse-flow reactors are examples of flow-through reactors, which can be used to carry out oxygen storage and the oxidative coupling reaction.

Oxygen storage and production of C5+ hydrocarbons

Disclosed are reactors and reaction processes for contacting hydrocarbon reactant in the presence of oxygen stored and released within a thermal mass region of the reactor, and catalytically converting at least a portion of alkane, e.g., methane, in the hydrocarbon reactant to produce a reaction mixture comprising a C5+ composition. Oxygen storage and release for carrying out the catalytic conversion is achieved by including an oxygen storage material in a thermal mass region of the reactor. Flow-through reactors can be used to carry out oxygen storage and the hydrocarbon conversion reactions. Reverse-flow reactors are examples of flow-through reactors, which can be used to carry out oxygen storage and the hydrocarbon conversion reactions.

КАТАЛИТИЧЕСКИЙ РЕАКТОР С НИСХОДЯЩИМ ПОТОКОМ

Изобретение может быть использовано, например, для гидроочистки и гидрокрекинга в операциях переработки нефти. Каталитический реактор с нисходящим потоком имеет множество слоев катализатора, в которые проходит смесь газа и жидкости. Область между последовательными слоями катализатора снабжена распределительной системой для распределения и смешивания газа и жидкости перед контактом со следующим слоем катализатора. Ниже поддона для поддержания катализатора расположена линия нагнетания газа. Собирающий поддон приспособлен для приема газа и жидкости. Выше уровня собирающего поддона продолжаются коллекторы слива. Камера смешения приспособлена для приема газа и жидкости, спускающихся от коллекторов слива. Ниже камеры смешения расположен отбойник. Ниже отбойника размещен первый распределительный поддон, имеющий на всем протяжении отверстия и трубки. По меньшей мере одна из трубок снабжена распределительным устройством, которое способно разделять камеру трубки на, по меньшей мере. две камеры. Ниже ...

СПОСОБ ПОЛУЧЕНИЯ АММИАКА

СПОСОБ ПОЛУЧЕНИЯ АКРИЛОВОЙ КИСЛОТЫ ИЗ ФОРМАЛЬДЕГИДА И УКСУСНОЙ КИСЛОТЫ

СПОСОБ И УСТРОЙСТВО ДЛЯ СНИЖЕНИЯ ЗАГРЯЗНИТЕЛЕЙ ОКРУЖАЮЩЕЙ СРЕДЫ В ТЯЖЕЛОМ СУДОВОМ ЖИДКОМ ТОПЛИВЕ

ПРЕОБРАЗОВАНИЕ КАРБОНАТА МЕТАЛЛА В ХЛОРИД МЕТАЛЛА

Fuel cell system with combined passive and active sorbent beds

Reactor and reaction method for reacting carbon monoxide and hydrogen in the presence of a carrier liquid to form a hydrocarbon product

A method of forming a hydrocarbon product, the method comprising a first step of enriching a carrier liquid with carbon monoxide and hydrogen and a subsequent step of bringing the enriched carrier liquid into contact with a catalyst in a first reaction zone of a reactor, wherein the catalyst catalyses reaction of the carbon monoxide and hydrogen to form the hydrocarbon product.

PROCESS AND DEVICE FOR REDUCING ENVIRONMENTAL CONTAMINATES IN HEAVY MARINE FUEL OIL

A process and device for reducing the environmental contaminants in a ISO 8217 compliant Feedstock Heavy Marine Fuel Oil, the process involving: mixing a quantity of the Feedstock Heavy Marine Fuel Oil with a quantity of Activating Gas mixture to give a feedstock mixture; contacting the feedstock mixture with one or more catalysts to form a Process Mixture from the feedstock mixture; separating the Product Heavy Marine Fuel Oil liquid components of the Process Mixture from the gaseous components and by-product hydrocarbon components of the Process Mixture and, discharging the Product Heavy Marine Fuel Oil. The Product Heavy Marine Fuel Oil is compliant with ISO 821 7 for residual marine fuel oils and has a sulfur level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05 % wt. to 0.5 % wt.. The Product Heavy Marine Fuel Oil can be used as or as a blending stock for an ISO 8217 compliant, IMO MARPOL Annex VI (revised) compliant low sulfur or ultralow sulfur heavy ...

METHOD AND APPARATUS FOR GENERATING AND FOR FUSING ULTRA-DENSE HYDROGEN

Disclosed is a method for generating and for fusing ultra-dense hydrogen in which molecular hydrogen is fed into at least one cavity and catalyzed, where the splitting and subsequent condensation of the molecular hydrogen is initiated on a catalyst of the cavity to form an ultra-dense hydrogen, the ultra-dense hydrogen is exposed to pressure or electromagnetic radiation to initiate fusion of the ultra-dense hydrogen in the at least one cavity and the reaction heat is led out from the at least one cavity, where the pressure as mechanical resonance or the electromagnetic radiation as electromagnetic resonance amplifies the field and therefore the effect. Furthermore, an apparatus for carrying out the method is disclosed.

PROCESS FOR THE AMMONIA PRODUCTION

Process and plant for the synthesis of ammonia from a hydrocarbon feedstock, comprising: primary reforming with steam and air-fired secondary reforming wherein primary reforming is performed at a temperature and pressure of at least 790 °C and 50 bar, and secondary reforming is carried out substantially in absence of excess air, the so obtained make-up synthesis gas having a H2 to N2 molar ratio in the range 2.5 to 3.

SYSTEMS AND PROCESSES FOR CONVERSION OF ETHYLENE FEEDSTOCKS TO HYDROCARBON FUELS

Systems, processes, and catalysts are disclosed for obtaining fuel and fuel blends containing selected ratios of open-chain and closed-chain fuel-range hydrocarbons suitable for production of alternate fuels including gasolines, jet fuels, and diesel fuels. Fuel-range hydrocarbons may be derived from ethylene-containing feedstocks and ethanol-containing feedstocks.

UREA HYDROLYSIS REACTOR FOR SELECTIVE CATALYTIC REDUCTION

This disclosure features a urea conversion catalyst located within a urea decomposition reactor (e.g., a urea decomposition pipe) of a diesel exhaust aftertreatment system. The urea conversion catalyst includes a refractory metal oxide and a cationic dopant. The urea conversion catalyst can decrease the temperature at which urea converts to ammonia, can increase the urea conversion yield, and can decrease the likelihood of incomplete urea conversion.

MIXING AND DISTRIBUTION DEVICE COMPRISING A DISTRIBUTION TRAY WITH PERIPHERAL APERTURES

APPARATUS AND METHOD

SYSTEMS AND PROCESSES FOR CONVERSION OF ETHYLENE FEEDSTOCKS TO HYDROCARBON FUELS

Systems, processes, and catalysts are disclosed for obtaining fuel and fuel blends containing selected ratios of open-chain and closed-chain fuel-range hydrocarbons suitable for production of alternate fuels including gasolines, jet fuels, and diesel fuels. Fuel-range hydrocarbons may be derived from ethylene-containing feedstocks and ethanol-containing feedstocks.

Material arrangement for fusion reactor and method for producing the same

A material arrangement for a fusion reactor comprising at least one material which is configured as a foam-like carrier material for condensable binding and fusing of hydrogen. The carrier material is provided with positively charged vacancies for condensing hydrogen atoms, small pores for receiving the condensate and for accelerating the condensation after previous penetration of atoms or molecules into these, and large pores for transporting a catalyst into the small pores. Furthermore, a method for producing the material arrangement is disclosed.

METHODS OF CATALYTIC HYDROGENATION FOR ETHYLENE GLYCOL FORMATION

Embodiments described herein generally relate to hydrogenation catalysts, syntheses of hydrogenation catalysts, and apparatus and methods for hydrogenation. Methods for forming a hydrogenation catalyst may include mixing a silica generating precursor with a copper precursor and adding an ammonium salt to an end pH of between about 5 to about 9. Methods for hydrogenating an oxalate may include forming a reaction mixture by flowing a hydrogenation catalyst to a reactor, flowing a hydrogen source to the reactor, and flowing an oxalate to the reactor, wherein the hydrogenation catalyst has a particle size between about 10 nm to about 40 nm. Methods may further include reacting the oxalate to form ethylene glycol.

СПОСОБ И УСТРОЙСТВО ДЛЯ УМЕНЬШЕНИЯ ГАЗОВЫДЕЛЕНИЯ ТРИТИЙСОДЕРЖАЩИМИ ОТХОДАМИ, ВЫДЕЛЯЕМЫМИ АТОМНОЙ ПРОМЫШЛЕННОСТЬЮ

Изобретение предпочтительно относится к способу уменьшения количества тритиевого водорода, выделяемого атомной промышленностью в процессе работы с радиоактивными отходами. Осуществление заявленного способа предполагает наличие по меньшей мере одного контейнера, содержащего по меньшей мере один блок тритийсодержащих отходов, которые могут содержать или выделять в виде газа тритиевый водород. Заявленный способ характеризуется тем, что приводят контейнер во взаимодействие со смесью, содержащей диоксид марганца (MnO), смешанный с соединением, содержащим серебро (Ag); затем приводят контейнер во взаимодействие по меньшей мере с цеолитом. Техническим результатом является уменьшение необходимости во вмешательстве человека в процесс улавливания тритиевого водорода, а также увеличение длительности эффективного улавливания тритиевого водорода. 2 н. и 28 з.п. ф-лы, 4 ил.

ПРЕОБРАЗОВАНИЕ КАРБОНАТА МЕТАЛЛА В ХЛОРИД МЕТАЛЛА

Изобретение может быть использовано в химической промышленности. Хлорид металла MClполучают взаимодействием карбоната металла в виде твердого вещества с фосгеном, дифосгеном и/или трифосгеном. Металл М выбирают из группы щелочных металлов, щелочноземельных металлов, Al и Zn, «х» соответствует валентности катиона металла. В качестве реагента дополнительно добавляют металл, который отличается от металла М карбоната или соответствует ему. 3 н. и 20 з.п. ф-лы, 1 табл., 17 ил.

СМЕСИТЕЛЬНОЕ И РАСПРЕДЕЛИТЕЛЬНОЕ УСТРОЙСТВО, СОДЕРЖАЩЕЕ РАСПРЕДЕЛИТЕЛЬНУЮ ТАРЕЛКУ С ПЕРИФЕРИЙНЫМИ ОТВЕРСТИЯМИ

Изобретение относится к области экзотермических реакций и более конкретно к реакциям гидроочистки, гидродесульфуризвции, гидроденитрогенизации, гидрокрекинга, гидрогенизации, гидродеоксигенирования или гидродеароматизации, выполняемым в реакторе с неподвижным слоем, более конкретно относится к устройству смешения и распределения текучих сред в реакторе с параллельным нисходящим потоком и к его применению для выполнения экзотермических реакций. Устройство для смешения и распределения текучих сред для каталитического реактора с нисходящим потоком содержит накопительную зону, смесительную зону и распределительную зону, содержащую распределительную тарелку, содержащую, по меньшей мере, одну первую зону, несущую множество трубок, и вторую зону; указанная смесительная зона содержится в кольцевой оболочке, расположенной в распределительной зоне, указанные смесительная зона и распределительная зона ограничиваются, по меньшей мере, одной кольцевой стенкой, содержащей, по меньшей мере, одну секцию ...

СОСТАВ ТЯЖЕЛОГО СУДОВОГО ЖИДКОГО ТОПЛИВА

Изобретение раскрывает тяжелое судовое жидкое топливо, состоящее из 100% гидрообработанного тяжелого судового топлива с высоким содержанием серы, причем перед гидрообработкой высокосернистое тяжелое судовое топливо соответствует стандарту ISO 8217:2017 и имеет товарное качество остаточного судового топлива, но имеет содержание серы (ISO 14596 или ISO 8754) более 0,5% мас., и при этом тяжелое судовое топливо является малосернистым и соответствует стандарту ISO 8217:2017, имеет товарное качество остаточного судового топлива и имеет содержание серы (ISO 14596 или ISO 8754) не более 0,5% мас. Также раскрываются варианты композиций, содержащие указанное гидропереработанное тяжелое судовое топливо и разбавители. Технический результат заключается в уменьшении загрязнений окружающей среды от тяжелого судового жидкого топлива (ТСЖТ) в процессе, который сводит к минимуму изменения желательных свойств ТСЖТ и сводит к минимуму ненужное производство побочных углеводородов (т.е. легких углеводородов ...

Fuel cell system with combined passive and active sorbent beds

A fuel cell system including a hydrocarbon fuel stream including a sulfur compound; a passive sorbent bed including a selective sulfur sorbent configured to remove the sulfur compound from the hydrocarbon fuel stream; SCSO reactor, and an active sorbent bed comprising a sulfur oxide sorbent, wherein the active sorbet bed is configured to receive an effluent stream from the SCSO reactor and remove at least a portion of the sulfur oxides via the sulfur oxide sorbent. During start-up of the fuel cell system, the hydrocarbon fuel stream may be directed along a first flow pathway through the passive sorbent bed to remove the sulfur compound from the fuel stream during a first time period and then directed along a second flow pathway during a second time period that does not pass through the passive sorbent bed, e.g., once the SCSO reactor/active sorbent bed have reached operating temperature.

PROCESS AND DEVICE OF REDUCTION OF THE DEGASIFICATION OF TRITIATED WASTE RESULTING FROM NUCLEAR INDUSTRY

La présente invention a notamment pour objet un procédé de réduction de la quantité d'hydrogène tritié (T2 ou HT) généré par au moins un colis comprenant au moins un déchet tritié (5) susceptible de contenir ou de dégazer de l'hydrogène tritié, le procédé étant caractérisé en ce qu'il comprend les étapes suivantes : - mise en présence du colis avec un mélange (2) comprenant du dioxyde de manganèse (MnO2) combiné à un composé comportant de l'argent (Ag), - mise en présence du colis avec au moins un tamis moléculaire (1). En outre, l'invention a notamment pour objet un dispositif de réduction de la quantité d'hydrogène tritié.

HEAVY MARINE FUEL OIL COMPOSITION

Multi-Stage Process and Device for Treatment Heavy Marine Fuel Oil and Resultant Composition and the Removal of Detrimental Solids

A multi-stage process for reducing the environmental contaminants in an ISO8217 compliant Feedstock Heavy Marine Fuel Oil involving a core desulfurizing process and a Detrimental Solids removal unit as either a pre-treating step or post-treating step to the core process. The Product Heavy Marine Fuel Oil complies with ISO 8217 for residual marine fuel oils and has a sulfur level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05 mass % to 1.0 mass and a Detrimental Solids content less than 60 mg/kg. A process plant for conducting the process is also disclosed.

Process and system for making cyclopentadiene and/or dicyclopentadiene

Processes and systems for making cyclopentadiene and/or dicyclopentadiene include converting acyclic C5 hydrocarbon(s) into CPD in a first reactor to obtain a first reactor hydrocarbon effluent, which is processed in an eductor to obtain an eductor effluent at higher total pressure than atmospheric pressure, separating the eductor effluent in a separator such as compression train to obtain a C5-rich fraction comprising CPD, dimerizing the C5-rich fraction in a second reactor to obtain a product effluent comprising DCPD, which is separated to obtain a DCPD-rich fraction. Multiple-stage of dimerization and separation steps can be optionally used to obtain multiple DCPD-rich fractions of various degrees of purity and quantity. C5-rich fractions from various stages of the process may be recycled to the first reactor, or converted into mogas components after selective hydrogenation. C5-rich fractions and mogas components may be optionally separated to produce value-adding chemicals.

СПОСОБ И УСТАНОВКА ДЛЯ ПОЛУЧЕНИЯ ПОЛИМЕРА СТИРОЛА В РЕАКТОРЕ С МЕХАНИЧЕСКОЙ МЕШАЛКОЙ

... 1. Способ (со)полимеризации стирола, осуществляемый с использованием содержащей стирол жидкой реакционной смеси для полимеризации в реакторе с механической мешалкой, представляющем собой аппарат, снабженный боковой стенкой в форме цилиндра вращения относительно вертикальной оси (А), нижним и верхним днищами, присоединенными к боковой стенке, и механическим устройством для перемешивания, включающим i) центральный вал с вертикальной осью, совпадающей с осью (А), и соединенный с системой привода, включающей двигатель для вращения центрального вала, ii) по меньшей мере один перемешивающий элемент, прикрепленный к центральному валу, и (iii) по меньшей мере одну направляющую перегородку, прикрепленную к аппарату, отличающийся тем, что используют направляющую перегородку, размещаемую на некотором расстоянии от боковой стенки аппарата и имеющую колонновидную форму с вертикальной осью и поперечное сечение, выбранное из одной из трех форм, включающих первую ромбовидную форму с длинной и короткой ...

REAKTORSYSTEM FUER GEFAEHRLICHE ABFAELLE.

PROCESS AND DEVICE TO REDUCE TRITIUM WASTE DEGASSING IN THE NUCLEAR INDUSTRY

La présente invention a notamment pour objet un procédé de réduction de la quantité d'hydrogène tritié (T2 ou HT) généré par au moins un colis comprenant au moins un déchet tritié (5) susceptible de contenir ou de dégazer de l'hydrogène tritié, le procédé étant caractérisé en ce qu'il comprend les étapes suivantes : - mise en présence du colis avec un mélange (2) comprenant du dioxyde de manganèse (MnO2) combiné à un composé comportant de l'argent (Ag), - mise en présence du colis avec au moins un tamis moléculaire (1). En outre, l'invention a notamment pour objet un dispositif de réduction de la quantité d'hydrogène tritié.

Fuel cell system with combined passive and active sorbent beds

APPARATUS AND METHOD

Methods of catalytic hydrogenation for ethylene glycol formation

Embodiments described herein generally relate to hydrogenation catalysts, syntheses of hydrogenation catalysts, and apparatus and methods for hydrogenation. Methods for forming a hydrogenation catalyst may include mixing a silica generating precursor with a copper precursor and adding an ammonium salt to an end pH of between about 5 to about 9. Methods for hydrogenating an oxalate may include forming a reaction mixture by flowing a hydrogenation catalyst to a reactor, flowing a hydrogen source to the reactor, and flowing an oxalate to the reactor, wherein the hydrogenation catalyst has a particle size between about 10 nm to about 40 nm. Methods may further include reacting the oxalate to form ethylene glycol.

Multi-Stage Process and Device Utilizing Structured Catalyst Beds and Reactive Distillation for the Production of a Low Sulfur Heavy Marine Fuel Oil

A multi-stage process for the production of an ISO8217 compliant Product Heavy Marine Fuel Oil from ISO 8217 compliant Feedstock Heavy Marine Fuel Oil involving a core process under reactive conditions in a Reaction System composed of one or more reaction vessels, wherein one or more of the reaction vessels contains one or more catalysts in the form of a structured catalyst bed and is operated under reactive distillation conditions. The Product Heavy Marine Fuel Oil has a sulfur level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05 mass % to 1.0 mass. A process plant for conducting the process for conducting the process is disclosed.

Verfahren zur Herstellung von Acrylsäure aus Formaldehyd und Essigsäure

Die vorliegende Erfindung betrifft ein Verfahren zur Herstellung von Acrylsäure aus Formaldehyd und Essigsäure, umfassend das Umsetzen von Formaldehyd und Essigsäure über eine Aldolkondensation in einer Reaktionseinheit umfassend n seriell angeordnete Reaktionszonen jeweils enthaltend einen Aldolkondensationskatalysator, wobei n mindestens 2 ist, und wobei mindestens ein eine Reaktionszone verlassender Stoffstrom vor dem Zuführen in die unmittelbar folgende Reaktionszone mit einem Stoffstrom enthaltend Formaldehyd und gegebenenfalls enthaltend Essigsäure vermischt wird. Ferner betrifft die vorliegende Erfindung eine Vorrichtung zur Herstellung von Acrylsäure aus Formaldehyd und Essigsäure und die Verwendung dieser Vorrichtung.

Systems and processes for conversion of ethylene feedstocks to hydrocarbon fuels

Systems, processes, and catalysts are disclosed for obtaining fuel and fuel blends containing selected ratios of open-chain and closed-chain fuel-range hydrocarbons suitable for production of alternate fuels including gasolines, jet fuels, and diesel fuels. Fuel-range hydrocarbons may be derived from ethylene-containing feedstocks and ethanol-containing feedstocks.

MATERIAL ARRANGEMENT FOR A FUSION REACTOR AND METHOD FOR PRODUCING THE SAME

Disclosed is a material arrangement for a fusion reactor comprising at least one material which is configured as a foam-like carrier material for condensable binding and fusing of hydrogen, where the carrier material is provided with positively charged vacancies for condensing hydrogen atoms, small pores for receiving the condensate and for accelerating the condensation after previous penetration of atoms or molecules into these and large pores for transporting a catalyst into the small pores. Furthermore a method for producing the material arrangement is disclosed.

MIXING AND DISTRIBUTION DEVICE INCLUDING A DISTRIBUTION TRAY WITH PERIPHERAL OPENINGS

Dispositif de mélange et de distribution de fluides pour un réacteur catalytique à écoulement descendant, ledit dispositif comprenant une zone de collecte (A), une zone de mélange (B) et une zone de distribution (C) comprenant un plateau de distribution (12) comportant au moins une première zone (C1) supportant une pluralité de cheminées (13) et une seconde zone (C2) ; ladite zone de mélange (B) est comprise dans une enceinte annulaire (15) située dans la zone de distribution (C), lesdites zones de mélange (B) et de distribution (C) étant délimitées par au moins une paroi annulaire (16) comprenant au moins une section de passage latéral (17a, 17b) apte au passage des fluides de ladite zone de mélange (B) à la première zone (C1) de ladite zone de distribution (C), et la seconde zone (C2) comprend une pluralité d'ouvertures (18) aptes au passage en partie des fluides hors de la zone de distribution (C).

DEVICE FOR MIXING AND DISPENSING COMPRISING A DISPENSING TRAY WITH PERIPHERAL OPENINGS

Dispositif de mélange et de distribution de fluides pour un réacteur catalytique à écoulement descendant, ledit dispositif comprenant une zone de collecte (A), une zone de mélange (B) et une zone de distribution (C) comprenant un plateau de distribution (12) comportant au moins une première zone (C1) supportant une pluralité de cheminées (13) et une seconde zone (C2) ; ladite zone de mélange (B) est comprise dans une enceinte annulaire (15) située dans la zone de distribution (C), lesdites zones de mélange (B) et de distribution (C) étant délimitées par au moins une paroi annulaire (16) comprenant au moins une section de passage latéral (17a, 17b) apte au passage des fluides de ladite zone de mélange (B) à la première zone (C1) de ladite zone de distribution (C), et la seconde zone (C2) comprend une pluralité d'ouvertures (18) aptes au passage en partie des fluides hors de la zone de distribution (C).

METHOD FOR SMOOTHING THE SURFACE CATALYTIC TREATMENT OF HYDROCARBON FEEDSTOCKS

La présente invention se rapporte à un réacteur pour le traitement catalytique d'une charge d'hydrocarbures comprenant : • une enveloppe (21) de forme cylindrique s'étendant selon un axe principal vertical (AX) et définissant une enceinte (22) qui contient une zone réactionnelle (24) comprenant un lit fixe (25) de particules de catalyseur; • une zone de collecte (28) d'un effluent réactionnel située en aval de la zone réactionnelle (24) par rapport au sens d'écoulement de la charge; • au moins un moyen d'entrée (23) de la charge d'hydrocarbures; • une tubulure centrale (29) d'évacuation des particules de catalyseur • au moins deux tubulures (31) de soutirage de l'effluent agencées dans le fond du réacteur (20), Le réacteur est caractérisé en ce que le rapport X entre la section transversale de passage S de la tubulure d'évacuation des particules de catalyseur et la somme des sections transversales de passage S' des tubulures de soutirage de l'effluent est comprise entre 1 et 12.

Multi-stage process and device for treatment heavy marine fuel oil and resultant composition including ultrasound promoted desulfurization

A multi-stage process for reducing the environmental contaminants in an ISO8217 compliant Feedstock Heavy Marine Fuel Oil involving a core desulfurizing process and a ultrasound treatment process as either a pre-treating step or post-treating step to the core process. The Product Heavy Marine Fuel Oil complies with ISO 8217 for residual marine fuel oils and has a sulfur level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05 mass % to 1.0 mass. A process plant for conducting the process is also disclosed.

Process for the ammonia production

Process and plant for the synthesis of ammonia from a hydrocarbon feedstock, comprising: primary reforming with steam and air-fired secondary reforming wherein primary reforming is performed at a temperature and pressure of at least 790 °C and 50 bar, and secondary reforming is carried out substantially in absence of excess air, the so obtained make-up synthesis gas having a H ...

Ozone/water contactor

MATERIAL ARRANGEMENT FOR A FUSION REACTOR AND METHOD FOR PRODUCING THE SAME

Disclosed is a material arrangement for a fusion reactor comprising at least one material which is configured as a foam-like carrier material for condensable binding and fusing of hydrogen, where the carrier material is provided with positively charged vacancies for condensing hydrogen atoms, small pores for receiving the condensate and for accelerating the condensation after previous penetration of atoms or molecules into these and large pores for transporting a catalyst into the small pores. Furthermore a method for producing the material arrangement is disclosed.

A METHOD FOR REVAMPING A SECONDARY REFORMER

A method for revamping a secondary reformer (1), the reformer comprising an internal gas riser pipe (8) for routing a process gas from a bottom gas inlet to a combustion chamber (5) located above a catalytic zone (6), distribution means (9) for introduction of an oxidation agent such as process air into said combustion chamber, wherein the original distribution means of the oxidation agent are discontinued, the gas riser pipe is shortened (8') and the outlet end of the shortened gas riser pipe is arranged to deliver a gas flow directed upwards; a new burner (20) is installed on top of the reactor, said new burner being arranged to deliver an oxidization agent such as process air with a downward flow, thus obtaining a counterflow mixing zone (23) and formation of a diffusion flame above the outlet end of the gas riser pipe.

OZONE/WATER CONTACTOR

An gas/fluid contactor is provided for reacting water and other fluids with an ozone-containing gas. The contactor comprises an elongate tubular reaction chamber having a gas/fluid combining chamber adjacent the inlet to draw an ozone-containing gas into the device and to provide an initial mixing between the gas and the fluid. One or more mixing chambers are positioned within the reaction chamber, each being filled with a material that provides a matrix of solid elements with interstices of between 0.1 and 2.0 mm. in diameter between the solid elements.

Method for producing acrylic acid from formaldehyde and acetic acid

METHOD AND DEVICE FOR REDUCING THE DEGASSING TRITIATED WASTE FROM NUCLEAR INDUSTRY

Systems and processes for conversion of ethylene feedstocks to hydrocarbon fuels

Systems, processes, and catalysts are disclosed for obtaining fuel and fuel blends containing selected ratios of open-chain and closed-chain fuel-range hydrocarbons suitable for production of alternate fuels including gasolines, jet fuels, and diesel fuels. Fuel-range hydrocarbons may be derived from ethylene-containing feedstocks and ethanol-containing feedstocks.

Apparatus for producing trichlorosilane and method for producing trichlorosilane

An apparatus for producing trichlorosilane in which metallurgical grade silicon powder supplied to a reactor is reacted with hydrogen chloride gas while being fluidized by the hydrogen chloride gas, thereby discharging trichlorosilane generated by the reaction from the reactor, includes: a plurality of gas flow controlling members which are installed along a vertical direction in an annular shape R from an inner peripheral wall of the reactor in an internal space of the reactor; and a heat transfer tube which is installed along the vertical direction in the annular space R and through which a heating medium passes.

Split Flow Contactor

Systems and methods for contacting a liquid, gas, and/or a multi-phase mixture with particulate solids. The system can include a body having a first head and a second head disposed thereon. Two or more discrete fixed beds can be disposed across a cross-section of the body. One or more unobstructed fluid flow paths can bypass each fixed bed, and one or more baffles can be disposed between the fixed beds.

Method and apparatus for catalytic and thermochemical reactions

The invention relates to a hybrid reverse flow catalytic apparatus having two reaction zones: a homogeneous reaction zone in porous ceramic and a heterogeneous reaction zone with catalyst, arranged in two different catalyst beds. A first catalytic bed located in a central region of the reactor is provided with a low activity catalyst and a second catalyst bed located in a peripheral region of the reactor is provided with a high activity catalyst. The provision of two catalyst beds containing different catalysts reduces the effect of radial temperature gradients in the reactor and improves the overall efficiency of the reactor. The invention also relates to method of performing catalytic and thermochemical reactions in said apparatus.

Method of Producing Gaseous Products Using a Downflow Reactor

Reactor systems and methods are provided for the catalytic conversion of liquid feedstocks to synthesis gases and other noncondensable gaseous products. The reactor systems include a heat exchange reactor configured to allow the liquid feedstock and gas product to flow concurrently in a downflow direction. The reactor systems and methods are particularly useful for producing hydrogen and light hydrocarbons from biomass-derived oxygenated hydrocarbons using aqueous phase reforming. The generated gases may find used as a fuel source for energy generation via PEM fuel cells, solid-oxide fuel cells, internal combustion engines, or gas turbine gensets, or used in other chemical processes to produce additional products. The gaseous products may also be collected for later use or distribution.

Apparatus and method for hydroconversion

An apparatus is disclosed for the hydroconversion of hydrocarbon feedstock with a hydrogen gas at elevated temperature and pressure with the use of a catalyst. The apparatus is a reactor vessel with a grid plate distributor for improved gas liquid distribution. The distributor comprises a grid plate and a bubble cap assembly with a plurality of tubular risers extending through the grid plate. Each tubular riser has an upper section above the grid plate and a lower section below the grid plate, the lower section terminated with an open bottom end for ingress of the hydrogen gas and hydrocarbon feedstock, the upper section having a closed top terminated with a housing cap. Each tubular riser has at least a vertical slot and a least a side hole sufficiently sized such that in operation, the liquid level in the zone below the grid plate is above the vertical slot and below the side hole opening.

Method Of Operating A Fluid Bed Reactor

Method of operating a three-phase slurry reactor includes feeding at a low level at least one gaseous reactant into a vertically extending slurry body of solid particles suspended in a suspension liquid, the slurry body being contained in at least two vertically extending shafts housed within a common reactor shell, each shaft being divided into a plurality of vertically extending channels at least some of which are in slurry flow communication and the slurry body being present in at least some of the channels. The gaseous reactant is allowed to react as it passes upwardly through the slurry body present in at least some of the channels of the shafts, thereby to form a non-gaseous and/or a gaseous product. Gaseous product, if present, and/or unreacted gaseous reactant is allowed to disengage from the slurry body in a head space above the slurry body.

Processes for Producing Vinyl Acetate Composition Having Low Impurity Content

The present invention, in one embodiment, is to a process for inhibiting impurity formation a vinyl acetate formation reaction. The process comprises the step of providing a reactor comprising an inlet section, an outlet section, a filler (or fillers), and a catalyst block section. The filler is disposed in the outlet section. The catalyst block section may be in communication with and configured between the inlet and outlet sections. The process further comprises the steps of introducing the reactants to the inlet section and contacting the reactants in the catalyst block section under conditions effective to form a crude vinyl acetate composition. The process may further comprise the step of directing the crude vinyl acetate composition into the outlet section, which comprises the filler.

Tube bundle reactor having a structured packing

A tubular reactor for carrying out a catalytically supported, homogeneous chemical reaction in the gas phase at an elevated temperature and a subsequent cooling, wherein the reactor is arranged upright, and therefore the tubes extend vertically and the as flows downward through the tubes. The tubes are filled with a catalyst bed in the upper part thereof extending in the reaction zone of the reactor and are filled with a structured packing in the lower part, the cooling zone of the reactor.

Bi-Modal Radial Flow Reactor

A bi-modal radial flow reactor comprising a cylindrical outer housing surrounding at least five cylindrical, concentric zones, including at least three annulus vapor zones and at least two catalyst zones. The at least two catalyst zones comprise an outer catalyst zone and an inner catalyst zone. The at least three annulus vapor zones comprise an outer annulus vapor zone, a middle annulus vapor zone, and a central annulus vapor zone, wherein the central annulus vapor zone extends along a centerline of the bi-modal radial flow reactor. The outer catalyst zone is intercalated with the outer annulus vapor zone and the middle annulus vapor zone, and the inner catalyst zone is intercalated with the middle annulus vapor zone and the central annulus vapor zone. A removable head cover can be fixably coupled to a top of the cylindrical outer housing to seal a top of the bi-modal radial flow reactor.

REACTOR AND METHOD FOR MAXIMIZING METHANOL YIELD BY USING CATALYST LAYERS

The invention relates to a reactor for the catalytic production of methanol, in which at least two catalyst layers are arranged. The first catalyst layer is arranged upstream and the second catalyst layer is arranged downstream. The activity of the first catalyst layer is higher than the activity of the second catalyst layer. 1. Reactor for the catalytic production of methanol , comprising at least two catalyst layers for the production of methanol arranged in the reactor , wherein the first catalyst layer is arranged upstream and the second catalyst layer is arranged downstream , and wherein the activity of the first catalyst layer for the production of methanol is higher than the activity of the second catalyst layer.2. Reactor according to claim 1 , wherein the catalyst layers are arranged directly adjacent to each other.3. Reactor according to claim 1 , wherein the catalyst layers are arranged in a single packed bed filling.4. Reactor according to claim 1 , wherein the at least two catalyst layers have an essentially identical layer thickness.5. Reactor according to claim 1 , wherein further catalyst layers for the production of methanol claim 1 , are arranged in the reactor claim 1 , wherein the further catalyst layers are each arranged downstream of the second catalyst layer claim 1 , and wherein the activity of the further catalyst layers for the production of methanol successively increases towards the downstream end of the reactor.6. Reactor according to claim 4 , wherein further catalyst layers for the production of methanol claim 4 , are arranged in the reactor claim 4 , wherein the further catalyst layers are each arranged downstream of the second catalyst layer claim 4 , and wherein the activity of the further catalyst layers for the production of methanol successively increases towards the downstream end of the reactor.7. Reactor according to claim 5 , wherein the layer thickness of the first catalyst layer is smaller than the layer thickness of the ...

Catalytic oxidation method and method for producing conjugated diene

An object of the present invention is to suppress performance deterioration of a molybdenum composite oxide-based catalyst at the time of performing gas-phase catalytic partial oxidation with molecular oxygen by using a tubular reactor. The present invention relates to a catalytic oxidation method using a tubular reactor in which a Mo compound layer containing a Mo compound and a composite oxide catalyst layer containing a Mo composite oxide catalyst are arranged in this order from a reaction raw material supply port side and under a flow of a mixed gas containing 75 vol % of air and 25 vol % of water vapor at 440° C., a Mo sublimation amount of the Mo compound is larger than a Mo sublimation amount of the Mo composite oxide catalyst under the same conditions.

Conversion of Metal Carbonate into Metal Chloride

A method for producing metal chloride MClx− includes reacting metal carbonate in solid form using phosgene, diphosgene and/or triphosgene to form metal chloride MClx−, wherein the metal M is selected from the group containing alkali metals, alkaline earth metals, Al and Zn, Li and Mg, or Li, for example, and x corresponds to the valency of the metal cations. An apparatus for performing such method is also disclosed. 1. A method for producing metal chloride MCl , the method comprising:providing phosgene, diphosgene and/or triphosgene,{'sup': x+', '−, 'sub': 'x', 'reacting metal carbonate as solid with the phosgene, diphosgene and/or triphosgene to produce metal chloride MCl,'}wherein the metal M is selected from the group consisting of the alkali metals, alkaline earth metals, Al and Zn, Li and Mg, and Li, andwherein x indicates the valence of the metal cation.2. The method of claim 1 , further comprising adding M as an additional reactant.3. The method of claim 2 , wherein at least one of:the metal M is used together with the metal carbonate, orphosgene, diphosgene and/or triphosgene is prepared in situ by reaction of chlorine with carbon monoxide.4. The method of claim 1 , further comprising subsequently reacting the metal chloride to produce metal M.5. The method of claim 4 , further comprising reacting the produced metal M at least partly with carbon dioxide to produce metal carbonate claim 4 , to thereby form a metal circuit.6. The method of claim 1 , wherein the reaction is performed in a grid reactor or a mechanically moved fixed-bed reactor or in a cyclone reactor.7. The method of claim 1 , wherein the phosgene claim 1 , diphosgene and/or triphosgene is prepared by the reaction of carbon monoxide and chlorine.8. The method of claim 7 , wherein the carbon monoxide is produced by a reaction of metal carbonate with the metal M and/or from an electrolysis of carbon dioxide.9. An apparatus for reacting metal carbonate as solid with phosgene claim 7 , diphosgene ...

Method for producing carbonates

In an embodiment, a method of producing a carbonate comprises reacting carbon monoxide and chlorine in a phosgene reactor in the presence of a catalyst to produce a first product comprising phosgene; wherein carbon tetrachloride is present in the first product in an amount of 0 to 10 ppm by volume based on the total volume of phosgene; and reacting a monohydroxy compound with the phosgene to produce the carbonate; wherein the phosgene reactor comprises a tube, a shell, and a space located between the tube and the shell; wherein the tube comprises one or more of a mini-tube section and a second tube section; a first concentric tube concentrically located in the shell; a twisted tube; an internal scaffold; and an external scaffold.

CATALYST BED COMPRISING SILVER CATALYST BODIES AND PROCESS FOR THE OXIDATIVE DEHYDROGENATION OF OLEFINICALLY UNSATURATED ALCOHOLS

The present invention relates to a catalyst bed comprising silver catalyst bodies and a reactor comprising such a catalyst bed. Further, the invention relates to the use of the catalyst bed and the reactor for gas phase reactions, in particular for the oxidative dehydrogenation of organic compounds under exothermic conditions. In a preferred embodiment, the present invention relates to the preparation of olefinically unsaturated carbonyl compounds from olefinically unsaturated alcohols by oxidative dehydrogenation utilizing a catalyst bed comprising metallic silver catalyst bodies. 118.-. (canceled)19. A process for the preparation of an olefinically unsaturated carbonyl compound in a tubular reactor comprising a plurality of reactor tubes , comprising reacting an olefinically unsaturated alcohol with oxygen in the presence of a catalyst bed , comprising full-metallic silver catalyst bodies , wherein the catalyst bed has a packing density of the full-metallic silver catalyst bodies in the range of 3.0 g/cmto 10.0 g/cm.20. The process according to claim 19 , wherein the catalyst bed has a packing density of the full-metallic silver catalyst bodies in the range of 5.5 g/cmto 10.0 g/cm.21. The process according to claim 19 , wherein the catalyst bed has a void space ratio in the range of 5% to 70% claim 19 , based on the volume of the catalyst bed not occupied by the catalyst bodies per volume of the catalyst bed.22. The process according to claim 19 , wherein the full-metallic silver catalyst bodies have a mean particle size of 0.5 mm to 5.0 mm.23. The process according to claim 19 , wherein the full-metallic silver bodies have a cylindrical shape or spherical shape or sphere-like shape or combinations thereof.24. The process according to claim 19 , wherein the full-metallic silver bodies have a geometric surface area in the range of 100 mm/g to 600 mm/g.25. The process according to claim 19 , wherein the catalyst bed is located in a tube reactor.26. The process ...

CATALYTIC REACTION ANALYSIS DUAL REACTOR SYSTEM AND A CALIBRATION METHOD FOR CORRECTING NON-CATALYTIC EFFECTS USING THE DUAL REACTOR SYSTEM

A catalytic reaction analysis dual reactor system and a method for measuring the catalytic activity of a catalyst by correcting for non-catalytic effects with the catalytic reaction analysis dual reactor system. The dual reactor system contains a first reactor comprising a first catalyst on a first catalyst support, and a second reactor comprising a second catalyst support, wherein the particle size and amount of the first catalyst and the second catalyst support are substantially the same, and the effect of the catalyst is isolated by correcting the result obtained from the first reactor containing the catalyst with the result obtained from the second reactor containing the catalyst support. 1. A catalytic reaction analysis dual reactor system , comprising:a gas loop comprising an inert gas source, a feed gas source, a gas feed line, a first reactor feed line and second reactor feed line, wherein the inert gas source and the feed gas source are in fluid communication with the gas feed line and the gas feed line is in fluid communication with the first and second reactor feed lines;a first reactor comprising a first catalyst chamber loaded with a catalyst comprising a first catalyst on a first catalyst support, a first reactor inlet on an upstream side of the first catalyst chamber and a first reactor outlet on a downstream side of the first catalyst chamber;a second reactor comprising a second catalyst chamber loaded with a second catalyst support, a second reactor inlet on an upstream side of the second catalyst chamber and a second reactor outlet on a downstream side of the second catalyst chamber;wherein the first and second catalyst chambers are substantially the same and the particle size and amount of the first catalyst and the second catalyst support are substantially the same;a gas analyzer comprising an analysis feed line downstream of and connected to the first and second reactor outlets;wherein the first and second reactor are connected in parallel to ...

USE OF TREATING ELEMENTS TO FACILITATE FLOW IN VESSELS

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. 1. A method of improving flow distribution of one or more streams in a process vessel comprising:passing the one or more streams through an upstream processing zone and a downstream processing zone within the process vessel, the upstream processing zone and downstream processing zone each containing one or more beds of processing materials; andpassing the one or more streams through a redistribution treating zone located between the upstream processing zone and downstream processing zone, wherein the redistribution treating zone contains a plurality of treating elements.2. The method of claim 1 , wherein the treating elements are randomly-packed treating elements.3. The method of claim 1 , wherein one or more of the treating elements are ceramic reticulates.4. The method of claim 1 , wherein one or more of the treating elements have at least one opening formed therein. This application is a continuation application and claims the benefit, and priority benefit, of U.S. patent application Ser. No. 15/265,405, filed Sep. 14, 2016, which claims the benefit and priority benefit of U.S. Provisional Patent Application Ser. No. 62/314,069, filed Mar. 28, 2016 and U.S. Provisional Patent Application Ser. No. 62/294,768, filed Feb. 12, 2016, the contents of each are incorporated by reference herein in their entirety.The presently disclosed subject matter relates to facilitating ...

PROCESS FOR PRODUCING BTX FROM A C5-C12 HYDROCARBON MIXTURE

The invention relates to a process for producing BTX comprising: (a) contacting a feedstream comprising C5-C12 hydrocarbons in the presence of hydrogen with a reforming catalyst to produce a reformed product stream, wherein the reforming catalyst comprises a hydrogenation metal and a support of an amorphous alumina, (b) contacting the reformed product stream in the presence of hydrogen with a hydrocracking catalyst to produce a hydrocracking product stream comprising BTX, wherein the hydrocracking catalyst comprises a hydrogenation metal and a zeolite and (c) separating the BTX from the hydrocracking product stream, wherein the hydrocracking catalyst comprises 0.01-1 wt %, preferably 0.01-0.5 wt %, of the hydrogenation metal in relation to the total catalyst weight and the zeolite has a pore size of 5-8 A and a silica (SiO2) to alumina (AI2O3) molar ratio of 5-200, preferably 30-120, wherein step (b) or steps (a) and (b)_are performed at a temperature of 425-580° C., a pressure of 300-5000 kPa gauge and a Weight Hourly Space Velocity of 0.1-15 hpreferably 0.1-10 h. 1. A process for producing BTX comprising:{'sub': 5', '12, '(a) contacting a feedstream comprising C-Chydrocarbons in the presence of hydrogen with a reforming catalyst to produce a reformed product stream, wherein the reforming catalyst comprises a hydrogenation metal and a support of an amorphous alumina,'}(b) contacting the reformed product stream in the presence of hydrogen with a hydrocracking catalyst to produce a hydrocracking product stream comprising BTX, wherein the hydrocracking catalyst comprises a hydrogenation metal and a zeolite and(c) separating the BTX from the hydrocracking product stream,wherein the hydrocracking catalyst comprises 0.01-1 wt % of the hydrogenation metal in relation to the total catalyst weight and the zeolite has a pore size of 5-8 Å and a silica to alumina molar ratio of 5-200,{'sup': '−1', 'wherein step (b) or steps (a) and (b) are performed at a temperature of 425- ...

Multi-Stage Process and Device Utilizing Structured Catalyst Beds for Production of a Low Sulfur Heavy Marine Fuel Oil

A multi-stage process for the distributive production of an ISO 8217 compliant Product Heavy Marine Fuel Oil from ISO 8217 compliant Feedstock Heavy Marine Fuel Oil involving a core process under reactive conditions in a Reaction System composed of one or more reaction vessels, wherein one or more of the reaction vessels contains one or more catalysts in the form of a structured catalyst bed. The Product Heavy Marine Fuel Oil has a sulfur level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05 mass % to 1.0 mass. A process plant for conducting the process for conducting the process is disclosed that can utilize the one or more reaction vessels, wherein one or more of the reaction vessels contains one or more catalysts in the form of a structured catalyst bed. 1. A process for the production of a Product Heavy Marine Fuel Oil , the process comprising: mixing a quantity of Feedstock Heavy Marine Fuel Oil with a quantity of Activating Gas mixture to give a Feedstock Mixture; contacting the Feedstock Mixture with one or more catalysts under reactive conditions to promote the formation of a Process Mixture from said Feedstock Mixture , wherein said one or more catalysts are in the form of a structured catalyst bed; receiving said Process Mixture and separating the liquid components of the Process Mixture from the bulk gaseous components of the Process Mixture; and separating any residual gaseous components and by-product hydrocarbon components from the Product Heavy Marine Fuel Oil.2. The process of claim 1 , wherein the structured catalyst bed comprises a plurality of catalyst retention structures claim 1 , each catalyst retention structure composed of a pair of fluid permeable corrugated metal sheets claim 1 , wherein the pair of the fluid permeable corrugated metal sheets are aligned such that the corrugations are out of phase and thereby defining a catalyst rich space and a catalyst lean space within the structured catalyst bed claim 1 , ...

FLOW DISTRIBUTOR AND REACTOR USING SUCH FLOW DISTRIBUTOR

A cylindrical flow distributor () for performing, by means of solid reaction members, a biological or chemical transformation, or physical or chemical trapping from, or release of agents to, a fluidic media is provided. The flow distributor () comprises: a top wall (); a bottom wall () comprising a central through going opening (); and an outer wall () extending between the top wall () and the bottom wall (). The top wall (), the bottom wall () and an inner envelope surface () of said outer wall () together define a confinement () configured to contain solid reaction membersor a rigid body of a reaction member material. The outer wall () comprises a first plurality of longitudinally extending ribs () arranged side by side with longitudinal gaps () extending in the circumferential direction between two adjacent ribs (), and a circumferentially extending first scaffold () encircling and being fixedly attached to a peripheral outer surface () of said plurality of longitudinally extending ribs (). Further, a reactor using such flow distributor () is provided. 1. A cylindrical flow distributor for performing , by means of solid reaction members , a biological or chemical transformation , or physical or chemical trapping from , or release of agents to , a fluidic media , the flow distributor comprising:a top wall;a bottom wall comprising a central through going opening;an outer wall extending between the top wall and the bottom wall; andan inner wall;wherein the outer wall comprises a first plurality of longitudinally extending ribs arranged side by side along a longitudinal centerline of the flow distributor with gaps extending in the circumferential direction between two adjacent ribs, and a circumferentially extending first scaffold encircling and being fixedly attached to a peripheral outer surface of said plurality of longitudinally extending ribs;wherein the inner wall comprises a second scaffold having an extension along an axial direction of the flow distributor, ...

MOVING BED CATALYTIC REACTOR FOR MANAGING INTERRUPTIONS TO THE CIRCULATION OF CATALYST, AND PROCESS USING SAID REACTOR

The present invention describes a catalytic reactor operating as a moving bed to manage interruptions in the circulation of catalyst while at the same time avoiding mechanical damage to the contact means containing the catalyst. The invention also concerns a refining or petrochemicals process using the reactor in accordance with the invention. 1571351157. A catalytic reactor employing a moving bed catalyst , in which the catalyst is enclosed in baskets () and in which said baskets are movable along a substantially vertical axis and provided with flaps ( , ) which are themselves substantially vertical , installed in the lower portion of said baskets () , and in which , during an interruption to the circulation of catalyst , a storage space () for catalyst located in the lower portion of the reactor is opened up by lifting the assembly of the basket () and the attached flaps () upwards.2. The catalytic reactor according to claim 1 , in which circulation of the catalyst under gravity is resumed as soon as the circulation is re-established.35553. The moving bed catalytic reactor according to claim 1 , in which the catalyst is enclosed in baskets () which are annular in shape claim 1 , wherein the walls are constituted by screens which allow the feed to pass from the exterior towards the interior of the basket () claim 1 , then the reaction effluents to pass from the interior of the basket () towards a centre pipe ().4713121412145141112. The moving bed catalytic reactor according to claim 1 , in which the flaps ( claim 1 , ) slide in vertical sleeves () and are provided with windows () which are obstructed by the sleeves () during normal circulation claim 1 , said windows () being opened up when the basket () is lifted following an interruption to the circulation claim 1 , thus allowing the catalyst to pass through said windows () towards a storage zone () located in the lower portion of the reactor between the sleeve () and the wall of the catalyst.51411. The moving bed ...

System and method for producing hydrogen

To allow hydrogen to be supplied to a dehydrogenation reaction unit for dehydrogenating an organic hydride by using a highly simple structure so that the activity of the dehydrogenation catalyst of the dehydrogenation reaction unit is prevented from being rapidly reduced. The hydrogen production system ( 1 ) comprises a first dehydrogenation reaction unit ( 3 ) for producing hydrogen by a dehydrogenation reaction of an organic hydride in presence of a first catalyst, and a second dehydrogenation reaction unit ( 4 ) for receiving a product of the first dehydrogenation reaction unit, and producing hydrogen by a dehydrogenation reaction of the organic hydride remaining in the product in presence of a second catalyst, wherein an amount of the first catalyst used in the first dehydrogenation reaction unit is equal to or less than an amount of the second catalyst used in the second dehydrogenation reaction unit, and an amount of hydrogen produced in the first dehydrogenation reaction unit is less than an amount of hydrogen produced in the second dehydrogenation reaction unit.

REACTORS, SYSTEMS, AND METHODS FOR FORMING SOLID PRODUCTS

A reactor includes a vessel, a gas inlet, a solid outlet, a catalyst support configured to at least partially retain a catalyst material and allow a tail gas to pass therethrough, and a tail gas outlet. The gas inlet is in fluid communication with the solid outlet. A system for producing a solid product includes a reactor, a compressor, a heater, a make-up reactive gas inlet, and a solids discharge means for removing the solid product from the solid outlet of the reactor. Methods of forming solid products include providing a catalyst material in a vessel having a porous catalyst support, delivering a reactive gas to the vessel, reacting the reactive gas to form a solid product and a tail gas in the vessel, passing the tail gas through a portion of the catalyst material to separate the solid product from the tail gas, and removing the solid product.

Methods and Systems for Forming a Hydrocarbon Product

A method of forming a hydrocarbon product comprises reacting at least one carbon oxide and at least one lower hydrocarbon in the presence of a plurality of catalyst-containing structures each comprising a nanofiber bound to at least one catalyst nanoparticle to form at least one higher hydrocarbon. Other methods of forming a hydrocarbon are also disclosed, as is a system forming a hydrocarbon product.

METHOD FOR PROVIDING A CATALYTICALLY ACTIVE FIXED BED FOR HYDROGENATING ORGANIC COMPOUNDS

Described herein is a process for providing a catalytically active fixed bed for hydrogenation of organic compounds, in which a fixed bed including monolithic shaped bodies as catalyst supports or consisting of monolithic shaped bodies is introduced into a reactor and the fixed bed is then contacted with at least one catalyst or a precursor thereof. The fixed beds laden with a catalyst that are obtained in this way are especially suitable for the hydrogenation of organic compounds in the presence of CO, wherein the conversion is at least 90%. They are notable in that only a very small proportion, if any, of the catalyst introduced is released into the reaction medium. 1. A process for providing a catalytically active fixed bed comprising monolithic shaped bodies as catalyst supports or consisting of monolithic shaped bodies laden with a catalyst comprising at least one metal selected from Ni , Fe , Co , Cu , Cr , Pt , Ag , Au , Pd , Mn , Re , Ru , Rh and Ir , in whicha) a fixed bed comprising monolithic shaped bodies or consisting of monolithic shaped bodies is introduced into a reactor,b) the fixed bed is contacted with a suspension of the at least one catalyst or the precursor thereof in a liquid medium, and the suspension of the at least one catalyst or the precursor thereof is at least partly conducted in a liquid circulation stream, the catalyst or the precursor comprising at least one metal selected from Ni, Fe, Co, Cu, Cr, Pt, Ag, Au, Pd, Mn, Re, Ru, Rh and Ir, to obtain a fixed bed laden with the catalyst or the precursor,c) the laden fixed bed obtained in step b) is optionally subjected to an activation,{'sub': 1', '4, 'd) the laden fixed bed obtained in step b) or the activated fixed bed obtained in step c) is optionally subjected to a treatment with a wash medium selected from water, C-C-alkanols, and mixtures thereof, and'}e) the fixed bed obtained after the activation in step c) or after the treatment in step d) is optionally contacted with a dopant ...

USE OF TREATING ELEMENTS TO FACILITATE FLOW IN VESSELS

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. 1. A method of improving flow distribution of one or more streams in a process vessel comprising:passing the one or more streams through more than one processing zone within the process vessel, wherein each processing zone contains processing materials; andpassing the one or more streams through a redistribution treating zone located within the processing vessel and between an upstream processing zone and a downstream processing zone, wherein the redistribution treating zone comprises at least one layer of fixed material which provides porous structures to facilitate stream flow redistribution by laterally dispersing the one or more streams to provide improved contact between the one or more streams and the downstream processing materials within the processing vessel,wherein there is no space between the upstream processing zone and the redistribution treating zone, andwherein the redistribution zone is located adjacent to both the upstream processing zone and the downstream processing zone.2. The method of claim 1 , wherein a bed zone is disposed upstream of the upstream processing zone.3. The method of claim 1 , wherein certain of the processing materials from the upstream processing zone mix into the redistribution treating zone to create a combo-zone having both processing zone functionality and treating zone functionality.4. The method of claim 1 , wherein the ...

Catalyst Reactor Basket

A catalyst reactor basket is provided that includes an outer side wall extending along the outer circumferential periphery and an inner side wall disposed within the outer side wall. An aperture is sized and shaped to allow a fluid to flow axially with respect to the basket. First and second covers are disposed on opposite ends of the outer side wall and inner side wall and a dividing wall is disposed between the first and second covers. The dividing wall defines a first and second chamber within the inner volume of the basket. A plurality of partitions are disposed within the first and second chambers. The plurality of partitions define a plurality of compartments within the first and second chambers, each compartment being sized and shaped to receive a catalyst. 111-. (canceled)12. A catalyst reactor basket arranged to receive a combination of catalysts in separate chambers , comprising:an outer side wall extending along the outer periphery of the basket and extending to define an inner volume of the basket;an inner side wall disposed within the outer side wall, the inner side wall extending to define an aperture that defines a inner boundary of the volume of the basket, the aperture being sized and shaped to allow a fluid to flow axially with respect to the basket;first and second covers disposed on opposite ends of the outer side wall and inner side wall, the first and second covers defining respective ends of the inner volume of the basket, at least a portion of the first and second covers being fluid permeable; anda dividing wall disposed between the first and second covers, the dividing wall defining a first and second chamber within the inner volume of the basket, at least a portion of the dividing wall being fluid permeable, wherein each of the first and second chambers being sized to receive a respective catalyst so as to enable a two-stage reaction in a single pass of the fluid in the axial direction.13. The catalyst reactor basket as in claim 12 , ...

GAS-SOLID REACTOR

A reactor technology is disclosed for carrying out thermochemical processes namely splitting reactions of gas molecules fed into the reactor where at least one of the product species is temporarily stored within the reactor. 1. A gas-solid reactor body with multiple structured flow paths (channels) , locally parallel to and/or perpendicular and/or at an angle to the walls of the channels , enabling substantial reduction of composition gradients along the main direction of the flow as the solid material of the reactor undergoes oxidation and reduction processes reacting with gas species carried by the flow.2. The reactor of wherein the solid material comprises of from about 30% to about 100% in mass fraction of mixed/doped oxides from the group:substituted ferrites, pure mixed/doped cerium oxides, perovskites or Ruddlesden-Popper phases, and the remaining solid material of from about 0% to about 70% being a thermally resistant ceramic of the oxide type or non-oxide type.3. The reactor of claim 1 , wherein said flow paths have internal structure comprising thin porous elements with thickness of from about 0.1 mm to about 5 mm and porosity of from about 10% to about 80%4. The reactor of made by any of the following processes or combination of them: extrusion claim 1 , casting claim 1 , 3D printing/additive or subtractive manufacturing claim 1 , robocasting claim 1 , gel casting.5. The reactor of wherein one or more of the gas species is HO and/or CO. This application is a Continuation-In-Part of U.S. patent application Ser. No. 13/011,667 filed on Jan. 21, 2011 which is a divisional of U.S. patent application Ser. No. 11/918,359 filed on Jan. 3, 2008 which is a U.S. National Phase Stage Entry of International Application No. PCT/EP2006/061238 filed on Mar. 31, 2006 which claims priority to Application No. DE 10 2005 017 216.4 filed on Apr. 14, 2005 and Application EP 05106614.0 filed on Jul. 19, 2005.The present invention relates to gas molecules splitting methods and ...

PSEUDO-ISOTHERMAL REACTOR

The present disclosure relates in a broad form to a pseudo-isothermal flow reactor () for an exothermal reaction comprising at least two reaction enclosures () and a cooling medium enclosure () configured to hold a cooling medium under pressure at the boiling point of said cooling medium, said reaction enclosures () having an outer surface configured to be in thermal contact with the cooling medium, and each of said reaction enclosures () having an inlet and an outlet with the associated benefit of enabling a two-stage pseudo-isothermal operation while only requiring a single cooling medium enclosure () and only single cooling medium circuit. 1. A pseudo-isothermal flow reactor for an exothermal reaction comprising at least two reaction enclosures and a cooling medium enclosure configured to hold a cooling medium under pressure at the boiling point of said cooling medium , said reaction enclosures having an outer surface configured to be in thermal contact with the cooling medium , each of said reaction enclosures having a reaction enclosure inlet and a reaction enclosure outlet and said cooling medium enclosure having a cooling medium inlet and a cooling medium outlet and each of said inlets and outlets being individually connectable.2. A reactor according to further comprising a catalytically active material inside at least 50% or 80% of the volume of at least one reaction enclosure.3. A reactor according to claim 1 , further comprising an inlet manifold wherein at least one of said first reaction enclosure and said second reaction enclosure comprises a multitude of reaction tubes claim 1 , such as at least 2 claim 1 , 50 claim 1 , 100 or 1000 reaction tubes claim 1 , each tube having a tube inlet in fluid connection with said inlet manifold claim 1 , which is configured to receive a fluid stream from said reaction enclosure inlet and to distribute said fluid stream between the tube inlets of said multitude of reaction tubes.4. A reactor according to claim 1 , ...

FUEL REFORMER AND FUEL CELL

A fuel reformer 20 producing a reformed gas by catalysis by using a fuel gas includes a combustion chamber 24, a combustion nozzle 30, an exhausting pipe 15, a gas distribution gap 25, an outer reforming portion 43, a fuel gas introduction pipe 10, and a reformed gas outlet pipe 11. The combustion nozzle 30 is located in the combustion chamber 24. A columnar protruding portion 40 is provided in the combustion chamber 24. 1. A fuel reformer producing a reformed gas by catalysis by using a fuel gas , the fuel reformer comprising:a body portion in which a tubular combustion chamber extending between a first end and a second end is provided;a combustion nozzle located closer to the first end of the combustion chamber and generating a flame by injecting a combustion gas;an exhausting pipe located closer to the second end and exhausting an exhaust gas generated in the combustion chamber;a gas distribution gap isolated from an inner portion of the combustion chamber and provided along an outer shell of the combustion chamber;an outer reforming portion formed by filling the gas distribution gap with a reforming catalyst;a fuel gas introduction pipe located upstream of the outer reforming portion and introducing a fuel gas to the gas distribution gap; and in the inner portion of the combustion chamber, provided is a columnar protruding portion;', separated from the outer reforming portion with a gap interposed therebetween so as to communicate with the fuel gas introduction pipe and the gas distribution gap, and', 'protruding from the second end side toward the combustion nozzle., 'including an inner space isolated from the combustion chamber,'}], 'a reformed gas exhaust pipe located downstream of the outer reforming portion and exhausting a reformed gas from the gas distribution gap, wherein2. The fuel reformer of claim 1 , wherein:a columnar reforming portion is formed by filling the inner space of the columnar protruding portion with a reforming catalyst.3. The fuel ...

OLEFIN CONVERSION PROCESS

A process for the production of Colefins, which may include: contacting a hydrocarbon mixture comprising alpha-pentenes with an isomerization catalyst to form an isomerization product comprising beta-pentenes; contacting ethylene and the beta-pentenes with a first metathesis catalyst to form a first metathesis product comprising butenes and propylene, as well as any unreacted ethylene and Colefins; and fractionating the first metathesis product to for an ethylene fraction, a propylene fraction, a butene fraction, and a Cfraction. 1. A system for the production of Colefins , the system comprising:an isomerization reaction zone for contacting a hydrocarbon mixture comprising alpha-pentenes with an isomerization catalyst to form an isomerization product comprising beta-pentenes;{'sub': '5', 'a first metathesis reaction zone for contacting ethylene and the beta-pentenes with a first metathesis catalyst to form a first metathesis product comprising butenes and propylene, as well as any unreacted ethylene and Colefins;'}{'sub': '5', 'a separation system for fractionating the first metathesis product to form an ethylene fraction, a propylene fraction, a butene fraction, and a Cfraction; and'}a second metathesis reaction zone for contacting the propylene with a second metathesis catalyst, which may be the same or different than the first metathesis catalyst, to convert at least a portion of the propylene to ethylene and 2-butene and form a second metathesis product.2. The system of claim 1 , further comprising a flow conduit for feeding the first metathesis product and the second metathesis product to a common fractionation system.3. The system of claim 2 , further comprising a flow conduit for withdrawing a propylene product stream.4. The system of claim 3 , further comprising a control system for adjusting a rate of withdrawing the propylene product stream to produce a selected ratio of butene to propylene product.5. The system of claim 1 , further comprising one or more ...

METHOD AND APPARATUS FOR GENERATING AND FOR FUSING ULTRA-DENSE HYDROGEN

A method for generating and for fusing ultra-dense hydrogen in which molecular hydrogen is fed into at least one cavity and catalyzed, where the splitting and subsequent condensation of the molecular hydrogen is initiated on a catalyst of the cavity to form an ultra-dense hydrogen. The ultra-dense hydrogen is exposed to pressure or electromagnetic radiation to initiate fusion of the ultra-dense hydrogen in the at least one cavity and the reaction heat is led out from the at least one cavity. The pressure as mechanical resonance or the electromagnetic radiation as electromagnetic resonance amplifies the field and therefore the effect. Also, an apparatus for carrying out the method is disclosed. 113-. (canceled)14. A method for generating and for fusing ultra-dense hydrogen , in which molecular hydrogen is led into at least one cavity and catalyzed , comprising the following steps:initiating condensation of the molecular hydrogen at a catalyst of the cavity to an ultra-dense hydrogen,initiating fusion of the ultra-dense hydrogen in the at least one cavity, andguiding reaction heat out from the at least one cavity.15. The method according to claim 14 , wherein molecular hydrogen is bound to the ultra-dense hydrogen after the condensing.16. The method according to claim 14 , wherein the fusion is initiated electrically claim 14 , electromagnetically or mechanically.17. The method according to claim 14 , wherein the reaction heat guided out from the at least one cavity is used for further initiation of fusion.18. The method according to claim 14 , wherein the reaction heat guided out from the at least one cavity is converted into mechanical claim 14 , electrical or chemical energy.19. An apparatus for carrying out a method for generating and for fusing ultra-dense hydrogen claim 14 , in which molecular hydrogen is led into at least one cavity and catalyzed claim 14 , comprising the steps of initiating condensation of the molecular hydrogen at a catalyst of the cavity to ...

Hydrocarbon Dehydrocyclization in the Presence of Carbon Dioxide

The invention relates to converting non-aromatic hydrocarbon in the presence of CO 2 to produce aromatic hydrocarbon. CO 2 methanation using molecular hydrogen produced during the aromatization increases aromatic hydrocarbon yield. The invention also relates to equipment and materials useful in such upgrading, to processes for carrying out such upgrading, and to the use of such processes for, e.g., natural gas upgrading.

Cover system for a solid particle lining and reactor comprising such a system

The invention relates to a cover system ( 5 ) for a solid particle lining ( 3 ) comprising an articulated structure ( 11 ) and an annular casing ( 13 ) covering the articulated structure ( 11 ), the casing ( 13 ) being formed by metal plates ( 16, 17 ) sealingly mounted so as to be movable relative to each other, the articulated structure ( 11 ) having metal skirts ( 31 ) forming articulated concentric circles ( 33 ) for supporting the plates ( 16, 17 ) of the casing ( 13 ) and adapting to the deformations of the lining ( 3 ), and metal elements ( 35 ) forming articulated spacers ( 37 ) making it possible to maintain a spacing between the articulated concentric circles ( 33 ) and to adapt to the deformations of the lining ( 3 ).

AXIAL-RADIAL FLOW CATALYTIC CHEMICAL REACTOR WITH TWO LAYERS OF CATALYST

Axial-radial flow reactor comprising a catalytic bed () of a hollow cylindrical shape, having a vertical axis (), a base (), a radial gas inlet section (b), an axial gas inlet section () and a radial gas outlet section (b), wherein the catalytic bed () comprises: a first cylindrical annular region () containing a layer of a first catalyst (A) and a layer of a second catalyst (B), the layer of the first catalyst being above the layer of the second catalyst; a second cylindrical annular region () coaxial to the first annular region and containing only the first catalyst (A). 1. A catalytic reactor adapted to process a gas flow by sequential passage through a first catalyst and a second catalyst ,said reactor comprising a catalytic bed of a hollow cylindrical shape, having a vertical axis, a base, a radial gas inlet section, an axial gas inlet section and a radial gas outlet section, arranged to determine an axial-radial flow through the catalytic bed, the axial inlet section being at an upper end of the catalytic bed;wherein said catalytic bed comprises:a first cylindrical annular portion extending from said base of the catalytic bed to the axial inlet section, and containing only the first catalyst;a second cylindrical annular portion extending from said base of the catalytic bed to the axial inlet section, said second annular portion containing a layer of said first catalyst and a layer of said second catalyst, the layer of the first catalyst being above the layer of the second catalyst, and said first annular portion and second annular portion being arranged coaxially one around the other.2. The reactor according to claim 1 , wherein the first catalyst is intended to catalyse a first chemical reaction and the second catalyst is intended to catalyse a second reaction claim 1 , said first reaction and second reaction being different.3. The reactor according to claim 1 , wherein a boundary between said first annular portion and said second annular portion is a ...

Use of treating elements to facilitate flow in vessels

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.

EFFICIENT OXIDATIVE COUPLING OF METHANE PROCESSES AND SYSTEMS

The present disclosure provides oxidative coupling of methane (OCM) systems for small scale and world scale production of olefins. An OCM system may comprise an OCM subsystem that generates a product stream comprising C compounds and non-C impurities from methane and an oxidizing agent. At least one separations subsystem downstream of, and fluidically coupled to, the OCM subsystem can be used to separate the non-C impurities from the C compounds. A methanation subsystem downstream and fluidically coupled to the OCM subsystem can be used to react Hwith CO and/or COin the non-C impurities to generate methane, which can be recycled to the OCM subsystem. The OCM system can be integrated in a non-OCM system, such as a natural gas liquids system or an existing ethylene cracker. 1. A method for producing hydrocarbon compounds including two or more carbon atoms (C compounds) , the method comprising:{'sub': 2', '2', '2+', '2', '6', '2', '4', '4, '(a) performing an oxidative coupling of methane (OCM) reaction in an OCM reactor to produce an OCM effluent stream comprising carbon monoxide (CO), carbon dioxide (CO), hydrogen (H), one or more C compounds including ethane (CH) and ethylene (CH), and methane (CH);'}(b) directing the OCM effluent stream to a heat recovery steam generator (HRSG) system;(c) with the HRSG system, transferring heat from the OCM effluent stream to a water stream to produce steam;{'sub': 2+', '2', '2', '4, '(d) separating the OCM effluent stream into a first stream comprising at least some of the one or more C compounds and a second stream comprising CO, CO, H, and CH,'}wherein the method has a carbon efficiency of at least about 50%.2. The method of claim 1 , further comprising directing the OCM effluent stream to a cracking unit prior to step (b).3. The method of claim 2 , further comprising directing a stream comprising CHto the cracking unit claim 2 , wherein the stream comprising CHis external to the OCM reactor.4. The method of claim 2 , wherein the ...

Ammonia Oxidation Reactor With Internal Filter Element

A reaction vessel for oxidation of ammonia to nitrogen monoxide in the presence of a catalyst is provided. The catalyst can become dislodged during the oxidation. The reaction vessel includes a reactor body having a top portion, a bottom portion, and a middle portion. The top and middle portions cooperate to define a cavity where the ammonia is catalytically oxidized to provide the nitrogen monoxide. The reaction vessel also includes an internal filter element. The internal filter element includes a filter cage that defines an interior volume and a filter medium disposed adjacent to the filter cage. The internal filter element collects the catalyst dislodged during the oxidation. 1. A reaction vessel for oxidation of ammonia to nitrogen monoxide in the presence of a catalyst which can become dislodged during the oxidation , said reaction vessel comprising: 'wherein said top and middle portions cooperate to define a cavity where the ammonia is catalytically oxidized to provide the nitrogen monoxide;', 'a reactor body having a top portion, a bottom portion, and a middle portion,'}a filter plate extending across said reactor body dividing said bottom portion from said cavity; and wherein said internal filter element comprises a filter cage defining an interior volume and a filter medium disposed adjacent to said filter cage and protruding upwardly from said filter plate into said cavity, and', 'wherein said internal filter element collects said catalyst dislodged during the oxidation., 'an internal filter element provided on said filter plate,'}2. The reaction vessel of wherein said filter medium comprises ceramic.3. The reaction vessel of further comprising a heat removal device positioned in said cavity above said internal filter element.4. The reaction vessel of wherein said filter medium is disposed in said interior volume of said filter cage.5. The reaction vessel of wherein said internal filter element is further defined as a plurality of internal filter elements ...

CATALYTIC COMPOSITE AND IMPROVED PROCESS FOR DEHYDROGENATION OF HYDROCARBONS

A catalytic composite for a cyclic process of adiabatic, non-oxidative dehydrogenation of an alkane into an olefin, comprising a dehydrogenation catalyst, a semimetal and a carrier supporting the catalyst and the semimetal. During the reduction and/or regeneration stages of the adiabatic process, the semimetal releases heat which can be used to initiate the dehydrogenation reactions, which are endothermic in nature, thereby reducing the need for hot air flow and combustion of coke as heat input. The semi-metal is inert towards the dehydrogenation reaction itself, alkane feed and olefin product as well as other side reactions of the cyclic process such as cracking and decoking. 1. A catalytic composite suitable for a cyclic process of adiabatic , non-oxidative dehydrogenation of an alkane into an olefin , comprising:a dehydrogenation catalyst;a semimetal; anda carrier supporting the dehydrogenation catalyst and the semimetal;wherein the semimetal is inert towards the dehydrogenation, and releases heat in situ when exposed to at least one of a reducing stage and an oxidizing stage of the cyclic process.2. The catalytic composite of claim 1 , wherein the semimetal is at least one of boron claim 1 , silicon claim 1 , germanium claim 1 , arsenic claim 1 , antimony claim 1 , tellurium claim 1 , polonium claim 1 , astatine and a combination thereof3. The catalytic composite of claim 1 , wherein the semimetal is antimony.4. The catalytic composite of claim 1 , wherein the semimetal releases more than 700 kJ of heat per mole of the semimetal per reduction and oxidation cycle.5. The catalytic composite of claim 1 , wherein the semimetal is present in the catalytic composite in an amount of from 1 to 50 wt. % based on the total weight of the catalytic composite.6. The catalytic composite of claim 1 , wherein the semimetal has an average particle size of 0.25-0.75 μm.7. The catalytic composite of claim 1 , wherein the semimetal has an average particle size of 20-80 nm.8. The ...

Catalyst System and Use in Heavy Aromatics Conversion Processes

Disclosed are a catalyst system and its use in a process for the conversion of a feedstock containing C 8 + aromatic hydrocarbons to produce light aromatic products, comprising benzene, toluene and xylene. The catalyst system comprises (a) a first catalyst bed comprising a first catalyst composition, said first catalyst composition comprising a zeolite having a constraint index of 3 to 12 combined (i) optionally with at least one first metal of Group 10 of the IUPAC Periodic Table, and (ii) optionally with at least one second metal of Group 11 to 15 of the IUPAC Periodic Table; and (b) a second catalyst bed comprising a second catalyst composition, said second catalyst composition comprising (i) a meso-mordenite zeolite, combined (ii) optionally with at least one first metal of Group 10 of the IUPAC Periodic Table, and (iii) optionally with at least one second metal of Group 11 to 15 of the IUPAC Periodic Table, wherein said meso-mordenite zeolite is synthesized from TEA or MTEA and having a mesopore surface area of greater than 30 m 2 /g and said meso-mordenite zeolite comprises agglomerates composed of primary crystallites, wherein said primary crystallites have an average primary crystal size as measured by TEM of less than 80 nm and an aspect ratio of less than 2.

METHODS, SYSTEMS, AND CATALYSTS FOR THE DIRECT CONVERSION OF SYNGAS TO HIGH-OCTANE HYDROCARBONS

The present disclosure relates to a method that includes converting a gas stream that contains hydrogen (H) and carbon monoxide (CO) to a second mixture that contains a hydrocarbon, for example, a hydrocarbon having between 3 and 15 carbon atoms, where the converting is performed using a first catalyst configured to convert Hand CO to methanol, a second catalyst configured to convert methanol to dimethyl ether (DME), and a third catalyst configured to convert DME to the hydrocarbon. 1. A method comprising:{'sub': '2', 'converting a gas stream comprising hydrogen (H) and carbon monoxide (CO) to a second mixture comprising a hydrocarbon having between 3 and 15 carbon atoms, wherein{'sub': '2', 'the converting is performed using a first catalyst configured to convert Hand CO to methanol,'}a second catalyst configured to convert methanol to dimethyl ether (DME), anda third catalyst configured to convert DME to the hydrocarbon.2. The method of claim 1 , wherein the first catalyst comprises copper and a zinc oxide.3. The method of claim 2 , wherein the first catalyst further comprises at least one of silica claim 2 , alumina claim 2 , zirconia claim 2 , or ceria.4. The method of claim 1 , wherein the second catalyst comprises at least one of an alumina or silica.5. The method of claim 1 , wherein the third catalyst comprises at least one of copper or a zeolite.6. The method of claim 5 , wherein the zeolite comprises a beta zeolite having a silica to alumina ratio between about 20:1 and about 300:1.7. The method of claim 6 , wherein the copper in the third catalyst is present at a concentration between about 1 wt % and about 20 wt % claim 6 , relative to the total weight of the third catalyst.8. The method of claim 1 , wherein the first catalyst and the second catalyst are present at a ratio between about 1:1 and about 8:1.9. The method of claim 8 , wherein the second catalyst and the third catalyst are present at a ratio between about 0.1:1 and about 5:2.10. The method of ...

OXYGEN STRIPPING IN ETHERIFICATION, ETHERS DECOMPOSITION AND ISOOCTENE PRODUCTION

A process for supplying deaerated water to a chemical plant that includes a distillation column for separating a reaction effluent comprising water and a product. The process includes inventorying the distillation column with aerated water (water having an oxygen content of greater than 50 ppbw, such as greater than 1 ppmw). The aerated water in the distillation column may then be distilled to produce an oxygen-containing overheads and a bottoms fraction comprising deaerated water. The deaerated water in the bottoms fraction ma be transported to an upstream or a downstream unit operation, and utilizing the deaerated water in the upstream or downstream unit operation. The reaction effluent is fed to the distillation column, transitioning the distillation column from separating oxygen from water to operations for separating the product from the water. 1. A process for supplying deaerated water to a chemical plant , wherein the chemical plant includes a distillation column for separating a reaction effluent comprising water and a product , the process comprising:inventorying the distillation column with aerated water having an oxygen content of greater than 50 ppbw;distilling the aerated water in the distillation column to produce an oxygen-containing overheads and a bottoms fraction comprising deaerated water;transporting the deaerated water in the bottoms fraction to an upstream or a downstream unit operation;utilizing the deaerated water in the upstream or downstream unit operation; andfeeding the reaction effluent to the distillation column, transitioning the distillation column from separating oxygen from water to operations for separating the product from the water.2. The process of claim 1 , wherein the deaerated water comprises less than 15 ppbw oxygen.3. The process of claim 1 , wherein the deaerated water comprises from less than 1 ppbw to no more than 10 ppbw oxygen.4. The process of claim 1 , wherein the distillation column comprises an overheads ...

SMALL CHANNEL SHORT FIXED BED ADIABATIC REACTOR FOR OXIDATIVE COUPLING OF METHANE

Disclosed herein are systems and processes for the conversion of a methane feedstock to C hydrocarbons. 1. A reactor system for an oxidative conversion of methane comprising:a reactor vessel having a reactant inlet and a product outlet;a pre-heating component disposed within the reactor vessel configured to receive feedstock from the reactant inlet; andone or more reactor bodies configured to receive the feedstock from the reactant inlet via the pre-heating component, each reactor body having a plurality of channels extending there through, wherein the channels are configured to receive a catalyst.2. The reactor system of :{'sup': th', 'th, 'wherein the channels have a diameter, and wherein the catalyst has a particle size of from about ¼to about 1/20the size of the diameter of a channel, and'}wherein the reactor system further comprises one or more walls disposed adjacent one or more of the first surface and the second surface, wherein the walls are configured to maintain the catalyst within the channels.3. The reactor system of claim 1 , wherein the pre-heating component comprises a silicon carbide claim 1 , quartz claim 1 , a metal coated with inert materials claim 1 , or a combination thereof.4. The reactor system of claim 1 , wherein the plurality of channels extend in parallel and are conterminous.5. The reactor system of claim 1 , wherein the reactor bodies have a cylindrical shape and have a diameter of about 20 mm or greater.6. The reactor system of claim 1 , wherein at least one channel of the plurality of channels has a length no greater than 300 mm.7. The reactor system of claim 1 , at least one channel of the plurality of channels has a diameter of less than about 10 mm.8. The reactor system of claim 1 , at least one channel of the plurality of channels has a diameter of about 5 mm.9. The reactor system of claim 1 , wherein the reactor body comprises an inert material having a thermal conductivity of at least about 2 Watts per meter Kelvin.10. The ...

Reactors and systems for oxidative coupling of methane

In an aspect, the present disclosure provides a method for the oxidative coupling of methane to generate hydrocarbon compounds containing at least two carbon atoms (C 2+ compounds). The method can include mixing a first gas stream comprising methane with a second gas stream comprising oxygen to form a third gas stream comprising methane and oxygen and performing an oxidative coupling of methane (OCM) reaction using the third gas stream to produce a product stream comprising one or more C 2+ compounds.

Heavy Aromatics Conversion Processes and Catalyst Compositions Used Therein

Disclosed are processes for conversion of a feedstock comprising C aromatic hydrocarbons to lighter aromatic products in which the feedstock and optionally hydrogen are contacted in the presence of a first and a second catalyst composition under conversion conditions effective to produce said lighter aromatic products comprising benzene, toluene and xylene. In the process, the C aromatic hydrocarbons are dealkylated to form C-Caromatic hydrocarbon and the C olefins formed are saturated. The remaining C aromatic hydrocarbons are transalkylated with the C-Caromatic hydrocarbon. The first and second catalyst compositions each comprise a zeolite, a first metal, and optionally a second metal, and are treated with a source of sulfur and/or a source of steam. 125.-. (canceled)27. The process of claim 26 , wherein said first catalyst composition and/or said second catalyst composition is treated with said source of sulfur in one or more stages at temperatures in the range 204° C. (400° F.) up to about 480° C. (900° F.).28. The process of claim 26 , wherein said source of sulfur is one or more of hydrogen sulfide claim 26 , carbon disulfide and alkylsulfides which are selected from the group consisting of methylsulfide claim 26 , dimethylsulfide claim 26 , dimethyldisulfide claim 26 , diethylsulfide claim 26 , dibutyl sulfide claim 26 , and mixtures of two or more thereof.29. The process of claim 26 , wherein said first zeolite and/or said second zeolite are treated with a source of steam.30. The process of claim 26 , wherein said source of steam comprises up to about 100% steam at temperatures in the range of about 260° C. (500° F.) to about 649° C. (1200° F.) and said treatment is in one or more temperature stages.31. The process of claim 26 , wherein said first metal of Group 6 is selected from the group consisting of chromium claim 26 , molybdenum claim 26 , tungsten and mixtures of two or more thereof.32. The process of claim 26 , wherein said second metal of Group 9 is ...

Cooled reactor for the production of dimethyl ether from methanol

A cooled reactor for the production of dimethyl ether by catalytic dehydration of methanol in the gas phase, the reactor having an adiabatic catalyst bed as starting zone, a moderator zone cooled by direct or indirect heat exchange, and optionally an adiabatic catalyst bed as conditioning zone. The conversion of methanol to dimethyl ether is increased and the formation of undesired by-products is decreased.

Boroaluminosilicate Molecular Sieves and Methods for Using Same for Xylene Isomerization

Boroaluminosilicate molecular sieve catalysts are provided and are useful for hydrocarbon conversion reactions including isomerization of xylenes in C8 aromatics feedstocks to produce p-xylene. Advantageously, it has been found that the boroaluminosilicate molecular sieve catalysts of the invention are more selective than conventional commercial xylene isomerization catalysts, resulting in reduced formation of transmethylation byproducts (C7 and C9 aromatics) while simultaneously providing a high degree of xylene isomerization. 1. A boroaluminosilicate molecular sieve having an average crystallite size less than 2 μm.2. The boroaluminosilicatc molecular sieve of claim 1 , wherein the average crystallite size is between 50 nm to 1 μm.3. The boroaluminosilicate molecular sieve of claim 1 , wherein the alkali metal content is less than 400 ppmw.4. The boroaluminosilicate molecular sieve of claim 1 , wherein the alkali metal content is less than 150 ppmw.5. A method of increasing the proportion of p-xylene (pX) in a hydrocarbon-containing feed stream comprising xylene isomers claim 1 , said method comprising:{'claim-ref': {'@idref': 'CLM-00001', 'claim 1'}, 'contacting the hydrocarbon-containing feed stream with an isomerization catalyst of and under conditions suitable to yield a stream enriched in p-xylene with respect to the hydrocarbon-containing feed stream.'}6. A method of increasing the proportion of p-xylene (pX) in a hydrocarbon-containing feed stream comprising xylene isomers claim 1 , said method comprising:contacting the hydrocarbon-containing feed stream with an isomerization catalyst under conditions suitable to yield a stream enriched in p-xylene with respect to the hydrocarbon-containing feed stream, whereinthe isomerization catalyst comprises a boroaluminosilicate molecular sieve prepared using an amine base.7. The method of claim 6 , wherein the boroaluminosilicate molecular sieve is prepared using ethylenediamine.8. The method of claim 6 , wherein the ...

METHODS FOR SELECTING A LOADING PRESSURE DROP TOLERANCE SPECIFICATION FOR A MULTITUBULAR FIXED-BED REACTOR

A method for a selecting a loading pressure drop tolerance specification for a plurality of tubes in a multitubular fixed-bed reactor, wherein the plurality of tubes comprise a packed bed of epoxidation catalyst, the method comprising: defining a first loading pressure drop tolerance range for the plurality of tubes based on a desired maximum variation in outlet oxygen concentration, relative to the mean, for the plurality of tubes; defining a second loading pressure drop tolerance range for the plurality of tubes based on a desired maximum number of tube corrections for the plurality of tubes; and selecting the loading pressure drop tolerance specification for the plurality of tubes such that the entirety of the loading pressure drop tolerance specification falls within the first loading pressure drop tolerance range and the second loading pressure drop tolerance range. 1. A method for a selecting a loading pressure drop tolerance specification for a plurality of tubes in a multitubular fixed-bed reactor , wherein the plurality of tubes comprise a packed bed of epoxidation catalyst , the method comprising:defining a first loading pressure drop tolerance range for the plurality of tubes based on a desired maximum variation in outlet oxygen concentration, relative to the mean, for the plurality of tubes;defining a second loading pressure drop tolerance range for the plurality of tubes based on a desired maximum number of tube corrections for the plurality of tubes; andselecting the loading pressure drop tolerance specification for the plurality of tubes such that the entirety of the loading pressure drop tolerance specification falls within the first loading pressure drop tolerance range and the second loading pressure drop tolerance range.2. The method of wherein the desired maximum variation in the outlet oxygen concentration is no more than ±0.4 mol %.3. The method of wherein the desired maximum variation in the outlet oxygen concentration is no more than ±0.2 mol ...

DEVICES AND METHODS FOR HYDROGEN GENERATION VIA AMMONIA DECOMPOSITION

Systems and methods for hydrogen generation via ammonia decomposition that utilize a fixed bed reactor configured to receive inflows of NHand oxidant and to produce an outflow of high purity H. The fixed bed reactor contains a fixed bed of a NHdecomposition catalyst wherewith the NHdecomposes to form Nand H; a plurality of ceramic hollows fibers with a high surface to volume ratio disposed in the fixed bed, the hollow fibers having an Hselective membrane disposed thereon for extracting Hfrom Nand to form a permeate of the high purity Hand a retentate of primarily N; and a catalytic Hburner also disposed in the fixed bed, the catalytic Hburner for burning a portion of the Hwith the oxidant to provide thermal energy for the NHdecomposition. 1. A method for generating hydrogen via ammonia decomposition , the method comprising:introducing ammonia into a system comprising: [{'sub': 3', '3', '2', '2, 'a fixed bed of a NHdecomposition catalyst for NHdecomposition to form Nand H;'}, {'sub': 2', '2', '2', '2', '2, 'a plurality of ceramic hollows fibers with a high surface to volume ratio disposed in the fixed bed, the hollow fibers having an Hselective membrane disposed thereon for extracting Hfrom Nand to form a permeate comprising high purity Hand a retentate comprising primarily N; and'}, {'sub': 2', '2', '2', '3, 'a catalytic Hburner also disposed in the fixed bed, the catalytic Hburner for burning a portion of the Hto provide thermal energy for the NHdecomposition;'}], 'a fixed bed membrane reactor containing;'}{'sub': 3', '2', '2, 'decomposing at least a portion of the ammonia via the fixed bed of the NHdecomposition catalyst and thermal energy produced by the catalytic Hburner to form ammonia decomposition products including H; and'}{'sub': '2', 'separating at least a portion of the Hfrom the decomposition products.'}2. The method of wherein the ammonia introduced into the system comprises NHvapor at 10-15 bar.3. The method of wherein the separating at least a portion ...

PROCESS FOR CONVERTING LPG TO HIGHER HYDROCARBON(S)

The present invention relates to a process for converting a feed comprising C2-C4 alkanes to higher hydrocarbon(s) including aromatic hydrocarbon(s) in n reaction zones operated in series, wherein m reaction zones are not participating in the conversion process and only (n-m) reaction zones are operated under reaction conditions sufficient to convert at least a portion of said a feed comprising C2-C4 alkanes to an effluent having said higher hydrocarbon(s). An object of the present invention is to provide a process for converting LPG to higher hydrocarbon(s) including aromatic hydrocarbon(s) wherein a high reactant, i.e. ethane, propane and/or butane, conversion can be achieved. 1. A process for converting LPG to higher hydrocarbon(s) including aromatic hydrocarbon(s) in n reaction zones operated in series , wherein m reaction zones are not participating in the conversion process and only (n-m) reaction zones are operated under reaction conditions sufficient to convert at least a portion of said LPG to an effluent having said higher hydrocarbon(s) , wherein each reaction zone is initially numbered serially with a designator from 1 to n , the process comprising:(a) providing a quantity of catalytic material within each reaction zone;(b) providing to the reaction zone designated as 1 a hydrocarbon feedstock containing LPG;(c) heating at least a portion of the effluent of the said reaction zone designated as 1 to the inlet temperature of the reaction zone designated as 2, and more generally, heating at least a portion of the effluent of each reaction zone with a designator equal or smaller than (n-m−1) to the inlet temperature of the reaction zone with a designator larger by one than that of the reaction zone from which said effluent originates;(d) transferring said at least portion of said effluent of the said reaction zone designated as 1 to said reaction zone designated as 2, and more generally, transferring said at least portion of said reaction zone with a ...

REACTORS AND METHODS FOR PRODUCING SOLID CARBON MATERIALS

A reactor for producing a solid carbon material comprising at least one reaction chamber configured to produce a solid carbon material and water vapor through a reduction reaction between at least one carbon oxide and at least one gaseous reducing material in the presence of at least one catalyst material. Additional reactors, and related methods of producing a solid carbon material, and of forming a reactor for producing a solid carbon material are also described. 1. A reactor for producing a solid carbon material , comprising:at least one reaction chamber configured to produce a solid carbon material and water vapor through a reduction reaction between at least one carbon oxide and at least one gaseous reducing material in the presence of at least one catalyst material structure comprising a catalyst material at least partially extending through the at least one reaction chamber;at least one cooling chamber operatively communicating with the at least one reaction chamber and configured to condense the water vapor produced in the at least one reaction chamber; andat least one conveying mechanism configured to transport the at least one catalyst material structure through the at least one reaction chamber.2. The reactor of claim 1 , wherein the at least one reaction chamber is configured to produce the solid carbon material through at least one of a Bosch reaction claim 1 , a Boudouard reaction claim 1 , and a methane reduction reaction.3. The reactor of claim 1 , wherein the at least one reaction chamber is configured to withstand an operating temperature greater than or equal to about 450° C.4. (canceled)5. The reactor of claim 1 , wherein the at least one cooling chamber is configured to have an operating temperature of less than or equal to about 50° C.6. The reactor of claim 1 , further comprising a heat exchange zone operatively associated with each of at least one effluent gas line and at least one return gas line extending between the at least one reaction ...

Process for the ammonia production

Process and plant for the synthesis of ammonia from a hydrocarbon feedstock, comprising: primary reforming with steam and air-fired secondary reforming wherein primary reforming is performed at a temperature and pressure of at least 790° C. and 50 bar, and secondary reforming is carried out substantially in absence of excess air, the so obtained make-up synthesis gas having a H 2 to N 2 molar ratio in the range 2.5 to 3.

Process And Reactor Comprising A Plurality Of Catalyst Receptacles

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.

PROCESSES FOR PRODUCING OLEFINS FROM PARAFFINS

Processes for catalytic dehydrogenation of paraffin stream is disclosed. The process includes passing a first portion of the paraffin-containing feedstream through a select catalytic reactor in a plurality of catalytic reactors. An internal differential pressure is measured in the select catalytic reactor. A second portion of the paraffin-containing feed stream is bypassed around the select catalytic reactor when the measured internal differential pressure is above a predetermined limit of the internal differential pressure. The bypassed second portion is passed to at least one other catalytic reactor in the plurality of reactors located downstream of the select catalytic reactor being bypassed. 118.-. (canceled)19. A process for dehydrogenation of a hydrocarbon-containing feed stream comprising:a) passing a first portion of the hydrocarbon-containing feedstream through at a first catalytic dehydrogenation reactor to provide a first effluent stream, the hydrocarbon-containing feedstream comprising propane, butane, or a combination thereof;b) measuring a first internal differential pressure across an inner screen or an outer screen in the first catalytic dehydrogenation reactor and bypassing a second portion of the hydrocarbon-containing feed stream around the first catalytic dehydrogenation reactor when the first internal differential pressure is above a first predetermined limit;c) passing a first portion of first effluent stream and at least a portion of the bypassed second portion of the hydrocarbon-containing feed stream to a second catalytic dehydrogenation reactor to provide a second effluent stream;d) measuring a second internal differential pressure across an inner screen or an outer screen in the second catalytic dehydrogenation reactor and bypassing a second portion of first effluent stream around the second catalytic dehydrogenation reactor when the second internal differential pressure is above a second predetermined limit;e) passing a first portion of ...

USE OF TREATING ELEMENTS TO FACILITATE FLOW IN VESSELS

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. 1passing the one or more streams through an upstream processing zone and a downstream processing zone within the process vessel, the upstream processing zone and downstream processing zone each containing one or more beds of processing materials;passing the one or more streams through a redistribution treating zone located between the upstream processing zone and downstream processing zone, wherein the redistribution treating zone comprises a single layer of a fixed, form-fit fibrous mesh material conforming to the interior dimensions of the process vessel; andlaterally dispersing the one or streams with the fibrous mesh material to provide improved contact between the one or more streams and the processing materials in the downstream processing zone.. A method of improving flow distribution of one or more streams in a process vessel comprising: This application is a continuation application and claims the benefit, and priority benefit, of U.S. patent application Ser. No. 15/720,751, filed Sep. 29, 2017, which is a continuation and claims the benefit, and priority benefit, of U.S. patent application Ser. No. 15/676,603, filed Aug. 14, 2017, which claims the benefit and priority benefit of U.S. patent application Ser. No. 15/265,405, filed Sep. 14, 2016, which claims the benefit and priority benefit of U.S. Provisional Patent Application Ser. No. 62/314,069, filed Mar. ...

Conversion of Metal Carbonate to Metal Chloride

A process for preparing metal chloride Mx+Clx−, in which metal carbonate in solid form is reacted with a chlorinating agent selected from chlorine and oxalyl chloride to give metal chloride Mx+Clx−, where the metal M is selected from the group of the alkali metals, alkaline earth metals, Al and Zn, Li and Mg, or Li, and x corresponds to the valency of the metal cation, and wherein metal M is additionally added as a reactant to the metal carbonate/chlorinating agent reaction. 1. A method for producing metal chloride MCl , comprising:providing a chlorinating agent,{'sup': x+', '−, 'sub': 'x', 'reacting metal carbonate as a solid with the chlorinating agent to form metal chloride MCl,'}wherein metal M being selected from the group of metals consisting of the alkali metals, alkaline earth metals, Al and Zn, Li and Mg, and Li, andwherein x corresponds to the valence of the metal cation, andadditionally adding metal M as a reactant to the reaction of metal carbonate with the chlorinating agent.2. The method of claim 1 , wherein the metal M added as a reactant with a metal/metal carbonate weight ratio of less than 5/10 in order to generate thermal energy.3. The method of claim 2 , wherein the metal M is used together with the metal carbonate for the reaction with the chlorinating agent.4. The method of claim 1 , wherein the chlorinating agent comprises chlorine or oxalyl chloride.5. The method of claim 1 , wherein the metal chloride is subsequently reacted to produce metal M.6. The method of claim 5 , wherein the metal M produced by the subsequent reaction of the metal chloride is reacted at least partly with carbon dioxide to produce metal carbonate claim 5 , to form a metal circuit.7. The method of claim 1 , wherein the reaction occurs in a grid reactor or a mechanically moved fixed-bed reactor or in a cyclone reactor.8. The method of claim 7 , wherein the reaction occurs in a grid reactor claim 7 , in which the chlorinating agent is added as a gas in cocurrent with the ...

Manufacture of Methylolalkanes with Augmented Heat Transfer and Improved Temperature Control

A multistage tubular reaction system and method for preparing methylol derivatives of an aldehyde includes a tubular reaction system with a plurality of successive reactor stages comprising a plurality of jacketed reaction tubes provided with a cooling system adapted to control flow of a cooling medium through said jacketed reaction tubes. The cooling medium flow is controlled independently in different stages in response to temperature measurements in the reaction system to regulate temperature. In order to further reduce temperature spikes and byproduct generation, aldehyde is stepwise added to the production stream at a plurality of feed ports proximate to reaction tubes equipped with tube inserts to enhance mixing and heat transfer. 2. The method according to claim 1 , wherein the production stream is fed to a plurality of tubular reaction sections provided with tube inserts following addition of the Cor higher condensable aldehyde and/or base.3. The method according to claim 2 , wherein said tube inserts are displacement flow inserts.4. The method according to claim 3 , wherein said tube inserts are wire-wrapped tube inserts.6. The method according to claim 1 , wherein there is provided a cooling control system adapted to control temperature and flow of a cooling medium claim 1 , and the flow of the cooling medium is independently controlled in different stages of the reaction system in response to temperature measurements in respective stages.7. The method according to claim 6 , wherein said tubular reaction system with a plurality of reaction stages includes tubular reaction sections jacketed with a cooling medium.8. The method according to claim 1 , wherein the methylolalkane is trimethylolpropane and the aldehyde which is condensable with formaldehyde is n-butyraldehyde.9. The method according to claim 1 , wherein the methylolalkane is neopentyl glycol and the aldehyde which is condensable with formaldehyde is isobutyraldehyde.10. The method according to ...

Process for Conversion of Dimethyl Sulfide to Methyl Mercaptan

Disclosed herein are systems and processes involving the catalyzed cleavage reaction of dimethyl sulfide to methyl mercaptan. The catalyzed cleavage reaction can be a standalone system or process, or can be integrated with a methyl mercaptan production plant. 1. A process for conversion of dimethyl sulfide to methyl mercaptan , comprising:contacting dimethyl sulfide in a combined feed stream with a catalyst in the presence of an excess amount of hydrogen sulfide in a reactor to yield a reactor effluent comprising methyl mercaptan, hydrogen sulfide, and carbon disulfide, wherein the catalyst comprises alumina, NiMo on an alumina support, CoMo on an alumina support, or a combination thereof:wherein the step of contacting has, in the reactor effluent, a conversion of dimethyl sulfide of greater than 50% and a selectivity to methyl mercaptan of greater than 95%.2. The process of claim 1 , wherein carbon disulfide is present in the reactor effluent in an amount of less than about 2 mole % based on a total moles of methyl mercaptan claim 1 , hydrogen sulfide claim 1 , dimethyl disulfide claim 1 , and carbon disulfide in the reactor effluent.3. (canceled)4. The process of claim 1 , further comprising:{'sub': '2', 'separating the reactor effluent into a recycle HS stream and a methyl mercaptan stream; and'}{'sub': '2', 'recycling the recycle HS stream for use in the step of contacting.'}5. The process of claim 1 , wherein the step of contacting is performed at a hydrogen sulfide to dimethyl sulfide mole ratio of at least 3:1 and less than 100:1.6. The process of claim 1 , wherein the step of contacting is performed at a weight average temperature in a range of from about 265° C. to about 305° C.7. The process of claim 1 , wherein the step of contacting is performed at a weight hourly space velocity of about 0.2 to about 15 g dimethyl sulfide/g cat./hr.8. The process of claim 1 , wherein the step of contacting is performed at a hydrogen sulfide to dimethyl sulfide mole ratio ...

APPARATUS AND METHOD FOR CRACKING GASES

An apparatus for cracking gases with a supply line () for a carbon-containing gas, by means of which the gas is capable of being supplied to a first heat exchanger () with a fill of a thermal storage mass, a first combustion chamber () which is arranged downstream in the direction of flow of the gas and which, in particular, has a supply device capable of being regulated for another oxygen-containing gas, by means of which a partial oxidation of the carbon-containing gas is carried out by the hypostoichiometric supply of oxygen, and a reactor () which is arranged downstream of the first combustion chamber () in the direction of flow of the gas which has a fill of a catalytically acting material for the catalytic splitting of impurities of the carbon-containing gas. According to the invention a second combustion chamber () with a supply device—in particular capable of being regulated—for an oxygen-containing gas, by means of which a partial oxidation of the catalytically prepared carbon-containing gas is carried out by the hypostoichiometric supply of oxygen, is arranged downstream of the reactor () in the direction of flow of the carbon-containing gas, and a second heat exchanger () with a fill of a thermal storage mass is arranged downstream of this combustion chamber in the direction of flow of the gas, wherein the direction of flow of the carbon-containing gas is capable of being reversed at least in a region which encloses the first and second heat exchanger (), the first and second combustion chamber () and the reactor (). 1. An apparatus for cracking gases with a supply line for a carbon-containing gas , by means of which the gas is capable of being supplied to a first heat exchanger with a fill of a thermal storage mass , a first combustion chamber which is arranged downstream in the direction of flow of the gas and which , in particular , has a supply device capable of being regulated for another oxygen-containing gas , by means of which a partial oxidation ...

Method and Catalyst System for the Production of Para-Xylene

A catalyst system is disclosed for producing para-xylene from a Chydrocarbon mixture comprising ethylbenzene and at least one xylene isomer other than para-xylene. The catalyst system comprises a first catalyst bed and a second catalyst bed. The first catalyst bed comprises a first zeolite and a rhenium hydrogenation component. The first zeolite has a constraint index from 1 to 12, an average crystal size from 0.1 to 1 micron and has been selectivated to have an ortho-xylene sorption time of greater than 1200 minutes based on its capacity to sorb 30% of the equilibrium capacity of ortho-xylene at 120° C. and an ortho-xylene partial pressure of 4.5±0.8 mm of mercury. The second catalyst bed comprises a second zeolite and a rhenium hydrogenation component. The second zeolite has a constraint index ranging from 1 to 12 and an average crystal size of less than 0.1 micron. 1. A catalyst system for producing para-xylene from a Chydrocarbon mixture comprising ethylbenzene and at least one xylene isomer other than para-xylene , the catalyst system comprising a first catalyst bed (1) and a second catalyst bed (2) , wherein:the first catalyst bed (1) comprises a first catalyst comprising a first zeolite and a hydrogenation component comprising rhenium, wherein the first zeolite has a constraint index ranging from 1 to 12 and an average crystal size from 0.1 to 1 micron, and wherein the first zeolite has been selectivated so as to have an ortho-xylene sorption time of greater than 1200 minutes based on its capacity to sorb 30% of the equilibrium capacity of ortho-xylene at 120° C. and an ortho-xylene partial pressure of 4.5±0.8 mm of mercury; andthe second catalyst bed (2) comprises a second catalyst comprising a second zeolite and a hydrogenation component comprising rhenium, wherein the second zeolite has a constraint index ranging from 1 to 12 and an average crystal size of less than 0.1 micron, and wherein the second zeolite has an ortho-xylene sorption time of less than ...

Steam-Less Process for Converting Butenes to 1,3-Butadiene

Processes, systems, and catalysts for the conversion of 2-butene to 1,3-butaidene without the use of steam or, in some embodiments, with a reduced use of steam as compared to prior art processes are provided. The catalyst includes tungsten trioxide (WO) on an inorganic support includes activated magnesium oxide (MgO) and may be referred to as a “dual catalyst” or a “co-catalyst.” Embodiments of the catalyst. A process for the production of 1,3-butadiene may include contacting a feed stream of 2-butene with a WO-inorganic support catalyst or a MgO and WO-inorganic support catalyst and may be performed without steam in the feed stream. 1. A method for producing 1 ,3-butadiene , comprising:receiving a feed stream comprising 2-butene;contacting the feed stream with a catalyst in the presence of an oxidant to convert the 2-butene to 1-3-butadiene, the catalyst comprising tungsten oxide impregnated on an inorganic support.2. The method of claim 1 , wherein the feed stream does not include steam.3. The method of claim 1 , wherein the oxidant comprises air.4. The method of claim 1 , wherein the contacting is performed at a temperature in the range of 400° C. to 550° C.5. The method of claim 1 , wherein the feed stream comprises 1-butene.6. The method of claim 1 , wherein the inorganic support comprises silica.7. The method of claim 1 , wherein the catalyst comprises magnesium oxide.8. The method of claim 7 , wherein the magnesium oxide has a surface area in the range of 30 meters-squared/gram (m/g) to 200 m/g.9. The method of claim 7 , wherein the catalyst comprises a first layer of the tungsten oxide impregnated on the inorganic support claim 7 , a second layer of the tungsten oxide impregnated on the inorganic support claim 7 , and a layer of the magnesium oxide positioned between the first layer and the second layer.10. The method of claim 7 , wherein the catalyst comprises a layer of the magnesium oxide disposed on a layer of the tungsten oxide impregnated on the ...

OLEFIN CONVERSION PROCESS

Processes for the production of olefins are disclosed, which may include: contacting a hydrocarbon mixture comprising linear butenes with an isomerization catalyst to form an isomerization product comprising 2-butenes and 1-butenes; contacting the isomerization product with a first metathesis catalyst to form a first metathesis product comprising 2-pentene and propylene, as well as any unreacted Colefins, and byproducts ethylene and 3-hexene; and fractionating the first metathesis product to form a C3-fraction and a C5 fraction comprising 2-pentene. The 2-pentene may then be advantageously used to produce high purity 1-butene, 3-hexene, 1-hexene, propylene, or other desired products. 1. A system for the production of olefins , the system comprising: contacting a hydrocarbon mixture comprising linear butenes with an isomerization catalyst to form an isomerization product comprising 2-butenes and 1-butenes; and', {'sub': '4', 'contacting the isomerization product with a first metathesis catalyst to form a first metathesis product comprising 2-pentene and propylene, as well as any unreacted Colefins, and byproducts ethylene and 3-hexene;'}], 'an isomerization/metathesis reaction system fora fractionation system for fractionating the first metathesis product to form a C3-fraction and a C5 fraction comprising 2-pentene as essentially the only C5 olefin; anda flow conduit for feeding at least a portion of the C3-fraction to the isomerization/metathesis reaction system.2. The system of claim 1 , wherein the flow conduit for recycling the C3-fraction is configured to introduce the C3-fraction upstream of the isomerization catalyst claim 1 , upstream of the metathesis catalyst claim 1 , or both.3. The system of claim 1 , further comprising a metathesis reactor for contacting ethylene and the C5 fraction with a second metathesis catalyst claim 1 , which may be the same or different than the first metathesis catalyst claim 1 , to convert at least a portion of the 2-pentene and ...

MIXING DEVICE FOR A DOWN-FLOW HYDROPROCESSING REACTOR

An improved vortex-type mixing device for a down-flow hydroprocessing reactor is described. The device provides improved overall mixing efficiency of an existing mixing volume in the mixing of gas and liquid phases in two-phase systems while reducing the pressure drop through the device, as compared with prior art devices. Typical hydroprocessing applications include hydrotreating, hydrofinishing, hydrocracking and hydrodewaxing. 1. A mixing device for a multi-bed down-flow catalytic reactor , the mixing device comprising:a. a top plate having an inner surface and a periphery;b. a base plate extending parallel to the top plate, the base plate having an inner surface, a periphery, and a base plate aperture, wherein the top and base plates are separated by a distance to define an interior region of the mixing device;c. a plurality of inwardly-directed vanes contained within the interior region of the mixing device extending perpendicular to and interposed between the inner surfaces of the top and base plates, wherein the vanes are inwardly-directed from the periphery of the top and base plates toward the base plate aperture and are spaced around the area extending from the base plate aperture to the periphery of the top and base plates; andd. a mixing region;wherein, the mixing device does not include a weir ring extending from the inner surface of the base plate or a bubble cap extending from the inner surface of the top plate.2. The mixing device of claim 1 , wherein the base plate aperture is circular.3. The mixing device of claim 1 , wherein the vanes are straight or curved.4. The mixing device of claim 3 , wherein the vanes are inwardly-curved.5. The mixing device of claim 1 , wherein each vane comprises an outer end proximal to the periphery of the top plate and an interior end proximal to the mixing region claim 1 , the mixing device further comprising a plurality of inlet regions defined as an area bound by neighboring vanes and the corresponding interior end ...

ETHYLENE-TO-LIQUIDS SYSTEMS AND METHODS

Integrated systems are provided for the production of higher hydrocarbon compositions, for example liquid hydrocarbon compositions, from methane using an oxidative coupling of methane system to convert methane to ethylene, followed by conversion of ethylene to selectable higher hydrocarbon products. Integrated systems and processes are provided that process methane through to these higher hydrocarbon products. 1. A system , comprising:{'sub': 2', '4', '2', '4', '3', '6', '2', '2', '4, 'an ethylene-to-liquids (ETL) reactor that (i) receives an olefin feed stream at a first temperature, said olefin feed stream comprising (1) ethylene (CH) at a concentration of at least about 0.5 mole percent (mol %), (2) CHand propylene (CH) at a combined concentration of at most about 10 mol %, and (3) carbon monoxide (CO) or carbon dioxide (CO), and (ii) as part of an ETL process, facilitates conversion of CHto higher hydrocarbon products with the aid of an ETL catalyst to yield a product stream comprising said higher hydrocarbon products that is at a second temperature which is higher than said first temperature, wherein said ETL process liberates heat, wherein said higher hydrocarbon products comprise an olefin compound and an aromatic compound; and'}a separations module in fluid communication with said ETL reactor that recovers from said product stream a liquid stream comprising said higher hydrocarbon products, wherein said higher hydrocarbon products include (i) at least 5 compounds having 5 different carbon numbers, said 5 different carbon numbers selected from 4 through 20, wherein each of said at least 5 compounds is at a concentration of at least 5 weight percent (wt %) of said liquid stream, and (ii) a paraffin compound, an isoparaffin compound, and a naphthene compound,wherein at least about 80% of said heat liberated in said ETL process provides a difference between said first temperature and said second temperature of between about 50° C. and about 150° C.2. The system ...

Catalytic Alkane Conversion and Olefin Separation

Disclosed is a hydrocarbon conversion process that is less energy intensive than comparable processes. The hydrocarbon conversion process is particularly desirable for converting alkanes, such as methane into C 2+ olefins, such as ethylene and propylene, particularly with increasing selectivity to ethylene production. It is also desirable for effectively removing a C 2 composition (i.e., ethane, ethylene and/or acetylene) produced from the catalytic conversion of hydrocarbon comprised of C 2+ olefins. In addition, the hydrocarbon process is desirable for providing a substantially non-cryogenic separation of the desired C 2 compositions from the hydrocarbons (e.g., methane) present in the reaction mixture.

Systems for selective naphtha reforming

Systems for reforming a hydrocarbon feedstock, where the system is operable to selectively reform different sub-components of the hydrocarbon feedstock using at least two structurally-distinct reforming catalysts. Advantages may include a decreased rate of reforming catalyst deactivation and an increased yield of a liquid hydrocarbon reformate product that is characterized by at least one of an increased octane rating and a decreased vapor pressure compared to the liquid hydrocarbon reformate product of conventional one-step reforming systems.

SYSTEMS AND METHODS FOR PARTIAL OR COMPLETE OXIDATION OF FUELS

A system used for converting multiple fuel feedstocks may include three reactors. The reactor system combination can be so chosen that one of the reactors completely or partially converts the fuel while the other generates the gaseous product required by utilizing the gaseous product from the second reactor. The metal-oxide composition and the reactor flow-patterns can be manipulated to provide the desired product. A method for optimizing the system efficiency where a pressurized gaseous fuel or a pressurized utility is used for applications downstream can be used to any system processing fuels and metal-oxide. 1. A system for the production of syngas , comprising:a first reactor comprising a plurality of oxygen carrying particles comprising a first metal oxide, wherein the first reactor is configured to provide a counter-current contact mode between the first metal oxide and a first fuel to reduce the first metal oxide to a second metal oxide;{'sub': 2', '2', '2', '2', '2, 'a second reactor in communication with the first reactor, the second reactor configured to oxidize the second metal oxide to a third metal oxide, and further configured to reduce the third metal oxide to a fourth metal oxide with a second fuel to provide a partially or fully oxidized gaseous fuel comprising one or more of CO, CO, H, and HO, wherein the second metal oxide is oxidized to the third metal oxide using an enhancing gas of COand HO, the partially or fully oxidized gaseous fuel, or a combination thereof, to generate syngas; and'}a third reactor in communication with the second reactor, the third reactor configured to regenerate the first metal oxide by oxidizing the fourth metal oxide with an oxygen source.2. The system of claim 1 , wherein the counter-current contact mode between the first metal oxide and the first fuel is such that the first metal oxide moves downward and the first fuel moves upward.3. The system of claim 1 , wherein the first metal oxide is introduced to the top of ...

METHOD FOR PRE-REFORMING HYDROCARBONS

There is proposed a method for pre-reforming a hydrocarbonaceous feed stream into a pre-reforming product containing carbon oxides, hydrogen and hydrocarbons, in which the adiabatically operated pre-reforming reactor comprises at least two reaction zones designed as fixed beds in a common reactor vessel, which are in fluid connection with each other and are filled with beds of granular, nickel-containing catalyst active for pre-reforming, wherein the first reaction zone in flow direction is filled with a catalyst active for high-temperature pre-reforming and the last reaction zone in flow direction is filled with a catalyst active for low-temperature pre-reforming. 111-. (canceled)12. A method for pre-reforming a hydrocarbonaceous feed stream into a pre-reforming product containing carbon oxides , hydrogen and hydrocarbons , the method comprising the step of introducing the hydrocarbonaceous feed stream into a multistage , adiabatically operated pre-reforming reactor under pre-reforming conditions to obtain a pre-reforming product , wherein the pre-reforming reactor is a shaft reactor , wherein the pre-reforming reactor comprises at least two reaction zones designed as fixed beds in a common reactor vessel , which are in fluid connection with each other and are filled with beds of granular , nickel-containing catalyst active for the pre-reforming , wherein the first reaction zone in flow direction is filled with a catalyst active for high-temperature pre-reforming and the last reaction zone in flow direction is filled with a catalyst active for low-temperature pre-reforming.13. The method according to claim 12 , wherein the hydrocarbonaceous feed stream comprises methane and C hydrocarbons claim 12 , wherein the pre-reforming product has a reduced amount of C hydrocarbons and an increased amount of methane as compared to the hydrocarbonaceous feed stream.14. The method according to claim 12 , wherein the hydrocarbonaceous feed stream comprises natural gas with a ...

SYSTEMS FOR PYROLYSIS VAPOR UPGRADING

This disclosure relates to systems for the fast pyrolysis of organic matter. More specifically, it relates to systems for the catalytic modification of vapors created during the fast pyrolysis of organic matter to create transportation fuel or a transportation fuel component. The inventive systems either catalytically stabilize or convert at least a first portion of pyrolysis vapors, then combine them with a portion of raw, unconverted bio-derived pyrolysis vapors at a temperature and pressure sufficient for molecules of the combined vapors to react and produce hydrocarbons of increased molecular weight that are suitable for use as a hydrocarbon transportation fuel or component thereof. 1. A system for producing biomass-derived hydrocarbon fuel or a component thereof , comprising:(a) A first and second portion of pyrolysis vapors; a. at least one inlet for receiving the first portion of pyrolysis vapors, and', 'b. at least one catalyst contained inside the reactor for contacting and at least partly upgrading the first portion of pyrolysis vapors to produce an upgraded first portion,', 'c. at least one outlet for conveying the upgraded first portion out of the reactor;, '(b) A reactor having(c) a reaction zone located downstream from the reactor for receiving and combining the upgraded first portion with the second portion of pyrolysis vapors at a temperature and pressure sufficient for molecules of the combined upgraded first portion and the second portion of pyrolysis vapors to react and produce hydrocarbon molecules having molecular weights that are within the boiling range of at least one of gasoline, diesel and gasoil fuels and that are suitable for use as a hydrocarbon transportation fuel or component thereof.2. The system of claim 1 , wherein the at least one catalyst comprises multiple catalysts that may be arranged in separate catalyst beds or as mixtures of catalyst.3. The system of claim 1 , comprising one or more additional portions of pyrolysis vapors ...

REFORMER TUBE HAVING INTERNAL HEAT EXCHANGE

A reformer tube for producing synthesis gas by steam reforming of hydrocarbon-containing feed gases, preferably natural gas, includes one or more helically coiled heat exchanger tubes which are arranged within a catalyst bed of a reforming catalyst and are helically coiled over part of their length located within the catalyst bed and are otherwise straight are present, where the straight proportion of the heat exchanger tubes and/or the helix pitch of the helically coiled part alters within the catalyst bed and matching to requirements of the pressure drop, the heat exchange properties, and the corrosion resistance. 1. A reformer tube for converting a hydrocarbonaceous feedstock into a synthesis gas product comprising a carbon oxide and hydrogen under steam reforming conditions , the reformer tube comprising:(a) an outer tube comprising an open tube end, a closed tube end, and a bed of a solid catalyst active suitable for steam reforming, wherein the outer tube is configured to be heated from outside;(b) a feed gas stream inlet, configured to feed in the feedstock, wherein the feed gas stream inlet is arranged at the open tube end and is in fluid connection with the catalyst bed;(c) a helically-coiled heat exchanger tube arranged within the catalyst bed, wherein a helically-coiled heat exchanger tube inlet end is in fluid connection with the catalyst bed and a helically-coiled heat exchanger tube outlet end is in fluid connection with a synthesis gas product stream outlet, and wherein the helical-coiled heat exchanger tube is in heat exchanging relationship with the catalyst bed and the feed gas stream flowing through the catalyst bed; and(d) a synthesis gas product stream outlet arranged at the open tube end and in fluid connection with the outlet end of the helically-coiled heat exchanger tube, but not in fluid connection with the inlet for the feed gas stream,wherein the feed gas stream initially flows through the catalyst bed and subsequently in counterflow ...

Apparatus And Method For Heterogeneous Catalytic Reactions

An apparatus for use in heterogeneous catalytic reactions comprising a column reactor comprising a plurality of trays mounted one above another, each adapted to hold a predetermined liquid volume and a charge of particles of a solid catalyst thereon; means for introducing a liquid phase reactant above the uppermost tray; means for introducing a vapour phase reactant below the lowermost tray; means for removing a liquid phase post-reaction stream from below the lowermost tray; means for removing a vapour phase post-reaction stream from above the uppermost tray; vapour upcomer means associated with each tray adapted to allow vapour to enter that tray from below; undertow means associated with each tray adapted to remove liquid from that tray and the column reactor before being introduced into the column reactor at a lower tray; means for temporarily directing said liquid removed from a tray to bypass at least one lower tray and be reintroduced to the column reactor at a tray located below said at least one bypassed tray; means for removing the liquid and catalyst from said at least one bypassed tray: and means for replacing a liquid and catalyst inventory on said at least one bypassed tray. 1. An apparatus for use in heterogeneous catalytic reactions comprising:(a) a column reactor comprising a plurality of trays mounted one above another, each adapted to hold a predetermined liquid volume and a charge of particles of a solid catalyst thereon;(b) means for introducing a liquid phase reactant above the uppermost tray;(c) means for introducing a vapour phase reactant below the lowermost tray;(d) means for removing a liquid phase post-reaction stream from below the lowermost tray;(e) means for removing a vapour phase post-reaction stream from above the uppermost tray;(f) vapour upcomer means associated with each tray adapted to allow vapour to enter that tray from below;(g) underflow means associated with each tray adapted to remove liquid from that tray and the column ...

UREA HYDROLYSIS REACTOR FOR SELECTIVE CATALYTIC REDUCTION

This disclosure features a urea conversion catalyst located within a urea decomposition reactor (e.g., a urea decomposition pipe) of a diesel exhaust aftertreatment system. The urea conversion catalyst includes a refractory metal oxide and a cationic dopant. The urea conversion catalyst can decrease the temperature at which urea converts to ammonia, can increase the urea conversion yield, and can decrease the likelihood of incomplete urea conversion. 1. A urea decomposition reactor , comprising:a urea conversion catalyst;wherein the urea conversion catalyst comprises a refractory metal oxide and a cationic dopant.2. The urea decomposition reactor of claim 1 , wherein the refractory metal oxide is selected from the group consisting of cerium oxide claim 1 , titanium oxide claim 1 , zirconium oxide claim 1 , aluminum oxide claim 1 , silicon oxide claim 1 , hafnium oxide claim 1 , vanadium oxide claim 1 , niobium oxide claim 1 , tantalum oxide claim 1 , chromium oxide claim 1 , molybdenum oxide claim 1 , tungsten oxide claim 1 , ruthenium oxide claim 1 , rhodium oxide claim 1 , iridium oxide claim 1 , nickel oxide claim 1 , and any combination thereof.3. The urea decomposition reactor of claim 1 , wherein the refractory metal oxide is selected from the group consisting of titanium oxide claim 1 , zirconium oxide claim 1 , cerium oxide claim 1 , and any combination thereof.4. The urea decomposition reactor of claim 1 , wherein the refractory metal oxide is zirconium oxide or cerium oxide.5. The urea decomposition reactor of claim 1 , wherein the cationic dopant is an oxide comprising Mg claim 1 , Ni claim 1 , Ti claim 1 , V claim 1 , Nb claim 1 , Ta claim 1 , Cr claim 1 , Mo claim 1 , W claim 1 , W claim 1 , Mn claim 1 , Fe claim 1 , Zn claim 1 , Ga claim 1 , Al claim 1 , In claim 1 , Ge claim 1 , Si claim 1 , Sn claim 1 , Co claim 1 , Ni claim 1 , Ba claim 1 , La claim 1 , Ce claim 1 , and Nb.6. The urea decomposition reactor of claim 1 , wherein the urea conversion ...

ETHYLENE-TO-LIQUIDS SYSTEMS AND METHODS

Integrated systems are provided for the production of higher hydrocarbon compositions, for example liquid hydrocarbon compositions, from methane using an oxidative coupling of methane system to convert methane to ethylene, followed by conversion of ethylene to selectable higher hydrocarbon products. Integrated systems and processes are provided that process methane through to these higher hydrocarbon products. 1111.-. (canceled)112. A method , comprising:(a) directing an olefin-containing stream comprising an olefin into an ethylene-to-liquids (ETL) reactor comprising an ETL catalyst that facilitates conversion of at least a portion of said olefin to higher hydrocarbon compounds to yield an ETL product stream comprising said higher hydrocarbon compounds;{'sub': 4+', '3, '(b) directing at least a portion of said ETL product stream into a de-propanizer that separates said higher hydrocarbon compounds into a bottom stream comprising hydrocarbon compounds with four or more carbon atoms (C compounds) and an overhead stream comprising hydrocarbon compounds with three carbon atoms (Ccompounds); and'}{'sub': '3', '(c) directing at least a portion of said Ccompounds into said ETL reactor.'}113. The method of wherein said olefin comprises ethylene claim 112 , propylene claim 112 , or a combination thereof.114. The method of claim 112 , further comprising claim 112 , prior to (a) claim 112 , directing a hydrocarbon feedstream comprising feedstream hydrocarbons into a cracking reactor comprising a cracking catalyst that facilitates a cracking of said feedstream hydrocarbons to produce a cracked stream comprising cracked hydrocarbons claim 112 , wherein said cracked hydrocarbons have a lower molecular weight than said feedstream hydrocarbons claim 112 , and using at least a subset of said cracked hydrocarbons to generate said olefin-containing stream.115. The method of claim 114 , further comprising directing said cracked stream into a separations unit that separates said ...

SHELL AND TUBE OXIDATION REACTOR WITH IMPROVED RESISTANCE TO FOULING

The present disclosure relates to a single shell open interstage reactor (“SSOI”). The SSOI comprises a first reaction stage, an interstage heat exchanger, an open interstage region, and a second reaction stage. The SSOI may be configured for upflow or downflow operation. Further, the open interstage region of the SSOI may comprise a supplemental oxidant feed. When the open interstage region comprises a supplemental oxidant feed, the SSOI may further comprise a supplemental oxidant mixing assembly. Processes for producing acrylic acid through the oxidation of propylene are also disclosed. 1. An upflow single shell open interstage reactor comprising:a) a first shell-and-tube reaction stage comprising a plurality of reaction tubes, wherein the reaction tubes of the first reaction stage comprise a first catalyst;b) an interstage heat exchanger;c) an open interstage region; andd) a second shell-and-tube reaction stage comprising a plurality of reaction tubes, wherein the reaction tubes of the second reaction stage comprise a second catalyst;wherein said interstage heat exchanger is positioned between said first reaction stage and said open interstage region, andwherein said reactor is configured for upflow operation.2. The reactor of claim 1 , wherein said interstage heat exchanger is a shell-and-tube heat exchanger and comprises a plurality of interstage heat exchanger tubes.3. The reactor of claim 2 , wherein said interstage heat exchanger tubes are coaxially continuous with the reaction tubes of the first reaction stage.4. The reactor of claim 2 , wherein said interstage heat exchanger tubes comprise a catalyst retaining device.5. The reactor of claim 4 , wherein said catalyst retaining device is capable of inducing turbulence within the said interstage heat exchanger tubes.6. The reactor of claim 2 , wherein said interstage heat exchanger tubes comprise high void fraction claim 2 , turbulence-inducing inserts.7. The reactor of claim 6 , wherein said inserts have a ...

REACTIVE RECTIFICATION COLUMN FOR PERFORMING CHEMICAL REACTIONS

A device for performing chemical reactions, in which one starting substance is in the liquid phase and one product is in the gaseous phase, is proposed, comprising a reaction zone which includes two catalytic sections, each section having a feed channel and an overflow well which simultaneously acts as the feed channel for the next section, such that liquid from each section passes into the overflow well of this section and via it enters the lower part of the next section, the device being designed to permit removal of the gaseous products of each section, bypassing the remaining sections. 1. A device for performing chemical reactions over a fixed bed of catalyst , in which at least one starting substance is in the liquid phase and at least one product is in the gaseous phase , comprising a reaction zone which includes at least two catalytic sections situated one under the other , each section having a feed channel and an overflow well which simultaneously acts as the feed channel for the next section in the liquid flow direction , such that liquid from each section passes into the overflow well of this section and via it enters the lower part of the next section , the overflow well of the last section in the liquid flow direction being open to permit free outflow of the liquid phase , while a distributor is situated above the feed well of the first section in the liquid flow direction to feed liquid phase into the first section in the liquid flow direction , the device being designed to permit the removal of the gaseous products of each section , bypassing the remaining sections.2. The device as claimed in claim 1 , wherein at least one overflow well/feed channel forms at least part of the outer rim of the reaction zone.3. The device as claimed in claim 1 , wherein a feed channel is formed such that the liquid present therein forms a hydraulic seal so that the gaseous phase present in the section cannot enter the feed channel.4. The device as claimed in claim 1 , ...

A METHOD FOR THE PRODUCTION OF HIGH PURITY BUTADIENE AND N-BUTENE FROM N-BUTANE USING AN OXIDATIVE DEHYDROGENATION PROCESS IN A CONTINUOUS-FLOW MULTI-LAYER-CATALYST FIXED-BED REACTOR

Systems and methods for the production of n-butene isomers and/or 1,3-butadiene are disclosed. The systems and method involve an oxidative dehydrogenation (ODH) process for the production of n-butene isomers and 1,3-butadiene light olefins using an adjustable, multi-purpose, and multi-layer-catalyst bed for a reactor. 1. A method of producing n-butene (CHCHCH═CH) and/or 1 ,3-butadiene (HC═CH—CH═CH) , the method comprising:{'sub': 4', '4', '10, 'flowing a feed stream comprising Chydrocarbons, including n-butane (CH), to a reactor, the reactor including a catalyst bed that comprises three separate catalytic layers arranged in series with respect to the flow of the feed stream, wherein a first inert layer of material is disposed between a first catalytic layer of the three separate catalytic layers and a second catalytic layer of the three separate catalytic layers, wherein a second inert layer of material is disposed between the second catalytic layer and a third catalytic layer of the three separate catalytic layers,'}contacting the n-butane with the first catalytic layer under reaction conditions sufficient to convert n-butane to n-butene and 1,3-butadiene, wherein the first catalytic layer is adapted to catalyze conversion of n-butane to n-butene and 1,3-butadiene; andflowing n-butene and/or 1,3-butadiene from the reactor.2. The method of claim 1 , wherein the feed stream comprises primarily n-butane.3. The method of claim 1 , wherein the feed stream comprises 85 to 99 wt. % n-butane claim 1 , 1 to 10 wt. % of n-butene claim 1 , and 0 to 5 wt. % of residual Ccompounds.4. The method of claim 1 , wherein each catalytic layer comprises different catalytic materials from the other catalytic layers.5. The method of claim 1 , further comprising:contacting a first portion of the n-butene with the second catalytic layer under reaction conditions sufficient to convert the first portion of the n-butene to 1,3-butadiene, wherein the second catalytic layer is adapted to ...

USE OF TOP DIVIDING WALL IN ISOMERIZATION UNIT

The invention is directed to a combined naphtha hydrotreating (NHT) and isomerization process scheme, which includes dividing wall columns (DWC) that replace multiple distillation columns and allow optimized heat integration within the system. The disclosed design provides reductions in both capital and energy costs compared to conventional schemes. 1. An isomerization unit comprising: a first side configured as a stabilizer column; and', 'a second side configured as naphtha splitter column;, 'a first dividing wall column comprising a first side configured as a depentanizer column; and', 'a second side configured as a deisohexanizer column., 'a second dividing wall column;'}2. The isomerization unit of claim 1 , further comprising:a deisopentanizer column coupled to the first dividing wall column configured to receive a light naphtha overhead stream from the second side of the first dividing wall column;an isomerization reactor coupled to the deisopentanizer column and configured to receive a bottoms stream from the deisopentanizer column; anda stabilizer column coupled to the isomerization reactor and configured to receive a stream comprising unstable isomerate from the isomerization reactor and to feed stable isomerate to the second dividing wall column.3. The isomerization unit of claim 1 , wherein the first dividing wall column comprises a first condenser and a second condenser claim 1 , the first condenser configured to reflux a portion of an overheads stream from the first side of the first dividing wall column to an overheads section of the first side of the first dividing wall column claim 1 , and the second condenser configured to reflux a portion of an overheads stream from the second side of the first dividing wall column to an overheads section of the second side of the first dividing wall column.4. The isomerization unit of claim 1 , wherein the second dividing wall column comprises a first condenser and a second condenser claim 1 , the first condenser ...

Process

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.

Hydrocarbon Dehydrocyclization in the Presence of Carbon Dioxide

The invention relates to converting non-aromatic hydrocarbon in the presence of COto produce aromatic hydrocarbon. COmethanation using molecular hydrogen produced during the aromatization increases aromatic hydrocarbon yield. The invention also relates to equipment and materials useful in such upgrading, to processes for carrying out such upgrading, and to the use of such processes for, e.g., natural gas upgrading. 1. A hydrocarbon conversion process , comprising:{'sub': 2+', '2, '(a) providing a feed comprising ≧1 wt. % of C non-aromatic hydrocarbon and ≧0.1 wt. % of CO;'} the first catalyst includes (i) ≧0.005 wt. % of a dehydrogenation component which comprises one or more of Ga, Zn, Mo, W, La, Pt, and Pd, and (ii) ≧10 wt. % of a molecular sieve component, the molecular sieve component comprising at least one molecular sieve having a Constraint Index in the range of from 1 to 12, and', {'sub': '2', 'the second catalyst includes ≧0.005 wt. % of a COconversion component which comprises one or more of Ru, Rh, Ni, Co, and Fe;'}], '(b) providing first and second catalysts, wherein'}{'sub': 2+', '2, "(c) exposing the feed to the first catalyst under conversion conditions effective for (i) converting ≧10 wt. % of the feed's C non-aromatic hydrocarbon to aromatic hydrocarbon and molecular hydrogen and (ii) increasing aromatic hydrocarbon yield by reacting ≧1 wt. % of the feed's COwith at least a portion of the molecular hydrogen in the presence of the second catalyst to produce methane and water."}2. The process of claim 1 , wherein the feed comprises ≧1 wt. % of CO; 10 wt. % to 40 wt. % ethane; 20 wt. % to 50 wt. % propane claim 1 , and 20 wt. % to 50 wt. % butanes claim 1 , and further comprises 1 wt. % to 40 wt. % methane and ≦1 wt. % of aromatic hydrocarbon.3. The process of claim 1 , wherein the COreaction of step (c) has a greater selectivity for methane than CO.4. The process of claim 1 , wherein (i) the first catalyst includes (i) ≧0.01 wt. % of the ...

Hydrocarbon Dehydrocyclization

The invention relates to hydrocarbon dehydrocyclization to produce products such as aromatic hydrocarbon, to equipment and materials useful for dehydrocyclization, to processes for carrying out dehydrocyclization, and to the use of dehydrocyclization for, e.g., natural gas upgrading. The dehydrocyclization is carried out in a catalytic reaction zone of a reverse-flow reactor. 1. A hydrocarbon dehydrocyclization process , the process comprising:{'sub': '2+', '(a) providing a feed comprising C non-aromatic hydrocarbon;'}(b) providing an oxidant and a gaseous fuel; (i) a pre-heated reaction zone, and', '(ii) a dehydrocyclization catalyst located in the reaction zone, the dehydrocyclization catalyst comprising a molecular sieve component and a dehydrogenation component;, '(c) providing a reverse-flow reactor, the reverse-flow reactor including'} (i) establishing a forward flow of the feed to the reaction zone,', '(ii) transferring heat from the reaction zone to the feed to produce a heated feed and a cooled reaction zone,', {'sub': '2+', "(iii) reacting at least a portion of the heated feed flow's C non-aromatic hydrocarbon in the presence of the dehydrocyclization catalyst under dehydrocyclization conditions which include a temperature a temperature ≧400° C. and a pressure ≧0 psi gauge (psig) (101 kPa) to produce a forward flow of a reaction product comprising molecular hydrogen and aromatic hydrocarbon,"}, '(iv) depositing coke on or proximate to the dehydrocyclization catalyst,', '(v) conducting the forward flow of reaction product from the reaction zone and away from the reverse-flow reactor, and', '(vi) decreasing the feed flow to the reaction zone; and, '(d) during a first time interval,'} (i) establishing a reverse flow of the fuel and a reverse flow of the oxidant toward the reverse-flow reactor, the oxidant flow comprising first and second portions of the oxidant,', '(ii) combusting the first portion of the oxidant flow under combustion conditions with at least ...

Process and reactor for dehydration of propanol to propylene

A reactor design and configuration and a process for the catalytic dehydration of propanol to propylene where the reactor train is comprised of a multi-stage single reactor vessel or multiple reactor vessels wherein each stage and/or vessel has different length, internal diameter, and volume than the other stages and/or vessels and in addition the stages and/or reactor vessels are connected in series or in parallel arrangement, preferably used with an improved means of introducing the propanol feedstock and a heat carrying inert gas to the improved reactor train.

Process And Device For Treating High Sulfur Heavy Marine Fuel Oil For Use As Feedstock In A Subsequent Refinery Unit

A multi-stage process for transforming a high sulfur ISO 8217 compliant Feedstock Heavy Marine Fuel Oil involving a core desulfurizing process that produces a Product Heavy Marine Fuel Oil that can be used as a feedstock for subsequent refinery process such as anode grade coking, needle coking and fluid catalytic cracking. The Product Heavy Marine Fuel Oil exhibits multiple properties desirable as a feedstock for those processes including a sulfur level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05 mass % to 1.0 mass. A process plant for conducting the process is also disclosed. 1. A process for treating high sulfur Heavy Marine Fuel Oil for use as feedstock in a subsequent refinery unit , the process comprising: mixing a quantity of Feedstock Heavy Marine Fuel Oil with a quantity of Activating Gas mixture to give a Feedstock Mixture; contacting the Feedstock Mixture with one or more catalysts under reactive conditions to form a Process Mixture from said Feedstock Mixture; receiving said Process Mixture and separating the liquid components of the Process Mixture from the bulk gaseous components of the Process Mixture; subsequently separating any residual gaseous components and by-product hydrocarbon components from the Process Mixture to form a Product Heavy Marine Fuel Oil; and , discharging the Product Heavy Marine Fuel Oil.2. The process of wherein the Feedstock Heavy Marine Fuel Oil complies with ISO 8217 (2017) and has a sulfur content (ISO 14596 or ISO 8754) between the range of 5.0 mass % to 1.0 mass % and wherein the Product Heavy Marine Fuel Oil has a sulfur content (ISO 14596 or ISO 8754) between the range of 0.50 mass % to 0.05 mass %.3. The process of claim 2 , further comprising fractionating the Product Heavy Marine Fuel Oil to remove a light to middle distillate fraction claim 2 , said light to middle distillate fraction have a maximum boiling point less than 650° F.4. The process of wherein the one or more catalysts ...

METHOD FOR REVAMPING A SECONDARY REFORMER

A method for revamping a secondary reformer (), the reformer comprising an internal gas riser pipe () for routing a process gas from a bottom gas inlet to a combustion chamber () located above a catalytic zone (), distribution means () for introduction of an oxidation agent such as process air into said combustion chamber, wherein the original distribution means of the oxidation agent are discontinued, the gas riser pipe is shortened () and the outlet end of the shortened gas riser pipe is arranged to deliver a gas flow directed upwards; a new burner () is installed on top of the reactor, said new burner being arranged to deliver an oxidization agent such as process air with a downward flow, thus obtaining a counterflow mixing zone () and formation of a diffusion flame above the outlet end of the gas riser pipe. 1. A method for revamping a secondary reformer wherein said reformer comprises:a vertical pressure vessel,a bottom inlet for a process gas;a combustion chamber and a catalytic zone, the catalytic zone being located below the combustion chamber;an internal gas riser pipe connected to said bottom inlet of a process gas;distribution means for introduction of an oxidation agent such as process air into said combustion chamber;wherein said gas riser pipe has a gas outlet end which is above the combustion chamber and comprises means arranged to direct the process gas downwards, so that said process gas traverses the combustion chamber and then the catalytic zone flowing from top to bottom, and the method comprises at least the following steps:discontinuing the original distribution means of the oxidation agent,shortening the gas riser pipe so that the gas outlet end of the gas riser pipe is brought to a lower height in the pressure vessel and closer to the catalytic zone, compared to the original gas riser pipe, and the outlet end of the shortened gas riser pipe is arranged to deliver a gas flow directed upwards; andinstalling a new burner on top of the reactor, ...

METHOD AND APPARATUS FOR PREPARATION OF LACTIDE USING LACTIDE PURIFICATION PROCESS

The present invention relates to a method and apparatus for preparation of lactide using a lactide purification process, comprising introducing an aqueous solution comprising lactic acid into a reactor filled with a catalyst and reacting the same to produce crude lactide vapor; and purifying the crude lactide vapor to produce lactide crystals, wherein a first purification comprises collecting and crystallizing the crude lactide vapor using a first solvent to produce lactide crystals, and separating the lactide crystal from a residue through filtration. 1. A method for preparing lactide comprising:(i) introducing an aqueous solution comprising lactic acid into a reactor filled with a catalyst and reacting the same to produce crude lactide vapor; and(ii) purifying the crude lactide vapor produced in the step (i) to produce lactide crystals, wherein the step (ii) comprises:(ii-a) collecting and crystallizing the crude lactide vapor using a first solvent to produce lactide crystals, and (ii-b) separating the lactide crystals from a residue through filtration.2. The method of claim 1 , wherein the first solvent is at least one selected from the group consisting of ethanol claim 1 , propanol claim 1 , and butanol.3. The method of claim 1 , wherein the first solvent cools claim 1 , collects claim 1 , and crystallizes the crude lactide vapor at a temperature between 5° C. and 20° C.4. The method of claim 1 , wherein the solubility of lactide in the first solvent is 0.1 or less at a temperature between 5° C. and 20° C.5. The method of claim 1 , wherein the vapor pressure of the first solvent is between 5 hPa and 70 hPa at 20° C.6. The method of claim 1 , wherein the steps (ii-a) and (ii-b) are conducted simultaneously.7. The method of claim 1 , further comprising (iii) re-purifying the lactide crystals after the step (ii) claim 1 ,wherein the step (iii) comprises:(iii-a) dissolving the lactide crystals in a second solvent which has the same components as the first solvent,( ...

PROCESS FOR THE PREPARATION OF METHANOL IN PARALLEL REACTORS

In a process for the preparation of methanolin parallel reactors, comprising the steps of (a) reacting carbon oxides and hydrogen in the presence of a methanol catalyst in a first methanol reactor to obtain a first methanol-containing effluent, (b) introducing and reacting unconverted synthesis gas in a second methanol reactor in the presence of a methanol catalyst to obtain a second methanol-containing effluent, the first methanol reactor and the second methanol reactor being connected in parallel, (c) combining the first and second effluent, and (d) cooling and separating the combined and cooled effluent into a methanol-containing liquid phase and unconverted synthesis gas, the methanol catalyst in the first methanol reactor is indirectly cooled by boiling water and the methanol catalyst in the second methanol reactor is either directly or indirectly cooled by the unconverted synthesis gas prior to conversion into the second effluent. 1. Process for the preparation of methanol , comprising the steps ofa) reacting carbon oxides and hydrogen in the presence of a methanol catalyst in a first methanol reactor to obtain a first methanol-containing effluent;b) introducing and reacting unconverted synthesis gas in a second methanol reactor in the presence of a methanol catalyst to obtain a second methanol-containing effluent, the first methanol reactor and the second methanol reactor being connected in parallel;c) combining the first and second effluent, andd) cooling and separating the combined and cooled effluent into a methanol-containing liquid phase and unconverted synthesis gas,wherein the first methanol reactor is a boiling-water reactor and the second methanol reactor is a gas-cooled reactor or a multistage packed-bed reactor.2. The process of claim 1 , wherein the methanol catalyst in the first methanol reactor is indirectly cooled by boiling water and the methanol catalyst in the second methanol reactor is indirectly cooled by the unconverted synthesis gas ...

DUAL STAGE LIGHT ALKANE CONVERSION TO FUELS

A process and system for the conversion of a feedstock comprising C3-C5 light alkanes to a C5+ hydrocarbon product, for example, a BTX-rich hydrocarbon product, by performing the alkane activation (first-stage) and the oligomerization/aromatization (second-stage) in separate stages, which allows each conversion process to occur at optimal reaction conditions thus increasing the overall hydrocarbon product yield. The alkane activation or first-stage is operated at a higher temperature than the second-stage since light alkanes are much less reactive than light olefins. Since aromatization of olefins is more efficient at higher pressure, the second-stage is maintained at a higher pressure than the first-stage. Further, fixed-bed catalysts are used in each of the first-stage and the second-stage. 1. A method for converting light hydrocarbon feedstock to produce liquid transportation fuels , the method comprising:contacting a light hydrocarbon feedstock comprising at least one C3-C5 alkane with a first fixed-bed catalyst in a first-stage conversion reactor to produce a first-stage effluent, wherein reaction conditions in the first-stage conversion reactor comprise a first temperature in a range from 400 degrees Celsius to 650 degrees Celsius and a first pressure in a range from 0 psig to 100 psig;separating the first-stage effluent in a first separator to produce a first condensed liquid hydrocarbon comprising at least five carbon atoms, and a gas phase product comprising at least one C2-C4 olefin;contacting the gas phase product with a second fixed-bed catalyst in a second-stage conversion reactor to produce a second-stage effluent, wherein reaction conditions in the second-stage conversion reactor comprise a second temperature lower than the first temperature and in a range from 200 degrees Celsius to 400 degrees Celsius and a second pressure in a range from 0 psig to 500 psig; andseparating the second-stage effluent in a second separator to produce a second condensed ...

FIXED BED RADIAL FLOW REACTOR FOR LIGHT PARAFFIN CONVERSION

Systems and methods are provided for conversion of light paraffinic gases to form liquid products in a process performed in a fixed bed radial-flow reactor. The light paraffins can correspond to C paraffins. Examples of liquid products that can be formed include C-Caromatics, such as benzene, toluene, and xylene. The fixed bed radial-flow reactor can allow for improved control over the reaction conditions for paraffin conversion in spite of the fixed bed nature of the reactor. This can allow the process to operate with improved efficiency while reducing or minimizing the complexity of operation relative to non-fixed bed reactor systems. 112.-. (canceled)13. A method for processing a paraffin-containing feed , comprising:{'sub': 3+', '6', '12, 'exposing a feed comprising about 30 vol % to about 70 vol % of C paraffins to one or more fixed beds of a conversion catalyst to form a conversion effluent comprising C-Caromatics, the one or more fixed beds of the conversion catalyst comprising fixed beds in one or more radial flow reactors, a combined pressure drop across the one or more fixed beds being less than about 100 kPag, the one or more radial flow reactors comprising{'b': '1', 'an outer annular volume defined by an interior of a reactor wall and an exterior of a gas-permeable wall, the interior of the reactor wall defining an outer annular radius R;'}{'b': '3', 'a central volume defined by the interior of a central column and a column cap, the interior of the central column defining a column radius R; and'}{'b': '2', 'an inner annular volume defined by an interior of the gas-permeable wall, an exterior of the central column, an inner annular top, and an inner annular bottom, the interior of the gas-permeable wall defining an inner annular radius R, the inner annular volume comprising a catalyst bed, the inner annular volume being in direct fluid communication with the outer annular volume through the gas-permeable wall, the inner annular volume being in direct ...

NH3 SYNTHESIS CONFIGURATION FOR LARGE-SCALE INSTALLATIONS

A method and device for producing ammonia from a syngas in a heterogeneous gas catalysis process in at least two reaction devices connected in series. Each reaction device includes at least two catalyst beds through which the syngas is conducted and in which an at least partial conversion of the syngas into the product gas is carried out. At least one first heat exchanger is provided in the first reaction device, and the fresh syngas is pre-heated in the first heat exchanger. The syngas exiting the first catalyst bed and which includes the product and non-converted reactants is cooled before entering the second catalyst bed. According to an embodiment of the invention, the pre-heating process is carried out in a first heat exchanger arranged between the first and the second catalyst bed. Thus, synthesis conversion can be increased without substantially increasing the process gas quantity. 118.-. (canceled)19. A method for preparing ammonia from a synthesis gas A under heterogeneous gas catalysis in at least a first reaction apparatus series-connected to a second reaction apparatus , the first reaction apparatus comprising at least a first catalyst bed and a second catalyst bed , and a first heat exchanger disposed between the first and second catalyst beds , comprising:passing the synthesis gas A through the first catalyst bed and the second catalyst bed to at least partially convert the synthesis gas A to product gas B,preheating the fresh synthesis gas A in the first heat exchanger,cooling the synthesis gas B comprising product and unconverted reactants that exits from the first catalyst bed prior to entry into the second catalyst bed,providing an intermediate heat exchanger in the flow pathway between the first reaction apparatus and the second reaction apparatus,utilizing the hot product gas stream exiting from the second catalyst bed without prior cooling for raising of steam and/or for preheating of boiler feed water in the intermediate heat exchanger,wherein ...

METHOD FOR PREPARING A HYDROSILANE USING HETERO ATOM CONTAINING ACTIVATED CARBON

The present invention relates to a method for preparing a hydrosilane using heteroatom-containing activated carbon, more particularly to a method for economically preparing a high-purity hydrosilane by redistribution of a chlorosilane using a heteroatom-containing activated carbon catalyst. 2. The method for preparing a hydrosilane according to claim 1 , wherein the chlorosilane is trichlorosilane or dichlorosilane.3. The method for preparing a hydrosilane according to claim 1 , wherein the heteroatom-containing activated carbon comprises 0.01-15 wt % of a group 15 heteroatom having an unshared electron pair based on the total weight of the catalyst.4. The method for preparing a hydrosilane according to or claim 1 , wherein the heteroatom is nitrogen claim 1 , phosphorus or a combination thereof.5. The method for preparing a hydrosilane according to claim 1 , wherein the redistribution is conducted at a reaction temperature of 40-500° C.6. The method for preparing a hydrosilane according to claim 5 , wherein the redistribution is conducted at a reaction temperature of 150-300° C. while maintaining the stability of the catalyst.7. The method for preparing a hydrosilane according to claim 1 , wherein the redistribution is conducted at a reaction pressure of 1-10 bar.8. The method for preparing a hydrosilane according to claim 1 , which further comprises claim 1 , before the redistribution claim 1 , vaporizing the chlorosilane by preheating to 40-300° C.9. The method for preparing a hydrosilane according to claim 1 , which further comprises claim 1 , after the redistribution claim 1 , cooling the hydrosilane.10. The method for preparing a hydrosilane according to claim 1 , wherein the reaction is conducted while supplying the chlorosilane at a rate of 2-200 WHSV based on the amount of the catalyst.11. An apparatus for preparing a hydrosilane claim 1 , comprising:a preheater into which a chlorosilane is injected and in which the chlorosilane is vaporized;a reactor which ...

CATALYTICALLY HEATED FUEL PROCESSOR WITH REPLACEABLE STRUCTURED SUPPORTS BEARING CATALYST FOR FUEL CELL

A highly compact heat integrated fuel processor, which can be used for the production of hydrogen from a fuel source, suitable to feed a fuel cell, is described. The fuel processor assembly comprises a catalytic reforming zone () and a catalytic combustion zone (), separated by a wall (). Catalyst able to induce the reforming reactions is placed in the reforming zone and catalyst able to induce the combustion reaction is placed in the combustion zone, both in the form of coating on a suitable structured substrate, in the form of a metal monolith. Fe—Cr—Al—Y steel foils, in corrugated form so as to enhance the available area for reaction, can be used as suitable substrates. The reforming and the combustion zones can be either in rectangular shape, forming a stack with alternating combustion/reforming zones or in cylindrical shape forming annular sections with alternating combustion/reforming zones, in close contact to each other. The close placement of the combustion and reforming catalyst facilitate efficient heat transfer through the wall which separates the reforming and combustion chambers. 1. A reformer for the production of hydrogen for fuel cell applications , from a fuel source , the reformer comprising:a combustion zone and a reforming zone, the combustion zone being configured to receive at least a combustion fuel and convert the combustion fuel into heat to provide the heat to the reforming zone disposed annularly about the combustion zone, wherein said reforming and combustion zones are separated by a separating wall;the combustion zone on one side of the separating wall containing a combustion structured catalyst support coated with a catalyst to induce the fuel combustion reaction;the reforming zone being configured to receive at least a reforming fuel and to produce a reformate containing primarily hydrogen; andthe reforming zone on another side of the separating wall containing a reforming structured catalyst support coated with a catalyst able to ...

Selective series-flow hydroprocessing system

Aromatic extraction and hydrocracking processes are integrated to optimize the hydrocracking units design and/or performance. By processing aromatics-rich and aromatic-lean fractions separately, the hydrocracking operating severity and or catalyst reactor volume requirement decreases.

REMOVABLE BASKET FOR CATALYTIC REACTOR

The present invention relates to a removable basket for a catalytic reactor comprising a horizontal base () and a plurality of vertical side walls () and/or at least one ellipsoidal side wall, and a plurality of vertical chimneys () that are open at their lower () and upper () ends, each chimney comprising a lower part () comprising the lower end fastened to the base and extending between the side walls, in which a first chimney comprises an upper part () extending above the side walls, and the upper part of the first chimney is suitable for being inserted into a lower part of a chimney of another removable basket. The present invention also relates to a filtration and distribution device comprising said removable basket, a reactor comprising said device, and a hydrotreating and/or hydrocracking process using said reactor. 2183274. Removable basket according to claim 1 , in which the height (h) of the upper part () of the first chimney () is smaller than or equal to the height (H) of the lower part () of a second chimney () of the removable basket.334274183. Removable basket according to claim 1 , in which the chimneys ( claim 1 , ) form tubes having a circular cross section claim 1 , and the diameter (D) of the lower part () of a second chimney () of the removable basket is greater than the diameter (d) of the upper part () of the first chimney ().4482847. Removable basket according to claim 1 , also comprising a second chimney () comprising an upper part () extending above the side walls () claim 1 , and in which the upper part () of the second chimney () is suitable for being inserted into a lower part () of a chimney of another removable basket.5284173. Removable basket according to claim 4 , in which the height (h) of the upper part () of the second chimney () is smaller than or equal to the height (H) of the lower part () of the first chimney ().634173284. Removable basket according to claim 4 , in which the chimneys ( claim 4 , ) form tubes having a circular ...

SYSTEMS AND METHODS FOR THE OXIDATIVE COUPLING OF METHANE

The present disclosure provides systems and methods for producing olefins via an oxidative coupling of methane (OCM) process. The systems and methods may comprise the use of a staged process comprising at least one non-adiabatic section that is in thermal communication with a heat transfer medium and at least one substantially adiabatic section. The systems and methods may also comprise the use of a diluent stream which may improve methane conversion in an OCM reactor and an ethylene/ethane ratio in a post-bed cracking unit. The methods and systems may further comprise injecting oxygen (O) and a paraffin into a gas stream containing a radical transfer agent to provide a reaction mixture. The reaction mixture may be held in a vessel for a time period greater than an auto-ignition delay time (AIDT), such that the reaction mixture may ignite to liberate heat and convert to a product mixture comprising olefins. 1. A method for producing an olefin , the method comprising:{'sub': 4', '2, '(a) producing a gas stream comprising methane (CH), oxygen (O), and a diluent; and'}{'sub': 4', '2+, '(b) passing the gas stream over an oxidative coupling of methane (OCM) catalyst at a pressure of at least 2 bar(g) to convert at least some of the CHinto hydrocarbon compounds having two or more carbon atoms (C compounds),'}wherein a ratio of diluent molecules to carbon atoms in the gas stream is at least 0.1:1.2. The method of claim 1 , wherein the diluent comprises water (HO).3. The method of claim 1 , wherein the diluent comprises carbon dioxide (CO).4. The method of claim 1 , wherein the diluent comprises HO and CO.5. The method of claim 1 , wherein the ratio of diluent molecules to carbon atoms in the gas stream is at least 0.5:1.6. The method of claim 1 , wherein the ratio of diluent molecules to carbon atoms in the gas stream is at most 20:1.7. The method of claim 1 , wherein the ratio of diluent molecules to carbon atoms in the gas stream is from 0.1:1 to 5:1.8. The method of ...

SYSTEM AND METHOD FOR PHOTOELECTROCHEMICAL AIR PURIFICATION

An air purification system including a filter assembly including a substrate including a fibrous media, and a photocatalytic material disposed on the substrate, wherein the photocatalytic material includes a first quantity of crushed nanostructures; and a photon source arranged to illuminate the photocatalytic material with optical radiation. 1. An air purification system comprising:a housing defining a lumen, a filter attachment region, an inlet, an outlet, and a flow pathway between the inlet and the outlet; a substrate comprising a fibrous media, and', 'a photocatalytic material disposed on the substrate, wherein the photocatalytic material is comprised of a first quantity of nanoparticles and a second quantity of crushed nanostructures, wherein the photocatalytic material comprises a homogenous distribution of the first quantity of nanoparticles and the second quantity of crushed nanostructures, and wherein the ratio of the first quantity to the second quantity by mass is greater than one;, 'a filter assembly retained within the lumen intersecting the flow pathway and coupled to the filter attachment region, wherein the filter assembly comprisesa photon source coupled to the housing and arranged to illuminate the photocatalytic material with optical radiation, wherein the optical radiation is at least partially visible; anda flow control mechanism coupled to the housing and arranged along the flow pathway, wherein the flow control mechanism is configured to urge airflow along the flow pathway between the inlet and the outlet of the housing.2. The system of claim 1 , wherein the crushed nanostructures comprise at least one of crushed nanorods and crushed nanotubes.3. The system of claim 2 , wherein the crushed nanostructures and nanoparticles comprise a metal oxide photocatalyst.4. The system of claim 1 , wherein the crushed nanostructures define a size distribution claim 1 , wherein a peak of the size distribution corresponds to a plasmonic resonance frequency ...

REACTOR

A reactor includes: a shell with first and second ends, an fluid inlet at the first end for receiving a process fluid, and an outlet at the second end for discharging a reacted process fluid, and a plurality of elongate containment units within the shell for containing a particulate catalyst or sorbent, each containment unit including two perforate members defining a space in which the particulate catalyst or sorbent may be placed, the perforate members mounted between two fluid-impermeable end members, wherein one end member extends across the containment unit to provide a closed end and the other end member closes the space thereby providing an open end through which a process fluid may enter or exit the containment unit, and a header assembly connected to the open ends of the containment units and either the fluid inlet or fluid outlet. A process using the reactor is also described. 119-. (canceled)20. A reactor comprising: a shell with first and second ends , a process fluid inlet at the first end for receiving a process fluid , and a process fluid outlet at the second end for discharging a reacted or decontaminated process fluid , and a plurality of elongate containment units within said shell for containing a particulate catalyst or sorbent , each containment unit comprising two perforate members defining a space in which the particulate catalyst or sorbent may be placed , said perforate members mounted between two process fluid-impermeable end members , wherein one end member extends across the containment unit to provide a closed end and the other end member closes the space thereby providing an open end through which a process fluid may enter or exit the containment unit , and a header assembly connected to the open ends of the containment units and either said process fluid inlet or said process fluid outlet , wherein each containment unit comprises an outer perforate member an inner perforate member , arranged concentrically , and a central void within ...

Shaped catalyst particle

The invention concerns particles which may include a catalytically active component, in the form of a three-dimensional ellipsoidal shape having three major axes at least two of which axes are of different lengths. Beds of such particles are useful for forming particle beds through which a fluid may flow.

FIXED-BED REACTOR, METHOD FOR PREPARING A FIXED-BED REACTOR, AND USE OF A FIXED-BED REACTOR

A fixed bed () is provided for a fixed-bed reactor (). The fixed bed () contains a particulate carrier and at least one reactive substance. The carrier is a silicate compound and the reactive substance is an organometallic pyridine compound. A method for preparing such a fixed bed is provided. The method includes the steps of preparing the carrier, preparing an impregnation and treating the carrier with the impregnation. In addition, a gas-measuring tube is provided with a correspondingly prepared fixed bed as well. A method uses organometallic pyridinium compounds, especially pyridinium dichromate, in a fixed-bed reactor for detecting alcohol compounds and for preparing formaldehyde and/or acetaldehyde. 1. A fixed bed for a fixed-bed reactor , the fixed bed comprising:a particulate carrier; andat least one reactive substance, wherein the carrier is a silica compound and the reactive substance is an organometallic pyridine compound.2. A fixed bed in accordance with claim 1 , wherein the pyridine compound is selected from among pyridinium chlorochromate claim 1 , pyridinium dichromate and bispyridine chromium trioxide.3. A fixed bed in accordance with claim 1 , wherein the carrier is impregnated with the reactive substance.4. A fixed bed in accordance with claim 1 , wherein the carrier has a charge of the organometallic pyridine compound in a quantity of at most 10 wt. % or less.5. A fixed bed in accordance with claim 1 , wherein the silica compound is a silica gel with a particle size distribution of at least 0.1 mm to at most 1.5 mm.7. A method in accordance with claim 6 , wherein the inorganic phosphorus compound is a phosphorus compound that is selected from among phosphinic acid claim 6 , phosphonic acid and/or phosphoric.8. A method in accordance with claim 6 , wherein the solvent of the impregnation contains at least one additional acid.9. A method in accordance with claim 6 , wherein the preparation of the impregnation comprises the dissolution of the ...

New catalyst system for producing maleic anhydride by means of the catalytic oxidation of n-butane

The invention relates to a catalyst system for producing maleic anhydride by means of the catalytic oxidation of n-butane, comprising at least one reactor tube, which has two catalyst layers consisting of different catalyst particles, characterized in that the geometric surface area per catalyst particle is greater in the catalyst layer that is first in the gas flow direction than in the second catalyst layer. The invention further relates to a process for producing maleic anhydride by means of the catalytic oxidation of n-butane, wherein a mixture of oxygen and n-butane is fed through the catalyst system according to the invention and the at least one reactor tube is at elevated temperature.

Process and System for Making Cyclopentadiene and/or Dicyclopentadiene

Processes and systems for making cyclopentadiene and/or dicyclopentadiene include converting acyclic C5 hydrocarbon(s) into CPD in a first reactor to obtain a product mixture, washing the product mixture with a wash oil, separating the washed product mixture in a separation sub-system such as compression train to obtain a C5-rich fraction comprising CPD, dimerizing the C5-rich fraction in a dimerization reactor to obtain a product effluent, followed by separating the product effluent to obtain a DCPD-rich fraction. Wash oil can be recovered and recycled. Multiple-stage of dimerization and separation steps can be used to obtain multiple DCPD-rich fractions of various purity and quantity. C5-rich fractions from various stages of the process may be recycled to the first reactor, or converted into mogas components after selective hydrogenation. C5-rich fractions and mogas components may be optionally separated to produce value-adding chemicals.

Process and System for Making Cyclopentadiene and/or Dicyclopentadiene

Processes and systems for making cyclopentadiene and/or dicyclopentadiene include converting acyclic C5 hydrocarbon(s) into CPD in a first reactor to obtain a product mixture, separating the product mixture in a separation sub-system such as compression train to obtain a C5-rich fraction comprising CPD and essentially depleted of hydrogen and C1-C4 hydrocarbons, dimerizing the C5-rich fraction in a dimerization reactor to obtain a product effluent comprising DCPD, followed by separating the product effluent to obtain a DCPD-rich fraction. Multiple-stage of dimerization and separation steps can be optionally used to obtain multiple DCPD-rich fractions of various degrees of purity and quantity. C5-rich fractions from various stages of the process may be recycled to the first reactor, or converted into mogas components after selective hydrogenation. C5-rich fractions and mogas components may be optionally separated to produce value-adding chemicals. 1. A process for making cyclopentadiene (CPD) and/or dicyclopentadiene (DCPD) , the process comprising:(I) feeding a C5 feedstock comprising at least one acyclic C5 hydrocarbon into a first reactor;(II) contacting the at least one acyclic C5 hydrocarbon with a catalyst under conversion conditions to obtain a first reactor hydrocarbon effluent comprising: C5 components including CPD and acyclic diolefins; light components including hydrogen and C1-C4 hydrocarbons; one-ring aromatics; and multiple-ring aromatics;(III) separating the first rector hydrocarbon effluent to produce (i) a light components-rich fraction and (ii) a first C5-rich fraction comprising CPD;(IV) supplying at least a portion of the first C5-rich fraction into a second reactor operating under a first set of dimerization conditions;(V) obtaining a second reactor effluent from in the second reactor comprising CPD and DCPD; and(VI) separating at least a portion of the second reactor effluent to obtain a first DCPD-rich fraction comprising dicyclopentadiene ( ...